[go: up one dir, main page]

WO2025090864A1 - Récupération améliorée de lithium à partir de réservoirs souterrains - Google Patents

Récupération améliorée de lithium à partir de réservoirs souterrains Download PDF

Info

Publication number
WO2025090864A1
WO2025090864A1 PCT/US2024/052957 US2024052957W WO2025090864A1 WO 2025090864 A1 WO2025090864 A1 WO 2025090864A1 US 2024052957 W US2024052957 W US 2024052957W WO 2025090864 A1 WO2025090864 A1 WO 2025090864A1
Authority
WO
WIPO (PCT)
Prior art keywords
lithium
liquid resource
reservoir
ion exchange
fluid
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/US2024/052957
Other languages
English (en)
Inventor
Andrew Liam PROCTER
Thomas William GOODE
Matthew Simmons
Thomas Alan WILSON
Nicolás Andrés GROSSO GIORDANO
David Henry SNYDACKER
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 Minerals Uk Ltd
Lilac Solutions Inc
Original Assignee
Lilac Minerals Uk Ltd
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 Minerals Uk Ltd, Lilac Solutions Inc filed Critical Lilac Minerals Uk Ltd
Publication of WO2025090864A1 publication Critical patent/WO2025090864A1/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
    • C22B3/02—Apparatus therefor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/02—Oxides; Hydroxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/04—Halides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/06—Sulfates; Sulfites
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/08—Carbonates; Bicarbonates
    • 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
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching

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 process of recovering lithium from a reservoir comprising: a) producing a liquid resource comprising lithium from the reservoir; b) extracting at least a portion of the lithium from the liquid resource; c) injecting a fluid into the reservoir; wherein a) and c) are performed simultaneously.
  • a process of increasing the extraction of lithium from a subsurface reservoir comprising: a) producing a liquid resource comprising lithium from the subsurface reservoir and treating the liquid resource by at least one of the following: i) modulating the pH of the liquid resource; ii) modulating the lithium concentration of the liquid resource; iii) contacting the liquid resource with a chemical additive, wherein the chemical additive is an oxidant or a reductant; or iv) removing metal impurities or organic impurities from the liquid resource; b) extracting at least a portion of the lithium from the liquid resource to generate a synthetic lithium solution and a depleted liquid resource; c) injecting a fluid into the reservoir, wherein the fluid comprises the depleted liquid resource and one or more of additional water, dissolved salts, a supercritical fluid, a non- aqueous fluid, or a gas.
  • a system for the extraction of lithium from a subsurface reservoir comprising: a) one or more production wells, wherein a liquid resource comprising lithium from the subsurface reservoir is produced; b) a treatment unit configured to treat the liquid resource by at least one of the following: WSGR Docket No.50741-724.601 i) modulating the pH of the liquid resource; ii) modulating the lithium concentration of the liquid resource; iii) contacting the liquid resource with a chemical additive, wherein the chemical additive is an oxidant or a reductant; or iv) removing metal impurities or organic impurities from the liquid resource; c) a lithium extraction unit configured to extract at least a portion of the lithium from the liquid resource to generate a synthetic lithium solution and a depleted liquid resource; d) one or more injection wells configured to inject a fluid into the reservoir, wherein the fluid comprises the depleted liquid resource and one or more of additional water, dissolved salts
  • FIG.1 illustrates the effective porosity of a reservoir for producing a liquid resource therefrom according to methods in the current state of the art.
  • FIG.2 illustrates the effective porosity of a reservoir for producing a liquid resource therefrom according to methods described in the present disclosure comprising injecting a fluid (e.g., a water-miscible fluid) into the reservoir.
  • a fluid e.g., a water-miscible fluid
  • FFI Free Fluid Index
  • BVI Bound Volume Irreducible
  • CBW Clay Bound Water
  • T2 nuclear magnetic resonance T2 relaxation time
  • NMR nuclear magnetic resonance.
  • FIG.3 provides a schematic of a process wherein injection of a fluid into a reservoir enhances lithium recovery from an immature modern salar reservoir.
  • FIG.4 provides a schematic of a process wherein injection of a fluid into a reservoir enhances lithium recovery from a mature modern day reservoir.
  • WSGR Docket No.50741-724.601 provides a schematic of a process wherein injection of a fluid into a reservoir enhances lithium recovery from a US carbonate reservoir.
  • FIG.6 provides a schematic of a process wherein injection of a fluid into a reservoir enhances lithium recovery from a European sandstone reservoir.
  • FIG.7 provides a schematic of a process wherein injection of a fluid into a reservoir enhances lithium recovery from a European fractured reservoir.
  • FIG.8 illustrates a series of steps associated with one example of a dispersion test that employs core samples imbued with a radioactive tracer.
  • FIG.9 provides a schematic of a process wherein injection of supercritical fluid CO 2 into a reservoir enhances lithium recovery therefrom.
  • FIG.10 provides a schematic of a process wherein injection of a fluid into a reservoir enhances the efficiency of a direct lithium extraction process, owing to changes in composition of the liquid resource over time that result from the continued injection of fluid.
  • FIG.11 provides a schematic of a process wherein injection of a fluid into a reservoir enhances lithium recovery from a reservoir fractured via hydraulic simulation.
  • DETAILED DESCRIPTION OF THE INVENTION [0019]
  • the singular forms “a,” “an,” and “the” include plural referents unless the context clearly dictates otherwise.
  • reference to “an agent” includes a plurality of such agents
  • reference to “the cell” includes reference to one or more cells (or to a plurality of cells) and equivalents thereof known to those skilled in the art, and so forth.
  • the words “column” and “vessel” are used interchangeably.
  • the vessel is 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, 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.
  • mass concentration of an ionic species is stated; for example, 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 (NO 3 -), or sulfate (SO 4 2- ).
  • an ion may comprise chloride (Cl-), nitrate (NO 3 -), or sulfate (SO 4 2- ).
  • the term “synthetic lithium solution” describes a solution comprising lithium that is not present in nature and obtained by a process for processing, WSGR Docket No.50741-724.601 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. In some embodiments, a synthetic lithium solution is used in place of a liquid resource. In some embodiments, a synthetic lithium solution is combined with a liquid resource. In some embodiments, 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). In some embodiments, a synthetic lithium solution is a brine concentrated by solar evaporation. [0025] The term “direct lithium extraction,” as used herein, 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.
  • the term “eluate,” as used herein, refers to a liquid input to employed for the removal of lithium from a lithium-selective sorbent.
  • An eluate can be acidic.
  • An eluate that has been placed in contact with a lithium-selective sorbent that releases lithium into the eluate is a lithium eluate.
  • a lithium eluate is a synthetic lithium solution.
  • a synthetic lithium solution is a lithium eluate.
  • the eluate is an acidic solution.
  • the protons of the acidic eluate displace the lithium on the ion exchange material to yield a synthetic lithium eluate.
  • lithium purity refers to the chemical purity of a lithium chemical, lithium compound, or a solution that comprises lithium or a lithium compound. In some embodiments, 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.
  • 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 used in any step or process according to the methods and systems for lithium recovery from a liquid resource as described herein.
  • the process fluid is the liquid resource.
  • the process fluid is the adjusting fluid.
  • the process fluid is the raffinate.
  • 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.
  • buffer refers to a solution that can resist pH change upon the addition of an acidic or basic components. A buffer can neutralize small amounts of added acid or base, thus maintaining the pH of a solution comprising the buffer.
  • a buffer is a solution comprising a weak acid and a salt of the corresponding conjugate base.
  • a buffer is a solution comprising a weak base and a salt of the corresponding conjugate acid.
  • a non-limiting example of a buffer is a solution of boric acid and sodium hydroxide.
  • 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.
  • the section headings used herein are for organizational purposes only and are not to be construed as limiting the subject matter described or preclude the combination of the subject matter of the disclosure under any one section heading with any other subject matter of the disclosure under any other section heading or any other subject matter of the disclosure.
  • Embodiments described herein with any one or more features can be readily combined with the features of any embodiments described further herein. Embodiments described herein are not limiting so as to wholly describe all embodiments of the disclosure.
  • the Liquid Resource As a liquid resource flows through an ion exchange device, the ion exchange material absorbs lithium while releasing hydrogen, causing a decrease in the pH of the liquid resource from which lithium is being extracted. pH values of less than about 6 in said liquid resource result in sub-optimal performance of the ion-exchange process because the higher hydrogen concentrations found at low pH result in the reversal of ion-exchange, wherein hydrogen is absorbed while lithium is released.
  • Said sub-optimal process performance is manifested as, but is not limited to, a slower uptake of lithium by the ion exchange material, lower purity of the lithium eluted from the ion exchange material, lower lithium uptake capacity of the ion exchange material, degradation of the ion exchange material, decreased lifetime of the ion exchange material which necessitates more frequent replacement thereof, slower elution of lithium from the ion exchange material in the presence of acid, and higher amounts of acid being required for the elution of lithium from the ion exchange material.
  • the pH value of the liquid resource can be maintained above a value of 6 by addition of an alkali.
  • said alkali is added before flow of the liquid resource through a bed or ion exchange material, or after flow of said liquid resource through a bed of ion exchange material, but not within the bed of ion exchange material where the lithium extraction process occurs.
  • the pH of the liquid resource decreases to a suboptimal value of less than about 6 during the time it takes for the liquid resource to flow through a bed of ion exchange material.
  • systems WSGR Docket No.50741-724.601 and methods described herein are used to moderate the decrease in pH of the liquid resource during contact of the liquid resource with ion exchange material.
  • a system e.g., a concentration modulation unit
  • concentration modulation unit is used to adjust the concentration of lithium in the liquid resource before it contacts an ion exchange material that extracts lithium from the liquid resource while releasing protons into the liquid resource.
  • said system decreases the lithium concentration of the liquid resource, such that less lithium is absorbed by the ion exchange material over the same amount of contact time, and therefore fewer protons are released into the liquid resource by the ion exchange material during this absorption process, leading to a higher pH of the liquid resource as it contacts the ion exchange material.
  • adjustment of the lithium concentration in the liquid resource is achieved by mixing the liquid resource with a raffinate stream, said raffinate stream comprising the liquid resource which has contacted ion exchange material to absorb a portion of the lithium.
  • Raffinate or a raffinate stream can comprise a lithium-depleted liquid resource.
  • a solution comprising a liquid resource and a raffinate can comprise a concentration-adjusted liquid resource according to some embodiments.
  • the production of lithium chemicals and lithium feedstocks suitable for industrial applications can involve the recovery of lithium from resources that contain lithium in addition to other components. Resources containing lithium in addition to other components can be a liquid resource.
  • the liquid resource is selected from the following list: a paleo brine, an oilfield brine, a subsurface brine, a natural brine, a salar brine, a dissolved salt flat brine, a lake brine, a geothermal brine, seawater, or combinations thereof.
  • a liquid resource is selected from the following list: a subsurface brine, a natural brine, a salar brine, a dissolved salt flat brine, a lake brine, a geothermal brine, seawater, 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.
  • the liquid resource is injected into a reservoir, salt lake, salt flat, basin, or other WSGR Docket No.50741-724.601 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.
  • a method for lithium recovery comprises placing a liquid resource or a solution comprising a liquid resource into contact with ion exchange material.
  • the lithium concentration of the liquid resource is adjusted before, during, or after lithium recovery.
  • a liquid resource is an aqueous solution comprising lithium suitable for use according to the methods and systems for lithium recovery disclosed herein.
  • the liquid resource is selected from the following list: a paleo brine, an oilfield brine, a subsurface brine, a natural brine, a salar brine, a dissolved salt flat brine, a lake brine, a geothermal brine, seawater, or combinations thereof.
  • a liquid resource is selected from the following list: a subsurface brine, a natural brine, a salar brine, a dissolved salt flat brine, a lake brine, a geothermal brine, seawater, or combinations thereof.
  • the liquid resource is a geothermal brine.
  • the liquid resource is a geothermal brine, a paleo brine, or an oilfield brine.
  • the liquid resource is a brine.
  • the liquid resource 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 liquid resource is heated or cooled to precipitate or dissolve species in the brine, or to facilitate removal of metals from the liquid resource.
  • the liquid resource 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 liquid resource 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 liquid resource contains WSGR Docket No.50741-724.601 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 liquid resource 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 greater than 150,000 mg/L.
  • the liquid resource 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 liquid resource 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 liquid resource 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 liquid resource 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 liquid resource 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 liquid resource is treated to produce a pre-treated liquid resource which has certain metals removed.
  • the term liquid resource as used in this disclosure shall be understood to also encompass a pre-treated liquid resource as described herein.
  • the pre-treated liquid resource 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 pre-treated liquid resource 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 pre-treated liquid resource 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 pre-treated liquid resource 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.
  • the pre-treated liquid resource contains WSGR Docket No.50741-724.601 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 pre-treated liquid resource e.g., the treated liquid resource
  • a lithium-depleted liquid resource is a raffinate.
  • the lithium- depleted liquid resource 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 pH of the liquid resource 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 liquid resource 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 liquid resource is corrected to precipitate or dissolve metals.
  • metals are precipitated from the liquid resource to form precipitates.
  • precipitates include transition metal hydroxides, oxy-hydroxides, sulfide, flocculants, aggregate, agglomerates, or combinations thereof.
  • the precipitates comprise 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 combinations 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.
  • WSGR Docket No.50741-724.601 precipitates are redissolved by combining the precipitates with an acidic solution.
  • precipitates are redissolved by combining the precipitates with an acidic solution in a mixing apparatus.
  • precipitates are redissolved by combining the precipitates with an acidic solution using a high-shear mixer.
  • Treatment of the Liquid Resource [0046]
  • the pH of the liquid resource is adjusted (e.g., modulated, regulated) before, during and/or after contact with ion exchange material to maintain the pH within a range that is suitable, preferred, or ideal for lithium recovery.
  • bases such as NaOH, LiOH, KOH, Mg(OH)2, Ca(OH)2, CaO, NH3, Na 2 SO 4 , K 2 SO 4 , NaHSO 4 , KHSO 4 , NaOCl, KOCl, NaClO 4 , KClO 4 , NaH 2 BO 3 , Na 2 HBO 3 , Na 3 BO 3 , KH 2 BO 3 , K 2 HBO 3 , K 3 BO 3 , MgHBO 3 , CaHBO 3 , NaHCO 3 , KHCO 3 , NaCO 3 , KCO 3 , MgCO3, CaCO3, Na2O, K2O, Na2CO3, K2CO3, Na3PO4, Na2HPO4, NaH2PO4, K3PO4, K2HPO4, KH2PO4, CaHPO4, MgHPO4, sodium acetate, potassium acetate, magnesium acetate, poly
  • precipitates For liquid resources that contain divalent ions such as Mg, Ca, Sr, or Ba, addition of base to the liquid resource can cause the formation of precipitates, such as Mg(OH) 2 or Ca(OH) 2 , which can hinder lithium recovery.
  • precipitates hinder lithium recovery in at least three ways. First, formation of precipitates can remove base from solution, leaving less base available in solution to neutralize protons and maintain pH within a range that is suitable, preferred, or ideal for lithium recovery. Second, precipitates that form due to base addition can hinder flow through an ion exchange device, including hindering flow over the surfaces of ion exchange material, through the pores of porous ion exchange beads, and through the voids between ion exchange material.
  • This hindering of flow can prevent lithium from being absorbed by the ion exchange material utilized in lithium recovery.
  • the hindering of flow can also cause large pressure differences between the inlet and outlet of an ion exchange device utilized for lithium recovery.
  • precipitates in an ion exchange device utilized for lithium recovery can dissolve when placed in contact with an acid eluent, and thereby contaminate the synthetic lithium solution produced by the ion exchange device utilized for lithium recovery.
  • an ideal pH range for the liquid resource is optionally 5 to 7
  • a preferred pH range is optionally 4 to 8
  • a suitable pH range is optionally 1 to 9.
  • an pH range for the liquid resource is optionally about 1 to about 14, about 2 to about 13, about 3 to WSGR Docket No.50741-724.601 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.
  • 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 liquid resource 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 centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, or a pusher centrifuge.
  • the filter uses a scroll or a vibrating device.
  • the filter is horizontal, vertical, or uses 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 filter cake growth.
  • gravitational, magnetic, centrifugal sedimentation, or other means of solid-liquid separation are used before, during, or after filtering to prevent filter 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 in 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 liquid resource tank to another liquid resource tank, from an acid tank to another acid tank, from a washing tank to another washing tank, from a liquid resource 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 liquid resource tank.
  • solid-liquid separation apparatuses use gravitational sedimentation.
  • solid-liquid separation apparatuses 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 comprise 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 comprise a tray thickener with a series of thickeners oriented vertically with a center axle and raking components.
  • solid-liquid separation apparatuses comprise a lamella type thickener with inclined plates or tubes that are smooth, flat, rough, or corrugated.
  • solid- liquid separation apparatuses comprise a gravity clarifier that comprises 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 comprise a particle trap. [0055] In some embodiments, the solid-liquid separation apparatuses use centrifugal sedimentation.
  • solid-liquid separation apparatuses comprise 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 comprise multiple feed points. In some embodiments, 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 such that precipitated metals get trapped at the bottom and center of the apparatus due to a “teacup effect”.
  • a chemical additive is added to the liquid resource.
  • a chemical additive is added to the synthetic lithium solution.
  • a chemical additive is added to the aqueous wash solution.
  • treatment of the liquid resource comprises adding a chemical additive to the liquid resource.
  • a redox modulation unit is configured to add a chemical additive to the liquid resource, the synthetic lithium solution, or a combination thereof.
  • a system configured to treat the liquid resource is configured to add a chemical additive to the liquid resource.
  • a chemical additive is a redox agent.
  • a chemical additive is an oxidant.
  • a chemical additive is a reductant.
  • 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 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, hypoflurite, 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 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 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 WSGR Docket No.50741-724.601 producing a lithium product from a liquid resource.
  • the methods and systems disclosed herein utilize ion exchange materials.
  • 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.
  • 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.
  • ion exchange particles are utilized as a mixture that comprises coated ion exchange particles and uncoated ion exchange particles.
  • ion exchange particles comprise one or more ion exchange materials.
  • ion exchange particles comprise a lithium- selective sorbent.
  • ion exchange beads are a construct that comprises ion exchange material that can be used according to the methods and systems described herein.
  • ion exchange beads comprise ion exchange material.
  • the ion exchange material is coated or uncoated.
  • the ion exchange beads are porous.
  • ion exchange beads comprise one or more ion exchange materials.
  • ion exchange beads comprise a lithium-selective sorbent.
  • Ion exchange beads can have diameters less than about one millimeter, contributing to a high pressure difference across a packed bed of ion exchange beads 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 ion exchange beads. 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 ion exchange beads comprises two vessels, three vessels, four vessels, five vessels, six vessels, seven vessels, eight WSGR Docket No.50741-724.601 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.
  • the ion exchange material absorb lithium while releasing hydrogen, where both the lithium and hydrogen are cations.
  • an eluent is used to elute the lithium from the ion exchange material to produce a lithium eluate.
  • a lithium eluate can be a synthetic lithium solution according to some embodiments.
  • an eluent comprises acid or an acid 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.
  • ion exchange beads comprise ion exchange materials in addition to other components.
  • ion exchange beads 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 exchange process can be repeated to extract lithium from a liquid resource and yield a synthetic lithium solution.
  • 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 ion exchange beads that can be loaded into an ion exchange device.
  • ion exchange beads comprise ion exchange materials in addition to other components and can be utilized in methods for lithium recovery and systems for lithium recovery.
  • the ion exchange beads as loaded into an ion exchange device, can be loaded such that void spaces are present between the ion exchange beads, 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 ion exchange beads hold their constituent ion exchange particles in place and prevent free movement of ion exchange particles throughout the ion exchange device. [0070] When ion exchange material is formed into ion exchange beads, the penetration of liquid resource and acid into the ion exchange beads by convention and diffusion can become unacceptably slow. A slow rate of convection and diffusion of the acid and liquid resource into the ion exchange beads can slow the kinetics of lithium absorption and release thereby.
  • the ion exchange beads comprise networks of pores that facilitate the transport of liquids flowed through an ion exchange device into the ion exchange beads.
  • the geometry and physical dimensions of pore networks in ion exchange beads 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 ion exchange bead leads to a more effective delivery lithium and hydrogen to the ion exchange material therein. More effective delivery of lithium and hydrogen to the ion exchange material within an ion exchange bead can lead to greater lithium recovery according to the methods and systems described herein. [0072]
  • the ion exchange beads are formed by mixing of ion exchange material, a structural matrix material, and a filler material.
  • the ion WSGR Docket No.50741-724.601 exchange beads are formed by mixing of ion exchange material and a structural matrix material. In some embodiments, the ion exchange beads are formed by mixing of ion exchange material and a structural matrix material. In some embodiments, the components of an ion exchange bead combined to form a physical mixture or a composite. In some embodiments wherein an ion exchange bead comprises a filler material, the filler material can be removed therefrom to form network of pores therein and yield a porous ion exchange bead. The filler material is dispersed in the bead in such a way to leave behind a pore structure that enables transport of lithium and hydrogen with fast kinetics.
  • an ion exchange bead comprises one or more ion exchange materials, one or more structural matrix materials, and one or more filler materials.
  • Ion exchange beads according to embodiments as described herein can be porous ion exchange beads.
  • 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 ion exchange beads 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 ion exchange beads 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 ion exchange beads 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 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 WSGR Docket No.50741-724.601 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 coating material is selected to facilitate one or more of the following objectives: using a coating material that has minimal negative impacts on the diffusion of lithium and hydrogen between the ion exchange material within the ion exchange particles and the liquid resource, enabling adherence of the ion exchange particles to a structural support or structural matrix material, and suppressing structural and mechanical degradation of the ion exchange particles.
  • the liquid resource containing lithium is flowed through the ion exchange device so that the ion exchange beads absorb lithium from the liquid resource while releasing hydrogen.
  • an acid is pumped through the ion exchange device so that the ion exchange beads 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.
  • ion exchange beads 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 beads are moved between multiple ion exchange devices, wherein the ion exchange beads form a moving bed that can be transferred from one ion exchange device to another.
  • ion exchange beads 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.
  • 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 particles are used in an ion exchange device
  • 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 when 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, WSGR Docket No.50741-724.601 Li2SnO3, Li4Ti5O12, Li4Mn5O12, LiMn2O4, Li1.6Mn1.6O4, LiAlO2, LiCuO2, LiTiO2, Li4TiO4, Li 7 Ti 11 O 24 , Li 3 VO 4 , Li 2 Si 3 O 7 , Li 2 CuP 2 O 7 , 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 In some embodiments, a coating material used to form a coating on an ion exchange material or on ion exchange particles that comprise an ion exchange material 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: TiO 2 , ZrO 2 , MoO 2 , SnO 2 , Nb 2 O 5 , Ta 2 O 5 , SiO 2 , Li 2 TiO 3 , Li 2 ZrO 3 , Li 2 SiO 3 , Li 2 MnO 3 , Li 2 MoO 3 , LiNbO 3 , LiTaO 3 , AlPO 4 , 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 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.
  • measurements of average particle diameter can vary according to the method of determination utilized. Determination of said average particle diameter according to one method to obtain one or more values shall be understood to inherently encompass all other values that may be obtained using other methods.
  • 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. In some embodiments, 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. In some embodiments, the average particle diameter is determined using laser diffraction, wherein an Anton-Parr particle size analyzer (PSA) instrument is used. In some embodiments, 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. [0084] In some embodiments, 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 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 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 WSGR Docket No.50741-724.601 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.
  • 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.
  • 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.
  • 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.
  • 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 structural matrix material is selected from the following list: a polymer, an oxide, a phosphate, or combinations thereof.
  • a structural matrix material is selected from the following list: polyvinyl fluoride, polyvinylidene difluoride, polyvinyl chloride, polyvinylidene dichloride, polyethylene, polypropylene, WSGR Docket No.50741-724.601 polyphenylene sulfide, polytetrafluoroethylene, polytetrafluoroethylene, sulfonated polytetrafluoroethylene, polystyrene, polydivinylbenzene, polybutadiene, sulfonated polymer, carboxylated polymer, Nafion, copolymers thereof, and combinations thereof.
  • a structural matrix material is selected from the following list: polyvinylidene difluoride, polyvinyl chloride, sulfonated polytetrafluoroethylene, polystyrene, polydivinylbenzene, copolymers thereof, or combinations thereof.
  • a structural matrix material is selected from the following list: titanium dioxide, zirconium dioxide, silicon dioxide, solid solutions thereof, or combinations thereof.
  • the structural matrix material is selected for its thermal durability, acid resistance, and/or other chemical resistance.
  • the porous ion exchange bead is formed by a process comprising mixing ion exchange particles, structural matrix material, and filler material together at once.
  • the porous ion exchange bead is formed by a process comprising mixing the ion exchange particles and the structural matrix material, and then mixing the resulting mixture with the filler material. In some embodiments, the porous ion exchange bead is formed by a process comprising mixing the ion exchange particles and the filler material, and then mixing the resulting mixture with the structural matrix material. In some embodiments, the porous ion exchange bead is formed by a process comprising mixing the structural matrix material and the filler material, and then mixing the resulting mixture with the ion exchange particles.
