CN114737222A - Process for deeply removing copper, arsenic and lead in nickel electrolysis mixed acid system anolyte - Google Patents
Process for deeply removing copper, arsenic and lead in nickel electrolysis mixed acid system anolyte Download PDFInfo
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- CN114737222A CN114737222A CN202210451019.2A CN202210451019A CN114737222A CN 114737222 A CN114737222 A CN 114737222A CN 202210451019 A CN202210451019 A CN 202210451019A CN 114737222 A CN114737222 A CN 114737222A
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- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 238000000034 method Methods 0.000 title claims abstract description 47
- 239000010949 copper Substances 0.000 title claims abstract description 39
- 230000008569 process Effects 0.000 title claims abstract description 39
- 229910052802 copper Inorganic materials 0.000 title claims abstract description 38
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 34
- 229910052785 arsenic Inorganic materials 0.000 title claims abstract description 30
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 239000002253 acid Substances 0.000 title claims abstract description 26
- 238000005868 electrolysis reaction Methods 0.000 title claims abstract description 21
- 238000005406 washing Methods 0.000 claims abstract description 50
- 239000002893 slag Substances 0.000 claims abstract description 42
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 32
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 31
- 239000012535 impurity Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- 238000001914 filtration Methods 0.000 claims abstract description 8
- 238000012432 intermediate storage Methods 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims description 27
- 230000002378 acidificating effect Effects 0.000 claims description 14
- 230000035484 reaction time Effects 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 238000004537 pulping Methods 0.000 claims 1
- XMLHXNDHTWFTJE-UHFFFAOYSA-N [Cu].[Pb].[As] Chemical compound [Cu].[Pb].[As] XMLHXNDHTWFTJE-UHFFFAOYSA-N 0.000 abstract 1
- 230000007547 defect Effects 0.000 abstract 1
- 238000005580 one pot reaction Methods 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 7
- 238000003723 Smelting Methods 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- WWNBZGLDODTKEM-UHFFFAOYSA-N sulfanylidenenickel Chemical compound [Ni]=S WWNBZGLDODTKEM-UHFFFAOYSA-N 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- VETKVGYBAMGARK-UHFFFAOYSA-N arsanylidyneiron Chemical compound [As]#[Fe] VETKVGYBAMGARK-UHFFFAOYSA-N 0.000 description 2
- AYJRCSIUFZENHW-UHFFFAOYSA-L barium carbonate Chemical compound [Ba+2].[O-]C([O-])=O AYJRCSIUFZENHW-UHFFFAOYSA-L 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910001415 sodium ion Inorganic materials 0.000 description 2
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 229910001431 copper ion Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- BMWMWYBEJWFCJI-UHFFFAOYSA-K iron(3+);trioxido(oxo)-$l^{5}-arsane Chemical compound [Fe+3].[O-][As]([O-])([O-])=O BMWMWYBEJWFCJI-UHFFFAOYSA-K 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
- C25C1/06—Electrolytic production, recovery or refining of metals by electrolysis of solutions or iron group metals, refractory metals or manganese
- C25C1/08—Electrolytic production, recovery or refining of metals by electrolysis of solutions or iron group metals, refractory metals or manganese of nickel or cobalt
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention discloses a process for deeply removing copper, arsenic and lead in anolyte of a nickel electrolysis mixed acid system, which comprises the following steps: s1, introducing anolyte and hydrogen sulfide gas at the inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, and the flow rate of the hydrogen sulfide gas is 196 mL/min-234 mL/min; s2, fully mixing the anolyte and the hydrogen sulfide gas in a reactor for reaction, and simultaneously adjusting the hydrogen sulfide flow rate according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is-30-20 mV; s3, feeding the reacted solution into an intermediate storage tank from the outlet of the reactor, and filtering to obtain impurity-removed solution and impurity-removed slag; s4, washing the impurity-removed slag by weak acid water. Aiming at the defects of the prior art, the invention provides a simple and low-cost copper-arsenic-lead deep removal process for purifying the soluble anode nickel electrolytic anolyte of the mixed acid system, and realizes the simultaneous deep removal of copper, arsenic and lead by one-step reaction.
