CN104313320A - Saturated crystal separation method for zinc and magnesium in zinc electrolyte by using strong acid - Google Patents
Saturated crystal separation method for zinc and magnesium in zinc electrolyte by using strong acid Download PDFInfo
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- CN104313320A CN104313320A CN201410567990.7A CN201410567990A CN104313320A CN 104313320 A CN104313320 A CN 104313320A CN 201410567990 A CN201410567990 A CN 201410567990A CN 104313320 A CN104313320 A CN 104313320A
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- Prior art keywords
- zinc
- magnesium
- strong acid
- electrolyte
- zinc electrolyte
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- 239000011701 zinc Substances 0.000 title claims abstract description 64
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 52
- 239000003792 electrolyte Substances 0.000 title claims abstract description 31
- 239000011777 magnesium Substances 0.000 title claims abstract description 20
- 239000002253 acid Substances 0.000 title claims abstract description 17
- 238000000926 separation method Methods 0.000 title claims abstract description 17
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims abstract description 13
- 229910052749 magnesium Inorganic materials 0.000 title claims abstract description 13
- 229920006395 saturated elastomer Polymers 0.000 title claims abstract description 9
- 239000013078 crystal Substances 0.000 title abstract 2
- 238000000034 method Methods 0.000 claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 238000002156 mixing Methods 0.000 claims abstract description 10
- 238000003756 stirring Methods 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 6
- PGTXKIZLOWULDJ-UHFFFAOYSA-N [Mg].[Zn] Chemical compound [Mg].[Zn] PGTXKIZLOWULDJ-UHFFFAOYSA-N 0.000 claims description 18
- 239000006228 supernatant Substances 0.000 claims description 13
- 238000005868 electrolysis reaction Methods 0.000 claims description 10
- 239000011259 mixed solution Substances 0.000 claims description 10
- 239000002244 precipitate Substances 0.000 claims description 8
- 238000002425 crystallisation Methods 0.000 claims description 7
- 230000008025 crystallization Effects 0.000 claims description 7
- 238000003723 Smelting Methods 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- 239000002893 slag Substances 0.000 claims description 6
- 241001062472 Stokellia anisodon Species 0.000 claims description 5
- 239000004568 cement Substances 0.000 claims description 5
- 238000007667 floating Methods 0.000 claims description 5
- 238000012545 processing Methods 0.000 claims description 2
- 239000002699 waste material Substances 0.000 abstract description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 10
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 abstract description 6
- 239000002351 wastewater Substances 0.000 abstract description 6
- 239000000654 additive Substances 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000001556 precipitation Methods 0.000 abstract description 4
- 229910052943 magnesium sulfate Inorganic materials 0.000 abstract description 3
- 235000019341 magnesium sulphate Nutrition 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000012535 impurity Substances 0.000 abstract description 2
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 abstract description 2
- 229960001763 zinc sulfate Drugs 0.000 abstract description 2
- 229910000368 zinc sulfate Inorganic materials 0.000 abstract description 2
- 238000006386 neutralization reaction Methods 0.000 abstract 1
- 239000008151 electrolyte solution Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000002000 scavenging effect Effects 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000010563 solid-state fermentation Methods 0.000 description 1
- 238000012549 training Methods 0.000 description 1
- 238000004065 wastewater treatment 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
- Electrolytic Production Of Metals (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a saturated crystal separation method for zinc and magnesium in zinc electrolyte by using strong acid. The method comprises the following steps: mixing by using strong acid; stirring and swirling; carrying out precipitation separation; reusing separated matters and the like. The method disclosed by the invention can be used for separating zinc and magnesium in the zinc electrolyte due to a phenomenon that zinc sulfate and magnesium sulfate can be massively and quickly separated out under a special high-temperature and high acid condition. In the whole production process, no impurities are imported without discharge of wastewater and water residues and sulfuric acid in the flow can be fully recycled, so that the electrolytic waste liquid is fully recovered without discharge, the environmental expense of wastewater and waste residue by the conventional neutralization precipitation method and the consumption of additives are saved, and the electric consumption can be effectively lowered. The method disclosed by the invention is simple and convenient in process, short in flow, easy to operate, investment-saving and low in consumption. The additives and the treated electrolytic waste liquid can be fully recycled, so that rational utilization and maximum benefit of enterprise resources are fully achieved and relatively good economic and social benefits are obtained.
