CN1299995C - Production process of copper sulfate from copper sulfide ore - Google Patents
Production process of copper sulfate from copper sulfide ore Download PDFInfo
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- CN1299995C CN1299995C CNB021101388A CN02110138A CN1299995C CN 1299995 C CN1299995 C CN 1299995C CN B021101388 A CNB021101388 A CN B021101388A CN 02110138 A CN02110138 A CN 02110138A CN 1299995 C CN1299995 C CN 1299995C
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- copper
- extraction
- copper sulfate
- leaching
- acid
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- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 title claims abstract description 44
- 229910000365 copper sulfate Inorganic materials 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- OMZSGWSJDCOLKM-UHFFFAOYSA-N copper(II) sulfide Chemical compound [S-2].[Cu+2] OMZSGWSJDCOLKM-UHFFFAOYSA-N 0.000 title abstract 5
- 239000010949 copper Substances 0.000 claims abstract description 62
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 54
- 229910052802 copper Inorganic materials 0.000 claims abstract description 50
- 238000000605 extraction Methods 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 24
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000002386 leaching Methods 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 14
- 238000002425 crystallisation Methods 0.000 claims abstract description 12
- 239000012074 organic phase Substances 0.000 claims abstract description 12
- 235000011149 sulphuric acid Nutrition 0.000 claims abstract description 11
- 239000002253 acid Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 230000008025 crystallization Effects 0.000 claims abstract description 5
- 239000007787 solid Substances 0.000 claims abstract description 5
- 239000000203 mixture Substances 0.000 claims abstract description 4
- 239000010413 mother solution Substances 0.000 claims abstract 3
- 239000000243 solution Substances 0.000 claims abstract 2
- 238000001354 calcination Methods 0.000 claims description 25
- 239000012452 mother liquor Substances 0.000 claims description 15
- BWFPGXWASODCHM-UHFFFAOYSA-N copper monosulfide Chemical compound [Cu]=S BWFPGXWASODCHM-UHFFFAOYSA-N 0.000 claims description 13
- 239000000047 product Substances 0.000 claims description 10
- 239000001117 sulphuric acid Substances 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 8
- -1 5-nonyl salicyl Chemical group 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 7
- 239000012535 impurity Substances 0.000 claims description 7
- 239000013078 crystal Substances 0.000 claims description 5
- JWLRQNQOJOZVOX-UHFFFAOYSA-N 2-(N-hydroxy-C-methylcarbonimidoyl)-4-nonylphenol Chemical compound CCCCCCCCCC1=CC=C(O)C(C(C)=NO)=C1 JWLRQNQOJOZVOX-UHFFFAOYSA-N 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 229910052717 sulfur Inorganic materials 0.000 claims description 4
- 239000011593 sulfur Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 3
- 125000003118 aryl group Chemical group 0.000 claims description 2
- 239000000706 filtrate Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 239000003795 chemical substances by application Substances 0.000 abstract description 14
- 238000005516 engineering process Methods 0.000 abstract description 9
- 239000000654 additive Substances 0.000 abstract description 3
- 239000000843 powder Substances 0.000 abstract 3
- 239000004576 sand Substances 0.000 abstract 3
- 239000013522 chelant Substances 0.000 abstract 1
- 239000007800 oxidant agent Substances 0.000 abstract 1
- 238000011084 recovery Methods 0.000 description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 7
- 238000000746 purification Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000013019 agitation Methods 0.000 description 2
- BERDEBHAJNAUOM-UHFFFAOYSA-N copper(I) oxide Inorganic materials [Cu]O[Cu] BERDEBHAJNAUOM-UHFFFAOYSA-N 0.000 description 2
- LBJNMUFDOHXDFG-UHFFFAOYSA-N copper;hydrate Chemical compound O.[Cu].[Cu] LBJNMUFDOHXDFG-UHFFFAOYSA-N 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000011889 copper foil Substances 0.000 description 1
- 229910000366 copper(II) sulfate Inorganic materials 0.000 description 1
- JZCCFEFSEZPSOG-UHFFFAOYSA-L copper(II) sulfate pentahydrate Chemical compound O.O.O.O.O.[Cu+2].[O-]S([O-])(=O)=O JZCCFEFSEZPSOG-UHFFFAOYSA-L 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
Images
Classifications
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- 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 production process for preparing copper sulfate from a copper sulfide ore, which is characterized in that no additives are added into copper sulfide ore powder, the copper sulfide ore powder is directly put in a Luqi's fluidizing reactor, and the copper sulfide ore powder is roasted into roasted sand copper at the temperature of 660 to 710 DEG C; the acid dissolving rate reaches more than 98%, and the water dissolving rate reaches 60 to 70%. The SO2 which is discharged from the fluidizing reactor can be directly used for preparing acid; the roasted sand copper is mixed with a dilute copper sulfate solution which is returned from an extraction process, and then, sulfuric acid is additionally added into the mixture to adjust the ratio of liquid to solids, which is 1 to 2: 1; the concentration of the ultimate acid (H2SO4) which is leached out is controlled to be less than or equal to 20 g/l. When copper is leached out, no oxidizing agents are added; the leaching rate of the copper is larger than or equal to 98%; a secondary mother solution which is formed after crystallization is extracted and purified by a chelate extraction agent, and the copper is directly recycled in a copper sulfate form. After the extraction liquid is back extracted by dilute sulfuric acid, the extraction liquid which is back extracted is returned to the leaching process to be used for leaching out roasted sand copper, and an organic phase which contains the extraction agent returns the secondary mother solution extracting process. The present invention has the advantages of simple technology and low production cost, and the total yield of the copper sulfate can reach more than 96%.
Description
Technical field
The present invention is relevant with the production technology of copper sulfate, more specifically says so about produced the improvement of copper sulfate production technology by copper-sulphide ores.
Background technology
The production of copper sulfate in the prior art, a kind of is that tankage with some copper are that raw material is produced copper sulfate.Patent such as CN1067454A, CN1127221A also discloses direct with the copper mine copper sulfate of getting made of stones.It is the production technology of raw material production copper sulfate that the CN1079207A patent has then been reported with the cupric sulfide.The CN1079207A patent is to add vitriol or inorganic salt such as nitrate, carbonate in copper-sulphide ores, makes calcining copper through roasting, makes copper sulfate by leaching thereafter.
In the above-mentioned production technique, in leach liquor, added iron powder or oxygenants such as nitric acid, nitrite respectively and eliminated iron in the leach liquor, precipitate and separate thereafter.The adding of multiple auxiliary agent has not only increased production cost, has also increased the impurity in the leach liquor, and influences the difficulty of copper sulfate subsequent production operation and the purity of product.Especially the secondary crystal mother liquor of copper sulfate production because impurities is more in the mother liquor, can only change into the copper sulfate that retains in the secondary mother liquid copper in the forms recovery mother liquors such as copper sponge or Red copper oxide in the prior art.So not only increase equipment and production cost, and reduced the actual total recovery of copper sulfate.
Summary of the invention
The object of the present invention is to provide that a kind of technology is simple, energy consumption is low, the utilization ratio height of copper, production cost be low, can produce the production technology of high purity and high copper sulfate yield.
Solution of the present invention is to adopt following technology to produce copper sulfate, and it comprises following key step:
1, the cupric sulfide breeze directly becomes calcining copper with the roasting of lucci type fluidizing reactor, and maturing temperature is 660-710 ℃, and control is 35-45m/s by the gas flow rate of blast cap, and the ebullated bed gas flow rate is 0.5-0.8m/s, and roasting time is 7-9 hour;
2, put into calcining copper and return vitriolated light copper-bath and mixes from extraction workshop section in leaching vat, and add sulfuric acid, adjusting its liquid-solid ratio is 1-2: 1, and sulfur acid (H when termination is leached in control
2SO
4)≤20g/L leaches copper sulfate down at 80-90 ℃, makes to contain Cu in the leach liquor
++At 150-300g/L, the leaching yield of copper is more than 98%;
3, leach liquor is removed residue after filtration, and the filtrate crystallisation by cooling obtains finished product copper sulfate, and its copper sulfate content is more than 96%;
4, mother liquor contains Cu through being concentrated into behind the primary crystallization
++Behind the 150-300g/L, to obtain content be finished product copper sulfate more than 94% to crystallisation by cooling once more;
5, mother liquor is removed wherein impurity with the extraction of general formula (I) chelating extractant behind the secondary crystal, reclaims the copper sulfate in the mother liquor;
6, after extraction liquid was stripped with dilute sulphuric acid, the sulfur acid copper anti-stripping agent that obtains returned the leaching operation and is used for the leaching of calcining copper.
Of the present invention primarily being characterised in that do not add any additives, directly the cupric sulfide breeze put into lucci type fluidized bed roasting kiln roasting and becomes calcining copper.This improvement makes gas bring up to 45m/s by the gas flow rate of blast cap by original 18m/s, boiling and heat and mass transfer process have been strengthened, air is mixed equably with the cupric sulfide breeze to be contacted, speed of response is accelerated, the roasting residence time shortens to 7-9 hour, has improved the throughput of siege.Its sour molten rate of the calcining copper that burns till reaches more than 98%; Maturing temperature of the present invention is controlled at 660-710 ℃, not only can improve the throughput of siege, and can make the ferrous iron in the calcining change into ferric iron to greatest extent, do not need to add any oxygenant, not only reduce production cost but also can obtain the fine leach liquor, alleviated the burden of the impurity and purification of subsequent handling.Leach liquor only need pass through forced filtration, can obtain leach liquor comparatively pure, that copper content is higher, does not need other impurity and purification to handle and concentrate, and gets final product direct crystallisation by cooling, obtains the copper sulfate finished product of content 〉=96%.
It is that the cupric sulfide breeze that enters stoving oven only needs drying a little that the present invention uses another characteristics of lucci type stoving oven roasting calcining copper, makes moisture content be lower than 8% and gets final product.Because calcining process do not need to add any additives, so the SO that goes out of roasting calcining copper bar
2, its concentration is 3.5-5%, can also be directly used in system sulfuric acid, has both reached the purpose of comprehensive utilization, has reduced production cost, has also reduced SO
2Tail gas is to the pollution of environment.
Another key character of the present invention is the purification treatment technology to secondary mother liquid.In the mother liquor of the leach liquor of calcining copper after twice crystallization enrichment plurality of impurities, it mainly contains Fe
+++, Fe
++, Zn
++, Mn
++, Ni
++, Ca
++, Mg
++Deng, if recirculation is used, can influence the copper sulfate quality product.Therefore be in the prior art Cu with iron filings
++Be replaced as copper sponge or with glucose with Cu
++Be reduced into method such as Red copper oxide and reclaim copper in the secondary mother liquid.These methods though the copper in the mother liquor is able to recycling, have in fact still influenced the actual recovery of copper sulfate, have also increased production unit and cost.
The characteristics that the present invention handles secondary mother liquid just are to adopt solvent extration directly with the copper sulfate in the copper sulfate form recovery secondary mother liquid, and will extract the pure copper-bath that reclaims and return and leach the leaching that operation is used for calcining copper once more, form a kind of closed circulation.Both save the energy, tooling cost, also improved the yield of copper sulfate.
The present invention's used chelating extractant in extraction process is the compound and the derivative thereof of following general formula (I) expression:
In the formula: R
1Be selected from C
9-12Alkyl;
R
2Be selected from hydrogen; C
1-2Alkyl or aryl.
The extraction agent that the present invention preferentially selects for use is: a kind of or its mixture in 5-nonyl salicyl aldooxime, 2-hydroxyl-5-nonyl phenyl methyl ketone oxime and the 2-hydroxyl-5-dodecyl diphenylketoxime.
Extraction process of the present invention comprises following key step:
1, secondary mother liquid transfers to and contains Cu
++8-12g/L does the extraction of three stage countercurrents with the chelating extractant of general formula (I), and extraction is in a ratio of: organic phase: water=1-1.5: 1, and PH is 1.8-2.0;
2, the organic phase after the extraction is made the secondary countercurrent reextraction with dilute sulphuric acid again and is got, and reextraction is in a ratio of: organic phase: water=2-2.5: 1.
Can obtain containing Cu by extraction process of the present invention
++The anti-stripping agent of 50g/L, the rate of recovery of extracting copper 〉=98% extracts cupric＜0.2g/L in the surplus liquid.
Adopt extraction process of the present invention, can obtain highly purified copper-bath, this solution can be used for production SILVER REAGENT and feed-grade bluestone, also can be used as the raw material of high value added products such as production pure copper powder, Copper Foil.The present invention then directly returns this highly purified copper-bath and leaches the leaching that operation is used for new round calcining copper.So the production cost of production technique copper sulfate of the present invention is low, the yield height, its total recovery is more than 96%.
Description of drawings
Fig. 1 is a technological process of production synoptic diagram of the present invention.
Among the figure, 1 becomes calcining copper for the roasting of cupric sulfide breeze, from the low concentration SO of roasting fire grate
2Gas is used to make sulfuric acid; The 2nd, calcining copper leaches copper sulfate with returning vitriolated light copper-bath with the dilute sulphuric acid pulp of adding; The 3rd, behind the leach liquor elimination residue for the first time crystallisation by cooling obtain containing 96% above finished product copper sulfate; 4 is that mother liquor crystallization for the second time after concentrating obtains containing 94% above copper sulfate finished product; The 5th, secondary mother liquid extraction agent extracting copper; The 6th, to strip with dilute sulphuric acid, the water that contains light copper sulfate returns the leaching operation and is used for the leaching of calcining copper, and the organic phase that contains extraction agent is returned the secondary mother liquid extraction process.
Embodiment
One, example the 1,2, the 3rd, and the cupric sulfide breeze becomes the embodiment of calcining copper with the roasting of lucci type fluidizing reactor, and the water content of cupric sulfide breeze is lower than 8%.
| Embodiment | 1 | 2 | 3 | |
| Roasting condition | Maturing temperature, ℃ | 670 | 690 | 710 |
| Gas velocity, m/s | 0.55 | 0.65 | 0.75 | |
| Roasting time, h | 8.5 | 8 | 7.5 | |
| The calcining performance | The molten rate of copper acid, % | 98.30 | 98.15 | 98.06 |
| The water-soluble rate of copper, % | 67.25 | 64.30 | 61.25 | |
Two, example 4,5 is the embodiment of calcining copper leaching
Embodiment 4: get the calcining 1000g of cupric 19.80%, control liquid-solid ratio 1.2: 1 was 80-90 ℃ of following agitation leach 60 minutes, whole acid concentration is controlled at below the 20g/L, the leaching yield of copper is 98.10%, and leach liquor is separated out copper sulfate crystal 778g, the rate of recovery 96.07%.
Embodiment 5, get the calcining 1000g of cupric 23.78%, control liquid-solid ratio 1.5: 1,80-90 ℃ of following agitation leach 60 minutes, whole acid concentration was controlled at below the 15g/L, and the leaching yield of copper is 98.21%, leach liquor is separated out copper sulfate crystal 934g, the rate of recovery 96.03%.
Three, example 6,7,8 is the embodiment of secondary mother liquid extracting and purifying processing.
Embodiment 6, with 5-nonyl salicyl aldooxime extraction treatment secondary mother liquid.
Get 1 liter of secondary mother liquid, contain Cu in the adjusting mother liquor
++Be 12g/L, PH is 1.8, adds the kerosin of 15% extraction agent, and the control extraction is in a ratio of 1.5: 1 does the extraction of three stage countercurrents.Copper bearing organic phase is carried out secondary with the dilute sulphuric acid of 180g/L and is stripped, and control is in a ratio of cupric 50g/L in 2.5: 1 anti-stripping agents, and cupric is less than 0.2g/L in the raffinate, and the rate of recovery of copper is 98.16%.
Embodiment 7, with 2-hydroxyl-5-dodecyl diphenylketoxime extraction treatment secondary mother liquid.
Get 1 liter of secondary mother liquid, contain Cu in the adjusting mother liquor
++Be 8g/L, PH is 2, adds the kerosin of 20% extraction agent, and the control extraction is in a ratio of 1: 1 does the extraction of three stage countercurrents.Copper bearing organic phase is carried out the secondary reextraction with the dilute sulphuric acid of 180g/L, and control is in a ratio of 2: 1, cupric 42g/L in the anti-stripping agent, and cupric is less than 0.2g/L in the raffinate, and the rate of recovery of copper is 98.08%.
Embodiment 8, with 2-hydroxyl-5-nonyl phenyl methyl ketone oxime extraction treatment secondary mother liquid.
Get 1 liter of secondary mother liquid, contain Cu in the adjusting mother liquor
++Be 10g/L, PH is 2, adds the kerosin of 20% extraction agent, and the control extraction is in a ratio of 1.5: 1 does the extraction of three stage countercurrents.Copper bearing organic phase is carried out the secondary reextraction with the dilute sulphuric acid of 180g/L, and control is in a ratio of 2.5: 1, cupric 49g/L in the anti-stripping agent, and cupric is less than 0.2g/L in the raffinate, and the rate of recovery of copper is 98.12%.
Embodiment 9, handle secondary mother liquid with 5-nonyl salicyl aldooxime and 1: 1 mixture extraction of 2-hydroxyl-5 nonyl phenyl methyl ketone oxime.
Get 1 liter of secondary mother liquid, transfer to during extraction and contain Cu in the mother liquor
++10-12g/L, pH value are 1.8, and extraction is in a ratio of 1.5: 1, do the extraction of three stage countercurrents.Copper bearing organic phase is carried out secondary with the dilute sulphuric acid of 180g/L and is stripped, and control is in a ratio of 2.5: 1, in the anti-stripping agent in the cupric 50g/L raffinate cupric be less than 0.2g/L, the rate of recovery 98.36% of copper.
Claims (3)
1, a kind ofly produce the production technique of copper sulfate, comprise breeze roasting, the leaching of calcining copper, crystallisation by cooling, crystalline mother solution treating processes, it is characterized in that comprising successively following key step by copper-sulphide ores:
1-1 cupric sulfide breeze is directly used in the roasting of lucci type fluidizing reactor and becomes calcining copper, and maturing temperature is 660-710 ℃, and control fluidizing furnace gas velocity is 0.5-0.8m/s, and roasting time is 7-9 hour;
1-2 puts into calcining copper and mixes with the vitriolated light copper-bath that returns from extraction workshop section in leaching vat, and add sulfuric acid, and the adjustment liquid-solid ratio is 1-2: 1, and sulfur acid≤20g/L when stopping is leached in control, leach copper sulfate down at 80-90 ℃, make to contain Cu in the leach liquor
2+At 150-300g/L;
The 1-3 leach liquor is removed residue after filtration, and the filtrate crystallisation by cooling obtains the copper sulfate finished product;
Mother liquor is after being concentrated into cupric 150-300g/L behind the 1-4 primary crystallization, and crystallisation by cooling obtains the copper sulfate finished product once more;
Mother liquor behind the 1-5 secondary crystal with the extraction of general formula (I) chelating extractant, is removed impurity, reclaims the copper sulfate in the mother liquor; Said general formula (I) is:
In the formula: R
1Be selected from C
9-12Alkyl; R
2Be selected from hydrogen, C
1-2Alkyl or aryl;
The 1-6 extraction liquid obtains sulfur acid copper stripping solution after stripping with dilute sulphuric acid, returns and leaches the leaching that operation is used for calcining copper.
2, according to the described copper sulfate production technique of claim 1, it is characterized in that said extraction process is further comprising the steps of in operation steps 1-5:
The 2-1 secondary mother liquid transfers to and contains Cu
2+8-12g/L, with the extraction of general formula (I) chelating extractant, extraction is in a ratio of: organic phase: water=1-1.5: 1 under the condition of pH value 1.8-2.0;
Organic phase after the 2-2 extraction is stripped with dilute sulphuric acid again, and reextraction is in a ratio of: organic phase: water=2-2.5: 1.
3, according to the described copper sulfate production technique of claim 2, it is selected from a kind of in 5-nonyl salicyl aldooxime, 2-hydroxyl-5-nonyl phenyl methyl ketone oxime, the 2-hydroxyl-5-dodecyl diphenylketoxime or its mixture to it is characterized in that said general formula (I) chelating extractant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021101388A CN1299995C (en) | 2002-03-28 | 2002-03-28 | Production process of copper sulfate from copper sulfide ore |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021101388A CN1299995C (en) | 2002-03-28 | 2002-03-28 | Production process of copper sulfate from copper sulfide ore |
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|---|---|
| CN1370742A CN1370742A (en) | 2002-09-25 |
| CN1299995C true CN1299995C (en) | 2007-02-14 |
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| CNB021101388A Expired - Fee Related CN1299995C (en) | 2002-03-28 | 2002-03-28 | Production process of copper sulfate from copper sulfide ore |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2255046C1 (en) * | 2003-11-06 | 2005-06-27 | Закрытое акционерное общество "Кыштымский медеэлектролитный завод" | Method for preparing copper sulfate |
| CN101643846B (en) * | 2009-08-31 | 2011-04-13 | 江西理工大学 | Complex copper sulphide ore thermal activating-pressure leaching technology |
| CN106916946B (en) * | 2017-03-30 | 2018-11-27 | 浙江华友钴业股份有限公司 | A kind of high-sulfur cobalt copper mine treatment process of the high leaching rate of low cost |
| CN118006919A (en) * | 2024-04-10 | 2024-05-10 | 矿冶科技集团有限公司 | A method for improving the leaching effect of copper sulfide ore by collaborative treatment |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1067454A (en) * | 1992-06-27 | 1992-12-30 | 林西县福利冶金化工厂 | The method of produce copper sulfate with copper ore |
| CN1196096A (en) * | 1995-09-07 | 1998-10-14 | 亨凯尔公司 | copper recovery method |
-
2002
- 2002-03-28 CN CNB021101388A patent/CN1299995C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1067454A (en) * | 1992-06-27 | 1992-12-30 | 林西县福利冶金化工厂 | The method of produce copper sulfate with copper ore |
| CN1196096A (en) * | 1995-09-07 | 1998-10-14 | 亨凯尔公司 | copper recovery method |
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| CN1370742A (en) | 2002-09-25 |
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