CN115074551B - A synergistic extraction method for selective separation of lithium and transition metals from spent batteries using hydrophobic deep eutectic solvents - Google Patents

Abstract

The application discloses a synergistic extraction method for selectively separating lithium and transition metal from waste batteries by using a hydrophobic eutectic solvent, belongs to the technical field of hydrometallurgy, provides a synergistic extraction method with good separation and extraction effects, and particularly discloses a hydrophobic eutectic and tributyl phosphate (TBP) synergistic extractant and a method for separating lithium and transition metal from waste lithium battery leachate. The method comprises the following steps: (1) configuring a hydrophobic eutectic solvent; (2) configuring an extracted organic phase; (3) nickel cobalt manganese co-extraction; (4) back extraction of nickel, cobalt and manganese; (5) lithium precipitation. The application has good extraction effect on nickel cobalt manganese transition metal, the purity of lithium in the residual water phase is high, the efficient recovery of valuable metals in the waste lithium battery anode material leaching solution is realized, and the used eutectic solvent has small pollution, simple synthesis and low price, thus being a novel green solvent.

Description

A method for selective separation of lithium and transition from spent batteries using hydrophobic deep eutectic solvents Synergistic extraction methods for metals

Technical field

The invention belongs to the technical field of hydrometallurgy, and in particular relates to a hydrophobic deep eutectic solvent and tributyl phosphate synergistic extraction agent and a method for extracting and separating lithium and transition metals in waste lithium battery leachate.

Background technique

In an era when the decarbonization of energy and transportation systems has become one of the most important international challenges, lithium-ion batteries (LIB) are widely used in electronic equipment, electric vehicles, renewable energy storage, etc. due to their excellent energy storage capabilities. Reduce transportation’s dependence on fossil fuels. As a key metal element in lithium-ion batteries, lithium has attracted widespread attention due to its light weight. It is expected that the demand for lithium carbonate will exceed 5 million tons by 2025. According to global average recyclable content (RC) data, transition metals rank first among all recycled elements (especially nickel and cobalt), which will lead to the depletion of natural resources. The total market for automotive lithium-ion batteries alone is expected to reach $221 billion by 2024. However, the increase in the production of lithium-ion batteries has not only led to serious shortages of lithium, nickel and cobalt. Used lithium-ion batteries will also seriously pollute the environment, and the content and purity of valuable metals in them are higher than those in nature. If not recycled, it will cause It is a huge waste of resources and does not conform to the concept of clean energy and resource utilization.

At present, the common recycling methods of waste lithium batteries are mainly pyrometallurgy and hydrometallurgy processes. The hydrometallurgical process has the characteristics of high selectivity, low energy consumption, and no harmful gases. It is more in line with the concept of green environmental protection than the pyrometallurgical process. In the hydrometallurgical process, the battery is first pretreated by various physical methods, and then various metals are dissolved in acid, and the acid leachate of Li, Co, Ni and Mn is obtained after purification. Hydrochloric acid or sulfuric acid is more economical than other leaching agents and is commonly used for acid reduction leaching of metals in lithium-ion batteries during hydrometallurgical processes. Among various metal recovery methods, solvent extraction is widely used for metal separation due to its simple operation, high recovery rate, and good adjustability.

CN112442596A discloses a method for separating nickel, cobalt and manganese from batteries containing nickel, cobalt and manganese. Nickel, cobalt and manganese are separated step by step through multi-stage countercurrent extraction using a carboxylic acid extractant. CN111850302B discloses a method for separating metals from waste lithium batteries using diketone compounds as extraction agents and organic phosphine compounds as co-extraction agents. After multi-stage countercurrent extraction, the extraction rate of nickel, cobalt and manganese reaches more than 99%. However, most of these extraction processes require multi-stage extraction, which increases the loss of the extraction agent to a certain extent, which not only increases the cost, but also causes a waste of resources. At the same time, the use of these traditional extraction agents not only has limited extraction effects, but also is restricted by the characteristics of volatile, environmentally polluting, and toxic extractants. Therefore, developing an extraction method that not only has high extraction efficiency, is simple, and is also environmentally friendly is needed. The "green solvent" is crucial.

Contents of the invention

In response to the above problems, the present invention uses a hydrophobic eutectic and tributyl phosphate to collaboratively extract nickel, cobalt and manganese in waste lithium batteries, leaving lithium in the raffinate. Single-stage extraction can achieve higher extraction and separation effects. , which is environmentally friendly and has low operating costs.

