CN113046572A - Cobalt chloride production process - Google Patents
Cobalt chloride production process Download PDFInfo
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- CN113046572A CN113046572A CN202110263737.2A CN202110263737A CN113046572A CN 113046572 A CN113046572 A CN 113046572A CN 202110263737 A CN202110263737 A CN 202110263737A CN 113046572 A CN113046572 A CN 113046572A
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- GVPFVAHMJGGAJG-UHFFFAOYSA-L cobalt dichloride Chemical compound [Cl-].[Cl-].[Co+2] GVPFVAHMJGGAJG-UHFFFAOYSA-L 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000000605 extraction Methods 0.000 claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 29
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910017052 cobalt Inorganic materials 0.000 claims abstract description 20
- 239000010941 cobalt Substances 0.000 claims abstract description 20
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000012141 concentrate Substances 0.000 claims abstract description 16
- 238000001704 evaporation Methods 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 16
- 239000002002 slurry Substances 0.000 claims abstract description 16
- 238000004537 pulping Methods 0.000 claims abstract description 12
- 229910052742 iron Inorganic materials 0.000 claims abstract description 11
- 150000001868 cobalt Chemical class 0.000 claims abstract description 10
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000000706 filtrate Substances 0.000 claims abstract description 8
- 239000002562 thickening agent Substances 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 238000000498 ball milling Methods 0.000 claims abstract description 4
- XNZJTLSFOOXUAS-UHFFFAOYSA-N cobalt hydrochloride Chemical compound Cl.[Co] XNZJTLSFOOXUAS-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000013067 intermediate product Substances 0.000 claims abstract description 4
- 238000002386 leaching Methods 0.000 claims abstract description 4
- 238000003825 pressing Methods 0.000 claims abstract description 4
- 239000002893 slag Substances 0.000 claims abstract description 4
- 239000002253 acid Substances 0.000 claims description 21
- 238000005406 washing Methods 0.000 claims description 21
- 238000007127 saponification reaction Methods 0.000 claims description 16
- 229910052802 copper Inorganic materials 0.000 claims description 15
- 239000010949 copper Substances 0.000 claims description 15
- 229910052748 manganese Inorganic materials 0.000 claims description 15
- 239000011572 manganese Substances 0.000 claims description 15
- 239000003513 alkali Substances 0.000 claims description 10
- 230000008020 evaporation Effects 0.000 claims description 9
- 238000002425 crystallisation Methods 0.000 claims description 8
- 230000008025 crystallization Effects 0.000 claims description 8
- 238000000034 method Methods 0.000 claims description 7
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 6
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 claims description 6
- 239000012074 organic phase Substances 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- 229910052725 zinc Inorganic materials 0.000 claims description 6
- 239000011701 zinc Substances 0.000 claims description 6
- 229940044175 cobalt sulfate Drugs 0.000 claims description 5
- 229910000361 cobalt sulfate Inorganic materials 0.000 claims description 5
- KTVIXTQDYHMGHF-UHFFFAOYSA-L cobalt(2+) sulfate Chemical compound [Co+2].[O-]S([O-])(=O)=O KTVIXTQDYHMGHF-UHFFFAOYSA-L 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 4
- 238000005119 centrifugation Methods 0.000 claims description 3
- 239000003086 colorant Substances 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- 239000012452 mother liquor Substances 0.000 claims description 3
- 229910052759 nickel Inorganic materials 0.000 claims description 3
- 238000004806 packaging method and process Methods 0.000 claims description 3
- 239000012071 phase Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims 1
- 238000002360 preparation method Methods 0.000 claims 1
- 239000013078 crystal Substances 0.000 description 7
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/043—Sulfurated acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G51/00—Compounds of cobalt
- C01G51/01—Preparation or separation involving a liquid-liquid extraction, an adsorption or an ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G51/00—Compounds of cobalt
- C01G51/08—Halides; Oxyhalides
- C01G51/085—Chlorides; Oxychlorides
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Metallurgy (AREA)
- Mechanical Engineering (AREA)
- Materials Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Geochemistry & Mineralogy (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Inorganic Compounds Of Heavy Metals (AREA)
Abstract
The invention relates to the field of cobalt salt production, in particular to a production process of cobalt chloride. The invention relates to a cobalt chloride production process, which comprises the following steps: (1) adding water into one part of the cobalt concentrate, performing ball milling and slurrying, and processing by a thickener to obtain cobalt concentrate slurry; pulping a part of cobalt concentrate to obtain a cobalt salt intermediate pulping material; (2) pulping the cobalt concentrate slurry and the cobalt salt intermediate product slurry, and adding sulfuric acid and hydrogen peroxide for leaching; (3) treating the leached slurry by a thickener to obtain overflow liquid; (4) removing iron from the overflow liquid, and performing filter pressing to obtain iron slag and iron-removed filtrate; (5) extracting the iron-removed filtrate by using P204 and P507; (6) adding hydrochloric acid after residue extraction, and removing oil; (7) evaporating and crystallizing to obtain the cobalt hydrochloride.
