CN108642519B - Environment-friendly zinc electrolysis process - Google Patents
Environment-friendly zinc electrolysis process Download PDFInfo
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- CN108642519B CN108642519B CN201810571700.4A CN201810571700A CN108642519B CN 108642519 B CN108642519 B CN 108642519B CN 201810571700 A CN201810571700 A CN 201810571700A CN 108642519 B CN108642519 B CN 108642519B
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- 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
- C25C1/16—Electrolytic production, recovery or refining of metals by electrolysis of solutions of zinc, cadmium or mercury
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- 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
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/20—Obtaining zinc otherwise than by distilling
- C22B19/24—Obtaining zinc otherwise than by distilling with leaching with alkaline solutions, e.g. ammonia
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- 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
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
- C22B7/008—Wet processes by an alkaline or ammoniacal leaching
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
- C25C7/06—Operating or servicing
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- 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 relates to an environment-friendly zinc electrolysis process, which comprises the following steps: s1: collecting waste liquid generated by electrolytic zinc; s2: mixing the waste liquid obtained in the step S1 with zinc ash, leaching zinc, and enabling the pH value of the solution to be more than or equal to 5.0 after leaching; s3: separating out the liquid of the step S2; s4: removing iron from the liquid separated in the step S3; s5: separating out the liquid in the step S4; s6: injecting the liquid separated in the step S5 into an electrolytic bath for electroanalysis of zinc, and conveying the electrolyzed waste liquid to the step S1 for recycling; adding ammonia or ammonium salt or their mixture into the liquid at any step S1-S6 to convert the ammonia-ammonium buffer solution into NH 3 Calculating NH in the circulating liquid 3 The minimum mass percentage content is not lower than 2 percent. The invention has no waste gas and waste water, the flow is easier to control, the plate is not easy to burn, the process flow is shortened, the total cost is reduced, the quality is controllable, and the requirement on raw materials is low.
Description
Technical Field
The invention relates to an electrolytic zinc process, in particular to an environment-friendly electrolytic zinc process.
Background
In the industry, the zinc electrolysis process mainly comprises three types, namely, a sulfuric acid method: the raw material requirements are too high (the requirements on fluorine, chlorine, copper, cobalt, nickel, cadmium, arsenic, tellurium and germanium, organic matters and zinc content are all met). The cathode plate is generally an aluminum plate, the aluminum plate is low in strength and easy to break, and the electrolyte can be stuck when containing fluorine. The anode plate is reversely dissolved, so that the lead content in the electrolyte is high, the anode mud is required to be cleaned regularly, time is wasted, the electrolyte is subjected to dip dyeing when the anode mud is cleaned, and meanwhile, in order to prevent the reverse dissolution, the anode protection is required to be carried out in the electrolysis, so that the power consumption is increased, the process flow and the medicament cost are increased, and the like. The chlorine in the electrolyte causes the anode plate to kill the head and generates the volatilization pollution of hydrochloric acid. The requirement for clean and pure bloom is high, the requirement for each harmful index is high, and various burning plates are often generated even under strict control. The difficulty of producing the 0# zinc is high. The process needs chlorine washing, generates waste water, consumes a large amount of medicaments and energy, increases the process flow and makes the process flow complicated. The electrolysis in an acidic environment generates a large amount of hydrochloric acid steam, pollutes the environment, cannot cut off the power in the process, and has high cell pressure, high cost, complex material consumption and the like. A large amount of hydrochloric acid steam generated on the electrolytic bath is discharged