In order to achieve the above objects, the present invention adopts the following technical solutions:

(1) Prepare the water phase: simulate the components of the waste lithium battery leachate, and prepare the water phase containing lithium, nickel, cobalt and manganese metal ions;

(2) Prepare a hydrophobic deep eutectic solvent: heat and mix lidocaine and n-decanoic acid to obtain a hydrophobic deep eutectic solvent;

(3) Prepare organic phase: mix the hydrophobic deep eutectic solvent obtained in step (2) and tributyl phosphate to obtain an organic phase;

(4) Add the organic phase obtained in step (3) to the aqueous phase obtained in step (1) for mixing and extraction, and centrifuge to separate the phases to obtain a nickel-cobalt-manganese-loaded organic phase and a lithium-containing raffinate;

(5) Add a precipitating agent to the lithium-containing raffinate in step (4) to obtain lithium carbonate precipitation;

(6) Add the stripping agent to the nickel-cobalt-manganese-loaded organic phase in step (4) to obtain a nickel-cobalt-manganese stripping liquid and a regenerated organic phase;

Further, in step (1), the pH of the aqueous phase of the simulated waste battery leachate is 2 to 6, and the valuable metal contents are Li=300~400mg/L, Ni=1300~1500mg/L, Co=600~700mg/L, and Mn. =800～900mg/L.

Further, lidocaine and n-decanoic acid in the hydrophobic deep eutectic solvent prepared in step (2) are combined through hydrogen bonding, and the ratio of the amounts of substances is 1:1. Heat and melt n-decanoic acid, add it to lidocaine, and mix under 50°C water bath heating conditions to obtain a hydrophobic deep eutectic solvent.

Further, the organic phase prepared in step (3) contains the following structural formula:

Further, the ratio of the volume of tributyl phosphate to the hydrophobic eutectic in the organic phase prepared in step (3) = 6:4~4:6;

Further, the extraction process parameters in step (4) are the volume ratio of the added aqueous phase and the organic phase (A/O)=3:1~1:3, the extraction temperature is 10~30°C, and the extraction level is 1. , the mixing time is 20~30min, the mixing speed is 200~500r/min, the aqueous phase and the organic phase are fully mixed and placed in a centrifuge, the centrifugation speed is 6000~8000r/min, the centrifugation time is 10 The phases are separated for ~30 minutes to obtain the nickel-cobalt-manganese-loaded organic phase and the lithium-containing raffinate.

Further, the precipitant added in step (5) is 1.5 mol/sodium carbonate solution, and the ratio of the volume of the added sodium carbonate to the lithium-containing raffinate is 2.

Further, the back-extraction process of step (6) uses 2 mol/L HCl as the back-extraction agent, and the back-extraction parameter is the volume ratio of the added hydrochloric acid to the nickel-cobalt-manganese-loaded organic phase (A/O) = 2:1. The temperature is 24°C, the back-extraction level is level 1, the mixing time is 30 minutes, the mixing speed is 300r/min, mix thoroughly and then placed in a centrifuge, the centrifugation speed is 8000r/min, the centrifugation time is 10min The phases are then separated to obtain the nickel-cobalt-manganese stripping solution and the regenerated organic phase.

Description of the drawings

Figure 1 is a process flow chart of the extraction and separation method of valuable metals in waste lithium battery leachate provided by the present invention.

The present invention will be further described in detail below with examples. However, the following examples are only simple examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention shall be determined by the claims.

Detailed ways

In order to better illustrate the present invention and facilitate understanding of the technical solutions of the present invention, typical but non-limiting examples of the present invention are as follows:

Example 1

This embodiment provides a synergistic extraction agent between a hydrophobic deep eutectic solvent and tributyl phosphate and its method for extracting and separating lithium and transition metals in waste lithium battery leachate, as shown in Figure 1.

