[go: up one dir, main page]

WO2025226673A1 - Procédés et systèmes améliorés pour générer une solution de lithium à partir d'un matériau échangeur d'ions - Google Patents

Procédés et systèmes améliorés pour générer une solution de lithium à partir d'un matériau échangeur d'ions

Info

Publication number
WO2025226673A1
WO2025226673A1 PCT/US2025/025758 US2025025758W WO2025226673A1 WO 2025226673 A1 WO2025226673 A1 WO 2025226673A1 US 2025025758 W US2025025758 W US 2025025758W WO 2025226673 A1 WO2025226673 A1 WO 2025226673A1
Authority
WO
WIPO (PCT)
Prior art keywords
lithium
solution
ion exchange
exchange material
synthetic
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/US2025/025758
Other languages
English (en)
Inventor
Nicolás Andrés GROSSO GIORDANO
David Henry SNYDACKER
David Calder GRAUER
Nathan Alexander CHAO
Garrett LAU
Amos Indranada
Jasper Shaun KELLY
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lilac Solutions Inc
Original Assignee
Lilac Solutions Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Lilac Solutions Inc filed Critical Lilac Solutions Inc
Publication of WO2025226673A1 publication Critical patent/WO2025226673A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
    • B01J39/08—Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/016—Modification or after-treatment of ion-exchangers
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • C22B26/12—Obtaining lithium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • Lithium is an essential element for high-energy rechargeable batteries and other technologies. Lithium can be found in a variety of liquid solutions, including natural and synthetic brines and leachate solutions from minerals and recycled products.
  • a method for lithium recovery comprising: a) forming an eluent solution by dissolving a gas in an aqueous solution at a pressure of about 0 to 50 barg, wherein the pH of the eluent solution is less than 7 following dissolution of the gas; b) contacting an ion exchange material to a liquid resource, wherein the ion exchange material absorbs lithium ions from the liquid resource to yield a lithium-depleted liquid resource and a lithiated ion exchange material; c) contacting the lithiated ion exchange material to the eluent solution, wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution; and d) separating the synthetic lithium solution from the ion exchange material.
  • a method for lithium recovery comprising: a) forming an eluent solution by dissolving a gas in an aqueous solution at a pressure of about 0 to 50 barg, wherein the pH of the eluent solution is at most 7 following dissolution of the gas; b) contacting an ion exchange material to a liquid resource, wherein the ion exchange material absorbs lithium ions from the liquid resource to yield a lithium-depleted liquid resource and a lithiated ion exchange material; WSGR Docket No.50741-726.601 c) contacting the lithiated ion exchange material to the eluent solution, wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution; and d) separating the synthetic lithium solution from the ion exchange material.
  • a method for lithium recovery comprising: a) forming an eluent solution by dissolving a gas in an aqueous solution at a pressure exceeding atmospheric pressure, wherein the pH of the eluent solution is from about 3 to 5 following dissolution of the gas; b) contacting an ion exchange material to a liquid resource, wherein the ion exchange material absorbs lithium ions from the liquid resource to yield a lithium-depleted liquid resource and a lithiated ion exchange material; c) contacting the lithiated ion exchange material to the eluent solution, wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution; and d) separating the synthetic lithium solution from the ion exchange material.
  • a method for lithium recovery comprising: a) forming an eluent solution by dissolving a gas in an aqueous solution at a pressure exceeding 0 barg, wherein the pH of the eluent solution is less than 7 following dissolution of the gas; b) contacting an ion exchange material to a liquid resource, wherein the ion exchange material absorbs lithium ions from the liquid resource to yield a lithium-depleted liquid resource and a lithiated ion exchange material; c) contacting the lithiated ion exchange material to the eluent solution, wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution with a concentration of lithium greater than about 1 mg/L; and d) separating the synthetic lithium solution from the ion exchange material.
  • a method for lithium recovery comprising: a) forming an eluent solution by dissolving a gas in an aqueous solution at a pressure exceeding 0 barg, wherein the pH of the eluent solution is at most 7 following dissolution of the gas; WSGR Docket No.50741-726.601 b) contacting an ion exchange material to a liquid resource, wherein the ion exchange material absorbs lithium ions from the liquid resource to yield a lithium-depleted liquid resource and a lithiated ion exchange material; c) contacting the lithiated ion exchange material to the eluent solution, wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution with a concentration of lithium of at least about 1 mg/L; and d) separating the synthetic lithium solution from the ion exchange material.
  • a method for lithium recovery comprising: a) contacting an ion exchange material to a liquid resource, wherein the ion exchange material absorbs lithium ions from the liquid resource to yield a lithium-depleted liquid resource and a lithiated ion exchange material; b) contacting the lithiated ion exchange material to an eluent solution, wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution, and wherein the eluent solution comprises an acid; c) separating the synthetic lithium solution from the ion exchange material; d) dissolving a gas in the synthetic lithium solution to yield an intermediate solution, e) processing the intermediate solution to yield a purified lithium solution and a regeneration solution, wherein the regeneration solution comprises the acid; and f) directing at least a portion of the regeneration solution to provide the eluent solution.
  • a system for lithium recovery comprising: a) first subsystem configured to: i. contact a lithiated ion exchange material to an eluent solution; wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution and an ion exchange material; and ii. retain the ion exchange material within the first subsystem when the synthetic lithium solution is separated from the ion exchange material and exits the first subsystem; and b) a second subsystem configured to form the eluent solution by dissolving a gas in an aqueous solution; wherein the pH of the eluent solution is less than about 7.
  • a system for lithium recovery comprising: WSGR Docket No.50741-726.601 a) first subsystem configured to: i. contact a lithiated ion exchange material to an eluent solution; wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution and an ion exchange material; and ii.
  • the first subsystem is further configured to: iii. contact the ion exchange material to a liquid resource; wherein the ion exchange material absorbs lithium from the liquid resource to generate the lithiated ion exchange material and a lithium-depleted liquid resource; and iv.
  • the system further comprises: c) a third subsystem configured to process the synthetic lithium solution to provide a lithium chemical.
  • FIG.1 provides a method for lithium extraction, such as that described in Example 1, including a system configured for use in carrying out said method.
  • FIG.2 provides a method for lithium extraction, such as that described in Example 2, including a system configured for use in carrying out said method.
  • FIG.3 provides a method for lithium extraction, such as that described in Example 3, including a system configured for use in carrying out said method.
  • FIG.4 provides a method for lithium extraction, such as that described in Example 4, including a system configured for use in carrying out said method that comprises lithium extraction device 402.
  • FIG.4A, FIG.4B, and FIG.4C each provide components of the lithium extraction device 402.
  • FIG.5 (left) provides a method for lithium extraction, such as that described in Example 5, including a system configured for use in carrying out said method that comprises lithium extraction system 502; (right) provides lithium extraction system 502 in further detail.
  • FIG.6 provides a method for lithium extraction, such as that described in Example 6, including a system configured for use in carrying out said method.
  • FIG.7 provides a method for lithium extraction, such as that described in Example 7, including a system configured for use in carrying out said method.
  • FIG.8 provides a method for processing a synthetic lithium solution, such as that described in Example 8, including a system configured for use in carrying out said method.
  • FIG.9 provides a method for lithium extraction, such as that described in Example 9, including a system configured for use in carrying out said method.
  • FIG.10 provides a method for lithium extraction, such as that described in Example 10, including a system configured for use in carrying out said method.
  • FIG.11 provides a method for processing a synthetic lithium solution, such as that described in Example 11, including a system configured for use in carrying out said method.
  • FIG.12 provides a method for lithium extraction, such as that described in Example 12, including a system configured for use in carrying out said method.
  • WSGR Docket No.50741-726.601 provides a method for lithium extraction, such as that described in Example 13, including a system configured for use in carrying out said method.
  • FIG.14 provides a method for purification of a lithium eluate and production of battery grade lithium carbonate, such as that described in Example 14, including a system configured for use in carrying out said method.
  • FIG.15 provides an illustration of the relationship between gas pressure and lithium concentration of an eluate solution according to some embodiments of the disclosure, such as described in Example 15.
  • FIG.16 provides an illustration of the relationship between salt concentration and identity and lithium concentration of an eluate solution according to some embodiments of the disclosure, such as described in Example 16.
  • DETAILED DESCRIPTION OF THE INVENTION [0032] Lithium is an essential element for batteries and other technologies. Lithium is found in a variety of liquid resources, including natural and synthetic brines and leachate solutions from minerals, clays, and recycled products. Lithium is optionally extracted from such liquid resources using an ion exchange process based on inorganic ion exchange materials. These inorganic ion exchange materials absorb lithium from a liquid resource while releasing hydrogen, and then elute lithium in acid while absorbing hydrogen.
  • This ion exchange process is optionally repeated to extract lithium from a liquid resource and yield a synthetic lithium solution.
  • the synthetic lithium solution is optionally further processed into chemicals for the battery industry or other industries.
  • Current methods of lithium production require that large volumes of water and chemical reagents be used to extract lithium. Ion exchange dramatically reduces these two requirements, but still requires acid and base as reagents.
  • the disclosure provided herein completely eliminates the use of liquid acids (e.g., mineral acids) in lithium production by ion- exchange, replacing them with gases that, when dissolved in water, generate protons used in the ion exchange process.
  • a typical source of proton includes an acidic solution, said solution comprising a mineral or organic acid, which in some embodiments is selected from hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, acetic acid, carbonic acid, or combinations thereof.
  • Such acids are commonly used in the chemical industry.
  • such acid is generated by dissolving a gas in water.
  • the strength of said acid is diminished relative to the strength of mineral acids, yet this acidity is sufficient for supplying the protons (H + ) ions necessary to elute lithium.
  • the following are non limiting embodiments of the generation of the dissolution of a gas in water or an aqueous liquid, and the generation of acidic protons therefrom: WSGR Docket No.50741-726.601 (18) HNO3 ⁇ NO3- + H + [0037] It will be understood by those skilled in the art that other chemical species can also be involved in the generation of acidity, with the ultimate result being that a proton, either free (H + ) or in association with water (H3O + ) is generated in an aqueous solution.
  • the terms “lithium”, “lithium ion”, and “Li + ” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary.
  • the terms “hydrogen”, “hydrogen ion”, “proton”, and “H + ” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary.
  • the words “column” and “vessel” are used interchangeably. In some embodiments described herein referring to a “vessel”, the vessel is a column. In some embodiments described herein referring to a “column”, the column is a vessel.
  • the pH of the system or “the pH of” a component of a system, for example one or more tanks, vessels, columns, pH modulating units, or pipes used to establish fluid communication between one or more tanks, vessels, columns, or pH modulating units, WSGR Docket No.50741-726.601 refers to the pH of the liquid medium contained or present in the system, or contained or present in one or more components thereof.
  • the liquid medium contained in the system, or one or more components thereof is a liquid resource.
  • the liquid medium contained in the system, or one or more components thereof is a brine.
  • the liquid medium contained in the system is an acid solution, an aqueous solution, a wash solution, a salt solution, a salt solution comprising lithium ions, or a lithium-enriched solution.
  • pH is equal to the negative logarithmic value of the concentration of protons in the aqueous solution.
  • the pH of the solutions described herein are preferably determined with a pH probe. However, many of the solutions described herein comprise high concentrations of ions (e.g., sodium) that are known to interfere with pH probe sensors. Therefore, solutions with high ion concentrations can lead to shifted readings.
  • concentration refers to the amount of a chemical species within a given amount of liquid. In some embodiments, said concentration can be specified as the mass of a species dissolved in an amount of liquid (e.g. mg/L), or the number of moles of a species dissolved in an amount of liquid (e.g. mol/L).
  • concentration can be specified by the ratio of moles or mass of the species of interest to one or more other species dissolved in the same liquid.
  • concentration can be specified by the ratio of moles or mass of the species of interest to one or more other species dissolved in the same liquid.
  • a concentration of sodium (Na) is stated to be 100 milligrams per liter (mg/L).
  • the stated concentration refers to the mass concentration of the ion in solution, and does not include the mass of the anion; in the example stated above, such an ion may comprise chloride (Cl-), nitrate (NO3-), or sulfate (SO4 2- ).
  • the term “synthetic lithium solution” describes a solution comprising lithium that is not present in nature and obtained by a process for processing, refining, recovering or purifying lithium.
  • a synthetic lithium solution can be yielded by placing an acid into contact with a lithium-selective sorbent.
  • a synthetic lithium solution is a lithium eluate.
  • the term “synthetic lithium solution”, “lithium eluate”, or “eluate” are used interchangeably; therefore, embodiments described herein in relation to one of these terms shall be understood to apply to synthetic lithium solutions, lithium eluates, eluates, or a combination thereof.
  • a synthetic lithium solution, lithium eluate, or eluate is concentrated to yield a concentrated WSGR Docket No.50741-726.601 synthetic lithium solution, concentrated lithium eluate, or concentrated eluate; therefore, these concentrated solutions contain the same chemical species but at a higher solute concentration. Therefore, embodiments described herein in relation to a synthetic lithium solution, lithium eluate, or eluate shall be understood to apply to their concentrated counterparts.
  • a synthetic lithium solution is used in place of a liquid resource.
  • a synthetic lithium solution is combined with a liquid resource.
  • a synthetic lithium solution is a leachate solution (e.g., a leachate of one or more ores, a leachate of one or more minerals, a leachate of one or more clays, a leachate of waste or recycled materials comprising lithium).
  • a synthetic lithium solution is a brine concentrated by solar evaporation.
  • direct lithium extraction refers to a process involving the sorption or adsorption of lithium from solution. Direct lithium extraction can be carried out with a lithium-selective sorbent.
  • a lithium-selective sorbent can comprise an ion exchange material.
  • eluent refers to a liquid input to employed for the removal of lithium from a lithium-selective sorbent.
  • contact of an eluent to a lithium-selective sorbent to remove lithium from said sorbent generates an eluate (or equivalently termed lithium eluate or synthetic lithium solution).
  • An eluent can be acidic.
  • An eluent that has been placed in contact with a lithium-selective sorbent that releases lithium into the eluate is a lithium eluate.
  • the eluate is an acidic solution.
  • the protons of the acidic eluent displace the lithium on the ion exchange material to yield a synthetic lithium eluate.
  • the eluent comprises a gas dissolved in a liquid.
  • the eluent comprises carbon dioxide dissolved in a water.
  • the eluent comprises an acid dissolved in a liquid.
  • lithium purity can be expressed as the percentage of lithium in a solution as on the basis of the total metal ion content of the solution. In some embodiments, lithium purity is expressed in terms of the quantities or percentages of specific impurities that may be present in a lithium compound or a solution that comprises lithium.
  • the term “process fluid” refers to any liquid or solution that is used in any step or process according to the methods and systems for lithium recovery from a liquid resource as described herein. In some embodiments, the process fluid is the liquid resource. In WSGR Docket No.50741-726.601 some embodiments, the process fluid is the adjusting fluid. In some embodiments, the process fluid is the raffinate. In some embodiments, the process fluid is water.
  • the process fluid is acid (e.g., an acidic solution, a solution comprising acid).
  • the process fluid is base (e.g., a basic solution, a solution comprising base).
  • base e.g., a basic solution, a solution comprising base.
  • mother liquor is a liquid byproduct of a process for the generation of solid lithium carbonate from a lithium-containing solution.
  • Mother liquor as described herein is an aqueous solution that comprises lithium and additional salts.
  • pressure is quantified and measured in units commonly sued in the art, including bar, atmospheres (atm), psi (pounds per square inch), Pascals (Pa), Megapascals (MPa), and other commonly used unit.
  • Said units are sometimes specified in terms of their absolute pressure, or their pressure relative to the atmosphere.
  • absolute pressure this may optionally be indicated by adding “a” to the unit, as in psia, bara, atma, etc.
  • relative of “gauge” pressure this may optionally be indicated by adding “g” to the unit, as in psig, barg, atmg, etc.
  • the absolute pressure can be calculated by addition of the local atmospheric pressure to the gauge pressure. When “g” and “a” are not included in the units, all pressures herein are understood to be gauge pressures.
  • a system, a method, or a process for lithium recovery from a liquid resource may be employed in a system, a method, or a process for producing a lithium product from a liquid resource.
  • the methods and systems disclosed herein utilize ion exchange materials.
  • the lithium selective sorbent comprises an ion exchange material.
  • an ion exchange material is utilized in a variety of forms or as a constituent of a construct that comprises one or more ion exchange materials (e.g., a lithium selective sorbent composite).
  • an ion exchange material is utilized in a form that specifically enables or optimizes the performance of the method or system in which the ion exchange material is utilized.
  • an ion exchange material is utilized as a constituent of a construct that specifically enables or optimizes the performance of the method or system in which the ion exchange material is utilized.
  • ion exchange materials are coated. [0052] In some embodiments, ion exchange material is in the form of ion exchange particles. In some embodiments, ion exchange material is in the form of uncoated ion exchange particles. In some embodiments, ion exchange material is in the form of coated ion exchange particles.
  • ion exchange particles are coated or uncoated. In some embodiments, ion exchange particles are utilized as a mixture that comprises coated ion exchange particles and uncoated ion exchange particles. In some embodiments, ion exchange particles comprise one or more ion exchange materials. In some embodiments, ion exchange particles comprise a lithium- selective sorbent. [0053] In some embodiments, lithium selective sorbent composites are a construct that comprises ion exchange material that can be used according to the methods and systems described herein. In some embodiments, lithium selective sorbent composites comprise ion exchange material. In some embodiments, the ion exchange material is coated or uncoated. In some embodiments, the lithium selective sorbent composites are porous.
  • lithium selective sorbent composites comprise one or more ion exchange materials. In some embodiments, lithium selective sorbent composites comprise a lithium-selective sorbent. [0054] In some embodiments, lithium selective sorbent composites are formed into a bead, said bead comprising an ion exchange material.
  • ion exchange beads should be understood to apply to any embodiments for “ion exchange material”, or for any material composition comprising an ion exchange material, including but not limited to coated ion exchange material(s), beads comprising coated ion exchange material(s), ion exchange materials embedded in a structural support, ion exchange materials embedded in a matrix, composites comprising ion exchange material(s), lithium selective sorbent composites – wherein the lithium selective sorbent comprises an ion exchange material – , or combinations thereof.
  • lithium selective sorbent composites have diameters less than about one millimeter, contributing to a high pressure difference across a packed bed of lithium selective sorbent composite as a liquid resource and other fluids are pumped through the packed bed by application of an appropriate force.
  • lithium selective sorbent WSGR Docket No.50741-726.601 composites have diameters of at most about one millimeter, contributing to a high pressure difference across a packed bed of lithium selective sorbent composite as a liquid resource and other fluids are pumped through the packed bed by application of an appropriate force.
  • vessels with optimized geometries can be used to reduce the flow distance through the packed bed of lithium selective sorbent composite. These vessels can be networked with pH modulation units to achieve adequate control of the pH of the liquid resource.
  • a network of vessels loaded with lithium selective sorbent composite comprises two vessels, three vessels, four vessels, five vessels, six vessels, seven vessels, eight vessels, nine vessels, 10 vessels, 11 vessels, 12 vessels, 13-14 vessels, 15-20 vessels, 20-30 vessels, 30-50 vessels, 50-70 vessels, 70-100 vessels, or more than 100 vessels.
  • ion exchange material or a form thereof, or a construct comprised thereof, is loaded into an ion exchange device described herein.
  • an ion exchange device comprises a column, tank, or vessel.
  • an ion exchange device is a component of a system for lithium recovery from a liquid resource. Alternating flows of liquid resource, eluent, and other process fluids are optionally flowed through an ion exchange device to extract lithium from the liquid resource and produce a synthetic lithium solution, which is eluted from the ion exchange device using an eluent.
  • Lithium is an essential element for batteries and other technologies. Lithium is found in a variety of liquid resources, including natural and synthetic brines and leachate solutions from minerals, clays, and recycled products.
  • Lithium can be extracted from such liquid resources using an ion exchange process that utilizes ion exchange materials.
  • lithium selective sorbent composite comprise ion exchange materials in addition to other components.
  • lithium selective sorbent composite are utilized in methods for lithium recovery and systems for lithium recovery. Ion exchange materials can absorb lithium from a liquid resource while releasing hydrogen, and then elute lithium in acid while absorbing hydrogen. In methods for lithium recovery from a liquid resource, the ion WSGR Docket No.50741-726.601 exchange process can be repeated to extract lithium from a liquid resource and yield a synthetic lithium solution. The synthetic lithium solution can be further processed into chemicals for the battery industry or other industries.
  • ion exchange particles comprise ion exchange materials.
  • Ion exchange particles can be in the form of small particles, which together constitute a fine powder. Small sizes of ion exchange particles may be required to minimize the diffusion distance that lithium must travel to reach the core of the ion exchange particles and ensure the entirety of the ion exchange material within the ion exchange particle is utilized in the course of an ion exchange process or method for lithium recovery.
  • ion exchange particles are coated with coating materials that can minimize dissolution of the ion exchange particles while allowing efficient transfer of lithium and hydrogen to and from the ion exchange particles.
  • ion exchange material and/or ion exchange particles can be formed into lithium selective sorbent composite that can be loaded into an ion exchange device.
  • lithium selective sorbent composite comprise ion exchange materials in addition to other components and can be utilized in methods for lithium recovery and systems for lithium recovery.
  • the lithium selective sorbent composite as loaded into an ion exchange device, can be loaded such that void spaces are present between the lithium selective sorbent composite, and these void spaces can facilitate flow of liquids through the column. In some embodiments, a flow is initiated, modulated, or terminated by pumping. In some embodiments, the lithium selective sorbent composite hold their constituent ion exchange particles in place and prevent free movement of ion exchange particles throughout the ion exchange device. [0061] When ion exchange material is formed into lithium selective sorbent composite, the penetration of liquid resource and acid into the lithium selective sorbent composite by convention and diffusion can become unacceptably slow.
  • a slow rate of convection and diffusion of the acid and liquid resource into the lithium selective sorbent composite can slow the kinetics of lithium absorption and release thereby.
  • Slow kinetics of lithium absorption and release can create problems for the operation of an ion exchange device.
  • Slow kinetics of lithium absorption and release can consequently require correspondingly slow flow rates through an ion exchange device.
  • Slow kinetics of lithium absorption and release can also lead to low lithium recovery from the liquid resource and inefficient use of acid to elute the lithium according to the methods and systems described herein.
  • the lithium selective sorbent composites comprise networks of pores that facilitate the transport of liquids flowed through an ion exchange device into lithium selective sorbent composites.
  • the geometry and physical dimensions of pore networks in lithium selective sorbent composites can be strategically controlled to allow for faster and more complete access of liquid resource, washing water, acid, and other process fluids into the interior of the ion exchange bead. Faster and more complete access of liquid resource, washing water, acid, and other process fluids into the interior of the lithium selective sorbent composites leads to a more effective delivery lithium and hydrogen to the ion exchange material therein.
  • Another challenge to consider and overcome in a method or system for lithium recovery from a liquid resource using ion exchange materials is the undesired dissolution and degradation of the ion exchange materials.
  • Undesired dissolution and degradation of the ion exchange materials can occur during a step comprising lithium elution from the ion exchange material in acid.
  • Undesired dissolution and degradation of the ion exchange materials can occur during a step comprising lithium extraction from a liquid resource by the ion exchange material.
  • the lithium selective sorbent composites contain coated ion exchange particles that are comprised of an ion exchange material and a coating material.
  • the coating material can protect the ion exchange material from undesired dissolution and degradation during lithium elution from the ion exchange material into acid, during lithium uptake from a liquid resource into the ion exchange material, and during other steps of an ion exchange process according to the methods and systems described herein.
  • use of lithium selective sorbent composites that comprise coated ion exchange particles allows for the use of a concentrated acid as an acid eluent to yield a synthetic lithium solution.
  • an ion exchange material is selected for use in lithium selective sorbent composites based on one or more properties of the ion exchange material.
  • desirable properties of the ion exchange material comprise high lithium absorption capacity, high selectivity for lithium extraction from a liquid resource relative to WSGR Docket No.50741-726.601 extraction of other ions such as sodium and magnesium, strong lithium uptake in liquid resources including those with low concentrations of lithium, facile elution of lithium with a small excess of acid, fast ionic diffusion throughout the ion exchange material, combinations thereof, and sub-combinations thereof.
  • a coating material is selected for use as a coating for ion exchange particles based on its ability to prevent undesirable dissolution and chemical degradation of the ion exchange particles during lithium elution from the ion exchange particles in acid and also during lithium uptake by the ion exchange particles from liquid resources.
  • the liquid resource containing lithium is flowed through the ion exchange device so that the lithium selective sorbent composites absorb lithium from the liquid resource while releasing hydrogen.
  • an acid is pumped through the ion exchange device so that the lithium selective sorbent composites release lithium into the acid while absorbing hydrogen.
  • the ion exchange device is operated in a co-flow mode wherein the liquid resource and acid are alternately flowed through the ion exchange device in the same direction.
  • the ion exchange device is operated in counter-flow mode wherein the liquid resource and acid are alternately flowed through the ion exchange device in opposite directions.
  • water or other solutions is flowed through the ion exchange device for purposes such as adjusting pH in the ion exchange device or removing potential contaminants.
  • lithium selective sorbent composites form a fixed bed or a moving bed, wherein the moving bed can move in a direction opposed to the flows of liquid resource and acid.
  • lithium selective sorbent composites are moved between multiple ion exchange devices, wherein the lithium selective sorbent composites form a moving bed that can be transferred from one ion exchange device to another.
  • lithium selective sorbent composites are moved between multiple ion exchange devices, wherein different ion exchange devices are independently configured to accommodate a flow of liquid resource, a flow of acid, a flow of water, or a flow of another process fluid.
  • the liquid resource before or after the liquid resource is flowed through an ion exchange device, the liquid resource is subjected to other processes including other ion exchange processes, solvent extraction, evaporation, chemical treatment, precipitation to remove lithium, precipitation to remove other chemical species, or to otherwise treat the liquid resource.
  • the liquid resource containing lithium is flowed through the ion exchange device so that the ion exchange particles absorb lithium from the liquid resource while releasing hydrogen.
  • an acid is pumped through the ion exchange device so that the ion exchange particles release lithium into the acid while absorbing hydrogen.
  • the ion exchange device is operated in a co-flow mode wherein the liquid resource and acid are alternately flowed through the ion exchange device in the same direction.
  • the ion exchange device is operated in counter-flow mode wherein the liquid resource and acid are alternately flowed through the ion exchange device in opposite directions.
  • water or other solutions are flowed through the ion exchange device for purposes such as adjusting pH in the ion exchange device or removing potential contaminants.
  • ion exchange particles form a fixed bed or a moving bed, wherein the moving bed can move in a direction opposed to the flows of liquid resource and acid.
  • ion exchange particles are moved between multiple ion exchange devices, wherein the ion exchange particles form a moving bed that can be transferred from one ion exchange device to another.
  • ion exchange particles are moved between multiple ion exchange devices, wherein different ion exchange devices are independently configured to accommodate a flow of liquid resource, a flow of acid, a flow of water, or a flow of another process fluid.
  • the liquid resource before or after the liquid resource is flowed through an ion exchange device, the liquid resource is subjected to other processes including other ion exchange processes, solvent extraction, evaporation, chemical treatment, precipitation to remove lithium, precipitation to remove other chemical species, or to otherwise treat the liquid resource.
  • ion exchange material is treated with acid a synthetic lithium solution is produced.
  • the synthetic lithium solution is further processed to produce lithium chemicals.
  • lithium chemicals produced from synthetic lithium solutions are provided for an industrial application.
  • lithium chemicals produced from synthetic lithium solutions are further processed to produce one or more alternative lithium chemicals that are contemplated for use in an application for which the one or more alternative lithium chemicals is better suited as compared to the lithium chemicals.
  • the lithium selective sorbent is a protonated ion exchange material or an adsorbent.
  • said protonated ion exchange material is generated by treating a pre-activated ion exchange material with an acid.
  • said pre-activated ion exchange material comprises LiFePO4, LiMnPO4, Li2MTiO3, Li2MnO3, Li2SnO3, Li4Ti5O12, Li4Mn5O12, LiMn2O4, Li1.6Mn1.6O4, LiAlO2, LiCuO2, LiTiO2, Li4TiO4, Li7Ti11O24, Li3VO4, Li2Si3O7, Li2CuP2O7, modifications thereof, solid solutions thereof, or a combination thereof.
  • said lithium selective sorbent is an adsorbent.
  • the adsorbent comprises a crystalline lithium salt aluminate, a lithium aluminum intercalate, LiCl ⁇ 2Al(OH) 3 , crystalline aluminum trihydroxide (Al(OH) 3 ), gibbsite, beyerite, nordstrandite, alumina hydrate, bauxite, amorphous aluminum trihydroxide, activated alumina layered lithium-aluminum double hydroxides, Li Al2(OH)6Cl, combinations thereof, compounds thereof, or solid solutions thereof.
  • the adsorbent comprises a lithium aluminum intercalate.
  • a pre-activated ion exchange material is selected from the following list: an oxide, a phosphate, an oxyfluoride, a fluorophosphate, or combinations thereof.
  • an oxide, a phosphate, an oxyfluoride, a fluorophosphate, or combinations thereof independently further comprise: (i) lithium, and (ii) manganese or titanium.
  • the ion exchange material is an oxide that further comprises: (i) lithium, and (ii) manganese or titanium.
  • a coating material used to form a coating on the lithium selective sorbent is selected from the following list: a carbide, a nitride, an oxide, a phosphate, a fluoride, a polymer, carbon, a carbonaceous material, or combinations thereof.
  • the coating material comprises an oxide different from the oxide of the ion exchange material.
  • a coating material is selected from the following list: TiO2, ZrO2, MoO2, SnO2, Nb2O5, Ta2O5, SiO2, Li2TiO3, Li2ZrO3, Li2SiO3, Li2MnO3, Li2MoO3, LiNbO3, LiTaO3, AlPO4, LaPO4, ZrP2O7, MoP2O7, Mo2P3O12, BaSO4, AlF3, SiC, TiC, ZrC, Si3N4, ZrN, BN, carbon, graphitic carbon, amorphous carbon, hard carbon, diamond-like carbon, solid solutions thereof, or combinations thereof.
  • a coating material is selected from the following WSGR Docket No.50741-726.601 list: TiO2, ZrO2, MoO2, SiO2, Li2TiO3, Li2ZrO3, Li2SiO3, Li2MnO3, LiNbO3, AlF3, SiC, Si3N4, graphitic carbon, amorphous carbon, diamond-like carbon, or combinations thereof.
  • the ion exchange particles have an average diameter that is selected from the following list: less than 10 nm, less than 100 nm, less than 1,000 nm, less than 10,000 nm, or less than 100,000 nm.
  • the ion exchange particles have an average size that is selected from the following list: less than 200 nm, less than 2,000 nm, or less than 20,000 nm. In some embodiments, the ion exchange particles have an average diameter that is selected from the following list: at most 10 nm, at most 100 nm, at most 1,000 nm, at most 10,000 nm, or at most 100,000 nm. In some embodiments, the ion exchange particles have an average size that is selected from the following list: at most 200 nm, at most 2,000 nm, or at most 20,000 nm. [0072] It is recognized that measurements of average particle diameter can vary according to the method of determination utilized.
  • the average particle diameter can be determined using sieve analysis.
  • the average particle diameter can be determined using optical microscopy.
  • the average particle diameter can be determined using electron microscopy.
  • the average particle diameter can be determined using laser diffraction.
  • the average particle diameter is determined using laser diffraction, wherein a Bettersizer ST instrument is used.
  • the average particle diameter is determined using a Bettersizer ST instrument.
  • the average particle diameter is determined using laser diffraction, wherein an Anton-Parr particle size analyzer (PSA) instrument is used.
  • PSA Anton-Parr particle size analyzer
  • the average particle diameter is determined using an Anton-Parr PSA instrument.
  • the average particle diameter can be determined using dynamic light scattering.
  • the average particle diameter can be determined using static image analysis.
  • the average particle diameter can be determined using dynamic image analysis.
  • the ion exchange particles are secondary particles comprised of smaller primary particles that have an average diameter selected from the following list: less than 10 nm, less than 100 nm, less than 1,000 nm, or less than 10,000 nm.
  • smaller primary particles comprise an ion exchange material.
  • the ion exchange particles are secondary particles comprised of smaller primary particles that have an average diameter selected from the following list: at most 10 nm, at most 100 nm, at most 1,000 nm, or at most 10,000 nm.
  • smaller primary particles comprise an ion exchange material.
  • the ion exchange material or the ion exchange particles comprising an ion exchange material have a coating comprising a coating material with a thickness selected from the following list: less than 1 nm, less than 10 nm, less than 100 nm, or less than 1,000 nm.
  • the coating material has a thickness selected from the following list: less than 1 nm, less than 10 nm, or less than 100 nm.
  • the ion exchange material or the ion exchange particles comprising an ion exchange material have a coating comprising a coating material with a thickness selected from the following list: at most 1 nm, at most 10 nm, at most 100 nm, or at most 1,000 nm.
  • the coating material has a thickness selected from the following list: at most 1 nm, at most 10 nm, or at most 100 nm.
  • the ion exchange material and the coating material form one or more concentration gradients such that the chemical composition of coated ion exchange particles comprising the ion exchange material and the coating material ranges between two or more compositions.
  • the ion exchange material and the coating material form a concentration gradient within the coated ion exchange particles comprising the ion exchange material and the coating material that extends over a thickness selected from the following list: less than 1 nm, less than 10 nm, less than 100 nm, less than 1,000 nm, less than 10,000 nm, or less than 100,000 nm.
  • the ion exchange material and the coating material form a concentration gradient within the coated ion exchange particles comprising the ion exchange material and the coating material that extends over a thickness selected from the following list: at most 1 nm, at most 10 nm, at most 100 nm, at most 1,000 nm, at most 10,000 nm, or at most 100,000 nm.
  • coating thickness may be measured by any one or more of electron microscopy, optical microscopy, couloscopy, nanoindentation, atomic force microscopy, and X-ray fluorescence.
  • coating thickness may be inferred or extrapolated from data obtained according to an analytical method that indicates the bulk composition of the coated ion exchange particle, or the ion exchange material that further comprises the coating material. In some embodiments, coating thickness may be inferred by differential analysis of data obtained by analysis of ion exchange material that further comprises a coating material and data obtained by analysis ion exchange material that does not further comprise a coating material. In some embodiments, coating thickness may be inferred by differential analysis of data obtained by analysis of one or more coated ion exchange particles and data obtained by analysis of one or more uncoated ion exchange particles.
  • the ion exchange material is synthesized by a method selected from the following list: hydrothermal, solvothermal, sol-gel, solid state, molten salt flux, ion exchange, microwave, ball milling, precipitation, or vapor deposition. In some embodiments, the ion exchange material is synthesized by a method selected from the following list: hydrothermal, solid state, or microwave.
  • a coating material is deposited to form a coating by a method selected from the following list: chemical vapor deposition, atomic layer deposition, physical vapor deposition, hydrothermal, solvothermal, sol-gel, solid state, molten salt flux, ion exchange, microwave, wet impregnation, precipitation, titration, aging, ball milling, or combinations thereof.
  • the coating material is deposited to form a coating by a method selected from the following list: chemical vapor deposition, hydrothermal, titration, solvothermal, wet impregnation, sol-gel, precipitation, microwave, or combinations thereof.
  • a coating material is deposited to form a coating with physical characteristics selected from the following list: crystalline, amorphous, full coverage, partial coverage, uniform, non-uniform, or combinations thereof.
  • multiple coating materials are deposited to form multiple coatings on the ion exchange material in an arrangement selected from the following list: concentric, patchwork, or combinations thereof.
  • the lithium selective sorbent composites comprise a porogen that is a salt that can be dissolved out of the lithium selective sorbent composites to form a network of pores within the lithium selective sorbent composites.
  • the lithium selective sorbent composites comprise a porogen that is a salt that can be dissolved out of the lithium selective sorbent composites using a solution selected from the following list: water, ethanol, isopropyl alcohol, a surfactant mixture, an acid, a base, or combinations thereof.
  • the lithium selective sorbent composites comprise a porogen that is a material that thermally decomposes to form a gas at high temperature such that the thermal decomposition of the filler material forms a network of pores within the lithium selective sorbent composite.
  • the lithium selective sorbent composites comprise a porogen that is a material that thermally decomposes to form a gas at high temperature wherein the gas is selected from the following list: water vapor, oxygen, nitrogen, chlorine, carbon dioxide, nitrogen oxides, organic vapors, or combinations thereof.
  • the lithium selective sorbent composites are formed from dry powder.
  • the lithium selective sorbent composites are formed using a WSGR Docket No.50741-726.601 mechanical press, a pellet press, a tablet press, a pill press, a rotary press, or combinations thereof.
  • the lithium selective sorbent composites are approximately spherical with an average diameter selected from the following list: less than 10 ⁇ m, less than 100 ⁇ m, less than 1 mm, less than 1 cm, or less than 10 cm. In some embodiments, the lithium selective sorbent composites are approximately spherical with an average diameter selected from the following list: less than 200 ⁇ m, less than 2 mm, or less than 20 mm. In some embodiments, the lithium selective sorbent composites are approximately spherical with an average diameter selected from the following list: at most 10 ⁇ m, at most 100 ⁇ m, at most 1 mm, at most 1 cm, or at most 10 cm.
  • the lithium selective sorbent composites are approximately spherical with an average diameter selected from the following list: at most 200 ⁇ m, at most 2 mm, or at most 20 mm. [0084] In some embodiments, the lithium selective sorbent composites are tablet-shaped with a diameter of less than 1 mm, less than 2 mm, less than 4 mm, less than 8 mm, or less than 20 mm and with a height of less than 1 mm, less than 2 mm, less than 4 mm, less than 8 mm, or less than 20 mm.
  • the lithium selective sorbent composites are tablet- shaped with a diameter of at most 1 mm, at most 2 mm, at most 4 mm, at most 8 mm, or at most 20 mm and with a height of at most 1 mm, at most 2 mm, at most 4 mm, at most 8 mm, or at most 20 mm.
  • the lithium selective sorbent composites are embedded in a support structure, which can be a membrane, a spiral-wound membrane, a hollow fiber membrane, or a mesh.
  • the ion exchange beads are embedded on a support structure comprised of a polymer, a ceramic, or combinations thereof.
  • the lithium selective sorbent composites are loaded directly into an ion exchange column with no additional support structure.
  • the liquid resource has a lithium concentration selected from the following list: less than 100,000 mg/L, less than 10,000 mg/L, less than 1,000 mg/L, less than 100 mg/L, less than 10 mg/L, or combinations thereof. In some embodiments, the liquid resource has a lithium concentration selected from the following list: less than 5,000 mg/L, less than 500 mg/L, less than 50 mg/L, or combinations thereof.
  • the liquid resource has a lithium concentration selected from the following list: at most 100,000 mg/L, at most 10,000 mg/L, at most 1,000 mg/L, at most 100 mg/L, at most 10 mg/L, or combinations thereof. In some embodiments, the liquid resource has a lithium concentration selected from the following list: at most 5,000 mg/L, at most 500 mg/L, at most 50 mg/L, or combinations thereof.
  • the acid used for eluting lithium from the ion exchange material is selected from the following list: hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, acetic acid, or combinations thereof.
  • the acid used for eluting lithium from the ion exchange material is selected from the following list: hydrochloric acid, sulfuric acid, nitric acid, or combinations thereof.
  • the acid used for recovering lithium from the ion exchange material has an acid concentration selected from the following list: less than 0.1 M, less than 1.0 M, less than 5 M, less than 10 M, or combinations thereof. In some embodiments, the acid used for recovering lithium from the ion exchange material has an acid concentration selected from the following list: at most 0.1 M, at most 1.0 M, at most 5 M, at most 10 M, or combinations thereof. [0089] In some embodiments, the ion exchange material is utilized in an ion exchange process repeatedly over a number of cycles selected from the following list: greater than 10 cycles, greater than 30 cycles, greater than 100 cycles, greater than 300 cycles, or greater than 1,000 cycles.
  • the ion exchange material is utilized in an ion exchange process repeatedly over a number of cycles selected from the following list: greater than 50 cycles, greater than 100 cycles, or greater than 200 cycles. In some embodiments, the ion exchange material is utilized in an ion exchange process repeatedly over a number of cycles selected from the following list: at least 10 cycles, at least 30 cycles, at least 100 cycles, at least 300 cycles, at least 500 cycles, at least 1,000 cycles, at least 2,000 cycles, or at least 5,000 cycles.
  • a cycle comprises contacting a lithium-selective sorbent with a liquid resource to provide a lithiated lithium-selective sorbent and contacting the lithiated lithium-selective sorbent with an acidic solution (e.g., acid) to provide a synthetic lithium solution (e.g., lithium eluate).
  • an acidic solution e.g., acid
  • the lithium-selective sorbent is used (e.g., a process for generating a synthetic lithium solution is conducted) for at least 10 cycles, at least 50 cycles, at least 100 cycles, at least 250 cycles, at least 500 cycles, at least 1000 cycles, at least 2000 cycles, at least 3000 cycles, at least 4000 cycles, at least 5000 cycles, at least 6000 cycles, at least 7000 cycles, at least 8000 cycles, at least 9000 cycles, or at least 10000 cycles.
  • the synthetic lithium solution that is yielded from the ion exchange material is further processed into lithium chemicals, lithium compounds, or lithium raw materials using methods selected from the following list: solvent extraction, ion exchange, chemical precipitation, electrodialysis, electrowinning, evaporation with direct solar energy, evaporation with concentrated solar energy, evaporation with a heat transfer medium heated by concentrated solar energy, evaporation with heat from a geothermal brine, evaporation with heat from combustion, or combinations thereof.
  • the synthetic lithium solution that is yielded from the ion exchange material is further processed into lithium chemicals selected from the following list: lithium chloride, lithium carbonate, lithium hydroxide, lithium metal, lithium metal oxide, lithium metal phosphate, lithium sulfide, or combinations thereof.
  • the synthetic lithium solution that is yielded from the ion exchange material is further processed into lithium chemicals that are solid, liquid, hydrated, or anhydrous.
  • the lithium chemicals produced using the synthetic lithium solution are used in an industrial application selected from the following list: lithium batteries, metal alloys, glass, grease, or combinations thereof.
  • the lithium chemicals produced using the synthetic lithium solution derived from the ion exchange material are used in an industrial application selected from the following list: lithium batteries, metal alloys, glass, grease, or combinations thereof.
  • the lithium chemicals produced using the synthetic lithium solution derived from the coated ion exchange particles are used in an application selected from the following list: lithium batteries, lithium-ion batteries, lithium sulfur batteries, lithium solid-state batteries, and combinations thereof.
  • the ion exchange materials are synthesized in a lithiated state, wherein a sublattice of the ion exchange material is fully or partially occupied by lithium.
  • the ion exchange materials are synthesized in a hydrogenated state, wherein a sublattice of the ion exchange material is fully or partially occupied by hydrogen.
  • the term lithium-selective sorbent comprises all lithium-selective ion exchange materials.
  • Ion exchange materials that selectively absorb and release lithium ions are lithium-selective ion exchange materials.
  • lithium selective sorbent composites comprise a lithium-selective sorbent.
  • ion exchange particles comprise a lithium-selective sorbent.
  • lithium-selective sorbents comprise an inorganic material that selectively absorbs lithium over other ions.
  • a lithium selective sorbent is a crystalline lithium salt aluminate, a lithium aluminum intercalate, LiCl ⁇ 2Al(OH)3, crystalline aluminum trihydroxide (Al(OH)3), gibbsite, WSGR Docket No.50741-726.601 beyerite, nordstrandite, alumina hydrate, bauxite, amorphous aluminum trihydroxide, activated alumina layered lithium-aluminum double hydroxides, LiAl2(OH)6Cl, combinations thereof, compounds thereof, or solid solutions thereof.
  • Lithium-selective ion exchange materials can be used in a method for lithium recovery from a liquid resource.
  • Lithium-selective ion exchange materials can be used in a system for lithium recovery from a liquid resource.
  • Lithium-selective ion exchange materials can be used in an ion exchange device.
  • Lithium-selective ion exchange materials absorb lithium from a liquid resource while releasing hydrogen, and then elute lithium in an eluent while absorbing hydrogen from the eluent. This ion exchange process is optionally repeated to extract lithium from a liquid resource and yield a synthetic lithium solution.
  • the synthetic lithium solution is optionally further processed into chemicals for the battery industry or other industries.
  • the performance parameters of lithium recovery by an ion exchange material are reflected in the ability of the ion exchange material to absorb lithium from a liquid resource in high quantity and in high purity over long periods time.
  • a given amount of an ion exchange material contacts a given amount of liquid resource, wash solution, eluent solution, or other process fluids
  • the effectiveness of selective lithium absorption, washing, lithium release/elution, or other treatment depends on effective contact of process fluids with the ion exchange material.
  • effective contact implies that a given amount of ion exchange material is contacted with the same amount of process fluid, and that the composition of said fluid is the same as that contacting the entirety of the ion exchange material.
  • devices for lithium recovery be configured in a manner such that the ion exchange material can make uniform contact with process fluids.
  • uniform contact implies that a liquid resource from which lithium is extracted uniformly contacts an ion exchange material which absorbs lithium while releasing protons.
  • Optimizing the performance parameters of lithium recovery is advantageous for lithium production from liquid resources using ion exchange processes that utilize one or more ion exchange materials.
  • Disclosed herein are methods and systems for optimizing the performance parameters of lithium recovery using ion exchange materials that comprise lithium- selective sorbents by adjusting the concentration of lithium and pH of a liquid resource to be placed in contact with the ion exchange material.
  • Adjusting the concentration of lithium in a liquid resource can yield a concentration-adjusted liquid resource according to some embodiments.
  • WSGR Docket No.50741-726.601 [0099] Adjusting the concentration of lithium in a liquid resource can result in the most optimal utilization of an ion exchange material utilized for lithium recovery, and helps ensure a prolonged lifetime of the ion exchange material.
  • the concentration of lithium in a liquid resource is increased to result in the most optimal utilization of an ion exchange material.
  • the concentration of lithium in a liquid resource is decreased to result in the most optimal utilization of an ion exchange material.
  • the pH of the liquid resource is adjusted in addition to the concentration of lithium in a liquid resource to result in the most optimal utilization of an ion exchange material.
  • the most optimal utilization of an ion exchange material results in improved or optimized performance parameters for lithium recovery.
  • improved or optimized performance parameters comprise a longer useful lifetime of the ion exchange material used in the methods and systems described herein.
  • improved or optimized performance parameters comprise a higher lithium production rate for flow of the same amount of liquid resource across the ion exchange material used in the methods and systems described herein.
  • improved or optimized performance parameters comprise a higher lithium purity of the lithium provided by the ion exchange material used in the methods and systems described herein.
  • improved or optimized performance parameters comprise a greater quantity of lithium provided by a given quantity of ion exchange material over its useful lifetime when the ion exchange material is used according to the methods and systems described herein. In some embodiments, improved or optimized performance parameters comprise an increase in overall lithium recovery.
  • lithium is extracted from the liquid resources using inorganic lithium-selective sorbents that absorb lithium ions preferentially over other ions.
  • lithium- selective sorbents comprise lithium-selective ion exchange materials.
  • the term “lithium-selective ion-exchange material” refers to embodiments of “lithium-selective sorbent”.
  • the lithium-selective sorbent is a lithium-selective ion-exchange material. In some embodiments, the lithium-selective sorbent comprises lithium-selective ion-exchange particles. In some embodiments, the lithium selective sorbent comprises ion exchange particles. In some embodiments, the lithium-selective sorbent is an ion exchange material.
  • WSGR Docket No.50741-726.601 Process of extracting lithium from a liquid resource [0102]
  • a process for lithium extraction from a liquid resource comprising treating ion exchange beads alternately with acid, brine, and optionally other solutions, in a configuration where the beads move in the net opposite direction to the acid, brine, and optionally other solutions, thereby producing a lithium-enriched solution from the liquid resource.
  • the process comprises: (a) treating the ion exchange beads with acid under conditions suitable to absorb hydrogen to generate hydrogen-enriched beads and release lithium to generate a lithium-enriched solution; (b) optionally, washing the hydrogen-enriched beads with water to generate hydrogen-enriched beads substantially free of residual acid; (c) treating the hydrogen-enriched beads with the liquid resource under conditions suitable to absorb lithium to generate lithium-enriched beads; (d) optionally, washing the lithium-enriched beads with water to generate lithium-enriched beads substantially free of liquid resource; and (e) repeating the cycle to produce a lithium-enriched solution from the liquid resource.
  • the process of extracting lithium occurs by contacting solutions described above with ion exchange beads occurs within one or more of the devices for lithium extraction disclosed herein.
  • Non-limiting Examples of lithium extraction with such devices are provided in Examples 1 to 13 and associated Figures 1 to 13.
  • a process for lithium extraction from a liquid resource comprising treating ion exchange material alternately with acid, brine, and optionally other solutions, in a configuration where the ion exchange material moves in the net opposite direction to the acid, brine, and optionally other solutions, thereby producing a lithium- enriched solution from the liquid resource.
  • a process for lithium extraction from a liquid resource comprising treating ion exchange material alternately with acid, the liquid resource, and optionally other solutions, in a configuration where the ion exchange material moves in the net opposite direction to the acid, liquid resource, and optionally other solutions, thereby producing a lithium-enriched solution from the liquid resource.
  • a process for lithium extraction from a liquid resource comprising treating ion exchange material alternately with acid, brine, and optionally other solutions, in a configuration where the ion exchange material moves in the net opposite direction to the acid, brine, and optionally other solutions, thereby producing a lithium- enriched solution from the brine.
  • the process comprises: (a) treating the ion exchange material with acid under conditions suitable to absorb hydrogen to generate hydrogen-enriched material and release lithium to generate a lithium-enriched solution; (b) WSGR Docket No.50741-726.601 optionally, washing the hydrogen-enriched material with water to generate hydrogen-enriched material substantially free of residual acid; (c) treating the hydrogen-enriched material with the liquid resource under conditions suitable to absorb lithium to generate lithium-enriched material; (d) optionally, washing the lithium-enriched beads with water to generate lithium- enriched beads substantially free of liquid resource; and (e) repeating the cycle to produce a lithium-enriched solution from the liquid resource.
  • the ion exchange beads comprise ion exchange particles that reversibly exchange lithium and hydrogen and a structural matrix material, and having a pore network.
  • the liquid resource comprises a natural brine, a dissolve salt flat, a concentrated brine, a processed brine, a filtered brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, leachate from ores, leachate from minerals, leachate from clays leachate from recycled products, leachate from recycled materials, or combinations thereof.
  • a process for lithium extraction from a liquid resource comprising treating ion exchange beads alternately with acid, brine, and optionally other solutions, in a configuration where the beads move in the net opposite direction to the acid, brine, and optionally other solutions, thereby producing a lithium-enriched solution from the liquid resource
  • the process comprises: a) treating the ion exchange beads with acid under conditions suitable to absorb hydrogen to generate hydrogen-enriched beads and release lithium to generate a lithium-enriched solution; b) optionally, washing the hydrogen- enriched beads with water to generate hydrogen-enriched beads substantially free of residual acid; c) treating the hydrogen-enriched beads with the liquid resource under conditions suitable to absorb lithium to generate lithium-enriched beads; d) optionally, washing the lithium- enriched beads with water to generate lithium-enriched beads substantially free of liquid resource; and e) repeating the cycle to produce a lithium-enriched solution from the liquid resource.
  • a process for lithium extraction from a liquid resource comprising treating ion exchange particles alternately with the liquid resource, washing fluid, and acid, in a system for the extraction of lithium ions from a liquid resource, comprising: a. an ion exchange material; b. a ion exchange vessel; and c. a pH modulating setup for increasing the pH of the liquid resource in the system.
  • a process for lithium extraction from a liquid resource comprising treating ion exchange particles alternately with the liquid resource, a washing fluid, and an acid solution, with a system for the extraction of lithium ions from a WSGR Docket No.50741-726.601 liquid resource, comprising a stirred rank reactor, an ion exchange material, a pH modulating setup for increasing the pH of the liquid resource in the ion exchange vessel, and a compartment for containing the ion exchange material in the ion exchange vessel while allowing for removal of liquid resource, washing fluid, and acid solutions from the ion exchange vessel.
  • An aspect of the disclosure herein is a process for the extraction of lithium ions from a liquid resource, comprising: a) contacting an ion exchange material with the liquid resource; and b) increasing the pH of the liquid resource before contact with the ion exchange material, during contact with the ion exchange material, after contact with the ion exchange material and combinations thereof.
  • the process of contacting a liquid resource with an ion exchange material occurs within one or more of the devices for lithium extraction disclosed herein. In some embodiments, several such devices are connected, and the liquid resource undergoes a treatment to increase its pH when flowing from one such vessel to the next.
  • Another aspect described herein is a process for the extraction of lithium ions from a liquid resource, comprising: a) contacting an ion exchange material with the liquid resource; and b) increasing the pH of the liquid resource before contact with the ion exchange material, during contact with the ion exchange material, after contact with the ion exchange material, or combinations thereof.
  • increasing the pH of the liquid resource is before contacting the ion exchange material with the liquid resource.
  • increasing the pH of the liquid resource is during contacting the ion exchange material with the liquid resource.
  • increasing the pH of the liquid resource is after contacting the ion exchange material with the liquid resource.
  • increasing the pH of the liquid resource is before and during contacting the ion exchange material with the liquid resource. In some embodiments of the process, increasing the pH of the liquid resource is before and after contacting the ion exchange material with the liquid resource. In some embodiments of the process, increasing the pH of the liquid resource is during and after contacting the ion exchange material with the liquid resource. In some embodiments of the process, increasing the pH of the liquid resource is before, during, and after contacting the ion exchange material with the liquid resource. WSGR Docket No.50741-726.601 [0112] An aspect of the disclosure herein is a process, wherein the ion exchange material is loaded into a column.
  • the process further comprises: a) loading a liquid resource into one or more liquid resource tanks; b) connecting the column to the one or more liquid resource tanks; and c) passing the liquid resource from the one or more liquid resource tanks through the column, wherein the passing of the liquid resource occurs at least once.
  • the process further comprises increasing the pH of the liquid resource in one or more pH increasing tanks.
  • the process further comprises settling precipitates in one or more settling tanks.
  • the process further comprises storing the liquid resource in one or more storing tanks prior to or after circulating the liquid resource through the column.
  • An aspect of the disclosure herein is a process, wherein the process further comprises: a) loading the liquid resource into one or more liquid resource tanks; b) connecting the column to the one or more liquid resource tanks; c) passing the liquid resource from the one or more liquid resource tanks through the column, wherein the passing of the liquid resource occurs at least once; d) increasing the pH of the liquid resulting from c. in one or more pH increasing tanks; e) settling precipitates of the liquid resulting from d. in one or more settling tanks; and f) storing the liquid resulting from e. in one or more storing tanks.
  • An aspect of the disclosure herein is a process, wherein the ion exchange material is loaded in a plurality of columns.
  • a plurality of tanks is connected to the plurality of columns, wherein each of the plurality of tanks is immediately connected to one of the plurality of columns.
  • two or more of the plurality of columns forms at least one circuit.
  • at least one circuit is selected from a liquid resource circuit, a water washing circuit and an acid solution circuit.
  • the pH of the liquid resource is increased in the plurality of tanks connected to the plurality of columns in the liquid resource circuit.
  • the liquid resource circuit includes a plurality of columns connected to a plurality of tanks, wherein each of the plurality of tanks is immediately connected to one of the plurality of columns.
  • An aspect of the disclosure herein is a process, wherein the process further comprises: a) passing the liquid resource through a plurality of columns in the liquid resource circuit; b) passing an acid solution through a plurality of columns in the acid solution circuit one or more times; and c) passing water through a plurality of columns in the water washing circuit.
  • the process further comprises interchanging a plurality of columns between the liquid resource circuit, the water washing circuit and the acid solution circuit, such that: a) at least one of the plurality of columns in the liquid resource circuit becomes at least WSGR Docket No.50741-726.601 one of the plurality of columns in the water washing circuit and/or at least one of the plurality of columns in the acid solution circuit; b) at least one of the plurality of columns in the water washing circuit becomes at least one of the plurality of columns in the acid solution circuit and/or at least one of the plurality of columns in the liquid resource circuit; and/or c) at least one of the plurality of columns in the acid solution circuit becomes at least one of the plurality of columns in the liquid resource circuit and/or at least one of the plurality of columns in the water washing circuit.
  • An aspect of the disclosure herein is a process, wherein the ion exchange material is loaded into one or more compartments in a tank.
  • the process further comprises moving the liquid resource through the one or more compartments in the tank.
  • the tank comprises injection ports.
  • the process further comprises using the injection ports to increase the pH of the liquid resource before contact with the ion exchange material, during contact with the ion exchange material, after contact with the ion exchange material and combinations thereof.
  • the process further comprises using the injection ports to increase the pH of the liquid resource before contact with the ion exchange material, during contact with the ion exchange material, after contact with the ion exchange material, or combinations thereof.
  • An aspect of the disclosure herein is a process, wherein the column further comprises a plurality of injection ports.
  • the process further comprises using the plurality of injection ports to increase the pH of the liquid resource before contact with the ion exchange material, during contact with the ion exchange material, after contact with the ion exchange material and combinations thereof.
  • the process further comprises using the plurality of injection ports to increase the pH of the liquid resource before contact with the ion exchange material, during contact with the ion exchange material, after contact with the ion exchange material, or combinations thereof.
  • the ion exchange material comprises a plurality of ion exchange particles.
  • the plurality of ion exchange particles in the ion exchange material is selected from uncoated ion exchange particles, coated ion exchange particles and combinations thereof.
  • the ion exchange material is an ion exchange material.
  • the ion exchange material comprises a network of pores that allows liquids to move quickly from the surface of the ion exchange material to the plurality WSGR Docket No.50741-726.601 of ion exchange particles.
  • the ion exchange material is in the form of ion exchange beads. [0121]
  • the ion exchange material extracts lithium ions from a liquid resource.
  • the pH of the liquid resource optionally decreases.
  • Increasing the pH of the liquid resource in the system maintains the pH in a range that is suitable for lithium ion uptake by the ion exchange material.
  • increasing the pH comprises measuring the pH of the system and adjusting the pH of the system to an ideal pH range for lithium extraction.
  • an ideal pH range for the brine is optionally 6 to 9
  • a preferred pH range is optionally 4 to 9
  • an acceptable pH range is optionally 2 to 9.
  • increasing the pH comprises measuring the pH of the system and wherein the pH of the system is less than 6, less than 4, or less than 2, the pH of the system is adjusted to a pH of 2 to 9, a pH of 4 to 9, or a pH of 6 to 9.
  • increasing the pH comprises measuring the pH of the system and wherein the pH of the system is at most 6, at most 4, or at most 2, the pH of the system is adjusted to a pH of 2 to 9, a pH of 4 to 9, or a pH of 6 to 9.
  • the liquid resource is selected from the following list: a natural brine, a dissolved salt flat, a geothermal brine, seawater, concentrated seawater, desalination effluent, a concentrated brine, a processed brine, liquid from an ion exchange process, liquid from a solvent extraction process, a synthetic brine, leachate from ores, leachate from minerals, leachate from clays, leachate from sediments, leachate from recycled products, leachate from recycled materials, or combinations thereof.
  • a liquid resource is selected from the following list: a natural brine, a dissolved salt flat, a concentrated brine, a processed brine, a synthetic brine, a geothermal brine, liquid from an ion exchange process, liquid from a solvent extraction process, leachate from minerals, leachate from clays, leachate from recycled products, leachate from recycled materials, or combinations thereof.
  • the liquid resource is optionally pre-treated prior to entering the ion exchange reactor to remove suspended solids, hydrocarbons, organic molecules, iron, certain metals, or other chemical or ionic species.
  • the liquid resource is optionally fed into the ion exchange reactor without any pre-treatment following from its source.
  • the liquid resource is injected into a reservoir, salt lake, salt flat, basin, or other geologic deposit after lithium has been removed from the liquid resource.
  • other species are recovered from the liquid resource before or after lithium recovery.
