CN109234522B - Comprehensive recovery processing method for cobalt-sulfur concentrate - Google Patents
Comprehensive recovery processing method for cobalt-sulfur concentrate Download PDFInfo
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Abstract
The invention belongs to the technical field of nonferrous metallurgy, and particularly relates to a comprehensive recovery treatment method of cobalt-sulfur concentrate. It is to oxidize, boil and roast the cobalt-sulfur concentrate to obtain roasted product and SO2Flue gas, SO2The flue gas is purified and dedusted and then enters a flue gas acid making system to make acid; cooling the calcine, performing ball milling to obtain fine particles, performing slurrying pre-soaking on the fine particles, performing continuous selective leaching by using a continuous pressure leaching system, and performing pre-neutralization on lime milk pulp to obtain supernatant and filter residues, treating the supernatant, and then, introducing the treated supernatant into a copper extraction system for extraction to obtain cathode copper, post-electrodeposition liquid and raffinate; washing the filter residue to obtain a washing liquid, taking the electro-deposition liquid and the washing liquid as a slurrying liquid to perform slurrying and pre-dipping treatment on the calcine, and allowing the raffinate to enter a cobalt precipitation process and a magnesium precipitation process to obtain solid cobalt and magnesium materials, and conveying the solid cobalt and magnesium materials to a slag yard for storage. The method can effectively recover cobalt and copper in the ore at one time, has high recovery rate of cobalt and copper, can effectively treat low-grade cobalt-sulfur concentrate, and realizes the maximum utilization of resources.
Description
Technical Field
The invention relates to the technical field of nonferrous metallurgy, in particular to a comprehensive recovery processing method of cobalt-sulfur concentrate.
Background
At present, the processing technology of cobalt-sulfur concentrate at home and abroad can be divided into the following steps: 1) fire smelting: the cobalt-sulfur concentrate is treated by a pyrogenic process, and pyrogenic processes such as oxygen-enriched blowing, continuous blowing, anode furnace refining and the like are adopted. The method comprises the following steps of firstly converting copper sulfide and cobalt sulfide in the cobalt-sulfur concentrate into copper matte, then refining the copper matte, casting the copper matte into an anode plate, and then recovering the copper and cobalt by adopting electrolytic refining, wherein the process flow is simple, the raw material adaptability is strong, the processing capacity is high, but the problem of low grade of the low-grade cobalt-sulfur concentrate exists, the recovery rate of the cobalt in the process is low, and the market price of the cobalt is very high, so that the pyrometallurgical treatment is not paid; 2) sulfating roasting: sulfating roasting has the characteristics of low sintering temperature and low energy consumption, can directly convert cobalt-copper sulfide in a mine into soluble cobalt-copper sulfate, and can directly separate valuable metals from the mine by adopting a water leaching mode, so the process can greatly shorten the comprehensive recovery processing flow of cobalt-sulfur concentrate, but the sulfating roasting process also has the problem of low cobalt recovery rate which is only about 75 percent, and has low processing capacity and high roasting process control requirement, when the roasting temperature is high, part of cobalt, copper and iron form insoluble ferrite to reduce the leaching rate, and when the roasting temperature is low, the cobalt-copper sulfide is incompletely converted, and in addition, the iron leaching rate is high, so the iron removal cost is high, the slag quantity is large, and the cobalt-copper entrainment loss is large; 3) bioleaching: bioleaching is a new metallurgical technology, and mainly adopts bioleaching-extraction-washing-back extraction processes. The energy consumption of bioleaching is low, the method has good adaptability to ores with low grade and complex components, but the iron leaching rate is higher, the post-treatment cost is high, the bioleaching treatment capacity is small, and the method is not suitable for large-scale application.
In the prior art, no matter the cobalt-sulfur concentrate is treated by pyrometallurgical smelting, sulfating roasting or bioleaching, the cobalt-sulfur concentrate is difficult to be systematically recycled, and particularly, the problem of low recovery rate exists for the cobalt with high market price.
