WO2018174148A1 - 金属酸化鉱の製錬方法 - Google Patents
金属酸化鉱の製錬方法 Download PDFInfo
- Publication number
- WO2018174148A1 WO2018174148A1 PCT/JP2018/011357 JP2018011357W WO2018174148A1 WO 2018174148 A1 WO2018174148 A1 WO 2018174148A1 JP 2018011357 W JP2018011357 W JP 2018011357W WO 2018174148 A1 WO2018174148 A1 WO 2018174148A1
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- WO
- WIPO (PCT)
- Prior art keywords
- scandium
- oxide ore
- nickel
- metal oxide
- cobalt
- Prior art date
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- 238000000034 method Methods 0.000 title claims abstract description 104
- 238000003723 Smelting Methods 0.000 title claims abstract description 42
- 229910044991 metal oxide Inorganic materials 0.000 title claims abstract description 42
- 150000004706 metal oxides Chemical class 0.000 title claims abstract description 42
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 162
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 96
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 81
- 229910017052 cobalt Inorganic materials 0.000 claims abstract description 75
- 239000010941 cobalt Substances 0.000 claims abstract description 75
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims abstract description 75
- 239000000243 solution Substances 0.000 claims abstract description 61
- 238000001471 micro-filtration Methods 0.000 claims abstract description 49
- 238000011084 recovery Methods 0.000 claims abstract description 45
- 238000002386 leaching Methods 0.000 claims abstract description 35
- 239000002002 slurry Substances 0.000 claims abstract description 35
- 239000000706 filtrate Substances 0.000 claims abstract description 32
- 238000000926 separation method Methods 0.000 claims abstract description 23
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 22
- 238000005987 sulfurization reaction Methods 0.000 claims abstract description 18
- 239000003929 acidic solution Substances 0.000 claims abstract description 16
- 239000002253 acid Substances 0.000 claims abstract description 15
- 230000003472 neutralizing effect Effects 0.000 claims abstract description 9
- 229910052706 scandium Inorganic materials 0.000 claims description 92
- SIXSYDAISGFNSX-UHFFFAOYSA-N scandium atom Chemical compound [Sc] SIXSYDAISGFNSX-UHFFFAOYSA-N 0.000 claims description 92
- 239000007788 liquid Substances 0.000 claims description 86
- 239000012528 membrane Substances 0.000 claims description 40
- 238000006386 neutralization reaction Methods 0.000 claims description 30
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 24
- 239000012510 hollow fiber Substances 0.000 claims description 24
- 238000000638 solvent extraction Methods 0.000 claims description 18
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 16
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 16
- 239000010419 fine particle Substances 0.000 claims description 13
- HYXGAEYDKFCVMU-UHFFFAOYSA-N scandium oxide Chemical compound O=[Sc]O[Sc]=O HYXGAEYDKFCVMU-UHFFFAOYSA-N 0.000 claims description 10
- 239000011148 porous material Substances 0.000 claims description 9
- 238000005342 ion exchange Methods 0.000 claims description 8
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 6
- 239000003480 eluent Substances 0.000 claims description 6
- 239000003456 ion exchange resin Substances 0.000 claims description 6
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical group S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 abstract description 20
- 239000002184 metal Substances 0.000 abstract description 20
- 239000002562 thickening agent Substances 0.000 abstract description 15
- 229910052976 metal sulfide Inorganic materials 0.000 abstract description 11
- 229910001111 Fine metal Inorganic materials 0.000 abstract description 7
- 239000011859 microparticle Substances 0.000 abstract description 3
- 238000001556 precipitation Methods 0.000 abstract description 2
- 230000001376 precipitating effect Effects 0.000 abstract 1
- 238000000605 extraction Methods 0.000 description 34
- 238000004062 sedimentation Methods 0.000 description 34
- 238000001914 filtration Methods 0.000 description 26
- 239000012535 impurity Substances 0.000 description 22
- 239000003960 organic solvent Substances 0.000 description 15
- 239000011347 resin Substances 0.000 description 12
- 229920005989 resin Polymers 0.000 description 12
- 238000005486 sulfidation Methods 0.000 description 11
- 229920002472 Starch Polymers 0.000 description 10
- 239000013522 chelant Substances 0.000 description 10
- 239000008107 starch Substances 0.000 description 10
- 235000019698 starch Nutrition 0.000 description 10
