CN106834679A - The method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions - Google Patents
The method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions Download PDFInfo
- Publication number
- CN106834679A CN106834679A CN201710097359.9A CN201710097359A CN106834679A CN 106834679 A CN106834679 A CN 106834679A CN 201710097359 A CN201710097359 A CN 201710097359A CN 106834679 A CN106834679 A CN 106834679A
- Authority
- CN
- China
- Prior art keywords
- lead
- concentrate
- leaching
- sulfonic acid
- sulfide ore
- 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.)
- Granted
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
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/16—Extraction of metal compounds from ores or concentrates by wet processes by leaching in organic solutions
- C22B3/1608—Leaching with acyclic or carbocyclic agents
- C22B3/1616—Leaching with acyclic or carbocyclic agents of a single type
- C22B3/165—Leaching with acyclic or carbocyclic agents of a single type with organic acids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/06—Preparation of sulfur; Purification from non-gaseous sulfides or materials containing such sulfides, e.g. ores
-
- 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
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet processes
-
- 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
- C25C1/18—Electrolytic production, recovery or refining of metals by electrolysis of solutions of lead
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention discloses the method that lead in concentrate of lead sulfide ore is leached in a kind of two sections of adverse current pressure oxidations of sulfonic acid solutions, the method is reacted in autoclave after sulfonic acid solutions are mixed with concentrate of lead sulfide ore, surfactant, oxidation catalyst is done using iron ion, by neutral oxygen leaching and this two sections of counterflow leaching process of acid oxygen leaching, the selectively leaching of lead is realized；And the sulphur in concentrate is oxidized to elementary sulfur, in remaining in slag.Neutral leachate obtains metallic lead with useless electric effusion by electrodeposition；Useless electric effusion enters acidic leaching next time or for preparing new electric effusion.The method not only realizes the high efficiency extraction of lead, and realizes recycling for leachate and electric effusion, is produced without waste liquid, meets the requirement of environmental protection.
Description
Technical field
The present invention relates to a kind of method for extracting lead from concentrate of lead sulfide ore by Whote-wet method, more particularly to a kind of sulfonic acid is molten
The method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of liquid, belongs to Non-ferrous Metallurgy field.
Background technology
Sulfonic acid solutions are in nature stable existence, not oxidizable and reduction.Sulfonic acid has multiple use, is that medicine and agricultural chemicals are former
Material, can be used as dehydrating agent, paint solidification accelerator, fibre finish, obtain extensive use as electric brush plating liquor solvent in recent years.
Metal metilsulfate is widely applied in field of electrochemical deposition, wherein the application related to surface finishing industry includes:Tin,
Fluoboric acid and borofluoride are substituted in lead and Terne Electroplating；Wire and steel bar are tin plating；The metal essence of silver, copper, nickel and palladium
Decorations；Nickel, tin, lead, tin-lead and cadmium coater are stripped from copper and its alloy, zinc and its alloy surface using dipping and spraying process.
Domestic more than 80% lead is the pyrogenic process production from concentrate of lead sulfide ore at present.Traditional pyrometallurgical smelting of lead is using sintering
By burning-blast furnace reduction process, there is that energy consumption is big, low concentration SO2Exhaust emission environment, is prohibitted the use of by country.Current state
The present lead metallurgical method of inside and outside use has bottom blowing molten pool melting (such as QSL methods, Shuikoushan method), Flash Smelting Furnace melting (such as Ji Fusai
Special method), top-blown submergence smelting process (such as Ausmelt method, ISA methods) method, these smelting processes, reaction temperature is 1100
More than DEG C, high energy consumption, lead steam are high, pollute environment.
