A device and method for preferentially extracting lithium-nickel and simultaneously realizing nickel-lithium separation from waste ternary lithium battery positive electrode materials

Abstract

This invention belongs to the field of resource recycling technology and discloses a device for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation. The device includes: a reaction vessel internally divided into a reaction chamber and an adsorption chamber by a separator; the separator has channels allowing ions to pass through; a high-speed shear disperser disposed in the middle of the reaction chamber; and an ozone generator and a peristaltic pump connected to the reaction chamber. This invention also discloses a method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation. This invention, through the design of an integrated reaction device, highly couples the two core steps of leaching and separation of waste ternary lithium battery cathode materials in time and space; while selectively leaching lithium and nickel occurs in the reaction chamber, dissolved Ni²⁺ is also extracted. + Driven by a centrifugal flow field, and guided by the targeted adsorption of ion exchange resin in the adsorption chamber, efficient migration and simultaneous enrichment are achieved, enabling precise separation of lithium and nickel ions.

Description

Technical Field

[0001] This invention belongs to the field of resource recycling, and in particular relates to an apparatus and method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation. Background Technology

[0002] With the rapid development of my country's new energy vehicle industry, an increasing number of retired ternary lithium-ion power batteries will be generated in the future. These retired nickel-cobalt-manganese ternary lithium-ion batteries contain a large amount of toxic and harmful substances, which will seriously endanger the environment and human health. Furthermore, retired lithium-ion batteries contain abundant valuable metals, which can serve as important secondary resources. Therefore, to achieve the recycling of valuable metal resources and reduce the adverse environmental impact of solid waste, the sustainable recycling of spent lithium-ion batteries is an urgent priority.

[0003] Currently, the recycling methods for spent lithium-ion battery materials are mainly divided into hydrometallurgical routes, pyrometallurgical routes, and pyrometallurgical + hydrometallurgical routes. The traditional pyrometallurgical route converts transition metal compounds into molten metals, while lithium (Li) is lost in the slag as oxides. In the traditional hydrometallurgical route, Li is recovered in the final step, and a certain amount of Li is inevitably entrained during the transition metal precipitation and separation process, leading to Li loss. Therefore, the preferential extraction of Li has attracted increasing attention from researchers. The pyrometallurgical + hydrometallurgical route selectively converts lithium in the cathode material into metal compounds with different solubilities than other metals such as nickel, cobalt, and manganese, thus allowing selective leaching of lithium and separation from other metals. Although this method has a short process flow, it is energy-intensive and easily generates CO and SO. x NO x The use of additives in leaching can introduce impurities into the leaching process, requiring further purification to obtain high-purity lithium carbonate. For example, patent document CN112062143A discloses a method for acid-free preparation of lithium hydrochloride from spent lithium-ion batteries. This method involves mixing spent lithium-ion battery cathode powder with calcium chloride and calcining at high temperature. The calcined product is washed with water and filtered. Lithium sulfate is added to the filtrate to remove calcium, followed by further filtration. The filtrate is then concentrated by evaporation, and sodium carbonate is added to obtain high-purity lithium carbonate. However, this method introduces calcium ions as impurities, necessitating purification of the lithium-rich leaching solution. In contrast, the hydrometallurgical oxidative leaching method offers the highest lithium recovery rate, promoting the efficient extraction of lithium-rich lithium. + While leaching, it prevents Co from... 2+ and Mn 2+ The leaching process exhibits excellent selectivity; however, the commonly used oxidants in existing methods are H2O2, Na2S2O8, and NaClO, which are expensive and limit their large-scale industrial application. Summary of the Invention

[0004] The technical problem to be solved by the present invention is to overcome the deficiencies and defects mentioned in the background art above, and to provide an apparatus and method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation.

[0005] To solve the above-mentioned technical problems, the technical solution proposed by this invention is as follows:

[0006] A device for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously separating nickel and lithium, comprising: A reaction vessel, the interior of which is divided into a reaction chamber and an adsorption chamber by a partition; the partition is provided with channels that allow ions to pass through; The high-speed shear disperser, located in the middle of the reaction chamber, is used to shear and disperse the slurry in the chamber and generate a centrifugal flow field that drives the solution to flow into the adsorption chamber. The reaction chamber is connected to an ozone generator and a peristaltic pump; the ozone generator is used to introduce ozone into the reaction chamber as an oxidant; the peristaltic pump is used to pump acid into the reaction chamber to adjust and maintain the pH value of the reaction system. The adsorption chamber is used to contain ion exchange resin that adsorbs nickel ions. Under the centrifugal flow field generated by the high-speed shear disperser, the Ni ions leached from the reaction chamber... 2+ It flows with the solution into the adsorption chamber and is simultaneously adsorbed by the resin.

