CN203754783U - System for treating calcined zinc ore - Google Patents
System for treating calcined zinc ore Download PDFInfo
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- CN203754783U CN203754783U CN201420135648.5U CN201420135648U CN203754783U CN 203754783 U CN203754783 U CN 203754783U CN 201420135648 U CN201420135648 U CN 201420135648U CN 203754783 U CN203754783 U CN 203754783U
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- entrance
- outlet
- supernatant liquor
- leaching
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- 239000011701 zinc Substances 0.000 title claims abstract description 143
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 111
- 238000002386 leaching Methods 0.000 claims abstract description 102
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 85
- 239000003930 superacid Substances 0.000 claims abstract description 39
- 230000007935 neutral effect Effects 0.000 claims abstract description 36
- 229910052742 iron Inorganic materials 0.000 claims abstract description 33
- 238000001914 filtration Methods 0.000 claims abstract description 26
- 238000005406 washing Methods 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims description 129
- 239000006228 supernatant Substances 0.000 claims description 129
- 230000003472 neutralizing effect Effects 0.000 claims description 55
- 239000000047 product Substances 0.000 claims description 48
- 239000000706 filtrate Substances 0.000 claims description 46
- 239000002893 slag Substances 0.000 claims description 37
- 239000002002 slurry Substances 0.000 claims description 24
- 239000004576 sand Substances 0.000 claims description 23
- 238000002156 mixing Methods 0.000 claims description 22
- 239000007921 spray Substances 0.000 claims description 19
- 150000004965 peroxy acids Chemical class 0.000 claims description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 7
- 238000007670 refining Methods 0.000 claims description 7
- 239000003792 electrolyte Substances 0.000 claims description 6
- 230000002000 scavenging effect Effects 0.000 claims description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 4
- 239000011707 mineral Substances 0.000 claims description 4
- 239000001117 sulphuric acid Substances 0.000 claims description 3
- 235000011149 sulphuric acid Nutrition 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 abstract description 15
- 239000002184 metal Substances 0.000 abstract description 15
- 238000011084 recovery Methods 0.000 abstract description 10
- 239000002253 acid Substances 0.000 abstract description 8
- 150000002739 metals Chemical class 0.000 abstract description 4
- 238000006386 neutralization reaction Methods 0.000 abstract description 3
- 238000005507 spraying Methods 0.000 abstract description 2
- 230000008719 thickening Effects 0.000 abstract 5
- 238000000034 method Methods 0.000 description 72
- 239000000243 solution Substances 0.000 description 59
- 230000008569 process Effects 0.000 description 41
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 23
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 20
- 239000010949 copper Substances 0.000 description 19
- 239000000203 mixture Substances 0.000 description 19
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 16
- 229910052793 cadmium Inorganic materials 0.000 description 13
- 229910052802 copper Inorganic materials 0.000 description 13
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 12
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 11
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 11
- 239000008151 electrolyte solution Substances 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000011133 lead Substances 0.000 description 10
- 239000011787 zinc oxide Substances 0.000 description 10
- 239000000292 calcium oxide Substances 0.000 description 9
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 9
- 229910017052 cobalt Inorganic materials 0.000 description 9
- 239000010941 cobalt Substances 0.000 description 9
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 9
- 239000000395 magnesium oxide Substances 0.000 description 9
- 229910052709 silver Inorganic materials 0.000 description 9
- 239000004332 silver Substances 0.000 description 9
- 239000002699 waste material Substances 0.000 description 9
- 238000003723 Smelting Methods 0.000 description 8
- 150000002500 ions Chemical class 0.000 description 8
- 229910004298 SiO 2 Inorganic materials 0.000 description 7
- 230000008901 benefit Effects 0.000 description 6
- 239000012141 concentrate Substances 0.000 description 6
- 238000005868 electrolysis reaction Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 5
- 238000009854 hydrometallurgy Methods 0.000 description 5
- 229910052738 indium Inorganic materials 0.000 description 5
- APFVFJFRJDLVQX-UHFFFAOYSA-N indium atom Chemical compound [In] APFVFJFRJDLVQX-UHFFFAOYSA-N 0.000 description 5
- 229910020630 Co Ni Inorganic materials 0.000 description 4
- 239000000654 additive Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000011362 coarse particle Substances 0.000 description 4
- 238000005137 deposition process Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000010419 fine particle Substances 0.000 description 4
- 239000003517 fume Substances 0.000 description 4
- 229910052759 nickel Inorganic materials 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 230000000996 additive effect Effects 0.000 description 3
- 229910052785 arsenic Inorganic materials 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 229910052797 bismuth Inorganic materials 0.000 description 3
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000003500 flue dust Substances 0.000 description 3
- 229910052731 fluorine Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 235000010755 mineral Nutrition 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 2
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 2
- 241000080590 Niso Species 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 229910001308 Zinc ferrite Inorganic materials 0.000 description 2
- 239000003570 air Substances 0.000 description 2
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011737 fluorine Substances 0.000 description 2
- 229910052732 germanium Inorganic materials 0.000 description 2
- GNPVGFCGXDBREM-UHFFFAOYSA-N germanium atom Chemical compound [Ge] GNPVGFCGXDBREM-UHFFFAOYSA-N 0.000 description 2
- 229910052598 goethite Inorganic materials 0.000 description 2
- AEIXRCIKZIZYPM-UHFFFAOYSA-M hydroxy(oxo)iron Chemical compound [O][Fe]O AEIXRCIKZIZYPM-UHFFFAOYSA-M 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 2
- 229910052748 manganese Inorganic materials 0.000 description 2
- 239000011572 manganese Substances 0.000 description 2
- 229920002401 polyacrylamide Polymers 0.000 description 2
- 239000012286 potassium permanganate Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 235000012239 silicon dioxide Nutrition 0.000 description 2
- 229960001866 silicon dioxide Drugs 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- WGEATSXPYVGFCC-UHFFFAOYSA-N zinc ferrite Chemical compound O=[Zn].O=[Fe]O[Fe]=O WGEATSXPYVGFCC-UHFFFAOYSA-N 0.000 description 2
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- -1 bismuth Chemical class 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 229910052595 hematite Inorganic materials 0.000 description 1
- 239000011019 hematite Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 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 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 229910052935 jarosite Inorganic materials 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 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 utility model discloses a system for treating calcined zinc ore. The system for treating the calcined zinc ore comprises a neutral leaching device, a first thickening device, a neutralization treatment device, a second thickening device, a high acid leaching device, a third thickening device, a super acid leaching device, a fourth thickening device, a first washing and filtering device, a spraying and iron removing device, a grading device, a fifth thickening device and a second washing and filtering device. By adopting the system for treating the calcined zinc ore in the embodiment of the utility model, recovery rate of valuable metals can be obviously increased.
Description
Technical field
The utility model relates to field of metallurgy, and particularly, the utility model relates to a kind of system of processing zinc roasted ore.
