CN101898802A - Method for extracting cobalt from low-grade cobalt residue to produce cobalt chloride - Google Patents
Method for extracting cobalt from low-grade cobalt residue to produce cobalt chloride Download PDFInfo
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- CN101898802A CN101898802A CN 201010235351 CN201010235351A CN101898802A CN 101898802 A CN101898802 A CN 101898802A CN 201010235351 CN201010235351 CN 201010235351 CN 201010235351 A CN201010235351 A CN 201010235351A CN 101898802 A CN101898802 A CN 101898802A
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Abstract
The invention discloses a method for extracting cobalt from low-grade cobalt residue to produce cobalt chloride. The method comprises the steps of reduction leaching cobalt residue generated by oxidizing, hydrolyzing, precipitating and removing cobalt, performing P204 extraction edulcoration and P507 nickel-cobalt separation, evaporating and crystallizing to produce crystallization cobalt chloride. The invention has the characteristics of simple process path, less investment, low energy consumption, low operation cost, no environmental pollution, high cobalt and nickel leaching rate, convenient operation, low production cost, and the like. Accordingly, the invention provides an extremely effective, economical and applicable way for developing and utilizing the chemical low-grade cobalt residue with complex chemical composition.
Description
Technical field
The present invention relates to from the low-grade cobalt residue of complex chemical composition to extract the method for cobalt production cobalt chloride, especially a kind ofly remove reduction of dissolved the cobalt slag that cobalt produces from oxidation, hydrolytic precipitation, abstraction impurity removal, the nickel cobalt separates, the method for evaporative crystallization production cobalt chloride.
Background technology
The content of cobalt is 0.0018% in the earth's crust, has verified land cobalt reserves and has been about 1,000 ten thousand t, mainly is present in nickel, copper, iron or the silver ore with the associated element form, and independent cobalt deposits only accounts for 5% of reserves.The cobalt of association in nickel sulfide ore is the main cobalt ore resource of China.Cobalt grade in ore is lower, only is 0.03%～0.05%, composes with the isomorph form to be stored in nickel, copper sulfurized ore and the pyrite, can't become cobalt concentrate with the beneficiation method enrichment, generally makes it be enriched in certain slag in putting forward the nickel process and is difficult to reclaim cobalt.Therefore, how to leach the low-grade cobalt residue of complex chemical composition, cobalt changes solution over to, removes various impurity, fully reclaims, utilizes limited resources, has become the main goal in research of scientific research personnel.For this reason, the present inventor has invented the method that effective processing changes into low-grade cobalt residue through concentrating on studies for many years and many times test.
Summary of the invention
For overcoming the deficiency that prior art is difficult to handle low-grade cobalt residue, it is little to the invention provides a kind of investment, and technology is simple, and energy consumption is low, and production cost is low, extracts the method for cobalt production cobalt chloride in the high cobalt slag of cobalt nickel recovery.
Purpose of the present invention is achieved through the following technical solutions, and a kind of method from low-grade cobalt residue extraction cobalt production cobalt chloride may further comprise the steps:
A, get oxydrolysis precipitation and remove the cobalt slag that cobalt produces, calculate by quality ratio, press the cobalt slag: water: sulfuric acid: reductive agent=1: 5: 0.5: 0.4 mixes, agitation leach 2～3 hours, after-filtration is finished in leaching, with residue washing, filtrate and washing water merge as leaching filtrate then, and the filter residue after the washing abandons;
B, the leaching filtrate that steps A is obtained are adopted P204 to carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and are removed impurity, obtain P204 raffinate, washings, strip liquor and back extraction iron liquid, P204 raffinate and washings are merged, strip liquor, back extraction iron liquid are got rid of;
C, P204 raffinate, washings are carried out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid with P507, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, P507 raffinate and washings are merged, reclaim nickel, with P507 back extraction iron liquid removal system;
D, with P507 strip liquor evaporative crystallization, centrifugal, obtain CoCl
26H
2O.
The cobalt amount that contains of cobalt slag is 5% in the described steps A.
Reductive agent described in the steps A is S-WAT or hydrogen peroxide.
Described P204 is phosphonic acids (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P204 is 18%.
Described P507 is 2-ethylhexyl phosphoric acid list (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P507 is 18%.
It is to carry out in the steel basin that opens wide that the reduction of described steps A is leached.