[0007] In the above-described device, preferably, the partition is a partition plate integrally formed with the reaction vessel. The partition plate has multiple through holes to form ion channels for liquid exchange. Filter cloth, preferably polypropylene filter cloth, is provided on both sides of the partition plate to cover the ion channels. AB glue is used to fix and completely cover the ion channels to prevent direct flow of materials on both sides of the chamber.

[0008] In the above-described device, preferably, the side wall of the adsorption chamber is provided with an openable and closable discharge port near the bottom, and the discharge port is closed by a piston.

[0009] Preferably, in the above-described apparatus, the cutter head of the high-speed shear disperser is located in the central region of the reaction chamber; a stainless steel pipe is connected to the end of the ozone generator outlet pipe and the end of the peristaltic pump delivery pipe, and the outlet end of the stainless steel pipe extends directly to the center of the end of the high-speed shear disperser cutter head. The high-speed shear disperser cutter head consists of a stator and a high-speed rotating rotor, and the cutter head is located in the central region of the reaction chamber; when the rotor of the high-speed shear disperser rotates at high speed, a strong negative pressure zone is formed in the central region of the cutter head, drawing in the surrounding fluid; after the fluid is accelerated between the stator and rotor slits, it is thrown out at high speed along the tangential direction, forming a high-intensity vortex flow field (i.e., centrifugal flow field) with distinct radial and tangential velocity components. This flow field not only enhances the mixing and mass transfer within the reaction chamber, but its radial component also provides a continuous driving force for the fluid to flow from the center of the reaction chamber to the periphery (including the direction of the separator), thereby actively pushing the solution to the adsorption chamber, greatly enhancing the Ni 2+ The convective mass transfer rate to the resin surface enables real-time coupling of leaching and adsorption.

[0010] As a general inventive concept, this invention also provides a method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation using the above-mentioned device, comprising the following steps: (1) In the reaction chamber, waste ternary lithium battery cathode material is mixed with water to form a slurry, and the high-speed shear disperser is started; (2) Add sufficient amount of ion exchange resin for selective adsorption of nickel ions into the adsorption chamber; (3) Acid and oxidant ozone are added to the reaction system in the reaction chamber through a peristaltic pump and an ozone generator, respectively, and a leaching reaction is carried out under oxidizing and acidic conditions to selectively leach lithium and nickel in the cathode material; (4) During the leaching reaction, acid solution is continuously added through a peristaltic pump to maintain the pH of the system in the range of 2-5; at the same time, the centrifugal flow field generated by the high-speed shear disperser drives the Ni-containing fluid. 2+ The solution continuously flows through the adsorption chamber, containing Ni 2+ Nickel is simultaneously adsorbed by ion exchange resin, thus achieving separation of nickel from lithium in the leachate.

[0011] In the above method, preferably, in step (3), the acid is introduced into the center of the end of the high-speed shear disperser blade to participate in the reaction; the amount of ozone used satisfies the total molar ratio of ozone to cobalt and manganese being 1.5-3.0:1.

[0012] In the preferred embodiment of the above method, in step (3), the reaction temperature of the leaching reaction process is 20℃-80℃, the reaction time is 4 hours-10 hours, and the solid-liquid ratio of the leaching reaction is 100-500g / L.

[0013] In the preferred embodiment of the above method, in step (3), concentrated sulfuric acid with a concentration of 98% is first pumped in at a S / Li molar ratio of 0.5 to create a transient strong acid environment in the local reaction system. Subsequently, acid is continuously or intermittently added during the reaction to maintain the pH value of the system. In this process, a specified amount of 98% concentrated sulfuric acid solution is pumped in from the center of the cutter head to form a transient strong acid microenvironment. After rapidly destroying the structure of the positive electrode material, sufficient ozone is introduced for oxidation and lithium extraction. During the reaction, a small amount of 98% concentrated sulfuric acid solution is continuously pumped in to adjust the pH value of the solution.

[0014] In the above method, preferably, in step (2), when the high-speed shear disperser is started, its rotation speed is controlled to be 4000rpm-8000rpm.