At present, the method that research wet method extracts lead from concentrate of lead sulfide ore both at home and abroad has：①FeCl3Oxidizing process：PbS+2FeCl3
=PbCl2+2FeCl2+S0, various dissoluble lead-Chloro complexes are formed under higher temperature, increased by adding alkali metal chloride
Cl-Total concentration, can make lead in solution main with PbCl4 2-Form exist, then crystallisation by cooling goes out PbCl2, re-dry, most
Electrolytic metal lead and chlorine in low-temperature molten salt system afterwards, chlorine are returned and leached, but it has problem and is：Hydrochloric acid is volatile, corruption
Erosion equipment, high temperature chlorine is difficult to collect, and lead chloride produces lead oxide with air contact in molten-salt electrolysis lead, hinders electrolysis
Carry out.Also there is the research that ozone-hydrogen peroxide-ferric trichloride co-oxidation is extracted, its reaction equation is as follows：
PbS+4H2O2+ 2NaCl=PbCl2+Na2SO4+4H2O
3PbS+4O3+ 6NaCl=3PbCl2+3Na2SO4
PbS+2NaCl+8FeCl3+4H2O=PbCl2+Na2SO4+8FeCl2+8HCl
8FeCl2+H2O2+3H2O+O3+ 8HCl=8FeCl3+8H2O
PbCl2+2Cl-=[PbCl4]2-
2. galena-pyrolusite two-ores method：Born in oxidisability oxidation galena using manganese dioxide in pyrolusite
Sulfidion, so as to leach lead, manganese element simultaneously.Reaction equation is as follows：
PbS+MnO2+ 4HCl=PbCl2+MnCl2+S+2H2O
PbCl2+2Cl-=[PbCl4]2-
3. the Oxidation Leaching in fluosilicic acid medium：Oxidant used has oxygen, H2O2、Fe2(SiF6)3, their reaction is:
2PbS+O2+2H2SiF6=2PbSiF6+2S0+2H2O
PbS+H2O2+H2SiF6=PbSiF6+S0+2H2O
PbS+Fe2(SiF6)3=PbSiF6+S0+2FeSiF6
Using oxygen, H2O2Leach lead, it is purified after can be with electrodeposition lead；Fe2(SiF6)3For oxidant, it is necessary to using conjunctiva
Electrodeposition, negative electrode obtains lead, anode regeneration Fe2(SiF6)3.But leaching agent fluoride is unstable, easy decomposition produces hydrogen fluoride gas,
It is harmful, cause operating environment poor.
The content of the invention
For existing pyrometallurgical smelting of lead and wet underwater welding lead method have that environmental pollution is serious, leaching agent corrosivity is big,
The problems such as operating environment difference, it is to propose a kind of environmental protection, efficiently pass through Whote-wet method from vulcanized lead that the purpose of the present invention is
The method that lead is extracted in concentrate.
In order to realize above-mentioned technical purpose, vulcanization is leached the invention provides a kind of two sections of adverse current pressure oxidations of sulfonic acid solutions
The method of lead in lead concentrate, the method is comprised the following steps：
1) after mixing concentrate of lead sulfide ore, surfactant with leaching agent containing sulfonic acid, it is transferred in autoclave, leads to in system
Enter oxygen, carry out neutral leaching, solid-liquor separation obtains neutral leachate and neutral leaching residue.
2) the neutral leachate described in is made into lead electric effusion with useless electric effusion carries out electro-deposition lead, obtains metal stereotype and gives up
Electric effusion；
3) after the neutral leaching residue described in mixes with acid lixiviant, it is transferred in autoclave, to oxygen is passed through in system, enters
Row acidic leaching, after solid-liquor separation, obtains acid leaching solution and acidic leaching residue；Described acid lixiviant is produced by electro-deposition lead
Raw useless electric effusion supplements its free sulfonic concentration to obtaining in the range of 0.3~2.5mol/L；
4) acid leaching solution enters neutral leaching next time and uses as leaching agent containing sulfonic acid；The acidic leaching residue
Carry out reclaiming elementary sulfur and noble metal.
Preferred scheme, the leaching agent containing sulfonic acid includes pyrovinic acid and/or ethylsulfonic acid.
Preferred scheme, neutral leaching condition is：The liquid-solid ratio of leaching agent containing sulfonic acid and concentrate of lead sulfide ore for 3mL/g~
15mL/g, surfactant qualities are the 0.05~0.5% of concentrate of lead sulfide ore quality, and reaction temperature is 105~170 DEG C, stirring
Speed is 100~800 revs/min, and oxygen presses 0.2~1.5MPa, and the reaction time is 0.5~3h, and reaction end pH value is more than 5.0.
More preferably scheme, surfactant used includes at least in ligninsulfonate, o-phenylenediamine, m-phenylene diamine (MPD)
Kind.
Preferred scheme, the condition of the acidic leaching is：Neutral leaching residue is 3mL/g with the liquid-solid ratio of acid lixiviant
~15mL/g, extraction temperature is 110~170 DEG C, and mixing speed is 200~800 revs/min, and oxygen presses 0.2~1.5MPa, during leaching
Between be 0.5~3.0h, it is 0.1~0.8mol/L to leach terminal point control system acidity.