Background technology
The leading technique of current zinc hydrometallurgy is divided into the large class of direct leaching two of sulfuric acid+leaching and zinc ore concentrate, wherein sulfuric acid+leaching comprises that again conventional two sections of leachings and hot acid leach, for the difference of heavy iron method, hot acid leaches and has derived again the techniques such as jarosite process, goethite process, hematite process.The direct leaching of zinc ore concentrate comprises that pressure leaching and normal pressure oxygen soak two kinds.All there is the deficiency of self in various technique above.
Utility model content
The utility model is intended to one of solve the problems of the technologies described above at least to a certain extent.For this reason, an object of the present utility model is to propose a kind of system of processing zinc roasted ore, and this system can significantly improve the recovery utilization rate of valuable metal.
Aspect one of the present utility model, the utility model proposes a kind of system of processing zinc roasted ore.Obtain embodiment according to the utility model, this system comprises:
Neutral leaching device, described neutral leaching device has mineral supplying opening, oxygenant supplying opening, electrolyte supply mouth and the neutral product that leaches and exports;
The first dense device, described the first dense device has neutral leaching product entrance, the first supernatant liquor exports and the liquid outlet of first end, and the described neutral product entrance that leaches is connected with the outlet of described neutrality leaching product;
Neutralizing treatment device, described neutralizing treatment device has the first end liquid entrance and the outlet of neutralizing treatment product, and described the first end liquid entrance is connected with described the first end liquid outlet;
The second dense device, described the second dense device has neutralizing treatment product entrance, the second supernatant liquor outlet and the liquid outlet of second end, and described neutralizing treatment product entrance is connected with described neutralizing treatment product outlet;
Peracid leaching device, described peracid leaching device has the second end liquid entrance and the outlet of high Ore Leaching product, and described the second end liquid entrance is connected with described the second end liquid outlet;
The 3rd dense device, described the 3rd dense device has high Ore Leaching product entrance, the 3rd supernatant liquor outlet and the liquid outlet of the 3rd end, and described high Ore Leaching product entrance is connected with described high Ore Leaching product outlet;
Super acid leaching device, described super acid leaching device has the 3rd end liquid entrance, electrolyte entrance, sulphuric acid soln entrance and super acid and leaches product outlet, and described the 3rd end liquid entrance is connected with described the 3rd end liquid outlet;
The 4th dense device, described the 4th dense device has super acid and leaches product entrance, the 4th supernatant liquor outlet and the liquid outlet of the 4th end, and described super acid leaches product entrance and is connected with the outlet of described super acid leaching product;
The first washing and filtering device, described the first washing and filtering device has the 4th end liquid entrance, plumbous silver-colored slag outlet and the first filtrate outlet, and described the 4th end liquid entrance is connected with described the 4th end liquid outlet;
Spray deironing apparatus, described spray deironing apparatus has the second supernatant liquor entrance, material inlet and the outlet of iron ore slurry, and described the second supernatant liquor entrance is connected with described the second supernatant liquor outlet;
Sorting equipment, described sorting equipment has iron ore slurry entrance, coarse sand outlet and mixing solutions outlet, and described iron ore slurry entrance is connected with the outlet of described iron ore slurry;
The 5th dense device, described the 5th dense device has mixing solutions entrance, the 5th supernatant liquor outlet and the liquid outlet of the 5th end, and described mixing solutions entrance is connected with described mixing solutions outlet; And
The second washing and filtering device, described the second washing and filtering device has the 5th end liquid entrance, scum outlet and the second filtrate outlet, and described the 5th end liquid entrance is connected with described the 5th end liquid outlet.
Leach treatment process and can significantly improve scum quality using zinc roasted ore or oxygenant flue dust as the neutralizing agent of spray deironing treating processes by employing super acid according to the system of the processing zinc roasted ore of the utility model embodiment, and significantly reduce plumbous silver-colored slag slag rate, in the plumbous silver-colored slag of gained, plumbous silver is of high grade simultaneously, in addition, obtain plumbous silver-colored slag and can deliver to plumbous reduction furnace for smelting direct production lead bullion, thereby can realize plumbous zinc complementation, wet fire is compatible, the technique object of energy-saving and emission-reduction, open up new way for reducing zinc hydrometallurgy production cost, realize smelting waste slag innoxious, the object of resource utilization, promote the lifting of Business Economic Benefit.
In addition, can also there is following additional technical characterictic according to the system of the processing zinc roasted ore of the utility model above-described embodiment:
In embodiment more of the present utility model, the system of described processing zinc roasted ore further comprises: refining plant, and described refining plant has the first supernatant liquor entrance and scavenging solution outlet, and described the first supernatant liquor entrance is connected with described the first supernatant liquor outlet.Thus, can significantly improve the recovery utilization rate of valuable metal.
In embodiment more of the present utility model, described neutralizing treatment device further has the 3rd supernatant liquor entrance and coarse sand entrance, and described the 3rd supernatant liquor entrance is connected with described the 3rd supernatant liquor outlet, and described coarse sand entrance is connected with described coarse sand outlet.Thus, can further improve the recovery utilization rate of valuable metal.
In embodiment more of the present utility model, described peracid leaching device further has the 4th supernatant liquor entrance and the first filtrate entrance, described the 4th supernatant liquor entrance is connected with described the 4th supernatant liquor outlet, and described the first filtrate entrance is connected with described the first filtrate outlet.Thus, can further improve the recovery utilization rate of valuable metal.
In embodiment more of the present utility model, described neutral leaching device further has the 5th supernatant liquor entrance and the second filtrate entrance, described the 5th supernatant liquor entrance is connected with described the 5th supernatant liquor outlet, and described the second filtrate entrance is connected with described the second filtrate outlet.Thus, can further improve the recovery utilization rate of valuable metal.
Additional aspect of the present utility model and advantage in the following description part provide, and part will become obviously from the following description, or recognize by practice of the present utility model.
Brief description of the drawings
Above-mentioned and/or additional aspect of the present utility model and advantage accompanying drawing below combination is understood becoming the description of embodiment obviously and easily, wherein:
Fig. 1 is according to the structural representation of the system of the processing zinc roasted ore of an embodiment of the utility model;
Fig. 2 is according to the structural representation of the system of the processing zinc roasted ore of another embodiment of the utility model;
Fig. 3 is according to the structural representation of the system of the processing zinc roasted ore of another embodiment of the utility model;
Fig. 4 utilizes the system of the processing zinc roasted ore of an embodiment of the utility model to process the schematic flow sheet of the method for zinc roasted ore;
Fig. 5 utilizes the system of the processing zinc roasted ore of another embodiment of the utility model to process the schematic flow sheet of the method for zinc roasted ore;
Fig. 6 utilizes the system of the processing zinc roasted ore of another embodiment of the utility model to process the schematic flow sheet of the method for zinc roasted ore.
Embodiment
Describe embodiment of the present utility model below in detail, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has the element of identical or similar functions from start to finish.Be exemplary below by the embodiment being described with reference to the drawings, be intended to for explaining the utility model, and can not be interpreted as restriction of the present utility model.