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 9
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 239000002245 particle Substances 0.000 description 8
- 238000011001 backwashing Methods 0.000 description 7
- 238000005201 scrubbing Methods 0.000 description 7
- 239000007787 solid Substances 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 6
- 239000002244 precipitate Substances 0.000 description 6
- 150000004763 sulfides Chemical class 0.000 description 6
- 238000004140 cleaning Methods 0.000 description 5
- LQPWUWOODZHKKW-UHFFFAOYSA-K scandium(3+);trihydroxide Chemical compound [OH-].[OH-].[OH-].[Sc+3] LQPWUWOODZHKKW-UHFFFAOYSA-K 0.000 description 5
- 229910052782 aluminium Inorganic materials 0.000 description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 4
- 238000009854 hydrometallurgy Methods 0.000 description 4
- 150000002739 metals Chemical class 0.000 description 4
- 239000000725 suspension Substances 0.000 description 4
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 229910052804 chromium Inorganic materials 0.000 description 3
- 239000011651 chromium Substances 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000010828 elution Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 230000001112 coagulating effect Effects 0.000 description 2
- 229910001710 laterite Inorganic materials 0.000 description 2
- 239000011504 laterite Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- OMMFSGNJZPSNEH-UHFFFAOYSA-H oxalate;scandium(3+) Chemical compound [Sc+3].[Sc+3].[O-]C(=O)C([O-])=O.[O-]C(=O)C([O-])=O.[O-]C(=O)C([O-])=O OMMFSGNJZPSNEH-UHFFFAOYSA-H 0.000 description 2
- 235000006408 oxalic acid Nutrition 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000011701 zinc Substances 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- IPRPPFIAVHPVJH-UHFFFAOYSA-N (4-hydroxyphenyl)acetaldehyde Chemical compound OC1=CC=C(CC=O)C=C1 IPRPPFIAVHPVJH-UHFFFAOYSA-N 0.000 description 1
- 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
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 229910052595 hematite Inorganic materials 0.000 description 1
- 239000011019 hematite Substances 0.000 description 1
- NBZBKCUXIYYUSX-UHFFFAOYSA-N iminodiacetic acid Chemical compound OC(=O)CNCC(O)=O NBZBKCUXIYYUSX-UHFFFAOYSA-N 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 235000014413 iron hydroxide Nutrition 0.000 description 1
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical group [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 1
- NCNCGGDMXMBVIA-UHFFFAOYSA-L iron(ii) hydroxide Chemical compound [OH-].[OH-].[Fe+2] NCNCGGDMXMBVIA-UHFFFAOYSA-L 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- HCWCAKKEBCNQJP-UHFFFAOYSA-N magnesium orthosilicate Chemical compound [Mg+2].[Mg+2].[O-][Si]([O-])([O-])[O-] HCWCAKKEBCNQJP-UHFFFAOYSA-N 0.000 description 1
- 239000000391 magnesium silicate Substances 0.000 description 1
- 229910052919 magnesium silicate Inorganic materials 0.000 description 1
- 235000019792 magnesium silicate Nutrition 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
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000011268 mixed slurry Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000012074 organic phase Substances 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 150000003141 primary amines Chemical class 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 150000003325 scandium Chemical class 0.000 description 1
- 229910000346 scandium sulfate Inorganic materials 0.000 description 1
- QHYMYKHVGWATOS-UHFFFAOYSA-H scandium(3+);trisulfate Chemical compound [Sc+3].[Sc+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O QHYMYKHVGWATOS-UHFFFAOYSA-H 0.000 description 1
- 150000003335 secondary amines Chemical class 0.000 description 1
- 239000011669 selenium Substances 0.000 description 1
- 229910052711 selenium Inorganic materials 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 1
- 229910052979 sodium sulfide Inorganic materials 0.000 description 1
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003512 tertiary amines Chemical class 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B59/00—Obtaining rare earth metals
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/263—Chemical reaction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2642—Aggregation, sedimentation, flocculation, precipitation or coagulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/02—Hollow fibre modules
-
- 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
Definitions
- the present invention relates to a smelting method for obtaining a mixed sulfide of nickel and cobalt from a metal oxide ore containing nickel and cobalt.