Preferred scheme, the condition of the electro-deposition lead is：Current density is 80~400A/m2, electric effusion temperature 30~
65℃。
More preferably scheme, during electro-deposition lead, with graphite cake, ti-supported lead dioxide electric net or titanium-based platinum guaze as anode
Plate, with Lead initiated plate electrode, titanium plate or stainless steel plate as minus plate；The minus plate periphery is more long than the positive plate 1~3 centimetre.
Two sections of adverse current pressure oxidations of the sulfonic acid solutions that the present invention is provided leach the method for lead in concentrate of lead sulfide ore including following
Step (accompanying drawing 1 is shown in technological process)：
1) by concentrate of lead sulfide ore, surfactant (such as ligninsulfonate, o-phenylenediamine, m-phenylene diamine (MPD)) and last time acid
Property leach acid immersion liquid (it includes sulfonic acid) mixing for obtaining, carry out pressurised oxygen in the autoclave of uniform temperature and oxygen pressure
Change and leach, finally make leachate into weakly acidic pH；And making ferrous ions therein into trivalent, precipitation enters into neutral leaching residue
In, then carry out solid-liquor separation and obtain neutral leachate and neutral leaching residue.Neutral leaching condition is：The liquid of leaching agent and concentrate
Gu than being 3mL/g~15mL/g, surfactant is concentrate amount 0.05~0.5%, and reaction temperature is 105~170 DEG C, stirring speed
It is 100~800 revs/min to spend, oxygen press 0.2~1.5MPa, the reaction time be 0.5~3h, reaction end pH value more than 5.0, in
Property leach key reaction have：
2PbS+4RSO3H+O2=2Pb (RSO3)2+S0+2H2O
PbS+2RSO3H+2Fe3+=2Pb (RSO3)2+S0+2Fe2++H2O
4Fe2++O2+6H2O=4FeOOH+8H+
R is CH in reaction equation3、C2H5。
2) above-mentioned neutral leachate is made into the sulfonic acid solutions of certain lead concentration with useless electric effusion, and electro-deposition obtains metallic lead
Plate and useless electric effusion.Electro-deposition leads part is：Current density is 80~400A/m2, 30~65 DEG C of electric effusion temperature.Electrodeposition lead mistake
Cheng Zhong, with graphite cake, ti-supported lead dioxide electric net or titanium-based platinum guaze as positive plate, with Lead initiated plate electrode, titanium plate or stainless steel plate as cloudy
Pole plate；The minus plate periphery is more long than the positive plate 1~3 centimetre.Electrolytic deposition process key reaction has：
4Pb(RSO3)2+2H2O=4Pb+O2+4RSO3H
3) above-mentioned neutral leaching residue (using the useless electric effusion of sulfonic acid solutions regulation, makes its free sulfonic with sulfonic acid leaching agent
Concentration is in the range of 0.3~2.5mol/L) mix, neutrality leaches the iron for precipitating and enters solution with sulfonic acid reaction dissolving,
Pressure oxidation leaching is carried out in uniform temperature and the autoclave of oxygen pressure, the neutral sulphur for leaching unreacted vulcanized lead is oxidized
Into elementary sulfur, acidic leaching residue is entered into, and lead dissolving enters solution.After solid-liquor separation, obtain acid leaching solution and soaked with acid
Slag tap.The condition of acidic leaching is：Leaching agent is mainly the sulfonic acid of useless electric effusion and supplement, the concentration of free sulfonic for 0.3~
2.5mol/L, extraction temperature is 110~170 DEG C, and mixing speed is 200~800 revs/min, and oxygen presses 0.2~1.5MPa, during leaching
Between 0.5~3.0h, it is 0.1-0.8mol/L to leach terminal acidity；Acidic leaching process key reaction has：
FeOOH+3H+=Fe3++2H2O
PbS+2RSO3H+2Fe3+=2Pb (RSO3)2+S0+2Fe2++H2O
2PbS+4RSO3H+O2=2Pb (RSO3)2+S0+2H2O
4) the neutral leaching that above-mentioned acid leaching solution enters next time uses, and leached mud reclaims elementary sulfur and valuable gold
Category.
Compared with the prior art, the beneficial effect that technical scheme is brought：With pyrometallurgical smelting of lead, lead, lead oxide are eliminated
Steam volatilizees, and without SO2The discharge of flue gas, it is to avoid environmental pollution；Lead is refined with existing wet method, leaching agent toxicity is low, corruption
Corrosion is small, good operational environment.Additionally, the present invention realizes the complete alternation between electric effusion, leachate, produced without waste liquid, met
Environmental requirement.In sum, the method for the present invention is a kind of green, the method for the extraction lead of cleaning.