  • the pH of the liquid resource is adjusted before, during, or after lithium recovery.
  • the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
  • the liquid resource comprises industrial effluents containing lithium.
  • the industrial effluents are selected from the following list: bleed streams from bicarbonation purification of lithium carbonate, mother liquors from lithium chemical production processes, waste streams from lithium hydroxide production, recycling process effluents from battery manufacturing, wastewater from lithium processing facilities, spent electrolytes from lithium battery production, lithium-containing industrial wastewaters, lithium-bearing byproduct streams from lithium refineries, residual solutions from lithium salt crystallization processes, or combinations thereof.
  • the industrial effluent is a bicarbonation stream from the purification of lithium carbonate, comprising a lithium carbonate stream treated with carbon dioxide to convert the lithium carbonate into soluble lithium bicarbonate.
  • said bicarbonation stream contains lithium at a concentration of 10 to 8,000 mg/L and has a pH of between at least 6 and at most 12.
  • other industrial effluent streams containing lithium have a pH range of 0 to 14, preferably 2 to 12, and most preferably 6 to 10, with lithium concentrations ranging from 10 to 10,000 mg/L, including concentrations of 10 to 50 mg/L, 50 to 100 mg/L, 100 to 500 mg/L, 500 to 1,000 mg/L, 1,000 to 5,000 mg/L, and 5,000 to 10,000 mg/L.
  • the industrial effluents are optionally pre-treated prior to lithium extraction to remove suspended solids, adjust pH, remove specific impurities, or a combination thereof.
  • the industrial effluents are processed without pre-treatment to recover lithium via the ion exchange processes described herein.
  • the brine is at a temperature of -20 to 20 °C, 20 to 50 °C, 50 to 100 °C, 100 to 200 °C, or 200 to 400 °C.
  • the brine is heated or cooled to precipitate or dissolve species in the brine, or to facilitate removal of metals from the brine.
  • the brine contains lithium at a concentration of less than 1 mg/L, 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, 2,000 to 5,000 mg/L, 5,000 to 10,000 mg/L, 10,000 to 20,000 mg/L, 20,000 to 80,000 mg/L, or greater than 80,000 mg/L.
  • the brine contains lithium at a concentration of at most 1 mg/L, 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, 2,000 to 5,000 mg/L, 5,000 to 10,000 mg/L, 10,000 to 20,000 mg/L, 20,000 to 80,000 mg/L, or at least 80,000 mg/L.
  • the brine contains magnesium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains calcium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains strontium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains barium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains magnesium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains calcium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains strontium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains barium at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains multivalent cations at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to WSGR Docket No.50741-726.601 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains multivalent ions at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains non- lithium impurities at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains transition metals at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains iron at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains manganese at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or greater than 150,000 mg/L.
  • the brine contains multivalent cations at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains multivalent ions at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains non-lithium impurities at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains transition metals at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains iron at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine contains manganese at a concentration of 0.01 to 0.1 mg/L, 0.1 to 1 mg/L, 1 to 10 mg/L, 10 to 100 WSGR Docket No.50741-726.601 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 100,000 mg/L, 100,000 to 150,000 mg/L, or at least 150,000 mg/L.
  • the brine is treated to produce a feed brine which has certain metals removed.
  • the feed brine contains iron at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
  • the feed brine contains manganese at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
  • the feed brine contains lead at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed brine contains zinc at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed brine contains lithium at a concentration of 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or greater than 2,000 mg/L.
  • the brine is treated to produce a feed brine which has certain metals removed.
  • the feed brine contains iron at a concentration of at most 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
  • the feed brine contains manganese at a concentration of at most 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
  • the feed brine contains lead at a concentration of at most 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
  • the feed brine contains zinc at a concentration of at most 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
  • the feed brine contains lithium at a concentration of 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or at least 2,000 mg/L.
  • the feed brine is processed to recover metals such as lithium and yield a spent brine or raffinate.
  • the raffinate contains residual quantities of the recovered metals at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, or 1,000 to 10,000 mg/L.
  • the feed brine is processed to recover metals such as lithium and yield a spent brine or raffinate.
  • the raffinate contains residual quantities of the recovered metals at a concentration of at most 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, 100 to 1,000 mg/L, or 1,000 to 10,000 mg/L.
  • the pH of the brine is corrected to less than 0, 0 to 1, 1 to 2, 2 to 4, 4 to 6, 6 to 8, 4 to 8, 8 to 9, 9 to 10, 9 to 11, or 10 to 12.
  • the pH of the WSGR Docket No.50741-726.601 brine is corrected to 2 to 4, 4 to 6, 6 to 8, 4 to 8, 8 to 9, 9 to 10, 9 to 11, or 10 to 12.
  • the pH of the brine is corrected to precipitate or dissolve metals. In one embodiment, the pH of the brine is corrected to at most 0, 0 to 1, 1 to 2, 2 to 4, 4 to 6, 6 to 8, 4 to 8, 8 to 9, 9 to 10, 9 to 11, or 10 to 12. [0132] In one embodiment, metals are precipitated from the brine to form precipitates. In one embodiment, precipitates include transition metal hydroxides, oxy-hydroxides, sulfide, flocculants, aggregate, agglomerates, or combinations thereof.
  • the precipitates include Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, ,Zr, Hf, V, Nb, Ta, Cr, Mo, W ,Mn, Tc, Fe, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, Br, I, At, other metals, or a combination thereof.
  • the precipitates are concentrated into a slurry, a filter cake, a wet filter cake, a dry filter cake, a dense slurry, or a dilute slurry.
  • the precipitates contain iron at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain manganese at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain lead at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain arsenic at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain magnesium at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, ,Zr, Hf, V, Nb, Ta, Cr, Mo, W ,Mn, Tc, Fe, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, Br, I, At, or other metals at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates are toxic and/or radioactive.
  • the precipitates contain iron at a concentration of at most 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain manganese at a concentration of at most 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain lead at a concentration of at most 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain arsenic at a concentration of at most 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to WSGR Docket No.50741-726.601 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain magnesium at a concentration of at most 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • the precipitates contain Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd, Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, Br, I, At, or other metals at a concentration of at most 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
  • precipitates are redissolved by combining the precipitates with acid. In one embodiment, precipitates are redissolved by combining the precipitates with acid in a mixing apparatus. In one embodiment, precipitates are redissolved by combining the precipitates with acid using a high-shear mixer.
  • Lithium is an essential element for batteries and other technologies. Lithium is found in a variety of liquid resources, including natural and synthetic brines and leachate solutions from minerals, clays, and recycled products. Lithium is optionally extracted from such liquid resources using an ion exchange process based on inorganic ion exchange materials.
  • Ion exchange materials absorb lithium from a liquid resource while releasing hydrogen, and then elute lithium into an acidic solution while absorbing hydrogen. This ion exchange process is optionally repeated to extract lithium from a liquid resource and yield a concentrated lithium solution. The concentrated lithium solution is optionally further processed into chemicals for the battery industry or other industries.
  • Ion exchange materials are optionally formed into beads and the beads are optionally loaded into ion exchange columns, stirred tank reactors, other reactors, or other systems for lithium extraction.
  • Alternating flows or aliquots of brine, acidic solution, and optionally other solutions are flowed through or flowed into an ion exchange column, reactors, or reactor system to extract lithium from the brine and produce a lithium concentrate, which is eluted from the column using the acidic solution.
  • the ion exchange material absorbs lithium while releasing hydrogen, where both the lithium and hydrogen are cations.
  • the release of hydrogen during lithium uptake will acidify the brine and limit lithium uptake unless the pH of the brine is optionally maintained in a suitable range to facilitate thermodynamically favorable lithium uptake and concomitant hydrogen release.
  • pH of the liquid resource is maintained near a set-point through addition of base to neutralized protons released from the ion exchange material into the liquid resource.
  • WSGR Docket No.50741-726.601 Treatment of the liquid resource [0137]
  • the pH of the liquid resource is adjusted before, during and/or after contact with the lithium-selective ion exchange material to maintain the pH in range that is suitable for lithium uptake.
  • bases such as NaOH, Ca(OH)2, CaO, KOH, or NH3 are optionally added to the brine as solids, aqueous solutions, or in other forms.
  • precipitation can remove base from solution, leaving less base available in solution to neutralize protons and maintain pH in a suitable range for lithium uptake in the ion exchange column.
  • precipitates that form due to base addition can clog the ion exchange column, including clogging the surfaces and pores of ion exchange beads and the voids between ion exchange beads. This clogging can prevent lithium from entering the beads and being absorbed by the ion exchange material.
  • an ideal pH range for the brine is optionally 5 to 7
  • a preferred pH range is optionally 4 to 8
  • an acceptable pH range is optionally 1 to 9.
  • an pH range for the brine is optionally about 1 to about 14, about 2 to about 13, about 3 to about 12, about 4 to about 12, about 4.5 to about 11, about 5 to about 10, about 5 to about 9, about 2 to about 5, about 2 to about 4, about 2 to about 3, about 3 to about 8, about 3 to about 7, about 3 to about 6, about 3 to about 5, about 3 to about 4, about 4 to about 10, about 4 to about 9, about 4 to about 8, about 4 to about 7, about 4 to about 6, about 4 to about 5, about 5 to about 6, about 5 to about 7, about 5 to about 8, about 6 to about 7, about 6 to about 8, or about 7 to about 8. [0139]
  • the liquid resource is subjected to treatment prior to ion exchange.
  • said treatment comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
  • precipitated metals are removed from the brine using a filter.
  • the filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a WSGR Docket No.50741-726.601 centrifugal filter with a fixed or moving bed, a metal screen, a perforated basket centrifuge, a three-point centrifuge, a peeler type centrifuge, or a pusher centrifuge.
  • the filter may use a scroll or a vibrating device.
  • the filter is horizontal, vertical, or may use a siphon.
  • a filter cake is prevented, limited, or removed by using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, or pumping suspensions across the surface of the filter.
  • the precipitated metals and a liquid is moved tangentially to the filter to limit cake growth.
  • gravitational, magnetic, centrifugal sedimentation, or other means of solid-liquid separation are used before, during, or after filtering to prevent cake formation.
  • a filter comprises a screen, a metal screen, a sieve, a sieve bend, a bent sieve, a high frequency electromagnetic screen, a resonance screen, or combinations thereof.
  • one or more particle traps are a solid-liquid separation apparatus.
  • one or more solid-liquid separation apparatuses are used in series or parallel.
  • a dilute slurry is removed from the tank, transferred to an external solid-liquid separation apparatus, and separated into a concentrated slurry and a solution with low or no suspended solids.
  • the concentrated slurry is returned to the tank or transferred to a different tank.
  • precipitate metals are transferred from a brine tank to another brine tank, from an acid tank to another acid tank, from a washing tank to another washing tank, from a brine tank to a washing tank, from a washing tank to an acid tank, from an acid tank to a washing tank, or from an acid tank to a brine tank.
  • solid-liquid separation apparatuses may use gravitational sedimentation.
  • solid-liquid separation apparatuses may include a settling tank, a thickener, a clarifier, a gravity thickener.
  • solid-liquid separation apparatuses are operated in batch mode, semi-batch mode, semi-continuous mode, or continuous mode.
  • solid-liquid separation apparatuses include a circular basin thickener with slurry entering through a central inlet such that the slurry is dispersed into the thickener with one or more raking components that rotate and concentrate the ion exchange particles into a zone where the particles can leave through the bottom of the thickener.
  • solid-liquid separation apparatuses include a deep cone, a deep cone tank, a deep cone compression tank, or a tank wherein the slurry is compacted by weight.
  • solid-liquid separation apparatuses include a tray thickener with a series of thickeners oriented vertically with a center axle and raking components.
  • solid-liquid separation apparatuses include a lamella type thickener with inclined plates or tubes that are smooth, flat, rough, or corrugated.
  • solid-liquid separation apparatuses include a gravity clarifier that is a rectangular basin with feed at one end and overflow at the opposite end optionally with paddles and/or a chain mechanism to move particles.
  • the solid-liquid separation apparatuses are a particle trap. [0145] In some embodiments, the solid-liquid separation apparatuses use centrifugal sedimentation.
  • solid-liquid separation apparatuses may include a tubular centrifuge, a multi-chamber centrifuge, a conical basket centrifuge, a scroll-type centrifuge, a sedimenting centrifuge, or a disc centrifuge.
  • precipitated metals are discharged continuously or intermittently from the centrifuge.
  • the solid-liquid separation apparatus is a hydrocyclone.
  • solid-liquid separation apparatus is an array of hydrocyclones or centrifuges in series and/or in parallel.
  • sumps are used to reslurry the precipitated metals.
  • the hydrocyclones have multiple feed points.
  • a hydrocyclone is used upside down.
  • liquid is injected near the apex of the cone of a hydrocyclone to improve sharpness of cut.
  • a weir rotates in the center of the particle trap with a feed of slurried precipitated metals entering near the middle of the apparatus, and precipitated metals get trapped at the bottom and center of the apparatus due to a “teacup effect”.
  • Treatment of the ion exchange material with chemical additives [0146]
  • described herein is a system for contacting the ion exchange material with chemical additives.
  • a system for extracting lithium from a liquid resource comprises the system for contacting the ion exchange material with chemical additives.
  • a method for extracting lithium from a liquid resource comprises contacting the ion exchange material with chemical additives. In some embodiments, a method for extracting lithium from a liquid resource comprises contacting the liquid resource, the wash solution, or the acidic solution with chemical additives prior to contacting the liquid resource, the wash solution, or the acidic solution with the ion exchange WSGR Docket No.50741-726.601 material. In some embodiments, the process of producing lithium by ion exchange makes use of said system to add chemical additives. In some embodiments, the ion exchange material is contacted with a chemical additive by directly treating the ion exchange material with the chemical additive.
  • the ion exchange material is contacted with a chemical additive by treating the liquid resource with one or more chemical additives, and then contacting said liquid resource containing chemical additives with the ion exchange material to absorb the lithium in the liquid resource.
  • the ion exchange material is contacted with a chemical additive by treating the process water with one or more chemical additives, and then contacting said process water containing chemical additives with the ion exchange material to wash the ion exchange material.
  • the ion exchange material is contacted with a chemical additive by treating an acid with one or more chemical additives, and then contacting said acid with the ion exchange material to elute lithium.
  • the ion exchange material is contacted with a chemical additive by treating a base with one or more chemical additives, and then contacting said base with the ion exchange material to adjust the pH of the liquid resource.
  • the ion exchange material is contacted with one or more chemical additives before lithium is absorbed from a liquid resource thereby.
  • the ion exchange material is contacted with one or more chemical additives while lithium is absorbed from a liquid resource thereby.
  • the ion exchange material is contacted with one or more chemical additives after lithium is absorbed from a liquid resource thereby.
  • the ion exchange material is contacted with one or more chemical additives before entrained brine is removed from the ion exchange beads by washing, direct application, or other methods. In some embodiments, the ion exchange material is contacted with one or more chemical additives while entrained brine is removed from the ion exchange beads by washing or other methods. In some embodiments, the ion exchange material is contacted with one or more chemical additives after entrained brine is removed from the ion exchange beads by washing or other methods. In some embodiments, the brine is removed from the ion exchange beads by treatment with a stream comprising one or more chemical additives.
  • said stream comprising one or more chemical additives comprises water, brine, a liquid resource, an aqueous solution, or a gas.
  • the ion exchange material is contacted with one or more chemical additives before said ion exchange beads are contacted with an acid to elute lithium.
  • the ion exchange material is contacted with one or more chemical additives while said ion exchange beads are contacted with an acid to elute lithium.
  • the ion exchange material is contacted with one or more chemical additives after said ion exchange beads are contacted with an acid to elute lithium.
  • the ion exchange material is contacted with chemical additives before and after each of steps (lithium absorption, removal of entrained brine, and elution) described above. In some embodiments, the ion exchange material is contacted with chemical additives before and/or after some of each of steps (lithium absorption, removal of entrained brine, and elution) described above. [0148] In some embodiments, the ion exchange material is contacted with chemical additives during each ion exchange cycle wherein each cycle comprises lithium absorption and lithium elution. In some embodiments, the ion exchange material is contacted with chemical additives during each ion exchange cycle or every other ion exchange cycle wherein each cycle comprises lithium absorption and lithium elution.
  • the ion exchange material is contacted with chemical additives every second ion exchange cycle wherein each cycle comprises lithium absorption and lithium elution. In some embodiments, the ion exchange material is contacted with chemical additives in even or uneven intervals of ion exchange cycles, wherein each cycle comprises lithium absorption and lithium elution. [0149] In some embodiments, the ion exchange material is contacted with one or more chemical additives during continuous cycles, wherein each cycle comprises lithium absorption and lithium elution. In some embodiments, the ion exchange material is contacted with one or more chemical additives during a single cycle, or a series of selected cycles.
  • the exposure of the ion exchange material to the one or more chemical additives during a period of cycles is paused or omitted.
  • one or more chemical additives are independently added (e.g., to the liquid resource, the washing solution, the acid solution, the ion exchange material, the raffinate, the lithium eluate) in discrete quantities at regular intervals throughout an ion exchange cycle.
  • one or more chemical additives are independently added in varying quantities at regular intervals throughout an ion exchange cycle.
  • one or more chemical additives are independently added in discrete quantities at irregular intervals throughout an ion exchange cycle.
  • one or more chemical additives are independently added in varying quantities at irregular intervals throughout an ion exchange cycle. Accordingly, one or more chemical additives can be independently added one or more times during an ion exchange cycle. In some embodiments, during an ion exchange cycle one or more chemical additives are independently added (e.g., to WSGR Docket No.50741-726.601 the liquid resource, the washing solution, the acid solution, the ion exchange material, the raffinate, the lithium eluate) 1 time to 10 times. [0151] In some embodiments, the ion exchange material is contacted with a chemical additive during absorption of lithium from a liquid resource.
  • the ion exchange material is contacted with a chemical additive during washing with a washing solution. In some embodiments, the ion exchange material is contacted with a chemical additive during washing with a washing process water. In some embodiments, the ion exchange material is contacted with a chemical additive during elution of absorbed lithium with an acid. In some embodiments, the ion exchange material is contacted with a chemical additive during one or more of the steps of ion exchange: absorption of lithium from a liquid resource, washing with a washing solution, or elution with an acid. [0152] In some embodiments, treatment of the liquid resource, wash water, or acid with the chemical additive occurs in a mixing tank.
  • treatment of the liquid resource, wash water, or acid with the chemical additive occurs in a mixing tank fitted with an agitator, an eductor, a nozzle, or a combination thereof.
  • treatment of the liquid resource, wash water, or acid with the chemical additive occurs in an inline mixer.
  • treatment of the liquid resource, wash water, or acid with the chemical additive occurs in an electrochemical cell.
  • treatment of the ion exchange material with a chemical additive adjusts the oxidation-reduction potential of the liquid resource, the process water, the acid, the base, the ion-exchange material or combinations thereof.
  • treatment of the ion exchange material with a chemical additive increases or decreases the oxidation-reduction potential of the liquid resource, the process water, the acid, the base, the ion-exchange material or combinations thereof.
  • treatment with a chemical additive is performed in conjunction with pH adjustment.
  • said pH adjustment is performed by addition of an acid or a base.
  • pH adjustment is performed to maintain the pH of the solution comprising said chemical additive at a value of about 1, about 2, about 3, about 4, about 5, about 6, about 7, about 8, about 9, about 10, about 11, about 12, about 13, or about 14.
  • pH adjustment is performed to maintain the pH of the solution comprising said chemical additive at a value of about 1 to about 14.
  • treatment of the ion exchange material with a chemical additive increases the oxidation state of the elements that the ion exchange material is comprised of.
  • treatment of the ion exchange material with a chemical WSGR Docket No.50741-726.601 additive decreases the oxidation state of the elements that the ion exchange material is comprised of.
  • treatment of the ion exchange material with a chemical additive increases the oxidation state of the elements that the ion exchange material is comprised of at the surface of the ion-exchange particles.
  • treatment of the ion exchange material with a chemical additive decreases the oxidation state of the elements that the ion exchange material is comprised of at the surface of the ion-exchange particles.
  • treatment of the ion exchange material with a chemical additive decreases the oxidation-reduction potential of the ion exchange material.
  • treatment of the ion exchange material with a chemical additive increases the oxidation-reduction potential of the ion exchange material.
  • treatment of the ion exchange material with a chemical additive decreases the oxidation-reduction potential at the surface of the ion-exchange material.
  • treatment of the ion exchange material with a chemical additive increases the oxidation-reduction potential at the surface of the ion-exchange material.
  • treatment of the ion exchange material with a chemical additive prevents a change in the crystal structure of the ion exchange material.
  • treatment of the ion exchange material with a chemical additive slows the change in the crystal structure of the ion exchange material.
  • treatment of the ion exchange material with a chemical additive prevents the decay of the ion exchange material.
  • treatment of the ion exchange material with a chemical additive prevents the decay of the oxide in the ion exchange material.
  • treatment of the ion exchange material with a chemical additive prevents the decay of the polymer matrix in the ion exchange material. In some embodiments, treatment of the ion exchange material with a chemical additive preserves the textural properties of the ion exchange material. In some embodiments, treatment of the ion exchange material with a chemical additive prevents the dissolution of the ion exchange material in the liquid resource, wash solution, acid, or combinations thereof. In some embodiments, treatment of the ion exchange material with a chemical additive increases the lifetime of the ion exchange material results in an increased production of lithium carbonate equivalents per kilogram of ion exchange material during the lifetime of said ion exchange material.
  • treatment of the ion exchange material with a chemical additive increases the purity of the lithium eluted from the ion exchange material.
  • Non-limiting exemplary embodiments in the WSGR Docket No.50741-726.601 examples section illustrate these types of effects of chemical additives on the ion exchange material.
  • contact of the ion exchange material with a chemical additive increases the lifetime of the ion exchange beads from about 100 cycles to about 1000 cycles of ion exchange, from about 10 cycles to about 100 cycles, from about 50 cycles to about 100 cycles, from about 100 cycles to about 200 cycles, from about 100 cycles to about 500 cycles, from about 100 cycles to about 1000 cycles, from about 200 cycles to about 500 cycles, from about 200 cycles to about 1000 cycles, from about 500 cycles to about 1000 cycles.
  • contact of the chemical additive results in an increase of the lifetime of the ion exchange beads by about 50 cycles to about 10,000 cycles.
  • contact of the ion exchange material with a chemical additive decreases the dissolution of the ion exchange material per cycle of ion exchange from about 1 % to about 0.01 % by mass, from about 1 % to about 0.1 % by mass, from about 1 % to about 0.5 % by mass, from about 10 % to about 0.01 % by mass, from about 10 % to about 0.1 % by mass, from about 10 % to about 1 % by mass, from about 0.5 % to about 0.01 % by mass, from about 0.5 % to about 0.1 % by mass, from about 0.1 % to about 0.01 % by mass.
  • contact of the ion exchange material with a chemical additive increases the molar purity of the lithium in the eluent from approximately 75 % to approximately 95 %, from approximately 75 % to approximately 90 %, from approximately 75 % to approximately 85 %, from approximately 75 % to approximately 80 %, from approximately 80 % to approximately 95 %, from approximately 80 % to approximately 90 %, from approximately 80 % to approximately 85 %, from approximately 85 % to approximately 95 %, from approximately 85 % to approximately 90 %.
  • the chemical additive comprises a redox agent.
  • a redox agent is a chemical agent that adjusts the oxidation-reduction potential of a liquid when dosed and mixed into said liquid.
  • the redox agent comprises a gas. In some embodiments, the redox agent comprises a liquid. In some embodiments, the redox agent comprises a solid. In some embodiments, the redox agent comprises a solution. In some embodiments, the redox agent comprises an aqueous solution. In some embodiments, the redox agent comprises a nonaqueous solution.
  • the chemical additive comprises an oxidant.
  • An oxidant is a chemical agent that adjusts the oxidation-reduction potential of a liquid to a higher value, leading to a chemical environment that is more oxidizing.
  • an oxidant such as WSGR Docket No.50741-726.601 sodium hypochlorite adjusts the oxidation-reduction potential of water from a value of about 350 mV to a value of about 600 mV, when dosed at about 600 mg/L.
  • the resulting oxidizing chemical environment may cause species in contact in said environments to undergo oxidation reactions.
  • Such oxidation reactions involve the loss of electrons of those species, resulting in them acquiring a higher oxidation state or valence state.
  • the resulting oxidizing environments prevent species in contact with said environment from undergoing reduction reactions.
  • said oxidant comprises one of more of oxygen, air, ozone, hydrogen peroxide, fluorine, chlorine, bromine, iodine, nitric acid, a nitrate compound, sodium hypochlorite, bleach, a chlorite, a chlorate, a perchlorate, potassium permanganate, a permanganate, sodium perborate, a perborate, mixtures thereof or combinations thereof.
  • said oxidant comprises one of more of oxygen, air, ozone, hydrogen peroxide, fluorine, chlorine, bromine, iodine, nitric acid, a nitrate compound, sodium hypochlorite, bleach, potassium permanganate, a permanganate (e.g., a permanganate compound, a permanganate salt, a solution comprising permanganate), sodium perborate, a perborate (e.g., a perborate compound , a perborate salt, a solution comprising perborate), hypochlorous acid, lithium hypochlorite, sodium hypochlorite, potassium hypochlorite, magnesium hypochlorite, calcium hypochlorite, strontium hypochlorite, a persulfate (e.g., a persulfate compound, , a persulfate salt, a solution comprising persulfate), hexavalent chromium compounds (e
  • the chemical additive does not comprise air. In some embodiments, the chemical additive is not air.
  • oxidants comprising bromine include bromine, hypobromite, hypobromous acid, bromite, bromate, tribromide, and perbromate, including salts thereof with countercations comprising lithium, sodium, potassium, magnesium, calcium, or strontium, and including solutions thereof.
  • oxidants comprising fluorine include fluorine, hypofluorous acid, hypofluorite, fluorite, fluorate, and perfluorate, including salts thereof with countercations comprising lithium, sodium, potassium, magnesium, calcium, or strontium, and including solutions thereof.
  • oxidants comprising iodine include iodine, hypoiodous acid, hypoiodite, iodiite, iodate, periodate, and triiodine, including salts thereof with countercations comprising lithium, sodium, potassium, magnesium, calcium, or strontium, and including solutions thereof.
  • oxidants comprising chlorine include chlorine, hypochlorite, chlorite, chlorate, and perchlorate, including salts WSGR Docket No.50741-726.601 thereof with countercations comprising lithium, sodium, potassium, magnesium, calcium, or strontium, and including solutions thereof.
  • the chemical additive does not include air, ozone, or hydrogen sulfide scavengers.
  • the chemical additive comprises a reductant.
  • a reductant is a chemical agent that adjusts the oxidation-reduction potential of a liquid to a lower value, leading to a chemical environment that is more reducing.
  • a reductant such as hydrogen adjusts the oxidation-reduction potential of water from a value of about 350 mV to a value of about 0 mV, when bubbled through water.
  • the resulting reducing chemical environment may cause species in contact in said environments to undergo reduction reactions.
  • Such reduction reactions involve the gain of electrons of those species, resulting in them acquiring a lower oxidation state or valence state.
  • the resulting reducing environments prevent species in contact with said environment from undergoing oxidation reactions.
  • said reductant comprises one of more of sodium bisulfite, sodium metabisulfite, sodium borohydride, formic acid, ascorbic acid, oxalic acid, potassium iodide, hydrogen, other reducing species, mixtures thereof, or combinations thereof.
  • one or more of the chemical additives are contacted with the ion exchange material as a pure gas, as a pure liquid, a mixture thereof, or a solution thereof.
  • a chemical additive is added (e.g., to the liquid resource, the washing solution, the acid solution, the ion exchange material, the raffinate, the lithium eluate) at a temperature (or within a temperature range) that is pre-determined, wherein the temperature (or temperature range) is the temperature (or temperature range) of the liquid or material to which the chemical additive is being added.
  • a chemical additive is added (e.g., to the liquid resource, the washing solution, the acid solution, the ion exchange material, the raffinate, the lithium eluate) at a temperature in the range of about -20 degrees Celsius to about 200 degrees Celsius, wherein the temperature is the temperature of the liquid or material to which the chemical additive is being added.
  • the chemical additive is dosed into the liquid resource, wash solution, or acidic eluent at a specific concentration chosen to optimize the performance of the system. In some embodiments, the chemical additive is dosed into the liquid resource, wash solution, or acidic eluent at a specific concentration chosen to optimize the performance of the method. In some embodiments, the concentration of the chemical additive in said liquid resource, wash solution, or acidic eluent is greater than about 0.1 milligrams per liter and less than about 10,000 milligrams per liter. In some embodiments, said concentration is greater WSGR Docket No.50741-726.601 than about 1 milligram per liter and less than about 50 milligrams per liter.
  • said concentration is greater than about 50 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, said concentration is greater than about 100 milligrams per liter and less than about 200 milligrams per liter. In some embodiments, said concentration is greater than about 200 milligrams per liter and less than about 300 milligrams per liter. In some embodiments, said concentration is greater than about 300 milligrams per liter and less than about 400 milligrams per liter. In some embodiments, said concentration is greater than about 400.0 milligrams per liter and less than about 500.0 milligrams per liter.
  • said concentration is greater than about 500.0 milligrams per liter and less than about 600.0 milligrams per liter. In some embodiments, said concentration is greater than about 600.0 milligrams per liter and less than about 700.0 milligrams per liter. In some embodiments, said concentration is greater than about 700.0 milligrams per liter and less than about 800.0 milligrams per liter. In some embodiments, said concentration is greater than about 800.0 milligrams per liter and less than about 1200.0 milligrams per liter. In some embodiments, said concentration is greater than about 1000.0 milligrams per liter and less than about 4000.0 milligrams per liter.
  • said concentration is greater than about 4000.0 milligrams per liter and less than about 10,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 9000.0 milligrams per liter and less than about 100,000.0 milligrams per liter. In some embodiments, the concentration of the chemical additive in said liquid resource, wash solution, or acidic eluent is at least about 0.1 milligrams per liter and at most about 10,000 milligrams per liter. In some embodiments, said concentration is at least about 1 milligram per liter and at most about 50 milligrams per liter. In some embodiments, said concentration is at least about 50 milligrams per liter and at most about 100 milligrams per liter.
  • said concentration is at least about 100 milligrams per liter and at most about 200 milligrams per liter. In some embodiments, said concentration is at least about 200 milligrams per liter and at most about 300 milligrams per liter. In some embodiments, said concentration is at least about 300 milligrams per liter and at most about 400 milligrams per liter. In some embodiments, said concentration is at least about 400.0 milligrams per liter and at most about 500.0 milligrams per liter. In some embodiments, said concentration is at least about 500.0 milligrams per liter and at most about 600.0 milligrams per liter.
  • said concentration is at least about 600.0 milligrams per liter and at most about 700.0 milligrams per liter. In some embodiments, said concentration is at least about 700.0 milligrams per liter and at most about 800.0 milligrams per liter. In some embodiments, said concentration is at least about 800.0 WSGR Docket No.50741-726.601 milligrams per liter and at most about 1200.0 milligrams per liter. In some embodiments, said concentration is at least about 1000.0 milligrams per liter and at most about 4000.0 milligrams per liter. In some embodiments, said concentration is at least about 4000.0 milligrams per liter and at most about 10,000.0 milligrams per liter.
  • said concentration is at least about 9000.0 milligrams per liter and at most about 100,000.0 milligrams per liter.
  • ozone is dosed into the liquid resource at a specific concentration chosen to optimize the performance of the system.
  • sodium hypochlorite is dosed into the liquid resource at a specific concentration chosen to optimize the performance of the system.
  • sodium hypochlorite is dosed into the liquid resource at a specific concentration chosen to optimize the performance of the method.
  • the concentration of the sodium hypochlorite in said liquid resource is greater than about 0.1 milligrams per liter and less than about 1,000 milligrams per liter.
  • said concentration is greater than about 1 milligram per liter and less than about 50 milligrams per liter. In some embodiments, said concentration is greater than about 50 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, said concentration is greater than about 100 milligrams per liter and less than about 200 milligrams per liter. In some embodiments, said concentration is greater than about 200 milligrams per liter and less than about 300 milligrams per liter. In some embodiments, said concentration is greater than about 300 milligrams per liter and less than about 400 milligrams per liter.
  • said concentration is greater than about 400.0 milligrams per liter and less than about 500.0 milligrams per liter. In some embodiments, said concentration is greater than about 500.0 milligrams per liter and less than about 600.0 milligrams per liter. In some embodiments, said concentration is greater than about 600.0 milligrams per liter and less than about 700.0 milligrams per liter. In some embodiments, said concentration is greater than about 700.0 milligrams per liter and less than about 800.0 milligrams per liter. In some embodiments, said concentration is greater than about 800.0 milligrams per liter and less than about 1,000.0 milligrams per liter.
  • said concentration is greater than about 1000.0 milligrams per liter and less than about 3,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 21000.0 milligrams per liter and less than about 5,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 4000.0 milligrams per liter and less than about 10,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 9000.0 milligrams per liter and less than about 50,000.0 milligrams per liter.
  • said concentration is greater than WSGR Docket No.50741-726.601 about 40,000.0 milligrams per liter and less than about 100,000.0 milligrams per liter.
  • the concentration of the sodium hypochlorite in said liquid resource is at least about 0.1 milligrams per liter and at most about 1,000 milligrams per liter.
  • said concentration is at least about 1 milligram per liter and at most about 50 milligrams per liter.
  • said concentration is at least about 50 milligrams per liter and at most about 100 milligrams per liter.
  • said concentration is at least about 100 milligrams per liter and at most about 200 milligrams per liter.
  • said concentration is at least about 200 milligrams per liter and at most about 300 milligrams per liter. In some embodiments, said concentration is at least about 300 milligrams per liter and at most about 400 milligrams per liter. In some embodiments, said concentration is at least about 400.0 milligrams per liter and at most about 500.0 milligrams per liter. In some embodiments, said concentration is at least about 500.0 milligrams per liter and at most about 600.0 milligrams per liter. In some embodiments, said concentration is at least about 600.0 milligrams per liter and at most about 700.0 milligrams per liter.
  • said concentration is at least about 700.0 milligrams per liter and at most about 800.0 milligrams per liter. In some embodiments, said concentration is at least about 800.0 milligrams per liter and at most about 1,000.0 milligrams per liter. In some embodiments, said concentration is at least about 1000.0 milligrams per liter and at most about 3,000.0 milligrams per liter. In some embodiments, said concentration is at least about 21000.0 milligrams per liter and at most about 5,000.0 milligrams per liter. In some embodiments, said concentration is at least about 4000.0 milligrams per liter and at most about 10,000.0 milligrams per liter.
  • said concentration is at least about 9000.0 milligrams per liter and at most about 50,000.0 milligrams per liter. In some embodiments, said concentration is at least about 40,000.0 milligrams per liter and at most about 100,000.0 milligrams per liter.
  • hydrogen peroxide is dosed into the liquid resource at a specific concentration chosen to optimize the performance of the system. In some embodiments, hydrogen peroxide is dosed into the liquid resource at a specific concentration chosen to optimize the performance of the method. In some embodiments, the concentration of the hydrogen peroxide in said liquid resource is greater than about 0.1 milligrams per liter and less than about 1,000 milligrams per liter.
  • said concentration is greater than about 1 milligram per liter and less than about 50 milligrams per liter. In some embodiments, said concentration is greater than about 50 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, said concentration is greater than about 100 milligrams per liter and less than about 200 milligrams per liter. In some embodiments, WSGR Docket No.50741-726.601 said concentration is greater than about 200 milligrams per liter and less than about 300 milligrams per liter. In some embodiments, said concentration is greater than about 300 milligrams per liter and less than about 400 milligrams per liter.
  • said concentration is greater than about 400.0 milligrams per liter and less than about 500.0 milligrams per liter. In some embodiments, said concentration is greater than about 500.0 milligrams per liter and less than about 600.0 milligrams per liter. In some embodiments, said concentration is greater than about 600.0 milligrams per liter and less than about 700.0 milligrams per liter. In some embodiments, said concentration is greater than about 700.0 milligrams per liter and less than about 800.0 milligrams per liter. In some embodiments, said concentration is greater than about 800.0 milligrams per liter and less than about 1,000.0 milligrams per liter.
  • said concentration is greater than about 1000.0 milligrams per liter and less than about 3,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 21000.0 milligrams per liter and less than about 5,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 4000.0 milligrams per liter and less than about 10,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 9000.0 milligrams per liter and less than about 50,000.0 milligrams per liter. In some embodiments, said concentration is greater than about 40,000.0 milligrams per liter and less than about 100,000.0 milligrams per liter.
  • the concentration of the hydrogen peroxide in said liquid resource is at least about 0.1 milligrams per liter and at most about 1,000 milligrams per liter. In some embodiments, said concentration is at least about 1 milligram per liter and at most about 50 milligrams per liter. In some embodiments, said concentration is at least about 50 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, said concentration is at least about 100 milligrams per liter and at most about 200 milligrams per liter. In some embodiments, said concentration is at least about 200 milligrams per liter and at most about 300 milligrams per liter.
  • said concentration is at least about 300 milligrams per liter and at most about 400 milligrams per liter. In some embodiments, said concentration is at least about 400.0 milligrams per liter and at most about 500.0 milligrams per liter. In some embodiments, said concentration is at least about 500.0 milligrams per liter and at most about 600.0 milligrams per liter. In some embodiments, said concentration is at least about 600.0 milligrams per liter and at most about 700.0 milligrams per liter. In some embodiments, said concentration is at least about 700.0 milligrams per liter and at most about 800.0 milligrams per liter.
  • said concentration is at least about 800.0 milligrams per liter and at most about 1,000.0 milligrams per liter.
  • said WSGR Docket No.50741-726.601 concentration is at least about 1000.0 milligrams per liter and at most about 3,000.0 milligrams per liter.
  • said concentration is at least about 21000.0 milligrams per liter and at most about 5,000.0 milligrams per liter.
  • said concentration is at least about 4000.0 milligrams per liter and at most about 10,000.0 milligrams per liter.
  • said concentration is at least about 9000.0 milligrams per liter and at most about 50,000.0 milligrams per liter. In some embodiments, said concentration is at least about 40,000.0 milligrams per liter and at most about 100,000.0 milligrams per liter.
  • ozone is dosed into the wash solution at a specific concentration chosen to optimize the performance of the system. In some embodiments, ozone is dosed into the wash solution at a specific concentration chosen to optimize the performance of the method. In some embodiments, the concentration of the ozone in said wash solution is greater than about 0.1 milligrams per liter and less than about 10,000 milligrams per liter.
  • the concentration of the ozone in said wash solution is at least about 0.1 milligrams per liter and at most about 10,000 milligrams per liter.
  • sodium hypochlorite is dosed into the wash solution at a specific concentration chosen to optimize the performance of the system.
  • sodium hypochlorite is dosed into the wash solution at a specific concentration chosen to optimize the performance of the method.
  • the concentration of the sodium hypochlorite in said wash solution is greater than about 0.1 milligrams per liter and less than about 10,000 milligrams per liter.
  • the concentration of the sodium hypochlorite in said wash solution is at least about 0.1 milligrams per liter and at most about 10,000 milligrams per liter.
  • hydrogen peroxide is dosed into the wash solution at a specific concentration chosen to optimize the performance of the system.
  • hydrogen peroxide is dosed into the wash solution at a specific concentration chosen to optimize the performance of the method.
  • the concentration of the hydrogen peroxide in said wash solution is greater than about 0.1 milligrams per liter and less than about 10,000 milligrams per liter.
  • the concentration of the hydrogen peroxide in said wash solution is at least about 0.1 milligrams per liter and at most about 10,000 milligrams per liter.
  • sodium metabisulfite is dosed into the wash solution at a specific concentration chosen to optimize the performance of the system.
  • sodium metabisulfite is dosed into the wash solution at a specific concentration chosen to optimize the performance of the method.
  • the concentration of WSGR Docket No.50741-726.601 the sodium metabisulfite in said wash solution is greater than about 0.1 milligrams per liter and less than about 10,000 milligrams per liter.
  • the concentration of the sodium metabisulfite in said wash solution is at least about 0.1 milligrams per liter and at most about 10,000 milligrams per liter.
  • the value of oxidation-reduction potential of the liquid resource is greater than about 50.0 mV and less than about 800.0 mV. In some embodiments, the value of oxidation-reduction potential of the liquid resource is at least about 50.0 mV and at most about 800.0 mV.
  • treatment of the liquid resource with a chemical additive adjusts the oxidation-reduction potential of the liquid resource.
  • the value of oxidation-reduction potential of the wash solution is greater than about 50.0 mV and less than about 800.0 mV. In some embodiments, the value of oxidation-reduction potential of the wash solution is at least about 50.0 mV and at most about 800.0 mV. In some embodiments, treatment of the wash solution with a chemical additive adjusts the oxidation-reduction potential of the wash water solution. [0178] In some embodiments, treatment of the acidic solution with a chemical additive adjusts the oxidation-reduction potential of the acidic solution. In some embodiments, the value of oxidation-reduction potential of the acidic solution is greater than about 50.0 mV and less than about 800.0 mV.
  • the value of oxidation-reduction potential of the acidic solution is at least about 50.0 mV and at most about 800.0 mV.
  • treatment of the ion exchange material with a chemical additive adjusts the oxidation-reduction potential of the ion exchange material.
  • the value of oxidation-reduction potential of the ion exchange material is greater than about 50.0 mV and less than about 800.0 mV. In some embodiments, the value of oxidation-reduction potential of the ion exchange material is at least about 50.0 mV and at most about 800.0 mV.
  • contacting a chemical additive with the ion exchange material results in a change in the oxidation state of one or more cations within said ion exchange material.
  • said change in the oxidation state of one or more cations within said ion exchange material has an absolute value of 1, 2, 3, 4, 5, 6, or 7.
  • said change in the oxidation state of one or more cations within said ion exchange material has an absolute value of 1 or 2.
  • said change in the oxidation state of one or more cations within said ion exchange material has an absolute value WSGR Docket No.50741-726.601 of 1.
  • said change in the oxidation state of one or more cations within said ion exchange material has an absolute value of 2.
  • contact of a chemical additive with the ion exchange material results in an increase in the oxidation state of one or more cations within said ion exchange material.
  • contact of a chemical additive with the ion exchange material results in a change in the oxidation state of one or more cations within said ion exchange material from 1 to 2, from 2 to 3, from 2 to 4, from 3 to 4, from 4 to 5, from 5 to 6, and/or from 6 to 7.
  • contact of a chemical additive with the ion exchange material results in a decrease in the oxidation state of one or more cations within said ion exchange material.
  • contact of a chemical additive with the ion exchange material results in a change in the oxidation state of one or more cations within said ion exchange material from 7 to 6, from 6 to 5, from 5 to 4, from 4 to 3, from 4 to 2, from 3 to 2, and/or from 2 to 1.
  • the oxidation state of one or more cations within the ion exchange material prior to contacting a chemical additive is 1, 2, 3, 4, 5, 6, or 7.
  • the oxidation state of one or more cations within the ion exchange material prior to contacting a chemical additive is 2 or 3. In some embodiments, the oxidation state of one or more cations within the ion exchange material prior to contacting a chemical additive is 1. In some embodiments, the oxidation state of one or more cations within the ion exchange material after contacting a chemical additive is 1, 2, 3, 4, 5, 6, or 7. In some embodiments, the oxidation state of one or more cations within the ion exchange material after contacting a chemical additive is 3 or 4. In some embodiments, the oxidation state of one or more cations within the ion exchange material after contacting a chemical additive is 1.
  • the one or more cations within the ion exchange material comprises manganese. In some embodiments, the one or more cations within the ion exchange material comprises titanium. In some embodiments, the one or more cations within the ion exchange material comprises lithium. In some embodiments, the one or more cations within the ion exchange material comprises hydrogen. [0181] In some embodiments, contacting a chemical additive with the ion exchange material results in a change (e.g., an increase, a decrease) in the average oxidation state of the cations within said ion exchange material (e.g., the number average oxidation state of all cations within the ion exchange material or an aliquot or a particle thereof).
  • a change e.g., an increase, a decrease
  • contacting a chemical additive with the ion exchange material results in a change in the average oxidation state of the cations within said ion exchange material, wherein the absolute value of said change in the average oxidation state is in the range of about 0.1 to about 1.0.
  • the change is a decrease.
  • the change is an increase.
  • said change in the average oxidation state of the cations within said ion exchange material has an absolute value of about 0.1, about 0.2, about 0.3, about 0.4, about 0.5, about 0.6, about 0.7, about 0.8, about 0.9, or about 1.0.
  • the average oxidation state of the cations within the ion exchange material prior to contacting a chemical additive is about 1.0, about 1.1, about 1.2, about 1.3, about 1.4, about 1.5, about 1.6, about 1.7, about 1.8, about 1.9, about 2.0, about 2.1, about 2.2, about 2.3, about 2.4, about 2.5, about 2.6, about 2.7, about 2.8, about 2.9, about 3.0, about 3.1, about 3.2, about 3.3, about 3.4, about 3.5, about 3.6, about 3.7, about 3.8, about 3.9, about 4.0, about 4.1, about 4.2, about 4.3, about 4.4, about 4.5, about 4.6, about 4.7, about 4.8, about 4.9, about 5.0, about 5.1, about 5.2, about 5.3, about 5.4, about 5.5, about 5.6, about 5.7, about 5.8, about 5.9, about 6.0, about 6.1, about 6.2, about 6.3, about 6.4, about 6.5
  • the average oxidation state of the cations within the ion exchange material prior to contacting a chemical additive is about 1.4, about 1.5, about 1.6, about 1.7, about 1.8, about 1.9, about 2.0, about 2.1, about 2.2, about 2.3, about 2.4, about 2.5, or about 2.6.
  • the average oxidation state of the cations within the ion exchange material after contacting a chemical additive is about 1.0, about 1.1, about 1.2, about 1.3, about 1.4, about 1.5, about 1.6, about 1.7, about 1.8, about 1.9, about 2.0, about 2.1, about 2.2, about 2.3, about 2.4, about 2.5, about 2.6, about 2.7, about 2.8, about 2.9, about 3.0, about 3.1, about 3.2, about 3.3, about 3.4, about 3.5, about 3.6, about 3.7, about 3.8, about 3.9, about 4.0, about 4.1, about 4.2, about 4.3, about 4.4, about 4.5, about 4.6, about 4.7, about 4.8, about 4.9, about 5.0, about 5.1, about 5.2, about 5.3, about 5.4, about 5.5, about 5.6, about 5.7, about 5.8, about 5.9, about 6.0, about 6.1, about 6.2, about 6.3, about 6.4, about 6.5,
  • the average oxidation state of the cations within the ion exchange material after contacting a chemical additive is about 1.6, about 1.7, about 1.8, about 1.9, about 2.0, about 2.1, about 2.2, about 2.3, about 2.4, about 2.5, about 2.6, or about 2.7.
  • treatment of the liquid resource, wash water, or acidic eluent solution with a chemical additive results in the destruction of a soluble chemical species.
  • the treated liquid resource, wash water, or acidic eluent solution has a different pH than before treatment.
  • the pH of said treated liquid resource, wash water, or acidic eluent solution is adjusted prior to contact with the ion exchange material.
  • the treated liquid resource, wash water, or acidic WSGR Docket No.50741-726.601 eluent solution has a different oxidation-reduction potential than before treatment.
  • the oxidation-reduction potential of said treated liquid resource, wash water, or acidic eluent solution is adjusted prior to contact with the ion exchange material.
  • Vessels for beds of ion exchange beads [0186] For commercial production of lithium using ion exchange, it is desirable to construct large-scale ion exchange modules containing large quantities of ion exchange beads. However, most large vessels capable of holding about one tonne or more of ion exchange beads have large fluid flow distances of about one meter or more. These fluid flow distances cause large pressure drops.
  • the ion exchange beads are loaded into vessels facilitating flow across the ion exchange beads with a shorter fluid flow distance. These vessels are designed to evenly distribute flow of the liquid resource and other fluids through the ion exchange beads. In some embodiments, these vessels minimize the distance that the fluid flows as it contacts the ion exchange beads. In some embodiments, the vessels contain fluidized beds of ion exchange beads. In some embodiments, the vessels contain fixed beds of ion exchange beads. [0187] In some embodiments, the vessel is oriented vertically, horizontally, or at any angle relative to the horizontal axis. In some embodiments, the vessel is cylindrical, rectangular, spherical, another shape, or a combinations thereof.
  • the vessel can have a constant cross-sectional area or a varying cross-sectional area.
  • the vessel has a height to diameter ratio of less than about 0.1, 0.5, less than about 1, less than about 2, less than about 5, less than about 10, more than about 0.1, more than about 0.5, more than about 1, more than about 2, more than about 5, more than about 10.
  • the vessel has a height to diameter ratio of at most about 0.1, at most about 0.5, at most about 1, at most about 2, at most about 5, at most about 10, more than about 0.1, more than about 0.5, more than about 1, more than about 2, more than about 5, more than about 10.
  • the vessel internal is coated with a polymeric or rubber material.
  • the vessel is equipped with an outlet collector tray. In one embodiment the vessel has multiple injection ports for the inlet or outlet flow. In one embodiment the flow is introduced from the bottom, top, middle of the vessel, or a combination of thereof. In one embodiment the vessel is outfitted with baffles or plates to break fluid jets. [0189] In some embodiments, the vessel or vessels are constructed to facilitate the formation of an eluent solution comprising a dissolved gas. In some embodiments, the vessel WSGR Docket No.50741-726.601 or vessels are constructed to facilitate the formation of an eluent solution comprising an acid. In some embodiments, said acid comprises a gas dissolved in water. In some embodiments, said acid comprises carbon dioxide dissolved in water.
  • the vessel is constructed to maintain an operating pressure that results in a high concentration of said gas in water, resulting in optimal acidity for elution of lithium.
  • the pressure of operation of said vessel is at least 5 psi, 10 psi, 50 psi, 100 psi, 500 psi, 1000 psi or 5000 psi.
  • Ion exchange beads contained within vessels with minimal flow distance [0190] In some embodiments, these vessels containing the ion exchange beads are designed to minimize the distance that the fluid flows as it contacts the ion exchange beads. In some embodiments, said design minimizes the energy required to contact a fluid with the ion exchange beads.
  • said fluid is a liquid resource, a washing solution, a solution containing a chemical additive, or an acidic eluent solution.
  • the ion exchange beads contained within such a vessel have an average particle diameter less than about 10 ⁇ m, less than about 20 ⁇ m, less than about 30 ⁇ m, less than about 40 ⁇ m, less than about 50 ⁇ m, less than about 60 ⁇ m, less than about 70 ⁇ m, less than about 80 ⁇ m, less than about 90 ⁇ m, less than about 100 ⁇ m, less than about 200 ⁇ m, less than about 300 ⁇ m, less than about 400 ⁇ m, less than about 500 ⁇ m, less than about 600 ⁇ m, less than about 700 ⁇ m, less than about 800 ⁇ m, less than about 900 ⁇ m, less than about 1000 ⁇ m, less than about 2000 ⁇ m.
  • the ion exchange beads contained within such a vessel have an average particle diameter at most about 10 ⁇ m, at most about 20 ⁇ m, at most about 30 ⁇ m, at most about 40 ⁇ m, at most about 50 ⁇ m, at most about 60 ⁇ m, at most about 70 ⁇ m, at most about 80 ⁇ m, at most about 90 ⁇ m, at most about 100 ⁇ m, at most about 200 ⁇ m, at most about 300 ⁇ m, at most about 400 ⁇ m, at most about 500 ⁇ m, at most about 600 ⁇ m, at most about 700 ⁇ m, at most about 800 ⁇ m, at most about 900 ⁇ m, at most about 1000 ⁇ m, at most about 2000 ⁇ m.
  • the ion exchange beads have an average particle diameter more than about 10 ⁇ m, more than about 20 ⁇ m, more than about 30 ⁇ m, more than about 40 ⁇ m, more than about 50 ⁇ m, more than about 60 ⁇ m, more than about 70 ⁇ m, more than about 80 ⁇ m, more than about 90 ⁇ m, more than about 100 ⁇ m, more than about 200 ⁇ m, more than about 300 ⁇ m, more than about 400 ⁇ m, more than about 500 ⁇ m, more than about 600 ⁇ m, more than about 700 ⁇ m, more than about 800 ⁇ m, more than about 900 ⁇ m, more than about 1000 ⁇ m, more than about 2000 ⁇ m.
  • the ion exchange beads have a typical particle size from about 10 ⁇ m to about 20 ⁇ m, from about 20 ⁇ m to about 40 ⁇ m, from about 40 ⁇ m to about 80 ⁇ m, from about 80 WSGR Docket No.50741-726.601 ⁇ m to about 200 ⁇ m, from about 100 ⁇ m to about 400 ⁇ m, from about 200 ⁇ m to about 800 ⁇ m, from about 400 ⁇ m to about 1000 ⁇ m, from about 600 ⁇ m to about 2000 ⁇ m, from about 1000 ⁇ m to about 2000 ⁇ m.
  • Embodiments comprising devices comprising one or more filter banks containing a lithium-selective sorbent [0192]
  • An aspect of the disclosure herein is a device for lithium extraction from a liquid resource.
  • said device comprises one or more filter banks containing a lithium-selective sorbent.
  • An example of a filter bank is shown in Figure 4, while the multiple filter banks within a lithium extraction device are shown in Figure 4C.
  • said sorbent is an ion-exchange material.
  • each filter bank comprises a compartment containing a lithium-selective sorbent, wherein said compartment is contained within porous partitions.
  • said compartment contains a bed or cake of said sorbent.
  • said filter bank contains pipes, shapes, and flow paths that connect said sorbent-containing compartment to a fluid distribution manifold that the delivers flow to and form said sorbent.
  • two porous partitions are located at opposing ends of the compartment containing a lithium-selective sorbent, such that fluid can flow from one partition, through the sorbent, and out of the second partition. In some embodiments, more than two such partitions are located within a filter bank.
  • said porous partition is a mesh, cloth, other woven material, a screen, or a combination thereof.
  • said porous partition is attached a mechanical device, plate, flow distributor, or scaffolding.
  • the porous partition is adjacent to a flow distribution compartment or surface, which distributes flow from inlet orifices to the entire surface of said porous partition.
  • the term “flow distribution surface” and “flow distribution compartment” refer to components of lithium extraction devices that ensure well-distributed and uniform flow to and from components in said device.
  • said flow distribution surface ensures that fluid entering the filter bank through said orifices is distributed to the entire flow distribution surface, such that it can travel through said porous partition and evenly flow into and across the sorbent.
  • the flow distribution surface comprises surface textured features, such that a void is created between a non-porous surface and the porous partition.
  • a void is created between a non-porous surface and the porous partition.
  • An example of such a void is shown in Figure 4 and insert Figure 4C, where the surface is denoted 4013 and the porous partition 4014.
  • this WSGR Docket No.50741-726.601 void creates a resistance-free space for fluid to flow from the orifices that deliver flow to the filter bank to the porous partition.
  • the shape of said flow distribution surface conforms to the shape of the filter bank. In some embodiments, the shape of said flow distribution surface conforms to the shape of the porous partition.
  • the shape of said flow distribution surface conforms to the shape of the sorbent cake or bed.
  • the compartment containing the lithium selective sorbent or ion-exchange beads is treated with a fluid.
  • the compartment containing the lithium selective sorbent or ion-exchange beads is treated with water or other solutions for the purposes of adjusting the concentration, composition, pH, or contaminant level of the fluid flowing through the vessel.
  • the compartment containing the lithium selective sorbent or ion-exchange beads is treated with a lithium-containing liquid resource to absorb lithium.
  • the compartment containing the lithium selective sorbent or ion-exchange beads is treated with an acidic solution to release absorbed lithium.
  • the compartment containing the lithium selective sorbent or ion-exchange beads is treated with multiple fluids.
  • fluid in order to contact the lithium- selective sorbent with said fluid, fluid is directed from the inlet of the lithium extraction device to the one or more filter banks in said device.
  • said direction of flow is achieved by means of optional inlet-and outlet- flows to and from said compartment within a filter bank.
  • inlet- and outlet flows are located at the top, bottom, center, off-center, or side of said compartments.
  • such inlet- and outlet flows are located at the top, bottom, center, off-center, or side of said filter bank.
  • the inlet- and outlet flows to and from said compartment are injected and removed from the internal space of said compartments by means of piping, tubing, orifices, or other internal components that protrude into said compartment.
  • one or more pipes are in fluid contact with each filter bank, with each of said pipes delivering or removing fluid flows to and from said filter bank.
  • one such pipe is present in the filter bank.
  • two such pipes are present in the filter bank.
  • three such pipes are present in the filter bank.
  • four such pipes are present in the filter bank.
  • five such pipes are present in the filter bank.
  • pipes, orifices, and flow distribution surfaces are configured to direct a flow of a liquid resource through the one or more filter banks and out of said one or more filter banks, wherein the sorbent material contained in said filter bank selectively absorbs lithium.
  • pipes, orifices, and flow distribution surfaces are configured to uniformly distribute the flow of liquid through the sorbent material contained in the filter bank.
  • said flow uniformity implies that each volume of sorbent material within the filter bank is contacted with the same volume of liquid resource within a given time period.
  • uniform distribution of flow through the sorbent material results in a higher lithium absorption capacity of the sorbent, a higher selectivity for lithium absorption by the sorbent over other ions present in the liquid resource, a minimized distance required to flow the liquid through the one or more filter banks, a reduced change in pressure when flowing liquid across the one or more filter banks, a longer life time of the sorbent, a longer life time of the ion-exchange material, or a combination thereof.
  • the devices, vessels, system, and methods described herein utilize a flow distribution compartment to optimize the flow of various solutions or gases through the devices, vessels, pipes, filter banks, and lithium-selective sorbents materials.
  • the inlet- and outlet flows to and from the flow distribution compartments are injected and remove from the internal space of said compartments by means of piping, tubing, or other internal components that protrude into said compartment.
  • the inlet- and outlet flows to and from the flow distribution compartments are injected and remove from the internal space of said compartments by means of piping, tubing, or other internal components that protrude into said compartment
  • the flow distribution compartment are optionally treated with a lithium containing resource, hydrogen ion-containing acid, water, or other solutions for the purposes of adjusting the concentration, composition, pH, or contaminant level of the fluid flowing through the vessel. This is achieved by means of an optional inlet-and outlet- flows to and from the flow distribution compartment.
  • said partition comprises a filter, a solid-liquid separation device, or other solid-retaining material.
  • a partition is in contact with the lithium selective sorbent.
  • said partition is a permeable partition.
  • said permeable partition is a porous partition.
  • said permeable partition is a slitted partition that provides support for the ion-exchange bead bed, chemical protection, aids WSGR Docket No.50741-726.601 filtration, or a combination thereof.
  • said permeable partition is a porous partition that provides structural support for the bed of lithium-selective sorbent, chemical protection, aids filtration, or a combination thereof.
  • the partition between the flow distribution compartment and the compartment containing the ion-exchange beads consists of a porous partition that provides structural support for the ion-exchange bead bed, chemical protection, aids filtration, or a combination thereof.
  • the porous partition is a porous polymer partition.
  • the porous partition is a mesh or polymer membrane.
  • the porous partition comprises one or more meshes of similar or different composition, of similar or different aperture sizes, of similar or different percent open area.
  • the porous partition comprises one or more meshes to provide structural support and/or filtration capabilities.
  • the porous partition comprises a v-wire screen, a sintered metal screen, a sintered polymer screen, a flat screen, a cylindrical screen, a screen comprised of wire with cylindrical cross section, a screen comprised of wire with square cross section, a screen comprised of wire with rectangular cross section, a screen comprised of wire with rhomboidal cross section, a screen comprised of wire with triangular cross section, a screen comprised of wire with irregular cross section, a slotted wire screen, a mesh, or a combination thereof, wherein said porous partition is coarse, fine, or a combination thereof.
  • the porous partition, fluid conduits, fluid orifices, and flow distribution surfaces are assembled to form a filter bank.
  • a filter bank An example of such a filter bank is shown in Figure 4.
  • said filter banks comprise a one or more filter plates.
  • said filer banks are assembled from two opposing filter plates.
  • Figure 4C shows how two filter plates 40204 come together to form a filter bank 415, said filter bank containing a lithium selective sorbent within compartment 405 in said filter bank.
  • the bed of ion exchange material is contained within said filter bank.
  • the bed of lithium selective sorbent is contained within said filter bank.
  • said bed of ion exchange material has a characteristic “thickness”, wherein “thickness” is defined as the average dimension of the said solid mass, measured in a direction that is parallel to the direction of fluid flow through the filter bank.
  • the typical thickness of the bed of lithium selective sorbent is less than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 WSGR Docket No.50741-726.601 m.
