CN103215435A - Method for comprehensively recycling zinc, copper, lead, gold, silver and sulfur from floatation silver concentrate - Google Patents
Method for comprehensively recycling zinc, copper, lead, gold, silver and sulfur from floatation silver concentrate Download PDFInfo
- Publication number
- CN103215435A CN103215435A CN2013101519181A CN201310151918A CN103215435A CN 103215435 A CN103215435 A CN 103215435A CN 2013101519181 A CN2013101519181 A CN 2013101519181A CN 201310151918 A CN201310151918 A CN 201310151918A CN 103215435 A CN103215435 A CN 103215435A
- Authority
- CN
- China
- Prior art keywords
- zinc
- flotation
- silver
- copper
- lead
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to a method for comprehensively recycling zinc, copper, lead, gold, silver and sulfur from floatation silver concentrate. The method comprises the following steps of: firstly carrying out size mixing on flotation silver concentrate, mixing the flotation silver concentrate and zinc electrolytic waste liquid for size mixing in the size mixing process, wherein the sulfuric acid concentration of the zinc electrolytic waste liquid is 180-250g/L, and the proportion of the flotation silver concentrate to the zinc electrolytic waste liquid is 1: (6-10); then adding the flotation silver concentrate subjected to size mixing to a high-pressure reactor for carrying out high-temperature high-pressure dispersion; after the high-temperature high-pressure dispersion is ended, carrying out oxygen pressure acid leaching on the flotation silver concentrate, then carrying out filtering separation on the flotation silver concentrate by a filter press, and filtering and separating to obtain leachate and leaching residues, wherein the leachate enters an electrolytic zinc system so as to recycle copper, zinc, lead, gold, silver, while elemental sulfur is enriched in the form of leaching residues, and finally returning to a bottom blowing furnace of a lead system for recycling.
Description
Technical field
The present invention relates to the Metal smelting technical field, particularly a kind of method that from the flotation silver preparation concentrate, comprehensively reclaims zinc, copper, lead, gold and silver, sulphur.
Background technology
Conventional Zn system flotation silver preparation concentrate is directly to return lead system comprehensively to reclaim zinc, copper, lead, gold and silver, sulphur mostly, the flotation silver preparation concentrate directly returns lead system and comprehensively reclaims zinc, copper, lead, gold and silver, sulphur, shortcomings such as flow process complexity, cost height, the rate of recovery be low are arranged, had a strong impact on comprehensive recovery benefit.
At present, oxygen presses the acidleach technology to obtain widespread use in the zinc hydrometallurgy field, as utilize oxygen to press the acidleach technology that lead and zinc bulk concentrate oxygenation pressurization back sulfuric acid is leached, and will entering the zinc electrolytic system after the leach liquor removal of impurities again, leached mud has valence component through effectively handling to reclaim.
And the flotation silver preparation concentrate is different from lead and zinc bulk concentrate, and at first the flotation silver preparation concentrate is the product of conventional zinc hydrometallurgy acid leaching residue through flotation, and the flotation silver preparation concentrate has argentiferous height and zinc, copper, plumbous low characteristics.Next is that the flotation silver preparation concentrate has experienced 800～900 ℃ of fluidized bed roastings, normal pressure acidleach, ore dressing flotation three process, so silver, copper, lead, zinc thing phase composition complexity in the flotation silver preparation concentrate, silver in the flotation silver preparation concentrate mainly is silver sulfide and simple substance silver, zinc mainly is zinc in zinc sulphide and the franklinite, sulphur is mainly sulphur and elementary sulfur in the sulfide, and iron is mainly iron and the ironic hydroxide in the franklinite.Contain flocculation agent (polyacrylamide very strong) and multiple beneficiation reagent (as multiple organism such as xanthate, whipping agents) besides in the flotation silver preparation concentrate as coherency.Therefore, the flotation silver preparation concentrate is a kind of material of more complicated, the raw material that its employing oxygen different from the past presses acid leaching process to handle.
Summary of the invention
The objective of the invention is to overcome the above-mentioned deficiency of prior art and provide a kind of from the flotation silver preparation concentrate the comprehensive method that reclaims zinc, copper, lead, gold and silver, sulphur.
Technical scheme of the present invention is: a kind of method that comprehensively reclaims zinc, copper, lead, gold and silver, sulphur from the flotation silver preparation concentrate, at first the flotation silver preparation concentrate is sized mixing and the High Temperature High Pressure dispersion, make the flotation silver preparation concentrate carry out oxygen again after strengthening dispersion under the condition of High Temperature High Pressure and press acidleach and filtering separation, filtering separation obtains leach liquor and leached mud.Leach liquor enters electric Zn system and reclaims copper and zinc, and lead, gold and silver and element sulphur then obtain enrichment with the form of leached mud, finally turn back to the lead system bottom convertor and reclaim.
Its concrete steps are as follows:
A, the flotation silver preparation concentrate is sized mixing, adopt the flotation silver preparation concentrate to mix with the zinc electrolysis waste solution in the process of sizing mixing and size mixing, the sulfuric acid concentration of zinc electrolysis waste solution is 180～250g/L, and the ratio of flotation silver preparation concentrate and zinc electrolysis waste solution is 1:6～10;
B, High Temperature High Pressure are disperseed, flotation silver preparation concentrate ore pulp after sizing mixing joined carry out High Temperature High Pressure in the autoclave and disperse, temperature when High Temperature High Pressure is disperseed in the autoclave is 140～180 ℃, feed pressurized air simultaneously, keep pressure 0.7～1.5MPa, 0.5～3 hour time, make flotation silver preparation concentrate ore pulp under the condition of High Temperature High Pressure, strengthen dispersion;
C, oxygen are pressed acidleach, in autoclave, the flotation silver preparation concentrate ore pulp after disperseing through High Temperature High Pressure is carried out oxygen and press acidleach, oxygen presses acidleach to feed compressed oxygen, it is 1.0～1.5 MPa that oxygen is pressed, time is 3.0～4.5 hours, utilize oxygen earlier oxidation of divalent iron ion to be become ferric ion, under high temperature, highly compressed condition, ferric ion and zinc sulphide are reacted then.In the acidleach process copper is converted into copper sulfate, zinc is converted into zinc sulfate, and iron is converted into ferric sulfate and ferrous sulfate, and wherein the copper more than 90%, the dissolving of 85% zinc enter leach liquor, and oxygen presses the main chemical reactions of acidleach as follows:
ZnS+H
2SO
4+1/2O
2=ZnSO
4+H
2O+S
0
2Fe(OH)
3+3H
2SO
4=Fe
2(SO
4)
3+6H
2O
ZnS+Fe
2(SO
4)
3?=ZnSO
4+2FeSO
4+S
0
2FeSO
4+H
2SO
4+1/2O
2=Fe
2(SO
4)
3+H
2O
CuO+?H
2SO
4=CuSO
4+H
2O
D, filtering separation, by pressure filter the flotation silver preparation concentrate through the acidleach of peroxide pressure is carried out filtering separation, obtain leach liquor and leached mud, leach liquor enters electric Zn system and reclaims copper and zinc, lead, gold and silver and elemental sulfur then obtain enrichment with the form of leached mud, finally turn back to the lead system bottom convertor and reclaim.
Above-mentioned flotation silver preparation concentrate is the product of conventional zinc hydrometallurgy acid leaching residue through flotation, its composition is: Pb 2 ~ 6%, Cu 1 ~ 6%, Fe 10 ~ 30%, Zn 20 ~ 40%, S 15 ~ 30%, Au 10 ~ 20g/t, Ag 4000 ~ 10000g/t, wherein, Pb, Cu, Fe, Zn, S composition are weight percentage, and Au, Ag composition are weight ratio.
The present invention compared with prior art has following characteristics:
The present invention at first flotation silver preparation concentrate ore pulp is sized mixing and High Temperature High Pressure is disperseed, and then carry out oxygen and press acidleach and filtering separation, the copper more than 90%, the dissolving of 85% zinc enter leach liquor, and lead, gold and silver, sulphur are enriched in the leached mud, leach liquor enters Zn system, and leached mud enters lead system.Realized the zinc in the flotation silver preparation concentrate, copper, lead, gold and silver, sulphur are carried out the recovery of the other class of branch name, effectively reduced the recovery production cost, improved the comprehensive economic and technical norms that reclaim of flotation silver preparation concentrate.