The components of the acid leachate of the simulated waste lithium battery in this embodiment are as follows:

element Li Ni Co Mn Content(mg/L) 377.9 1502 601.9 885.3

According to the extraction and separation method described in this example, the prepared simulated waste lithium battery aqueous phase has pH=2;

In the extraction and separation method described in this embodiment, lidocaine and n-decanoic acid in the prepared hydrophobic deep eutectic solvent are combined through hydrogen bonding, and the ratio of the amounts of substances is 1:1. Heat and melt n-decanoic acid, add it to lidocaine, and mix under 50°C water bath heating conditions to obtain a hydrophobic deep eutectic solvent;

In the extraction and separation method described in this embodiment, the configured hydrophobic deep eutectic solvent is added to tributyl phosphate, where the volume ratio of the added tributyl phosphate to the hydrophobic deep eutectic is 6:4, to obtain The organic phase;

In the extraction and separation method described in this embodiment, the configured organic phase is added to the aqueous phase. The extraction process parameters are the volume ratio of the aqueous phase to the organic phase (A/O) = 2:1, and the extraction temperature is 10°C. The extraction level is level 1. The mixing time is 20 minutes and the rotation speed is 200 r/min. After thorough mixing, place it in a centrifuge at a centrifugal speed of 6000 r/min. After centrifugation for 10 minutes, the phases are separated to obtain the nickel-cobalt-manganese-loaded organic phase and the lithium-containing extract. Remaining liquid.

In the extraction and separation method described in this embodiment, a sodium carbonate solution with a concentration of 1.5 mol/L is added to the lithium-containing raffinate. The volume ratio of the added sodium carbonate solution to the lithium-containing raffinate is 2:1, and the precipitation is sufficient. After washing, a lithium carbonate solution is obtained.

In the extraction and separation method described in this embodiment, the back-extraction process uses 2 mol/L HCl as the back-extraction agent. The back-extraction parameters are: the volume ratio of the added HCl to the nickel-cobalt-manganese loaded organic phase (A/O) = 2: 1. The stripping temperature is 24°C, the stripping level is 1, the mixing time is 30min, the rotation speed is 300r/min, mix thoroughly and place it in a centrifuge, the centrifugation speed is 8000r/min, the centrifugation time is After 10 minutes, the phases were separated to obtain the nickel-cobalt-manganese stripping solution and the regenerated organic phase.

The extraction experimental results of Example 1 are as follows:

element Initial solution concentration (mg/L) Concentration of raffinate (mg/L) Extraction rate Li 377.9 348.8 7.70% Ni 1502 12.8 99.15% Co 601.9 13 97.84% Mn 885.3 67.8 92.34%

In this embodiment, after single-stage extraction, the extraction rate of nickel, cobalt and manganese reached more than 92%. At the same time, a high-purity lithium salt solution was obtained in the raffinate, achieving effective separation of lithium and transition metals in spent lithium batteries. .

Example 2

This embodiment provides a synergistic extraction agent between a hydrophobic deep eutectic solvent and tributyl phosphate and its method for extracting and separating lithium and transition metals in waste lithium battery leachate, as shown in Figure 1.

The components of the acid leachate of the simulated waste lithium battery in this embodiment are as follows:

element Li Ni Co Mn Content(mg/L) 377.9 1502 601.9 885.3

According to the extraction and separation method described in this example, the prepared simulated waste lithium battery aqueous phase has pH=6;

In the extraction and separation method described in this embodiment, lidocaine and n-decanoic acid in the prepared hydrophobic deep eutectic solvent are combined through hydrogen bonding, and the ratio of the amounts of substances is 1:1. Heat and melt n-decanoic acid, add it to lidocaine, and mix under 50°C water bath heating conditions to obtain a hydrophobic deep eutectic solvent;

In the extraction and separation method described in this embodiment, the configured hydrophobic deep eutectic solvent is added to tributyl phosphate, where the volume ratio of the added tributyl phosphate to the hydrophobic deep eutectic is 4:6, to obtain The organic phase;

In the extraction and separation method described in this embodiment, the configured organic phase is added to the aqueous phase. The extraction process parameters are the volume ratio of the aqueous phase to the organic phase (A/O) = 2:1, and the extraction temperature is 30°C. The extraction level is level 1. The mixing time is 30 minutes and the rotation speed is 500 r/min. After thorough mixing, it is placed in a centrifuge at a centrifugal speed of 8000 r/min. After centrifugation for 30 minutes, the phases are separated to obtain the nickel-cobalt-manganese-loaded organic phase and lithium-containing organic phase. raffinate.

In the extraction and separation method described in this embodiment, a sodium carbonate solution with a concentration of 1.5 mol/L is added to the lithium-containing raffinate. The volume ratio of the added sodium carbonate solution to the lithium-containing raffinate is 2:1, and the precipitation is sufficient. After washing, a lithium carbonate solution is obtained.

