CN101148698A - Extraction method for removing calcium and magnesium from copper-cobalt ore leachate - Google Patents
Extraction method for removing calcium and magnesium from copper-cobalt ore leachate Download PDFInfo
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- CN101148698A CN101148698A CNA2007100715004A CN200710071500A CN101148698A CN 101148698 A CN101148698 A CN 101148698A CN A2007100715004 A CNA2007100715004 A CN A2007100715004A CN 200710071500 A CN200710071500 A CN 200710071500A CN 101148698 A CN101148698 A CN 101148698A
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- magnesium
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- cobalt
- extraction
- ethylhexyl
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- 229910052749 magnesium Inorganic materials 0.000 title claims abstract description 45
- RYTYSMSQNNBZDP-UHFFFAOYSA-N cobalt copper Chemical compound [Co].[Cu] RYTYSMSQNNBZDP-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 238000000605 extraction Methods 0.000 title claims description 59
- 239000011777 magnesium Substances 0.000 title claims description 42
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims description 41
- 239000011575 calcium Substances 0.000 title claims description 39
- 229910052791 calcium Inorganic materials 0.000 title claims description 39
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims description 38
- 239000012074 organic phase Substances 0.000 claims abstract description 40
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 27
- 238000000034 method Methods 0.000 claims abstract description 24
- SEGLCEQVOFDUPX-UHFFFAOYSA-N di-(2-ethylhexyl)phosphoric acid Chemical compound CCCCC(CC)COP(O)(=O)OCC(CC)CCCC SEGLCEQVOFDUPX-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000003350 kerosene Substances 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000003960 organic solvent Substances 0.000 claims abstract description 6
- 239000012071 phase Substances 0.000 claims abstract description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 52
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 32
- 239000010941 cobalt Substances 0.000 claims description 29
- 229910017052 cobalt Inorganic materials 0.000 claims description 29
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 29
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 21
- 238000000638 solvent extraction Methods 0.000 claims description 21
- 229910052742 iron Inorganic materials 0.000 claims description 17
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 15
- 238000007127 saponification reaction Methods 0.000 claims description 15
- 239000001117 sulphuric acid Substances 0.000 claims description 15
- 235000011149 sulphuric acid Nutrition 0.000 claims description 15
- 239000002904 solvent Substances 0.000 claims description 12
- 238000005406 washing Methods 0.000 claims description 9
- 241000220317 Rosa Species 0.000 claims description 6
- 239000008346 aqueous phase Substances 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000000284 extract Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 229940044175 cobalt sulfate Drugs 0.000 abstract description 5
- 229910000361 cobalt sulfate Inorganic materials 0.000 abstract description 5
- KTVIXTQDYHMGHF-UHFFFAOYSA-L cobalt(2+) sulfate Chemical compound [Co+2].[O-]S([O-])(=O)=O KTVIXTQDYHMGHF-UHFFFAOYSA-L 0.000 abstract description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract description 2
- 229910001424 calcium ion Inorganic materials 0.000 abstract description 2
- 150000001868 cobalt Chemical class 0.000 abstract description 2
- 229910000428 cobalt oxide Inorganic materials 0.000 abstract description 2
- 229910001425 magnesium ion Inorganic materials 0.000 abstract description 2
- 239000000203 mixture Substances 0.000 abstract 2
- -1 2- ethyl hexyl phosphonate ester Chemical class 0.000 abstract 1
- 150000002500 ions Chemical class 0.000 abstract 1
- 239000005416 organic matter Substances 0.000 abstract 1
- PUZPDOWCWNUUKD-UHFFFAOYSA-M sodium fluoride Chemical compound [F-].[Na+] PUZPDOWCWNUUKD-UHFFFAOYSA-M 0.000 description 8
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 description 6
- 238000001556 precipitation Methods 0.000 description 6
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000011775 sodium fluoride Substances 0.000 description 4
- 235000013024 sodium fluoride Nutrition 0.000 description 4
- DDFHBQSCUXNBSA-UHFFFAOYSA-N 5-(5-carboxythiophen-2-yl)thiophene-2-carboxylic acid Chemical compound S1C(C(=O)O)=CC=C1C1=CC=C(C(O)=O)S1 DDFHBQSCUXNBSA-UHFFFAOYSA-N 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- YCYBZKSMUPTWEE-UHFFFAOYSA-L cobalt(ii) fluoride Chemical compound F[Co]F YCYBZKSMUPTWEE-UHFFFAOYSA-L 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009388 chemical precipitation Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 125000001153 fluoro group Chemical group F* 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910001453 nickel ion Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc 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 process of extracting Co and eliminating Ca from copper-cobalt ore includes obtaining mixture leachate with soluble sulfate of Co, Ni, Ca and Mg; and extracting the mixture leachate with organic solvent, which comprises organic matter bis(2-ethyl hexyl) phosphoric acid or 2- ethyl hexyl phosphonate ester in 15-25 vol% and kerosene in 75-85 vol%. The organic solvent extracting procedure includ es two steps, the first step of transferring Ca into the organic phase while leaving Co, Ni and Mg in the water phase, and the second step of transferring Co to the organic phase while leaving Ni and Mg in the water phase. The process can obtain cobalt sulfate solution with Co content up to 90-100 g/l, Ca ion content lowered to 0.01 g/l, Ni ion content lowered to 0.005 g/l, and Mg ion content lowered to 0.1 g/l and suitable for producing T-cobalt oxide and cobalt salt.
Description
Technical field
The present invention relates to a kind of extracting method of cobalt, particularly a kind of method from copper-cobalt mine leachate removing calcium with solvent extraction magnesium.
Background technology
The general operation that adopts traditional chemical precipitation purification and solvent extraction to combine of the sour molten leach liquor of copper cobalt ore is carried out purification and impurity removal, its flow process is: the solution that contains cobalt and impurity Ni, Fe, Ca, Mg, Cu, Mn, Zn etc. is earlier in oxidation and deironing, reagent precipitation calcium-magnesium removing is then through solvent extraction deep impurity-removing and separation of Cobalt and Nickel.
Reagent precipitation calcium-magnesium removing, method in common is to add Sodium Fluoride or ammonium fluoride at present, makes calcium magnesium and fluorine form the fluorochemical precipitation of indissoluble, removes by filter.The shortcoming of this method is: (1) Sodium Fluoride solubleness is little, and long reaction time needs heating, and energy consumption of reaction is big, and the fluorochemical sedimentation and filtration poor performance that generates; (2) Sodium Fluoride or ammonium fluoride cost an arm and a leg, and it is higher to purify the calcium-magnesium removing cost; (3) because the solubility product of cobaltous fluoride in water is smaller, in Sodium Fluoride or ammonium fluoride precipitator method calcium-magnesium removing, also there is a certain amount of cobalt to generate the cobaltous fluoride precipitation and enters in the slag, cause the yield of cobalt to reduce; (4) fluorine-containing in the waste water, cause the wastewater treatment difficulty.
Summary of the invention
The objective of the invention is provides a kind of method technology simple, reliable in order to solve above-mentioned the deficiencies in the prior art, the purification expense is low, and cobalt yield height is energy-conservation, need not increase facility investment, removal effect is good and can not cause the method from copper-cobalt mine leachate removing calcium with solvent extraction magnesium of environmental pollution.
In order to achieve the above object, a kind of method provided by the invention from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, it comprises the solubility rose vitriol that obtains from the copper cobalt ore, nickel, calcium, magnesium mixing leach liquor, it is characterized in that the solubility rose vitriol, nickel, calcium, magnesium mixing leach liquor organic solvent extraction, described organic extraction solvent is to contain the organism of volume ratio 15% to 25% and contain 75% to 85% kerosene, described organism is di-(2-ethylhexyl)phosphoric acid or di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester, described is that leach liquor is carried out two step removing calcium with solvent extraction magnesium with organic solvent extraction: the first step is with the solubility rose vitriol after the deironing, nickel, calcium, the magnesium leach liquor is regulated the pH value 2.0 to 5.0, extract with the extraction solvent that contains di-(2-ethylhexyl)phosphoric acid earlier, make calcium change organic phase over to and cobalt, nickel, magnesium remaines in aqueous phase; Dilute sulphuric acid with 0.5N to 2.0N concentration washs load organic phases again, make cobalt, nickel, magnesium further enter water, load organic phases is again through the hydrochloric acid back extraction of 1N to 4N concentration, calcium back extraction in the organic phase is come out, after the anti-iron of the hydrochloric acid of 5N to 7N concentration remaining iron back extraction in the organic phase is come out; Second step was with the extraction solvent that contains di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester the di-(2-ethylhexyl)phosphoric acid raffinate to be extracted again, make cobalt change organic phase over to, and nickel, magnesium change aqueous phase over to, dilute sulphuric acid with 0.5N to 2.0N concentration washs load organic phases again, and then with the dilute sulphuric acid of 2.0N to 4.0N concentration the cobalt back extraction in the organic phase is come out, after the hydrochloric acid of 5N to 7N concentration the iron back extraction in the organic phase is come out.