Brief description of the drawings
【Fig. 1】It is process chart of the invention.
Specific embodiment
Further illustrated with reference to example, following instance is intended to further illustrate the present invention and not enters one to invention
Step is limited.
Embodiment 1
Experiment concentrate of lead sulfide ore chemical composition such as table 1 used.
The chemical composition of the concentrate of lead sulfide ore of table 1
| Element | Pb | S | Fe | Ag |
| Composition/% | 48.71 | 17.32 | 7.76 | 0.0057 |
Concentrate of lead sulfide ore 250g (its chemical composition such as table 1) is taken, acid leaching solution 1200mL is added, its chemical composition is：
Pb2+110g/L, iron ion total concentration is 0.21mol/L, and pyrovinic acid concentration of dissociating is 0.4mol/L；And add the wooden sulphurs of 0.5g
Sour calcium, is polytetrafluoroethylene (PTFE) in 2000mL autoclaves inner bag, and mixing speed 550r/min is passed through oxygen and maintains pressure 0.6MPa,
React 2.5h at 130 DEG C of temperature, to solution ph 5.3, iron ion total concentration less than after 4mg/L, Separation of Neutral leachate with
Neutral leaching residue.
Neutral leaching residue adds the useless electric effusions of 1200mL, useless electric effusion composition to be：Pb2+37g/L, pyrovinic acid concentration of dissociating
It is 1.1mol/L, in 2000mL autoclaves, inner bag is polytetrafluoroethylene (PTFE), and mixing speed 500r/min is passed through oxygen and maintains pressure
0.6MPa, 1.2h is reacted at 140 DEG C of temperature.Reaction completion is separated by filtration acid leaching solution and acidic leaching residue.
Neutral leachate adds useless electric effusion 1500mL, and the electric effusion composition that gives up is：Pb2+35g/L, pyrovinic acid concentration of dissociating
It is 1.2mol/L, is made into the solution of lead content 80g/L.Ti-supported lead dioxide electric net is anode, and lead flake is negative electrode, pole span 4cm, electrodeposition
Temperature is 35 DEG C, and current density is 200A/m2Under the conditions of electrodeposition 16h, current efficiency reaches 99.90%.
Acidic leaching residue dry weight 131.0g, lead-in-dreg 1.56%, analysis result shows the leaching rate of lead up to 98.32%, and
Noble silver, gold are fully entered in leached mud.
Comparative example 1
Concentrate of lead sulfide ore 250g (its chemical composition such as table 1) is taken, acid leaching solution 1200mL is added, its chemical composition is：
Pb2+110g/L, iron ion total concentration is 0.21mol/L, and pyrovinic acid concentration of dissociating is 0.4mol/L；And add the wooden sulphurs of 0.5g
Sour calcium, is polytetrafluoroethylene (PTFE) in 2000mL autoclaves inner bag, and mixing speed 550r/min is passed through oxygen and maintains pressure 1.2MPa,
React 2.5h at 180 DEG C of temperature, to solution ph 5.3, iron ion total concentration less than after 4mg/L, Separation of Neutral leachate with
Neutral leaching residue.
Neutral leaching residue adds the useless electric effusions of 1200mL, useless electric effusion composition to be：Pb2+37g/L, pyrovinic acid concentration of dissociating
It is 1.1mol/L, in 2000mL autoclaves, inner bag is polytetrafluoroethylene (PTFE), and mixing speed 500r/min is passed through oxygen and maintains pressure
1.2Mpa, 1.2h is reacted at 180 DEG C of temperature.Reaction completion is separated by filtration acid leaching solution and acidic leaching residue.
Acidic leaching residue dry weight 221.0g, lead-in-dreg 28.56%, analysis result shows the leaching rate only 48.17% of lead, and
Noble silver has 45.64% to enter in leachate, and this is that have part sulphur to be oxidized to sulfate radical, makes lead ion into PbSO4Into
In slag.