Disclosure of Invention
The invention aims to solve the defects of the prior art and provides a comprehensive recovery processing method of cobalt-sulfur concentrate, which can effectively recover cobalt and copper in ore at one time, has high recovery rate of cobalt and copper, can effectively process low-grade cobalt-sulfur concentrate and realizes the maximum utilization of resources.
The comprehensive recovery processing method of the cobalt-sulfur concentrate is characterized by comprising the following steps of:
1) oxidizing, boiling and roasting the cobalt-sulfur concentrate to convert metal sulfide in the cobalt-sulfur concentrate into oxide to obtain roasted sand and SO2Recovering heat generated in the roasting process from flue gas; SO (SO)2The flue gas is purified and dedusted and then enters a flue gas acid making system to make acid; cooling the roasted sand, performing ball milling to obtain fine particles, and performing slurrying and presoaking on the fine particles to obtain presoaked mixed liquid;
2) transferring the pre-soaking mixed solution obtained in the step 1) into a continuous pressure leaching system for continuous selective leaching to obtain slurry, carrying out pre-neutralization on the slurry by lime milk pulp, carrying out solid-liquid separation on reaction liquid after pre-neutralization by a concentration separator to obtain supernatant and filter residue, allowing most of iron to enter the filter residue in the form of hematite, carrying out acid leaching on cobalt and copper to enter the solution to become a cobalt and copper sulfate solution in the supernatant, and carrying out concentrated countercurrent washing on the filter residue by water to obtain washing liquid and washed residue; the supernatant fluid enters the next extraction procedure, the washing liquid is used as slurrying liquid and returns to the step 1) for slurrying and pre-dipping treatment of the calcine, and the washed slag is conveyed to a tailing neutralizing tank for neutralizing treatment and then discharged;
3) cooling the supernatant obtained in the step 2), then carrying out fine filtration, and allowing the obtained fine-filtered liquid to enter a copper extraction system for extraction so as to separate copper from cobalt in the solution, wherein the copper is enriched into a copper sulfate solution, and the raffinate is to be treated;
4) enabling the copper sulfate solution in the step 3) to enter a rotational flow electrodeposition system, performing rotational flow electrolysis to obtain 1# cathode copper and a post-electrodeposition solution, mixing the post-electrodeposition solution with the washing solution in the step 1), and returning the mixture to a slurry solution to perform slurry pre-impregnation on the calcine in the step 1);
5) allowing the raffinate obtained in the step 3) to enter a cobalt precipitation process, performing cobalt precipitation by using magnesium oxide slurry as a precipitator, precipitating and separating cobalt from the slurry after the cobalt is converted into cobalt hydroxide, and performing flash evaporation, drying and dehydration on the cobalt hydroxide to obtain a crude cobalt hydroxide product, wherein the separated slurry is a magnesium sulfate solution;
6) the magnesium sulfate solution in the step 5) enters a magnesium precipitation process, lime milk pulp is used as a precipitator, magnesium hydroxide and calcium sulfate precipitation are generated by magnesium precipitation, solid-liquid separation is carried out on the slurry after precipitation, and solid materials are calcium-magnesium residues and are sent to a slag yard for storage; the filtrate was recovered and used for wet milling in a ball mill, slurrying of lime, magnesium oxide.
The comprehensive recovery and treatment method of the cobalt-sulfur concentrate is characterized in that the roasting temperature of the cobalt-sulfur concentrate in the step 1) is 800-950 ℃, the cooling temperature of the roasted sand is 240-260 ℃, preferably 250 ℃, and the granularity and the mesh number in the fine material are less than 150 meshes and account for more than 90 percent.
The comprehensive recovery processing method of the cobalt-sulfur concentrate is characterized in that when the finely ground material in the step 1) is slurried, the liquid-solid ratio is 3-5:1, saturated steam is introduced in the slurrying process to raise the temperature, and the slurrying end point temperature is controlled to be 70-80 ℃.