into the air, equipment facilities are damaged, and the environment is polluted, namely an ammonia method: for example, compared with the file CN107099665A, the leaching rate is not high, the zinc content in the waste residue is high, the ammonia is easy to volatilize, the environment is polluted, the cost of producing electrolytic zinc by an ammonia method is high, the electric effect is poor, the casting rate is low, the ammonia recovery is difficult, and the like. The ammonia process utilizes the complexing property of ammonia to form Zn (NH) from zinc 3 ) 4 2+ The sufficient amount of NH is needed to be added before the zinc raw material is dissolved to realize the zinc transfer 3 To ensure that zinc can react with NH 3 Combine to form Zn (NH) 3 ) 4 2+ Forming a solution and ensuring a high amount of Zn (NH) 3 ) 4 2+ Is present to meet the amount of zinc required for electrolysis. If ammonium salt is additionally added, the main purpose is to form a buffering effect with ammonia, so that the solution added with a large amount of ammonia does not have too high pH value, because the pH value is too high, alkalinity is increased, ammonia is easy to volatilize, the solubility of ammonia is reduced, and the leaching amount of zinc is influenced. Zn (NH) 3 ) 4 2+ ⇌Zn 2+ +4NH 3 . When zinc is leached by adding zinc raw material, the balance is moved leftwards, and at this time, a large amount of ammonia is needed to react with zinc in the raw material, so that the zinc content in the solution is increased. During electrolysis, a lot of ammonia receives protons and turns into ammonium, ammonium salt crystals are easily formed, and in addition, a lot of ammonia on the anode is decomposed into nitrogen and hydrogen due to electrolysis, and the balance is promoted to move to the right due to the precipitation of cathode zinc and the consumption of ammonia. The zinc is carried by the above circulation, and it can be seen that a large amount of ammonia is consumed in the process. According to the leaching requirement of zinc, ammonia is added before or during zinc leaching. Most are in the form of ammonia. In the whole process, the ammonia consumption is very large, and a large amount of free ammonia is easily volatilized due to the dissolution problem, so the ammonia smell is very large. The traditional ammonia electrolysis equation is as follows:
cathode: zn (NH) 3 ) 4 2+ +2e=Zn+NH 3 ↑
Anode: 4OH - -4e=2H 2 O+O 2 ↑
2NH 3 =N 2 ↑+H 2 ↓ (condition: electrifying)
Zn (NH) in solution 3 ) 4 2+ 2 electrons are obtained, and simple substance zinc is separated out
Extraction method: only replaces the leaching process of the sulfuric acid method, other defects of the sulfuric acid method still exist, the extracting agent kerosene is generally used for extraction, the safety is particularly poor, and the post process after extraction is complex.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide an environment-friendly zinc electrolysis process.
The technical scheme adopted by the invention for solving the technical problems is as follows: an environment-friendly zinc electrolysis process comprises the following steps:
s1: collecting waste liquid generated by electrolyzing zinc;
s2: mixing the waste liquid obtained in the step S1 with zinc ash, stirring and soaking until the pH value of the solution is more than or equal to 5.0 and less than or equal to 7 and the content of zinc in the solution is more than or equal to 30 g/L;
s3: the liquid configured in the step S2 is subjected to pressure filtration through a pressure filter to separate the liquid;
s4: removing iron from the liquid separated in the step S3 to ensure that the iron content in the solution is below 40 mg/L;
s5: performing filter pressing treatment on the solution obtained in the step S4 to separate liquid;
s6: injecting the liquid separated in the step S5 into an electrolytic bath for electroanalysis of zinc, and conveying the electrolyzed waste liquid to the step S1 for continuous recycling;
adding ammonia or ammonium salt or mixture thereof into the liquid in any step of the above steps S1-S6 to form ammonia-ammonium buffer solution in the circulating liquid, and converting the ammonia-ammonium buffer solution into NH 3 Calculating the NH content of the liquid to be added to the ammonia-ammonium buffer solution 3 The mass percentage content is more than 2 percent. The circulating liquid refers to the liquid in each step after the ammonia-ammonium buffer solution is added.