  • the porous ion exchange bead is formed by a process comprising mixing the ion exchange particles, the structural matrix material, and/or the filler material with a solvent that dissolves one or more of the components of the mixture. In some embodiments, the porous ion exchange bead is formed by a process comprising mixing the ion exchange particles, the structural matrix material, and/or the filler material as dry powders in a mixer or ball mill. In some embodiments, the porous ion exchange bead is formed by a process comprising mixing the ion exchange particles, the structural matrix material, and/or the filler material in a spray drier.
  • the structural matrix material is a polymer that is dissolved in a solvent and subsequently mixed with the ion exchange particles and/or filler material using a solvent from the following list: N-methyl-2-pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, or combinations thereof.
  • the filler material is a salt that is dissolved in a solvent and subsequently mixed with the ion exchange particles and/or structural matrix material using a solvent from the following list: water, ethanol, isopropyl alcohol, acetone, or combinations thereof.
  • the ion exchange beads comprise a filler material that is a salt that can be dissolved out of the ion exchange bead to form a network of pores within the ion exchange bead.
  • the ion exchange beads comprise a filler material that is a salt that can be dissolved out of the ion exchange bead using a solution selected from the following list: water, ethanol, isopropyl alcohol, a surfactant mixture, an acid, a base, or combinations thereof.
  • the ion exchange beads comprise a filler material 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 ion exchange bead.
  • the ion exchange beads comprise a filler material 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 ion exchange beads are formed from dry powder.
  • the ion exchange beads are formed using a mechanical press, a pellet press, a tablet press, a pill press, a rotary press, or combinations thereof.
  • the ion exchange beads are formed from a solvent slurry by dripping the solvent slurry into a solution comprising a different solvent.
  • the solvent slurry comprises N-methyl-2- pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, or combinations thereof.
  • the solution comprising a different solvent comprises water, ethanol, iso-propyl alcohol, acetone, or combinations thereof.
  • the ion exchange beads 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.
  • the porous ion exchange bead 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.
  • the ion exchange beads 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 ion exchange beads 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 ion exchange beads 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 WSGR Docket No.50741-724.601 than 100 mg/L, less than 10 mg/L, or combinations thereof.
  • 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 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.
  • 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. 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 50 cycles, greater than 100 cycles, or greater than 200 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
  • a synthetic lithium solution e.g., lithium eluate
  • 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: WSGR Docket No.50741-724.601 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.
  • ion exchange beads 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, beyerite, nordstrandite, alumina hydrate, bauxite, amorphous aluminum trihydroxide, activated alumina layered lithium-aluminum double hydroxides, LiAl 2 (OH) 6 Cl, 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 WSGR Docket No.50741-724.601 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.
  • 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.
  • 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- selective sorbents comprise lithium-selective ion exchange materials.
  • 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 beads. In some embodiments, the lithium selective sorbent comprises ion exchange beads. 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. [0117] In some embodiments, lithium-selective sorbents include other inorganic materials that selectively absorb lithium over other ions.
  • lithium-selective sorbents selectively absorb lithium over other ions by processes that do not comprise ion exchange.
  • the lithium-selective sorbent is 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, LiAl2(OH)6Cl, combinations thereof, compounds thereof, or solid solutions thereof.
  • An aspect of the invention described herein is a device wherein the lithium-selective sorbent comprises an ion exchange material.
  • An aspect of the invention described herein is a process wherein the lithium-selective sorbent comprises an ion-exchange material.
  • An aspect of the invention described herein is a system wherein the lithium-selective sorbent comprises an ion-exchange material.
  • An aspect of the invention described herein is a lithium-selective sorbent which extracts lithium from a liquid resource.
  • An aspect of the disclosure is a device, system, and associated process wherein the lithium-selective sorbent comprises a lithium aluminate intercalate.
  • the lithium aluminate intercalate mixed with a polymer material.
  • the polymer 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 polymer material comprises a co-polymer, a block co- polymer, a linear polymer, a branched polymer, a cross-linked polymer, a heat-treated polymer, a solution processed polymer, co-polymers thereof, mixtures thereof, or combinations thereof.
  • the polymer material 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), types of poly
  • the polymer 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 polymer material is combined with the lithium aluminate intercalate particles by dry mixing, mixing in solvent, emulsion, extrusion, bubbling one solvent into another, casting, heating, evaporating, vacuum evaporation, spray drying, vapor deposition, chemical vapor deposition, microwaving, hydrothermal synthesis, polymerization, co-polymerization, cross-linking, irradiation, catalysis, foaming, other deposition methods, or combinations thereof.
  • the polymer material is combined with the lithium aluminate intercalate particles using a solvent comprising N-methyl-2-pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, ethanol, acetone, other solvents, or combinations thereof.
  • a solvent comprising N-methyl-2-pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, ethanol, acetone, other solvents, or combinations thereof.
  • a coating can be deposited onto the lithium aluminate intercalate WSGR Docket No.50741-724.601 particles using a solvent comprising N-methyl-2-pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, ethanol, acetone, or combinations thereof.
  • the lithium aluminate intercalate comprises particles that have an average diameter less than about 10 nm, less than about 100 nm, less than about 1,000 nm, less than about 10,000 nm, or less than about 100,000 nm.
  • the lithium aluminate intercalate comprises particles that have an average size less than about 100 nm, less than about 1,000 nm, or less than about 10,000 nm.
  • the lithium aluminate intercalate particles comprise secondary particles comprised of smaller primary particles wherein the smaller primary particles have an average diameter less than about 10 nm, less than about 100 nm, less than about 1,000 nm, less than about 10,000 nm, or less than about 100,000 nm.
  • the lithium aluminate intercalate particles have an average diameter less than about 10 nm, less than about 100 nm, less than about 1,000 nm, less than about 10,000 nm, or less than about 100,000 nm.
  • the lithium aluminate intercalate particles have an average size less than about 100 nm, less than about 1,000 nm, or less than about 10,000 nm.
  • the lithium aluminate intercalate particles are optionally secondary particles comprised of smaller primary particles that have an average diameter less than about 10 nm, less than about 100 nm, less than about 1,000 nm, less than about 10,000 nm, or less than about 100,000 nm.
  • a system for lithium recovery from a liquid resource comprising an ion exchange device wherein one or more vessels are independently configured to simultaneously accommodate porous ion exchange beads moving in one direction and alternately acid, liquid resource, and optionally other process fluids moving in the net opposite direction.
  • This lithium recovery system produces an eluate that comprises lithium and optionally contains other ions.
  • an ion exchange device for lithium recovery from a liquid resource comprising a stirred tank reactor, an ion exchange material, and a pH modulating unit for increasing the pH of the liquid resource in the stirred tank reactor.
  • an ion exchange device for lithium recovery from a liquid resource comprising a stirred rank reactor, an ion exchange material, a pH modulating unit for increasing the pH of the liquid resource in the stirred tank reactor, and a compartment WSGR Docket No.50741-724.601 for containing the ion exchange material in the stirred tank reactor while allowing for removal of liquid resource, washing fluid, acid, and other process fluids from the stirred tank reactor.
  • at least one of the one or more vessels are fitted with a conveyer system suitably outfitted to move porous ion exchange beads upward and simultaneously allow a net flow of acid, liquid resource, and optionally other process fluids, downward.
  • the conveyor system comprises fins with holes.
  • the fins slide upward over a sliding surface that is fixed in place
  • all of the one or more vessels are fitted with a conveyor system suitably outfitted to move porous ion exchange beads upward and simultaneously allow a net flow of acid, liquid resource, and optionally other process solutions, downward.
  • the vessels are columns.
  • structures with holes are used to move the ion exchange material through one or more vessels.
  • the holes in the structures with holes are less than 10 microns, less than 100 microns, less than 1,000 microns, or less than 10,000 microns in diameter.
  • the structures with holes are attached to a conveyer system.
  • the structures with holes comprise a porous compartment, porous partition, or another porous structure.
  • the structures with holes contain a bed of fixed or fluidized ion exchange material.
  • the structures with holes contain ion exchange material while allowing liquid resource, aqueous solution, acid solution, or other process fluids to pass through the structures with holes.
  • the porous ion exchange beads comprise one or more ion exchange materials that reversibly exchange lithium and hydrogen and a structural matrix material sufficient to form and support a pore network.
  • the liquid resource comprises a paleo brine, an oilfield brine, a subsurface brine, a natural brine, a salar brine, a dissolved salt flat brine, a lake brine, a geothermal brine, seawater, or combinations thereof.
  • Methods of Modulating pH for the Extraction of Lithium [0128] An aspect of the invention described 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 invention described herein is a method of extracting lithium ions from a liquid resource, comprising: flowing the liquid resource through the plurality of columns WSGR Docket No.50741-724.601 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 invention described 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.
  • the liquid resource is optionally pre-treated prior to entering the ion exchange reactor to remove suspended solids, hydrocarbons, or organic molecules. In some embodiments, the liquid resource is optionally entered the ion exchange reactor without any pre-treatment following from its source. [0133] In some embodiments, 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 ppm, less than 100 ppm, less than 10 ppm, or combinations thereof. In some embodiments, 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 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, 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, or combinations thereof.
  • the acid solution comprises 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 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 WSGR Docket No.50741-724.601 than 5 M, less than 10 M, or combinations thereof.
  • the acid used for recovering lithium from the porous ion exchange beads has a concentration greater than 10 M.
  • acids with distinct concentrations are used during the elution process.
  • 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 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 synthetic 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 synthetic lithium solution that is yielded from the ion exchange reactor is concentrated using reverse osmosis or membrane technologies.
  • the synthetic lithium solution that is yielded from the ion exchange reactor e.g., extraction unit, extraction subsystem
  • the synthetic lithium solution that is yielded from the ion exchange reactor is further processed into lithium chemicals (e.g., lithium products) 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 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, WSGR Docket No.50741-724.601 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.
  • 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 liquid resource 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.
  • 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 material, 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. [0146] 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 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 WSGR Docket No.50741-724.601 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.
  • the lithiated ion exchange material is washed with an aqueous solution (e.g., an aqueous wash solution).
  • the method further comprises, prior to b), flowing the lithiated ion exchange material into a stripping system.
  • the method further comprises, prior to b), flowing the lithiated ion exchange material into a stripping system and stripping the lithiated ion exchange material.
  • 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.
  • 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. In some embodiments, 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. In some embodiments, base is added to the liquid resource to maintain the pH of the liquid 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 WSGR Docket No.50741-724.601 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.
  • 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.
  • the pH of the liquid resource drops out of a target pH range due to release of protons from an ion exchange material and a pH modulating setup adjusts 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 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. In some embodiments, the pH of the liquid resource is controlled in a certain range and then the pH of the liquid resource is allowed to drop. In some embodiments, 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. In some embodiments, base is added to a liquid resource to neutralize protons with monitoring of volumes or quantities of the base. In some embodiments, 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. In some embodiments, the rate of change of the pH of the liquid resource is measured to monitor the rate of lithium uptake. In some embodiments, 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. In some embodiments, the porous partition is a porous polymer partition. In some embodiments, the porous partition is a mesh or membrane. In some embodiments, the porous partition is a polymer mesh or polymer membrane. In some embodiments, the porous partition comprises one or more layers of mesh, membrane, or other porous structure.
  • the porous partition comprises one or more coarse meshes that provide structural support and one or more fine meshes and/or membranes that provide filtration.
  • the porous partition comprises a polyether ether ketone mesh, a polypropylene mesh, a polyethylene mesh, a polysulfone mesh, a polyester mesh, a polyamide mesh, a polytetrafluoroethylene mesh, an ethylene tetrafluoroethylene polymer mesh, a stainless steel mesh, a stainless steel mesh coated in polymer, a stainless steel mesh coated in ceramic, or a combination thereof, wherein the mesh WSGR Docket No.50741-724.601 is a course mesh, a fine mesh, or a combination thereof.
  • the porous polymer partition comprises a mesh comprising one or more blends of two or more of a polyether ether ketone, a polypropylene, a polyethylene, a polysulfone, a polyester, a polyamide, a polytetrafluoroethylene, or an ethylene tetrafluoroethylene polymer.
  • the porous partition comprises a polyether ether ketone membrane, a polypropylene membrane, a polyethylene membrane, a polysulfone membrane, a polyester membrane, a polyamide membrane, a polytetrafluoroethylene membrane, an ethylene tetrafluoroethylene polymer membrane, or combinations thereof.
  • the method further comprises, after a), draining the liquid resource through the porous partition after the production of the lithiated 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.
  • 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.
  • WSGR Docket No.50741-724.601 [0158]
  • 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.
  • 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 plurality of tanks to produce a lithiated ion exchange material, wherein each of the plurality of tanks in 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 (i) one or more compartments, and (ii)
  • 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 system of b); d) flowing an acid solution into the
  • 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 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 selected from the following list: a paleo brine, an oilfield brine, a subsurface brine, a natural brine, a salar brine, a dissolved salt flat brine, a lake brine, a geothermal brine, seawater, or combinations WSGR Docket No.50741-724.601 thereof.
  • the liquid resource is a brine.
  • the liquid resource comprises a natural brine, a synthetic brine, or a mixture of a natural and a synthetic brine.
  • the acid solution comprises hydrochloric acid, sulfuric acid, phosphoric acid, hydrobromic acid, chloric acid, perchloric acid, nitric acid, formic 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.
  • the acid solution comprises hydrochloric acid.
  • the acid solution comprises sulfuric acid.
  • the acid solution comprises phosphoric acid.
  • Continuous Process for Lithium Extraction 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 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 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 materials are typically small particles, which together constitute a fine powder. Small particle size is required to minimize the diffusion distance that lithium must travel into the core of the ion exchange particles. In some cases, these particles are coated with protective surface coatings to minimize dissolution of the ion exchange materials while allowing efficient transfer of lithium and hydrogen to and from the particles, as disclosed in WO2018089932 and incorporated in its entirety by reference.
  • One major challenge for lithium extraction using inorganic ion exchange particles is the loading of the particles into an ion exchange column in such a way that brine and acid can be pumped efficiently through the column with minimal clogging.
  • the materials can be formed into beads, and the beads can be loaded into the column.
  • This bead loading creates void spaces between the beads, and these void spaces facilitate pumping through the column.
  • the beads hold WSGR Docket No.50741-724.601 the ion exchange particles in place and prevent free movement of the particles throughout the column.
  • a slow rate of convection and diffusion of the acid and liquid resource solutions into the bead slows the kinetics of lithium absorption and release.
  • Such slow kinetics can create problems for column operation. Slow kinetics can require slow pumping rates through the column. Slow kinetics can also lead to low lithium recovery from the liquid resource and inefficient use of acid to elute the lithium.
  • an alternate phase is contacted with the ion exchange beads (e.g., lithium selective sorbent) during one or more of the steps of the process step.
  • the use of alternate phase speeds up the kinetics of ion exchange, enhances the forming of the ion exchange bed, controls liquid level height in one or more process tanks, or a combination thereof.
  • 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 is a liquid or gas.
  • said alternate phase is a non-aqueous liquid.
  • the alternate phase is non- aqueous liquid.
  • the alternate phase is a non-aqueous solution.
  • the alternate phase is an organic liquid such as an alkane, alcohol, oil, bio-organic oil, ester, ether, hydrocarbon, or a combination thereof.
  • the alternate phase is butane, pentane, hexane, acetone, diethyl ether, butanol, or combinations thereof.
  • 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 beads are porous ion exchange beads with networks of pores that facilitate the transport into the beads of solutions that are pumped through an ion exchange column. Pore networks can be strategically controlled to provide fast and distributed access for the liquid resource and acid solutions to penetrate into the bead and deliver lithium and hydrogen to the ion exchange particles.
  • the ion exchange beads are formed by mixing of ion exchange particles, a matrix material, and a filler material. These components are mixed and formed into a bead. Then, the filler material is removed from the bead to leave behind pores.
  • the filler material is dispersed in the bead in such a way to leave behind a pore structure that enables transport of lithium and hydrogen with fast kinetics.
  • This method can involve multiple ion exchange materials, multiple polymer materials, and multiple filler materials.
  • 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 synthetic lithium solution WSGR Docket No.50741-724.601 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.
  • the porous ion exchange beads can contain coated ion exchange particles for lithium extraction that are comprised of an ion exchange material and a coating material protecting the particle surface.
  • the coating protects the ion exchange material from dissolution and degradation during lithium elution in acid, during lithium uptake from a liquid resource, and during other aspects of an ion exchange process.
  • This coated particle enables the use of concentrated acids in the ion exchange process to yield synthetic lithium solutions.
  • 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, and fast ionic diffusion.
  • a coating material is selected to protect the particle from dissolution and chemical degradation during lithium recovery in acid and also during lithium uptake in various liquid resources.
  • the coating material is selected to facilitate one or more of the following objectives: diffusion of lithium and hydrogen between the particles and the liquid resources, enabling adherence of the particles to a structural support, and suppressing structural and mechanical degradation of the particles.
  • 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 can 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 can be operated in counter-flow mode with a liquid resource and acid solution alternately flowing through the column in opposite directions. Between flows of the liquid resource and the acid solution, the column can be treated or washed with water or other solutions for purposes such as adjusting pH in the column or removing potential contaminants.
  • the beads can form a fixed or moving bed, and the moving bed can move in counter-current to the liquid resource and acid flows.
  • the beads can be moved between multiple columns with moving beds where different columns are used for liquid resource, acid, water, or other flows.
  • the pH of the liquid can 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 WSGR Docket No.50741-724.601 through the column, the liquid resource can 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 liquid resource.
  • an 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 for protecting the surface of the ion exchange material 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.
  • a coating material is selected from the following list: TiO 2 , ZrO 2 , MoO 2 , SnO 2 , Nb 2 O 5 , Ta 2 O 5 , SiO 2 , Li 2 TiO 3 , Li 2 ZrO 3 , Li 2 SiO 3 , Li 2 MnO 3 , Li 2 MoO 3 , LiNbO 3 , LiTaO 3 , AlPO 4 , 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 list: TiO 2 , ZrO 2 , MoO 2 , SiO 2 , Li 2 TiO 3 , Li 2 ZrO 3 , Li 2 SiO 3 , Li 2 MnO 3 , LiNbO 3 , AlF 3 , 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.
  • 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.
  • the ion exchange particles have 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 and a coating material form one or more concentration gradients where the chemical composition of the particle ranges between two or more compositions.
  • the ion exchange materials and the coating materials form a concentration gradient 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 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 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 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 with physical characteristics selected from the following list: crystalline, amorphous, full coverage, partial coverage, uniform, non-uniform, or combinations thereof.
  • multiple coatings are deposited on the ion exchange material in an arrangement selected from the following list: concentric, patchwork, or combinations thereof.
  • the matrix is selected from the following list: a polymer, an oxide, a phosphate, or combinations thereof.
  • a structural support is selected from the following list: polyvinyl fluoride, polyvinylidene difluoride, polyvinyl chloride, polyvinylidene dichloride, polyethylene, polypropylene, polyphenylene sulfide, WSGR Docket No.50741-724.601 polytetrafluoroethylene, polytetrafluoroethylene, sulfonated polytetrafluoroethylene, polystyrene, polydivinylbenzene, polybutadiene, sulfonated polymer, carboxylated polymer, Nafion, copolymers thereof, and combinations thereof.
  • a structural support is selected from the following list: polyvinylidene difluoride, polyvinyl chloride, sulfonated polytetrafluoroethylene, polystyrene, polydivinylbenzene, copolymers thereof, or combinations thereof.
  • a structural support is selected from the following list: titanium dioxide, zirconium dioxide, silicon dioxide, solid solutions thereof, or combinations thereof.
  • the matrix material is selected for thermal resistance, acid resistance, and/or other chemical resistance. [0199]
  • the porous bead is formed by mixing the ion exchange particles, the matrix material, and the filler material together at once.
  • the porous bead is formed by first mixing the ion exchange particles and the matrix material, and then mixing with the filler material. In some embodiments, the porous bead is formed by first mixing the ion exchange particles and the filler material, and then mixing with the matrix material. In some embodiments, the porous bead is formed by first mixing the matrix material and the filler material, and then mixing with the ion exchange particles. [0200] In some embodiments, the porous bead is formed by mixing the ion exchange particles, the matrix material, and/or the filler material with a solvent that dissolves once or more of the components.
  • the porous bead is formed by mixing the ion exchange particles, the matrix material, and/or the filler material as dry powders in a mixer or ball mill. In some embodiments, the porous bead is formed by mixing the ion exchange particles, the matrix material, and/or the filler material in a spray drier.
  • the matrix material is a polymer that is dissolved and mixed with the ion exchange particles and/or filler material using a solvent from the following list: n- methyl-2-pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, or combinations thereof.
  • the filler material is a salt that is dissolved and mixed with the ion exchange particles and/or matrix material using a solvent from the following list: water, ethanol, iso-propyl alcohol, acetone, or combinations thereof.
  • the filler material is a salt that is dissolved out of the bead to form pores using a solution selected from the following list: water, ethanol, iso-propyl alcohol, a surfactant mixture, an acid a base, or combinations thereof.
  • the filler material is a material that thermally decomposes to form a gas at high temperature so that the gas can leave the bead to form pores, where the gas is selected from the following list: water WSGR Docket No.50741-724.601 vapor, oxygen, nitrogen, chlorine, carbon dioxide, nitrogen oxides, organic vapors, or combinations thereof.
  • the porous ion exchange bead is formed from dry powder using a mechanical press, a pellet press, a tablet press, a pill press, a rotary press, or combinations thereof.
  • the porous ion exchange bead is formed from a solvent slurry by dripping the slurry into a different liquid solution.
  • the solvent slurry can be formed using a solvent of n-methyl-2-pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, or combinations thereof.
  • the different liquid solution can be formed using water, ethanol, iso-propyl alcohol, acetone, or combinations thereof.
  • the porous ion exchange bead is 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.
  • the porous ion exchange bead is embedded in a support structure, which can be a membrane, a spiral-wound membrane, a hollow fiber membrane, or a mesh.
  • the porous ion exchange bead is embedded on a support structure comprised of a polymer, a ceramic, or combinations thereof.
  • the porous ion exchange bead is loaded directly into an ion exchange column with no additional support structure.
  • the liquid resource is selected from the following list: a paleo brine, an oilfield brine, a subsurface brine, a natural brine, a salar brine, a dissolved salt flat brine, a lake brine, a geothermal brine, seawater, 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 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 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, acetic acid, or WSGR Docket No.50741-724.601 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, or combinations thereof.
  • the acid used for recovering lithium from the porous ion exchange beads 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.
  • 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.
  • the porous ion exchange beads perform the ion exchange reaction repeatedly over a number of cycles selected from the following list: greater than 50 cycles, greater than 100 cycles, or greater than 200 cycles.
  • the synthetic 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, or combinations thereof.