The comprehensive recovery processing method of the cobalt-sulfur concentrate is characterized in that saturated steam is introduced into the selective leaching in the step 2), so that the selective leaching temperature is 130-150 ℃, and oxygen is introduced at the same time, wherein the pressure is 1.3-1.5 MPa.
The comprehensive recovery processing method of the cobalt-sulfur concentrate is characterized in that a copper extracting agent adopted by a copper extracting system in the step 3) is lix984n, after extraction, an organic phase is subjected to back extraction by using a solution after electrodeposition or an acid solution containing 95-100g/L of sulfuric acid, so that copper in the organic phase enters the solution, the copper is enriched, the copper-rich solution containing copper is controlled to be more than 30g/L after the back extraction, and the copper content of a raffinate is controlled to be less than 0.2 g/L.
The comprehensive recovery treatment method for the cobalt-sulfur concentrate is characterized in that the reaction conditions of a cyclone electric-deposition system in the step 4) are as follows: the current density is 400-550A/square meter, and the reaction endpoint is that copper contained in the solution after electrodeposition is less than 8 g/L.
The comprehensive recovery processing method of the cobalt-sulfur concentrate is characterized in that the PH value of the end point of the cobalt precipitation reaction in the step 5) is 8-9, and the cobalt content in the cobalt precipitation filtrate is less than 0.03 g/L.
The comprehensive recovery treatment method of the cobalt-sulfur concentrate is characterized in that the pH value of a reaction solution at the end point of magnesium precipitation reaction in the step 5) is 10-12, and the pH value is preferably 11.
Compared with the prior art, the invention has the following beneficial effects:
1) according to the invention, cobalt-sulfur concentrate is treated by adopting a comprehensive treatment process combining a pyrogenic process and a wet process, pyrogenic desulphurization is adopted, structural form conversion of cobalt and copper is realized, the wet process adopts continuous pressure leaching, the cobalt and copper are completely leached at high temperature and high pressure, copper and cobalt are recycled by stages in a subsequent process, and leached slag and calcium-magnesium slag are properly treated, the process has the greatest advantage of ensuring high recovery rate of cobalt and copper, including treatment of low-grade cobalt-sulfur concentrate, so that the maximum utilization of resources is realized, and the problems of low recovery rate of cobalt and low-grade cobalt-sulfur concentrate treatment cost existing in the prior art are effectively solved;
2) the invention simultaneously considers the reasonable treatment and the reutilization of the waste gas, the waste residue and the waste water, the sulfur dioxide flue gas generated by the pyrogenic process is used for preparing acid, the obtained sulfuric acid is completely used for production, the produced waste residue is subjected to harmless treatment, and the produced waste water can be recycled, so the whole process is environment-friendly, energy-saving and consumption-reducing;
3) according to the system, the copper-containing leachate is treated by adopting the cyclone electrolysis technology, and the advantages of selective electrodeposition and deep copper removal of the cyclone electrodeposition technology are utilized, so that the electrode copper is extracted from the copper-containing leachate in one step, and meanwhile, the technology has low requirement on the copper concentration in the initial feed liquid, can carry out deep copper removal and has high direct copper yield;
4) in the invention, the raffinate phase is subjected to cobalt precipitation reaction by using magnesium oxide with mild alkalinity as a precipitator, so that the precipitation of other metal impurities can be avoided while cobalt precipitation is ensured, the cobalt content in the cobalt precipitation slag is improved, the process is reasonable, the magnesium oxide is cheap and easy to obtain, and the treatment cost is low.
Drawings
FIG. 1 is a schematic view of a process flow diagram of an embodiment of the present invention.
