CN115369237A - Method for balancing production and consumption of manganese ions in zinc smelting - Google Patents

Method for balancing production and consumption of manganese ions in zinc smelting Download PDF

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CN115369237A
CN115369237A CN202211147792.6A CN202211147792A CN115369237A CN 115369237 A CN115369237 A CN 115369237A CN 202211147792 A CN202211147792 A CN 202211147792A CN 115369237 A CN115369237 A CN 115369237A
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zinc
electrodeposition
manganese
acid leaching
leaching
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CN115369237B (en
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张梅
晋家强
谢富华
张化碧
杨丽菊
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Yunnan Chihong Resources Comprehensive Utilization Co ltd
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Yunnan Chihong Resources Comprehensive Utilization Co ltd
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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
    • C22B19/22—Obtaining zinc otherwise than by distilling with leaching with acids
    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • 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
    • 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
    • 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

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
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  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Electrolytic Production Of Metals (AREA)

Abstract

The invention relates to a method for balancing production and consumption of manganese ions in zinc smelting, belongs to the technical field of zinc hydrometallurgy, and comprises five steps of roasting, intermediate leaching, acid leaching, purifying and electrodeposition. The invention realizes the change control of the generation amount of manganese ions by controlling the content of insoluble sulfur in zinc roasted ore, adding excessive manganese powder in the middle leaching process and changing and controlling the pH value in acid leaching so as to meet the consumption of manganese ions in different periods of normal operation of electrodeposition, concentrated scraping of anode mud on an anode plate, large overhaul and re-production and the like. The method does not increase the yield of acid leaching residue and does not bring impurities, thereby saving the consumption of purified zinc powder and saving the production cost.

Description

Method for balancing production and consumption of manganese ions in zinc smelting
Technical Field
The invention belongs to the technical field of zinc hydrometallurgy, and particularly relates to production and consumption balance of manganese ions in zinc smelting.
Background
In zinc wet smelting, manganese powder is added during roasting ore leaching, ferrous iron in ore pulp is oxidized, ferric hydroxide is used for precipitation in the late stage of middle leaching, impurities such as arsenic, antimony, indium and the like are hydrolyzed and precipitated together with iron, manganese in the ferrous iron oxide in the manganese powder enters a middle supernatant (supernatant obtained by neutral leaching) in a manganese sulfate (manganese ion) form, and when the middle supernatant is purified and electrodeposited, the manganese ion in a solution is separated out on an anode plate in a manganese dioxide form to form a protective layer in the process of electrodeposition so as to delay the corrosion of the anode plate and play a role in stably controlling the lead content of a zinc sheet. When the content of manganese ions in the electrolyte is low, the corrosion of the anode plate is aggravated, the lead content of the zinc sheet is increased, and the quality of the product is reduced. It can be seen that manganese ions are essential beneficial elements in zinc hydrometallurgy, so that the maintenance of the manganese ion content in the system is very important.
The consumption of manganese ions in the process of electrodeposition is greatly changed, during normal production, the consumption of manganese ions is relatively low, the consumption of manganese ions is increased when an anode concentrates on a scraper (scrapes anode mud), the consumption of manganese ions is highest about 1 month after the large overhaul and the production recovery of an electrodeposition system, and the manganese ions need to be timely supplemented according to different production stages to maintain the balance of the manganese ions in the system.
In the conventional zinc leaching smelting process, the content of ferrous iron in leached ore pulp is limited, and the manganese ion amount generated by oxidizing ferrous iron is not enough to maintain the manganese ion balance in the system. Therefore, production enterprises need to separately arrange a leaching tank, leach manganese ions in the leaching tank, and then supply the leached manganese ions to the electro-hydraulic fluid. Particularly during anode concentration scraper or large overhaul and production recovery, a large amount of manganese ions need to be supplemented to maintain manganese ion balance. The manganese supplementing mode has high cost and increased labor cost.
In addition, the existing manganese replenishment mode brings a large amount of impurity ions, such as iron, cobalt, nickel and the like, in the process of replenishing the manganese ions, so that the yield of acid leaching slag is increased, the consumption of zinc powder is increased during purification, and the production cost is increased.
Disclosure of Invention
In order to overcome the problems in the prior art, the invention provides a method for balancing the production and consumption of zinc smelting manganese ions, which controls the content of insoluble sulfur in zinc roasting ores by controlling the roasting temperature and the excess air coefficient during roasting; manganese powder is added in the middle leaching process, and the generation amount of manganese ions is controlled by controlling the pH value of the acid leaching ore pulp in the acid leaching process, so that the production and consumption balance of the manganese ions is realized.
In order to realize the purpose, the invention is realized by the following technical scheme:
the method for balancing production and consumption of the manganese ions in zinc smelting comprises the following steps:
(1) Roasting: roasting and desulfurizing the zinc concentrate by using a fluidized bed furnace to produce zinc roasted ore; the content of insoluble sulfur in the zinc roasted ore is controlled by controlling the roasting temperature and the air excess coefficient.
(2) Intermediate leaching: and (3) adding acid leaching solution into the zinc electrodeposition waste liquid, adding manganese powder and zinc roasted ore, and controlling the end point pH value to precipitate the leached impurities of iron, arsenic, antimony and indium in the zinc roasted ore.
(3) Acid leaching: adding zinc electrodeposition waste liquid into the middle leaching bottom flow, carrying out acid leaching, controlling the pH value of acid leaching ore pulp according to the variable required by electrodeposition on manganese ions, filtering the acid leaching ore pulp to obtain acid leaching liquid and acid leaching slag, and returning the acid leaching liquid to the step (1) for neutral leaching.
(4) Purification: adding zinc powder into the supernatant to remove impurities such as copper, cadmium, cobalt, nickel and the like to obtain a new solution.