  • the typical thickness of the bed of lithium selective sorbent is more than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the typical thickness of the bed of lithium selective sorbent is at most about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the bed of lithium selective sorbent is more than about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the bed of lithium selective sorbent is from about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 8 cm, from about 8 cm to about 20 cm, from about 20 cm to about 40 cm, from about 40 cm to about 80 cm, from about 80 cm to about 120 cm, from about 120 cm to about 2 m, from about 2 m to about 4 m.
  • the typical thickness of the bed of lithium selective sorbent is selected from 18 mm, 25 mm, 32 mm, 40 mm, 50 mm, or 60 mm.
  • the bed of ion exchange material is contained within said filter bank. In some embodiments, the bed of lithium selective sorbent is contained within said filter bank.
  • said bed of ion exchange material has a characteristic “cross sectional length” of said bed, defined as the average dimension of the said solid mass, measured in a direction that is perpendicular to the direction of fluid flow through the filter bank.
  • the cross-sectional length of said bed is less than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the cross-sectional length of said bed is more than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the cross- sectional length of said bed is at most about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at WSGR Docket No.50741-726.601 most about 4 m.
  • the cross-sectional length of said bed is more than about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the cross-sectional length of said bed is from about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 8 cm, from about 8 cm to about 20 cm, from about 20 cm to about 40 cm, from about 40 cm to about 80 cm, from about 80 cm to about 120 cm, from about 120 cm to about 2 m, from about 2 m to about 4 m, from about 4 m to about 8 m.
  • the cross-sectional length is selected from: about 250 mm, 320 mm, 470 mm, 630 mm, 800 mm, 1000 mm, 1200 mm, 1500 mm, 2000 mm, 4000 mm.
  • the bed of sorbent material is not square, and comprises a cross-sectional length that is selected from two of the following dimensions: about 250 mm, 320 mm, 470 mm, 630 mm, 800 mm, 1000 mm, 1200 mm, 1500 mm, 2000 mm, 4000 mm.
  • the cross-sectional length of the bed of lithium-selective sorbent is 2000 mm x 4000 mm, 1500 mm x 2000 mm, 2500 mm by 5000 mm, or a combination thereof.
  • the device containing ion-exchange beads is comprised of multiple and separate ion-exchange compartments arranged within a single vessel.
  • the lithium extraction devices comprises multiple individual filter banks – each containing an individual lithium-selective sorbent compartment – where lithium is absorbed by said lithium selective sorbent.
  • said compartments comprise individual filter banks.
  • a single lithium extraction device comprises about two, about three, about five, about ten, about twenty, about thirty, about fifty, WSGR Docket No.50741-726.601 about one-hundred, about one hundred and fifty, or about two-hundred individual lithium extraction compartments.
  • the multiple filter banks are held together by a device that applies a mechanical force that presses the individual filter banks together.
  • said device comprises a hydraulic system, comprising one more pistons and one or more devices to apply a hydraulic force on said piston.
  • the mechanical force is applied to one structurally reinforced component that is in contact with the first plate in the stack of filter banks, and the compressive force is distributed across all filter plates in the device.
  • said force is applied by means of a pressurized hydraulic fluid system, pressurized air system, mechanical tensions system, or combinations thereof.
  • the pressure applied to compress all filter bank together is less than 50 psi, less than 150 psi, less than 500 psi, less than 1000 psi, less than 2500 psi, or less than 5000 psi.
  • the pressure applied to compress all filter bank together is at most 50 psi, at most 150 psi, at most 500 psi, at most 1000 psi, at most 2500 psi, or at most 5000 psi.
  • the pressure applied is more than 50 psi, more than 150 psi, more than 500 psi, more than 1000 psi, more than 2500 psi, or more than 5000 psi. In some embodiments, the pressure applied is from 50 psi to 150 psi, from 150 psi to 500 psi, from 500 psi to 1000 psi, from 1000 psi to 2500 psi, from 2500 psi to 5000 psi.
  • An aspect of the disclosure herein is a device for lithium extraction from a liquid resource, wherein said device comprises one or more filter banks containing a lithium-selective sorbent. In some embodiments, said lithium extraction comprises a filter press.
  • a filter press is a filtration device known in the field of filtration and solids-liquid separation.
  • An aspect of the disclosure herein is the use of a filter press to extract lithium, wherein said filter press is filled with a lithium-selective sorbent, and said sorbent is contacted with a liquid resource comprising lithium in said filter press.
  • said sorbent is an ion-exchange material.
  • a filter press comprises multiple filter plates, wherein said filter two filter plates come together to form a filter chamber or filter bank.
  • each filter bank comprises a compartment containing a lithium-selective sorbent, wherein said compartment is contained within porous partitions.
  • said compartment contains a bed or cake of said sorbent.
  • said filter bank contains pipes, shapes, and flow paths that connect said sorbent-containing compartment to a fluid distribution manifold that the delivers flow to and form said sorbent.
  • two porous partitions are located at opposing ends of the compartment containing a lithium-selective sorbent, such that fluid can flow from one partition, through the sorbent, and out of the second partition. In some embodiments, more than two such partitions are located within a filter bank.
  • said porous partition is a mesh, cloth, other woven material, a screen, or a combination thereof.
  • said porous partition is attached a mechanical device, plate, flow distributor, or scaffolding.
  • the porous partition is a filter cloth.
  • said partition comprises a filter, a solid-liquid separation device, or other solid-retaining material.
  • a partition is in contact with the lithium selective sorbent.
  • said partition is a permeable partition.
  • said permeable partition is a porous partition.
  • said permeable partition is a slitted partition that provides support for the ion-exchange bead bed, chemical protection, aids filtration, or a combination thereof.
  • said permeable partition is a porous partition that provides structural support for the bed of lithium-selective sorbent, chemical protection, aids filtration, or a combination thereof.
  • the partition between the flow distribution compartment and the compartment containing the ion-exchange beads consists of a porous partition that provides structural support for the ion-exchange bead bed, chemical protection, aids filtration, or a combination thereof.
  • the porous partition is a porous polymer partition.
  • the porous partition is a mesh or polymer membrane.
  • the porous partition comprises one or more meshes of similar or different composition, of similar or different aperture sizes, of similar or different percent open area.
  • the porous partition comprises one or more meshes to provide structural support and/or filtration capabilities.
  • the porous partition comprises a v-wire screen, a sintered metal screen, a sintered polymer screen, a flat screen, a cylindrical screen, a screen comprised of wire with cylindrical cross section, a screen comprised of wire with square cross section, a screen comprised of wire with rectangular cross section, a screen comprised of wire with rhomboidal WSGR Docket No.50741-726.601 cross section, a screen comprised of wire with triangular cross section, a screen comprised of wire with irregular cross section, a slotted wire screen, a mesh, or a combination thereof, wherein said porous partition is coarse, fine, or a combination thereof.
  • the porous partition comprises polyether ether ketone, polypropylene, polyethylene, polysulfone mesh, polyester mesh, polyamide, polytetrafluoroethylene, ethylene tetrafluoroethylene polymer, stainless steel, stainless steel mesh coated in polymer, stainless steel mesh coated in ceramic, titanium, or a combination thereof.
  • the porous partition comprises ion exchange particles.
  • the porous partition comprises porous ion exchange particles.
  • the porous partition comprises a mixture of ion exchange particles with other polymers described above.
  • the porous partition comprises multiple layers. [0210] In some embodiments, the porous partition is a single layer filtration fabric.
  • the porous partition is a double layer filtration fabric. In some embodiments, the porous partition is a multi-layer filtration fabric. In some embodiments, the porous partition is a spun fabric. In some embodiments, the porous partition is a is a mixture of fabrics. In some embodiments, the porous partition is a woven fabric. In some embodiments, said fabric is manufactured with one or more weave patterns, including but not limited to a plain, twill, satin, oxford, leno or basket-weave.
  • the porous partition consists of openings in that are of a typical characteristic size of less than about 1 ⁇ m, less than about 2 ⁇ m, less than about 5 ⁇ m, less than about 10 ⁇ m, less than about 20 ⁇ m, less than about 30 ⁇ m, less than about 40 ⁇ m, less than about 50 ⁇ m, less than about 60 ⁇ m, less than about 70 ⁇ m, less than about 80 ⁇ m, less than about 90 ⁇ m, less than about 100 ⁇ m, less than about 200 ⁇ m, less than about 300 ⁇ m, less than about 400 ⁇ m, less than about 500 ⁇ m, less than about 600 ⁇ m, less than about 700 ⁇ m, less than about 800 ⁇ m, less than about 900 ⁇ m, less than about 1000 ⁇ m, less than about 2000 ⁇ m.
  • the porous partition consists of openings in that are of a typical characteristic size of at most about 1 ⁇ m, at most about 2 ⁇ m, at most about 5 ⁇ m, at most about 10 ⁇ m, at most about 20 ⁇ m, at most about 30 ⁇ m, at most about 40 ⁇ m, at most about 50 ⁇ m, at most about 60 ⁇ m, at most about 70 ⁇ m, at most about 80 ⁇ m, at most about 90 ⁇ m, at most about 100 ⁇ m, at most about 200 ⁇ m, at most about 300 ⁇ m, at most about 400 ⁇ m, at most about 500 ⁇ m, at most about 600 ⁇ m, at most about 700 ⁇ m, at most about 800 ⁇ m, at most about 900 ⁇ m, at most about 1000 ⁇ m, at most about 2000 ⁇ m.
  • the porous partition consists of openings in that are of a typical characteristic size of more than about 1 ⁇ m, more than about 2 ⁇ m, more than about 5 ⁇ m, more than about WSGR Docket No.50741-726.601 10 ⁇ m, more than about 20 ⁇ m, more than about 30 ⁇ m, more than about 40 ⁇ m, more than about 50 ⁇ m, more than about 60 ⁇ m, more than about 70 ⁇ m, more than about 80 ⁇ m, more than about 90 ⁇ m, more than about 100 ⁇ m, more than about 200 ⁇ m, more than about 300 ⁇ m, more than about 400 ⁇ m, more than about 500 ⁇ m, more than about 600 ⁇ m, more than about 700 ⁇ m, more than about 800 ⁇ m, more than about 900 ⁇ m, more than about 1000 ⁇ m, more than about 2000 ⁇ m.
  • the porous partition consists of openings in that are of a typical characteristic size from about 20 ⁇ m to about 40 ⁇ m, from about 40 ⁇ m to about 80 ⁇ m, from about 80 ⁇ m to about 200 ⁇ m, from about 100 ⁇ m to about 400 ⁇ m, from about 200 ⁇ m to about 800 ⁇ m, from about 400 ⁇ m to about 1000 ⁇ m, from about 600 ⁇ m to about 2000 ⁇ m, from about 1000 ⁇ m to about 2000 ⁇ m.
  • the porous partition consists of openings in that are of a typical characteristic size of from about 1 ⁇ m to about 2 ⁇ m, from about 2 ⁇ m to about 4 ⁇ m, from about 4 ⁇ m to about 10 ⁇ m, from about 10 ⁇ m to about 20 ⁇ m, from about 20 ⁇ m to about 40 ⁇ m, from about 40 ⁇ m to about 100 ⁇ m, from about 100 ⁇ m to about 200 ⁇ m, from about 200 ⁇ m to about 400 ⁇ m, from about 400 ⁇ m to about 1000 ⁇ m, from about 1000 ⁇ m to about 2000 ⁇ m.
  • the porous partition consists of openings in that are of a typical characteristic size of from about 1 ⁇ m to about 10 ⁇ m, from about 10 ⁇ m to about 100 ⁇ m, from about 100 ⁇ m to about 1000 ⁇ m, from about 1000 ⁇ m to about 10000 ⁇ m.
  • the air permeability of said permeable partition measured at 200 Pa, in units of liters per meter square per second, is less than about 1, less than about 5, less than about 10, less than about 50, less than about 100, less than about 500, less than about 1000, less than about 5000, less than about 10,000.
  • the air permeability of said permeable partition measured at 200 Pa, in units of liters per meter square per second, is at most about 1, at most about 5, at most about 10, at most about 50, at most about 100, at most about 500, at most about 1000, at most about 5000, at most about 10,000. In some embodiments, the air permeability of said permeable partition, measured at 200 Pa, in units of liters per meter square per second, is more than about 1, more than about 5, more than about 10, more than about 50, more than about 100, more than about 500, more than about 1000, more than about 5000, more than about 10,000.
  • the air permeability of said permeable partition is from about 0.1 to about 1, from about 1 to about 5, from about 5 to about 10, from about 10 to about 50, from about 50 to about 100, from about 100 to about 500, from about 500 to about 1000, from about 1000 to about 5000, from about 5,000 about 10,000.
  • the porous partition comprises an ion exchange material and a porous polymer.
  • the porous partition comprises an ion exchange material and a porous fiber.
  • the porous partition comprises an ion exchange material and cellulose.
  • the porous partition comprises an ion exchange material and a mesh or polymer membrane.
  • said partition comprises one or more meshes of similar or different composition, of similar or different aperture sizes, of similar or different percent open area.
  • side porous partition comprises one or more meshes to provide structural support and/or filtration capabilities.
  • side porous partition comprises one or partitions, one or more of which comprise an ion exchange material.
  • the porous partition comprises a v-wire screen, a sintered metal screen, a sintered polymer screen, a flat screen, a cylindrical screen, a screen comprised of wire with cylindrical cross section, a screen comprised of wire with square cross section, a screen comprised of wire with rectangular cross section, a screen comprised of wire with rhomboidal cross section, a screen comprised of wire with triangular cross section, a screen comprised of wire with irregular cross section, a slotted wire screen, a mesh, or a combination thereof, wherein said porous partition is coarse, fine, or a combination thereof.
  • said porous partition comprises polyether ether ketone, polypropylene, polyethylene, polysulfone mesh, polyester mesh, polyamide, polytetrafluoroethylene, ethylene tetrafluoroethylene polymer, stainless steel, stainless steel mesh coated in polymer, stainless steel mesh coated in ceramic, titanium, or a combination thereof.
  • the porous partition comprises ion exchange particles.
  • the porous partition comprises porous ion exchange particles.
  • the porous partition comprises a mixture of ion exchange particles with other polymers described above.
  • the porous partition comprises multiple layers.
  • the porous partition comprising an ion exchange material extracts lithium in the lithium extraction device.
  • the porous partition comprising an ion exchange material is the only component that extracts lithium in the lithium extraction device.
  • the porous partition comprises an ion exchange material, while the filter bank is filled with a packed bed of the same ion exchange material.
  • the porous partition comprises an ion exchange material, while the filter bank is filled with a packed bed a different ion exchange material.
  • the porous partition comprises an ion exchange material, while the filter bank is filled with a packed bed a different lithium selective sorbent.
  • said porous partition optionally contains structures to enable said partition to be incorporated into the assembly of the filter bank.
  • these structures comprise, but are not limited to, holes, slits, cutouts, perforations, protrusions, gaskets, or rings.
  • said structures comprise a flexible cylinder that forms an octagonal shape spanning the entire porous partition, providing a structural reinforcement.
  • the porous surface is contained within said octagon.
  • said reinforcement is surrounded by the material that the porous partition is made of.
  • said structural reinforcement is caulked into an octagonally- shaped groove on the filter bank using a mallet, resulting in the porous partition being immobilized directly onto the filter bank.
  • the filter cloths are gasketed.
  • the filter cloths are non-gasketed. In some embodiments, the filter cloths span more than one filter bank.
  • the compartment containing the lithium selective sorbent or ion-exchange beads is treated with a fluid. In some embodiments, the compartment containing the lithium selective sorbent or ion-exchange beads is treated with water or other solutions for the purposes of adjusting the concentration, composition, pH, or contaminant level of the fluid flowing through the vessel. In some embodiments, the compartment containing the lithium selective sorbent or ion-exchange beads is treated with a lithium-containing liquid resource to absorb lithium.
  • the compartment containing the lithium selective sorbent or ion-exchange beads is treated with an acidic solution to release absorbed lithium. In some embodiments, the compartment containing the lithium selective sorbent or ion-exchange beads is treated with multiple fluids. In some embodiments, in order to contact the lithium- selective sorbent with said fluid, fluid is directed from the inlet of the lithium extraction device to the one or more filter plates in said device. In some embodiments, said direction of flow is achieved by means of optional inlet-and outlet- flows to and from said compartment within a filter plate. In some embodiments, such inlet- and outlet flows are located at the top, bottom, center, off-center, or side of said compartments.
  • such inlet- and outlet flows are located at the top, bottom, center, off-center, or side of said filter plate.
  • the inlet- and outlet flows to and from said compartment are injected and removed from the internal space of said compartments by means of piping, tubing, orifices, or other internal components that protrude into said compartment.
  • one or more pipes are in fluid contact with each filter plate, with each of said pipes delivering or removing fluid flows to and from said filter plate.
  • one such pipe is present in the filter plate.
  • two such pipes are present in the filter plate.
  • three such pipes are present in the filter plate.
  • four such pipes are present in the filter plate. In some embodiments, five such pipes are present in the filter plate. In a preferred embodiment, four such fluid deliver pipes are located at the four corners of a filter plate. In some embodiments, more than five such pipes are present in the filter plate.
  • said pipes have a diameter of less than about 1 mm, less than about 2 mm, less than about 5 mm, less than about 10 mm, less than about 20 mm, less than about 30 mm, less than about 40 mm, less than about 50 mm, less than about 60 mm, less than about 70 mm, less than about 80 mm, less than about 90 mm, less than about 100 mm, less than about 200 mm, less than about 500 mm, less than about 1000 mm, less than about 1500 mm, less than about 2000 mm.
  • said pipes have a diameter of at most about 1 mm, at most about 2 mm, at most about 5 mm, at most about 10 mm, at most about 20 mm, at most about 30 mm, at most about 40 mm, at most about 50 mm, at most about 60 mm, at most about 70 mm, at most about 80 mm, at most about 90 mm, at most about 100 mm, at most about 200 mm, at most about 500 mm, at most about 1000 mm, at most about 1500 mm, at most about 2000 mm.
  • said pipes or have a diameter of more than about 1 mm, more than about 2 mm, more than about 5 mm, more than about 10 mm, more than about 20 mm, more than about 30 mm, more than about 40 mm, more than about 50 mm, more than about 60 mm, more than about 70 mm, more than about 80 mm, more than about 90 mm, more than about 100 mm, more than about 200 mm, more than about 500 mm, more than about 1000 mm, more than about 1500 mm, more than about 2000 mm.
  • said pipes or have a diameter of about 1 mm to about 2 mm, from about 2 mm to about 4 mm, from about 4 mm to about 10 mm, from about 10 mm to about 20 mm from about 20 mm to about 40 mm, from about 40 mm to about 100 mm, from about 100 mm to about 500 mm, from about 500 mm to about 1500 mm, from about 1500 mm to about 2000 mm.
  • said pipes or have a length of less than about 1 cm, less than about 2 cm, less than about 5 cm, less than about 10 cm, less than about 20 cm, less than about 30 cm, less than about 40 cm, less than about 50 cm, less than about 60 cm, less than about 70 cm, less than about 80 cm, less than about 90 cm, less than about 100 cm, less than about 200 cm, less than about 500 cm, less than about 10 m.
  • said pipes or have a length of at most about 1 cm, at most about 2 cm, at most about 5 cm, at most about 10 cm, at most about 20 cm, at most about 30 cm, at most about 40 cm, at most about 50 cm, at most about 60 cm, at most about 70 cm, at most about 80 cm, at most about 90 cm, at most about 100 cm, at most WSGR Docket No.50741-726.601 about 200 cm, at most about 500 cm, at most about 10 m.
  • said pipes or have a length of more than about 1 cm, more than about 2 cm, more than about 5 cm, more than about 10 cm, more than about 20 cm, more than about 30 cm, more than about 40 cm, more than about 50 cm, more than about 60 cm, more than about 70 cm, more than about 80 cm, more than about 90 cm, more than about 100 cm, more than about 200 cm, more than about 500 cm, more than about 10 m.
  • said or pipes have a length of about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 10 cm, from about 10 cm to about 20 cm, from about 20 cm to about 50 cm, from about 50 cm to about 100 cm, from about 100 cm to about 200 cm, from about 200 cm to about 10 m.
  • said pipes have a diameter of less than about 1 mm, less than about 2 mm, less than about 5 mm, less than about 10 mm, less than about 20 mm, less than about 30 mm, less than about 40 mm, less than about 50 mm, less than about 60 mm, less than about 70 mm, less than about 80 mm, less than about 90 mm, less than about 100 mm, less than about 200 mm, less than about 500 mm, less than about 1000 mm, less than about 1500 mm, less than about 2000 mm.
  • said pipes have a diameter of at most about 1 mm, at most about 2 mm, at most about 5 mm, at most about 10 mm, at most about 20 mm, at most about 30 mm, at most about 40 mm, at most about 50 mm, at most about 60 mm, at most about 70 mm, at most about 80 mm, at most about 90 mm, at most about 100 mm, at most about 200 mm, at most about 500 mm, at most about 1000 mm, at most about 1500 mm, at most about 2000 mm.
  • said pipes or have a diameter of more than about 1 mm, more than about 2 mm, more than about 5 mm, more than about 10 mm, more than about 20 mm, more than about 30 mm, more than about 40 mm, more than about 50 mm, more than about 60 mm, more than about 70 mm, more than about 80 mm, more than about 90 mm, more than about 100 mm, more than about 200 mm, more than about 500 mm, more than about 1000 mm, more than about 1500 mm, more than about 2000 mm.
  • said pipes or have a diameter of about 1 mm to about 2 mm, from about 2 mm to about 4 mm, from about 4 mm to about 10 mm, from about 10 mm to about 20 mm from about 20 mm to about 40 mm, from about 40 mm to about 100 mm, from about 100 mm to about 500 mm, from about 500 mm to about 1500 mm, from about 1500 mm to about 2000 mm.
  • said pipes or have a length of less than about 1 cm, less than about 2 cm, less than about 5 cm, less than about 10 cm, less than about 20 cm, less than about 30 cm, less than about 40 cm, less than about 50 cm, less than about 60 cm, less than about 70 cm, less than about 80 cm, less than about 90 cm, less than about 100 cm, less than about 200 cm, less than about 500 cm, less than about 10 m.
  • said pipes or have a length of more than about 1 cm, more than about 2 cm, more than about 5 cm, more than about 10 cm, more than about 20 cm, more than about 30 cm, more than about 40 cm, more than about 50 cm, more than about 60 cm, more than about 70 cm, more than about 80 cm, more than about 90 cm, more than about 100 cm, more than about 200 cm, more than about 500 cm, more than about 10 m.
  • said or pipes have a length of about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 10 cm, from about 10 cm to about 20 cm, from about 20 cm to about 50 cm, from about 50 cm to about 100 cm, from about 100 cm to about 200 cm, from about 200 cm to about 10 m.
  • the ratio of the diameter of said pipe to the dimension of the filter plate is less than about 0.01, less than about 0.1, less than about 1, less than about 10, less than about 100. In some embodiments, the ratio of the diameter of said pipe to the dimension of the filter plate is at most about 0.01, at most about 0.1, at most about 1, at most about 10, at most about 100.
  • the ratio of the diameter of said pipe to the dimension of the filter plate is more than about 0.01, more than about 0.1, more than about 1, more than about 10, more than about 100. In some embodiments, the ratio of the diameter of said pipe to the dimension of the filter plate is from about 0.01 to about 0.1, from about 0.1 to about 1, from about 1 to about 10, from about 10 to about 100. In some embodiments, one or more pipes of equivalent or different dimensions are found within a filter plate. In some embodiments, one or more of these pipes are connected. In some embodiments, one or more of said pipes are oriented with respect to each other in parallel, perpendicular, at an angle, in varying geometries, or in a combination thereof.
  • the ratio of the diameters of pipes within the same filter plate is less than about 0.01, less than about 0.1, less than about 1, less than about 10, less than about 100. In some embodiments, the ratio of the diameters of pipes within the same filter plate is at most about 0.01, at most about 0.1, at most about 1, at most about 10, at most about 100. In some embodiments, the ratio of the diameters of pipes within the same filter plate is more than about 0.01, more than about 0.1, more than about 1, more than about 10, more than about 100. In some embodiments, the ratio of the diameters of pipes within the same filter plate is from about 0.01 to about 0.1, from about 0.1 to about 1, from about 1 to about 10, from about 10 to about 100.
  • said additional pipes are connected to one or more orifices which deliver fluid to and from the flow distribution surface.
  • orifices provide a fluid connection from the piping that delivers flow to the filter plate to the flow distribution surfaces.
  • one such orifice delivers flow.
  • more than one orifice delivers flow.
  • 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20 orifices deliver flow.
  • more than 20 orifices deliver flow.
  • said orifices have a diameter of less than about 1 mm, less than about 2 mm, less than about 5 mm, less than about 10 mm, less than about 20 mm, less than about 30 mm, less than about 40 mm, less than about 50 mm, less than about 60 mm, less than about 70 mm, less than about 80 mm, less than about 90 mm, less than about 100 mm.
  • said orifices have a diameter of at most about 1 mm, at most about 2 mm, at most about 5 mm, at most about 10 mm, at most about 20 mm, at most about 30 mm, at most about 40 mm, at most about 50 mm, at most about 60 mm, at most about 70 mm, at most about 80 mm, at most about 90 mm, at most about 100 mm.
  • said orifices have a diameter of more than about 1 mm, more than about 2 mm, more than about 5 mm, more than about 10 mm, more than about 20 mm, more than about 30 mm, more than about 40 mm, more than about 50 mm, more than about 60 mm, more than about 70 mm, more than about 80 mm, more than about 90 mm, more than about 100 mm. In some embodiments, said orifices have a diameter of about 1 mm to about 2 mm, from about 2 mm to about 4 mm, from about 4 mm to about 10 mm, from about 10 mm to about 20 mm.
  • said orifices have a length of less than about 1 cm, less than about 2 cm, less than about 5 cm, less than about 10 cm, less than about 20 cm, less than about 30 cm, less than about 40 cm, less than about 50 cm, less than about 60 cm, less than about 70 cm, less than about 80 cm, less than about 90 cm, less than about 100 cm, less than about 200 cm, less than about 500 cm, less than about 10 m.
  • said orifices have a length of at most about 1 cm, at most about 2 cm, at most about 5 cm, at most about 10 cm, at most about 20 cm, at most about 30 cm, at most about 40 cm, at most about 50 cm, at most about 60 cm, at most about 70 cm, at most about 80 cm, at most about 90 cm, at most about 100 cm, at most about 200 cm, at most about 500 cm, at most about 10 m.
  • said orifices have a length of more than about 1 cm, more than about 2 cm, more than about 5 cm, more than about 10 cm, more than about 20 cm, more than about 30 cm, more than about 40 cm, more than about 50 cm, more than about 60 cm, more than about 70 cm, more than about 80 cm, more than about 90 cm, more than about 100 cm, more than about 200 cm, more than about 500 cm, more than about 10 m.
  • said orifices have a length of WSGR Docket No.50741-726.601 about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 10 cm, from about 10 cm to about 20 cm, from about 20 cm to about 50 cm, from about 50 cm to about 100 cm, from about 100 cm to about 200 cm, from about 200 cm to about 10 m.
  • pipes, orifices, and flow distribution surfaces are configured to direct a flow of a liquid resource through the one or more filter plates and out of said one or more filter plates, wherein the sorbent material contained in said filter plate selectively absorbs lithium.
  • pipes, orifices, and flow distribution surfaces are configured to uniformly distribute the flow of liquid through the sorbent material contained in the filter plate.
  • said flow uniformity implies that each volume of sorbent material within the filter plate is contacted with the same volume of liquid resource within a given time period.
  • uniform distribution of flow through the sorbent material results in a higher lithium absorption capacity of the sorbent, a higher selectivity for lithium absorption by the sorbent over other ions present in the liquid resource, a minimized distance required to flow the liquid through the one or more filter plates, a reduced change in pressure when flowing liquid across the one or more filter plates, a longer life time of the sorbent, a longer life time of the ion-exchange material, or a combination thereof.
  • the devices, vessels, system, and methods described herein utilize a flow distribution compartment to optimize the flow of various solutions or gases through the devices, vessels, pipes, filter plates, and lithium-selective sorbents materials.
  • the inlet- and outlet flows to and from the flow distribution compartments are injected and remove from the internal space of said compartments by means of piping, tubing, or other internal components that protrude into said compartment.
  • the inlet- and outlet flows to and from the flow distribution compartments are injected and remove from the internal space of said compartments by means of piping, tubing, or other internal components that protrude into said compartment.
  • the flow distribution compartment are optionally treated with a lithium containing resource, hydrogen ion-containing acid, water, or other solutions for the purposes of adjusting the concentration, composition, pH, or contaminant level of the fluid flowing through the vessel. This is achieved by means of an optional inlet-and outlet- flows to and from the flow distribution compartment.
  • the porous partition, fluid conduits, fluid orifices, and flow distribution surfaces are assembled to form a filter plate.
  • a filter plate An example of such a filter plates is shown in Figure 4B.
  • said filter plates contain structural supports that allow said plates to be mounted within a larger lithium extraction device.
  • solid filter plates comprise a compartment containing a lithium-selective sorbent or ion-exchange material.
  • multiple filter plates are found within a single lithium extraction device, such that they form a stack of filter plates.
  • said stack of filter plates is formed into a filter press
  • said filter press is oriented vertically, horizontally, or slanted with respect to the ground.
  • the bed of ion exchange material is contained within said filter bank.
  • the bed of lithium selective sorbent is contained within said filter bank.
  • said bed of ion exchange material has a characteristic “thickness”, wherein “thickness” is defined as the average dimension of the said solid mass, measured in a direction that is parallel to the direction of fluid flow through the filter bank.
  • the typical thickness of the chamber containing solids between filter plates is less than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the typical thickness of the chamber containing solids between filter plates is more than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the typical thickness of the chamber containing solids between filter plates is at most about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the chamber containing solids between filter plates is more than about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the chamber containing solids between filter plates is from about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 8 cm, from about 8 cm to about 20 cm, from about 20 cm to about 40 cm, from about 40 cm to about 80 cm, from about 80 cm to about 120 cm, from about 120 cm to about 2 m, from about 2 m to about 4 m.
  • the WSGR Docket No.50741-726.601 typical thickness of the chamber containing solids between filter plates is selected from 18 mm, 25 mm, 32 mm, 40 mm, 50 mm, or 60 mm.
  • the chamber holds a maximum volume of solids, this is the maximum volume of lithium selective sorbent that can be contained within each filter bank.
  • said volume is less than about 1 mL, less than about 10 mL, less than about 100 mL, less than about 1 L, less than about 10 L, less than about 100 L, less than about 1 cubic meter, less than about 10 cubic meters.
  • said volume is at most about 1 mL, at most about 10 mL, at most about 100 mL, at most about 1 L, at most about 10 L, at most about 100 L, at most about 1 cubic meter, at most about 10 cubic meters.
  • said volume is more than about 1 mL, more than about 10 mL, more than about 100 mL, more than about 1 L, more than about 10 L, more than about 100 L, more than about 1 cubic meter, more than about 10 cubic meters. In some embodiments, said volume is from about 0.1 mL to about 1 mL, from about 1 mL to about 10 mL, from about 10 mL to about 100 mL, from about 100 mL to about 1 L, from about 1 L to about 10 L, from about 10 L to about 100 L, from about 100 L to about 1 cubic meter, from about 1 cubic meter to about 10 cubic meters, from about 10 cubic meters.
  • the porous partition in the chamber comprises a fixed surface area per chamber.
  • said area is less than about 1 cm 2 , less than about 10 cm 2 , less than about 100 cm 2 , less than about 1,000 cm 2 , less than about 1 m 2 , less than about 10 m 2 , less than about 100 m 2 , less than about 1000 m 2 .
  • said area is at most about 1 cm 2 , at most about 10 cm 2 , at most about 100 cm 2 , at most about 1,000 cm 2 , at most about 1 m 2 , at most about 10 m 2 , at most about 100 m 2 , at most about 1000 m 2 .
  • said volume is more than about 1 cm 2 , more than about 10 cm 2 , more than about 100 cm 2 , more than about 1,000 cm 2 , more than about 1 m 2 , more than about 10 m 2 , more than about 100 m 2 , more than about 1000 m 2 . In some embodiments, said volume is from about 0.1 cm 2 to about 1 cm 2 , from about 1 cm 2 to about 10 cm 2 , from about 10 cm 2 to about 100 cm 2 , from about 100 cm 2 to about 1,000 cm 2 , from about 1,000 cm 2 to about 1 m 2 , from about 1 m 2 to about 10 m 2 , from about 10 m 2 to about 100 m 2 , from about 100 m 2 cubic meter to about 1,000 m 2 .
  • the bed of ion exchange material is contained between two filter plates.
  • said bed of ion exchange material has a characteristic “cross sectional length” of said bed, defined as the average dimension of the said solid mass, measured in a direction that is perpendicular to the direction of fluid flow through the filter bank.
  • the cross-sectional length of said bed is less than about 1 cm, less WSGR Docket No.50741-726.601 than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the cross-sectional length of said bed is at most about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the cross-sectional length of said bed is more than about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the cross-sectional length of said bed is more than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the cross- sectional length of said bed is from about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 8 cm, from about 8 cm to about 20 cm, from about 20 cm to about 40 cm, from about 40 cm to about 80 cm, from about 80 cm to about 120 cm, from about 120 cm to about 2 m, from about 2 m to about 4 m, from about 4 m to about 8 m.
  • the cross-sectional length is selected from: about 250 mm, 320 mm, 470 mm, 630 mm, 800 mm, 1000 mm, 1200 mm, 1500 mm, 2000 mm, 4000 mm.
  • the bed of sorbent material is not square, and comprises a cross-sectional length that is selected from two of the following dimensions: about 250 mm, 320 mm, 470 mm, 630 mm, 800 mm, 1000 mm, 1200 mm, 1500 mm, 2000 mm, 4000 mm.
  • the cross- sectional length of the bed of lithium-selective sorbent is 2000 mm x 4000 mm, 1500 mm x 2000 mm, 2500 mm by 5000 mm, or a combination thereof.
  • the device containing ion-exchange beads is comprised of multiple and separate ion-exchange compartments arranged within a single vessel.
  • the lithium extraction device comprises multiple and separate lithium extraction compartments arranged within a single vessel.
  • the lithium extraction devices comprises multiple individual filter banks – each containing an individual lithium- selective sorbent compartment – where lithium is absorbed by said lithium selective sorbent.
  • said compartments comprise individual filter banks.
  • said multiple compartments comprise the filter chambers contained between filter plates in a filter press.
  • a single lithium extraction device comprises about two, about three, about five, about ten, about twenty, about thirty, about fifty, about one-hundred, about one hundred and fifty, or about two-hundred individual lithium extraction compartments.
  • the multiple filter banks are held together by a device that applies a mechanical force that presses the individual filter banks together.
  • said device comprises a hydraulic system, comprising one more pistons and one or more devices to apply a hydraulic force on said piston.
  • the mechanical force is applied to one structurally reinforced component that is in contact with the first plate in the stack of filter banks, and the compressive force is distributed across all filter plates in the device.
  • said force is applied by means of a pressurized hydraulic fluid system, pressurized air system, mechanical tensions system, or combinations thereof.
  • the pressure applied to compress all filter bank together is less than 50 psi, less than 150 psi, less than 500 psi, less than 1000 psi, less than 2500 psi, or less than 5000 psi.
  • the pressure applied to compress all filter bank together is at most 50 psi, at most 150 psi, at most 500 psi, at most 1000 psi, at most 2500 psi, or at most 5000 psi. In some embodiments the pressure applied is more than 50 psi, more than 150 psi, more than 500 psi, more than 1000 psi, more than 2500 psi, or more than 5000 psi.
  • the pressure applied is from 50 psi to 150 psi, from 150 psi to 500 psi, from 500 psi to 1000 psi, from 1000 psi to 2500 psi, from 2500 psi to 5000 psi.
  • all beds are connected to a shared flow distribution manifold, such that flow of liquid to and from said beds of lithium-selective sorbent occur in parallel.
  • the filter press comprises filter plates.
  • filter plates comprise structures, flow distributors, orifices, fluid conduits, fluid conducts, membranes, structural supports, and any other component that is required for the assembly of a filter bank.
  • two filter plates are assembled together to form a filter bank between them, wherein said filter bank contains a space or chamber that can be loaded with a lithium-selective sorbent. An example of such an assembly is shown in FIG.
  • filter plates 40204 come together to form a single filter bank comprising a bed of lithium-selective sorbent 40215.
  • said filter plates are chamber filter plates.
  • said filter plates are recessed chamber filter plates.
  • said filter plates are diaphragm squeeze filter plates.
  • said filter plates are chosen from, but not limited to, one or more of the following types of filter plates commonly known in the field of the art: recessed, chamber recessed chamber, plate-and- frame, membrane squeeze, diaphragm squeeze, flush plate and frame, mineral plates, gasketed, non-gasketed, mixtures thereof or combinations thereof.
  • said filter plates are constructed out of a metal, stainless steel, carbon steel, titanium, Hastelloy, nickel, Inconel, Monel, tantalum, alloys thereof, or mixtures thereof.
  • said filter plates are construcuted out of polymer, a fluoropolymer, polyether ether ketone (PEEK), acrylonitrile butadiene styrene (ABS), nylon, polycarbonate, polyurethane, polyethylene terephthalate, polybutylene terephthalate, polyethylene, polypropylene, high-density polyethylene, polyphenylene sulfide, tetrapolyethylene, PVDF, EPDM, Viton, rubber, Bunna- N, natural rubber, mixtures thereof, or combinations thereof.
  • the assembled filter banks constitute a filter press, and said filter press is used to contain a lithium-selective sorbent and used to extract lithium.
  • a single lithium extraction device comprises about two, about three, about five, about ten, about twenty, about thirty, about fifty, about one-hundred, about one hundred and fifty, or about two-hundred filter plates in said filter press.
  • the filter press comprises filter plates equipped with a membrane squeeze feature.
  • the filter press comprises membrane filter plates.
  • said membrane filter plates comprise one or more components that are deformed or expanded after the filter bank is filled with the lithium selective sorbent, in a manner that applies a compressive or “squeezing” force on said sorbent. Said deformable components are optionally referred to as a “membrane”.
  • said compression results in additional compaction of the bed of lithium-selective sorbent. In some embodiments, said compression increases the uniformity of the bed of lithium-selective sorbent. In some embodiments, said compression results in improved uniformity of flow when contacting said lithium-selective sorbent with a liquid stream. In some embodiments, said compression is applied continually during operation of the lithium-extraction device. In some embodiments, said compression is applied intermittently during operation of the lithium- extraction device. [0236] In some embodiments, the expandable membrane component that applies mechanical compression or “squeezing” on the sorbent comprises the flow distribution compartment or surface. An example of such a compartment is shown in Figure 4C.
  • a flow distribution compartment exists between the structure surface 40213 and the porous partition 40214.
  • Surface 40213 is flexible, such that hydraulic fluid or air can be injected into chamber 40212 by means of a hydraulic fluid or air distribution system, thereby “inflating” 40213 towards sorbent 40205.
  • such an operating may be denoted as a membrane squeeze.
  • the membrane comprises low density polyethylene, high density polyethylene, polypropylene, polyester, polytetrafluoroethylene (PTFE), types of polyamide, polyether ether ketone (PEEK), polysulfone, polyvinylidene fluoride (PVDF), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), polybutadiene, acrylonitrile butadiene styrene (ABS), polyvinyl chloride (PVC), ethylene tetrafluoroethylene polymer (ETFE), poly(chlorotrifluoroethylene) (PCTFE), ethylene chlorotrifluoro ethylene (Halar), polyvinylfluoride (PVF), fluorinated ethylene-propylene (FEP), perfluorinated elastomer, chlorotrifluoroethylenevinylidene fluoride (FKM), perfluoropolyether (PFPE), perfluorinated
  • a coating material comprises polyvinylidene fluoride (PVDF), polyvinyl chloride (PVC), ethylene chlorotrifluoro ethylene (Halar), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), acrylonitrile butadiene styrene (ABS), expanded polystyrene (EPS), polyphenylene sulfide, sulfonated polymer, carboxylated polymer, other polymers, co- polymers thereof, mixtures thereof, or combinations thereof.
  • PVDF polyvinylidene fluoride
  • PVC polyvinyl chloride
  • Halar ethylene chlorotrifluoro ethylene
  • PVPCS poly (4-vinyl pyridine-co-styrene)
  • PS polystyrene
  • ABS acrylonitrile butadiene styrene
  • EPS expanded polystyrene
  • a filter cake of lithium selective sorbent is held within said filter bank, wherein said cake is formed by flowing a suspension of said sorbent through said filter bank.
  • the pressure applied to deform the membrane is less than 5 psi, less than 25 psi, less than 50 psi, less than 100 psi, less than 150 psi, less than 250 psi, or less than 500 psi. In some embodiments, the pressure applied to deform the membrane is at most 5 psi, at most 25 psi, at most 50 psi, at most 100 psi, at most 150 psi, at most 250 psi, or at most 500 psi.
  • the pressure applied to deform the membrane component of the filter bank is more than 5 psi, more than 25 psi, more than 50 psi, more than 100 psi, more than 150 psi, more than 250 psi, or more than 500 psi.
  • the pressure applied to deform the membrane component of the filter bank is from about 1 psi to about 5 psi, from about 5 psi to about 25 psi, from about 25 psi to about 50 psi, from about 50 psi to about 100 psi, from about 100 psi to about 150 psi, from about 150 psi to about 250 psi, from about 250 psi to about 500 psi.
  • the pressure applied to deform the membrane component of the filter bank remains constant during operation of the lithium extraction device. In some embodiments, the pressure applied to deform the membrane component of the filter bank is varied during operation of the lithium extraction device.
  • the pressure applied to deform the membrane component of the filter bank is applied after said filter bank is loaded with said sorbent, and then released. In some embodiments, the pressure applied to deform the membrane component of the filter bank is applied after said filter bank is loaded with said sorbent, and then maintained during all subsequent operations. In some embodiments, the pressure applied to deform the membrane component of the filter bank is applied when the lithium-selective sorbent is contacted with a liquid resource comprising lithium. In some embodiments, the pressure applied to deform the membrane component of the filter bank is applied when the lithium-selective sorbent is contacted with an acidic eluent that releases lithium form said sorbent.
  • the pressure applied to deform the membrane component of the filter bank is applied during washing of the lithium-selective sorbent with a washing solution. In some embodiments, the pressure applied to deform the membrane component of the filter bank is applied without a liquid stream being in contact with the lithium selective sorbent. [0238] In some embodiment, the pressure on the deformable flow distribution surface is applied by means of compressed air or a compressed liquid. In some embodiment, the pressure on the deformable flow distribution surface is applied by a hydraulic system. In some embodiment, the pressure on the deformable flow distribution surface is applied by a mechanical device, such as a piston.
  • the pressure thus applied on the bed of lithium selective sorbent decreases the volume of said bed. In some embodiments, the pressure thus applied on the bed of lithium selective sorbent decreases the volume of said bed by about 0.01 %, by about 0.1 %, by about 1 %, by about 5 %, by about 10 %, by about 25 %, by about 50 %, by about 75 %, or by about 100 %.
  • the pressure thus applied on the bed of lithium selective sorbent decreases the volume of said bed by more than about 0.01 %, by more than about 0.1 %, by more than about 1 %, by more than about 5 %, by more than about 10 %, by more than about 25 %, by more than about 50 %, by more than about 75 %, or by more than about 100 %.
  • the pressure thus applied on the bed of lithium selective sorbent decreases the volume of said bed by less than about 0.01 %, by less than about 0.1 %, by less than about 1 %, by less than about 5 %, by less than about 10 %, by less than about 25 %, by less than about 50 %, by less than about 75 %, or by less than about 100 %.
  • the pressure thus applied on the bed of lithium selective sorbent decreases the volume of said bed by at most about 0.01 %, by at most about 0.1 %, by at most about 1 %, by at most about 5 %, by at most about 10 %, by at most about 25 %, by at most about 50 %, by at most about 75 %, or by at most about 100 %.
  • the pressure thus applied on the bed of lithium selective sorbent decreases the volume of said bed from about 0.01 % to about 0.1 %, from about 0.1 % to about 1 %, from about 1 % to about 5 %, from about 5 % to about 10 %, from about 10 % to about 25 %, from about 25 % to about 50 %, from about 50 % to about 75 %, from about 75 % to about 100 %.
  • said deformable components or membrane are welded to the rest of the filter bank.
  • said components are replaceable.
  • said components are manufactured of the same material as the rest of the filter bank.
  • said components are manufactured of a different material from the rest of the filter bank.
  • WSGR Docket No.50741-726.601 [0241]
  • the deformable component applies pressure on the bed of lithium-selective sorbent from one side of said bed. In some embodiments, the deformable component applies pressure on the bed of lithium-selective sorbent from both sides of said bed. In some embodiments, the deformable component applies pressure on the bed of lithium- selective sorbent from multiple directions.
  • the direct from which pressure is applied varies with time. In some embodiments, the direct from which pressure is applied depends on the fluid which is being contacted with the lithium-selective sorbent.
  • the deformable component is a membrane.
  • the lithium selective sorbent is loaded into the lithium extraction device.
  • said lithium-selective sorbent is an ion exchange material.
  • the lithium selective sorbent is loaded into the lithium extraction device, and pressure is applied on the loaded sorbent using the deformable component in the filter bank.
  • the lithium selective sorbent is loaded into the lithium extraction device, and the loaded sorbent is squeezed using a membrane in said filter bank.
  • said pressure is applied on the loaded sorbent after initial loading of said sorbent, and then released.
  • said pressure is applied on the loaded sorbent during the entire operation of said device for lithium extraction, during certain periods of said operation. In some embodiments, said pressure is applied on the loaded sorbent when said sorbent absorbs lithium from a liquid resource. In some embodiments, said pressure is applied on the loaded sorbent when said sorbent releases the absorbed lithium to produce an acidic eluent solution. In some embodiments, said pressure is applied on the loaded sorbent when said sorbent is being washed with a wash solution. In some embodiments, said pressure is applied on the loaded sorbent when said sorbent is contacted with water. In some embodiments, said pressure is applied on the loaded sorbent when said sorbent is contacted with a gas.
  • the lithium selective sorbent is loaded into the lithium extraction device.
  • the lithium selective sorbent in order to load said sorbent into the device, is suspended in a fluid within a vessel.
  • suspension of a solid in a liquid is also termed “fluidization”, or fluidization of said solids.
  • said fluid is water, a liquid resource containing lithium, a brine, an acidic eluent solution, an acidic solution, or a mixture thereof.
  • said fluid is a gas flown in a manner that fluidizes the sorbent.
  • the sorbent is suspended in a liquid by agitating sorbent in said liquid, such that the solids are distributed uniformly or non-uniformly throughout the fluid.
  • the distribution of WSGR Docket No.50741-726.601 solids in said fluid allows for the solids to be conveyed out of the vessel where it is contained.
  • suspension of said solids occurs by agitation of solid solids and said fluid, wherein agitation occurs with a mechanical agitator, an eductor, fluid recirculation, baffles, shaking, tapping or a combination thereof.
  • the fluidization of said ion exchange material occurs by means of contact with one or more gases phases.
  • the fluidization of said ion exchange material occurs by means of contact with a liquid resource, a wash solution, an acidic solution, one or more alternate phases or combinations thereof.
  • said ion exchange material is fluidized during contact with said liquid resource.
  • said ion exchange material is fluidized during contact with said acidic solution.
  • said ion exchange material is fluidized during contact with said alternate phase.
  • said ion exchange material is fluidized during contact with said wash solution.
  • initial fluidization of the solids is aided by contacting a pressurized gas with said solid sorbent and said fluid.
  • said aiding occurs by the additional turbulence and break up of the consolidated solids at the bottom of the vessel where said solids are stored.
  • said gas is air, nitrogen, argon, oxygen, chlorine, a different gas, or a combination thereof.
  • injection of said gas for contact with the solid and fluid occurs through one or more of a pipe, tubing, channels, slits, beams, baffles, baskets, scallops, nozzles, or a mesh.
  • the components that direct flow within the vessel are perforated.
  • the openings or perforations in the components that distribute flow are shaped as circles, ovals, vertical or horizontal slits, squares, crosses, rectangles, triangles, irregular shapes, or a combination thereof.
  • flow of the gas occurs from the top to the bottom of the vessel. In some embodiments, flow of the gas occurs from the bottom to the top of the vessel. In some embodiments, flow of the gas occurs from the inside to the outside of the vessel. In some embodiments, flow of the gas occurs from the outside to the inside of the vessel.
  • the vessel has an internal nozzle designed to distribute flow of the gas evenly. In one embodiment, the vessel has nozzles placed equidistant with each other on a support plate.
  • the nozzles are spaced out so that each nozzle covers the same area.
  • the nozzles have slits or holes of width of less than 0.1 ⁇ m, less than 1 ⁇ m, less than 10 ⁇ m, less than 100 ⁇ m, or less than 1 mm.
  • the vessel has mesh with holes less than 0.1 ⁇ m, less than 1 ⁇ m, less than 10 ⁇ m, less than 100 ⁇ m, or less than 1000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of less than about 10 ⁇ m, less than about 20 ⁇ m, less than about 30 ⁇ m, less than about 40 ⁇ m, less than about 50 ⁇ m, less than about 60 ⁇ m, less than about 70 ⁇ m, less than about 80 ⁇ m, less than about 90 ⁇ m, less than about 100 ⁇ m, less than about 200 ⁇ m, less than about 300 ⁇ m, less than about 400 ⁇ m, less than about 500 ⁇ m, less than about 600 ⁇ m, less than about 700 ⁇ m, less than about 800 ⁇ m, less than about 900 ⁇ m, less than about 1000 ⁇ m, less than about 2000 ⁇ m, less than about 4000 ⁇ m, less than about 8000 ⁇
  • the nozzles have slits or holes of width of at most 0.1 ⁇ m, at most 1 ⁇ m, at most 10 ⁇ m, at most 100 ⁇ m, or at most 1 mm.
  • the vessel has mesh with holes at most 0.1 ⁇ m, at most 1 ⁇ m, at most 10 ⁇ m, at most 100 ⁇ m, or at most 1000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of at most about 10 ⁇ m, at most about 20 ⁇ m, at most about 30 ⁇ m, at most about 40 ⁇ m, at most about 50 ⁇ m, at most about 60 ⁇ m, at most about 70 ⁇ m, at most about 80 ⁇ m, at most about 90 ⁇ m, at most about 100 ⁇ m, at most about 200 ⁇ m, at most about 300 ⁇ m, at most about 400 ⁇ m, at most about 500 ⁇ m, at most about 600 ⁇ m, at most about 700 ⁇ m, at most about 800 ⁇ m, at most about 900 ⁇ m, at most about 1000 ⁇ m, at most about 2000 ⁇ m, at most about 4000 ⁇ m, at most about 8000 ⁇ m, or at most about 10000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of more than about 10 ⁇ m, more than about 20 ⁇ m, more than about 30 ⁇ m, more than about 40 ⁇ m, more than about 50 ⁇ m, more than about 60 ⁇ m, more than about 70 ⁇ m, more than about 80 ⁇ m, more than about 90 ⁇ m, more than about 100 ⁇ m, more than about 200 ⁇ m, more than about 300 ⁇ m, more than about 400 ⁇ m, more than about 500 ⁇ m, more than about 600 ⁇ m, more than about 700 ⁇ m, more than about 800 ⁇ m, more than about 900 ⁇ m, more than about 1000 ⁇ m, more than about 2000 ⁇ m, more than about 4000 ⁇ m, more than about 8000 ⁇ m, or more than about 10000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of less than about 10 ⁇ m to about 20 ⁇ m, from about 20 ⁇ m to about 40 ⁇ m, from about 40 ⁇ m to about 80 ⁇ m, from about 80 ⁇ m to about 200 ⁇ m, from about 100 ⁇ m to about 400 ⁇ m, from about 200 ⁇ m to about 800 ⁇ m, from about 400 ⁇ m to about 1000 ⁇ m, from about 600 ⁇ m to about 2000 ⁇ m, from about 1000 ⁇ m to about 2000 ⁇ m, from about 2000 ⁇ m to about 4000 ⁇ m, from about 4000 ⁇ m to about 8000 ⁇ m, from about 6000 ⁇ m to about 10000 ⁇ m.
  • a gas is contacted with the lithium selective sorbent for more than about 10 milliseconds, more than about 100 milliseconds, more than about 1 second, more WSGR Docket No.50741-726.601 than about 10 seconds, more than about 100 seconds, more than about 1 minute, more than about 10 minutes, more than about 100 minutes, more than about 1 hour, more than about 10 hours, more than about 100 hours.
  • a gas is contacted with the ion exchange beads for at most about 10 milliseconds, at most about 100 milliseconds, at most about 1 second, at most about 10 seconds, at most about 100 seconds, at most about 1 minute, at most about 10 minutes, at most about 100 minutes, at most about 1 hour, at most about 10 hours, at most about 100 hours.
  • a gas is contacted with the ion exchange beads for less than about 10 milliseconds, less than about 100 milliseconds, less than about 1 second, less than about 10 seconds, less than about 100 seconds, less than about 1 minute, less than about 10 minutes, less than about 100 minutes, less than about 1 hour, less than about 10 hours, less than about 100 hours.
  • an gas is contacted with the ion exchange beads from about 10 milliseconds to about 100 milliseconds, from about 100 milliseconds to about 1 second, from about 1 second to about 10 seconds, from about 10 seconds to about 100 seconds, from about 100 seconds to about 1 minute, from about 1 minute to about 10 minutes, from about 10 minutes to about 100 minutes, from about 1 hour to about 10 hours, from about 10 hours to about 100 hours.
  • a gas is injected to contact lithium selective sorbent at a pressure of more than about 0.1 psi, more than about 1 psi, more than about 5 psi, more than about 10 psi, more than about 50 psi, more than about 100 psi, more than about 500 psi, more than about 1000 psi, more than about 500 psi, more than about 1000 psi.
  • a gas is injected to contact the ion exchange beads at a pressure of at most about 0.1 psi, at most about 1 psi, at most about 5 psi, at most about 10 psi, at most about 50 psi, at most about 100 psi, at most about 500 psi, at most about 1000 psi, at most about 500 psi, at most about 1000 psi.
  • a gas is injected to contact the ion exchange beads at a pressure of less than about 0.1 psi, less than about 1 psi, less than about 5 psi, less than about 10 psi, less than about 50 psi, less than about 100 psi, less than about 500 psi, less than about 1000 psi, less than about 500 psi, less than about 1000 psi.
  • an gas is injected to contact the ion exchange beads at a pressure from about 0.1 psi to about 5 psi, from about 5 psi to about 10 psi, from about 10 psi to about 50 psi, from about 50 psi to about 100 psi, from about 100 psi to about 500 psi, from about 500 psi to about 1000 psi, from about 1000 psi to about 5000 psi, from about 5000 psi to about 10,000 psi.
  • the suspended lithium selective sorbent is loaded into the lithium extraction device.
  • the suspended sorbent is conveyed from the vessel described above and into a filer press.
  • conveyance of said suspension occurs by use of a mechanical device.
  • said mechanical device comprises a double- diaphragm pump, and air operated double-diaphragm pump, a diaphragm pump, a positive displacement pump, a centrifugal pump, a vortex pump, a slurry pump, or combinations thereof.
  • said suspension is conveyed from said vessel and into said ion exchange device by pressurizing the top of said vessel, such that the liquid suspension is forced by pressure-driven flow to exist said vessel through a pipe.
  • the suspension of sorbent that is loaded into the ion exchange device has a solids content of less than about 0.001 % v/v (solids volume per total solution volume), of less than about 0.01 % v/v, of less than about 0.1 % v/v, of less than about 1 % v/v, of less than about 10 % v/v, of less than about 50 % v/v, of less than about 75 % v/v, of less than about 100 % v/v.
  • the suspension of sorbent that is loaded into the ion exchange device has a solids content of at most about 0.001 % v/v (solids volume per total solution volume), of at most about 0.01 % v/v, of at most about 0.1 % v/v, of at most about 1 % v/v, of at most about 10 % v/v, of at most about 50 % v/v, of at most about 75 % v/v, of at most about 100 % v/v.
  • the suspension of sorbent that is loaded into the ion exchange device has a solids content of more than about 0.001 % v/v (solids volume per total solution volume), of more than about 0.01 % v/v, of more than about 0.1 % v/v, of more than about 1 % v/v, of more than about 10 % v/v, of more than about 50 % v/v, of more than about 75 % v/v.
  • the suspension of sorbent that is loaded into the ion exchange device has a solids content of from about 0.001 % v/v (solids volume per total solution volume) to about 0.01 % v/v, from about 0.01 % v/v to about 0.1 % v/v, of from about 0.1 % v/v to about 1 % v/v, of from about 1 % v/v to about 10 % v/v, of from about 10 % v/v to about 50 % v/v, of from about 50 % v/v to about 75 % v/v, of from 75 % v/v to about 100 % v/v.
  • the suspension of sorbent is a thick suspension. In some embodiments, said suspension of sorbents is a slurry. [0252] In some embodiments, the said suspension of sorbent is conveyed into the filter press via a pipe. In some embodiments, said suspension of sorbent is conveyed into filter press through one inlet port. In some embodiments, said suspension of sorbent is conveyed into said lithium extraction device through one or more inlet ports. In some embodiments, said suspension of sorbent is conveyed into said lithium extraction device through two inlet ports.
  • said suspension of sorbent is conveyed into said lithium extraction device through two inlet ports that are connected to opposite ends of the lithium extraction device.
  • one or more of said inlet ports connect to a common piping system that is in fluid contact with all filter banks within said lithium extraction device.
  • one or more of said inlet ports connect to a common piping system that is in fluid contact with all filter banks within said lithium extraction device.
  • one or more of said inlet ports connect to a common conduit or piping system that is in fluid contact with all filter banks within said lithium extraction device.
  • Conduit 410 spans the entire stack of filter banks at their center, and is connected to a fluid inlet port at the end of the device (416).
  • the location of the fluid conduit for said suspension is the same in all filter banks across the entire device.
  • the location of the fluid conduit for said suspension is the different in different filter banks that comprise said device.
  • the location of the fluid conduit for the sorbent is above the filter bank, below the filter bank, or off to one of the sides of the filter bank.
  • the outlet of the conduit for conveyance of sorbent into individual filter bank is dictated by the location of the slurry inlet port in a filter plate.
  • the center of the filter bank is the center of symmetry of said filter bank when observed in the direction of normal fluid flow through said bed.
  • said conduit is located at the center of the filter plate.
  • said conduit is located off-center from the center of the filter plate, wherein off-center implies a location in any of the radial directions from said center.
  • the ratio (distance from the center of said filter plate to the slurry inlet) to (distance from the center of plate to the edge of said plate) is less than about 0.1, less than about 0.25, less than about 0.4, less than about 0.5, less than about 0.75, less than about 0.9.
  • the ratio (distance from the center of said filter plate to the slurry inlet) to (distance from the center of plate to the edge of said plate) is at most about 0.1, at most about 0.25, at most about 0.4, at most about 0.5, at most about 0.75, at most about 0.9. In some embodiments, the ratio In some embodiments, the ratio (distance from the center of said filter plate to the slurry inlet) to (distance from the center of plate to the edge of said plate) is more than about 0.1, more than about 0.25, more than about 0.4, more than about 0.5, more than about 0.75, more than about 0.9.
  • the ratio (distance from the center of said filter plate to the slurry inlet) to (distance from the center of plate to the edge of said plate) is from about 0.01 to about 0.1, from about 0.1 to about 0.25, from about 0.25 to about 0.4, from about 0.4 to about 0.5, WSGR Docket No.50741-726.601 from about 0.5 to about 0.75, from about 0.75 about 0.9.
  • the outlet of the conduit for conveyance of sorbent into individual filter bank is located within said filter plate towards the top, bottom, side, or corner of said filter bed. In some embodiments, the outlet of the conduit for conveyance of sorbent into individual filter bank is outside said filter bank.
  • the outlet of the conduit for conveyance of sorbent into individual filter bank is located outside the bed of sorbent, at the top, bottom, side, or corner of the lithium extraction device but outside of the bed of sorbent, wherein bed of sorbent is defined as the sorbent that absorbs lithium during operation of the device.
  • bed of sorbent is defined as the sorbent that absorbs lithium during operation of the device.
  • fluid flows out of said filter bank through one or more of said porous partitions, and out of four of the pipes that connect said filter bank to the rest of the lithium extraction device. In some embodiments, fluid flows out of said filter bank through one or more of said porous partitions, and out of more than of one of the pipes that connect said filter bank to the rest of the lithium extraction device.
  • the lithium extraction device comprising a filter press has a single inlet for conveyance of the suspension of sorbent into said filter press; such a configuration of a filter press is called a "single end feed” filter press.
  • the lithium extraction device comprising a filter press has two inlets for conveyance of the suspension of sorbent into said filter press, located at opposite ends of the device; such a configuration of a filter press is called a "double-end feed” filter press.
  • the bed of sorbent within said filter bank is filled with sorbent until the physical volume available in said filter bank is fully occupied by said sorbent.
  • the maximum fill level is determined based on the pressure required to pump the suspension of sorbent in fluid into said filter bank; when a certain pressure and pumping rate is reached, the filter banks are considered completely filled.
  • the filter banks are filled with sorbent until the pressure required to pump said suspended sorbent into said device is more than about 0.1 psi, more than about 1 psi, more than about 5 psi, more than about 10 psi, more than about 20 psi, more than about 50 psi, more than about 75 psi, more than about 100 psi, more than about 200 psi, more than about 500 psi.
  • the filter banks are filled with sorbent until the pressure required to pump said suspended sorbent into said device is at most about 0.1 psi, at most about 1 psi, at most about 5 psi, at most about 10 psi, at most about 20 psi, at most about 50 psi, at most about 75 psi, at most about 100 psi, at most about 200 psi, at most about 500 psi.
  • the filter banks are filled with sorbent until the pressure required to pump said suspended sorbent into said device is less than about 0.1 psi, less than about 1 psi, less than about 5 psi, less than about 10 psi, less than about 20 psi, less than about 50 psi, less than about 75 psi, less than about 100 psi, less than about 200 psi, less than about 500 psi.
  • the filter banks are filled with sorbent until the pressure required to pump said suspended sorbent into said device is from about 0.1 psi to about 5 psi, from about 5 psi to about 10 psi, from about 10 psi to about 20 psi, from about 20 psi to about 50 psi, from about 50 psi to about 100 psi, from about 100 psi to about 250 psi, from about 250 psi to about 500 psi, from about 500 psi to about 1000 psi.
  • the filter banks are filled with sorbent until the rate at which the suspended sorbent is pumped into said device is less than about 0.1 %, less than about 1%, less than about 10 %, less than about 50 %, or less than about 75 % of the initial rate at which the suspended sorbent is pumped into said device (when said device is empty). In some embodiments, the filter banks are filled with sorbent until the rate at which the suspended sorbent is pumped into said device is at most about 0.1 %, at most about 1%, at most about 10 %, at most about 50 %, or at most about 75 % of the initial rate at which the suspended sorbent is pumped into said device (when said device is empty).
  • the filter banks are filled with sorbent until the rate at which the suspended sorbent is pumped into said device is more than about 0.1 %, more than about 1%, more than about 10 %, more than about 50 %, or more than about 75 % of the initial rate at which the suspended sorbent is pumped into said device (when said device is empty).
  • the filter banks are filled with sorbent until the rate at which the suspended sorbent is pumped into said device is from about 0.01 % to about 0.1 %, from about 0.1 % to about 1%, from about 1% to about 10 %, from about WSGR Docket No.50741-726.601 10 % to about 50 %, from about 50 % to about 75 % of the initial rate at which the suspended sorbent is pumped into said device (when said device is empty).
  • such a device is constructed by using a series of filter banks wherein the filters contain ion exchange beads.
  • such a device is constructed where multiple ion-exchange compartments are arranged vertically or horizontally.
  • such filter banks are separated to load and unloaded the ion exchange beads.
  • the ion exchange beads are conveyed into the filter banks as a slurry to load the ion exchange beads into the ion exchange vessel.
  • loading of the ion exchange beads occurs in the same direction, opposite direction, orthogonal direction, or other direction relative the normal direction of flow during the ion exchange process.
  • the tension holding the filter bank together is increased, decreased, or maintained during the ion exchange process.
  • ion-exchange compartments are added or removed from the vessel by mechanical means, such that the number of ion-exchange compartments are adjusted.
  • ion-exchange compartments and their components are mechanically separated to clean out, replace, and fill in compartments and partitions between compartments.
  • the ion exchange compartment within each ion-exchange compartment is partially filled with ion exchange beads, such that ion exchange beads freely move within their containing compartment during contacting with fluid.
  • the ion exchange compartment is filled to its capacity with ion exchange beads, such that ion exchange beads are fixed in place and cannot freely move within the containing compartment during contacting with fluid.
  • the ion exchange compartment is partially filled, and becomes completely filled by the change in volume of ion exchange beads that occurs when contacting said beads with certain fluids.
  • the ion exchange compartment is configured such that ion exchange beads enter and leave the ion-exchange compartment conveyed by the fluid which they are contacting, in the top-down or down-top direction.
  • the ion exchange beads are loaded into and unloaded from said compartments through the top or bottom of the compartments, through the sides, or by mechanically separating and opening the ion-exchange compartment to expose the compartment and subsequently filling said compartment with ion-exchange beads.
  • the typical length of the vessel containing the ion-exchange compartments is less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 100 cm, less than about 200 cm, less than about 400 cm, less than about 600 cm, less than about 800 cm, less than about 1 m, less than WSGR Docket No.50741-726.601 about 2 m, less than about 4 m, less than about 6 m, less than about 8 m, less than about 10 m, less than about 20 m, less than about 40 m.
  • the typical length of the vessel containing the ion-exchange compartments is at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 100 cm, at most about 200 cm, at most about 400 cm, at most about 600 cm, at most about 800 cm, at most about 1 m, at most about 2 m, at most about 4 m, at most about 6 m, at most about 8 m, at most about 10 m, at most about 20 m, at most about 40 m.
