CN115323192A

CN115323192A - Treatment process of nickel/cobalt intermediate product

Info

Publication number: CN115323192A
Application number: CN202210893882.3A
Authority: CN
Inventors: 崔俊; 秦汝勇; 郑江峰; 文定强; 杨诗旻; 叶伟明; 张颖
Original assignee: Guangdong Jiana Energy Technology Co Ltd; Qingyuan Jiazhi New Materials Research Institute Co Ltd; Jiangxi Jiana Energy Technology Co Ltd
Current assignee: Guangdong Jiana Energy Technology Co Ltd; Qingyuan Jiazhi New Materials Research Institute Co Ltd; Jiangxi Jiana Energy Technology Co Ltd
Priority date: 2022-07-27
Filing date: 2022-07-27
Publication date: 2022-11-11

Abstract

The application belongs to the technical field of wet metallurgy, and particularly relates to a treatment process of a nickel/cobalt intermediate product, which comprises the following steps: and carrying out primary leaching treatment and secondary leaching treatment on the nickel intermediate product or the cobalt intermediate product to obtain a primary leaching solution and a secondary leaching solution, carrying out extraction and impurity removal treatment on the primary leaching solution to obtain a product solution, and returning to the primary leaching after copper removal treatment on a small amount of the secondary leaching solution. Compared with the procedures of direct decoppering treatment and deironing treatment on the leachate by one-stage leaching of the old process, the treatment process provided by the application only needs to decoppering treatment on a small amount of two-stage leachate, and does not need deironing treatment, so that the loss of an organic extractant in the decoppering treatment process is reduced, equipment required for deironing treatment is omitted, the content of iron and aluminum in the obtained one-stage leachate is far lower than that of the leachate obtained by the old process after the iron and aluminum are removed, the auxiliary material cost and the equipment cost are greatly reduced, the process flexibility and the treatment efficiency are greatly improved.

Description

Treatment process of nickel/cobalt intermediate product

Technical Field

The application belongs to the technical field of hydrometallurgy, and particularly relates to a treatment process of a nickel/cobalt intermediate product.

Background

At present, the domestic treatment process aiming at the nickel/cobalt intermediate product basically comprises the following steps: firstly, reducing and leaching a nickel/cobalt intermediate product by using sulfuric acid and a reducing agent to obtain a crude cobalt nickel sulfate solution and acid leaching residues (discarding); secondly, recovering copper in the crude cobalt nickel sulfate solution by using a copper extraction method; thirdly, removing iron and aluminum in the solution by using an iron vitriol method (yellow sodium iron vitriol, yellow potassium iron vitriol and yellow ammonium iron vitriol) to obtain a cobalt-nickel sulfate solution with iron, aluminum and copper removed; and fourthly, performing fine machining on the cobalt nickel sulfate solution without iron, aluminum and copper by using an extraction method to obtain pure cobalt sulfate, nickel sulfate and manganese sulfate solutions or pure cobalt sulfate, nickel sulfate and manganese sulfate products of a further processing plant.

The above treatment process is originally used for fine machining of cobalt-nickel raw ores, and the treatment of nickel/cobalt intermediate products has the following problems: 1. the iron and aluminum content in the raw materials is not high, so that the concentration of the iron and aluminum in the leached solution is low, the efficiency of removing iron and aluminum by using a chemical method is low (the using amount of auxiliary materials is large, the impurity removal rate is low), the prepared iron slag has poor crystal form (complete iron vitriol slag cannot be obtained in most of the time), the filtering performance is poor, and the content of valuable metals in the slag is high; 2. the copper content in the raw material is not high, so that the flow ratio of an organic phase to a water phase of a leached solution in the extraction process is small, and the loss of the organic phase caused by the dissolution of the organic phase in the water phase is increased due to the large flow of the water phase; 3. the process flexibility is poor, no matter copper extraction or iron removal is problematic, cobalt nickel sulfate solution for removing iron, aluminum and copper for subsequent extraction cannot be produced, the iron removal process is highly dependent on copper extraction, if copper extraction (due to high extraction fixed investment cost, only one extraction line is usually arranged, and no standby line is arranged) is problematic, the iron removal process is forced to stop, and the whole process before extraction is nearly paralyzed.

Disclosure of Invention

The application aims to provide a treatment process of a nickel/cobalt intermediate product, and aims to solve the problems of poor flexibility, low treatment efficiency and high cost of the existing treatment process for the nickel/cobalt intermediate product to a certain extent.

In order to achieve the purpose of the application, the technical scheme adopted by the application is as follows:

a treatment process of a nickel/cobalt intermediate product comprises the following steps:

carrying out primary leaching treatment on the nickel intermediate product or the cobalt intermediate product, and separating to obtain a primary leaching solution and a primary leaching residue;

extracting and impurity removing treatment is carried out on the first-stage leaching solution to obtain a product solution;

performing second-stage leaching treatment on the first-stage leaching residue, and separating to obtain a second-stage leaching solution and a second-stage leaching residue;

carrying out copper removal treatment on the second-stage leaching solution to obtain a copper-removed solution and a copper-rich solution;

and recovering the copper-removed liquid, and merging the recovered liquid into a nickel intermediate product or a cobalt intermediate product for primary leaching treatment.

The application provides a processing technology of nickel cobalt intermediate product adopts two sections to leach and handles, directly carries out procedures such as decoppering to one section leachate with old technology and handles and deironing processing, and the processing technology that this application provided only needs to carry out the decoppering to a small amount of two sections leachate and handles, has saved the required equipment quantity of deironing processing, has reduced the organic loss in the decoppering processing procedure, greatly reduced treatment cost. Meanwhile, the impurity contents of Fe, cu and Al in the first-stage leaching solution can meet or even be lower than the requirement of directly entering extraction in the industry, the process flow of the main body process is greatly shortened, the copper removal treatment and the first-stage leaching are not strongly linked, even if a short-term problem occurs in the copper removal treatment process, only one-stage leaching residue needs to be stored partially, the first-stage leaching is not influenced to supply cobalt nickel sulfate solution for the subsequent extraction process, and the flexibility of the whole process is greatly improved.

