CN1027977C - Wet processing method for high-arsenic lead anode mud - Google Patents
Wet processing method for high-arsenic lead anode mud Download PDFInfo
- Publication number
- CN1027977C CN1027977C CN92104421A CN92104421A CN1027977C CN 1027977 C CN1027977 C CN 1027977C CN 92104421 A CN92104421 A CN 92104421A CN 92104421 A CN92104421 A CN 92104421A CN 1027977 C CN1027977 C CN 1027977C
- Authority
- CN
- China
- Prior art keywords
- antimony
- arsenic
- silver
- gold
- copper
- 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.)
- Expired - Fee Related
Links
- 229910052785 arsenic Inorganic materials 0.000 title claims abstract description 31
- 238000003672 processing method Methods 0.000 title description 2
- 238000000034 method Methods 0.000 claims abstract description 47
- 239000010949 copper Substances 0.000 claims abstract description 34
- 229910052787 antimony Inorganic materials 0.000 claims abstract description 32
- 229910052802 copper Inorganic materials 0.000 claims abstract description 31
- 239000010931 gold Substances 0.000 claims abstract description 30
- 229910052709 silver Inorganic materials 0.000 claims abstract description 30
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 29
- 229910052737 gold Inorganic materials 0.000 claims abstract description 28
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910052797 bismuth Inorganic materials 0.000 claims abstract description 26
- 239000004332 silver Substances 0.000 claims abstract description 26
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 claims abstract description 25
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims abstract description 25
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 claims abstract description 23
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 21
- 239000012141 concentrate Substances 0.000 claims abstract description 18
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910052714 tellurium Inorganic materials 0.000 claims abstract description 16
- PORWMNRCUJJQNO-UHFFFAOYSA-N tellurium atom Chemical compound [Te] PORWMNRCUJJQNO-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 8
- 238000006722 reduction reaction Methods 0.000 claims abstract description 8
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000000460 chlorine Substances 0.000 claims abstract description 7
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 7
- 230000003647 oxidation Effects 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 230000007062 hydrolysis Effects 0.000 claims abstract description 4
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 4
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract description 3
- 239000000463 material Substances 0.000 claims abstract 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 6
- 239000006256 anode slurry Substances 0.000 claims description 6
- VUEDNLCYHKSELL-UHFFFAOYSA-N arsonium Chemical compound [AsH4+] VUEDNLCYHKSELL-UHFFFAOYSA-N 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 6
- 230000001698 pyrogenic effect Effects 0.000 claims description 6
- 238000000975 co-precipitation Methods 0.000 claims description 5
- 238000002386 leaching Methods 0.000 claims description 5
- 239000002244 precipitate Substances 0.000 claims description 4
- 238000001556 precipitation Methods 0.000 claims description 4
- 239000000047 product Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 230000033116 oxidation-reduction process Effects 0.000 claims description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 claims 1
- 235000011941 Tilia x europaea Nutrition 0.000 claims 1
- 239000004571 lime Substances 0.000 claims 1
- 239000008267 milk Substances 0.000 claims 1
- 210000004080 milk Anatomy 0.000 claims 1
- 235000013336 milk Nutrition 0.000 claims 1
- 238000006386 neutralization reaction Methods 0.000 claims 1
- 238000010129 solution processing Methods 0.000 claims 1
- 239000012452 mother liquor Substances 0.000 abstract description 11
- 238000011084 recovery Methods 0.000 abstract description 11
- 238000004821 distillation Methods 0.000 abstract description 6
- 238000005660 chlorination reaction Methods 0.000 abstract description 4
- 238000005868 electrolysis reaction Methods 0.000 abstract description 2
- 230000003472 neutralizing effect Effects 0.000 abstract 2
- 230000001376 precipitating effect Effects 0.000 abstract 2
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 20
- 239000010970 precious metal Substances 0.000 description 7
- 229910052745 lead Inorganic materials 0.000 description 5
- 239000010944 silver (metal) Substances 0.000 description 4
- 239000003500 flue dust Substances 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 101100493820 Caenorhabditis elegans best-1 gene Proteins 0.000 description 1
- 101100494265 Caenorhabditis elegans best-15 gene Proteins 0.000 description 1
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- OEYOHULQRFXULB-UHFFFAOYSA-N arsenic trichloride Chemical group Cl[As](Cl)Cl OEYOHULQRFXULB-UHFFFAOYSA-N 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000010946 fine silver Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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
A wet treatment method of high-arsenic lead anode mud. The method is to put the material in hydrochloric acid medium and introduce chlorine to control the potential chlorination. The chlorination residue can be treated by sodium hydroxide solution and then is subjected to ignition method-electrolysis to obtain pure silver and gold; or extracting silver by wet method or fire method after extracting gold by wet method. Introducing SO into chlorination liquid2Precipitating tellurium concentrate by reduction or catalytic reduction; recovering arsenic by a distillation method; recovering antimony by a distillation raffinate hydrolysis method; neutralizing and precipitating the antimony hydrolyzed mother liquor to obtain bismuth concentrate; and (4) neutralizing and precipitating the bismuth-precipitating mother liquor after oxidation to obtain copper concentrate. And (3) recovery rate: 99% of gold and silver, 90% to 96% of antimony and bismuth and 90% to 98% of copper.