  • the typical length of the said vessel is more than about 10 cm, more than about 20 cm, more than about 40 cm, more than about 60 cm, more than about 80 cm, more than about 100 cm, more than about 200 cm, more than about 400 cm, more than about 600 cm, more than about 800 cm, more than about 1 m, more than about 2 m, more than about 4 m, more than about 6 m, more than about 8 m, more than about 10 m, more than about 20 m, more than about 40 m.
  • the typical length of said vessel is from about 10 cm to about 20 cm, from about 20 cm to about 40 cm, from about 40 cm to about 80 cm, from about 80 cm to about 2 m from about 1 m to about 4 m, from about 2 m to about 8 m, from about 4 m to about 10 m, from about 6 m to about 20 m, from about 10 m to about 40 m.
  • the devices, vessels, system, and methods described herein utilize a flow distribution compartment to optimize the flow of various liquids, solutions or gases through the devices, vessels, and systems.
  • the flow distribution compartment is an inner flow distribution compartment and/or outer flow distribution compartment.
  • the flow distribution compartment and/or ion-exchange bead compartment is empty, partially filled, or fully filled with fluid, or a combination thereof. In some embodiments, the flow distribution compartment and/or ion-exchange bead compartment are cylindrical, rectangular, irregular, or a combination thereof. In some embodiments, the flow distribution compartment has a constant cross-sectional area or a varying cross-sectional area.
  • the filter banks comprise one or more flow distribution compartments. In some embodiments, the filter bank comprise two flow distribution compartments. In some embodiments, said flow distribution compartments comprise a flow distribution surface. In some embodiments, said flow distribution compartment comprises inlet orifices, a void, and a permeable partition.
  • said void is formed between the porous partition and the flow distribution surface.
  • the uniformity of flow across the lithium selective sorbent can be further enhanced by mechanically compressing the sorbent-bed by a deformable flow WSGR Docket No.50741-726.601 distribution surface.
  • this deformable surface optionally comprises a membrane, as described herein.
  • pressure is applied in a chamber behind the flow distribution surface.
  • the combination of such mechanical compression with a membrane and the construction of the flow distribution surface enables for most optimal flow distribution across the bed of lithium-selective sorbent, thereby resulting in its optimal performance for ion exchange.
  • said mechanical compression is applied during fluid flow. In some embodiments, said mechanical compression is applied during loading of the sorbent into the filter bank, and is not applied during operation of the device as a lithium extraction device. In some embodiments, said compression is applied during contact with a liquid resource. In some embodiments, said compression is applied during contact with a wash solution. In some embodiments, said compression is applied during contact with an acidic eluent. In some embodiments, said compression is applied at different times, wherein the time between cycles of compression and release is constant, increases with time, decreases with time, varies sinusoidally, is non-uniform, or a combination thereof.
  • the surfaces of filter plates contain surface features to allow for an even distribution of flow of fluid across the filter cloth and into out of the filter bank.
  • One embodiment of said flow distribution surfaces was described above, as shown in Figure 4 by flow distribution surface 40213.
  • these surface features are shaped as circles, pips, ovals, hexagons, squares, rectangles, rectangular ovals, spheres, grooves, flat surfaces, uneven surfaces, stars, dimples, other geometric shapes, mixtures thereof, or combinations thereof.
  • said features have a protrusion from the surface of less than about 1 mm, less than about 2 mm, less than about 5 mm, less than about 10 mm, less than about 20 mm, less than about 30 mm, less than about 40 mm, less than about 50 mm, less than about 60 mm, less than about 70 mm, less than about 80 mm, less than about 90 mm, less than about 100 mm.
  • said features have a protrusion from the surface of at most about 1 mm, at most about 2 mm, at most about 5 mm, at most about 10 mm, at most about 20 mm, at most about 30 mm, at most about 40 mm, at most about 50 mm, at most about 60 mm, at most about 70 mm, at most about 80 mm, at most about 90 mm, at most about 100 mm.
  • said features have a protrusion from the surface of more than about 1 mm, more than about 2 mm, more than about 5 mm, more than about 10 mm, more than about 20 mm, more than about 30 mm, more than about 40 mm, more than about 50 mm, more than about 60 mm, more than about 70 mm, more than about 80 mm, more than about 90 mm, more than about 100 mm.
  • said features have a WSGR Docket No.50741-726.601 protrusion from the surface of about 1 mm to about 2 mm, from about 2 mm to about 4 mm, from about 4 mm to about 10 mm, from about 10 mm to about 20 mm.
  • said features have a length of less than about 1 cm, less than about 2 cm, less than about 5 cm, less than about 10 cm, less than about 20 cm, less than about 30 cm, less than about 40 cm, less than about 50 cm, less than about 60 cm, less than about 70 cm, less than about 80 cm, less than about 90 cm, less than about 100 cm, less than about 200 cm, less than about 500 cm, less than about 10 m.
  • said features have a length of at most about 1 cm, at most about 2 cm, at most about 5 cm, at most about 10 cm, at most about 20 cm, at most about 30 cm, at most about 40 cm, at most about 50 cm, at most about 60 cm, at most about 70 cm, at most about 80 cm, at most about 90 cm, at most about 100 cm, at most about 200 cm, at most about 500 cm, at most about 10 m.
  • said features have a length of more than about 1 cm, more than about 2 cm, more than about 5 cm, more than about 10 cm, more than about 20 cm, more than about 30 cm, more than about 40 cm, more than about 50 cm, more than about 60 cm, more than about 70 cm, more than about 80 cm, more than about 90 cm, more than about 100 cm, more than about 200 cm, more than about 500 cm, more than about 10 m.
  • said features have a length of about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 10 cm, from about 10 cm to about 20 cm, from about 20 cm to about 50 cm, from about 50 cm to about 100 cm, from about 100 cm to about 200 cm, from about 200 cm to about 10 m.
  • the shape of said flow distribution surface conforms to the shape of the filter bank. In some embodiments, the shape of said flow distribution surface conforms to the shape of the porous partition. In some embodiments, the shape of said flow distribution surface conforms to the shape of the sorbent cake or bed.
  • the filter plates comprise structural supports, fasteners, beams, adhesives, compression fittings, gaskets or other structural components for fastening of all components of the filter bank.
  • the filter plates comprise pipes, tubes, conduits, conducts, and orifices that direct flow into individual filter banks.
  • the filter press is constructed to facilitate the flow of a liquid through the filter bank. In some embodiments, such a liquid flow is enabled by the construction of the filter bank. In some embodiments, the filter plates are constructed to facilitate their manufacturing, while enabling facile assembly into a filter press comprising multiple filter banks.
  • the fluid conduits that deliver and remove fluid flow to and from the flow distribution compartments, chambers, and surfaces described above are WSGR Docket No.50741-726.601 configured to uniformly distribute flow across the bed of lithium selective sorbent.
  • said fluid conduits comprise orifices.
  • the fluid flown in this manner is a liquid resource comprising lithium, such that the lithium-selective sorbent absorbs lithium from said liquid resource.
  • the fluid flown in this manner is a wash solution comprising water, such that entrained fluids are removed from the bed of lithium-selective sorbent.
  • the lithium selective sorbent is an ion exchange material and the fluid flown in this manner is an acidic eluent solution comprising protons, such that the lithium selective sorbent releases lithium while absorbing protons.
  • the fluid flown in this manner is water, such that the lithium selective sorbent releases lithium.
  • the flows described herein are alternated through the same ion exchange material that is held within the filter bank. [0273] In some embodiments, the fluid flown is a liquid.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is less than about 1 mL/min, less than about 10 mL/min, less than about 100 mL/min, less than about 1 L/min, less than about 10 L/min, less than about 100 L/min, less than about 1,000 L/min, less than about 10,000 L/min. In some embodiments, the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is at most about 1 mL/min, at most about 10 mL/min, at most about 100 mL/min, at most about 1 L/min, at most about 10 L/min, at most about 100 L/min, at most about 1,000 L/min, at most about 10,000 L/min.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is more than about 1 mL/min, more than about 10 mL/min, more than about 100 mL/min, more than about 1 L/min, more than about 10 L/min, more than about 100 L/min, more than about 1,000 L/min, more than about 10,000 L/min.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is from about 1 mL/min to about 10 mL/min, from about 10 mL/min to about 100 mL/min, from about 100 mL/min to about 1 L/min, from about 1 L/min to about 10 L/min, from about 10 L/min to about 100 L/min, from about 100 L/min to about 1,000 L/min, from about 1,000 L/min to about 10,000 L/min.
  • the fluid flown is a liquid.
  • the ratio of volume of lithium-selective sorbent to flow rate of fluid through the bed of lithium selective sorbent, which has units of time, indicates the characteristic contact time of fluid with the bed of lithium selective sorbent.
  • said characteristic contact time is less than about 1 second, less than about 10 seconds, less than about 1 minute, less than about 5 minutes, less than about 10 minutes, less than about 1 hours, less than about 10 hours, less than about 1 WSGR Docket No.50741-726.601 day.
  • said characteristic contact time is at most about 1 second, at most about 10 seconds, at most about 1 minute, at most about 5 minutes, at most about 10 minutes, at most about 1 hours, at most about 10 hours, at most about 1 day.
  • said characteristic contact time is more than about 1 second, more than about 10 seconds, more than about 1 minute, more than about 5 minutes, more than about 10 minutes, more than about 1 hours, more than about 10 hours, more than about 1 day. In some embodiments, said characteristic contact time is from about 0.1 second to about 1 second, from about 1 second to about 10 seconds, from about 10 seconds to about 1 minute, from about 1 minute to about 5 minutes, from about 5 minutes to about 10 minutes, from about 10 minutes to about 1 hours, from about 1 hours to about 10 hours, from about 1 hours to about 1 day. [0275] In some embodiments, the fluid flown is a liquid.
  • the ratio of volume of flow rate of fluid through the bed to the surface area of the bed, which has units of length per time, indicates the characteristic flux of fluid through the bed of lithium selective sorbent.
  • said characteristic flux is less than about 1 mm/min, less than 1 cm/min, less than about 10 cm/min, less than about 1 m/min, less than about 10 m/min, less than about 100 m/min.
  • said characteristic flux is at most about 1 mm/min, at most 1 cm/min, at most about 10 cm/min, at most about 1 m/min, at most about 10 m/min, at most about 100 m/min.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is more than about 1 mm/min, more than 1 cm/min, more than about 10 cm/min, more than about 1 m/min, more than about 10 m/min, more than about 100 m/min. In some embodiments, the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is from about 0.1 mm/min to about 1 mm/min, from about 1 mm/min to about 1 cm/min, from about 1 cm/min to about 10 cm/min, from about 10 cm/min to about 1 m/min, from about 1 m/min to about 10 m/min, from about 10 m/min to about 100 m/min.
  • the fluid flown is a gas.
  • said gas is air, nitrogen, argon, or a different gas.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is less than about 1 mL/min, less than about 10 mL/min, less than about 100 mL/min, less than about 1 L/min, less than about 10 L/min, less than about 100 L/min, less than about 1,000 L/min, less than about 10,000 L/min.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is at most about 1 mL/min, at most about 10 mL/min, at most about 100 mL/min, at most about 1 L/min, at most about 10 L/min, at most about 100 L/min, at most about 1,000 L/min, at most about 10,000 L/min.
  • the flow rate of fluid through the bed of WSGR Docket No.50741-726.601 lithium selective sorbent in one filter bank is more than about 1 mL/min, more than about 10 mL/min, more than about 100 mL/min, more than about 1 L/min, more than about 10 L/min, more than about 100 L/min, more than about 1,000 L/min, more than about 10,000 L/min.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is from about 1 mL/min to about 10 mL/min, from about 10 mL/min to about 100 mL/min, from about 100 mL/min to about 1 L/min, from about 1 L/min to about 10 L/min, from about 10 L/min to about 100 L/min, from about 100 L/min to about 1,000 L/min, from about 1,000 L/min to about 10,000 L/min.
  • the fluid flown is a gas. In some embodiments, said gas is air, nitrogen, argon, or a different gas.
  • the ratio of volume of lithium- selective sorbent to flow rate of fluid through the bed of lithium selective sorbent indicates the characteristic contact time of fluid with the bed of lithium selective sorbent.
  • said characteristic contact time is less than about 1 second, less than about 10 seconds, less than about 1 minute, less than about 5 minutes, less than about 10 minutes, less than about 1 hours, less than about 10 hours, less than about 1 day.
  • said characteristic contact time is at most about 1 second, at most about 10 seconds, at most about 1 minute, at most about 5 minutes, at most about 10 minutes, at most about 1 hours, at most about 10 hours, at most about 1 day.
  • said characteristic contact time is more than about 1 second, more than about 10 seconds, more than about 1 minute, more than about 5 minutes, more than about 10 minutes, more than about 1 hours, more than about 10 hours, more than about 1 day. In some embodiments, said characteristic contact time is from about 0.1 second to about 1 second, from about 1 second to about 10 seconds, from about 10 seconds to about 1 minute, from about 1 minute to about 5 minutes, from about 5 minutes to about 10 minutes, from about 10 minutes to about 1 hours, from about 1 hours to about 10 hours, from about 1 hours to about 1 day.
  • the fluid flown is a gas. In some embodiments, said gas is air, nitrogen, argon, or a different gas.
  • the ratio of volume of flow rate of fluid through the bed to the surface area of the bed, which has units of length per time, indicates the characteristic flux of fluid through the bed of lithium selective sorbent.
  • said characteristic flux is less than about 1 mm/min, less than 1 cm/min, less than about 10 cm/min, less than about 1 m/min, less than about 10 m/min, less than about 100 m/min.
  • said characteristic flux is at most about 1 mm/min, at most 1 cm/min, at most about 10 cm/min, at most about 1 m/min, at most about 10 m/min, at most about 100 m/min.
  • the flow rate of fluid through the bed of lithium WSGR Docket No.50741-726.601 selective sorbent in one filter bank is more than about 1 mm/min, more than 1 cm/min, more than about 10 cm/min, more than about 1 m/min, more than about 10 m/min, more than about 100 m/min.
  • the flow rate of fluid through the bed of lithium selective sorbent in one filter bank is from about 0.1 mm/min to about 1 mm/min, from about 1 mm/min to about 1 cm/min, from about 1 cm/min to about 10 cm/min, from about 10 cm/min to about 1 m/min, from about 1 m/min to about 10 m/min, from about 10 m/min to about 100 m/min.
  • the pressure applied to flow said fluid across the ion- exchange bed is less than 5 psi, less than 25 psi, less than 50 psi, less than 100 psi, less than 150 psi, less than 250 psi, or less than 500 psi. In some embodiments, the pressure applied to flow said fluid across the ion-exchange bed is at most 5 psi, at most 25 psi, at most 50 psi, at most 100 psi, at most 150 psi, at most 250 psi, or at most 500 psi.
  • the pressure applied to flow said fluid across the ion-exchange bed is more than 5 psi, more than 25 psi, more than 50 psi, more than 100 psi, more than 150 psi, more than 250 psi, or more than 500 psi.
  • the pressure applied to flow said fluid across the ion- exchange bed is from about 1 psi to about 5 psi, from about 5 psi to about 25 psi, from about 25 psi to about 50 psi, from about 50 psi to about 100 psi, from about 100 psi to about 150 psi, from about 150 psi to about 250 psi, from about 250 psi to about 500 psi.
  • the filter press comprises multiple filter banks. In some embodiments, when operation of the device is complete, filter plates are separated such that an individual filter bank is exposed, thereby allowing the sorbent contained in said filter bank to fall of said filter bank by gravity.
  • a separation requires for the pressure holding the stack of filter plates together to be released.
  • an operator physically separates each plate from the next.
  • an automated system physically separates all plates simultaneously.
  • an operator positions an automated system that separates one plate at a time.
  • a solid receiving device is position below the lithium- extraction device, such that said device contains the discharged material, and such that said discharged material can be subsequently conveyed away.
  • said solids receiving device is a tray, a hopper, a fork liftable hopper.
  • said discharged material are received by a drip tray, which is fitted with a motor to open downwards, thereby allowing said solids to be discharged to a second system.
  • a conveyor belt is positioned below the filter press, such that the solids can be WSGR Docket No.50741-726.601 automatically removed and conveyed away after discharge.
  • the filter press is positioned above a tank, such that the solids can fall directly into said tank after discharge.
  • the filter press is positioned above an agitated tank.
  • the filter press is positioned above a tank containing a liquid resource comprising lithium, such that the discharged lithium-selective sorbent absorbs lithium when discharged from the device into the tank. In some embodiments, the filter press is positioned above a tank containing an acidic eluent, such that the discharged lithium-selective sorbent releases lithium when discharged from the device into the tank. In some embodiments, the filter press is positioned above a tank containing a wash solution, such that the discharged lithium-selective sorbent is washed when discharged from the device.
  • the solid sorbent is discharged from the device about once per year, about once per month, about once per week, about once per day, about twice per day, about three times per day, about one time per hour, about twice per hour, or about five times per hour.
  • the lithium-selective sorbent is discharged in coordination with the lithium extraction process.
  • the lithium-selective sorbent is discharged after it has contacted a liquid resource containing lithium.
  • the lithium-selective sorbent is discharged after it is saturated with lithium, having contacted a liquid resource containing lithium.
  • the lithium-selective sorbent is discharged after a certain amount of contact time with a lithium containing liquid resource. In some embodiments, the lithium-selective sorbent is discharged after it has contacted a wash solution. In some embodiments, the lithium-selective sorbent is discharged after it has contacted an aqueous solution. In some embodiments, said aqueous solution releases the lithium contained in said lithium selective sorbent. In some embodiments, the lithium-selective sorbent is discharged after it has contacted an acidic eluent solution, such that lithium from said sorbent has been released. [0283] In some embodiments, the filter press is filled with a lithium selective sorbent.
  • the volume of sorbent that is contained within said device is less than about 1 mL, less than about 10 mL, less than about 100 mL, less than about 1 L, less than about 10 L, less than about 100 L, less than about 1 cubic meter, less than about 10 cubic meters, less than about 100 cubic meters, less than about 1,000 cubic meters, or less than about 10,000 cubic meters.
  • the volume of sorbent that is contained within said device is at most about 1 mL, at most about 10 mL, at most about 100 mL, at most about 1 L, at most about 10 L, at most about 100 L, at most about 1 cubic meter, at most about 10 cubic meters, at most about 100 cubic meters, at most about 1,000 cubic meters, or at most about WSGR Docket No.50741-726.601 10,000 cubic meters.
  • the volume of sorbent that is contained within said device is more than about 1 mL, more than about 10 mL, more than about 100 mL, more than about 1 L, more than about 10 L, more than about 100 L, more than about 1 cubic meter, more than about 10 cubic meters, more than about 100 cubic meters, more than about 1,000 cubic meters, or more than about 10,000 cubic meters.
  • the volume of sorbent that is contained within said device is from about 0.1 mL to about 1 mL, from about 1 mL to about 10 mL, from about 10 mL to about 100 mL, from about 100 mL to about 1 L, from about 1 L to about 10 L, from about 10 L to about 100 L, from about 100 L to about 1 cubic meter, from about 1 cubic meter to about 10 cubic meters, from about 10 cubic meters to about 100 cubic meters, from about 100 cubic meters to about 1,000 cubic meters, or from about 1,000 cubic meters to about 10,000 cubic meters.
  • the amount of lithium-selective sorbent that can be contained said device can be adjusted by positioning a “back up plate” device.
  • said “back up plate” device comprises a plate that is connected to the rest of the piping in the lithium extraction device on only one side, and is not connected to the pipe that conveys the lithium selective sorbent into the device.
  • the effect of this “back up plate” is to not allow any solids of fluid flow to filters located beyond the back up late.
  • said backup plate splits the filter press into two sections.
  • a backup plate when said filter press has process connections from both sides, can be positions such that two sides of the same press can be used for independent fluid flows. In some embodiments, this allows two sections of the filter press to be configured to be in different stages of the ion-exchange process simultaneously. In some embodiments, this allows for lower down-time and higher lithium productivity of the ion exchange device.
  • one or more dividing plates are positioned within the device, wherein said dividing plate is constructed such that fluid that exits from one section of the filter press is sent to the inlet of a subsequent section of the filter press. In some embodiments, one such plate is present in the filter press. In some embodiments, two or more sch plates are present in the filter press.
  • An aspect of the disclosure herein is a device for lithium extraction from a liquid resource, wherein said device comprises one or more filter banks containing a lithium-selective sorbent.
  • said lithium extraction comprises a vertical pressure filter.
  • said vertical pressure filter comprises multiple filter banks, or filter plates, which are mechanically held together to form a vertical stack.
  • a vertical pressure filter is a filtration device known in the field of filtration and solids-liquid separation.
  • a vertical pressure filter to extract lithium, wherein said vertical pressure filter is filled with a lithium-selective sorbent, and said sorbent is contacted with a liquid resource comprising lithium in said filter press.
  • said sorbent is an ion-exchange material.
  • a vertical pressure filter comprises multiple filter plates or filter trays, wherein each filter plate or filter trays comprises a filter bank.
  • each filter bank comprises a compartment containing a lithium-selective sorbent, wherein said compartment is contained within porous partitions.
  • said compartment contains a bed or cake of said sorbent.
  • said filter bank contains pipes, shapes, tubes, hoses and flow paths that connect said sorbent-containing compartment to a fluid distribution manifold that the delivers flow to and form said sorbent.
  • a porous partitions are located at the bottom of the filter bank. In some embodiments, more than two such partitions are located within a filter bank. In some embodiments, said porous partition is a mesh, cloth, other woven material, a screen, or a combination thereof. In some embodiments, said porous partition is attached a mechanical device, plate, flow distributor, or scaffolding.
  • the ion exchange material is loaded in a column.
  • the pH modulating setup is connected to the column loaded with the ion exchange material.
  • the pH modulating setup comprises one or more tanks.
  • the ion exchange material is loaded in a vessel.
  • the pH modulating setup is in fluid communication with the vessel loaded with the ion exchange material.
  • the pH WSGR Docket No.50741-726.601 modulating setup is in fluid communication with the column loaded with the ion exchange material.
  • one or more ion exchange columns are loaded with a fixed or fluidized bed of ion exchange beads.
  • the ion exchange column is a cylindrical construct with entry and exit ports.
  • the ion exchange column is optionally a non-cylindrical construct with entry and exit ports.
  • the system is a recirculating batch system, which comprises an ion exchange column that is connected to one or more tanks for mixing base into the brine, settling out any precipitates following base addition, and storing the brine prior to reinjection into the ion exchange column or the other tanks.
  • the brine is loaded into one or more tanks, pumped through the ion exchange column, pumped through a series of tanks, and then returned to the ion exchange column in a loop.
  • the brine optionally traverses this loop repeatedly.
  • the brine is recirculated through the ion exchange column to enable optimal lithium uptake by the beads.
  • base is added to the brine in such a way that pH is maintained at an adequate level for lithium uptake and in such a way that the amount of base-related precipitates in the ion exchange column is minimized.
  • the brine pH drops in the ion exchange column due to hydrogen release from the ion exchange beads during lithium uptake, and the brine pH is adjusted upward by the addition of base as a solid, aqueous solution, or other form.
  • the ion exchange system drives the ion exchange reaction to near completion, and the pH of the brine leaving the ion exchange column approaches the pH of the brine entering the ion exchange column.
  • the amount of base added is optionally controlled to neutralize the hydrogen released by the ion exchange beads in such a way that no basic precipitates form.
  • an excess of base or a transient excess of base is optionally added in such a way that basic precipitates form.
  • the basic precipitates form transiently and then are redissolved partially or fully by the hydrogen that is released from the ion exchange column.
  • base is optionally added to the brine flow prior to the ion exchange column, after the ion exchange column, prior to one or more tanks, or after one or more tanks.
  • the tanks include a mixing tank where the base is mixed with the brine.
  • the tanks include a settling tank, where precipitates such as Mg(OH)2 optionally settle to the bottom of the settling tank to WSGR Docket No.50741-726.601 avoid injection of the precipitates into the ion exchange column.
  • the tanks include a storage tank where the brine is stored prior to reinjection into the ion exchange column, mixing tank, settling tank, or other tanks.
  • the tanks include an acid recirculation tank.
  • some tanks in the recirculating batch reactor optionally serve a combination of purposes including base mixing tank, settling tank, acid recirculation tank, or storage tank.
  • a tank optionally does not fulfil two functions at the same time.
  • a tank is not a base mixing tank and a settling tank.
  • base is added to a mixing tank, which is optionally a continuous stirred tank system, a confluence of acidified brine flow and base flow followed by a static mixer, a confluence of acidified brine flow and base flow followed by a paddle mixer, a confluence of acidified brine flow and base flow followed by a turbine impeller mixer, or a continuous stirred tank system in the shape of a vertical column which is well mixed at the bottom and settled near the top.
  • the base is optionally added as a solid or as an aqueous solution.
  • the base is optionally added continuously at a constant or variable rate.
  • the base is optionally added discretely in constant or variable aliquots or batches. In one embodiment, the base is optionally added according to one or more pH meters, which optionally samples brine downstream of the ion exchange column or elsewhere in the recirculating batch system. In one embodiment, filters are optionally used to prevent precipitates from leaving the mixing tank. In one embodiment, the filters are optionally plastic mesh screens, small packed columns containing granular media such as sand, silica, or alumina, small packed columns containing porous media filter, or a membrane.
  • the settling tank is optionally a settling tank with influent at bottom and effluent at top or a settling tank with influent on one end and effluent on another end.
  • chambered weirs are used to fully settle precipitates before brine is recirculated into reactor.
  • solid base precipitates are collected at the bottom of the settling tank and recirculated into the mixer.
  • precipitates such as Mg(OH)2 optionally settle near the bottom of the tank.
  • brine is removed from the top of the settling tank, where the amount of suspended precipitates is minimal.
  • the precipitates optionally settle under forces such as gravity, centrifugal action, or other forces.
  • filters are optionally used to prevent precipitates from leaving the settling tank.
  • the filters are optionally plastic mesh screens, small packed columns containing granular media such as sand, silica, or alumina, small packed columns containing porous media filter, or a WSGR Docket No.50741-726.601 membrane.
  • baffles are optionally used to ensure settling of the precipitate and to prevent the precipitate from exiting the settling tank and entering the column.
  • ion exchange columns are optionally connected to one or more tanks or set of tanks. In one embodiment of the recirculating batch system, there are optionally multiple ion exchange columns recirculating brine through a shared set of mixing, settling, and storage tanks. In one embodiment of the recirculating batch system, there is optionally one ion exchange column recirculating brine through multiple sets of mixing, settling, and storage tanks.
  • the pH modulating setup comprises a plurality of tanks connected to the plurality of columns, wherein each of the plurality of tanks is immediately connected to one of the plurality of columns.
  • two or more of the plurality of tanks connected to the plurality of columns forms at least one circuit.
  • three or more of the plurality of tanks connected to the plurality of columns forms at least two circuits.
  • three or more of the plurality of tanks connected to the plurality of columns forms at least three circuits.
  • at least one circuit is a liquid resource circuit.
  • At least one circuit is a water washing circuit. In an embodiment, at least one circuit is an acid solution circuit. In an embodiment, at least two circuits are water washing circuits.
  • the system is a column interchange system where a series of ion exchange columns are connected to form a brine circuit, an acid circuit, a water washing circuit, and optionally other circuits.
  • brine flows through a first column in the brine circuit, then into a next column in the brine circuit, and so on, such that lithium is removed from the brine as the brine flows through one or more columns.
  • base is added to the brine before or after each ion exchange column or certain ion exchange columns in the brine circuit to maintain the pH of the brine in a suitable range for lithium uptake by the ion exchange beads.
  • acid flows through a first column in the acid circuit, then into the next column in the acid circuit, and so on, such that lithium is eluted from the WSGR Docket No.50741-726.601 columns with acid to produce a lithium concentrate.
  • acid flows through a first column in the acid circuit, then optionally into a next column in the acid circuit, and so on, such that lithium is eluted from the columns with acid to produce a lithium concentrate.
  • water flows through a first column in the water washing circuit, then optionally into a next column in the water washing circuit, and so on, such that brine in the void space, pore space, or head space of the columns in the water washing circuit is washed out.
  • ion exchange columns are interchanged between the brine circuit, the water washing circuit, and the acid circuit.
  • the first column in the brine circuit is loaded with lithium and then interchanged into the water washing circuit to remove brine from the void space, pore space, or head space of the column.
  • the first column in the water washing circuit is washed to remove brine, and then interchanged to the acid circuit, where lithium is eluted with acid to form a lithium concentrate.
  • the first column in the acid circuit is eluted with acid and then interchanged into the brine circuit to absorb lithium from the brine.
  • two water washing circuits are used to wash the columns after both the brine circuit and the acid circuit.
  • only one water washing circuit is used to wash the columns after the brine circuit, whereas excess acid is neutralized with base or washed out of the columns in the brine circuit.
  • each column in the brine circuit contains one or more tanks or junctions for mixing base into the brine and optionally settling any basic precipitates that form following base addition.
  • each column in the brine circuit has associated one or more tanks or junctions for removing basic precipitates or other particles via settling or filtration.
  • each column or various clusters of columns have associated one or more settling tanks or filters that remove particles including particles that detach from ion exchange beads.
  • WSGR Docket No.50741-726.601 [0303]
  • the number of the columns in the brine circuit is optionally less than about 3, less than about 10, less than about 30, or less than about 100.
  • the number of the columns in the acid circuit is optionally less than about 3, less than about 10, less than about 30, or less than about 100.
  • the number of the columns in the water washing circuit is optionally less than about 3, less than about 10, less than about 30, or less than about 100.
  • the number of the columns in the brine circuit is optionally at most about 3, at most about 10, at most about 30, or at most about 100. In one embodiment of the column interchange system, the number of the columns in the acid circuit is optionally at most about 3, at most about 10, at most about 30, or at most about 100. In one embodiment of the column interchange system, the number of the columns in the water washing circuit is optionally at most about 3, at most about 10, at most about 30, or at most about 100. In certain embodiments, the number of columns in the brine circuit is 1 to 10. In some embodiments, the number of columns in the acid circuit is 1 to 10. In some embodiments, the number of columns in washing circuit is 1 to 10.
  • ion exchange columns are optionally supplied with fresh ion exchange beads without interruption to operating columns.
  • ion exchange columns with beads that have been depleted in capacity is optionally replaced with ion exchange columns with fresh ion exchange beads without interruption to operating columns.
  • the columns contain fluidized beds of ion exchange material.
  • the columns have means of created a fluidized bed of ion exchange material such as overhead stirrers or pumps.
  • the columns contain fluidized beds of ion exchange material.
  • the system is an interchange system and the vessels are stirred tank reactors.
  • base is added directly to the columns or other tanks containing the ion exchange material.
  • base is added to the brine or another solution in a separate mixing tank and then added to the columns or other tanks containing the ion exchange material.
  • WSGR Docket No.50741-726.601 [0306]
  • ion exchange beads are loaded into ion exchange columns and following lithium uptake from brine, lithium is eluted from the ion exchange columns using an acid recirculation loop.
  • acid is flowed through an ion exchange column, into a tank, and then recirculated through the ion exchange column to optimize lithium elution.
  • ion exchange beads are loaded into ion exchange columns and following lithium uptake from brine, lithium is eluted from each ion exchange column using a once-through flow of acid.
  • ion exchange beads are loaded into an ion exchange column and following lithium uptake from brine, lithium is eluted from the ion exchange column using a column interchange circuit.
  • ion exchange columns are loaded with lithium by flowing brine through the columns using a recirculating batch system and then lithium is eluted from the columns using a column interchange system.
  • ion exchange columns are loaded with lithium by flowing brine through the columns using a column interchange system and then lithium is eluted from the columns using a recirculating batch system.
  • ion exchange columns are loaded with lithium by flowing brine through the columns using a recirculating batch system and then lithium is eluted from the columns using a recirculating batch system.
  • ion exchange columns are loaded with lithium by flowing brine through the columns using a column interchange system and then lithium is eluted from the columns using a column interchange system.
  • Stirred Tank system [0308]
  • the pH modulating setup is a tank comprising: a) one or more compartments; and b) a means for moving the liquid resource through the one or more compartments.
  • the ion exchange material is loaded in at least one compartment.
  • the means for moving the liquid resource through the one or more compartments is a pipe.
  • the means for moving the liquid resource through the one or more compartments is a pipe and suitably a configured pump.
  • the tank further comprises a means for circulating the liquid resource throughout the tank.
  • the means for circulating the liquid resource throughout the tank is a mixing device.
  • the tank further comprises an injection port.
  • WSGR Docket No.50741-726.601 [0309]
  • the tank further comprises one or more injection ports.
  • the tank further comprises a plurality of injection ports.
  • An aspect described herein is a system for the extraction of lithium ions from a liquid resource, comprising a tank, wherein the tank further comprises: a) one or more compartments; b) an ion exchange material; c) a mixing device; and d) a pH modulating setup for changing the pH of the system, wherein the ion exchange material is used to extract lithium ions from the liquid resource.
  • the pH modulating setup changes the pH of the liquid resource in the system.
  • the ion exchange material is loaded in at least one of the one or more compartments. In some embodiments, the ion exchange material is fluidized in at least one of the one or more compartments.
  • the ion exchange material is non- fluidized in at least one of the one or more compartments. In some embodiments, the ion exchange material occupies a fixed position in at least one of the one or more compartments.
  • the pH modulating setup comprises a pH measuring device and an inlet for adding base. In some embodiments, the pH measuring device is a pH probe. In some embodiments, the inlet is a pipe. In some embodiments, the inlet is an injection port. [0313] In one embodiment of the ion exchange system, a plurality of stirred tank reactors are used to mix ion exchange material with a liquid resource, washing fluid, and acid solution.
  • the stirred tank reactors are different sizes and contain different volumes of a liquid resource, washing fluid, and acid solution.
  • the stirred tanks are cylindrical, conical, rectangular, pyramidal, or a combination thereof.
  • the ion exchange material moves through the plurality of stirred tank reactors in the opposite direction of the liquid resource, the washing fluid, or the acid solution.
  • a plurality of stirred tank reactors are used where one or more stirred tank reactors mix the ion exchange material with a liquid resource, one or more stirred tank reactors mix the ion exchange material with a washing fluid, and one or more stirred tank reactors mix the ion exchange material with an acid solution.
  • stirred tank reactors are operated in a continuous, semi-continuous, or batch mode where a liquid resource flows continuously, semi-continuously, or batch-wise through the stirred tank reactor.
  • stirred tank reactors are operated in a continuous, semi-continuous, or batch mode where the ion exchange material flows continuously, semi-continuously, or batch- wise through the stirred tank reactor.
  • stirred tank reactors are operated in a mode where the ion exchange material remains in the tank while WSGR Docket No.50741-726.601 flows of liquid resource, washing fluid, or acid solution are flowed through the tank in continuous, semi-continuous, or batch flows.
  • ion exchange material is loaded into or removed from the stirred tank reactors through the top, the bottom, or the side of the tank.
  • stirred tank reactors are arranged into a network where flows of brine, washing fluid, and acid solutions are directly through different columns.
  • a network of stirred tank reactors may involve physical movement of the ion exchange material through the various stirred tank reactors. In one embodiment, a network of stirred tank reactors may involve no physical movement of the ion exchange material through the various stirred tank reactors. In one embodiment, a network of stirred tank reactors may involve switching of flows of brine, washing fluid, and acid solutions through the various stirred tank reactors. In one embodiment, brine may into stirred tank reactors in continuous or batch mode. In one embodiment, brine is mixed with ion exchange material in one or more reactors before exiting the system. In one embodiment, a network of stirred tank reactors may involve a brine circuit with counter-current exposure of ion exchange material to flows of brine.
  • a network of stirred tank reactors may involve a washing circuit with counter-current exposure of ion exchange material to flows of washing fluid.
  • a network of stirred tank reactors may involve an acid circuit with counter-current exposure of ion exchange material to flows of acid solution.
  • the washing fluid is water, an aqueous solution, or a solution containing an anti- scalant.
  • An aspect described herein is a system for the extraction of lithium ions from a liquid resource, comprising: a) a plurality of columns, wherein each of the plurality of columns comprises an ion exchange material; and b) a pH modulating setup for changing the pH of the liquid resource in the system, wherein the pH modulating setup is in fluid communication with each of the plurality of columns, wherein the ion exchange material is used to extract lithium ions from the liquid resource.
  • the pH modulating setup comprises a plurality of tanks, wherein each of the plurality of tanks is immediately connected to one of the plurality of columns. In one embodiment, the pH modulating setup comprises a plurality of tanks, wherein each of the plurality of tanks is in immediate liquid communication with one of the plurality of columns. In some embodiments, two or more of the plurality of tanks connected to two or more of the plurality of columns forms at least one circuit. In some embodiments, two or more of the plurality of tanks connected to two or more of the plurality of columns forms at least two circuits.
  • the pH modulating setup comprises a plurality of tanks, wherein each of the plurality of tanks is connected to the of the plurality of columns through a filtration system. In some embodiments, two or more of the plurality of tanks are connected to two or more of the plurality of columns through a filter system to form at least one circuit. In some embodiments, two or more of the plurality of tanks are connected to two or more of the plurality of columns through a filter system to form at least two circuits.
  • the filtration system comprises a bag filter, a candle filter, a cartridge filter, a media filter, a depth filter, a sand filter, a membrane filter, an ultrafiltration system, a microfiltration filter, a nanofiltration filter, a cross-flow filter, a dead-end filter, a drum filter, a filter press, or a combination thereof.
  • the openings in this filter are of less than about 0.02 ⁇ m, less than about 0.1 ⁇ m, less than about 0.2 ⁇ m, less than about 1 ⁇ m, less than about 2 ⁇ m, less than about 5 ⁇ m, less than about 10 ⁇ m, less than about 25 ⁇ m, less than about 100 ⁇ m, less than about 1000 ⁇ m. In some embodiments, the openings in this filter are of at most about 0.02 ⁇ m, at most about 0.1 ⁇ m, at most about 0.2 ⁇ m, at most about 1 ⁇ m, at most about 2 ⁇ m, at most about 5 ⁇ m, at most about 10 ⁇ m, at most about 25 ⁇ m, at most about 100 ⁇ m, at most about 1000 ⁇ m.
  • the perforated openings in outer-perforated walls are of dimension of more than about 0.02 ⁇ m, more than about 0.1 ⁇ m, more than about 0.2 ⁇ m, more than about 1 ⁇ m, more than about 2 ⁇ m, more than about 5 ⁇ m, more than about 10 ⁇ m, more than about 25 ⁇ m, more than about 100 ⁇ m.
  • the perforated openings in outer-perforated walls are of dimension of about 0.02 ⁇ m to about 0.1 ⁇ m, from about 0.1 ⁇ m to about 0.2 ⁇ m, from about 0.2 ⁇ m to about 0.5 ⁇ m, from about 0.5 ⁇ m to about 1 ⁇ m, from about 1 ⁇ m to about 5 ⁇ m, from about 5 ⁇ m to about 10 ⁇ m, from about 10 ⁇ m to about 25 ⁇ m, from about 25 ⁇ m to about 100 ⁇ m.
  • the filter martial comprises low density polyethylene, high density polyethylene, polypropylene, polyester, polytetrafluoroethylene (PTFE), types of polyamide, polyether ether ketone (PEEK), polysulfone, polyvinylidene fluoride (PVDF), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), polybutadiene, acrylonitrile butadiene styrene (ABS), polyvinyl chloride (PVC), ethylene tetrafluoroethylene polymer (ETFE), poly(chlorotrifluoroethylene) (PCTFE), ethylene chlorotrifluoro ethylene (Halar), polyvinylfluoride (PVF), fluorinated ethylene-propylene (FEP), perfluorinated elastomer, chlorotrifluoroethylenevinylidene fluoride (FKM), perfluoropolyether (PFPE),
  • a coating material comprises polyvinylidene fluoride (PVDF), polyvinyl chloride (PVC), ethylene chlorotrifluoro ethylene (Halar), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), acrylonitrile butadiene styrene (ABS), expanded polystyrene (EPS), polyphenylene sulfide, sulfonated polymer, carboxylated polymer, other polymers, co- polymers thereof, mixtures thereof, or combinations thereof.
  • PVDF polyvinylidene fluoride
  • PVC polyvinyl chloride
  • Halar ethylene chlorotrifluoro ethylene
  • PVPCS poly (4-vinyl pyridine-co-styrene)
  • PS polystyrene
  • ABS acrylonitrile butadiene styrene
  • EPS expanded polystyrene
  • the filter martial comprises iron, stainless steel, nickel, carbon steel, titanium, Hastelloy, Inconel, zirconium, tantalum, alloys thereof, mixtures thereof, or combinations thereof.
  • at least one circuit is a liquid resource circuit.
  • at least one circuit is a water washing circuit.
  • at least two circuits are water washing circuits.
  • at least one circuit is an acid solution circuit.
  • An aspect described herein is a system for the extraction of lithium ions from a liquid resource comprising an ion exchange material and a plurality of vessels, wherein each of the plurality of vessels is configured to transport the ion exchange material along the length of the vessel and the ion exchange material is used to extract lithium ions from the liquid resource.
  • at least one of the plurality of vessels comprises an acidic solution.
  • at least one of the plurality of vessels comprises the liquid WSGR Docket No.50741-726.601 resource.
  • each of the plurality of vessels is configured to transport the ion exchange material by a pipe system or an internal conveyer system.
  • An aspect described herein is a system for the extraction of lithium ions from a liquid resource comprising an ion exchange material and a plurality of columns, wherein each of the plurality of columns is configured to transport the ion exchange material along the length of the column and the ion exchange material is used to extract lithium ions from the liquid resource.
  • at least one of the plurality of columns comprises an acidic solution.
  • at least one of the plurality of columns comprises the liquid resource.
  • each of the plurality of columns is configured to transport the ion exchange material by a pipe system or an internal conveyer system.
  • an aspect of the disclosure provided herein is a system, wherein the column further comprises a plurality of injection ports, wherein the plurality of injection ports are used to increase the pH of the liquid resource in the system
  • the system is a mixed base system comprising an ion exchange column and a mixing chamber where base is mixed into the brine immediately prior to injection of the brine into the column.
  • the system is a ported ion exchange column system with multiple ports for injection of aqueous base spaced at intervals along the direction of brine flow through the column.
  • the system has a moving bed of beads that moves in a direction opposite to the flow of brine and base is injected at one or more fixed points in the column in a region near where the ion exchange reaction occurs at a maximum rate in the column to neutralize the protons released from the ion exchange reaction.
  • the base added to the brine is optionally NaOH, KOH, Mg(OH)2, Ca(OH)2, CaO, NH3, Na2SO4, K2SO4, NaHSO4, KHSO4, NaOCl, KOCl, NaClO4, KClO4, NaH2BO4, Na2HBO4, Na3BO4, KH2BO4, K2HBO4, K3BO4, MgHBO4, CaHBO4, NaHCO3, KHCO3, NaCO3, KCO3, MgCO3, CaCO3, Na2O, K2O, Na2CO3, K2CO3, WSGR Docket No.50741-726.601 Na3PO4, Na2HPO4, NaH2PO4, K3PO4, K2HPO4, KH2PO4, CaHPO4, MgHPO4, sodium acetate, potassium acetate, magnesium acetate, poly(vinylpyridine), poly(vinylamine), polyacrylonitrile, other bases, or combinations thereof.
  • the base is optionally added to the brine in its pure form or as an aqueous solution. In one embodiment, the base is optionally added in a gaseous state such as gaseous NH3. In one embodiment, the base is optionally added to the brine in a steady stream, a variable stream, in steady aliquots, or in variable aliquots. In one embodiment, the base is optionally created in the brine by using an electrochemical cell to remove H2 and Cl2 gas, which is optionally combined in a separate system to create HCl acid to be used for eluting lithium from the system or for other purposes. [0331] In some embodiments, a solid base is mixed with a liquid resource to create a basic solution.
  • a solid base is mixed with a liquid resource to create a basic solution, and the resulting basic solution is added to a second volume of a liquid resource to increase the pH of the second volume of the liquid resource.
  • solid base is mixed with a liquid resource to create a basic solution, wherein the resulting basic solution is used to adjust or control the pH of a second solution.
  • a solid base is mixed with a liquid resource to create a basic slurry.
  • a solid base is mixed with a liquid resource to create a basic slurry, and the resulting basic slurry is added to a second volume of a liquid resource to increase the pH of the second volume of the liquid resource.
  • solid base is mixed with a liquid resource to create a basic slurry, wherein the resulting basic slurry is used to adjust or control the pH of a second solution.
  • base is added to a liquid resource as a mixture or slurry of base and liquid resource.
  • the brine flows through a pH control column containing immobilized regeneratable OH-containing ion exchange resins which react with hydrogen ions, or regeneratable base species such as immobilized polypyridine, which conjugate HCl, thereby neutralizing the acidified brine.
  • the ion exchange resin When the ion exchange resin has been depleted of its OH groups or is saturated with HCl, it is optionally regenerated with a base such as NaOH.
  • pH meters are optionally installed in tanks, pipes, column, and other components of the system to monitor pH and control the rates and amounts of base addition at various locations throughout the system.
  • the columns, tanks, pipes, and other components of the system are optionally constructed using plastic, metal with a plastic lining, or other materials that are resistant to corrosion by brine or acid.
  • the ion exchange columns are optionally washed with water that is mildly acidic, optionally including a buffer, to remove any basic precipitates from the column prior to acid elution.
  • the lithium is flushed out of the ion exchange column using acid.
  • the acid is optionally flowed through the column one or more times to elute the lithium.
  • the acid is optionally flowed through the ion exchange column using a recirculating batch system comprised of the ion exchange column connected to a tank.
  • the tank used for acid flows is optionally the same tank used for the brine flows.
  • the tank used for acid flows is optionally a different tank than the one used for brine flows.
  • the acid is distributed at the top of the ion exchange column and allowed to percolate through and immediately recirculated into the column with no extra tank.
  • acid addition optionally occurs without a tank used for acid flows.
  • the column is optionally washed with water after the brine and/or acid steps, and the effluent water from washing is optionally treated using pH neutralization and reverse osmosis to yield process water.
  • the ion exchange column is optionally shaped like a cylinder, a rectangle, or another shape.
  • the ion exchange column optionally has a cylinder shape with a height that is greater or less than its diameter.
  • the ion exchange column optionally has a cylinder shape with a height that is less than 10 cm, less than 1 meter, or less than 10 meters.
  • the ion exchange column optionally has a cylinder shape with a diameter that is less than 10 cm, less than 1 meter, or less than 10 meters. In one embodiment, the ion exchange column optionally has a cylinder shape with a height that is greater or at most its diameter. In one embodiment, the ion exchange column optionally has a cylinder shape with a height that is at most 10 cm, at most 1 meter, or at most 10 meters. In one embodiment, the ion exchange column optionally has a cylinder shape with a diameter that is at most 10 cm, at most 1 meter, or at most 10 meters.
  • the system is optionally resupplied with fresh ion exchange beads by swapping out an ion exchange column with a new column loaded with fresh ion exchange beads.
  • the WSGR Docket No.50741-726.601 system is optionally resupplied with fresh ion exchange beads by removing the beads from the column and loading new beads into the column.
  • new beads are optionally supplied to all columns in the system simultaneously.
  • new beads are optionally supplied to one or more columns at a time.
  • new beads are optionally supplied to one or more columns without interruption to other columns that optionally continue operating.
  • brine pumping optionally continues until the ion exchange beads approach a point of lithium saturation over a period of time that is optionally less than about 1 hours, less than about 2 hours, less than about 4 hours, less than about 8 hours, less than about 24 hours, less than about 48 hours, or less than about one week.
  • brine pumping optionally continues until the ion exchange beads approach a point of lithium saturation over a period of time that is optionally greater than about one week.
  • brine pumping optionally continues until the ion exchange beads approach a point of lithium saturation over a period of time that is optionally at most about 1 hours, at most about 2 hours, at most about 4 hours, at most about 8 hours, at most about 24 hours, at most about 48 hours, or at most about one week.
  • brine pumping optionally continues until the ion exchange beads approach a point of lithium saturation over a period of time that is optionally at least about one week.
  • brine pumping optionally continues until the ion exchange beads approach a point of lithium saturation over a period of time that is optionally between 30 minutes and 24 hours.
  • acid pumping optionally continues until the ion exchange beads approach a point of hydrogen saturation over a period of time that is optionally less than about 1 hours, less than about 2 hours, less than about 4 hours, less than about 8 hours, less than about 24 hours, or less than about 48 hours.
  • brine pumping optionally continues until the ion exchange beads approach a point of hydrogen saturation over a period of time that is optionally greater than about one 48 hours.
  • acid pumping optionally continues until the ion exchange beads approach a point of hydrogen saturation over a period of time that is optionally at most about 1 hours, at most about 2 hours, at most about 4 hours, at most about 8 hours, at most about 24 hours, or at most about 48 hours.
  • brine pumping optionally continues until the ion exchange beads approach a point of hydrogen saturation over a period of time that is optionally at least about WSGR Docket No.50741-726.601 48 hours.
  • brine pumping optionally continues until the ion exchange beads approach a point of hydrogen saturation over a period of time that is optionally between 30 minutes and 24 hours.
  • ion exchange vessels are designed to facilitate flow across the ion exchange beads with a shorter fluid flow distance.
  • the vessel can be oriented vertically, horizontally, or at any angle relative to the horizontal axis.
  • the vessel can be cylindrical, rectangular, spherical, another shape, or a combinations thereof.
  • the vessel can have a constant cross-sectional area or a varying cross-sectional area.
  • the typical thickness of the distribution compartment within the vessel containing the ion-exchange compartments is less than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the typical thickness of the distribution compartment within the vessel containing the ion-exchange compartments is more than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the typical thickness of the distribution compartment within the vessel containing the ion-exchange compartments is at most about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the distribution compartment within the vessel containing the ion-exchange compartments is more than about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at WSGR Docket No.50741-726.601 most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the distribution compartment within the vessel containing the ion-exchange compartments is from about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 8 cm, from about 8 cm to about 20 cm, from about 20 cm to about 40 cm, from about 40 cm to about 80 cm, from about 80 cm to about 120 cm, from about 120 cm to about 2 m, from about 2 m to about 4 m.
  • the typical thickness of the compartment containing ion- exchange beads within the vessel containing the ion-exchange compartments is less than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the typical thickness of the compartment containing ion-exchange beads within the vessel containing the ion-exchange compartments is more than about 1 cm, less than about 2 cm, less than about 4 cm, less than about 6 cm, less than about 8 cm, less than about 10 cm, less than about 20 cm, less than about 40 cm, less than about 60 cm, less than about 80 cm, less than about 1 m, less than about 2 m, less than about 4 m.
  • the typical thickness of the compartment containing ion-exchange beads within the vessel containing the ion-exchange compartments is at most about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the compartment containing ion-exchange beads within the vessel containing the ion-exchange compartments is more than about 1 cm, at most about 2 cm, at most about 4 cm, at most about 6 cm, at most about 8 cm, at most about 10 cm, at most about 20 cm, at most about 40 cm, at most about 60 cm, at most about 80 cm, at most about 1 m, at most about 2 m, at most about 4 m.
  • the typical thickness of the compartment containing ion-exchange beads within the vessel containing the ion-exchange compartments is from about 1 cm to about 2 cm, from about 2 cm to about 4 cm, from about 4 cm to about 8 cm, from about 8 cm to about 20 cm, from about 20 cm to about 40 cm, from about 40 cm to about 80 cm, from about 80 cm to about 120 cm, from about 120 cm to about 2 m, from about 2 m to about 4 m.
  • an alternate phase is contacted with the ion exchange material within an ion exchange device. In some embodiments, contact between the ion exchange beads and the alternate phase is maximized and made possible by the design of this ion exchange device.
  • the alternate phase improves lithium extraction performance by reducing the time required to absorb hydrogen to generate hydrogen-enriched beads and release lithium to generate a lithium-enriched solution; reducing the time and water required for washing the hydrogen-enriched beads with water to generate hydrogen-enriched beads substantially free of residual acid; reducing the time required for treating the hydrogen- enriched beads with the liquid resource under conditions suitable to absorb lithium to generate lithium-enriched beads; reducing the time and water required for washing the lithium-enriched beads with water to generate lithium-enriched beads substantially free of liquid resource; improving the life-time and total lithium produce by the ion exchange material; improving the speed of pH adjustment using alkali; improving the solid-liquid mixing efficiency; and reducing the time required to drain liquids from the ion exchange vessel.
  • the alternate phase is a liquid or gas. In some embodiments, said alternate phase is a non-aqueous liquid. In some embodiments, the alternate phase is non- aqueous liquid. In some embodiments, the alternate phase is a non-aqueous solution. In some embodiments, the alternate phase is an organic liquid such as an alkane, alcohol, oil, bio- organic oil, ester, ether, hydrocarbon, or a combination thereof. In some embodiments, the alternate phase is butane, pentane, hexane, acetone, diethyl ether, butanol, or combinations thereof. In some embodiments, the alternate is a gas such as air, nitrogen, argon, or a combination thereof.
  • the alternate phase comprises a compressed or pressurized gas.
  • the ion exchange bed is a fixed bed that does move during the ion exchange process.
  • the ion exchange bed is a fluidized bed that is agitated at one or more periods during the ion exchange process.
  • Methods of modulating pH for the extraction of lithium [0349] An aspect of the disclosure provided herein is a method of extracting lithium ions from a liquid resource, comprising: flowing the liquid resource through the column of the system described above to produce a lithiated ion exchange material; and treating the resulting lithiated ion exchange material with an acid solution to produce a salt solution comprising lithium ions.
  • An aspect of the disclosure provided herein is a method of extracting lithium ions from a liquid resource, comprising: flowing the liquid resource through the plurality of columns of the system described above to produce a lithiated ion exchange material; and WSGR Docket No.50741-726.601 treating the resulting lithiated ion exchange material with an acid solution to produce a salt solution comprising lithium ions.
  • An aspect of the disclosure provided herein is a method of extracting lithium ions from a liquid resource, comprising: flowing the liquid resource through the tank of the system described above to produce a lithiated ion exchange material; and treating the resulting lithiated ion exchange material with an acid solution to produce a salt solution comprising lithium ions.
  • An aspect of the disclosure provided herein is a method of extracting lithium ions from a liquid resource, comprising: flowing the liquid resource through the column of the system described above to produce a lithiated ion exchange material; and treating the resulting lithiated ion exchange material with an acid solution to produce a salt solution comprising lithium ions.
  • the liquid resource is selected from the following list: a natural brine, a dissolved salt flat, a geothermal brine, seawater, concentrated seawater, desalination effluent, a concentrated brine, a processed brine, liquid from an ion exchange process, liquid from a solvent extraction process, a synthetic brine, leachate from ores, leachate from minerals, leachate from clays, leachate from recycled products, leachate from recycled materials, or combinations thereof.
  • a liquid resource is selected from the following list: a natural brine, a dissolved salt flat, a concentrated brine, a processed brine, a synthetic brine, a geothermal brine, liquid from an ion exchange process, liquid from a solvent extraction process, leachate from minerals, leachate from clays, leachate from recycled products, leachate from recycled materials, or combinations thereof.
  • the liquid resource is optionally pre-treated prior to entering the ion exchange reactor to remove suspended solids, hydrocarbons, or organic molecules.
  • the liquid resource is optionally entered the ion exchange reactor without any pre-treatment following from its source.
  • the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
  • the liquid resource is selected with a lithium concentration selected from the following list: less than 100,000 ppm, less than 10,000 ppm, less than 1,000 WSGR Docket No.50741-726.601 ppm, less than 100 ppm, less than 10 ppm, or combinations thereof.
  • a liquid resource is selected with a lithium concentration selected from the following list: less than 5,000 ppm, less than 500 ppm, less than 50 ppm, or combinations thereof.
  • the liquid resource is selected with a lithium concentration selected from the following list: at most 100,000 ppm, at most 10,000 ppm, at most 1,000 ppm, at most 100 ppm, at most 10 ppm, or combinations thereof.
  • a liquid resource is selected with a lithium concentration selected from the following list: at most 5,000 ppm, at most 500 ppm, at most 50 ppm, or combinations thereof.
  • the acid used for recovering lithium from the ion exchange reactor is selected from the following list: hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, carbonic acid, acetic acid, or combinations thereof.
  • the acid used for recovering lithium from the porous ion exchange beads is selected from the following list: hydrochloric acid, sulfuric acid, nitric acid, carbonic acid, acetic acid, or combinations thereof.
  • the acid solution comprises hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, carbonic acid, acetic acid, or combinations thereof.
  • the acid used for recovering lithium from the ion exchange system has a concentration selected from the following list: less than 0.1 M, less than 1.0 M, less than 5 M, less than 10 M, or combinations thereof. In some embodiments, the acid used for recovering lithium from the porous ion exchange beads has a concentration greater than 10 M.
  • the acid used for recovering lithium from the ion exchange system has a concentration selected from the following list: at most 0.1 M, at most 1.0 M, at most 5 M, at most 10 M, or combinations thereof. In some embodiments, the acid used for recovering lithium from the porous ion exchange beads has a concentration at least 10 M. [0359] In an embodiment, acids with distinct concentrations are used during the elution process. In an embodiment, acid with a lower concentration is first added to elute lithium from the ion exchange material and then additional acid of a greater concentration is added to elute more lithium into the solution and increase the concentration of lithium in the eluate.
  • the ion exchange beads perform the ion exchange reaction repeatedly while maintaining adequate lithium uptake capacity over a number of cycles selected from the following list: greater than 10 cycles, greater than 30 cycles, greater than 100 cycles, greater than 300 cycles, or greater than 1,000 cycles.
  • the porous ion exchange beads perform the ion exchange reaction repeatedly over a number of cycles WSGR Docket No.50741-726.601 selected from the following list: greater than 50 cycles, greater than 100 cycles, or greater than 200 cycles.
  • adequate lithium uptake capacity is optionally defined as a percentage of initial uptake capacity selected from the following list: greater than 95%, greater than 90%, greater than 80%, greater than 60%, or greater than 20%.
  • adequate lithium uptake capacity is optionally defined as a percentage of initial uptake capacity such as less than 20%.
  • the ion exchange beads perform the ion exchange reaction repeatedly while maintaining adequate lithium uptake capacity over a number of cycles selected from the following list: at least 10 cycles, at least 30 cycles, at least 100 cycles, at least 300 cycles, or at least 1,000 cycles.
  • the porous ion exchange beads perform the ion exchange reaction repeatedly over a number of cycles selected from the following list: at least 50 cycles, at least 100 cycles, or at least 200 cycles.
  • adequate lithium uptake capacity is optionally defined as a percentage of initial uptake capacity selected from the following list: at least 95%, at least 90%, at least 80%, at least 60%, or at least 20%.
  • the concentrated lithium solution that is yielded from the ion exchange reactor is further processed into lithium raw materials using methods selected from the following list: solvent extraction, ion exchange, chemical precipitation, electrodialysis, electrowinning, electrolysis, evaporation with direct solar energy, evaporation with concentrated solar energy, evaporation with a heat transfer medium heated by concentrated solar energy, evaporation with heat from a geothermal brine, evaporation with heat from combustion, pH neutralization, or combinations thereof.
  • the concentrated lithium solution that is yielded from the ion exchange reactor is concentrated using reverse osmosis or membrane technologies.
  • the concentrated lithium solution that is yielded from the ion exchange reactor is further processed into lithium chemicals selected from the following list: lithium chloride, lithium carbonate, lithium hydroxide, lithium metal, lithium metal oxide, lithium metal phosphate, lithium sulfide, or combinations thereof.
  • the concentrated lithium solution that is yielded from the porous ion exchange beads is further processed into lithium chemicals that are solid, liquid, hydrated, or anhydrous.
  • the lithium chemicals produced using the ion exchange reactor are used in an industrial application selected from the following list: lithium batteries, metal alloys, glass, grease, or combinations thereof.
  • the lithium chemicals produced using the coated ion exchange particles are used in an application selected WSGR Docket No.50741-726.601 from the following list: lithium batteries, lithium-ion batteries, lithium sulfur batteries, lithium solid-state batteries, and combinations thereof.
  • the ion exchange materials are synthesized in a lithiated state with a sublattice fully or partly occupied by lithium.
  • the ion exchange materials are synthesized in a hydrated state with a sublattice fully or partly occupied by hydrogen.
  • the ion exchange material extracts lithium ions from a liquid resource.
  • the pH of the liquid resource optionally decreases.
  • Increasing the pH of the liquid resource in the system by using a pH modulating setup maintains the pH in a range that is suitable for lithium ion uptake by the ion exchange material.
  • the pH modulating setup comprises measuring the pH of the system and adjusting the pH of the system to an ideal pH range for lithium extraction.
  • an ideal pH range for the brine is optionally 6 to 9
  • a preferred pH range is optionally 4 to 9
  • an acceptable pH range is optionally 2 to 9.
  • the pH modulating setup comprises measuring the pH of the system and wherein the pH of the system is less than 6, less than 4, or less than 2, the pH of the system is adjusted to a pH of 2 to 9, a pH of 4 to 9, or a pH of 6 to 9.
  • the pH modulating setup comprises measuring the pH of the system and wherein the pH of the system is at most 6, at most 4, or at most 2, the pH of the system is adjusted to a pH of 2 to 9, a pH of 4 to 9, or a pH of 6 to 9.
  • Another aspect described herein is a method of extracting lithium ions from a liquid resource, comprising: a) flowing the liquid resource into a system comprising a tank to produce a lithiated ion exchange mateiral, wherein the tank further comprises (i) one or more compartments, (ii) an ion exchange material, (iii) a mixing device, and (iv) a pH modulating setup for changing the pH of the liquid resource in the system; and b) treating the lithiated ion exchange material from a) with an acid solution to produce a hydrogen-rich ion exchange material and a salt solution comprising lithium ions.
  • the method further comprises, prior to b), washing the lithiated ion exchange material with an aqueous solution. In some embodiments, the method further comprises, subsequent to b), washing the hydrogen-rich ion exchange material with an aqueous solution. In some embodiments, the aqueous solution is water. [0368] In some embodiments, the method further comprises, prior to b), flowing the lithiated ion exchange material into a washing system. In some embodiments, the method WSGR Docket No.50741-726.601 further comprises, prior to b), transferring a suspension comprising the lithiated ion exchange material.