Description
Technical field
The invention belongs to the electrolytic zinc technical field of hydrometallurgy industry, be specifically related to the strong acid saturated crystallization separation method of zinc-magnesium in a kind of zinc electrolyte.
Background technology
In zinc electrolysis production process, inevitably containing the foreign metal such as lead, nickel, copper, magnesium in raw material zinc ore, to electrolytic zinc quality influence very greatly, the current efficiency when magnesium elements wherein in zinc liquid can have a strong impact on electrolysis and the purity of electrolytic zinc product.Along with constantly carrying out of electrolytic process, Zn content in electrolytic solution will constantly reduce, sulfuric acid content constantly increases, in order to keep the stable of electrolytic condition, needing to extract a part from the waste liquid of electrolysis turns back to sulphuric leachate, at this moment, be used to soak ore deposit together with the anolyte of sulfuric acid containing magnesium ion, and in leaching and scavenging process, magnesium ion in waste liquid can not be effectively removed, so electrolytic zinc anolyte is in recycling, magnesium ion is enrichment gradually, and electrolytic process energy consumption is significantly increased.In order to reduce energy consumption, usual employing electrolytic solution open circuit, discharge the electrolytic solution in once electrolytic groove every day, in this part electrolytic solution of discharge, sulfuric acid, zinc, Mg content are all higher, for avoiding environmental pollution and waste, generally the electrolytic solution of discharging first is neutralized with calcium hydroxide, then add sulfide precipitation to filter, throw out returns pyrometallurgical smelting, outer row after wastewater treatment.Although the method is simple, implement easily, directly to neutralize, still there is following problem: 1., because acid concentration in waste liquid is high, need to add a large amount of calcium hydroxide and neutralized, can produce a large amount of waste residue, be also a kind of waste to sour resource simultaneously; 2., precipitation process with the addition of sulfide, and easily cause secondary pollution after the hydrogen sulfide emission of generation, the emission treatment cost of investment in later stage is higher; 3., generate slag in zinc recovering utilize cost higher, waste water be difficult to direct reuse need discharge, enterprise's production cost is high, and resource circulation utilization rate is low.
Summary of the invention
In order to solve Problems existing in background technology, the object of the present invention is to provide one can from zinc electrolyte effective separating magnesium sulphate, the zinc-magnesium strong acid saturated crystallization separation method that realize wastewater zero discharge and solid waste zero generation while reduction electrolytic zinc power consumption, energy-conserving and environment-protective, cost of investment be low, resource circulation utilization can be realized.
The object of the present invention is achieved like this, and this separation method comprises following processing step:
1., strong acid allotment: pending zinc electrolyte is placed in stirred pot, opens that slowly to add concentration after whipping appts in tank be the vitriol oil of 98%, zinc electrolyte is 1:0.8 ~ 0.9 with the volume ratio newly adding the vitriol oil;
2., eddy flow is stirred: accelerate to stir when mixeding liquid temperature reaches 110 ~ 120 DEG C, form eddy flow, mixing speed is 1000 ~ 1200 revs/min, and churning time is 3 ~ 5 minutes;
3., precipitate and separate: imported in settling tank by mixed solution after having stirred and staticly settle, mixed solution is separated into the zinc-magnesium cured article being deposited in downside and the supernatant liquor floating over upside;
4., isolate reuse: transparent limpid supernatant liquor pump is returned the reuse of wet method electrolysis Zn system, and the zinc-magnesium cured article bottom being deposited in send batching in pyrometallurgical smelting fuming furnace to smelt and reclaims zinc, and it is broken rear as cement raw material that magnesium becomes slag making element water.
