WO2024250140A1 - Utilisation de ferrocyanure de lithium, anolyte, et procédé d'extraction de lithium à partir de saumure de lac salé au moyen d'une désintercalation électrique - Google Patents

Utilisation de ferrocyanure de lithium, anolyte, et procédé d'extraction de lithium à partir de saumure de lac salé au moyen d'une désintercalation électrique Download PDF

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Publication number
WO2024250140A1
WO2024250140A1 PCT/CN2023/098284 CN2023098284W WO2024250140A1 WO 2024250140 A1 WO2024250140 A1 WO 2024250140A1 CN 2023098284 W CN2023098284 W CN 2023098284W WO 2024250140 A1 WO2024250140 A1 WO 2024250140A1
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Prior art keywords
lithium
deintercalation
salt lake
electro
lake brine
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PCT/CN2023/098284
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English (en)
Chinese (zh)
Inventor
李爱霞
谢英豪
余海军
李长东
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Hunan Brunp Recycling Technology Co Ltd
Guangdong Brunp Recycling Technology Co Ltd
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Hunan Brunp Recycling Technology Co Ltd
Guangdong Brunp Recycling Technology Co Ltd
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Priority to PCT/CN2023/098284 priority Critical patent/WO2024250140A1/fr
Priority to CN202380009314.5A priority patent/CN116964233B/zh
Publication of WO2024250140A1 publication Critical patent/WO2024250140A1/fr
Anticipated expiration legal-status Critical
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    • 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 extraction and recovery methods of lithium resources from salt lake brine include electrodialysis, evaporation crystallization, solvent extraction, precipitation, ion exchange and adsorption.
  • the adsorption method has low cost and high efficiency.
  • acid washing is required to produce secondary waste during the exchange and adsorption process, and the permeability and solubility of the adsorbent are poor, which seriously limits its industrial application.
  • the solvent extraction method has high yield, simple operation, and is easy to scale up industrially, but this method uses a large amount of organic solvents, which can easily lead to environmental pollution and equipment corrosion.
  • Traditional lithium extraction methods have the disadvantages of high cost, high energy consumption, and low separation efficiency.
  • Electrodeintercalation is a new research direction for lithium extraction from salt lakes and is a green and efficient lithium extraction technology from salt lakes.
  • Electrochemical lithium extraction is developed based on the working principle of lithium iron phosphate batteries.
  • the specific application idea is: using the reverse working principle of aqueous lithium battery deintercalation, in essence, the lithium ions in the solution are intercalated into the cathode material for subsequent processing, using the lithium battery positive electrode material with a "memory effect" on lithium ions as the electrode material, salt lake brine as the cathode electrolyte, and a magnesium-free supporting electrolyte as the anode electrolyte, thus forming an electrochemical deintercalation system of "lithium-rich adsorption material
  • the cathode obtains electrons to undergo a reduction reaction, so that the lithium ions in the salt lake brine are embedded in the cathode material, thereby achieving separation, and then through subsequent processing and separation operations, the effect of efficient lithium extraction is finally achieved.
  • CN102382984B discloses a method for electro-deintercalation and lithium extraction using a "rocking chair" electrode system (LiFePO 4 /FePO 4 ): the electrolytic cell is divided into two compartments by an anion selective exchange membrane: the LiFePO 4 electrode is placed in a recovery solution (0.5 mol/L NaCl), and the FePO 4 is placed in a raw material solution (lithium-containing brine). Under the electric field, the LiFePO 4 anode undergoes an oxidation (lithium removal) reaction, and the cathode undergoes a reduction (lithium insertion) reaction. In this process, the anions (Cl - ) in the raw material solution will migrate across the anion exchange membrane in the middle to the recovery solution.
  • the cathode will embed a lithium ion while the anode releases a lithium ion.
  • the cathode lithium embedding process is affected by the viscosity of the brine and the lithium ion concentration in the solution, resulting in a slower cathode lithium embedding process than the anode lithium de-lithiation process, leading to a mismatch between the de-lithiation and embedding capacities of the cathode and cathode.
  • the difference in the rates of lithium de-intercalation and lithium embedding between the cathode and cathode increases.