Below in conjunction with the drawings and specific embodiments the present invention is further described.
Description of drawings
Accompanying drawing 1 is a process flow sheet of the present invention.
Embodiment
Embodiment one: a kind of method that comprehensively reclaims zinc, copper, lead, gold and silver, sulphur from the flotation silver preparation concentrate, described flotation silver preparation concentrate is the product of conventional zinc hydrometallurgy acid leaching residue through flotation, its composition is: Pb 2 ~ 6%, Cu 1 ~ 6%, Fe 10 ~ 30%, Zn 20 ~ 40%, S 15 ~ 30%, Au 10 ~ 20g/t, Ag 4000 ~ 10000g/t, wherein, Pb, Cu, Fe, Zn, S composition are weight percentage, and Au, Ag composition are weight ratio.
In the above-mentioned Ag composition: the simple substance silver content is that 1738～4347 g/t, silver sulfide content are that 1992～4981g/t, silver suboxide content are that silver content is that silver content is that silver content is 28～70 g/t in 1～25 g/t, the silicate in 239～597 g/t, the sulfate radical in 1～25g/t, the sulfide; In the above-mentioned Zn composition: zinc sulfate content is 1.21 ~ 2.42%, zinc oxide content is 1.58～3.16%, zinc sulphide content is 10.13～20.27%, zinc content is 7.07～14.14% in the franklinite; In the above-mentioned S composition: sulphate content is 2.19～4.37%, sulfide content is 6.59～13.18%, element sulfur content is 6.22～12.44 %.
Its concrete steps are as follows:
A, the flotation silver preparation concentrate is sized mixing, adopt the flotation silver preparation concentrate to mix with the zinc electrolysis waste solution in the process of sizing mixing and size mixing, the sulfuric acid concentration of zinc electrolysis waste solution is 180～250g/L, and the ratio of flotation silver preparation concentrate and zinc electrolysis waste solution is 1:6～10;
B, High Temperature High Pressure are disperseed, to join through the flotation silver preparation concentrate ore pulp after sizing mixing and carry out the High Temperature High Pressure dispersion in the autoclave, temperature when High Temperature High Pressure is disperseed in the autoclave is 140～180 ℃, feed pressurized air simultaneously, keep pressure 0.7～1.5MPa, 0.5～3 hour time, make flotation silver preparation concentrate ore pulp under the condition of High Temperature High Pressure, strengthen dispersion;
C, oxygen are pressed acidleach, in autoclave, the flotation silver preparation concentrate ore pulp after disperseing through High Temperature High Pressure is carried out oxygen and press acidleach, oxygen presses acidleach to add oxygen, it is 1.0～1.5 MPa that oxygen is pressed, time is 3.0～4.5 hours, utilize oxygen earlier oxidation of divalent iron ion to be become ferric ion, under high temperature, highly compressed condition, ferric ion and zinc sulphide are reacted then.In the acidleach process copper is converted into copper sulfate, zinc is converted into zinc sulfate, and iron is converted into ferric sulfate and ferrous sulfate, and wherein the copper more than 90%, the dissolving of 85% zinc enter leach liquor, and oxygen presses the main chemical reactions of acidleach as follows:
ZnS+H
2SO
4+1/2O
2=ZnSO
4+H
2O+S
0
2Fe(OH)
3+3H
2SO
4=Fe
2(SO
4)
3+6H
2O
ZnS+Fe
2(SO
4)
3?=ZnSO
4+2FeSO
4+S
0
2FeSO
4+H
2SO
4+1/2O
2=Fe
2(SO
4)
3+H
2O
CuO+?H
2SO
4=CuSO
4+H
2O
D, filtering separation, by pressure filter the flotation silver preparation concentrate through the acidleach of peroxide pressure is carried out filtering separation, obtain leach liquor and leached mud, leach liquor enters electric Zn system and reclaims copper and zinc, lead, gold and silver and elemental sulfur then obtain enrichment with the form of leached mud, finally turn back to the lead system bottom convertor and reclaim.
In the leached mud: Zn content is 7.58%, Cu content is 0.32%, Fe content is 10.78%, Pb content is 5.33%, S content is 38.02%, Au content is that 26.86 g/t, Ag content are 12021 g/t; Slag meter leaching yield: Zn is 87.06%, Cu is 97.88%, Fe is 87.57%; Gu slag rate: Pb is 99.47%, S is 100.37%, Au is 100.51%, Ag is 99.94%.
Claims (2)
1. comprehensive method that reclaims lead, zinc, gold and silver, copper, sulphur from the flotation silver preparation concentrate, it is characterized in that: at first the flotation silver preparation concentrate is sized mixing and the High Temperature High Pressure dispersion, make the flotation silver preparation concentrate after strengthening dispersion under the condition of High Temperature High Pressure, carry out oxygen again and press acidleach and filtering separation, obtain leach liquor and leached mud after the filtering separation, leach liquor enters electric Zn system and reclaims copper and zinc, lead, gold and silver and elemental sulfur then obtain enrichment with the form of leached mud, finally turn back to the lead system bottom convertor and reclaim;
Its concrete steps are as follows:
A, the flotation silver preparation concentrate is sized mixing, adopt the flotation silver preparation concentrate to mix with the zinc electrolysis waste solution in the process of sizing mixing and size mixing, the sulfuric acid concentration of zinc electrolysis waste solution is 180～250g/L, and the ratio of flotation silver preparation concentrate and zinc electrolysis waste solution is 1:6～10;
B, High Temperature High Pressure are disperseed, to join through the flotation silver preparation concentrate ore pulp after sizing mixing and carry out the High Temperature High Pressure dispersion in the autoclave, temperature when High Temperature High Pressure is disperseed in the autoclave is 140～180 ℃, feed pressurized air simultaneously, keep pressure 0.7～1.5MPa, 0.5～3 hour time, make flotation silver preparation concentrate ore pulp under the condition of High Temperature High Pressure, strengthen dispersion;
C, oxygen is pressed acidleach, in autoclave, the flotation silver preparation concentrate ore pulp after disperseing through High Temperature High Pressure is carried out oxygen and press acidleach, oxygen presses acidleach to add oxygen, it is 1.0～1.5 MPa that oxygen is pressed, time is 3.0～4.5 hours, utilize oxygen earlier oxidation of divalent iron ion to be become ferric ion, then at high temperature, ferric ion and zinc sulphide are reacted, in the acidleach process, copper is converted into copper sulfate, zinc is converted into zinc sulfate, iron is converted into ferric sulfate and ferrous sulfate, wherein the copper more than 90%, 85% zinc dissolving enters leach liquor, and oxygen presses the main chemical reactions of acidleach as follows:
ZnS+H
2SO
4+1/2O
2=ZnSO
4+H
2O+S
0
2Fe(OH)
3+3H
2SO
4=Fe
2(SO
4)
3+6H
2O
ZnS+Fe
2(SO
4)
3?=ZnSO
4+2FeSO
4+S
0
2FeSO
4+H
2SO
4+1/2O
2=Fe
2(SO
4)
3+H
2O
CuO+?H
2SO
4=CuSO
4+H
2O
D, filtering separation, by pressure filter the flotation silver preparation concentrate through the acidleach of peroxide pressure is carried out filtering separation, obtain leach liquor and acid leaching residue, leach liquor enters electric Zn system and reclaims copper and zinc, lead, gold and silver and elemental sulfur then obtain enrichment with the form of acid leaching residue, finally turn back to the lead system bottom convertor and reclaim.
2. a kind of method that from the flotation silver preparation concentrate, comprehensively reclaims lead, zinc, gold and silver, copper, sulphur according to claim 1, it is characterized in that: described flotation silver preparation concentrate is the product of conventional zinc hydrometallurgy acid leaching residue through flotation, its composition is: Pb 2 ~ 6%, Cu 1 ~ 6%, Fe 10 ~ 30%, Zn 20 ~ 40%, S 15 ~ 30%, Au 10 ~ 20g/t, Ag 4000 ~ 10000g/t, wherein, Pb, Cu, Fe, Zn, S composition are weight percentage, and Au, Ag composition are weight ratio.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013101519181A CN103215435A (en) | 2013-04-27 | 2013-04-27 | Method for comprehensively recycling zinc, copper, lead, gold, silver and sulfur from floatation silver concentrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013101519181A CN103215435A (en) | 2013-04-27 | 2013-04-27 | Method for comprehensively recycling zinc, copper, lead, gold, silver and sulfur from floatation silver concentrate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103215435A true CN103215435A (en) | 2013-07-24 |
Family
ID=48813580
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013101519181A Pending CN103215435A (en) | 2013-04-27 | 2013-04-27 | Method for comprehensively recycling zinc, copper, lead, gold, silver and sulfur from floatation silver concentrate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103215435A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103484670A (en) * | 2013-10-12 | 2014-01-01 | 河南豫光锌业有限公司 | Process for comprehensively recovering valuable metal from floatation silver concentrates of zinc hydrometallurgy system |
| CN103993170A (en) * | 2014-06-12 | 2014-08-20 | 湖南水口山有色金属集团有限公司 | Method for recycling metals from copper-lead-zinc-arsenic-antimony bulk concentrate |
| CN104032145A (en) * | 2014-06-23 | 2014-09-10 | 贵州顶效开发区宏达金属综合回收有限公司 | Method for extracting and separating Ag and Cu from flotation silver concentrate |
| CN104722410A (en) * | 2015-02-16 | 2015-06-24 | 巴彦淖尔紫金有色金属有限公司 | Method for extracting and separating valuable metal from hot-acid leaching residues produced by wet-process zinc smelting |
| CN104841564A (en) * | 2015-05-15 | 2015-08-19 | 西北矿冶研究院 | Lead-silver residue flotation combined collecting agent and application process thereof |
| CN107916337A (en) * | 2017-11-27 | 2018-04-17 | 中国恩菲工程技术有限公司 | The processing system of silver preparation concentrate |
| CN109750173A (en) * | 2017-11-07 | 2019-05-14 | 呼伦贝尔驰宏矿业有限公司 | A kind of high-iron sphalerite zinc metallurgy and the system and technique for handling associated metal altogether |
| CN112410555A (en) * | 2020-11-10 | 2021-02-26 | 株洲冶炼集团股份有限公司 | Comprehensive recovery method for flotation silver concentrate from zinc hydrometallurgy acidic leaching residue |
| CN113403483A (en) * | 2021-05-26 | 2021-09-17 | 来宾华锡冶炼有限公司 | Method for extracting silver from high-iron, high-tin and high-indium flotation silver concentrate |
| CN114350966A (en) * | 2022-01-17 | 2022-04-15 | 株洲冶炼集团股份有限公司 | Method for comprehensively recycling zinc anode mud by flotation silver concentrate matching treatment |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101643857A (en) * | 2009-08-25 | 2010-02-10 | 西部矿业股份有限公司 | Comprehensive recovery method of complex polymetal sulphide ore containing copper, lead and zinc |
| CN101972703A (en) * | 2010-10-27 | 2011-02-16 | 株洲市湘麒科技开发有限公司 | Beneficiation method for recovering zinc, lead and silver from zinc leaching residue |
-
2013
- 2013-04-27 CN CN2013101519181A patent/CN103215435A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101643857A (en) * | 2009-08-25 | 2010-02-10 | 西部矿业股份有限公司 | Comprehensive recovery method of complex polymetal sulphide ore containing copper, lead and zinc |
| CN101972703A (en) * | 2010-10-27 | 2011-02-16 | 株洲市湘麒科技开发有限公司 | Beneficiation method for recovering zinc, lead and silver from zinc leaching residue |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103484670A (en) * | 2013-10-12 | 2014-01-01 | 河南豫光锌业有限公司 | Process for comprehensively recovering valuable metal from floatation silver concentrates of zinc hydrometallurgy system |
| CN103993170A (en) * | 2014-06-12 | 2014-08-20 | 湖南水口山有色金属集团有限公司 | Method for recycling metals from copper-lead-zinc-arsenic-antimony bulk concentrate |
| CN104032145A (en) * | 2014-06-23 | 2014-09-10 | 贵州顶效开发区宏达金属综合回收有限公司 | Method for extracting and separating Ag and Cu from flotation silver concentrate |
| CN104032145B (en) * | 2014-06-23 | 2015-07-29 | 贵州顶效开发区宏达金属综合回收有限公司 | The method of a kind of extraction and isolation Ag, Cu from flotation of silver concentrate |
| CN104722410A (en) * | 2015-02-16 | 2015-06-24 | 巴彦淖尔紫金有色金属有限公司 | Method for extracting and separating valuable metal from hot-acid leaching residues produced by wet-process zinc smelting |
| CN104722410B (en) * | 2015-02-16 | 2017-09-19 | 巴彦淖尔紫金有色金属有限公司 | The method that separating valuable metals are extracted from the high acid leach residue of wet method zinc abstraction output |
| CN104841564A (en) * | 2015-05-15 | 2015-08-19 | 西北矿冶研究院 | Lead-silver residue flotation combined collecting agent and application process thereof |
| CN109750173A (en) * | 2017-11-07 | 2019-05-14 | 呼伦贝尔驰宏矿业有限公司 | A kind of high-iron sphalerite zinc metallurgy and the system and technique for handling associated metal altogether |
| CN107916337A (en) * | 2017-11-27 | 2018-04-17 | 中国恩菲工程技术有限公司 | The processing system of silver preparation concentrate |
| CN112410555A (en) * | 2020-11-10 | 2021-02-26 | 株洲冶炼集团股份有限公司 | Comprehensive recovery method for flotation silver concentrate from zinc hydrometallurgy acidic leaching residue |
| CN113403483A (en) * | 2021-05-26 | 2021-09-17 | 来宾华锡冶炼有限公司 | Method for extracting silver from high-iron, high-tin and high-indium flotation silver concentrate |
| CN114350966A (en) * | 2022-01-17 | 2022-04-15 | 株洲冶炼集团股份有限公司 | Method for comprehensively recycling zinc anode mud by flotation silver concentrate matching treatment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103215435A (en) | Method for comprehensively recycling zinc, copper, lead, gold, silver and sulfur from floatation silver concentrate | |
| CN103526024B (en) | Novel clean environment-friendly comprehensive recovery process for high-indium high-iron zinc concentrate | |
| CN100404708C (en) | Two-section roasting production process for recovering Au, Cu, Ag, As and S from As and C containing aurin ore | |
| CN102994747B (en) | Technology for recovering metallic copper from high-lead copper matte | |
| CA2160488C (en) | Recovery of metals from sulphidic material | |
| CN102586600B (en) | Process for recycling valuable metal from lead copper matte | |
| CN102191391B (en) | Method for extracting germanium from high-impurity low-grade complex zinc oxide powder | |
| CN105039713A (en) | Method for leaching solid arsenic out of arsenic sulfide slag through one step and enriching valuable metal | |
| CN102051478B (en) | Wet process for treating lead copper matte | |
| CN102230083B (en) | Method for separating copper from lead copper matte | |
| CN101225476A (en) | Process for reclaiming copper from lead copper matte | |
| CN109971953A (en) | A method of enhanced oxidation extracts valuable metal from the sulfide mineral containing non-ferrous metal | |
| CN105177307B (en) | Method for recycling copper-nickel-cobalt from low grade nickel matte through abrasive flotation separation | |
| CN104017991A (en) | Process for efficiently and selectively separating copper in lead copper matte | |
| CN101245407B (en) | Selecting-smelting method for processing complex hard-washing low ore grade pulmbous sulfide zincium mine | |
| CN110846496B (en) | Sulfating roasting smelting method of sulfur-containing copper-cobalt concentrate | |
| CN100385022C (en) | Leach extraction method | |
| CN110777264A (en) | Method suitable for independent smelting of various complex gold concentrates | |
| CN103805789B (en) | A kind of method of comprehensively recovering valuable metal of copper nickel slag | |
| CN103484694A (en) | Method for extracting bismuth from copper-bismuth concentrate | |
| CN113846214B (en) | Method for treating zinc-containing material in zinc hydrometallurgy production | |
| CN1204277C (en) | Method for extracting copper from copper-containing sulfide minerals | |
| CN114908257A (en) | Method for producing high-quality nickel sulfate solution | |
| CN104004907A (en) | Method for separating copper from lead matte and comprehensively utilizing lead matte | |
| CN107971123B (en) | Dressing and smelting method of iron coated mixed copper ore |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20130724 |