- the mixed sulfide of nickel and cobalt formed by adding a sulfiding agent to the aqueous sulfate solution is mixed
- a suspension containing sulfide (hereinafter, simply referred to as “sulfide slurry”) is recovered by subjecting it to a sedimentation treatment using a sedimentation apparatus such as a thickener.
- the metal sulfide as a precipitate is recovered from the bottom of the device, while the sulfide slurry in the sulfide slurry
- the aqueous solution component overflows and is recovered as an overflow solution to become a poor solution.
- the suspended solids consist of fine metal sulfides remaining in the aqueous solution, which do not become precipitates, but overflow into the poor liquid and are subjected to final neutralization and other metal oxidation. It is discharged outside the factory as tailing residue along with the pressure acid leaching residue of the ore. For this reason, the suspended solids consisting of fine metal sulfides remaining in the overflow liquid and discharged out of the system are lost in recovering the metal components.
- Patent Document 1 as a method for reducing the recovery loss of a metal component, a part of metal sulfide recovered from the bottom of a sedimentation separator such as thickener is fractionated, and after adjusting the particle size, a sulfurization reaction is performed.
- a method of reducing fine suspended solids contained in an overflow liquid of a sedimentation separator such as thickener by repeating as a seed crystal in the process is disclosed.
- the average particle size of metal sulfide recovered from the bottom of a sedimentation separator such as thickener is 10 ⁇ m to 100 ⁇ m, but the average particle size of fine suspended solids in the overflow liquid is 1 ⁇ m or less. It is actually difficult to improve the recovery by advancing the sedimentation of the minute, which entails enlarging the sedimentation separation apparatus such as thickener.
- the present invention has been proposed in view of the above-described circumstances, and in a metal oxide ore smelting method for obtaining metal sulfide, the metal sulfide is concentrated and separated by a sedimentation separator such as a thickener. Furthermore, it aims at providing the smelting method which can collect
- the present inventors have made extensive studies to solve the above-described problems.
- the fine metal sulfide is efficiently recovered by performing microfiltration using a filtration membrane such as a hollow fiber membrane having a predetermined pore size for the overflow liquid containing fine particles of metal sulfide. It has been found that by repeating the recovered metal sulfide in the sulfiding process, the recovery loss of the metal component can be effectively reduced as a smelting method, and the present invention has been completed.
- the first invention of the present invention is a smelting method of a metal oxide ore containing nickel and cobalt, and a leaching step of obtaining an acidic solution of nickel and cobalt by pressure acid leaching of the metal oxide ore. And a neutralization step of performing a neutralization treatment on the acidic solution, and a sulfurization step of adding a sulfurizing agent to the obtained neutralized final solution to perform a sulfurization treatment to obtain a mixed sulfide slurry of nickel and cobalt And a sedimentation step for sedimentation and separation of the mixed sulfide from the slurry of the mixed sulfide, and fine filtration of the mixed sulfide remaining in the overflow liquid by microfiltration of the overflow liquid after separating the mixed sulfide And a microfiltration step of obtaining a filtrate.
- the second invention of the present invention is the neutralization according to the first invention, wherein the mixed sulfide fine particles obtained by microfiltration in the microfiltration step are subjected to sulfurization treatment in the sulfurization step. This is a metal oxide ore smelting method added to the final solution.
- a third invention of the present invention is the production of a metal oxide ore according to the first or second invention, wherein in the microfiltration step, microfiltration is performed using a hollow fiber membrane having a pore diameter of 0.2 ⁇ m or less. It is a smelting method.
- a fourth invention of the present invention is a metal oxide ore smelting method according to any one of the first to third inventions, wherein in the leaching step, pressure acid leaching is performed using sulfuric acid.
- the mixed sulfide slurry obtained in the sulfiding step is depressurized and the sulfiding agent used in the sulfiding treatment is reduced. This is a method for smelting metal oxide ore to be recovered.
- the sixth invention of the present invention is a method for refining metal oxide ore according to any one of the first to fifth inventions, wherein the sulfiding agent is hydrogen sulfide gas.
- the metal oxide ore is a nickel oxide ore containing scandium, and the filtrate obtained in the microfiltration step is used. This is a metal oxide ore smelting method using scandium as a raw material for recovery.
- the metal oxide ore is a nickel oxide ore containing scandium, and is obtained from the filtrate obtained in the microfiltration step. It further has a scandium recovery step for recovering scandium, and the scandium recovery step includes an ion exchange step for passing the filtrate through the ion exchange resin, and a concentration treatment for the eluate eluted from the ion exchange resin.
