CN114540626A - Method for gradient recovery of valuable metals in waste acid by using antimony electrodeposition barren solution - Google Patents
Method for gradient recovery of valuable metals in waste acid by using antimony electrodeposition barren solution Download PDFInfo
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Abstract
The invention relates to a method for recovering valuable metals in waste acid in a gradient manner by utilizing antimony electrodeposition barren solution, which belongs to the technical field of chemical metallurgy and comprises the following steps: the method comprises the following steps: placing a certain amount of antimony electrodeposition barren solution into a reaction tank, and slowly adding waste acid into the antimony electrodeposition barren solution to obtain copper sulfide slag containing noble metals and copper removal wastewater; step 2, placing a certain amount of waste acid into a reaction tank, and then adding the copper-removal wastewater obtained in the step 1 into the reaction tank to obtain copper-containing arsenic sulfide slag and arsenic-removal wastewater; and 3, placing the arsenic-removed wastewater obtained in the step 2 into a reaction tank, and then adding antimony electrodeposition barren liquor into the reaction tank to obtain arsenic-containing antimony sulfide slag and antimony-removed wastewater. According to the method for recovering valuable metals in the waste acid in a gradient manner by utilizing the antimony electrodeposition barren solution, disclosed by the invention, the antimony electrodeposition barren solution and the waste acid are jointly treated, so that the purpose of 'treating wastes with processes of wastes and changing wastes into valuables' can be achieved, and the method has a profound significance for improving the economic benefit of enterprises and making green and sustainable development roads.
Description
Technical Field
The invention relates to a method for recovering valuable metals in waste acid in a gradient manner, in particular to a method for recovering valuable metals in waste acid in a gradient manner by utilizing antimony electrodeposition barren solution, and belongs to the technical field of chemical metallurgy.
Background
In the non-ferrous smelting industry, flue gas generated in the smelting process is generally sent to a sulfuric acid system to prepare acid, before the flue gas is prepared into acid, the flue gas is washed and decontaminated through a purification process, and in order to avoid the over-high impurity concentration in washing water, the acid preparation system needs to discharge a part of waste acid, namely waste acid. Acid plants that use pyrite as a feedstock also produce large quantities of contaminated acid, approximately 50kg of contaminated acid per ton of sulfuric acid produced. Because the flue gas contains a large amount of fine particle smoke dust, metal pollutants such as arsenic, mercury, lead, zinc, cadmium and the like, and SO2And SO3And the substances enter the waste acid in the washing process, so that the property of the waste acid is very complex, the waste acid cannot be directly utilized, the sulfuric acid resource is wasted, the environment is harmed, and the waste acid must be subjected to harmless treatment.
The traditional treatment process method adopts a chemical precipitation method or a lime neutralization method, the lime neutralization method treatment process usually generates a large amount of neutralization slag, and the large amount of neutralization slag needs a large stacking space; the chemical precipitation method generally adopts a vulcanizing agent as a precipitator, and the vulcanizing agent is prepared by a sodium hydrosulfide acidolysis method or hydrogen production by methanol cracking-hydrogen production by sulfur vapor synthesis; the two treatment processes have the problems of difficult treatment of neutralization slag, high preparation cost of hydrogen sulfide and the like.
The antimony-containing gold concentrate is treated by the traditional roasting process, most of arsenic and antimony enter flue gas, and the arsenic and the antimony are difficult to separate due to similar chemical properties; the ore blending of the sulfur-making gold-catching process has strict requirements on arsenic and antimony and can not be blended in large quantities. At present, antimony-gold concentrate is treated by separating gold and antimony by adopting methods of alkaline leaching and electrowinning antimony and recovering antimony, wherein the treatment method of the generated electrowinning barren solution is to obtain crude antimony crystalline salt by adopting freezing crystallization; and recovering valuable metals such as gold, silver and the like from the leaching residues by adopting a pyrogenic process or a wet process.
The crude antimony crystal salt mainly contains sodium sulfide, but contains higher sodium hydrosulfide, sodium thiosulfate and the like, and cannot be sold directly, and the sodium sulfide can be deliquesced and acidified in the air for a long time in the long-term stacking process, so that the hydrogen sulfide gas is continuously released, and great pressure is caused to the environmental protection and safe production of enterprises; the crude antimony crystal salt is treated by an acidification method, the reaction is rapid and difficult to control, and the generated hydrogen sulfide has low concentration and cannot be directly applied.