  • CN115818801A discloses a method for using a Pb- FePO4 system for electric deintercalation and lithium extraction, using FePO4 as the cathode and Pb as the anode to adsorb lithium in brine, and then replacing the brine to remove lithium ions, which can make the capacity of lithium deintercalation and lithium insertion of the anode and cathode more matched, but the lithium extraction process needs to be divided into two steps of lithium insertion and lithium deintercalation, which complicates the lithium extraction process and affects the efficiency of lithium extraction.
  • the purpose of the present disclosure includes providing the use of lithium ferrocyanide in preparing an anolyte for lithium electrolysis and deintercalation in salt lake brine.
  • the purpose of the present disclosure includes providing the use of lithium ferrocyanide in preparing an anolyte for reducing the difference in lithium deintercalation rates between the cathode and the anode in the electro-deintercalation of lithium from lake brine.
  • the purpose of the present disclosure also includes providing an anolyte for lithium electrolysis and extraction from salt lake brine.
  • the purpose of the present disclosure also includes providing a method for extracting lithium by electro-deintercalation of salt lake brine.
  • the purpose of the present disclosure also includes providing a method for recovering salt lake brine.
  • the present disclosure provides the use of lithium ferrocyanide in preparing an anolyte for lithium electro-deintercalation and extraction from salt lake brine.
  • the lithium ferrocyanate is added into the anode chamber of a salt lake brine electro-deintercalation lithium extraction system.
  • the concentration of the lithium ferrocyanate in the anolyte is 0.05-1 mol/L.
  • the concentration of the lithium ferrocyanate in the anolyte is 0.2-0.5 mol/L.
  • the anolyte further comprises a supporting electrolyte.
  • the supporting electrolyte includes lithium chloride.
  • the concentration of lithium chloride in the anolyte is 40-60 mmol/L.
  • the present disclosure provides an anolyte for lithium electrolysis and extraction from salt lake brine, the components of which include lithium ferrocyanate.
  • the concentration of the lithium ferrocyanate in the anolyte is 0.05-1 mol/L.
  • the components further include a supporting electrolyte.
  • the supporting electrolyte includes lithium chloride.
  • the concentration of lithium chloride in the anolyte is 40-60 mmol/L.
  • the present disclosure provides a method for extracting lithium by electro-deintercalation of salt lake brine, comprising:
  • the salt lake brine is subjected to electro-deintercalation and lithium extraction by using a salt lake brine electro-deintercalation and lithium extraction device, the salt lake brine electro-deintercalation and lithium extraction device comprising an electrolytic cell, an anion exchange membrane, an anode and a cathode, the anion exchange membrane is placed in the electrolytic cell to vertically divide the electrolytic cell into a cathode chamber and an anode chamber, the anode is placed in the anode chamber, and the cathode is placed in the cathode chamber;
  • a voltage is applied to the cathode and the anode to perform electro-deintercalation and lithium extraction.
  • the anode chamber is filled with the anode electrolyte for electro-deintercalation and lithium extraction of salt lake brine as described in any of the above embodiments.
  • the lithium ferrocyanate is added to the anode chamber before or during the process of lithium electro-extraction.
  • the voltage applied to the cathode and the anode is 0.4-0.8V.
  • the time for the lithium electrolysis is 2-6 hours.
  • the positions of the cathode and the anode are swapped, a voltage is applied, and the above steps are repeated until lithium is enriched from the cathode chamber to the anode chamber to form a lithium-rich solution.
  • the concentration of lithium in the lithium-rich solution is 3.5-4.1 g/L.
  • the salt lake brine includes lithium-containing brine.
  • the anode includes at least one of LiFePO 4 , LiMn 2 O 4 , LiNi 1/3 Co 1/3 Mn 1/3 O 2 , and Li 7 Ti 5 O 12 .
  • the present disclosure provides a method for resource recovery of salt lake brine, which includes the method for electro-deintercalation and extraction of lithium from salt lake brine as described in any of the above-mentioned embodiments.
  • the beneficial effects of the present invention include:
  • the lithium de-lithiation rate of LiFePO 4 is significantly faster than the lithium insertion rate of FePO 4.
  • the present disclosure provides a new application of lithium ferrocyanate, by adding lithium ferrocyanate Li 4 Fe(CN) 6 as an anode electrolyte into the anode chamber.
  • the Li 4 Fe(CN) 6 in the anode chamber undergoes an oxidation reaction when powered on, Fe(CN 6 ) 4- ⁇ Fe(CN 6 ) 3- , resulting in a reduction in the amount of lithium ions released from the anode, thereby ensuring that the cathode FePO 4 can fully insert lithium.
  • FIG1 is a diagram showing the working principle of the method for extracting lithium from salt lake brine by electro-deintercalation provided in the present invention.
  • any values of the ranges disclosed in this disclosure are not limited to the precise ranges or values, and these ranges or values should be understood to include values close to these ranges or values.
  • the endpoint values of each range, the endpoint values of each range and the individual point values, and the individual point values can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.
  • the present disclosure provides a new application of lithium ferrocyanide. Specifically, the present disclosure provides the application of lithium ferrocyanide in preparing an anolyte for lithium electro-deintercalation and extraction from salt lake brine.
  • lithium ferrocyanate is purchased from the market, and the manufacturer is Hunan Hanrun Materials Development Co., Ltd.
  • the present disclosure found that when lithium ferrocyanate is added to the anode chamber as the anode electrolyte in the electro-deintercalation and extraction of lithium from lake brine, it can undergo an oxidation reaction during the electro-deintercalation process to reduce the amount of lithium ions released from the anode, thereby reducing the difference in lithium deintercalation rates between the cathode and the anode, and at the same time can also reduce the capacity difference between lithium deintercalation and lithium insertion.
  • lithium ferrocyanide is dissolved in the solution of the anode chamber to form a lithium ferrocyanide solution.
  • concentration of lithium ferrocyanide in the anolyte is 0.05-1 mol/L, and optionally, the concentration of lithium ferrocyanide in the anolyte is 0.2-0.5 mol/L.
  • the concentration of lithium ferrocyanide in the anolyte can be, for example, 0.05 mol/L, 0.1 mol/L, 0.2 mol/L, 0.3 mol/L, 0.4 mol/L, 0.5 mol/L, 0.6 mol/L, 0.7 mol/L, 0.8 mol/L, 0.9 mol/L, 1 mol/L, any one of them or a range value between any two of them.
  • the present application also provides an anolyte for extracting lithium from salt lake brine by electro-deintercalation, wherein the component includes lithium ferrocyanate, and the concentration of lithium ferrocyanate in the anolyte is 0.05-1 mol/L.
  • the concentration of lithium ferrocyanate in the anolyte can be, for example, 0.05 mol/L, 0.1 mol/L, 0.2 mol/L, 0.3 mol/L, 0.4 mol/L, 0.5 Any one of 0.6 mol/L, 0.7 mol/L, 0.8 mol/L, 0.9 mol/L, 1 mol/L or a range value between any two of them.
  • the components further include a supporting electrolyte, the supporting electrolyte includes lithium chloride, and the concentration of lithium chloride in the anolyte is 40-60 mmol/L.
  • the present disclosure also provides a method for extracting lithium by electro-deintercalation of salt lake brine, which comprises the following steps:
  • the anode and cathode are selected to form an electrode system, and the electrolytic cell is vertically divided into a cathode chamber and an anode chamber by an anion exchange membrane.
  • the present disclosure can be applied to a variety of electrode systems, including but not limited to LiFePO 4 /FePO 4 , LiMn 2 O 4 /Li 1-x Mn 2 O 4 , LiNi 1/3 Co 1/3 Mn 1/3 O 2 /Li 1-x Ni 1/3 Co 1/3 Mn 1/3 O 2 , Li 7 Ti 5 O 12 /Li 7-x Ti 5 O 12 , etc.
  • the cathode includes at least one of FePO 4 , Li 1-x Mn 2 O 4 , Li 1-x Ni 1/3 Co 1/3 Mn 1/3 O 2 and Li 7-x Ti 5 O 12 , wherein x represents a lithium-deficient state.
  • the salt lake brine may be any lithium-containing salt lake brine, mainly targeting high magnesium-lithium ratio brine.
  • Salt lake brine includes but is not limited to one or more of sulfate brine, chloride brine and carbonate brine.
  • the composition of the salt lake brine includes 0.21-0.47 g/L Li + , 69.3 g/L Na + , 111.20 g/L Mg 2+ , 6.43 g/L K + , 2.99 g/L Ca 2+ , 8.24 g/L SO 4 2- .
  • the supporting electrolyte includes lithium chloride, and the concentration of lithium chloride is 40-60 mmol/L.
  • a voltage is applied to the cathode and the anode for lithium electrolysis.
  • the applied voltage is 0.4-0.8V, and the time for lithium electrolysis is 2-6h.
  • the applied voltage may be, for example, any one of 0.4 V, 0.5 V, 0.6 V, 0.7 V, 0.8 V, or a range between any two thereof.
  • the time for the electro-deintercalation of lithium is any one of 2 h, 3 h, 4 h, 5 h, 6 h, or a range between any two thereof.
  • the Li4Fe (CN) 6 in the anode chamber undergoes an oxidation reaction when powered on, Fe( CN6 ) 4- ⁇ Fe( CN6 ) 3- , resulting in a reduction in the amount of lithium ions released from the anode, ensuring that the cathode FePO4 can fully embed lithium, fully ensuring the adsorption capacity of the electrode, reducing the capacity mismatch problem, and improving the lithium recovery rate.
  • the present invention discloses a method for recovering resources of salt lake brine, which comprises the above-mentioned method for extracting lithium by electro-deintercalation of salt lake brine.
  • This embodiment provides a method for extracting lithium by electro-deintercalation of salt lake brine, which comprises the following steps:
  • the concentration of Li 4 Fe(CN) 6 in the anolyte is 0.3 mol/L, and the concentration of lithium chloride is 50 mmol/L.
  • This embodiment provides a method for extracting lithium by electro-deintercalation of salt lake brine, which comprises the following steps:
  • LiFePO 4 is used as the anode
  • FePO 4 after delithiation of LiFePO 4 is used as the cathode.
  • the anode and cathode are separated into a cathode chamber and an anode chamber by a monovalent selective anion exchange membrane.
  • the cathode chamber is injected with salt lake brine to be extracted with lithium, and Li 4 Fe(CN) 6 and supporting electrolyte (lithium chloride) are added to the anode chamber.
  • Li 4 Fe(CN) 6 solution and lithium chloride are used together as the anode electrolyte.
  • composition of brine is: 0.47g/L Li + , 69.3g/L Na + , 111.20g/L Mg 2+ , 6.43g/L K + , 2.99g/L Ca 2+ , 8.24 g/L SO 4 2- .
  • the concentration of Li 4 Fe(CN) 6 in the anolyte is 0.5 mol/L, and the concentration of lithium chloride is 50 mmol/L.
  • This embodiment provides a method for extracting lithium by electro-deintercalation of salt lake brine, which comprises the following steps:
  • the cathode chamber is injected with salt lake brine to be extracted with lithium, and Li 4 Fe(CN) 6 and supporting electrolyte (lithium chloride) are added to the anode chamber.
  • Li 4 Fe(CN) 6 solution and lithium chloride are used together as the anode electrolyte.
  • composition of the brine is: 0.47g/L Li + , 69.3g/L Na + , 111.20g/L Mg 2+ , 6.43g/L K + , 2.99g/L Ca 2+ , and 8.24g/L SO 4 2- .
  • the concentration of Li 4 Fe(CN) 6 in the anolyte is 0.05 mol/L, and the concentration of lithium chloride is 50 mmol/L.
  • Embodiment 4 is a diagrammatic representation of Embodiment 4:
  • This embodiment provides a method for extracting lithium by electro-deintercalation of salt lake brine, which comprises the following steps:
  • LiFePO 4 is used as the anode
  • FePO 4 after delithiation of LiFePO 4 is used as the cathode.
  • the anode and cathode are separated into a cathode chamber and an anode chamber by a monovalent selective anion exchange membrane.
  • the cathode chamber is injected with salt lake brine from which lithium is to be extracted, and the anode chamber is added with lithium chloride solution as the anode electrolyte.
  • composition of the brine is: 0.47g/L Li + , 69.3g/L Na + , 111.20g/L Mg 2+ , 6.43g/L K + , 2.99g/L Ca 2+ , and 8.24g/L SO 4 2- .
  • the concentration of lithium chloride in the anolyte was 50 mmol/L.
  • step (3) the voltage applied for electrical deintercalation in step (3) is 0.4 V, and the other steps are the same as those in embodiment 1.
  • step (3) the voltage applied for electrical deintercalation in step (3) is 0.8 V, and the other steps are the same as those in embodiment 1.
  • step (1) LiMn 2 O 4 is used as the anode and Li 1-x Mn 2 O 4 is used as the cathode.
  • step (1) LiMn 2 O 4 is used as the anode and Li 1-x Mn 2 O 4 is used as the cathode.
  • step (1) LiMn 2 O 4 is used as the anode and Li 1-x Mn 2 O 4 is used as the cathode.
  • step (1) LiMn 2 O 4 is used as the anode and Li 1-x Mn 2 O 4 is used as the cathode.
  • step (1) LiMn 2 O 4 is used as the anode and Li 1-x Mn 2 O 4 is used as the cathode.
  • composition of the brine in step (2) is: 0.47 g/L Li + , 69.3 g/L Na + , 111.20 g/L Mg 2+ , 6.43 g/L K + , 2.99 g/L Ca 2+ , 8.24 g/L SO 4 2- .
  • This comparative example is substantially the same as Example 1, except that in step (3) of this comparative example, Li 4 Fe(CN) 6 is not added into the anode chamber, but only lithium chloride solution (the concentration of lithium chloride is 50 mmol/L) is added.
  • the other steps are the same as Example 1.
  • This comparative example is substantially the same as Example 1, except that in step (3) of this comparative example, only Li 4 Fe(CN) 6 is added into the anode chamber, wherein the concentration of Li 4 Fe(CN) 6 is 0.3 mol/L, and no lithium chloride solution is added.
  • the other steps are the same as Example 1.
  • This comparative example is substantially the same as Example 1, except that in step (3) of this comparative example, the concentration of Li 4 Fe(CN) 6 added into the anode chamber is 0.01 mol/L.
  • This comparative example is substantially the same as Example 1, except that in step (3) of this comparative example, the concentration of Li 4 Fe(CN) 6 added into the anode chamber is 1.5 mol/L.
  • This comparative example is basically the same as Example 1, except that in step (3) of this comparative example, the anode chamber Li 4 Fe(CN) 6 was added to replace potassium sulfate.
  • the lithium recovery rate is calculated as (C 0 -C e )/C 0 ⁇ 100%, where C 0 is the initial lithium ion concentration of the brine, measured in g/L; and Ce is the lithium ion concentration of the brine after electrolysis, measured in g/L.
  • the concentration of the obtained lithium-rich solution is calculated by direct detection.
  • Example 1 Examples 7-13 and Comparative Examples 3-4 that when the concentration of Li 4 Fe(CN) 6 is controlled at 0.2-0.5 mol/L, it is more conducive to increasing the adsorption capacity of the electrode.
  • Example 1 and Comparative Example 1 it can be seen from Example 1 and Comparative Example 1 that adding Li 4 Fe(CN) 6 to the recovery liquid can significantly increase the adsorption capacity of the electrode, thereby increasing the concentration of lithium in the recovery liquid and improving the lithium recovery rate.
  • adding Li 4 Fe(CN) 6 to the anode can ensure the embedding amount of the cathode ion sieve, thereby making the capacity of the anode and cathode for lithium deintercalation more matched and improving the lithium extraction efficiency.
  • Example 1 and Comparative Example 2 it can be seen from Example 1 and Comparative Example 2 that when only Li 4 Fe(CN) 6 is used as the anolyte, the ionization equilibrium constant of Li 4 Fe(CN) 6 alone is not high, resulting in a lithium extraction index that is significantly lower than that in Example 1.
  • using Li 4 Fe(CN) 6 and a supporting electrolyte together as the anolyte can improve the conductivity of the solution, thereby increasing the lithium extraction efficiency.
  • Example 1 Comparative Example 7 that when other reagents are selected to replace Li 4 Fe(CN) 6 , the effect is significantly worse than that of Example 1.
  • the LiFePO 4 -FePO 4 electrode system is used for lithium extraction reaction, and the lithium removal rate of LiFePO 4 is significantly faster than the lithium insertion rate of FePO 4.
  • the present disclosure provides a new application of lithium ferrocyanate, by adding lithium ferrocyanate Li 4 Fe(CN) 6 as an anode electrolyte into the anode chamber, with the increase of the electrical deinsertion time, the Li 4 Fe(CN) 6 in the anode chamber undergoes an oxidation reaction under power-on, Fe(CN 6 ) 4- ⁇ Fe(CN 6 ) 3- , resulting in a reduction in the amount of lithium ions released from the anode, ensuring that the cathode FePO 4 can fully embed lithium, fully ensuring the adsorption capacity of the electrode, reducing the capacity mismatch problem, and improving the lithium recovery rate.
  • the lithium de-lithiation rate of LiFePO 4 is significantly faster than the lithium insertion rate of FePO 4.

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  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
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  • Electrolytic Production Of Metals (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)

Abstract

La présente divulgation relève du domaine technique de l'extraction de lithium à partir de saumure, et concerne en particulier l'utilisation de ferrocyanure de lithium, un anolyte et un procédé d'extraction de lithium à partir de saumure de lac salé au moyen d'une désintercalation électrique. Le procédé comprend l'extraction de lithium à partir de saumure de lac salé au moyen d'une désintercalation électrique à l'aide d'un dispositif d'extraction de lithium par désintercalation électrique de saumure de lac salé. Le dispositif d'extraction de lithium par désintercalation électrique de saumure de lac salé comprend un bain électrolytique, une membrane échangeuse d'anions, une anode et une cathode, la membrane échangeuse d'anions étant disposée dans le bain électrolytique pour diviser verticalement le bain électrolytique en une chambre de cathode et une chambre d'anode ; l'anode étant disposée dans la chambre d'anode ; et la cathode étant disposée dans la chambre de cathode. Une tension est appliquée à la cathode et à l'anode, de manière à effectuer une extraction de lithium au moyen d'une désintercalation électrique, et un anolyte est ajouté dans la chambre d'anode pendant le processus d'extraction de lithium au moyen d'une désintercalation électrique. Dans la présente divulgation, en ajoutant du ferrocyanure de lithium dans une chambre d'anode en tant qu'anolyte, la quantité d'intercalation d'un tamis d'ions de cathode peut être garantie, de telle sorte que la capacité de désintercalation de lithium de la cathode et de l'anode est plus adaptée, et l'efficacité d'extraction de lithium est améliorée.
PCT/CN2023/098284 2023-06-05 2023-06-05 Utilisation de ferrocyanure de lithium, anolyte, et procédé d'extraction de lithium à partir de saumure de lac salé au moyen d'une désintercalation électrique Ceased WO2024250140A1 (fr)

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Application Number Priority Date Filing Date Title
PCT/CN2023/098284 WO2024250140A1 (fr) 2023-06-05 2023-06-05 Utilisation de ferrocyanure de lithium, anolyte, et procédé d'extraction de lithium à partir de saumure de lac salé au moyen d'une désintercalation électrique
CN202380009314.5A CN116964233B (zh) 2023-06-05 2023-06-05 亚铁氰酸锂的应用、阳极电解液和盐湖卤水电脱嵌提锂方法

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1694979A (zh) * 2002-11-04 2005-11-09 詹森药业有限公司 将亚铁氰化物电化学氧化成铁氰化物的方法
US20130186760A1 (en) * 2010-11-19 2013-07-25 Central South University Method and device for extracting and enriching lithium
CN112996931A (zh) * 2018-10-26 2021-06-18 新加坡国立大学 锂离子电池材料回收方法
US20220246998A1 (en) * 2021-02-02 2022-08-04 Wisconsin Alumni Research Foundation Aqueous energy storage systems with desalination capabilities
CN115818801A (zh) * 2022-12-20 2023-03-21 中南大学 一种从盐湖卤水中提取锂的方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1694979A (zh) * 2002-11-04 2005-11-09 詹森药业有限公司 将亚铁氰化物电化学氧化成铁氰化物的方法
US20130186760A1 (en) * 2010-11-19 2013-07-25 Central South University Method and device for extracting and enriching lithium
CN112996931A (zh) * 2018-10-26 2021-06-18 新加坡国立大学 锂离子电池材料回收方法
US20220246998A1 (en) * 2021-02-02 2022-08-04 Wisconsin Alumni Research Foundation Aqueous energy storage systems with desalination capabilities
CN115818801A (zh) * 2022-12-20 2023-03-21 中南大学 一种从盐湖卤水中提取锂的方法

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