(5) Electrodeposition: and (3) adding the new solution into zinc electrodeposition circulating solution for electrodeposition to obtain zinc sheets, and returning electrodeposition waste liquid to the step (1) for leaching and the step (2) for acid leaching.
Further, in the step (1), the roasting temperature is controlled to be 890-950 ℃, and the air excess coefficient is 1.1-1.3; controlling the content of insoluble sulfur in the zinc roasted ore by 0.4-0.8% by weight.
Further, in the step (2), manganese powder is added in excess, and the excess coefficient is 1.2-1.4.
Further, in the step (3), the variable control range of the pH value of the acid leaching ore pulp is 2.0-3.0.
Further, the production amount of manganese ions in the step (2) and the step (3) and the consumption amount of manganese ions in the step (5) are kept in balance.
Furthermore, the consumption of the manganese ions in the step (5) is 4-8kg/t.
Further, the manganese ion content in the electrodeposition waste liquid in the step (4) is 3.0-3.5g/L.
Further, the acid leaching slag in the step (3) is sent to a pyrometallurgical furnace for treatment.
The invention has the beneficial effects that:
insoluble sulfur in zinc roasted ore is used as a reducing agent for manganese powder leaching, the insoluble sulfur in the roasted ore is matched with the control of the pH value of subsequent acid leaching by controlling the roasting condition, the generation amount of manganese ions is variably controlled by regulating the pH value of acid leaching in the acid leaching process, the demand of electrodeposition in different generation stages such as normal operation, concentrated anode mud scraping, and large-scale after-overhaul repeated production periods on the concentration of the manganese ions can be met, the production consumption balance of the manganese ions is realized, the yield of acid leaching slag is not increased, impurities are not brought in, the consumption of purified zinc powder is saved, and the production cost is saved.
The manganese ion regulation and control and the roasting process form a complete zinc electrodeposition process, the manganese ion generation amount is controlled in the existing acid leaching process, no production process is required to be additionally added, a manganese leaching tank is not required to be additionally built, and the generation cost and the labor consumption are reduced.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail below, and it is apparent that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. Other embodiments that can be obtained by persons skilled in the art without making any creative effort based on the embodiments of the present invention belong to the protection scope of the present invention.
The method for balancing production and consumption of manganese ions in zinc smelting comprises the following steps:
(1) Roasting: removing sulfur from zinc concentrate by fluidized bed roaster at 890-950 deg.C with air excess coefficient of 1.1-1.3 to obtain zinc roasted ore with insoluble sulfur content of 0.4-0.8 wt%. The desulfurized calcine is subjected to dry ball milling and is mixed with the calcine to prepare the zinc roasted ore containing insoluble sulfur. The excessive low insoluble sulfur in the zinc roasted ore can cause the manganese powder added in the subsequent acid leaching to be difficult to react, and the aim of manganese supplement can not be realized; excessive insoluble sulfur increases the amount of acid leaching residue, increases the cost of pyrogenic treatment of acid leaching residue, and when the insoluble sulfur is controlled to 0.4-0.8% by weight, the insoluble sulfur in the zinc roasted ore and manganese powder can react to generate manganese ions, and the zinc content of the acid leaching residue is kept stable.
(2) Intermediate leaching: and (2) adding the pickle liquor into the zinc electrodeposition waste liquor, and adding manganese powder and the zinc roasted ore in the step (1). In the early stage of the intermediate leaching, the manganese powder oxidizes ferrous iron in the ore pulp into ferric iron to generate manganese ions, and because the content of the ferrous iron in the zinc roasted ore is stable, the generation amount of the manganese ions in the intermediate leaching is relatively stable; in the later stage of middle leaching, the end-point pH value of the ore pulp is controlled to be 5.0-5.4, so that impurities such as leached iron, arsenic, antimony, indium and the like in the zinc roasted ore are precipitated, and a middle supernatant and a middle leaching underflow are produced.
(3) Acid leaching: adding zinc electrodeposition waste liquid into the middle leaching bottom flow for acid leaching. The leaching amount of manganese is controlled by controlling different pH values.
The generation amount of manganese ions is related to the pH value (acidity) of ore pulp and the surplus coefficient of manganese powder besides the content of insoluble sulfur in zinc roasted ore. When the content of insoluble sulfur in the zinc roasted ore is high, the acidity control of the acid leaching ore pulp is high, and the surplus coefficient of manganese powder is large, the generation amount of manganese ions is the largest, and otherwise, the generation amount is the smallest; and the insoluble sulfur content of the zinc roasted ore, the acidity control of the acid leaching ore pulp and the manganese powder surplus coefficient are in a positive correlation relationship, if the three are short of the positive correlation relationship, the generation amount of manganese ions is influenced, and the aim of adjusting the generation amount of the manganese ions cannot be fulfilled. The content of insoluble sulfur in the zinc roasted ore, the acidity of the acid leaching ore pulp and the surplus coefficient of manganese powder are controlled in a linkage manner, so that the generation amount of manganese ions is controlled.
Controlling the pH value of the ore pulp to be 2.0-3.0, controlling the surplus coefficient of manganese powder to be 1.2-1.4 percent, and adjusting the generation amount of manganese ions when the insoluble sulfur in the zinc roasted ore is 0.4-0.8 percent by weight so as to meet the requirements of zinc electrolyte liquid on the concentration of the manganese ions in different production stages.
The higher the acidity is, the more beneficial the generation of manganese ions is, but when the pH value of the acid leaching pulp is less than 2.0, the clarification and filtration of the acid leaching pulp are deteriorated, and when the pH value of the acid leaching pulp is more than 3.0, the manganese powder and the insoluble sulfur are difficult to react. Therefore, through experimental research, the pH value of the ore pulp is controlled and controlled to be 2.0-3.0.
The manganese powder excess coefficient = manganese powder actual input/manganese powder theoretical input. The theoretical input amount of the manganese powder is the amount of the manganese powder required by the electrohydrops theory (calculated by taking the manganese ion leached from the manganese powder).
(4) Purifying: adding zinc powder into the supernatant to remove impurities such as copper, cadmium, cobalt, nickel and the like to obtain a new solution. The amount of manganese ions in the solution does not increase or decrease during the purification process.
(5) Electrodeposition: and (3) adding the new solution into zinc electrodeposition circulating solution for electrodeposition to obtain zinc sheets, and returning electrodeposition waste liquid to middle leaching and acid leaching. The electrodeposition reaction formula is:
main reaction: zn 2+ +H 2 O+2e=Zn↓+2H + +1/2O 2 ↑ （1）
Side reactions at the anode: mn (Mn) 2+ +2H 2 O-2e=MnO 2 ↓+4H + （2）
When the reaction formula (2) occurs, manganese ions are consumed on the anode due to manganese dioxide precipitation, and through determination, the consumption of the manganese ions is about 4kg/t. zinc sheets when the electrodeposition is normally produced, the consumption of the manganese ions is 5.5kg/t. zinc sheets when the anode concentrates on the scraper, the large overhaul and the repeated production of the electrodeposition system are about 1 month, and the consumption of the manganese ions further increases to about 8kg/t. zinc sheets. Therefore, aiming at different manganese ion consumption, different temperatures and air excess coefficients need to be controlled during roasting, different manganese powder excess coefficients need to be controlled during intermediate leaching, and different acidity needs to be controlled during acid leaching so as to control different manganese ion generation amounts, thereby realizing the production and consumption balance of manganese ions. When the manganese ion content in the electrodeposition waste liquid is less than 3.0g/L, the manganese ion will be depleted gradually, when the manganese ion content in the electrodeposition waste liquid is more than 3.5g/L, the cell voltage will be increased to increase the direct current consumption, and in order to enable the manganese ion concentration to have an adjusting space, the manganese ion content in the electrodeposition waste liquid needs to be controlled to be 3.0-3.5g/L.
Example 1
A method for balancing the production and consumption of manganese ions in zinc smelting (during normal production of electrodeposition).
(1) Roasting: roasting and desulfurizing the zinc concentrate in a fluidized bed furnace, controlling the roasting temperature to 950 ℃ and the air excess coefficient to 1.3 percent, wherein the obtained zinc roasted ore contains 0.4 percent by weight of insoluble sulfur.
(2) Intermediate leaching: and (2) adding acid leaching solution into the zinc electrodeposition waste liquid, adding excessive manganese powder and the zinc roasted ore in the step (1), controlling the excessive coefficient of the manganese powder to be 1.2, and producing a middle supernatant and a middle leaching bottom flow by the end point pH value of 5.0-5.4.
(3) Acid leaching: adding zinc electrodeposition waste liquid into the middle leaching bottom flow, performing acid leaching, and controlling the pH value of acid leaching pulp to be 3.0.
(4) Purification: adding zinc powder into the supernatant to remove impurities such as copper, cadmium, cobalt, nickel and the like to obtain a new solution.
(5) Electrodeposition: and (3) adding the new solution into zinc electrodeposition circulating solution for electrodeposition to obtain zinc sheets, and returning electrodeposition waste liquid to the step (2) for leaching and the step (3) for acid leaching.
Before implementation, the electrodeposition waste liquid contains 3.1g/L of manganese ions, the average consumption of the manganese ions is 4.1kg/t. Zinc sheets in the normal production time, and the concentration change of the manganese ions in the electrodeposition liquid in the whole production process is 3.1-3.3g/L.
Example 2
Method for balancing production and consumption of manganese ions in zinc smelting (during anode mud concentrated scraping on anode plate)
(1) Roasting: roasting and desulfurizing the zinc concentrate in a fluidized bed roaster at the roasting temperature of 920 ℃ and the air excess coefficient of 1.2 percent, wherein the content of insoluble sulfur in the obtained zinc roasted ore is 0.6 percent by weight.
(2) Intermediate leaching: and (3) adding acid leaching solution into the zinc electrodeposition waste liquid, adding excessive manganese powder and the zinc roasted ore in the step (1), controlling the excessive coefficient of the manganese powder to be 1.3, and producing a middle supernatant and a middle leaching underflow at the end point pH value of 5.0-5.4.
(3) Acid leaching: adding zinc electrodeposition waste liquid into the middle leaching bottom flow, performing acid leaching, and controlling the pH value of acid leaching pulp to be 2.5.
(4) Purifying: adding zinc powder into the supernatant to remove impurities such as copper, cadmium, cobalt, nickel and the like to obtain a new solution.
(5) Electrodeposition: and (3) adding the new solution into zinc electrodeposition circulating solution for electrodeposition to obtain zinc sheets, and returning electrodeposition waste liquid to the step (2) for leaching and the step (3) for acid leaching.
Before implementation, the manganese ion content of the electrodeposition waste liquid is 3.2g/L, the average manganese ion consumption is 5.5kg/t during the anode concentration scraper, the manganese ion concentration in the electrodeposition liquid in the whole scraper process is changed to 3.1-3.5 g/L, the manganese ion concentration in the electrodeposition liquid is stably controlled, and the lead of the zinc sheet produced by electrodeposition is stable.
Example 3
Method for balancing production and consumption of manganese ions in zinc smelting (about 1 month after zinc electrodeposition large overhaul and recovery)
(1) Roasting: roasting and desulfurizing the zinc concentrate in a fluidized bed roaster at 890 ℃ under the condition that the air excess coefficient is 1.1, wherein the content of insoluble sulfur in the obtained zinc roasted ore is 0.8 percent by weight.
(2) Intermediate leaching: and (3) adding acid leaching solution into the zinc electrodeposition waste liquid, adding excessive manganese powder and the zinc roasted ore in the step (1), controlling the excessive coefficient of the manganese powder to be 1.4, and generating middle supernatant and middle leaching underflow at the end point pH value of 5.0-5.5.
(3) Acid leaching: adding zinc electrodeposition waste liquid into the middle leaching bottom flow, performing acid leaching, and controlling the pH value of acid leaching pulp to be 2.0.
(4) Purifying: adding zinc powder into the supernatant to remove impurities such as copper, cadmium, cobalt, nickel and the like to obtain a new solution.
(5) Electrodeposition: and (3) adding the new solution into zinc electrodeposition circulating solution for electrodeposition to obtain zinc sheets, and returning electrodeposition waste liquid to the step (2) for leaching and the step (3) for acid leaching.
Before implementation, the manganese ion content of the electrodeposition waste liquid is 3.2g/L, about 1 month after the zinc electrodeposition large overhaul and the production recovery, the average manganese ion consumption is 7.9kg/t. Zinc sheets, the manganese ion concentration in the electrodeposition liquid in the process is changed to 3.1-3.5 g/L, the manganese ion concentration in the electrodeposition liquid is stably controlled, and the lead content of the zinc sheets produced by electrodeposition is stable.
Finally, it is noted that the above-mentioned preferred embodiments illustrate rather than limit the invention, and that, although the invention has been described in detail with reference to the above-mentioned preferred embodiments, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the scope of the invention as defined by the appended claims.

