Processing of lithium-ion battery electrode powder and nickel-cobalt intermediates simultaneously

Abstract

The present invention belongs to the field of resource recycling technology and discloses a process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates. The process comprises the following steps: leaching the electrode powder to obtain leachate I and leachate residue I; removing copper, iron, aluminum, calcium, and magnesium from leachate I to obtain calcium-magnesium slag and a solution after the removal of calcium and magnesium; leaching the nickel-cobalt intermediate to obtain leachate II and leachate residue II; removing iron and aluminum from leachate II and then extracting and removing zinc to obtain raffinate II; using raffinate II to leach the calcium-magnesium slag to obtain leachate III and leachate residue III; treating the leached residue III with sulfuric acid and roasting to obtain calcium-magnesium sulfate and tail gas HF; absorbing the tail gas HF with liquid caustic soda, and returning the evaporated and concentrated product to the step of removing calcium and magnesium. The present invention transforms F into valuables, realizing the resource utilization of F without the need to treat F-containing wastewater; and achieving the enrichment of valuable metals in lithium-ion battery electrode powder and nickel-cobalt intermediates, as well as the effective integration of process flows, which is beneficial to the extraction of valuable metals and can eliminate the need for a concentration process.

Description

Technical Field

[0001] The present invention belongs to the technical field of resource recycling and utilization, and specifically relates to a process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates. Background Art

[0002] With the rapid development of China's new energy vehicle industry, battery scrapping has gradually reached a significant scale, and the environmental impacts posed by the large number of discarded lithium-ion batteries cannot be ignored. Furthermore, lithium-ion batteries contain a large number of valuable metals and other renewable components, possessing a rich resource base and high recycling value. Furthermore, metals such as lithium, cobalt, and nickel are essential raw materials for power battery production. Driven by the combined forces of environmental protection, strategic value, and economic viability, and particularly with the promulgation and implementation of relevant national policies and the development and improvement of relevant standards, the recycling of used lithium-ion batteries is imperative and will generate significant economic and environmental benefits.

[0003] CN112831662A discloses a method for recycling nickel-cobalt-manganese oxide ternary positive electrode powder, wherein the nickel-cobalt-manganese oxide ternary positive electrode powder, co-leaching powder and sulfuric acid are mixed in water, reacted and leached, and the pH value of the reaction end system is controlled to be 1.5-2. 0, solid-liquid separation to obtain a leachate; the co-leached powder is at least one of nickel sulfide powder and high-grade nickel matte powder; the leachate is sequentially subjected to copper removal and iron and aluminum removal treatments to obtain a copper-, iron-, and aluminum-removed mixed solution; the copper-, iron-, and aluminum-removed mixed solution is extracted and separated with a saponified Cyanex272 extractant to obtain manganese, thereby obtaining a nickel- and cobalt-containing raffinate and a manganese-loaded organic phase; the nickel- and cobalt-containing raffinate is extracted and separated with a saponified Cyanex272 extractant to obtain a nickel-containing raffinate and a cobalt-loaded organic phase; the nickel-containing raffinate is extracted and separated with a saponified P507 extractant to obtain nickel-loaded organic phase; the manganese-loaded organic phase, cobalt-loaded organic phase, and nickel-loaded organic phase are stripped with sulfuric acid to obtain manganese sulfate, cobalt sulfate, and nickel sulfate. During the leaching process of used lithium-ion batteries, impurities such as Ca and Mg enter the solution along with the main metals, significantly impacting subsequent processes.

[0004] CN115286021A discloses a method for recovering magnesium oxide from a nickel-cobalt intermediate leach solution (in this technical field, nickel-cobalt intermediates refer to intermediates from nickel and cobalt hydrometallurgy, such as nickel-cobalt hydroxide (MHP) and crude cobalt hydroxide). The method involves extracting and enriching magnesium with an acidic phosphorus-containing extractant, then stripping it with hydrochloric acid to produce a high-concentration magnesium chloride solution. The magnesium chloride solution is then purified to remove Ni and Co impurities. The purified magnesium chloride solution is then pyrolyzed to produce primary magnesium oxide and hydrogen chloride tail gas. The hydrogen chloride tail gas is then scrubbed and absorbed to produce dilute hydrochloric acid, which is returned to the extraction system for reuse. The magnesium oxide product produced by spray pyrolysis is then crushed, hydrated, and washed with pure water to transform it into magnesium hydroxide for solid-liquid separation. The washed solid residue is then dried and calcined at high temperature to produce a high-purity magnesium oxide product. This process is complex.

