CN117327903A - Process for simultaneous processing of lithium-ion battery electrode powder and nickel-cobalt intermediate products - Google Patents

Abstract

The invention belongs to the technical field of resource recycling and utilization. It discloses a process for synchronously processing lithium-ion battery electrode powder and nickel-cobalt intermediate products, which includes the following steps: leaching the electrode powder to obtain leaching liquid I and leaching slag I; leaching liquid I is subjected to copper and iron removal. Aluminum, calcium and magnesium are removed to obtain calcium-magnesium slag and calcium-magnesium-removed liquid; the nickel-cobalt intermediate is leached to obtain leachate II and leaching residue II; leachate II is subjected to iron and aluminum removal, and zinc is extracted to obtain raffinate II; The raffinate II is leached from the calcium magnesium slag to obtain the leaching liquid III and the leaching residue III; the leaching residue III is subjected to sulfation and roasting treatment to obtain calcium magnesium sulfate and tail gas HF; liquid caustic soda is used to absorb the tail gas HF, and the evaporated and concentrated product is returned for decalcification Magnesium step. The invention turns F from waste into treasure and realizes the resource utilization of F without the need to treat F-containing wastewater; it realizes the enrichment of valuable metals in lithium-ion battery electrode powder and nickel-cobalt intermediate products and the effective integration of technological processes, and has It is beneficial to the extraction of valuable metals and can save the concentration process.

Description

Process for simultaneous processing of lithium-ion battery electrode powder and nickel-cobalt intermediate products

Technical field

The invention belongs to the technical field of resource recycling, and specifically relates to a process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediate products.

Background technique

With the rapid development of the country's new energy vehicle industry, battery scrapping has gradually taken shape, and the environmental problems caused by a large number of scrapped lithium-ion batteries cannot be ignored. At the same time, lithium-ion batteries contain a large amount of valuable metals and other renewable components. They contain rich resources and have extremely high recycling value. Metals such as lithium, cobalt, and nickel are basic raw materials for power battery production. Driven by the combined forces of environmental protection demands, strategic value, and economics, especially with the promulgation and implementation of relevant national policies and the formulation and improvement of relevant standards, the recycling of used lithium-ion batteries is imperative and will generate huge economic benefits. and environmental benefits.

CN112831662A discloses a recycling method of lithium nickel cobalt manganate ternary cathode powder. The lithium nickel cobalt manganate ternary cathode powder, co-leaching powder and sulfuric acid are mixed in water, reacted and leached, and the reaction end point system is controlled. The pH value is 1.5 to 2.0, and the leachate is obtained by solid-liquid separation; the co-leached powder is at least one of nickel sulfide powder and high matte nickel powder; the leachate is sequentially subjected to copper removal treatment and iron and aluminum removal treatment to obtain copper removal A mixed solution of iron and aluminum; use the saponified Cyanex272 extractant to extract and separate the manganese from the copper-removed mixed solution to obtain a nickel-cobalt-containing raffinate and a manganese-loaded organic phase; use saponified Cyanex272 to extract the nickel-cobalt-containing raffinate. The nickel-containing raffinate is extracted and separated with a saponified P507 extractant to obtain a nickel-loaded organic phase; the manganese-loaded organic phase and the cobalt-loaded organic phase are obtained. The phase and the nickel-loaded organic phase are back-extracted 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 also enter the solution along with the main metal, and the impurities will have a greater impact on subsequent processes.

CN115286021A discloses a method for recovering magnesium oxide from a leaching solution of nickel and cobalt intermediates (in this technical field, nickel and cobalt intermediates refer to intermediates of nickel and cobalt wet smelting, such as nickel and cobalt hydroxide (MHP), crude Cobalt hydroxide, etc.), first use acidic phosphorus-containing extractant to extract and enrich magnesium, and use hydrochloric acid to back-extract to obtain a high-concentration magnesium chloride solution. The magnesium chloride solution is purified and impurities are removed to remove Ni and Co impurities in the magnesium chloride solution. The purified The final magnesium chloride solution is pyrolyzed to obtain primary magnesium oxide and hydrogen chloride tail gas. The hydrogen chloride tail gas is washed and absorbed to produce dilute hydrochloric acid, which is returned to the extraction system for use. The magnesium oxide product produced by spray pyrolysis is then crushed and hydrated with pure water and washed to transform into magnesium hydroxide solid-liquid separation. After washing, the solid residue is dried and roasted at high temperature to produce a high-purity magnesium oxide product. The process is complex.

