WO2023050805A1 - Procédé d'élimination du fluor dans des batteries au lithium-ion - Google Patents

Procédé d'élimination du fluor dans des batteries au lithium-ion Download PDF

Info

Publication number
WO2023050805A1
WO2023050805A1 PCT/CN2022/090071 CN2022090071W WO2023050805A1 WO 2023050805 A1 WO2023050805 A1 WO 2023050805A1 CN 2022090071 W CN2022090071 W CN 2022090071W WO 2023050805 A1 WO2023050805 A1 WO 2023050805A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluorine
liquid
acid
aluminum hydroxide
reaction
Prior art date
Application number
PCT/CN2022/090071
Other languages
English (en)
Chinese (zh)
Inventor
欧阳石保
李长东
乔延超
陈若葵
阮丁山
蔡勇
Original Assignee
广东邦普循环科技有限公司
湖南邦普循环科技有限公司
湖南邦普汽车循环有限公司
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 广东邦普循环科技有限公司, 湖南邦普循环科技有限公司, 湖南邦普汽车循环有限公司 filed Critical 广东邦普循环科技有限公司
Publication of WO2023050805A1 publication Critical patent/WO2023050805A1/fr

Links

Images

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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • C22B7/007—Wet processes by acid leaching
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/0423—Halogenated acids or salts thereof
    • 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
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/043—Sulfurated acids or salts thereof
    • 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
    • C22B47/00—Obtaining manganese
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
    • C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium
    • C25C3/18—Electrolytes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the invention belongs to the technical field of treating waste lithium batteries, and in particular relates to a method for removing fluorine from waste lithium batteries.
  • Lithium battery is a very promising energy storage battery, which is widely used in various electronic products and new energy vehicles. It is reported that more than 500,000 tons of lithium batteries are discarded every year in the world. With the continuous development of the economy, it is estimated that the global demand for lithium batteries will increase by 10 times in 2030, and the number of discarded batteries will also surge accordingly. Therefore, the recycling of these scrapped lithium batteries has also become an urgent problem to be solved.
  • the traditional wet recycling route of waste lithium batteries is to first discharge, disassemble, and crush the lithium batteries to obtain battery powder, and then leaching the battery powder with acid to recover nickel, cobalt, manganese, and lithium metals. Since the electrolyte of waste lithium batteries contains lithium hexafluorophosphate, and sodium fluoride will be introduced after leaching and impurity removal, the nickel-cobalt-manganese solution after battery powder leaching and impurity removal contains 1-3 g/L of fluorine. The fluorine-containing nickel-cobalt-manganese solution is extracted and acid-backwashed to obtain a nickel-cobalt-manganese sulfate solution, and then the precursor is synthesized.
  • the fluorine-containing raffinate is poured into the waste water treatment tank, and treated by fluoride removal, heavy metal removal, oil removal, etc., and the waste water is discharged after passing the treatment.
  • fluoride ions are highly corrosive to equipment, the longer the process and the more treatment steps, the greater the loss of equipment; 2) the extraction When the fluorine concentration is high, a part of fluorine will enter the nickel-cobalt-manganese sulfate solution, thereby affecting the quality of the product; 3) It will have a certain impact on the subsequent removal of heavy metals, oil removal, and COD removal from wastewater.
  • the present invention aims to solve at least one of the technical problems in the above-mentioned prior art. For this reason, the present invention provides a kind of method for removing fluorine in waste lithium batteries, and the effect of removing fluorine of this method for removing fluorine is good, and fluorine can be removed to below 15mg/L, and after the liquid recovery after removing fluorine, nickel-cobalt-manganese-lithium is poured into After the waste water workshop, there is no need to remove fluorine again.
