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WO2025226431A1 - Procédé de lixiviation alcaline de métaux utiles à partir de batteries au lithium-ion - Google Patents

Procédé de lixiviation alcaline de métaux utiles à partir de batteries au lithium-ion

Info

Publication number
WO2025226431A1
WO2025226431A1 PCT/US2025/023388 US2025023388W WO2025226431A1 WO 2025226431 A1 WO2025226431 A1 WO 2025226431A1 US 2025023388 W US2025023388 W US 2025023388W WO 2025226431 A1 WO2025226431 A1 WO 2025226431A1
Authority
WO
WIPO (PCT)
Prior art keywords
lithium
ammonium
combination
metal
mass
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/US2025/023388
Other languages
English (en)
Inventor
Yi Ji
Zhen TIAN
Jonathan MELO
Kinnor CHATTOPADHYAY
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.)
Albemarle Corp
Original Assignee
Albemarle Corp
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 Albemarle Corp filed Critical Albemarle Corp
Publication of WO2025226431A1 publication Critical patent/WO2025226431A1/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
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • C22B26/12—Obtaining lithium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/70—Chemical treatment, e.g. pH adjustment or oxidation
    • 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
    • C22B21/00—Obtaining aluminium
    • C22B21/0015—Obtaining aluminium by wet processes
    • C22B21/0023—Obtaining aluminium by wet processes from waste materials
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C22B23/0446—Leaching processes with an ammoniacal liquor or with a hydroxide of an alkali or alkaline-earth metal
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/12—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic alkaline solutions
    • C22B3/14—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic alkaline solutions containing ammonia or ammonium salts
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • 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
    • C22B47/00—Obtaining manganese
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M10/00—Secondary cells; Manufacture thereof
    • H01M10/54—Reclaiming serviceable parts of waste accumulators
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/84—Recycling of batteries or fuel cells