Description
Technical Field
The invention relates to the technical field of mixed acid system soluble anode nickel electrolytic purification and impurity removal, in particular to a process for deeply removing copper, arsenic and lead in a nickel electrolytic mixed acid system anolyte.
Background
In the mixed acid system soluble anode nickel electrolysis process, the copper removal mainly adopts a sulfide precipitation method, and comprises the traditional copper removal process of nickel concentrate and nickel anode mud and the copper removal process of amorphous nickel sulfide. The copper removing process of nickel concentrate and nickel anode mud has the problems of low efficiency, incomplete reaction and high nickel content in slag caused by a large amount of nickel concentrate entering copper removing slag. The copper-removing slag can not directly enter a copper smelting system, the treatment process is long, and the cost is high. The problem of the copper removal process of the amorphous nickel sulfide is that a certain amount of sodium ions are introduced and enriched by copper ion activation and nickel sulfide preparation, so that the sodium discharge pressure of the sodium ions in a system is increased. Although the content of nickel in the copper removing slag is low, the copper removing slag contains high chlorine radicals and cannot directly enter a copper smelting system for treatment.
In the mixed acid system soluble anode nickel electrolysis process, hydrogen peroxide is mainly added into the anode liquid for purifying and removing arsenic in the anode liquid, so that trivalent arsenic in the solution is oxidized into pentavalent arsenic, a certain iron-arsenic ratio in the solution is ensured, arsenic and iron form stable ferric arsenate precipitate to be removed, and iron is required to be added into the anode liquid when the iron-arsenic ratio is insufficient. The method has low arsenic removal efficiency and large reagent consumption, and iron supplement increases the subsequent iron removal burden.
In the mixed acid system soluble anode nickel electrolysis process, the anode liquid purification and lead removal mainly adopts a coprecipitation method. The method comprises the steps of adding barium carbonate into the anolyte to enable lead and barium to be coprecipitated, and properly increasing the cobalt removal potential and the end point pH value in the cobalt removal process to enable lead to be oxidized and coprecipitated. The two methods have low lead removal efficiency, and particularly lead removal in the cobalt removal process causes large slag amount and large nickel loss.
Disclosure of Invention
Aiming at the technical problem, the invention provides a process for deeply removing copper, arsenic and lead in anolyte of a nickel electrolysis mixed acid system.
In order to achieve the above purpose, the technical scheme of the invention is as follows:
a process for deeply removing copper, arsenic and lead in an anolyte of a nickel electrolysis mixed acid system comprises the following steps:
s1, introducing anolyte and hydrogen sulfide gas at the inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, and the flow rate of the hydrogen sulfide gas is 196 mL/min-234 mL/min;
s2, fully mixing the anolyte and the hydrogen sulfide gas in the step S1 in a reactor for reaction, adjusting the flow rate of the hydrogen sulfide according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is-30-20 mV, and recovering tail gas generated in the process to obtain a reacted solution;
s3, feeding the reacted solution obtained in the step S2 into an intermediate storage tank from an outlet of the reactor, and filtering to obtain impurity-removed liquid and impurity-removed slag;
and S4, washing the impurity-removed slag obtained in the step S3 by using weak acidic water, wherein washing water in the washing process is mixed into the impurity-removed liquid.
Wherein, in step S1, the pH of the anolyte: 1-2.
Wherein, in the step S1, the temperature of the anode solution is 60-75 ℃.
Wherein, in the step S2, the reaction time is 15-20 min.
In step S4, the pH range of the weak acidic water for impurity removal washing is 3 to 5.
In the step S4, the solid-to-solid ratio of the impurity-removing slag washing liquid is 2-4: 1.
In the step S4, the impurity and slag removing washing mode is 2-3 stages of counter-current pulp washing.