  • the synthetic 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 synthetic 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 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. In some embodiments, the ion exchange materials are synthesized in a hydrated state with a sublattice fully or partly occupied by hydrogen.
  • An aspect of the invention 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. [0218] 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. In some embodiments, one or more particle traps comprise one filter.
  • 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. [0219] 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. [0220] In some embodiments, one or more particle traps comprise one or more meshes. In some embodiments, one or more particle traps comprises one mesh.
  • 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
  • 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. [0224] In some embodiments, 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.
  • WSGR Docket No.50741-724.601 [0225]
  • 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.
  • one or more particle traps comprise one or more centrifugal sedimentation devices internal to said tank.
  • one or more particle traps comprise 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 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.
  • the ion exchange particles are stirred by a mixer.
  • the ion exchange particles are stirred by a propeller.
  • 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. [0227] 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 WSGR Docket No.50741-724.601 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.
  • the lithium eluate solution (e.g., synthetic lithium 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, WSGR Docket No.50741-724.601 distillation, reverse osmosis, evaporation, purification, chemical precipitation, membrane electrolysis, or combinations thereof.
  • the lithium eluate is purified using hydroxide precipitation, carbonate precipitation, other precipitate, ion exchange, solvent extraction, and/or other extraction methods to remove divalent ions, multivalent ions, boron, or other chemical species.
  • the lithium eluate is concentrated using reverse osmosis, mechanical evaporation, mechanical vapor recompression, solar thermal heating, concentrated solar thermal heating, and/or solar evaporation.
  • 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.
  • impurities are removed from a synthetic lithium solution or a solution comprising lithium using an impurities selective ion exchange material, nanofiltration, chemical precipitation, electrochemical separation, 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.
  • Lithium Carbonate Precipitation [0238] In some embodiments, lithium chloride present in a lithium solution is converted to lithium carbonate. In some embodiments, a lithium solution is a synthetic lithium solution.
  • soda ash or equivalently sodium carbonate, is added to a lithium solution to WSGR Docket No.50741-724.601 increase the carbonate concentration of the solution (e.g., provide a lithium solution with an increased carbonate concentration).
  • soda ash is added to a lithium solution as a solid.
  • soda ash is added to a lithium solution as a liquid solution.
  • soda ash is added to a lithium solution as a slurry.
  • lithium hydroxide present in a lithium solution is converted to lithium carbonate.
  • lithium hydroxide present in a lithium solution is converted to lithium bicarbonate.
  • a lithium solution is a synthetic lithium solution.
  • carbon dioxide is added to a lithium solution to increase the carbonate concentration of the solution (e.g., provide a lithium solution with an increased carbonate concentration).
  • carbon dioxide is added to a lithium solution as a gas.
  • carbon dioxide is added to a lithium solution as a solution.
  • carbon dioxide is added to a lithium solution as a supercritical fluid.
  • carbon dioxide is added to a lithium solution as a solid.
  • a lithium solution with an increased carbonate concentration is heated to generate solid lithium carbonate.
  • the lithium solution and the soda ash are independently heated before they are combined, but the lithium solution with an increased carbonate concentration is not in itself heated.
  • a lithium solution with an increased carbonate concentration reaches a temperature of about 355 K to generate solid lithium carbonate.
  • a lithium solution with an increased carbonate concentration reaches a temperature of about 345 K to of about 365 K to generate solid lithium carbonate.
  • the generation of solid lithium carbonate takes place in a single tank.
  • the generation of solid lithium carbonate takes place in multiple tanks.
  • the generation of solid lithium carbonate takes place in multiple tanks arranged so that the outlet of one tank is fed into a subsequent tank.
  • each subsequent tank has a higher solids content than the previous tank.
  • the generation of solid lithium carbonate takes place in multiple tanks in fluid contact or communication with one another.
  • the tanks where lithium carbonate precipitates are crystallizers.
  • the crystallization tanks are heated. In some embodiments, the crystallization tanks are not heated. In some embodiments, the crystallization tanks are insulated. In some embodiments, the crystallization tanks are agitated tanks. In some embodiments, the crystallization tanks are mechanical vapor recompression units.
  • the crystallization tanks comprise one or more draft tube baffle crystallizers, which comprise an agitator, a center tube, and a cylindrical baffle to allowed clarified liquor to be withdrawn and thicken the operating slurry magma density.
  • only one crystallizer is WSGR Docket No.50741-724.601 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.
  • soda ash is added only to the first crystallizer in a series of crystallization tanks.
  • soda ash is added to the first two crystallizers in the series of crystallization tanks. In some embodiments, soda ash is added to the first three crystallizers in the series of crystallization tanks. In some embodiments, soda ash is added to all crystallizers in the series of crystallization tanks. [0242] In some embodiments, solid crystals of lithium carbonate are added to the first tank. In some embodiments, this facilitates the precipitation of lithium carbonate with desired properties. In some embodiments, solid crystals of lithium carbonate are added to several of the tanks where crystallization occurs. In some embodiments, said solid crystals are fed into the first tank as a slurry.
  • said slurry is collected from a thickener at the outlet of a series of lithium carbonate crystallization tanks.
  • sodium carbonate is added as a solution.
  • the concentration of sodium carbonate in said solution is approximately 30 % on a weight basis.
  • the concentration of sodium carbonate in said solution is higher than 25 % but lower than 35 % on a weight basis.
  • the concentration of sodium carbonate in said solution is higher than 10 % but lower than 20 % on a weight basis.
  • the concentration of sodium carbonate in said solution is higher than 20 % but lower than 30 % on a weight basis.
  • the concentration of sodium carbonate in said solution is higher than 30 % but lower than 40 % on a weight basis.
  • said solution is added at a temperature of about 70 to about 80 °C. In some embodiments, said solution is added at a temperature of about 75 to about 85 °C. In some embodiments, said solution is added at a temperature of about 80 to about 90 °C. In some embodiments, said solution is added at a temperature of about 90 to about 100 °C. In some embodiments, said solution is filtered prior to addition to the lithium carbonate precipitation tanks.
  • said solution of sodium carbonate is prepared by dissolving sodium carbonate in a liquid. In some embodiments, said liquid is water.
  • said liquid is water that has been used to wash lithium carbonate crystals. In some embodiments, said liquid contains dissolved lithium carbonate. In some embodiments, said liquid is filtered. [0245] In some embodiments, the size of solids produced in the crystallizers is from about 60 to about 70 microns. In some embodiments, the size of solids produced in the crystallizers is from about 75 to about 85 microns. In some embodiments, the side of the solids produced in the WSGR Docket No.50741-724.601 crystallizers is 80 microns. In some embodiments, the size of solids produced in the crystallizers is from about 60 to about 70 microns.
  • the size of solids produced in the crystallizers is from about 70 to about 80 microns. In some embodiments, the size of solids produced in the crystallizers is from about 80 to about 90 microns. In some embodiments, the size of solids produced in the crystallizers is from about 90 to about 100 microns. In some embodiments, the size of solids produced in the crystallizers is from about 100 to about 120 microns. In some embodiments, the size of solids produced in the crystallizers is from about 120 to about 140 microns. In some embodiments, the size of solids produced in the crystallizers is from about 140 to about 200 microns.
  • the individual lithium carbonate crystals have a size of from about 20 to about 40 microns, but these crystals aggregate to form larger solids. In some embodiments, the final lithium carbonate crystals are micronized to a size of about 5 microns.
  • solid lithium carbonate is separated from its mother liquor. In some embodiments, solid lithium carbonate is separated from its mother liquor by centrifugation. In some embodiments, solid lithium carbonate is separated from its mother liquor by employing a filter press. In some embodiments, solid lithium carbonate is separated from its mother liquor by employing a belt filter. In some embodiments, the solids are washed with water to remove impurities.
  • the lithium carbonate solids are redissolved in water and recrystallized with a second system as the one described above, resulting in a solid lithium carbonate product with reduced impurities.
  • the lithium carbonate solids are re-slurried in pure water, re-separated in a solid-liquid separator, and re-washed.
  • the lithium carbonate solids are re-slurried in water, carbon dioxide is added to dissolve the solids, and said solids are recrystallized, resulting in solids of higher purity. In some embodiments, said dissolution occurs at ambient temperature.
  • lithium phosphate is generated in a solid form, wherein the lithium phosphate comprises lithium derived from a synthetic lithium solution.
  • the synthetic lithium solution is obtained according to a process for extracting lithium from a liquid resource with a lithium selective sorbent. The synthetic lithium solution can have previously been subjected to one or more steps or processes for purifying or otherwise modulating the synthetic lithium solution prior to the precipitation of WSGR Docket No.50741-724.601 lithium phosphate therefrom.
  • a synthetic lithium solution can be purified by adding a first aliquot of phosphate to precipitate impurities as detailed herein to provide a synthetic lithium solution reduced in impurities from which lithium phosphate is then precipitated.
  • lithium phosphate obtained as a solid or in solution according to the processes and methods described herein can comprise lithium in addition to any one or more of phosphate (PO 4 3- ), hydrogen phosphate (HPO 4 2- ), dihydrogen phosphate (H 2 PO 4 - ), phosphoric acid (H3PO4), salts thereof (e.g., salts with sodium, potassium rubidium, ammonium, etc.), and combinations thereof.
  • the stoichiometry and compositions of solids comprising lithium (e.g., lithium phosphate) obtained according to any of the methods and processes detailed under this sub- heading shall be understood to depend on at least the concentrations of the various components in the synthetic lithium solution.
  • the stoichiometry and compositions of solids comprising lithium obtained according to any of the methods and processes detailed under this sub-heading can depend on one or more of pH, temperature, and oxidation-reduction potential of the synthetic lithium solution.
  • the solids comprising lithium (e.g., lithium phosphate) comprise Li 3 PO 4 .
  • the solids comprising lithium (e.g., lithium phosphate) comprise Li2HPO4.
  • the solids comprising lithium comprise LiH2PO4. In some embodiments, the solids comprising lithium (e.g., lithium phosphate) comprise hydroxide. In some embodiments, the solids comprising lithium (e.g., lithium phosphate) comprise water (e.g., waters of hydration incorporated into the crystalline lattice of one or more compounds that constitute the solids comprising lithium). In some embodiments, lithium phosphate obtained from a synthetic lithium solution is used as a precursor in the synthesis of LiFePO 4 .
  • phosphate e.g., a phosphate salt
  • a phosphate source e.g., a phosphate salt
  • a salt comprising at least a cation derived from the phosphate source remains dissolved in solution.
  • sodium phosphate Na 3 PO 4
  • Na 3 PO 4 sodium phosphate
  • sodium phosphate Na3PO4
  • sodium phosphate Na3PO4
  • ammonium phosphate (NH4)3PO4) is added to a synthetic lithium solution to precipitate lithium from the synthetic lithium solution in the form of lithium phosphate.
  • WSGR Docket No.50741-724.601 ammonium phosphate ((NH4)3PO4) is added to a synthetic lithium solution to precipitate lithium from the synthetic lithium solution in the form of lithium phosphate, wherein the ammonium cations also serve to neutralize base within the synthetic lithium solution.
  • the lithium phosphate obtained is substantially free of impurities (e.g., Ca, Mg, Mn, Fe, Sr, etc.).
  • impurities e.g., Ca, Mg, Mn, Fe, Sr, etc.
  • phosphate is added to a synthetic lithium solution to precipitate compounds of calcium, magnesium, manganese, iron, and strontium from the synthetic lithium solution while also precipitating lithium from the synthetic lithium solution in the form of lithium phosphate.
  • phosphate is added to the synthetic lithium solution in the form of phosphate (PO 4 3- ), hydrogen phosphate (HPO 4 2- ), dihydrogen phosphate (H 2 PO 4 -), phosphoric acid (H 3 PO 4 ), including salts thereof (e.g., salts with sodium, potassium rubidium, ammonium, etc.) and combinations thereof.
  • phosphate PO 4 3-
  • hydrogen phosphate HPO 4 2-
  • dihydrogen phosphate H 2 PO 4 -
  • phosphoric acid H 3 PO 4
  • salts thereof e.g., salts with sodium, potassium rubidium, ammonium, etc.
  • a phosphate source is added to the synthetic lithium solution in the form of phosphate (PO 4 3- ), hydrogen phosphate (HPO 4 2- ), dihydrogen phosphate (H 2 PO 4 -), phosphoric acid (H 3 PO 4 ), including salts thereof (e.g., salts with sodium, potassium rubidium, ammonium, etc.) and combinations thereof.
  • a phosphate source comprises one or more cations selected from: sodium, potassium, and ammonium.
  • the synthetic lithium solution comprises one or more anions selected from: chloride, carbonate, bromide, sulfate, and nitrate; wherein the one or more anions remain dissolved in solution following the precipitation of lithium phosphate from the synthetic lithium solution.
  • the quantity of phosphate added to the synthetic lithium solution is between about 0.1 to about 10 molar equivalents with respect to the quantities of lithium in the synthetic lithium solution. In some embodiments, between about 0.1 to about 1 molar equivalents of phosphate are added to the synthetic lithium solution. In some embodiments, between about 1 to about 2 molar equivalents of phosphate are added to the synthetic lithium solution.
  • between about 2 to about 3 molar equivalents of phosphate are added to the synthetic lithium solution. In some embodiments, between about 3 to about 4 molar equivalents of phosphate are added to the synthetic lithium solution. In some embodiments, between about 4 to about 5 molar equivalents of phosphate are added to the synthetic lithium solution. In some embodiments, between about 5 to about 6 molar equivalents of phosphate are added to the synthetic lithium solution. In some embodiments, between about 6 to about 7 molar equivalents of phosphate are added to the synthetic lithium solution. In some embodiments, between about 7 to about 8 molar equivalents of phosphate are added to the synthetic lithium solution.
  • between about 8 to about 9 molar equivalents of phosphate are added to the synthetic lithium solution. In some embodiments, between about 9 to about 10 molar equivalents of phosphate are added to the synthetic lithium solution. In some WSGR Docket No.50741-724.601 embodiments, about 0.1, about 0.5, about 1, about 2, about 3, about 4, about 5, about 6, about 7, about 8, about 9, or about 10 equivalents of phosphate are added to the synthetic lithium solution. [0252] In some embodiments, the pH of the synthetic lithium solution is modulated before the addition of phosphate. In some embodiments, the pH of the synthetic lithium solution is modulated after the addition of phosphate. In some embodiments, the pH of the synthetic lithium solution is modulated by the addition of phosphate.
  • the pH of the synthetic lithium solution is modulated by the addition of an acid. In some embodiments, the pH of the synthetic lithium solution is modulated by the addition of a base. Said modulation can raise the pH of the synthetic lithium solution. Said modulation can lower the pH of the synthetic lithium solution. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 0 and about 14. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 0. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 1. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 2. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 3. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 4.
  • the pH of the synthetic lithium solution following said modulation is about 5. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 6. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 7. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 8. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 9. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 10. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 11. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 12. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 13. In some embodiments, the pH of the synthetic lithium solution following said modulation is about 14.
  • the pH of the synthetic lithium solution following said modulation is between about 1 and about 3. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 1 and about 4. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 1 and about 7. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 2 and about 4. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 2 and about 7. In some embodiments, the pH of the synthetic lithium solution following WSGR Docket No.50741-724.601 said modulation is between about 3 and about 7. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 4 and about 7.
  • the pH of the synthetic lithium solution following said modulation is between about 7 and about 9. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 7 and about 11. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 7 and about 13. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 9 and about 11. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 9 and about 13. In some embodiments, the pH of the synthetic lithium solution following said modulation is between about 11 and about 13. [0253] In some embodiments, the oxidation-reduction potential of the synthetic lithium solution is modulated before the addition of phosphate.
  • modulation of a oxidation-reduction potential can be achieved by adding a chemical additive.
  • the oxidation-reduction potential of the synthetic lithium solution is modulated after the addition of phosphate.
  • the oxidation-reduction potential of the synthetic lithium solution is modulated by the addition of phosphate.
  • Said modulation can raise the oxidation-reduction potential of the synthetic lithium solution.
  • Said modulation can lower the oxidation-reduction potential of the synthetic lithium solution.
  • the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 50.0 mV and less than about 800.0 mV.
  • the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 100.0 mV and less than about 500.0 mV. In some embodiments, the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 200.0 mV and less than about 400.0 mV. In some embodiments, the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about -450.0 mV and less than about 0.0 mV. In some embodiments, the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about -200.0 mV and less than about 50.0 mV.
  • the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about -50.0 mV and less than about 100.0 mV. In some embodiments, the oxidation- reduction potential of the synthetic lithium solution following modulation is greater than about 50.0 mV and less than about 300.0 mV. In some embodiments the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 100.0 mV and less than about 400.0 mV. In some embodiments, the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 200.0 mV and less than about 600.0 WSGR Docket No.50741-724.601 mV.
  • the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 300.0 mV and less than about 800.0 mV. In some embodiments, the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 500.0 mV and less than about 1000.0 mV. In some embodiments, the oxidation-reduction potential of the synthetic lithium solution following modulation is greater than about 750.0 mV and less than about 1100.0 mV. [0254] In some embodiments of the methods, processes, and systems disclosed herein, following the precipitation of lithium phosphate from a synthetic lithium solution, the synthetic lithium solution is retained in a tank for a period of time that is a residence time.
  • the synthetic lithium solution is retained in a tank for a period of time that is a residence time.
  • the synthetic lithium solution is agitated during the residence time.
  • the synthetic lithium solution is not agitated during the residence time.
  • the residence time is between about 1 second and about 10 days.
  • the residence time is between about 1 second and about 300 seconds.
  • the residence time is between about 1 minute and about 5 minutes.
  • the residence time is between about 5 minutes and about 10 minutes.
  • the residence time is between about 10 minutes and about 30 minutes.
  • the residence time is between about 30 minutes and about 60 minutes. In some embodiments, the residence time is between about 1 hour and about 3 hours. In some embodiments, the residence time is between about 3 hour and about 6 hours. In some embodiments, the residence time is between about 6 hour and about 12 hours. In some embodiments, the residence time is between about 12 hour and about 24 hours. In some embodiments, the residence time is between about 1 day and about 2 days. In some embodiments, the residence time is between about 2 days and about 3 days. In some embodiments, the residence time is between about 3 days and about 5 days. In some embodiments, the residence time is between about 5 days and about 7 days. In some embodiments, the residence time is between about 7 days and about 10 days.
  • the synthetic lithium solution is separated from any solids present in the tank.
  • the synthetic lithium solution is separated from any solids present in the tank (e.g., lithium phosphate) by a method of liquid- solid separation.
  • lithium phosphate solids are separated from a liquid phase using a particle trap.
  • the methods, processes, and systems disclosed herein comprise a liquid-solid separation method.
  • said methods comprise filtration, gravity WSGR Docket No.50741-724.601 sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
  • said method comprises filtration.
  • the filter is a belt filter, 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 may use a scroll or a vibrating device.
  • the filter is horizontal, vertical, or may use a siphon.
  • a liquid-solid separation method is used to collect lithium phosphate for further use.
  • precipitation of lithium phosphate comprises the addition of seed crystals to the synthetic lithium solution.
  • the addition of seed crystals to the synthetic lithium solution increases the rate of precipitation (of impurities and/or lithium) from the synthetic lithium solution.
  • the addition of seed crystals to the synthetic lithium solution increases the average particle size (by volume) of the precipitates obtained by precipitation (of impurities and/or lithium) from the synthetic lithium solution.
  • the seed crystals comprise the same chemical compound as the compound being precipitated from the synthetic lithium solution (e.g., lithium phosphate).
  • the seed crystals do not comprise the same chemical compound as the compound being precipitated from the synthetic lithium solution.
  • the seed crystals have an average diameter of about 0.1 micron to about 5 mm. In some embodiments, the seed crystals have an average diameter of about 0.1 micron to about 1 micron. In some embodiments, the seed crystals have an average diameter of about 1 micron to about 10 microns. In some embodiments, the seed crystals have an average diameter of about 10 microns to 100 microns. In some embodiments, the seed crystals have an average diameter of about 100 microns to 500 microns. In some embodiments, the seed crystals have an average diameter of about 500 microns to 1 mm.
  • the seed crystals have an average diameter of about 1 mm to 2 mm. In some embodiments, the seed crystals have an average diameter of about 2 mm to 3 mm. In some embodiments, the seed crystals have an average diameter of about 3 mm to 5 mm. [0257] In some embodiments, seed crystals are added in a quantity between about 0.01 g/L and about 10 g/L. In some embodiments, seed crystals are added in a quantity between about 0.1 g/L and about 10 g/L. In some embodiments, seed crystals are added in a quantity between about 1 g/L and about 10 g/L.
  • seed crystals are added in a quantity between about 1.0 g/L and about 10 g/L, about 2.0 g/L and about 10 g/L, about 3.0 g/L and about 10 g/L, about WSGR Docket No.50741-724.601 4.0 g/L and about 10 g/L, about 5.0 g/L and about 10 g/L, about 6.0 g/L and about 10 g/L, about 7.0 g/L and about 10 g/L, about 8.0 g/L and about 10 g/L, or about 9.0 g/L and about 10 g/L.
  • seed crystals are added in a quantity between about 0.10 g/L and about 1.0 g/L, about 0.20 g/L and about 1.0 g/L, about 0.30 g/L and about 1.0 g/L, about 0.40 g/L and about 1.0 g/L, about 0.50 g/L and about 1.0 g/L, about 0.60 g/L and about 1.0 g/L, about 0.70 g/L and about 1.0 g/L, about 0.80 g/L and about 1.0 g/L, or about 0.90 g/L and about 1.0 g/L.
  • seed crystals are added in a quantity between about 0.01 g/L and about 0.1 g/L, about 0.02 g/L and about 0.1 g/L, about 0.03 g/L and about 0.1 g/L, about 0.04 g/L and about 0.1 g/L, about 0.05 g/L and about 0.1 g/L, about 0.06 g/L and about 0.1 g/L, about 0.07 g/L and about 0.1 g/L, about 0.08 g/L and about 0.1 g/L, or about 0.09 g/L and about 0.1 g/L.
  • seed crystals are added in a quantity that is about 1.0 g/L, about 2.0 g/L, about 3.0 g/L, about 4.0 g/L, about 5.0 g/L, about 6.0 g/L, about 7.0 g/L, about 8.0 g/L, about 9.0 g/L, or about 10 g/L.
  • seed crystals are added in a quantity that is about 0.10 g/L, about 0.20 g/L, about 0.30 g/L, about 0.40 g/L, about 0.50 g/L, about 0.60 g/L, about 0.70 g/L, about 0.80 g/L, about 0.90 g/L, or about 1.0 g/L.
  • seed crystals are added in a quantity that is about 0.01 g/L, about 0.02 g/L, about 0.03 g/L, about 0.04 g/L, about 0.05 g/L, about 0.06 g/L, about 0.07 g/L, about 0.08 g/L, about 0.09 g/L, or about 0.1 g/L.
  • seed crystals are added in a quantity that is below 0.05 g/L, then the average diameter of said seed crystals is below 6 microns or above 25 microns. In some embodiments, if seed crystals are added in a quantity that is below 0.05 g/L, then the average diameter of said seed crystals is below 6 microns.
  • lithium phosphate is converted into one or more other compounds of lithium.
  • the other compounds of lithium have a higher aqueous solubility as compared to that of lithium phosphate.
  • the other compounds of lithium comprise: lithium hydroxide, lithium chloride, lithium bromide, lithium fluoride, lithium sulfate, lithium hydroxide monohydrate, lithium carbonate, lithium bicarbonate, lithium hydrogencarbonate, or combinations thereof.
  • WSGR Docket No.50741-724.601 It shall be understood for the purposes of the present disclosure that embodiments directed to the conversion of lithium phosphate are also operably directed to the solids comprising lithium and phosphate as detailed herein that can be obtained from synthetic lithium solutions as detailed herein.
  • solid lithium phosphate or a suspension thereof in an aqueous medium is added to a solution or suspension of an anion source (e.g., a metathesis salt) in an aqueous medium to provide a solution of one or more other lithium compounds.
  • an anion source e.g., a metathesis salt
  • solid lithium phosphate or a suspension thereof in an aqueous medium is added to solid lithium phosphate or a suspension thereof in an aqueous medium to provide a solution of one or more other lithium compounds.
  • solid lithium phosphate or a suspension thereof in an aqueous medium is added to a solution or suspension of an anion source (e.g., a metathesis salt) in an aqueous medium to provide a solution of one or more other lithium compounds and a suspension of precipitates that comprise phosphate (e.g., the solid phosphate salt).
  • an acid is added to facilitate the conversion of lithium phosphate into one or more other lithium compounds.
  • a base is added to facilitate the conversion of lithium phosphate into one or more other lithium compounds.
  • an acid is added to reduce the solubility of the precipitates that comprise phosphate.
  • the base comprises NaOH, KOH, Mg(OH) 2 , Ca(OH) 2 , CaO, Sr(OH) 3 , organic bases (e.g., acetate, formate, propanoate, citrate, lactate, other carboxylates, methoxide, ethoxide, isopropoxide, butoxides, other alkoxides, amines), other bases, or combinations thereof.
  • the base comprises NaOH or KOH.
  • a solubilizing agent is added to facilitate the conversion of lithium phosphate into one or more other lithium compounds.
  • the anion source (e.g., the metathesis salt) comprises an anion selected from: chloride, bromide, fluoride, bicarbonate, sulfate, hydroxide, nitrate, and combinations thereof.
  • the anion source comprises an acid selected from: hydrochloric acid, hydrobromic acid, hydrofluoric acid, sulfuric acid, nitric acid, organic acids (e.g., acetic acid, formic acid, propanoic acid, citric acid, lactic acid, other carboxylic acids), or combinations thereof.
  • the anion source comprises hydrochloric acid.
  • the anion source comprises nitric acid.
  • the anion source comprises sulfuric acid.
  • the anion source (e.g., the metathesis salt) WSGR Docket No.50741-724.601 comprises a cation selected from: calcium, magnesium, strontium, barium, sodium, potassium, aluminum, and combinations thereof.
  • the anion source comprises one or more of Al(OH) 3, CaCl 2 , CaSO 4 , Ca(OH) 2 , MgCl 2 , MgSO 4 , and Mg(OH) 2 .
  • the anion source comprises Ca(OH)2.
  • the anion source comprises Mg(OH)2.
  • the anion source comprises CaCl2.
  • the anion source comprises MgCl 2 . In some embodiments, the anion source comprises CaSO4. In some embodiments, the anion source comprises MgSO4. In some embodiments, the anion source comprises Al(OH)3.