Drawings

In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings needed to be used in the embodiments or the prior art descriptions will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.

FIG. 1 is a schematic view of a process flow for treating a nickel/cobalt intermediate provided by an embodiment of the present application;

FIG. 2 is a schematic diagram of a process flow for preparing a nickel/cobalt intermediate product according to an embodiment of the present application

Detailed Description

In order to make the technical problems, technical solutions and beneficial effects to be solved by the present application more clearly apparent, the present application is further described in detail below with reference to the embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the present application and are not intended to limit the present application.

In this application, the term "and/or" describes an association relationship of associated objects, meaning that there may be three relationships, e.g., a and/or B, which may mean: a is present alone, A and B are present simultaneously, and B is present alone. Wherein A and B can be singular or plural. The character "/" generally indicates that the former and latter associated objects are in an "or" relationship.

In the present application, "at least one" means one or more, "a plurality" means two or more. "at least one of the following" or similar expressions refer to any combination of these items, including any combination of the singular or plural items. For example, "at least one (one) of a, b, or c," or "at least one (one) of a, b, and c," may each represent: a, b, c, a-b (i.e. a and b), a-c, b-c, or a-b-c, wherein a, b, and c can be single or multiple respectively.

It should be understood that, in various embodiments of the present application, the sequence numbers of the above-mentioned processes do not mean the execution sequence, some or all of the steps may be executed in parallel or executed sequentially, and the execution sequence of each process should be determined by its function and inherent logic, and should not constitute any limitation to the implementation process of the embodiments of the present application.

The terminology used in the embodiments of the present application is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. As used in the examples of this application and the appended claims, the singular forms "a", "an", and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.

The weight of the related components mentioned in the description of the embodiments of the present application may not only refer to the specific content of each component, but also represent the proportional relationship of the weight among the components, and therefore, the content of the related components is scaled up or down within the scope disclosed in the description of the embodiments of the present application as long as it is scaled up or down according to the description of the embodiments of the present application. Specifically, the mass in the description of the embodiments of the present application may be a mass unit known in the chemical field such as μ g, mg, g, kg, etc.

The terms "first" and "second" are used for descriptive purposes only and are used for distinguishing purposes such as substances from one another, and are not to be construed as indicating or implying relative importance or implying any number of technical features indicated. For example, a first XX may also be referred to as a second XX, and similarly, a second XX may also be referred to as a first XX, without departing from the scope of embodiments of the present application. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature.

An embodiment of the present application provides a processing process of a nickel/cobalt intermediate product, as shown in fig. 1, including the following steps:

s1: carrying out primary leaching treatment on the nickel intermediate product or the cobalt intermediate product, and separating to obtain a primary leaching solution and a primary leaching residue;

s2: extracting and impurity removing treatment is carried out on the first-stage leaching solution to obtain a product solution;

s3: performing second-stage leaching treatment on the first-stage leaching residue, and separating to obtain a second-stage leaching solution and a second-stage leaching residue;

s4: carrying out copper removal treatment on the second-stage leaching solution to obtain a copper-removed solution and a copper-rich solution;

s5: and recovering the copper-removed liquid, and merging the recovered liquid into a nickel intermediate product or a cobalt intermediate product for primary leaching treatment.

The nickel/cobalt intermediate product is a crude product obtained by processing a nickel/cobalt raw ore into cobalt and nickel containing crude products, such as crude cobalt hydroxide, crude nickel hydroxide, crude cobalt carbonate or crude nickel carbonate, because the copper content in the nickel/cobalt intermediate product is not high, if a section of leachate is directly subjected to extraction and copper removal, the flow ratio of an organic phase and an aqueous phase in the extraction process is small, the extraction capacity of the organic phase is wasted, and the loss of the organic phase caused by the dissolution of the organic phase in the aqueous phase is increased. The treatment process provided by the embodiment of the application only needs to carry out copper removal treatment on a small amount of two-stage leachate. Saves the organic loss in the copper removal treatment process and saves the equipment and auxiliary material consumption required in the iron and aluminum removal treatment process. If an old treatment route is adopted, the process flexibility is poor, no matter copper extraction or iron removal is in problem, cobalt nickel sulfate solution for removing iron, aluminum and copper for subsequent extraction cannot be produced, and the iron removal process highly depends on copper extraction. If the copper extraction is in trouble, the iron removal process is forced to stop, and the whole process before extraction is close to paralysis. In the two-stage leaching treatment process provided by the embodiment of the application, the link between the copper removal process and the one-stage leaching process is not strong, even if the short-term problem occurs in the copper extraction, only one-stage leaching residue needs to be stored in a part of empty space, the one-stage leaching is still not influenced to supply cobalt nickel sulfate liquid for the subsequent extraction process, and the flexibility of the whole process is greatly improved.

In step S1, in the embodiment of the present application, the first leaching process includes the following steps:

and soaking the nickel intermediate product or the cobalt intermediate product in the primary treatment solution until the amount of the primary leaching residues is reduced and the primary leaching residues are black. The operation of the first-stage leaching treatment is simple, complex equipment is not needed, and the treatment end point is clear and easy to judge. As shown in fig. 2, only one stage of leaching is performed in the old process, and in order to completely dissolve out high-valence cobalt and high-valence manganese, an excessive amount of reducing agent is added, so that black slag is converted into grey, yellow and white acid leaching slag (i.e. high-valence cobalt and high-valence manganese are completely dissolved out), the volume of the obtained leaching solution is large, the concentrations of copper, iron and aluminum in the leaching solution are low, the consumption of auxiliary materials in the subsequent processes of copper extraction, iron and aluminum removal and the like is large, and the overall cost is high. Even if the nickel/cobalt intermediate products are completely the same, the first-stage leachate provided by the embodiment of the application has larger component difference compared with the old process leachate, and under the condition that the cobalt or nickel concentration is fixed (mainly determining the wastewater amount or the product liquid concentration to meet the extraction requirement), as the end point pH value is higher than the pH value of Fe, al and Cu precipitate, the Fe, cu and Al in the first-stage leachate are greatly reduced, and the subsequent extraction difficulty can be reduced as a result.