In description of the present utility model, it will be appreciated that, term " first ", " second " be only for describing object, and can not be interpreted as instruction or hint relative importance or the implicit quantity that indicates indicated technical characterictic.Thus, one or more these features can be expressed or impliedly be comprised to the feature that is limited with " first ", " second ".In description of the present utility model, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the utility model, unless otherwise clearly defined and limited, the terms such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and for example, can be to be fixedly connected with, and can be also to removably connect, or connect integratedly; Can be mechanical connection, can be also electrical connection; Can be to be directly connected, also can indirectly be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, can understand as the case may be the concrete meaning of above-mentioned term in the utility model.
Aspect one of the present utility model, the utility model proposes a kind of system of processing zinc roasted ore.System below with reference to the processing zinc roasted ore of Fig. 1-3 couple the utility model embodiment is described in detail.According to embodiment of the present utility model, this system comprises:
Neutral leaching device 100: according to embodiment of the present utility model, neutral leaching device 100 has mineral supplying opening 101, oxygenant supplying opening 102, electrolyte supply mouth 103 and the neutral product that leaches and exports 104, and for zinc roasted ore being mixed with oxygenant and electrolytic solution and carrying out neutrality and leach processing, thereby can obtain neutral leach liquor.According to embodiment of the present utility model, the composition of zinc roasted ore is also not particularly limited, according to specific embodiment of the utility model, zinc roasted ore can be zinc, the cadmium of 0.1～0.5wt%, the lead of 1～3wt%, the copper of 0.2～1.0wt%, the iron of 8～20wt%, the sulphur of 0.1～2.5wt%, the calcium oxide of 0.5～1.0wt%, the magnesium oxide of 0.5～1.0wt%, the silicon-dioxide of 1.0～5.0wt% and a small amount of arsenic, silver, fluorine, chlorine, indium, germanium, cobalt and the nickel etc. that contain 45～55wt%.
According to embodiment of the present utility model, the particular type of oxygenant is also not particularly limited, and according to specific embodiment of the utility model, oxygenant can be for being selected from least one in manganese ore powder, potassium permanganate, air and oxygen.According to embodiment of the present utility model, the particular type of electrolytic solution is also not particularly limited, and according to specific embodiment of the utility model, electrolytic solution can be zinc electrolysis waste solution.According to specific embodiment of the utility model, Zn in zinc electrolysis waste solution
2+concentration can be 45-55g/L, H
2sO
4concentration can be 160-180g/L.According to embodiment of the present utility model, the condition that neutral leaching is processed is also not particularly limited, according to specific embodiment of the utility model, neutral leaching processed and can under the terminal acidity that be 4.8～5.2 with pH at the temperature of 50～70 degrees Celsius, be carried out completing for 1.5～2.5 hours.In this step, particularly, first, under the effect of oxygenant, make zinc, copper, cadmium etc. be oxidized into oxide compound, then under the effect of electrolytic solution, mainly carry out following chemical reaction:
ZnO+H
2SO
4=ZnSO
4+H
2O
CuO+H
2SO
4=CuSO
4+H
2O
CdO+H
2SO
4=CdSO
4+H
2O
The first dense device 200: according to embodiment of the present utility model, the first dense device 200 has neutral leach product entrance 201, the first supernatant liquor outlet 202 and the first end liquid outlet 203, according to specific embodiment of the utility model, the neutral product entrance 201 that leaches is connected with neutrality leaching product outlet 104, and for the neutral leach liquor obtaining is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid.According to embodiment of the present utility model, the first supernatant liquor main component: Zn
2+concentration can be 140～160g/L, Fe
alwaysthe concentration of ion can be lower than 30mg/L, Cu
2+concentration can be 200～1000mg/L, Cd
2+concentration can be 200～600mg/L, the first end liquid main component: the content of zinc element can be 18～22wt%, the content of ferro element can be 10～15wt%.In this step, particularly, neutral leach liquor is added in thickener, through natural subsidence process carry out liquid-solid separation after adding polyacrylamide flocculant simultaneously.
Neutralizing treatment device 300: according to embodiment of the present utility model, neutralizing treatment device 300 has the first end liquid entrance 301 and neutralizing treatment product outlet 302, according to specific embodiment of the utility model, the first end liquid entrance 301 is connected with the first end liquid outlet 203, for the first end liquid obtaining is carried out to neutralizing treatment, thereby can obtain the solution through neutralizing treatment.According to embodiment of the present utility model, the condition of neutralizing treatment is also not particularly limited, according to specific embodiment of the utility model, neutralizing treatment can carry out completing for 1.5～2.5 hours under the terminal acidity that be 1.5～2.5 with pH at the temperature of 60～75 degrees Celsius.In this step, concrete, in the first end liquid obtaining, contain a large amount of zinc by neutralizing treatment, can make most of zinc be dissolved in solution, thereby can improve the zinc concentration in solution, for follow-up spray deironing is prepared.
The second dense device 400: according to embodiment of the present utility model, the second dense device 400 has neutralizing treatment product entrance 401, the second supernatant liquor outlet 402 and the second end liquid outlet 403, according to specific embodiment of the utility model, neutralizing treatment product entrance 401 is connected with neutralizing treatment product outlet 302, and carry out the second dense processing for the solution of the process neutralizing treatment to obtaining, thereby can obtain respectively the second supernatant liquor and the second end liquid.According to embodiment of the present utility model, the second supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysionic concn can be 5～35g/L, and the content of the second end liquid main component Zn element is 15～25wt%, and the content of Fe element is 15～25wt%.
Peracid leaching device 500: according to embodiment of the present utility model, peracid leaching device 500 has the second end liquid entrance 501 and high Ore Leaching product outlet 502, according to specific embodiment of the utility model, the second end liquid entrance 501 is connected with the second end liquid outlet 403, and for the second end liquid obtaining is carried out to high Ore Leaching processing, thereby can obtain the solution through high Ore Leaching processing.According to embodiment of the present utility model, the condition of high Ore Leaching processing is also not particularly limited, according to specific embodiment of the utility model, high Ore Leaching processing can be to carry out at least 2 hours under 40～70g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.The main chemical reactions occurring is:
ZnFe
2O
4+4H
2SO
4=Fe
2（SO
4）
3+ZnSO
4+4H
2O
ZnO+H
2SO
4=ZnSO
4+H
2O
The 3rd dense device 600: according to embodiment of the present utility model, the 3rd dense device 600 has high Ore Leaching product entrance 601, the 3rd supernatant liquor outlet 602 and the 3rd end liquid outlet 603, according to specific embodiment of the utility model, high Ore Leaching product entrance 601 is connected with high Ore Leaching product outlet 502, and for the solution of the high Ore Leaching processing of the process obtaining is carried out to the 3rd dense processing, thereby can obtain respectively the 3rd supernatant liquor and the 3rd end liquid.According to embodiment of the present utility model, the 3rd supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 15～30g/L, H
2sO
4concentration can be 40～70g/L; The 3rd end liquid main component: the content of zinc element can be 5～12wt%, the content of ferro element can be 5～15wt%.