In general, the current processes for processing lithium-ion power battery electrode powder and nickel-cobalt intermediates are independent of each other, and the independent processes are relatively complex and have low economic benefits.

Contents of the invention

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

The lithium-ion battery electrode powder mentioned in the present invention refers to the positive electrode powder of binary, ternary, or multi-component lithium ion batteries or the mixed powder of positive electrode powder and negative electrode powder.

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

A process for simultaneously processing lithium-ion battery electrode powder and nickel-cobalt intermediate products, including the following steps:

Leach the electrode powder to obtain leaching liquid I and leaching residue I;

After removing copper, iron and aluminum from leaching liquid I, NaF is used to remove calcium and magnesium to obtain calcium-magnesium slag and calcium-magnesium-removed liquid;

Add acid to the liquid after calcium and magnesium removal to adjust the acidity, and then extract with TBP extractant to obtain raffinate I and organic load phase I; adjust the pH value of raffinate I, and then use part of it to strip the organic load phase I. Obtain stripping liquid I, blank phase I and stripping residue I;

The stripping residue I is returned for calcium and magnesium removal; the blank phase I is returned to the TBP extractant extraction process; the stripping liquid I is evaporated and concentrated to obtain Yuanming powder;

Leach the nickel-cobalt intermediate product to obtain leach liquid II and leach residue II;

After removing iron and aluminum from the leaching liquid II, the zinc is extracted and removed to obtain the raffinate II;

Use raffinate II to leach calcium and magnesium slag to obtain leachate III and leaching residue III;

The leachate III and the partially adjusted pH value raffinate I are mixed and used to extract nickel, cobalt, manganese and lithium;

The leaching residue III is subjected to sulfation and roasting treatment to obtain calcium magnesium sulfate and tail gas HF.

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

It is further preferred that the reducing agent is at least one selected from the group consisting of sodium metabisulfite, sodium sulfite, and hydrogen peroxide.

In a further preferred embodiment, the process of removing copper from leach solution I is: using sodium thiosulfate to remove copper at a temperature of 85-95°C.

In a further preferred solution, the process of removing iron and aluminum from leach solution I is: adding sodium carbonate to remove iron and aluminum, the temperature is 85-95°C, and the end-point pH is 3.5-5.0.

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

In a further preferred embodiment, the composition of the TBP extraction agent is: the volume ratio of TBP to kerosene is 1:0.7-4.

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

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

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

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

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

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

In a further preferred solution, the process of removing iron and aluminum from leach solution II is: adding sodium carbonate to remove iron and aluminum, the temperature is 85-95°C, and the end-point pH is 3.5-5.0.

In a further preferred embodiment, P204 is used to extract zinc.

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

In a further preferred embodiment, the temperature at which raffinate II leaches calcium and magnesium slag is 85-95°C.

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

In a further preferred embodiment, liquid caustic soda is used to absorb the tail gas HF, and the evaporated and concentrated product is returned to the calcium and magnesium removal step.

The invention has the following obvious beneficial effects:

In the existing technology, NaF is usually used to remove calcium and magnesium, which produces a large amount of F-containing wastewater or waste gas, making subsequent treatment difficult. The invention turns F from waste into treasure, realizes resource utilization of F, eliminates the need to treat F-containing wastewater, and greatly reduces production costs. Moreover, F in the process flow is circulated in the entire process system, which not only saves production costs, but also achieves harmless treatment of F.

The processing flow of intermediate nickel and cobalt products is simplified, eliminating the need for complex separation processes of nickel, cobalt and magnesium.