  • the method further comprises, prior to b), flowing the lithiated ion exchange material into a washing system and washing the lithiated ion exchange material with a solution. In some embodiments, the method further comprises, prior to b), flowing the lithiated ion exchange material into a washing system and washing the lithiated ion exchange material with a solution comprising water. In some embodiments, the method further comprises, prior to b), flowing the lithiated ion exchange material into a washing system and washing the lithiated ion exchange material with an aqueous solution. In some embodiments, the lithiated ion exchange material is washed with an aqueous solution.
  • the method further comprises, prior to b), flowing the lithiated ion exchange material into a stripping system. In some embodiments, the method further comprises, prior to b), flowing the lithiated ion exchange material into a stripping system and stripping the lithiated ion exchange material. In some embodiments, the method further comprises, prior to b), flowing the lithiated ion exchange material into a stripping system and stripping volatile components from the lithiated ion exchange material. In some embodiments, the method further comprises, prior to b), flowing the lithiated ion exchange material into a stripping system and stripping volatile components comprising water from the lithiated ion exchange material.
  • the pH modulating setup comprises a pH measuring device and an inlet for adding base to the tank.
  • the pH measuring device is a pH probe.
  • the inlet is a pipe.
  • the inlet is an injection port.
  • the method further comprises, during a), measuring a change in pH of the liquid resource using the pH modulating setup.
  • the measured change in pH triggers adding a base to maintain lithium uptake.
  • a change in pH to below a pH value of about 2 to about 9 triggers the addition of a base to maintain lithium uptake.
  • a change in pH to below a pH value of about 2, of about 3, of about 4, of about 5, of about 6, of about 7, of about 8, or of about 9 triggers the addition of a base to maintain lithium uptake.
  • a change in pH to below a pH of about 2 to about 4, of about 3 to about 5, of about 4 to about 6, of about 5 to about 7, of about 6 to about 8, or of about 7 to about 9 triggers the addition of a base to maintain lithium uptake.
  • base is added to the liquid resource to maintain the pH of the liquid resource in a range of about 2-3, 3-4, 4-5, 5-6, 6-7, 7-8, or 8-9.
  • base is added to the liquid resource to maintain the pH of the liquid WSGR Docket No.50741-726.601 resource in a range of about 4-5, 5-6, 6-7, or 7-8.
  • base is added to the liquid resource to maintain the pH of the liquid resource in a range of about 4.0-4.5, 4.5-5.0, 5.0-5.5, 5.5-6.0, 6.0-6.5, 6.5-7.0, 7.0-7.5, or 7.5-8.0.
  • the pH of a liquid resource is maintained in a target range that is high enough to facilitate lithium uptake and low enough to avoid precipitation of metal salts from the liquid resource.
  • the pH of a liquid resource is maintained below a pH of about 8 to avoid precipitation of Mg salts. In some embodiments, the pH of a liquid resource is maintained below a pH of about 2, below a pH of about 3, below a pH of about 4, below a pH of about 5, below a pH of about 6, below a pH of about 7, below a pH of about 8, or below a pH of about 9 to avoid precipitation of metal salts. In some embodiments, the pH of the liquid resource may drop out of a target pH range due to release of protons from an ion exchange material and a pH modulating setup may adjust the pH of the liquid resource back to within a target pH range.
  • the pH of the liquid resource is adjusted above a target pH range prior to the liquid resource entering the system and then protons released from the ion exchange material may decrease the pH of the system into the target range.
  • the pH of the liquid resource is controlled in a certain range and the range is changed over time.
  • the pH of the liquid resource is controlled in a certain range and then the pH of the liquid resource is allowed to drop.
  • the pH of the liquid resource is controlled in a certain range and then the pH of the liquid resource is allowed to drop to solubilize colloids or solids.
  • base is added to a liquid resource to neutralize protons without measuring pH.
  • base is added to a liquid resource to neutralize protons with monitoring of volumes or quantities of the base.
  • the pH of the liquid resource is measured to monitor lithium uptake by an ion exchange material.
  • the pH of the liquid resource is monitored to determine when to separate a liquid resource from an ion exchange material.
  • the rate of change of the pH of the liquid resource is measured to monitor the rate of lithium uptake.
  • the rate of change of the pH of the liquid resource is measured to determine when to separate a liquid resource from an ion exchange material.
  • the tank further comprises a porous partition.
  • the method further comprises, after a), draining the liquid resource through the porous partition after the production of the lithiated ion exchange material (e.g., the lithium- rich ion exchange material). In some embodiments, the method further comprises, after b), draining the salt solution comprising lithium ions through the porous partition after the production of the hydrogen-rich ion exchange material (e.g., the ion exchange material).
  • the lithiated ion exchange material e.g., the lithium- rich ion exchange material
  • the method further comprises, after b), draining the salt solution comprising lithium ions through the porous partition after the production of the hydrogen-rich ion exchange material (e.g., the ion exchange material).
  • the method further comprises, subsequent to a), flowing the lithiated ion exchange material into another system comprising a tank to produce the hydrogen- rich ion exchange material and the salt solution comprising lithium ions, wherein the tank of the other system further comprises (i) one or more compartments, and (ii) a mixing device.
  • the system comprises a plurality of tanks and each of the plurality of tanks further comprises (i) one or more compartments, (ii) an ion exchange material, (iii) a mixing device, and (iv) a pH modulating setup for changing the pH of the system.
  • An aspect described herein is a method of extracting lithium ions from a liquid resource, comprising: a) flowing the liquid resource into a first system comprising a tank, wherein the tank of the first system further comprises (i) one or more compartments, (ii) an ion exchange material, (iii) a mixing device, and (iv) a pH modulating setup for changing the pH of the liquid resource in the first system, to produce a lithiated ion exchange material; b) flowing the lithiated ion exchange material of a) into a second system comprising a tank, wherein the tank of the second system further comprises (i) one or more compartments, and (ii) a mixing device; and c) treating the lithiated ion exchange from b) with an acid solution to produce a hydrogen-rich ion exchange material and a salt solution comprising lithium ions.
  • the method further comprises, subsequent to a), washing the lithiated ion exchange material with an aqueous solution.
  • the method further comprises, prior to b), adding an aqueous solution to the lithiated ion exchange material to form a fluidized lithiated ion exchange material.
  • the method further comprises, subsequent to c), washing the hydrogen-rich ion exchange material with an aqueous solution.
  • the aqueous solution is water.
  • the pH modulating setup comprises a pH measuring device and an inlet for adding base.
  • the pH measuring device is a pH probe.
  • the inlet is a pipe. In some embodiments, the inlet is an injection port. [0380] In some embodiments, the method further comprises, during a), measuring a change in pH of the liquid resource using the pH modulating setup. In some embodiments, the change in pH triggers adding a base to maintain lithium uptake.
  • An aspect described herein is a method of extracting lithium ions from a liquid resource, comprising: a) flowing the liquid resource into a first system comprising a plurality of tanks to produce a lithiated ion exchange material, wherein each of the plurality of tanks in WSGR Docket No.50741-726.601 the first system is in fluid communication with every other one of the plurality of tanks in the first system and, each of the plurality of tanks in the first system further comprises (i) one or more compartments, (ii) an ion exchange material, (iii) a mixing device, and (iv) a pH modulating setup for changing the pH of each of the plurality of tanks in the first system; b) flowing the lithiated ion exchange material into a second system comprising a plurality of tanks, wherein each of the plurality of tanks in the second system is in fluid communication with every other one of the plurality of tanks in the second system and, each of the plurality of tanks in the second system further comprises
  • the method further comprises, subsequent to c), washing the hydrogen-rich ion exchange material with an aqueous solution in at least one of the plurality of tanks in the second system.
  • the method is operated in a batch mode. In some embodiments, the method is operated in a continuous mode. In some embodiments, the method is operated in continuous and batch mode. In some embodiments, the method is operated in continuous mode, a batch mode, a semi-continuous mode, or combinations thereof.
  • the pH modulating setup comprises a pH measuring device and an inlet for adding base. In some embodiments, the pH measuring device is a pH probe. In some embodiments, the inlet is a pipe.
  • the inlet is an injection port.
  • the method further comprises, during a), measuring a change in pH of the liquid resource using the pH modulating setup.
  • the change in pH triggers adding a base to maintain lithium uptake.
  • An aspect described herein is a method of extracting lithium ions from a liquid resource, comprising: a) flowing the liquid resource into a first system comprising a tank to produce a lithiated ion exchange material, wherein the tank further comprises (i) one or more compartments, (ii) ion exchange material, and (iii) a mixing device; b) flowing the lithiated ion exchange material from a) into a second system comprising a tank, wherein the tank further comprises (i) one or more compartments, (ii) an acid solution, and (iii) a mixing device; and c) stripping the lithiated ion exchange material to produce hydrogen-rich ion exchange material and a salt solution comprising lithium ions.
  • An aspect described herein is a method of extracting lithium ions from a liquid resource, comprising: a) providing a system comprising an ion exchange material, a tank comprising one or more compartments; and a mixing device, wherein (i) the ion exchange material is oxide-based and exchanges hydrogen ions with lithium ions, and (ii) the mixing device is capable of moving the liquid resource around the tank comprising one or more compartments; b) flowing the liquid resource into the system of a), thereby contacting the liquid resource with the ion exchange material, wherein the ion exchange material exchanges hydrogen ions with lithium ions in the liquid resource to produce lithiated ion exchange material; c) removing the liquid resource from
  • the salt solution comprising lithium ions undergoes crystallization.
  • a method of extracting lithium ions from a liquid resource comprising: a) flowing the liquid resource through a system comprising an ion exchange material and a plurality of columns, wherein the plurality of columns is configured to transport the ion exchange material along the length of the column, to produce a lithiated ion exchange material; and b) treating the lithiated ion exchange material from a) with an acid solution to produce a salt solution comprising lithium ions.
  • An aspect described herein is a method of extracting lithium ions from a liquid resource, comprising: a) providing a system comprising an ion exchange material and a plurality of columns, wherein each of the plurality of columns is configured to transport the ion exchange material along the length of the column; b) flowing the liquid resource through a first one of the plurality of columns to produce a lithiated ion exchange material; c) flowing the lithiated ion exchange material from b) into a second one of the plurality of columns; and d) treating the lithiated ion exchange material from c) with an acid solution to produce a hydrogen-rich ion exchange material and a salt solution comprising lithium ions.
  • the method further comprises, subsequent to b), flowing the lithiated ion exchange material into another one of the plurality of columns and washing the lithiated ion exchange material with an aqueous solution. In some embodiments, the method further comprises, subsequent to d), flowing the hydrogen-rich ion exchange material into WSGR Docket No.50741-726.601 another one of the plurality of columns and washing the hydrogen-rich ion exchange material with an aqueous solution.
  • An aspect described herein is a method of extracting lithium ion from a liquid resource, comprising: a) providing a system comprising an ion exchange material and a plurality of columns, wherein each of the plurality of columns is configured to transport the ion exchange material along the length of the column; b) flowing the liquid resource through a first one of the plurality of columns to produce a lithiated ion exchange material; c) flowing the lithiated ion exchange material from b) into a second one of the plurality of columns; d) washing the lithiated ion exchange material from c) with an aqueous solution; e) flowing the lithiated ion exchange material from d) into a third one of the plurality of columns; and f) treating the lithiated ion exchange material from e) with an acid solution to produce a hydrogen-rich ion exchange material and a salt solution comprising lithium ions.
  • the method further comprises: g) flowing the hydrogen-rich ion exchange material into a fourth one of the plurality of columns; and h) washing the hydrogen-rich ion exchange material with an aqueous solution.
  • each of the plurality of columns is configured to transport the ion exchange material by a pipe system or an internal conveyer system.
  • each of the plurality of columns is configured to transport the ion exchange material by a pipe system.
  • each of the plurality of columns is configured to transport the ion exchange material by an internal conveyer system.
  • the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a desalination effluent, a concentrated brine, a processed brine, waste brine from a bromine-extraction process, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
  • the liquid resource is a brine. In some embodiments of the methods described herein, the liquid resource comprises a natural brine, a synthetic brine, or a mixture of a natural and a synthetic brine. In some embodiments of the methods described herein, the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a desalination effluent, a concentrated brine, a processed brine, waste brine from a bromine-extraction process, an oilfield brine, a liquid from an ion exchange process, or combinations thereof.
  • the eluent or eluent solution is an acid solution (e.g., an acidic solution).
  • the acid solution comprises hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, carbonic acid, acetic acid, or combinations thereof.
  • the acid solution comprises hydrochloric acid, sulfuric acid, phosphoric acid, nitric acid, or combinations thereof.
  • the acid solution comprises hydrochloric acid, sulfuric acid, phosphoric acid, or combinations thereof. In some embodiments of the methods described herein the acid solution comprises hydrochloric acid. In some embodiments of the methods described herein the acid solution comprises sulfuric acid. In some embodiments of the methods described herein the acid solution comprises phosphoric acid. In some embodiments of the methods described herein the acid solution comprises carbonic acid.
  • treatment of said ion exchange beads elutes lithium, to produce a synthetic lithium solution.
  • said acid comprises a gas dissolved in water.
  • said acid comprises carbon dioxide dissolved in water.
  • said acid comprises carbonic acid.
  • said acid can be alternatively referred to as an eluent, or eluent solution. Treating ion exchange beads with said eluent (or acid) results in the formation of a synthetic lithium solution, also called an eluent.
  • Nonlimiting embodiments, methods, and systems used for eluting lithium from ion exchange beads by treatment of said ion exchange beads with an acidic eluent are described herein.
  • the process comprises: (a) treating the ion exchange beads with acid under conditions suitable to absorb hydrogen to generate hydrogen-enriched beads and release lithium to generate a lithium-enriched solution; (b) optionally, washing the hydrogen- enriched beads with water to generate hydrogen-enriched beads substantially free of residual acid; (c) treating the hydrogen-enriched beads with the liquid resource under conditions suitable to absorb lithium to generate lithium-enriched beads; (d) optionally, washing the WSGR Docket No.50741-726.601 lithium-enriched beads with water to generate lithium-enriched beads substantially free of liquid resource; and (e) repeating the cycle to produce a lithium-enriched solution from the liquid resource.
  • the process of extracting lithium occurs by contacting solutions described above with ion exchange beads occurs within one or more of the devices for lithium extraction disclosed herein.
  • Another major challenge for lithium extraction using inorganic ion exchange materials is dissolution and degradation of the materials, especially during lithium elution in acid but also during lithium uptake in liquid resources.
  • To yield a concentrated lithium solution from the ion exchange process it is desirable to use a concentrated acid solution to elute the lithium.
  • concentrated acid solutions dissolve and degrade inorganic ion exchange materials, which decreases the performance and lifespan of the materials.
  • a dilute and weakly acidic solution is used to elute lithium form the ion exchange material.
  • a gas is dissolved into a liquid is used to make a dilute acid eluent.
  • said eluent comprises carbon dioxide dissolved in water.
  • said carbon dioxide dissolved in water is weakly acidic.
  • Systems for recovering water and a dissolved gas from the eluent solution methods and systems are used to further concentrate the eluted lithium in the synthetic lithium solution produced by treatment of the ion exchange material with an acidic eluent.
  • said concentration involves removing water from the synthetic lithium solution.
  • said water is recycled to make an acidic eluent solution.
  • dissolved gas is recycled to make an acidic eluent solution.
  • the concentrated synthetic lithium solution is further converted to a lithium product, including but not limited to lithium carbonate or lithium hydroxide.
  • the concentration of lithium in the synthetic lithium solution eluted from the ion exchange beads, when said synthetic lithium solution exits the lithium extraction system is from about 0.1 to about 1, from about 1 to about 5, from about 5 to about 10, from about 10 to about 20, from about 20 to about 50, from about 50 to about 100, or from about 100 to about 250 mg/L of lithium.
  • the lithium salt in said synthetic lithium solution comprises lithium bicarbonate, lithium carbonate, or a combination thereof.
  • other ionic impurities are also eluted from the ion exchange material.
  • Other embodiments and compositions of synthetic lithium solutions produced from the ion exchange beads are described in “Compositions of eluates produced by lithium extraction from a liquid resource using ion exchange”. [0404] In some embodiments, the pressure, temperature, or pressure and temperature of the eluent solution is controlled to modulate the concentration of lithium eluted from the ion exchange beads.
  • Nonlimiting embodiments of the composition, pressures, temperatures, and properties of eluent solutions used to elute lithium are described in “Systems and methods for generating an eluent by injecting a gas into a liquid” and “Embodiments comprising a combination of one or more gases and one or more liquids.”
  • the synthetic lithium solution eluted from the ion exchange beads comprises bicarbonate or carbonate anions.
  • said synthetic solution is produced from an eluent comprising carbon dioxide dissolved in water.
  • cations eluted from said ion exchange beads include lithium, calcium, magnesium, strontium, and other cations that, when combined with bicarbonate or carbonate anions, can form solids carbonate salts.
  • Such solid carbonate salts can precipitate from solution and deposit, entrain, coat, scale, or otherwise hamper the operation of fluid handling equipment.
  • the pressure of an aqueous stream, including said synthetic lithium solution is modulated and maintained to prevent such precipitation.
  • the temperature of an aqueous stream, including said synthetic lithium solution is modulated and maintained to prevent such precipitation.
  • the pH of an aqueous stream, including said synthetic lithium solution is modulated and maintained to prevent such precipitation.
  • the dissolved CO2 of an aqueous stream, including said synthetic lithium solution is modulated and maintained to prevent such precipitation.
  • the synthetic lithium solution eluted from the ion exchange beads comprises conjugate anions of an organic acid.
  • said synthetic solution is produced from an eluent comprising an organic acid dissolved water.
  • the synthetic lithium solution eluted from the ion exchange beads comprises acetate anions.
  • said synthetic solution is produced from an eluent comprising acetic acid dissolved in water.
  • cations eluted from said ion exchange beads include lithium, calcium, magnesium, strontium, and other cations.
  • said synthetic lithium solutions comprising conjugate anions of an organic acid are contacted with a gas to generate the organic acid.
  • the conjugate anion is acetate
  • the acid is acetic acid.
  • a system for generating the organic acid from carbon dioxide and an eluate comprising acetate anions is described in Example 13.
  • the ion exchange material exhibits an ion exchange capacity, quantified as the mass of lithium contained in the ion exchange material that is available for exchange with protons.
  • said ion exchange capacity is about 1 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 2 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 4 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 6 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 10 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 14 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 18 mg of Li per gram of ion exchange material.
  • said ion exchange capacity is about 25 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 30 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 35 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 40 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 50 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 60 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 70 mg of Li per gram of ion exchange material.
  • said ion exchange capacity is about 80 mg of Li per gram of ion exchange material. In some embodiments, said ion exchange capacity is about 100 mg of Li per gram of ion exchange material.
  • WSGR Docket No.50741-726.601 [0409] In some embodiments, all of the ion exchange sites in the ion exchange material are exchanged during elution of the ion exchange material with an acid to generate a synthetic lithium solution. In some embodiments, about 1% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution.
  • about 1% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 1% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 1% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 1% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution.
  • about 2% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 4% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 6% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 8% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution.
  • about 10% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 15% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 20% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 25% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution.
  • about 30% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 40% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 50% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic WSGR Docket No.50741-726.601 lithium solution. In some embodiments, about 60% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution.
  • about 70% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 80% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 90% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution. In some embodiments, about 100% of the ion exchange sites are exchanged when an acidic eluent is contacted with the ion exchange material to generate a synthetic lithium solution.
  • the percentage of ion exchange sites exchanged when the acidic eluent is contacted with the ion exchange material depends on the acid used for elution.
  • vessels and systems that contain the ion exchange material are designed to facilitate elution of lithium using an eluent dissolved in water.
  • the ion exchange material is selected for high lithium absorption capacity, high selectivity for lithium in a liquid resource relative to other ions such as sodium and magnesium, strong lithium uptake in liquid resources including those with low concentrations of lithium, facile elution of lithium with a small excess of acid, low concentration of acid, and fast ionic diffusion.
  • the liquid resource containing lithium is pumped through the ion exchange column so that the ion exchange particles absorb lithium from the liquid resource while releasing hydrogen.
  • an acid solution is pumped through the column so that the particles release lithium into the acid solution while absorbing hydrogen.
  • the column may be operated in co-flow mode with the liquid resource and acid solution alternately flowing through the column in the same direction, or the column may be operated in counter-flow mode with a liquid resource and acid solution alternately flowing through the column in opposite directions.
  • the column may be treated or washed with water or other solutions for purposes such as adjusting pH in WSGR Docket No.50741-726.601 the column or removing potential contaminants.
  • the beads may form a fixed or moving bed, and the moving bed may move in counter-current to the brine and acid flows.
  • the beads may be moved between multiple columns with moving beds where different columns are used for brine, acid, water, or other flows.
  • the pH of the liquid may be adjusted with NaOH or other chemicals to facilitate the ion exchange reaction as well as handling or disposal of the spent liquid resource.
  • the liquid resource Before or after the liquid resource flows through the column, the liquid resource may be subjected to other processes including other ion exchange processes, solvent extraction, evaporation, chemical treatment, or precipitation to remove lithium, to remove other chemical species, or to otherwise treat the brine.
  • ion exchange particles When the ion exchange particles are treated with acid, a lithium solution is produced. This lithium solution may be further processed to produce lithium chemicals or lithium products. These lithium chemicals may be supplied for an industrial application.
  • an ion exchange material is selected from the following list: an oxide, a phosphate, an oxyfluoride, a fluorophosphate, or combinations thereof.
  • the acid used for recovering lithium from the porous ion exchange beads is selected from the following list: hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, carbonic acid, acetic acid, carbonic acid, or combinations thereof.
  • the acid used for recovering lithium comprises carbonic acid.
  • the acid used for recovering lithium from the porous ion exchange beads has a pH selected from the following list: from about 0 to about 0.1, from about 0.1 to about 1, from about 1 to about 2, from about 2 to about 3, from about 3 to about 4, from about 4 to about 5, from about 5 to about 6, from about 6 to about 7.
  • the acid used for recovering lithium from the porous ion exchange beads has a pH of about 3 to about 3.5.
  • the acid used for recovering lithium from WSGR Docket No.50741-726.601 the porous ion exchange beads has a pH of about 3.5 to about 4.
  • the acid used for recovering lithium from the porous ion exchange beads has a pH of about 4 to about 5.
  • said pH is modulated by the pressure, temperature, or pressure and temperature of the eluent acid.
  • said pressure is less than about 1 psi, less than about 2 psi, less than about 5 psi, less than about 10 psi, less than about 50 psi, less than about 100 psi, less than about 500 psi, less than about 1000 psi, less than about 5000 psi.
  • said pressure is at most about 1 psi, at most about 2 psi, at most about 5 psi, at most about 10 psi, at most about 50 psi, at most about 100 psi, at most about 500 psi, at most about 1000 psi, at most about 5000 psi. In some embodiments, the pressure is more than about 1 psi, more than about 2 psi, more than about 5 psi, more than about 10 psi, more than about 50 psi, more than about 100 psi, more than about 500 psi, more than about 1000 psi, more than about 5000 psi.
  • the pressure is from about 1 psi to about 2 psi, from about 2 psi to about 5 psi, from about 5 psi to about 10 psi, from about 10 psi to about 50 psi, from about 50 psi to about 100 psi, from about 100 psi to about 500 psi, from about 500 psi to about 1000 psi, from about 1000 psi to about 5000 psi.
  • the temperature is from -20 to 150 ⁇ C, from -20 to 120 ⁇ C, from -20 to 100 ⁇ C, from -20 to 80 ⁇ C, from 0 to 80 ⁇ C, from 0 to 60 ⁇ C, from 0 to 40 ⁇ C, from 0 to 20 ⁇ C, from 0 to 10 ⁇ C, from 10 to 20 ⁇ C, from 20 to 30 ⁇ C, , from 30 to 40 ⁇ C, from 4 to 50 ⁇ C.
  • said pH is modulated by the pressure, temperature, or pressure and temperature of the solution comprising a gas dissolved in water.
  • said pH is modulated by the pressure, temperature, or pressure and temperature of the solution comprising carbon dioxide dissolved in water.
  • the pH of said solution modulated throughout the elution process.
  • the flow of eluent solution is adjusted throughout the lithium elution process.
  • the flow rate of the eluent solution is adjusted throughout the lithium elution process.
  • the eluent solution is flowed at a rate that is selected from: 0.01, 0.1, 1, 5, 10, 50, 100 bed volumes per minute, wherein bed volume corresponds to the volume of ion exchange beads or ion exchange material contained within the lithium extraction device.
  • the porous ion exchange beads perform the ion exchange reaction repeatedly over a number of cycles selected from the following list: greater than 10 cycles, greater than 30 cycles, greater than 100 cycles, greater than 300 cycles, or greater than 1,000 cycles, greater than 2,000 cycles, greater than 3,000 cycles, greater than 5,000 cycles, greater than 10,000 cycles.
  • the ion exchange materials performs the ion WSGR Docket No.50741-726.601 exchange reaction repeatedly over a number of cycles selected from the following list: greater than 10 cycles, greater than 30 cycles, greater than 100 cycles, greater than 300 cycles, or greater than 1,000 cycles, greater than 2,000 cycles, greater than 3,000 cycles, greater than 5,000 cycles, greater than 10,000 cycles.
  • the porous ion exchange beads perform the ion exchange reaction repeatedly over a number of cycles selected from the following list: at least 10 cycles, at least 30 cycles, at least 100 cycles, at least 300 cycles, or at least 1,000 cycles, at least 2,000 cycles, at least 3,000 cycles, at least 5,000 cycles, at least 10,000 cycles.
  • the ion exchange materials performs the ion exchange reaction repeatedly over a number of cycles selected from the following list: at least 10 cycles, at least 30 cycles, at least 100 cycles, at least 300 cycles, or at least 1,000 cycles, at least 2,000 cycles, at least 3,000 cycles, at least 5,000 cycles, at least 10,000 cycles.
  • the ion exchange materials performs the ion exchange reaction repeatedly over a number of cycles selected from the following list: from about 10 to about 50 cycles, from about 50 to about 100 cycles, from about 100 to about 500 cycles, from about 500 to about 1000 cycles, from about 1000 to about 2000 cycles, from about 2000 to about 5000 cycles, from about 5000 to about 10,000 cycles.
  • the conversion of dissolved carbon dioxide to lithium bicarbonate during the elution process ranges from about 0.001% to about 99%.
  • the conversion efficiency is about 1% to 10%.
  • the conversion efficiency is about 0.1% to 10%.
  • the conversion efficiency is about 0.1% to 5%.
  • the conversion efficiency is about 0.01% to 10%.
  • the conversion efficiency is about 0.001% to about 0.1%, about 0.1% to about 1%, or about 1% to about 5%.
  • this relatively low conversion efficiency is primarily due to the weakly acidic nature of carbonic acid formed from dissolved carbon dioxide, which has a significantly higher pH compared to conventional mineral acids like hydrochloric or sulfuric acid.
  • this lower acidity and conversion efficiency such embodiments of the processes disclosed herein remain advantageous because the unconverted carbon dioxide can be recovered downstream using methods described in the "System for recovering water and a dissolved gas from the eluent solution" section, allowing for recycling of the gas and regeneration of the eluent solution.
  • the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:1 to about 1:10,000, depending on process conditions.
  • WSGR Docket No.50741-726.601 covers a wide range from about 1:1 to about 1:1,000.
  • the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:10 to about 1:1,000.
  • the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:20 to about 1:1,000. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:20 to about 1:500. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:1 to about 1:100. In some embodiments with relatively high efficiency, the molar ratio may approach 1:1 to 1:10. In some embodiments of moderate efficiency systems, the molar ratio typically ranges from about 1:10 to about 1:100.
  • the molar ratio may be about 1:100 to about 1:5,000, indicating that only a small fraction of the dissolved carbon dioxide participates in the formation of lithium bicarbonate during elution.
  • the excess dissolved carbon dioxide serves to maintain the acidic conditions necessary for continued elution even as lithium concentration increases in the eluate and is subsequently recovered in downstream processing steps.
  • the concentrated lithium solution that is yielded from the porous ion exchange beads is further processed into lithium raw materials using methods selected from the following list: solvent extraction, ion exchange, chemical precipitation, electrodialysis, electrowinning, evaporation with direct solar energy, evaporation with concentrated solar energy, evaporation with a heat transfer medium heated by concentrated solar energy, evaporation with heat from a geothermal brine, evaporation with heat from combustion, water removal using a semi-permeable membrane, reverse osmosis, nanofiltration, microfiltration, ultrafiltration, or combinations thereof.
  • the concentrated lithium solution that is yielded from the porous ion exchange beads is further processed into lithium chemicals selected from the following list: lithium chloride, lithium carbonate, lithium hydroxide, lithium metal, lithium metal oxide, lithium metal phosphate, lithium sulfide, or combinations thereof.
  • the concentrated lithium solution that is yielded from the porous ion exchange beads is further processed into lithium chemicals that are solid, liquid, hydrated, or anhydrous.
  • Embodiments, systems, and methods of such treatments to the synthetic lithium solution, concentrated lithium solution, eluate, or a combination thereof are described in the following sections: System for recovering water and a dissolved gas from the eluent solution, Embodiments for Limiting or Eliminating Precipitation of Impurities in the Eluate Solution, WSGR Docket No.50741-726.601 Treatment of the eluate produced from lithium extraction to produce lithium products, Removal of impurities, Impurities Selective Ion Exchange Material, Nanofiltration, Precipitation, Pressure Adjustment Precipitation, Electrodialysis Separation, Electrolysis, electrodialysis, and other embodiments comprising treatment of a lithium solution in an electrochemical system, Temperature Reduction Precipitation, Precipitation of metal ions by adjustment of pH and oxidation reduction potential, Methods for Adjusting the pH of the Lithium Eluate, Methods for Precipitating Dissolved Transition Metals, Methods for Removal of Dissolved Impurities in
  • the lithium chemicals produced using the porous ion exchange beads are used in an industrial application selected from the following list: lithium batteries, metal alloys, glass, grease, or combinations thereof.
  • the lithium chemicals produced using the coated ion exchange particles are used in an application selected from the following list: lithium batteries, lithium-ion batteries, lithium sulfur batteries, lithium solid-state batteries, and combinations thereof.
  • the ion exchange materials are synthesized in a lithiated state with a sublattice fully or partly occupied by lithium.
  • the ion exchange materials are synthesized in a hydrated state with a sublattice fully or partly occupied by hydrogen.
  • An aspect of the disclosure described herein is a method of generating a lithium eluate solution from a liquid resource, comprising: providing an ion exchange reactor comprising a tank, ion exchange particles that selectively absorb lithium from a liquid resource and elute a lithium eluate solution when treated with an acid solution after absorbing lithium ions from said liquid resource, one or more particle traps, and provision to modulate pH of said liquid resource; flowing a liquid resource into said ion exchange reactor thereby allowing said ion exchange particles to selectively absorb lithium from said liquid resource; treating said ion exchange particles with an acid solution to yield said lithium eluate solution; and passing said lithium eluate solution through said one or more particle traps to collect said lithium eluate solution.
  • the tank has a conical shape. In some embodiments, the tank has a partial conical shape. In some embodiments, the conical shape allows the ion exchange particles to settle into a settled bed so that liquid can be removed from above the settled bed. In some embodiments, the partial conical shape allows the ion exchange particles to settle into a settled bed so that liquid can be removed from above the settled bed. [0428] In some embodiments, modulation of the pH of the liquid resource occurs in the tank. In some embodiment, modulation of the pH of the liquid resource occurs prior to injection into the tank. In some embodiments, one or more particle traps comprise one or more filters inside the tank.
  • one or more particle traps comprise one filter. In some embodiments, one or more particle traps comprise one filter. In some embodiments, one or more particle traps comprise two filters. In some embodiments, one or more particle traps comprise three filters. In some embodiments, one or more particle traps comprise four filters. In some embodiments, one or more particle traps comprise five filters. [0429] In some embodiments, one or more particle traps is located at the bottom of the tank. In some embodiments, one or more particle traps is located close to the bottom of the tank. In some embodiments, one or more particle traps is located above the bottom of the tank. [0430] In some embodiments, one or more particle traps comprise one or more meshes.
  • one or more particle traps comprises one mesh. In some embodiments, one or more particle traps comprises two meshes. In some embodiments, one or more particle traps comprises three meshes. In some embodiments, one or more particle traps comprises four meshes. In some embodiments, one or more particle traps comprises five meshes. In some embodiments, all the meshes of the one or more particle traps are identical. In some embodiments, at least one of the meshes of the one or more particle traps is not identical to the rest of the meshes of the one or more particle traps.
  • one or more meshes comprise a pore space of less than about 200 microns, less than about 175 microns, less than about 150 microns, less than about 100 microns, less than about 75 microns, less than about 50 microns, less than about 25 microns, less than about 10 microns, more than about 1 micron, more than about 5 micron, more than about 10 microns, more than about 20 microns, more than about 30 microns, more than about 40 microns, more than about 50 microns, more than about 60 microns, more than about 70 microns, more than about 80 microns, more than about 90 microns, more than about 100 microns, more than about 125 microns, more than about 150 microns, more than about 175 microns from about 1 micron to about 200 microns, from about 5 microns to about 175 microns, from about 10 microns to about 150 microns, from about 10 microns to about 100 microns to about 100 pore space
  • one or more meshes comprise a pore space of at most about 200 microns, at most about 175 microns, at most about 150 microns, at most about 100 microns, at most about 75 microns, at most about 50 microns, at most about 25 microns, or at most about 10 microns.
  • one or more particle traps comprise multi-layered meshes.
  • the multi-layered meshes comprise at least one finer mesh for filtration and at least one coarser mesh for structural support.
  • one or more particle traps comprise one or more meshes supported by a structural support.
  • one or more particle traps comprise one or more polymer meshes.
  • the one or more polymer meshes are selected from the group consisting of polyetheretherketone, ethylene tetrafluorethylene, polyethylene terephthalate, polypropylene, and combinations thereof.
  • one or more particle traps comprise one or more meshes comprising a metal wire mesh.
  • the metal wire mesh is coated with a polymer.
  • the ion exchange reactor is configured to move said ion exchange particles into one or more columns for washing.
  • the ion exchange reactor is configured to allow the ion exchange particles to settle into one or more columns for washing.
  • the columns are affixed to the bottom of said tank.
  • the one or more particle traps comprise one or more filters mounted in one or more ports through the wall of said tank.
  • the one or more particle traps comprise one or more filters external to said tank, and with provision for fluid communication between said one or more filters and said tank.
  • the one or more particle traps comprise one or more gravity sedimentation devices external to said tank, and with provision for fluid communication between said one or more gravity sedimentation devices and said tank.
  • one or more particle traps comprise one or more gravity sedimentation devices internal to said tank.
  • one or more particle traps comprise one or more centrifugal sedimentation devices external to said tank, and with provision for fluid communication between said one or more centrifugal sedimentation devices and said tank In some embodiments, one or more particle traps comprise one or more centrifugal sedimentation devices internal to said tank. In some embodiments, one or more particle traps comprise one or more settling tanks, one or more centrifugal devices, or WSGR Docket No.50741-726.601 combinations thereof external to said tank, and with provision for fluid communication between said one or more settling tanks, centrifugal devices, or combinations thereof, and said tank.
  • one or more particle traps comprise one or more meshes, one or more centrifugal devices, or combinations thereof external to said tank, and with provision for fluid communication between said one or more meshes, centrifugal devices, or combinations thereof, and said tank.
  • one or more particle traps comprise one or more settling tanks, one or more meshes, or combinations thereof external to said tank, and with provision for fluid communication between said one or more settling tanks, meshes, or combinations thereof, and said tank.
  • one or more particle traps comprise one or more meshes, one or more settling tanks, one or more centrifugal devices, or combinations thereof external to said tank, and with provision for fluid communication between said one or more meshes, one or more settling tanks, centrifugal devices, or combinations thereof, and said tank.
  • the ion exchange particles are stirred. In some embodiments, the ion exchange particles are stirred by a mixer. In some embodiments, the ion exchange particles are stirred by a propeller. In some embodiments, the ion exchange particles are fluidized by pumping solution into the tank near the bottom of the tank.
  • the ion exchange particles are fluidized by pumping solution from the tank back into the tank near the bottom of the tank. In some embodiments, the ion exchange particles are fluidized by pumping a slurry of the ion exchange particles from near the bottom of the tank to a higher level in the tank. [0437] In some embodiments, the method further comprises one or more staged elution tanks, wherein intermediate eluate solutions comprising mixtures of protons and lithium ions are stored and used further to elute lithium from said ion exchange particles that are freshly lithiated.
  • the method further comprises one or more staged elution tanks, wherein intermediate eluate solutions comprising mixtures of protons and lithium ions are mixed with additional acid and used further to elute lithium from said ion exchange particles.
  • the ion exchange particles further comprise a coating material.
  • the coating material is a polymer.
  • the coating of the coating material comprises a chloro-polymer, a fluoro-polymer, a chloro-fluoro- polymer, a hydrophilic polymer, a hydrophobic polymer, co-polymers thereof, mixtures thereof, or combinations thereof.
  • the pH of the lithium-enriched acidic eluent solution is regulated to control elution of lithium and/or non-lithium impurities.
  • pH of the lithium-enriched acidic solution is regulated by adding protons, such as an acid and/or an acidic solution, to the lithium-enriched acidic solution.
  • pH of the lithium-enriched acidic solution is regulated by adding protons, such as an acid and/or an acidic solution, to the impurities-enriched lithiated acidic solution prior to removing impurities.
  • the acid comprises sulfuric acid, phosphoric acid, hydrochloric acid, hydrobromic acid, carbonic acid, nitric acid, or combinations thereof.
  • the acidic solution is the same as the acidic solution originally contacted with the first lithium-enriched ion exchange material. In some embodiments, the acidic solution is the different from the acidic solution originally contacted with the first lithium- enriched ion exchange material.
  • more protons are added to the lithium-enriched acidic solution, forming a protonated lithium-enriched acidic solution that is again contacted with a lithium-enriched ion exchange material to elute more lithium into the protonated lithium- enriched acidic solution.
  • more protons are added to the lithium- enriched acidic solution by adding an acid or acidic solution thereto to form the protonated lithium-enriched acidic solution.
  • protons are added to a lithium- enriched acidic solution before passing through each vessel in a network of lithium-selective ion exchange vessels, as described herein.
  • Chemical properties and compositions of eluents generated by injecting a gas into a liquid is a method of generating a lithium eluent from a gas.
  • said eluent is generated by injecting a gas into a liquid.
  • said injection results in the dissolution of the gas.
  • said dissolution results in the formation of an acid.
  • said dissolution releases protons.
  • such acid is generated by dissolving a gas in water.
  • the protons used to elute lithium from the ion exchange material are supplied by an eluent generated by injecting a gas into a liquid.
  • the gas is selected from carbon dioxide, sulfur dioxide, sulfur monoxide, sulfur trioxide, a gaseous oxide of sulfur, nitrogen monoxide, nitrogen dioxide, a gaseous oxide of nitrogen, a mixture, a solution, or a combination thereof.
  • the gas is carbon dioxide.
  • the liquid into which the gas is dissolved is water.
  • the liquid into which the gas is dissolved is an aqueous solution.
  • the liquid into which the gas is dissolved is an aqueous mixture.
  • said aqueous solutions comprises water, one or more dissolved cations, and one or more dissolved anions.
  • said one or more cations comprises an ion of Lithium, Beryllium, Boron, Sodium, Magnesium, Aluminum, Silicon, Potassium, Calcium, Scandium, Titanium, Vanadium, Chromium, Manganese, Iron, Cobalt, Nickel, Copper, Zinc, Gallium, Germanium, Arsenic, Selenium, Rubidium, Strontium, Yttrium, Zirconium, Niobium, Molybdenum, Technetium, Ruthenium, Rhodium, Palladium, Silver, Cadmium, Indium, Tin, Antimony, Tellurium, Cesium, Barium, Lanthanum, Cerium, Praseodymium, Neodymium, Promethium, Samarium, Europium, Ga
  • said one or more cations comprises an ion of Magnesium or Calcium.
  • said one or more anions are selected from a chloride, a chlorate, a perchlorate, a hypochlorite, a fluoride, a bromide, a bromate, a hypobromite, an iodide, an iodate, a hypoiodite, a sulfate, a hydrogen sulfate, a sulfide, a thiosulfate, a nitrate, a nitrite, a phosphate, a hydrogen phosphate, a dihydrogen phosphate, an oxide, a hydroxide, a formate, an acetate, a chromate, a dichromate, a carbonate, a bicarbonate, or a mixture thereof.
  • said one or more anions are selected from a chloride, a bicarbonate, and a carbonate.
  • the composition and speciation WSGR Docket No.50741-726.601 of ions and anions in said aqueous solution depends on the pH, temperature, and pressure of said solution.
  • said eluents are aqueous solutions comprises water, optionally one or more dissolved cations, optionally one or more dissolved anions, and optionally one or more components that are miscible in water.
  • said component miscible in water compress an alcohol.
  • WSGR Docket No.50741-726.601 said alcohol comprises methanol, ethanol, propanol, butanol, pentanol, hexanol, benzyl alcohol, isopropyl alcohol, or a mixture thereof.
  • said component miscible in water comprises an organic acid.
  • said organic acid is a carboxylic acid.
  • said carboxylic acid comprises formic acid, acetic acid, propionic acid, butyric acid, benzoic acid, phthalic acid, terephthalic acid, another organic acid comprising a carboxylic acid moiety, or a mixture thereof.
  • the eluent comprises an acidic solution.
  • the acidic solution comprises an acid selected from an organic acid, an inorganic acid, or a polymeric acid.
  • said inorganic acid is selected from: hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, carbonic acid, or combinations thereof.
  • said inorganic acid is selected from: a carboxylic acid, formic acid, acetic acid, propionic acid, butyric acid, benzoic acid, phthalic acid, terephthalic acid, p-toluenesulfonic acid, toluenesulfonic acid, another sulfonic acid, a phosphonic acid, or a combination thereof.
  • said polymeric acid is selected from any polymer containing acidic groups, including but not limited to carboxylic acids or ammonium groups, including polyvinylsulfonic acid, polyacrylic acid, copolymers thereof, or combinations thereof.
  • the strength of said acid eluent formed by injecting a gas into a liquid is measured by its pH.
  • the pH of said acid eluent is less than about 0, less than about 1, less than about 2, less than about 3, less than about 4, less than about 5, less than about 6, less than about 7, less than about 8, less than about 9, less than about 10, less than about 10, less than about 11, less than about 12, less than about 13, less than about 14.
  • the pH of said acid eluent is at most about 0, at most about 1, at most about 2, at most about 3, at most about 4, at most about 5, at most about 6, at most about 7, at most about 8, at most about 9, at most about 10, at most about 10, at most about 11, at most about 12, at most about 13, at most about 14. In some embodiments, the pH of said acid eluent is more than about 0, more than about 1, more than about 2, more than about 3, more than about 4, more than about 5, more than about 6, more than about 7, more than about 8, more than about 9, more than about 10, more than about 10, more than about 11, more than about 12, more than about 13, more than about 14.
  • the pH of said acid eluent is more than about 0 but less than about 1, more than about 1 but less 2, more than about 2 but less than about 3, more than about 3but less than about 4, more than about 4 but less than about 5, more than about 5 but less than about 6, more than about 6 but less than about 7, more than about 7 but less than about 8, more than about 8 but less than about 9, more than about 9 WSGR Docket No.50741-726.601 but less than about 10, more than about 10 but less than about 10, more than about 10 but less than about 11, more than about 11 but less than about 12, more than about 12 but less than about 13, more than about 13 but less than about 14.
  • the pH of said acid eluent is more than about 0 but at most about 1, more than about 1 but less 2, more than about 2 but at most about 3, more than about 3but at most about 4, more than about 4 but at most about 5, more than about 5 but at most about 6, more than about 6 but at most about 7, more than about 7 but at most about 8, more than about 8 but at most about 9, more than about 9 but at most about 10, more than about 10 but at most about 10, more than about 10 but at most about 11, more than about 11 but at most about 12, more than about 12 but at most about 13, more than about 13 but at most about 14.
  • a typical source of proton includes an acidic solution, said solution comprising a mineral or organic acid, which in some embodiments is selected from hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, acetic acid, or combinations thereof. Such acid are commonly used in the chemical industry.
  • the pH of the acid eluent is higher than that of mineral acids; despite the higher pH and lower acidity form the eluent generated by injecting a gas into a liquid, this acidity is sufficient for supplying the protons (H + ) ions necessary to elute lithium.
  • this acidity is more effective at supplying the protons (H + ) ions necessary to elute lithium than a mineral acid.
  • Systems and methods for generating an eluent by injecting a gas into a liquid are a method of generating a lithium eluent from a gas.
  • said eluent is generated by injecting a gas into a liquid.
  • said injection results in the dissolution of the gas.
  • said dissolution results in the formation of an acid.
  • said dissolution releases protons.
  • such acid is generated by dissolving a gas in water.
  • an eluent solution produced by injecting a gas into a liquid, as described herein is used to elute lithium from an ion exchange material.
  • the eluent comprise carbon dioxide gas injected into liquid water.
  • the dissolution of carbon dioxide in water results in the formation of soluble carbon dioxide, carbonate, and hydrogen carbonate (bicarbonate) species, which results in an acidic WSGR Docket No.50741-726.601 solution pH of less than 7.
  • the dissolution of carbon dioxide into water is achieved by the systems described herein.
  • the injection of a gas into a liquid is achieved by systems that efficiently inject said gas into said liquid, in a manner that results in optimal contact of the liquid with the gas.
  • said optimal contact results in effective dissolution of the gas in the liquid.
  • said effective dissolution results in a lower pH for the eluent.
  • said effective dissolution results in more efficient elution of lithium from the ion exchange beads.
  • said more efficient elution results in a better performance of the ion exchange system.
  • the injection of a gas into a liquid is achieved by systems that efficiently inject said gas into said liquid.
  • Example 2 describes a liquid-gas contactor system comprising a sparging stone used to inject carbon dioxide into water, resulting in a solution pH of around 4.5.
  • Example 10 describes a liquid-gas contactor system comprising a sparging stone used to inject carbon dioxide into a pressurized tank containing water, where the high pressure maintained in said tank results in an eluate product with higher lithium concentration.
  • the liquid-gas contactor system comprises a vessel.
  • the liquid-gas contactor system comprises a pressure vessel.
  • said vessel comprises one or more compartments.
  • said vessel is constructed out of steel, stainless steel, titanium, Hastelloy, aluminum, mixtures thereof, alloys thereof, or combinations thereof.
  • said vessel is constructed out of fiberglass.
  • said vessel is constructed out of a metal.
  • said metal is coated with a second component.
  • said second component used for coating comprises glass, a polymer, a ceramic, a second metal, or a combination thereof.
  • said polymer comprises epoxy, rubber, a polymer coating, polyvinyl chloride, high density polyethylene, low density polyethylene, polypropylene, polyvinylidene difluoride, polytetrafluoroethylene, polystyrene, Acrylonitrile butadiene styrene, Polyether ether ketone, copolymers thereof, mixture thereof, or combinations thereof.
  • said pressure vessel operates at a pressure that is less than about 1 psi, less than about 2 psi, less than about 5 psi, less than about 10 psi, less than about 50 psi, less than about 100 psi, less than about 500 psi, less than about 1000 psi, less than about 5000 psi.
  • said pressure vessel operates at a pressure that is at most about 1 psi, at most about 2 psi, at most about 5 psi, at most about 10 psi, at most about WSGR Docket No.50741-726.601 50 psi, at most about 100 psi, at most about 500 psi, at most about 1000 psi, at most about 5000 psi.
  • the pressure is more than about 1 psi, more than about 2 psi, more than about 5 psi, more than about 10 psi, more than about 50 psi, more than about 100 psi, more than about 500 psi, more than about 1000 psi, more than about 5000 psi.
  • said pressure vessel operates at a pressure that is from about 1 psi to about 2 psi, from about 2 psi to about 5 psi, from about 5 psi to about 10 psi, from about 10 psi to about 50 psi, from about 50 psi to about 100 psi, from about 100 psi to about 500 psi, from about 500 psi to about 1000 psi, from about 1000 psi to about 5000 psi.
  • the liquid-gas contactor system comprises a component for injecting the gas into the liquid.
  • the operation of the system used for injecting a gas into a liquid is optimized to achieve an optimal eluent solution.
  • the liquid-gas contactor system comprises a component for injecting the carbon dioxide into water, in a manner that minimized the resulting solution pH.
  • the liquid-gas contactor system comprises one or more components that deliver gas flow into one or more locations within the vessel where the gas is injected.
  • said components comprise one or more injection ports.
  • the flow through said injection ports is modulated during the formation of the eluent solution, during elution, or at any point during the operation of the lithium extraction system.
  • the flow through said injection ports is modulated during the formation of the eluent solution, during elution, or at any point during the operation of the lithium extraction system.
  • the one or more injection ports are connected to a manifold.
  • the one or more injection ports are connected to a gas delivery system.
  • injection of said gas into a liquid occurs through one or more of a pipe, tubing, channels, slits, beams, baffles, baskets, scallops, nozzles, spargers, sparging stones, or a mesh.
  • the components that direct flow within the vessel are perforated.
  • the openings or perforations in the components that distribute flow are shaped as circles, ovals, vertical or horizontal slits, squares, crosses, rectangles, triangles, irregular shapes, or a combination thereof.
  • flow of the gas occurs from the top to the bottom of the vessel. In some embodiments, flow of the gas occurs from the bottom to the top of the vessel. In some embodiments, flow of the gas occurs from the inside to the outside of the vessel. In some embodiments, flow of the gas occurs from the outside to the inside of the vessel.
  • the vessel has one or more internal nozzles designed to distribute flow of the gas evenly.
  • the vessel has nozzles placed equidistant with each WSGR Docket No.50741-726.601 other. In some embodiments, said nozzles are placed in a square, circular, conical, cylindrical, or rectangular arrangement. In one embodiment the nozzles are spaced out so that each nozzle covers the same area. In one embodiment the nozzles have slits or holes of width of less than 0.1 ⁇ m, less than 1 ⁇ m, less than 10 ⁇ m, less than 100 ⁇ m, or less than 1 mm. In one embodiment, the vessel has mesh with holes less than 0.1 ⁇ m, less than 1 ⁇ m, less than 10 ⁇ m, less than 100 ⁇ m, or less than 1000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of less than about 10 ⁇ m, less than about 20 ⁇ m, less than about 30 ⁇ m, less than about 40 ⁇ m, less than about 50 ⁇ m, less than about 60 ⁇ m, less than about 70 ⁇ m, less than about 80 ⁇ m, less than about 90 ⁇ m, less than about 100 ⁇ m, less than about 200 ⁇ m, less than about 300 ⁇ m, less than about 400 ⁇ m, less than about 500 ⁇ m, less than about 600 ⁇ m, less than about 700 ⁇ m, less than about 800 ⁇ m, less than about 900 ⁇ m, less than about 1000 ⁇ m, less than about 2000 ⁇ m, less than about 4000 ⁇ m, less than about 8000 ⁇ m, or less than about 10000 ⁇ m.
  • the nozzles have slits or holes of width of at most 0.1 ⁇ m, at most 1 ⁇ m, at most 10 ⁇ m, at most 100 ⁇ m, or at most 1 mm.
  • the vessel has mesh with holes at most 0.1 ⁇ m, at most 1 ⁇ m, at most 10 ⁇ m, at most 100 ⁇ m, or at most 1000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of at most about 10 ⁇ m, at most about 20 ⁇ m, at most about 30 ⁇ m, at most about 40 ⁇ m, at most about 50 ⁇ m, at most about 60 ⁇ m, at most about 70 ⁇ m, at most about 80 ⁇ m, at most about 90 ⁇ m, at most about 100 ⁇ m, at most about 200 ⁇ m, at most about 300 ⁇ m, at most about 400 ⁇ m, at most about 500 ⁇ m, at most about 600 ⁇ m, at most about 700 ⁇ m, at most about 800 ⁇ m, at most about 900 ⁇ m, at most about 1000 ⁇ m, at most about 2000 ⁇ m, at most about 4000 ⁇ m, at most about 8000 ⁇ m, or at most about 10000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of more than about 10 ⁇ m, more than about 20 ⁇ m, more than about 30 ⁇ m, more than about 40 ⁇ m, more than about 50 ⁇ m, more than about 60 ⁇ m, more than about 70 ⁇ m, more than about 80 ⁇ m, more than about 90 ⁇ m, more than about 100 ⁇ m, more than about 200 ⁇ m, more than about 300 ⁇ m, more than about 400 ⁇ m, more than about 500 ⁇ m, more than about 600 ⁇ m, more than about 700 ⁇ m, more than about 800 ⁇ m, more than about 900 ⁇ m, more than about 1000 ⁇ m, more than about 2000 ⁇ m, more than about 4000 ⁇ m, more than about 8000 ⁇ m, or more than about 10000 ⁇ m.
  • the openings or perforation in one or more for the flow distribution components have a dimension of about 10 ⁇ m to about 20 ⁇ m, from about 20 ⁇ m to about 40 ⁇ m, from about WSGR Docket No.50741-726.601 40 ⁇ m to about 80 ⁇ m, from about 80 ⁇ m to about 200 ⁇ m, from about 100 ⁇ m to about 400 ⁇ m, from about 200 ⁇ m to about 800 ⁇ m, from about 400 ⁇ m to about 1000 ⁇ m, from about 600 ⁇ m to about 2000 ⁇ m, from about 1000 ⁇ m to about 2000 ⁇ m, from about 2000 ⁇ m to about 4000 ⁇ m, from about 4000 ⁇ m to about 8000 ⁇ m, from about 6000 ⁇ m to about 10000 ⁇ m.
  • a gas is injected into a liquid to form an eluent for more than about 10 milliseconds, more than about 100 milliseconds, more than about 1 second, more than about 10 seconds, more than about 100 seconds, more than about 1 minute, more than about 10 minutes, more than about 100 minutes, more than about 1 hour, more than about 10 hours, more than about 100 hours.
  • a gas is contacted with the ion exchange beads for less than about 10 milliseconds, less than about 100 milliseconds, less than about 1 second, less than about 10 seconds, less than about 100 seconds, less than about 1 minute, less than about 10 minutes, less than about 100 minutes, less than about 1 hour, less than about 10 hours, less than about 100 hours.
  • a gas is contacted with the ion exchange beads for at most about 10 milliseconds, at most about 100 milliseconds, at most about 1 second, at most about 10 seconds, at most about 100 seconds, at most about 1 minute, at most about 10 minutes, at most about 100 minutes, at most about 1 hour, at most about 10 hours, at most about 100 hours.
  • a gas is contacted with the ion exchange beads from about 10 milliseconds to about 100 milliseconds, from about 100 milliseconds to about 1 second, from about 1 second to about 10 seconds, from about 10 seconds to about 100 seconds, from about 100 seconds to about 1 minute, from about 1 minute to about 10 minutes, from about 10 minutes to about 100 minutes, from about 1 hour to about 10 hours, from about 10 hours to about 100 hours.
  • the liquid-gas contactor system in said vessel comprises a component for mixing the gas into the liquid.
  • said component comprises one or more of: a mechanical agitator, an eductor, a pump, a fluid recirculation device, baffles, shakers, or a combination thereof.
  • the vessel contains one or more baffles arranged in parallel to the shaft of the mechanical agitator, to improve mixing.
  • the vessel is agitated with a mechanical agitator comprising a motor, a shaft, and one or more impellers mounted on said shaft.
  • said one or more impellers comprise propellers, anchor impellers, hydrofoils, pitched blade turbines, curved blade turbines, spiral turbine, flat blade turbines, radial blades, or a combination thereof.
  • said impellers contain one or more blades.
  • the shaft and impellers are comprised of carbon steel, stainless steel, WSGR Docket No.50741-726.601 titanium, Hastelloy, or a combination thereof.
  • the shaft and impellers are coated with glass, epoxy, rubber, a polymer coating, or combinations thereof.
  • the liquid-gas contact system is controlled by monitoring the pH, oxidation-reduction potential, pressure, and flow of the liquid or gas components in said system.
  • the controls comprise valves, pumps, pressure regulator, pressure relief devices, other gas or fluid control devices, or a combination thereof.
  • the operation of the system used for injecting a gas into a liquid is optimized to achieve an optimal eluent solution.
  • said optimal eluent solution has a low pH, is easier to pump, maintains dissolution of the gas, minimizes the consumption of the gas, results in improved lithium extraction performance, or a combination thereof.
  • the liquid-gas contactor system in said vessel comprises a component for adding the gas components as a solid.
  • said solid comprises solidified gas.
  • said solidified gas comprises the gaseous component cooled to a temperature at which it becomes a solid.
  • the as is carbon dioxide
  • the solid is solid carbon dioxide, also known as dry ice.
  • the solid is added at a temperature of about 195 K. In some embodiments, said solid is added directly to the liquid. In embodiments where said liquid comprises water, addition of said cold solid to said water will cause the sublimation of the solid, thus evolving carbon dioxide, and the cooling of the water. In said embodiments, the evolution of the gas from said solid directly into the liquid leads to efficient mixing and dissolution of the carbon dioxide gas into the liquid. In some embodiments, the liquid cool as the solid component sublimes, thereby increasing the dissolution of the liquid into the gas. In some embodiments, the addition of dry ice into the liquid is used as a means to control the temperature of the eluent. In some embodiments, the pressure at which the vessel operates is modulated as the dry ice sublimes into the water.
  • optimal operation comprises injecting the gas into a vessel at an optimal system pressure.
  • said pressure is maintained within a pressure vessel that contains a liquid into which the gas is dissolved, and an overhead of gas in equilibrium with the liquid.
  • said pressure is less than about 1 psi, less than about 2 psi, less than about 5 psi, less than about 10 psi, less than about 50 psi, less than about 100 psi, less than about 500 psi, less than about 1000 psi, less than about 5000 psi.
  • said pressure is at most about 1 psi, at most about 2 psi, at most about 5 WSGR Docket No.50741-726.601 psi, at most about 10 psi, at most about 50 psi, at most about 100 psi, at most about 500 psi, at most about 1000 psi, at most about 5000 psi.
  • the pressure is more than about 1 psi, more than about 2 psi, more than about 5 psi, more than about 10 psi, more than about 50 psi, more than about 100 psi, more than about 500 psi, more than about 1000 psi, more than about 5000 psi.
  • the pressure is from about 1 psi to about 2 psi, from about 2 psi to about 5 psi, from about 5 psi to about 10 psi, from about 10 psi to about 50 psi, from about 50 psi to about 100 psi, from about 100 psi to about 500 psi, from about 500 psi to about 1000 psi, from about 1000 psi to about 5000 psi.
  • the pressure in the vessel is similar to the pressure of the operating pressure of the lithium extraction system. In some embodiments, the pressure in the vessel is lower than the pressure of the operating pressure of the lithium extraction system.
  • optimal operation comprises injecting the gas into a vessel at an optimal gas flow rate.
  • said gas is injected into a pressure vessel.
  • said flow rate is about 0.001, 0.01, 0.1, 1, 10, 100, or 1000 vessel volumes per minute, about 0.01 tank volumes per minute.
  • said flow rate is from about 0.001 to about 0.01, from about 0.01 to about 0.1, from about 0.1 to about 1, from about 1 to about 10, from about 10 to about 100, from about 100 to about 1000 vessel volumes per minute tank volumes per minute.
  • the flow rate of gas into the vessel is similar to the rate of gas consumption in the lithium extraction system.
  • optimal operation comprises controlling the temperature of the system.
  • a lower system temperature results in higher dissolution of carbon dioxide into the liquid to from an eluent.
  • a lower system temperature results in a lower solution pH.
  • both the pressure and the temperature of the system are modulated.
  • the temperature is less than about 500, 250, 100, 75, 50, 40, 30, 25, 20, 15, 10, 5, or 0 degrees Celsius.
  • the temperature is at most about 500, 250, 100, 75, 50, 40, 30, 25, 20, 15, 10, 5, or 0 degrees Celsius.
  • the temperature is more than about 500, 250, 100, 75, 50, 40, 30, 25, 20, 15, 10, 5, or 0 degrees Celsius. In some embodiments, the temperature is from about than about 500 to 100, 100 to 75, 75 to 50, 50 to 40, 40 to 30, 30 to 25, 25 to 20, 20 to 15, 15 to 10, 10 to 5, or 5 to 0 degrees Celsius.
  • WSGR Docket No.50741-726.601 [0470] In some embodiments, the pressure in the vessel is lower than the pressure of the operating pressure of the lithium extraction system. In some embodiments, the pressure in the vessel is higher than the pressure of the operating pressure of the lithium extraction system.
  • Embodiments comprising a combination of one or more gases and one or more liquids
  • An aspect of the disclosure provided herein is a method of generating a lithium eluent from a gas.
  • said eluent is generated by injecting a gas into a liquid.
  • said injection results in the dissolution of the gas.
  • said dissolution results in the formation of an acid.
  • said dissolution releases protons.
  • such acid is generated by dissolving a gas in water.
  • the gas comprises a mixture of gases.
  • said comprises two or more gases selected from: carbon dioxide, sulfur dioxide, sulfur monoxide, sulfur trioxide, a gaseous oxide of sulfur, nitrogen monoxide, nitrogen dioxide, a gaseous oxide of nitrogen, a mixture, a solution, or a combination thereof.
  • the volumes, ratios, flows, or pressures of said gases is controlled to yield an optimal eluent liquid.
  • the liquid comprises a mixture of one or more liquids.
  • the liquid comprises a mixture of one or more liquids and a gas.
  • said gas is carbon dioxide.
  • the liquid comprises a mixture of one or more liquids and one or more gases.
  • said one or more gases are more soluble in the mixture of said one or more liquids than in a single liquid.
  • the solubility of said gas in said mixture of one or more liquids is more than about 0.001, 0.01, 0.1, 1, 10, 100, 1000 g/L, or the gas and liquids are fully miscible.
  • the liquid comprises a mixture of one or more liquids.
  • said one or more liquids are selected from water and a nonaqueous liquid.
  • the nonaqueous liquid is selected from an organic liquid such as an alkane, alcohol, oil, bio-organic oil, ester, ether, hydrocarbon, a carboxylic acid, an organic acid, or a combination thereof.
  • the alcohol is methanol, ethanol, propanol, isopropanol, butanol, pentanol, hexanol, or a combination thereof.
  • said acid is formic acid, acetic acid, propanoic acid, butanoic acid, or a combination thereof.
  • the nonaqueous component is selected WSGR Docket No.50741-726.601 so as to facilitate its downstream separation from water.
  • the volumetric ratio of water to the nonaqueous liquid is about 1 to 0.001, 0.01, 0.1, 1, 10, 100, 1000.
  • the volumes, ratios, flows, pressures, mixtures, temperatures, physical properties, or flow properties of the one or more gas and the one or more liquids is set, controlled, modulated, or adjusted, optionally in a continuous basis, to yield an optimal eluent liquid.