Description
Treatment method of high arsonium lead anode mud wet process the invention relates to precious metals metallurgy.
The present invention is the improvement invention of Chinese patent application application number 89103853.1 patent applications.Plumbous positive mud is one of main raw material that extracts silver and gold, and traditional pyrogenic processing method is: lead anode gets precious metals containing lead through retailoring, and the precious metals containing lead oxidation refining gets slightly silver, and thick silver-colored electrolysis gets product silver.The shortcoming of pyrogenic process is silver-colored direct yield lower (85～90%), and part silver is dispersed in flue dust and the slag, and the valency that has in the slag does not have the plain comprehensive difficulty that reclaims, and the As in the flue dust, Sb still do not have desirable separation method, easily cause environmental pollution." extracting precious metal from the anode sludge " (patent No. CN85106670 of people such as the bear Zong Guo of Kunming Institute of Precious Metals invention with the CONTROLLED POTENTIAL method, applying date 85.8.31), propose with the method for CONTROLLED POTENTIAL method from lead, antimony, nickel anode extraction precious metal, more effective to the enrichment of precious metals metallurgy process, separate precious metal; But this method leaching condition is stronger to equipment corrosion, to the extraction of silver not deeply, the comprehensive recovery of copper, antimony, bismuth, arsenic is not related to." a kind of method of lead anode slurry wet processing " (application number 89103853 of people such as the Hu Xuming of Kunming Institute of Precious Metals invention, applying date 89.6.3) a lead anode slurry wet processing general flow has been proposed, silver-colored, golden direct yield height (Ag96～98%, Au～98%), antimony, bismuth, copper also can comprehensively reclaim, but further separating of arsenic and antimony, bismuth, copper is also undesirable, particularly contains the high lead anode slurry of arsenic.
The objective of the invention is on " a kind of method of lead anode slurry wet processing " basis of people such as Hu Xuming invention, wet processing process to anode mud with high As and Pb (arsenic content 10～40%) further improves, solve the difficult problem of separating of arsenic and antimony in the leach liquor, bismuth, copper, propose both to have made all comprehensive recovery of arsenic and antimony, bismuth, copper, it is minimum to take into account the gold and silver loss again, the technical qualification that the rate of recovery is high.
Method provided by the present invention, be that said anode mud with high As and Pb is placed 3～5N hydrochloric acid medium, best 4NHCl medium, solid: liquid=1: 4～8, under best 1: 4～6 conditions, 10～50 ℃ of temperature, best 15～20 ℃, the oxidation reduction potential control that feeding chlorine makes system is at 360～450mv, and best 380～400mv carries out selectivity and leaches, the enrichment of gained leach liquor arsenic, antimony, bismuth, copper, tellurium, gold and silver have small part to enter solution (Au～2%, Ag～1%), afterwards step recovery: slag has been slagged tap enrichment silver, gold, after can handling with sodium hydroxide solution, the method-electrorefining of starting to exchange fire gets fine silver, gold; After also can wet gold extraction again with wet method or pyrogenic process desilver; Chloridizing leach solution feeds SO
2Gas reduces or adds a small amount of KI again and carries out catalytic reduction, makes Sb
+ 5→ Sb
+ 3, As
+ 5→ As
+ 3, tellurium precipitate reduction, chloridizing with controlled voltage leach the gold of loss and silver is over half and tellurium coprecipitation enters the tellurium concentrate, and control reduction terminal point is As
+ 5→ As
+ 3～100%(connects distillation) or＞70%(do not distill); The mother liquor of precipitate reduction pound is 100～110 ℃ of temperature, and distill under normal pressure best≤107 ℃, and arsenic distills out with water and HCl with the AsCl3 form, and condensation is reclaimed.Distillation mother liquor or tellurium precipitate reduction mother liquor add water hydrolysis antimony 40～50 ℃ of temperature, get antimony concentrate.Heavy antimony mother liquor adds sodium carbonate solution at～40 ℃ to be handled to pH2～4, precipitated bismuth.Feed chlorine oxidation in the heavy bismuth mother liquor, make Cu
+ 1Complete oxidation is Cu
+ 2, then in temperature～50 ℃, add milk of lime with sodium hydroxide solution and be neutralized to pH7～9, precipitated copper and residue arsenic, copper ore concentrates.Process indicator: Au, Ag total yield～99%, antimony, bismuth 90～96%, copper 90～98%, heavy copper raffinate pH7～9, Cu, Bi, Sb content＜1mg/l, As0.5mg/l reaches emission standard.