[0005] In general, the current processes for processing lithium-ion battery electrode powder and nickel-cobalt intermediates are independent of each other, and each independent process is relatively complex and has low economic benefits. Summary of the Invention

[0006] The object of the present invention is to provide a process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates.

[0007] The lithium-ion battery electrode powder described in the present invention refers to the positive electrode powder or the mixed powder of positive electrode powder and negative electrode powder of binary, ternary and multi-element lithium-ion batteries.

[0008] The specific technical solutions provided by the present invention are as follows:

[0009] A process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates comprises the following steps:

[0010] Leaching the electrode powder to obtain leachate I and leach residue I;

[0011] After the copper, iron and aluminum are removed from the leachate I, calcium and magnesium are removed with NaF to obtain calcium and magnesium slag and liquid after calcium and magnesium removal;

[0012] Acid is added to the solution after calcium and magnesium removal to adjust the acidity, and then the solution is extracted with TBP extractant to obtain raffinate I and organic load phase I; the pH value of the raffinate I is adjusted, and then a portion of the raffinate I is used for stripping the organic load phase I to obtain stripping solution I, blank phase I, and stripping residue I;

[0013] The stripping residue I is returned to remove calcium and magnesium; the blank phase I is returned to the TBP extraction process; the stripping solution I is evaporated and concentrated to obtain sodium sulfate;

[0014] Leaching nickel-cobalt intermediates to obtain leachate II and leach residue II;

[0015] After the iron and aluminum are removed from the leachate II, zinc is extracted to obtain the raffinate II;

[0016] leaching calcium and magnesium residues with raffinate II to obtain leachate III and leach residue III;

[0017] Leachate III and part of the pH-adjusted raffinate I are mixed and used to extract nickel, cobalt, manganese and lithium;

[0018] The leaching residue III is treated by sulfuric acid roasting to obtain calcium magnesium sulfate and tail gas HF.

[0019] In a further preferred embodiment, the leaching reagent for leaching the electrode powder is a mixed solution of sulfuric acid and a reducing agent, the concentration of sulfuric acid in the mixed solution is 180-250 g / L, and the concentration of the reducing agent is 100-200 g / L; the solid-liquid ratio during leaching is 1 g:3-5 mL, and the leaching temperature is 85-95°C.

[0020] More preferably, the reducing agent is at least one selected from sodium metabisulfite, sodium sulfite, and hydrogen peroxide.

[0021] In a further preferred embodiment, the copper removal process of leachate I is as follows: copper removal is carried out using sodium thiosulfate at a temperature of 85-95°C.

[0022] In a further preferred embodiment, the process of removing iron and aluminum from the leachate I is as follows: adding sodium carbonate to remove iron and aluminum, the temperature is 85-95°C, and the end point pH is 3.5-5.0.

[0023] In a further preferred embodiment, sulfuric acid is added to the solution after calcium and magnesium removal to adjust the acidity to a sulfuric acid concentration of 0.1-1 mol / L.

[0024] In a further preferred embodiment, the composition of the TBP extractant is: the volume ratio of TBP to kerosene is 1:0.7-4.

[0025] The kerosene described in the present invention is 260# sulfonated kerosene commonly used in the extraction field.

[0026] In a further preferred embodiment, the O / A ratio during extraction with the TBP extractant is 1:1-3.

[0027] In the present invention, the O / A ratio is the extraction phase ratio, which refers to the volume ratio of the organic phase to the aqueous phase during liquid-liquid extraction.

[0028] In a further preferred embodiment, an alkali solution is added to adjust the pH value of the raffinate I to 3-4; preferably, the alkali solution is at least one of an aqueous solution of NaOH, sodium carbonate, and sodium bicarbonate.

[0029] In a further preferred embodiment, the return amount of the raffinate after pH adjustment is controlled so that the O / A ratio during the stripping of the organic loaded phase I is 4-15:1.

[0030] In a further preferred embodiment, the leaching agent for leaching the nickel-cobalt intermediate is a sulfuric acid solution with a concentration of 180-250 g / L; further preferably, during the leaching of the nickel-cobalt intermediate, the solid-liquid ratio is 1 g:4-6 mL, and the leaching temperature is 85-95°C.

[0031] In a further preferred embodiment, the process of removing iron and aluminum from leachate II is as follows: adding sodium carbonate to remove iron and aluminum, the temperature is 85-95°C, and the end point pH is 3.5-5.0.