  • Embodiments comprising a combination of one or more gases, one or more liquids, and one or more dissolved solids
  • An aspect of the disclosure provided herein is a method of generating a lithium eluent from a gas.
  • said eluent is generated by injecting a gas into a liquid. In some embodiments, said injection results in the dissolution of the gas. In some embodiments, said dissolution results in the formation of an acid. In some embodiments, said dissolution releases protons. In one aspect of the disclosure provided herein, such acid is generated by dissolving a gas in water. In embodiments of the disclosure provided herein, the gas comprises a mixture of gases. In embodiments of the disclosure provided herein, the liquid comprises a mixture of one or more liquids.
  • a further aspect of the disclosure provided herein is an eluent solution used to elute lithium form an ion exchange material, wherein one or more solids are dissolved in the eluent solution to enhance the elution properties of said eluent solution.
  • the one or more solids comprise a mineral salt. Exemplary embodiments are provided in Example 16 and associated Figure 16.
  • An aspect of the invention disclosed herein is a method for lithium recovery from a liquid resource, the method comprising: a) Dissolving a solid into water to form an aqueous solution; b) forming an eluent solution by dissolving a gas in an aqueous solution at a pressure of about 0 to 50 barg, wherein the pH of the eluent solution is at most 7 following dissolution of the gas; c) contacting an ion exchange material to a liquid resource, wherein the ion exchange material absorbs lithium ions from the liquid resource to yield a lithium-depleted liquid resource and a lithiated ion exchange material; d) contacting the lithiated ion exchange material to the eluent solution, wherein the lithiated ion exchange material releases lithium into the eluent solution to generate a synthetic lithium solution; and WSGR Docket No.50741-726.601 e) separating the synthetic lithium solution from the ion exchange
  • the aqueous solution to form an eluent solution comprises water.
  • the aqueous solution further comprises a solid.
  • the solid is a mineral salt.
  • the mineral salt comprises calcium, magnesium, potassium, sodium, or a combination thereof.
  • the mineral salt comprises magnesium, potassium, sodium, or a combination thereof.
  • the mineral salt comprises sulfate, chloride, or a combination thereof.
  • the mineral salt comprises one or more of: sodium sulfate, potassium sulfate, magnesium sulfate, calcium sulfate, sodium chloride, potassium chloride, magnesium chloride, or calcium chloride.
  • the mineral salt comprises sodium chloride, potassium chloride, magnesium chloride, sodium sulfate, potassium sulfate, magnesium sulfate, or a combination thereof.
  • the concentration of the mineral salt in the aqueous solution is from about 0.001 to about 10 M (mol/L). In some embodiments, the concentration of the mineral salt in the aqueous solution is from about 0.01 to about 2 M (mol/L).
  • the inclusion of the mineral salt in the aqueous solution increases the concentration of the gas dissolved in the eluent solution, thereby decreasing the pH of the eluent solution as compared to an eluent solution formed from an aqueous solution not comprising the mineral salt.
  • the inclusion of the mineral salt in the aqueous solution increases the concentration of the gas dissolved in the eluent solution, thereby decreasing the pH of the eluent solution as compared to an eluent solution formed from an aqueous solution not comprising the mineral salt; wherein the gas is CO2.
  • the solid increases the concentration of lithium in the synthetic lithium solution.
  • the inclusion of the mineral salt in the aqueous solution increases the concentration of the lithium dissolved in the synthetic lithium solution, as compared to a synthetic lithium solution formed from an eluent solution made with an aqueous solution not comprising the mineral salt.
  • the inclusion of the mineral salt in the aqueous solution increases the concentration of the lithium dissolved in the synthetic lithium solution, as compared to a synthetic lithium solution formed from an eluent solution made with an aqueous solution not comprising the mineral salt; wherein the gas is CO2.
  • the concentration of lithium in the synthetic lithium solution increases by about 10%, about 20%, about 50%, about 100%, about 200%, about 500%, or about 1,000%.
  • the concentration of lithium in the synthetic lithium solution increases by about 10%. In some embodiments, the concentration of lithium in the WSGR Docket No.50741-726.601 synthetic lithium solution increases by about 20%. In some embodiments, the concentration of lithium in the synthetic lithium solution increases by about 50% or more.
  • said solid is dissolved in a solution of a gas in water. In some embodiments, said solid is dissolved in a solution of carbon dioxide in water. In some embodiments, the solids comprises a salt. In some embodiments, said salt comprises a cation and an anion. In some embodiments, said cation is selected from: lithium, sodium, potassium, cesium, magnesium, calcium, strontium, aluminum, iron, or a combination thereof.
  • said anion is selected from: fluoride, chloride, bromide, iodide, carbonate, sulfate, sulfite, nitrate, nitrate, or a combination thereof.
  • said salt is selected from one or more of: sodium sulfate, potassium sulfate, magnesium sulfate, calcium sulfate, sodium chloride, potassium chloride, magnesium chloride, or calcium chloride.
  • the dissolution of the solid enhances the properties of the eluent solution.
  • said enhancement results in a higher concentration of the lithium in the eluate solution, a higher purity in the eluate product eluted from the ion exchange material, a lower degradation rate of the ion exchange material, a combination thereof, or any other effect that enhances the performance of lithium extraction process.
  • the concentration of the dissolved solid in the solution is from about 0.001 to about 10 M (mol/L).
  • the concentration is from about 0.001 to about 0.01, from about 0.01 to about 0.05, from about 0.5 to about 0.1, from about 0.1 and to about 0.25, from about 0.25 to about 0.5, from about 0.5 to about 1, from about 1 to about, from about 2 to about 5, or from about 5 to about 10 mol/L. In some embodiments, the concentration is varied during the elution of the ion exchange material.
  • a further aspect of the disclosure provided herein is the integration of an eluent solution comprising one or more dissolved solids with a purification and conversion system used to convert a synthetic lithium carbonate solution into a solid lithium carbonate product.
  • the purification and conversions systems and configured to recover the dissolved solid and separate it from the lithium, the former being recycled to reform an eluent solution and the latter being further converted into a lithium product.
  • Methods and systems for generating a gas used for elution [0486]
  • the gas injected into the liquid to generate an eluent is generated by a chemical or physical process.
  • the gas injected into the liquid to generate an eluent is concentrated by a chemical or physical process before it is injected.
  • the gas injected into the liquid to generate an eluent is produced or concentrated from a different gas prior to its use to generate an eluent.
  • the gas injected into the liquid to generate an eluent is produced or concentrated from a different stream in the lithium extraction system.
  • said gas is carbon dioxide.
  • said gas is selected from: carbon dioxide, sulfur dioxide, sulfur monoxide, sulfur trioxide, a gaseous oxide of sulfur, nitrogen monoxide, nitrogen dioxide, a gaseous oxide of nitrogen, a mixture, a solution, or a combination thereof.
  • the gas is generated from a system that captures the gas from a furnace.
  • the gas is an oxide of nitrogen.
  • the gas is an oxide of sulfur.
  • the gas is carbon dioxide.
  • said system captures the gas into water, thereby generating acid.
  • the gas is generated from a system that captures the gas from flue gas.
  • said flue gas is a gas produced from the combustion of a fuel.
  • the gas is generated from a system that captures carbon dioxide from flue gas.
  • carbon dioxide is capture from a flue gas by absorption into a liquid.
  • said liquid comprises an amine.
  • carbon dioxide is capture from a flue gas by absorption into a solid.
  • the system that absorbs the gas comprises a scrubber or an absorber.
  • the gas is generated from a system that captures the gas from air.
  • said system is a system design to directly capture carbon dioxide from air, also known as direct air capture.
  • the direct air capture system comprises a solid sorbent.
  • said solid sorbent comprises an organic molecule, a polymer, a ceramic, an oxide a surface-modified oxide, an amine modified solid, a metal organic framework, activated carbon, a surface-modified activated carbon, a zeolite, a functionalized zeolite, a mixture thereof, a composite thereof, a chemically-modified material thereof.
  • the direct air capture system comprises a liquid.
  • the direct air capture system comprises a basic or alkaline functionality, either as a dissolved species in a liquid, or as a solid.
  • the direct air capture system comprises a solution.
  • said solution comprises a base.
  • said base comprises LiOH, NaOH, KOH, CsOH, Ca(OH)2, Mg(OH)2, a mixture thereof, or a different base.
  • contact of carbon dioxide with said solution produced a solid carbonate.
  • said carbonates are treated with an acid to release carbon dioxide.
  • said acid and said base are produced in an electrochemical system.
  • said acid and said base are further used as reagents in the lithium extraction system.
  • the gas is further purified before its use to generate an eluent solution.
  • said purification includes demisting, drying, compressing, cooling, expanding, heating, distilling, or a combination thereof.
  • said gas is compressed before being used for forming an eluent.
  • said gas is compressed to a pressure of about 1, 10, 50, 100, 500, 1000, or 10,000 psi.
  • System for regenerating an acid using an acid gas and a semi-permeable membrane [0493] An aspect of the disclosure provided herein is a system to regenerate an acid from a solution comprising water, a conjugate base of said acid, cations, and a dissolved gas, by treating said solution in a system comprising a semi-permeable membrane. Non-limiting embodiments of said system are described in Examples 12 and 13.
  • the solution is a synthetic lithium solution.
  • the conjugate base is selected from: an inorganic conjugate base, an organic conjugate base, or a polymeric conjugate base.
  • the conjugate base is a conjugate base of one or more of the following inorganic acids: hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic acid, carbonic acid, or combinations thereof.
  • the conjugate base is a conjugate base of one or more of the following organic acids: a carboxylic acid, formic acid, acetic acid, propionic acid, butyric acid, benzoic acid, phthalic acid, terephthalic acid, p- toluenesulfonic acid, toluenesulfonic acid, another sulfonic acid, a phosphonic acid, or a combination thereof.
  • organic acids a carboxylic acid, formic acid, acetic acid, propionic acid, butyric acid, benzoic acid, phthalic acid, terephthalic acid, p- toluenesulfonic acid, toluenesulfonic acid, another sulfonic acid, a phosphonic acid, or a combination thereof.
  • Cations, anions, and the concentration of said cations and anions in solution are described in the section “Compositions of eluates produced by lithium extraction from a liquid resource using ion exchange”.
  • the solution from which an acid is regenerated is a synthetic lithium solution.
  • the solution from which an acid is regenerated is treated in a system to dissolve a gas in said solution.
  • the gas is dissolved into the synthetic lithium solution after said synthetic solution is produced by the ion exchange system.
  • the eluent solution comprises a gas dissolved in water, and the gas remains in solution after elution of lithium from the ion exchange beads, WSGR Docket No.50741-726.601 resulting in a synthetic lithium solution already containing a dissolved gas.
  • the resulting solution comprises water, a conjugate base of said acid, cations, and a dissolved gas.
  • said solution is treated in a unit comprising a semi-permeable membrane, wherein said semi permeable preferably enables certain cations and certain anions to permeate through, while other cations and anions are rejected.
  • the rejected anions include the conjugate base anions.
  • the anions that permeate through the semi-permeable membrane include bicarbonate.
  • the cations that permeate through the semi-permeable membrane include lithium.
  • the solution comprises acetate conjugate base anions, lithium, and dissolved carbon dioxide and bicarbonate anions, and the semi-permeable membrane selectively permeates bicarbonate and lithium.
  • acetate anions are rejected together with a proton released with the bicarbonate anion.
  • a permeate stream comprising lithium bicarbonate is generated, while acetic acid is regenerated in the reject side of the semi-permeable membrane.
  • Non- limiting embodiments of such a system are described in Examples 12 and 13.
  • said semi-permeable membrane is a nanofiltration membrane. In some embodiments, said semi-permeable membrane is a reverse osmosis membrane. In some embodiments, said semi-permeable membrane is a ultrafiltration membrane. In some embodiments, said semi-permeable membrane is a reverse osmosis membrane, a low-salt rejection reverse osmosis membrane, an osmotically assisted reverse osmosis membrane, a nanofiltration membrane, an ultrafiltration membrane, or a combination thereof. In some embodiments, said semi-permeable membrane comprises multiple membranes.
  • the semi-permeable membrane comprises Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof.
  • the membranes are comprised of a functionalized polymer structure which is Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof.
  • the polymer structures of the membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
  • WSGR Docket No.50741-726.601 [0500]
  • the membrane is comprised of a functionalized polymer structure.
  • the polymer structure is comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
  • the functional groups are part of the polymer backbone.
  • functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions.
  • the functional group is benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilized quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
  • the membranes have a thickness of less than 10 ⁇ m, less than 50 ⁇ m, less than 200 ⁇ m, less than 400 ⁇ m, or less than 1,000 ⁇ m.
  • the membranes have a thickness of greater than 1,000 ⁇ m. In one some embodiments of the semi-permeable membrane, the membranes have a thickness of at most 10 ⁇ m, at most 50 ⁇ m, at most 200 ⁇ m, at most 400 ⁇ m, or at most 1,000 ⁇ m. In one embodiment of the membrane electrolysis cell, the membranes have a thickness of at least 1,000 ⁇ m.
  • the membrane has a thickness of about 1 ⁇ m to about 1000 ⁇ m, about 1 ⁇ m to about 800 ⁇ m, about 1 ⁇ m to about 600 ⁇ m, about 1 ⁇ m to about 400 ⁇ m, about 1 ⁇ m to about 200 ⁇ m, about 1 ⁇ m to about 100 ⁇ m, about 1 ⁇ m to about 90 ⁇ m, about 1 ⁇ m to about 80 ⁇ m, about 1 ⁇ m to about 70 ⁇ m, about 1 ⁇ m to about 60 ⁇ m, about 1 ⁇ m to about 50 ⁇ m, about 1 ⁇ m to about 40 ⁇ m, about 1 ⁇ m to about 30 ⁇ m, about 1 ⁇ m to about 20 ⁇ m, about 1 ⁇ m to about 15 ⁇ m, or about 1 ⁇ m to about 10 ⁇ m.
  • the membranes comprise pores.
  • said pores have a diameter of about 0.1, 1, 2, 5, 10, 25, 50 or 100 nm.
  • said pores have a diameter of about 0.1, 1, 2, 5, 10, 25, 50 or 100 ⁇ m.
  • said semi-permeable unit comprises a comprises a semi- permeable membrane.
  • said membrane is a reverse osmosis membrane, a WSGR Docket No.50741-726.601 low-salt rejection reverse osmosis membrane, an osmotically assisted reverse osmosis membrane, a nanofiltration membrane, or a combination thereof.
  • said membrane is contained in a membrane element.
  • said element comprises a spiral wound membrane.
  • said element comprises a hollow fiber membrane.
  • said element comprises a polymeric membrane, or a ceramic membrane.
  • multiple membranes are contained within a single pressure housing.
  • a single membrane is contained within a single pressure housing.
  • the operating pressure of said reverse osmosis system is greater than about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, 500, 1000, 2000, 5000 psi.
  • the operating pressure of said reverse osmosis system is at least about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, 500, 1000, 2000, 5000 psi.
  • an energy recovery device is used to recover the energy of the high-pressure stream when this stream is depressurized, and said energy is used to pressurize the inlet stream into the unit comprising the semi-permeable membrane.
  • an energy recovery device is used to recover the energy of the high-pressure stream when this stream is depressurized, and said energy is used to pressurize the inlet stream into the unit comprising the nanofiltration membrane.
  • the selectivity of the rejection of the conjugate base by the semi-permeable membrane is about 1%, 5%, 10%, 20%, 40%, 60%, 80%, 90%, 99%, or 99.9% of the inlet conjugate base.
  • the permeate stream comprises from about 0.01 to about 1%, from about 1% to about 5%, from about 5% to about 10%, from about 10% to about 25%, from about 25% to about 50%, from about 50% to about 75%, from about 75% to about 90%, from about 90% to about 99%, from about 99% to about 99.9%, from about 99.9% to about 99.99% of the lithium content in the inlet to said system.
  • the permeate stream comprises from about 0.01 to about 1%, from about 1% to about 5%, from about 5% to about 10%, from about 10% to about 25%, from about 25% to about 50%, from about 50% to about 75%, from about 75% to about 90%, from about 90% to about 99%, from about 99% to about 99.9%, from about 99.9% to about 99.99% of the bicarbonate content in the inlet to said system.
  • System for recovering water and a dissolved gas from the eluent solution [0505]
  • An aspect of the disclosure provided herein is a system to recover water, a dissolved gas, or a combination thereof from an aqueous stream.
  • An aspect of the disclosure provided herein is a system to recover water, a dissolved gas, or a combination thereof from an WSGR Docket No.50741-726.601 eluate generated by eluting lithium from ion exchange beads using an eluate comprising a gas dissolved in water.
  • said gas is carbon dioxide.
  • the recovered water, the recovered gas, or both are recycled.
  • the recycle of said water, said gas, or both is used to produce an eluent solution.
  • a non-limiting example of a system for recovering water and a gas to regenerate an eluent solution is included in Example 6.
  • the water content of the eluate or other aqueous stream is lowered to generate water and a concentrated eluate or other concentrated aqueous stream (e.g., a concentrated lithium solution).
  • the concentrated eluate is further processed to produce a lithium product.
  • said product is lithium carbonate.
  • the water content of an eluate or other aqueous stream is lowered after the carbonate content of the eluate or other aqueous stream has been lowered by a prior-implemented process.
  • the water content of an eluate or other aqueous stream is lowered before any process has been implemented that lowers the carbonate content of the eluate or other aqueous stream. In some embodiments, the water content of an eluate or other aqueous stream is lowered before without lowering the carbonate content of the eluate or other aqueous stream. In some embodiments, the water content of an eluate or other aqueous stream is lowered while controlling the pressure in the system to avoid the precipitation of dissolved species to form solids. [0508] In some embodiments, a water removal unit is configured to lower the water content of an eluate or other aqueous stream.
  • the water content of an eluate or other aqueous stream is lowered by employing a system comprising a semi-permeable membrane.
  • said semi-permeable membrane is impermeable to at least a fraction of the solids dissolved in the synthetic lithium solution, thereby allowing water to pass across the membrane to generate a permeate solution, while retaining at least a fraction the solids dissolved to generate and a concentrated synthetic lithium solution.
  • said semi-permeable membrane allows water molecules to move across it, but does not allow salts dissolved in water to move across it.
  • the permeate stream comprises about 1%, 5%, 10%, 20%, 40%, 60%, 80%, 90%, 99%, or WSGR Docket No.50741-726.601 99.9% of the water content in the inlet to said system.
  • the permeate stream comprises from about 0.01 to about 1%, from about 1% to about 5%, from about 5% to about 10%, from about 10% to about 25%, from about 25% to about 50%, from about 50% to about 75%, from about 75% to about 90%, from about 90% to about 99%, from about 99% to about 99.9%, from about 99.9% to about 99.99% of the water content in the inlet to said system.
  • the retante stream comprises about 1%, 5%, 10%, 20%, 40%, 60%, 80%, 90%, 99%, or 99.9% of the dissolved solids content in the inlet to said system.
  • the retentate stream comprises from about 0.01 to about 1%, from about 1% to about 5%, from about 5% to about 10%, from about 10% to about 25%, from about 25% to about 50%, from about 50% to about 75%, from about 75% to about 90%, from about 90% to about 99%, from about 99% to about 99.9%, from about 99.9% to about 99.99% of the total dissolved solid content in the inlet to said system.
  • the conversion of dissolved carbon dioxide to lithium bicarbonate during the elution process ranges from about 0.001% to about 99%.
  • the conversion efficiency is about 1% to 10%.
  • the conversion efficiency is about 0.1% to 10%.
  • the conversion efficiency is about 0.1% to 5%. In some embodiments, the conversion efficiency is about 0.01% to 10%. In some embodiments, the conversion efficiency is about 0.001% to about 0.1%, about 0.1% to about 1%, or about 1% to about 5%. In such embodiments, this relatively low conversion efficiency is primarily due to the weakly acidic nature of carbonic acid formed from dissolved carbon dioxide, which has a significantly higher pH compared to conventional mineral acids like hydrochloric or sulfuric acid.
  • the unconverted carbon dioxide can be recovered downstream using methods described in the "System for recovering water and a dissolved gas from the eluent solution" section, allowing for recycling of the gas and regeneration of the eluent solution.
  • over 50% of the unconverted carbon dioxide is recovered and recycled back into the elution process, significantly improving the overall economics and sustainability of the system.
  • over 70% of the unconverted carbon dioxide is recovered and recycled back into the elution process, significantly improving the overall economics and sustainability of the system.
  • the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:1 to about 1:10,000, depending on process conditions. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:1 to about 1:1,000.
  • the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:10 to about 1:1,000. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:20 to about 1:1,000. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:20 to about 1:500. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:1 to about 1:100. In some embodiments with relatively high efficiency, the molar ratio may approach 1:1 to 1:10. In some embodiments of moderate efficiency systems, the molar ratio typically ranges from about 1:10 to about 1:100.
  • the molar ratio may be about 1:100 to about 1:5,000, indicating that only a small fraction of the dissolved carbon dioxide participates in the formation of lithium bicarbonate during elution.
  • the excess dissolved carbon dioxide serves to maintain the acidic conditions necessary for continued elution even as lithium concentration increases in the eluate and is subsequently recovered in downstream processing steps.
  • Example 17 describes an embodiment where a membrane system is used to recover water and carbon dioxide from an eluate solution using a reverse osmosis membrane.
  • said water removal unit comprises a reverse osmosis (RO) semi-permeable membrane.
  • said water unit comprises a nanofiltration semi-permeable membrane.
  • said system comprises more than one system for lowering the water content.
  • said system comprises than one reverse osmosis systems.
  • said system comprises one or more membrane systems.
  • said reverse osmosis comprises an osmotically assisted reverse osmosis system.
  • said reverse osmosis comprises a forward osmosis system.
  • said reverse osmosis comprises a single pass system, a two pass system, a three pass system, a four pass system, a five pass system, a six pass system, a seven pass system, an eight pass system, a nine pass system, a ten pass system, a twenty pass system, a system with more passes, or a combination thereof.
  • said reverse osmosis comprises a brine staged system.
  • WSGR Docket No.50741-726.601 [0512]
  • the stream from which water is removed also called the concentrate, is recycled to the feed of one or more reverse osmosis (RO) units in said system.
  • one or more streams comprising water, salt, gas, or a combination thereof are redirected to one or more locations within the system to maximize the recovery of water in the system. In some embodiments, one or more streams comprising water, salt, gas, or a combination thereof are redirected to one or more locations within the system to maximize the recovery of lithium in the system.
  • said reverse osmosis (RO) system comprises a brackish water RO system. In some embodiments, said reverse osmosis system comprises a seawater RO system. In some embodiments, said reverse osmosis system comprises a low salinity RO system. In some embodiments, said reverse osmosis system comprises an osmotically assisted reverse osmosis system.
  • said osmotically assisted reverse osmosis system comprises two or more types of reverse osmosis membranes, wherein a first membrane is a conventional reverse osmosis membrane, and the second or more membranes have a lower salt rejection than the first membrane.
  • said water removal unit comprises a forward osmosis unit.
  • said water removal unit comprises a comprises a membrane.
  • said membrane is a reverse osmosis membrane, a low-salt rejection reverse osmosis membrane, an osmotically assisted reverse osmosis membrane, a nanofiltration membrane, or a combination thereof.
  • said membrane is contained in a membrane element.
  • said element comprises a spiral wound membrane. In some embodiments, said element comprises a hollow fiber membrane. In some embodiments, said element comprises a polymeric membrane, or a ceramic membrane. In some embodiments, multiple membranes are contained within a single pressure housing. In some embodiments, a single membrane is contained within a single pressure housing. [0516] In some embodiments, the operating pressure of said water removal unit is greater than about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, 500, 1000, 2000, or 5000 psi. In some embodiments, the operating pressure of said reverse osmosis system is greater than about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, 500, 1000, 2000, or 5000 psi.
  • the transmembrane pressure of the semi-permeable membrane in the water removal unit is greater than about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, 500, 1000, 2000, or 5000 psi. In some embodiments, the operating pressure of said water removal unit is at least about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, 500, 1000, 2000, or 5000 psi. In some embodiments, the operating pressure of said reverse osmosis system is at least about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, WSGR Docket No.50741-726.601 500, 1000, 2000, or 5000 psi.
  • the transmembrane pressure of the semi- permeable membrane in the water removal unit is at least about 1, 5, 10, 15, 20, 30, 40, 50, 100, 200, 500, 1000, 2000, or 5000 psi.
  • the transmembrane pressure (the pressure across the semi-permeable membrane) of each of the one or more semi- permeable membranes in the water removal unit is from about 0 to about 1 psi, from about 1 to about 5 psi, from about 5 to about 10 psi, from about 10 to about 20 psi, from about 20 to about 50 psi, from about 50 to about 100 psi, from about 100 to about 150 psi, from about 150 to about 200 psi, from about 200 to about 300 psi, from about 300 to about 500 psi, from about 500 to about 750 psi, from about 750 to about 1000 psi, or from about 1000 to about 2000 psi.
  • the flux of each of the one or more semi-permeable membranes in the water removal unit is from about 0 to about 1 gallons per square foot per day (abbreviated gfd), from about 1 to about 5 gfd, from about 5 to about 10 gfd, from about 10 to about 20 gfd, from about 20 to about 50 gfd, from about 50 to about 100 gfd, from about 100 to about 150 gfd, from about 150 to about 200 gfd, from about 200 to about 300 gfd, from about 300 to about 500 gfd, from about 500 to about 750 gfd, from about 750 to about 1000 gfd, or from about 1000 to about 2000 gfd.
  • gfd gallons per square foot per day
  • the flux through said membrane varies with transmembrane pressure.
  • any one or more of the operating parameters of the water removal unit including but not limited to transmembrane pressure, feed flow rate, salinity, salt-rejection, water recovery, and any other operating parameter, is controlled to increase flux across the semi-permeable membrane, increase membrane life, improve permeate quality, maximize reject concentration, or a combination thereof.
  • an energy recovery device is used to recover the energy of the high-pressure stream when this stream is depressurized, and said energy is used to pressurize the inlet stream into the unit comprising the semi-permeable membrane.
  • an energy recovery device is used to recover the energy of the high-pressure stream when this stream is depressurized, and said energy is used to pressurize the inlet stream into the unit comprising the reverse osmosis membrane.
  • the pressurized synthetic lithium solution generate by the lithium extraction system is directly fed into the water removal unit, and this pressure is used to provide at least a portion of the pressure required for water removal.
  • the water content of an eluate or other aqueous stream is lowered by employing a mechanical vapor recompression system.
  • the water content of an eluate or other aqueous stream is lowered by employing a multiple effects evaporator.
  • the water content of an eluate or other aqueous stream is WSGR Docket No.50741-726.601 lowered by employing an evaporation pond.
  • an evaporation pond is an open vessel or depression configured to expose a liquid solution to air currents and optionally sunlight for the purpose of lowering the water content of the liquid solution.
  • the water content of an eluate or other aqueous stream is lowered by distillation of water from the eluate or other aqueous stream. In some embodiments, distillation involves the evaporation, condensation and collection of water from a liquid solution.
  • the water content of a eluate or other aqueous stream is lowered by heating the eluate or other aqueous stream. In some embodiments, heating of an eluate or other aqueous stream may optionally involve boiling the eluate or other aqueous stream.
  • a water removal unit is configured to lower the water content of an eluate or other aqueous stream. In some embodiments, the water content of an eluate or other aqueous stream is lowered by employing a mechanical vapor recompression system. In some embodiments, the water content of an eluate or other aqueous stream is lowered by employing a multiple effects evaporator.
  • the water content of an eluate or other aqueous stream is lowered by employing an evaporation pond.
  • an evaporation pond is an open vessel or depression configured to expose a liquid solution to air currents and optionally sunlight for the purpose of lowering the water content of the liquid solution.
  • the water content of an eluate or other aqueous stream is lowered by distillation of water from the eluate or other aqueous stream.
  • distillation involves the evaporation, condensation and collection of water from a liquid solution.
  • the water content of a eluate or other aqueous stream is lowered by heating the eluate or other aqueous stream.
  • heating of an eluate or other aqueous stream may optionally involve boiling the eluate or other aqueous stream.
  • a water removal unit is configured to affect the temperature of the eluate or other aqueous stream as its water content is being lowered.
  • the eluate or other aqueous stream is at a temperature of -20 to 150 ⁇ C when its water content is being lowered.
  • the eluate or other aqueous stream is at a temperature of -20 to 120 ⁇ C when its water content is being lowered.
  • the eluate or other aqueous stream is at a temperature of -20 to 100 ⁇ C when its water content is being lowered.
  • the eluate or other aqueous stream is at a temperature of -20 to 80 ⁇ C when its water content is being lowered. In some embodiments, the eluate or other aqueous stream is at a temperature of 0 to 150 ⁇ C when its water content is being lowered. In some embodiments, the eluate or other aqueous stream is at a temperature of 20 to 150 ⁇ C WSGR Docket No.50741-726.601 when its water content is being lowered. In some embodiments, the eluate or other aqueous stream is at a temperature of 40 to 120 ⁇ C when its water content is being lowered.
  • the eluate or other aqueous stream is at a temperature of 40 to 100 ⁇ C when its water content is being lowered.
  • the system where the water content of the eluate or other aqueous stream is lowered comprises one or more crystallization systems.
  • a water removal unit comprises one or more crystallization systems.
  • said one or more crystallization systems comprise a crystallizer.
  • said one or more crystallization systems comprise an evaporative crystallizer.
  • the crystallizers are heated.
  • the crystallizers are insulated.
  • the crystallizers are agitated tanks.
  • the crystallizers are mechanical vapor recompression units.
  • the crystallizers comprise one or more draft tube baffle crystallizers, which independently comprise an agitator, a center tube, and a cylindrical baffle to allow clarified liquor to be withdrawn and thicken the operating slurry magma density.
  • only one crystallizer is present in the system.
  • two crystallizers in series are present in the system.
  • three crystallizers in series are present in the system.
  • four crystallizers in series are present in the system.
  • five or more crystallizers are present in the system.
  • acid, a base, or a combination thereof are added to said crystallizers.
  • solids crystallize in said crystallizer.
  • solids are removed from said crystallizers.
  • said solids are removed continuously, semi-continuously, in batches, or a combination thereof.
  • solids are removed from the bottom, the top, or the middle of the crystallizer.
  • said solids are removed from a specially designed section of said crystallizer.
  • liquids are removed from said crystallizers.
  • said liquids are removed continuously, semi-continuously, in batches, or a combination thereof.
  • liquids are removed from the bottom, the top, or the middle of the crystallizer.
  • a water removal unit is configured to provide a concentrated lithium solution.
  • a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is one of the products generated by lowering the water content WSGR Docket No.50741-726.601 of a eluate or other aqueous stream.
  • a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) has a higher lithium concentration than the eluate or other aqueous stream from which it was generated.
  • a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) has a higher sodium concentration than the eluate or other aqueous stream from which it was generated.
  • a concentrated eluate or other aqueous stream e.g., a concentrated lithium solution
  • a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) has a higher chloride concentration than the eluate or other aqueous stream from which it was generated.
  • a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) has a higher carbonate concentration than the eluate or other aqueous stream from which it was generated.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is greater than about 1000.0 milligrams per liter and less than about 30000 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 100 milligrams per liter and less than about 500 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 500 milligrams per liter and less than about 1000 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is greater than about 1000 milligrams per liter and less than about 5000 milligrams per liter. In some embodiments the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 5000 milligrams per liter and less than about 10000 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 10000 milligrams per liter and less than about 50000 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is greater than about 50000 milligrams per liter and less than about 100000 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater WSGR Docket No.50741-726.601 than about 100000 milligrams per liter and less than about 200000 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is greater than about 200000 milligrams per liter and less than about 300000 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 300000 milligrams per liter and less than about 500000 milligrams per liter. [0525] In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 1000.0 milligrams per liter and less than about 30000 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 100 milligrams per liter and less than about 500 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 500 milligrams per liter and less than about 1000 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream is greater than about 1000 milligrams per liter and less than about 5000 milligrams per liter. In some embodiments the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 5000 milligrams per liter and less than about 10000 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 10000 milligrams per liter and less than about 50000 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream is greater than about 50000 milligrams per liter and less than about 100000 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 100000 milligrams per liter and less than about 200000 milligrams per liter. In some embodiments the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 200000 milligrams per liter and less than about 300000 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream e.g., a concentrated lithium solution
  • WSGR Docket No.50741-726.601 is greater than about 300000 milligrams per liter and less than about 500000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is greater than about 1000.0 milligrams per liter and less than about 30000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 100 milligrams per liter and less than about 500 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 500 milligrams per liter and less than about 1000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is greater than about 1000 milligrams per liter and less than about 5000 milligrams per liter. In some embodiments the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 5000 milligrams per liter and less than about 10000 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 10000 milligrams per liter and less than about 50000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is greater than about 50000 milligrams per liter and less than about 100000 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 100000 milligrams per liter and less than about 200000 milligrams per liter. In some embodiments the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is greater than about 200000 milligrams per liter and less than about 300000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is greater than about 300000 milligrams per liter and less than about 500000 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is at least about 1000.0 milligrams per liter and at most about 30000 milligrams per liter.
  • the concentration of WSGR Docket No.50741-726.601 lithium in a concentrated eluate or other aqueous stream is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 100 milligrams per liter and at most about 500 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is at least about 500 milligrams per liter and at most about 1000 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 1000 milligrams per liter and at most about 5000 milligrams per liter. In some embodiments the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 5000 milligrams per liter and at most about 10000 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is at least about 10000 milligrams per liter and at most about 50000 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 50000 milligrams per liter and at most about 100000 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 100000 milligrams per liter and at most about 200000 milligrams per liter.
  • the concentration of lithium in a concentrated eluate or other aqueous stream is at least about 200000 milligrams per liter and at most about 300000 milligrams per liter. In some embodiments, the concentration of lithium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 300000 milligrams per liter and at most about 500000 milligrams per liter. [0528] In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 1000.0 milligrams per liter and at most about 30000 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 100 milligrams per liter and at most about 500 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream is at least WSGR Docket No.50741-726.601 about 500 milligrams per liter and at most about 1000 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 1000 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream is at least about 5000 milligrams per liter and at most about 10000 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 10000 milligrams per liter and at most about 50000 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 50000 milligrams per liter and at most about 100000 milligrams per liter.
  • the concentration of sodium in a concentrated eluate or other aqueous stream is at least about 100000 milligrams per liter and at most about 200000 milligrams per liter. In some embodiments the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 200000 milligrams per liter and at most about 300000 milligrams per liter. In some embodiments, the concentration of sodium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 300000 milligrams per liter and at most about 500000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is at least about 1000.0 milligrams per liter and at most about 30000 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 100 milligrams per liter and at most about 500 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is at least about 500 milligrams per liter and at most about 1000 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 1000 milligrams per liter and at most about 5000 milligrams per liter. In some embodiments the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 5000 milligrams per liter and at most about 10000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is at least about 10000 milligrams per liter and at most about 50000 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 50000 milligrams per liter and at most about 100000 milligrams per liter.
  • the concentration of potassium in a concentrated eluate or other aqueous stream is at least about 100000 milligrams per liter and at most about 200000 milligrams per liter. In some embodiments the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 200000 milligrams per liter and at most about 300000 milligrams per liter. In some embodiments, the concentration of potassium in a concentrated eluate or other aqueous stream (e.g., a concentrated lithium solution) is at least about 300000 milligrams per liter and at most about 500000 milligrams per liter.
  • solid salts are generated in the course of lowering the water content of an eluate or other aqueous stream. In some embodiments, solid salts are crystallized in the course of lowering the water content of an eluate or other aqueous stream. In some embodiments, the solid salts comprise sodium chloride and potassium chloride. In some embodiments, the solid salts comprise sodium chloride. In some embodiments, the solid salts are essentially free of lithium. In some embodiments, the solid salts are collected for further use. In some embodiments, the solid salts are dissolved in water to yield a solution of solid salts.
  • the solid salts are dissolved in water obtained as a product of lowering the water content of a eluate or other aqueous stream to yield a solution of solid salts.
  • the solid salts comprise less than 1% of carbonate salts.
  • the solid salts comprise at most 1% of carbonate salts.
  • the solid salts contain a negligible amount of carbonate salts.
  • a removal system is used generated solid salts in the course of lowering the water content of a eluate or other aqueous stream.
  • more than one water removal system is used, wherein one removal system produces solids of different type and purity. In some embodiments, multiple removal systems are utilized.
  • a first removal system is utilized to generate solid that is 80% or more sodium chloride by weight of the solid, and a second removal system us utilized to generate a mixture of sodium chloride and potassium chloride in which sodium chloride is present in less than 80% by weight.
  • a first removal system is utilized to generate solid that is 80% or more sodium chloride by weight of the solid, and a second removal system us WSGR Docket No.50741-726.601 utilized to generate a mixture of sodium chloride and potassium chloride in which sodium chloride is present in less than 80% by weight.
  • the methods, processes, and systems disclosed herein comprise a liquid-solid separation method to remove the generated solid salts and separate them from the eluate or other aqueous stream.
  • the eluate or other aqueous stream recovered from the solid salts recovered by said method are recycled to the water removal system.
  • said water removal system is an evaporative crystallizer.
  • the recycling of said eluate or other aqueous stream ensures that any lithium contained within said eluate or other aqueous stream is further recovered when eluate or other aqueous stream is removed from the water removal system.
  • said methods for removal of the solid salts generated comprise filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
  • said method comprises filtration.
  • the filter is a belt filter, filter press, plate- and-frame filter press, recessed-chamber filter press, pressure vessel containing filter elements, candle filter, pressure filter, pressure-leaf filter, Nutsche filter, rotary drum filter, rotary disc filter, cartridge filter, bag filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforated basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a decanter centrifuge, or a pusher centrifuge.
  • the filter uses a scroll or a vibrating device. In some embodiments, the filter is horizontal, vertical, or may use a siphon. In some embodiments, a liquid-solid separation method is used to collect the solids salts for further use. In some embodiments, the method of liquid-solid separation is configured to wash the separated solids. In some embodiments, said solids are washed with water. In some embodiments, said water is recycled into the water removal system such that the water is recovered from said wash water, and reused. [0534] In some embodiments, the solids salts comprise sodium chloride. In some embodiments, the solids salts comprise potassium chloride. In some embodiments, the solids salts comprise a mixture of sodium chloride and potassium chloride.
  • the solids salts comprise lithium chloride.
  • the purity of the solid salts on a mass basis is greater than 50%, greater than 60%, greater than 70%, greater than 80%, greater than 90%, greater than 95%, greater than 99%, greater than 99.5 %, or greater than 99.9 %.
  • the purity of the solid salts on a mass basis is at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 99%, at least 99.5 %, or at least 99.9 %.
  • WSGR Docket No.50741-726.601 [0535]
  • said solids salt are recovered and used in a separate process.
  • a solution of solid salts is used as a chemical precursor for generating acid and base. In some embodiments, a solution of solid salts is used as a chemical precursor for generating hydrochloric acid and sodium hydroxide. In some embodiments, a solution of solid salts is further purified and used as a chemical precursor for generating hydrochloric acid and sodium hydroxide. In some embodiments, a solution of solid salts is used as a chemical precursor for generating hydrochloric acid, sodium hydroxide, and potassium hydroxide. [0536] In some embodiments, a solution of solid salts is used as an input to a chloralkali plant that generates acid and base.
  • a solution of solid salts is used an input to a chloralkali plant that generates hydrochloric acid and sodium hydroxide. In some embodiments, a solution of solid salts is used as an input to a chloralkali plant that generates hydrochloric acid, sodium hydroxide, and potassium hydroxide. In some embodiments, a chloralkali plant comprises a system for electrolysis of an aqueous solution containing sodium and chloride to generate chlorine, hydrogen, and sodium hydroxide. In some embodiments, a chloralkali plant comprises a system for electrolysis of an aqueous solution containing sodium, potassium, and chloride to generate chlorine, hydrogen, potassium hydroxide and sodium hydroxide.
  • a chloralkali plant comprises a unit that promotes conversion of chlorine and hydrogen gases into hydrochloric acid.
  • the hydrochloric acid generated by a chloralkali plant is used as a reagent in lithium-selective ion exchange processes.
  • the sodium hydroxide generated by a chloralkali plant is used as a reagent in lithium-selective ion exchange processes.
  • the potassium hydroxide generated by a chloralkali plant is used as a reagent in lithium- selective ion exchange processes.
  • a solution of solid salts is used as an input to a plant that generates acid and base.
  • a said plant comprises a 3-compartment bipolar electrodialysis plant. In some embodiments, said plant comprises a 2-compartment bipolar electrodialysis plant. In some embodiments, said plant comprises a multiple electrodialysis circuits. In some embodiments, said plant comprises an electrolysis cell.
  • Embodiments for Limiting or Eliminating Precipitation of Impurities in the Eluate Solution [0538] In one embodiment, lithium and non-lithium impurities are absorbed from a lithium resource into an ion exchange material. In one embodiment, lithium and non-lithium impurities are eluted from an ion exchange material into an acidic solution.
  • lithium WSGR Docket No.50741-726.601 and non-lithium impurities are eluted from an ion exchange material into an acidic solution containing dissolved species that may precipitate at certain concentrations.
  • lithium and non-lithium impurities are eluted from an ion exchange material into an acidic solution containing dissolved species that are reduced in concentration to avoid precipitation.
  • lithium and non-lithium impurities are eluted from an ion exchange material into an acidic solution where said non-lithium impurities precipitate at certain concentrations.
  • lithium and multivalent impurities are absorbed from a lithium resource into an ion exchange material.
  • lithium and multivalent impurities are eluted from an ion exchange material into an acidic solution. In one embodiment, lithium and multivalent impurities are eluted from an ion exchange material into an acidic solution containing carbonate anions. In one embodiment, lithium and multivalent impurities are eluted from an ion exchange material into an acidic solution containing carbonate anions such that the multivalent impurities and carbonate anions may react to form insoluble salts that can precipitate. In one embodiment, lithium and multivalent impurities are eluted from an ion exchange material into a solution containing carbonate anions such that the multivalent impurities and carbonate anions that may react to form insoluble salts that can precipitate.
  • lithium and multivalent cations are eluted from an ion exchange material into a solution containing carbonate anions wherein the concentrations of carbonate anions and multivalent cations are limited to avoid precipitation of insoluble carbonate compounds.
  • lithium and multivalent cations are eluted from an ion exchange material into a solution containing carbonate anions wherein the concentrations of multivalent cations are limited to avoid precipitation of insoluble carbonate compounds.
  • lithium and multivalent cations are eluted from an ion exchange material into a solution containing carbonate anions wherein the concentrations of multivalent cations are limited using nanofiltration to avoid precipitation of insoluble carbonate compounds.
  • lithium and multivalent cations are eluted from a first ion exchange material into a solution containing carbonate anions wherein the concentrations of multivalent cations are decreased using a second ion exchange material to avoid precipitation of insoluble carbonate compounds.
  • lithium and multivalent cations are eluted from a first ion exchange material into a solution containing carbonate anions wherein the concentrations of multivalent cations are limited using a second ion exchange material that is selective for multivalent cations to avoid precipitation of insoluble carbonate compounds.
  • lithium and multivalent cations are eluted from an ion exchange material into a solution containing carbonate anions wherein the concentrations of multivalent cations are decreased to avoid precipitation of insoluble carbonate compounds.
  • lithium and multivalent cations are eluted from an ion exchange material into a solution containing carbonate anions and the concentration of multivalent cations in the carbonate solution is decreased to avoid precipitation of insoluble carbonate compounds.
  • a carbonate solution is contacted with an ion exchange material to elute lithium along with impurities, the carbonate solution is processed to reduce the concentration of impurities, and the carbonate solution is again contacted with an ion exchange material to elute more lithium along with impurities.
  • a carbonate solution is contacted with an ion exchange material to elute lithium along with impurities, the carbonate solution is processed to reduce the concentration of multivalent cations, and the carbonate solution is again contacted with an ion exchange material to elute more lithium along with impurities.
  • a carbonate solution is contacted with an ion exchange material to elute lithium along with impurities, the carbonate solution is processed to reduce the concentration of multivalent cations, the carbonate solution is again contacted with an ion exchange material to elute more lithium along with impurities, and the concentration of multivalent cations is maintained at a sufficiently low level to avoid precipitation of insoluble salts.
  • a carbonate solution is contacted with an ion exchange material to elute a target metal along with impurities, the carbonate solution is processed to reduce the concentration of impurities, and the carbonate solution is again contacted with an ion exchange material to elute more of the target metal along with impurities.
  • a carbonate solution is contacted with an ion exchange material to elute a target metal along with impurities, the carbonate solution is processed to reduce the concentration of multivalent cations, and the carbonate solution is again contacted with an ion exchange material to elute more of the target metal along with impurities.
  • a carbonate solution is contacted with an ion exchange material to elute a target metal along with impurities, the carbonate solution is processed to reduce the concentration of multivalent cations, the carbonate solution is again contacted with an ion exchange material to elute more of the target metal along with impurities, and the concentration of multivalent cations is maintained at a sufficiently low level to avoid precipitation of insoluble salts.
  • an acidic carbonate solution is contacted with an ion exchange material to elute lithium along with impurities, the acidic carbonate solution is processed to WSGR Docket No.50741-726.601 reduce the concentration of impurities, and the acidic carbonate solution is again contacted with an ion exchange material to elute more lithium along with more impurities.
  • the pH of the acidic carbonate solution is regulated to control elution of lithium and/or impurities.
  • pH of the acidic carbonate solution is regulated by measuring pH with a pH probe and adding sulfuric acid and/or a solution containing sulfuric acid to the acidic carbonate solution.
  • pH of the acidic carbonate solution is regulated adding sulfuric acid and/or a solution containing sulfuric acid to the acidic carbonate solution.
  • the carbonate solution used to elute lithium from the ion exchange material is replaced with a different solution.
  • the carbonate solution used to elute lithium from the ion exchange material is replaced with a solution comprising carbonate, nitrate, phosphate, chloride, bromide, fluoride, borate, iodide, carbonate, or combinations thereof.
  • a solution comprising anions is contacted with an ion exchange material to elute lithium along with impurities, the solution is processed to reduce the concentration of impurities, and the solution is again contacted with an ion exchange material to elute more lithium along with impurities, where the anions are selected from a list including carbonate, nitrate, phosphate, chloride, bromide, fluoride, borate, iodide, carbonate, or combinations thereof.
  • a fluidized bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution to avoid the formation of precipitates.
  • a fluidized bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic carbonate solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution to avoid the formation of carbonate precipitates.
  • a fluidized bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic solution to WSGR Docket No.50741-726.601 elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the fluidized bed to a unit for removing multivalent impurities before the acidic solution is returned to the fluidized bed.
  • a fluidized bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the fluidized bed to a nanofiltration unit for selective removal of multivalent impurities, and then the acidic solution is returned to the fluidized bed.
  • a fluidized bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the fluidized bed to a second ion exchange unit containing a second ion exchange material that is selective for removing multivalent impurities, and then the acidic solution is returned to the fluidized bed.
  • a fluidized bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the fluidized bed to a unit for removing multivalent impurities before the acidic solution is passed to a second fluidized bed of ion exchange material for elution of more lithium into the acidic solution.
  • a fluidized bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the fluidized bed to a nanofiltration unit for selective removal of multivalent impurities, and then the acidic solution is passed to a second fluidized bed of ion exchange material for elution of more lithium into the acidic solution.
  • a fluidized bed of ion WSGR Docket No.50741-726.601 exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the fluidized bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the fluidized bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the fluidized bed to a second ion exchange unit containing a second ion exchange material that is selective for removing multivalent impurities, and then the acidic solution is passed to a second fluidized bed of ion exchange material for elution of more lithium into the acidic solution.
  • the acidic solution flows through multiple fluidized beds of ion exchange material for elution of lithium and impurities, and impurities are removed from the acidic solution between the multiple fluidized beds.
  • the acidic solution flows through multiple fluidized beds of ion exchange material for elution of lithium and impurities, and impurities are removed from the acidic solution between the multiple fluidized beds using nanofiltration.
  • the acidic solution flows through multiple fluidized beds of a first ion exchange material which is lithium-selective for elution of lithium and impurities, and impurities are removed from the acidic solution between the multiple fluidized beds using a second ion exchange material that is selective for multivalent ions.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution to avoid the formation of precipitates.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic carbonate solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution to avoid the formation of carbonate precipitates.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic WSGR Docket No.50741-726.601 solution by circulating the acidic solution from the packed bed to a unit for removing multivalent impurities before the acidic solution is returned to the packed bed.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the packed bed to a nanofiltration unit for selective removal of multivalent impurities, and then the acidic solution is returned to the packed bed.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the packed bed to a second ion exchange unit containing a second ion exchange material that is selective for removing multivalent impurities, and then the acidic solution is returned to the packed bed.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the packed bed to a unit for removing multivalent impurities before the acidic solution is passed to a second packed bed of ion exchange material for elution of more lithium into the acidic solution.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the packed bed to a nanofiltration unit for selective removal of multivalent impurities, and then the acidic solution is passed to a second packed bed of ion exchange material for elution of more lithium into the acidic solution.
  • a packed bed of ion exchange material is contacted with brine to absorb lithium from the brine into the ion WSGR Docket No.50741-726.601 exchange material, the packed bed of ion exchange material is optionally washed to remove residual brine from the ion exchange material, the packed bed of ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and multivalent impurities are removed from the acidic solution by circulating the acidic solution from the packed bed to a second ion exchange unit containing a second ion exchange material that is selective for removing multivalent impurities, and then the acidic solution is passed to a second packed bed of ion exchange material for elution of more lithium into the acidic solution.
  • the acidic solution flows through multiple packed beds of ion exchange material for elution of lithium and impurities, and impurities are removed from the acidic solution between the multiple packed beds.
  • the acidic solution flows through multiple packed beds of ion exchange material for elution of lithium and impurities, and impurities are removed from the acidic solution between the multiple packed beds using nanofiltration.
  • the acidic solution flows through multiple packed beds of a first ion exchange material which is lithium-selective for elution of lithium and impurities, and impurities are removed from the acidic solution between the multiple packed beds using a second ion exchange material that is selective for multivalent ions.
  • the packed beds are partially or occasionally fluidized. In some embodiments, the fluidized beds are partially or occasionally packed. In some embodiments, the packed or fluidized beds are washed before and/or after contracting with brine and/or acid using water or washing solutions containing water, salt, chelating compounds, ethylenediaminetetraacetic acid, salt of ethylenediaminetetraacetate, compounds of ethylenediaminetetraacetate, and/or anti-scalants.
  • the acidic solution used to elute lithium from the lithium-selective ion exchange material contains water, salt, chelating compounds, ethylenediaminetetraacetic acid, salt of ethylenediaminetetraacetate, compounds of ethylenediaminetetraacetate, and/or anti-scalants.
  • dilution water is used to limit and/or prevent formation of insoluble precipitates.
  • multivalent impurities are removed from a lithium salt solution using precipitation.
  • multivalent impurities are removed from a lithium salt solution using precipitation through addition of base.
  • multivalent impurities are removed from a lithium salt solution using precipitation through addition of sodium hydroxide, sodium carbonate, and/or other compounds.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from WSGR Docket No.50741-726.601 the selective ion exchange material, and the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, more protons are added to the acidic solution, and the acidic solution is again contacted with the lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, more acid is added to the acidic solution, and the acidic solution is again contacted with the lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution in a first vessel, more protons are added to the acidic solution, and the acidic solution is again contacted with lithium selective ion exchange material to elute more lithium into the acidic solution in a second vessel.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution in a vessel, more protons are added to the acidic solution, and the acidic solution is again contacted with lithium selective ion exchange material to elute more lithium into the acidic solution in the vessel.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed from the WSGR Docket No.50741-726.601 acidic solution, more protons are added to the acidic solution, and the acidic solution is again contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, more protons are added to the acidic solution, impurities are removed from the acidic solution, and the acidic solution is again contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed from the acidic solution using nanofiltration or multivalent-selective ion exchange materials, more protons are added to the acidic solution, and the acidic solution is again contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, more protons are added to the acidic solution, impurities are removed from the acidic solution using nanofiltration or multivalent-selective ion exchange materials, and the acidic solution is again contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • an acidic solution is contacted with a lithium selective ion exchange material that has previously been loaded with lithium by contacting the lithium selective ion exchange material with a liquid resource, the acidic solution is treated to remove multivalent impurities, and the acidic solutions is again contacted with a lithium selective ion exchange material that has previously been loaded with lithium by contacting the lithium selective ion exchange material with a liquid resource.
  • an acidic solution is contacted with a lithium selective ion exchange material to elute lithium, the acidic solution is treated to remove multivalent impurities, and the acidic solutions is again contacted WSGR Docket No.50741-726.601 with a lithium selective ion exchange material to elute lithium.
  • an acidic solution is contacted with a lithium selective ion exchange material to elute lithium, the acidic solution is treated to remove multivalent impurities, more protons are added to the acidic solution, and the acidic solutions is again contacted with a lithium selective ion exchange material to elute lithium.
  • an acidic solution is contacted with a lithium selective ion exchange material to elute lithium, more protons are added to the acidic solution, the acidic solution is treated to remove multivalent impurities, and the acidic solutions is again contacted with a lithium selective ion exchange material to elute lithium.
  • an acidic solution is contacted with a lithium selective ion exchange material to elute lithium in a vessel, the acidic solution is treated to remove multivalent impurities, and the acidic solutions is contacted with a lithium selective ion exchange material to elute lithium in said vessel.
  • an acidic solution is contacted with a lithium selective ion exchange material to elute lithium in a first vessel, the acidic solution is treated to remove multivalent impurities, and the acidic solutions is contacted with a lithium selective ion exchange material to elute lithium in a second vessel.
  • multivalent impurities are removed with a multivalent cation selective ion exchange material.
  • multivalent impurities are removed using nanofiltration membranes.
  • the lithium selective ion exchange materials is in a tank, a column, or a stirred tank reactor. In some embodiments, the lithium selective ion exchange material is in a fixed or fluidized bed.
  • an acidic solution is flowed through multiple vessels loaded with a lithium selective ion exchange material to elute lithium. In some embodiments, an acidic solution is flowed through multiple vessels loaded with a lithium selective ion exchange material to elute lithium and multivalent cation impurities are removed between the vessels. In some embodiments, an acidic solution is flowed through multiple vessels loaded with a lithium selective ion exchange material to elute lithium.
  • an acidic solution is flowed through multiple vessels loaded with a lithium selective ion exchange material to elute lithium, multivalent cation impurities are removed between the multiple vessels, and more protons are added to the acid solution between the multiple vessels.
  • an acidic solution is recirculated through a vessel loaded a lithium selective ion exchange material to elute lithium.
  • an acidic solution is recirculated through a vessel loaded a lithium selective ion exchange material to elute lithium and multivalent cation impurities are removed between the recirculations.
  • an acidic solution is recirculated through a vessel loaded a lithium selective ion exchange material to elute lithium, WSGR Docket No.50741-726.601 multivalent cation impurities are removed between the recirculations, and more protons are added to the acid solution between the recirculations.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, and the acidic solution is prepared in an acidic solution mixing unit.
  • the acidic solution mixing unit is a tank, an in-line mixing device, a stirred tank reactor, another mixing unit, or combinations thereof.
  • the acid solution mixing tank is used to service one vessel containing lithium selective ion exchange material.
  • the acid solution mixing tank is used to service multiple vessels containing lithium selective ion exchange material in parallel or series. In one embodiment, the acid solution mixing tank is used to service multiple vessels containing lithium selective ion exchange material in sequence.
  • the acidic solution is comprised of sulfuric acid, phosphoric acid, hydrochloric acid, hydrobromic acid, carbonic acid, nitric acid, or combinations thereof.
  • lithium is eluted from a lithium selective ion exchange material using sulfuric acid, phosphoric acid, hydrochloric acid, nitric acid, or combinations thereof.
  • lithium is eluted from a lithium selective ion exchange material using an acid solution comprising carbonate, phosphate, nitrate, borate, or combinations thereof.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed using a combination of nanofiltration, multivalent cation selective ion exchange material, other methods of removing multivalent impurities, or combinations thereof.
  • impurities are removed from an acidic lithium solutions using combinations of nanofiltration, multivalent cation selective ion exchange material, other methods of removing multivalent impurities in parallel, series, or combinations thereof.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted WSGR Docket No.50741-726.601 with an acidic solution to elute lithium into the acidic solution, impurities are removed from the acidic solution using nanofiltration membrane units arranged in series and/or parallel, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • anti-scalants, chelants, or other means of anti-scaling are used to avoid scaling in the nanofiltration membrane units.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed from the acidic solution using multivalent cation selective ion exchange materials, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed from the acidic solution using multivalent cation selective ion exchange material in a packed bed, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed from the acidic solution using multivalent cation selective ion exchange material arranged in a network of columns, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic WSGR Docket No.50741-726.601 solution, impurities are removed from the acidic solution using multivalent cation selective ion exchange material arranged in a network of columns with a first absorption column position for absorbing impurities and a last absorption column position for absorbing trace amounts of impurities, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed from the acidic solution using multivalent cation selective ion exchange material arranged in a lead-lag configuration, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a multivalent cation selective ion exchange material is arranged in a variation of a lead-lag setup.
