CN105603190B - A kind of method that cleaning copper electrolyte reclaims valuable metal - Google Patents
A kind of method that cleaning copper electrolyte reclaims valuable metal Download PDFInfo
- Publication number
- CN105603190B CN105603190B CN201510999788.6A CN201510999788A CN105603190B CN 105603190 B CN105603190 B CN 105603190B CN 201510999788 A CN201510999788 A CN 201510999788A CN 105603190 B CN105603190 B CN 105603190B
- Authority
- CN
- China
- Prior art keywords
- filtrate
- arsenic
- copper
- bismuth
- concentration
- 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.)
- Active
Links
Classifications
-
- 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
-
- 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
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0084—Treating solutions
- C22B15/0086—Treating solutions by physical methods
-
- 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
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0084—Treating solutions
- C22B15/0089—Treating solutions by chemical methods
- C22B15/0091—Treating solutions by chemical methods by cementation
-
- 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
- C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
- C22B23/0469—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods by chemical substitution, e.g. by cementation
-
- 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
- C22B3/46—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes by substitution, e.g. by cementation
-
- 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
- C22B30/00—Obtaining antimony, arsenic or bismuth
- C22B30/02—Obtaining antimony
-
- 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
- C22B30/00—Obtaining antimony, arsenic or bismuth
- C22B30/06—Obtaining bismuth
-
- 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
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Electrolytic Production Of Metals (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a kind of method that cleaning copper electrolyte reclaims valuable metal.It comprises the following steps：(1) copper sulphate is recovered by filtration in copper electrolyte evaporative crystallization；(2) arsenic sulfide slag is added into cupric electrolysis filtrate, and copper sulfide and antimony trisulfide are recovered by filtration after the completion of reaction；(3) cupric electrolysis filtrate evaporative crystallization is separated by filtration arsenic oxide arsenoxide and bismuth oxide；(4) Selectively leaching and bismuth in (3) is reclaimed；(5) cupric electrolysis filtrate high performance vulcanization deeply removing arsenic；(6) cupric electrolysis filtrate diffusion dialysis separation and recovery sulfuric acid；(7) diffusion dialysis stoste reclaims nickel using neutralization precipitation method.Overall process of the present invention uses wet method, high-efficiency environment friendly energy-conservation, with preferable application value.
Description
Technical field
The invention belongs to metallurgical engineering and environmental project crossing domain, and in particular to a kind of valuable gold of cupric electrolysis Recovery Purifying
The method of category.
Background technology
At present, smelting enterprise produces copper products using the technique of pyrometallurgical smelting-electrorefining.Due to universal in copper concentrate
The other elements of association, cause complicated component in electrolyte, contain substantial amounts of foreign ion such as arsenic, antimony, the bismuth for being unfavorable for electrolysis
Deng.These foreign ions can not only be deposited on negative electrode, and can form the drift earth of positive pole, have a strong impact on the use longevity of battery lead plate
The quality of life and tough cathode.Therefore, electrolyte be both needed to before electrolysis purification.
Traditional method for purifying copper electrolyte is electrodeposition decopper(ing) dearsenification method, and it is used by most smelting enterprises.Closely
Nian Lai, world's researcher has made some improvement, such as continuous decopper(ing) dearsenification electrodeposition method, periodic reverse current electricity on this basis
Area method and limiting current density electrodeposition method etc..Though with preferable decopper(ing) dearsenification effect, there is following deficiency：1) insoluble sun is used
Pole is electrolysed, and current efficiency is low, high energy consumption；2) when copper ion concentration is reduced to certain value in electrolyte, negative electrode can separate out severe toxicity
Arsine gas；3) substantial amounts of black copper mud is generated during electrodeposition, arsenic antimony bismuth is enriched with wherein, and black copper mud returns to pyrogenic process and melted
The process that copper is reclaimed in refining result in the pernicious closed cycle enrichment in smelting system of arsenic antimony bismuth, it is impossible to form effectively open circuit.
Therefore, how electrolyte is purified, arsenic antimony bismuth is formed effective open circuit out of system, to reduce to refining
Influence is the problem of enterprise is in the urgent need to address.In addition, nickel and sulfuric acid containing high concentration in electrolyte, in purification process,
Need to consider the recovery to it, further to reduce the production cost of enterprise.