Detailed Description
The technical solution of the present invention is illustrated by the following specific examples, but the scope of the present invention is not limited thereto:
as shown in the figure, the comprehensive recovery processing method of the cobalt-sulfur concentrate comprises the following steps:
1) performing oxidizing boiling roasting on the cobalt-sulfur concentrate, wherein the roasting temperature of the cobalt-sulfur concentrate is 800-950 ℃, and metal sulfide in the cobalt-sulfur concentrate is converted into oxide to obtain roasted sand and SO2Recovering heat generated in the roasting process from flue gas; SO (SO)2The flue gas is purified and dedusted and then enters a flue gas acid making system to make acid; cooling the roasted sand, performing ball milling to obtain fine particles, and performing slurrying and presoaking on the fine particles to obtain a presoaking mixed solution, wherein the cooling temperature of the roasted sand is 240-260 ℃, the preferable temperature is 250 ℃, and the particle size number of the fine material is less than 150 meshes and accounts for more than 90%;
2) transferring the pre-soaking mixed solution obtained in the step 1) into a continuous pressure leaching system for continuous selective leaching to obtain slurry, and introducing saturated steam into the selective leaching system to ensure that the selective leaching temperature is 130-150 ℃, and simultaneously introducing oxygen under the pressure of 1.3-1.5 MPa; the slurry is pre-neutralized by lime milk pulp, the reaction liquid after pre-neutralization is subjected to solid-liquid separation by a concentration separator to obtain supernatant and filter residue, most iron enters the filter residue in the form of hematite, cobalt and copper are leached by acid and enter the solution to become cobalt and copper sulfate solution in the supernatant, and the filter residue is subjected to concentration countercurrent washing by water to obtain washing liquid and washed residue; enabling the supernatant to enter the next extraction procedure, returning the washing liquid to the slurrying liquid to slurry and presoaked the calcine obtained in the step 1), conveying the washed slag to a tailing neutralizing tank for neutralization treatment, and discharging;
3) cooling the supernatant obtained in the step 2), then carrying out fine filtration, allowing the obtained fine-filtered liquid to enter a copper extraction system for extraction, separating copper from cobalt in the solution, enriching the copper into a copper sulfate solution, and treating raffinate, wherein a copper extraction agent adopted by the copper extraction system is lix984n, after extraction, carrying out back extraction on an organic phase by using an electrodeposition liquid or an acid liquid containing 95-100g/L of sulfuric acid, allowing the copper in the organic phase to enter the solution, so as to enrich the copper, controlling the copper-enriched liquid after the back extraction to contain more than 30g/L, and controlling the copper content of the raffinate to be less than 0.2 g/L;
4) enabling the copper sulfate solution in the step 3) to enter a cyclone electrodeposition system, performing cyclone electrolysis to obtain No. 1 cathode copper and an electrodeposited liquid, mixing the electrodeposited liquid with the washing liquid in the step 1), returning the slurry liquid to perform slurry pre-impregnation on the calcine in the step 1), wherein the current density of the cyclone electrolysis is 400-550A/square meter, and the reaction end point is that the copper content in the electrodeposited liquid is less than 8 g/L;
5) allowing the raffinate obtained in the step 3) to enter a cobalt precipitation process, performing cobalt precipitation by using magnesium oxide slurry as a precipitator, precipitating and separating cobalt from the slurry after the cobalt is converted into cobalt hydroxide, and performing flash evaporation, drying and dehydration on the cobalt hydroxide to obtain a crude cobalt hydroxide product, wherein the separated slurry is a magnesium sulfate solution; the PH value of the end point of the cobalt precipitation reaction is 8-9, and the cobalt content in the cobalt precipitation filtrate is less than 0.03 g/L;
6) the magnesium sulfate solution in the step 5) enters a magnesium precipitation process, lime milk pulp is used as a precipitator, magnesium hydroxide and calcium sulfate precipitation are generated by magnesium precipitation, solid-liquid separation is carried out on the slurry after precipitation, and solid materials are calcium-magnesium residues and are sent to a slag yard for storage; the filtrate is recovered and used for wet grinding of a ball mill, slurrying of lime and magnesium oxide, and the pH value of the reaction liquid at the end of the magnesium precipitation reaction is 10-12, preferably 11.