The invention has the beneficial effects that: the invention provides a simple and low-cost deep removal process for copper, arsenic and lead for the purification of the soluble anode nickel electrolysis anolyte of a mixed acid system. By the one-step method, more than 99.8% of copper, more than 40% of lead and more than 90% of arsenic in the anolyte can be removed, the anolyte containing 0.5-2 mg/L, Pb 2-4 mg/L, As 1-4 mg/L of Cu is obtained after impurity removal, and the indexes of copper, lead and arsenic are superior to those of the anolyte obtained after copper removal. Meanwhile, the impurity-removing slag contains more than or equal to 55 percent of Cu, less than or equal to 2 percent of Ni and less than or equal to 0.2 percent of Cl, can be directly used as a raw material of a copper smelting system, and shortens the impurity-removing slag treatment process. The method reduces the cost of purifying the soluble anode nickel electrolytic anolyte of the mixed acid system and removing the impurity slag, and has good application prospect.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in further detail with reference to the accompanying drawings in conjunction with the following detailed description. It should be understood that the description is intended to be exemplary only, and is not intended to limit the scope of the present invention. Moreover, in the following description, descriptions of well-known structures and techniques are omitted so as to not unnecessarily obscure the concepts of the present invention.
Example 1
As shown in figure 1, the process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system comprises the following steps:
s1, introducing anolyte and hydrogen sulfide gas into an inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, the flow rate of the hydrogen sulfide gas is 214mL/min, and impurity components in the anolyte are as follows: Cu0.55g/L, Pb0.0048g/L and As0.034g/L;
s2, fully mixing the anolyte and the hydrogen sulfide gas in the step S1 in a reactor for reaction, adjusting the flow rate of the hydrogen sulfide according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is-30 mV, and recovering tail gas generated in the process to obtain a reacted solution;
s3, feeding the reacted solution obtained in the step S2 into an intermediate storage tank from an outlet of the reactor, and filtering to obtain impurity-removed liquid and impurity-removed slag;
s4, washing the impurity-removed slag obtained in the step S3 by using weak acidic water, wherein washing water in the washing process is mixed into the impurity-removed liquid, and the impurity-removed liquid comprises the following components: Cu0.00058g/L, Pb0.0026g/L and As0.001g/L, and the components of the impurity-removed slag are as follows: cu55.56%, Ni1.64% and Cl0.022%. The removal rate of copper is 99.9 percent, the removal rate of lead is 45.8 percent and the removal rate of arsenic is 97 percent.
Wherein, in step S1, the pH of the anolyte: 1.43.
in step S1, the anode solution temperature is 66.5 ℃.
Wherein, in the step S2, the reaction time is 15 min.
In step S4, the pH range of the weak acidic water for impurity removal washing is 3.
In the step S4, the solid-to-solid ratio of the impurity-removing slag washing liquid is 2: 1.
In the step S4, the impurity and slag removing washing mode is 2-3 stages of counter-current pulp washing.
Example 2
As shown in figure 1, the process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system comprises the following steps:
s1, introducing anolyte and hydrogen sulfide gas into an inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, the flow rate of the hydrogen sulfide gas is 234mL/min, and impurity components in the anolyte are as follows: Cu0.7g/L, Pb0.0071g/L and As0.05g/L;
s2, fully mixing the anolyte and the hydrogen sulfide gas in the step S1 in a reactor for reaction, adjusting the flow rate of the hydrogen sulfide according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is 0mV, and recovering tail gas generated in the process to obtain a reacted solution;
s3, feeding the reacted solution obtained in the step S2 into an intermediate storage tank from an outlet of the reactor, and filtering to obtain impurity-removed liquid and impurity-removed slag;
s4, washing the impurity-removed slag obtained in the step S3 by using weak acidic water, wherein the washing water in the washing process is merged into the liquid after impurity removal, and the liquid after impurity removal comprises the following components: Cu0.0011g/L, Pb0.0039g/L and As0.0024g/L, and impurity-removed slag components: cu56.56%, Ni0.7% and Cl0.082%. The removal rate of copper is 99.8 percent, the removal rate of lead is 45.1 percent and the removal rate of arsenic is 95.2 percent.
Wherein, in step S1, the pH of the anolyte: 1.26.
in step S1, the anode solution temperature is 65.2 ℃.