In the embodiment of the application, the mass percent of the nickel element in the nickel intermediate product is 5-45%, and the mass percent of the cobalt element in the cobalt intermediate product is 5-45%. The nickel/cobalt intermediate product is a crude product obtained by processing nickel/cobalt raw ore into cobalt and nickel containing crude products, such as crude cobalt hydroxide, crude nickel hydroxide, crude cobalt carbonate or crude nickel carbonate, and also includes but is not limited to metal elements such as nickel, cobalt, copper, iron, aluminum, magnesium, manganese and the like, wherein the mass percentage of the copper element is 0.01-7%, the mass percentage of the iron element is 0.01-7%, the mass percentage of the aluminum element is 0.01-3%, the mass percentage of the magnesium element is 0.5-10%, and the mass percentage of the manganese element is 0.5-10%.

In embodiments herein, the primary treatment liquor comprises a first acid leach liquor including, but not limited to, at least one of hydrochloric acid, sulfuric acid, and the like, for reacting with the nickel intermediate or cobalt intermediate such that the nickel or cobalt is ionically dissolved in the primary leach liquor.

In a further embodiment of the present application, the primary treatment liquid further comprises a first reducing agent, and the first reducing agent comprises at least one of sodium metabisulfite, sulfur dioxide, sodium sulfite, hydrogen peroxide and glucose. Divalent cobalt and divalent manganese in the nickel/cobalt intermediate product are easily partially oxidized into high-valence cobalt and high-valence manganese in the air, so that the high-valence cobalt and high-valence manganese components are increased due to transportation or storage of partial nickel/cobalt intermediate product raw materials, and under the condition of not adding a first reducing agent, although divalent cobalt and divalent manganese in the nickel intermediate product or cobalt intermediate product can be dissolved out in the first-stage leaching treatment, the high-valence cobalt and high-valence manganese cannot be dissolved out little basically, so that the first-stage leaching slag amount in the first-stage leaching is large, and the leaching rates of cobalt and nickel in the first-stage leaching solution are low. The addition of the first reducing agent can dissolve most of high-valence cobalt and high-valence manganese in the primary leaching treatment, and simultaneously prevent ferric iron from being reduced into ferrous iron to be dissolved out, so that the slag amount of primary leaching slag is reduced, the nickel dissolution rate or the cobalt dissolution rate of the primary leaching treatment is improved, and the concentration of iron ions in the primary leaching solution is ensured to be less than 0.01g/L.

It is noted that no heating is required during the first leaching treatment without the addition of the first reducing agent. When the first reducing agent is added, the reaction temperature can be properly heated and controlled between 50 ℃ and 100 ℃, and the preferable temperature is between 85 ℃ and 95 ℃, so that the dissolution efficiency of the high-valence nickel or cobalt is improved.

Under the condition of adding a proper amount of first reducing agent and heating, 80-90% of nickel/cobalt in the nickel/cobalt intermediate product can be dissolved out, the dissolution rate of part of raw material nickel/cobalt can reach 90-98%, the slag amount of the first-stage leaching slag is 3-20% of the weight of the original nickel/cobalt intermediate product, and the slag amount of part of raw material can be lower than 3%.

In the practice of the present applicationIn the example, the pH value of the first leaching treatment is 2.5-7.0, so that most of cobalt and nickel in the nickel/cobalt intermediate product are dissolved into divalent nickel ions and divalent cobalt ions, and the pH value of the reaction end point is controlled to ensure that Fe ³⁺ (pH of 2.5 or more) and Al ³⁺ (pH 3.0 or higher) Cu ²⁺ (pH 4.0 or higher) in a trace amount. The first-stage leachate obtained in the method contains most of cobalt and nickel elements in the nickel/cobalt intermediate product, and the first-stage leachate can directly enter an extraction stage without removing copper, iron and aluminum because the contents of Fe, cu and Al are extremely low.

In a further embodiment of the present application, the end point PH of the first leach treatment is between 4.0 and 6.5, when the nickel ion concentration or the cobalt ion concentration in the first leach solution is between 30 and 140g/L. In some embodiments, if the object to be treated is a cobalt intermediate, the cobalt concentration in the first-stage leaching solution is 60-100 g/L; if the object to be treated is a nickel intermediate product, the concentration of nickel in the first-stage leaching solution is 60-140 g/L. At this time, the concentration of iron ions in the first-stage leachate is below 0.01g/L, the concentration of aluminum is below 0.01g/L, the concentration of copper is below 0.5g/L, and the concentration is lower than the requirement of cobalt sulfate or nickel sulfate solution in the extraction stage, and further copper, iron and aluminum do not need to be removed.

In a further embodiment of the present application, the first acid leaching solution and the first reducing agent may be added to react the nickel/cobalt intermediate product to a PH of 1.0 to 3.5, and then a small amount of the nickel/cobalt intermediate product may be added to adjust the PH to the final PH of 4.0 to 6.5. Since the nickel/cobalt intermediate is insoluble in water, the PH of the slurry is also 4.0 to 7.0 when only water (common water, pure water, tap water) is added to the first pickle liquor and the first reducing agent, so that in order to ensure that the nickel/cobalt intermediate reacts with the first pickle liquor and the first reducing agent sufficiently, the PH can be adjusted to 1.0 to 3.5 by adding the first pickle liquor and the first reducing agent in excess, and then adding a small amount of the nickel/cobalt intermediate to adjust the PH to the end point PH of 4.0 to 6.5. If the ratio of the first pickle liquor, the first reducing agent and the batch of the nickel/cobalt intermediate product is known in advance through experiments, the sulfuric acid and the reducing agent can also be added at one time to maintain the pH value of the end point between 4.0 and 6.5.