  • a multivalent cation selective ion exchange material is eluted using a second acidic solution. In one embodiment, a multivalent cation selective ion exchange material is eluted using hydrochloric acid. In one embodiment, a multivalent cation selective ion exchange material is regenerated using sodium hydroxide. In one embodiment, a multivalent cation selective ion exchange material is operated in stirred tank reactors, fluidized beds, or packed beds arranged in series and/or parallel. In one embodiment, a lithium selective ion exchange material is operated in stirred tank reactors, fluidized beds, or packed beds arranged in series and/or parallel.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are removed from the acidic solution by adding phosphate to precipitate phosphate compounds, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium WSGR Docket No.50741-726.601 into the acidic solution, impurities are removed from the acidic solution by adding phosphoric acid to precipitate phosphate compounds, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, Ca, Mg, Sr, and/or Ba are removed from the acidic solution by adding phosphoric acid to precipitate Ca, Mg, Sr, and/or Ba phosphate compounds, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, multivalent impurities are precipitated from the acidic solution by adding oxalate, oxalic acid, citrate, citric acid, or combinations thereof, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, multivalent impurities are precipitated from the acidic solution by adding a precipitant comprising oxalate, oxalic acid, citrate, citric acid, or combinations thereof, the precipitant concentration is decreased by adding cations to the acidic solution, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted WSGR Docket No.50741-726.601 with an acidic solution to elute lithium into the acidic solution, multivalent impurities are precipitated and removed from the acidic solution by adding oxalate, oxalate anions are precipitated and removed from the acidic solution by adding zinc, iron, manganese, other transition metals, other cations, or combinations thereof, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, multivalent impurities are precipitated and removed from the acidic solution by adding citrate, citrate anions are precipitated and removed from the acidic solution by adding cations, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, cation impurities are precipitated from the acidic solution by adding anion precipitants, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, cation impurities are precipitated and removed from the acidic solution by adding anion precipitants, the anions precipitants are precipitated and removed from the acidic solution by adding cation precipitants, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from WSGR Docket No.50741-726.601 the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are precipitated by temporarily reducing the temperature of the acidic solution, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are precipitated by changing the temperature of the acidic solution, more protons are added to the acidic solution, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a lithium selective ion exchange material is contacted with a liquid resource to load lithium onto the lithium selective ion exchange material, the lithium selective ion exchange material is optionally washed to remove residual liquid resource from the selective ion exchange material, the lithium selective ion exchange material is contacted with an acidic solution to elute lithium into the acidic solution, impurities are precipitated by decreasing the temperature of the acidic solution, protons are added to the acidic solution and the acidic solution is heated or allowed to warm, and the acid solutions is contacted with lithium selective ion exchange material to elute more lithium into the acidic solution.
  • a chelating agent or anti-scalant is used to form a soluble complex to avoid precipitation in an acidic lithium solution. In one embodiment, a chelating agent or anti-scalant is used to form a soluble complex to avoid or redissolve precipitates.
  • a chelating agent or anti-scalants is used to limit or reduce precipitation of multivalent cations and the chelating agent or antiscalant is selected from the list of ethylenediaminetetraacetic acid (EDTA), disodium EDTA, calcium disodium EDTA, tetrasodium EDTA, citric acid, maleic acid, silicate compounds, amorphous silicate compounds, crystalline layered silicate compounds, phosphonic acid compounds, aminotris(methylenephosphonic acid) (ATMP), nitrilotrimethylphosphonic acid (NTMP), ethylenediamine tetra(methylene phosphonic acid) (EDTMP), diethylenetriamine penta(methylene phosphonic acid) (DTPMP), polyphosphonate, polyacrylate, polyacrylic acid, nitrilotriacetic acid (NTA), sodium hexametaphosphate (SHMP), or combinations thereof.
  • EDTA ethylenediaminetetraacetic acid
  • NTA
  • a threshold inhibitor is used to block development of nuclei in an acidic lithium solution.
  • a retarded is used to block the growth of precipitates in WSGR Docket No.50741-726.601 an acidic lithium solution.
  • compounds are used to limit, control, eliminate, or redissolve precipitates including phosphinopolycarboxylic acid, sulfonated polymer, polyacrylic acid, p-tagged sulfonated polymer, diethylenetriamine penta, bis-hexamethylene triamine, compounds thereof, modifications thereof, or combinations thereof.
  • the acidic solution comprises lithium carbonate, lithium hydrogen carbonate, sulfuric acid, or combinations thereof.
  • the acidic solution comprises lithium carbonate, lithium hydrogen carbonate, sulfuric acid, lithium chloride, hydrochloric acid, lithium nitrate, nitric acid, lithium phosphate, lithium hydrogen phosphate, lithium dihydrogen phosphate, phosphoric acid, lithium bromide, bromic acid, or combinations thereof.
  • lithium and other metals are recovered from the liquid resource. In some embodiments, the methods described for lithium recovery are applied to recover other metals.
  • compositions of eluates produced by lithium extraction from a liquid resource using ion exchange [0572] Lithium extraction via any of the aforementioned methods produces an eluate enriched in lithium, whereby the majority of impurities in the liquid resource are rejected and a purified lithium stream is produced.
  • the eluate enriched in lithium is alternatively described as an eluate, a lithium eluate, a synthetic lithium solution, or a concentrated synthetic lithium solution.
  • the concentrated lithium solution is an aqueous solution comprising lithium and other dissolved ions, and is donated as an eluate.
  • Said eluate is produced by treatment of an ion exchange material that has absorbed lithium with an acidic eluent to produce an eluent.
  • Said eluent is acidic and contains lithium in combination with other cations and anions that are present in the liquid resource from which lithium is extracted.
  • Said eluent can be contacted with ion exchange material in one or more of the aforementioned ion exchange vessels to produce an eluate.
  • Said eluate is stored in one or more different vessels that are part of an ion exchange network.
  • the concentration of lithium and other ions in solution vary depending on the liquid resource from which lithium is extracted.
  • the eluate is produced by contacting the lithiated ion exchange materials with an acidic solution which comprises sulfuric acid, phosphoric acid, hydrochloric acid, hydrobromic acid, carbonic acid, nitric acid, or combinations thereof.
  • an acidic solution which comprises sulfuric acid, phosphoric acid, hydrochloric acid, hydrobromic acid, carbonic acid, nitric acid, or combinations thereof.
  • lithium is eluted from a lithium selective ion WSGR Docket No.50741-726.601 exchange material using sulfuric acid, phosphoric acid, hydrochloric acid, nitric acid, or combinations thereof.
  • lithium is eluted from a lithium selective ion exchange material using an acid solution comprising sulfate, phosphate, nitrate, borate, or combinations thereof.
  • Exemplary embodiments of the present disclosure include compositions of the concentrated lithium eluate produced by contacting an acid with an ion exchange material lithiated by lithium from a liquid resource.
  • the concentrated lithium solution contains other ions, comprising but not limited to one or more ions of lithium, sodium, calcium, magnesium, potassium, boron, strontium, barium, zirconium, titanium, vanadium, iron, copper, manganese, molybdenum, aluminum, niobium, sulfate, chloride, fluoride, bromide, nitrate, carbonate, bicarbonate, hydrogencarbonate, phosphate, borate, mixtures thereof or combinations thereof.
  • the concentration of lithium is greater than about 200.0 milligrams per liter and less than about 8000 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 200 milligrams per liter and less than about 4000 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 2000 milligrams per liter and less than about 8000 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 200 milligrams per liter and less than about 1000 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 200 milligrams per liter and less than about 500 milligrams per liter.
  • the concentration of lithium is greater than about 1000 milligrams per liter and less than about 4000 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 1000.0 milligrams per liter and less than about 2000.0 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 2000.0 milligrams per liter and less than about 3000.0 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 3000.0 milligrams per liter and less than about 4000.0 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 4000.0 milligrams per liter and less than about 5000.0 milligrams per liter.
  • the concentration of lithium is greater than about 5000.0 milligrams per liter and less than about 6000.0 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 6000.0 milligrams per liter and less than about 8000.0 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 8000.0 milligrams per liter and less than about 10000.0 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 10000.0 milligrams per liter and less than about WSGR Docket No.50741-726.601 12000.0 milligrams per liter.
  • the concentration of lithium is greater than about 12000.0 milligrams per liter and less than about 20000.0 milligrams per liter. [0577] In some embodiments, the concentration of lithium depends on the properties of the eluent used to elute lithium and generate an eluate. [0578] In some embodiments, the concentration of lithium is greater than about 0.1 milligrams per liter and less than about 1 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 1 milligrams per liter and less than about 10 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 10 milligrams per liter and less than about 20 milligrams per liter.
  • the concentration of lithium is greater than about 10 milligrams per liter and less than about 50 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 20 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of lithium is greater than about 100 milligrams per liter and less than about 1000 milligrams per liter. [0579] In some embodiments, the concentration of barium is greater than about 0.1 milligrams per liter and less than about 750 milligrams per liter. In some embodiments, the concentration of boron is greater than about 10.0 milligrams per liter and less than about 5000 milligrams per liter.
  • the concentration of calcium is greater than about 10.0 milligrams per liter and less than about 5000 milligrams per liter.
  • the concentration of magnesium is greater than about 10.0 milligrams per liter and less than about 5000 milligrams per liter.
  • the concentration of potassium is greater than about 10.0 milligrams per liter and less than about 5000 milligrams per liter.
  • the concentration of sodium is greater than about 10.0 milligrams per liter and less than about 5000 milligrams per liter.
  • the concentration of strontium is greater than about 10.0 milligrams per liter and less than about 5000 milligrams per liter.
  • the concentration of aluminum is greater than about 0.001 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of copper is greater than about 0.001 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of iron is greater than about 0.001 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of manganese is greater than about 0.001 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of molybdenum is greater than about 0.1 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of WSGR Docket No.50741-726.601 niobium is greater than about 0.001 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of titanium is greater than about 0.001 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of vanadium is greater than about 0.01 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of zirconium is greater than about 0.001 milligrams per liter and less than about 750 milligrams per liter.
  • the concentration of bicarbonate is greater than about 1000.0 milligrams per liter and less than about 30000 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 100 milligrams per liter and less than about 500 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 500 milligrams per liter and less than about 1000 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 1000 milligrams per liter and less than about 5000 milligrams per liter.
  • the concentration of bicarbonate is greater than about 5000 milligrams per liter and less than about 10000 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 10000.0 milligrams per liter and less than about 50000.0 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 50000.0 milligrams per liter and less than about 100000.0 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 100000.0 milligrams per liter and less than about 200000.0 milligrams per liter.
  • the concentration of bicarbonate is greater than about 200000.0 milligrams per liter and less than about 300000.0 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 300000.0 milligrams per liter and less than about 500000.0 milligrams per liter. [0582] In some embodiments, the concentration of bicarbonate is greater than about 0.1 milligrams per liter and less than about 1 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 1 milligrams per liter and less than about 10 milligrams per liter.
  • the concentration of bicarbonate is greater than about 1 milligrams per liter and less than about 20 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 10 milligrams per liter and less than about 50 milligrams per liter. In some embodiments, the concentration of bicarbonate is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some WSGR Docket No.50741-726.601 embodiments, the concentration of bicarbonate is greater than about 100 milligrams per liter and less than about 1000 milligrams per liter. [0583] In some embodiments, the concentration of bicarbonate is dependent on the pH of the solution.
  • bicarbonate is the principal anion contained within the solution. In some embodiments, bicarbonate anions are contained in the lithium eluate when carbon dioxide dissolved in water is used as an eluent. [0584] In some embodiments, the concentration of carbonate is greater than about 1000.0 milligrams per liter and less than about 30000 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 100 milligrams per liter and less than about 500 milligrams per liter.
  • the concentration of carbonate is greater than about 500 milligrams per liter and less than about 1000 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 1000 milligrams per liter and less than about 5000 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 5000 milligrams per liter and less than about 10000 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 10000.0 milligrams per liter and less than about 50000.0 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 50000.0 milligrams per liter and less than about 100000.0 milligrams per liter.
  • the concentration of carbonate is greater than about 100000.0 milligrams per liter and less than about 200000.0 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 200000.0 milligrams per liter and less than about 300000.0 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 300000.0 milligrams per liter and less than about 500000.0 milligrams per liter. [0585] In some embodiments, the concentration of carbonate is greater than about 0.1 milligrams per liter and less than about 1 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 1 milligrams per liter and less than about 10 milligrams per liter.
  • the concentration of carbonate is greater than about 1 milligrams per liter and less than about 20 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 10 milligrams per liter and less than about 50 milligrams per liter. In some embodiments, the concentration of carbonate is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the WSGR Docket No.50741-726.601 concentration of carbonate is greater than about 100 milligrams per liter and less than about 1000 milligrams per liter. [0586] In some embodiments, the concentration of carbonate is dependent on the pH of the solution.
  • carbonate is the principal anion contained within the solution.
  • carbonate anions are contained in the lithium eluate when carbon dioxide dissolved in water is used as an eluent.
  • the lithium eluate comprises dissolved carbon dioxide gas.
  • the concentration of carbon dioxide is greater than about 1000.0 milligrams per liter and less than about 30000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 100 milligrams per liter and less than about 500 milligrams per liter.
  • the concentration of carbon dioxide is greater than about 500 milligrams per liter and less than about 1000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 1000 milligrams per liter and less than about 5000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 5000 milligrams per liter and less than about 10000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 10000.0 milligrams per liter and less than about 50000.0 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 50000.0 milligrams per liter and less than about 100000.0 milligrams per liter.
  • the concentration of carbon dioxide is greater than about 100000.0 milligrams per liter and less than about 200000.0 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 200000.0 milligrams per liter and less than about 300000.0 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 300000.0 milligrams per liter and less than about 500000.0 milligrams per liter. [0588] In some embodiments, the concentration of carbon dioxide is greater than about 0.1 milligrams per liter and less than about 1 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 1 milligrams per liter and less than about 10 milligrams per liter.
  • the concentration of carbon dioxide is greater than about 1 milligrams per liter and less than about 20 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 10 milligrams per liter and less than about 50 milligrams per liter. In some embodiments, the concentration of carbon dioxide is greater than about 10 milligrams per liter and less than about 100 milligrams per WSGR Docket No.50741-726.601 liter. In some embodiments, the concentration of carbon dioxide is greater than about 100 milligrams per liter and less than about 1000 milligrams per liter.
  • the concentration of lithium is at least about 200.0 milligrams per liter and at most about 8000 milligrams per liter. In some embodiments, the concentration of lithium is at least about 200 milligrams per liter and at most about 4000 milligrams per liter. In some embodiments, the concentration of lithium is at least about 2000 milligrams per liter and at most about 8000 milligrams per liter. In some embodiments, the concentration of lithium is at least about 200 milligrams per liter and at most about 1000 milligrams per liter. In some embodiments, the concentration of lithium is at least about 200 milligrams per liter and at most about 500 milligrams per liter.
  • the concentration of lithium is at least about 1000 milligrams per liter and at most about 4000 milligrams per liter. In some embodiments, the concentration of lithium is at least about 1000.0 milligrams per liter and at most about 2000.0 milligrams per liter. In some embodiments, the concentration of lithium is at least about 2000.0 milligrams per liter and at most about 3000.0 milligrams per liter. In some embodiments, the concentration of lithium is at least about 3000.0 milligrams per liter and at most about 4000.0 milligrams per liter. In some embodiments, the concentration of lithium is at least about 4000.0 milligrams per liter and at most about 5000.0 milligrams per liter.
  • the concentration of lithium is at least about 5000.0 milligrams per liter and at most about 6000.0 milligrams per liter. In some embodiments, the concentration of lithium is at least about 6000.0 milligrams per liter and at most about 8000.0 milligrams per liter. In some embodiments, the concentration of lithium is at least about 8000.0 milligrams per liter and at most about 10000.0 milligrams per liter. In some embodiments, the concentration of lithium is at least about 10000.0 milligrams per liter and at most about 12000.0 milligrams per liter. In some embodiments, the concentration of lithium is at least about 12000.0 milligrams per liter and at most about 20000.0 milligrams per liter.
  • the concentration of lithium is at least about 0.1 milligrams per liter and at most about 1 milligrams per liter. In some embodiments, the concentration of lithium is at least about 1 milligrams per liter and at most about 10 milligrams per liter. In some embodiments, the concentration of lithium is at least about 10 milligrams per liter and at most about 20 milligrams per liter. In some embodiments, the concentration of lithium is at least about 10 milligrams per liter and at most about 50 milligrams per liter. In some embodiments, the concentration of lithium is at least about 20 milligrams per liter and at most about 100 milligrams per liter.
  • the concentration of lithium is at least about 100 milligrams per liter and at most about 1000 milligrams per liter.
  • WSGR Docket No.50741-726.601 [0591]
  • the concentration of barium is at least about 0.1 milligrams per liter and at most about 750 milligrams per liter.
  • the concentration of boron is at least about 10.0 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of calcium is at least about 10.0 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of magnesium is at least about 10.0 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of potassium is at least about 10.0 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of sodium is at least about 10.0 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of strontium is at least about 10.0 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of aluminum is at least about 0.001 milligrams per liter and at most about 750 milligrams per liter.
  • the concentration of copper is at least about 0.001 milligrams per liter and at most about 750 milligrams per liter. In some embodiments, the concentration of iron is at least about 0.001 milligrams per liter and at most about 750 milligrams per liter. In some embodiments, the concentration of manganese is at least about 0.001 milligrams per liter and at most about 750 milligrams per liter. In some embodiments, the concentration of molybdenum is at least about 0.1 milligrams per liter and at most about 750 milligrams per liter.
  • the concentration of niobium is at least about 0.001 milligrams per liter and at most about 750 milligrams per liter.
  • the concentration of titanium is at least about 0.001 milligrams per liter and at most about 750 milligrams per liter.
  • the concentration of vanadium is at least about 0.01 milligrams per liter and at most about 750 milligrams per liter.
  • the concentration of zirconium is at least about 0.001 milligrams per liter and at most about 750 milligrams per liter.
  • the concentration of bicarbonate is at least about 1000.0 milligrams per liter and at most about 30000 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 100 milligrams per liter and at most about 500 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 500 milligrams per liter and at most about 1000 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 1000 milligrams per liter and at most about 5000 milligrams per liter.
  • the concentration of bicarbonate is at least about 5000 milligrams per liter and at most about 10000 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 10000.0 milligrams per liter and at most about 50000.0 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 50000.0 milligrams per liter and at most about 100000.0 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 100000.0 milligrams per liter and at most about 200000.0 milligrams per liter.
  • the concentration of bicarbonate is at least about 200000.0 milligrams per liter and at most about 300000.0 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 300000.0 milligrams per liter and at most about 500000.0 milligrams per liter. [0594] In some embodiments, the concentration of bicarbonate is at least about 0.1 milligrams per liter and at most about 1 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 1 milligrams per liter and at most about 10 milligrams per liter.
  • the concentration of bicarbonate is at least about 1 milligrams per liter and at most about 20 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 10 milligrams per liter and at most about 50 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of bicarbonate is at least about 100 milligrams per liter and at most about 1000 milligrams per liter. [0595] In some embodiments, the concentration of bicarbonate is dependent on the pH of the solution. In some embodiments, bicarbonate is the principal anion contained within the solution.
  • bicarbonate anions are contained in the lithium eluate when carbon dioxide dissolved in water is used as an eluent.
  • the concentration of carbonate is at least about 1000.0 milligrams per liter and at most about 30000 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 100 milligrams per liter and at most about 500 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 500 milligrams per liter and at most about 1000 milligrams per liter.
  • the concentration of carbonate is at least about 1000 milligrams per liter and at most about 5000 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 5000 milligrams per liter and at most about 10000 milligrams per liter. In some embodiments, the concentration of carbonate is at least WSGR Docket No.50741-726.601 about 10000.0 milligrams per liter and at most about 50000.0 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 50000.0 milligrams per liter and at most about 100000.0 milligrams per liter.
  • the concentration of carbonate is at least about 100000.0 milligrams per liter and at most about 200000.0 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 200000.0 milligrams per liter and at most about 300000.0 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 300000.0 milligrams per liter and at most about 500000.0 milligrams per liter. [0597] In some embodiments, the concentration of carbonate is at least about 0.1 milligrams per liter and at most about 1 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 1 milligrams per liter and at most about 10 milligrams per liter.
  • the concentration of carbonate is at least about 1 milligrams per liter and at most about 20 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 10 milligrams per liter and at most about 50 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of carbonate is at least about 100 milligrams per liter and at most about 1000 milligrams per liter. [0598] In some embodiments, the concentration of carbonate is dependent on the pH of the solution. In some embodiments, carbonate is the principal anion contained within the solution.
  • carbonate anions are contained in the lithium eluate when carbon dioxide dissolved in water is used as an eluent.
  • the lithium eluate comprises dissolved carbon dioxide gas.
  • the concentration of carbon dioxide is at least about 1000.0 milligrams per liter and at most about 30000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 10 milligrams per liter and at most about 100 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 100 milligrams per liter and at most about 500 milligrams per liter.
  • the concentration of carbon dioxide is at least about 500 milligrams per liter and at most about 1000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 1000 milligrams per liter and at most about 5000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 5000 milligrams per liter and at most about 10000 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 10000.0 milligrams per liter and at most about 50000.0 WSGR Docket No.50741-726.601 milligrams per liter.
  • the concentration of carbon dioxide is at least about 50000.0 milligrams per liter and at most about 100000.0 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 100000.0 milligrams per liter and at most about 200000.0 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 200000.0 milligrams per liter and at most about 300000.0 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 300000.0 milligrams per liter and at most about 500000.0 milligrams per liter.
  • the concentration of carbon dioxide is at least about 0.1 milligrams per liter and at most about 1 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 1 milligrams per liter and at most about 10 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 1 milligrams per liter and at most about 20 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 10 milligrams per liter and at most about 50 milligrams per liter. In some embodiments, the concentration of carbon dioxide is at least about 10 milligrams per liter and at most about 100 milligrams per liter.
  • the concentration of carbon dioxide is at least about 100 milligrams per liter and at most about 1000 milligrams per liter.
  • the concentration of carbonate, bicarbonate, and carbon dioxide is dependent on the pH, temperature, pressure, or a combination thereof.
  • carbonate or bicarbonate are the majority of the anions contained within the solution.
  • said carbonate and bicarbonate anions are contained in the lithium eluate when carbon dioxide dissolved in water is used as an eluent.
  • said lithium and said carbonate and bicarbonate anions are further process into a lithium product.
  • said lithium product is lithium carbonate.
  • said lithium product is lithium hydroxide.
  • the conversion of dissolved carbon dioxide to lithium bicarbonate during the elution process ranges from about 0.001% to about 99%. In some embodiments, the conversion efficiency is about 1% to 10%. In some embodiments, the conversion efficiency is about 0.1% to 10%. In some embodiments, the conversion efficiency is about 0.1% to 5%. In some embodiments, the conversion efficiency is about 0.01% to 10%. In some embodiments, the conversion efficiency is about 0.001% to about 0.1%, about 0.1% to about 1%, or about 1% to about 5%.
  • this relatively low conversion efficiency is primarily due to the weakly acidic nature of carbonic acid formed from dissolved carbon dioxide, which has a significantly higher pH compared to conventional mineral acids WSGR Docket No.50741-726.601 like hydrochloric or sulfuric acid.
  • WSGR Docket No.50741-726.601 like hydrochloric or sulfuric acid.
  • such embodiments of the processes disclosed herein remain advantageous because the unconverted carbon dioxide can be recovered downstream using methods described in the "System for recovering water and a dissolved gas from the eluent solution" section, allowing for recycling of the gas and regeneration of the eluent solution.
  • over 90% of the unconverted carbon dioxide is recovered and recycled back into the elution process, significantly improving the overall economics and sustainability of the system.
  • the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:1 to about 1:10,000, depending on process conditions. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:1 to about 1:1,000. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:10 to about 1:1,000. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:20 to about 1:1,000. In some embodiments, the molar ratio of lithium to dissolved carbon dioxide in the eluate covers a wide range from about 1:20 to about 1:500.
  • the concentration of chloride is greater than about 0.001 and less than about 100,000 milligrams per liter.
  • the concentration of hydrogencarbonate (bicarbonate) is greater than about 1000.0 milligrams per liter and less than about 30000 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 10 milligrams per liter and less than about 100 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 100 milligrams per liter and less than about 500 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 500 milligrams per liter and less than about 1000 milligrams per liter.
  • the concentration of hydrogencarbonate is greater than about 1000 milligrams per liter and less than about 5000 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 5000 milligrams per liter and less than about 10000 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 10000.0 milligrams per liter and less than about 50000.0 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 50000.0 milligrams per liter and less than about 100000.0 milligrams per liter.
  • the concentration of hydrogencarbonate is greater than about 100000.0 milligrams per liter and less than about 200000.0 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 200000.0 milligrams per liter and less than about 300000.0 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is greater than about 300000.0 milligrams per liter and less than about 500000.0 milligrams per liter. [0606] In some embodiments, the concentration of nitrate is greater than about 0.001 milligrams per liter and less than about 30000 milligrams per liter.
  • the concentration of phosphate is greater than about 0.001 milligrams per liter and less than about 30000 milligrams per liter. In some embodiments, the concentration of sulfate is greater than about 0.001 milligrams per liter and less than about 30000 milligrams per liter.
  • the value of pH is greater than about 1.0 and less than about 4.0. In some embodiments, the value of pH is greater than about 0.0 and less than about 1.0. In some embodiments, the value of pH is greater than about 1.0 and less than about 2.0. In some embodiments, the value of pH is greater than about 2.0 and less than about 3.0. In some embodiments, the value of pH is greater than about 3.0 and less than about 4.0.
  • the value of pH is greater than about 4.0 and less than about 5.0. In some embodiments, the value of pH is greater than about 5.0 and less than about 6.0. In some embodiments, the value of pH is greater than about 6.0 and less than about 7.0. In some embodiments, the value of pH is greater than about 7.0 and less than about 8.0. In some embodiments, the value of pH is greater than about 8.0 and less than about 9.0. In some embodiments, the value of pH is greater than about 9.0 and less than about 10.0. In some embodiments, the value of pH is greater than about 10.0 and less than about 11.0. In some embodiments, the value of pH is greater than about 11.0 and less than about 12.0.
  • the value of oxidation-reduction potential is greater than about 50.0 mV and less than about 800.0 mV. In some embodiments, the value of oxidation- reduction potential is greater than about 100.0 mV and less than about 500.0 mV. In some WSGR Docket No.50741-726.601 embodiments, the value of oxidation-reduction potential is greater than about 200.0 mV and less than about 400.0 mV. In some embodiments, the value of oxidation-reduction potential is greater than about -450.0 mV and less than about 0.0 mV. In some embodiments, the value of oxidation-reduction potential is greater than about -200.0 mV and less than about 50.0 mV.
  • the value of oxidation-reduction potential is greater than about -50.0 mV and less than about 100.0 mV. In some embodiments, the value of oxidation-reduction potential is greater than about 50.0 mV and less than about 300.0 mV. In some embodiments, the value of oxidation-reduction potential is greater than about 100.0 mV and less than about 400.0 mV. In some embodiments, the value of oxidation-reduction potential is greater than about 200.0 mV and less than about 600.0 mV. In some embodiments, the value of oxidation- reduction potential is greater than about 300.0 mV and less than about 800.0 mV.
  • the value of oxidation-reduction potential is greater than about 500.0 mV and less than about 1000.0 mV. In some embodiments, the value of oxidation-reduction potential is greater than about 750.0 mV and less than about 1100.0 mV. [0609] In some embodiments, the concentration of chloride is at least about 0.001 and at most about 100,000 milligrams per liter. [0610] In some embodiments, the concentration of hydrogencarbonate (bicarbonate) is at least about 1000.0 milligrams per liter and at most about 30000 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is at least about 10 milligrams per liter and at most about 100 milligrams per liter.
  • the concentration of hydrogencarbonate is at least about 100 milligrams per liter and at most about 500 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is at least about 500 milligrams per liter and at most about 1000 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is at least about 1000 milligrams per liter and at most about 5000 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is at least about 5000 milligrams per liter and at most about 10000 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is at least about 10000.0 milligrams per liter and at most about 50000.0 milligrams per liter.
  • the concentration of hydrogencarbonate is at least about 50000.0 milligrams per liter and at most about 100000.0 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is at least about 100000.0 milligrams per liter and at most about 200000.0 milligrams per liter. In some embodiments, the concentration of hydrogencarbonate is at least about 200000.0 milligrams per liter and at most about 300000.0 milligrams per liter. In some embodiments, the WSGR Docket No.50741-726.601 concentration of hydrogencarbonate is at least about 300000.0 milligrams per liter and at most about 500000.0 milligrams per liter.
  • the concentration of nitrate is at least about 0.001 milligrams per liter and at most about 30000 milligrams per liter.
  • the concentration of phosphate is at least about 0.001 milligrams per liter and at most about 30000 milligrams per liter.
  • the concentration of sulfate is at least about 0.001 milligrams per liter and at most about 30000 milligrams per liter.
  • the value of pH is at least about 1.0 and at most about 4.0. In some embodiments, the value of pH is at least about 0.0 and at most about 1.0.
  • the value of pH is at least about 1.0 and at most about 2.0. In some embodiments, the value of pH is at least about 2.0 and at most about 3.0. In some embodiments, the value of pH is at least about 3.0 and at most about 4.0. In some embodiments, the value of pH is at least about 4.0 and at most about 5.0. In some embodiments, the value of pH is at least about 5.0 and at most about 6.0. In some embodiments, the value of pH is at least about 6.0 and at most about 7.0. In some embodiments, the value of pH is at least about 7.0 and at most about 8.0. In some embodiments, the value of pH is at least about 8.0 and at most about 9.0.
  • the value of pH is at least about 9.0 and at most about 10.0. In some embodiments, the value of pH is at least about 10.0 and at most about 11.0. In some embodiments, the value of pH is at least about 11.0 and at most about 12.0. [0613] In some embodiments, the elution of lithium from the ion exchange material continues effectively only while the pH of the eluate remains below a certain critical value. In some embodiments, this critical pH value may be within a range of about 1.0 to about 8.0. In some embodiments, the critical pH value is about 3.0, about 4.0, about 5.0, about 6.0, or about 7.0. In some embodiments, the critical pH value is about 6.0. In some embodiments, the critical pH value is about 5.0.
  • the efficiency of further lithium elution decreases significantly.
  • the maximum concentration of lithium that can be eluted is about 140 mg/L.
  • the critical pH is about 5 and the concentration of lithium in the synthetic lithium solution is at most about 140 mg/L.
  • the eluate also contains sodium, magnesium, calcium, potassium, strontium, or other impurities in a range of about 0.1 mg/L to about 100 mg/L.
  • the critical pH value is determined by the specific ion exchange material used, the composition of the liquid resource from which lithium was WSGR Docket No.50741-726.601 extracted, the temperature of the system, and other operational parameters.
  • the critical pH may be as low as about 2.0 or as high as about 8.0.
  • the relationship between pH and maximum lithium concentration follows a predictable correlation that allows for optimization of elution conditions based on the desired lithium concentration in the eluate.
  • the efficiency of the elution process is optimized by monitoring the pH of the eluent or eluate solution to remain below the critical value.
  • the process involves periodic or continuous addition of carbon dioxide to the system to counteract the pH increase that occurs as lithium and carbonate or bicarbonate concentration builds in the eluate (e.g., the synthetic lithium solution).
  • a staged elution process is employed wherein fresh acidic eluent solution is introduced once the lithium concentration approaches the theoretical maximum for a given pH condition.
  • the maximum achievable lithium concentration varies significantly based on the critical pH value: at a pH of about 2.0, the maximum lithium concentration may be lower than at a critical pH of about 6.0, because the lower pH corresponds to a higher concentration of available hydrogen ions for exchanging with lithium ions on the ion exchange material, while the higher pH corresponds to a higher amount of lithium and bicarbonate ions having been eluted.
  • the concentration of lithium bicarbonate in solution increases until reaching a theoretical maximum that depends on the equilibrium conditions at that pH.
  • the pressure of the system can be adjusted to modify the maximum achievable lithium concentration at any given critical pH.
  • the eluent solution is used to elute lithium from an ion exchange material at a pressure of about 1 to about 30 bar. In some WSGR Docket No.50741-726.601 embodiments, the eluent solution is used to elute lithium from an ion exchange material at a pressure of about 2 to about 30 bar. In some embodiments, the eluent solution is used to elute lithium from an ion exchange material at a pressure of about 5 to about 30 bar. In some embodiments, the eluent solution is used to elute lithium from an ion exchange material at a pressure of about 10 to about 30 bar.
  • the eluent solution is used to elute lithium from an ion exchange material at a pressure of about 1 to about 20 bar. In some embodiments, the eluent solution is used to elute lithium from an ion exchange material at a pressure of about 1 to about 15 bar. In some embodiments, the synthetic lithium solution is maintained at about the same pressure as the eluant solution for the purpose of retaining the gas (e.g., the carbon dioxide) dissolved therein for subsequent collection and recycling of said gas. [0616] In some embodiments, the value of oxidation-reduction potential is at least about 50.0 mV and at most about 800.0 mV.
  • the value of oxidation-reduction potential is at least about 100.0 mV and at most about 500.0 mV. In some embodiments, the value of oxidation-reduction potential is at least about 200.0 mV and at most about 400.0 mV. In some embodiments, the value of oxidation-reduction potential is at least about -450.0 mV and at most about 0.0 mV. In some embodiments, the value of oxidation-reduction potential is at least about -200.0 mV and at most about 50.0 mV. In some embodiments, the value of oxidation-reduction potential is at least about -50.0 mV and at most about 100.0 mV.
  • the value of oxidation-reduction potential is at least about 50.0 mV and at most about 300.0 mV. In some embodiments, the value of oxidation-reduction potential is at least about 100.0 mV and at most about 400.0 mV. In some embodiments, the value of oxidation- reduction potential is at least about 200.0 mV and at most about 600.0 mV. In some embodiments, the value of oxidation-reduction potential is at least about 300.0 mV and at most about 800.0 mV. In some embodiments, the value of oxidation-reduction potential is at least about 500.0 mV and at most about 1000.0 mV.
  • the value of oxidation- reduction potential is at least about 750.0 mV and at most about 1100.0 mV.
  • the eluate comprises lithium and one or more salts.
  • said one or more salts originate form salts dissolved in the eluent solution to enhance the elution properties of the same. Salts, compositions, concentrations, and methods related to the dissolution of one or more salts in an eluent solution are described in Embodiments comprising a combination of one or more gases, one or more liquids, and one or more dissolved solids and exemplified in Example 16.
  • the lithium eluate solution that is yielded from the ion exchange reactor is further processed into lithium chemicals selected from the following list: lithium sulfate, lithium chloride, lithium carbonate, lithium phosphate, lithium hydroxide, lithium metal, lithium metal oxide, lithium metal phosphate, lithium sulfide, or combinations thereof.
  • the lithium eluate solution that is yielded from the ion exchange reactor is further processed into lithium chemicals that are solid, aqueous, liquid, slurry form, hydrated, or anhydrous.
  • the lithium eluate solution that is yielded from the ion exchange reactor is further processed using acid recovery, acid recycling, acid regeneration, distillation, reverse osmosis, evaporation, purification, chemical precipitation, membrane electrolysis, or combinations thereof.
  • the lithium eluate e.g., the synthetic lithium solution
  • the purification unit configured to purify the synthetic lithium solution.
  • the purification unit configured to purify the synthetic lithium solution and further configured to modify the pH of the synthetic lithium solution.
  • the purification unit comprises a water removal unit.
  • the water removal unit is configured to concentrate the synthetic lithium solution.
  • the lithium eluate is processed to crystallize a lithium product after the lithium eluate is previously processed using one or more stages of precipitation, softening, ion exchange, reverse osmosis (including seawater, ultra-high pressure, or osmotically assisted reverse osmosis).
  • the lithium eluate is processed to crystallize a lithium product.
  • the lithium eluate is processed to crystallize a lithium product by removing a gas from the lithium eluate or processed lithium eluate.
  • said gas is carbon dioxide and said product is lithium carbonate.
  • said gas is removed by pressure adjustment, sparging of a gas different WSGR Docket No.50741-726.601 from the gas being removed, or a combination thereof. In some embodiments, the gas removed is recycled.
  • the lithium eluate is processed to crystallize a lithium product in more than one crystallization unit. In some embodiments, the lithium eluate is processed to crystallize a lithium product in two, three, four or five separate crystallization units. In some embodiments, a mother liquor is generated by separating the crystallized lithium carbonate from the remaining liquid, termed mother liquor.
  • an optional water removal unit configured to concentrate the mother liquor after crystallization, and the mother liquor thus concentrated is fed to the next crystallization unit.
  • a gas including carbon dioxide
  • a lithium eluate is processed into a lithium stream that is treated with sodium carbonate to precipitate lithium carbonate.
  • a lithium chloride stream is treated with sodium carbonate to precipitate lithium carbonate.
  • a lithium sulfate stream is treated with sodium carbonate to precipitate lithium carbonate.
  • a lithium nitrate stream is treated with sodium carbonate to precipitate lithium carbonate.
  • a lithium eluate is processed into a lithium stream that is treated with sodium hydroxide to crystallize a lithium hydroxide product.
  • a lithium sulfate stream is treated with sodium hydroxide to crystallize a lithium hydroxide product.
  • a lithium chloride stream is treated with sodium hydroxide to crystallize a lithium hydroxide product.
  • a lithium nitrate stream is treated with sodium hydroxide to crystallize a lithium hydroxide product.
  • Removal of impurities [0625] In some embodiments, impurities are removed from the lithium eluate, an IEL eluate and/or new IEL eluate.
  • the eluate treated to remove impurities by any of the methods described herein is termed a purified lithium eluate.
  • said purified lithium eluate can be further purified to produce a new purified lithium eluate. It shall be understood that all the purification methods described herein for removal of impurities can be applied to a lithium eluate, a purified lithium eluate, an impurities-enriched eluate, or generally to any solution comprising lithium and an impurity that is not lithium.
  • said purification is done by an impurities selective ion exchange material, nanofiltration, chemical precipitation, electrochemical separation, WSGR Docket No.50741-726.601 temperature reduction precipitation, other methods of removing impurities, or combinations thereof.
  • impurities are removed using combinations of impurities selective ion exchange material, nanofiltration, chemical precipitation, electrochemical separation, temperature reduction precipitation, other methods of removing multivalent impurities, or combinations thereof, in parallel, in series, or combinations thereof.
  • the purification unit is configured to remove impurities from the synthetic lithium solution using an impurities selective ion exchange material, nanofiltration, chemical precipitation, electrochemical separation, temperature reduction precipitation, other methods of removing impurities, or combinations thereof.
  • Impurities Selective Ion Exchange Material [0627] In some embodiments, for any lithium extraction process or system described herein, impurities are removed by contacting an eluate or modified with an impurities selective ion exchange material. In some embodiments, for any lithium extraction process or system described herein, impurities are at least removed by contacting a lithium eluate or purified lithium eluate with an impurities selective ion exchange material.
  • impurities selective ion exchange material comprises multivalent impurities selective ion exchange material.
  • the multivalent impurities selective ion exchange material comprises multivalent cation selective (MCS) ion exchange material.
  • MCS ion exchange material is provided in a packed bed.
  • MCS ion exchange material is provided in a fluidized bed.
  • MCS ion exchange material is located in a MCS vessel.
  • MCS ion exchange material is arranged in a network of MCS vessels.
  • MCS ion exchange material is arranged in a network of MCS vessels, wherein IEL acidic solution is sequentially passed through the network of MCS vessels, such that multivalent cations are absorbed from the IEL acidic solution as it passes through each MCS vessel.
  • the amount of multivalent cations absorbed from a IEL acidic solution passing through a network of MCS vessels decreases from a first MCS vessel in the sequence of IEL acidic solution flow to a last MCS vessel in said sequence.
  • the last MCS vessel in said sequence absorbs trace amounts of multivalent cations.
  • the sequence of the plurality of MCS vessels is rearranged based on the saturation of the MCS ion exchange material in each MCS vessel.
  • MCS ion exchange material is arranged in a lead-lag configuration.
  • the MCS ion exchange material is arranged in a variation of a lead-lag setup.
  • the MCS ion exchange material is eluted WSGR Docket No.50741-726.601 using a second acidic solution.
  • the MCS ion exchange material is eluted using hydrochloric acid.
  • the MCS ion exchange material is regenerated using sodium hydroxide, potassium hydroxide, or a combination thereof.
  • the MCS ion exchange material is provided in one or more stirred tank reactors, tanks, columns, fluidized beds, packed beds, or combinations thereof, and arranged in series and/or parallel.
  • a multivalent cation selective (MCS) ion exchange material is selective for cations with a charge of 2+, 3+, 4+, 5+, 6+, or combinations thereof.
  • the multivalent selective cation exchange material is comprised of polystyrene, polybutadiene, mixtures thereof, modifications thereof, or combinations thereof.
  • the multivalent selective cation exchange material is comprised of polystyrene, polystyrene functionalized with sulfonate, polystyrene-polybutadiene copolymer functionalized with sulfonate group and/or phosphonate group, poly(2-acrylamido-2-methyl-1- propanesulfonic acid) (PolyAMPS), poly(styrene-co-divinylbenzene) copolymer functionalized with sulfonate group, phosphonate group, iminodiacetic group, carboxylic acid group, mixtures thereof, modifications thereof, or combinations thereof.
  • the ion exchange material for impurity removal is comprised of polystyrene, polybutadiene, mixtures thereof, modifications thereof, or combinations thereof.
  • the ion exchange material for impurity removal is comprised of polystyrene, polybutadiene, poly divinyl benzene, divinyl benzene, polystyrene functionalized with sulfonate, polystyrene- polybutadiene copolymer functionalized with sulfonate group and/or phosphonate group, poly(2-acrylamido-2-methyl-1-propanesulfonic acid) (PolyAMPS), poly(styrene-co- divinylbenzene) copolymer functionalized with sulfonate group, phosphonate group, iminodiacetic group, carboxylic acid group, mixtures thereof, modifications thereof, or combinations thereof.
  • the ion exchange material for impurity removal from the acidic lithium solution is a styrene butadiene copolymer with sulfonic acid functional groups.
  • the ion exchange material for impurity removal comprises beads with a mean diameter of about 10-50 microns, 50-100 microns, 100-200 microns, 200-400 microns, 300- 500 microns, 400-600 microns, 600-800 microns, 200-500 microns, 400-800 microns, 500- 1000 microns, 800-1600 microns, or 1000-2000 microns.
  • the ion exchange material for impurity removal from the acidic lithium solution is a mixture of styrene, divinylbenzene, butadiene, or combinations thereof.
  • the ion exchange material for impurity removal from the acidic lithium solution is a copolymer of styrene, divinylbenzene, butadiene, or combinations thereof functionalized with sulfonic-acid groups.
  • the ion exchange material for impurity removal from the acidic lithium solution is a mixture of styrene, divinylbenzene, butadiene, or combinations thereof functionalized with sulfonic-acid groups.
  • the ion exchange material for impurity removal from the acidic lithium solution is a copolymer of styrene, divinylbenzene, butadiene, or combinations thereof WSGR Docket No.50741-726.601 functionalized with phosphonic-acid groups.
  • the ion exchange material for impurity removal from the acidic lithium solution is a mixture of styrene, divinylbenzene, butadiene, or combinations thereof functionalized with phosphonic-acid groups.
  • the ion exchange material for impurity removal from the acidic lithium solution is a copolymer functionalized with sulfonic-acid groups.
  • the ion exchange material for impurity removal from the acidic lithium solution is a styrene-butadiene copolymer functionalized with sulfonic acid groups. In one embodiment, the ion exchange material for impurity removal from the acidic lithium solution is a divinylbenzene-butadiene copolymer functionalized with sulfonic acid groups. In one embodiment, the ion exchange material for impurity removal from the acidic lithium solution is a styrene-butadiene-divinylbenzene copolymer functionalized with sulfonic acid groups.
  • the ion exchange material for impurity removal from the acidic lithium solution is a styrene-divinylbenzene copolymer functionalized with phosphonic acid groups. In one embodiment, the ion exchange material for impurity removal from the acidic lithium solution is a styrene-butadiene copolymer functionalized with phosphonic acid groups. In one embodiment, the ion exchange material for impurity removal from the acidic lithium solution is a divinylbenzene-butadiene copolymer functionalized with phosphonic acid groups.
  • the ion exchange material for impurity WSGR Docket No.50741-726.601 removal from the acidic lithium solution is a vinylidene copolymer functionalized with sulfonic acid or phosphonic acid groups. In one embodiment, the ion exchange material for impurity removal from the acidic lithium solution is an acrylonitrile copolymer functionalized with sulfonic acid or phosphonic acid groups. [0639] In some embodiments, the ion exchange material for impurity removal from the acidic lithium solution is a polymer functionalized with phosphoric or phosphinic acid groups.
  • nanofiltration membrane material is comprised of cellulose, cellulose acetate, cellulose diacetate, cellulose triacetate, polyamide, poly(piperazine-amide), mixtures thereof, modifications thereof, or combinations thereof.
  • the nanofiltration membrane material is comprised of a thin-film composite.
  • the nanofiltration membrane material is comprised of polyamide with a support comprised of polyacrylonitrile (PAN), polyethersulfone, polysulfone, polyphenylene sulfone, cellulose acetate, polyimide, polypropylene, polyketone, polyethylene terephthalate, mixtures thereof, modifications thereof, or combinations thereof.
  • PAN polyacrylonitrile
  • the nanofiltration membrane material is comprised of polyethylene terephthalate.
  • the nanofiltration membrane material is comprised of ceramic material.
  • the nanofiltration membrane material is comprised of alumina, zirconia, yttria stabilized zirconia, titania, silica, mixtures thereof, modifications thereof, or combinations thereof.
  • impurities are removed from the acidic solution (e.g., synthetic lithium solution) using precipitation.
  • impurities are removed from the acidic solution using electrochemical precipitation.
  • impurities are removed from the acidic solution using chemical, carbonate precipitation, hydroxide precipitation, phosphate precipitation, or combinations thereof.
  • impurities are removed from the acidic solution by adding phosphate to precipitate calcium phosphate, magnesium phosphate, barium phosphate, and/or other phosphate compounds.
  • multivalent impurities are removed from the IEL acidic solution through carbonate precipitation, hydroxide precipitation, phosphate precipitation, or combinations thereof. In some embodiments, multivalent impurities are removed from the IEL acidic solution by adding phosphate to precipitate calcium phosphate, magnesium phosphate, barium phosphate, and/or other phosphate compounds. In some embodiments, multivalent impurities are removed from the IEL acidic solution by adding sodium phosphate, potassium phosphate, phosphoric acid, and/or other phosphate compounds to precipitate calcium phosphate, magnesium phosphate, barium phosphate, and/or other phosphate compounds. In some embodiments, residual phosphate is removed from the IEL acidic solution.
  • residual phosphate is removed from the IEL acidic solution using ion exchange or precipitation. In some embodiments, residual phosphate is removed from the IEL acidic solution using precipitation with aluminum or iron.
  • multivalent impurities are removed from the IEL acidic solution by adding phosphoric acid to precipitate phosphate compounds. In some embodiments, adding phosphoric acid removes Ca, Mg, Sr, and/or Ba from the IEL acidic solution through precipitation of Ca, Mg, Sr, and/or Ba phosphate compounds.
  • multivalent impurities are removed from the IEL acidic solution by adding an oxalate, oxalic acid, citrate, citric acid, or combinations thereof.
  • the oxalate, oxalic acid, citrate, citric acid, or combinations thereof are added as a precipitant, such that multivalent impurities are precipitated.
  • the precipitant concentration in the IEL acidic solution is subsequently decreased through precipitation by adding cation precipitants to the IEL acidic solution.
  • multivalent impurities are removed from the IEL acidic solution by adding oxalate to the IEL acidic solution to precipitate the multivalent impurities.
  • residual oxalate anions are precipitated and removed from the resulting lithium enriched acidic solution by adding cation precipitants.
  • cation precipitants comprise zinc, iron, manganese, other transition metals, other cations, or combinations thereof.
  • multivalent impurities are removed from the IEL acidic solution by adding citrate to the IEL acidic solution to precipitate the multivalent impurities.
  • residual citrate anions are precipitated and removed from the resulting lithium enriched acidic solution by adding cation precipitants.
  • cation precipitants comprise zinc, iron, manganese, other transition metals, other cations, or combinations thereof.
  • multivalent impurities are removed from the IEL acidic solution by adding anion precipitants to the IEL acidic solution to precipitate the multivalent impurities.
  • residual anions are precipitated and removed from the resulting lithium enriched acidic solution by adding cation precipitants.
  • cation precipitants comprise zinc, iron, manganese, other transition metals, other cations, or combinations thereof.
  • Pressure Adjustment Precipitation [0647] In an aspect described herein, precipitation of impurities is brought about in part by adjustment of the pressure of the process stream containing the eluate or purified eluate. A non-limiting embodiment of said precipitation is described in Example 8.
  • precipitated solids comprise a carbonate of calcium, magnesium, strontium, barium, beryllium, or a combination thereof. In some embodiments, the precipitated solids comprise a phosphate. In some embodiments, the precipitated solids comprise a hydroxide. [0650] In some embodiments, the pressure is modulated to allow the precipitation of some solids, while maintaining other species in solution. In some embodiments, the pH is modulated to allow the precipitation of some solids, while maintaining other species in solution. In some embodiments, the pH and pressure are modulated to allow the precipitation of some solids, while maintaining other species in solution. In some embodiments, said pH and said pressure are modulated in stages, to precipitate specific impurity species.
  • the pH is raised by adding a base.
  • said base comprises NaOH, KOH, LiOH, RbOH, Mg(OH)2, Ca(OH)2, Sr(OH)2, Ba(OH)2, NH4OH, Sr(OH)2 or other basic compounds.
  • the pH is lowered by adding an acid.
  • said acid comprises hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, carbonic acid, a solid acid, or a combination thereof.
  • the pH is lowered by adding an acid gas.
  • said acid gas is carbon dioxide.
  • impurities are at least removed from an impurities-enriched lithiated (IEL) acidic solution by passing through one or more electrodialysis membranes to separate multivalent impurities.
  • electrodialysis is used to remove impurities from an acidic lithium solution.
  • electrodialysis is a membrane separation technology in which certain charged species are allowed to pass through a membrane with assistance from an applied electric field.
  • electrodialysis is used to remove impurities from an acidic lithium solution where water is retained in the feed phase while charged ions pass through selective ion exchange membranes.
  • electrodialysis is used to WSGR Docket No.50741-726.601 remove impurities from an acidic lithium solution where selective cation exchange membranes are used to obtain separation of monovalent and multivalent ions by means of different transport kinetics through the membrane.
  • electrodialysis is used to remove impurities from an acidic lithium solution using a polymer-based membrane with functional groups.
  • electrodialysis is used to remove impurities from an acidic lithium solution using cation exchange membranes that are functionalized with negatively charged functional groups such as sulfonic, carboxyl, other functional groups, or combinations thereof which allows cations to pass through while preventing anions from passing.
  • electrodialysis is used to remove impurities from an acidic lithium solution with a rinse solution or additional membranes near the electrodes to wash out ions near the electrodes to prevent the generation of chlorine or hydrogen gas on the electrodes. In some embodiments, electrodialysis is used to remove impurities from an acidic lithium solution where divalent or multivalent cations would move through a membrane slower than monovalent ions.
  • Electrolysis, electrodialysis, and other embodiments comprising treatment of a lithium solution in an electrochemical system comprising: a) providing an ion exchange unit, wherein said ion exchange unit comprises an ion exchange material; b) contacting the ion exchange material in the ion exchange unit with the liquid resource, wherein hydrogen ions from the ion exchange material are exchanged with lithium ions from the liquid resource to produce a lithium-enriched ion exchange material in the ion exchange unit; c) treating the lithium-enriched ion exchange material with an acid solution, wherein the lithium ions from the lithium-enriched ion exchange material are exchanged with hydrogen ions from the acid solution to produce a lithium eluate; d) providing a membrane cell in fluid communication with the ion exchange unit, wherein the membrane cell comprises (i) a first compartment containing an electrochemically reducing electrode, (ii) a
  • the lithium-enriched ion exchange material is treated in the ion exchange unit.
  • the lithium eluate is produced in the ion exchange unit.
  • the lithium eluate is passed from the ion exchange unit to the membrane cell.
  • the ion exchange material in the ion exchange unit is treated with an acid solution to produce a hydrogen-enriched ion exchange material in the ion exchange unit.
  • b) further comprises pH modulation, wherein the pH modulation maintains an equilibrium in favor of hydrogen ions from the hydrogen-rich ion exchange material being exchanged with lithium ions from the liquid resource.
  • the process further comprises treating the lithium-enriched ion exchange material with base in addition to the acid solution.
  • the base is Ca(OH)2 or NaOH.
  • one of the processing systems is a membrane electrolysis system.
  • the membrane electrolysis system produces a lithium salt solution and an acid that is returned to the ion exchange system.
  • the membrane electrolysis system converts a lithium sulfate solution into a lithium hydroxide solution and a sulfuric acid solution that is returned to the ion exchange system.
  • the membrane electrolysis system converts a lithium chloride solution into a lithium hydroxide solution and hydrochloric acid that is returned to the ion exchange system. In one embodiment, the membrane electrolysis system converts a lithium chloride solution into a lithium hydroxide solution, hydrogen gas, and chlorine gas, and the hydrogen and chlorine gases are converted to hydrochloric acid, which is returned to the ion exchange system.
  • one of the processing systems is an electrochemical cell system. In one embodiment, the electrochemical cell system produces a lithium salt solution and an acid that is returned to the ion exchange system.
  • the electrochemical cell system converts a lithium sulfate solution into a lithium hydroxide solution and a sulfuric acid solution that is returned to the ion exchange system. In one embodiment, the electrochemical cell system converts a lithium chloride solution into a lithium hydroxide solution and hydrochloric acid that is returned to the ion exchange system. In one embodiment, the electrochemical cell system converts a lithium chloride solution into a lithium hydroxide solution, hydrogen gas, and chlorine gas, and the hydrogen and chlorine gases are converted to hydrochloric acid, which is returned to the ion exchange system.
  • WSGR Docket No.50741-726.601 In one embodiment, one of the processing systems is an electrodialysis system.
  • the integrated system includes one or more electrolysis systems.
  • an electrolysis system is comprised of one or more membrane electrolysis cells.
  • an electrolysis system converts a lithium salt solution to form a lithium hydroxide solution, an acidified solution, and optionally a dilute lithium salt solution.
  • the lithium salt solution is or is derived from a lithium eluate solution, produced by an ion exchange system, that has optionally been concentrated and/or purified.
  • acidified solution from an electrolysis system is returned to an ion exchange system to elute more lithium eluate solution.
  • the integrated system includes one or more electrolysis systems.
  • an electrolysis system is comprised of one or more electrochemical cells.
  • an electrolysis system converts a lithium salt solution to form a lithium hydroxide solution, an acidified solution, and optionally a dilute lithium salt solution.
  • the lithium salt solution is or is derived from a lithium eluate solution, produced by an ion exchange system that has optionally been concentrated and/or purified.
  • acidified solution from an electrolysis system is returned to an ion exchange system to elute more lithium eluate solution.
  • the integrated system includes one or more electrolysis systems.
  • an electrolysis system is comprised of one or more electrodialysis cells.
  • an electrolysis system converts a lithium salt solution to form a lithium hydroxide solution, an acidified solution, and optionally a dilute lithium salt solution.
  • the lithium salt solution is or is derived from a lithium eluate solution, produced by an ion exchange system that has optionally been concentrated and/or purified.
  • acidified solution from an electrolysis system is returned to an ion exchange system to elute more lithium eluate solution.
  • a lithium salt solution contains unreacted acid from the ion exchange system.
  • unreacted acid in the lithium salt solution from an ion exchange system passes through an electrolysis system, and is further acidified to form an acidified solution.
  • a lithium salt solution derived from an ion exchange system is purified to remove impurities without neutralizing the unreacted acid in the lithium salt solution, and is then fed into an electrolysis system.
  • an acidified solution produced by an electrolysis system contains lithium ions from the lithium salt solution fed into the electrolysis system.
  • an acidified solution containing lithium ions leaves the electrolysis system, and is fed back to an ion exchange system to elute lithium, to produce more lithium salt solution.
  • the electrolysis cells are electrochemical cells.
  • the membranes may be cation-conducting and/or anion-conducting membranes.
  • the electrochemical cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
  • the electrolysis cells are electrodialysis cells.
  • the membranes are cation- conducting and/or anion-conducting membranes.
  • the electrodialysis cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
  • the electrolysis cells are membrane electrolysis cells.
  • the membranes are cation-conducting and/or anion-conducting membranes.
  • the membrane electrolysis cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
  • the membrane electrolysis cell is a three-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions separating a compartment with an electrochemically reducing electrode from a central compartment, and with an anion-conducting membrane that allows for transfer of anions ions separating a compartment with an electrochemically oxidizing electrode from the central compartment.
  • the cation-conducting membrane prevents transfer of anions such as chloride, WSGR Docket No.50741-726.601 sulfate, or hydroxide.
  • the anion-conducting membrane prevents transfer of cations such as lithium, sodium, or protons.
  • the membranes are comprised of Nafion ® , sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co- polymers, other membrane materials, composites, or combinations thereof.
  • the cation exchange membranes are comprised of a functionalized polymer structure which is Nafion ® , sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof.
  • the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
  • the membranes are comprised of Nafion ® , sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof.
  • the cation exchange membranes are comprised of a functionalized polymer structure which is Nafion ® , sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof.
  • the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
  • the membranes are comprised of Nafion ® , sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof.
  • the cation exchange membranes are comprised of a functionalized polymer structure which is Nafion ® , sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co- polymers, different polymers, composites of polymers, or combinations thereof.
  • the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
  • an anion exchange membrane is comprised of a functionalized polymer structure.
  • the polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, WSGR Docket No.50741-726.601 polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
  • the functional groups are part of the polymer backbone.
  • an anion exchange membrane is comprised of a functionalized polymer structure.
  • the polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
  • the functional groups are part of the polymer backbone.
  • functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions.
  • the functional group is benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilised quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
  • an anion exchange membrane is comprised of a functionalized polymer structure.
  • the polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
  • the functional groups are part of the polymer backbone.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

