WO2025129485A1 - 一种锂的电化学提取装置及方法 - Google Patents

一种锂的电化学提取装置及方法 Download PDF

Info

Publication number
WO2025129485A1
WO2025129485A1 PCT/CN2023/140140 CN2023140140W WO2025129485A1 WO 2025129485 A1 WO2025129485 A1 WO 2025129485A1 CN 2023140140 W CN2023140140 W CN 2023140140W WO 2025129485 A1 WO2025129485 A1 WO 2025129485A1
Authority
WO
WIPO (PCT)
Prior art keywords
lithium
cathode
anode
chamber
plate
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/CN2023/140140
Other languages
English (en)
French (fr)
Inventor
张添全
阮丁山
蒋银龙
李凤光
李长东
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.)
Hunan Brunp Recycling Technology Co Ltd
Guangdong Brunp Recycling Technology Co Ltd
Original Assignee
Hunan Brunp Recycling Technology Co Ltd
Guangdong Brunp Recycling Technology Co Ltd
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 Hunan Brunp Recycling Technology Co Ltd, Guangdong Brunp Recycling Technology Co Ltd filed Critical Hunan Brunp Recycling Technology Co Ltd
Priority to PCT/CN2023/140140 priority Critical patent/WO2025129485A1/zh
Priority to CN202380012428.5A priority patent/CN118176327A/zh
Publication of WO2025129485A1 publication Critical patent/WO2025129485A1/zh
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

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
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
    • C25C1/02—Electrolytic production, recovery or refining of metals by electrolysis of solutions of light metals
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • C25C7/02—Electrodes; Connections thereof