Claims (7)

1. A method for balancing production and consumption of manganese ions in zinc smelting is characterized by comprising the following steps:
roasting: roasting and desulfurizing the zinc concentrate by using a fluidized bed furnace to produce zinc roasted ore; controlling the content of insoluble sulfur in the zinc roasted ore by controlling the roasting temperature and the air excess coefficient;
intermediate leaching: adding acid leaching solution into the zinc electrodeposition waste liquid, adding manganese powder and the zinc roasted ore in the step (1), controlling the end point pH value to be 5.0-5.4, precipitating iron, arsenic, antimony and indium impurities leached from the zinc roasted ore, and producing a middle supernatant and a middle leaching underflow;
acid leaching: adding zinc electrodeposition waste liquid into the middle leaching bottom flow, performing acid leaching, controlling the pH value of acid leaching pulp according to the variable required by electrodeposition on manganese ions, filtering the acid leaching pulp to obtain acid leaching liquid and acid leaching slag, and returning the acid leaching liquid to the step (2);
purification: adding zinc powder into the supernatant to remove impurities such as copper, cadmium, cobalt, nickel and the like to obtain a new solution;
electrodeposition: and (3) adding the new solution into zinc electrodeposition circulating solution for electrodeposition to obtain zinc sheets, and returning electrodeposition waste liquid to the step (2) for leaching and the step (3) for acid leaching.
2. The method according to claim 1, wherein in the step (1), the calcination temperature is controlled to be 890 to 950 ℃ and the air excess coefficient is 1.1 to 1.3; controlling the content of insoluble sulfur in the zinc roasted ore by 0.4-0.8% by weight.
3. The method according to claim 1, wherein in the step (2), the manganese powder is added in an excess amount with an excess factor of 1.2 to 1.4.
4. The method of claim 1, wherein in the step (3), the variable control range of the pH value of the acid leaching pulp is 2.0-3.0.
5. The method according to claim 1, 3 or 4, wherein the amounts of manganese ions generated in step (2) and step (3) and the amounts of manganese ions consumed in step (5) are balanced.
6. The method according to claim 1 or 5, wherein the consumption of manganese ions in step (5) is 4-8kg/t.
7. The method according to claim 1, wherein the manganese ion content in the electrodeposition waste liquid in the step (5) is 3.0 to 3.5g/L.
CN202211147792.6A 2022-09-21 2022-09-21 Method for balancing production consumption of zinc smelting manganese ions Active CN115369237B (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4071421A (en) * 1976-08-11 1978-01-31 Sherritt Gordon Mines Limited Process for the recovery of zinc
US4439288A (en) * 1983-07-11 1984-03-27 Exxon Research & Engineering Company Process for reducing Zn consumption in zinc electrolyte purification
CN104233373A (en) * 2013-06-13 2014-12-24 无锡市森信精密机械厂 Zinc smelting technology for low-zinc high-iron roasting ore by wet method
CN110358932A (en) * 2019-08-19 2019-10-22 新疆紫金有色金属有限公司 A kind of high silicate zinc concentrate hydrometallurgical processes
CN111519040A (en) * 2020-05-12 2020-08-11 云南金鼎锌业有限公司 Zinc oxide concentrate leaching equipment and leaching mode thereof
CN114517258A (en) * 2022-01-11 2022-05-20 云南云铜锌业股份有限公司 Two-stage zinc hydrometallurgy leaching method for improving copper recovery rate

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4071421A (en) * 1976-08-11 1978-01-31 Sherritt Gordon Mines Limited Process for the recovery of zinc
US4439288A (en) * 1983-07-11 1984-03-27 Exxon Research & Engineering Company Process for reducing Zn consumption in zinc electrolyte purification
CN104233373A (en) * 2013-06-13 2014-12-24 无锡市森信精密机械厂 Zinc smelting technology for low-zinc high-iron roasting ore by wet method
CN110358932A (en) * 2019-08-19 2019-10-22 新疆紫金有色金属有限公司 A kind of high silicate zinc concentrate hydrometallurgical processes
CN111519040A (en) * 2020-05-12 2020-08-11 云南金鼎锌业有限公司 Zinc oxide concentrate leaching equipment and leaching mode thereof
CN114517258A (en) * 2022-01-11 2022-05-20 云南云铜锌业股份有限公司 Two-stage zinc hydrometallurgy leaching method for improving copper recovery rate

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