Super acid leaching device 700: according to embodiment of the present utility model, super acid leaching device 700 has the 3rd end liquid entrance 701, electrolyte entrance 702, sulphuric acid soln entrance 703 and super acid and leaches product outlet 704, according to specific embodiment of the utility model, the 3rd end liquid entrance 701 is connected with the 3rd end liquid outlet 603, and leach processing for the 3rd end liquid obtaining being carried out to super acid, thereby can obtain leaching through super acid the solution of processing.According to embodiment of the present utility model, super acid-treated condition is also not particularly limited, according to specific embodiment of the utility model, super acid leaches and processes can be to carry out at least 2 hours under 100～120g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.In this step, concrete, in the 3rd end liquid, add the vitriol oil and zinc electrolysis waste solution, adopt the strengthening of high temperature peracid to leach the zinc ferrite that is difficult to leaching, can further improve thus the leaching yield of zinc.The main chemical reactions occurring is: ZnFe
2o
4+ 4H
2sO
4=Fe
2(SO
4)
3+ ZnSO
4+ 4H
2o.
The 4th dense device 800: according to embodiment of the present utility model, the 4th dense device 800 has super acid and leaches product entrance 801, the 4th supernatant liquor outlet 802 and the 4th end liquid outlet 803, according to specific embodiment of the utility model, super acid leaches product entrance 801 and is connected with super acid leaching product outlet 704, and carry out the 4th dense processing for the obtained solution that leaching is processed through super acid, thereby can obtain respectively the 4th supernatant liquor and the 4th end liquid.According to embodiment of the present utility model, the 4th supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 10～35g/L, H
2sO
4concentration can be 100～120g/L, the 4th end liquid main component: the content of zinc element can be 4～10wt%, and the content of ferro element can be 5～15wt%, and the content of lead element can be 10～20wt%.
The first washing and filtering device 900: according to embodiment of the present utility model, the first washing and filtering device 900 put there is the 4th end liquid entrance 901, plumbous silver-colored slag outlet 902 and the first filtrate outlet 903, according to specific embodiment of the utility model, the 4th end liquid entrance 901 is connected with the 4th end liquid outlet 803, and for described the 4th end liquid obtaining is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate.
Spray deironing apparatus 1000: according to embodiment of the present utility model, spray deironing apparatus 1000 has the second supernatant liquor entrance 1001, material inlet 1002 and iron ore slurry outlet 1003, according to specific embodiment of the utility model, the second supernatant liquor entrance 1001 is connected with the second supernatant liquor outlet 402, and be suitable for utilizing zinc roasted ore and/or zinc oxide fumes to described the second supernatant liquor is sprayed to deironing processing, thereby can obtain iron ore slurry.According to embodiment of the present utility model, the condition of spray deironing processing is also not particularly limited, and according to specific embodiment of the utility model, spray deironing processing can be carried out under the terminal acidity that be 3.0～4.5 with pH at the temperature of 80～90 degrees Celsius.The main chemical reactions occurring is:
Fe
2（SO
4）
3+H
2O+3ZnO=2FeO.OH↓+3ZnSO
4
Sorting equipment 1100: according to embodiment of the present utility model, sorting equipment 1100 has iron ore slurry entrance 1101, coarse sand outlet 1102 and mixing solutions outlet 1103, according to specific embodiment of the utility model, iron ore slurry entrance 1101 is connected with iron ore slurry outlet 1003, and for iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.In this step, concrete, obtained iron ore slurry is carried out to cyclone classification or screw classifying, fine particle (scum) is separated with coarse particles (unreacted is calcining completely), the fine particle of separating carries out dense processing, and coarse particles returns to neutralizing treatment.
The 5th dense device 1200: according to embodiment of the present utility model, the 5th dense device 1200 has mixing solutions entrance 1201, the 5th supernatant liquor outlet 1202 and the 5th end liquid outlet 1203, according to specific embodiment of the utility model, mixing solutions entrance 1201 is connected with mixing solutions outlet 1103, and for mixing solutions being carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid.According to embodiment of the present utility model, the 5th supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysthe concentration of ion can be 1～4g/L, the 5th end liquid main component: the content of zinc element can be 5.0～12.0wt%, and the content of ferro element can be 25～35wt%.
The second washing and filtering device 1300: according to embodiment of the present utility model, the second washing and filtering device 1300 has the 5th end liquid entrance 1301, scum outlet 1302 and the second filtrate outlet 1303, according to specific embodiment of the utility model, the 5th end liquid entrance 1301 is connected with the 5th end liquid outlet 1203, and for the 5th end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate.
Can effectively implement the method for above-mentioned processing zinc roasted ore according to the system of the processing zinc roasted ore of the utility model embodiment.
With reference to figure 2, according to embodiment of the present utility model, the system of processing zinc roasted ore further comprises:
Refining plant 1400: according to embodiment of the present utility model, refining plant 1400 has the first supernatant liquor entrance 1401 and scavenging solution outlet 1402, according to specific embodiment of the utility model, the first supernatant liquor entrance 1401 is connected with the first supernatant liquor outlet 202, and for the first supernatant liquor is carried out to purifying treatment.In this step, particularly, purifying treatment is in fact by adding zinc dust precipitation copper removal, cadmium, or adds Zinc dust Cementation for Cobalt Removal, nickel in the time that other additive (as antimonic salt) exists.Thus, can make the Cu in the first supernatant liquor by purifying treatment
2+, Cd
2+, Co
2+, Ni
2+deng impurity except within the permission content range of zinc electrolytic deposition process, guarantee the zinc metal sheet that normally carries out and produce better quality of electrolytic deposition process, simultaneously, by the inrichment of scavenging process, making has a valency associated element in raw material, as Cu, Cd, Co etc. obtain enrichment, and can obtain byproduct copper ore concentrates, Spongy Cadmium and cobalt concentrate through processing.Its main main chemical reactions equation is as follows:
CuSO
4+Zn=Cu↓+ZnSO
4
CdSO
4+Zn=Cd↓+ZnSO
4
CoSO
4+Zn=Co↓+ZnSO
4
NiSO
4+Zn=Ni↓+ZnSO
4
With reference to figure 3, according to embodiment of the present utility model, according to the utility model embodiment, neutralizing treatment device 300 further has the 3rd supernatant liquor entrance 303 and coarse sand entrance 304, according to specific embodiment of the utility model, the 3rd supernatant liquor entrance 303 is connected with the 3rd supernatant liquor outlet 602, and coarse sand entrance 304 exports 1102 with coarse sand and is connected, and for the 3rd supernatant liquor and coarse sand are returned and carry out neutralizing treatment.It should be noted that, coarse sand entrance 304 and the 3rd supernatant liquor entrance 303 can be same mouthful.Thus, thus, can utilize the acid in zinc oxide neutralization the 3rd supernatant liquor in the first end liquid, thereby the qualified front liquid of deironing can be provided.
According to embodiment of the present utility model, peracid leaching device 500 further has the 4th supernatant liquor entrance 503 and the first filtrate entrance 504, according to specific embodiment of the utility model, the 4th supernatant liquor entrance 503 is connected with the 4th supernatant liquor outlet 802, the first filtrate entrance 504 is connected with the first filtrate outlet 903, and for the 4th supernatant liquor and the first filtrate returning are carried out to high Ore Leaching processing.It should be noted that, the 4th supernatant liquor entrance 503 and the first filtrate entrance 504 can be same mouthful.Thus, can significantly improve the leaching yield of zinc.
According to embodiment of the present utility model, described neutral leaching device 100 further has the 5th supernatant liquor entrance 105 and the second filtrate entrance 106, according to specific embodiment of the utility model, the 5th supernatant liquor entrance 105 is connected with the 5th supernatant liquor outlet 1202, the second filtrate entrance 106 is connected with the second filtrate outlet 1303, and for the 5th supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.It should be noted that, the 5th supernatant liquor entrance 105 and the second filtrate entrance 106 can be same mouthful.Thus, can further improve the recovery utilization rate of valuable metal.
Understand for convenient, utilize the method for the system processing zinc roasted ore of the processing zinc roasted ore of the utility model embodiment to be described in detail below with reference to Fig. 4-6 pair.According to embodiment of the present utility model, the method comprises:
S100: neutral leaching processed
According to embodiment of the present utility model, roasted ore mixed with oxygenant and electrolytic solution and carry out neutrality and leach processing, thereby can obtain neutral leach liquor.According to embodiment of the present utility model, the composition of zinc roasted ore is also not particularly limited, according to specific embodiment of the utility model, zinc roasted ore can be zinc, the cadmium of 0.1～0.5wt%, the lead of 1～3wt%, the copper of 0.2～1.0wt%, the iron of 8～20wt%, the sulphur of 0.1～2.5wt%, the calcium oxide of 0.5～1.0wt%, the magnesium oxide of 0.5～1.0wt%, the silicon-dioxide of 1.0～5.0wt% and a small amount of arsenic, silver, fluorine, chlorine, indium, germanium, cobalt and the nickel etc. that contain 45～55wt%.
According to embodiment of the present utility model, the particular type of oxygenant is also not particularly limited, and according to specific embodiment of the utility model, oxygenant can be for being selected from least one in manganese ore powder, potassium permanganate, air and oxygen.According to embodiment of the present utility model, the particular type of electrolytic solution is also not particularly limited, and according to specific embodiment of the utility model, electrolytic solution can be zinc electrolysis waste solution.According to specific embodiment of the utility model, Zn in zinc electrolysis waste solution
2+concentration can be 45-55g/L, H
2sO
4concentration can be 160-180g/L.According to embodiment of the present utility model, the condition that neutral leaching is processed is also not particularly limited, according to specific embodiment of the utility model, neutral leaching processed and can under the terminal acidity that be 4.8～5.2 with pH at the temperature of 50～70 degrees Celsius, be carried out completing for 1.5～2.5 hours.In this step, particularly, first, under the effect of oxygenant, make zinc, copper, cadmium etc. be oxidized into oxide compound, then under the effect of electrolytic solution, mainly carry out following chemical reaction:
ZnO+H
2SO
4=ZnSO
4+H
2O
CuO+H
2SO
4=CuSO
4+H
2O
CdO+H
2SO
4=CdSO
4+H
2O
S200: the first dense processing
According to embodiment of the present utility model, obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid.According to embodiment of the present utility model, the first supernatant liquor main component: Zn
2+concentration can be 140～160g/L, Fe
alwaysthe concentration of ion can be lower than 30mg/L, Cu
2+concentration can be 200～1000mg/L, Cd
2+concentration can be 200～600mg/L, the first end liquid main component: the content of zinc element can be 18～22wt%, the content of ferro element can be 10～15wt%.In this step, particularly, neutral leach liquor is added in thickener, through natural subsidence process carry out liquid-solid separation after adding polyacrylamide flocculant simultaneously.
S300: neutralizing treatment
According to embodiment of the present utility model, the first obtained end liquid is carried out to neutralizing treatment, thereby can obtain the solution through neutralizing treatment.According to embodiment of the present utility model, the condition of neutralizing treatment is also not particularly limited, according to specific embodiment of the utility model, neutralizing treatment can carry out completing for 1.5～2.5 hours under the terminal acidity that be 1.5～2.5 with pH at the temperature of 60～75 degrees Celsius.In this step, concrete, in the first end liquid obtaining, contain a large amount of zinc by neutralizing treatment, can make most of zinc be dissolved in solution, thereby can improve the zinc concentration in solution, for follow-up spray deironing is prepared.
S400: the second dense processing
According to embodiment of the present utility model, the solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid.According to embodiment of the present utility model, the second supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysionic concn can be 5～35g/L, and the content of the second end liquid main component Zn element is 15～25wt%, and the content of Fe element is 15～25wt%.
S500: high Ore Leaching processing
According to embodiment of the present utility model, the second obtained end liquid is carried out to high Ore Leaching processing, thereby can obtain the solution through high Ore Leaching processing.According to embodiment of the present utility model, the condition of high Ore Leaching processing is also not particularly limited, according to specific embodiment of the utility model, high Ore Leaching processing can be to carry out at least 2 hours under 40～70g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.The main chemical reactions occurring is:
ZnFe
2O
4+4H
2SO
4=Fe
2（SO
4）
3+ZnSO
4+4H
2O
ZnO+H
2SO
4=ZnSO
4+H
2O
S600: the 3rd dense processing
According to embodiment of the present utility model, the solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid.According to embodiment of the present utility model, the 3rd supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 15～30g/L, H
2sO
4concentration can be 40～70g/L; The 3rd end liquid main component: the content of zinc element can be 5～12wt%, the content of ferro element can be 5～15wt%.With reference to figure 5, according to embodiment of the present utility model, the 3rd supernatant liquor can be returned and carries out neutralizing treatment.Thus, can utilize the acid in zinc oxide neutralization the 3rd supernatant liquor in the first end liquid, thereby the qualified front liquid of deironing can be provided.
S700: super acid leaches to be processed
According to embodiment of the present utility model, the 3rd obtained end liquid is carried out to super acid and leach processing, thereby can obtain leaching through super acid the solution of processing.According to embodiment of the present utility model, super acid-treated condition is also not particularly limited, according to specific embodiment of the utility model, super acid leaches and processes can be to carry out at least 2 hours under 100～120g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.In this step, concrete, in the 3rd end liquid, add the vitriol oil and zinc electrolysis waste solution, adopt the strengthening of high temperature peracid to leach the zinc ferrite that is difficult to leaching, can further improve thus the leaching yield of zinc.The main chemical reactions occurring is: ZnFe
2o
4+ 4H
2sO
4=Fe
2(SO
4)
3+ ZnSO
4+ 4H
2o.
S800: the 4th dense processing
According to embodiment of the present utility model, the obtained solution that leaching is processed through super acid is carried out to the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid.According to embodiment of the present utility model, the 4th supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 10～35g/L, H
2sO
4concentration can be 100～120g/L, the 4th end liquid main component: the content of zinc element can be 4～10wt%, and the content of ferro element can be 5～15wt%, and the content of lead element can be 10～20wt%.
S900: the first washing and filtering
According to embodiment of the present utility model, the 4th obtained end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate.With reference to figure 5, according to embodiment of the present utility model, can return and carry out high Ore Leaching processing by the first obtained filtrate with the 4th supernatant liquor, can improve thus the leaching yield of zinc.
S1000: spray deironing processing
According to embodiment of the present utility model, utilize the second supernatant liquor that zinc roasted ore and/or zinc oxide fumes obtain S400 to spray deironing processing, thereby can obtain iron ore slurry.According to embodiment of the present utility model, the condition of spray deironing processing is also not particularly limited, and according to specific embodiment of the utility model, spray deironing processing can be carried out under the terminal acidity that be 3.0～4.5 with pH at the temperature of 80～90 degrees Celsius.The main chemical reactions occurring is:
Fe
2（SO
4）
3+H
2O+3ZnO=2FeO.OH↓+3ZnSO
4
S1100: stage treatment
According to embodiment of the present utility model, obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.With reference to figure 5, according to embodiment of the present utility model, obtained coarse sand can be returned and carries out neutralizing treatment, so that liquid before qualified deironing to be provided.In this step, concrete, obtained iron ore slurry is carried out to cyclone classification or screw classifying, fine particle (scum) is separated with coarse particles (unreacted is calcining completely), the fine particle of separating carries out dense processing, and coarse particles returns to neutralizing treatment.
S1200: the 5th dense processing
According to embodiment of the present utility model, above obtained mixing solutions is carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid.According to embodiment of the present utility model, the 5th supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysthe concentration of ion can be 1～4g/L, the 5th end liquid main component: the content of zinc element can be 5.0～12.0wt%, and the content of ferro element can be 25～35wt%.
S1300: the second washing and filtering
According to embodiment of the present utility model, above the 5th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate.With reference to figure 5, according to embodiment of the present utility model, the 5th obtained supernatant liquor and the second filtrate returning can be carried out to neutrality leaching processing.
Utilize the method for the system processing zinc roasted ore of the processing zinc roasted ore of the utility model embodiment to leach treatment process and can significantly improve scum slag rate using zinc roasted ore or oxygenant flue dust as the neutralizing agent of spray deironing treating processes by employing super acid, and significantly reduce plumbous silver-colored slag slag rate, in the plumbous silver-colored slag of gained, plumbous silver is of high grade, simultaneously, the method has adopted zinc hydrometallurgy hot acid leaching-Spraying Precipitator in Iron Removal, adhere to that liquid walks short circuit, material walk long distances, 2 reinforced, the feature of 3 acid addings, the comprehensive lead that reclaims, silver, copper, cadmium, cobalt, indium, the valuable metals such as bismuth, effectively improve the recovery utilization rate of valuable metal, in addition, the method is simple compared with other procedure, only by regulating the speed that adds of neutralizing agent (roasted ore) and iron-containing liquor, need not reduction process and add other additive, can realize scum and the effective of plumbous silver-colored slag separates, the scum obtaining can be delivered to the plumbous plumbous warm sludge of smelting of fuming furnace collocation of smelting and process together, the plumbous silver-colored slag of higher-grade obtaining send plumbous reduction furnace for smelting direct production lead bullion, realize plumbous zinc complementation, wet fire is compatible, the technique object of energy-saving and emission-reduction, open up new way for reducing zinc hydrometallurgy production cost, realize smelting waste slag innoxious, the object of resource utilization, promote the lifting of Business Economic Benefit.
With reference to figure 6, according to embodiment of the present utility model, the method for processing zinc roasted ore further comprises:
S1400: purifying treatment
According to embodiment of the present utility model, the first obtained supernatant liquor is carried out to purifying treatment.In this step, particularly, purifying treatment is in fact by adding zinc dust precipitation copper removal, cadmium, or adds Zinc dust Cementation for Cobalt Removal, nickel in the time that other additive (as antimonic salt) exists.Thus, can make the Cu in the first supernatant liquor by purifying treatment
2+, Cd
2+, Co
2+, Ni
2+deng impurity except within the permission content range of zinc electrolytic deposition process, guarantee the zinc metal sheet that normally carries out and produce better quality of electrolytic deposition process, simultaneously, by the inrichment of scavenging process, making has a valency associated element in raw material, as Cu, Cd, Co etc. obtain enrichment, and can obtain byproduct copper ore concentrates, Spongy Cadmium and cobalt concentrate through processing.Its main main chemical reactions equation is as follows:
CuSO
4+Zn=Cu↓+ZnSO
4
CdSO
4+Zn=Cd↓+ZnSO
4
CoSO
4+Zn=Co↓+ZnSO
4
NiSO
4+Zn=Ni↓+ZnSO
4
As mentioned above, the method for utilizing the system of the processing zinc roasted ore of the utility model embodiment to process zinc roasted ore can have and is selected from following advantage one of at least:
The method of utilizing the system of the processing zinc roasted ore of the utility model embodiment to process zinc roasted ore adheres to that liquid walks short circuit, material walk long distances, the feature of 2 reinforced, 3 acid addings, comprehensively reclaim the valuable metals such as lead, silver, copper, cadmium, cobalt, indium, bismuth, effectively improved the recovery utilization rate of valuable metal;
The method operation that utilizes the system of the processing zinc roasted ore of the utility model embodiment to process zinc roasted ore is controlled simple, and what only need to control neutralizing agent (roasted ore or zinc oxide fumes) and iron-containing liquor adds speed, temperature, pH value;
Utilize method that the system of the processing zinc roasted ore of the utility model embodiment processes zinc roasted ore without adding Na
+, NH
4 +the additives such as salt;
The method of utilizing the system of the processing zinc roasted ore of the utility model embodiment to process zinc roasted ore adopts low iron to sink iron, makes Fe
3+enter solution with injection mode;
Utilize method that the system of the processing zinc roasted ore of the utility model embodiment processes zinc roasted ore without reduction operation, lower concentration ferric iron directly generates goethite precipitation;
Utilize the system of the processing zinc roasted ore of the utility model embodiment to process the dust rate of method scum pyrogenic attack output of zinc roasted ore low, flue dust quality is good;
Utilize the system of the processing zinc roasted ore of the utility model embodiment to process method removing impurities (F, Cl, As, Sb, the Si etc.) ability of zinc roasted ore strong;
Utilize the system of the processing zinc roasted ore of the utility model embodiment to process the method equipment configuration of zinc roasted ore simple, without high pressure or specific installation;
Utilize the system of the processing zinc roasted ore of the utility model embodiment to process the plumbous silver of super acid leached mud (plumbous silver-colored slag) in the method for zinc roasted ore of high grade, plumbous as the refining of the direct Song Qian of byproduct smeltery.
Below with reference to specific embodiment, the utility model is described, it should be noted that, these embodiment are only descriptive, and limit never in any form the utility model.
Embodiment 1
Zinc roasting mineral phase composite table 1:
Table 1
| Composition | Zn | Cd | Pb | Cu | Fe | S | S SO4 | CaO | MgO | SiO 2 |
| Amount to/% | 52.38 | 0.22 | 1.71 | 0.57 | 15.6 | 0.4 | 1.31 | 0.91 | 0.68 | 3.42 |
| Composition | As | Ag | F | Cl | In | Ge | Co | Ni | ||
| Amount to/g/t | 7970 | 194 | 23.9 | 51.2 | 228 | 4.55 | 433 | 399 |
Get the 100kg zinc roasted ore of said components, it is processed, specifically comprise the following steps:
Under the terminal acidity that is 5.2 with pH after roasted ore is mixed with oxygenant and electrolytic solution, carry out neutrality and leach processing 2 hours at the temperature of 65 degrees Celsius, thereby can obtain neutral leach liquor; Obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid; Under the terminal acidity that is 2.0 with pH, the first obtained end liquid is carried out to neutralizing treatment 2 hours at the temperature of 70 degrees Celsius, thereby can obtain the solution through neutralizing treatment; The solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid; At the temperature of 95 degrees Celsius, process 2 hours for the second obtained end liquid being carried out under 60g/L condition to high Ore Leaching with terminal acidity, thereby can obtain the solution through high Ore Leaching processing; The solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid; At the temperature of 95 degrees Celsius, be under 100g/L condition with terminal acidity, the 3rd obtained end liquid carried out to super acid and leach processing 2 hours, thereby can obtain leaching through super acid the solution of processing; The obtained solution that leaching is processed through super acid is carried out to the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid; The 4th obtained end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate, and return and carry out high Ore Leaching processing by the first obtained filtrate with the 4th supernatant liquor; Under the terminal acidity that is 4.0 with pH at the temperature of 90 degrees Celsius, utilize zinc roasted ore to spray deironing processing to the second supernatant liquor obtaining, thereby can obtain iron ore slurry; Obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.And obtained coarse sand and the 3rd supernatant liquor are returned and carry out neutralizing treatment; Above obtained mixing solutions is carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid; Above the 5th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate, and the 5th obtained supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.
The composition of the first supernatant liquor, scum and the plumbous silver-colored slag obtaining after processing by aforesaid method is in Table 2-4:
The first supernatant liquor composition is as following table 2:
Table 2
| Element | Zn | Cu | Cd | Co | Ni |
| Composition g/L | 130～140 | 0.47 | 0.28 | 0.04 | 0.037 |
Scum slag rate 46%, main component is as following table 3:
Table 3
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 10 | 1.34 | 0.29 | 30 | 2.57 | 0.72 | 0.16 | 3.35 | 0.0152 | 0.044 |
Plumbous silver-colored slag slag rate 12%, main component is as following table 4:
Table 4
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 5.0 | 11.4 | 0.76 | 12 | 15.0 | 5.77 | 0.68 | 19.47 | 0.1265 | 0.015 |
Embodiment 2
Get the 100kg zinc roasted ore of said components, it is processed, specifically comprise the following steps:
Under the terminal acidity that is 5.0 with pH after roasted ore is mixed with oxygenant and electrolytic solution, carry out neutrality and leach processing 2.5 hours at the temperature of 70 degrees Celsius, thereby can obtain neutral leach liquor; Obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid; Under the terminal acidity that is 1.5 with pH, the first obtained end liquid is carried out to neutralizing treatment 2 hours at the temperature of 65 degrees Celsius, thereby can obtain the solution through neutralizing treatment; The solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid; At the temperature of 95 degrees Celsius, process 4 hours for the second obtained end liquid being carried out under 55g/L condition to high Ore Leaching with terminal acidity, thereby can obtain the solution through high Ore Leaching processing; The solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid; At the temperature of 95 degrees Celsius, be under 120g/L condition with terminal acidity, the 3rd obtained end liquid carried out to super acid and leach processing 4 hours, thereby can obtain leaching through super acid the solution of processing; The obtained solution that leaching is processed through super acid is carried out to the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid; The 4th obtained end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate, and return and carry out high Ore Leaching processing by the first obtained filtrate with the 4th supernatant liquor; Under the terminal acidity that is 3.8 with pH at the temperature of 90 degrees Celsius, utilize zinc oxide fumes to spray deironing processing to the second supernatant liquor obtaining, thereby can obtain iron ore slurry; Obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.And obtained coarse sand and the 3rd supernatant liquor are returned and carry out neutralizing treatment; Above obtained mixing solutions is carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid; Above the 5th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate, and the 5th obtained supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.
The composition of the first supernatant liquor, scum and the plumbous silver-colored slag obtaining after processing by aforesaid method is in Table 5-7:
The first supernatant liquor composition is as following table 5:
Table 5
| Element | Zn | Cu | Cd | Co | Ni |
| Composition g/L | 130～140 | 0.5 | 0.3 | 0.05 | 0.04 |
Scum slag rate 44%, main component is as following table 6:
Table 6
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 8 | 1.5 | 0.2 | 32 | 2.6 | 0.76 | 0.17 | 3.58 | 0.018 | 0.05 |
Plumbous silver-colored slag slag rate 10%, main component is as following table 7:
Table 7
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 4.5 | 15 | 0.76 | 10 | 15.2 | 5.77 | 0.68 | 19.48 | 0.15 | 0.015 |
Comparative example
Get the 100kg zinc roasted ore of said components, it is processed, specifically comprise the following steps:
Under the terminal acidity that is 5.2 with pH after roasted ore is mixed with oxygenant and electrolytic solution, carry out neutrality and leach processing 2 hours at the temperature of 65 degrees Celsius, thereby can obtain neutral leach liquor; Obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid; Under the terminal acidity that is 2.0 with pH, the first obtained end liquid is carried out to neutralizing treatment 2 hours at the temperature of 70 degrees Celsius, thereby can obtain the solution through neutralizing treatment; The solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid; At the temperature of 90 degrees Celsius, process 2 hours for the second obtained end liquid being carried out under 50g/L condition to high Ore Leaching with terminal acidity, thereby can obtain the solution through high Ore Leaching processing; The solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid; The 3rd end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate, and return and carry out high Ore Leaching processing by the first obtained filtrate with the 3rd supernatant liquor; Under the condition that is 3.5 with terminal acidity at the temperature of 90 degrees Celsius, utilize bicarbonate of ammonia and sodium bicarbonate to spray deironing processing to the second supernatant liquor obtaining, thereby can obtain iron ore slurry; Obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions; And obtained coarse sand and the second supernatant liquor are returned and carry out neutralizing treatment; Above obtained mixing solutions is carried out to the 4th dense processing, thereby can obtain respectively the 4th supernatant liquor and the 4th end liquid; Above the 4th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate, and the 4th obtained supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.
The composition of the first supernatant liquor, scum and the plumbous silver-colored slag obtaining after processing by aforesaid method is in Table 8-10:
The first supernatant liquor composition is as following table 8:
Table 8
| Element | Zn | Cu | Cd | Co | Ni |
| Composition g/L | 130～140 | 0.4 | 0.2 | 0.02 | 0.02 |
Scum slag rate: 28%, main component is as following table 9:
Table 9
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 4.2 | 0.15 | 0.16 | 26 | 11.85 | 0.6 | 0.2 | 3.2 | 0.004 | 0.015 |
Plumbous silver-colored slag slag rate: 26%, main component is as following table 10:
Table 10
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 5.8 | 3.4 | 0.2 | 20 | 10.6 | 1.35 | 0.8 | 7.9 | 0.02 | 0.014 |
As can be seen here, the scum rate in embodiment 1-2 is high compared with comparative example, and plumbous silver-colored slag rate is low compared with comparative example, simultaneously without adding Na
+, NH
4 +the heavy chalybeate such as salt, and in plumbous silver-colored slag, plumbous silver is of high grade, can comprehensively reclaim the valuable metals such as lead, silver, copper, cadmium, cobalt, indium, bismuth, effectively improve valuable metal recovery utilization ratio, the plumbous silver-colored slag of higher-grade obtaining send plumbous reduction furnace for smelting direct production lead bullion, has realized the technique object of plumbous zinc complementation, wet fire compatibility, energy-saving and emission-reduction, has opened up new way for reducing zinc hydrometallurgy production cost, realize that smelting waste slag is innoxious, the object of resource utilization, promoted the lifting of Business Economic Benefit.
In the description of this specification sheets, the description of reference term " embodiment ", " some embodiment ", " example ", " concrete example " or " some examples " etc. means to be contained at least one embodiment of the present utility model or example in conjunction with specific features, structure, material or the feature of this embodiment or example description.In this manual, the schematic statement of above-mentioned term is not necessarily referred to identical embodiment or example.And specific features, structure, material or the feature of description can be with suitable mode combination in any one or more embodiment or example.
Although illustrated and described embodiment of the present utility model above, be understandable that, above-described embodiment is exemplary, can not be interpreted as restriction of the present utility model, those of ordinary skill in the art can change above-described embodiment in the situation that not departing from principle of the present utility model and aim in scope of the present utility model, amendment, replacement and modification.
Claims (5)
1. a system of processing zinc roasted ore, is characterized in that, comprising:
Neutral leaching device, described neutral leaching device has mineral supplying opening, oxygenant supplying opening, electrolyte supply mouth and the neutral product that leaches and exports;
The first dense device, described the first dense device has neutral leaching product entrance, the first supernatant liquor exports and the liquid outlet of first end, and the described neutral product entrance that leaches is connected with the outlet of described neutrality leaching product;
Neutralizing treatment device, described neutralizing treatment device has the first end liquid entrance and the outlet of neutralizing treatment product, and described the first end liquid entrance is connected with described the first end liquid outlet;
The second dense device, described the second dense device has neutralizing treatment product entrance, the second supernatant liquor outlet and the liquid outlet of second end, and described neutralizing treatment product entrance is connected with described neutralizing treatment product outlet;
Peracid leaching device, described peracid leaching device has the second end liquid entrance and the outlet of high Ore Leaching product, and described the second end liquid entrance is connected with described the second end liquid outlet;
The 3rd dense device, described the 3rd dense device has high Ore Leaching product entrance, the 3rd supernatant liquor outlet and the liquid outlet of the 3rd end, and described high Ore Leaching product entrance is connected with described high Ore Leaching product outlet;
Super acid leaching device, described super acid leaching device has the 3rd end liquid entrance, electrolyte entrance, sulphuric acid soln entrance and super acid and leaches product outlet, and described the 3rd end liquid entrance is connected with described the 3rd end liquid outlet;
The 4th dense device, described the 4th dense device has super acid and leaches product entrance, the 4th supernatant liquor outlet and the liquid outlet of the 4th end, and described super acid leaches product entrance and is connected with the outlet of described super acid leaching product;
The first washing and filtering device, described the first washing and filtering device has the 4th end liquid entrance, plumbous silver-colored slag outlet and the first filtrate outlet, and described the 4th end liquid entrance is connected with described the 4th end liquid outlet;
Spray deironing apparatus, described spray deironing apparatus has the second supernatant liquor entrance, material inlet and the outlet of iron ore slurry, and described the second supernatant liquor entrance is connected with described the second supernatant liquor outlet;
Sorting equipment, described sorting equipment has iron ore slurry entrance, coarse sand outlet and mixing solutions outlet, and described iron ore slurry entrance is connected with the outlet of described iron ore slurry;
The 5th dense device, described the 5th dense device has mixing solutions entrance, the 5th supernatant liquor outlet and the liquid outlet of the 5th end, and described mixing solutions entrance is connected with described mixing solutions outlet; And
The second washing and filtering device, described the second washing and filtering device has the 5th end liquid entrance, scum outlet and the second filtrate outlet, and described the 5th end liquid entrance is connected with described the 5th end liquid outlet.
2. the system of processing zinc roasted ore according to claim 1, is characterized in that, further comprises:
Refining plant, described refining plant has the first supernatant liquor entrance and scavenging solution outlet, and described the first supernatant liquor entrance is connected with described the first supernatant liquor outlet.
3. the system of processing zinc roasted ore according to claim 1, it is characterized in that, described neutralizing treatment device further has the 3rd supernatant liquor entrance and coarse sand entrance, and described the 3rd supernatant liquor entrance is connected with described the 3rd supernatant liquor outlet, and described coarse sand entrance is connected with described coarse sand outlet.
4. the system of processing zinc roasted ore according to claim 1, it is characterized in that, described peracid leaching device further has the 4th supernatant liquor entrance and the first filtrate entrance, described the 4th supernatant liquor entrance is connected with described the 4th supernatant liquor outlet, and described the first filtrate entrance is connected with described the first filtrate outlet.
5. the system of processing zinc roasted ore according to claim 1, it is characterized in that, described neutral leaching device further has the 5th supernatant liquor entrance and the second filtrate entrance, described the 5th supernatant liquor entrance is connected with described the 5th supernatant liquor outlet, and described the second filtrate entrance is connected with described the second filtrate outlet.
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