CN101880770A - Application of extractant and method for extracting zinc from ammonia solution - Google Patents
Application of extractant and method for extracting zinc from ammonia solution Download PDFInfo
- Publication number
- CN101880770A CN101880770A CN2010102413744A CN201010241374A CN101880770A CN 101880770 A CN101880770 A CN 101880770A CN 2010102413744 A CN2010102413744 A CN 2010102413744A CN 201010241374 A CN201010241374 A CN 201010241374A CN 101880770 A CN101880770 A CN 101880770A
- Authority
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- China
- Prior art keywords
- zinc
- ammonia
- extractant
- ammonia solution
- extracting
- 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.)
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Links
- 239000011701 zinc Substances 0.000 title claims abstract description 69
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 62
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 22
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 title claims abstract description 19
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 235000011114 ammonium hydroxide Nutrition 0.000 title claims abstract description 17
- 238000000605 extraction Methods 0.000 claims abstract description 67
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000012074 organic phase Substances 0.000 claims abstract description 13
- 239000003350 kerosene Substances 0.000 claims abstract description 7
- STCOOQWBFONSKY-UHFFFAOYSA-N tributyl phosphate Chemical compound CCCCOP(=O)(OCCCC)OCCCC STCOOQWBFONSKY-UHFFFAOYSA-N 0.000 claims abstract 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 52
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 32
- 229910021529 ammonia Inorganic materials 0.000 claims description 26
- 239000003795 chemical substances by application Substances 0.000 claims description 21
- 239000011787 zinc oxide Substances 0.000 claims description 16
- 239000000839 emulsion Substances 0.000 claims description 8
- -1 dodecyl ester Chemical group 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 claims description 4
- 125000004079 stearyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 claims description 3
- 239000012071 phase Substances 0.000 abstract description 7
- 239000000284 extract Substances 0.000 abstract description 6
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 abstract description 5
- 239000002253 acid Substances 0.000 abstract description 5
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 abstract description 4
- 229960001763 zinc sulfate Drugs 0.000 abstract description 4
- 229910000368 zinc sulfate Inorganic materials 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 3
- 239000012141 concentrate Substances 0.000 abstract 2
- 229940093635 tributyl phosphate Drugs 0.000 abstract 2
- 125000005907 alkyl ester group Chemical group 0.000 abstract 1
- 238000005191 phase separation Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 13
- 238000004070 electrodeposition Methods 0.000 description 7
- 238000004945 emulsification Methods 0.000 description 5
- 238000005192 partition Methods 0.000 description 5
- 230000005501 phase interface Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000005363 electrowinning Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- HTKOEZNJRNUCKF-UHFFFAOYSA-N C(CCCCCCCCCCC)SC(C(C(C)=O)C(C)=O)=S Chemical compound C(CCCCCCCCCCC)SC(C(C(C)=O)C(C)=O)=S HTKOEZNJRNUCKF-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- BGHCVCJVXZWKCC-UHFFFAOYSA-N Tetradecane Chemical group CCCCCCCCCCCCCC BGHCVCJVXZWKCC-UHFFFAOYSA-N 0.000 description 1
- 239000003929 acidic solution Substances 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- QNDQILQPPKQROV-UHFFFAOYSA-N dizinc Chemical compound [Zn]=[Zn] QNDQILQPPKQROV-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to application of an extractant and a method for extracting zinc from ammonia solution, which comprises the following steps: adopting novel efficient extractant 2-acetyl-3-oxo-alkyl dithiophosphate acid alkyl ester, thinner sulfonated kerosene and demulsifier tri-butyl-phosphate (TBP) to form an organic phase; extracting Zn (II) from the ammonia solution; adopting sulfuric acid for back extraction, so as to separate and concentrate Zn in the solution; and then converting zinc sulfate solution so as to regenerate the organic phase. The novel efficient synthetized extractant of the invention has the following characteristics that: 1) the extracant can extract Zn from the ammonia solution with low density in the wider range of the pH value to get the concentration of Zn; and 2) the extractant has quick extracting speed, quick phase separation, no emulsify and no a third phase, and can take the sulfuric to be as the back extracant. In all, the invention can effectively, quickly, cleanly separate and concentrate Zn in the ammonia solution, is free from waste water, waste residues and exhaust emission, and is an environmental-friendly zinc extractant and a zinc extractant method.
Description
Technical field
The present invention relates to metallurgical technology field, the application that is specifically related to a kind of extraction agent reaches the method for extracting zinc from the ammonia leach liquor of zinc oxide ore or zinc oxide material.