In the extraction and separation method described in this embodiment, the back-extraction process uses 2 mol/L HCl as the back-extraction agent. The back-extraction parameters are: the volume ratio of the added HCl to the nickel-cobalt-manganese loaded organic phase (A/O) = 2: 1. The stripping temperature is 24°C, the stripping level is 1, the mixing time is 30min, the rotation speed is 300r/min, mix thoroughly and place it in a centrifuge, the centrifugation speed is 8000r/min, the centrifugation time is After 15 minutes, the phases were separated to obtain the nickel-cobalt-manganese stripping solution and the regenerated organic phase.

The extraction experimental results of Example 2 are as follows:

element Initial solution concentration (mg/L) Concentration of raffinate (mg/L) Extraction rate Li 377.9 323.7 14.34% Ni 1502 2.2 99.85% Co 601.9 1.9 99.68% Mn 885.3 16.6 98.12%

In this embodiment, after single-stage extraction, the extraction rate of nickel, cobalt and manganese reaches 98%. At the same time, a high-purity lithium salt solution is obtained in the raffinate, achieving effective separation of lithium and transition metals in spent lithium batteries.

Example 3

This embodiment provides a synergistic extraction agent between a hydrophobic deep eutectic solvent and tributyl phosphate and its method for extracting and separating lithium and transition metals in waste lithium battery leachate, as shown in Figure 1.

The components of the acid leachate of the simulated waste lithium battery in this embodiment are as follows:

element Li Ni Co Mn Content(mg/L) 360.9 1453 587.1 862.8

According to the extraction and separation method described in this example, the prepared simulated waste lithium battery aqueous phase has pH=3;

In the extraction and separation method described in this embodiment, lidocaine and n-decanoic acid in the prepared hydrophobic deep eutectic solvent are combined through hydrogen bonding, and the ratio of the amounts of substances is 1:1. Heat and melt n-decanoic acid, add it to lidocaine, and mix under 50°C water bath heating conditions to obtain a hydrophobic deep eutectic solvent;

In the extraction and separation method described in this embodiment, the configured hydrophobic deep eutectic solvent is added to tributyl phosphate, where the volume ratio of the added tributyl phosphate to the hydrophobic deep eutectic is 4:6, to obtain The organic phase;

In the extraction and separation method described in this embodiment, the configured organic phase is added to the aqueous phase. The extraction process parameters are the volume ratio of the aqueous phase to the organic phase (A/O) = 3:1, and the extraction temperature is 24°C. The extraction level is level 1. The mixing time is 30 minutes and the rotation speed is 300 r/min. Mix thoroughly and place it in a centrifuge. The centrifugation speed is 8000 r/min. Centrifuge for 10 minutes and then separate the phases. The nickel-cobalt-manganese-loaded organic phase and lithium-containing raffinate are obtained.

In the extraction and separation method described in this embodiment, a sodium carbonate solution with a concentration of 1.5 mol/L is added to the lithium-containing raffinate. The volume ratio of the added sodium carbonate solution to the lithium-containing raffinate is 2:1, and the precipitation is sufficient. After washing, a lithium carbonate solution is obtained.

In the extraction and separation method described in this embodiment, the back-extraction process uses 2 mol/L HCl as the back-extraction agent. The back-extraction parameters are: the volume ratio of the added HCl to the nickel-cobalt-manganese loaded organic phase (A/O) = 2: 1. The stripping temperature is 24°C, the stripping level is 1, the mixing time is 30min, the rotation speed is 300r/min, mix thoroughly and place it in a centrifuge, the centrifugation speed is 8000r/min, the centrifugation time is After 10 minutes, the phases were separated to obtain the nickel-cobalt-manganese stripping solution and the regenerated organic phase.

The extraction experimental results of Example 3 are as follows:

element Initial solution concentration (mg/L) Concentration of raffinate (mg/L) Extraction rate Li 360.1 306.9 14.96% Ni 1453 18.7 98.71% Co 587.1 13.9 97.63% Mn 862.8 51.9 93.98%

In this embodiment, after single-stage extraction, the extraction rate of nickel, cobalt and manganese reaches 93%. At the same time, a high-purity lithium salt solution is obtained in the raffinate, achieving effective separation of lithium and transition metals in spent lithium batteries.

Example 4

This embodiment provides a synergistic extraction agent between a hydrophobic deep eutectic solvent and tributyl phosphate and its method for extracting and separating lithium and transition metals in waste lithium battery leachate, as shown in Figure 1.

The components of the acid leachate of the simulated waste lithium battery in this embodiment are as follows:

element Li Ni Co Mn Content(mg/L) 360.9 1453 587.1 862.8

According to the extraction and separation method described in this example, the prepared simulated waste lithium battery aqueous phase has pH=3;

In the extraction and separation method described in this embodiment, lidocaine and n-decanoic acid in the prepared hydrophobic deep eutectic solvent are combined through hydrogen bonding, and the ratio of the amounts of substances is 1:1. Heat and melt n-decanoic acid, add it to lidocaine, and mix under 50°C water bath heating conditions to obtain a hydrophobic deep eutectic solvent;

In the extraction and separation method described in this embodiment, the configured hydrophobic deep eutectic solvent is added to tributyl phosphate, where the volume ratio of the added tributyl phosphate to the hydrophobic deep eutectic is 4:6, to obtain The organic phase;

In the extraction and separation method described in this embodiment, the configured organic phase is added to the aqueous phase. The extraction process parameters are the volume ratio of the aqueous phase to the organic phase (A/O) = 1:3, and the extraction temperature is 24°C. The extraction level is level 1. The mixing time is 30 minutes and the rotation speed is 300 r/min. After thorough mixing, it is placed in a centrifuge at a centrifugal speed of 8000 r/min. After centrifugation for 10 minutes, the phases are separated to obtain the nickel-cobalt-manganese-loaded organic phase and lithium-containing organic phase. raffinate.

In the extraction and separation method described in this embodiment, a sodium carbonate solution with a concentration of 1.5 mol/L is added to the lithium-containing raffinate. The volume ratio of the added sodium carbonate solution to the lithium-containing raffinate is 2:1, and the precipitation is sufficient. After washing, a lithium carbonate solution is obtained.

In the extraction and separation method described in this embodiment, the back-extraction process uses 2 mol/L HCl as the back-extraction agent. The back-extraction parameters are: the volume ratio of the added HCl to the nickel-cobalt-manganese loaded organic phase (A/O) = 2: 1. The stripping temperature is 24°C, the stripping level is 1, the mixing time is 30min, the rotation speed is 300r/min, mix thoroughly and place it in a centrifuge, the centrifugation speed is 8000r/min, the centrifugation time is After 10 minutes, the phases were separated to obtain the nickel-cobalt-manganese stripping solution and the regenerated organic phase.

The extraction experimental results of Example 4 are as follows:

element Initial solution concentration (mg/L) Concentration of raffinate (mg/L) Extraction rate Li 360.1 299.9 16.90% Ni 1453 0.8 99.94% Co 587.1 1.2 99.80% Mn 862.8 6.5 99.25%

In this embodiment, after single-stage extraction, the extraction rate of nickel, cobalt and manganese reaches 99%. At the same time, a high-purity lithium salt solution is obtained in the raffinate, achieving effective separation of lithium and transition metals in spent lithium batteries.

Example 5

This embodiment provides a synergistic extraction agent between a hydrophobic deep eutectic solvent and tributyl phosphate and its method for extracting and separating lithium and transition metals in waste lithium battery leachate, as shown in Figure 1.

The components of the acid leachate of the simulated waste lithium battery in this embodiment are as follows:

According to the extraction and separation method described in this example, the prepared simulated waste lithium battery aqueous phase has pH=3;

In the extraction and separation method described in this embodiment, lidocaine and n-decanoic acid in the prepared hydrophobic deep eutectic solvent are combined through hydrogen bonding, and the ratio of the amounts of substances is 1:1. Heat and melt n-decanoic acid, add it to lidocaine, and mix under 50°C water bath heating conditions to obtain a hydrophobic deep eutectic solvent;

In the extraction and separation method described in this embodiment, the configured hydrophobic deep eutectic solvent is added to tributyl phosphate, where the volume ratio of the added tributyl phosphate to the hydrophobic deep eutectic is 4:6, to obtain The organic phase;

In the extraction and separation method described in this embodiment, the configured organic phase is added to the aqueous phase. The extraction process parameters are the volume ratio of the aqueous phase to the organic phase (A/O) = 1:2, and the extraction temperature is 24°C. The extraction level is level 1. The mixing time is 30 minutes and the rotation speed is 300 r/min. After thorough mixing, it is placed in a centrifuge at a centrifugal speed of 8000 r/min. After centrifugation for 10 minutes, the phases are separated to obtain the nickel-cobalt-manganese-loaded organic phase and lithium-containing organic phase. raffinate.

In the extraction and separation method described in this embodiment, a sodium carbonate solution with a concentration of 1.5 mol/L is added to the lithium-containing raffinate. The volume ratio of the added sodium carbonate solution to the lithium-containing raffinate is 2:1, and the precipitation is sufficient. After washing, a lithium carbonate solution is obtained.

In the extraction and separation method described in this embodiment, the back-extraction process uses 2 mol/L HCl as the back-extraction agent. The back-extraction parameters are: the volume ratio of the added HCl to the nickel-cobalt-manganese loaded organic phase (A/O) = 2: 1. The stripping temperature is 24°C, the stripping level is 1, the mixing time is 30min, the rotation speed is 300r/min, mix thoroughly and place it in a centrifuge, the centrifugation speed is 8000r/min, the centrifugation time is After 10 minutes, the phases were separated to obtain the nickel-cobalt-manganese stripping solution and the regenerated organic phase.

The extraction experimental results of Example 5 are as follows:

element Initial solution concentration (mg/L) Concentration of raffinate (mg/L) Extraction rate Li 377.9 307.3 18.68% Ni 1502 0.6 99.96% Co 601.9 1.3 99.78% Mn 885.3 9.2 98.96%

In this embodiment, after single-stage extraction, the extraction rate of nickel, cobalt and manganese reaches 98%. At the same time, a high-purity lithium salt solution is obtained in the raffinate, achieving effective separation of lithium and transition metals in spent lithium batteries.

Claims (5)

1. A synergistic extraction method for selectively separating lithium and transition metals from waste batteries using a hydrophobic eutectic solvent, comprising the steps of:

(1) Preparing an aqueous phase: simulating the components of the waste lithium battery leaching solution, and preparing to obtain a water phase containing lithium, nickel, cobalt and manganese metal ions; wherein the pH value of the water phase is 2-6, the content of valuable metals is Li=300-400 mg/L, ni=1300-1500 mg/L, co=600-700 mg/L and Mn=800-900 mg/L respectively;

(2) Preparing a hydrophobic eutectic solvent: the lidocaine and the n-decanoic acid are combined through hydrogen bonding, and the mass ratio is 1:1; heating and melting n-decanoic acid, adding the melted n-decanoic acid into lidocaine, and mixing under the water bath heating condition of 50 ℃ to obtain a hydrophobic eutectic solvent;

(3) Preparing an organic phase: mixing the hydrophobic eutectic solvent obtained in the step (2) with tributyl phosphate to obtain an organic phase; tributyl phosphate to hydrophobic eutectic volume ratio in the organic phase = 6:4 to 4:6;

(4) Adding the organic phase obtained in the step (3) into the water phase obtained in the step (1) for mixed extraction, and obtaining a nickel-cobalt-manganese loaded organic phase and a lithium-containing raffinate after centrifugal phase separation;

(5) Adding a precipitant into the lithium-containing raffinate in the step (4) to obtain lithium carbonate precipitate;

(6) And (3) adding a stripping agent into the nickel-cobalt-manganese loaded organic phase in the step (4) to obtain nickel-cobalt-manganese stripping solution and a regenerated organic phase.

2. The extraction process of claim 1, wherein the organic phase formulated in step (3) comprises the following structural formula:

3. the extraction method according to claim 1, wherein in the step (4), the extraction process parameters are the volume ratio of the added aqueous phase to the organic phase, namely, a/o=3:1-1:3, the extraction temperature is 10-30 ℃, the extraction stage number is 1, the mixing and stirring time is 20-30 min, the mixing and stirring speed is 200-500 r/min, the aqueous phase and the organic phase are fully and uniformly mixed and then placed in a centrifuge, the centrifugation speed is 6000-8000 r/min, and the centrifugation time is 10-30 min for phase separation, so as to obtain the nickel-cobalt-manganese loaded organic phase and the lithium-containing raffinate.

4. The extraction process according to claim 1, wherein the precipitant added in step (5) is 1.5 mol/sodium carbonate solution and the ratio of the added sodium carbonate to the volume of the lithium-containing raffinate is 2.

5. The extraction method according to claim 1, wherein the step (6) of stripping process uses 2mol/L HCl as stripping agent, the stripping parameter is the volume ratio of added hydrochloric acid to nickel cobalt manganese loaded organic phase, i.e. a/o=2:1, the stripping temperature is 24 ℃, the stripping stage number is 1, the mixing stirring time is 30min, the mixing stirring speed is 300r/min, the fully mixed solution is placed in a centrifuge, the centrifugal speed is 8000r/min, the centrifugal time is 10min, and then phase separation is carried out to obtain nickel cobalt manganese stripping solution and regenerated organic phase.