Definitions

  • impurities e.g., Fe, Al, Zn
  • the present disclosure provides a process comprising.
  • ESS-L1-8131 WO more metal-containing compounds, wherein the metal is selected from the group consisting of lithium, cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing; (B) separating an alkaline leachate from the combination; (C) infusing one or more oxidizing agents into the alkaline leachate; (D) adjusting the pH of the alkaline leachate to enhance formation of a precipitate comprising one or more metal-containing compounds, wherein the metal is selected from the group consisting of lithium, cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing; and (E) infusing one or more of carbon dioxide, sodium carbonate, sodium bicarbonate, lithium carbonate, and lithium bicarbonate into the alkaline leachate to enhance formation of an additional precipitate comprising one or more metal-containing compounds, where in the metal is selected from the group consisting of cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing.
  • the ammonium system comprises the ammonia source and a buffer.
  • the buffer comprises ammonium carbonate, ammonium bicarbonate, lithium carbonate, lithium bicarbonate, sodium carbonate, sodium bicarbonate, carbonic acid, or a combination of any two or more of the foregoing.
  • the ammonia source comprises ammonium hydroxide, ammonium sulfate, ammonium chloride, or any combination of two or more of the foregoing.
  • the ammonium system further comprises a reducing agent.
  • the reducing agent comprises ammonium sulfite, hydrogen peroxide, or a combination of the two.
  • the pH of the ammonium system in step (A) of the process is in the range of about 7 to about 14. In other aspects of the invention the pH of the ammonium system is in the range of about 8 to about 11.
  • the terms “a,” “an,” and “the” are intended to include plural alternatives, e.g., at least one, one or more, and one or more than one, unless otherwise specified.
  • the term “contacting” is used herein to describe systems, compositions, processes, and methods in which the components are contacted, combined, or brought together in any order, in any manner, and for any length of time, unless otherwise specified. For example, the components can be combined by blending or mixing, using any suitable technique.
  • the terms “room temperature” or “ambient temperature” are used herein to describe any temperature from 15° C to 35° C wherein no external heat or cooling source is directly applied to the reaction vessel.
  • room temperature and “ambient temperature” encompass the individual temperatures and any and all ranges, subranges, and combinations of subranges of temperatures from 15°C to 35°C wherein no external heating or cooling source is directly applied to the reaction vessel.
  • atmospheric pressure or “ambient pressure” is used herein to describe an earth air pressure wherein no external pressure modifying means is utilized. Generally, unless practiced at extreme earth altitudes, “atmospheric pressure” is about 1 atmosphere (alternatively, about 14.7 psi or about 101 kPa).
  • the terms “battery” and “lithium battery” refer to a lithium-ion battery; similarly, the terms “batteries” and “lithium batteries” refer to lithium-ion batteries.
  • the term “about” means that amounts, sizes, formulations, parameters, and other quantities and characteristics are not and need not be exact, but may be approximate including being larger or smaller, as desired, reflecting tolerances, conversion factors, Atty Docket No. ESS-L1-8131 WO rounding off, measurement errors, and the like, and other factors known to those of skill in the art. In general, an amount, size, formulation, parameter or other quantity or characteristic is “about” or “approximate” whether or not expressly stated to be such.
  • the ammonium-based leaching aspect of the processes disclosed herein is an effective process feature enabling the processes to achieve selective extraction of valuable metals (e.g., Li, Co, Ni) from black mass.
  • Such a process employs an ammonium system for selective Li, cobalt (Co), and nickel (Ni) leaching where manganese (Mn) is eliminated from the leachate.
  • the leaching efficiencies are remarkable, as will be noted from the examples below.
  • Embodiments disclosed herein can provide the materials listed as suitable for satisfying a particular feature of the embodiment delimited by the term “or.”
  • Feature X can be A, B, or C.
  • a mass e.g., black mass formed from shredded lithium- ion battery active material components, preferably separated from other non-active Atty Docket No.
  • WO lithium-ion battery components such as plastic casings and the like
  • a liquid ammonium system comprising an ammonia source
  • the battery mass is one that has been formed from at least disused or end-of-life lithium-ion batteries.
  • the lithium- ion battery mass is generally in the form of a powder, preferably a granular powder.
  • the lithium-ion battery mass is preferably a granular powder, and preferably has an average particle size of about 500 microns or less, more preferably about 300 microns or less.
  • the lithium-ion battery black mass can be subjected to particle size reductions techniques such as grinding or milling to achieve the desired particle sizes.
  • the (lithium-ion battery) mass contains graphite from the lithium-ion battery.
  • the mass is subjected to an optional process to remove the graphite.
  • the process for removal of graphite from the mass is frequently a flotation process; the flotation process can have more than one stage.
  • Typical flotation procedures for graphite removal from the mass include froth flotation; in froth flotation, the foaming agent can be 4-methyl-2-pentanol (methyl isobutyl carbinol), and the graphite collector can be kerosene.
  • the product of the flotation procedure is a 'clean' mass preferably containing little or no graphite.