Definitions

  • the present application relates to the technical field of electrochemical metallurgy, and in particular to a device and method for electrochemical extraction of lithium.
  • Lithium metal and its compounds are widely used in industries such as glass, metallurgy, ceramics, lubricants and refrigerants.
  • industries such as glass, metallurgy, ceramics, lubricants and refrigerants.
  • emerging industries such as electric vehicles, wind power, and nuclear power
  • the demand for lithium resources in social development has gradually increased by leaps and bounds.
  • heat treatment equipment is mainly used in combination with tank reactors and solid-liquid separation equipment.
  • the current electrochemical lithium extraction can only extract single-phase lithium-containing materials, which makes the scope of application small and the extraction efficiency is not high, so the energy consumption is large and it is not conducive to environmental protection.
  • the purpose of the present application is to provide a lithium electrochemical extraction device and method, which can extract lithium from solid phase materials or liquid phase materials containing lithium, and has high efficiency in extracting lithium and environmental protection effects.
  • a lithium electrochemical extraction device comprising:
  • a first circulation tank comprises a first inlet and a first outlet which are connected to each other;
  • a second circulation tank comprises a second inlet and a second outlet which are connected to each other;
  • the stack has an anode chamber and a cathode chamber separated by a diaphragm, the anode chamber is provided with an anode plate, and the cathode chamber is provided with a cathode plate;
  • the first outlet is connected to the inlet of the anode chamber through the circulation pump, and the outlet of the anode chamber is connected to the first inlet
  • the second outlet is connected to the inlet of the cathode chamber through the second circulation pump, and the outlet of the cathode chamber is connected to the second inlet;
  • anode plate is used to transfer the lithium contained in the anode slurry in the anode chamber from the solid phase to the liquid phase
  • the cathode plate is used to transfer the lithium contained in the cathode slurry in the cathode chamber from the liquid phase to the solid phase.
  • an anode plate is disposed in the middle of each anode chamber, and a cathode plate is disposed in the middle of each cathode chamber.
  • the anode plate and the cathode plate are in plate shape, and the distance L between the anode plate and the diaphragm and the distance L between the cathode plate and the diaphragm satisfy 0mm ⁇ L ⁇ 80mm.
  • two anode plates are correspondingly disposed on both sides of each anode chamber, and two cathode plates are correspondingly disposed on both sides of each cathode chamber.
  • the anode plate and the cathode plate are porous in shape; the distance between the anode plate and the diaphragm and the distance L between the cathode plate and the diaphragm satisfy 0mm ⁇ L ⁇ 80mm.
  • the anode chambers and cathode chambers are staggered and arranged vertically.
  • the fuel cell stack further includes a liquid distribution pipe, which is disposed at the inlet and outlet of the anode chamber and extends along the length direction of the anode chamber, and the liquid distribution pipe is disposed at the inlet and outlet of the cathode chamber and extends along the length direction of the cathode chamber.
  • a plurality of through holes are evenly distributed on the surface of the liquid distribution tube.
  • the first circulation tank further includes a first feed port and a first discharge port, the first feed port is connected to the first outlet, the first discharge port is connected to the first inlet, or/and the second circulation tank further includes a second feed port and a second discharge port, the second feed port is connected to the second outlet, and the second discharge port is connected to the second inlet.
  • the anode plate is made of graphite, lead, lead alloy, titanium and
  • One of the coated titanium, the coated titanium is one of the following: lead dioxide coated on titanium, titanium manganese alloy coated on titanium, manganese dioxide coated on titanium, iridium or ruthenium oxide coated on titanium, and tin antimony oxide coated on titanium.
  • the cathode plate is made of one of iron, nickel, copper, zinc, aluminum, lead, manganese, stainless steel, iron-nickel alloy, aluminum alloy, zinc alloy, lead alloy, and manganese alloy.
  • the present application provides a method for electrochemical extraction of lithium, using the above-mentioned electrochemical extraction device of lithium, comprising the following steps:
  • the first circulation pump is turned on to transport the anode slurry from the first circulation tank into the anode chamber of the fuel cell stack.
  • the fuel cell stack is connected to a power source to electrolyze the anode slurry so that the lithium in the anode slurry is transferred from the solid phase to the liquid phase.
  • the anode slurry that has completed the electrolysis is discharged from the anode chamber into the first circulation tank.
  • the anode slurry that has completed electrolysis is discharged from the first circulation tank, and a lithium-rich solution is obtained through solid-liquid separation.
  • the solid phase lithium-containing material is a positive electrode material of a recycled lithium-ion battery.
  • the solid phase lithium-containing material is obtained by the following method:
  • the second circulation pump is turned on to transport the cathode slurry from the second circulation tank into the cathode chamber of the stack.
  • the stack is connected to a power source to electrolyze the cathode slurry so that the lithium in the cathode slurry is transferred from the liquid phase to the solid phase.
  • the cathode slurry that has completed the electrolysis is discharged from the cathode chamber into the second circulation tank.
  • the cathode slurry that has completed electrolysis is discharged from the second circulation tank, and then undergoes solid-liquid separation to obtain the solid-phase lithium-containing material.
  • the lithium intercalation and deintercalation material is one of lithium iron phosphate, lithium manganese oxide, and lithium nickel cobalt manganese oxide.
  • the present application provides a lithium electrochemical extraction device and method. Compared with the prior art, Its beneficial effects are:
  • the first outlet of the first circulation tank is connected to the inlet of the anode chamber through the first circulation pump, and the outlet of the anode chamber is connected to the first inlet of the first circulation tank;
  • the second outlet of the second circulation tank is connected to the inlet of the cathode chamber through the second circulation pump, and the outlet of the cathode chamber is connected to the second inlet of the second circulation tank.