Simultaneous processing of lithium-ion battery electrode powder and nickel-cobalt intermediate products, using the raffinate during the treatment of nickel-cobalt intermediate products to leach the calcium-magnesium slag obtained during the processing of lithium-ion battery electrode powder, to realize the intermediate between lithium-ion battery electrode powder and nickel-cobalt intermediate products The enrichment of valuable metals in the product and the effective integration of the process flow save production costs, and are conducive to the extraction of valuable metals and can eliminate the need for concentration processes.

Description of drawings

Figure 1 is a process flow diagram provided by the present invention.

Detailed ways

In order to facilitate understanding of the present invention, the present invention will be described more comprehensively and in detail below with reference to the accompanying drawings and preferred embodiments. However, the protection scope of the present invention is not limited to the following specific embodiments.

Unless otherwise defined, all technical terms used below have the same meanings as commonly 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 the present invention.

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

The following embodiments adopt the process flow chart shown in Figure 1.

In the embodiment of the present invention, the contents of metal elements in the electrode powder, nickel-cobalt intermediate products, calcium and magnesium removal liquid, and leach liquid III are all detected by ICP (atomic emission spectrometer).

Example 1

The contents of some metals in electrode powder are shown in Table 1.

Table 1 Contents of some metals in electrode powder

The contents of some metals in nickel and cobalt intermediate products are shown in Table 2.

Table 2 Contents of some metals in nickel and cobalt intermediate products

The concentration of sulfuric acid in the mixed solution of leaching electrode powder is 250g/L, and the concentration of sodium metabisulfite is 100g/L. To leach electrode powder, the solid-liquid ratio in the leaching process is 1g:3mL, and the leaching temperature is 95°C. After leaching, leaching liquid I and leaching residue I are obtained.

The leachate I is treated to remove copper, iron and aluminum: use sodium thiosulfate to remove copper at a temperature of 95°C; then add sodium carbonate to remove iron and aluminum at a temperature of 95°C and end-point pH=3.5.

Continue to add NaF to the leaching liquid I, stir the reaction until no more precipitation is formed, and obtain the calcium and magnesium removal liquid and calcium and magnesium slag. When NaF is added to leach solution I, not only calcium and magnesium are precipitated, but most of the lithium and a small amount of nickel, cobalt, manganese, etc. are precipitated in the calcium and magnesium slag.

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

Table 3 Contents of some elements in the solution after calcium and magnesium removal (g/L)

Add sulfuric acid to the solution after calcium and magnesium removal, adjust the concentration of sulfuric acid in the solution to 0.5 mol/L, and then add an extraction agent with a volume ratio of TBP and kerosene of 1:2 for extraction. The O/A ratio during extraction is 1: 1. After extraction, raffinate I and loaded organic phase I are obtained.

Use sodium hydroxide solution to adjust the pH value of the raffinate I to 3.5, and then take part of the pH-adjusted raffinate I according to the O/A ratio of 10:1 for stripping the loaded organic phase I to obtain the stripping liquid Ⅰ. Blank organic phase and stripping residue. There are nickel, cobalt, manganese, and lithium ions in the raffinate I, and there is HF in the loaded organic phase I. When the raffinate I is stripped and loaded with the organic phase I, the stripped HF combines with nickel, cobalt, manganese, and lithium ions. NiF ₂ , MnF ₂ , CoF ₂ , and LiF precipitates are generated, which are stripping residues.

The blank organic phase is returned to the extraction process of the calcium and magnesium removal solution; the stripping liquid I is used to recover Yuanming powder; the stripping residue is returned to the calcium and magnesium removal process.

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

Steps to remove iron and aluminum from leachate II: add sodium carbonate to remove iron and aluminum, control pH = 4.1, temperature to 90°C, and then use P204 to extract zinc in leachate II to obtain raffinate II.

The raffinate II is used to leach the calcium and magnesium slag produced during the leaching process of electrode powder. The solid-liquid ratio during leaching is 1g:5mL, and the leaching temperature is 85°C. After leaching is completed, leaching liquid III and leaching residue III are obtained.