Wherein, in the step S2, the reaction time is 15 min.
Wherein, in the step S4, the pH range of the weakly acidic water for removing the impurity residues and washing is 5.
In the step S4, the solid-to-solid ratio of the impurity-removing slag washing liquid is 4: 1.
In the step S4, the impurity and slag removing washing mode is 2-3 stages of counter-current pulp washing.
Example 3
As shown in figure 1, the process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system comprises the following steps:
s1, introducing anolyte and hydrogen sulfide gas at the inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, the flow rate of the hydrogen sulfide gas is 196 mL/min, and the impurity components in the anolyte are as follows: Cu0.55g/L, Pb0.0053g/L and As0.059g/L;
s2, fully mixing the anolyte and the hydrogen sulfide gas in the step S1 in a reactor for reaction, adjusting the flow rate of the hydrogen sulfide according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is-10 mV, and recovering tail gas generated in the process to obtain a reacted solution;
s3, feeding the reacted solution obtained in the step S2 into an intermediate storage tank from an outlet of the reactor, and filtering to obtain impurity-removed liquid and impurity-removed slag;
s4, washing the impurity-removed slag obtained in the step S3 by using weak acidic water, wherein washing water in the washing process is mixed into the impurity-removed liquid, and the impurity-removed liquid comprises the following components: Cu0.0008g/L, Pb0.0027g/L, As0.0037g/L, impurity-removed slag component: cu57.6%, Ni0.83%, Cl0.095%. The removal rate of copper is 99.9 percent, the removal rate of lead is 49.1 percent and the removal rate of arsenic is 93.7 percent.
Wherein, in step S1, the pH of the anolyte: 1.54.
in step S1, the anode solution temperature is 65.2 ℃.
Wherein, in the step S2, the reaction time is 15 min.
In step S4, the pH range of the weak acidic water for impurity removal washing is 4.
In the step S4, the solid-to-solid ratio of the impurity removal residue washing solution is 3: 1.
In the step S4, the impurity and slag removing washing mode is 2-3 stages of counter-current pulp washing.
Example 4
As shown in figure 1, the process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system comprises the following steps:
s1, introducing anolyte and hydrogen sulfide gas at the inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, and the flow rate of the hydrogen sulfide gas is 196 mL/min;
s2, fully mixing the anolyte and the hydrogen sulfide gas in the step S1 in a reactor for reaction, adjusting the flow rate of the hydrogen sulfide according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is 20mV, and recovering tail gas generated in the process to obtain a reacted solution;
s3, feeding the reacted solution obtained in the step S2 into an intermediate storage tank from an outlet of the reactor, and filtering to obtain impurity-removed liquid and impurity-removed slag;
and S4, washing the impurity-removed slag obtained in the step S3 by using weak acidic water, wherein washing water in the washing process is mixed into the impurity-removed liquid.
Wherein, in step S1, the pH of the anolyte: 1.
in step S1, the anode solution temperature is 60 ℃.
Wherein, in the step S2, the reaction time is 16 min.
In step S4, the pH range of the weak acidic water for impurity removal washing is 5.
In the step S4, the solid-to-solid ratio of the impurity-removing slag washing liquid is 2: 1.
In the step S4, the impurity and slag removing washing mode is 2-3 stages of counter-current pulp washing.
Example 5
As shown in figure 1, the process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system comprises the following steps:
s1, introducing anolyte and hydrogen sulfide gas at the inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, and the flow rate of the hydrogen sulfide gas is 234 mL/min;
s2, fully mixing the anolyte and the hydrogen sulfide gas in the step S1 in a reactor for reaction, adjusting the flow rate of the hydrogen sulfide according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is 15mV, and recovering tail gas generated in the process to obtain a reacted solution;
s3, feeding the reacted solution obtained in the step S2 into an intermediate storage tank from an outlet of the reactor, and filtering to obtain impurity-removed liquid and impurity-removed slag;
and S4, washing the impurity-removed slag obtained in the step S3 by using weak acidic water, wherein washing water in the washing process is mixed into the impurity-removed liquid.
Wherein, in the step S1, the anolyte pH: 2.
In step S1, the anode solution temperature is 75 ℃.
Wherein, in the step S2, the reaction time is 20 min.
In step S4, the pH range of the weak acidic water for impurity removal washing is 3.
In the step S4, the solid-to-solid ratio of the impurity-removing slag washing liquid is 4: 1.
In the step S4, the impurity and slag removal washing manner is 2-3 stages of counter-current slurry washing.
It should be understood that the above-described embodiments of the present invention are merely illustrative of or explaining the principles of the invention and are not to be construed as limiting the invention. Therefore, any modification, equivalent replacement, improvement and the like made without departing from the spirit and scope of the present invention should be included in the protection scope of the present invention. Further, it is intended that the appended claims cover all such variations and modifications as fall within the scope and boundaries of the appended claims or the equivalents of such scope and boundaries.
Claims (7)
1. A process for deeply removing copper, arsenic and lead in an anolyte of a nickel electrolysis mixed acid system is characterized by comprising the following steps:
s1, introducing anolyte and hydrogen sulfide gas at the inlet of the reactor, wherein the flow rate of the anolyte is 650mL/min, and the flow rate of the hydrogen sulfide gas is 196 mL/min-234 mL/min;
s2, fully mixing the anolyte and the hydrogen sulfide gas in the step S1 in a reactor for reaction, adjusting the flow rate of the hydrogen sulfide according to the potential of the solution at the outlet of the reactor to control the impurity removal depth, wherein the potential control range is-30-20 mV, and recovering tail gas generated in the process to obtain a reacted solution;
s3, feeding the reacted solution obtained in the step S2 into an intermediate storage tank from an outlet of the reactor, and filtering to obtain impurity-removed liquid and impurity-removed slag;
and S4, washing the impurity-removed slag obtained in the step S3 by using weak acidic water, wherein the washing water in the washing process is added into the impurity-removed liquid.
2. The process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system according to claim 1, which is characterized in that: in step S1, the anolyte pH: 1-2.
3. The process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system according to claim 1, which is characterized in that: in the step S1, the temperature of the anode solution is 60-75 ℃.
4. The process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system according to claim 1, which is characterized in that: in the step S2, the reaction time is 15-20 min.
5. The process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system according to claim 1, which is characterized in that: in the step S4, the pH range of the weak acidic water for impurity removing slag washing is 3-5.
6. The process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system according to claim 5, which is characterized in that: in the step S4, the solid-to-solid ratio of the impurity-removing slag washing liquid is 2-4: 1.
7. The process for deeply removing copper, arsenic and lead in the anolyte of the nickel electrolysis mixed acid system according to claim 6, which is characterized in that: in the step S4, the impurity and slag removing washing mode is 2-3 sections of counter-current pulping washing.
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| CN111411229A (en) * | 2020-04-29 | 2020-07-14 | 长沙华时捷环保科技发展股份有限公司 | Process for efficiently separating nickel and copper in nickel electrolyte |
| CN112387139A (en) * | 2020-12-03 | 2021-02-23 | 浙江科菲科技股份有限公司 | Device for removing copper ions in nickel electrolysis mixed acid system by using hydrogen sulfide gas |
| CN214287612U (en) * | 2020-12-03 | 2021-09-28 | 浙江科菲科技股份有限公司 | Device for removing copper ions in nickel electrolysis mixed acid system by using hydrogen sulfide gas |
| CN114107697A (en) * | 2021-11-05 | 2022-03-01 | 金川集团股份有限公司 | Lead removal method for nickel chloride solution |
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Effective date of registration: 20240411 Address after: 737104 No. 2 Lanzhou Road, Beijing Road Street, Jinchuan District, Jinchang City, Gansu Province Applicant after: Jinchuan Group Nickel Cobalt Co.,Ltd. Country or region after: China Address before: 737103 No. 98, Jinchuan Road, Jinchang, Gansu Applicant before: JINCHUAN GROUP Co.,Ltd. Country or region before: China |