The content of the invention
The present invention is directed to the defects, mesh such as big, the difficult recovery of valuable metal of high energy consumption, cost in current method for purifying copper electrolyte
Be a kind of energy-saving and environmental protection, the purification method of high efficiente callback valuable metal are provided.After processed by the invention, in electrolyte
Copper, antimony, bismuth, nickel, arsenic and sulfuric acid can realize high efficiente callback, greatly reduce the production cost of enterprise, improve efficiency.
A kind of method that cleaning copper electrolyte reclaims valuable metal, comprises the following steps：
1) copper sulphate is recovered by filtration in copper electrolyte evaporation and concentration and obtains cupric electrolysis filtrate；
2) arsenones or arsenic sulfide slag are added in cupric electrolysis filtrate, copper sulfide, sulphur is filtrated to get after heating response
Change antimony precipitation and copper removal removes antimony filtrate；
3) by copper removal except antimony filtrate is concentrated by evaporation, by filtered after concentrate crystallisation by cooling arsenic oxide arsenoxide and bismuth oxide mixing
Sediment and concentration filtrate；
4) by arsenic oxide arsenoxide and the mixed sediment sulfuric acid and sodium chloride Selectively leaching bismuth of bismuth oxide, mistake after the completion of leaching
Filter to obtain arsenic oxide arsenoxide and rich bismuth leachate；
5) chlorine oxygen bismuth and tail washings are filtered to obtain after rich bismuth leachate being adjusted into pH value, standing with alkali；
6) by step 3) obtained concentration filtrate adds vulcanizing agent and carries out depth vulcanization, and rich arsenic slag is filtered to obtain after the completion of reaction
With dearsenification filtrate；
7) dearsenification filtrate is reclaimed into sulfuric acid with diffusion dialysis；
8) diffusion dialysis stoste reclaims nickel using neutralization precipitation method.
Step 1) described in copper electrolyte derive from the electricity that produces in Copper making industry pyrometallurgical smelting-electrolytic refining process
Solve liquid.
Step 1) in copper electrolyte the concentration of copper be 1~55g/L.
Step 2) in arsenic sulfide slag from smelting enterprise with vulcanization method precipitate obtained by arsenic slag, including：Waste acid arsenic slag,
One or more in electrolysis waste solution arsenic slag.
Step 2) in by arsenic sulfide slag by As/Cu mol ratios be 1~5:1 ratio is added in cupric electrolysis filtrate, 50
Reacted at~80 DEG C and copper sulfide, antimony trisulfide precipitation and copper removal are filtrated to get after 0.5~3h except antimony filtrate.
Step 3) in by copper removal except antimony filtrate is concentrated by evaporation to H2SO4Concentration is 700-900g/L, and concentrate is placed in into temperature
For filtered after crystallisation by cooling 1-3h at 15~40 DEG C arsenic oxide arsenoxide and bismuth oxide mixed sediment and concentration filtrate.
Step 4) in by arsenic oxide arsenoxide and the mixed sediment sulfuric acid and sodium chloride Selectively leaching bismuth of bismuth oxide, leach bar
Part is sulfuric acid concentration 1-5mol/L, and chlorine ion concentration is 2-3mol/L, and solid-liquid mass ratio is 1-5, extraction time at least 2h, leaching
Temperature is 25-60 DEG C, and arsenic oxide arsenoxide and rich bismuth leachate are filtered to obtain after the completion of leaching.
Step 5) in by rich bismuth leachate with alkali adjust pH to 2-4, stand 1-4h after filter to obtain chlorine oxygen bismuth and tail washings.Step
5) tail washings in is recycling in potassium cloride.
Step 6) by step 3) obtained concentration filtrate carries out depth vulcanization, add according to S/As mol ratios for 1-5 ratio
Enter vulcanizing agent, temperature is at 15~40 DEG C, reaction 0.5-3h carries out depth dearsenification, and rich arsenic slag and dearsenification are filtered to obtain after the completion of reaction
Filtrate.Step 6) obtained rich arsenic slag is added to cupric electrolysis filtrate as arsenic sulfide slag and is used for carrying out copper sulfide, antimony trisulfide precipitating.