The present invention compared with prior art has following beneficial effect: adopt such scheme, can from the cobalt slag of low-grade complex chemical composition, leach by reduction, the P204 abstraction impurity removal, P507 nickel cobalt separates, evaporative crystallization production crystallization cobalt chloride, its industrial scale is changeable, and raw material resources utilize scope wide, need not big investment and treatment facility, it is simple that the present invention has a processing route, invest for a short time, energy consumption is low, working cost, free from environmental pollution, cobalt, nickel leaching yield height, easy and simple to handle, characteristics such as production cost is low.Thereby, for the development and use of the chemical low-grade cobalt residue of complex chemical composition provide very effective and affordable approach.
Following table has provided the main economic and technical norms that suitable low-grade cobalt residue of the present invention is extracted cobalt production crystallization cobalt chloride:
| Sequence number | Project name | Index | Sequence number | Project name | Index |
| 1 | The cobalt leaching yield | 99％ | 10 | The P507 saponification degree | 60％ |
| 2 | Leach liquor contains cobalt | 10g/L | 11 | Evaporating pressure (vacuum tightness) | 0.06MPa |
| 3 | Leach liquor PH | 2.0 | 12 | Vaporization temperature | 70～75℃ |
| 4 | Extraction temperature | 70～80℃ | 13 | The crystallization terminal temperature | 38℃ |
| 5 | Leach liquid-solid ratio | 5∶1 | 14 | Steam consumption | 20t/tCoCl 2·6H 2O |
| 6 | Extraction time | 2～3 hours | 15 | Power consumption | 2800kwh/tCoCl 2 ·6H 2O |
| 7 | The P204 extraction phase is than (O: A) | 1∶1 | 16 | The water consumption | 15m 3/tCoCl 2·6 H 2O |
| 8 | The P204 saponification degree | 60％ | 17 | Production cost | 15000 yuan/tCoCl 2·6H 2O |
| 9 | The P507 extraction phase is than (O: A) | 1∶1 |
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Embodiment
The process flow diagram of Fig. 1 has embodied overall flow of the present invention, and according to this figure, the method that the present invention extracts cobalt production cobalt chloride from low-grade cobalt residue specifically comprises following step:
A, get oxydrolysis precipitation and remove the cobalt slag that cobalt produces, calculate by quality ratio, press the cobalt slag: water: sulfuric acid: reductive agent=1: 5: 0.5: 0.4 mixes, agitation leach 2～3 hours, after finishing, leaching carries out twice filtration, with residue washing, filtrate and washing water merge as leaching filtrate then, and the filter residue after the washing abandons;
B, the leaching filtrate that steps A is obtained are adopted P204 to carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and are removed impurity, obtain P204 raffinate, washings, strip liquor and back extraction iron liquid, P204 raffinate and washings are merged, strip liquor, back extraction iron liquid are got rid of;
C, P204 raffinate, washings are carried out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid with P507, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, P507 raffinate and washings are merged, reclaim nickel, with P507 back extraction iron liquid removal system;
D, with P507 strip liquor evaporative crystallization, centrifugal, obtain CoCl
26H
2O.
Below in conjunction with specific embodiment the present invention is described further.
Embodiment 1
A, at 20m
3Add 15m in the steel basin
3Water, the cobalt slag that contains cobalt 5% drops into 3t, sulfuric acid 1.5t, S-WAT 1.2t, heating keeps 70 ℃, agitation leach 2 hours.
B, the material after will leaching filter through 2 times, collect filtrate, then filter residue is added water washing after, filter residue contains cobalt≤0.18%, directly abandons.
The filtrate of C, step B and washing water merge, and obtain leaching filtrate.
D, leach filtrate and adopt P204[phosphonic acids (2-ethylhexyl) fat] carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and remove most of impurity, obtain P204 raffinate, washings, strip liquor, back extraction iron liquid.Raffinate and washings are merged strip liquor, back extraction iron liquid removal system.
E, P204 raffinate, washings are with P507[2-ethylhexyl phosphoric acid list (2-ethylhexyl) fat] carry out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, raffinate and washings are merged, reclaim nickel, back extraction iron liquid removal system.
F, P507 strip liquor evaporative crystallization, centrifugal obtain CoCl
26H
2O.Cobalt chloride contains cobalt 〉=24%, meets industry standard.
Embodiment 2
A, at 20m
3Add 15m in the steel basin
3Water, the cobalt slag that contains cobalt 5% drops into 3t, sulfuric acid 1.5t, S-WAT 1.2t, heating keeps 80 ℃, agitation leach 3 hours.