[0015] Preferably, the above method further includes, after step (4): The leachate and cobalt- and manganese-containing leachate residue in the reaction chamber are separated from the adsorption resin and lithium-containing leachate in the adsorption chamber. Then, sodium carbonate solution is added to the leachate to precipitate lithium carbonate product. The precipitation is carried out under heating conditions at a temperature of 80℃-95℃. After the reaction is completed, the ion exchange resin in the adsorption chamber is soaked in 0.5-1 mol / L sulfuric acid solution for 30-60 min to obtain a pure nickel sulfate solution.

[0016] In the above method, preferably, the waste ternary lithium battery cathode material includes at least one of NCM111, NCM523, NCM622, and NCM811.

[0017] The principle behind this invention for preferential extraction of lithium and nickel is as follows: the leaching of Li is unaffected by redox potential and can be effectively dissolved in both acidic and alkaline environments. In contrast, the leaching of nickel, cobalt, and manganese is controlled by pH and redox potential. Under strong oxidizing conditions, nickel, cobalt, and manganese are oxidized to form NiOOH, Co3O4, and MnO2; however, NiOOH dissolves under strong acid conditions to form Ni. 2+ Co3O4 and MnO2 are relatively stable. Therefore, under strong oxidizing conditions, lithium and nickel can be preferentially extracted from waste ternary lithium battery cathode materials by controlling the pH of the solution.

[0018] Based on the above principles, this invention uses ozone as an oxidant, adjusts the pH of the solution, and uses the device of this application to enhance the lithium-nickel extraction and separation effects: (1) Enhanced reaction process: Sulfuric acid solution is pumped into the center of the high-speed shear disperser cutter head to create an instantaneous strong acid microenvironment. Combined with the synergistic effect of multi-dimensional stress fields such as mechanical crushing, impact tearing, and turbulent shearing, the stable structure of the cathode material is rapidly destroyed, thereby significantly improving the reaction kinetic efficiency; (2) Enhanced separation and mass transfer: The centrifugal flow field generated by the high-speed rotation of the rotor drives ion migration and couples the targeted adsorption of ion exchange resin to achieve Ni 2+ The efficient migration and simultaneous enrichment of lithium and nickel ions ultimately achieve efficient separation of lithium and nickel ions.

[0019] Compared with the prior art, the beneficial effects of the present invention are as follows: (1) This invention uses ozone (O3) as a green oxidant for oxidative leaching under precisely controlled pH conditions. This process is highly selective, enabling lithium (Li) leaching rates to reach over 96%, nickel (Ni) leaching rates to reach over 94%, while cobalt (Co) and manganese (Mn) leaching rates are effectively suppressed to extremely low levels (<0.5%). Compared to traditional wet processes where lithium is easily lost in the final recovery step, and pyrometallurgical or chlorination roasting methods that easily introduce impurity ions such as calcium and sodium requiring subsequent impurity removal, this invention uses oxygen as a source to prepare ozone. The reagent is widely available and inexpensive, and the entire leaching process does not introduce any foreign metal impurities, ensuring the high purity (≥99%) of the final product (lithium carbonate) from the source.

[0020] (2) This invention, through the design of an integrated reaction device, highly couples the two core steps of leaching and separating waste ternary lithium battery cathode materials in time and space; while selectively leaching lithium and nickel is carried out in the reaction chamber, dissolved Ni² + Driven by a centrifugal flow field, and guided by the targeted adsorption of ion exchange resin in the adsorption chamber, efficient migration and simultaneous enrichment are achieved, enabling precise separation of lithium and nickel ions. This design directly eliminates the need for subsequent cumbersome solvent extraction and stepwise precipitation processes, significantly simplifying the process flow and reducing the number of operating units. Furthermore, the enhanced flow field improves mass transfer efficiency, and the coupled processes reduce intermediate energy consumption, resulting in a significant reduction in energy consumption and chemical reagent consumption during production.

[0021] (3) This invention utilizes a high-speed shear disperser to create an instantaneous strong acid microenvironment and a high-intensity shear field, which generates violent mechanical crushing and impact tearing effects on the positive electrode material particles, rapidly destroying their stable layered crystal structure, greatly increasing the reaction interface, and improving the reaction rate and efficiency of lithium ion insertion / extraction and nickel dissolution. At the same time, the fluid dynamics generated by the centrifugal flow field, combined with the targeted adsorption effect of the ion exchange resin in the adsorption chamber, together constitute a powerful driving force for ion migration, which enables the leached nickel ions to migrate efficiently and directionally and be enriched simultaneously, solving the problem of slow speed and low efficiency of relying solely on diffusion mass transfer. Attached Figure Description

[0022] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0023] Figure 1 This is a schematic diagram of the device for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation according to the present invention. Figure 2 This is a diagram of a rectangular groove structure. Figure 3 This is a diagram of the partition structure.