  • the recovery rate of fluorine is as high as 99%, and the purity of sodium hexafluoroaluminate obtained after defluorination is as high as 98%. It can be used as a co-solvent in the electrolytic aluminum industry, and the potential value of recovery is great.
  • the present invention adopts the following technical solutions:
  • a method for defluorinating waste lithium battery leachate comprising the following steps:
  • the waste lithium battery further includes dismantling, crushing, sorting and screening the waste lithium battery to obtain waste lithium battery powder and aluminum slag before oxidative acid leaching.
  • the oxidant is one of hydrogen peroxide or sodium sulfite.
  • the first acid is one of sulfuric acid or hydrochloric acid.
  • the specific steps for preparing the aluminum hydroxide are: mixing aluminum slag and sodium hydroxide, reacting, and separating solid and liquid to obtain a metaaluminic acid solution; adding sulfuric acid to the metaaluminic acid solution , ultrasonic treatment, and solid-liquid separation to obtain aluminum hydroxide with a particle size of 13-25 ⁇ m.
  • Ultrasonic treatment can prepare aluminum hydroxide with smaller particle size.
  • the aluminum hydroxide is aluminum hydroxide hydrate.
  • it also includes washing the aluminum hydroxide with pure water for 2-3 times, drying at 60-80° C. for 6-8 hours, grinding, and sieving to obtain.
  • the solid-to-liquid ratio of the aluminum slag powder and sodium hydroxide is 1:(3-5) (g:mL).
  • the mass concentration of the sodium hydroxide is 15-30%.
  • reaction temperature is 60-80° C.
  • reaction time is 30-60 minutes.
  • the reaction temperature after adding sulfuric acid to the metaaluminic acid solution is 60-85°C
  • the stirring rate of the reaction is 150-300rpm
  • the addition rate of sulfuric acid is 0.5-2mL/min
  • the power of ultrasonic treatment is 200- 400W
  • the pH at the end of the reaction is 4.5-6.0.
  • the pH adjustment by adding alkali is to adjust the pH to 5.0-5.5.
  • the alkali is one of sodium hydroxide and potassium hydroxide.
  • the amount of aluminum hydroxide added is 0.6-0.99 times the theoretical amount required for the fluorine reaction in the fluorine-containing purification liquid.
  • the aluminum hydroxide that is not enough to react with fluorine is added for the first time in order to ensure the purity of the sodium hexafluoroaluminate generated.
  • the temperature of the precipitation reaction is 30-60° C.
  • the time of the precipitation reaction is 30-50 minutes.
  • the acid is one of sulfuric acid and hydrochloric acid.
  • the acid is sulfuric acid; the mass concentration of the sulfuric acid is 10-30%.
  • the said adding acid to adjust the pH is to adjust the pH to 4.0-5.5.
  • the amount of aluminum hydroxide added is 1.5 to 2.5 times the theoretical amount required for the fluorine reaction in the liquid after defluorination. Adding excessive aluminum hydroxide for the second time is to ensure that the fluorine in the liquid after defluorination can be removed to the minimum.
  • the temperature of the precipitation reaction is 30-60° C.
  • the time of the precipitation reaction is 30-50 minutes.
  • step (3) it also includes returning the filter residue to step (2) until the aluminum hydroxide in the filter residue is converted into sodium hexafluoroaluminate.
  • the filter residue is a mixture of hydrated aluminum hydroxide and sodium hexafluoroaluminate.
  • the present invention also provides the application of the sodium hexafluoroaluminate prepared in the step (2) in electrolytic aluminum.
  • the defluorination recovery process of the present invention after the waste lithium battery is oxidized and leached with acid and oxidant, aluminum hydroxide is used to defluoride twice, and the addition of aluminum hydroxide with ultra-fine particle size is controlled during the first defluorination process. amount, so that the hydrated aluminum hydroxide is completely converted into sodium hexafluoroaluminate, the purity is as high as 98%, and then the second defluorination is carried out, and the fluorine can be removed to below 15mg/L. After entering the wastewater workshop, there is no need to remove fluorine again, and the recovery rate of fluorine is as high as 99%.