Example 1: the invention relates to a comprehensive recovery processing method of cobalt-sulfur concentrate, the technological process of which is shown in figure 1, and the method comprises the following steps:
1) roasting the cobalt-sulfur concentrate in a fluidized bed roaster, using diesel oil as fuel, blowing oxygen-enriched air to support combustion, controlling the temperature in the roaster at 800-950 ℃ to obtain calcine and SO2Flue gas, SO2The method comprises the steps of using waste heat of flue gas for producing steam in a boiler, purifying the steam to prepare acid, cooling roasted calcine to 250 ℃, grinding the calcine by using a wet ball mill, mixing the ground fine material with more than 94% of granularity less than 150 meshes in a mass ratio of 4:1, pulping, stirring, introducing saturated steam for pre-leaching, and obtaining pre-leaching mixed solution after the temperature of reaction liquid is raised to 80 ℃ and the reaction is finished;
2) transferring the pre-soaking mixed liquor obtained in the step 1) into a pressure kettle, introducing saturated steam and oxygen, performing selective leaching reaction at the temperature of 140 ℃ and under the pressure of 1.3MPa in the pressure kettle, allowing the pre-soaking mixed liquor to stay in the pressure kettle for about 5 hours, adding lime milk into the produced slurry for pre-neutralization, adjusting the pH value of the feed liquid to 3.0, performing solid-liquid separation by using a concentration separator to obtain supernatant and filter residue, allowing most iron to enter the filter residue in the form of hematite, leaching cobalt copper into the solution by acid to obtain a cobalt copper sulfate solution, controlling the mass content of solids in the filter residue to be more than 25%, controlling the mass content of the solids in the supernatant to be less than 5%, and performing concentrated countercurrent washing on the obtained filter residue by using clear water to obtain washing liquid and washing residue; the supernatant fluid enters the next extraction procedure, the washing liquid is used as slurrying liquid and returns to the step 1) for slurrying and pre-dipping treatment of the calcine, and the washed slag is conveyed to a tailing neutralizing tank for neutralizing treatment and then discharged;
3) cooling the supernatant obtained in the step (2), then carrying out fine filtration, allowing the obtained fine-filtered liquid to enter a copper extraction system for copper extraction, separating copper from cobalt in the solution, standing and layering to obtain a raffinate phase and a copper extraction load organic phase, wherein copper is enriched into a copper sulfate solution, and the copper content of a raffinate is less than 0.2 g/L; washing the obtained copper extraction loaded organic by dilute sulfuric acid of about 10g/L, and performing back extraction on sulfuric acid solution of about 100g/L or the solution after electrodeposition to obtain copper sulfate back extraction solution, wherein the copper content of the back extraction solution is controlled to be more than 30 g/L;
4) enabling the strip liquor obtained in the step 3) to enter a rotational flow electrodeposition system to realize selective electrodeposition, eliminating concentration polarization in the electrodeposition process, improving the direct recovery rate of copper, controlling the current density to be 400-550A/square meter during electrodeposition, carrying out electrodeposition reaction to obtain 1# cathode copper and post-electrodeposition liquor, and when the copper content in the post-electrodeposition liquor is less than 8g/L, recovering the post-electrodeposition liquor and returning the post-electrodeposition liquor to the step (1) to be used as slurry liquor to pre-slurry the calcine;
5) adding MgO into the raffinate phase obtained in the step 3), performing cobalt precipitation reaction, when the PH value of the reaction liquid is 8.5, converting cobalt into cobalt hydroxide, precipitating from slurry, after the reaction is finished, performing solid-liquid separation to obtain cobalt precipitation filtrate and solid materials, controlling the cobalt content in the cobalt precipitation filtrate to be less than 0.03g/L, performing flash evaporation drying on the obtained solid materials to obtain a finished product cobalt hydroxide crude product, and directly selling the finished product cobalt hydroxide crude product, wherein the separated cobalt precipitation filtrate is a magnesium sulfate solution;
6) adding lime milk into the cobalt precipitation filtrate obtained in the step 5), taking the lime milk as a precipitator, carrying out magnesium precipitation reaction, finishing the magnesium precipitation reaction when the pH value of the reaction liquid is 11, carrying out solid-liquid separation on the reaction liquid, and sending the obtained solid materials, namely magnesium hydroxide and calcium sulfate products, to a slag yard for storage; the filtrate was recovered and used for wet milling in a ball mill, slurrying of lime, magnesium oxide.