- a method for smelting metal oxide ores is a nickel oxide ore containing scandium, and is obtained from the filtrate obtained in the microfiltration step. It further has a scandium recovery step for recovering scandium, and the scandium recovery step includes an ion exchange step for passing the filtrate through the ion exchange resin, and a concentration treatment for the eluate eluted from the ion exchange resin.
- the present invention in a metal oxide ore smelting method for obtaining a metal sulfide, when the metal sulfide is concentrated and separated by a sedimentation separator such as a thickener, the fine metal sulfide contained in the overflow liquid It is possible to provide a smelting method that can efficiently recover the metal and reduce the recovery loss of the metal component.
- the metal oxide smelting method according to the present invention is a method for smelting a metal oxide ore containing nickel and cobalt. Specifically, a step of obtaining an acidic solution of nickel and cobalt by pressure acid leaching a metal oxide ore containing nickel and cobalt, a step of neutralizing the acidic solution, and the obtained neutralization It has a step of adding a sulfiding agent to the final solution and subjecting it to a sulfiding treatment to obtain a mixed sulfide slurry of nickel and cobalt, and a settling separation step of settling and separating the mixed sulfide from the mixed sulfide slurry.
- This smelting method is characterized by having a step of finely filtering the overflow liquid after separating the mixed sulfide to obtain fine particles of the mixed sulfide and filtrate remaining in the overflow liquid.
- the smelting method of a metal oxide having such a configuration valuable metals such as nickel and cobalt contained in the metal oxide can be effectively leached and recovered, and a mixed sulfide of nickel and cobalt can be recovered.
- the fine metal sulfide contained in the separated overflow liquid can also be efficiently recovered, and the recovery loss of the metal component can be reduced.
- the metal oxide to be subjected to the smelting method is not particularly limited, and examples thereof include nickel oxide ore containing nickel and cobalt.
- the nickel oxide ore as an example of a metal oxide contains scandium together with nickel and cobalt.
- this embodiment a specific embodiment of the metal oxide smelting method according to the present invention is performed using nickel oxide ore containing nickel and cobalt, and further scandium as a metal oxide to be smelted ( Hereinafter, it is referred to as “this embodiment”) and will be described in detail.
- FIG. 1 is a process diagram showing an example of the flow of a nickel oxide ore hydrometallurgy method according to the present embodiment.
- this hydrometallurgical method is a leaching step S1 in which a metal oxide ore containing nickel and cobalt is subjected to pressure acid leaching to obtain an acidic solution of nickel and cobalt, and neutralized with respect to the acidic solution.
- the sulfurization step S3 for adding a sulfurizing agent to the obtained neutralized final solution and performing the sulfurization treatment to obtain a mixed sulfide slurry of nickel and cobalt
- the mixed sulfide slurry Precipitation separation step S4 for separating and separating the mixed sulfide
- microfiltration step S5 for finely filtering the overflow liquid after separating the mixed sulfide to obtain mixed sulfide fine particles and filtrate remaining in the overflow liquid And having.
- leaching step S1 nickel oxide ore containing nickel and cobalt is subjected to pressure acid leaching to obtain an acidic solution (leaching solution) of nickel and cobalt.
- an acid such as sulfuric acid is added to a slurry of nickel oxide ore using a high-temperature pressurized container (autoclave), and the mixture is stirred while being pressurized at a temperature of 240 ° C. to 260 ° C. And a leaching residue is formed.
- the process in the leaching step S1 can be performed according to a conventionally known HPAL process.
- nickel oxide ore examples include so-called laterite ores such as limonite ore and saprolite ore.
- Laterite ore usually has a nickel content of 0.8 to 2.5% by mass, and is contained as a hydroxide or siliceous clay (magnesium silicate) mineral.
- These nickel oxide ores contain scandium.
- the leaching slurry comprising the obtained leaching solution and the leaching residue is washed, and solid-liquid separation is performed into the leaching solution containing nickel, cobalt, scandium, and the like and the leaching residue that is hematite.
- a flocculant is added as appropriate, and the treatment is performed by solid-liquid separation equipment such as a thickener.
- the leaching slurry is first diluted with a cleaning liquid, and then the leaching residue in the slurry is concentrated as a thickener sediment.
- solid-liquid separation tanks such as thickeners connected in multiple stages and perform solid-liquid separation while washing the leach slurry in multiple stages.
- the neutralization process is performed with respect to the leaching liquid which is the acidic solution obtained by the leaching process S1. Specifically, this is a step of adjusting the pH by adding a neutralizing agent to the leachate to obtain a neutralized starch containing an impurity element and a neutralized final solution.
- a neutralizing agent to the leachate to obtain a neutralized starch containing an impurity element and a neutralized final solution.
- valuable metals such as nickel, cobalt, and scandium are included in the neutralization final solution, and most of the impurities including iron and aluminum become neutralized starch.
- neutralizing agent conventionally known neutralizing agents can be used, and examples thereof include calcium carbonate, slaked lime, and sodium hydroxide.
- the pH in the neutralization treatment in the neutralization step S2, it is preferable to adjust the pH to a range of 1 to 4 and more preferably to a range of 1.5 to 2.5 while suppressing oxidation of the separated leachate. preferable. If the pH is less than 1, neutralization may be insufficient, and the neutralized starch and the neutralized final solution may not be separated. On the other hand, when the pH exceeds 4, not only impurities such as aluminum but also valuable metals such as scandium and nickel may be contained in the neutralized starch.
- Sulfurization process S3 adds a sulfidizing agent to the neutralization final solution obtained by neutralization process S2, performs a sulfidation process, and obtains the mixed sulfide slurry of nickel and cobalt.
- a sulfide containing nickel and cobalt with a small amount of impurity components is added to the obtained neutralized final solution by adding a sulfiding agent such as hydrogen sulfide gas, sodium sulfide, sodium hydrogen sulfide and the like.
- a sulfiding agent such as hydrogen sulfide gas, sodium sulfide, sodium hydrogen sulfide and the like.
- a slurry containing (a mixed sulfide of nickel and cobalt), a nickel concentration at a low level, and a sulfided end solution containing scandium or the like is generated.
- the leachate that is the object of sulfidation may contain not only nickel and cobalt but also zinc.
- a process of recovering zinc as a sulfide by a sulfidation reaction is performed prior to generating a mixed sulfide of nickel and cobalt by a sulfidation reaction.
- the conditions for the sulfurization reaction at this time are generally performed under conditions that are more relaxed than those for nickel and cobalt.
- the mixed sulfide of nickel and cobalt is separated by sedimentation from the mixed sulfide slurry obtained in the sulfurization process S3.
- the sedimentation process in the sedimentation step S4 is performed by a sedimentation apparatus such as a thickener, for example, and a mixed sulfide of nickel and cobalt is aggregated and settled by adding a flocculant to the mixed sulfide slurry.
- a mixed sulfide slurry obtained by sulfidation is fed to a sedimentation tank, and a mixed sulfide of nickel and cobalt is agglomerated based on the addition of a flocculant. And settles to the bottom of the settling tank. Then, the mixed sulfide that has agglomerated and settled is separated and recovered from the bottom of the sedimentation tank. From the bottom of the settling tank, as an underflow, a suspension in which the concentration of the mixed sulfide of nickel and cobalt is concentrated to about 25% by mass to 35% by mass is recovered.
- the aqueous solution component in the mixed sulfide slurry overflows from the settling tank as an aqueous solution from which the mixed sulfide of nickel and cobalt is separated.
- the aqueous solution overflowing from the settling tank that is, the overflow liquid is a clarified liquid after the mixed sulfide of nickel and cobalt is separated as described above, and is a poor liquid in which the concentration of nickel and cobalt is reduced.
- the overflow liquid is separated and discharged from the sedimentation separator as a poor liquid.
- the poor solution has a pH of about 1 to 3 and contains impurity elements such as iron, magnesium, and manganese that are contained without being sulfided.
- microfiltration step S5 the overflow liquid separated and discharged in the sedimentation separation process S4 is microfiltered to obtain mixed sulfide fine particles and filtrate remaining in the overflow liquid.
- the mixed sulfide of nickel and cobalt and the overflow liquid (poor liquid) from which the mixed sulfide has been separated are separated by, for example, sedimentation treatment using a flocculant. Collected.
- fine mixed sulfides with poor sedimentation may remain at a rate of, for example, about 50 mg / L as the concentration of nickel and cobalt.
- the overflow liquid is separated and discharged from the settling separator, and then neutralized and discharged outside the system. Therefore, the mixed sulfide of nickel and cobalt consisting of fine particles remaining in the overflow liquid Are also discharged at the same time, resulting in a recovery loss of the metal component.
- a microfiltration process for performing microfiltration processing on the overflow liquid separated and discharged from the sedimentation separation process S4 is provided.
- the separated and discharged overflow liquid is microfiltered to separate the mixed sulfide fine particles of nickel and cobalt remaining in the overflow liquid and the filtrate after microfiltration, and the mixed sulfide Collect the fine particles.
- the separated and collected mixed sulfide fine particles are added to the neutralized final solution accommodated in the reaction vessel in the sulfiding step S3.
- fine mixed sulfide particles of nickel and cobalt remaining in the overflow liquid can be effectively recovered.
- concentration of nickel and cobalt in the filtrate obtained after filtration is about 10 mg / L or less.
- recovery loss of a metal component can be reduced by returning the collect
- the particle size of the mixed sulfide of nickel and cobalt contained in the overflow liquid is about 0.25 ⁇ m to 3 ⁇ m. Therefore, the microfiltration in the microfiltration step S5 is preferably one capable of effectively capturing mixed sulfides having a particle size of about 0.25 ⁇ m to 3 ⁇ m.
- the microfiltration treatment is preferably performed using a hollow fiber membrane as the filtration membrane.
- the hollow fiber membrane preferably has a pore size of 1.0 ⁇ m or less, more preferably 0.5 ⁇ m or less, and still more preferably 0.2 ⁇ m or less.
- the supply time (supply flow rate) of the overflow liquid to a filtration membrane such as a hollow fiber membrane is not particularly limited, but per unit membrane area depending on the SS (suspended substance) concentration in the overflow liquid. It is preferable to set the SS load for 1 minute to be 50 mg / L or less.
- the filtration process can be performed without increasing the pressure applied to the filtration membrane such as the hollow fiber membrane so much by circulating the low-concentration slurry through the filtration membrane at such a low flow rate that the SS load is 50 mg / L or less. Therefore, the filtration membrane is hardly damaged and can be used for a long period of time.
- the captured mixed sulfide is peeled off by washing the filtration membrane.
- an acidic solution can be used, and is not particularly limited.
- a filtrate (clarified liquid) recovered by filtration that does not contain particles larger than the opening of the filtration membrane, preferably not to clog the filtration membrane.
- Back washing with is preferred. By such backwashing or the like, a suspension containing a mixed sulfide of nickel and cobalt is obtained at a slurry concentration of, for example, about 1.5 g / L to 3 g / L.
- the mixed sulfide of nickel and cobalt that has been distributed to the overflow liquid during sedimentation separation can be efficiently recovered. Can do.
- the mixed sulfidation of nickel and cobalt is performed in the same manner as increasing the residence time of the sulfiding treatment in the sulfiding step S3. Objects can be recovered more efficiently, and recovery loss of metal components can be reduced.
- the fine particles grow further, and the particle size of the mixed sulfide obtained by the sulfidation process in the sulfidation step S3 is increased. Can also be expected.
- the mass of the mixed sulfide of nickel and cobalt added by repetition of the recovered mixed sulfide to the sulfiding step S3 is the sum of the mass of the mixed sulfide of nickel and cobalt generated in the sulfiding treatment of the sulfiding step S3. In contrast, it is less than 1%. Therefore, there is no problem of increasing the load of the sulfurization treatment.
- the nickel oxide ore to be smelted contains scandium together with nickel and cobalt.
- Scandium is similar in behavior to nickel and the like, and is leached into the leachate in the leaching process (leaching step S1) in the hydrometallurgical process, and neutralized as a mother liquor that generates mixed sulfides in the sulfiding step S3 It will be included in the final solution.
- this scandium does not form a sulfide depending on the sulfidation treatment in the sulfidation step S3, and moves into a poor liquid (overflow liquid). Therefore, scandium and nickel and cobalt are effectively separated by the above-described hydrometallurgical process.
- the filtrate obtained through the microfiltration step S5 becomes a solution containing scandium, which is a valuable metal.
- FIG. 2 is a process diagram showing a flow of a smelting method further including a scandium recovery process S6.
- a mixed sulfide of nickel and cobalt can be recovered while reducing loss, and a scandium recovery step S6 for recovering scandium from the filtrate obtained by the microfiltration step S5 is provided. Therefore, higher purity scandium can be efficiently recovered.
- the smelting method according to the present embodiment has a microfiltration step S5, and efficiently recovers the mixed sulfide of nickel and cobalt remaining in the poor liquid, and the nickel in the filtrate.
- the concentration of cobalt and cobalt can be effectively reduced, and by collecting scandium using the filtrate as a collection raw material, it can be prevented from becoming an obstacle to the selective recovery process of scandium. Can be recovered.
- FIG. 3 is a process diagram showing an example of the flow of the scandium recovery process S6.
- an ion exchange step S61 for passing the filtrate obtained in the microfiltration step S5 through the ion exchange resin and an eluent eluted from the ion exchange resin are used.
- the ion exchange step S61 is a step of obtaining scandium eluent by separating scandium from other impurity components by an ion exchange reaction using a chelate resin.
- an adsorption step in which a filtrate is brought into contact with a chelate resin and scandium is adsorbed on the chelate resin, and an aluminum adsorbed on the chelate resin by bringing sulfuric acid into contact with the chelate resin adsorbing scandium
- An aluminum removal step to remove the selenium a scandium elution step to contact the chelate resin with sulfuric acid to obtain a scandium eluate, and a chromium removal step to remove the chromium adsorbed on the rate resin by contacting the chelate resin that has undergone the scandium elution step with sulfuric acid , And the like.
- the chelate resin is not particularly limited, and for example, a resin having iminodiacetic acid as a functional group can be used.
- the scandium adsorbed on the chelate resin can be eluted (scandium elution step) by, for example, contacting the chelate resin with sulfuric acid having a concentration range of 0.3 N or more and less than 3 N. Thereby, the scandium eluent which scandium concentrated can be obtained efficiently.
- the concentration step S62 is a step of concentrating scandium by removing impurity components by subjecting the scandium eluent obtained through the ion exchange step S61 to a concentration treatment such as neutralization.
- a concentration treatment such as neutralization.
- the concentration step S62 for example, as shown in FIG. 3, a step of performing a two-step neutralization treatment can be exemplified.
- a neutralizing agent such as sodium hydroxide is added to the scandium eluent so that the pH of the solution is 3.5-4.
- the first stage of neutralization is carried out so that the pH is adjusted to a range of 5, preferably about 4.
- most of the impurities such as iron and chromium, which are less basic than scandium, become precipitates in the form of hydroxide (eg, iron hydroxide), and solid-liquid separation such as filtration
- the primary neutralized starch and the primary neutralized filtrate are separated.
- a neutralizing agent such as sodium hydroxide is further added to the primary neutralized filtrate obtained by the first-stage neutralization, and the pH of the filtrate is 5
- the neutralization of the second stage is carried out so that the pH is adjusted to a range of about 5 to 6.5, preferably about 6.
- scandium hydroxide is obtained as a secondary neutralized starch, and nickel, which is a basic component higher than scandium, does not precipitate, so that it remains in the secondary neutralized filtrate.
- a secondary neutralized starch that is, a scandium hydroxide (scandium hydroxide) from which impurities have been separated can be obtained.
- the concentration of nickel and cobalt is increased by the microfiltration step S5 that is the preceding step. Since it is effectively reduced, the separation process of scandium and nickel in the concentration step S62 can be performed at a low cost and in a short time.
- a dissolving step S73 an acid is added to the neutralized starch (secondary neutralized starch) mainly composed of scandium hydroxide obtained by the two-step neutralization treatment. A re-dissolved solution of scandium is obtained. The solution thus obtained is used as an extraction starting solution in the solvent extraction step S63 of the next step.
- an acid for dissolving the neutralized starch it is preferable to use sulfuric acid. By using sulfuric acid, the resulting solution is a solution of scandium sulfate.
- solvent extraction step S63 the solution (scandium-containing solution) obtained through the concentration step S62 is used as an extraction start solution, and this is contacted with an extractant to perform a solvent extraction process to obtain an extraction residual solution containing scandium. It is a process.
- the mode in the solvent extraction step S63 is not particularly limited.
- a scandium-containing solution that is an extraction start liquid and an extractant that is an organic solvent are mixed to extract impurities and a slight amount of scandium.