It is noted that the first pickle liquor and the first pickle liquorThe addition amount of the reducing agent is different from that of the prior art, and the first leaching treatment provided by the embodiment of the application aims to dissolve most of cobalt and nickel in the nickel/cobalt intermediate product and does not need to completely dissolve the cobalt and nickel in the nickel/cobalt intermediate product. At the same time, to ensure Fe in the nickel/cobalt intermediate ³⁺ Is not reduced to Fe ²⁺ The Fe content in the first-stage leaching solution exceeds the standard, and the dosage of the first reducing agent cannot be excessive, namely the dosage of the first reducing agent cannot be added to the dosage of completely dissolving out the cobalt and nickel in the nickel/cobalt intermediate product. The dosage of the reducing agent can be judged according to the color of the slag in the reaction system, the colors of the high-valence cobalt and the high-valence manganese are black, and even if Fe appears when a large amount of the high-valence cobalt and the high-valence manganese slag exists ²⁺ And also oxidized into Fe by high-valence cobalt and high-valence manganese ³⁺ And enters the first leaching residue by controlling the pH value of the end point.

In step S2, in the embodiment of the present application, the extracting agent for the extraction impurity removal process includes at least one of bis (2-ethylhexyl) phosphate (P204), mono-2 ethylhexyl 2 ethylhexylphosphonate (P507), and C272 extracting agent, and is a crude cobalt nickel sulfate (cobalt nickel chloride) extraction process flow that is conventional in the industry, i.e., P204-P507, P204-C272. In the extraction process, an extractant and metal ions in the solution form an extract compound and enter an organic solvent to form an organic mixture. The organic mixture is mixed with the strip liquor and the metal ions are returned to the strip liquor. The removal of impurity ions and the separation of nickel and cobalt are realized by utilizing the difference of the extraction capacities of different extracting agents to different metal ions. The di (2-ethylhexyl) phosphate (P204) is mainly used for extracting impurities such as iron, copper, zinc, manganese, aluminum, calcium and the like; 2-ethylhexyl phosphoric acid mono-2-ethylhexyl ester (P507) is mainly used for the extractive separation of cobalt and magnesium; the C272 extractant is a new extractant developed by cyanamide company in USA for separating cobalt and nickel, the main component is di (2, 4-trimethyl amyl) phosphonic acid, it can be dissolved in aromatic and aliphatic diluent completely, it is very stable under heating, acid, alkali conditions, it has very good extraction performance to cobalt and nickel in sulfate medium and chloride medium. The product solution obtained by extraction impurity removal treatment, namely cobalt sulfate solution or nickel sulfate solution, has high impurity removal rate and extremely low impurity metal content.

In step S3, in an embodiment of the present application, the secondary leaching process includes the following steps:

soaking the first-stage leaching residue in the second-stage treatment solution until the first-stage leaching residue is converted from black to gray, yellow or white. The operation of the second-stage leaching treatment is simple, complex equipment is not needed, the treatment end point is clear and easy to judge, the reducing agent in the step can be slightly excessive, so that the residual cobalt and nickel in the first-stage leaching residue are completely dissolved out, the second-stage leaching residue and the second-stage leaching solution are obtained, the second-stage leaching residue is acid leaching residue and can be discarded or sold after being washed, and the second-stage leaching solution is combined into the first-stage leaching solution after copper is removed. Because the slag amount of the first-stage leaching slag is 3-20% of the weight of the original nickel/cobalt intermediate product, the slag amount of partial raw materials can be lower than 3%, the treatment is simpler, and even if the second-stage treatment liquid is excessive, on the premise of ensuring higher dissolution rate, the required excessive second-stage treatment liquid is greatly reduced compared with the excessive leaching liquid in the old process, the cost is saved, and the utilization rate of the treatment liquid is greatly improved.

In the embodiment of the application, the secondary treatment liquid comprises a second acid leaching solution, and the second acid leaching solution comprises at least one of hydrochloric acid and sulfuric acid and is used for dissolving out nickel or cobalt in the primary leaching slag as much as possible.

In the embodiment of the application, the secondary treatment liquid further comprises a second reducing agent, the second reducing agent comprises but is not limited to sodium metabisulfite, sulfur dioxide, sodium sulfite, hydrogen peroxide and glucose, the treatment temperature of the secondary leaching treatment is 50-100 ℃, and the second reducing agent is used for dissolving out high-valence cobalt, high-valence manganese and high-valence nickel which are not dissolved out of the primary leaching residue, reducing the residue amount of the secondary leaching residue and improving the dissolution rate of the secondary leaching treatment. In the second leaching process, the amount of the second reducing agent needs to be controlled to be slightly excessive, so that the high-valence cobalt and the high-valence manganese are completely reduced to 2-valence to be dissolved out, i.e. the black first-stage leaching residue is changed into grey, yellow and white acid leaching residue.

In the embodiment of the application, the pH value of the secondary leaching treatment is 0.5-2.5, so that the nickel or cobalt in the nickel-cobalt intermediate product can be dissolved out more fully. In a further embodiment of the present application, the PH of the secondary leaching treatment is preferably 1.0 to 1.5.

In the embodiment of the application, the concentration of nickel ions or cobalt ions in the secondary leaching solution is 5-100 g/L. Because the amount of cobalt and nickel contained in the second-stage leachate is less than 20 percent of the total nickel and cobalt in the nickel/cobalt intermediate product, even if the concentration of cobalt and nickel in the second-stage leachate is lower, the volume of the second-stage leachate is not larger than that of the first-stage leachate, and the concentration of cobalt and nickel in the first-stage leachate can be controlled to be 5-100 g/L as required. In a further embodiment of the application, the concentration of cobalt and nickel is controlled to be 30-70 g/L, so that the phenomenon of groove blockage caused by cobalt, nickel and calcium crystallization in copper extraction can be relieved.

In step S4, in the embodiment of the present application, a conventional copper extractant, such as LIX984, is used for copper extraction in the copper removal process, so as to obtain a copper-removed solution and a copper-rich solution. The solution in the copper extraction process is greatly different from the solution used for copper extraction in the old process, taking the example that the cobalt and nickel in the first-stage leachate are dissolved out by 80%, if the concentrations of the cobalt and nickel in the first-stage leachate, the second-stage leachate and the old process leachate are controlled to be consistent, the volume of the second-stage leachate is about 1/5 of that of the old process leachate, the concentrations of Fe, cu and Al in the second-stage leachate are about 5 times that of the old process leachate, the volume of the second-stage leachate is small, and the Cu concentration is small ²⁺ High concentration, and greatly reduced volume of water phase when copper extraction treatment is carried out. Therefore, the organic loss caused by the dissolution of the organic phase in the water phase can be greatly reduced, the operation is more convenient, and the extraction difficulty is greatly reduced.

In the embodiment of the application, the copper removal treatment and the first-stage leaching are not strongly linked, even if a short-term problem occurs in the copper removal treatment process, only one stage of leaching slag needs to be stored in a part of empty space, the first-stage leaching is still not influenced to supply cobalt nickel sulfate liquid for the subsequent extraction process, and the overall process flexibility is greatly improved

In the embodiment of the application, the copper-rich solution is further subjected to electrodeposition treatment to obtain a copper simple substance. And (3) carrying out electrochemical deposition treatment on the copper-rich solution to deposit a copper simple substance on the cathode, wherein the deposited copper simple substance can be used for preparing a copper plate.

In step S5, in the embodiment of the present application, the solution after copper removal is recovered and merged into the nickel intermediate product or the cobalt intermediate product to perform a first-stage leaching treatment, so that a closed-loop treatment is formed, and the recovery rate is high.

In order to make the details and operations of the above-mentioned embodiments of the present invention clearly understood by those skilled in the art, and to make the progress of the nickel/cobalt intermediate processing technology and the preparation method thereof obvious, the above-mentioned technical solutions are illustrated by a plurality of examples below.

Example 1: the treatment of the cobalt intermediate, as shown in fig. 1, comprises the following steps:

s1: and putting 12 tons of the cobalt intermediate product into a 40-square reaction tank, adding water, and stirring to prepare the cobalt intermediate product into slurry. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 2.0-2.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank, and stopping adding the sulfuric acid and the sodium metabisulfite when red and black slag of the cobalt sulfate solution can be obviously seen in the reaction tank (namely the slag liquid is clear). Slowly adding a small amount of cobalt intermediate slurry into the reaction tank, regulating the pH value in the reaction tank to 5.0-5.5, stopping adding the cobalt intermediate slurry, continuously stirring for 0.5h, and performing filter pressing on the slag and the liquid in the reaction tank to obtain a first-stage leaching solution and a first-stage leaching residue. The elemental analysis of the cobalt intermediate, the first-stage leachate and the first-stage leaching residue are shown in Table 1.1.

TABLE 1.1 analysis of metallic elements in cobalt intermediate, primary leach liquor and primary leach residue

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Cobalt intermediate (%)	31.03	0.09	1.92	0.14	0.59	0.02	4.57
First-stage extract (g/L)	98.87	0.28	2.93	0.0014	0.019	0.0022	13.71
								One-stage extract (%)	12.11	0.03	2.3	0.31	1.18	0.03	0.18

S2: adding a proper amount of sulfuric acid into a first-stage leachate (pure solution without slag) storage tank obtained in the step S1, adjusting the pH value to 3.0, directly feeding the solution with the adjusted pH value into a conventional P204 extraction system to remove iron, zinc, aluminum, calcium, copper and manganese, and then separating cobalt and magnesium through P507 to obtain a cobalt sulfate solution, namely a product solution. Elemental analysis in the product solution is shown in table 1.2.

TABLE 1.2 analysis of metal elements in the product solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Product solution (g/L)	111.79	0.0037	0.0029	0.0009	0.0011	0.0017	0.0044

S3: and (3) putting the first-stage leaching residues obtained in the step (S1) into a reaction tank, adding water, and stirring to prepare a slurry from the first-stage leaching residues. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 1.0-1.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank to control the pH value in the reaction process to be 1.0-2.0, reacting until the color of slag in the reaction tank is completely changed from black to grey, and stopping adding the sulfuric acid and the sodium metabisulfite. And continuously stirring for reaction for 30min, and filtering to obtain second-stage leaching residue and second-stage leaching liquid. Acid leaching slag is discharged after acid washing and water washing, and the second-stage leachate is subjected to subsequent treatment. The analysis of some elements in the washed acid sludge and the second-stage leachate is shown in Table 1.3.

TABLE 1.3 analysis of metal elements in the two-stage leach residue and the two-stage leach solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Second stage leach residue (%)	0.028	0.0012	0.0037	0.89	0.011	0.03	0.87
Two-stage leachate (g/L)	60.32	0.14	3.45	1.47	2.95	0.21	0.82

S4: and (3) carrying out conventional copper extraction in the industry on the two-stage leaching solution obtained in the step (S3) by using LIX984, carrying out electrodeposition treatment on the obtained copper-rich solution, and carrying out subsequent treatment on the obtained copper-removed solution.

S5: and (4) merging the copper-removed liquid obtained in the step (S5) into a first leaching treatment process.

Example 2: the treatment of the cobalt intermediate product comprises the following steps:

s1: 12 tons of cobalt intermediate product is put into a 40-square reaction tank, water and the solution after copper removal in example 1 are added, and stirring is started to adjust the cobalt intermediate product into slurry. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 2.0-2.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank, and stopping adding the sulfuric acid and the sodium metabisulfite when red and black slag of the cobalt sulfate solution can be obviously seen in the reaction tank (namely the slag liquid is clear). Slowly adding a small amount of cobalt intermediate slurry into the reaction tank, regulating the pH value in the reaction tank to 5.0-5.5, stopping adding the cobalt intermediate slurry, continuously stirring for 0.5h, and performing filter pressing on the slag and the liquid in the reaction tank to obtain a first-stage leaching solution and a first-stage leaching residue. The elemental analysis of the cobalt intermediate, the first-stage leachate and the first-stage leaching residue are shown in Table 2.1.