[0032] In a further preferred embodiment, zinc is removed by extraction with P204.

[0033] In a further preferred embodiment, the solid-liquid ratio of the raffinate II to the calcium-magnesium slag leached is 1 g:3-5 mL.

[0034] In a further preferred embodiment, the temperature of the raffinate II for leaching calcium and magnesium slag is 85-95°C.

[0035] In a further preferred embodiment, the conditions of the sulfation roasting treatment at least include: a temperature of 150-200° C. and a time of 2-4 hours.

[0036] In a further preferred embodiment, liquid alkali is used to absorb the tail gas HF, and the product after evaporation and concentration is returned to the calcium and magnesium removal step.

[0037] The present invention has the following obvious beneficial effects:

[0038] The existing technology typically uses NaF to remove calcium and magnesium, generating large amounts of F-containing wastewater or exhaust gas, which is difficult to handle. This invention transforms F into valuable resources, eliminating the need for F-containing wastewater treatment and significantly reducing production costs. Furthermore, the F in the process flow is recycled throughout the entire system, saving production costs and ensuring harmless treatment of F.

[0039] The processing flow of nickel-cobalt intermediates is simplified, eliminating the need for complex separation processes of nickel, cobalt and magnesium.

[0040] Simultaneously process lithium-ion battery electrode powder and nickel-cobalt intermediates, and use the raffinate from the nickel-cobalt intermediate processing process to leach the calcium-magnesium slag obtained from the lithium-ion battery electrode powder processing process, thereby achieving the enrichment of valuable metals in the lithium-ion battery electrode powder and the nickel-cobalt intermediates and the effective integration of the process flow, saving production costs, being beneficial to the extraction of valuable metals and eliminating the concentration process. BRIEF DESCRIPTION OF THE DRAWINGS

[0041] Figure 1 The process flow chart provided by the present invention. DETAILED DESCRIPTION

[0042] To facilitate understanding of the present invention, the present invention will be described in more comprehensive and detailed form below in conjunction with the accompanying drawings and preferred embodiments. However, the protection scope of the present invention is not limited to the following specific embodiments.

[0043] Unless otherwise defined, all technical terms used hereinafter have the same meanings as those generally understood by those skilled in the art. The technical terms used herein are only for the purpose of describing specific embodiments and are not intended to limit the scope of protection of the present invention.

[0044] Unless otherwise specified, various raw materials, reagents, instruments and equipment used in the present invention can be purchased from the market or prepared by existing methods.

[0045] The following examples adopt Figure 1 The process flow diagram shown.

[0046] In the embodiment of the present invention, the contents of metal elements in the electrode powder, the nickel-cobalt intermediate, the solution after calcium and magnesium removal, and the leachate III were all detected by ICP (atomic emission spectrometry).

[0047] Example 1

[0048] The contents of some metals in the electrode powder are shown in Table 1.

[0049] Table 1 Content of some metals in electrode powder

[0050]

[0051] The contents of some metals in nickel-cobalt intermediates are shown in Table 2.

[0052] Table 2 Content of some metals in nickel-cobalt intermediates

[0053]

[0054] The concentration of sulfuric acid in the mixed solution for leaching the electrode powder was 250 g / L, the concentration of sodium metabisulfite was 100 g / L, the solid-liquid ratio during the leaching process was 1 g:3 mL, and the leaching temperature was 95° C. After leaching, leachate I and leach residue I were obtained.

[0055] The leachate I was treated to remove copper, iron and aluminum: sodium thiosulfate was used to remove copper at a temperature of 95°C; then sodium carbonate was added to remove iron and aluminum at a temperature of 95°C, with an end point pH of 3.5.

[0056] Continue to add NaF to leachate I and stir the reaction until no more precipitation is generated, obtaining a calcium and magnesium-removed solution and a calcium-magnesium slag. Adding NaF to leachate I not only precipitates calcium and magnesium, but also precipitates most of the lithium and a small amount of nickel, cobalt, and manganese in the calcium-magnesium slag.

[0057] The contents of some elements in the solution after calcium and magnesium removal were analyzed, and the results are shown in Table 3.

[0058] Table 3 Content of some elements in the solution after calcium and magnesium removal (g / L)

[0059]

[0060] Sulfuric acid was added to the solution after calcium and magnesium removal to adjust the concentration of the sulfuric acid to 0.5 mol / L. Extraction was then performed with a volume ratio of TBP to kerosene of 1:2, and an O / A ratio of 1:1. After extraction, raffinate I and loaded organic phase I were obtained.