[0024] Figure 4 This is a structural diagram of the end of the cutter head of a high-speed shearing disperser.

[0025] Legend: 1. Rectangular trough; 2. Baffle plate; 3. Reaction chamber; 4. Adsorption chamber; 5. Through hole; 6. Filter cloth; 7. Piston; 8. High-speed shear disperser. Detailed Implementation

[0026] To facilitate understanding of the present invention, the present invention will be described more fully and in detail below with reference to the accompanying drawings and preferred embodiments, but the scope of protection of the present invention is not limited to the following specific embodiments.

[0027] Unless otherwise defined, all technical terms used herein have the same meaning as commonly understood by those skilled in the art. The technical terms used herein are for the purpose of describing particular embodiments only and are not intended to limit the scope of the invention.

[0028] Unless otherwise specified, all raw materials, reagents, instruments and equipment used in this invention can be purchased from the market or prepared by existing methods.

[0029] Example 1: A device for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation, such as... Figures 1-4 As shown, the system includes an acrylic reaction vessel, preferably a rectangular trough 1, which is internally divided into a reaction chamber 3 and an adsorption chamber 4 by a partition. The partition has through holes 5 that allow ions to pass through. A high-speed shear disperser 8 is disposed within the reaction chamber 3, with its blade located in the central region of the reaction chamber 3. The blade end includes a stator and a high-speed rotating rotor. The partition is a baffle 2 integrally formed with the reaction vessel, and the baffle 2 has multiple through holes forming ion channels. AB glue is applied to the side walls of the baffle 2, outside the ion channels, to fix a polypropylene filter cloth 6 that completely covers the ion channels. An openable and closable discharge port is located near the bottom of the side wall of the adsorption chamber 4, and a piston 7 is located at the discharge port. An ozone generator, a peristaltic pump, and a pH meter are connected inside the reaction chamber 3. A stainless steel pipe is connected to the end of the ozone generator's outlet pipe and the peristaltic pump's delivery pipe, and the outlet end of the stainless steel pipe extends directly to the center of the high-speed shear disperser blade end.

[0030] Example 2: A method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously separating nickel and lithium, using the apparatus described in Example 1, specifically includes the following steps: 20g of waste ternary lithium-ion battery cathode material was added to 100mL of aqueous solution in reaction chamber 3 to prepare the slurry. The high-speed shear disperser 8 was turned on, and the rotor speed was set to 6000rpm. Amberlite IRC747 resin was added to adsorption chamber 4. Then, 98% sulfuric acid was pumped in at a S / Li molar ratio of 0.5. Sufficient ozone was then introduced at a total ozone-to-cobalt-manganese molar ratio (O3 / (Co+Mn)) of 1.5:1 to oxidize and extract lithium. During the reaction, 98% sulfuric acid solution was continuously pumped in via a peristaltic pump to control the pH of the system solution at 3.5, and the reaction temperature was 40℃. Simultaneously with the lithium extraction reaction, the sufficient amount of Amberlite IRC747 resin pre-filled in the adsorption chamber 4 was used to adsorb Ni... 2+ Adsorption was carried out. After 6 hours of reaction, the piston 7 at the bottom of adsorption chamber 4 was opened to release and collect the material in adsorption chamber 4 for solid-liquid separation, obtaining the adsorbed ion exchange resin and part of the lithium extraction leachate. The solution in reaction chamber 3 was poured out and solid-liquid separation was performed to obtain a pure lithium extraction leachate and a leachate residue enriched with cobalt and manganese. A saturated sodium carbonate solution was added to the lithium extraction leachate, and the mixture was heated in a water bath at 85°C for 90 minutes. After mixing, stirring, and filtration, a white precipitate was obtained. The white precipitate was washed to obtain lithium carbonate. The adsorbed ion exchange resin was washed with 0.5 mol / L sulfuric acid solution for 60 minutes to obtain a pure nickel sulfate solution.