Claims (7)
1. the method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions, it is characterised in that：Including following step
Suddenly：
1) after mixing concentrate of lead sulfide ore, surfactant with leaching agent containing sulfonic acid, it is transferred in autoclave, to being passed through oxygen in system
Gas, carries out neutral leaching, and solid-liquor separation obtains neutral leachate and neutral leaching residue；
2) the neutral leachate described in is made into lead electric effusion with useless electric effusion carries out electro-deposition lead, obtains metal stereotype with useless electrodeposition
Liquid；
3) neutral leaching residue described in mixes with acid lixiviant, is transferred in autoclave, to oxygen is passed through in system, carries out acidity
Leach, after solid-liquor separation, obtain acid leaching solution and acidic leaching residue；Described acid lixiviant is by giving up that electro-deposition lead is produced
Electric effusion supplements its free sulfonic concentration to obtaining in the range of 0.3~2.5mol/L；
4) acid leaching solution enters neutral leaching next time and uses as leaching agent containing sulfonic acid, and the acidic leaching residue is reclaimed
Elementary sulfur and noble metal.
2. the method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions according to claim 1, its
It is characterised by：The leaching agent containing sulfonic acid includes pyrovinic acid and/or ethylsulfonic acid.
3. the method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions according to claim 1, its
It is characterised by：Neutral leaching condition is：Leaching agent containing sulfonic acid is 3mL/g~15mL/g, surface with the liquid-solid ratio of concentrate of lead sulfide ore
Activating agent quality for concentrate of lead sulfide ore quality 0.05~0.5%, reaction temperature be 105~170 DEG C, mixing speed be 100~
800 revs/min, oxygen presses 0.2~1.5MPa, and the reaction time is 0.5~3h, and reaction end pH value is more than 5.0.
4. the method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of the sulfonic acid solutions according to claim 1 or 3,
It is characterized in that：Surfactant used includes at least one in ligninsulfonate, o-phenylenediamine, m-phenylene diamine (MPD).
5. the method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions according to claim 1, its
It is characterised by：The condition of the acidic leaching is：Neutral leaching residue is 3mL/g~15mL/g with the liquid-solid ratio of acid lixiviant,
Extraction temperature be 110~170 DEG C, mixing speed be 200~800 revs/min, oxygen press 0.2~1.5MPa, extraction time be 0.5~
3.0h, it is 0.1~0.8mol/L to leach terminal point control system acidity.
6. the method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions according to claim 1, its
It is characterised by：The condition of the electro-deposition lead is：Current density is 80~400A/m2, 30~65 DEG C of electric effusion temperature.
7. the method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of the sulfonic acid solutions according to claim 1 or 6,
It is characterized in that：During electro-deposition lead, with graphite cake, ti-supported lead dioxide electric net or titanium-based platinum guaze as positive plate, with lead beginning pole
Piece, titanium plate or stainless steel plate are minus plate；The minus plate periphery is more long than the positive plate 1~3 centimetre.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710097359.9A CN106834679B (en) | 2017-02-22 | 2017-02-22 | The method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710097359.9A CN106834679B (en) | 2017-02-22 | 2017-02-22 | The method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106834679A true CN106834679A (en) | 2017-06-13 |
| CN106834679B CN106834679B (en) | 2018-08-17 |
Family
ID=59133913
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710097359.9A Active CN106834679B (en) | 2017-02-22 | 2017-02-22 | The method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106834679B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110396608A (en) * | 2019-08-02 | 2019-11-01 | 中南大学 | A kind of methane sulfonic acid system bismuth sulfide concentrate oxygen leaching method |
| CN110629043A (en) * | 2019-09-04 | 2019-12-31 | 长沙有色冶金设计研究院有限公司 | Bismuth extraction method based on phase transformation of bismuth sulfide ore |
| CN112064062A (en) * | 2020-11-10 | 2020-12-11 | 矿冶科技集团有限公司 | Method for preparing crude lead by waste lead plaster without pre-desulfurization combined electrolysis |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101003854A (en) * | 2007-01-22 | 2007-07-25 | 中国科学院过程工程研究所 | New method for soaking out enriched ores of high indium, high iron, and high sulfur zinc |