The advantage of method is: 1, gold and silver rate of recovery height, the gold and silver that are lost in the chloridizing with controlled voltage leach liquor are recovered in again in the tellurium concentrate, make total recovery～99% of gold and silver.2, arsenic removal distillation is more thorough, and hydrochloric acid can reclaim with appropriate mode, makes in the hydrolysis and the alkaline consumption of bismuth, copper reduces.3, antimony, bismuth, copper comprehensive recovery height (to concentrate rate of recovery antimony, bismuth 90～96%, copper 90～98%).4, corrodibility is little, and equipment solves well.5, if adopt the simple and easy method that does not distill arsenic of this law proposition, method is simple, but simplified apparatus.
Embodiment
Example 1, content are (weight %): Au0.03, Pb10.24, Cu3.40, Bi8.46, Sb33.12, Te0.38, the low golden anode mud with high As and Pb of As17.15 is at 4HNCl, temperature～20 ℃, solid: under liquid=1: 5 condition, feed the chlorine CONTROLLED POTENTIAL and leach at 380～420mv, can be with the tellurium leaching of the arsenic 98% or more, antimony, bismuth, copper and about 80%; Hydrochloric acid leachate adds a small amount of KI and feeds the gaseous sulfur dioxide reduction, and tellurium deposition rate＞99%, the gold and silver (Au～2%, Ag～1.4%) that enter leach liquor when chloridizing with controlled voltage leaches respectively has～and 50% co-precipitation enters the tellurium concentrate; Heavy tellurium mother liquor (As(+3)/As is total=and～90%, Sb(+3)/and Sb is total=and 100%) under normal pressure, 102～107 ℃ of arsenic removal distillations of temperature, contain the arsenic phlegma and can use sulfide precipitation, store up with the red arsenic form, hydrochloric acid returns leaching usefulness, or the phlegma condensing crystal is produced commodity As
2O
3, steaming raffinate with 40～50 ℃ of hot water hydrolytic precipitation antimony, heavy antimony mother liquor adds the sodium carbonate solution precipitated bismuth in 40～50 ℃, behind the logical chlorine oxidation of heavy bismuth mother liquor, in 40 ℃ of hydro-oxidation sodium solutions and an amount of milk of lime pH=7～9 that neutralize, precipitated copper and remain arsenic.To the concentrate rate of recovery: antimony, bismuth＞96%, copper＞98%.Heavy copper raffinate pH=8 contains Cu, Bi, Sb＜1mg/l, and As0.5mg/l reaches emission standard.
The hydrochloric acid leached mud contains Cu＜0.3%, Bi＜0.05%, Sb＜0.9%, As＜0.08%, Pb=40%, Au～0.115%, Ag～24.6%, after can handling with sodium hydroxide solution, the method-electrorefining of starting to exchange fire gets product silver, gold, after also can wet gold extraction again with wet method or pyrogenic process desilver, gold and silver total recovery～99%.
Example 2, content (weight %) are: Au0.014, Ag11.85, Pb14.70, Cu1.87, Sb20.66, Bi11.48, Te0.46, the low golden anode mud with high As and Pb of As13.46, by example 1 condition CONTROLLED POTENTIAL chlorination, the amount that gold and silver enter leach liquor is respectively～2% ,～1%; Leach liquor adds a small amount of KI ventilation body SO
2Reduction, tellurium deposition rate＞96%, the tellurium concentrate is advanced in each 50% co-precipitation of gold and silver that enters the chloridizing with controlled voltage leach liquor; Heavy tellurium mother liquor (As(+3)/As is total=and～80%, Sb(+3)/and Sb is total=and～98%) hydrolytic precipitation antimony, reclaim bismuth, copper by example 1 identical step process then.Antimony concentrate contains Sb70.1%, As1.1%, antimony direct yield 73%, arsenic scatter coefficient 1.61%; The bismuth concentrate contains Bi54.3%, As0.13%, bismuth direct yield 91%, arsenic scatter coefficient 0.2%; Copper ore concentrates contains Cu1.51%, As12.7%, copper direct yield 90%, arsenic scatter coefficient～75%; Heavy copper raffinate contains Cu4.2mg/l, Sb2.0mg/l, Bi5.0mg/l, As0.5mg/l after the high ferro dearsenification.Chloridizing with controlled voltage leached mud composition is similar to example 1, and after can handling with sodium hydroxide solution, the method-electrorefining of starting to exchange fire gets product silver, gold; Also can extract silver, gold and silver total yield 99% with wet method or pyrogenic process again behind the wet gold extraction.
Method of the present invention can also be used to contain the flue dust and the copper anode mud of arsenic, antimony, the enrichment process of goldmud from cyanide processing except that being used for the lead anode slurry processing.
Claims (4)
1, treatment method of high arsonium lead anode mud wet process is characterized in that:
A, the lead anode slurry material is placed 3～5N hydrochloric acid medium, solid: under the condition of liquid=1: 4～8, temperature feeds chlorine for 10～50 ℃ makes the oxidation reduction potential control of system carry out the selectivity leaching at 360～450Mv, the enrichment of gained solution arsenic, antimony, bismuth, copper, tellurium, the enrichment of gained leached mud silver, golden, after the sodium hydroxide solution processing, the method-electrorefining of starting to exchange fire gets product silver, gold; Or behind the wet gold extraction again with wet method or pyrogenic process desilver;
B, A, gained leach liquor are fed SO
2Gas reduces or adds a small amount of KI again and carries out catalytic reduction, makes Sb
+ 5→ Sb
+ 3, As
+ 5→ As
+ 3, the sulphur precipitate reduction, the gold and silver co-precipitation of A, leaching loss enters the tellurium concentrate;
C, B, gained solution are distilled for 100～110 ℃ in temperature, and condensation is reclaimed arsenic and is got AsC13, HCl;
D, with C, gained vinasse or B, gained solution 40～50 ℃ of temperature, add water hydrolysis antimony, antimony concentrate;
E, with D, gained solution in temperature～50 ℃, add sodium carbonate solution neutralization precipitation bismuth, the control endpoint pH is 2～4;
F, E, gained solution are fed chlorine oxidation, making 1 valency copper complete oxidation is divalent copper, in temperature～50 ℃, with sodium hydroxide solution add lime milk solution neutralize copper ore concentrates, a small amount of arsenic co-precipitation under C, step are heated up in a steamer enters copper ore concentrates.
2, treatment method of high arsonium lead anode mud wet process as claimed in claim 1, when it is characterized in that carrying out 1A, process, the oxidation reduction potential control of said system is at 380～400mv, 15～20 ℃ of temperature, 4NHCl, solid: liquid=1: 4～6.
3, treatment method of high arsonium lead anode mud wet process as claimed in claim 1, when it is characterized in that carrying out 1B, process, add a small amount of K1 make pentavalent arsenic be reduced to arsenious reducing degree for～100% or＞70%.
4, treatment method of high arsonium lead anode mud wet process as claimed in claim 1, when it is characterized in that carrying out 1C, process, controlled temperature＜107 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN92104421A CN1027977C (en) | 1992-06-02 | 1992-06-02 | Wet processing method for high-arsenic lead anode mud |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN92104421A CN1027977C (en) | 1992-06-02 | 1992-06-02 | Wet processing method for high-arsenic lead anode mud |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1079510A CN1079510A (en) | 1993-12-15 |
| CN1027977C true CN1027977C (en) | 1995-03-22 |
Family
ID=4940791
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN92104421A Expired - Fee Related CN1027977C (en) | 1992-06-02 | 1992-06-02 | Wet processing method for high-arsenic lead anode mud |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1027977C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1045796C (en) * | 1996-09-16 | 1999-10-20 | 昆明贵金属研究所 | Method for extracting gold, silver and valuable metals from high-arsenic copper anode mud |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1045795C (en) * | 1996-09-16 | 1999-10-20 | 昆明贵金属研究所 | Method for recovering platinum and lead from anode slime of hydrogen peroxide production by electrolysis |
| CN1045794C (en) * | 1996-09-16 | 1999-10-20 | 昆明贵金属研究所 | Method for extracting gold, silver and valuable metals from high-arsenic lead anode mud |
| CN1051114C (en) * | 1996-10-25 | 2000-04-05 | 昆明贵金属研究所 | Pretreatment method before wet method acid immersion for lead anode mud |
| CN101787440B (en) * | 2010-03-29 | 2011-08-10 | 广西华锡集团股份有限公司 | Method for wet processing of high antimony-lead anode mud |