  • the aluminum slag obtained after dismantling and crushing the lithium battery is added to the sodium hydroxide solution for reaction, and then filtered to obtain the sodium metaaluminate solution, and the hydrated aluminum hydroxide with a particle size of 13-25 ⁇ m is synthesized by adding sulfuric acid assisted by ultrasound for use in Fluoride removal not only has a good effect of removing fluoride, but also greatly reduces the cost of removing fluoride.
  • the nickel-cobalt-manganese-lithium solution is defluorinated in the previous stage, it prevents fluorine from entering the nickel-cobalt-manganese solution during extraction, thereby improving the quality of the product.
  • the present invention uses incomplete defluorination to control the purity of sodium hexafluoroaluminate.
  • the fluorine-containing purification solution first undergoes incomplete defluorination, and by controlling the addition of hydrated aluminum hydroxide, the hydrated aluminum hydroxide is completely converted Sodium hexafluoroaluminate, after washing and drying, the purity of sodium hexafluoroaluminate is as high as 98%. It can be used as a cosolvent in the electrolytic aluminum industry, which not only recovers fluorine, but also brings great economic benefits.
  • Fig. 1 is the flowchart of the method for removing fluorine in the waste lithium battery of the embodiment 1 of the present invention.
  • Pretreatment disassemble, crush, sort and sieve the waste lithium battery after discharge to obtain battery powder and aluminum slag;
  • composition content of the fluorine-containing purification liquid of the present embodiment is as shown in table 1:
  • composition content of the liquid after a defluoridation of the present embodiment is as shown in table 2:
  • composition content of the liquid after the secondary defluoridation of the present embodiment is as shown in table 3:
  • Fig. 1 is the flow chart of the method for removing fluorine in the waste lithium battery of the embodiment of the present invention 1, can obtain from Fig. 1, after dismantling, crushing, sorting and sieving after the waste lithium battery is firstly discharged, obtain battery powder and
  • Aluminum slag use aluminum slag to make aluminum hydroxide to defluoride the leaching solution after oxidative acid leaching twice to obtain nickel cobalt manganese sulfate solution.
  • Pretreatment disassemble, crush, sort and sieve the waste lithium battery after discharge to obtain battery powder and aluminum slag;
  • composition content of the fluorine-containing purification liquid of the present embodiment is as shown in table 4:
  • composition content of the liquid after a defluoridation of the present embodiment is as shown in table 5:
  • composition content of the liquid after the secondary defluorination of the present embodiment is as shown in Table 6:
  • Pretreatment disassemble, crush, sort and sieve the waste lithium battery after discharge to obtain battery powder and aluminum slag;
  • composition content of the fluorine-containing purification liquid of the present embodiment is as shown in table 7:
  • composition content of the liquid after a defluoridation of the present embodiment is as shown in Table 8:
  • composition content of the liquid after the secondary defluoridation of the present embodiment is as shown in Table 9:
  • Pretreatment disassemble, crush, sort and sieve the waste lithium battery after discharge to obtain battery powder and aluminum slag;
  • the component content of the fluorine-containing purification liquid of this comparative example is as shown in table 10:
  • composition content of the liquid after the primary defluoridation of this comparative example is as shown in table 11:
  • composition content of the liquid after the secondary defluoridation of this comparative example is as shown in table 12:
  • the method for removing fluorine in the waste lithium battery of this comparative example comprises the following specific steps:
  • Pretreatment disassemble, crush, sort and sieve the waste lithium battery after discharge to obtain battery powder and aluminum slag;
  • the component content of the fluorine-containing purification liquid of this comparative example is as shown in table 13:
  • composition content of the liquid after the primary defluoridation of this comparative example is as shown in table 14:
  • composition content of the liquid after the secondary defluoridation of this comparative example is as shown in table 15:
  • step (4) hydrated aluminum hydroxide of twice the theoretical amount required for the reaction with fluorine is added to the fluorine-containing purification solution, stirred and reacted at 60°C for 50 minutes, and 30% Sulfuric acid maintains the pH of the solution at 4.0. After the reaction, filter to obtain the fluorine-removing slag and the first-time fluoride-removing solution. The purity reaches 93%, and the nickel-cobalt-manganese-lithium content is 0.17%.
  • Table 16 shows the content and purity data of fluorine, nickel, cobalt, manganese and lithium in the slag obtained by incomplete defluorination in Example 1-3 and Comparative Example 1-2. The specific data are tested by fluorine ion selective electrode and ICP-AES equipment get.
  • the slag obtained by incomplete defluorination in the example has a high fluorine content, and the purity of the produced sodium hexafluoroaluminate is as high as 98%, and the content of nickel, cobalt, manganese, and lithium is lower than 0.2%, which is obviously better than that of the comparative example.
  • Table 17 shows the fluorine concentration and fluorine removal rate data in the leachate after deep defluorination in Example 1-3 and Comparative Example 1-2, and the specific data are obtained from the test of fluoride ion selective electrode equipment.
  • Comparative example 1 0.032 95% Comparative example 2 0.057 93%
  • Table 18 shows the content and purity data of fluorine, nickel, cobalt, manganese and lithium in the slag obtained by incomplete defluorination in Example 1-3 and Comparative Example 1-2. The specific data are tested by fluorine ion selective electrode and ICP-AES equipment get.
  • Table 19 shows the data of fluorine concentration and fluorine removal rate in the leachate after deep defluorination in Example 1-3 and Comparative Example 1-2, and the specific data were obtained by testing with fluoride ion selective electrode equipment.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Mechanical Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Secondary Cells (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention concerne le domaine technique du traitement des batteries au lithium-ion, et divulgue un procédé d'élimination du fluor de batteries au lithium-ion. Le procédé consiste à : ajouter un agent oxydant et un premier acide à la poudre de batterie au lithium résiduaire pour effectuer une oxydation et une lixiviation acide ainsi qu'une séparation solide-liquide en vue d'obtenir un liquide de purification contenant du fluor ; ajouter de l'hydroxyde d'aluminium au liquide de purification contenant du fluor pour effectuer une réaction de précipitation, ajouter un acide pour ajuster le pH et effectuer une séparation solide-liquide pour obtenir un liquide défluoré et de l'hexafluoroaluminate de sodium ; ajouter de l'hydroxyde d'aluminium au liquide défluoré pour effectuer une réaction de précipitation secondaire, ajouter un acide pour ajuster le pH, effectuer une séparation solide-liquide et collecter la phase liquide pour l'extraction et l'obtention d'une solution de sulfate de nickel-cobalt-manganèse. Dans la présente invention, après l'oxydation et la lixiviation de batteries au lithium-ion à l'aide d'un acide, de l'hydroxyde d'aluminium est ensuite utilisé pour effectuer un traitement d'élimination du fluor à deux reprises. Dans le traitement d'élimination de fluor primaire, par régulation de la quantité d'ajout d'hydroxyde d'aluminium, l'hydroxyde d'aluminium est complètement converti en hexafluoroaluminate de sodium, et la pureté atteint 98 % ; puis un traitement d'élimination de fluor secondaire est effectué, le fluor peut être éliminé à une valeur inférieure à 15 mg/L, et le taux de récupération de fluor atteint 99 %.
PCT/CN2022/090071 2021-09-30 2022-04-28 Procédé d'élimination du fluor dans des batteries au lithium-ion WO2023050805A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202111162084.5 2021-09-30
CN202111162084.5A CN113943864A (zh) 2021-09-30 2021-09-30 一种废旧锂电池中除氟的方法

Publications (1)

Publication Number Publication Date
WO2023050805A1 true WO2023050805A1 (fr) 2023-04-06

Family

ID=79329632

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2022/090071 WO2023050805A1 (fr) 2021-09-30 2022-04-28 Procédé d'élimination du fluor dans des batteries au lithium-ion

Country Status (2)

Country Link
CN (1) CN113943864A (fr)
WO (1) WO2023050805A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113943864A (zh) * 2021-09-30 2022-01-18 广东邦普循环科技有限公司 一种废旧锂电池中除氟的方法
CN117223150A (zh) * 2023-07-19 2023-12-12 广东邦普循环科技有限公司 一种三元电池粉浸出方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2014156649A (ja) * 2013-02-18 2014-08-28 Jx Nippon Mining & Metals Corp 廃正極材及び廃電池からの金属回収方法
CN111139367A (zh) * 2019-12-30 2020-05-12 江西赣锋循环科技有限公司 一种废旧电池回收LiCl溶液深度除氟的方法
CN112079371A (zh) * 2020-08-24 2020-12-15 湖南邦普循环科技有限公司 一种镍钴锰溶液中除氟的回收方法
CN113943864A (zh) * 2021-09-30 2022-01-18 广东邦普循环科技有限公司 一种废旧锂电池中除氟的方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105506290B (zh) * 2015-11-30 2018-01-09 湖南邦普循环科技有限公司 一种铁铝渣综合利用的方法
CN110669933B (zh) * 2019-10-21 2021-04-27 金驰能源材料有限公司 一种去除镍钴锰溶液中氟的方法
CN112126783B (zh) * 2020-08-25 2022-06-14 湖南邦普循环科技有限公司 一种镍钴锰溶液中铁铝资源化的回收方法
CN112813270A (zh) * 2020-12-30 2021-05-18 江苏海普功能材料有限公司 废旧镍钴锰三元锂电池正极材料回收方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2014156649A (ja) * 2013-02-18 2014-08-28 Jx Nippon Mining & Metals Corp 廃正極材及び廃電池からの金属回収方法
CN111139367A (zh) * 2019-12-30 2020-05-12 江西赣锋循环科技有限公司 一种废旧电池回收LiCl溶液深度除氟的方法
CN112079371A (zh) * 2020-08-24 2020-12-15 湖南邦普循环科技有限公司 一种镍钴锰溶液中除氟的回收方法
CN113943864A (zh) * 2021-09-30 2022-01-18 广东邦普循环科技有限公司 一种废旧锂电池中除氟的方法

Also Published As

Publication number Publication date
CN113943864A (zh) 2022-01-18

Similar Documents

Publication Publication Date Title
CN112357899B (zh) 一种废旧磷酸铁锂电池的综合回收利用方法
CN111370800B (zh) 一种废旧磷酸铁锂正极材料的回收方法
WO2023050805A1 (fr) Procédé d'élimination du fluor dans des batteries au lithium-ion
CN110835682B (zh) 废旧锂离子电池正、负极活性材料协同处理的方法
CN107267759A (zh) 一种锂离子电池正极材料的综合回收方法
WO2022041845A1 (fr) Procédé de récupération pour éliminer le fluor d'une solution de nickel-cobalt-manganèse
CN109022793B (zh) 一种从含钴镍锰中至少一种的正极材料废粉中选择性浸出锂的方法
WO2023173773A1 (fr) Procédé de recyclage de batterie au lithium-ion et son application
CN114214517B (zh) 去除锂电池正极浸出液中氟的方法
WO2023050804A1 (fr) Procédé d'élimination efficace du fluor d'une batterie au lithium usagée
CN114349030B (zh) 一种磷酸铁锂废旧正极片的综合湿法回收利用方法
CN111471864A (zh) 一种废旧锂离子电池浸出液中回收铜、铝、铁的方法
WO2022267419A1 (fr) Procédé de récupération de cuivre élémentaire dans une poudre de batterie au lithium-ion usagée et application
CN103805788A (zh) 一种从铜镍渣中回收铜钴镍的方法
CN113912033A (zh) 一种前置提锂的废旧磷酸铁锂电池正负极混粉的回收方法
CN113802017A (zh) 一种萃取法分离回收废旧磷酸铁锂电池正极材料酸浸出液中铝的方法
CN108199106B (zh) 一种镍钴锰三元前驱体生产过程废料的回收工艺
CN112701372B (zh) 一种三元电池废料中除去单质铜的方法及其应用
CN114180546A (zh) 一种含钛磷酸铁锂废料制备无水磷酸铁的方法
WO2023193517A1 (fr) Procédé de traitement d'un alliage cuivre-cobalt de batterie au lithium usagée et son utilisation
WO2024045529A1 (fr) Procédé de recyclage complet de suspension de déchets d'électrode positive ternaire
CN116411182A (zh) 一种从锂电池中选择性回收锂的方法
CN115784188A (zh) 回收制备电池级磷酸铁的方法
CN116632395A (zh) 一种废旧电池中有价金属的回收方法
WO2023093163A1 (fr) Procédé de récupération d'une plaque d'électrode positive de batterie au 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: 22874203

Country of ref document: EP

Kind code of ref document: A1