La présente divulgation concerne des procédés et des systèmes d'élution de métaux, tels que le lithium, à partir de matériaux échangeurs d'ions à l'aide de solutions acides obtenues par dissolution d'un gaz, tel que du dioxyde de carbone, dans une phase aqueuse.
PCT/US2025/025758 2024-04-23 2025-04-22 Procédés et systèmes améliorés pour générer une solution de lithium à partir d'un matériau échangeur d'ions Pending WO2025226673A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202463637853P 2024-04-23 2024-04-23
US63/637,853 2024-04-23

Publications (1)

Publication Number Publication Date
WO2025226673A1 true WO2025226673A1 (fr) 2025-10-30

Family

ID=97490847

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2025/025758 Pending WO2025226673A1 (fr) 2024-04-23 2025-04-22 Procédés et systèmes améliorés pour générer une solution de lithium à partir d'un matériau échangeur d'ions

Country Status (1)

Country Link
WO (1) WO2025226673A1 (fr)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060115407A1 (en) * 1998-07-16 2006-06-01 Boryta Daniel A Production of lithium compounds directly from lithium containing brines
US20150197830A1 (en) * 2012-07-31 2015-07-16 Research Institute Of Industrial Science & Technology Method for Extracting Lithium from Solution Containing Lithium
WO2019160982A1 (fr) * 2018-02-17 2019-08-22 Lilac Solutions, Inc. Système intégré d'extraction et de conversion de lithium
US20200248283A1 (en) * 2017-08-02 2020-08-06 Jx Nippon Mining & Metals Corporation Method for dissolving lithium compound, method for manufacturing lithium carbonate, and method for recovering lithium from lithium ion secondary cell scrap
US20230049146A1 (en) * 2021-03-23 2023-02-16 Gradiant Corporation Lithium recovery from liquid streams
US20230132311A1 (en) * 2020-04-21 2023-04-27 Jx Nippon Mining & Metals Corporation Method for producing lithium hydroxide
US20230399720A1 (en) * 2020-11-10 2023-12-14 Fortum Oyj Process for recovering and purifying lithium

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060115407A1 (en) * 1998-07-16 2006-06-01 Boryta Daniel A Production of lithium compounds directly from lithium containing brines
US20150197830A1 (en) * 2012-07-31 2015-07-16 Research Institute Of Industrial Science & Technology Method for Extracting Lithium from Solution Containing Lithium
US20200248283A1 (en) * 2017-08-02 2020-08-06 Jx Nippon Mining & Metals Corporation Method for dissolving lithium compound, method for manufacturing lithium carbonate, and method for recovering lithium from lithium ion secondary cell scrap
WO2019160982A1 (fr) * 2018-02-17 2019-08-22 Lilac Solutions, Inc. Système intégré d'extraction et de conversion de lithium
US20230132311A1 (en) * 2020-04-21 2023-04-27 Jx Nippon Mining & Metals Corporation Method for producing lithium hydroxide
US20230399720A1 (en) * 2020-11-10 2023-12-14 Fortum Oyj Process for recovering and purifying lithium
US20230049146A1 (en) * 2021-03-23 2023-02-16 Gradiant Corporation Lithium recovery from liquid streams

Similar Documents

Publication Publication Date Title
US10648090B2 (en) Integrated system for lithium extraction and conversion
JP7379351B2 (ja) リチウムの抽出と変換のための統合システム
US11964876B2 (en) Lithium extraction in the presence of scalants
US11377362B2 (en) Lithium production with volatile acid
US12370468B2 (en) Lithium extraction enhanced by an alternate phase
US11235282B2 (en) Processes for producing lithium compounds using forward osmosis
US12162773B2 (en) Extraction of lithium with chemical additives
WO2023215313A1 (fr) Élimination d'impuretés contenues dans un éluat de lithium
US20250283193A1 (en) Synthetic lithium solutions with controlled impurity profiles
US20250327149A1 (en) Integrated systems and methods for lithium recovery
WO2021252381A1 (fr) Extraction de lithium en présence de scalants
WO2022109156A1 (fr) Production de lithium avec de l'acide volatil
WO2025029953A1 (fr) Systèmes et procédés pour minimiser l'utilisation d'eau externe dans la production de lithium
EP4623115A2 (fr) Extraction de lithium à partir de saumures avec des concentrations d'ions modulées
WO2023063928A1 (fr) Procédés de production de composés de lithium par osmose inverse
WO2024220812A1 (fr) Procédés et systèmes de traitement de composés de lithium
WO2025226673A1 (fr) Procédés et systèmes améliorés pour générer une solution de lithium à partir d'un matériau échangeur d'ions