[0061] The pH of raffinate I is adjusted to 3.5 using sodium hydroxide solution. A portion of the pH-adjusted raffinate I is then used to strip the loaded organic phase I, based on an O / A ratio of 10:1. This produces stripper I, a blank organic phase, and a stripper residue. Raffinate I contains nickel, cobalt, manganese, and lithium ions, while loaded organic phase I contains HF. When stripper I strips loaded organic phase I, the stripped HF combines with the nickel, cobalt, manganese, and lithium ions to form NiF2, MnF2, CoF2, and LiF precipitates, which form the stripper residue.

[0062] The blank organic phase is returned to the extraction process of the solution after calcium and magnesium removal; the stripping solution I is used to recover sodium sulfate; and the stripping residue is returned to the calcium and magnesium removal process.

[0063] The nickel-cobalt intermediate was leached with sulfuric acid solution, the concentration of the sulfuric acid solution was 250 g / L, the solid-liquid ratio during leaching was 1 g:6 mL, and the temperature during leaching was 90° C., to obtain leachate II and leach residue II.

[0064] The steps of removing iron and aluminum from leachate II are as follows: adding sodium carbonate to remove iron and aluminum, controlling pH=4.1 and temperature to 90°C, and then using P204 to extract zinc in leachate II to obtain raffinate II.

[0065] The raffinate II was used to leach calcium and magnesium residues produced during the treatment of electrode powder. The solid-liquid ratio during leaching was 1 g:5 mL, and the leaching temperature was 85° C. After leaching, leachate III and leach residue III were obtained.

[0066] The contents of some metals in leachate III were analyzed and tested, and the results are shown in Table 4.

[0067] Table 4 Content of some metals in leachate III

[0068]

[0069] The leachate III and the raffinate I which has been adjusted in pH value but not used for stripping are mixed and then used to extract nickel, cobalt, manganese and lithium.

[0070] 98% concentrated sulfuric acid is added to the leach residue III at a mass ratio of 1:1.5. After stirring and mixing, the mixture is calcined at 200°C for 3 hours to produce calcium and magnesium sulfates and tail gas HF. The tail gas HF is absorbed with liquid caustic soda and then concentrated to produce NaF, which is then returned to the step of removing calcium and magnesium from the electrode powder leachate.

[0071] Example 2

[0072] The contents of some metals in the electrode powder are shown in Table 5.

[0073] Table 5 Content of some metals in electrode powder

[0074]

[0075] The contents of some metals in nickel-cobalt intermediates are shown in Table 6.

[0076] Table 6 Content of some metals in nickel-cobalt intermediates

[0077]

[0078] The mixed solution for leaching the electrode powder contained 200 g / L sulfuric acid and 150 g / L hydrogen peroxide. The solid-liquid ratio during the leaching process was 1 g:4 mL, and the leaching temperature was 85°C. After leaching, leachate I and leach residue I were obtained.

[0079] The leachate I was treated to remove copper, iron and aluminum: sodium thiosulfate was used to remove copper at a temperature of 85°C; then sodium carbonate was added to remove iron and aluminum at a temperature of 85°C, with an end point pH of 5.0.

[0080] Continue to add NaF to leachate I and stir the reaction until no more precipitation is generated, obtaining a calcium and magnesium-removed solution and a calcium-magnesium slag. Adding NaF to leachate I not only precipitates calcium and magnesium, but also precipitates most of the lithium and a small amount of nickel, cobalt, and manganese in the calcium-magnesium slag.

[0081] The contents of some elements in the solution after calcium and magnesium removal were analyzed, and the results are shown in Table 7.

[0082] Table 7 Content of some elements in the solution after calcium and magnesium removal (g / L)

[0083]

[0084] Sulfuric acid was added to the solution after calcium and magnesium removal to adjust the concentration of the sulfuric acid to 1 mol / L. Extraction was then performed with a volume ratio of TBP to kerosene of 1:0.7. The O / A ratio during extraction was 1:2. After extraction, raffinate I and loaded organic phase I were obtained.

[0085] The pH value of the raffinate I was adjusted to 4.0 with a sodium hydroxide solution. A portion of the raffinate I after adjusting the pH value was taken according to an O / A ratio of 4:1 and then used for stripping the loaded organic phase I to obtain stripping solution I, a blank organic phase and stripping residue.