Step 7) diffusion dialysis reclaim sulfuric acid be added in copper electrolyte be used for reclaim copper sulphate.Or for arsenic oxide arsenoxide
With the Selectively leaching of bismuth oxide mixed sediment bismuth.
The advantage of the present invention：
1. technique is simple, energy consumption is low, and consumption is substantial amounts of arsenic sulfide slag, greatly reduces the production cost of enterprise.
2. valuable metal and sulfuric acid have obtained high efficiente callback, whole technical process non-secondary pollution, waste liquid in electrolyte
It can be utilized with waste residue in system interior circulation, realize the purpose of clean manufacturing.
Brief description of the drawings
Fig. 1 is process chart of the invention.
Embodiment
Following examples are that the present invention is further illustrated, rather than the limitation present invention.
Embodiment 1
The electrolyte 500ml of certain copper smelting plant is taken, sulfuric acid concentration is 289g/L, and other essential elements and content are as follows：
The copper electrolyte essential element of table 1 and concentration (g/L)
Above-mentioned electrolyte is concentrated by evaporation to 250ml crystallisation by cooling filtering, copper in 29g cupric sulfate pentahydrates, filtrate is obtained
Concentration is about 60g/L, and other essential element concentration are doubled, and arsenic sulfide slag is pressed into n (As)：N (Cu) adds for 1.2 ratio
Precipitation and copper removal that copper sulfide and antimony trisulfide are filtrated to get after 3h are reacted into filtrate, at 80 DEG C except antimony filtrate, copper removal is filtered except antimony
The concentration of copper is 41.2mg/L in liquid, and the concentration of antimony is 97.8mg/L, and the overall recovery of copper and the rate of recovery of antimony are respectively
99.9% and 87.5%.By above-mentioned copper removal except antimony filtrate be concentrated by evaporation to sulfuric acid concentration be 800g/L after cooling and standings 2h, filtering
Mixed sediment and the concentration filtrate of arsenic oxide arsenoxide and bismuth oxide are obtained, gained mixed sediment villaumite is leached, leaching condition is
196g/L sulfuric acid, chlorine ion concentration is 2mol/L, and liquid-solid ratio is 5, and extraction temperature is 50 DEG C, leaches 2h, mistake after the completion of leaching
The concentration for filtering to obtain bismuth in high-grade arsenic oxide arsenoxide and rich bismuth leachate, leachate is 3.2g/L, and leachate adds sodium hydroxide and adjusts pH
To 3,2h is stood, chlorine oxygen bismuth is filtrated to get, the rate of recovery of bismuth is 90.5%.Foregoing concentration filtrate is added into vulcanizing agent to carry out deeply
Degree vulcanization, adds vulcanizing agent, temperature is at 20 DEG C, reaction 2h carries out depth dearsenification, instead according to S/As mol ratios for 1.5 ratio
Rich arsenic slag and dearsenification filtrate are filtered to obtain after the completion of answering.Dearsenification filtrate is entered into diffusion dialysis, the sour rate of recovery is 90%, after recovery
Sulfuric acid concentration is less than 10% up to 720g/L, the mobility of nickel, and sulfuric acid is back to electrolysis system after recovery.Diffusion dialysis stoste adds
Enter sodium carbonate to be neutralized, the direct yield of nickel is 99%.