  • the solubilizing agent comprises a gas. In some embodiments, the gas comprises HCl gas, CO 2 , SO 2 , SO 3 , H 2 S, NO, NO 2 , or combinations thereof. In some embodiments, the solubilizing agent comprises carbon dioxide. In some embodiments, the solubilizing agent comprises SO 2 . In some embodiments, the solubilizing agent comprises glycerol.
  • the solubilizing agent comprises a chelating agent (e.g., a chelator) as detailed herein.
  • the chelating agent is selected from EDTA, egtazic acid, citric acid, a compound comprising oxalate, salts thereof, or combinations thereof.
  • the chelating agent is selected from EDTA, citric acid, a compound comprising oxalate, or combinations thereof.
  • the chelating agent is EDTA.
  • the chelating agent is citric acid.
  • the chelating agent comprises oxalate.
  • the chelating agent is egtazic acid.
  • the chelating agent comprises a minopolycarboxylic acid, a nitrilotriacetic acid, a salt thereof, or a combination thereof.
  • the pH of the aqueous medium wherein lithium phosphate is converted into one or more other lithium compounds is modulated prior to addition of the anion source. In some embodiments, the pH of the aqueous medium wherein lithium phosphate is converted into one or more other lithium compounds is modulated following addition of the anion source. In some embodiments, the pH of the aqueous medium wherein lithium phosphate is converted into one or more other lithium compounds is modulated by the addition of the anion source.
  • the pH of the aqueous medium is modulated by the addition of an acid. In some embodiments, the pH of aqueous medium is modulated by the addition of a base. Said modulation can raise the pH of the aqueous medium. Said modulation can lower the pH of the aqueous medium. In some embodiments, the pH of the aqueous medium following said modulation is between about 0 and about 14. In some embodiments, the pH of the aqueous medium following said modulation is about 0. In some embodiments, the pH of the aqueous medium following said modulation is about 1. In some embodiments, the pH of the aqueous medium following said modulation is about 2.
  • the pH of the aqueous WSGR Docket No.50741-724.601 medium following said modulation is about 3. In some embodiments, the pH of the aqueous medium following said modulation is about 4. In some embodiments, the pH of the aqueous medium following said modulation is about 5. In some embodiments, the pH of the aqueous medium following said modulation is about 6. In some embodiments, the pH of the aqueous medium following said modulation is about 7. In some embodiments, the pH of the aqueous medium following said modulation is about 8. In some embodiments, the pH of the aqueous medium following said modulation is about 9. In some embodiments, the pH of the aqueous medium following said modulation is about 10.
  • the pH of the aqueous medium following said modulation is about 11. In some embodiments, the pH of the aqueous medium following said modulation is about 12. In some embodiments, the pH of the aqueous medium following said modulation is about 13. In some embodiments, the pH of the aqueous medium following said modulation is about 14. In some embodiments, the pH of the aqueous medium following said modulation is between about 1 and about 3. In some embodiments, the pH of the aqueous medium following said modulation is between about 1 and about 4. In some embodiments, the pH of the aqueous medium following said modulation is between about 1 and about 7. In some embodiments, the pH of the aqueous medium following said modulation is between about 2 and about 4.
  • the pH of the aqueous medium following said modulation is between about 2 and about 7. In some embodiments, the pH of the aqueous medium following said modulation is between about 3 and about 7. In some embodiments, the pH of the aqueous medium following said modulation is between about 4 and about 7. In some embodiments, the pH of the aqueous medium following said modulation is between about 7 and about 9. In some embodiments, the pH of the aqueous medium following said modulation is between about 7 and about 11. In some embodiments, the pH of the aqueous medium following said modulation is between about 7 and about 13. In some embodiments, the pH of the aqueous medium following said modulation is between about 9 and about 11.
  • the pH of the aqueous medium following said modulation is between about 9 and about 13. In some embodiments, the pH of the aqueous medium following said modulation is between about 11 and about 13.
  • the precipitates e.g., the solid phosphate salt
  • the precipitates comprise about 100% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise about 90% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise more than 90% of the phosphate derived from the lithium phosphate.
  • the precipitates comprise about 80% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates (e.g., the WSGR Docket No.50741-724.601 solid phosphate salt) comprise more than 80% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 70% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise about 60% of the phosphate derived from the lithium phosphate.
  • the precipitates comprise about 50% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise about 40% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise about 30% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 20% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise about 10% of the phosphate derived from the lithium phosphate.
  • the precipitates comprise less than about 10% of the phosphate derived from the lithium phosphate.
  • the precipitates form following modulation of the pH of the aqueous medium. In some embodiments, lowering the pH of the aqueous medium increases the quantity of precipitates (e.g., the solid phosphate salt). In some embodiments, increasing the pH of the aqueous medium increases the quantity of precipitates (e.g., the solid phosphate salt).
  • the composition of the precipitates can vary just as the composition of the synthetic lithium solution, the source of phosphate added thereto, and the lithium phosphate solids obtained therefrom can vary.
  • the precipitates e.g., the solid phosphate salt
  • the precipitates are described and characterized, in part or in whole, in terms of their elemental and/or ionic constituents.
  • the precipitates are described and characterized, in part or in whole, in terms of their chemical properties (e.g., solubility, including pH-dependent solubility).
  • the composition of the precipitates is inferred by differential analysis of the synthetic lithium solution before and after the precipitates are formed therefrom. In some embodiments, the composition of the precipitates varies with dependence on the pH of the synthetic lithium solution. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise one chemical compound. In some embodiments, the precipitates (e.g., the solid phosphate salt) comprise multiple chemical compounds.
  • the aqueous medium comprises about 100% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 90% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises more than 90% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 80% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises more than 80% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 70% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 60% of the lithium derived from the lithium phosphate.
  • the aqueous medium comprises about 50% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 40% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 30% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 20% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises about 10% of the lithium derived from the lithium phosphate. In some embodiments, the aqueous medium comprises less than about 10% of the lithium derived from the lithium phosphate. In some embodiments, the lithium content of the aqueous medium increases following modulation of the pH of the aqueous medium.
  • the one or more other lithium compounds are separated from the aqueous medium by nanofiltration.
  • nanofiltration utilizes one or more nanofiltration membrane units arranged in series and/or parallel.
  • nanofiltration utilizes a nanofiltration membrane material.
  • the 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 WSGR Docket No.50741-724.601 terephthalate, mixtures thereof, modifications thereof, or combinations thereof.
  • 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.
  • the nanofiltration membrane material is comprised of carbon, carbon nanotubes, graphene oxide, mixtures thereof, modifications thereof, or combinations thereof.
  • the nanofiltration membrane material is comprised of zeolite mixed matrix membrane with polyamide and/or polysulfone support, alumina filled polyvinyl alcohol mixed matrix membrane materials, mixtures thereof, modifications thereof, or combinations thereof.
  • nanofiltration provides a first solution comprising lithium and a second solution comprising phosphate.
  • lithium phosphate is converted to one or more other lithium compounds in a vessel.
  • the vessel is a mixing tank.
  • said vessel is a jacketed vessel.
  • said jacket is used to add heat to or remove heat from said vessel.
  • said vessel contains two or more baffles.
  • said vessel contains nozzles for injecting liquid, air, gas, or a combination thereof.
  • said nozzles are used for recirculating the contents of said vessel.
  • said nozzles are used for mixing said vessel.
  • air is used to recirculate the contents of said vessel.
  • the vessel comprises agitators.
  • said agitators comprise one or more impellers.
  • 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, titanium, Hastelloy, or a combination thereof.
  • the shaft and impellers are coated with glass, epoxy, rubber, a polymer coating, or combinations thereof.
  • fluidization by means of said agitator is aided by baffles mounted inside of said tank (e.g., vessel).
  • said baffles comprise flat rectangular structures mounted onto the side of the tank. In some embodiments, said baffles are oriented perpendicular to the plane of agitator of the impeller. In some embodiments, the presence of one or more baffles aid with the fluidization of the ion exchange beads inside the vessel. In some embodiments, the presence of one or more baffles reduce the swirling and vortexing associated with fluidization by an impeller. In some embodiments, the presence of said baffles results in more uniform suspension of particles (e.g., lithium phosphate, anion source, precipitates) in the WSGR Docket No.50741-724.601 aqueous medium.
  • particles e.g., lithium phosphate, anion source, precipitates
  • the presence of said baffles results in reduce attrition of particles being fluidized.
  • said baffles are constructed to span the entire vertical length of the vessel. In some embodiments, the baffles are constructed to span from about the height of the settled bed of ion exchange beads to the top of the vessel. In some embodiments, the baffles are constructed to span from about 6” from the bottom of the vessel to the top of the vessel. In some embodiments, there is a gap between the wall of the vessel and the baffle. In some embodiments, said gap measures less than 1/8”, less than 1 ⁇ 4”, less than 1 ⁇ 2”, or less than 1”. In some embodiments, said baffles measure a width that is equivalent to approximately one twelfth of the width of the vessel.
  • said baffles measure a width that is equivalent to approximately less than one tenth of the width of the vessel. In some embodiments, said baffles measure a width that is equivalent to more than approximately one fifteenth of the width of the vessel. In some embodiments, all baffles are of equivalent dimensions. In some embodiments, baffles are not of the same dimensions. In some embodiments, the tank contains two baffles. In some embodiments, the tank contains three baffles. In some embodiments, the tank contains four baffles. In some embodiments, the tank contains more than four baffles. [0270] In some embodiments, the vessel is configured such that the pressure inside the vessel can be at a non-ambient value.
  • the pressure inside the vessel is between about 0.01 bar and about 100 bar. In some embodiments, the pressure inside the vessel is about 0.1 bar, about 0.2 bar, about 0.3 bar,ph about 0.4 bar, about 0.5 bar, about 0.6 bar, about 0.7 bar, about 0.8 bar, about 0.9 bar, or about 1 bar. In some embodiments, the pressure inside the vessel is about 1 bar, about 2 bar, about 3 bar, about 4 bar, about 5 bar, about 6 bar, about 7 bar, about 8 bar, about 9 bar, or about 10 bar.
  • the pressure inside the vessel is about 1 bar to about 2 bar, about 2 bar to about 3 bar, about 3 bar to about 4 bar, about 4 bar to about 5 bar, about 5 bar to about 6 bar, about 6 bar to about 7 bar, about 7 bar to about 8 bar, about 8 bar to about 9 bar, or about 9 bar to about 10 bar. In some embodiments, the pressure inside the vessel is about 10 bar, about 20 bar, about 30 bar, about 40 bar, about 50 bar, about 60 bar, about 70 bar, about 80 bar, about 90 bar, or about 100 bar.
  • the pressure inside the vessel is about 10 bar to about 20 bar, about 20 bar to about 30 bar, about 30 bar to about 40 bar, about 40 bar to about 50 bar, about 50 bar to about 60 bar, about 60 bar to about 70 bar, about 70 bar to about 80 bar, about 80 bar to about 90 bar, or about 90 bar to about 100 bar.
  • lithium phosphate is converted to one or more other lithium compounds using two or more separate vessels.
  • a first vessel contains lithium phosphate.
  • the first vessel is configured to pass an aqueous medium into the first vessel, wherein the aqueous medium contacts the lithium phosphate and WSGR Docket No.50741-724.601 partially dissolves the lithium phosphate, and pass the aqueous medium out of the first vessel, wherein the aqueous medium exiting the first vessel is free of lithium phosphate particles or lithium phosphate solids.
  • a second vessel contains an anion source that is dissolved or suspended in an aqueous medium.
  • the second vessel is configured to add the aqueous medium exiting the first vessel to the dissolved or suspended anion source.
  • the precipitates form in the second vessel.
  • the concentration of lithium dissolved in the second vessel increases as more aqueous medium exiting the first vessel is added thereto.
  • One or more first vessels can be used in conjunction with one or more second vessels.
  • the first vessel comprises a filter press.
  • the first vessel comprises a filter.
  • the first vessel comprises a particle trap.
  • lithium phosphate is converted to one or more other lithium compounds using two or more separate vessels.
  • a first vessel contains an anion source.
  • the first vessel is configured to pass an aqueous medium into the first vessel, wherein the aqueous medium contacts the anion source and partially dissolves the anion source, and pass the aqueous medium out of the first vessel, wherein the aqueous medium exiting the first vessel is free of anion source particles or anion source solids.
  • a second vessel contains lithium phosphate that is dissolved or suspended in an aqueous medium.
  • the second vessel is configured to add the aqueous medium exiting the first vessel to the dissolved or suspended lithium phosphate.
  • the precipitates form in the second vessel.
  • the concentration of lithium dissolved in the second vessel increases as more aqueous medium exiting the first vessel is added thereto.
  • One or more first vessels can be used in conjunction with one or more second vessels.
  • the first vessel comprises a filter press.
  • the first vessel comprises a filter.
  • the first vessel comprises a particle trap. Conversion of Synthetic Lithium Solutions Comprising Phosphate into Other Compounds of Lithium [0273]
  • lithium phosphate is converted into one or more other compounds of lithium.
  • the other compounds of lithium have a higher aqueous solubility as compared to that of lithium phosphate.
  • the other compounds of lithium comprise: lithium hydroxide, lithium chloride, lithium bromide, lithium fluoride, lithium sulfate, lithium hydroxide WSGR Docket No.50741-724.601 monohydrate, lithium carbonate, lithium bicarbonate, lithium hydrogencarbonate, or combinations thereof.
  • phosphoric acid is used to elute lithium from a lithium-selective sorbent to provide a synthetic lithium solution comprising phosphate.
  • the synthetic lithium solution comprising phosphate is free of solid lithium phosphate.
  • said lithium compounds are in solution.
  • said lithium compounds are solid.
  • said lithium compound precipitate as a solid when contacted with an anion source (e.g., a metathesis salt).
  • an anion source e.g., a metathesis salt.
  • the synthetic lithium solution comprising phosphate is added to a solution or suspension of an anion source to provide a solution of one or more other lithium compounds.
  • an anion source is added to the synthetic lithium solution comprising phosphate to provide a solution of one or more other lithium compounds.
  • the synthetic lithium solution comprising phosphate is added to a solution or suspension of an anion source to provide a solution of one or more other lithium compounds and precipitates that comprise phosphate.
  • the synthetic lithium solution comprising phosphate is added to a solution or suspension of an anion source to provide precipitates that comprise lithium and phosphate.
  • the synthetic lithium solution comprising phosphate is added to a solution or suspension of a base to provide precipitates that comprise lithium and phosphate.
  • an acid is added to facilitate the conversion of lithium phosphate into one or more other lithium compounds.
  • a base is added to facilitate the conversion of lithium phosphate into one or more other lithium compounds.
  • an acid is added to reduce the solubility of the precipitates that comprise phosphate.
  • a base is added to reduce the solubility of the precipitates that comprise phosphate.
  • an acid is added to increase the solubility of the lithium phosphate.
  • the acid comprises hydrochloric acid, hydrobromic acid, hydrofluoric acid, sulfuric acid, nitric acid, organic acids (e.g., acetic acid, formic acid, propanoic acid, citric acid, lactic acid, other carboxylic acids), or combinations thereof.
  • the base comprises LiOH, NaOH, KOH, Mg(OH)2, Ca(OH) 2 , CaO, Sr(OH) 3 , organic bases (e.g., acetate, formate, propanoate, citrate, lactate, other carboxylates, methoxide, ethoxide, isopropoxide, butoxides, other alkoxides, amines), other bases, or combinations thereof.
  • the base comprises LiOH.
  • the base comprises NaOH.
  • the base comprises KOH.
  • a solubilizing agent is added to facilitate the conversion of lithium phosphate into one or more other lithium compounds.
  • the anion source (e.g., the metathesis salt) comprises an anion selected from: chloride, bromide, fluoride, bicarbonate, sulfate, hydroxide, nitrate, and combinations thereof.
  • the anion source is selected from: hydrochloric acid, hydrobromic acid, hydrofluoric acid, sulfuric acid, nitric acid, or combinations thereof.
  • the anion source comprises hydrochloric acid.
  • the anion source comprises nitric acid. In some embodiments the anion source comprises sulfuric acid. In some embodiments, the anion source comprises a cation selected from: calcium, magnesium, strontium, barium, sodium, potassium, aluminum, and combinations thereof. In some embodiments the anion source comprises one or more of Al(OH)3, CaCl2, CaSO4, Ca(OH) 2 , MgCl 2 , MgSO 4 , and Mg(OH) 2 . In some embodiments, the anion source comprises Ca(OH) 2 . In some embodiments, the anion source comprises Mg(OH) 2 . In some embodiments, the anion source comprises CaCl2. In some embodiments, the anion source comprises MgCl2.
  • the anion source comprises CaSO4. In some embodiments, the anion source comprises MgSO 4 . In some embodiments, the anion source comprises Al(OH) 3 . [0276] In some embodiments, the molar ratio of the anionic component (e.g., chloride, bromide, fluoride, bicarbonate, sulfate, hydroxide, nitrate, and combinations thereof) of the anion source (e.g., the metathesis salt) to the lithium present in the synthetic lithium solution is between about 0.1 to about 3.0. In some embodiments, said molar ratio is between about 0.7 to about 1.3. In some embodiments, said molar ratio is in the inclusive range of 0.7 to 1.3.
  • the anionic component e.g., chloride, bromide, fluoride, bicarbonate, sulfate, hydroxide, nitrate, and combinations thereof
  • the anion source e.g., the metathesis salt
  • said molar ratio is between about 0.1 to about 1.0, about 0.2 to about 1.0, about 0.3 to about 1.0, about 0.4 to about 1.0, about 0.5 to about 1.0, about 0.6 to about 1.0, about 0.7 to about 1.0, about 0.8 to about 1.0, or about 0.9 to about 1.0. In some embodiments, said molar ratio is between about 0.5 to about 1.0, about 0.5 to about 1.2, about 0.5 to about 1.5, about 0.5 to about 1.7, about 0.5 to about 2.0, or about 0.5 to about 3.0.
  • said molar ratio is between about 1.0 to about 1.2, about 1.0 to about 1.5, about 1.0 to about 1.7, about 1.0 to about 2.0, or about 1.0 to about 3.0. In some embodiments, said molar ratio is between about 2.0 to about 2.2, about 2.0 to about 2.5, about 2.0 to about 2.7, about 2.0 to about 3.0, or about 2.5 to about 3.0.
  • the solubilizing agent comprises carbon dioxide. In some embodiments, the solubilizing agent comprises SO2. In some embodiments, the solubilizing agent comprises a chelating agent as detailed herein.
  • the chelating agent is selected from EDTA, egtazic acid, citric acid, a compound comprising oxalate, salts thereof, or combinations thereof. In some embodiments, the chelating agent is selected from EDTA, WSGR Docket No.50741-724.601 citric acid, a compound comprising oxalate, or combinations thereof. In some embodiments, the chelating agent is EDTA. In some embodiments, the chelating agent is citric acid. In some embodiments, the chelating agent comprises oxalate. In some embodiments, the chelating agent is egtazic acid.
  • the chelating agent comprises a minopolycarboxylic acid, a nitrilotriacetic acid, a salt thereof, or a combination thereof.
  • the pH of the synthetic lithium solution comprising phosphate is modulated prior to contacting with the anion source. In some embodiments, the pH of the synthetic lithium solution comprising phosphate is modulated following contacting with the anion source. In some embodiments, the pH of the synthetic lithium solution comprising phosphate is modulated by contacting with the anion source. In some embodiments, the pH of the synthetic lithium solution comprising phosphate is modulated by the addition of an acid.
  • the pH of the synthetic lithium solution comprising phosphate is modulated by the addition of a base. Said modulation can raise the pH of the synthetic lithium solution comprising phosphate. Said modulation can lower the pH of the synthetic lithium solution comprising phosphate. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 0 and about 14. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 0. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 1. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 2. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 3.
  • the pH of the synthetic lithium solution comprising phosphate following said modulation is about 4. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 5. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 6. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 7. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 8. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 9. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 10. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 11.
  • the pH of the synthetic lithium solution comprising phosphate following said modulation is about 12. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is about 13. In some embodiments, the pH of WSGR Docket No.50741-724.601 the synthetic lithium solution comprising phosphate following said modulation is about 14. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 1 and about 3. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 1 and about 4. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 1 and about 7.
  • the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 2 and about 4. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 2 and about 7. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 3 and about 7. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 4 and about 7. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 7 and about 9. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 7 and about 11.
  • the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 7 and about 13. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 9 and about 11. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 9 and about 13. In some embodiments, the pH of the synthetic lithium solution comprising phosphate following said modulation is between about 11 and about 13. [0279] In some embodiments, the pH of the synthetic lithium solution comprising phosphate is modulated in stages. In some embodiments, said stages comprise modulating the pH of the synthetic lithium solution to one or more values described above. In some embodiments, one or more stages of pH modulation result in the formation of precipitates.
  • the composition of the precipitates changes from one stage to another.
  • pH modulation results in the precipitation of precipitates comprising phosphates.
  • pH modulation results in the precipitation of precipitates comprising a hydroxide.
  • pH modulation results in the precipitation of precipitates comprising an oxide.
  • the addition of an anion source e.g., metathesis salt results in the precipitation of precipitate comprising phosphates.
  • the addition of an acid, a base, or an anion source is limited in quantity so as to limit the amount precipitates that form following said addition.
  • WSGR Docket No.50741-724.601 converted to precipitates that are solids.
  • these precipitates are deficient in lithium and rich in impurities (e.g., Mg, Ca, Sr, Ba, Al, B, Fe, Mn, other cationic impurities).
  • said precipitates comprise less than 1 % Li, less than 5 % Li, less than 10 % Li, less than 25 % Li, or less than 50 % Li.
  • the low Li content of the precipitates generated by limited addition of an acid, a base, or an anion source allows for said precipitates to be separated from the salts that remain in solution, thereby resulting in a synthetic lithium solution that is further enriched in Li relative to the synthetic lithium solution prior to said limited addition.
  • said separation occurs in a solid-liquid separation device (e.g., a particle trap, a filter press)
  • the same or different acid, base, or anion source is further added the synthetic lithium solution enriched in Li to result in further precipitation of precipitates comprising lithium and phosphate.
  • the same or different acid, base, or anion source is further added the synthetic lithium solution enriched in Li to result in further precipitation of precipitates comprising phosphate, and provide a synthetic lithium solution that is further enriched in Li (e.g., comprises dissolved lithium in a higher purity).
  • the precipitates comprise about 100% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 90% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise more than 90% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 80% of the phosphate derived from the lithium phosphate.
  • the precipitates comprise more than 80% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 70% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 60% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 50% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 40% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 30% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise about 20% of the phosphate derived from the lithium phosphate.
  • the precipitates comprise about 10% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates comprise less than about 10% of the phosphate derived from the lithium phosphate. In some embodiments, the precipitates form following modulation of the pH of the synthetic lithium solution comprising phosphate. In some embodiments, lowering the pH of the synthetic lithium solution comprising phosphate increases the quantity of precipitates. In some WSGR Docket No.50741-724.601 embodiments, increasing the pH of the synthetic lithium solution comprising phosphate increases the quantity of precipitates.
  • the composition of the precipitates can vary just as the composition of the synthetic lithium solution, the source of phosphate added thereto, and the lithium phosphate solids obtained therefrom can vary.
  • the precipitates are described and characterized, in part or in whole, in terms of their elemental and/or ionic constituents.
  • the precipitates are described and characterized, in part or in whole, in terms of their chemical properties (e.g., solubility, including pH-dependent solubility).
  • the composition of the precipitates is inferred by differential analysis of the synthetic lithium solution before and after the precipitates are formed therefrom.
  • the composition of the precipitates varies with dependence on the pH of the synthetic lithium solution.
  • the precipitates comprise one chemical compound.
  • the precipitates comprise multiple chemical compounds.
  • the precipitates comprise one or more of: mono- potassium phosphate, di-potassium phosphate, tri-potassium phosphate, mono-sodium phosphate, di-sodium phosphate, tri-sodium phosphate, aluminum phosphate, zinc phosphate, poly-ammonium phosphate, sodium-hexa-metaphosphate, struvite, mono-magnesium phosphate, di-magnesium phosphate, tri-magnesium phosphate, hydroxyapatite, fluorapatite, chlorapatite, carbonate apatite, calcium-deficient hydroxyapatite, calcium-deficient fluorapatite, calcium- deficient chlorapatite, calcium-deficient carbonate apatite, one or more other
  • the solution of one or more other lithium compounds is further processed to provide solid lithium carbonate according to the methods and procedures detailed herein.
  • the solution of one or more other lithium compounds comprises lithium chloride
  • addition of sodium carbonate thereto could allow for the subsequent isolation of solid lithium carbonate from the solution according to any of the appropriate methods provided herein.
  • the solution of one or more other lithium compounds comprises lithium hydroxide
  • addition of carbon dioxide thereto could allow for the subsequent isolation of solid lithium carbonate from the solution according to any of the appropriate methods provided herein.
  • a liquid resource comprising lithium is present in reservoirs, such that the liquid resource must be produced from said reservoir prior to extracting lithium therefrom.
  • the reservoir is subterranean.
  • the liquid WSGR Docket No.50741-724.601 resource is contained in the free fluid porosity and capillary bound porosity of the reservoir prior to the production of said liquid resource therefrom.
  • the liquid resource is produced from the free fluid porosity and the capillary bound porosity of the reservoir during the production of said liquid resource therefrom.