[0086] The blank organic phase is returned to the extraction process of the solution after calcium and magnesium removal; the stripping solution I is used to recover sodium sulfate; and the stripping residue is returned to the calcium and magnesium removal process.

[0087] The nickel-cobalt intermediate was leached with sulfuric acid solution, the concentration of the sulfuric acid solution was 200 g / L, the leaching solid-liquid ratio was 1 g:4 mL, and the leaching temperature was 85° C., to obtain leachate II and leach residue II.

[0088] The steps of removing iron and aluminum from leachate II are as follows: adding sodium carbonate to remove iron and aluminum, pH=5.0, temperature=95°C, and then using P204 to extract zinc in leachate II to obtain raffinate II.

[0089] The raffinate II was used to leach calcium and magnesium residues produced during the treatment of electrode powder. The solid-liquid ratio during leaching was 1 g:4 mL, and the leaching temperature was 95°C. After the leaching was completed, leachate III and leach residue III were obtained.

[0090] The contents of some metals in leachate III were analyzed and tested, and the results are shown in Table 8.

[0091] Table 8 Content of some metals in leachate III

[0092]

[0093] The leachate III and the raffinate I which has been adjusted in pH value but not used for stripping are mixed and then used to extract nickel, cobalt, manganese and lithium.

[0094] Concentrated sulfuric acid is added to the leaching residue III at a mass ratio of 1:1.5. After stirring and mixing, the mixture is calcined at 150°C for 3 hours to produce calcium and magnesium sulfates and tail gas HF. The tail gas HF is absorbed with liquid caustic soda and then concentrated to produce NaF, which is then returned to the step of removing calcium and magnesium from the electrode powder leachate.

[0095] Example 3

[0096] The contents of some metals in the electrode powder are shown in Table 9.

[0097] Table 9 Content of some metals in electrode powder

[0098]

[0099] The contents of some metals in nickel-cobalt intermediates are shown in Table 10.

[0100] Table 10 Content of some metals in nickel-cobalt intermediates

[0101]

[0102] The concentration of sulfuric acid in the mixed solution for leaching the electrode powder was 180 g / L, the concentration of sodium sulfite was 200 g / L, the solid-liquid ratio during the leaching process was 1 g:5 mL, and the leaching temperature was 90° C. After leaching, leachate I and leach residue I were obtained.

[0103] The leachate I was treated to remove copper, iron and aluminum: sodium thiosulfate was used to remove copper at a temperature of 90°C; then sodium carbonate was added to remove iron and aluminum at a temperature of 90°C, with an end point pH of 4.5.

[0104] Continue to add NaF to leachate I and stir the reaction until no more precipitation is generated, obtaining a calcium and magnesium-removed solution and a calcium-magnesium slag. Adding NaF to leachate I not only precipitates calcium and magnesium, but also precipitates most of the lithium and a small amount of nickel, cobalt, and manganese in the calcium-magnesium slag.

[0105] The contents of some elements in the liquid after calcium and magnesium removal were analyzed, and the results are shown in Table 11.

[0106] Table 11 Content of some elements in the solution after calcium and magnesium removal (g / L)

[0107]

[0108] Sulfuric acid was added to the solution after calcium and magnesium removal to adjust the concentration of the sulfuric acid to 0.1 mol / L. Extraction was then performed with a volume ratio of TBP to kerosene of 1:4, and an O / A ratio of 1:3. After extraction, raffinate I and loaded organic phase I were obtained.

[0109] The pH value of the raffinate I was adjusted to 3.5 with a sodium hydroxide solution. Based on an O / A ratio of 15:1, a portion of the raffinate I after adjusting the pH value was taken for stripping the loaded organic phase I to obtain stripping solution I, a blank organic phase and stripping residue.

[0110] The blank organic phase is returned to the extraction process of the solution after calcium and magnesium removal; the stripping solution I is used to recover sodium sulfate; and the stripping residue is returned to the calcium and magnesium removal process.

[0111] The nickel-cobalt intermediate was leached with a sulfuric acid solution having a concentration of 180 g / L, a leaching solid-liquid ratio of 1 g:5 mL, and a leaching temperature of 95° C., to obtain leachate II and leach residue II.

[0112] The steps of removing iron and aluminum from leachate II are as follows: adding sodium carbonate to remove iron and aluminum, controlling pH=4.5 and temperature to 95°C, and then using P204 to extract zinc in leachate II to obtain raffinate II.