[0031] Example 3: A method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously separating nickel and lithium, using the apparatus described in Example 1, specifically includes the following steps: 20g of waste ternary lithium-ion battery cathode material was added to 150mL of aqueous solution in reaction chamber 3 to prepare the slurry. A high-speed shear disperser was started, and the rotor speed was set to 8000rpm. Amberlite IRC747 resin was added to the adsorption chamber. Then, 98% sulfuric acid was pumped in at a S / Li molar ratio of 0.5. Ozone was then introduced at a total ozone-to-cobalt-manganese molar ratio (O3 / (Co+Mn)) of 2.0:1 to oxidize and extract lithium. During the reaction, 98% sulfuric acid solution was continuously pumped in to control the pH of the system solution at 2, and the reaction temperature was 20℃. Simultaneously with the lithium extraction reaction, sufficient Amberlite IRC747 resin pre-filled in the adsorption chamber was used to adsorb Ni in adsorption chamber 4. 2+ Adsorption was carried out. After 4 hours of reaction, the piston 7 at the bottom of adsorption chamber 4 was opened to release and collect the material in adsorption chamber 4 for solid-liquid separation, obtaining the adsorbed ion exchange resin and part of the lithium extraction leachate. The solution in reaction chamber 3 was poured out and solid-liquid separation was performed to obtain a pure lithium extraction leachate and a leachate residue enriched with cobalt and manganese. A saturated sodium carbonate solution was added to the lithium extraction leachate, and the mixture was heated in a water bath at 95°C for 70 minutes. After mixing, stirring, and filtration, a white precipitate was obtained. The white precipitate was washed to obtain lithium carbonate. The adsorbed ion exchange resin was washed with 0.8 mol / L sulfuric acid solution for 45 minutes to obtain a pure nickel sulfate solution.

[0032] Example 4: A method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously separating nickel and lithium, using the apparatus described in Example 1, specifically includes the following steps: 20g of waste ternary lithium-ion battery cathode material was added to 200mL of aqueous solution in reaction chamber 3 to prepare the slurry. A high-speed shear disperser was started, and the rotor speed was set to 4000rpm. Amberlite IRC747 resin was added to the adsorption chamber. Then, 98% sulfuric acid was pumped in at a S / Li molar ratio of 0.5. Ozone was then introduced at a total ozone-to-cobalt-manganese molar ratio (O3 / (Co+Mn)) of 2.5:1 to oxidize and extract lithium. During the reaction, 98% sulfuric acid solution was continuously pumped in to control the pH of the system solution at 5, and the reaction temperature was 80℃. Simultaneously with the lithium extraction reaction, sufficient Amberlite IRC747 resin pre-filled in the adsorption chamber was used to adsorb Ni in adsorption chamber 4. 2+Adsorption was carried out. After 10 hours of reaction, the piston 7 at the bottom of adsorption chamber 4 was opened to release and collect the material in adsorption chamber 4 for solid-liquid separation, obtaining the adsorbed ion exchange resin and part of the lithium extraction leachate. The solution in reaction chamber 3 was poured out and solid-liquid separation was performed to obtain a pure lithium extraction leachate and a leachate residue enriched with cobalt and manganese. A saturated sodium carbonate solution was added to the lithium extraction leachate, and the mixture was heated in a water bath at 80°C for 100 minutes. After mixing, stirring, and filtration, a white precipitate was obtained. The white precipitate was washed to obtain lithium carbonate. The adsorbed ion exchange resin was washed with a 1.0 mol / L sulfuric acid solution for 30 minutes to obtain a pure nickel sulfate solution.

[0033] Comparative Example 1: The difference between this comparative example and Example 2 is that the sulfuric acid is added in a different way. The sulfuric acid is added directly and continuously to the reaction system and mixed (i.e., without creating a strong acid microenvironment at the center of the tip). The pH of the solution is controlled at 3.5. Other parameters and operations are the same as in Example 2.

[0034] Comparative Example 2: The difference between this comparative example and Example 3 is that after introducing ozone, the high-speed shear disperser is not turned on (no physical reinforcement), while the other processes and parameters are exactly the same as in Example 3.

[0035] The ion concentrations in the nickel sulfate solution and lithium extraction leachate obtained after the reaction in the above examples and comparative examples were tested. The leaching rates of each metal in the waste ternary cathode material are shown in Table 1. Ni 2+ The adsorption rate and the final lithium carbonate purity results are shown in Table 2.