Embodiment 2
The electrolyte 500ml of certain copper smelting plant is taken, sulfuric acid concentration is 267g/L, and other essential elements and content are as follows：
The copper electrolyte essential element of table 1 and concentration (g/L)
Above-mentioned electrolyte is concentrated by evaporation to 250ml crystallisation by cooling filtering, copper in 30g cupric sulfate pentahydrates, filtrate is obtained
Concentration is about 64g/L, and other essential element concentration are doubled, and arsenic sulfide slag is pressed into n (As)：N (Cu) adds for 1.3 ratio
Precipitation and copper removal that copper sulfide and antimony trisulfide are filtrated to get after 3h are reacted into filtrate, at 80 DEG C except antimony filtrate, copper removal is filtered except antimony
The concentration of copper is 44.5mg/L in liquid, and the concentration of antimony is 90.8mg/L, and the overall recovery of copper and the rate of recovery of antimony are respectively
99.9% and 89.7%.By above-mentioned copper removal except antimony filtrate be concentrated by evaporation to sulfuric acid concentration be 850g/L after cooling and standings 2h, filtering
Mixed sediment and the concentration filtrate of arsenic oxide arsenoxide and bismuth oxide are obtained, gained mixed sediment villaumite is leached, leaching condition is
196g/L sulfuric acid, chlorine ion concentration is 3mol/L, and liquid-solid ratio is 5, and extraction temperature is 50 DEG C, leaches 2h, mistake after the completion of leaching
The concentration for filtering to obtain bismuth in high-grade arsenic oxide arsenoxide and rich bismuth leachate, leachate is 3.4g/L, and leachate adds sodium hydroxide and adjusts pH
To 3,2h is stood, chlorine oxygen bismuth is filtrated to get, the rate of recovery of bismuth is 91.5%.Foregoing concentration filtrate is added into vulcanizing agent to carry out deeply
Degree vulcanization, adds vulcanizing agent, temperature is at 15 DEG C, reaction 2h carries out depth dearsenification, instead according to S/As mol ratios for 1.5 ratio
Rich arsenic slag and dearsenification filtrate are filtered to obtain after the completion of answering.Dearsenification filtrate is entered into diffusion dialysis, the sour rate of recovery is 90%, after recovery
Sulfuric acid concentration is less than 10% up to 740g/L, the mobility of nickel, and sulfuric acid is back to electrolysis system after recovery.Diffusion dialysis stoste adds
Enter sodium carbonate to be neutralized, the direct yield of nickel is 99%.
Claims (10)
1. a kind of method that cleaning copper electrolyte reclaims valuable metal, it is characterised in that comprise the following steps：
1) copper sulphate is recovered by filtration in copper electrolyte evaporation and concentration and obtains cupric electrolysis filtrate；
2) arsenones or arsenic sulfide slag are added in cupric electrolysis filtrate, copper sulfide, antimony trisulfide is filtrated to get after heating response
Precipitation and copper removal remove antimony filtrate；
3) by copper removal except antimony filtrate is concentrated by evaporation, by filtered after concentrate crystallisation by cooling arsenic oxide arsenoxide and bismuth oxide mixed precipitation
Thing and concentration filtrate；
4) by arsenic oxide arsenoxide and the mixed sediment sulfuric acid and sodium chloride Selectively leaching bismuth of bismuth oxide, filtered after the completion of leaching
Arsenic oxide arsenoxide and rich bismuth leachate；
5) chlorine oxygen bismuth and tail washings are filtered to obtain after rich bismuth leachate being adjusted into pH value, standing with alkali；
6) by step 3) obtained concentration filtrate adds vulcanizing agent and carries out depth vulcanization, and rich arsenic slag and de- is filtered to obtain after the completion of reaction
Arsenic filtrate；
7) dearsenification filtrate is reclaimed into sulfuric acid with diffusion dialysis；
8) diffusion dialysis stoste reclaims nickel using neutralization precipitation method.
2. the copper electrolyte described according to the method described in claim 1, it is characterised in that step 1) derives from Copper making row
The electrolyte produced in industry pyrometallurgical smelting-electrolytic refining process.
3. method according to claim 1 or 2, it is characterised in that step 1) in copper electrolyte copper concentration for 1~
55g/L。
4. the arsenic sulfide slag according to the method described in claim 1, it is characterised in that step 2) derives from smelting enterprise's sulphur
Arsenic slag obtained by change method precipitation, including：One or more in waste acid arsenic slag, electrolysis waste solution arsenic slag.
5. the method according to claim 1 or 4, it is characterised in that step 2) in by As/Cu mol ratios be by arsenic sulfide slag
1~5:1 ratio is added in cupric electrolysis filtrate, and copper sulfide, antimony trisulfide are filtrated to get after reacting 0.5~3h at 50~80 DEG C
Precipitation and copper removal remove antimony filtrate.
6. by copper removal except antimony filtrate is concentrated by evaporation to H according to the method described in claim 1, it is characterised in that step 3)2SO4
Concentration is 700-900g/L, and concentrate is placed in temperature to filter to obtain arsenic oxide arsenoxide and oxidation after crystallisation by cooling 1-3h at 15~40 DEG C
The mixed sediment of bismuth and concentration filtrate.