An example of a production project, a daily capacity of 800t/d of cobalt-sulphur concentrate feed, was processed as described in example 1, and the cobalt-sulphur concentrate feed had the following composition as shown in table 1 below:
table 1 cobalt sulphur concentrate raw material chemical composition (%)
Through the process treatment, 9400T/a standard cathode copper is produced in years, the product quality meets the national standard (GB/T467-1997), and the quality standard is shown in Table 2; 30 percent of crude cobalt hydroxide is produced annually at 15600t/a, the main chemical components of the crude cobalt hydroxide are shown in Table 3, the cobalt content is 4690t/a, and the total yield of copper and cobalt is 89.37 percent and 88.85 percent respectively. Compared with the conventional process, the method has the advantages of higher total yield of copper and cobalt and better recovery effect.
TABLE 299.95 Standard cathode copper quality standards (%)
15600T/a of crude cobalt hydroxide produced in the year, the cobalt content is more than or equal to 30 percent, the cobalt metal content is 4690T/a, the quality of the crude cobalt hydroxide product meets the YS/T1152-one 2016 industrial standard, and the main chemical components are shown in the table.
TABLE 3 crude cobalt hydroxide main chemical composition (%)
Remarking: the oxide of cobalt in the crude cobalt hydroxide can not be more than 1 percent, and the water content of the first-grade crude cobalt hydroxide, the second-grade crude cobalt hydroxide is not more than 30 percent.
The implementation of the invention described in this specification is merely a list of implementation forms of the inventive concept and the scope of protection should not be considered as limited to the specific forms set forth in the examples, but also as equivalent technical means as can be conceived by one skilled in the art based on the inventive concept.
Claims (7)
1. A comprehensive recovery processing method of cobalt-sulfur concentrate is characterized by comprising the following steps:
1) oxidizing, boiling and roasting the cobalt-sulfur concentrate to convert metal sulfide in the cobalt-sulfur concentrate into oxide to obtain roasted sand and SO2Recovering heat generated in the roasting process from flue gas; SO (SO)2The flue gas is purified and dedusted and then enters a flue gas acid making system to make acid; cooling the roasted sand, ball-milling to obtain fine particles, slurrying and presoaking the fine particles to obtain presoaked mixed solution, roasting the cobalt-sulfur concentrate at the temperature of 800-950 ℃, cooling the roasted sand at the temperature of 240-260 ℃, and fine-grindingWhen the post-material is pulped, introducing saturated steam in the pulping process to heat up, and controlling the pulping end point temperature to be 70-80 ℃;
2) transferring the pre-soaking mixed solution obtained in the step 1) into a continuous pressure leaching system for continuous selective leaching to obtain slurry, carrying out pre-neutralization on the slurry by lime milk pulp, carrying out solid-liquid separation on reaction liquid after pre-neutralization by a concentration separator to obtain supernatant and filter residue, allowing most of iron to enter the filter residue in the form of hematite, carrying out acid leaching on cobalt and copper to enter the solution to become a cobalt and copper sulfate solution in the supernatant, and carrying out concentrated countercurrent washing on the filter residue by water to obtain washing liquid and washed residue; enabling the supernatant to enter the next extraction procedure, returning the washing liquid as a slurrying liquid to the step 1) for slurrying and pre-dipping the calcine, conveying washed slag to a tailing neutralizing tank for neutralizing treatment and then discharging, introducing saturated steam into selective leaching, enabling the temperature of the selective leaching to be 130-150 ℃, and introducing oxygen at the same time, wherein the pressure is 1.3-1.5 MPa;