TABLE 2.1 analysis of metallic elements in cobalt intermediate, primary leach liquor and primary leach residue

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Cobalt intermediate (%)	31.03	0.09	1.92	0.14	0.59	0.02	4.57
First-stage extract (g/L)	101.87	-	5.87	0.0008	0.081	0.0005	15.71
								One-stage extract (%)	13.12	-	2.8	5.4	0.93	0.81	0.25

S2: adding a proper amount of sulfuric acid into a first-stage leachate (pure solution without slag) storage tank obtained in the step S1, adjusting the pH value to 3.0, directly feeding the solution with the adjusted pH value into a conventional P204 extraction system to remove iron, zinc, aluminum, calcium, copper and manganese, and then separating cobalt and magnesium through P507 to obtain a cobalt sulfate solution, namely a product solution. Elemental analysis in the product solution is shown in table 2.2.

TABLE 2.2 analysis of metal elements in the product solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Product solution (g/L)	115.64	0.0033	0.0021	0.0009	0.0009	0.0013	0.0041

S3: and (3) putting the first-stage leaching residues obtained in the step (S1) into a reaction tank, adding water, and stirring to prepare a slurry from the first-stage leaching residues. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 1.0-1.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank to control the pH value in the reaction process to be 1.0-2.0, reacting until the color of slag in the reaction tank is completely changed from black to grey, and stopping adding the sulfuric acid and the sodium metabisulfite. And continuously stirring and reacting for 30min, and filtering to obtain second-stage leaching residue and second-stage leaching liquid. Acid leaching slag is discharged after acid washing and water washing, and the second-stage leachate is subjected to subsequent treatment. The analysis of some elements in the washed acid sludge and the second-stage leachate is shown in Table 2.3.

TABLE 2.3 analysis of metal elements in the two-stage leach residue and the two-stage leach solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Second-stage leach residue (%)	0.051	-	0.0048	9.54	0.009	1.38	0.49
Two-stage leaching solution (g/L)	63.54	-	3.78	1.39	2.83	0.39	0.78

Example 3: the treatment of the cobalt intermediate product comprises the following steps:

s1: 12 tons of cobalt intermediate product is put into a 40-square reaction tank, water and the solution after copper removal in example 1 are added, and stirring is started to adjust the cobalt intermediate product into slurry. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 2.0-2.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank, and stopping adding the sulfuric acid and the sodium metabisulfite when red and black slag of the cobalt sulfate solution can be obviously seen in the reaction tank (namely the slag liquid is clear). Slowly adding a small amount of cobalt intermediate slurry into the reaction tank, adjusting the pH value in the reaction tank to 5.0-5.5, stopping adding the cobalt intermediate slurry, continuously stirring for 0.5h, and performing filter pressing on the slag and the liquid in the reaction tank to obtain a first-stage leaching solution and a first-stage leaching residue. The elemental analysis of the cobalt intermediate, the first-stage leachate and the first-stage leaching residue are shown in Table 3.1.

TABLE 3.1 analysis of metallic elements in cobalt intermediate, primary leach liquor and primary leach residue

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Cobalt intermediate (%)	31.35	0.12	3.14	1.89	0.21	1.12	7.58
First-stage extract (g/L)	101.87	0.31	5.87	0.0021	0.081	0.0008	22.86
								One-stage extract (%)	10.17	0.04	9.88	6.21	0.79	4.52	0.38

S2: adding a proper amount of sulfuric acid into a first-stage leachate (pure solution without slag) storage tank obtained in the step S1, adjusting the pH value to 3.0, directly feeding the solution with the adjusted pH value into a conventional P204 extraction system to remove iron, zinc, aluminum, calcium, copper and manganese, and then separating cobalt and magnesium through P507 to obtain a cobalt sulfate solution, namely a product solution. Elemental analysis of the product solution is shown in Table 3.2.

TABLE 3.2 analysis of metal elements in the product solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Product solution (g/L)	117.67	0.0027	0.0018	0.0008	0.0010	0.0011	0.0030

S3: and (3) putting the first-stage leaching residues obtained in the step (S1) into a reaction tank, adding water, and stirring to prepare a slurry from the first-stage leaching residues. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 1.0-1.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank to control the pH value in the reaction process to be 1.0-2.0, reacting until the color of slag in the reaction tank is completely changed from black to grey, and stopping adding sulfuric acid and sodium metabisulfite. And continuously stirring and reacting for 30min, and filtering to obtain second-stage leaching residue and second-stage leaching liquid. Acid leaching slag is discharged after acid washing and water washing, and the second-stage leachate is subjected to subsequent treatment. The elemental analysis of the washed acid sludge and a portion of the secondary leach solution are shown in Table 3.3.

TABLE 3.3 analysis of metal elements in the two-stage leach residue and the two-stage leach solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Second stage leach residue (%)	0.051	0.0043	0.0032	12.53	0.009	4.57	0.21
Two-stage leaching solution (g/L)	63.54	0.15	3.78	15.21	5.59	0.39	0.78

Example 4: the treatment of the cobalt intermediate product comprises the following steps:

s1: 12 tons of the cobalt intermediate product is put into a 40-square reaction tank, water and the solution after copper removal in example 1 are added, and stirring is started to adjust the cobalt intermediate product into slurry. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 2.0-2.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank, and stopping adding the sulfuric acid and the sodium metabisulfite when red and black slag of the cobalt sulfate solution can be obviously seen in the reaction tank (namely the slag liquid is clear). Slowly adding a small amount of cobalt intermediate slurry into the reaction tank, adjusting the pH value in the reaction tank to 2.5-3.0, stopping adding the cobalt intermediate slurry, continuously stirring for 0.5h, and performing filter pressing on the slag and the liquid in the reaction tank to obtain a first-stage leaching solution and a first-stage leaching residue. The elemental analysis of the cobalt intermediate, the first-stage leachate and the first-stage leaching residue are shown in Table 4.1.