[0113] The raffinate II was used to leach calcium and magnesium residues produced during the treatment of electrode powder. The solid-liquid ratio during leaching was 1 g:3 mL, and the leaching temperature was 90° C. After leaching, leachate III and leach residue III were obtained.

[0114] The contents of some metals in leachate III were analyzed and tested, and the results are shown in Table 12.

[0115] Table 12 Contents of some metals in leachate III

[0116]

[0117] The leachate III and the raffinate I which has been adjusted in pH value but not used for stripping are mixed and then used to extract nickel, cobalt, manganese and lithium.

[0118] Concentrated sulfuric acid is added to the leaching residue III at a mass ratio of 1:1.5. After stirring and mixing, the mixture is calcined at 200°C for 3 hours to produce calcium and magnesium sulfates and tail gas HF. The tail gas HF is absorbed with liquid caustic soda and then concentrated to produce NaF, which is then returned to the step of removing calcium and magnesium from the electrode powder leachate.

[0119] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principles of the present invention. These improvements and modifications should also be regarded as within the scope of protection of the present invention.

Claims

1. A process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates, characterized in that: The following steps are involved: Leaching the electrode powder to obtain leachate I and leach residue I; After removing copper, iron and aluminum from the leachate I, calcium and magnesium are removed using NaF to obtain calcium and magnesium slag and a liquid after calcium and magnesium removal; Acid is added to the liquid after calcium and magnesium removal to adjust the acidity, and then extracted with a TBP extractant to obtain a raffinate I and an organic loaded phase I; the pH value of the raffinate I is adjusted, and then a portion of the raffinate I is used to strip the organic loaded phase I to obtain a stripping solution I, a blank phase I, and a stripping residue I; wherein the blank phase I is returned to the TBP extractant extraction process; the stripping solution I is evaporated and concentrated to obtain sodium sulfate; Leaching nickel-cobalt intermediates to obtain leachate II and leach residue II; The leachate II is subjected to iron and aluminum removal, and zinc is extracted to obtain raffinate II; The calcium magnesium slag is leached with the raffinate II to obtain a leachate III and a leachate residue III; wherein the leachate III and the raffinate I after adjusting the pH value are mixed and used to extract nickel, cobalt, manganese and lithium; the leachate residue III is subjected to a sulfuric acid roasting treatment to obtain calcium magnesium sulfate and tail gas HF.

2. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to claim 1, characterized in that: The leaching agent for leaching the electrode powder is a mixed solution consisting of sulfuric acid and a reducing agent. The concentration of the sulfuric acid in the mixed solution is 180-250 g / L, and the concentration of the reducing agent is 100-200 g / L.

3. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to claim 2, characterized in that: The reducing agent is selected from at least one of sodium metabisulfite, sodium sulfite and hydrogen peroxide.

4. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to claim 2, characterized in that: The conditions for leaching the electrode powder at least include: a solid-liquid ratio of 1 g: 3-5 mL during leaching, and a leaching temperature of 85-95° C.

5. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: Sulfuric acid is added to the solution after calcium and magnesium removal to adjust the acidity to a concentration of 0.1-1 mol / L.

6. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The composition of the TBP extractant is as follows: the volume ratio of TBP to kerosene is 1:0.7-4.

7. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The O / A ratio during extraction with the TBP extractant is 1:1-3.

8. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: Alkali solution is added to adjust the pH value of the raffinate I to 3-4.

9. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The return amount of the raffinate I after adjusting the pH value is controlled so that the O / A ratio during the stripping of the organic load phase I is 4-15:

1.

10. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The leaching agent for leaching nickel-cobalt intermediates is a sulfuric acid solution with a concentration of 180-250 g / L.

11. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to claim 10, characterized in that: During the leaching process of nickel-cobalt intermediates, the solid-liquid ratio is 1g:4-6mL and the leaching temperature is 85-95℃.

12. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The solid-liquid ratio of calcium and magnesium slag leached from raffinate II is 1g:3-5mL.

13. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to claim 12, characterized in that: The temperature of leaching calcium and magnesium slag with raffinate II is 85-95℃.

14. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The conditions of the sulfation roasting treatment include at least: a temperature of 150-200° C. and a time of 2-4 hours.

15. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The stripping residue I is returned for removing calcium and magnesium.

16. The process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediates according to any one of claims 1 to 4, characterized in that: The tail gas HF is absorbed by liquid alkali, and the product after evaporation and concentration is returned to the calcium and magnesium removal step.

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