Find through lot of experiments research, zinc sulfate in zinc electrolyte and magnesium sulfate can be separated out fast in a large number at specific temperature and acidity, the present invention utilizes this characteristic to formulate technique and is separated the zinc-magnesium in zinc electrolyte, whole production process does not introduce any impurity, discharge without waste water and dregs, sulfuric acid in flow process all can reclaim use, achieve whole recyclings of electrolysis waste solution without outer row, save waste water, the expenses of environmental protection of Solid state fermentation and the consumption of additive in traditional moderate water-cut stage, effectively can reduce power consumption.Present invention process is easy, flow process is short, easy to operate, reduced investment, consumption are low, and the electrolysis waste solution after additive and process all can all be recycled, and fully achieves Appropriate application and the maximizing the benefits of ERM, has good economic benefit and social benefit.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is further illustrated, but limited the present invention never in any form, and any conversion done based on training centre of the present invention or replacement, all belong to protection scope of the present invention.
embodiment 1:
Get that 1000L Zn content is 51g/L, Mg content is the zinc electrolyte of 24.5g/L, be separated by the method for the invention.
1., strong acid allotment: pending zinc electrolyte is placed in stirred pot, in tank, slowly adding concentration after opening whipping appts is the vitriol oil of 98%, the mixing speed of whipping appts is 800 revs/min, solution is mixed, temperature-stable rises, quick-fried spattering does not occur, and zinc electrolyte is 1:0.8 with the volume ratio newly adding the vitriol oil;
2., eddy flow is stirred: accelerate to stir when mixeding liquid temperature reaches 110 DEG C, form eddy flow, mixing speed is 1200 revs/min, and churning time is 5 minutes;
3., precipitate and separate: imported in settling tank by mixed solution after having stirred and staticly settle, the time staticly settled is 90 minutes, and mixed solution is separated into the zinc-magnesium cured article being deposited in downside and the supernatant liquor floating over upside;
4., isolate reuse: transparent limpid supernatant liquor pump is returned the reuse of wet method electrolysis Zn system, and the zinc-magnesium cured article bottom being deposited in send batching in pyrometallurgical smelting fuming furnace to smelt and reclaims zinc, and it is broken rear as cement raw material that magnesium becomes slag making element water.
In the present embodiment, after testing, in supernatant liquor after precipitate and separate, Zn content is 1.96g/L, Mg content is 7.28g/L, the separation rate of zinc reaches 96%, the separation rate of magnesium reaches 70%, solve industry conventional difficulties, meet the social development in science and technology themes such as current energy-conserving and environment-protective, resource circulation utilization, there is good economic benefit and social benefit.
embodiment 2:
Get that 1000L Zn content is 51g/L, Mg content is the zinc electrolyte of 24.5g/L, be separated by the method for the invention.
1., pre-treatment: add in pending zinc electrolyte volume percent be 1% concentration be the vitriol oil of 98% and stir, make the temperature of zinc electrolyte be elevated to 36 DEG C;
2., strong acid allotment: pending zinc electrolyte is placed in stirred pot, in tank, slowly adding concentration after opening whipping appts is the vitriol oil of 98%, the mixing speed of whipping appts is 900 revs/min, solution is mixed, temperature-stable rises, quick-fried spattering does not occur, and zinc electrolyte is 1:0.85 with the volume ratio newly adding the vitriol oil;
3., eddy flow is stirred: accelerate to stir when mixeding liquid temperature reaches 115 DEG C, form eddy flow, mixing speed is 1100 revs/min, and churning time is 4 minutes;
4., precipitate and separate: imported in settling tank by mixed solution after having stirred and staticly settle, the time staticly settled is 60 minutes, and mixed solution is separated into the zinc-magnesium cured article being deposited in downside and the supernatant liquor floating over upside;
5., isolate reuse: transparent limpid supernatant liquor pump is returned the reuse of wet method electrolysis Zn system, and the zinc-magnesium cured article bottom being deposited in send batching in pyrometallurgical smelting fuming furnace to smelt and reclaims zinc, and it is broken rear as cement raw material that magnesium becomes slag making element water.