The contents of some metals in leachate III were analyzed and detected, and the results are shown in Table 4.

Table 4 Contents of some metals in leachate III

The leachate III is mixed with the pH-adjusted raffinate I that is not used for stripping and is used to extract nickel, cobalt, manganese and lithium.

Add 98% concentrated sulfuric acid to the leaching residue III. The mass ratio of leaching residue III and concentrated sulfuric acid is 1:1.5. After stirring and mixing, calcining at 200°C for 3 hours to obtain calcium magnesium sulfate and tail gas HF. Use liquid caustic soda to absorb the tail gas HF, and then concentrate to obtain NaF, which is then returned to the step of removing calcium and magnesium from the electrode powder leaching solution.

Example 2

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

Table 5 Contents of some metals in electrode powder

The contents of some metals in nickel and cobalt intermediate products are shown in Table 6.

Table 6 Contents of some metals in nickel and cobalt intermediate products

The concentration of sulfuric acid in the mixed solution of leaching electrode powder is 200g/L, and the concentration of hydrogen peroxide is 150g/L. To leach electrode powder, the solid-liquid ratio in the leaching process is 1g:4mL, and the leaching temperature is 85°C. After leaching, leaching liquid I and leaching residue I are obtained.

The leachate I is treated to remove copper, iron and aluminum: use sodium thiosulfate to remove copper at a temperature of 85°C; then add sodium carbonate to remove iron and aluminum at a temperature of 85°C and end-point pH=5.0.

Continue to add NaF to the leaching liquid I, stir the reaction until no more precipitation is formed, and obtain the calcium and magnesium removal liquid and calcium and magnesium slag. When NaF is added to leach solution I, not only calcium and magnesium are precipitated, but most of the lithium and a small amount of nickel, cobalt, manganese, etc. are precipitated in the calcium and magnesium slag.

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

Table 7 Contents of some elements in the solution after calcium and magnesium removal (g/L)

Add sulfuric acid to the solution after calcium and magnesium removal, adjust the concentration of sulfuric acid in the solution to 1 mol/L, and then add an extraction agent with a volume ratio of TBP and kerosene of 1:0.7 for extraction. The O/A ratio during extraction is 1:2 . After extraction, raffinate I and loaded organic phase I are obtained.

Use sodium hydroxide solution to adjust the pH value of raffinate I to 4.0. According to the O/A ratio of 4:1, take part of the pH-adjusted raffinate I and then use it to strip the loaded organic phase I to obtain the stripping liquid. Ⅰ. Blank organic phase and stripping residue.

The blank organic phase is returned to the extraction process of the calcium and magnesium removal solution; the stripping liquid I is used to recover Yuanming powder; the stripping residue is returned to the calcium and magnesium removal process.

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

Steps to remove iron and aluminum from leachate II: add sodium carbonate to remove iron and aluminum, pH=5.0, temperature=95°C, and then use P204 to extract zinc in leachate II to obtain raffinate II.

The raffinate II is used to leach the calcium and magnesium slag produced during the leaching process of electrode powder. The solid-liquid ratio during leaching is 1g:4mL, and the leaching temperature is 95°C. After leaching is completed, leaching liquid III and leaching residue III are obtained.

Analyze and detect the content of some metals in leachate III, and the results are shown in Table 8.

Table 8 Contents of some metals in leachate III

The leachate III is mixed with the pH-adjusted raffinate I that is not used for stripping and is used to extract nickel, cobalt, manganese and lithium.

Add concentrated sulfuric acid to the leaching residue III. The mass ratio of the leaching residue III and concentrated sulfuric acid is 1:1.5. After stirring and mixing, calcine at 150°C for 3 hours to obtain calcium magnesium sulfate and tail gas HF. Use liquid caustic soda to absorb the tail gas HF, and then concentrate to obtain NaF, which is then returned to the step of removing calcium and magnesium from the electrode powder leaching solution.