[0036] Table 1. Leaching rates of valuable metals in waste ternary lithium battery cathode materials

[0037] Table 2 Ni 2+ Adsorption rate and final lithium carbonate purity

[0038] The experimental results in Tables 1 and 2 show that in Comparative Example 1, the pH of the reaction system was controlled at 3.5 by continuously adding a small amount of 98% concentrated sulfuric acid. Under this condition, the stable layered structure of the cathode material was not effectively destroyed, hindering lithium ion intercalation and deintercalation, resulting in a reduced deintercalation rate. Therefore, at the same leaching time as in Example 2, the lithium leaching rate was relatively low. Comparative Example 2 did not introduce physical reinforcement, resulting in weak particle collision intensity and low frequency, which was also unfavorable for the destruction of the layered structure, and the lithium intercalation and deintercalation rate also decreased accordingly. Furthermore, the solution fluidity within the system was poor, and the adsorption resin was only immersed in the solution, resulting in insufficient contact between the solution and the resin, leading to Ni… 2+ The adsorption rate decreased significantly.

Claims

1. A device for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation, characterized in that, include: A reaction vessel, the interior of which is divided into a reaction chamber and an adsorption chamber by a partition; the partition is provided with channels that allow ions to pass through; A high-speed shear disperser is installed in the middle of the reaction chamber; The reaction chamber is connected to an ozone generator and a peristaltic pump.

2. The apparatus according to claim 1, characterized in that, The separator is a partition plate integrally formed with the reaction vessel, and the partition plate has ion channels formed by multiple through holes; filter cloth covering the ion channels is provided on both sides of the partition plate.

3. The apparatus according to claim 1, characterized in that, The adsorption chamber has an openable and closable discharge port located on the side wall near the bottom.

4. The apparatus according to claim 1, characterized in that, The blade of the high-speed shear disperser is located in the central area of ​​the reaction chamber; a stainless steel pipe is connected to the end of the ozone generator outlet pipe and the end of the peristaltic pump delivery pipe, and the outlet end of the stainless steel pipe extends directly to the center of the end of the blade of the high-speed shear disperser.

5. A method for preferentially extracting lithium and nickel from waste ternary lithium battery cathode materials and simultaneously achieving nickel-lithium separation using the apparatus described in any one of claims 1 to 4, characterized in that, Includes the following steps: (1) In the reaction chamber, waste ternary lithium battery cathode material is mixed with water to form a slurry, and the high-speed shear disperser is started; (2) Add sufficient amount of ion exchange resin for selective adsorption of nickel ions into the adsorption chamber; (3) Acid and oxidant ozone are added to the reaction system in the reaction chamber through a peristaltic pump and an ozone generator, respectively, and a leaching reaction is carried out under oxidizing and acidic conditions to selectively leach lithium and nickel in the cathode material, wherein nickel is leached as Ni 2+ Form enters the solution; (4) During the leaching reaction, acid solution is continuously added through a peristaltic pump to maintain the pH of the system in the range of 2-5; at the same time, the centrifugal flow field generated by the high-speed shear disperser drives the Ni-containing fluid. 2+ The solution continuously flows through the adsorption chamber, containing Ni 2+ Nickel is simultaneously adsorbed by ion exchange resin, thus achieving separation of nickel from lithium in the leachate.

6. The method according to claim 5, characterized in that, In step (3), the acid is introduced into the center of the end of the high-speed shear disperser blade to participate in the reaction; the amount of ozone used satisfies the total molar ratio of ozone to cobalt and manganese of 1.5-3.0:

1.

7. The method according to claim 5, characterized in that, In step (3), the leaching reaction temperature is 20℃-80℃, the reaction time is 4 hours-10 hours, and the solid-liquid ratio of the leaching reaction is 100-500g / L.

8. The method according to claim 7, characterized in that, In step (3), concentrated sulfuric acid with a concentration of 98% is pumped in first according to the S / Li molar ratio of 0.5 to form a strong acid environment in the local area of ​​the reaction system. Then, acid is continuously or intermittently added during the reaction to maintain the pH value of the system.

9. The method according to claim 5, characterized in that, In step (2), when the high-speed shear disperser is started, its rotation speed is controlled to be 4000 rpm-8000 rpm.

10. The method according to claim 5, characterized in that, Following step (4), the following is also included: The leachate and the leaching residue containing cobalt and manganese in the reaction chamber are separated; then, sodium carbonate solution is added to the leachate to precipitate lithium carbonate product, wherein the precipitation is carried out under heating conditions at a heating temperature of 80℃-95℃; after the reaction is completed, the ion exchange resin in the adsorption chamber is soaked in 0.5-1 mol / L sulfuric acid solution for 30-60 min to obtain a pure nickel sulfate solution.

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