Background technology
At present, zinc oxide ore is mainly with sulfuric acid leaching-extraction-electrodeposition process, but for the high zinc oxide ore of calcic magnesium basic gangue, then exists poor selectivity, acid big, the liquid-solid separation difficulty of consumption and purification and impurity removal burden heavily to wait technical barrier with the sulfuric acid extract technology.Therefore, this class ore is only suitable to adopt the ammonia leaching, but from ammonia solution electrowinning zinc, have only ammonium chloride system that reported in literature is arranged, but large-scale industrial application not as yet, and ammonium sulfate system and volatile salt system are not seen the document newspaper as yet.Electrowinning zinc is very sophisticated in the zinc sulfate acidic solution, but require the zinc concentration height, because it is low that the zinc oxide raw ore contains the zinc grade, zinc ion concentration can not satisfy the requirement of acid system electrodeposition process in the leach liquor, and solvent extraction is one of effective means of enrichment raising zinc ion concentration.Handle the low-grade zinc oxide ore technology so will realize ammonia process, gordian technique is effectively to realize from Zn
2+-NH
3Extract zinc in the complex solution, and then convert the sophisticated zinc sulfate acid system of electrodeposition process to, and significantly improve zinc concentration, make it to meet the electrodeposition requirement.
At present, research bibliographical information about extracting zinc from ammonia solution is few, mainly contain the agent of Lix series extraction, wherein Lix54 is best zinc extraction agent, the novel extraction agent of the HostarexDK-16 of researchs such as this extraction agent and U.S. K.S.Rao and the present invention's research and development all has β-diketone structure, but there are shortcoming in Lix54 and HostarexDK-16.The Lix54 extracting zinc when the pH of solution value is 8.5～9.0, just has higher zinc extraction yield, and at Zn-NH
3-(NH
4)
2SO
4-H
2The balance partition ratio of zinc in the O system (II) is the highest, D=4.5, and at Zn-NH
3-NH
4Cl-H
2O system and Zn-NH
3-NH
4HCO
3-H
2In the O system, the extraction equilibrium partition ratio of zinc (II) is littler, is respectively 3.0 and 1.8; And during Hostarex DK-16 extracting zinc, zinc (II) partition ratio and percentage extraction minimum, one-level extraction in the solution of pH＞8, percentage extraction is the highest has only 54%, and the viscosity of organic phase is big, divides phase velocity slow, manipulation require is more than 45 ℃.
Summary of the invention
The purpose of this invention is to provide a kind of at the application of the low ammonia solution of zinc concentration (being the ammonia leach liquor) with new and effective extraction agent 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester, and the method for extracting and separating enrichment zinc.The inventive method can be from hanging down zinc concentration (as Zn in wider pH value scope
2+In 4～25g/L) the ammonia solution zinc is rapidly and efficiently extracted enrichment, and rate of extraction is fast, phase-splitting is fast, not emulsification, third phase do not occur.
Application of the present invention is: the 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester of liquid state is used as extraction agent extracting zinc from the ammonia leach liquor of zinc oxide ore or zinc oxide material, and structural formula is:
In the formula, R is dodecyl ester～stearyl.
Above-mentioned R is dodecyl ester, tetradecane alkyl ester or cetyl ester most preferably.
2-ethanoyl-3-oxo-dithio butyric acid alkyl ester is the little liquid extraction agent of a kind of viscosity, and molecular weight is 345～429, and density is 1200～1300Kg/m
3, viscosity is less than 5.0 * 10 under the room temperature
-2PaS.
Method of the present invention is: with 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester, form organic phase extracting zinc from the ammonia leach liquor of zinc oxide ore or zinc oxide material, extraction agent: thinner with thinner (preferred sulfonated kerosene) and emulsion splitter (preferably phosphoric acid tri-n-butyl (TBP)): emulsion splitter is by 40%～60%: 35%～60%: the mixed of 0～5% volume percent; Strip with sulfuric acid, zinc is separated and enrichment.Water can be recycled.
The present invention can reach the purpose of extraction and enrichment zinc by extraction of ammonia leach liquor process and back extraction from low zinc concentration, and converts the zinc solution system to electrodeposition process sophisticated zinc sulfate acid system by ammonia gonosome system.
Ammonia leach liquor system is Zn-NH
3-(NH
4)
2SO
4-H
2O system, or Zn-NH
3-NH
4Cl-H
2O system, or Zn-NH
3-NH
4HCO
3-H
2The O system.
The technical qualification of extracting zinc are: the pH value of ammonia leach liquor is 8～11, and the total concn of ammonia and ammonium is 2～3mol/L, and ammonia concentration is 0.11～1.00mol/L.
Strip with sulfuric acid, strip liquor recycles zinc in solution and is enriched to and meets the electrodeposition requirement.The back extraction organic phase is returned extraction after regeneration, recycle, and the electrodeposition waste liquid replenishes behind the sulfuric acid as reverse-extraction agent.The extraction whole process does not have waste water and produces, and realizes cleaner production.
The present invention can realize low-grade zinc oxide ore, contain effective utilization of zinc resource of the useless ammonia solution of low zinc oxide material of zinc and low zinc concentration.
Collection zinc of the present invention agent has following characteristics: 1) can from the ammonia solution of lower concentration zinc zinc be extracted enrichment, 2 in wider pH value scope). rate of extraction is fast, and phase-splitting is fast, not emulsification, third phase do not occur, and available sulfuric acid is as reverse-extraction agent.In a word, the present invention can be efficiently, fast, zinc in the separation and concentration ammonia solution cleanly, whole process does not have waste water, waste residue and exhaust gas emission, is a kind of eco-friendly zinc extraction agent and collection zinc method.
Embodiment
Following examples are intended to illustrate the present invention rather than limitation of the invention further.
Embodiment 1:
(1) ammonia contains that the total concn of ammonia and ammonium is 2.00molL in the zinc aqueous solution
-1, ammonia concentration 0.11molL
-1, pH=8; It contains zinc and is respectively: 1. Zn-NH
3-NH
4HCO
3-H
2Zinc concentration is 6.03gL in the O solution
-12. Zn-NH
3-NH
4Cl-H
2Zinc concentration is 6.18gL in the O solution
-13. Zn-NH
3-(NH
4)
2SO
4-H
2Zinc concentration is 5.95gL in the O solution
-1
(2) extraction agent is formed: 40% (volume ratio) 2-ethanoyl-3-oxo-dithio butyric acid-dodecyl ester and 55% sulfonated kerosene and 5%TBP mix and form organic phase
(3) extraction and reextraction operational condition: at normal temperatures, by comparing A/O=1: 1 will (1) in ammonia contain the zinc aqueous solution respectively with (2) in extraction agent carry out one-level and extract, the extraction time is 5min; Use the zinciferous extracted organic phase of sulfuric acid back extraction then, by comparing A/O=1: 1 carries out three grades of back extractions, and the back extraction time is 3min.
(4) extraction and back extraction result: extraction and back extraction phase-splitting are fast, and no emulsification or third phase produce, and phase interface is clear; Zn-NH
3-NH
4HCO
3-H
2O solution, zinc extraction yield are 90.63%, partition ratio D=9.7, and three grades of back extraction ratios are near 98%; Zn-NH
3-NH
4Cl-H
2O solution, zinc extraction yield are 91.05%, distribution ratio D=10.2, and three grades of back extraction ratios of zinc reach more than 97%; Zn-NH
3-(NH
4)
2SO
4-H
2O solution, zinc extraction yield is up to 92.47%, partition ratio D=12.3, and three grades of back extraction ratios of zinc reach more than 97%.
Embodiment 2:
Zn-NH
3-(NH
4)
2SO
4-H
2O solution, wherein zinc concentration is 11.20gL
-1, ammonia and ammonium total concn are 3molL
-1, ammonia concentration 1.00molL
-1, pH=11.Form organic phase with 50% (volume ratio) 2-ethanoyl-3-oxo-dithio butyric acid-cetyl ester alkane and 50% sulfonated kerosene.At normal temperatures, by comparing A/O=2: 1 carries out one-level with water extracts, and the extraction time is 5min; The zinciferous extracted organic phase of sulfuric acid back extraction, by comparing A/O=1: 1 carries out three grades of back extractions, and the back extraction time is 3min.Zinc one-level percentage extraction all 〉=95% is up to 98.2%, distribution ratio D 〉=19, and the back extraction of zinc one-level can be up to more than 97% after having only 58.1%, three grade of back extraction.Extraction and back extraction phase-splitting are fast, and phase interface is clear, and no emulsification or third phase produce.
Embodiment 3:
Zn-NH
3-(NH
4)
2SO
4-H
2O solution, wherein zinc concentration is 16.680gL
-1, ammonia and ammonium total concn are 2.13molL
-1, ammonia concentration 0.24molL
-1, pH=9.With 60% (volume ratio) 2-ethanoyl-3-oxo-dithio butyric acid-tetradecyl ester alkane and 36% sulfonated kerosene and 4%TBP mixing composition organic phase.At normal temperatures, by comparing A/O=2: 1 carries out one-level with water extracts, and the extraction time is 5min; Carry out back extraction with sulfuric acid then, by comparing A/O=1: 1 carries out three grades of back extractions, and the back extraction time is 3min.Zinc one-level percentage extraction all 〉=97% is up to 99.12%, and distribution ratio D 〉=32.3 are up to 112.6; Can be after three grades of back extractions up to more than 97%; Extraction and back extraction phase-splitting are fast, and phase interface is clear, and no emulsification or third phase produce.Behind three grades of cycling extraction zinc, zinc concentration can reach 46.88gL in the strip aqueous
-1
Claims (8)
1. the method for an extracting zinc from ammonia solution, it is characterized in that, the extraction agent that is adopted is liquid 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester, and form organic phase extracting zinc from the ammonia leach liquor of zinc oxide ore or zinc oxide material, extraction agent: thinner with thinner and emulsion splitter: emulsion splitter is by 40%～60%: 35%～60%: the mixed of 0～5% volume percent; Strip with sulfuric acid, zinc is separated and enrichment; Extraction agent 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester, structural formula is:
In the formula, R is dodecyl ester～stearyl.
2. according to claim 1 from ammonia solution the method for extracting zinc, it is characterized in that ammonia leach liquor system is Zn-NH
3-(NH
4)
2SO
4-H
2O system, or Zn-NH
3-NH
4Cl-H
2O system, or Zn-NH
3-NH
4HCO
3-H
2The O system.
3. according to claim 1 and 2 from ammonia solution the method for extracting zinc, it is characterized in that the pH value of ammonia leach liquor is 8～11, the total concn of ammonia and ammonium is 2～3mol/L, ammonia concentration is 0.11～1.00mol/L.
4. according to claim 1 from ammonia solution the method for extracting zinc, it is characterized in that make thinner with sulfonated kerosene, tributyl phosphate is made emulsion splitter.
5.2-the application of ethanoyl-3-oxo-dithio butyric acid alkyl ester is characterized in that, with the 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester of the liquid state extraction agent as extracting zinc from the ammonia leach liquor of zinc oxide ore or zinc oxide material;
Described 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester has following structural formula:
In the formula, R is dodecyl ester～stearyl.
6. application according to claim 5 is characterized in that, 2-ethanoyl-3-oxo-dithio butyric acid alkyl ester and thinner and emulsion splitter are formed organic phase and be used to extract Zn.
7. application according to claim 6 is characterized in that organic phase is pressed extraction agent: thinner: emulsion splitter=40%～60%: 35%～60%: the mixed of 0～5% volume percent.
8. application according to claim 7 is characterized in that, thinner is a sulfonated kerosene, and emulsion splitter is a tributyl phosphate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102413744A CN101880770B (en) | 2010-07-30 | 2010-07-30 | Application of extractant and method for extracting zinc from ammonia solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102413744A CN101880770B (en) | 2010-07-30 | 2010-07-30 | Application of extractant and method for extracting zinc from ammonia solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101880770A true CN101880770A (en) | 2010-11-10 |
| CN101880770B CN101880770B (en) | 2012-05-09 |
Family
ID=43052910
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102413744A Expired - Fee Related CN101880770B (en) | 2010-07-30 | 2010-07-30 | Application of extractant and method for extracting zinc from ammonia solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101880770B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103710547A (en) * | 2013-12-25 | 2014-04-09 | 昆明理工大学 | Method for extracting zinc from zinc ammonia leaching liquid |
| CN109234530A (en) * | 2018-09-11 | 2019-01-18 | 福建紫金选矿药剂有限公司 | A kind of high-performance extraction diluent |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4563256A (en) * | 1984-12-31 | 1986-01-07 | Henkel Corporation | Solvent extraction process for recovery of zinc |
| CN101503760A (en) * | 2009-03-13 | 2009-08-12 | 昆明理工大学 | Method for extracting zinc from zinc oxide ore ammonia leaching solution |
| CN101565777A (en) * | 2009-05-18 | 2009-10-28 | 中南大学 | Method capable of increasing extraction rate of zinc in ammoniacal liquid |
-
2010
- 2010-07-30 CN CN2010102413744A patent/CN101880770B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4563256A (en) * | 1984-12-31 | 1986-01-07 | Henkel Corporation | Solvent extraction process for recovery of zinc |
| CN101503760A (en) * | 2009-03-13 | 2009-08-12 | 昆明理工大学 | Method for extracting zinc from zinc oxide ore ammonia leaching solution |
| CN101565777A (en) * | 2009-05-18 | 2009-10-28 | 中南大学 | Method capable of increasing extraction rate of zinc in ammoniacal liquid |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103710547A (en) * | 2013-12-25 | 2014-04-09 | 昆明理工大学 | Method for extracting zinc from zinc ammonia leaching liquid |
| CN103710547B (en) * | 2013-12-25 | 2016-03-30 | 昆明理工大学 | A kind of method of extracting zinc in zinc ammonia leaching solution |
| CN109234530A (en) * | 2018-09-11 | 2019-01-18 | 福建紫金选矿药剂有限公司 | A kind of high-performance extraction diluent |
| CN109234530B (en) * | 2018-09-11 | 2023-12-08 | 福建紫金选矿药剂有限公司 | High-performance extraction diluent |
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| Publication number | Publication date |
|---|---|
| CN101880770B (en) | 2012-05-09 |
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Granted publication date: 20120509 |