  • the first circulation tank is connected to the anode chamber in a circular manner, and the second circulation tank is connected to the cathode chamber in a circular manner, so that cyclic continuous extraction of lithium is realized, the efficiency of lithium extraction is high, resource recovery is achieved, and environmental protection effects are achieved.
  • FIG1 is a schematic diagram of the principle structure of a lithium electrochemical extraction device provided in an embodiment of the present application.
  • FIG2 is a schematic diagram of the first structure of a battery stack of a lithium electrochemical extraction device provided in an embodiment of the present application.
  • FIG3 is a schematic diagram of the second structure of the battery stack of the electrochemical extraction device for lithium provided in an embodiment of the present application.
  • FIG. 4 is a schematic diagram of the cross-sectional structure along the direction A in FIG. 2 .
  • first circulation tank 11. first inlet; 12. first outlet; 13. first feed port; 14. first outlet; 2. first circulation pump; 3. second circulation tank; 31. second inlet; 32. second outlet; 33. second feed port; 34. second outlet; 4. second circulation pump; 5. fuel cell stack; 51. diaphragm; 52. anode chamber; 53. cathode chamber; 54. anode plate; 55. cathode plate; 56. liquid distribution pipe; 561. through hole; X, length direction of anode chamber; Y, height direction of anode chamber.
  • first and second are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated, that is, the features defined as “first” and “second” may explicitly or implicitly include one or more of the features.
  • “multiple” means two or more.
  • the present application provides a lithium electrochemical extraction device, which, in some embodiments, includes a first circulation tank 1, a first circulation pump 2, a second circulation tank 3, a second circulation pump 4, and a stack 5.
  • the first circulation pump 2 circulates the anode slurry between the first circulation tank 1 and the anode chamber 52 of the stack 5;
  • the second circulation pump 4 circulates the cathode slurry between the second circulation tank 3 and the cathode chamber 53 of the stack 5.
  • the first circulation tank 1 includes a first inlet 11 and a first outlet 12 that are connected to each other;
  • the second circulation tank 3 includes a second inlet 31 and a second outlet 32 that are connected to each other;
  • the inside of the fuel cell stack 5 is provided with an anode chamber 52 and a cathode chamber 53 that are separated by a diaphragm 51, the anode chamber 52 is provided with an anode plate 54, and the cathode chamber 53 is provided with a cathode plate 55;
  • the first outlet 12 is connected to the inlet of the anode chamber 52 through the circulation pump 2, and the outlet of the anode chamber 52 is connected to the first inlet 11;
  • the second outlet 32 is connected to the inlet of the cathode chamber 53 through the second circulation pump 4, and the outlet of the cathode chamber 53 is connected to the second inlet 31.
  • the anode chamber 52 and the cathode chamber 53 are each equipped with at least one; the anode plate 54 is used to transfer the lithium contained in the anode slurry in the anode chamber 52 from the solid phase to the liquid phase, and the cathode plate 55 is used to transfer the lithium contained in the cathode slurry in the cathode chamber 53 from the liquid phase to the solid phase.
  • the first outlet 12 of the first circulation tank 1 is connected to the inlet of the anode chamber 52 through the first circulation pump 2, and the outlet of the anode chamber 52 is connected to the first inlet 11 of the first circulation tank 1;
  • the second outlet 32 of the second circulation tank 3 is connected to the cathode chamber through the second circulation pump 4.
  • the inlet of the cathode chamber 53 is connected, and the outlet of the cathode chamber 53 is connected to the second inlet 31 of the second circulation tank 3.
  • the first circulation tank 1 is circularly connected to the anode chamber 52, and the second circulation tank 3 is circularly connected to the cathode chamber 53, so that cyclic continuous extraction of lithium is realized, the efficiency of lithium extraction is high, resource recovery is achieved, and environmental protection effects are achieved.
  • an anode plate 54 is provided in the middle of each anode chamber 52, and a cathode plate 55 is provided in the middle of each cathode chamber 53.
  • the anode slurry in the anode chamber 52 flows along the two sides of the anode plate 54, and the cathode slurry in the cathode chamber 53 flows along the two sides of the cathode plate 55.
  • the above-mentioned structural arrangement makes the flow channel relatively narrow, which is easy to cause blockage; the advantage is that the distance between the anode plate 54 and the cathode plate 55 is relatively large, the working voltage is high, and the voltage adjustable range is large.
  • the anode plate 54 and the cathode plate 55 are in the shape of a plate or a porous shape.
  • the anode plate 54 and the cathode plate 55 have the function of collecting current, wherein the plate-shaped structure is easy to install and has a low preparation cost; the porous structure has a higher cost, but has a larger contact area with the anode slurry and the cathode slurry, making the lithium extraction efficiency higher.
  • two anode plates 54 are provided on both sides of each anode chamber 52, and two cathode plates 55 are provided on both sides of each cathode chamber 53.
  • the anode slurry in the anode chamber 52 flows along the gap between the two anode plates 54, and the cathode slurry in the cathode chamber 53 flows along the gap between the two cathode plates 55.
  • the advantage of the above structural setting is that the flow channel is relatively wide and not easy to cause blockage; however, the distance between the anode plate 54 and the cathode plate 55 is relatively small, the working voltage is low, and the voltage adjustable range is small.
  • the shape of the anode plate 54 and the cathode plate 55 is porous, for example, a mesh shape.
  • a mesh structure with holes inside
  • the distance L between the anode plate 54 and the diaphragm 51 and the distance L between the cathode plate 55 and the diaphragm 51 are sufficient. 0mm ⁇ L ⁇ 80mm, the distance within this range makes the plate-shaped anode plate 54 and cathode plate 55 not close to the diaphragm 51, so that ions can pass through the diaphragm 51 smoothly.
  • the mesh-shaped anode plate 54 and cathode plate 55 When the shape of the anode plate 54 and the cathode plate 55 is mesh-shaped; the distance between the anode plate 54 and the diaphragm 51 and the distance L between the cathode plate 55 and the diaphragm 51 meet 0mm ⁇ L ⁇ 80mm, the mesh-shaped anode plate 54 and cathode plate 55 have holes inside, so even if they are close to the diaphragm 51, ions can pass through the diaphragm 51.
  • the anode chamber 52 and the cathode chamber 53 are arranged alternately and are both vertically arranged, so that the anode slurry flows up and down in the anode chamber 52 along the height direction Y of the anode chamber, and the cathode slurry flows up and down in the cathode chamber 53 along the height direction of the cathode chamber 53.
  • the fuel cell stack also includes a liquid distribution pipe 56, which is arranged at the inlet and outlet of the anode chamber 52, so that the anode slurry flows into or out of the anode chamber 52 through the liquid distribution pipe 56, and the liquid distribution pipe 56 extends along the length X direction of the anode chamber 52, and the liquid distribution pipe 56 is arranged at the inlet and outlet of the cathode chamber 53, so that the cathode slurry flows into or out of the cathode chamber 53 through the liquid distribution pipe 56, and the liquid distribution pipe 56 extends along the length direction of the cathode chamber 53.
  • a plurality of through holes 561 are evenly distributed on the surface of the liquid distribution pipe 56, so that the anode slurry flows evenly in the anode chamber 52 and fully contacts the anode plate 54, and the cathode slurry flows evenly in the cathode chamber 53 and fully contacts the cathode plate 55, ensuring the normal progress of the electrochemical reaction, thereby reducing energy consumption.
  • the first circulation tank 1 further includes a first feed port 13 and a first discharge port 14, wherein the first feed port 13 is in communication with the first outlet 12, and the first outlet 14 is in communication with the first inlet 11.
  • the first inlet 11 is provided with a first three-way valve, so that the first inlet 11 is in communication with the first discharge port 14 and the first outlet 12 respectively through the first three-way valve.
  • the anode slurry is circulated in the first circulation tank 1 and the anode chamber 52 of the stack 5 to realize a cyclic electrochemical reaction, or the anode slurry is discharged from the first discharge port 14 after the electrochemical reaction is completed; the first feed port 13 is used to input anode slurry that needs to undergo an electrochemical reaction.
  • the second circulation tank 3 further includes a second feed port 33 and a second discharge port 34, the second feed port 33 is connected to the second outlet 32, and the second discharge port 34 is connected to the second inlet 31.
  • the second inlet 31 is provided with a second three-way valve, so that the second inlet 31 is connected with the second discharge port 34 and the second outlet 32 respectively through the second three-way valve.
  • the cathode slurry circulates in the second circulation tank 3 and the cathode chamber 53 of the stack 5 to realize a cyclic electrochemical reaction, or the cathode slurry is discharged from the second discharge port 34 after completing the electrochemical reaction; the second feed port 33 is used to input the cathode slurry that needs to undergo an electrochemical reaction.
  • the material of the anode plate 54 is one of graphite, lead, lead alloy, titanium and coated titanium.
  • the coated titanium is one of lead dioxide coated on titanium, titanium-manganese alloy coated on titanium, manganese dioxide coated on titanium, iridium or ruthenium oxide coated on titanium, and tin-antimony oxide coated on titanium.
  • the anode plate 54 can resist anodic oxidation in a neutral or acidic solution containing chlorine and will not be dissolved or corroded.
  • the material of the cathode plate 55 is one of iron, nickel, copper, zinc, aluminum, lead, manganese, stainless steel, iron-nickel alloy, aluminum alloy, zinc alloy, lead alloy, and manganese alloy. When the conductivity is met, the cathode plate 55 can be stably used in a chlorine-containing solution.
  • the present application provides a method for electrochemical extraction of lithium, and the following method for electrochemical extraction of lithium is performed by a lithium electrochemical extraction device, including the following steps:
  • Step 1 obtain a solid-phase lithium-containing material, and mix the solid-phase lithium-containing material with an electrolyte solution to form an anode slurry; wherein the electrolyte solution is used to slurry the solid-phase lithium-containing material, and the electrolyte solution can use a sulfate or chloride solution.
  • Step 2 turn on the first circulation pump 2 to transport the anode slurry from the first circulation tank 1 into the anode chamber 52 of the fuel cell stack 5.
  • the anode slurry that has completed the electrolysis is discharged from the anode chamber 52 into the first circulation tank 1.
  • Step 3 After repeating the previous step at least once, the anode slurry that has completed electrolysis is discharged from the first circulation tank 1, and a lithium-rich solution is obtained through solid-liquid separation.
  • the solid-phase lithium-containing material is a recovered positive electrode material of a lithium-ion battery.
  • the above method can be used to recover and utilize the lithium in the positive electrode material of the lithium-ion battery.
  • the solid phase lithium-containing material is obtained by the following steps:
  • Step 11 obtaining lithium-containing brine (which may be salt lake brine), and mixing the lithium-containing brine with a lithium-deintercalation material to form a cathode slurry;
  • Step 12 start the second circulation pump 4, so that the cathode slurry is transported from the second circulation tank 3 into the cathode chamber 53 of the stack 5, the stack 5 is connected to a power source to electrolyze the cathode slurry, so that the lithium in the cathode slurry is transferred from the liquid phase to the solid phase, and the cathode slurry that has completed the electrolysis is discharged from the cathode chamber 53 into the second circulation tank 3;
  • Step 13 After repeating the previous step at least once, the cathode slurry that has completed electrolysis is discharged from the second circulation tank 3, and then undergoes solid-liquid separation to obtain a solid-phase lithium-containing material.
  • Steps 11-13 can prepare the salt lake brine into a solid lithium-containing material, and the solid lithium-containing material can realize lithium recovery and extraction through steps 1-3, thereby achieving the purpose of extracting lithium from the salt lake brine.
  • the lithium-deintercalation material is one of lithium iron phosphate, lithium manganese oxide and lithium nickel cobalt manganese oxide.
  • the above materials can intercalate lithium ions when they gain electrons (being reduced) and release lithium ions when they lose electrons (being oxidized).

Landscapes

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

Abstract

一种锂的电化学提取装置及方法，涉及电化学冶金技术领域，其中，第一循环罐（1）包括相连通的第一入口（11）和第一出口（12）；第一循环泵（2）；第二循环罐（3）包括相连通的第二入口（31）和第二出口（32）；第二循环泵（4）；电堆（5）内部设有通过隔膜（51）进行隔离的阳极室（52）和阴极室（53），阳极室（52）设有阳极板（54），阴极室（53）设有阴极板（55）；第一出口（12）通过循环泵（2）与阳极室（52）的入口连通，阳极室（52）的出口与第一入口（11）连通；第二出口（32）通过第二循环泵（4）与阴极室（53）的入口连通，阴极室（53）的出口与第二入口（31）连通。该装置及方法能够从含锂的固相材料或液相材料中提取锂，且提取锂的效率高，达到环保效果。

Description

一种锂的电化学提取装置及方法 技术领域
本申请涉及电化学冶金技术领域，特别是涉及一种锂的电化学提取装置及方法。
背景技术
锂金属及其化合物广泛应用于玻璃、冶金、陶瓷、润滑剂和制冷剂等行业，同时随着电动汽车、风电、核电等新兴产业的迅速崛起，社会发展对锂资源的需求也逐渐呈现跳跃式增长。随着锂资源的提取从矿石提锂转向含锂卤水、海水提锂及废旧锂离子电池中的正极材料提锂，主要使用热处理设备配合罐式反应器和固液分离设备。目前的电化学提锂只能针对单一相的含锂材料进行提取，使的适用范围较小，并且提取效率不高，因此能耗较大，不利于环保。
发明内容
本申请的目的是提供一种锂的电化学提取装置及方法，能够从含锂的固相材料或液相材料中提取锂，且提取锂的效率高，具备环保效果。
为了实现上述目的，一方面本申请提供了一种锂的电化学提取装置，包括：
第一循环罐，包括相连通的第一入口和第一出口；
第一循环泵；
第二循环罐，包括相连通的第二入口和第二出口；
第二循环泵；以及
电堆，其内部设有通过隔膜进行隔离的阳极室和阴极室，所述阳极室设有阳极板，所述阴极室设有阴极板；所述第一出口通过所述循环泵与所述阳极室的入口连通，所述阳极室的出口与所述第一入口连 通；所述第二出口通过所述第二循环泵与所述阴极室的入口连通，所述阴极室的出口与所述第二入口连通；
其中，所述阳极室和阴极室均设有一个以上；所述阳极板用于使所述阳极室内的阳极浆料含有的锂从固相中转移到液相中，所述阴极板用于使所述阴极室内的阴极浆料含有的锂从液相中转移到固相中。
在一些实施例中，每个所述阳极室的中部设有一块阳极板，每个所述阴极室的中部设有一块阴极板。
在一些实施例中，所述阳极板和阴极板的形状为板状，所述阳极板与所述隔膜的距离以及所述阴极板与所述隔膜的距离L，满足0mm＜L≤80mm。
在一些实施例中，每个所述阳极室的两侧对应设有两块阳极板，每个所述阴极室的两侧对应设有两块阴极板。
在一些实施例中，所述阳极板和阴极板的形状为多孔状；所述阳极板与所述隔膜的距离以及所述阴极板与所述隔膜的距离L，满足0mm≤L≤80mm。
在一些实施例中，所述阳极室和阴极室交错排列，且均为竖向设置。
在一些实施例中，所述电堆还包括布液管，所述布液管设于所述阳极室的入口和出口处，且沿所述阳极室的长度方向延伸，以及所述布液管设于所述阴极室的入口和出口处，且沿所述阴极室的长度方向延伸。
在一些实施例中，所述布液管表面均布有多个通孔。
在一些实施例中，所述第一循环罐还包括第一进料口和第一出料口，所述第一进料口与所述第一出口连通，所述第一出料口与所述第一入口连通，或/和，所述第二循环罐还包括第二进料口和第二出料口，所述第二进料口与所述第二出口连通，所述第二出料口与所述第二入口连通。
在一些实施例中，所述阳极板的材质为石墨、铅、铅合金、钛和 涂层钛中的一种，所述涂层钛为钛材上涂覆二氧化铅、钛材上涂覆钛锰合金、钛材上涂覆二氧化锰、钛材上涂覆铱或钌氧化物、钛材上涂覆锡锑氧化物中的一种。
在一些实施例中，所述阴极板的材质为铁、镍、铜、锌、铝、铅、锰、不锈钢、铁镍合金、铝合金、锌合金、铅合金、锰合金中的一种。
另一方面本申请提供了一种锂的电化学提取方法，使用上述锂的电化学提取装置，包括以下步骤：
获取固相含锂材料，将所述固相含锂材料与电解质溶液混合形成阳极浆料；
开启第一循环泵，使所述阳极浆料自第一循环罐输送进入电堆的阳极室内，所述电堆接入电源对所述阳极浆料电解，使所述阳极浆料中的锂从固相中转移到液相中，完成电解的所述阳极浆料从所述阳极室排出进入到所述第一循环罐中。
重复上个步骤至少一次后，完成电解的所述阳极浆料自所述第一循环罐排出，且经过固液分离得到富锂溶液。
在一些实施例中，所述固相含锂材料为回收的锂离子电池的正极材料。
在一些实施例中，所述固相含锂材料通过以下方法得到：
获取含锂卤水，将所述含锂卤水与脱嵌锂材料混合形成阴极浆料；
开启第二循环泵，使所述阴极浆料自第二循环罐输送进入所述电堆的阴极室内，所述电堆接入电源对所述阴极浆料进行电解，使所述阴极浆料中的锂从液相中转移到固相中，完成电解的所述阴极浆料从所述阴极室排出进入到所述第二循环罐中；
重复上个步骤至少一次后，完成电解的所述阴极浆料自所述第二循环罐排出，再经过固液分离得到所述固相含锂材料。
在一些实施例中，所述脱嵌锂材料为磷酸铁锂、锰酸锂和镍钴锰酸锂中的一种。
本申请提供一种锂的电化学提取装置及方法，与现有技术相比， 其有益效果在于：
设置的第一循环罐的第一出口通过第一循环泵与阳极室的入口连通，阳极室的出口与第一循环罐的第一入口连通；第二循环罐的第二出口通过第二循环泵与阴极室的入口连通，阴极室的出口与第二循环罐的第二入口连通，电堆通电后在阳极室中能够从含锂的固相材料中提取锂，在阴极室中能够从含锂的液相材料中提取锂，并且第一循环罐与阳极室循环连通，第二循环罐与阴极室循环连通，实现循环连续提取锂，使得提取锂的效率高，实现资源回收，具备环保效果。
附图说明
图1为本申请实施例提供的锂的电化学提取装置的原理结构示意图。
图2为本申请实施例提供的锂的电化学提取装置的电堆第一结构示意图。
图3为本申请实施例提供的锂的电化学提取装置的电堆第二结构示意图。
图4为图2中沿A向的剖面结构示意图。
图中：1、第一循环罐；11、第一入口；12、第一出口；13、第一进料口；14、第一出料口；2、第一循环泵；3、第二循环罐；31、第二入口；32、第二出口；33、第二进料口；34、第二出料口；4、第二循环泵；5、电堆；51、隔膜；52、阳极室；53、阴极室；54、阳极板；55、阴极板；56、布液管；561、通孔；X、阳极室的长度方向；Y、阳极室的高度方向。
具体实施方式
下面将结合本申请实施例中的附图，对本申请实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本申请的一部分实施例，而不是全部的实施例。
需要理解的是，在本申请的描述中，术语“上”、“下”、“竖 直”、“水平”、“顶”、“底”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本申请和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本申请的限制。术语“第一”、“第二”仅用于描述目的，而不能理解为指示或暗示相对重要性或者隐含指明所指示的技术特征的数量，也即，限定有“第一”、“第二”的特征可以明示或者隐含地包括一个或者更多个该特征。此外，除非另有说明，“多个”的含义是两个或两个以上。
此外，下面所描述的本申请不同实施方式中所涉及的技术特征只要彼此之间未构成冲突就可以相互结合。
如图1-4所示，本申请提供的一种锂的电化学提取装置，在一些实施例中，包括第一循环罐1、第一循环泵2、第二循环罐3、第二循环泵4和电堆5。在工作时，第一循环泵2使阳极浆料在第一循环罐1与电堆5的阳极室52之间循环流动；第二循环泵4使阴极浆料在第二循环罐3与电堆5的阴极室53之间循环流动。
具体的，第一循环罐1包括相连通的第一入口11和第一出口12；第二循环罐3，包括相连通的第二入口31和第二出口32；电堆5内部设有通过隔膜51进行隔离的阳极室52和阴极室53，阳极室52设有阳极板54，阴极室53设有阴极板55；第一出口12通过循环泵2与阳极室52的入口连通，阳极室52的出口与第一入口11连通；第二出口32通过第二循环泵4与阴极室53的入口连通，阴极室53的出口与第二入口31连通。
其中，阳极室52和阴极室53均设有一个以上；阳极板54用于使阳极室52内的阳极浆料含有的锂从固相中转移到液相中，阴极板55用于使阴极室53内的阴极浆料含有的锂从液相中转移到固相中。
基于上述的设置，第一循环罐1的第一出口12通过第一循环泵2与阳极室52的入口连通，阳极室52的出口与第一循环罐1的第一入口11连通；第二循环罐3的第二出口32通过第二循环泵4与阴极室 53的入口连通，阴极室53的出口与第二循环罐3的第二入口31连通，电堆5通电后在阳极室52中能够从含锂的固相材料中提取锂，在阴极室53中能够从含锂的液相材料中提取锂，并且第一循环罐1与阳极室52循环连通，第二循环罐3与阴极室53循环连通，实现循环连续提取锂，使得提取锂的效率高，实现资源回收，具备环保效果。
如图2所示，在一个实施例中，每个阳极室52的中部设有一块阳极板54，每个阴极室53的中部设有一块阴极板55。在工作时，阳极室52内的阳极浆料顺着阳极板54的两侧流动，阴极室53内的阴极浆料顺着阴极板55的两侧流动，上述的结构设置使流道相对较窄，容易造成堵塞；优点是阳极板54和阴极板55的距离相对较大，工作电压较高，电压可调范围较大。
上述实施例中，阳极板54和阴极板55的形状为板状或多孔状。阳极板54和阴极板55具有汇集电流的功能，其中，板状的结构容易安装，且制备成本低；多孔状的结构成本较高，但是与阳极浆料和阴极浆料的接触面积更大，使提锂效率更高。
如图3所示，在一个实施例中，每个阳极室52的两侧对应设有两块阳极板54，每个阴极室53的两侧对应设有两块阴极板55。在工作时，阳极室52内的阳极浆料顺着两块阳极板54之间的间隔处流动，阴极室53内的阴极浆料顺着两块阴极板55之间的间隔处流动，上述的结构设置优点是使流道相对较宽，不容易造成堵塞；但是阳极板54和阴极板55的距离相对较小，工作电压较低，电压可调节范围较小。
上述实施例中，阳极板54和阴极板55的形状为多孔状，例如采用网状，此时，由于阳极板54和阴极板55与隔膜51的间距较小，只能采用网状结构(内部具有孔洞)使离子能够通过，来实现汇集电流的功能；若采用板状结构(内部不具有孔洞)会阻碍离子通过隔膜51，影响汇集电流的功能。
在一些实施例中，当阳极板54和阴极板55的形状为板状，阳极板54与所述隔膜51的距离以及阴极板55与所述隔膜51的距离L，满 足0mm＜L≤80mm，距离在该范围使得板状的阳极板54和阴极板55不会紧贴在隔膜51上，使离子的顺利通过隔膜51。当阳极板54和阴极板55的形状为网状；阳极板54与所述隔膜51的距离以及所述阴极板55与所述隔膜51的距离L，满足0mm≤L≤80mm，网状的阳极板54和阴极板55内部具有孔洞，因此即使紧贴在隔膜51上也能使离子通过隔膜51。
如图2和4所示，在一个实施例中，阳极室52和阴极室53交错排列，且均为竖向设置，使得阳极浆料在阳极室52内沿阳极室的高度方向Y上下流动，阴极浆料在阴极室53内沿阴极室53的高度方向上下流动，需要说明的是，阳极室52和阴极室53的内部结构相同；电堆还包括布液管56，布液管56设于阳极室52的入口和出口处，使阳极浆料通过布液管56流入或流出阳极室52，且布液管56沿阳极室52的长度X方向延伸，以及布液管56设于阴极室53的入口和出口处，使阴极浆料通过布液管56流入或流出阴极室53，且布液管56沿阴极室53的长度方向延伸。具体的，布液管56表面均布有多个通孔561，使得阳极浆料在阳极室52内均匀流动与阳极板54充分接触，阴极浆料在阴极室53内均匀流动与阴极板55充分接触，保证电化学反应的正常进行，从而能够降低能耗。
在一个实施例中，第一循环罐1还包括第一进料口13和第一出料口14，第一进料口13与第一出口12连通，第一出料口14与第一入口11连通。其中，第一入口11设有第一三通阀，使得第一入口11通过第一三通阀分别与第一出料口14及第一出口12连通，在运行时，通过控制第一三通阀，使阳极浆料在第一循环罐1与电堆5的阳极室52内循环流动实现循环电化学反应，或阳极浆料完成电化学反应后从第一出料口14内排出；第一进料口13用于输入需要进行电化学反应的阳极浆料。
在一个实施例中，第二循环罐3还包括第二进料口33和第二出料口34，第二进料口33与第二出口32连通，第二出料口34与第二入口 31连通。其中，第二入口31设有第二三通阀，使得第二入口31通过第二三通阀分别与第二出料口34及第二出口32连通，在运行时，通过控制第二三通阀，使阴极浆料在第二循环罐3与电堆5的阴极室53内循环流动实现循环电化学反应，或阴极浆料完成电化学反应后从第二出料口34内排出；第二进料口33用于输入需要进行电化学反应的阴极浆料。
具体的，阳极板54的材质为石墨、铅、铅合金、钛和涂层钛中的一种，涂层钛为钛材上涂覆二氧化铅、钛材上涂覆钛锰合金、钛材上涂覆二氧化锰、钛材上涂覆铱或钌氧化物、钛材上涂覆锡锑氧化物中的一种，在满足导电的状态下，阳极板54能够在含氯的中性或酸性溶液中耐阳极氧化，不被溶解和腐蚀；阴极板55的材质为铁、镍、铜、锌、铝、铅、锰、不锈钢、铁镍合金、铝合金、锌合金、铅合金、锰合金中的一种，在满足导电的状态下，阴极板55在含氯溶液中能稳定使用。
此外，本申请提供了一种锂的电化学提取方法，下列的锂的电化学提取方法由锂的电化学提取方装置执行。包括以下步骤：
步骤1、获取固相含锂材料，将固相含锂材料与电解质溶液混合形成阳极浆料；其中，电解质溶液的作用是浆化固相含锂材料，电解质溶液可使用硫酸盐或氯化物溶液。
步骤2、开启第一循环泵2，使阳极浆料自第一循环罐1输送进入电堆5的阳极室52内，电堆5接入电源对阳极浆料电解，使阳极浆料中的锂从固相中转移到液相中，完成电解的阳极浆料从阳极室52排出进入到第一循环罐1中。
步骤3、重复上个步骤至少一次后，完成电解的阳极浆料自第一循环罐1排出，且经过固液分离得到富锂溶液。
在一个实施例中，固相含锂材料为回收的锂离子电池的正极材料，此时通过上述方法能够实现锂离子电池的正极材料中锂的回收利用。
在另一个实施例中，固相含锂材料通过以下步骤获取：
步骤11、获取含锂卤水(可以是盐湖卤水)，将含锂卤水与脱嵌锂材料混合形成阴极浆料；
步骤12、开启第二循环泵4，使阴极浆料自第二循环罐3输送进入电堆5的阴极室53内，电堆5接入电源对阴极浆料进行电解，使阴极浆料中的锂从液相中转移到固相中，完成电解的阴极浆料从阴极室53排出进入到第二循环罐3中；
步骤13、重复上个步骤至少一次后，完成电解的阴极浆料自第二循环罐3排出，再经过固液分离得到固相含锂材料。
步骤11-13能够将盐湖卤水制备成固相含锂材料，而固相含锂材料通过步骤1-3实现锂的回收提取，因此达到盐湖卤水中提取锂的目的。
其中，脱嵌锂材料为磷酸铁锂、锰酸锂和镍钴锰酸锂中的一种。上述材料可以在得到电子时(被还原)，嵌入锂离子；在失去电子时(被氧化)，脱出锂离子。
以上所述仅是本申请的优选实施方式，应当指出，对于本技术领域的普通技术人员来说，在不脱离本申请技术原理的前提下，还可以做出若干改进和替换，这些改进和替换也应视为本申请的保护范围。

Claims (15)

  1. 一种锂的电化学提取装置，其特征在于，包括：
    第一循环罐(1)，包括相连通的第一入口(11)和第一出口(12)；
    第一循环泵(2)；
    第二循环罐(3)，包括相连通的第二入口(31)和第二出口(32)；
    第二循环泵(4)；以及
    电堆(5)，其内部设有通过隔膜(51)进行隔离的阳极室(52)和阴极室(53)，所述阳极室(52)设有阳极板(54)，所述阴极室(53)设有阴极板(55)；所述第一出口(12)通过所述循环泵(2)与所述阳极室(52)的入口连通，所述阳极室(52)的出口与所述第一入口(11)连通；所述第二出口(32)通过所述第二循环泵(4)与所述阴极室(53)的入口连通，所述阴极室(53)的出口与所述第二入口(31)连通；
    其中，所述阳极室(52)和阴极室(53)均设有一个以上；所述阳极板(54)用于使所述阳极室(52)内的阳极浆料含有的锂从固相中转移到液相中，所述阴极板(55)用于使所述阴极室(53)内的阴极浆料含有的锂从液相中转移到固相中。
  2. 根据权利要求1所述的锂的电化学提取装置，其特征在于，每个所述阳极室(52)的中部设有一块阳极板(54)，每个所述阴极室(53)的中部设有一块阴极板(55)。
  3. 根据权利要求2所述的锂的电化学提取装置，其特征在于，所述阳极板(54)和阴极板(55)的形状为板状，所述阳极板(54)与所述隔膜(51)的距离以及所述阴极板(55)与所述隔膜(51)的距离L，满足0mm＜L≤80mm。
  4. 根据权利要求1所述的锂的电化学提取装置，其特征在于，每个所述阳极室(52)的两侧对应设有两块阳极板(54)，每个所述阴极室(53)的两侧对应设有两块阴极板(55)。
  5. 根据权利要求2或4所述的锂的电化学提取装置，其特征在于，所述阳极板(54)和阴极板(55)的形状为多孔状；所述阳极板(54)与所述隔膜(51)的距离以及所述阴极板(55)与所述隔膜(51)的距离L，满足0mm≤L≤80mm。
  6. 根据权利要求1所述的锂的电化学提取装置，其特征在于，所述阳极室(52)和阴极室(53)交错排列，且均为竖向设置。
  7. 根据权利要求1所述的锂的电化学提取装置，其特征在于，所述电堆(5)还包括布液管(56)，所述布液管(56)设于所述阳极室(52)的入口和出口处，且沿所述阳极室(52)的长度方向(X)延伸，以及所述布液管(56)设于所述阴极室(53)的入口和出口处，且沿所述阴极室(53)的长度方向延伸。
  8. 根据权利要求7所述的锂的电化学提取装置，其特征在于，所述布液管(56)表面均布有多个通孔(561)。
  9. 根据权利要求1所述的锂的电化学提取装置，其特征在于，所述第一循环罐(1)还包括第一进料口(13)和第一出料口(14)，所述第一进料口(13)与所述第一出口(12)连通，所述第一出料口(14)与所述第一入口(11)连通；或/和，所述第二循环罐(3)还包括第二进料口(33)和第二出料口(34)，所述第二进料口(33)与所述第二出口(32)连通，所述第二出料口(34)与所述第二入口(31)连通。
  10. 根据权利要求1所述的锂的电化学提取装置，其特征在于，所述阳极板(54)的材质为石墨、铅、铅合金、钛和涂层钛中的一种，所述涂层钛为钛材上涂覆二氧化铅、钛材上涂覆钛锰合金、钛材上涂覆二氧化锰、钛材上涂覆铱或钌氧化物、钛材上涂覆锡锑氧化物中的一种。
  11. 根据权利要求1所述的锂的电化学提取装置，其特征在于，所述阴极板(55)的材质为铁、镍、铜、锌、铝、铅、锰、不锈钢、铁镍合金、铝合金、锌合金、铅合金、锰合金中的一种。
  12. 一种锂的电化学提取方法，其特征在于，使用如权利要求1-11任一项所述的锂的电化学提取装置，包括：
    获取固相含锂材料，将所述固相含锂材料与电解质溶液混合形成阳极浆料；
    开启第一循环泵(2)，使所述阳极浆料自第一循环罐(1)输送进入电堆(5)的阳极室(52)内，所述电堆(5)接入电源对所述阳极浆料电解，使所述阳极浆料中的锂从固相中转移到液相中，完成电解的所述阳极浆料从所述阳极室(52)排出进入到所述第一循环罐(1)中；
    重复上个步骤至少一次后，完成电解的所述阳极浆料自所述第一循环罐(1)排出，且经过固液分离得到富锂溶液。
  13. 根据权利要求12所述的锂的电化学提取方法，其特征在于，所述固相含锂材料为回收的锂离子电池的正极材料。
  14. 根据权利要求12所述的锂的电化学提取方法，其特征在于，所述固相含锂材料通过以下方法得到：
    获取含锂卤水，将所述含锂卤水与脱嵌锂材料混合形成阴极浆料；
    开启第二循环泵(4)，使所述阴极浆料自第二循环罐(3)输送进入所述电堆(5)的阴极室(53)内，所述电堆(5)接入电源对所述阴极浆料进行电解，使所述阴极浆料中的锂从液相中转移到固相中，完成电解的所述阴极浆料从所述阴极室(53)排出进入到所述第二循环罐(3)中；
    重复上个步骤至少一次后，完成电解的所述阴极浆料自所述第二循环罐(3)排出，再经过固液分离得到所述固相含锂材料。
  15. 根据权利要求13所述的锂的电化学提取方法，其特征在于，所述脱嵌锂材料为磷酸铁锂、锰酸锂和镍钴锰酸锂中的一种。
PCT/CN2023/140140 2023-12-20 2023-12-20 一种锂的电化学提取装置及方法 Pending WO2025129485A1 (zh)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/CN2023/140140 WO2025129485A1 (zh) 2023-12-20 2023-12-20 一种锂的电化学提取装置及方法
CN202380012428.5A CN118176327A (zh) 2023-12-20 2023-12-20 一种锂的电化学提取装置及方法

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CN2023/140140 WO2025129485A1 (zh) 2023-12-20 2023-12-20 一种锂的电化学提取装置及方法

Publications (1)

Publication Number Publication Date
WO2025129485A1 true WO2025129485A1 (zh) 2025-06-26

Family

ID=91349080

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2023/140140 Pending WO2025129485A1 (zh) 2023-12-20 2023-12-20 一种锂的电化学提取装置及方法

Country Status (2)

Country Link
CN (1) CN118176327A (zh)
WO (1) WO2025129485A1 (zh)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20200283921A1 (en) * 2019-03-08 2020-09-10 Liep Energy Ltd. Process for extraction and production of lithium salt products from brine
CN116119637A (zh) * 2023-03-09 2023-05-16 中南大学 一种废旧磷酸铁锂正极材料循环浸出和再生的方法
CN116377514A (zh) * 2023-05-09 2023-07-04 石家庄嘉硕电子技术有限公司 一种节能锂提取方法及装置
US20230212769A1 (en) * 2022-01-04 2023-07-06 Central South University Method and apparatus for extracting lithium from solution using bipolar electrodes
CN116926572A (zh) * 2023-07-07 2023-10-24 北京科技大学 电化学脱锂同步嵌锂修复回收磷酸铁锂正极材料的方法
CN117015623A (zh) * 2023-06-21 2023-11-07 广东邦普循环科技有限公司 一种电化学脱嵌提锂的方法
CN117165957A (zh) * 2023-08-21 2023-12-05 福建常青新能源科技有限公司 一种高值化利用废旧磷酸铁锂制备磷酸铁钠的方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20200283921A1 (en) * 2019-03-08 2020-09-10 Liep Energy Ltd. Process for extraction and production of lithium salt products from brine
US20230212769A1 (en) * 2022-01-04 2023-07-06 Central South University Method and apparatus for extracting lithium from solution using bipolar electrodes
CN116119637A (zh) * 2023-03-09 2023-05-16 中南大学 一种废旧磷酸铁锂正极材料循环浸出和再生的方法
CN116377514A (zh) * 2023-05-09 2023-07-04 石家庄嘉硕电子技术有限公司 一种节能锂提取方法及装置
CN117015623A (zh) * 2023-06-21 2023-11-07 广东邦普循环科技有限公司 一种电化学脱嵌提锂的方法
CN116926572A (zh) * 2023-07-07 2023-10-24 北京科技大学 电化学脱锂同步嵌锂修复回收磷酸铁锂正极材料的方法
CN117165957A (zh) * 2023-08-21 2023-12-05 福建常青新能源科技有限公司 一种高值化利用废旧磷酸铁锂制备磷酸铁钠的方法

Also Published As

Publication number Publication date
CN118176327A (zh) 2024-06-11

Similar Documents

Publication Publication Date Title
US6228527B1 (en) Magnesium solution phase catholyte seawater electrochemical system
US20120282508A1 (en) Partial flow cell
CN116837229B (zh) 一种基于流动电极电化学选择性提锂的系统及方法和应用
WO2013058375A1 (ja) ノンフローレドックス電池
CN113086961A (zh) 一种基于电化学的废旧磷酸铁锂修复回收方法
CN115287686A (zh) 盐湖提锂装置及提锂方法
US12553142B2 (en) Method and electrochemical system for recycling spent lithium-ion battery
CN116426975B (zh) 一种采用双极性电极从溶液中提取锂的方法和装置
US20200106118A1 (en) Bimetallic thermally-regenerative ammonia-based battery system, flow battery system and using methods
CN117165957A (zh) 一种高值化利用废旧磷酸铁锂制备磷酸铁钠的方法
CN115020756B (zh) 一种锌-溴/碘双液流电池
CN110564965B (zh) 一种金属锂合金及其制备方法与应用
CN114014416A (zh) 一种海水多级浓缩电解提锂装置及方法
CN220468095U (zh) 一种电化学提锂的模块化装置
WO2025030743A1 (zh) 一种电化学提锂的模块化装置
CN116288401B (zh) 一种铝水能源制氢系统
CN116426769B (zh) 一种无膜双极性电极从溶液中提取锂的方法和装置
CN107881523B (zh) 一种含碳浆料制氢工艺
CN118176327A (zh) 一种锂的电化学提取装置及方法
CN103972582A (zh) 一种二次电池
CN209929451U (zh) 一种氯镁燃料电池
CN114050358A (zh) 一种三腔室浓差铝空气电池系统
CN115028241A (zh) 一种镁空气海水淡化电池装置及并网设备
US20250257491A1 (en) Electrochemical membrane reactor systems for removing lithium from a lithium-containing solution and related methods
CN118076769B (zh) 电解废旧锂电池粉中有价金属离子的方法

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: 23961828

Country of ref document: EP

Kind code of ref document: A1