Disclosure of Invention
The purpose of the invention is: in order to overcome the defects in the prior art, the method for recovering valuable metals in the waste acid in a gradient manner by utilizing the antimony electrodeposition barren solution is provided, the antimony electrodeposition barren solution and the waste acid are jointly treated, waste is prepared from waste, and the sustainable green development of the smelting industry is promoted.
The technical scheme for solving the technical problems is as follows:
a method for recovering valuable metals in waste acid in a gradient manner by utilizing antimony electrodeposition barren solution comprises the following steps:
step 1, placing a certain amount of antimony electrodeposition barren solution into a reaction tank, slowly adding contaminated acid into the antimony electrodeposition barren solution, stirring for 0.5-1 h, and then performing filter pressing to obtain copper sulfide slag containing precious metals and copper-removed wastewater, wherein the copper sulfide slag is sent to pyrometallurgical ore blending treatment;
step 2, placing a certain amount of contaminated acid into a reaction tank, then adding the copper-removing wastewater obtained in the step 1 into the reaction tank, adjusting the pH of the solution in the reaction tank to be more than 0.5 and less than 1, stirring for 0.5-1 h, and then performing filter pressing to obtain copper-containing arsenic sulfide slag and arsenic-removing wastewater, wherein the arsenic sulfide slag can be sent to an arsenic roasting recovery workshop for ore blending treatment;
and 3, placing the arsenic-removal wastewater obtained in the step 2 into a reaction tank, then adding antimony electrodeposition barren solution into the reaction tank, adjusting the pH of the solution in the reaction tank to 3-5, stirring for 0.5-1 h, and then performing filter pressing to obtain arsenic-containing antimony sulfide slag and antimony-removal wastewater, wherein the antimony sulfide slag can be sent to an antimony workshop for ore blending treatment, and the antimony-removal wastewater is sent to a triple effect evaporation system for preparing sodium sulfate.
Furthermore, the concentration of each component in the antimony electrodeposition barren solution is as follows: sb ion concentration of 20-50 g/L, Na2The S concentration is 40-60 g/L, Au, the ion concentration is 1-5 mg/L, As, the ion concentration is 0.1-1 g/L, NaOH, and the concentration is 30-60 g/L; the concentration of each component in the waste acid is as follows: as ion concentration is 10-30 g/L, Cu ion concentration is 1-3 g/L, Fe ion concentration is 0.5-1 g/L, Sb ion concentration is 1-3 g/L, Zn ion concentration is 0.2-1 g/L, H2SO4The concentration is 20-80 g/L.
Further, in the step 1, the molar ratio of the waste acid to the antimony electrodeposition barren solution in the reaction tank is (1.1-1.2): 1.
furthermore, in step 1, the ratio of main components of the copper sulfide slag (dry basis) is as follows: 40-60% of Cu, 20-30% of S, less than or equal to 2% of As and less than or equal to 3% of Sb; the concentration of Cu ions in the copper removal wastewater is controlled to be less than or equal to 0.1 g/L.
Furthermore, in step 2, the arsenic sulfide slag (dry basis) comprises the following main components in percentage by weight: the content of As is 40-70%, the content of S is 15-25%, and the content of Sb is less than or equal to 5%; the concentration of As ions in the arsenic-removing wastewater is controlled to be less than or equal to 0.3 mg/L.
Furthermore, in step 3, the antimony sulfide slag (dry basis) comprises the following main components in percentage by weight: sb content is 50-65%, S content is 20-30%; the concentration of As ions in the antimony-removing wastewater is controlled to be less than or equal to 0.3mg/L, Sb and the concentration of As ions is controlled to be less than or equal to 0.5mg/L, Cu and the concentration of As ions is controlled to be less than or equal to 0.1mg/L, Zn and the concentration of As ions is controlled to be less than or equal to 10mg/L, Fe and the concentration of As ions is controlled to be less than or equal to 10 mg/L.
The invention has the beneficial effects that: the antimony electro-deposition barren solution and the waste acid are combined for treatment by combining the chemical properties of the antimony electro-deposition barren solution and the waste acid, so that on one hand, the energy consumption of freezing and crystallizing the electro-deposition barren solution is saved, and on the other hand, crude antimony crystallized salt does not need to be treated, so that the treatment cost of the electro-deposition barren solution is reduced; on the other hand, the electrowinning barren solution is used for replacing a vulcanizing agent, so that the treatment cost of the waste acid is reduced, valuable metals can be recycled in a gradient manner, the resource utilization in the field of chemical metallurgy is met, the aim of 'processing waste by waste and changing waste into valuable' can be fulfilled, and the electrowinning barren solution has the advantages of less treatment equipment investment, reasonable treatment process, high treatment efficiency, low treatment cost and the like; the method has profound significance for improving the economic benefit of enterprises and making the enterprises green and sustainable development roads.
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FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The principles and features of the present invention are described below in conjunction with the accompanying fig. 1, which is provided by way of example only to illustrate the present invention and not to limit the scope of the present invention.
Example 1
A method for recovering valuable metals in waste acid in a gradient manner by utilizing antimony electrodeposition barren solution comprises the following steps:
step 1, preparing two byproducts generated in the smelting industry, namely antimony electrodeposition barren solution and waste acid:
the antimony electrodeposition barren solution comprises the following components in concentration: sb ion concentration 30g/L, Na2The S concentration is 40g/L, Au, the ion concentration is 2mg/L, As, the ion concentration is 1g/L, NaOH, and the concentration is 40 g/L;
the concentration of each component in the waste acid is as follows: as ion concentration is 10g/L, Cu ion concentration 2g/L, Fe ion concentration 1g/L, Sb ion concentration 2g/L, Zn ion concentration 1g/L, H2SO4The concentration was 30 g/L.
Putting a certain amount of antimony electrodeposition barren solution into a reaction tank, and slowly adding contaminated acid into the antimony electrodeposition barren solution, wherein the molar ratio of the contaminated acid to the antimony electrodeposition barren solution in the reaction tank is 1.2: 1; stirring for 1h, and then performing filter pressing to obtain copper sulfide slag containing noble metals and copper-removing wastewater, wherein the copper sulfide slag is sent to pyrometallurgical ore blending treatment;
the main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
CuSO4+H2S→CuS+H2SO4
the copper sulfide slag (dry basis) comprises the following main components in percentage by weight: 40% of Cu, 30% of S, 2% of As and 3% of Sb; the concentration of Cu ions in the copper removal wastewater is 0.06 g/L;
step 2, placing a certain amount of contaminated acid into a reaction tank, then adding the copper removal wastewater obtained in the step 1 into the reaction tank, wherein the contaminated acid is excessive, adjusting the pH value of the solution in the reaction tank to be 0.8, stirring for 1 hour, and then performing filter pressing to obtain copper-containing arsenic sulfide slag and arsenic removal wastewater, wherein the arsenic sulfide slag can be sent to an arsenic roasting recovery workshop for ore blending treatment;
the main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
HAsO2+H2S→As2S3+H2O
CuSO4+H2S→CuS+H2SO4
the arsenic sulfide slag (dry basis) comprises the following main components in percentage by weight: the content of As is 40%, the content of S is 25%, and the content of Sb is 4%; the concentration of As ions in the arsenic-removing wastewater is 0.15 mg/L.
And 3, placing the arsenic-removal wastewater obtained in the step 2 into a reaction tank, then adding antimony electrodeposition barren liquor into the reaction tank, adjusting the pH of the solution in the reaction tank to be 5, stirring for 1h, and then performing filter pressing to obtain antimony sulfide slag containing arsenic and antimony-removal wastewater, wherein the antimony sulfide slag can be sent to an antimony workshop for ore blending treatment, and the antimony-removal wastewater is sent to a three-effect evaporation system for preparing sodium sulfate.
The main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
ZnSO4+H2S→ZnS+H2SO4
FeSO4+H2S→FeS+H2SO4
Na3SbS3+H2SO4→Na2SO4+H2S+Sb2S3
the antimony sulfide slag (dry basis) comprises the following main components in percentage by weight: sb content is 50% and S content is 25%; the concentration of As ions in the antimony removal wastewater is 0.1mg/L, Sb, the concentration of As ions is 0.2mg/L, Cu, the concentration of As ions is 0.1mg/L, Zn, and the concentration of As ions is 2mg/L, Fe.
Example 2
A method for recovering valuable metals in waste acid in a gradient manner by utilizing antimony electrodeposition barren solution comprises the following steps:
step 1, preparing two byproducts generated in the smelting industry, namely antimony electrodeposition barren solution and waste acid:
the antimony electrodeposition barren solution comprises the following components in concentration: sb ion concentration 40g/L, Na2The S concentration is 45g/L, Au, the ion concentration is 2mg/L, As, the ion concentration is 1g/L, NaOH, and the concentration is 50 g/L;
the concentration of each component in the waste acid is as follows: as ion concentration is 20g/L, Cu ion concentration 2g/L, Fe ion concentration 1g/L, Sb ion concentration 2g/L, Zn ion concentration 1g/L, H2SO4The concentration was 50 g/L.
Putting a certain amount of antimony electrodeposition barren solution into a reaction tank, and slowly adding contaminated acid into the antimony electrodeposition barren solution, wherein the molar ratio of the contaminated acid to the antimony electrodeposition barren solution in the reaction tank is 1.2: 1; stirring for 1h, and then performing filter pressing to obtain copper sulfide slag containing noble metals and copper-removing wastewater, wherein the copper sulfide slag is sent to pyrometallurgical ore blending treatment;
the main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
CuSO4+H2S→CuS+H2SO4
the copper sulfide slag (dry basis) comprises the following main components in percentage by weight: 50% of Cu, 30% of S, 2% of As and 3% of Sb; the concentration of Cu ions in the copper removal wastewater is 0.07 g/L;
step 2, placing a certain amount of contaminated acid into a reaction tank, then adding the copper removal wastewater obtained in the step 1 into the reaction tank, wherein the contaminated acid is excessive, adjusting the pH value of the solution in the reaction tank to be 0.8, stirring for 1 hour, and then performing filter pressing to obtain copper-containing arsenic sulfide slag and arsenic removal wastewater, wherein the arsenic sulfide slag can be sent to an arsenic roasting recovery workshop for ore blending treatment;
the main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
HAsO2+H2S→As2S3+H2O
CuSO4+H2S→CuS+H2SO4
the arsenic sulfide slag (dry basis) comprises the following main components in percentage by weight: 50% of As content, 20% of S content and 4% of Sb content; the concentration of As ions in the arsenic-removing wastewater is 0.2 mg/L.
And 3, placing the arsenic-removal wastewater obtained in the step 2 into a reaction tank, then adding antimony electrodeposition barren solution into the reaction tank, adjusting the pH value of the solution in the reaction tank to be 5, stirring for 1h, and then performing filter pressing to obtain antimony sulfide slag containing arsenic and antimony-removal wastewater, wherein the antimony sulfide slag can be sent to an antimony workshop for ore blending treatment, and the antimony-removal wastewater is sent to a triple effect evaporation system for preparing sodium sulfate.
The main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
ZnSO4+H2S→ZnS+H2SO4
FeSO4+H2S→FeS+H2SO4
Na3SbS3+H2SO4→Na2SO4+H2S+Sb2S3
the antimony sulfide slag (dry basis) comprises the following main components in percentage by weight: sb content is 60%, and S content is 25%; the concentration of As ions in the antimony-removing wastewater is 0.15mg/L, Sb, the concentration of As ions is 0.3mg/L, Cu, the concentration of As ions is 0.1mg/L, Zn, and the concentration of As ions is 2mg/L, Fe.
Example 3
A method for recovering valuable metals in waste acid in a gradient manner by utilizing antimony electrodeposition barren solution comprises the following steps:
step 1, preparing two byproducts generated in the smelting industry, namely antimony electrodeposition barren solution and waste acid:
the antimony electrodeposition barren solution comprises the following components in concentration: sb ion concentration of 50g/L, Na2The S concentration is 60g/L, Au, the ion concentration is 2mg/L, As, the ion concentration is 1g/L, NaOH, and the concentration is 60 g/L;
the concentration of each component in the waste acid is as follows: as ion concentration is 30g/L, Cu ion concentration 2g/L, Fe ion concentration 1g/L, Sb ion concentration 2g/L, Zn ion concentration 1g/L, H2SO4The concentration was 70 g/L.
Putting a certain amount of antimony electrodeposition barren solution into a reaction tank, and slowly adding contaminated acid into the antimony electrodeposition barren solution, wherein the molar ratio of the contaminated acid to the antimony electrodeposition barren solution in the reaction tank is 1.2: 1; stirring for 1h, and then performing filter pressing to obtain copper sulfide slag containing noble metals and copper-removing wastewater, wherein the copper sulfide slag is sent to pyrometallurgical ore blending treatment;
the main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
CuSO4+H2S→CuS+H2SO4
the copper sulfide slag (dry basis) comprises the following main components in percentage by weight: 55% of Cu, 30% of S, 2% of As and 3% of Sb; the concentration of Cu ions in the copper removal wastewater is 0.08 g/L;
step 2, placing a certain amount of waste acid into a reaction tank, adding the copper-removing wastewater obtained in the step 1 into the reaction tank, adjusting the pH of the solution in the reaction tank to be 0.8 when the waste acid is excessive, stirring for 1 hour, and performing filter pressing to obtain copper-containing arsenic sulfide slag and arsenic-removing wastewater, wherein the arsenic sulfide slag can be sent to an arsenic roasting recovery workshop for ore blending treatment;
the main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
HAsO2+H2S→As2S3+H2O
CuSO4+H2S→CuS+H2SO4
the arsenic sulfide slag (dry basis) comprises the following main components in percentage by weight: 60% of As content, 25% of S content and 4% of Sb content; the concentration of As ions in the arsenic-removing wastewater is 0.25 mg/L.
And 3, placing the arsenic-removal wastewater obtained in the step 2 into a reaction tank, then adding antimony electrodeposition barren liquor into the reaction tank, adjusting the pH of the solution in the reaction tank to be 5, stirring for 1h, and then performing filter pressing to obtain antimony sulfide slag containing arsenic and antimony-removal wastewater, wherein the antimony sulfide slag can be sent to an antimony workshop for ore blending treatment, and the antimony-removal wastewater is sent to a three-effect evaporation system for preparing sodium sulfate.
The main reaction is as follows:
Na2S+H2SO4→Na2SO4+H2S
NaOH+H2SO4→Na2SO4+H2O
ZnSO4+H2S→ZnS+H2SO4
FeSO4+H2S→FeS+H2SO4
Na3SbS3+H2SO4→Na2SO4+H2S+Sb2S3
the antimony sulfide slag (dry basis) comprises the following main components in percentage by weight: the Sb content is 65 percent, and the S content is 22 percent; the concentration of As ions in the antimony-removing wastewater is 0.2mg/L, Sb, the concentration of As ions is 0.4mg/L, Cu, the concentration of As ions is 0.1mg/L, Zn, and the concentration of As ions is 2mg/L, Fe.
From the ratio of the main components of the metal sulfide in each example, and the ion concentration of each metal in the wastewater, the following can be concluded:
the antimony electro-deposition barren solution and the waste acid are combined to be treated, so that on one hand, the energy consumption of freezing and crystallizing the antimony electro-deposition barren solution is saved, and on the other hand, crude antimony crystalline salt does not need to be treated, and the treatment cost of the antimony electro-deposition barren solution is reduced; on the other hand, the electrodeposition barren solution is used for replacing a vulcanizing agent, so that the treatment cost of the waste acid is reduced, valuable metals can be recycled in a gradient manner, the aim of 'processing waste with waste and changing waste into valuable' can be achieved, and the method has the advantages of low treatment equipment investment, reasonable treatment process, high treatment efficiency, low treatment cost and the like; the method has profound significance for improving the economic benefit of enterprises and making the enterprises green and sustainable development roads.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (6)
1. A method for recovering valuable metals in waste acid in a gradient manner by utilizing antimony electrodeposition barren solution is characterized by comprising the following steps: the method comprises the following steps:
step 1, placing a certain amount of antimony electrodeposition barren solution into a reaction tank, slowly adding contaminated acid into the antimony electrodeposition barren solution, stirring for 0.5-1 h, and then performing filter pressing to obtain copper sulfide slag containing precious metals and copper-removed wastewater, wherein the copper sulfide slag is sent to pyrometallurgical ore blending treatment;
step 2, placing a certain amount of contaminated acid into a reaction tank, then adding the copper-removing wastewater obtained in the step 1 into the reaction tank, adjusting the pH of the solution in the reaction tank to be more than 0.5 and less than 1, stirring for 0.5-1 h, and then performing filter pressing to obtain copper-containing arsenic sulfide slag and arsenic-removing wastewater, wherein the arsenic sulfide slag can be sent to an arsenic roasting recovery workshop for ore blending treatment;
and 3, placing the arsenic-removed wastewater obtained in the step 2 into a reaction tank, then adding antimony electrodeposition barren liquor into the reaction tank, adjusting the pH of the solution in the reaction tank to 3-5, stirring for 0.5-1 h, and then performing filter pressing to obtain antimony sulfide slag containing arsenic and antimony-removed wastewater, wherein the antimony sulfide slag can be sent to an antimony workshop for ore blending treatment, and the antimony-removed wastewater is sent to a three-effect evaporation system for preparing sodium sulfate.
2. The method for cascade recovery of valuable metals in waste acid by using antimony electrodeposition barren solution as claimed in claim 1, wherein: the antimony electrodeposition barren solution comprises the following components in concentration: sb ion concentration of 20-50 g/L, Na2The S concentration is 40-60 g/L, Au, the ion concentration is 1-5 mg/L, As, the ion concentration is 0.1-1 g/L, NaOH, and the concentration is 30-60 g/L; the concentration of each component in the waste acid is as follows: as ion concentration is 10-30 g/L, Cu ion concentration 1-3 g/L, Fe ion concentration 0.5-1 g/L, Sb ion concentration 1-3 g/L, Zn ion concentration 0.2-1 g/L, H2SO4The concentration is 20-80 g/L.
3. The method for cascade recovery of valuable metals in waste acid by using antimony electrodeposition barren solution as claimed in claim 1, wherein: in the step 1, the molar ratio of the waste acid to the antimony electrodeposition barren solution in the reaction tank is (1.1-1.2): 1.
4. the method for cascade recovery of valuable metals in waste acid by using antimony electrodeposition barren solution as claimed in claim 1, wherein: in the step 1, the copper sulfide slag (dry basis) comprises the following main components in percentage by weight: 40-60% of Cu, 20-30% of S, less than or equal to 2% of As and less than or equal to 3% of Sb; the concentration of Cu ions in the copper removal wastewater is controlled to be less than or equal to 0.1 g/L.
5. The method for cascade recovery of valuable metals in waste acid by using antimony electrodeposition barren solution as claimed in claim 1, wherein: in the step 2, the main components of the arsenic sulfide slag (dry basis) are as follows: the content of As is 40-70%, the content of S is 15-25%, and the content of Sb is less than or equal to 5%; the concentration of As ions in the arsenic-removing wastewater is controlled to be less than or equal to 0.3 mg/L.
6. The method for cascade recovery of valuable metals in waste acid by using antimony electrodeposition barren solution as claimed in claim 1, wherein: in step 3, the antimony sulfide slag (dry basis) comprises the following main components in percentage by weight: sb content is 50-65%, S content is 20-30%; the concentration of As ions in the antimony removal wastewater is controlled to be less than or equal to 0.3mg/L, Sb and the concentration of As ions is controlled to be less than or equal to 0.5mg/L, Cu and the concentration of As ions is controlled to be less than or equal to 0.1mg/L, Zn and the concentration of As ions is controlled to be less than or equal to 10mg/L, Fe and the concentration of As ions is controlled to be less than or equal to 10 mg/L.
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| CN105603190A (en) * | 2015-12-28 | 2016-05-25 | 中南大学 | Method for purifying and recovering valuable metal by copper electrolyte |
| CN109628953A (en) * | 2018-12-26 | 2019-04-16 | 浙江工业大学 | The method of arsenic removal antimony bismuth is gone in a kind of copper electrolyte |
| CN114084904A (en) * | 2021-11-08 | 2022-02-25 | 广西南国铜业有限责任公司 | Method for copper electrolyte purification and waste acid cooperative recycling treatment |
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| CN105603217A (en) * | 2015-12-28 | 2016-05-25 | 中南大学 | Method for enriching and recovering antimony in contaminated acid vulcanization residue |
| CN105603190A (en) * | 2015-12-28 | 2016-05-25 | 中南大学 | Method for purifying and recovering valuable metal by copper electrolyte |
| CN109628953A (en) * | 2018-12-26 | 2019-04-16 | 浙江工业大学 | The method of arsenic removal antimony bismuth is gone in a kind of copper electrolyte |
| CN114084904A (en) * | 2021-11-08 | 2022-02-25 | 广西南国铜业有限责任公司 | Method for copper electrolyte purification and waste acid cooperative recycling treatment |
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