In the present embodiment, after testing, in supernatant liquor after precipitate and separate, Zn content is 2g/L, Mg content is 4.3g/L, the separation rate of zinc reaches 96%, the separation rate of magnesium reaches 82%, solve industry conventional difficulties, meet the social development in science and technology themes such as current energy-conserving and environment-protective, resource circulation utilization, there is good economic benefit and social benefit.
embodiment 3:
Get that 1000L Zn content is 51g/L, Mg content is the zinc electrolyte of 24.5g/L, be separated by the method for the invention.
1., pre-treatment: add in pending zinc electrolyte volume percent be 0.5% concentration be the vitriol oil of 98% and stir, make the temperature of zinc electrolyte be elevated to 34 DEG C;
2., strong acid allotment: pending zinc electrolyte is placed in stirred pot, in tank, slowly adding concentration after opening whipping appts is the vitriol oil of 98%, the mixing speed of whipping appts is 1000 revs/min, solution is mixed, temperature-stable rises, quick-fried spattering does not occur, and zinc electrolyte is 1:0.9 with the volume ratio newly adding the vitriol oil;
3., eddy flow is stirred: accelerate to stir when mixeding liquid temperature reaches 120 DEG C, form eddy flow, mixing speed is 1000 revs/min, and churning time is 3 minutes;
4., precipitate and separate: imported in settling tank by mixed solution after having stirred and staticly settle, the time staticly settled is 40 minutes, and mixed solution is separated into the zinc-magnesium cured article being deposited in downside and the supernatant liquor floating over upside;
5., isolate reuse: transparent limpid supernatant liquor pump is returned the reuse of wet method electrolysis Zn system, and the zinc-magnesium cured article bottom being deposited in send batching in pyrometallurgical smelting fuming furnace to smelt and reclaims zinc, and it is broken rear as cement raw material that magnesium becomes slag making element water.
In the present embodiment, after testing, in supernatant liquor after precipitate and separate, Zn content is 1.9g/L, Mg content is 5.8g/L, the separation rate of zinc reaches 96%, the separation rate of magnesium reaches 76%, solve industry conventional difficulties, meet the social development in science and technology themes such as current energy-conserving and environment-protective, resource circulation utilization, there is good economic benefit and social benefit.
Claims (4)
1. the strong acid saturated crystallization separation method of zinc-magnesium in zinc electrolyte, is characterized in that comprising following processing step:
1., strong acid allotment: pending zinc electrolyte is placed in stirred pot, opens that slowly to add concentration after whipping appts in tank be the vitriol oil of 98%, zinc electrolyte is 1:0.8 ~ 0.9 with the volume ratio newly adding the vitriol oil;
2., eddy flow is stirred: accelerate to stir when mixeding liquid temperature reaches 110 ~ 120 DEG C, form eddy flow, mixing speed is 1000 ~ 1200 revs/min, and churning time is 3 ~ 5 minutes;
3., precipitate and separate: imported in settling tank by mixed solution after having stirred and staticly settle, mixed solution is separated into the zinc-magnesium cured article being deposited in downside and the supernatant liquor floating over upside;
4., isolate reuse: transparent limpid supernatant liquor pump is returned the reuse of wet method electrolysis Zn system, and the zinc-magnesium cured article bottom being deposited in send batching in pyrometallurgical smelting fuming furnace to smelt and reclaims zinc, and it is broken rear as cement raw material that magnesium becomes slag making element water.
2. the strong acid saturated crystallization separation method of zinc-magnesium in a kind of zinc electrolyte according to claim 1, it is characterized in that: step 1. before, also be provided with pretreatment process, first add in pending zinc electrolyte volume percent be 0.5 ~ 2% concentration be the vitriol oil of 98% and stir, make the temperature of zinc electrolyte be elevated to 34 ~ 36 DEG C.