Example 3

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

Table 9 Contents of some metals in electrode powder

The contents of some metals in nickel and cobalt intermediate products are shown in Table 10.

Table 10 Contents of some metals in nickel and cobalt intermediate products

The concentration of sulfuric acid in the mixed solution of leaching electrode powder is 180g/L, and the concentration of sodium sulfite is 200g/L. To leach electrode powder, the solid-liquid ratio in the leaching process is 1g:5mL, and the leaching temperature is 90°C. After leaching, leaching liquid I and leaching residue I are obtained.

The leachate I is treated to remove copper, iron and aluminum: use sodium thiosulfate to remove copper at a temperature of 90°C; then add sodium carbonate to remove iron and aluminum at a temperature of 90°C and end-point pH=4.5.

Continue to add NaF to the leaching liquid I, stir the reaction until no more precipitation is formed, and obtain the calcium-magnesium removal liquid and calcium-magnesium slag. When NaF is added to leach solution I, not only calcium and magnesium are precipitated, but most of the lithium and a small amount of nickel, cobalt, manganese, etc. are precipitated in the calcium and magnesium slag.

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

Table 11 Contents of some elements in the solution after calcium and magnesium removal (g/L)

Add sulfuric acid to the solution after calcium and magnesium removal, adjust the concentration of sulfuric acid in the solution to 0.1 mol/L, and then add an extraction agent with a volume ratio of TBP and kerosene of 1:4 for extraction. The O/A ratio during extraction is 1: 3. After extraction, raffinate I and loaded organic phase I are obtained.

Use sodium hydroxide solution to adjust the pH value of raffinate I to 3.5. According to the O/A ratio of 15:1, take part of the adjusted pH value of raffinate I for stripping the loaded organic phase I to obtain stripping liquid I. , blank organic phase and stripping residue.

The blank organic phase is returned to the extraction process of the calcium and magnesium removal solution; the stripping liquid I is used to recover Yuanming powder; the stripping residue is returned to the calcium and magnesium removal process.

The nickel-cobalt intermediate product is leached with a sulfuric acid solution with a concentration of 180g/L. The leaching solid-liquid ratio is 1g:5mL. The temperature during leaching is 95°C to obtain leachate II and leaching residue II.

Steps to remove iron and aluminum from leachate II: add sodium carbonate to remove iron and aluminum, control pH = 4.5, temperature 95°C, and then use P204 to extract zinc in leachate II to obtain raffinate II.

The raffinate II is used to leach the calcium and magnesium slag produced during the leaching process of electrode powder. The solid-liquid ratio during leaching is 1g:3mL, and the leaching temperature is 90°C. After leaching is completed, leaching liquid III and leaching residue III are obtained.

The contents of some metals in leachate III were analyzed and detected, and the results are shown in Table 12.

Table 12 Contents of some metals in leach solution III

The leachate III is mixed with the pH-adjusted raffinate I that is not used for stripping and is used to extract nickel, cobalt, manganese and lithium.

Add concentrated sulfuric acid to the leaching residue III. The mass ratio of the leaching residue III and the concentrated sulfuric acid is 1:1.5. After stirring and mixing, calcine at 200°C for 3 hours to obtain calcium magnesium sulfate and tail gas HF. Use liquid caustic soda to absorb the tail gas HF, and then concentrate to obtain NaF, which is then returned to the step of removing calcium and magnesium from the electrode powder leaching solution.

The above are only preferred embodiments of the present invention. It should be noted that those skilled in the art can make several improvements and modifications without departing from the principles of the present invention. These improvements and modifications can also be made. should be regarded as the protection scope of the present invention.