B, the material after will leaching filter through 2 times, collect filtrate, then filter residue is added water washing after, filter residue contains cobalt≤0.13%, directly abandons.
The filtrate of C, step B and washing water merge, and obtain leaching filtrate.
D, leach filtrate and adopt P204[phosphonic acids (2-ethylhexyl) fat] carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and remove most of impurity, obtain P204 raffinate, washings, strip liquor, back extraction iron liquid.Raffinate and washings are merged strip liquor, back extraction iron liquid removal system.
E, P204 raffinate, washings are with P507[2-ethylhexyl phosphoric acid list (2-ethylhexyl) fat] carry out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, raffinate and washings are merged, reclaim nickel, back extraction iron liquid removal system.
F, P507 strip liquor evaporative crystallization, centrifugal obtain CoCl
26H
2O.Cobalt chloride contains cobalt 〉=24%, meets industry standard.
Embodiment 3
A, at 20m
3Add 15m in the steel basin
3Water, the cobalt slag that contains cobalt 5% drops into 3t, sulfuric acid 1.5t, hydrogen peroxide 1.2t, heating keeps 75 ℃, agitation leach 2.5 hours.
B, the material after will leaching filter through 2 times, collect filtrate, then filter residue is added water washing after, filter residue contains cobalt≤0.15%, directly abandons.
The filtrate of C, step B and washing water merge, and obtain leaching filtrate.
D, leach filtrate and adopt P204[phosphonic acids (2-ethylhexyl) fat] carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and remove most of impurity, obtain P204 raffinate, washings, strip liquor, back extraction iron liquid.Raffinate and washings are merged strip liquor, back extraction iron liquid removal system.
E, P204 raffinate, washings are with P507[2-ethylhexyl phosphoric acid list (2-ethylhexyl) fat] carry out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, raffinate and washings are merged, reclaim nickel, back extraction iron liquid removal system.
F, P507 strip liquor evaporative crystallization, centrifugal obtain CoCl
26H
2O.Cobalt chloride contains cobalt 〉=24%, meets industry standard.
Embodiment 4
Present embodiment carries out according to following steps:
A, get oxydrolysis precipitation and remove the cobalt slag that cobalt produces, requiring the cobalt amount that contains of this cobalt slag is 5%, in the steel basin that opens wide, calculate by quality ratio, press the cobalt slag: water: sulfuric acid: S-WAT=1: 5: 0.5: 0.4 mixes agitation leach 2 hours, after-filtration is finished in leaching, with residue washing, filtrate and washing water merge as leaching filtrate then, and the filter residue after the washing abandons;
B, the leaching filtrate that steps A is obtained are adopted P204 to carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and are removed impurity, obtain P204 raffinate, washings, strip liquor and back extraction iron liquid, P204 raffinate and washings are merged, strip liquor, back extraction iron liquid are got rid of; Above-mentioned P204 is phosphonic acids (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P204 is 18%;
C, P204 raffinate, washings are carried out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid with P507, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, P507 raffinate and washings are merged, reclaim nickel, with P507 back extraction iron liquid removal system; Described P507 is 2-ethylhexyl phosphoric acid list (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P507 is 18%;
D, with P507 strip liquor evaporative crystallization, centrifugal, obtain CoCl
26H
2O.
Embodiment 5
Present embodiment carries out according to following steps:
A, get oxydrolysis precipitation and remove the cobalt slag that cobalt produces, requiring the cobalt amount that contains of this cobalt slag is 5%, in the steel basin that opens wide, calculate by quality ratio, press the cobalt slag: water: sulfuric acid: hydrogen peroxide=1: 5: 0.5: 0.4 mixes agitation leach 3 hours, after-filtration is finished in leaching, with residue washing, filtrate and washing water merge as leaching filtrate then, and the filter residue after the washing abandons;
B, the leaching filtrate that steps A is obtained are adopted P204 to carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and are removed impurity, obtain P204 raffinate, washings, strip liquor and back extraction iron liquid, P204 raffinate and washings are merged, strip liquor, back extraction iron liquid are got rid of; Above-mentioned P204 is phosphonic acids (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P204 is 18%;
C, P204 raffinate, washings are carried out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid with P507, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, P507 raffinate and washings are merged, reclaim nickel, with P507 back extraction iron liquid removal system; Described P507 is 2-ethylhexyl phosphoric acid list (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P507 is 18%;
D, with P507 strip liquor evaporative crystallization, centrifugal, obtain CoCl
26H
2O.