3. the strong acid saturated crystallization separation method of zinc-magnesium in a kind of zinc electrolyte according to claim 1, is characterized in that: step 1. in the mixing speed of whipping appts be 800 ~ 1000 revs/min.
4. the strong acid saturated crystallization separation method of zinc-magnesium in a kind of zinc electrolyte according to claim 1, is characterized in that: step 3. in time of staticly settling be 40 ~ 90 minutes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410567990.7A CN104313320B (en) | 2014-10-23 | 2014-10-23 | The strong acid saturated crystallization separation method of zinc-magnesium in a kind of zinc electrolyte |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410567990.7A CN104313320B (en) | 2014-10-23 | 2014-10-23 | The strong acid saturated crystallization separation method of zinc-magnesium in a kind of zinc electrolyte |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104313320A true CN104313320A (en) | 2015-01-28 |
| CN104313320B CN104313320B (en) | 2017-04-05 |
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| CN201410567990.7A Expired - Fee Related CN104313320B (en) | 2014-10-23 | 2014-10-23 | The strong acid saturated crystallization separation method of zinc-magnesium in a kind of zinc electrolyte |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104630471A (en) * | 2015-03-01 | 2015-05-20 | 云南驰宏锌锗股份有限公司 | Method and device for removing magnesium ions in zinc sulfate solution by virtue of pressure |
| CN104630469A (en) * | 2015-03-01 | 2015-05-20 | 云南驰宏锌锗股份有限公司 | Method and device for jointly removing organic matters and magnesium ions in zinc sulfate solution |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2075524C1 (en) * | 1993-03-10 | 1997-03-20 | Научно-производственный кооператив "Доминион" | Method of processing of zinc-containing solutions |
| JPH10297926A (en) * | 1997-04-24 | 1998-11-10 | Nittetsu Mining Co Ltd | Treatment of hydrochloric acid waste liquid dissolving iron and zinc therein |
| CN101360842A (en) * | 2005-12-22 | 2009-02-04 | Bhp比利通Ssm开发有限公司 | Recovery of solid magnesium sulfate hydrate |
| WO2009039579A1 (en) * | 2007-09-26 | 2009-04-02 | Bhp Billiton Ssm Development Pty Ltd | Acid recovery from metal sulfates |
| CN103539302A (en) * | 2013-10-31 | 2014-01-29 | 惠州市斯瑞尔环境化工有限公司 | Treatment method of zinc-containing and iron-containing waste acid |
-
2014
- 2014-10-23 CN CN201410567990.7A patent/CN104313320B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2075524C1 (en) * | 1993-03-10 | 1997-03-20 | Научно-производственный кооператив "Доминион" | Method of processing of zinc-containing solutions |
| JPH10297926A (en) * | 1997-04-24 | 1998-11-10 | Nittetsu Mining Co Ltd | Treatment of hydrochloric acid waste liquid dissolving iron and zinc therein |
| CN101360842A (en) * | 2005-12-22 | 2009-02-04 | Bhp比利通Ssm开发有限公司 | Recovery of solid magnesium sulfate hydrate |
| WO2009039579A1 (en) * | 2007-09-26 | 2009-04-02 | Bhp Billiton Ssm Development Pty Ltd | Acid recovery from metal sulfates |
| CN103539302A (en) * | 2013-10-31 | 2014-01-29 | 惠州市斯瑞尔环境化工有限公司 | Treatment method of zinc-containing and iron-containing waste acid |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104630471A (en) * | 2015-03-01 | 2015-05-20 | 云南驰宏锌锗股份有限公司 | Method and device for removing magnesium ions in zinc sulfate solution by virtue of pressure |
| CN104630469A (en) * | 2015-03-01 | 2015-05-20 | 云南驰宏锌锗股份有限公司 | Method and device for jointly removing organic matters and magnesium ions in zinc sulfate solution |
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| CN104313320B (en) | 2017-04-05 |
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