Describedly carry out in the two step removing calcium with solvent extraction magnesium processes: when the di-(2-ethylhexyl)phosphoric acid extraction calcium of the first step at leach liquor, adopt 8 grades to 15 grades extractions, dilute sulphuric acid with 0.5N to 2.0N concentration carries out 6 grades to 10 grades washings to load organic phases again, the hydrochloric acid of 1N to 4N concentration carries out 3 grades to 6 grades back extraction calcium, and the hydrochloric acid of 5N to 7N concentration carries out 3 grades to 5 grades back extraction iron; When the di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester extracting and separating cobalt in second step and nickel, magnesium, adopt 7 grades to 12 grades extractions, dilute sulphuric acid with 0.5N to 2.0N concentration carries out 5 grades to 8 grades washings to load organic phases again, with the dilute sulphuric acid of 2.0N to 4.0N concentration the cobalt in the organic phase is carried out 3 grades to 7 grades back extractions again and come out, the hydrochloric acid of last 5N to 7N concentration carries out 3 grades to 5 grades back extractions with the iron in the organic phase and comes out.The expression of above-mentioned " level " is number of times.As " 7 grades of extractions " is 7 extractions, and " 5 grades of washings " is 5 washings, and " 4 grades of anti-iron " is 4 times the iron back extraction to be operated.
During extraction, organic extraction solvent and the throughput ratio that is extracted between the phase are: the throughput ratio of di-(2-ethylhexyl)phosphoric acid extraction calcium is O/A=1: 2-3, and the throughput ratio of di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester separation of cobalt and nickel, magnesium is O/A=1: 1-2.At this, described O/A is: organic extraction solvent/be extracted phase.
Organism in the described organic extraction solvent, earlier carry out saponification with sodium hydroxide, control saponification degree by add-on to sodium hydroxide, wherein: the saponification degree of di-(2-ethylhexyl)phosphoric acid is controlled at 65%-68%, and the saponification degree of di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester is controlled at 62%-65%.
Because di-(2-ethylhexyl)phosphoric acid represents with normally used commodity chemical name P204, di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester represents with normally used commodity chemical name P507, and below both represent with P204 and P507 respectively.
In the present invention, because the calcium, the magnesium that exist in the extraction of sulfate medium are tedious, surpass 0.05g/L if enter the long-time calcic of feed liquid of P507 extracting and separating cobalt, nickel system, then after extraction for some time, might produce calcium sulfate precipitation in extraction section, so can by control P204 abstraction impurity removal compare (compare by flow and recently embody), saponification degree and pH, just can make P204 reach the purpose of preferential collection calcium.For the calcium sulfate precipitation of avoiding stripping section to generate indissoluble influences normally carrying out of extraction, so select for use hydrochloric acid to do reverse-extraction agent.
The invention has the beneficial effects as follows: (1) is combined as a whole P204 abstraction impurity removal and P507 separation of cobalt, nickel and deliming, magnesium dexterously; (2) the present invention separates calcium, nickel, magnesium from cobalt sulfate solution, make the cobalt contents in the cobalt sulfate solution reach 90g/L-100g/L, calcium ion is reduced to 0.01g/L, o.005g/L nickel ion is reduced to, magnesium ion is reduced to the following level of 0.1g/L, produces T-cobalt oxide and the specification of quality of producing cobalt salt thereby cobalt sulfate solution is met; (3) cost of the present invention is low, the efficient height; (4) technology of the present invention is simple, reliable, strong operability, safety; (5) to purify expense low in the present invention, and cobalt yield height is energy-conservation, need not increase facility investment, and removal effect is good and can not cause environmental pollution; (6) the present invention has the versatility on deliming, the magnesium method, promptly can be used for the cobalt sulfate solution calcium-magnesium removing of other any methods productions etc.
Description of drawings
Fig. 1 is an embodiment of the invention P204 extraction tandem table as a result;
Fig. 2 is an embodiment of the invention P507 extraction tandem table as a result.
Embodiment
The invention will be further described in conjunction with the accompanying drawings below by embodiment.
Embodiment
Embodiment:
A kind of method that present embodiment provides from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, be that the sulphuric leachate of the copper cobalt ore after the deironing is regulated its pH value 3.5 to 4.0 with sodium hydroxide, organic phase is by constituting as the P204 of extraction agent with as the kerosene of thinner, wherein the volume ratio of P204 is 15%, kerosene is 85%, saponification degree is 68%, stream is than O/A=1: 2-3, after 9 grades of contact extractions, make calcium change organic phase over to and cobalt, nickel, magnesium is stored among the water, dilute sulphuric acid with 1.2N concentration carries out 7 grades of washings to load organic phases again, make cobalt, nickel, magnesium enters water, and load organic phases comes out the calcium back extraction in the organic phase through 5 grades of back extractions of hydrochloric acid of 3N concentration, after 4 grades of anti-iron of the hydrochloric acid of 6N concentration remaining iron back extraction in the organic phase is come out.The result as shown in Figure 1.
The P204 raffinate is made the P507 feed liquid carry out 7 grades of extractions, make cobalt change organic phase over to, and nickel, magnesium change aqueous phase over to, dilute sulphuric acid with 1.2N concentration carries out 5 grades of washings to load organic phases again, isolate nickel in the organic phase, magnesium, and then with the dilute sulphuric acid of 3N concentration the cobalt back extraction in the organic phase is come out, after 4 grades of anti-iron of the hydrochloric acid of 6N concentration the iron back extraction in the organic phase is come out.Described organic phase is by constituting as the P507 of extraction agent with as the kerosene of thinner, and the volume ratio of P507 is 25%, kerosene is 75%, and saponification degree is 65%, and stream is than O/A=1: 1.The result as shown in Figure 2.
A kind of method provided by the invention from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, in comprehensive extracting and washing back extraction process, the total recovery of cobalt is greater than 99.5%, and the clearance of calcium is 98.2%, and the clearance of magnesium, nickel all can reach more than 97%.
Claims (5)
1. method from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, it comprises the solubility rose vitriol that obtains from the copper cobalt ore, nickel, calcium, magnesium mixing leach liquor, it is characterized in that the solubility rose vitriol, nickel, calcium, magnesium mixing leach liquor organic solvent extraction, described organic extraction solvent is to contain the organism of volume ratio 15% to 25% and contain 75% to 85% kerosene, described organism is di-(2-ethylhexyl)phosphoric acid or di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester, described is that leach liquor is carried out two step removing calcium with solvent extraction magnesium with organic solvent extraction: the first step is with the solubility rose vitriol after the deironing, nickel, calcium, the magnesium leach liquor is regulated the pH value 2.0 to 5.0, extract with the extraction solvent that contains di-(2-ethylhexyl)phosphoric acid earlier, make calcium change organic phase over to and cobalt, nickel, magnesium remaines in aqueous phase; Dilute sulphuric acid with 0.5N to 2.0N concentration washs load organic phases again, make cobalt, nickel, magnesium further enter water, load organic phases is again through the hydrochloric acid back extraction of 1N to 4N concentration, calcium back extraction in the organic phase is come out, after the anti-iron of the hydrochloric acid of 5N to 7N concentration remaining iron back extraction in the organic phase is come out; Second step was with the extraction solvent that contains di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester the di-(2-ethylhexyl)phosphoric acid raffinate to be extracted again, make cobalt change organic phase over to, and nickel, magnesium change aqueous phase over to, dilute sulphuric acid with 0.5N to 2.0N concentration washs load organic phases again, and then with the dilute sulphuric acid of 2.0N to 4.0N concentration the cobalt back extraction in the organic phase is come out, after the hydrochloric acid of 5N to 7N concentration the iron back extraction in the organic phase is come out.
2. a kind of method according to claim 1 from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, it is characterized in that carrying out in the two step removing calcium with solvent extraction magnesium processes: when the di-(2-ethylhexyl)phosphoric acid of the first step extracts calcium at leach liquor, adopt 8 grades to 15 grades extractions, dilute sulphuric acid with 0.5N to 2.0N concentration carries out 6 grades to 10 grades washings to load organic phases again, the hydrochloric acid of 1N to 4N concentration carries out 3 grades to 6 grades back extraction calcium, and the hydrochloric acid of 5N to 7N concentration carries out 3 grades to 5 grades back extraction iron; When the di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester extracting and separating cobalt in second step and nickel, magnesium, adopt 7 grades to 12 grades extractions, dilute sulphuric acid with 0.5N to 2.0N concentration carries out 5 grades to 8 grades washings to load organic phases again, with the dilute sulphuric acid of 2.0N to 4.0N concentration the cobalt in the organic phase is carried out 3 grades to 7 grades back extractions again and come out, the hydrochloric acid of last 5N to 7N concentration carries out 3 grades to 5 grades back extractions with the iron in the organic phase and comes out.
3. a kind of method according to claim 1 and 2 from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, when it is characterized in that extracting, organic extraction solvent and the throughput ratio that is extracted between the phase are: the throughput ratio of di-(2-ethylhexyl)phosphoric acid extraction calcium is O/A=1: 2-3, and the throughput ratio of di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester separation of cobalt and nickel, magnesium is O/A=1: 1-2.
4. a kind of method according to claim 1 and 2 from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, it is characterized in that the organism in the described organic extraction solvent, earlier carry out saponification with sodium hydroxide, control saponification degree by add-on to sodium hydroxide, wherein: the saponification degree of di-(2-ethylhexyl)phosphoric acid is controlled at 65%-68%, and the saponification degree of di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester is controlled at 62%-65%.
5. a kind of method according to claim 3 from copper-cobalt mine leachate removing calcium with solvent extraction magnesium, it is characterized in that the organism in the described organic extraction solvent, earlier carry out saponification with sodium hydroxide, control saponification degree by add-on to sodium hydroxide, wherein: the saponification degree of di-(2-ethylhexyl)phosphoric acid is controlled at 65%-68%, and the saponification degree of di-2-ethylhexyl phosphonic acid mono-2-ethylhexyl ester is controlled at 62%-65%.
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| CNB2007100715004A CN100552061C (en) | 2007-09-30 | 2007-09-30 | A method for extracting calcium and magnesium from copper-cobalt ore leaching solution |
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| CNB2007100715004A CN100552061C (en) | 2007-09-30 | 2007-09-30 | A method for extracting calcium and magnesium from copper-cobalt ore leaching solution |
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Cited By (30)
| Publication number | Priority date | Publication date | Assignee | Title |
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| KR101021180B1 (en) | 2010-07-27 | 2011-03-15 | 코스모화학 주식회사 | High purity cobalt sulfate production method |
| CN101643859B (en) * | 2008-08-07 | 2011-04-20 | 北京有色金属研究总院 | Process method for separating and purifying cobalt solution by extraction chromatography |
| CN102061390A (en) * | 2010-12-03 | 2011-05-18 | 安化金源新材料有限责任公司 | Method for directly producing high-purity electronic level cobaltous sulfate by using cobalt-containing waste |
| CN102181666A (en) * | 2011-05-06 | 2011-09-14 | 广西银亿科技矿冶有限公司 | Method for treating red soil nickel ore leaching liquid |
| CN102206834A (en) * | 2011-05-03 | 2011-10-05 | 四川省尼科国润新材料有限公司 | Method for directly producing electrolytic nickel by using low nickel matte |
| CN102417982A (en) * | 2011-11-29 | 2012-04-18 | 南通库博新材料有限公司 | Method for removing calcium and magnesium by adopting extraction method |
| CN102557153A (en) * | 2010-12-28 | 2012-07-11 | 上海轻工业研究所有限公司 | Method for removing calcium-magnesium impurities from nickel sulfate solution |
| CN101736151B (en) * | 2010-01-28 | 2012-07-25 | 浙江华友钴业股份有限公司 | Method for removing iron by oxidation and neutralization in cobalt wet smelting process |
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| CN104762485A (en) * | 2015-04-30 | 2015-07-08 | 河南佰利联化学股份有限公司 | Method for lowering calcium content in titanium slag |
| CN105803197A (en) * | 2014-12-29 | 2016-07-27 | 北京有色金属研究总院 | Method for removing calcium and magnesium from bioleaching solution of nickel cobalt by synergetic extraction method |
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