TABLE 4.1 analysis of metallic elements in cobalt intermediate, primary leach liquor and primary leach residue

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Cobalt intermediate (%)	31.35	0.12	2.81	0.12	0.03	0.02	7.58
First-stage leachate (g/L)	101.87	0.31	5.72	0.01	0.081	0.01	22.86
								One-stage extract (%)	10.24	0.04	9.27	5.21	0.34	0.57	0.28

S2: adding a proper amount of sulfuric acid into a first-stage leachate (pure solution without slag) storage tank obtained in the step S1, adjusting the pH value to 3.0, directly feeding the solution with the adjusted pH value into a conventional P204 extraction system to remove iron, zinc, aluminum, calcium, copper and manganese, and then separating cobalt and magnesium through P507 to obtain a cobalt sulfate solution, namely a product solution. Elemental analysis of the product solution is shown in Table 4.2.

TABLE 4.2 analysis of metal elements in the product solution

S3: and (3) putting the first-stage leaching residue obtained in the step (S1) into a reaction tank, adding water, and stirring to prepare a slurry from the first-stage leaching residue. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 1.0-1.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank to control the pH value in the reaction process to be 1.0-2.0, reacting until the color of slag in the reaction tank is completely changed from black to grey, and stopping adding the sulfuric acid and the sodium metabisulfite. And continuously stirring for reaction for 30min, and filtering to obtain second-stage leaching residue and second-stage leaching liquid. Acid leaching slag is discharged after acid washing and water washing, and the second-stage leachate is subjected to subsequent treatment. The elemental analysis of the washed acid sludge and a portion of the secondary leach solution are shown in Table 4.3.

TABLE 4.3 analysis of metal elements in the two-stage leach residue and the two-stage leach solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Second stage leach residue (%)	0.042	0.0043	0.0047	12.53	0.009	4.57	0.21
Two-stage leaching solution (g/L)	35.75	0.15	32.45	12.24	0.93	0.78	0.71

Example 5: the nickel intermediate product treatment comprises the following steps:

s1: 12 tons of nickel intermediate product is put into a 40-square reaction tank, water and the solution after copper removal in example 1 are added, and stirring is started to adjust the nickel intermediate product into slurry. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 2.0-2.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank, and stopping adding the sulfuric acid and the sodium metabisulfite when the green and black slag of the nickel sulfate solution can be obviously seen in the reaction tank (namely the slag liquid is clear). Slowly adding a small amount of nickel intermediate slurry into the reaction tank, regulating the pH value in the reaction tank to 2.5-3.0, stopping adding the nickel intermediate slurry, continuously stirring for 0.5h, and performing filter pressing on the slag and the liquid in the reaction tank to obtain a first-stage leaching solution and a first-stage leaching residue. The elemental analysis of the nickel intermediate, first-stage leach solution, and first-stage leach residue are shown in Table 5.1.

TABLE 5.1 analysis of metallic elements in the intermediate nickel product, first-stage leach solution and first-stage leach residue

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Nickel intermediate (%) (dry basis)	0.35	41.21	1.24	0.05	0.024	0.012	2.57
First-stage leachate (g/L)	0.89	112.2	1.57	0.01	0.035	0.01	5.78
								One-stage extract (%)	5.11	10.57	6.78	4.57	0.12	0.92	0.14

S2: adding a proper amount of sulfuric acid into a first-stage leachate (pure solution without slag) storage tank obtained in the step S1, adjusting the pH value to 3.0, directly feeding the solution with the adjusted pH value into a conventional P204 extraction system to remove iron, zinc, aluminum, calcium, copper and manganese, and then separating nickel and magnesium through C272 to obtain a nickel sulfate solution, namely a product solution. Elemental analysis in the product solution is shown in table 5.2.

TABLE 5.2 analysis of metal elements in the product solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Product solution (g/L)	0.047	119.7	0.0042	0.0014	0.0007	0.0015	0.0037

S3: and (3) putting the first-stage leaching residues obtained in the step (S1) into a reaction tank, adding water, and stirring to prepare a slurry from the first-stage leaching residues. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 1.0-1.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank to control the pH value in the reaction process to be 1.0-2.0, reacting until the color of slag in the reaction tank is completely changed from black to grey, and stopping adding the sulfuric acid and the sodium metabisulfite. And continuously stirring and reacting for 30min, and filtering to obtain second-stage leaching residue and second-stage leaching liquid. Acid leaching residues are discharged after acid washing and water washing, and the subsequent treatment is carried out on the two-stage leachate. The elemental analysis of a part of the acid-leached residues and the two-stage leachate after washing is shown in Table 5.3.

TABLE 5.3 analysis of metal elements in the two-stage leach residue and the two-stage leach solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Second stage leach residue (%)	0.012	0.13	0.0038	1.24	0.009	1.26	0.19
Two-stage leaching solution (g/L)	19.57	40.12	22.15	0.13	0.11	0.23	0.15

S4: and (4) carrying out conventional copper extraction in the industry on the two-section leaching solution obtained in the S3 by using LIX984, carrying out electrodeposition treatment on the obtained copper-rich solution, and carrying out subsequent treatment on the obtained copper-removed solution.

Example 6: the nickel intermediate product treatment comprises the following steps:

s1: 12 tons of nickel intermediate product is put into a 40-square reaction tank, water and the solution after copper removal in example 1 are added, and stirring is started to adjust the nickel intermediate product into slurry. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 2.0-2.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank, and stopping adding sulfuric acid and sodium metabisulfite when green and black residues (namely clear residue liquid) of the nickel sulfate solution can be obviously seen in the reaction tank. Slowly adding a small amount of nickel intermediate slurry into the reaction tank, regulating the pH value in the reaction tank to 4.5-5.0, stopping adding the nickel intermediate slurry, continuously stirring for 0.5h, and performing filter pressing on the slag and the liquid in the reaction tank to obtain a first-stage leaching solution and a first-stage leaching residue. The elemental analysis of the nickel intermediate, first-stage leachate and first-stage leachate are shown in Table 6.1.

TABLE 6.1 analysis of metallic elements in the intermediate products, primary leach liquors and primary leach residues of nickel

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Nickel intermediate (%) (dry basis)	1.21	40.15	1.28	1.21	0.35	0.42	3.57
First-stage leachate (g/L)	3.18	115.2	3.01	0.0012	0.12	0.0005	10.24
								One-stage leaching residue (%)	8.12	12.57	9.11	6.21	1.35	2.01	0.26

S2: adding a proper amount of sulfuric acid into a first-stage leachate (pure solution without slag) storage tank obtained in the step S1, adjusting the pH value to 3.0, directly feeding the solution with the adjusted pH value into a conventional P204 extraction system to remove iron, zinc, aluminum, calcium, copper and manganese, and then separating nickel and magnesium through C272 to obtain a nickel sulfate solution, namely a product solution. Elemental analysis in the product solution is shown in table 6.2.

TABLE 6.2 analysis of metal elements in the product solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Product solution (g/L)	0.041	124.7	0.0035	0.0016	0.0008	0.0017	0.0043

S3: and (3) putting the first-stage leaching residue obtained in the step (S1) into a reaction tank, adding water, and stirring to prepare a slurry from the first-stage leaching residue. Adding sulfuric acid into the reaction tank until the pH value in the reaction tank is 1.0-1.5, then heating to 90 ℃, slowly adding sulfuric acid and sodium metabisulfite into the reaction tank to control the pH value in the reaction process to be 1.0-2.0, reacting until the color of slag in the reaction tank is completely changed from black to grey, and stopping adding the sulfuric acid and the sodium metabisulfite. And continuously stirring and reacting for 30min, and filtering to obtain second-stage leaching residue and second-stage leaching liquid. Acid leaching slag is discharged after acid washing and water washing, and the second-stage leachate is subjected to subsequent treatment. The elemental analysis of a part of the acid-leached residues and the two-stage leachate after washing is shown in Table 6.3.

TABLE 6.3 analysis of metal elements in the two-stage leach residue and the two-stage leach solution

	Co	Ni	Mn	Fe	Cu	Al	Mg
								Second stage leach residue (%)	0.021	0.15	0.014	18.35	0.012	6.24	0.23
Two-stage leachate (g/L)	28.63	42.15	34.64	15.23	0.08	6.21	0.35

The above description is only exemplary of the present application and should not be taken as limiting the present application, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present application should be included in the protection scope of the present application.

Claims

1. A treatment process of a nickel/cobalt intermediate product is characterized by comprising the following steps:

carrying out primary leaching treatment on the nickel intermediate product or the cobalt intermediate product, and separating to obtain primary leaching liquid and primary leaching residue;

extracting and removing impurities from the first-stage leaching solution to obtain a product solution;

carrying out copper removal treatment on the two-stage leaching solution to obtain a copper-removed solution and a copper-rich solution;

and recovering the copper-removed liquid, and merging the copper-removed liquid into the nickel intermediate product or the cobalt intermediate product for the first-stage leaching treatment.

2. The treatment process of the nickel/cobalt intermediate product according to claim 1, wherein the mass percent of nickel element in the nickel intermediate product is 5-45%; and/or

The mass percentage of the cobalt element in the cobalt intermediate product is 5-45%.

3. The process of treating a nickel/cobalt intermediate as claimed in claim 1 or 2,

the concentration of iron ions in the first-stage leachate is lower than 0.01g/L, the concentration of aluminum ions is lower than 0.01g/L, and the concentration of copper ions is lower than 0.5g/L;

the concentration of nickel ions or cobalt ions in the first-stage leaching solution is 30-140 g/L; and/or

The concentration of nickel ions or cobalt ions in the second-stage leaching solution is 5-100 g/L;

the copper content in the second-stage leaching solution is 0.01-30g/L.

4. The process of treating a nickel/cobalt intermediate as claimed in claim 3, wherein the first leaching treatment comprises the steps of:

soaking the nickel intermediate product or the cobalt intermediate product in a first-stage treatment solution until the amount of the first-stage leaching slag is reduced and the first-stage leaching slag is black; and/or

The pH value of the first-stage leaching treatment is 2.5-7.0.

5. The process of claim 4, wherein the primary treatment liquid comprises a first acid leaching liquid, and the first acid leaching liquid comprises at least one of sulfuric acid and hydrochloric acid.

6. The nickel/cobalt intermediate product treatment process according to claim 5, wherein the primary treatment solution further comprises a first reducing agent, the first reducing agent comprises at least one of sodium metabisulfite, sulfur dioxide, sodium sulfite, hydrogen peroxide and glucose, and the treatment temperature of the primary leaching treatment is 50-100 ℃.

7. A process of treating a nickel/cobalt intermediate as claimed in claim 3, wherein the secondary leaching treatment comprises the steps of:

soaking the first-stage leaching residue in a second-stage treatment solution until the first-stage leaching residue is converted from black to grey, yellow or white; and/or

The pH value of the second-stage leaching treatment is 0.5-2.5.

8. The process according to claim 7, wherein the treatment of the intermediate nickel/cobalt product,

the secondary treatment liquid comprises a second acid immersion liquid, and the second acid immersion liquid comprises at least one of sulfuric acid and hydrochloric acid.

9. The process according to claim 8, wherein the treatment of the intermediate nickel/cobalt product,

the second-stage treatment solution also comprises a second reducing agent, the second reducing agent comprises at least one of sodium metabisulfite, sulfur dioxide, sodium sulfite, hydrogen peroxide and glucose, and the treatment temperature of the second-stage leaching treatment is 50-100 ℃.

10. The process for treating a nickel/cobalt intermediate product according to any one of claims 2 and 4 to 9, wherein the copper removal treatment is a copper extraction treatment; and/or

And carrying out electrodeposition treatment on the copper-rich solution to obtain a copper simple substance.