  • the contacting in step A) is performed in an ambient pressure system, such that if the reactions that occur produce heat or the combination is heated, the pressure does not increase significantly above ambient pressure. In a closed system, this can be accomplished by periodically relieving pressure increases, for example by briefly opening a valve to the atmosphere.
  • the (lithium-ion battery) mass comprises one or more metal-containing compounds.
  • the metal of the metal containing compounds is selected from the group consisting of lithium, cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing.
  • Typical non-limiting examples of the metal-containing compounds are copper, manganese, zinc, calcium, silicon, and the like.
  • the mass is derived from lithium nickel manganese cobalt oxide batteries, lithium nickel cobalt aluminum oxide batteries, and/or lithium manganese oxide batteries.
  • the mass is derived from Atty Docket No. ESS-L1-8131 WO one type of battery, preferably lithium nickel manganese cobalt oxide batteries or lithium nickel cobalt aluminum oxide batteries.
  • the mass is formed from lithium-ion batteries that exclude those of the iron phosphate or Li iron phosphate (LFP) type.
  • the mass in some aspects of the invention is also pre-treated to remove copper (Cu), unless known to be devoid of copper, so that copper is not present in any material amount in the leachate formed. It may also be preferred in some aspects of the invention that the mass is not derived from manganese-based lithium-ion batteries (e.g., those with lithium-ion manganese oxide cathode (LMO) material).
  • LMO lithium-ion manganese oxide cathode
  • the ammonium source of the liquid ammonium system in at least some aspects of the invention comprises either ammonium hydroxide, ammonium sulfate, ammonium chloride, or any combination of two or more of the foregoing.
  • the liquid ammonium system optionally may comprise additional components, including a buffer or a reducing agent, or both.
  • the buffer in some aspects of the invention comprises ammonium carbonate, ammonium bicarbonate, lithium carbonate, lithium bicarbonate, sodium carbonate, sodium bicarbonate, carbonic acid, or a combination of the two or more of the foregoing.
  • the reducing agent in some aspects of the invention comprises ammonium sulfite, hydrogen peroxide, or a combination of the two.
  • the liquid ammonium system’s components are typically in an aqueous solution.
  • the amount of the ammonium source present in the liquid ammonium system, and the amount of buffer and/or reducing agent, if used, may vary, but typically the amount of ammonium source will be in the range of about 0.5 M to about 5M, the amount of buffer if present will be in the range of 0 to about 5M, and the amount of reducing agent if present will be in the range of about 0 to about 2.5M.
  • the ammonium system employed in at least some aspects of the invention will just prior to contacting the mass have a pH in the range of about 7 to about 14. In yet other aspects of the invention, the pH of the ammonium system at that time will be in the range of about 8 to about 11.
  • the relative amounts of mass to liquid ammonium system employed is typically in the range of about 5g/L to about 1000g/L, preferably about 100g/L to about 750 g/L, more preferably about 125 g/L to about 500 g/L or about 300 g/L to about 700 g/L, where grams refer to the black mass and liters refer to the liquid ammonium system.
  • the contacting undertaken in this step will typically be in a reaction vessel or zone, typically under conditions that apply a physical agitation, usually stirring, to the Atty Docket No. ESS-L1-8131 WO combination of mass and ammonium system, over a period of time.
  • the agitation can be carried out by mixing or stirring in any conventional manner under a given reactor configuration to give the liquid ammonium system and particulate mass the opportunity to come into contact with one another for some period of time, and that period of time may vary widely depending upon the components and reaction conditions, but typically will be in the range of about 0.5 to about 8 hours, under ambient pressure conditions.
  • the stirring speed is in the range of about 100 to about 2000 rpm, preferably about 100 to about 1000 rpm, more preferably about 100 to about 500 rpm.
  • the mixture is maintained at one or more temperatures in the range of about 26° C to about 60° C during this leaching period.
  • B. Separation of Alkaline Leachate [0038] Following contacting of the mass and ammonium system, the resulting mixture is treated so that alkaline leachate can be recovered by separation from the remaining material in the mixture by methods known in the art, such as decantation, centrifugation, or filtration. The separation is carried out typically by filtration. The alkaline leachate usually contains the metals of interest.
  • an oxidizing agent is then infused into the recovered alkaline leachate.
  • the oxidizing agent is typically air or oxygen gas.
  • the oxidizer is infused by means such as bubblers, aerators, porous membranes or the like, so as to infuse the oxidizing agent in gas form into the alkaline leachate.
  • the infusion may be carried out at various temperature and pressure conditions over a varying time period, but typically is carried out at ambient pressure and temperature conditions and for a period of time in the range of 5 minutes to about 5 hours.
  • the amount of oxidizing agent infused will also vary but is typically in the range of about 1 Nl/(min ⁇ L) to about 50 Nl/(min ⁇ L) at ambient pressure and temperature conditions.
  • the pH of the alkaline leachate is adjusted to enhance formation of a precipitate comprising one or more metal-containing compounds, wherein the metal is selected from the group consisting of lithium, cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing.
  • the pH typically is adjusted by the addition of sodium hydroxide or another base of a type and quantity that brings the alkaline leachate pH in the range of about 10 to about 13.
  • E. Second Infusion to Enhance Precipitation After pH adjustment, one or more of carbon dioxide, sodium carbonate, sodium bicarbonate, lithium carbonate, and lithium bicarbonate are infused into the alkaline leachate to enhance formation of an additional precipitate comprising one or more metal- containing compounds, wherein the metal is selected from the group consisting of cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing.
  • one or more lithium compounds may be present in the precipitate due to incomplete recovery of lithium into the liquid phase, and/or by formation of additional precipitate comprising lithium compounds. This infusion may be carried about by a variety of means such as bubblers, aerators and porous membranes, and the like.
  • the temperature and pressure conditions under which the infusion is carried out may be under super-ambient, ambient, or sub-ambient temperature and pressure conditions, but most conveniently is carried out under ambient temperature and pressure conditions.
  • Examples [0042] The subject matter having been generally described, the following examples are given as particular embodiments of the subject matter of this disclosure and to demonstrate the practice and advantages thereof. It is understood that the examples are given by way of illustration and are not intended to limit the claims to follow in any manner.
  • Recovery rates i.e., amount recovered from liquid phase/initial amount in black mass
  • ICP-OES inductively coupled plasma optical emission spectroscopy
  • initial black mass characterization for each of the lithium-ion battery types indicated in the examples, was carried out as follows: 1) Black mass sample was homogenized using an acoustic mixer (LabRAM II, Resodyn Corporation), in case of any sample heterogeneity. This acoustic mixer was a low- frequency acoustic mixer that provided uniform mixing across a broad range of materials and can be applied to powder-powder systems. 2) Some of the homogenized black mass powder (initial mass recorded as m0) prepared in step 1) was heated at 110 °C in an oven for 12 hours.
  • the black mass powder sample was cooled to room temperature and weighed; the sample mass m1 was recorded.
  • the LOD% (Loss on Drying) (m 0 -m 1 )/m 0 ⁇ 100.
  • the LOD% was calculated and then used to estimate the volatile content in the initial black mass.
  • Some of the homogenized black mass powder (initial mass recorded as m 0 ) prepared in step 1) was heated at 850 °C in an oven for 5 hours. The sample was cooled to room temperature and weighed; the sample mass was recorded as m1.
  • the LOI% (Loss on Ignition) (m0 - m1)/m0 ⁇ 100.
  • Example 1 Ammonium leaching
  • Three runs were performed as follows. An aqueous solution having a volume of about 250 mL and containing ammonia hydroxide (about 1.0 M), ammonium sulfite (0.5 M), and ammonium carbonate (0.1 M) was prepared and transferred into 500 mL reaction flask equipped with agitation and heating system. The solution was agitated at a speed of about 200 rpm, while the solution was heated to a temperature of about 60°C. While the solution was heating, about 5 grams of a cathode powder or black mass was added into the 500 mL flask.
  • the cathode powder was lithium nickel manganese cobalt oxide cathode powder (6:2:2 molar proportion of Ni:Mn:Co, or NMC 622); in another run, the black mass was lithium nickel cobalt aluminum oxide (NCA) black mass. In the third run, the cathode powder was lithium manganese oxide cathode powder. [0047] For NMC 622 cathode powder, recovery rates were 91.5% of Li, 96.2% of Co, and 92.7% of Ni.
  • Example 2 Li carbonate/bicarbonate synthesis
  • Example 4 (alternative) [0050] An alkaline leachate collected after the procedure of Example 1 from NCA based black mass was used in a process according to that of Example 2, except the aeration of the alkaline leachate was carried out with carbon dioxide for 2 hours. Then, the pH of the leachate was adjusted and controlled to about 12 by adding sodium hydroxide. The alkaline leachate then was aerated with carbon dioxide for 2 hours. The slurry was generated from reaction flask, and the solid was filtered and washed with water. Li recovery rate in filtrate was 46.7%, with Co and Ni below the detection limit in the filtrate.
  • ESS-L1-8131 WO compounds wherein the metal is selected from the group consisting of lithium, cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing; (B) separating an alkaline leachate from the combination; (C) infusing one or more oxidizing agents into the alkaline leachate; (D) adjusting the pH of the alkaline leachate to enhance formation of a precipitate comprising one or more metal-containing compounds, wherein the metal is selected from the group consisting of lithium, cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing; and (E) infusing one or more of carbon dioxide, sodium carbonate, sodium bicarbonate, lithium carbonate, and lithium bicarbonate into the alkaline leachate to enhance formation of an additional precipitate comprising one or more metal-containing compounds, where in the metal is selected from the group consisting of cobalt, nickel, iron, aluminum, and any combination of two or more of the foregoing.
  • ammonium system comprises the ammonia source and a buffer.
  • the buffer comprises either ammonium carbonate, ammonium bicarbonate, lithium carbonate, lithium bicarbonate, sodium carbonate, sodium bicarbonate, carbonic acid, or a combination of the two.
  • the ammonia source comprises either ammonium hydroxide, ammonium sulfate, ammonium chloride, or any combination of two or more of the foregoing.
  • the ammonium system further comprises a reducing agent. 6.