  • the reservoir comprises unconsolidated sediment, such as sand, silt, gravel, clay, rubble, alluvium, or a combination thereof.
  • the reservoir comprises consolidated rock, such as sandstone, conglomerate, breccia, siltstone, claystone, mudstone, limestone, dolomite, igneous rock, evaporites, halite, metamorphic rock and interbeds, or a combination thereof.
  • the reservoir comprises sandstone.
  • said sandstone comprises quartz, lithics, micas, clays, volcanic minerals such as feldspars, or a combination thereof.
  • the reservoir comprises limestone.
  • said limestone comprises calcite, aragonite, dolomite, clays, or a combination thereof.
  • the reservoir comprises unconsolidated sediment.
  • said unconsolidated sediment comprises quartz, lithics, micas, clays, igneous minerals such as feldspars, organics, or a combination thereof.
  • the reservoir comprises igneous rock.
  • said igneous rock comprises basalt, diorite, andesite, granite, ignimbrite, tuff, ash, rhyolite, dacite, gabbro, pegmatite, peridotite, pumice, or a combination thereof.
  • the reservoir is unconfined.
  • an unconfined reservoir does not comprise a cap rock that separates the liquid resource, groundwater, and/or brine within said reservoir from contact with the atmosphere.
  • the reservoir is confined.
  • a confined reservoir comprises a cap rock (e.g., a layer of rock) that separates the liquid resource, groundwater, and/or brine within said reservoir from contact with the atmosphere.
  • the reservoir comprises a fracture.
  • the liquid resource is produced from a fracture in the reservoir.
  • the reservoir is located in a fault zone.
  • the liquid resource is produced from fault gouge, breccia, and/or fracture networks located within the fault zone.
  • fractures are intentionally produced into a reservoir before, during, or after producing a liquid resource therefrom.
  • fractures are formed in a reservoir using hydraulic stimulation.
  • the reservoir is a salar reservoir, an immature modern salar reservoir, a mature modern-day reservoir, a US carbonate reservoir, a European sandstone reservoir, or a European fractured reservoir.
  • the reservoir is a an WSGR Docket No.50741-724.601 immature modern salar reservoir, a mature modern-day reservoir, a US carbonate reservoir, a European sandstone reservoir, or a European fractured reservoir.
  • the reservoir is a salar reservoir, an immature modern salar reservoir, a mature modern-day reservoir, a carbonate reservoir, a sandstone reservoir, or a fractured reservoir.
  • the reservoir is a an immature modern salar reservoir, a mature modern-day reservoir, a carbonate reservoir, a sandstone reservoir, or a fractured reservoir.
  • the reservoir is a salar reservoir. [0289] In some embodiments, the reservoir has a depth of 0 to about 10,000 meters below the ground surface where the reservoir is located. In some embodiments, the depth is about 0.01 to about 5000 meters.
  • the depth is about 0.01 to about 100 meters, about 0.01 to about 500 meters, about 0.01 to about 1000 meters, about 0.01 to about 2000 meters, about 0.01 to about 3000 meters, about 0.01 to about 4000 meters, about 0.01 to about 5000 meters, about 0.01 to about 6000 meters, about 0.01 to about 7000 meters, about 0.01 to about 8000 meters, about 0.01 to about 9000 meters, or about 0.01 to about 10000 meters.
  • the depth is about 100 to about 1000 meters, about 100 to about 2000 meters, about 100 to about 3000 meters, about 100 to about 4000 meters, about 100 to about 5000 meters, about 100 to about 6000 meters, about 100 to about 7000 meters, about 100 to about 8000 meters, about 100 to about 9000 meters, or about 100 to about 10000 meters. In some embodiments, the depth is about 1000 to about 2000 meters, about 1000 to about 3000 meters, about 1000 to about 4000 meters, about 1000 to about 5000 meters, about 1000 to about 6000 meters, about 1000 to about 7000 meters, about 1000 to about 8000 meters, about 1000 to about 9000 meters, or about 1000 to about 10000 meters. In some embodiments, the depth is less than about 100 meters.
  • the depth is less than about 1000 meters. In some embodiments, the depth is less than about 5000 meters. In some embodiments, the depth is less than about 10000 meters.
  • the effective porosity of the reservoir is from 0 to about 50%. In some embodiments, the effective porosity is about 5 to about 40%. In some embodiments, the effective porosity is about 0.01 to about 1%, about 0.01 to about 5%, about 0.01 to about 10%, about 0.01 to about 20%, about 0.01 to about 30%, about 0.01 to about 40%, or about 0.01 to about 50%.
  • the effective porosity is about 1 to about 2%, about 2 to about 5%, about 5 to about 10%, about 5 to about 20%, about 5 to about 30%, about 5 to about 40%, or about 5 to about 50%. In some embodiments, the effective porosity is about 10 to about 20%, about 10 to about 30%, about 10 to about 40%, or about 10 to about 50%. In some embodiments, the effective porosity is less than about 50%. In some embodiments, the effective porosity is less than about 40%. In some embodiments, the effective porosity is less than about WSGR Docket No.50741-724.601 30%. In some embodiments, the effective porosity is less than about 20%. In some embodiments, the effective porosity is greater than about 5%.
  • the effective porosity is greater than about 10%.
  • the depth of a reservoir varies spatially, laterally, and vertically. In some embodiments, the effective porosity of a reservoir varies spatially, laterally, and vertically.
  • the solid density of the reservoir is about 0.1 to about 5 g/cm 3 . In some embodiments, the solid density of the reservoir is about 1 to about 4 g/cm 3 .
  • the solid density is about 0.1 to about 0.5 g/cm 3 , about 0.5 to about 1 g/cm 3 , about 1 to about 2 g/cm 3 , about 2 to about 3 g/cm 3 , about 3 to about 4 g/cm 3 , or about 4 to about 5 g/cm 3 . In some embodiments, the solid density is about 1 to about 2 g/cm 3 , about 1 to about 3 g/cm 3 , about 1 to about 4 g/cm 3 , or about 1 to about 5 g/cm 3 . In some embodiments, the solid density is greater than about 0.5 g/cm 3 .
  • the solid density is greater than about 1 g/cm 3 . In some embodiments, the solid density is greater than about 2 g/cm 3 . In some embodiments, the solid density is less than about 5 g/cm 3 . [0293] In some embodiments, the density of the liquid resource within the reservoir is about 1 to about 1.4 g/mL. In some embodiments, the density of the liquid resource within the reservoir is about 1.05 to about 1.3 g/mL.
  • the density is about 1 to about 1.05 g/mL, about 1.05 to about 1.1 g/mL, about 1.1 to about 1.2 g/mL, about 1.2 to about 1.3 g/mL, or about 1.3 to about 1.4 g/mL. In some embodiments, the density is less than about 1.4 g/mL. In some embodiments, the density is greater than about 1 g/mL. [0294] In some embodiments, the liquid resource is produced from the reservoir for up to about 100 years.
  • the liquid resource is produced from the reservoir for up to about 1 year, about 5 years, about 10 years, about 20 years, about 30 years, about 40 years, about 50 years, about 60 years, about 70 years, about 80 years, about 90, or about 100 years.
  • the amount of time that liquid resource is produced from the reservoir is the lifetime of the reservoir.
  • the lifetime of the reservoir is determined by historical matching and dynamic modeling of the lithium concentration of the liquid resource produced from the reservoir over time.
  • the lifetime of the reservoir is determined by an economic cut-off, such as a cut-off based upon the quality of lithium (e.g., lithium chemicals) produced from the liquid resource, or a cut-off based upon the expense of further producing the liquid resource from the reservoir.
  • a wellfield comprises one or more wells (e.g., production wells, injection wells) arranged in a pattern.
  • a production wellfield comprises one or more production wells arranged in a pattern.
  • an injection wellfield comprises one or more injection wells arranged in a pattern.
  • a production wellfield and an injection wellfield operate upon the same reservoir and are configured to operate simultaneously.
  • the pattern of wells in a wellfield can be configured to enhance the production of the liquid resource.
  • the pattern of wells in a wellfield can be configured to enhance the injection of the fluid.
  • a wellfield (e.g., a production wellfield, an injection wellfield) comprises 1 to about 10,000 wells (e.g., production wells, injection wells). In some embodiments, a wellfield (e.g., a production wellfield, an injection wellfield) comprises 1 to about 20,000 wells (e.g., production wells, injection wells).
  • the wellfield comprises 1 to about 10 wells, 1 to about 100 wells, 1 to about 1000 wells, 1 to about 2000 wells, 1 to about 3000 wells, 1 to about 4000 wells, 1 to about 5000 wells, 1 to about 6000 wells, 1 to about 7000 wells, 1 to about 8000 wells, 1 to about 9000 wells, 1 to about 10000 wells, 1 to about 11000 wells, 1 to about 12000 wells, 1 to about 13000 wells, 1 to about 14000 wells, 1 to about 15000 wells, 1 to about 16000 wells, 1 to about 17000 wells, 1 to about 18000 wells, 1 to about 19000 wells, or 1 to about 20000 wells.
  • the wellfield comprises less than about 10000 wells. In some embodiments, the wellfield comprises less than about 20000 wells. [0299] In some embodiments, two wells within a wellfield (e.g., a production wellfield, an injection wellfield) are spaced about 100 to about 10000 meters apart. In some embodiments, two wells are spaced about 100 to about 5000 meters apart.
  • a wellfield e.g., a production wellfield, an injection wellfield
  • two wells are spaced about 100 to about 500 meters apart, about 100 to about 1000 meters apart, about 100 to about 2000 meters apart, about 100 to about 3000 meters apart, about 100 to about 4000 meters apart, about 100 to about 5000 meters apart, about 100 to about 6000 meters apart, about 100 to WSGR Docket No.50741-724.601 about 7000 meters apart, about 100 to about 9000 meters apart, or about 100 to about 10000 meters apart.
  • two wells are spaced about 500 to about 1000 meters apart, about 1000 to about 2000 meters apart, about 1000 to about 3000 meters apart, about 1000 to about 4000 meters apart, about 1000 to about 5000 meters apart, about 1000 to about 6000 meters apart, about 1000 to about 7000 meters apart, about 1000 to about 9000 meters apart, or about 1000 to about 10000 meters apart.
  • two wells are spaced more than 100 meters apart. In some embodiments, two wells are spaced less than 10000 meters apart.
  • a production well and an injection well are spaced about 100 to about 10000 meters apart.
  • a production well and an injection well are spaced about 100 to about 5000 meters apart. In some embodiments, a production well and an injection well are spaced about 100 to about 500 meters apart, about 100 to about 1000 meters apart, about 100 to about 2000 meters apart, about 100 to about 3000 meters apart, about 100 to about 4000 meters apart, about 100 to about 5000 meters apart, about 100 to about 6000 meters apart, about 100 to about 7000 meters apart, about 100 to about 9000 meters apart, or about 100 to about 10000 meters apart.
  • a production well and an injection well are spaced about 500 to about 1000 meters apart, about 1000 to about 2000 meters apart, about 1000 to about 3000 meters apart, about 1000 to about 4000 meters apart, about 1000 to about 5000 meters apart, about 1000 to about 6000 meters apart, about 1000 to about 7000 meters apart, about 1000 to about 9000 meters apart, or about 1000 to about 10000 meters apart.
  • a production well and an injection well are spaced more than 100 meters apart. In some embodiments, a production well and an injection well are spaced less than 10000 meters apart.
  • one or more production wells and one or more injection wells are arranged in a 2-spot pattern, a 3-spot pattern, a 4-spot pattern, a 5-spot pattern, a 7-spot pattern, a 9-spot pattern, a line drive pattern, a peripheral flood pattern, or a combination thereof. In some embodiments, one or more production wells and one or more injection wells are not arranged in a pattern.
  • a well e.g., a production well, an injection well
  • the bore diameter is less than or equal to about 45 inches, about 40 inches, about 35 inches, about 30 inches, about 25 inches, about 20 inches, about 15 inches, about 10 inches, or about 5 inches.
  • a well e.g., a production well, an injection well
  • the diameter of said wellbore is from about 0.1 to about 0.5 inches, from about 0.5 inches to about 1 inch, from about 1 inch to about 1.5 inches, from about 1.5 inches to about 2 inches, from about 2 inches to about 3 inches, from about 3 inches to about 4 inches, from WSGR Docket No.50741-724.601 about 4 inches to about 5 inches, from about 5 inches to about 6 inches, from about 6 inches to about 8 inches, from about 8 inches to about 10 inches, from about 10 inches to about 12 inches, from about 12 inches to about 14 inches, from about 14 inches to about 17 inches, from about 17 inches to about 20 inches, from about 20 inches to about 24 inches, from about 24 inches to about 28 inches, from about 28 inches to about 32 inches, from about 32 inches to about 36 inches.
  • the wellbore is cased, or has a casing. In some embodiments, the wellbore is not cased, or has no casing. In some embodiments, the portion of the wellbore is cased, and a portion of the wellbore is not cased. In some embodiments, the casing stabilizes the borehole, allowing for efficient operation of said well. In some embodiments, the casing is configured to direct a liquid resource from a reservoir into a production well. In some embodiments, the casing is configured to direct a liquid resource into a reservoir from an injection well. In some embodiments, one or more casings are used along one or more section of the borehole.
  • said one or more casings comprise a conductor casing, a surface casing, an intermediate casing, a production, casing, or a liner. In some embodiments, said one or more casings are impermeable. In some embodiments, said one or more casings are permeable. In some embodiments, said one or more casings comprise cement. In some embodiments, said one or more casings comprise tubing. In some embodiments, said one or more casings comprise a metal casing, a plastic casing, or combinations thereof. In some embodiments, said one or more casings comprise a steel tubing, an iron tubing, a titanium tubing, a tubing made of a different metal, or combination thereof.
  • said one or more casings comprise a plastic tubing.
  • said plastic tubing comprises PVC, polypropylene, polyethylene, ABS, a different plastic, or a combination thereof.
  • said one or more casings comprises cement.
  • said one or more casing comprises a combination of cement with a metal and a different material, said different material optionally comprising a metal or a plastic casing.
  • said casing has a wall thickness about 0.1 mm, about 0.5 mm, about 1 mm, about 2 mm, about 3 mm, about 5 mm, about 7 mm, about 10 mm, about 15 mm, about 20 mm, about 25 mm, about 30 mm, about 40 mm, about 50 mm, about 70 mm, about 100 mm, a out 150 mm, about 200 mm, about 250 mm, a out 300 mm, about 400 mm, or about 500 mm.
  • said casing has a wall thickness that varies with depth.
  • the casing is perforated to allow for fluid communication between the well and the reservoir, leading to extraction of liquid from a reservoir or reinjection of a liquid into a reservoir.
  • sections of the casings are perforated and other sections are not.
  • sections of the casings are perforated and other sections WSGR Docket No.50741-724.601 are not, and the sections perforated are configured to allow for fluid communication of only certain sections of the wellbore with the reservoir.
  • said perforations comprise circles, round holes, irregularly shaped holes, slits, another regular geometric shape, another irregular geometric shape, or a combination thereof.
  • a production well comprises a pump.
  • the pump is selected from an electric submersible pump, a jet pump, an air lift, and a centrifugal pump.
  • an injection well comprises a pump.
  • a production well is configured to produce up to about 10,000 cubic meters of liquid resource per day. In some embodiments, a production well is configured to produce up to about 10,000 cubic meters, up to about 9,000 cubic meters, up to about 8,000 cubic meters, up to about 7,000 cubic meters, up to about 6,000 cubic meters, up to about 5,000 cubic meters, up to about 4,000 cubic meters, up to about 3,000 cubic meters, up to about 2,000 cubic meters, or up to about 1,000 cubic meters of liquid resource per day.
  • a production wellfield is configured to produce up to about 100 million cubic meters of liquid resource per day. In some embodiments, a production wellfield is configured to produce up to about 100 million cubic meters, up to about 90 million cubic meters, up to about 80 million cubic meters, up to about 70 million cubic meters, up to about 60 million cubic meters, up to about 50 million cubic meters, up to about 40 million cubic meters, up to about 30 million cubic meters, up to about 20 million cubic meters, up to about 10 million cubic meters, up to about 5 million cubic meters, or about up to about 1 million cubic meters of liquid resource per day. [0308] In some embodiments, an injection well is configured to inject up to about 10,000 cubic meters of liquid resource per day.
  • an injection well is configured to inject up to about 10,000 cubic meters, up to about 9,000 cubic meters, up to about 8,000 cubic meters, up to about 7,000 cubic meters, up to about 6,000 cubic meters, up to about 5,000 cubic meters, up to about 4,000 cubic meters, up to about 3,000 cubic meters, up to about 2,000 cubic meters, or up to about 1,000 cubic meters of fluid per day.
  • an injection wellfield is configured to inject up to about 100 million cubic meters of fluid per day.
  • an injection wellfield is configured WSGR Docket No.50741-724.601 to inject up to about 100 million cubic meters, up to about 90 million cubic meters, up to about 80 million cubic meters, up to about 70 million cubic meters, up to about 60 million cubic meters, up to about 50 million cubic meters, up to about 40 million cubic meters, up to about 30 million cubic meters, up to about 20 million cubic meters, up to about 10 million cubic meters, up to about 5 million cubic meters, or about up to about 1 million cubic meters of fluid per day.
  • the pressure at a production well e.g., the pressure at which the liquid resource is produced by said well
  • the pressure is from about 20 psi to about 8000 psi. In some embodiments, the pressure is about 0.1 psi to about 9000 psi, about 0.1 psi to about 8000 psi, about 0.1 psi to about 7000 psi, about 0.1 psi to about 6000 psi, about 0.1 psi to about 5000 psi, about 0.1 psi to about 4000 psi, about 0.1 psi to about 3000 psi, about 0.1 psi to about 2000 psi, about 0.1 psi to about 1000 psi, about 0.1 psi to about 9000 psi, about 10 psi to about 9000 psi, about 10 psi to about 8000 psi, about 10 psi to about 7000 psi, about 10 psi to about 6000 psi, about 10 pss
  • the pressure at an injection well (e.g., the pressure at which the fluid is injected into the reservoir by said well) ranges from about 0.1 psi to about 10,000 psi. In some embodiments, the pressure is from about 20 psi to about 8000 psi.
  • the pressure is about 0.1 psi to about 9000 psi, about 0.1 psi to about 8000 psi, about 0.1 psi to about 7000 psi, about 0.1 psi to about 6000 psi, about 0.1 psi to about 5000 psi, about 0.1 psi to about 4000 psi, about 0.1 psi to about 3000 psi, about 0.1 psi to about 2000 psi, about 0.1 psi to about 1000 psi, about 0.1 psi to about 9000 psi, about 10 psi to about 9000 psi, about 10 psi to about 8000 psi, about 10 psi to about 7000 psi, about 10 psi to about 6000 psi, about 10 psi to about 5000 psi, about 20 psi to about 9000 psi, about 0.1
  • a production wellfield and an injection wellfield are configured such that their respective production and injection rates are equal. In some embodiments, a production wellfield and an injection wellfield are configured such that their respective production and injection rates differ by about 1% or less. In some embodiments, a production wellfield and an injection wellfield are configured such that their respective production and injection rates differ by about 2% or less. In some embodiments, a production wellfield and an injection wellfield are configured such that their respective production and injection rates differ by about 5% or less. In some embodiments, a production wellfield and an injection wellfield are configured such that their respective production and injection rates differ by about 10% or less.
  • a production wellfield and an injection wellfield are configured such that WSGR Docket No.50741-724.601 their respective production and injection rates differ by about 20% or less. In some embodiments, a production wellfield and an injection wellfield are configured such that their respective production and injection rates differ by about 20% or more. In some embodiments, a production wellfield and an injection wellfield are configured such that their respective production and injection rates are unequal. In some embodiments, a production wellfield and an injection wellfield are configured such that their respective production and injection rates are modulated over time. [0313] In some embodiments, a production wellfield is configured to maximize the production of lithium from the reservoir in the form of the liquid resource.
  • an injection wellfield is configured to maximize the production of lithium from the reservoir in the form of the liquid resource.
  • a production wellfield is configured to minimize the costs associated with its operation.
  • an injection wellfield is configured to minimize the costs associated with its operation.
  • a production wellfield is configured to minimize the energy required to produce the liquid resource from the reservoir.
  • an injection wellfield is configured to minimize the energy required to inject the fluid into the reservoir.
  • a production well or an injection well comprises a filter or screen.
  • the filter or screen is configured to exclude particles above a given size.
  • the given size is selected based upon the average particle size of the solids within the reservoir where the production well or the injection well is located.
  • the well is operated to minimize sediment from entering the well.
  • operations are performed to remove solids from the well.
  • sediments form the well are removed periodically.
  • the flow rate of a production well or an injection well is selected or modulated based upon the lithological features or permeability of the reservoir where the production well or the injection well is located.
  • the reservoir has heterogeneous lithological features or permeability.
  • the wellbores are configured to optimize from flow from layers with said heterogeneous lithological features.
  • the casing of the wellbores is configured to optimize from flow from layers with said heterogeneous lithological features.
  • the casing of the wellbore changes according to the lithological features at different depths within the wellbore.
  • the spacings and flow rates of a production wellfield (and the individual production wells therein) and an injection wellfield (and the individual injection wells therein) are configured to maximize the recovery of lithium from the reservoir in the form of the liquid resource. In some embodiments, the spacings and flow rates of a production wellfield (and the individual production wells therein) and an injection wellfield (and the individual injection wells therein) are configured to maximize the recovery of lithium contained within the free fluid porosity and capillary bound porosity of the reservoir.
  • the spacings and flow rates of a production wellfield (and the individual production wells therein) and an injection wellfield (and the individual injection wells therein) are configured to maximize the concentration of lithium in the liquid resource produced from the reservoir. In some embodiments, the spacings and flow rates of a production wellfield (and the individual production wells therein) and an injection wellfield (and the individual injection wells therein) are configured to minimize the dilution of the liquid resource (e.g., the liquid resource as found naturally within the reservoir) by the injected fluid.
  • Fluid Injection into a Reservoir [0318] In some embodiments, the present disclosure provides a method for producing a liquid resource from a reservoir, the method comprising injecting a fluid into the reservoir.
  • the liquid resource is produced from the reservoir and the fluid is injected into the reservoir simultaneously.
  • injection of a fluid comprising water into a reservoir is termed a miscible waterflood.
  • the fluid comprises a depleted liquid resource.
  • the fluid consists of a depleted liquid resource.
  • the depleted liquid resource is produced by extracting at least a portion of the lithium content of the liquid resource.
  • the fluid comprises water.
  • the fluid is an aqueous solution.
  • the fluid comprises a treated liquid resource.
  • the fluid comprises a diluted liquid resource.
  • the depleted liquid resource is diluted, treated, or a combination thereof.
  • the liquid resource is a subsurface brine, such as a geothermal brine.
  • the fluid is a supercritical fluid.
  • the supercritical fluid is supercritical carbon dioxide.
  • said supercritical carbon dioxide is permanently sequestered following injection into the reservoir.
  • the fluid is miscible with water.
  • lithium is soluble in the fluid.
  • the injected fluid has a lithium concentration lower than the lithium concentration of the produced liquid resource.
  • the fluid is a gas.
  • the gas comprises air, nitrogen, oxygen, carbon dioxide, argon, or a combination thereof.
  • the fluid comprises a non-aqueous liquid. In some embodiments, the fluid is a non-aqueous liquid. [0320] In some embodiments, injection of the fluid into the reservoir is configured such that the entire effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that up to 100% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that up to about 90% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that up to 100% of the effective pore volume within the reservoir is filled.
  • injection of the fluid into the reservoir is configured such that up to about 80% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that up to about 70% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that up to about 60% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that up to about 50% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that about 1% to about 99% of the effective pore volume within the reservoir is filled.
  • injection of the fluid into the reservoir is configured such that about 1% to about 90% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that about 5% to about 90% of the effective pore volume within the reservoir is filled. In some embodiments, injection of the fluid into the reservoir is configured such that about 5% to about 75% of the effective pore volume within the reservoir is filled. [0321] In some embodiments, the injection of the fluid into the reservoir displaces the liquid resource contained within the effective pore space of the reservoir. In some embodiments, the injection of the fluid into the reservoir displaces the liquid resource contained within the capillary bound porosity of the reservoir. In some embodiments, the fluid is produced from the reservoir as the liquid resource following said displacement.
  • said displacement increases the usable quantity of liquid resource that is produced from the reservoir as compared to the usable quantity of liquid resource produced by conventional methods (e.g., gravity drainage). In some embodiments, said displacement leads to the production of a quantity of liquid resource that exceeds the volume of the free fluid porosity of the reservoir. In some embodiments, said displacement leads to the production of a quantity of liquid resource that contains an amount of lithium that exceeds the amount of lithium contained within the free fluid WSGR Docket No.50741-724.601 porosity of the reservoir. In some embodiments, said displacement results in a decrease in the lithium concentration of the liquid resource produced from the reservoir over time.
  • the injection of the fluid into the reservoir allows the dissolved ions in the liquid resource contained within the effective pore space of the reservoir to diffuse into the fluid. In some embodiments, the injection of the fluid into the reservoir allows the dissolved ions in the liquid resource contained within the capillary bound porosity of the reservoir to diffuse into the fluid. In some embodiments, the fluid is produced from the reservoir as the liquid resource following said diffusion. In some embodiments, said diffusion increases the usable quantity of liquid resource that is produced from the reservoir as compared to the usable quantity of liquid resource produced by conventional methods (e.g., gravity drainage). In some embodiments, said diffusion leads to the production of a quantity of liquid resource that exceeds the volume of the free fluid porosity of the reservoir.
  • said diffusion leads to the production of a quantity of liquid resource that contains an amount of lithium that exceeds the amount of lithium contained within the free fluid porosity of the reservoir. In some embodiments, said diffusion results in a decrease in the lithium concentration of the liquid resource produced from the reservoir over time.
  • the injection of the fluid into the reservoir allows clay bound water to diffuse into the effective pore space of the reservoir. In some embodiments, the injection of the fluid into the reservoir allows lithium ions associated with clay bound water to diffuse into the effective pore space of the reservoir. In some embodiments, the fluid is produced from the reservoir as the liquid resource following said diffusion.
  • said diffusion increases the usable quantity of liquid resource that is produced from the reservoir as compared to the usable quantity of liquid resource produced by conventional methods (e.g., gravity drainage). In some embodiments, said diffusion leads to the production of a quantity of liquid resource that exceeds the volume of the free fluid porosity of the reservoir. In some embodiments, said diffusion leads to the production of a quantity of liquid resource that contains an amount of lithium that exceeds the amount of lithium contained within the free fluid porosity of the reservoir. In some embodiments, said diffusion results in a decrease in the lithium concentration of the liquid resource produced from the reservoir over time. [0324] In some embodiments, injection of the fluid into the reservoir allows for 1.01 times the quantity of lithium to be produced from said reservoir over its lifetime.
  • injection of the fluid into the reservoir allows for at least 1.01 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 1.05 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows WSGR Docket No.50741-724.601 for at least 1.10 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 1.20 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 1.50 times the quantity of lithium to be produced from said reservoir over its lifetime.