Claims (6)
1. the method from low-grade cobalt residue extraction cobalt production cobalt chloride is characterized in that, may further comprise the steps:
A, get oxydrolysis precipitation and remove the cobalt slag that cobalt produces, calculate by quality ratio, press the cobalt slag: water: sulfuric acid: reductive agent=1: 5: 0.5: 0.4 mixes, agitation leach 2～3 hours, after-filtration is finished in leaching, with residue washing, filtrate and washing water merge as leaching filtrate then, and the filter residue after the washing abandons;
B, the leaching filtrate that steps A is obtained are adopted P204 to carry out 10 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 4 grades of back extractions of 0.5mol/L sulfuric acid, 4 grades of washed metals of 6mol/L hydrochloric acid and are removed impurity, obtain P204 raffinate, washings, strip liquor and back extraction iron liquid, P204 raffinate and washings are merged, strip liquor, back extraction iron liquid are got rid of;
C, P204 raffinate, washings are carried out 8 grades of extractions, 4 grades of washings of 0.25mol/L sulfuric acid, 6 grades of back extractions of 2.5mol/L hydrochloric acid, 4 grades of washed metals of 6mol/L hydrochloric acid with P507, realize that the nickel cobalt separates, obtain P507 raffinate, washings, strip liquor, back extraction iron liquid, P507 raffinate and washings are merged, reclaim nickel, with P507 back extraction iron liquid removal system;
D, with P507 strip liquor evaporative crystallization, centrifugal, obtain CoCl
26H
2O.
2. according to claims 1 described method from low-grade cobalt residue extraction cobalt production cobalt chloride, it is characterized in that: by quality ratio, the cobalt amount that contains of cobalt slag is 5% in the described steps A.
3. according to claims 1 described method from low-grade cobalt residue extraction cobalt production cobalt chloride, it is characterized in that: the reductive agent described in the steps A is S-WAT or hydrogen peroxide.
4. according to claims 1 described method from low-grade cobalt residue extraction cobalt production cobalt chloride, it is characterized in that: described P204 is phosphonic acids (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P204 is 18%.
5. according to claims 1 described method from low-grade cobalt residue extraction cobalt production cobalt chloride, it is characterized in that: described P507 is 2-ethylhexyl phosphoric acid list (2-ethylhexyl) fat, adopts the dissolving of 260# solvent oil, and the concentration of P507 is 18%.
6. according to claims 1 described method from low-grade cobalt residue extraction cobalt production cobalt chloride, it is characterized in that: it is to carry out in the steel basin that opens wide that described steps A reduction is leached.
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104743614A (en) * | 2013-12-30 | 2015-07-01 | 北京当升材料科技股份有限公司 | A preparing method of a cobalt chloride solution |
| CN105154683A (en) * | 2015-08-20 | 2015-12-16 | 湖南世纪垠天新材料有限责任公司 | Method for separating and recycling valuable metal in tungsten slag |
| CN107720837A (en) * | 2017-09-28 | 2018-02-23 | 上海至铂环保科技服务有限公司 | The method that nickel protoxide is prepared with waste nickel catalyst |
| CN108517403A (en) * | 2018-06-30 | 2018-09-11 | 贵州中伟资源循环产业发展有限公司 | A kind of method of metallic cobalt battery grade cobalt sulfate |
| CN108677009A (en) * | 2018-05-21 | 2018-10-19 | 兰州金川新材料科技股份有限公司 | A kind of depth abstraction impurity removal method of cobalt chloride solution |
| CN109706328A (en) * | 2019-01-31 | 2019-05-03 | 金驰能源材料有限公司 | A kind of method of metallic nickel acid dissoluting liquid back extraction load nickel cobalt manganese organic phase preparation ternary feed liquid |
| CN110894577A (en) * | 2019-09-10 | 2020-03-20 | 曾纪斌 | Method for improving leaching rate of zinc-cobalt slag produced by purifying electrolytic zinc solution |