Claims (10)

1. A process for synchronously processing electrode powder of a lithium ion battery and a nickel cobalt intermediate product is characterized by comprising the following steps:

leaching the electrode powder to obtain a leaching solution I and leaching slag I;

removing copper and iron and aluminum from the leaching solution I, and removing calcium and magnesium by using NaF to obtain calcium and magnesium slag and calcium and magnesium removed solution;

adding acid into the calcium and magnesium removed solution to adjust acidity, and then extracting with TBP extractant to obtain raffinate I and organic load phase I; regulating the pH value of the raffinate I, and then partially carrying out back extraction on the organic load phase I to obtain a back extraction liquid I, a blank phase I and back extraction slag I; wherein the empty white phase I returns to the TBP extractant extraction process; evaporating and concentrating the back extraction liquid I to obtain anhydrous sodium sulfate;

leaching the nickel cobalt intermediate product to obtain a leaching solution II and leaching slag II;

removing iron and aluminum from the leaching solution II, and extracting to remove zinc to obtain raffinate II;

leaching the calcium magnesium slag by using the raffinate II to obtain a leaching solution III and leaching slag III; wherein, the leaching solution III and the raffinate I with the pH value adjusted are mixed and then used for extracting nickel, cobalt, manganese and lithium; and the leached slag III is subjected to sulfating roasting treatment to obtain calcium magnesium sulfate and tail gas HF.

2. The process for synchronously processing the electrode powder of the lithium ion battery and the nickel cobalt intermediate product according to claim 1, wherein the leaching reagent for leaching the electrode powder is a mixed solution composed of sulfuric acid and a reducing agent, the concentration of the sulfuric acid in the mixed solution is 180-250g/L, and the concentration of the reducing agent is 100-200g/L;

preferably, the reducing agent is at least one selected from sodium metabisulfite, sodium sulfite and hydrogen peroxide;

preferably, the conditions for leaching the electrode powder at least include: the solid-to-liquid ratio at leaching was 1g:3-5mL, and the leaching temperature is 85-95 ℃.

3. The process for synchronously processing the electrode powder of the lithium ion battery and the nickel cobalt intermediate product according to claim 1 or 2, which is characterized in that sulfuric acid is added into the calcium and magnesium removal solution to adjust the acidity to the concentration of sulfuric acid of 0.1-1mol/L;

preferably, the TBP extractant comprises: the volume ratio of TBP to kerosene is 1:0.7-4;

preferably, the O/A ratio of the TBP extractant during extraction is 1:1-3.

4. A process for simultaneous treatment of lithium ion battery electrode powder and nickel cobalt intermediate product according to any of claims 1-3, wherein alkaline solution is added to adjust the pH of said raffinate i to 3-4.

5. The process for synchronously processing lithium ion battery electrode powder and nickel cobalt intermediate product according to any one of claims 1-4, wherein the return amount of the raffinate I after the pH value is regulated is controlled so that the O/A ratio in the process of stripping the organic load phase I is 4-15:1.

6. the process for synchronously treating electrode powder of lithium ion battery and nickel cobalt intermediate product according to any one of claims 1-5, wherein the leaching agent for leaching the nickel cobalt intermediate product is sulfuric acid solution with the concentration of 180-250 g/L;

preferably, in the process of leaching the nickel cobalt intermediate product, the solid-to-liquid ratio is 1g:4-6mL, and the leaching temperature is 85-95 ℃.

7. The process for synchronously processing the electrode powder of the lithium ion battery and the nickel cobalt intermediate product according to any one of claims 1 to 6, wherein the solid-to-liquid ratio of the calcium magnesium slag leached by the raffinate II is 1g:3-5mL;

preferably, the temperature of the leached calcium magnesium slag of the raffinate II is 85-95 ℃.

8. The process for simultaneous processing of lithium ion battery electrode powder and nickel cobalt intermediate product according to any one of claims 1-7, wherein the conditions of the sulfatizing roasting treatment at least comprise: the temperature is 150-200deg.C, and the time is 2-4h.

9. The process for simultaneous processing of lithium ion battery electrode powder and nickel cobalt intermediate product according to any of claims 1-8, wherein stripping slag i is returned for removal of calcium and magnesium.

10. The process for simultaneous processing of lithium ion battery electrode powder and nickel cobalt intermediate according to any of claims 1-9, wherein the tail gas HF is absorbed with liquid alkali and the product after evaporation concentration is returned to the calcium and magnesium removal step.