7. by arsenic oxide arsenoxide and the mixed sediment of bismuth oxide according to the method described in claim 1, it is characterised in that step 4)
With sulfuric acid and sodium chloride Selectively leaching bismuth, leaching condition is sulfuric acid concentration 1-5mol/L, and chlorine ion concentration is 2-3mol/L, Gu
Liquid mass ratio is 1-5, and extraction time at least 2h, extraction temperature is 25-60 DEG C, and arsenic oxide arsenoxide and rich bismuth leaching are filtered to obtain after the completion of leaching
Go out liquid.
8. rich bismuth leachate is adjusted into pH to 2-4 with alkali according to the method described in claim 1, it is characterised in that step 5),
Chlorine oxygen bismuth and tail washings are filtered to obtain after standing 1-4h.
9. according to the method described in claim 1, it is characterised in that step 6) by step 3) obtained concentration filtrate carries out depth
Vulcanization, adds vulcanizing agent, temperature is at 15~40 DEG C, reaction 0.5-3h carries out depth according to S/As mol ratios for 1-5 ratio
Rich arsenic slag and dearsenification filtrate are filtered to obtain after the completion of dearsenification, reaction.
10. the tail washings according to the method described in claim 1, it is characterised in that step 5) is recycling in potassium cloride；Step
The rapid rich arsenic slag 6) obtained is added to cupric electrolysis filtrate as arsenic sulfide slag and is used for carrying out copper sulfide, antimony trisulfide precipitation；Step 7)
The sulfuric acid that diffusion dialysis is reclaimed, which is added in copper electrolyte, is used for cupric electrolysis or in arsenic oxide arsenoxide and bismuth oxide mixed sediment
The Selectively leaching of bismuth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510999788.6A CN105603190B (en) | 2015-12-28 | 2015-12-28 | A kind of method that cleaning copper electrolyte reclaims valuable metal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510999788.6A CN105603190B (en) | 2015-12-28 | 2015-12-28 | A kind of method that cleaning copper electrolyte reclaims valuable metal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105603190A CN105603190A (en) | 2016-05-25 |
| CN105603190B true CN105603190B (en) | 2017-10-20 |
Family
ID=55983525
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510999788.6A Active CN105603190B (en) | 2015-12-28 | 2015-12-28 | A kind of method that cleaning copper electrolyte reclaims valuable metal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105603190B (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106044866A (en) * | 2016-06-03 | 2016-10-26 | 河南中原黄金冶炼厂有限责任公司 | Method for producing iron oxide black through metallurgical waste water |
| CN106834736A (en) * | 2016-12-29 | 2017-06-13 | 东营方圆有色金属有限公司 | The separating technology of copper and arsenic in arsenic sulfide slag |
| CN107338360B (en) * | 2017-07-17 | 2018-08-14 | 江西铜业股份有限公司 | A method of nickel salt in separation high price arsenic solution |
| CN108517538B (en) * | 2018-04-08 | 2019-11-29 | 长沙华时捷环保科技发展股份有限公司 | The method of waste solution of copper electrolysis synthetical recovery processing |
| CN108570559A (en) * | 2018-05-16 | 2018-09-25 | 江西铜业股份有限公司 | A method of the depth vulcanization separation cupro-nickel arsenic from high acid solution |
| CN110669932B (en) * | 2019-09-25 | 2021-04-20 | 中南大学 | Method for comprehensively utilizing copper electrolyte purification resources |
| CN112375905A (en) * | 2020-09-15 | 2021-02-19 | 西北矿冶研究院 | Method for recovering antimony and copper from electrolyzed liquid |
| CN114540626B (en) * | 2022-03-22 | 2023-06-20 | 山东恒邦冶炼股份有限公司 | Method for recycling valuable metals in contaminated acid in steps by utilizing antimony electrowinning lean solution |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1935705A (en) * | 2006-10-20 | 2007-03-28 | 云南冶金集团总公司技术中心 | Method for removing impurities suchas magnesium and recovering sulfuricacid and zinc from zinc electrolytic waste solution |
| CN103725888A (en) * | 2013-12-13 | 2014-04-16 | 金川集团股份有限公司 | Method for extracting nickel from copper electrolysis effluent |