  • injection of the fluid into the reservoir allows for at least 2.0 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 2.5 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 3.0 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 4.0 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 5.0 times the quantity of lithium to be produced from said reservoir over its lifetime.
  • injection of the fluid into the reservoir allows for at least 6.0 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 7.0 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 8.0 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 9.0 times the quantity of lithium to be produced from said reservoir over its lifetime. In some embodiments, injection of the fluid into the reservoir allows for at least 10.0 times the quantity of lithium to be produced from said reservoir over its lifetime.
  • injection of the fluid into the reservoir affects the composition of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir affects the composition of the liquid resource produced from the reservoir in a manner that makes the liquid resource more suitable for processing through a lithium extraction system. In some embodiments, injection of the fluid into the reservoir increases the lithium purity of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir decreases the lithium purity of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir increases the total dissolved solids in the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir decreases the total dissolved solids in the liquid resource produced from the reservoir.
  • injection of the fluid into the reservoir increases the total suspended solids in the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir decreases the total suspended solids in the WSGR Docket No.50741-724.601 liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir increases the temperature of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir decreases the temperature of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir increases the viscosity of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir decreases the viscosity of the liquid resource produced from the reservoir.
  • injection of the fluid into the reservoir increases the pH of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir decreases the pH of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir maintains the pH of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir increases the oxidation-reduction potential of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir decreases the oxidation-reduction potential of the liquid resource produced from the reservoir. In some embodiments, injection of the fluid into the reservoir maintains the oxidation- reduction potential of the liquid resource produced from the reservoir.
  • Example 2 of the present disclosure A non-limiting example of injecting a fluid into a reservoir is detailed in Example 2 of the present disclosure.
  • the methods for injecting a fluid into a reservoir described herein, including at least the configurations and effects associated with such methods, are applicable to at least the range of reservoirs described herein. Characterizing and Evaluating the Effects of Injecting Fluid into a Reservoir [0328] In some embodiments, the effects of injecting fluid into a reservoir from which a liquid resource is produced can be characterized and evaluated.
  • Such characterization and evaluation can assist in modulating the configuration and operating parameters (e.g., flow rate, pressure, etc.) of a production wellfield (and the individual production wells therein) and/or an injection wellfield (and the individual injection wells therein).
  • modulating the configuration and operating parameters of a production wellfield and/or an injection wellfield in turn modulates the observed effects of injecting fluid into the reservoir. Accordingly, said modulation and said characterization and evaluation may be conducted iteratively or continuously.
  • the effects of injecting fluid into a reservoir from which a liquid resource is produced can be characterized and evaluated using dispersion tests.
  • dispersion tests are used to determine the effective porosity of a reservoir from WSGR Docket No.50741-724.601 which the liquid resource is being produced.
  • a dispersion test can be used to determine the minimum connected pore volume around a given wellbore (e.g., the bore of a production well, the bore of an injection well).
  • a dispersion test can be used to determine the minimum connected pore volume within the rock. Such a determination can indicate whether the effective porosity is limited to the free fluid porosity of the reservoir or whether the liquid resource being produced is derived from the capillary bound porosity and/or the clay bound water in the reservoir.
  • Control tests can provide evidence as to whether the effective porosity of the reservoir is a result of the injection of a fluid into the reservoir. In some embodiments, if the measured minimum connected pore volume of a well exceeds the measured free fluid porosity of the reservoir (or the portion thereof that is accessible to the well), the capillary bound porosity of the reservoir is accessible to the well.
  • a non-limiting example of such a dispersion test is described in Example 8 of the present disclosure.
  • the results of dispersion tests are cross-referenced with nuclear magnetic resonance (NMR) data, such as borehole NMR data.
  • NMR nuclear magnetic resonance
  • the results of dispersion tests are expected to align with nuclear magnetic resonance data that distinguishes between the free fluid porosity and the capillary bound porosity of a reservoir.
  • the effects of injecting fluid into a reservoir can be characterized and evaluated by recording and deconvoluting transient pressure and flow rate data at a well or a wellfield. Said recording and deconvoluting can be used to determine the minimum connected pore volume around a given wellbore (e.g., the bore of a production well, the bore of an injection well).
  • Embodiments comprising a 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 filter press.
  • a filter press is a filtration device known in the field of filtration and solids-liquid separation.
  • 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 WSGR Docket No.50741-724.601 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 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, WSGR Docket No.50741-724.601 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 is a single layer filtration fabric. In some embodiments, 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 volume of brine that can be replaced with this immiscible fluid, when draining by gravity, is limited to about 50% of the total volume of brine presents in the rocks within the aquifer. Approximately 50% of the brine remains within the rocks as capillary bound water and clay bound water; this brine is not extracted via production wells, and the lithium in said brine is therefore not recovered during reservoir production.
  • lithium-bearing brine e.g., liquid resource
  • a fluid is simultaneously WSGR Docket No.50741-724.601 reinjected into the reservoir.
  • the fluid that is simultaneously reinjected is a lithium depleted brine.
  • the fluid can be water, or an aqueous solution.
  • the volume of the injected fluid is equal to the volume of produced brine, leading to pressure support and pore voidage replacement within the reservoir.
  • this miscible waterflood therefore allows for lithium that is within capillary bound pores to be extracted when the reinjected fluid migrates into the production wells. This results in (1) greater volumes of brine from a reservoir than traditionally applied immiscible production under gravity drainage, (2) greater quantities of lithium extracted from the reservoir, corresponding to the additional lithium found within capillary bound pores.
  • the net result is an increase overall lithium recovery from a reservoir than is traditionally produced from the free fluid volume through additional production of currently inaccessible capillary bound fluid within the pores of the reservoir.
  • the lithium can be recovered to produce lithium products through any of the conventional, emerging, or future methods used to economically extract lithium from brine, to produce lithium products such as lithium carbonate, lithium phosphate, lithium hydroxide, lithium sulfate, lithium metal, or other lithium compounds.
  • Example 3 Enhanced lithium recovery from an immature modern salar reservoir [0341] With reference to FIG.3, lithium recovery from a reservoir is enhanced by miscible flood process 304.
  • a lithium-enriched brine is produced from a sub-surface reservoir via pumping from a production well field 301, wherein the lithium-enriched brine is produced using an electrical submersible pump.
  • Production wells produce 1,000 m 3 /day and are spaced 1000 m apart, in a square arrangement.
  • the brine is produced from multiple subsurface reservoirs: an unconsolidated alluvial sand and gravel reservoir spanning from a depth of 50 m to 350 m, and a consolidated sand reservoir spanning from a depth of 50 m to 1500 m thick.
  • WSGR Docket No.50741-724.601 [0342]
  • the produced brine is pumped into lithium extraction system 302, where lithium is extracted from said brine via a selective ion exchange process.
  • This selective ion exchange process extracts the lithium from the brine, while all other ions exit the lithium extraction system 302 with the depleted brine.
  • the lithium concentration of the lithium-depleted brine is approximately 20% of the concentration in originally produced brine composition after its processing in system 302.
  • Lithium-depleted brine is reinjected into the reservoir in Step 303.
  • the rate at which said brine is reinjected is equivalent to the rate at which said brine is being produced in system 301.
  • To stay below the fracture pressure there are 2 injection wells for every producing well.
  • the brine is reinjected at between 20 to 300 psi in each well, the pressure depending on the type of reservoir and the depth at which the reinjection well is completed over.
  • Step 303 initiates a miscible waterflood process 304.
  • the reinjection fluid provides pressure support and pore voidage replacement between the producing wells and the reinjection wells.
  • This process allows for the recovery of capillary bound lithium-enriched brine, which can now exit via production wells in Step 301.
  • This lithium is produced in addition to the traditionally produced free fluid within the reservoir pore volume. This allows for two times greater lithium content in the reservoir to be recovered, compared to the currently applied immiscible production under gravity drainage.
  • step 303 results in mixing of lithium depleted brine with the liquid, leading to a decrease in the concentration of lithium in the reservoir, the magnitude of which is controlled by the well spacing and the reservoir connectivity, permeability and heterogeneity. In spite of this decrease in concentration, the total amount of fluid recovered from the reservoir is increased, because of the replacement of liquid in the reservoir with lithium depleted brine. In traditional lithium-brine production, steps 303 and 304 are omitted. Since lithium-depleted brine is not introduced into the reservoir via reinjection, the lithium concentration in the reservoir hosted brine decreases less than when steps 303 and 304 are applied.
  • step 403 initiates a miscible waterflood process 404.
  • the reinjection fluid provides pressure support and pore voidage replacement between the producing wells and the reinjection wells.
  • This process allows for the recovery of capillary WSGR Docket No.50741-724.601 bound lithium-enriched brine, which can now exit via production wells in Step 401. This lithium is produced in addition to the traditionally produced free fluid within the reservoir pore volume.
  • step 403 results in mixing of lithium depleted brine with the liquid, leading to a decrease in the concentration of lithium in the reservoir, the magnitude of which is controlled by the well spacing and the reservoir connectivity, permeability and heterogeneity. In spite of this decrease in concentration, the total amount of fluid recovered from the reservoir is increased, because of the replacement of liquid in the reservoir with lithium depleted brine. In traditional lithium-brine production, steps 403 and 404 are omitted.
  • Example 5 Enhanced lithium recovery from Paleo-brines: US carbonate reservoir [0348] With reference to FIG.5, lithium recovery from a reservoir is enhanced by miscible flood process 504. A lithium-enriched brine is produced from a sub-surface reservoir via pumping from a production well field 501, wherein the lithium-enriched brine is produced using an electrical submersible pump.
  • Production wells produce 3,000 m 3 /day and are spaced 5000 m apart, in a square arrangement.
  • the brine is produced from confined reservoirs: A carbonate oolite and dolomite up to 4000 m deep and 500 m thick.
  • the lithium enriched brine is capped by a thick impermeable anhydrite layer.
  • the produced brine is pumped into lithium extraction system 502, where lithium is extracted from said brine via a selective ion exchange process. This selective ion exchange process extracts the lithium from the brine, while all other ions exit the lithium extraction system 502 with the depleted brine.
  • the lithium concentration of the lithium-depleted brine is approximately 20% of the concentration in originally produced brine composition after its processing in system 502.
  • Step 503. Lithium-depleted brine is reinjected into the reservoir in Step 503.
  • the rate at which said brine is reinjected is equivalent to the rate at which said brine is being produced in system 501.
  • To stay below the fracture pressure there is 1 injection well for every producing well.
  • the brine is reinjected up to 5000 psi in each well, the pressure depending on the depth at which the WSGR Docket No.50741-724.601 reinjection well is completed over.
  • the reinjection wells are spaced between on average 5000 m from the production wells.
  • Step 503 initiates a miscible waterflood process 504.
  • the reinjection fluid provides pressure support and pore voidage replacement between the producing wells and the reinjection wells.
  • This process allows for the recovery of capillary bound lithium-enriched brine, which can now exit via production wells in Step 501.
  • This lithium is produced in addition to the traditionally produced free fluid within the reservoir pore volume. This allows for two times greater lithium content in the reservoir to be recovered, compared to the currently applied immiscible production under gravity drainage.
  • the injection of lithium-depleted brine in step 503 results in mixing of lithium depleted brine with the liquid, leading to a decrease in the concentration of lithium in the reservoir, the magnitude of which is controlled by the well spacing and the reservoir connectivity, permeability and heterogeneity.
  • Enhanced lithium recovery from Paleo-brines European sandstone reservoir [0353] With reference to FIG.6, lithium recovery from a reservoir is enhanced by miscible flood process 604.
  • a lithium-enriched brine is produced from a sub-surface reservoir via pumping from a production well field 601, wherein the lithium-enriched brine is produced using an electrical submersible pump.
  • Production wells produce 7000 m 3 /day and are spaced 5000 m apart, in a square arrangement.
  • the brine is produced from confined reservoirs: A sandstone 3000 m deep and 400 m thick.
  • the lithium enriched brine is capped by a thick impermeable evaporite layer.
  • the produced brine is pumped into lithium extraction system 602, where lithium is extracted from said brine via a selective ion exchange process.
  • This selective ion exchange process extracts the lithium from the brine, while all other ions exit the lithium extraction system 602 with the depleted brine.
  • the lithium concentration of the lithium-depleted brine is approximately 20% of the concentration in originally produced brine composition after its processing in system 602.
  • WSGR Docket No.50741-724.601 Lithium-depleted brine is reinjected into the reservoir in Step 603. The rate at which said brine is reinjected is equivalent to the rate at which said brine is being produced in system 601. To stay below the fracture pressure, there is 1 injection well for every producing well.
  • Step 603 initiates a miscible waterflood process 604.
  • the reinjection fluid provides pressure support and pore voidage replacement between the producing wells and the reinjection wells. This process allows for the recovery of capillary bound lithium-enriched brine, which can now exit via production wells in Step 601. This lithium is produced in addition to the traditionally produced free fluid within the reservoir pore volume. This allows for two times greater lithium content in the reservoir to be recovered, compared to the currently applied immiscible production under gravity drainage.
  • step 603 results in mixing of lithium depleted brine with the liquid, leading to a decrease in the concentration of lithium in the reservoir, the magnitude of which is controlled by the well spacing and the reservoir connectivity, permeability and heterogeneity. In spite of this decrease in concentration, the total amount of fluid recovered from the reservoir is increased, because of the replacement of liquid in the reservoir with lithium depleted brine.
  • steps 603 and 604 are omitted. Since lithium-depleted brine is not introduced into the reservoir via reinjection, the lithium concentration in the reservoir hosted brine decreases less than when steps 603 and 604 are applied.
  • Example 7 Enhanced Lithium recovery from Geothermal brines: European fractured reservoir [0358] With reference to FIG.7, lithium recovery from a reservoir is enhanced by miscible flood process 704. A geothermal lithium-enriched brine is produced from a sub-surface reservoir via pumping from a production well field 701, wherein the lithium-enriched brine is produced using an electrical submersible pump. Production wells produce 6500 m 3 /day and are spaced 2000 m apart, in a square arrangement.
  • the brine is produced from confined reservoirs: A highly fractured sandstone sequence 4000 m deep and 300 m thick.
  • the lithium enriched brine is capped by a thick impermeable clay layer.
  • WSGR Docket No.50741-724.601 [0359]
  • the produced brine is pumped into lithium extraction system 702, where lithium is extracted from said brine via a selective ion exchange process. This selective ion exchange process extracts the lithium from the brine, while all other ions exit the lithium extraction system 702 with the depleted brine.
  • the lithium concentration of the lithium-depleted brine is approximately 20% of the concentration in originally produced brine composition after its processing in system 702. [0360] Lithium-depleted brine is reinjected into the reservoir in Step 703.
  • Step 703 initiates a miscible waterflood process 704.
  • the reinjection fluid provides pressure support and pore voidage replacement between the producing wells and the reinjection wells. This process allows for the recovery of capillary bound lithium-enriched brine, which can now exit via production wells in Step 701.
  • step 703 results in mixing of lithium depleted brine with the liquid, leading to a decrease in the concentration of lithium in the reservoir, the magnitude of which is controlled by the well spacing and the reservoir connectivity, permeability and heterogeneity. In spite of this decrease in concentration, the total amount of fluid recovered from the reservoir is increased, because of the replacement of liquid in the reservoir with lithium depleted brine. In traditional lithium-brine production, steps 703 and 704 are omitted.
  • Example 8 Core dispersion test analysis [0363] With reference to FIG.8, a core analysis experiment to determine and prove the concept of enhanced lithium recovery from a miscible waterflood is described. Core samples 801 are prepared via cutting and cleaning prior to full saturation of the pore space with brine 802.
  • Brine WSGR Docket No.50741-724.601 is doped with cesium chloride, a radioactive tracer, and flowed through the core sample and numerous pore volumes are flowed 803.
  • the tracer concentration is measured via gamma ray detection 804 which allows for the quantification of the effective porosity of the core sample 804 and providing evidence that the capillary-bound fluid is accessible for production and swept by the miscible brine flood.
  • Example 9 CO2 injection to enhance lithium brine recovery [0364] With reference to FIG.9, lithium recovery from a reservoir is enhanced by injection of carbon dioxide into said reservoir in flood process 904.
  • a lithium-containing brine is produced from a sub-surface confined reservoir, wherein the brine exits to the surface driven by the autogenous pressure of the reservoir from well field 901.
  • the produced brine is pumped into lithium extraction system 902, where lithium is extracted from said brine.
  • This lithium extraction process extracts the lithium from the brine by concentrating said brine in solar evaporation ponds, resulting in the progressive concentration of lithium and precipitation of impurities.
  • Said impurities are concentrated via concentration- induced precipitation, as well as through reagent and pH-induced precipitation, and are remove through filtration.
  • the concentrated brine is subject to further purification and precipitation steps, conventionally used in the field of lithium production, to yield a lithium carbonate product.
  • Step 903 initiates a miscible flood process 904.
  • the injection fluid provides pressure support and pore voidage replacement between the producing wells and the injection wells.
  • This process allows for the recovery of capillary bound lithium-enriched brine, which can now exit via production wells in Step 901.
  • This lithium is produced in addition to the traditionally produced free fluid within the reservoir pore volume. This allows for two times greater lithium content in the reservoir to be recovered, compared to the currently applied primary production when brine is allowed to exit the reservoir under its autogenous pressure.
  • the injection of CO2 maintains the pressure of the reservoir to allow for continuous production of brine without additional pumping.
  • This selective ion exchange process extracts a portion of the lithium from the brine, while all other ions exit the lithium extraction system 1002 with the lithium-depleted brine.
  • the brine entering system 1002 has the following approximate average composition: 1000 mg/L of Li, 70,000 mg/L of Na, 1,500 mg/L of Mg, 800 mg/L of Ca, 5,000 mg/L of K, 1000 mg/L of B, and other minor cationic species as well as chloride counterions.
  • Depleted brine exiting system 1002 comprises 100 mg/L of Li and similar concentrations of other ions.
  • Step 1003 initiates a miscible waterflood process 1004.
  • the reinjection fluid provides pressure support and pore voidage replacement between the producing wells and the reinjection wells. This process allows for the recovery of capillary bound lithium into the lithium-containing brine, which can now exit via production wells in 1001.
  • 1002 comprises a direct lithium extraction system.
  • Said system contains a lithium selective ion exchange material, which is contacted with liquid resource produced by 1001; said ion exchange material selectively absorbs Li ions while releasing protons.
  • the decrease in Li concentration to 500 mg/L upon the miscible flood results in a diminished release of protons during lithium uptake, leading to a diminished drop in pH upon lithium uptake, which decreases the time required for lithium uptake to only 1 hour. Additionally, the processing of this lower lithium concentration brine results in an increase in the total number of cycles before the ion exchange beads must be replaced, to 3000 at a 500 mg/L inlet lithium concentration from 400 at a 1,000 mg/L lithium concentration. [0372] As such, the change in lithium concentration resulting from the miscible flood process 1004 results in a more optimal operation of the direct lithium extraction system 1002. Additionally, the miscible flood results in a higher total amount of lithium to be extracted from the lithium reservoir over the lifetime of said reservoir.
  • the unextracted lithium that is re-injected in with the depleted brine in 1003 mixes with the capillary bound lithium, and is eventually extracted from the reservoir again via system 1001.
  • said lithium is once again processed through system 1002, and a portion of said lithium is recovered.
  • the net effect is a higher overall recovery of lithium from the liquid resource, in addition to the higher overall increase to the amount of extractable lithium in the reservoir.
  • the combination of a miscible flood with the advantages that such miscible flood has for lithium extraction results in a more optimal operation of the lithium reservoir and associated lithium production system.
  • Example 11 Enhanced lithium recovery via hydraulic fracture stimulation
  • lithium recovery from a reservoir is enhanced by miscible flood process 1104.
  • a sub-surface, lithium-enriched brine reservoir is hydraulically stimulated with pressures up to 15,000 psi, forming fractures that increase the permeability of the reservoir allowing for production via pumping from a production well field 1101.
  • the produced brine is pumped into lithium extraction system 1102, where lithium is extracted from said brine via a selective ion exchange process. This selective ion exchange process extracts the lithium from the brine, while all other ions exit the lithium extraction system 1102 with the depleted brine.
  • the lithium concentration of the lithium-depleted brine is approximately 20% of the concentration in originally produced brine composition after its processing in system 1102.
  • Lithium-depleted brine is reinjected into the reservoir in Step 1103.
  • Step 1103 initiates a miscible waterflood process 1104.
  • the reinjection fluid provides pressure support and pore voidage replacement between the producing wells and the reinjection wells.
  • This WSGR Docket No.50741-724.601 process allows for the recovery of capillary bound lithium-enriched brine, which can now exit via production wells in Step 1101. This lithium is produced in addition to the traditionally produced free fluid within the reservoir pore volume. This allows for two times greater lithium content in the reservoir to be recovered, compared to the currently applied immiscible production under gravity drainage.
  • step 1103 The injection of lithium-depleted brine in step 1103 results in mixing of lithium depleted brine with the liquid, leading to a decrease in the concentration of lithium in the reservoir, the magnitude of which is controlled by the well spacing and the reservoir connectivity, permeability and heterogeneity. In spite of this decrease in concentration, the total amount of fluid recovered from the reservoir is increased, because of the replacement of liquid in the reservoir with lithium depleted brine. In traditional lithium-brine production, steps 1103 and 1104 are omitted. Since lithium-depleted brine is not introduced into the reservoir via reinjection, the lithium concentration in the reservoir hosted brine decreases less than when steps 1103 and 1104 are applied.
  • Example 12 Core dispersion tests indicating enhanced lithium recovery from a reservoir rock [0378] With reference to Table 1, the results of dispersion tests described in Example 8 are provided herein. The results of the core dispersion test provide data on the number of pore volumes of reinjected brine required to sweep the total pore space of a core sample, as required for a miscible flood to recover lithium within the pore space. The core samples were obtained from a Salar reservoir. [0379] The term "pore volume" refers to the volume of the pore space within the core plug sample.
  • the pore volume of each core plug was determined using a nuclear magnetic resonance (NMR) measurement on a Magritek 2 MHz Rock Core Analyser, using a brine doped with a Cesium Chloride Tracer.
  • the pore volumes calculated from NMR include total porosity (PHIT), effective porosity (PHIE) – corresponding to the free fluid priority–, and specific yield (Sy) – corresponding to the ratio of fluid that can drain by gravity –. All values are all measured as fractions of total volume (volume of porosity / volume of total sample).
  • the average number of pore volumes required to sweep the PHIE volume is 1.12, which exceeds 1.
  • displacement WSGR Docket No.50741-724.601 more than one pore volume is required to recover additional lithium from the totality of the pore space.
  • This process allows for the effective porosity volume (PHIE) to be produced during production, rather than solely the specific yield (Sy) achievable through traditional, non- reinjection production methods.
  • a process of recovering lithium from a reservoir comprising: a) producing a liquid resource comprising lithium from the reservoir; b) extracting at least a portion of the lithium from the liquid resource; c) injecting a fluid into the reservoir; wherein a) and c) are performed simultaneously.
  • said lithium selective sorbent is an adsorbent.
  • processing the synthetic lithium solution comprises generating lithium carbonate, lithium phosphate, lithium hydroxide, lithium sulfate, or any combination thereof.
  • processing the synthetic lithium solution comprises generating lithium carbonate.
  • processing the synthetic lithium solution comprises lithium phosphate.
  • processing the synthetic lithium solution comprises generating lithium hydroxide.
  • processing the synthetic lithium solution comprises generating lithium sulfate.
  • the chemical additive is an oxidant.
  • the 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, or any combinations thereof.
  • (101) The process of any one of embodiments 1 to 100, wherein the fluid injection of c) lowers the lithium concentration of the liquid resource in the reservoir.
  • (102) The process of embodiment 101, wherein the concentration of the liquid resource is lowered to increase the efficiency of lithium extraction by the lithium selective sorbent.
  • (103) The process of any one of embodiments 27 to 102, wherein the fluid injection of c) modulates the properties of the liquid resource such that b) generates a synthetic lithium solution with favorable properties.
  • (123) The system of any one of embodiments 117 to 122, wherein the one or more production wells are spaced in relation to the one or more injection wells by a distance of at least about 500 m, at least about 1000 m, at least about 1500 m, at least about 2000 m, at least about 3000 m, at least about 5000 m, at least about 10000 m.
  • (124) The system of any one of embodiments 117 to 123, wherein the reservoir is an immature modern salar reservoir, mature modern day reservoir, US carbonate reservoir, European sandstone reservoir, or European fractured reservoir.

Landscapes

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

Abstract

La présente invention concerne l'extraction de lithium à partir de réservoirs souterrains de saumures naturelles. L'invention concerne des systèmes et des procédés pour extraire du lithium piégé dans des réservoirs qui étaient auparavant inaccessibles.
PCT/US2024/052957 2023-10-27 2024-10-25 Récupération améliorée de lithium à partir de réservoirs souterrains Pending WO2025090864A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202363593706P 2023-10-27 2023-10-27
US63/593,706 2023-10-27

Publications (1)

Publication Number Publication Date
WO2025090864A1 true WO2025090864A1 (fr) 2025-05-01

Family

ID=95516612

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2024/052957 Pending WO2025090864A1 (fr) 2023-10-27 2024-10-25 Récupération améliorée de lithium à partir de réservoirs souterrains

Country Status (1)

Country Link
WO (1) WO2025090864A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US12374679B2 (en) 2017-08-02 2025-07-29 Lilac Solutions, Inc. Ion exchange system for lithium extraction
US12370468B2 (en) 2022-03-28 2025-07-29 Lilac Solutions, Inc. Lithium extraction enhanced by an alternate phase

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20220364203A1 (en) * 2019-11-01 2022-11-17 Korea Institute Of Geoscience And Mineral Resources Method for recovering lithium from brine
CN219262345U (zh) * 2022-12-30 2023-06-27 陕西省煤田地质集团有限公司 一种深层富锂卤水开采系统

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20220364203A1 (en) * 2019-11-01 2022-11-17 Korea Institute Of Geoscience And Mineral Resources Method for recovering lithium from brine
CN219262345U (zh) * 2022-12-30 2023-06-27 陕西省煤田地质集团有限公司 一种深层富锂卤水开采系统

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
GRANT ALEX, DOORNBOS CHRIS: "Much Ado About Unconfined Aquifers?", JADE COVE PARTNERS, 1 November 2020 (2020-11-01), XP093312132, Retrieved from the Internet <URL:https://www.jadecove.com/research/muchado> *
HOUSTON J., BUTCHER A., EHREN P., EVANS K., GODFREY L.: "The Evaluation of Brine Prospects and the Requirement for Modifications to Filing Standards", ECONOMIC GEOLOGY : BULLETIN OF THE SOCIETY OF ECONOMIC GEOLOGISTS, SOCIETY OF ECONOMIC GEOLOGISTS, US, vol. 106, no. 7, 1 October 2011 (2011-10-01), US , pages 1225 - 1239, XP093312130, ISSN: 0361-0128, DOI: 10.2113/econgeo.106.7.1225 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US12374679B2 (en) 2017-08-02 2025-07-29 Lilac Solutions, Inc. Ion exchange system for lithium extraction
US12370468B2 (en) 2022-03-28 2025-07-29 Lilac Solutions, Inc. Lithium extraction enhanced by an alternate phase

Similar Documents

Publication Publication Date Title
JP7379351B2 (ja) リチウムの抽出と変換のための統合システム
US20250323240A1 (en) Ion exchange system for lithium extraction
US20190256987A1 (en) Integrated system for lithium extraction and conversion
US11466191B2 (en) Treated geothermal brine compositions with reduced concentration of silica, iron and lithium
WO2025090864A1 (fr) Récupération améliorée de lithium à partir de réservoirs souterrains
US11377362B2 (en) Lithium production with volatile acid
US9012357B2 (en) Lithium extraction composition and method of preparation thereof
KR20230023714A (ko) 스케일런트의 존재 하에서의 리튬 추출
US20250283193A1 (en) Synthetic lithium solutions with controlled impurity profiles
US12370468B2 (en) Lithium extraction enhanced by an alternate phase
WO2023215313A1 (fr) Élimination d&#39;impuretés contenues dans un éluat de lithium
US11174532B1 (en) Processes for producing lithium compounds using reverse osmosis
EP4232192A1 (fr) Matériau composite et procédé d&#39;extraction de lithium au moyen de celui-ci
WO2025029953A1 (fr) Systèmes et procédés pour minimiser l&#39;utilisation d&#39;eau externe dans la production de lithium
WO2024077269A2 (fr) Systèmes intégrés et procédés associés pour la récupération de lithium
EP4623115A2 (fr) Extraction de lithium à partir de saumures avec des concentrations d&#39;ions modulées
WO2024220812A1 (fr) Procédés et systèmes de traitement de composés de lithium
AU2021468488A1 (en) Processes for producing lithium compounds using reverse osmosis
US20240271026A1 (en) Treated geothermal brine compositions with reduced concentration of silica, iron and lithium
WO2014172032A2 (fr) Procédés d&#39;élimination du potassium, du rubidium et du césium, séparément ou ensemble, dans des saumures, et compositions résultantes
WO2025226673A1 (fr) Procédés et systèmes améliorés pour générer une solution de lithium à partir d&#39;un matériau échangeur d&#39;ions
US20250161879A1 (en) Process and product
WO2024126601A1 (fr) Extraction de lithium

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 24883396

Country of ref document: EP

Kind code of ref document: A1