| CN102219193B (en) * | 2010-04-16 | 2013-07-31 | 北京矿冶研究总院 | Method for separating and recovering tellurium from copper-tellurium solution |
| CN102586604B (en) * | 2011-01-18 | 2013-05-08 | 郴州市金贵银业股份有限公司 | Technology for wet-processing anode mud containing arsenic and lead |
| CN103205576A (en) * | 2013-03-22 | 2013-07-17 | 安徽铜冠有色金属（池州）有限责任公司九华冶炼厂 | Method for treating lead anode slime |
| CN107419110B (en) * | 2017-08-10 | 2019-11-19 | 阳谷祥光铜业有限公司 | The technique of tellurium, antimony, selenium, Jin Heyin is recycled in a kind of venturi mud |
| AU2018232890B2 (en) * | 2017-12-19 | 2024-09-26 | Eco-Tec Inc. | Catalytic Regeneration of Resin for Antimony Removal |
| CN108034831B (en) * | 2018-01-15 | 2019-04-12 | 安徽工业大学 | A kind of integrated conduct method containing miscellaneous Gold Concentrate under Normal Pressure melting flue dust |
| CN109777962B (en) * | 2019-03-01 | 2021-01-05 | 昆明理工大学 | Method for removing arsenic from lead anode mud |
| CN110578059B (en) * | 2019-10-18 | 2020-12-18 | 江西铜业股份有限公司 | Method for separating antimony and tellurium from copper anode slime by controlling potential leaching |
| CN112609089B (en) * | 2021-01-11 | 2022-04-01 | 大冶有色金属有限责任公司 | Method for enriching tellurium from platinum-palladium concentrate |
| CN114892007B (en) * | 2022-05-18 | 2024-06-25 | 云南锡业股份有限公司铜业分公司 | Method for recycling valuable metals from selenium slag steamed by complex copper anode slime |
| CN115323187B (en) * | 2022-08-19 | 2023-08-22 | 中南大学 | Method for removing SnPbFe impurities in platinum group metal-rich copper anode slime |
-
1992
- 1992-06-02 CN CN92104421A patent/CN1027977C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1045796C (en) * | 1996-09-16 | 1999-10-20 | 昆明贵金属研究所 | Method for extracting gold, silver and valuable metals from high-arsenic copper anode mud |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1079510A (en) | 1993-12-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1027977C (en) | Wet processing method for high-arsenic lead anode mud | |
| US4615731A (en) | Hydrometallurgical processing of precious metal-containing materials | |
| AU640199B2 (en) | Hydrometallurgic method for processing raw materials containing zinc sulphide | |
| US4676828A (en) | Process for the leaching of sulphides containing zinc and iron | |
| US6696037B1 (en) | Method of recovering sulfur from minerals and other sulfur-containing compounds | |
| Gordon et al. | Improved leaching technologies in the electrolytic zinc industry | |
| CN1032764C (en) | Method for extracting noble metal and valuable metal from tin anode mud | |
| Harvey | The hydrometallurgical extraction of zinc by ammonium carbonate: a review of the Schnabel process | |
| FI74046C (en) | TILLVARATAGANDE AV ZINK UR ZINK INNEHAOLLANDE SULFIDMATERIAL. | |
| US4069041A (en) | Method of recovering non-ferrous metals from sulphidic materials | |
| EP0113649A1 (en) | A method for working-up complex sulphidic ore concentrates | |
| US4443253A (en) | Recovery of zinc from zinc containing sulphidic materials | |
| US4082629A (en) | Hydrometallurgical process for treating metal sulfides containing lead sulfide | |
| CN1020755C (en) | Wet method for treating lead anode slurry | |
| EP0155250B1 (en) | A method for recovering the metal values from materials containing iron | |
| JP3411320B2 (en) | Zinc smelting method | |
| US3959097A (en) | Selenium rejection during acid leaching of matte | |
| US3544306A (en) | Concentration of copper from copper ores,concentrates and solutions | |
| US5961691A (en) | Recovery of lead and others metals from smelter flue dusts | |
| AU2149092A (en) | Method for processing complex metal sulphide materials | |
| US7494528B2 (en) | Method for smelting copper concentrates | |
| EP0042702B1 (en) | Process for the recovery of lead and silver from minerals and process residues | |
| US20230193418A1 (en) | Sulphide oxidation in leaching of minerals | |
| JPS58126937A (en) | Recovery of metal valuable matters from mat | |
| EP0061468A1 (en) | Recovery of silver from ores and concentrates. |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |