CN1243838C - Technology for preparing cell-level high purified nickel sulfate by the selective leach of water quenching high grade nickel and sulfuric acid - Google Patents
Technology for preparing cell-level high purified nickel sulfate by the selective leach of water quenching high grade nickel and sulfuric acid Download PDFInfo
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- CN1243838C CN1243838C CNB2003101100920A CN200310110092A CN1243838C CN 1243838 C CN1243838 C CN 1243838C CN B2003101100920 A CNB2003101100920 A CN B2003101100920A CN 200310110092 A CN200310110092 A CN 200310110092A CN 1243838 C CN1243838 C CN 1243838C
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- nickel
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- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 40
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 238000005516 engineering process Methods 0.000 title claims abstract description 22
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 17
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 title abstract 3
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 title abstract 3
- 238000010791 quenching Methods 0.000 title abstract 3
- 230000000171 quenching effect Effects 0.000 title abstract 3
- 238000002425 crystallisation Methods 0.000 claims abstract description 32
- 239000010949 copper Substances 0.000 claims abstract description 29
- 230000008025 crystallization Effects 0.000 claims abstract description 29
- 238000000605 extraction Methods 0.000 claims abstract description 27
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910052802 copper Inorganic materials 0.000 claims abstract description 25
- 238000001704 evaporation Methods 0.000 claims abstract description 15
- 238000000227 grinding Methods 0.000 claims abstract description 15
- 230000008020 evaporation Effects 0.000 claims abstract description 8
- 229910000365 copper sulfate Inorganic materials 0.000 claims abstract description 7
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 claims abstract description 7
- 239000007787 solid Substances 0.000 claims description 28
- 238000002386 leaching Methods 0.000 claims description 27
- 238000000926 separation method Methods 0.000 claims description 27
- 238000004070 electrodeposition Methods 0.000 claims description 19
- HIRWGWMTAVZIPF-UHFFFAOYSA-N nickel;sulfuric acid Chemical compound [Ni].OS(O)(=O)=O HIRWGWMTAVZIPF-UHFFFAOYSA-N 0.000 claims description 14
- VDJVKLUWBYHLOA-UHFFFAOYSA-N nickel sulfuric acid Chemical compound [Ni].S(O)(O)(=O)=O.[Ni] VDJVKLUWBYHLOA-UHFFFAOYSA-N 0.000 claims description 7
- 238000009834 vaporization Methods 0.000 claims description 6
- 230000008016 vaporization Effects 0.000 claims description 6
- 239000012452 mother liquor Substances 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 239000003792 electrolyte Substances 0.000 claims description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 3
- 239000011707 mineral Substances 0.000 claims description 3
- 239000002002 slurry Substances 0.000 claims description 3
- 239000003570 air Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 22
- 239000002994 raw material Substances 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000000243 solution Substances 0.000 abstract description 4
- 239000000463 material Substances 0.000 abstract description 3
- 238000004537 pulping Methods 0.000 abstract 3
- 238000005363 electrowinning Methods 0.000 abstract 2
- 239000000284 extract Substances 0.000 abstract 1
- 239000010413 mother solution Substances 0.000 abstract 1
- 239000000843 powder Substances 0.000 abstract 1
- 235000011149 sulphuric acid Nutrition 0.000 abstract 1
- 238000007738 vacuum evaporation Methods 0.000 abstract 1
- 239000000203 mixture Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 238000005273 aeration Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000001627 detrimental effect Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 150000002815 nickel Chemical class 0.000 description 2
- 238000006213 oxygenation reaction Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 229910020630 Co Ni Inorganic materials 0.000 description 1
- DYPAOELAZODIQL-UHFFFAOYSA-N S(O)(O)(=O)=O.[C]=O Chemical compound S(O)(O)(=O)=O.[C]=O DYPAOELAZODIQL-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- XIKYYQJBTPYKSG-UHFFFAOYSA-N nickel Chemical compound [Ni].[Ni] XIKYYQJBTPYKSG-UHFFFAOYSA-N 0.000 description 1
- BFDHFSHZJLFAMC-UHFFFAOYSA-L nickel(ii) hydroxide Chemical compound [OH-].[OH-].[Ni+2] BFDHFSHZJLFAMC-UHFFFAOYSA-L 0.000 description 1
- 239000007774 positive electrode material Substances 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 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
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- Manufacture And Refinement Of Metals (AREA)
Abstract
The present invention relates to a technology of preparing the highly pure nickel sulfate of battery-grade by the selective extraction of water quenching high nickel matte and sulphuric acids. The technology is characterized in that the technology comprises the following steps: step 1, finely grinding high nickel matte, treating the ground high nickel matte with a first-stage normal pressure extraction working procedure, treating the lixivium with an evaporation crystallization working procedure and treating the extracted residues with a pulping and presoaking working procedure; step 2, treating the presoaked residues with a second-stage pressure extraction working procedure and returning the lixivium to the first-stage normal pressure extraction working procedure for normal pressure extraction; step 3, treating the extracted residues with a third-stage pressure extraction working procedure, preparing the lixivium into cathode copper with a copper electrowinning working procedure or preparing the lixivium into copper sulfate with the evaporation crystallization working procedure and returning the anode solution obtained from the copper electrowinning working procedure or the mother solution obtained from the evaporation crystallization working procedure to the pulping and presoaking working procedure for pulping and presoaking; step 4, preparing the battery-grade high purity nickel sulfate by treating the extracts obtained from the first-stage normal pressure extraction, the second-stage pressure extraction and the third-stage pressure extraction with the vacuum evaporation crystallization working procedure. The technology has the advantages of low cost of the raw materials of water quenching high nickel matte, advanced technology equipment and parameter, low consumption of auxiliary materials and powder, high productive efficiency, good product quality, clean production process, no pollution, etc.
Description
Technical field
The present invention relates to the hydrometallurgy field, is that cell-grade high-purity sulphuric acid nickel technology is produced in the leaching of the high ice of a kind of shrend nickel sulfuric acid selectivity.
Background technology
The reparation technology of single nickel salt is different and different with end-use because of raw material, and existing classical reparation technology is: with shrend electricity nickel or nickle carbonoxide sulfuric acid dissolution, rich nickel solution evaporative crystallization forms.Its advantage is that technical process is short, quality product is high, but because raw material price height, common this technology is not used; Another kind of technology is that low copper high ice nickel of employing or nickel-containing material are raw material, and through the whole precious metals of sulfuric acid pressurization leaching, single nickel salt is produced in purification separation, evaporation, crystallization again.But the purification separation operation of this technology is brought other foreign ion into (as Na
+, Cl
-Deng), be difficult to production cell-grade high-purity sulphuric acid nickel.
Summary of the invention
Technical problem to be solved by this invention provides a kind of technology advanced person, production process cleaning, pollution-free, and the production efficiency height, cost is low, and the high ice of the shrend of good product quality nickel sulfuric acid selectivity leaches produces cell-grade high-purity sulphuric acid nickel technology.
Solving the technical scheme that its technical problem adopts is:
The high ice of a kind of shrend nickel sulfuric acid selectivity leaches produces cell-grade high-purity sulphuric acid nickel technology, is characterized in comprising successively following steps;
(a) the broken high ice nickel fine grinding operation 1 of water, the granularity-320 orders-0.045mm after 1 fine grinding of fine grinding operation accounts for 72%, and-200 orders-0.074mm accounts for 90%;
(b) leach liquor, water, air, 93% sulfuric acid of the height of fine grinding ice nickel minerals slurry and liquid-solid separation circuit 6 are sent into 75～85 ℃ of the extraction temperatures that first section normal pressure leaches 2, the first sections normal pressures leachings of operation operation 2, extraction time 6～8h;
(c) ore pulp of first section normal pressure leaching enters liquid-solid separation circuit 3, first section normal pressure leach liquor after the separation send vacuum evaporating crystalization operation 10 to carry out evaporative crystallization and produces cell-grade high-purity sulphuric acid nickel, 90 ℃ of the vaporization temperatures of vacuum evaporating crystalization operation 10, vacuum tightness 0.06MPa, 38～40 ℃ of crystallisation by cooling terminal temperatures;
(d) liquid-solid isolating first section normal pressure leached mud, send into pulp preimpregnation operation 4 with the anolyte of copper electrodeposition in copper electrodeposition or the evaporative crystallization operation 9 or copper sulfate mother liquor, water, air, 93% sulfuric acid of evaporative crystallization, 70～80 ℃ of pulp preimpregnation operation 4 preimpregnation temperature, preimpregnation time 6～8h;
(e) ore pulp after the preimpregnation, oxygen directly inject 5, the second sections pressurization leachings of second section pressurization leaching operation operation, 5 total pressures, 0.65～0.75MPa, pressurization extraction time 3～4h, 150～165 ℃ of pressurization extraction temperatures;
(f) ore pulp of second section pressurization leaching enters liquid-solid separation circuit 6, and two sections pressurization leach liquors after the separation send first section normal pressure to leach operation 2;
(g) liquid-solid isolating second section pressurization leached mud adds water, air, 93% sulfuric acid and sends into the 3rd section pressurization and leach 7, the three sections pressurizations of operation and leach operation 7 total pressures 0.6～0.8MPa, 150～170 ℃ of extraction temperatures, extraction time 5～6h;
(h) the 3rd section pressurization leached ore pulp and entered liquid-solid separation circuit 8, the 3rd section leached mud otherwise processed after the separation;
(j) liquid-solid isolating the 3rd section leach liquor send copper electrodeposition or evaporative crystallization operation 9,55～60 ℃ of the copper electrodeposition electrolyte temperatures of copper electrodeposition or evaporative crystallization operation 9,85～90 ℃ of the vaporization temperatures of evaporative crystallization, evaporation vacuum tightness 0.04MPa, 50～60 ℃ of drying temperatures, the copper electrodeposition is made electrolytic copper or evaporative crystallization is made copper sulfate, and the anolyte of copper electrodeposition or the mother liquor of evaporative crystallization are sent pulp preimpregnation operation 4 again back to.
The high ice of shrend of the present invention nickel sulfuric acid selectivity leaches produces cell-grade high-purity sulphuric acid nickel technology, and it is low to have the high ice of a shrend nickel raw materials cost, technology advanced person, subsidiary material and power consumption are low, the labor productivity height, good product quality, production process cleaning, advantage such as pollution-free.The cell-grade high-purity sulphuric acid nickel that this technology is produced makes the detrimental impurity Ca, the Mg that are difficult in the product remove be reduced to Ca≤0.001%, Mg≤0.002%, and also other various detrimental impurity content are all less than 0.001%.Because product also contains cobalt, therefore, helps improving the performance of metal-hydrogen nickel battery (Ni/MH) positive electrode material (spherical nickel hydroxide).
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Embodiment
Utilize drawings and Examples that the present invention is further described below.
With reference to Fig. 1, the leaching of the high ice of shrend nickel sulfuric acid selectivity is produced cell-grade high-purity sulphuric acid nickel technology and is comprised following steps successively:
The broken high ice nickel fine grinding operation 1 of water adopts the fine grinding of two-stage overflow ball mill gravity flow series connection open circuit;
It is that the height ice nickel minerals slurry water of fine grinding and the leach liquor of liquid-solid separation circuit 6 are poured in the pulp groove that first section normal pressure leaches operation 2, continuously in the pulp groove bubbling air, add entry, 93% sulfuric acid, stir, carry out first section normal pressure at the normal pressure leaching vat and leach;
Liquid-solid separation circuit 3 is first section normal pressure leaching ore pulp to be sent into thickener carry out liquid-solid separation, and first section normal pressure leach liquor after the separation send vacuum evaporating crystalization operation 10;
Pulp preimpregnation operation 4 is with liquid-solid isolating first section normal pressure leached mud, and the mother liquor of the anolyte of copper electrodeposition or copper sulfate evaporative crystallization, water, air and 93% sulfuric acid are sent into pulp and given immersion trough and carry out preimpregnation in copper electrodeposition or the evaporative crystallization operation 9;
It is the ore pulp after the preimpregnation, oxygen directly to be injected carry out second section pressurization leaching in the autoclave that operation 5 is leached in second section pressurization;
Liquid-solid separation circuit 6 is ore pulps that second section pressurization leached, contain acid washing water enters thickener and carries out liquid-solid separation, and second section pressurization leach liquor after the separation send first section normal pressure to leach operation 2;
The 3rd section leaching operation 7 of pressurizeing is liquid-solid isolating second section pressurization leached mud to be added in water, air, the 93% sulfuric acid injection autoclave carry out the 3rd section pressurization leaching;
Liquid-solid separation circuit 8 is that the 3rd section pressurization leached ore pulp, contained acid washing water and enter pressure filter and carry out liquid-solid separation, the 3rd section pressurization leached mud otherwise processed after the separation;
Copper electrodeposition (or evaporative crystallization) operation 9 is liquid-solid isolating the 3rd section pressurization leach liquor to be entered the copper electrodeposition is made electrolytic copper or evaporative crystallization is made copper sulfate;
Vacuum evaporating crystalization operation 10 is that the normal pressure leach liquor of liquid-solid separation circuit 3 is produced cell-grade high-purity sulphuric acid nickel through vacuum evaporating crystalization.
The high ice of shrend nickel raw material is the commercially available prod that our company produces.Its main chemical (%)
Ni60～62；Co0.6～0.9；Cu9～12；Fe2～4；S20～22；SiO
2＜0.06；Al
2O
3＜0.01；CaO＜0.01；MgO0.07；Pb0.014；Zn0.004；Mn＜0.002；As0.042。
93% sulfuric acid is the commercially available prod that our company produces.
The high ice of shrend nickel fine grinding operation 1, with the fine grinding of two Ф 900 * 1800mm overflow ball mill polyphone open circuits, under feeding coal 500～530kgHGM/h and ore milling concentration 50～60% conditions, size-grade distribution after the two-stage fine grinding is that (0.045mm) account for 72% ,-200 orders (0.074mm) account for 90% to-320 orders.
Pulp, first section normal pressure leach the main technique condition of operation 2:
High ice nickel nickel leaching yield 15～25%;
Pulp, leaching ore pulp liquid-solid ratio 7～8/1[m
3/ t-HGM]
Pressurized air aeration quantity: 12～16m
3/ hm
3Ore pulp
Extraction temperature: 75～85 ℃
Extraction time: 6～8h
Leach terminal point solution pH value 〉=6.3
First section normal pressure leach liquor typical case composition:
Ni90～95g/l；Cu≤0.002g/l；Fe≤0.002g/l；Co0.7～0.9g/l；PH≥6.3。
First section normal pressure leached mud typical case composition:
Ni40～45％；Cu16～20％；Co0.3～0.4％；Fe4～5％；S19-20％。
Leaching yield: Ni15～25%; Cu＜o; Fe＜0.
Pulp preimpregnation operation 4 main technique conditions
Pulp, preimpregnation ore pulp liquid-solid ratio 5.6～6.2/1[m
3/ t-HGM].
Preimpregnation temperature: 70～80 ℃
Aeration quantity: 6～12m
3/ hm
3Ore pulp
The preimpregnation time: 6～8h
The pH value 1.5～2.5 of preimpregnation terminal point
Operation 5 main technique conditions are leached in second section pressurization
Autoclave oxygenation capacity: 6～8m
3/ hm
3Ore pulp
Autoclave total pressure: 0.65～0.75MPa, wherein oxygen partial pressure 0.15～0.25MPa in the still
Pressurization extraction time: 3～4h
The pressurization extraction temperature: 150～165 ℃, leaching process is a self-heating.
The typical composition of second section pressurization leach liquor:
Ni100gl；Cu5～15g/l；Fe＜1g/l；H
2SO
43～4g/l；PH1.5～2.5。
Second section pressurization leached mud typical case composition:
Ni5～15％；Cu35～55％；Co0.15％；Fe8～10％；S20-22％。
Second section pressurization leaching yield and first section normal pressure leaching yield accumulative total
Ni90～95％；Cu≤0；Fe≤0
Operation 7 main technique conditions are leached in the 3rd section pressurization
Leach ore pulp liquid-solid ratio 5.3/1[m
3Two sections slags of/t]
Solution contains acid: 5～10g/l
Extraction temperature: 150～170 ℃, leaching process is a self-heating.
Extraction time: 5～6h
Autoclave pressure: 0.6～0.8MPa
Oxygenation capacity: 12～18m
3/ hm
3Ore pulp
The typical composition of the 3rd section pressurization leach liquor:
Ni＜30g/l；Cu80～90g/l；Fe＜0.5g/l；H
2So
45～10g/l。
The 3rd section pressurization leaching yield and second section pressurization leaching yield, first section normal pressure leaching yield accumulative total
Ni99.5％；Co＞98％；Cu≥90％；S98％；Fe＜0
The main technique condition of copper electrodeposition or evaporative crystallization operation 9
Electrolyte temperature: 55～60 ℃;
85～90 ℃ of the vaporization temperatures of evaporative crystallization;
Evaporation vacuum tightness 0.04MPa;
50～60 ℃ of drying temperatures.
Evaporative crystallization is made the cobalt high-purity sulphuric acid nickel operation 10 main technique conditions that contain
Liquid PH3.5 before the evaporation～4.0
90 ℃ of vaporization temperatures, vacuum tightness 0.06MPa
38～40 ℃ of crystallisation by cooling terminal temperatures
Explained hereafter of the present invention contain cobalt high-purity sulphuric acid nickel product through Beijing Physichemistry Analysis ﹠ Measurment Centre, Beijing Mine and Metallurgy General Inst's analytical test, its result (%) is as following table:
| Ni+Co | Ni | Co | Cu | Fe | Pb | Zn |
| 22.25 | 22.07 | 0.18 | ＜0.0001 | ＜0.0001 | ＜0.0001 | ＜0.0005 |
| Ca | Mg | Al | Cd | Na + | K + | As |
| 0.00084 | 0.001 | ＜0.0005 | ＜0.0001 | 0.00026 | 0.00064 | ＜0.0005 |
| No 3 - | Cl - | NH 4 + | Mn | Water-insoluble | ||
| ＜0.001 | ＜0.001 | ＜0.001 | 0.00013 | 0.001 |
Claims (1)
1, the high ice of a kind of shrend nickel sulfuric acid selectivity leaches and produces cell-grade high-purity sulphuric acid nickel technology, it is characterized in that comprising successively following steps;
(a) the broken high ice nickel fine grinding operation (1) of water, the granularity-320 orders-0.045mm after fine grinding operation (1) fine grinding accounts for 72%, and-200 orders-0.074mm accounts for 90%;
(b) leach liquor, water, air, 93% sulfuric acid of the height of fine grinding ice nickel minerals slurry and liquid-solid separation circuit (6) are sent into first section normal pressure and are leached operation (2), 75～85 ℃ of the extraction temperatures of first section normal pressure leaching operation (2), extraction time 6～8h;
(c) ore pulp of first section normal pressure leaching enters liquid-solid separation circuit (3), first section normal pressure leach liquor after the separation send vacuum evaporating crystalization operation (10) to carry out evaporative crystallization and produces cell-grade high-purity sulphuric acid nickel, 90 ℃ of the vaporization temperatures of vacuum evaporating crystalization operation (10), vacuum tightness 0.06MPa, 38～40 ℃ of crystallisation by cooling terminal temperatures;
(d) liquid-solid isolating first section normal pressure leached mud, send into pulp preimpregnation operation (4) with the anolyte of copper electrodeposition or copper sulfate mother liquor, water, air, 93% sulfuric acid of evaporative crystallization in copper electrodeposition or the evaporative crystallization operation (9), 70～80 ℃ of pulp preimpregnation operation (4) preimpregnation temperature, preimpregnation time 6～8h;
(e) ore pulp after the preimpregnation, oxygen directly inject second section pressurization leaching operation (5), and operation (5) total pressure 0.65～0.75MPa is leached in second section pressurization, pressurization extraction time 3～4h, 150～165 ℃ of pressurization extraction temperatures;
(f) ore pulp of second section pressurization leaching enters liquid-solid separation circuit (6), and two sections pressurization leach liquors after the separation send first section normal pressure to leach operation (2);
(g) liquid-solid isolating second section pressurization leached mud adds water, air, 93% sulfuric acid and sends into the 3rd section pressurization and leach operation (7), and operation (7) total pressure 0.6～0.8MPa, 150～170 ℃ of extraction temperatures, extraction time 5～6h are leached in the 3rd section pressurization;
(h) the 3rd section pressurization leached ore pulp and entered liquid-solid separation circuit (8), the 3rd section leached mud otherwise processed after the separation;
(j) liquid-solid isolating the 3rd section leach liquor send copper electrodeposition or evaporative crystallization operation (9), 55～60 ℃ of the copper electrodeposition electrolyte temperatures of copper electrodeposition or evaporative crystallization operation (9), 85～90 ℃ of the vaporization temperatures of evaporative crystallization, evaporation vacuum tightness 0.04MPa, 50～60 ℃ of drying temperatures, the copper electrodeposition is made electrolytic copper or evaporative crystallization is made copper sulfate, and the anolyte of copper electrodeposition or the mother liquor of evaporative crystallization are sent pulp preimpregnation operation (4) again back to.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101100920A CN1243838C (en) | 2003-11-13 | 2003-11-13 | Technology for preparing cell-level high purified nickel sulfate by the selective leach of water quenching high grade nickel and sulfuric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101100920A CN1243838C (en) | 2003-11-13 | 2003-11-13 | Technology for preparing cell-level high purified nickel sulfate by the selective leach of water quenching high grade nickel and sulfuric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1544664A CN1544664A (en) | 2004-11-10 |
| CN1243838C true CN1243838C (en) | 2006-03-01 |
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| CN101886167A (en) * | 2010-07-01 | 2010-11-17 | 北京矿冶研究总院 | Method for producing cathode nickel by selective leaching-electrodeposition of high nickel matte |
| FI20110279A0 (en) * | 2011-08-29 | 2011-08-29 | Outotec Oyj | A method for recovering metals from material containing them |
| CA2856341C (en) * | 2011-11-22 | 2016-08-09 | Sumitomo Metal Mining Co., Ltd. | Method for producing high-purity nickel sulfate |
| CN104611552A (en) * | 2014-12-31 | 2015-05-13 | 金川集团股份有限公司 | Method for extracting nickel from brown iron ore |
| CN104611550A (en) * | 2014-12-31 | 2015-05-13 | 金川集团股份有限公司 | Method for extracting nickel, cobalt and iron from limonite |
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| CN107630146B (en) * | 2017-08-07 | 2019-12-20 | 中国恩菲工程技术有限公司 | Nickel recovery process |
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| CN115323189B (en) * | 2022-08-24 | 2024-09-06 | 中国恩菲工程技术有限公司 | Nickel-sulfur treatment method with high copper content |
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2003
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