| CN104894387A (en) * | 2015-05-25 | 2015-09-09 | 铜陵有色金属集团股份有限公司 | Technological method for extracting antimony and bismuth from rare and noble metallurgical slag |
-
2015
- 2015-12-28 CN CN201510999788.6A patent/CN105603190B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1935705A (en) * | 2006-10-20 | 2007-03-28 | 云南冶金集团总公司技术中心 | Method for removing impurities suchas magnesium and recovering sulfuricacid and zinc from zinc electrolytic waste solution |
| CN103725888A (en) * | 2013-12-13 | 2014-04-16 | 金川集团股份有限公司 | Method for extracting nickel from copper electrolysis effluent |
| CN104894387A (en) * | 2015-05-25 | 2015-09-09 | 铜陵有色金属集团股份有限公司 | Technological method for extracting antimony and bismuth from rare and noble metallurgical slag |
Non-Patent Citations (1)
| Title |
|---|
| 硫化法脱除铜电解废液中As，Sb，Bi的试验;钟云波 等;《中南工业大学学报》;19970831;第28卷(第4期);336-339 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105603190A (en) | 2016-05-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105603190B (en) | A kind of method that cleaning copper electrolyte reclaims valuable metal | |
| CN107017443B (en) | A method of the comprehensively recovering valuable metal from waste and old lithium ion battery | |
| CN102491287B (en) | Process for separating and recovering selenium from selenium-containing material | |
| CN111187913A (en) | Method for selectively recovering lithium and copper in waste lithium iron phosphate batteries | |
| CN102851707B (en) | The technique of a kind of alkaline leaching remanufacture electrolytic zinc powder and lead powder from smelting ash | |
| CN105779770B (en) | Method for recycling valuable metal in waste circuit board | |
| CN108624759B (en) | Method for comprehensively recovering valuable metals from white smoke | |
| CN103773972B (en) | A kind of processing method of raw material containing lead | |
| CN105648214B (en) | It is a kind of to control the method that current potential vulcanization separates valuable metal in solution | |
| JP5721213B2 (en) | Method for producing pure metal indium from zinc oxide and / or metal-containing solution | |
| CN105274565A (en) | Method for electrolyzing metals through wet method | |
| CN104419826B (en) | The method that ammonia soaks Zinc Oxide electrowinning zinc | |
| CN104561558A (en) | Method for treating selenium-containing mercury acid mud | |
| CN113511664A (en) | Method for preparing battery-grade lithium carbonate by selectively extracting lithium from battery waste | |
| CN112458280A (en) | Method for extracting valuable metals by leaching low grade nickel matte with acidic etching solution | |
| CN110512083A (en) | A kind of method of metal resource comprehensive utilization in oil-containing electroplating sludge | |
| CN105568002B (en) | Method of the bismuth enrichment with reclaiming in a kind of waste acid vulcanized slag | |
| CN105200242A (en) | Method for revering cadmium from arsenic-containing lead-smelting oxygen bottom-blown furnace dust | |
| CN107299228A (en) | A kind of method that zinc hydrometallurgy purification copper ashes extracts metallic copper | |
| CN107815540A (en) | A kind of method of hydrometallurgy metal nickel cobalt and its salt product | |
| CN104005051A (en) | Method for extracting electrodeposited zinc from zinc oxide powder in ammonium chloride solution system | |
| CN103194621A (en) | Method for treating sulfur slag | |
| CN110629042B (en) | Method for leaching antimony oxide material by tartaric acid system and producing metallic antimony by electrodeposition | |
| CN103221557B (en) | Method for producing nickel-ontaining acidic solution | |
| CN106591586A (en) | Method for recovering multiple kinds of metal from flue dust in copper smelting |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: Yuelu District City, Hunan province 410083 Changsha Lushan Road No. 932 Co-patentee after: Thiessens environmental Limited by Share Ltd Patentee after: Central South University Address before: Yuelu District City, Hunan province 410083 Changsha Lushan Road No. 932 Co-patentee before: CHANGSHA SCIENCE ENVIRONMENTAL TECHNOLOGY CO., LTD. Patentee before: Central South University |