Description
Technical Field
The invention relates to the field of cobalt salt production, in particular to a production process of cobalt chloride.
Background
Cobalt chloride is an inorganic substance, of the formula CoCl 2. Pink to red crystals and anhydrous blue. Slightly deliquescent and easily soluble in water, ethanol, ether, acetone and glycerol. Analytical reagents, indicators for humidity and moisture, ammonia absorbents.
The cobalt chloride crystals in the prior art are generally small, however, there are fields that need to use cobalt chloride crystals with larger crystals, such as the prior art CN201811265153.3 a method for producing battery grade cobalt sulfate crystals, the cobalt sulfate particle size is small.
Disclosure of Invention
The invention hopes to provide a cobalt chloride production process, and the specific scheme is as follows:
a cobalt chloride production process comprises the following steps:
(1) adding water into one part of the cobalt concentrate, performing ball milling and slurrying, and processing by a thickener to obtain cobalt concentrate slurry; pulping a part of cobalt concentrate to obtain a cobalt salt intermediate pulping material;
(2) pulping the cobalt concentrate slurry and the cobalt salt intermediate product slurry, and adding sulfuric acid and hydrogen peroxide for leaching;
(3) treating the leached slurry by a thickener to obtain overflow liquid;
(4) removing iron from the overflow liquid, and performing filter pressing to obtain iron slag and iron-removed filtrate;
(5) extracting the iron-removed filtrate by using P204 and P507;
(6) adding hydrochloric acid after residue extraction, and removing oil;
(7) evaporating and crystallizing to obtain cobalt hydrochloride;
the specific process of the step (7) is as follows;
(1) conveying the deoiled cobalt chloride solution and mother liquor raw materials to an MVR evaporation system, and when the temperature of a gas-liquid separation chamber reaches 70 ℃, ending preheating and enabling the system to enter an evaporation stage;
(2) continuously evaporating and concentrating along with the system, continuously concentrating cobalt chloride and cobalt sulfate in the forced circulation evaporation system to the concentration required by the design, and conveying the concentrated solution to a crystallization kettle after the density meets the concentration requirement;
(3) cooling the crystallization kettle by adding cooling water, and starting centrifugation when the material is cooled to 27-35 ℃; the temperature reduction speed is controlled to be reduced by 5 ℃ per hour on average;
(4) when the materials are full, the centrifuge automatically runs for 5 to 340 seconds at high speed, and then the materials are automatically discharged;
(5) standing the centrifugal material for 2-4h, and packaging.