3) cooling the supernatant obtained in the step 2), then carrying out fine filtration, and allowing the obtained fine-filtered liquid to enter a copper extraction system for extraction so as to separate copper from cobalt in the solution, wherein the copper is enriched into a copper sulfate solution, and the raffinate is to be treated;
4) enabling the copper sulfate solution in the step 3) to enter a rotational flow electrodeposition system, performing rotational flow electrolysis to obtain 1# cathode copper and a post-electrodeposition solution, mixing the post-electrodeposition solution with the washing solution in the step 1), and returning the mixture to a slurry solution to perform slurry pre-impregnation on the calcine in the step 1);
5) allowing the raffinate obtained in the step 3) to enter a cobalt precipitation process, performing cobalt precipitation by using magnesium oxide slurry as a precipitator, precipitating and separating cobalt from the slurry after the cobalt is converted into cobalt hydroxide, and performing flash evaporation, drying and dehydration on the cobalt hydroxide to obtain a crude cobalt hydroxide product, wherein the separated slurry is a magnesium sulfate solution;
6) the magnesium sulfate solution in the step 5) enters a magnesium precipitation process, lime milk pulp is used as a precipitator, magnesium hydroxide and calcium sulfate precipitation are generated by magnesium precipitation, solid-liquid separation is carried out on the slurry after precipitation, and solid materials are calcium-magnesium residues and are sent to a slag yard for storage; the filtrate was recovered and used for wet milling in a ball mill, slurrying of lime, magnesium oxide.
2. The comprehensive recovery and treatment method of cobalt-sulfur concentrate according to claim 1, characterized in that the cooling temperature of the calcine in step 1) is 250 ℃, and the grain size of the fine material is less than 150 meshes and accounts for more than 90%.
3. The method as claimed in claim 1, wherein the copper extractant used in the copper extraction system in step 3) is lix984n, and after extraction, the organic phase is stripped with the solution after electrodeposition or with the acid solution containing 95-100g/L sulfuric acid, so that the copper in the organic phase enters the solution, thereby enriching the copper, and the copper-enriched solution after stripping is controlled to contain copper >30g/L, and the raffinate contains copper <0.2 g/L.
4. The comprehensive recovery and treatment method of cobalt-sulfur concentrate according to claim 1, wherein the reaction conditions of the cyclone current-driven system in step 4) are as follows: the current density is 400-550A/m2The end point of the reaction is copper contained in the solution after electrodeposition<8g/L。
5. The comprehensive recovery and treatment method of cobalt-sulfur concentrate according to claim 1, wherein the pH value of the end point of the cobalt precipitation reaction in step 5) is 8-9, and the cobalt content in the cobalt precipitation filtrate is less than 0.03 g/L.
6. The comprehensive recovery and treatment method of cobalt-sulfur concentrate according to claim 1, wherein the pH value of the reaction solution at the end of the magnesium precipitation reaction in step 6) is 10-12.
7. The comprehensive recovery and treatment method of cobalt-sulfur concentrate according to claim 1, wherein the pH value of the reaction solution at the end of the magnesium precipitation reaction in step 6) is 11.
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| CN109852792A (en) * | 2019-03-30 | 2019-06-07 | 赣州逸豪优美科实业有限公司 | A kind of copper cobalt ore prepares the processing technology of cobalt hydroxide |
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| CN113789441B (en) * | 2021-08-06 | 2023-05-05 | 湖南德景源科技有限公司 | Combined leaching process of cobalt-sulfur concentrate and cobalt hydroxide ore |
| CN113955811A (en) * | 2021-10-21 | 2022-01-21 | 北方矿业有限责任公司 | Method for producing crude cobalt hydroxide from industrial cobalt-containing low-copper raffinate |
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