| CN113046574A (en) * | 2021-03-17 | 2021-06-29 | 沈阳有色金属研究院有限公司 | Method for preparing high-purity nickel and cobalt products by treating crude cobalt hydroxide with copper electrolysis decoppering post-treatment solution |
| CN113044889A (en) * | 2021-03-11 | 2021-06-29 | 浙江中金格派锂电产业股份有限公司 | Co-production process of cobalt sulfate and cobalt chloride |
| CN113474069A (en) * | 2019-03-26 | 2021-10-01 | 住友金属矿山株式会社 | Method for producing a solution containing nickel and cobalt from a nickel and cobalt-containing hydroxide |
| CN115321604A (en) * | 2022-07-29 | 2022-11-11 | 格林美（江苏）钴业股份有限公司 | Method for removing phosphorus in cobalt chloride solution by using iron oxide yellow |
| CN116903051A (en) * | 2023-07-13 | 2023-10-20 | 科立鑫(珠海)新能源有限公司 | Method for producing cobalt chloride by using low-grade cobalt slag |
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| 《有色金属（冶炼部分）》 20021231 周炳珍 用P204和P507脱除含钴废料中的杂质生产高纯度氯化钴 16、17、44 1-6 , 第6期 2 * |
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Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104743614A (en) * | 2013-12-30 | 2015-07-01 | 北京当升材料科技股份有限公司 | A preparing method of a cobalt chloride solution |
| CN105154683A (en) * | 2015-08-20 | 2015-12-16 | 湖南世纪垠天新材料有限责任公司 | Method for separating and recycling valuable metal in tungsten slag |
| CN105154683B (en) * | 2015-08-20 | 2017-05-17 | 湖南世纪垠天新材料有限责任公司 | Method for separating and recycling valuable metal in tungsten slag |
| CN107720837A (en) * | 2017-09-28 | 2018-02-23 | 上海至铂环保科技服务有限公司 | The method that nickel protoxide is prepared with waste nickel catalyst |
| CN107720837B (en) * | 2017-09-28 | 2019-07-30 | 上海至铂环保科技服务有限公司 | The method for preparing nickel protoxide with waste nickel catalyst |
| CN108677009A (en) * | 2018-05-21 | 2018-10-19 | 兰州金川新材料科技股份有限公司 | A kind of depth abstraction impurity removal method of cobalt chloride solution |
| CN108517403A (en) * | 2018-06-30 | 2018-09-11 | 贵州中伟资源循环产业发展有限公司 | A kind of method of metallic cobalt battery grade cobalt sulfate |
| CN109706328A (en) * | 2019-01-31 | 2019-05-03 | 金驰能源材料有限公司 | A kind of method of metallic nickel acid dissoluting liquid back extraction load nickel cobalt manganese organic phase preparation ternary feed liquid |
| CN113474069A (en) * | 2019-03-26 | 2021-10-01 | 住友金属矿山株式会社 | Method for producing a solution containing nickel and cobalt from a nickel and cobalt-containing hydroxide |
| CN110894577A (en) * | 2019-09-10 | 2020-03-20 | 曾纪斌 | Method for improving leaching rate of zinc-cobalt slag produced by purifying electrolytic zinc solution |
| CN110894577B (en) * | 2019-09-10 | 2022-04-01 | 广东利昌新材料有限公司 | Method for improving leaching rate of zinc-cobalt slag produced by purifying electrolytic zinc solution |
| CN113044889A (en) * | 2021-03-11 | 2021-06-29 | 浙江中金格派锂电产业股份有限公司 | Co-production process of cobalt sulfate and cobalt chloride |
| CN113046574A (en) * | 2021-03-17 | 2021-06-29 | 沈阳有色金属研究院有限公司 | Method for preparing high-purity nickel and cobalt products by treating crude cobalt hydroxide with copper electrolysis decoppering post-treatment solution |
| CN113046574B (en) * | 2021-03-17 | 2022-07-29 | 沈阳有色金属研究院有限公司 | Method for preparing high-purity nickel and cobalt products by treating crude cobalt hydroxide with copper electrolysis decoppering post-treatment solution |
| CN115321604A (en) * | 2022-07-29 | 2022-11-11 | 格林美（江苏）钴业股份有限公司 | Method for removing phosphorus in cobalt chloride solution by using iron oxide yellow |
| CN116903051A (en) * | 2023-07-13 | 2023-10-20 | 科立鑫(珠海)新能源有限公司 | Method for producing cobalt chloride by using low-grade cobalt slag |
| CN116903051B (en) * | 2023-07-13 | 2023-12-12 | 科立鑫(珠海)新能源有限公司 | Method for producing cobalt chloride by using low-grade cobalt slag |
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