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Abstract

L'invention concerne un procédé qui consiste à (A) mettre en contact une masse avec un système d'ammonium liquide contenant une source d'ammoniac pour former une combinaison, la masse ayant été formée à partir d'au moins des batteries au lithium-ion et comprenant un ou plusieurs composés contenant du métal, le métal étant choisi parmi le lithium, le cobalt, le nickel, le fer et/ou l'aluminium ; (B) séparer un lixiviat alcalin de la combinaison ; (C) à infuser un ou plusieurs agents oxydants dans le lixiviat alcalin ; (D) ajuster le pH du lixiviat alcalin pour améliorer la formation d'un précipité comprenant un ou plusieurs composés contenant du métal, le métal étant choisi parmi le lithium, le cobalt, le nickel, le fer et/ou l'aluminium ; et (E) infuser un ou plusieurs éléments parmi le dioxyde de carbone, le carbonate de sodium, le bicarbonate de sodium, le carbonate de lithium et le bicarbonate de lithium dans le lixiviat alcalin pour améliorer la formation d'un précipité supplémentaire comprenant un ou plusieurs composés contenant du métal, le métal étant choisi parmi le cobalt, le nickel, le fer et/ou l'aluminium.
PCT/US2025/023388 2024-04-25 2025-04-07 Procédé de lixiviation alcaline de métaux utiles à partir de batteries au lithium-ion Pending WO2025226431A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202463638463P 2024-04-25 2024-04-25
US63/638,463 2024-04-25

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20170233848A1 (en) * 2014-10-10 2017-08-17 Li-Technology Pty Ltd Recovery process
US20220010407A1 (en) * 2018-11-26 2022-01-13 Basf Se Battery recycling by hydrogen gas injection in leach
US20220017989A1 (en) * 2018-12-21 2022-01-20 A.C.N. 630 589 0507 Pty Ltd Battery recycling process
US20240120565A1 (en) * 2022-01-17 2024-04-11 Green Li-Ion Pte. Ltd. Process For Recycling Lithium Iron Phosphate Batteries

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20170233848A1 (en) * 2014-10-10 2017-08-17 Li-Technology Pty Ltd Recovery process
US20220010407A1 (en) * 2018-11-26 2022-01-13 Basf Se Battery recycling by hydrogen gas injection in leach
US20220017989A1 (en) * 2018-12-21 2022-01-20 A.C.N. 630 589 0507 Pty Ltd Battery recycling process
US20240120565A1 (en) * 2022-01-17 2024-04-11 Green Li-Ion Pte. Ltd. Process For Recycling Lithium Iron Phosphate Batteries

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