In the design, the ammonia-ammonium buffer solution is adopted, the higher pH value is adopted for leaching in the leaching section, so that the content of harmful impurities in the electrolyte is lower, the purification is easier, and a plurality of harmful impurities do not enter the electrolyte during leaching, thereby improving the quality of the electrolyte in the electrolysis section. In addition, the neutral electrolysis of the invention basically avoids plate burning, greatly reduces the tank pressure, reduces the technical requirements of factory production, and simultaneously reduces the production cost. Meanwhile, during electrolysis, no harmful gas is generated, and hydrochloric acid vapor is avoided. The electrolytic anode plate can makeOther inert electrodes, such as graphite anodes, are used, so that the electrolyte is not afraid of chlorine, and the condition of discharging sewage by washing chlorine by traditional electrolytic zinc is avoided. And by adopting neutral electrolysis, the requirement on anode protection is greatly reduced, the cleaning period of anode mud is longer, and if a graphite anode is adopted, anode protection is not needed, and the cleaning process of the anode mud is also not needed. Therefore, the complexity of the process is reduced, the efficiency is improved, and the consumption of the anode plate is reduced. From the environmental point of view, the traditional electrolytic zinc has the requirement on the index of fluorine and chlorine in the electrolyte, the chlorine reduction needs a large amount of water, the water washing is carried out, wastewater is generated, an ammonia-ammonium buffer system has double characteristics, ammonia in the solution has complexing characteristic, and meanwhile, the buffer solution plays a buffering role on acid in the solution, namely, in the system, even if a great amount of acid is added, the pH value still has no great change. The system containing a lot of acid has strong leaching capacity for zinc in zinc ash, high leaching speed, thorough and clean leaching and low leaching capacity for electrolyzing harmful impurities. Due to the change of the leaching process, the requirement on raw materials is greatly reduced, and the cost can be greatly reduced. The resources can be effectively utilized, and the method conforms to the national environmental protection policy. Due to NH 3 -NH 4 + The buffering effect and the complexing property of ammonia are realized by using the reaction of acid carried by the buffer solution and zinc in the zinc raw material under the neutral condition to dissolve the zinc into an ionic state and then partially form zinc-ammonia complex ions. By means of equilibrium shift, exchange between zinc ions and acid is achieved. The basic principle of complex buffering is as follows: zn (NH) 3 ) 4 2+ +4H + ⇌Zn 2+ +4NH 3 +4H + ⇌Zn 2+ +4NH 4 + . When the raw material zinc ash is added, ZnO and H in the raw material + Reaction to produce Zn 2+ Then partial formation of Zn (NH) 3 ) 4 2+ Promote the balance to move to the left, Zn in the system 2+ With Zn (NH) 3 ) 4 2+ Amount increased, NH 4 + The amount is reduced. During electrolysis, zinc ions in the solution are reduced because zinc in the solution is changed into metal zinc to be separated out, and OH is consumed at the anode - （4OH - -4e=2H 2 O + O2 ×) increases the acid in solution, forcing the equilibrium to move to the right, and the PH is not too high. The exchange of zinc and acid is achieved by the above cycle. Any one of ammonia or ammonium salts or a mixture thereof may be added at any station depending on the buffering capacity, i.e. acid-holding capacity, of the solution. The whole process is finished at about neutrality without ammonia smell. Depending on the buffer capacity, it is necessary to add ammonia or ammonium. The electrolysis principle of the invention is as follows: cathode: zn 2+ +2e = Zn, anode: 4OH - -4e=2H 2 The zinc ions in the O + O2 ↓solutionobtain 2 electrons to separate out simple substance zinc
As a further improvement of the design, the current density in the electrolytic cell in the step S6 is more than or equal to 200A/m 2 。
As a further improvement of the design, in the step S4, one or more of hydrogen peroxide, potassium permanganate, a special iron removal agent, a resin, and the like are added to remove iron from the liquid separated in the step S3.
The zinc content in the liquid in the step S2 is more than or equal to 30g/L, the production efficiency is higher, and the production cost is low.
As a further improvement of the present design, in step S2, the PH of the liquid is greater than or equal to 5.9 and less than or equal to 7.
As a further improvement of the design, the iron content in the liquid is controlled to be below 20mg/L in the step S4, electricity is saved, and the quality of the zinc sheets is higher.
As a further improvement of the design, one or more of a simple substance of zinc or a simple substance of manganese or a special purifying agent for electrolytic zinc is added into the liquid separated in the step S5 to remove cadmium and other impurities, the liquid is separated by pressure filtration, and the separated liquid is electrolyzed and separated out of zinc through the process of the step S6. Higher standard zinc sheets can be produced.
As a further improvement of the design, the waste liquid of step S6 is used to wash and filter-press the filter residue generated in step S3, and the filter-pressed liquid is processed in step S2. The utilization of zinc in the filter residue is convenient to improve.
As a further improvement of the design, a mixing process is added between the step S5 and the step S6, the mixing process mixes part of the waste liquid of the step S6 with the liquid separated from the step S5, the mixed liquid is processed again in the step S6, the zinc content in the mixed liquid of the waste liquid of the step S6 and the liquid separated from the step S5 is more than or equal to 15g/L, the production cost is low, the zinc content before electrolysis is more conveniently controlled, and the production management is facilitated.
As a further improvement of the design, the ammonia-ammonium buffer solution is a solution formed by one of ammonia and ammonium salt or a mixture of the ammonia and the ammonium salt. Under the condition of not changing the pH value, the acid required for dissolving the zinc ash can be greatly reserved. The zinc liquid dissolved from the waste liquid has higher quality and less harmful impurities.
The beneficial effects of the invention are: the invention is environment-friendly (no waste gas and waste water); the technical index requirement of the electrolyte is reduced, the electrolyte is easier to control and is not easy to burn; shortening the process flow and simplifying the operation; the cost is reduced in multiple aspects, and the total cost is greatly reduced; the product quality is more stable and controllable, and high-quality zinc can be obtained more easily; sixthly, the requirements on the raw materials are greatly reduced, a plurality of raw materials which are difficult to use or can not be used before can be used, and the range of the raw materials is widened.
Drawings
The invention is further illustrated by the following examples in conjunction with the drawings.
FIG. 1 is a schematic view of the shortest process flow of the present invention.
FIG. 2 is a schematic diagram of the longest process flow of the present invention.
Detailed Description
The present invention is described in detail below with reference to specific examples, wherein the exemplary examples and descriptions are provided only for explaining the present invention and are not intended to limit the present invention.
Example (b): the technical scheme adopted by the invention for solving the technical problems is as follows: an environment-friendly zinc electrolysis process comprises the following steps:
s1: collecting waste liquid generated by electrolytic zinc;
s2: mixing the waste liquid obtained in the step S1 with zinc ash, stirring and soaking until the pH value of the solution is more than or equal to 5.0 and less than or equal to 7 and the content of zinc in the solution is more than or equal to 30 g/L;
s3: the liquid configured in the step S2 is subjected to pressure filtration through a pressure filter to separate the liquid;
s4: removing iron from the liquid separated in the step S3 to ensure that the iron content in the solution is below 40mg/L, and removing iron by adding hydrogen peroxide or potassium permanganate solution or special iron removal agents or resin and the like;
s5: performing filter pressing treatment on the solution obtained in the step S4 to separate liquid;
s6: injecting the liquid separated in the step S5 into an electrolytic bath for electroanalysis of zinc, and conveying the electrolyzed waste liquid to the step S1 for continuous recycling;
adding ammonia or ammonium salt or mixture thereof into the liquid in any step of the above steps S1-S6 to form ammonia-ammonium buffer solution in the circulating liquid, and converting the ammonia-ammonium buffer solution into NH 3 Calculating the NH content of the liquid to be added to the ammonia-ammonium buffer solution 3 The mass percentage content is more than 2 percent.
In the design, the ammonia-ammonium buffer solution is adopted, the higher pH value is adopted in the leaching section for leaching, so that the content of harmful impurities in the electrolyte is lower, the purification is easier, and a plurality of harmful impurities do not enter the electrolyte during leaching, thereby improving the quality of the electrolyte in the electrolysis section. In addition, the neutral electrolysis of the invention basically avoids plate burning, greatly reduces the groove pressure, reduces the technical requirements of factory production and simultaneously reduces the production cost. Meanwhile, during electrolysis, no harmful gas is generated, and hydrochloric acid vapor is avoided. The electrolytic anode plate can use other inert electrodes, such as a graphite anode, so that the electrolyte is not afraid of chlorine, and the condition that the traditional electrolytic zinc washes chlorine and discharges sewage is avoided. And by adopting neutral electrolysis, the requirement on anode protection is greatly reduced, the cleaning period of anode mud is longer, and if a graphite anode is adopted, anode protection is not needed, and the cleaning process of the anode mud is also not needed. Thus not only reducing the complexity of the process, but also improving the efficiency and reducing the consumption of anode platesAnd (4) consuming. From the environmental point of view, the traditional electrolytic zinc increases the requirement on the index of fluorine and chlorine in the electrolyte, the chlorine reduction needs a large amount of water, the water washing is carried out, wastewater is generated, an ammonia-ammonium buffer system has double characteristics, ammonia in the solution has complexing characteristic, and meanwhile, the buffer solution plays a role in buffering acid in the solution, namely, in the system, even if a great amount of acid is added, the pH value still does not change greatly. The system containing a lot of acid has strong leaching capability to zinc in zinc ash, high leaching speed, thorough and clean leaching and low leaching capability to harmful impurities in electrolysis. Due to the change of the leaching process, the requirement on raw materials is greatly reduced, and the cost can be greatly reduced. The resources can be effectively utilized and the method conforms to the national environmental protection policy. Due to NH 3 -NH 4 + The buffering effect and the complexing property of ammonia are realized by using the reaction of acid carried by the buffer solution and zinc in the zinc raw material under the neutral condition to dissolve the zinc into an ionic state and then partially form zinc-ammonia complex ions. By means of equilibrium shift, exchange between zinc ions and acid is achieved. The basic principle of complex buffering is as follows: zn (NH) 3 ) 4 2+ +4H + ⇌Zn 2+ +4NH 3 +4H + ⇌Zn 2+ +4NH 4 + . When the raw material zinc ash is added, ZnO and H in the raw material + React to form Zn 2+ Then partial formation of Zn (NH) 3 ) 4 2+ Promote the balance to move to the left, Zn in the system 2+ With Zn (NH) 3 ) 4 2+ Amount increased, NH 4 + The amount is reduced. During electrolysis, zinc ions in the solution are reduced because zinc in the solution is changed into metal zinc to be separated out, and OH is consumed at the anode - （4OH - -4e=2H 2 O + O2 ×) increases the acid in solution, forcing the equilibrium to move to the right, and the PH is not too high. The exchange of zinc and acid is achieved by the above cycle. Depending on the buffer capacity of the solution, i.e. the acid-holding capacity, any one of ammonia or ammonium salts or mixtures thereof may be added at any stage. The whole process is finished at about neutral without ammonia smell. Depending on the buffer capacity, it is necessary to add ammonia or ammonium. The invention is electricThe solution principle is as follows: cathode: zn 2+ +2e = Zn, anode: 4OH - -4e=2H 2 The zinc ions in the O + O2 ↓ solution obtain 2 electrons to separate out simple substance zinc.
As a further improvement of the design, the current density in the electrolytic cell in the step S6 is more than or equal to 200A/m 2 。
As a further improvement of the design, in the step S4, one or more of hydrogen peroxide, potassium permanganate, a special iron removal agent, a resin, and the like are added to remove iron from the liquid separated in the step S3.
The zinc content in the liquid in the step S2 is more than or equal to 30g/L, the production efficiency is higher, and the production cost is low.
As a further improvement of the present design, in step S2, the PH of the liquid is greater than or equal to 5.9 and less than or equal to 7.
As a further improvement of the design, the iron content in the liquid is controlled to be below 20mg/L in the step S4, electricity is saved, and the quality of the zinc sheets is higher.
As a further improvement of the design, one or more of simple substances of zinc or manganese or special purifying agents for electrolytic zinc are added into the liquid separated in the step S5 to remove cadmium and other impurities, the liquid is separated by pressure filtration, and the separated liquid is electrolyzed and separated out of zinc by the process in the step S6. Higher standard zinc sheets can be produced.
As a further improvement of the design, the waste liquid in the step S6 is used for washing and pressure filtering the filter residue generated in the step S3, and the liquid obtained by pressure filtering is processed in the step S2. The utilization of zinc in the filter residue is convenient to improve.
As a further improvement of the design, a mixing process is added between the step S5 and the step S6, the mixing process mixes part of the waste liquid of the step S6 with the liquid separated from the step S5, the mixed liquid is processed again in the step S6, the zinc content in the mixed liquid of the waste liquid of the step S6 and the liquid separated from the step S5 is more than or equal to 15g/L, the production cost is low, the zinc content before electrolysis is more conveniently controlled, and the production management is facilitated.
As a further improvement of the design, the ammonia-ammonium buffer solution is a solution formed by one of ammonia and ammonium salt or a mixture of the ammonia and the ammonium salt. Under the condition of not changing the pH value, the acid required for dissolving the zinc ash can be greatly reserved. The zinc liquid dissolved from the waste liquid has higher quality and less harmful impurities.
The above description is only an embodiment of the present invention, and not intended to limit the scope of the present invention, and all equivalent flow transformations made by the present specification, or directly or indirectly applied to other related technical fields, are included in the scope of the present invention.
Claims (9)
1. An environment-friendly zinc electrolysis process is characterized by comprising the following steps:
s1: collecting waste liquid generated by electrolyzing zinc;
s2: mixing the waste liquid obtained in the step S1 with zinc ash, stirring and soaking until the pH value of the solution is more than or equal to 5.0 and less than or equal to 7 and the content of zinc in the solution is more than or equal to 30 g/L;
s3: the liquid configured in the step S2 is subjected to pressure filtration through a pressure filter, and the liquid is separated;
s4: removing iron from the liquid separated in the step S3 to ensure that the iron content in the solution is below 40 mg/L;
s5: performing filter pressing treatment on the solution obtained in the step S4 to separate liquid;
s6: injecting the liquid separated in the step S5 into an electrolytic bath for electroanalysis of zinc, and conveying the electrolyzed waste liquid to the step S1 for continuous recycling;
adding ammonia or ammonium salt or mixture thereof into the liquid in any step of the above steps S1-S6 to form ammonia-ammonium buffer solution in the circulating liquid, and converting the ammonia-ammonium buffer solution into NH 3 Calculating the NH content of the liquid to be added to the ammonia-ammonium buffer solution 3 The mass percentage content is more than 2 percent.
2. The environment-friendly zinc electrolysis process as claimed in claim 1, wherein the current density in the electrolysis bath in the step S6 is greater than or equal to 200A/m 2 。
3. The environment-friendly zinc electrolysis process as claimed in claim 2, wherein one or more of hydrogen peroxide, potassium permanganate, special iron removal agents or resins is/are added in the step S4 to remove iron from the liquid separated in the step S3.
4. The environment-friendly zinc electrolysis process as claimed in claim 1, wherein the liquid pH in step S2 is greater than or equal to 5.9 and less than or equal to 7.
5. The environment-friendly zinc electrolysis process as claimed in claim 1, wherein the iron content in the liquid in the step S4 is controlled to be below 20 mg/L.
6. The environment-friendly zinc electrolysis process as claimed in claim 1, wherein one or more of elemental zinc or elemental manganese or a special purifying agent for electrolytic zinc is added to the liquid separated in step S5 to remove cadmium and other impurities, and the liquid is separated by pressure filtration, and the separated liquid is electrolyzed to separate out zinc by the process of step S6.
7. The environment-friendly zinc electrolysis process as claimed in claim 1, wherein the waste liquid from step S6 is used to wash and filter-press the filter residue from step S3, and the filter-pressed liquid is processed in step S2.
8. The environment-friendly zinc electrolysis process as claimed in claim 1, wherein a mixing step is added between step S5 and step S6, the mixing step mixes part of the waste liquid from step S6 with the liquid separated from step S5, and the mixed liquid is treated again in step S6, and the content of zinc in the mixed liquid of the waste liquid from step S6 and the liquid separated from step S5 is not less than 15 g/L.
9. The environment-friendly zinc electrolysis process according to claim 8, wherein the ammonia-ammonium buffer solution is a solution formed by one or a mixture of ammonia and ammonium salt.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1069297A (en) * | 1991-08-02 | 1993-02-24 | 北京矿冶研究总院 | Method for producing zinc powder from zinc-containing material by leaching electrolysis method |
| CN1093418A (en) * | 1993-04-09 | 1994-10-12 | 广州市新技术应用研究所 | Complex compound electrolysis system zinc |
| CN1341760A (en) * | 2001-08-06 | 2002-03-27 | 邵家跃 | Wet zinc-smelting process |
| CN103060553A (en) * | 2012-12-29 | 2013-04-24 | 邓世碧 | Method for purifying zinc from zinc concentrate |
| CN104005051A (en) * | 2014-04-29 | 2014-08-27 | 戴兴征 | Method for extracting electrodeposited zinc from zinc oxide powder in ammonium chloride solution system |
| CN107099665A (en) * | 2017-06-20 | 2017-08-29 | 青铜峡市鼎辉工贸有限公司 | A kind of production technology of electrolytic zinc |
-
2018
- 2018-06-06 CN CN201810571700.4A patent/CN108642519B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1069297A (en) * | 1991-08-02 | 1993-02-24 | 北京矿冶研究总院 | Method for producing zinc powder from zinc-containing material by leaching electrolysis method |
| CN1093418A (en) * | 1993-04-09 | 1994-10-12 | 广州市新技术应用研究所 | Complex compound electrolysis system zinc |
| CN1341760A (en) * | 2001-08-06 | 2002-03-27 | 邵家跃 | Wet zinc-smelting process |
| CN103060553A (en) * | 2012-12-29 | 2013-04-24 | 邓世碧 | Method for purifying zinc from zinc concentrate |
| CN104005051A (en) * | 2014-04-29 | 2014-08-27 | 戴兴征 | Method for extracting electrodeposited zinc from zinc oxide powder in ammonium chloride solution system |
| CN107099665A (en) * | 2017-06-20 | 2017-08-29 | 青铜峡市鼎辉工贸有限公司 | A kind of production technology of electrolytic zinc |
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| CN108642519A (en) | 2018-10-12 |
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