| CN101113490A (en) * | 2007-09-12 | 2008-01-30 | 昆明理工大学 | Method for leaching indium from indium sulfide concentrate |
| US20140131220A1 (en) * | 2012-11-13 | 2014-05-15 | The University Of British Columbia | Recovering lead from a lead material including lead sulfide |
| WO2016183428A1 (en) * | 2015-05-13 | 2016-11-17 | Aqua Metals Inc. | Systems and methods for recovery of lead from lead acid batteries |
-
2017
- 2017-02-22 CN CN201710097359.9A patent/CN106834679B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101003854A (en) * | 2007-01-22 | 2007-07-25 | 中国科学院过程工程研究所 | New method for soaking out enriched ores of high indium, high iron, and high sulfur zinc |
| CN101113490A (en) * | 2007-09-12 | 2008-01-30 | 昆明理工大学 | Method for leaching indium from indium sulfide concentrate |
| US20140131220A1 (en) * | 2012-11-13 | 2014-05-15 | The University Of British Columbia | Recovering lead from a lead material including lead sulfide |
| WO2016183428A1 (en) * | 2015-05-13 | 2016-11-17 | Aqua Metals Inc. | Systems and methods for recovery of lead from lead acid batteries |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110396608A (en) * | 2019-08-02 | 2019-11-01 | 中南大学 | A kind of methane sulfonic acid system bismuth sulfide concentrate oxygen leaching method |
| CN110396608B (en) * | 2019-08-02 | 2021-06-18 | 中南大学 | Oxygen pressure leaching method for bismuth sulfide concentrate in methanesulfonic acid system |
| CN110629043A (en) * | 2019-09-04 | 2019-12-31 | 长沙有色冶金设计研究院有限公司 | Bismuth extraction method based on phase transformation of bismuth sulfide ore |
| CN112064062A (en) * | 2020-11-10 | 2020-12-11 | 矿冶科技集团有限公司 | Method for preparing crude lead by waste lead plaster without pre-desulfurization combined electrolysis |
| CN112064062B (en) * | 2020-11-10 | 2021-02-12 | 矿冶科技集团有限公司 | Method for preparing crude lead by waste lead plaster without pre-desulfurization combined electrolysis |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106834679B (en) | 2018-08-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106676270B (en) | A method of Whote-wet method extracts lead from lead plaster and concentrate of lead sulfide ore | |
| CN103014760B (en) | Production method of electrolytic manganese metal | |
| CN100554452C (en) | Method for extracting copper from copper-containing sulfide ore by wet process | |
| CN105200235B (en) | The method that valuable metal prepares tough cathode and LITHIUM BATTERY nickel sulfate is reclaimed from electroplating sludge | |
| CN106756008B (en) | The method that two sections of adverse current atmospheric pressure oxidations of sulfonic acid solutions leach lead in concentrate of lead sulfide ore | |
| CN107385219B (en) | Utilize the method for cyclone electrolytic cell processing nickel plated copper sludge recycling copper and mickel | |
| CN106834679B (en) | The method that lead in concentrate of lead sulfide ore is leached in two sections of adverse current pressure oxidations of sulfonic acid solutions | |
| CN107630146A (en) | nickel recovery method | |
| CN107201448B (en) | High tellurium copper Slag treatment method | |
| CN106834693A (en) | A kind of smelting zinc replacement slag wet method comprehensive reutilization method | |
| CN104775036A (en) | Method for recovering noble metal from waste titanium anodes with noble metal coatings | |
| CN107815540A (en) | A kind of method of hydrometallurgy metal nickel cobalt and its salt product | |
| WO2018014748A9 (en) | Process for preparing lead with ammonia electroreduction in ammonium chloride | |
| CN104419826B (en) | The method that ammonia soaks Zinc Oxide electrowinning zinc | |
| CN109825720B (en) | Combined metallurgy process for copper-cobalt alloy and cobalt salt mineral aggregate | |
| JPS62188791A (en) | Electrowinning method for ni, co, zn, cu, mn and cr | |
| CN107400781A (en) | A kind of recovery method of lead smelting waste material containing zinc | |
| CN110331284A (en) | A method of electrolytic manganese is prepared using pyrolusite | |
| CN105861822B (en) | A kind of acids reduction leaching method of cobalt copper mixed oxidization ore deposit | |
| CN103060842A (en) | Method for preparing electrodeposited cobalt under large flow | |
| Zheng et al. | Separation and recovery of Cu and As from copper electrolyte through electrowinning and SO2 reduction | |
| CN110055425A (en) | A kind of electroplating sludge heavy metal resources method | |
| CN109371245A (en) | Nickel refining system copper ashes recycling processing method | |
| CN100590230C (en) | Method for synchronously electrolyzing metal lead and manganese dioxide in chloride medium | |
| CN110331282B (en) | Process for dechlorinating cuprous ions by circulating in leaching solution of zinc hydrometallurgy |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |