CN105803191A - Zinc and iron separation method in zinc hydrometallurgy process - Google Patents
Zinc and iron separation method in zinc hydrometallurgy process Download PDFInfo
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- CN105803191A CN105803191A CN201610275924.1A CN201610275924A CN105803191A CN 105803191 A CN105803191 A CN 105803191A CN 201610275924 A CN201610275924 A CN 201610275924A CN 105803191 A CN105803191 A CN 105803191A
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 125
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 119
- 239000011701 zinc Substances 0.000 title claims abstract description 118
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 238000000034 method Methods 0.000 title claims abstract description 91
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 54
- 238000009854 hydrometallurgy Methods 0.000 title claims abstract description 33
- 238000000926 separation method Methods 0.000 title claims abstract description 19
- 238000002386 leaching Methods 0.000 claims abstract description 75
- 239000007788 liquid Substances 0.000 claims abstract description 67
- 239000002253 acid Substances 0.000 claims abstract description 58
- 239000002893 slag Substances 0.000 claims abstract description 48
- 229910052738 indium Inorganic materials 0.000 claims abstract description 30
- APFVFJFRJDLVQX-UHFFFAOYSA-N indium atom Chemical compound [In] APFVFJFRJDLVQX-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000012141 concentrate Substances 0.000 claims abstract description 23
- 229910052802 copper Inorganic materials 0.000 claims abstract description 21
- 239000010949 copper Substances 0.000 claims abstract description 21
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000000605 extraction Methods 0.000 claims abstract description 9
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910052709 silver Inorganic materials 0.000 claims abstract description 8
- 239000004332 silver Substances 0.000 claims abstract description 8
- KFZAUHNPPZCSCR-UHFFFAOYSA-N iron zinc Chemical compound [Fe].[Zn] KFZAUHNPPZCSCR-UHFFFAOYSA-N 0.000 claims description 21
- HVMJUDPAXRRVQO-UHFFFAOYSA-N copper indium Chemical compound [Cu].[In] HVMJUDPAXRRVQO-UHFFFAOYSA-N 0.000 claims description 20
- FOIXSVOLVBLSDH-UHFFFAOYSA-N Silver ion Chemical compound [Ag+] FOIXSVOLVBLSDH-UHFFFAOYSA-N 0.000 claims description 5
- 230000001174 ascending effect Effects 0.000 claims description 5
- 238000007654 immersion Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 229940083025 silver preparation Drugs 0.000 claims description 5
- 238000011084 recovery Methods 0.000 abstract description 13
- 238000005516 engineering process Methods 0.000 abstract description 5
- 230000007935 neutral effect Effects 0.000 abstract description 5
- 238000005868 electrolysis reaction Methods 0.000 abstract 2
- 239000012530 fluid Substances 0.000 abstract 2
- 238000005188 flotation Methods 0.000 abstract 1
- 229910052717 sulfur Inorganic materials 0.000 description 16
- 239000011593 sulfur Substances 0.000 description 16
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 15
- 239000000284 extract Substances 0.000 description 9
- 238000003723 Smelting Methods 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 229910001308 Zinc ferrite Inorganic materials 0.000 description 4
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- WGEATSXPYVGFCC-UHFFFAOYSA-N zinc ferrite Chemical compound O=[Zn].O=[Fe]O[Fe]=O WGEATSXPYVGFCC-UHFFFAOYSA-N 0.000 description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 3
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical group [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 3
- 239000005083 Zinc sulfide Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 3
- 229910052935 jarosite Inorganic materials 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000002791 soaking Methods 0.000 description 3
- 238000000638 solvent extraction Methods 0.000 description 3
- 150000003751 zinc Chemical class 0.000 description 3
- 238000009858 zinc metallurgy Methods 0.000 description 3
- 229910052984 zinc sulfide Inorganic materials 0.000 description 3
- DRDVZXDWVBGGMH-UHFFFAOYSA-N zinc;sulfide Chemical compound [S-2].[Zn+2] DRDVZXDWVBGGMH-UHFFFAOYSA-N 0.000 description 3
- 229910052598 goethite Inorganic materials 0.000 description 2
- 229910052595 hematite Inorganic materials 0.000 description 2
- 239000011019 hematite Substances 0.000 description 2
- AEIXRCIKZIZYPM-UHFFFAOYSA-M hydroxy(oxo)iron Chemical compound [O][Fe]O AEIXRCIKZIZYPM-UHFFFAOYSA-M 0.000 description 2
- NJWNEWQMQCGRDO-UHFFFAOYSA-N indium zinc Chemical compound [Zn].[In] NJWNEWQMQCGRDO-UHFFFAOYSA-N 0.000 description 2
- PJXISJQVUVHSOJ-UHFFFAOYSA-N indium(iii) oxide Chemical compound [O-2].[O-2].[O-2].[In+3].[In+3] PJXISJQVUVHSOJ-UHFFFAOYSA-N 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- -1 it is to avoid scum Substances 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 235000010269 sulphur dioxide Nutrition 0.000 description 2
- 239000011787 zinc oxide Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- SURQXAFEQWPFPV-UHFFFAOYSA-L iron(2+) sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Fe+2].[O-]S([O-])(=O)=O SURQXAFEQWPFPV-UHFFFAOYSA-L 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 238000010409 ironing Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000001089 mineralizing effect Effects 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052950 sphalerite Inorganic materials 0.000 description 1
- 239000004291 sulphur dioxide Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 229910000859 α-Fe Inorganic materials 0.000 description 1
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
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
-
- 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
- C22B15/0065—Leaching or slurrying
- C22B15/0067—Leaching or slurrying with acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/20—Obtaining zinc otherwise than by distilling
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/20—Obtaining zinc otherwise than by distilling
- C22B19/22—Obtaining zinc otherwise than by distilling with leaching with acids
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B58/00—Obtaining gallium or indium
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
The invention relates to a zinc and iron separation method in the zinc hydrometallurgy process and belongs to the technical field of hydrometallurgy. Firstly, zinc concentrate is subjected to low-temperature roasting to obtain zinc calcine; then the zinc calcine, zinc hydrometallurgy electrolysis post-liquid and produced weak acid fluid are subjected to neutral leaching, and neutral leachate containing 20 mg/L or less of iron and neutral leached residues are produced; the obtained neutral leached residues and indium and copper extraction post-liquid are mixed to be subjected to weak-acid leaching, and weak acid fluid containing 1 g/L or less of iron and weak acid residues are produced; the obtained weak acid residues are subjected to the silver flotation process, and silver concentrate and zinc and iron slag are produced; the obtained zinc and iron slag and zinc hydrometallurgy electrolysis post-liquid are subjected to high-temperature high-pressure leaching, and high-iron slag and high-pressure leachate containing 10 g/L or less of iron are produced; and the obtained high-pressure leachate is subjected to separation for recovery of copper and indium, and indium and copper extraction post-liquid is obtained in the process. According to the zinc and iron separation method, the leaching technology combining traditional hydrometallurgy leaching with pressure leaching is adopted, the leaching process is enhanced, and the slag treatment and deironing process is simplified, so that the zinc leaching rate is high, and the deironing efficiency is high.
Description
Technical field
The present invention relates to a kind of Zinc Hydrometallurgy Process zinc-iron separation method, belong to technical field of wet metallurgy.
Background technology
Marmatite is in mineralizing process, ferrum, indium replace the zinc atom in sphalerite with isomorph, adopt machinery ore grinding to be difficult to the method for ore dressing make zinc, ferrum, indium separate, cause that the zinc concentrate iron content of ore dressing output is higher, and be associated with the metals such as the indium of high level, copper.The zinc concentrate usual zinc grade of this high ferro is relatively low, and indium, copper content are high, and associate lead content is low.
In smelting process, inlay due to the ferrum in zinc concentrate and zinc and coexist, when roasting, inevitably produce a large amount of zinc ferrites.Conventional leaching flow process, zinc ferrite is not destroyed in meutral innersion process, and the zinc oxide not being dissolved, and most ferrum, indium, copper are stayed in neutral leaching residue.
In order to destroy zinc ferrite to reclaim zinc and indium, rotary kiln evaporation method or hot acid leaching-out technique generally need to be adopted to process.Rotary kiln evaporation method can effectively destroy zinc ferrite, output zinc oxide and Indium sesquioxide. and return zinc metallurgy flow process recovery zinc indium.But, rotary kiln evaporation method energy consumption is high, and zinc indium recovery is low, and a large amount of copper enter kiln slag, it is difficult to reclaim, and volatilization process output low concentration sulphur dioxide flue gas is difficult to administer.Hot acid leaches a kind of effective ways being to destroy zinc ferrite, and zinc, ferrum, indium together enter in solution, and ferrum major part is with Fe3+Form exists, and causes ferrum difficult separation and recycling.At present, the method separating ferrum from this solution is mainly jarosite process, goethite process and hematite process.When adopting jarosite process separation ferrum, indium and ferrum together enter Jarosite Residues, then adopt volatility process recovery indium from iron vitriol slag.Goethite process needs first by the Fe in solution3+It is reduced to Fe2+, with neutralizing hydrolysis method recovery indium, obtain indium slag.After heavy indium, liquid continues to be neutralized to pH is 2.5～4.2, adopts air oxidation deironing, obtain goethitum slag under 85～90 DEG C of conditions.But, it is low that above two hot acid leaches method for removing iron scum iron content, and the quantity of slag is big, and the scum obtained cannot utilize.Hematite process can effectively raise the response rate of zinc, indium, and fully utilizes the ferrum in mineral, but due to the particularity of bloodstone technique, only Iijima smeltery, autumn fields of Japan is successfully applied to commercial production at present.
Pressurization direct oxidation acid leaching process can directly process zinc sulfide concentrates, there is technological process short, zinc leaching rate high, but gained leached mud to be the low lead of high-sulfur high ferro low silver slag, need to increase sulfur floatation process, and when processing high ferro high-copper material, there is copper leaching rate and be difficult to control to, ferrum leaching rate is higher, it is necessary to the problems such as the heavy ferrum of secondary.Shi Youfu etc. adopt hot acid leachate Leaching Zinc concentrate in autoclave of conventional wet zine-smelting plant in " adopting pressure leaching process to optimize conventional wet zinc metallurgy flow process research " literary composition, application meutral innersion-hot acid leaching-hot acid leachate and zinc concentrate pressure leaching process, achieve the combination of pressure leaching and conventional wet zinc metallurgy, but its core process core remains the pressure leaching of zinc concentrate, its leached mud is identical with character with the pressure leaching process composition that applicable industry is put into practice, and equally exists slag for comprehensive and recycles the problem with harmless treatment.Therefore, the process of zinc leaching residue, efficiently separating of zinc-iron are that Zinc Hydrometallurgy Process perplexs zinc abstraction enterprise and the key problem of vast researcher for a long time.
Summary of the invention
For above-mentioned prior art Problems existing and deficiency, the present invention provides a kind of Zinc Hydrometallurgy Process zinc-iron separation method.This method adopts conventional wet to leach and pressure leaching combination extract technology, Strengthen education process, simplify Slag treatment and iron removal, zinc leaching rate is high, de-ironing efficiency is high, solve recovery rate of valuable metals in the iron removal step that Zinc Hydrometallurgy Process exists for a long time low, the problems such as slag environmental pollution, the present invention is achieved through the following technical solutions.
A kind of Zinc Hydrometallurgy Process zinc-iron separation method, it specifically comprises the following steps that
(1) zinc concentrate low-temperature bake obtains zinc calcine；
(2) weak acid liquid of zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output carries out meutral innersion, the middle immersion less than 20mg/L of the output iron content and middle leaching slag；
(3) after middle leaching slag step (2) obtained and the iron content of step (6) the output extraction indium copper less than 10g/L, liquid mixing carries out weak-acid leaching, the output iron content weak acid liquid less than 1g/L and weak acid slag；
(4) the weak acid slag that step (3) obtains is carried out silver floatation process, output silver preparation concentrate and zinc-iron slag；
(5) zinc-iron slag step (4) obtained and zinc hydrometallurgy electrolytic liquid are 1:3～4kg/L according to rate of charge, temperature be 150～200 DEG C, pressure be the saturated vapor pressure under 0.5～1.5MPa(corresponding temperature) carry out high pressure under condition and leach 2～4h, output height scum and the iron content high pressure leaching liquid less than 10g/L；
(6) the high pressure leaching liquid recovering copper that step (5) obtained, indium, obtain liquid after the iron content extraction indium copper less than 10g/L in the process.
The detailed process of described step (2) is: be 1:3～4:2～3kg/L/L by the weak acid liquid of zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output according to rate of charge, is meutral innersion 1.5～2.5h under 60～70 DEG C of conditions in temperature.
The detailed process of described step (3) is: by middle leaching slag with to extract after indium copper liquid according to rate of charge be 1:3～4kg/L, it is carry out weak-acid leaching 4～6h under 80～90 DEG C of conditions in temperature, adding zinc calcine in the process, the addition of zinc calcine is that every ascending takes liquid 50～70g after indium copper.
The high pressure leaching liquid sulfur acid 30～40g/L of above-mentioned steps (5) output.
The high scum of above-mentioned steps (5) output containing zinc less than 2wt%, iron content 40～50wt%.
The invention has the beneficial effects as follows:
(1) metal recovery rate is high.The present invention adopts low temperature calcining-conventional wet to leach and pressure leaching combination extract technology, Strengthen education process, solves pressure leaching process heat energy source problem, it is achieved that total leaching rate of zinc is more than 99%, total leaching rate of indium is more than 95%, and total leaching rate of copper is more than 98%.
(2) technological process is simple.Relative thermal Ore Leaching of the present invention-heavy iron process, achieve leaching to be synchronously performed with heavy ferrum, the reducing agent such as concentrate or the sulfur dioxide reduction ferric iron that first adds eliminating hot acid liquid is ferrous iron, the more oxidizing ferrous iron such as oxygen is the operation that ferric iron carries out heavy ferrum, simplifies technical process；The direct oxygen leaching technique of relative zinc concentrate, it is to avoid scum, sulfur slag and lead smelting gas coexist, and high pressure leaching process is without logical oxygen, and in leachate, iron content is low, and major part is ferrum at a low price, is conducive to the postorder of solution to process.
(3) smelting process clean and effective.The present invention adopts High Temperature High Pressure to leach the leached mud of conventional wet extract technology, leaches terminal acidity by controlling, it is achieved efficiently leaching and the synchronous precipitation of major part ferrum of zinc, eliminate traditional Rotary Kiln technique, it is to avoid smoke pollution.
Detailed description of the invention
Below in conjunction with detailed description of the invention, the invention will be further described.
Zinc sulfide concentrates is raw material, and its composition (wt%) is as follows: Zn45.23, Fe13.79, S31.83, Cu0.73, In0.0395, Ag0.0081, Pd0.45.The zinc calcine of following composition (wt.%) is obtained: Zn51.78, Fe16.58, S3.06, Cu0.92, In0.0458, Ag0.0097, Pd0.56 through low-temperature bake.The following examples are all with above-mentioned zinc sulfide concentrates and zinc calcine for raw material.
Embodiment 1
This Zinc Hydrometallurgy Process zinc-iron separation method, it specifically comprises the following steps that
(1) zinc concentrate low-temperature bake 5h at 850 ~ 900 DEG C obtains zinc calcine；
(2) weak acid liquid (containing zinc 150g/L, iron content 0.8g/L) of 100kg zinc calcine, zinc hydrometallurgy electrolytic liquid (containing zinc 45g/L, sulfur acid 160g/L) and step (3) output carries out meutral innersion, the middle immersion (containing zinc 152g/L, cupric 0.6g/L, iron content 15mg/L) less than 20mg/L of the output iron content and middle leaching slag (containing zinc 21wt%, iron content 29wt%)；Detailed process is: be 1:4:2Lkg/L/L by the weak acid liquid of zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output according to rate of charge, is meutral innersion 2h under 60 DEG C of conditions in temperature；
(3) after soaking the extraction indium copper of slag and step (6) output in 61kg step (2) obtained, liquid (containing zinc 106g/L, sulfur acid 30g/L, iron content 6.5g/L) mixing carries out weak-acid leaching, the output iron content weak acid liquid (containing zinc 150g/L, cupric 0.6g/L, iron content 0.8g/L) less than 1g/L and weak acid slag (containing zinc 18wt%, iron content 32wt%)；The detailed process of step (3) is: by middle leaching slag with to extract after indium copper liquid according to rate of charge be 1:3.3kg/L, is carry out weak-acid leaching 6h under 80 DEG C of conditions in temperature, adds zinc calcine in the process, and the addition of zinc calcine is that every ascending takes liquid 50g after indium copper；
(4) the weak acid slag that step (3) obtains is carried out silver floatation process, output silver preparation concentrate and zinc-iron slag；
(5) 65kg zinc-iron slag step (4) obtained and 200L zinc hydrometallurgy electrolytic liquid (containing zinc 45g/L, sulfur acid 160g/L) are 1:3.1kg/L according to rate of charge, temperature be 150 DEG C, pressure carry out high pressure when being 0.5MPa and leach 4h, high pressure leaching liquid less than 10g/L of output height scum (iron content 43wt%, containing zinc 1.41wt%, leaded 1.26wt%, sulfur-bearing 2.31wt%) and iron content (containing zinc 104g/L, sulfur acid 30g/L, containing indium 0.15g/L, cupric 1.26g/L, iron content 5.9g/L)；
(6) the high pressure leaching liquid recovering copper that step (5) obtained (adopts method of cementation to be directly separating recovery copper), indium (solvent extraction directly extracts separation and recovery indium), obtains in the process and extracts liquid (containing zinc 106g/L, sulfur acid 30g/L, iron content 6.5g/L) after indium copper.
After above-mentioned steps processes, total leaching rate of zinc is 99%, and total leaching rate of indium is 96%, and total leaching rate of copper is 97%.
Embodiment 2
This Zinc Hydrometallurgy Process zinc-iron separation method, it specifically comprises the following steps that
(1) zinc concentrate low-temperature bake 5h at 850 ~ 900 DEG C obtains zinc calcine；
(2) weak acid liquid (containing zinc 151g/L, iron content 0.3g/L) of 100kg zinc calcine, zinc hydrometallurgy electrolytic liquid (containing zinc 45g/L, sulfur acid 160g/L) and step (3) output carries out meutral innersion, the middle immersion (containing zinc 153g/L, cupric 0.5g/L, iron content 8mg/L) less than 20mg/L of the output iron content and middle leaching slag (containing zinc 23wt%, iron content 27wt%)；Detailed process is: be 1:3.6:2.5Lkg/L/L by the weak acid liquid of zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output according to rate of charge, is meutral innersion 1.5h under 70 DEG C of conditions in temperature；
(3) after soaking the extraction indium copper of slag and step (6) output in 65kg step (2) obtained, liquid (containing zinc 108g/L, sulfur acid 40g/L, iron content 4.6g/L) mixing carries out weak-acid leaching, the output iron content weak acid liquid (containing zinc 151g/L, cupric 0.5g/L, iron content 0.3g/L) less than 1g/L and weak acid slag (containing zinc 19wt%, iron content 31wt%)；The detailed process of step (3) is: by middle leaching slag with to extract after indium copper liquid according to rate of charge be 1:3.8kg/L, is carry out weak-acid leaching 4h under 90 DEG C of conditions in temperature, adds zinc calcine in the process, and the addition of zinc calcine is that every ascending takes liquid 68g after indium copper；
(4) the weak acid slag that step (3) obtains is carried out silver floatation process, output silver preparation concentrate and zinc-iron slag；
(5) 69kg zinc-iron slag step (4) obtained and 250L zinc hydrometallurgy electrolytic liquid (containing zinc 45g/L, sulfur acid 160g/L) are 1:3.6kg/L according to rate of charge, temperature be 200 DEG C, pressure carry out high pressure when being 1.5MPa and leach 2h, high pressure leaching liquid less than 10g/L of output height scum (iron content 49wt%, containing zinc 1.32wt%, leaded 1.08wt%, sulfur-bearing 1.97wt%) and iron content (containing zinc 109g/L, sulfur acid 40g/L, containing indium 0.11g/L, cupric 1.33g/L, iron content 4.2g/L)；
(6) the high pressure leaching liquid recovering copper that step (5) obtained (adopts method of cementation to be directly separating recovery copper), indium (solvent extraction directly extracts separation and recovery indium), obtains in the process and extracts liquid (containing zinc 108g/L, sulfur acid 40g/L, iron content 4.6g/L) after indium copper.
After above-mentioned steps processes, total leaching rate of zinc is 99%, and total leaching rate of indium is 95%, and total leaching rate of copper is 96%.
Embodiment 3
This Zinc Hydrometallurgy Process zinc-iron separation method, it specifically comprises the following steps that
(1) zinc concentrate low-temperature bake 5h at 850 ~ 900 DEG C obtains zinc calcine；
(2) weak acid liquid of 100kg zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output carries out meutral innersion, the middle immersion less than 20mg/L of the output iron content and middle leaching slag；Detailed process is: be 1:3:3Lkg/L/L by the weak acid liquid of zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output according to rate of charge, is meutral innersion 2.5h under 65 DEG C of conditions in temperature；
(3) after soaking the extraction indium copper of slag and step (6) output in 100kg step (2) obtained, liquid mixing carries out weak-acid leaching, the output iron content weak acid liquid less than 1g/L；The detailed process of step (3) is: by middle leaching slag with to extract after indium copper liquid according to rate of charge be 1:3kg/L, is carry out weak-acid leaching 5h under 85 DEG C of conditions in temperature, adds zinc calcine in the process, and the addition of zinc calcine is that every ascending takes liquid 55g after indium copper；
(4) the weak acid slag that step (3) obtains is carried out silver floatation process, output silver preparation concentrate and zinc-iron slag；
(5) 69kg zinc-iron slag step (4) obtained and zinc hydrometallurgy electrolytic liquid are 1:3.6kg/L according to rate of charge, temperature be 170 DEG C, pressure carries out high pressure and leaches 3h, output height scum and the iron content high pressure leaching liquid less than 10g/L when being 0.8MPa；
(6) the high pressure leaching liquid recovering copper that step (5) obtained (adopts method of cementation to be directly separating recovery copper), indium (solvent extraction directly extracts separation and recovery indium), obtains in the process and extracts liquid after indium copper.
After above-mentioned steps processes, total leaching rate of zinc is 99%, and total leaching rate of indium is 97%, and total leaching rate of copper is 97%.
Above the specific embodiment of the present invention is explained in detail, but the present invention is not limited to above-mentioned embodiment, in the ken that those of ordinary skill in the art possess, it is also possible under the premise without departing from present inventive concept, make various change.
Claims (3)
1. a Zinc Hydrometallurgy Process zinc-iron separation method, it is characterised in that specifically comprise the following steps that
(1) zinc concentrate low-temperature bake obtains zinc calcine；
(2) weak acid liquid of zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output carries out meutral innersion, the middle immersion less than 20mg/L of the output iron content and middle leaching slag；
(3) after middle leaching slag step (2) obtained and the iron content of step (6) the output extraction indium copper less than 10g/L, liquid mixing carries out weak-acid leaching, the output iron content weak acid liquid less than 1g/L and weak acid slag；
(4) the weak acid slag that step (3) obtains is carried out silver floatation process, output silver preparation concentrate and zinc-iron slag；
(5) zinc-iron slag step (4) obtained and zinc hydrometallurgy electrolytic liquid are 1:3～4kg/L according to rate of charge, temperature be 150～200 DEG C, pressure carries out high pressure and leaches 2～4h, output height scum and the iron content high pressure leaching liquid less than 10g/L when being 0.5～1.5MPa；
(6) the high pressure leaching liquid recovering copper that step (5) obtained, indium, obtain liquid after the iron content extraction indium copper less than 10g/L in the process.
2. Zinc Hydrometallurgy Process zinc-iron separation method according to claim 1, it is characterized in that: the detailed process of described step (2) is: be 1:3～4:2～3kg/L/L by the weak acid liquid of zinc calcine, zinc hydrometallurgy electrolytic liquid and step (3) output according to rate of charge, be meutral innersion 1.5～2.5h under 60～70 DEG C of conditions in temperature.
3. Zinc Hydrometallurgy Process zinc-iron separation method according to claim 1, it is characterized in that: the detailed process of described step (3) is: by middle leaching slag with to extract after indium copper liquid according to rate of charge be 1:3～4kg/L, it is carry out weak-acid leaching 4～6h under 80～90 DEG C of conditions in temperature, adding zinc calcine in the process, the addition of zinc calcine is that every ascending takes liquid 50～70g after indium copper.
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