Adding 30% liquid alkali to saponify P204, adjusting the flow of organic and liquid alkali, and controlling the saponification rate to 40-50%; if the saponification rate is lower than 50%, the liquid alkali flow can be increased, and if the saponification rate is higher than 50%, the liquid flow before extraction can be reduced; and (3) carrying out 9-stage countercurrent extraction on the saponified organic phase and the P204 pre-extraction solution, wherein the organic phase and the water phase are 1: 1. the flow rate per hour is determined according to the contents of Cu, Mn and Zn in the pre-extraction solution and the pH value of the solution, and if the contents of Cu, Mn and Zn are high, the saponification rate can be improved. And (3) washing the cobalt by adopting 1.2mol/L hydrochloric acid, wherein the flow of the washing acid is adjusted according to the content of impurities so as to control the 9 th-level organic to be light yellow. Counter-current back extraction of Cu and Mn is carried out by adopting 4.5mol/L hydrochloric acid, and the flow of copper and manganese is adjusted according to the content of copper and manganese in different raw materials so as to control the 5 th-level organic color to be green. The counter-current back extraction of the iron-reflecting section is carried out by adopting 6.0mol/L hydrochloric acid, the flow rate of the iron-reflecting acid is adjusted according to the concentration of the solution after the iron-reflecting, and H in the iron-reflecting acid+The content is controlled between 4.5 and 5.0g/L, above which the flow rate of the ferrate is reduced, and below which the flow rate is increased.
Performing countercurrent extraction of P204 raffinate and alkaline saponified P507, controlling saponification rate at 45-60%, and setting organic feed flow rate of extraction tank at 35-45m3H is used as the reference value. The washing section is 14-grade countercurrent washing, the washing acid is 1.2mol/L hydrochloric acid, and the flow rate of the washing acid is 1.8-3.0m3And h, adjusting the contents of Ni and Mg in the pre-extraction liquid and the pH, color and components of the washing liquid. The cobalt-removing section adopts 6-stage countercurrent back extraction, 5.5mol/L hydrochloric acid back extraction is adopted, the flow of the cobalt-removing acid is adjusted according to the actual situation, the 4 th-stage organic color of the cobalt-removing section is controlled to be blue, and the 5 and 6-stage organic colors of the cobalt-removing section are colorless. The iron-reflecting section adopts 2-stage countercurrent, 6.0mol/L hydrochloric acid is used for iron-reflecting, and the flow of the iron-reflecting acid is adjusted according to the amount of the organic load iron.
The invention uses special crystallization technology, especially controls the temperature and speed of crystallization cooling, thereby being capable of producing cobalt chloride crystals with larger crystal grains.
Meanwhile, the invention leads the finished product of the cobalt chloride to have better purity, color and luster by a special extraction process.
Detailed Description
A cobalt chloride production process comprises the following steps:
(1) adding water into one part of the cobalt concentrate, performing ball milling and slurrying, and processing by a thickener to obtain cobalt concentrate slurry; pulping a part of cobalt concentrate to obtain a cobalt salt intermediate pulping material;
(2) pulping the cobalt concentrate slurry and the cobalt salt intermediate product slurry, and adding sulfuric acid and hydrogen peroxide for leaching;
(3) treating the leached slurry by a thickener to obtain overflow liquid;
(4) removing iron from the overflow liquid, and performing filter pressing to obtain iron slag and iron-removed filtrate;
(5) extracting the iron-removed filtrate by using P204 and P507;
(6) adding hydrochloric acid after residue extraction, and removing oil;
(7) evaporating and crystallizing to obtain cobalt hydrochloride;
the specific process of the step (7) is as follows;
(1) conveying the deoiled cobalt chloride solution and mother liquor raw materials to an MVR evaporation system, and when the temperature of a gas-liquid separation chamber reaches 70 ℃, ending preheating and enabling the system to enter an evaporation stage;
(2) continuously evaporating and concentrating along with the system, continuously concentrating cobalt chloride and cobalt sulfate in the forced circulation evaporation system to the concentration required by the design, and conveying the concentrated solution to a crystallization kettle after the density meets the concentration requirement;
(3) cooling the crystallization kettle by adding cooling water, and starting centrifugation when the material is cooled to 27-35 ℃; the temperature reduction speed is controlled to be reduced by 5 ℃ per hour on average;
(4) when the materials are full, the centrifuge automatically runs for 5 to 340s at high speed (adjusted according to seasons), and then the materials are automatically discharged;
(5) standing the centrifugal material for 2-4h, and packaging.
Adding 30% liquid alkali to saponify P204, adjusting the flow of organic and liquid alkali, and controlling the saponification rate to 40-50%; if the saponification rate is lower than 50%, the liquid alkali flow can be increased, and if the saponification rate is higher than 50%, the liquid flow before extraction can be reduced; and (3) carrying out 9-stage countercurrent extraction on the saponified organic phase and the P204 pre-extraction solution, wherein the organic phase and the water phase are 1: 1. the flow rate per hour is determined according to the contents of Cu, Mn and Zn in the pre-extraction solution and the pH value of the solution, and if the contents of Cu, Mn and Zn are high, the saponification rate can be improved. And (3) washing the cobalt by adopting 1.2mol/L hydrochloric acid, wherein the flow of the washing acid is adjusted according to the content of impurities so as to control the 9 th-level organic to be light yellow. Counter-current back extraction of Cu and Mn is carried out by adopting 4.5mol/L hydrochloric acid, and the flow of copper and manganese is adjusted according to the content of copper and manganese in different raw materials so as to control the 5 th-level organic color to be green. The counter-current back extraction of the iron-reflecting section is carried out by adopting 6.0mol/L hydrochloric acid, the flow rate of the iron-reflecting acid is adjusted according to the concentration of the solution after the iron-reflecting, and H in the iron-reflecting acid+The content is controlled between 4.5 and 5.0g/L, above which the flow rate of the ferrate is reduced, and below which the flow rate is increased.
Performing countercurrent extraction on P204 raffinate and P507 after alkali saponification, wherein the saponification rate is controlled to be 45-60%, the organic feeding flow rate of an extraction box is generally set to be 35-45m3/h, the flow rate of an aqueous phase is adjusted according to the extraction level 1-3, the aqueous phase of the extraction level 1 is colorless, and the extraction level 2 is light red. The washing section is 14-grade countercurrent washing, the washing acid is 1.2mol/L hydrochloric acid, and the flow rate of the washing acid is 1.8-3.0m3And h, adjusting the contents of Ni and Mg in the pre-extraction liquid and the pH, color and components of the washing liquid. The cobalt-removing section adopts 6-stage countercurrentAnd (3) performing back extraction by adopting 5.5mol/L hydrochloric acid, adjusting the flow of the anti-cobaltic acid according to the actual condition, and controlling the 4 th-level organic color of the anti-cobaltic section to be blue and the 5 and 6-level organic colors of the anti-cobaltic section to be colorless. The iron-reflecting section adopts 2-stage countercurrent, 6.0mol/L hydrochloric acid is used for iron-reflecting, and the flow of the iron-reflecting acid is adjusted according to the amount of the organic load iron.
Although the present invention has been described with reference to the preferred embodiments, it should be understood that various changes and modifications can be made therein by those skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (9)
1. The cobalt chloride production process is characterized by comprising the following steps:
(1) adding water into one part of the cobalt concentrate, performing ball milling and slurrying, and processing by a thickener to obtain cobalt concentrate slurry; pulping a part of cobalt concentrate to obtain a cobalt salt intermediate pulping material;
(2) pulping the cobalt concentrate slurry and the cobalt salt intermediate product slurry, and adding sulfuric acid and hydrogen peroxide for leaching;
(3) treating the leached slurry by a thickener to obtain overflow liquid;
(4) removing iron from the overflow liquid, and performing filter pressing to obtain iron slag and iron-removed filtrate;
(5) extracting the iron-removed filtrate by using P204 and P507;
(6) adding hydrochloric acid after residue extraction, and removing oil;
(7) evaporating and crystallizing to obtain cobalt hydrochloride;
the specific process of the step (7) is as follows;
(1) conveying the deoiled cobalt chloride solution and mother liquor raw materials to an MVR evaporation system, and when the temperature of a gas-liquid separation chamber reaches 70 ℃, ending preheating and enabling the system to enter an evaporation stage;
(2) continuously evaporating and concentrating along with the system, continuously concentrating cobalt chloride and cobalt sulfate in the forced circulation evaporation system to the concentration required by the design, and conveying the concentrated solution to a crystallization kettle after the density meets the concentration requirement;
(3) cooling the crystallization kettle by adding cooling water, and starting centrifugation when the material is cooled to 27-35 ℃; the temperature reduction speed is controlled to be reduced by 5 ℃ per hour on average;
(4) when the materials are full, the centrifuge automatically runs for 5 to 340 seconds at high speed, and then the materials are automatically discharged;
(5) standing the centrifugal material for 2-4h, and packaging.
2. The cobalt chloride production process of claim 1, wherein the P204 raffinate is used for impurity removal, and comprises the following steps: adding 30% liquid alkali to saponify P204, adjusting the flow of organic and liquid alkali, and controlling the saponification rate to 40-50%; if the saponification rate is lower than 50%, the liquid alkali flow can be increased, and if the saponification rate is higher than 50%, the liquid flow before extraction can be reduced; and (3) carrying out 9-stage countercurrent extraction on the saponified organic phase and the P204 pre-extraction solution, wherein the organic phase and the water phase are 1: 1. the flow rate per hour is determined according to the contents of Cu, Mn and Zn in the pre-extraction solution and the pH value of the solution, and if the contents of Cu, Mn and Zn are high, the saponification rate can be improved.
3. The cobalt chloride production process of claim 2, further comprising the steps of: and (3) washing the cobalt by adopting 1.2mol/L hydrochloric acid, wherein the flow of the washing acid is adjusted according to the content of impurities so as to control the 9 th-level organic to be light yellow.
4. The cobalt chloride production process of claim 2, further comprising the steps of: counter-current back extraction of Cu and Mn is carried out by adopting 4.5mol/L hydrochloric acid, and the flow of copper and manganese is adjusted according to the content of copper and manganese in different raw materials so as to control the 5 th-level organic color to be green.
5. The cobalt chloride production process of claim 2, further comprising the steps of: the counter-current back extraction of the iron-reflecting section is carried out by adopting 6.0mol/L hydrochloric acid, the flow rate of the iron-reflecting acid is adjusted according to the concentration of the solution after the iron-reflecting, and H in the iron-reflecting acid+The content is controlled between 4.5 and 5.0g/L, above which the flow rate of the ferrate is reduced, and below which the flow rate is increased.
6. A process for the preparation of a chlorinated rubber composition as claimed in claim 1The cobalt production process is characterized by comprising the following steps: performing countercurrent extraction of P204 raffinate and alkaline saponified P507, controlling saponification rate at 45-60%, and setting organic feed flow rate of extraction tank at 35-45m3/h。
7. The process of claim 6, wherein: the washing section is 14-grade countercurrent washing, the washing acid is 1.2mol/L hydrochloric acid, and the flow rate of the washing acid is 1.8-3.0m3And h, adjusting the contents of Ni and Mg in the pre-extraction liquid and the pH, color and components of the washing liquid.
8. The process of claim 6, wherein: the cobalt-removing section adopts 6-stage countercurrent back extraction, 5.5mol/L hydrochloric acid back extraction is adopted, the flow of the cobalt-removing acid is adjusted according to the actual situation, the 4 th-stage organic color of the cobalt-removing section is controlled to be blue, and the 5 and 6-stage organic colors of the cobalt-removing section are colorless.
9. The process of claim 6, wherein: the iron-reflecting section adopts 2-stage countercurrent, 6.0mol/L hydrochloric acid is used for iron-reflecting, and the flow of the iron-reflecting acid is adjusted according to the amount of the organic load iron.
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Application publication date: 20210629 |