- the extraction step S81 for separating the extracted organic solvent and the extraction residual liquid leaving the scandium, and mixing the sulfuric acid solution with the extracted organic solvent to separate the slight scandium extracted into the organic solvent into the aqueous phase It is preferable to perform a solvent extraction process including a scrubbing step S82 for obtaining a post-washing solution and a back extraction step S83 for back-extracting impurities from the washed organic solvent by adding a back extractant to the washed organic solvent.
- the scandium-containing solution which is the extraction start solution
- the organic solvent containing the extractant are mixed to selectively extract the impurity components in the organic solvent, and the organic solvent containing the impurities and the extraction residual liquid And get.
- the extractant is not particularly limited as long as it can selectively extract an impurity component, and for example, an amine-based extractant can be used.
- the amine-based extractant is characterized by low selectivity with scandium and no need for a neutralizing agent at the time of extraction. Amine-based extraction of primary amine, secondary amine, and tertiary amine Agents are known.
- the scrubbing (washing) step S82 before the extraction liquid obtained in the extraction step S81 is back-extracted when scandium slightly coexists in the organic solvent in which the impurity component is extracted from the scandium-containing solution in the extraction step S81. Further, the organic solvent (organic phase) is subjected to a scrubbing (washing) treatment, and scandium is separated into an aqueous phase and recovered from the extractant. As described above, the scrubbing step S82 is provided to wash the organic solvent, and the scandium extracted by the extractant is separated, so that scandium can be separated in the cleaning liquid, and the scandium recovery rate is further enhanced. be able to.
- As the cleaning solution a sulfuric acid solution or a hydrochloric acid solution can be used.
- the impurity component is back extracted from the organic solvent from which the impurity component was extracted in the extraction step S81.
- a reverse extraction solution back extraction start liquid
- an organic solvent containing an extractant thereby causing a reverse reaction to the extraction process in the extraction step S81 and back-extracting impurity components.
- a liquid after back extraction is obtained.
- the back extraction solution for example, a solution containing a carbonate such as sodium carbonate or potassium carbonate can be used.
- the extraction agent after separating the impurity components by performing the back extraction process can be repeatedly used as the extraction agent again in the extraction step S81.
- the example in the solvent extraction process S63 mentioned above showed the aspect which removes an impurity component while transferring scandium to an extraction residual liquid using the extractant with low selectivity with scandium, it is not limited to this.
- an extractant having high selectivity with scandium may be used, separated from the impurity component, and scandium may be transferred into an organic solvent, and scandium may be contained in the solution after back extraction by back extraction treatment.
- the processing target of the next scandium oxide recovery step is the liquid after back extraction.
- the scandium oxide recovery step S64 oxidizes scandium from the extraction residual liquid obtained in the extraction step S81 in the solvent extraction step S63 and, after scrubbing in the scrubbing step S82, the washed solution after scrubbing. Recover in scandium form.
- the scandium recovery method is not particularly limited, and a known method can be used. Among them, a method (oxalate treatment) that recovers as an oxalate precipitate with an oxalic acid solution is more effective. In particular, it is preferable that impurities can be separated and high-purity scandium can be recovered. As another method, a method of obtaining a precipitate of hydroxide (scandium hydroxide) by adding an alkali and performing neutralization treatment can be applied.
- the extraction residual liquid and the post-washing liquid obtained in the solvent extraction step S63 are mixed with a predetermined amount of oxalic acid to precipitate scandium oxalate crystals.
- oxalic acid examples thereof include an oxalate forming step and a roasting step in which the obtained scandium oxalate crystals are washed with water and dried, and then roasted. Thereby, scandium oxide containing scandium with high purity can be recovered.
- the concentration of nickel and cobalt in the poor liquid is effectively reduced by having the microfiltration step S5, the filtrate obtained by the microfiltration step S5.
- the filtrate obtained by the microfiltration step S5. By collecting scandium using, extremely high purity scandium can be recovered.
- Nickel oxide ore containing nickel and cobalt was used as a raw material to obtain a leachate (acid solution) containing nickel and cobalt by pressure acid leaching with sulfuric acid. Then, hydrogen sulfide gas as a sulfiding agent was blown into the obtained acidic solution to cause a sulfidation reaction, thereby obtaining a mixed sulfide slurry of nickel and cobalt (mixed sulfide and acidic solution mixed slurry). Next, the mixed sulfide slurry of nickel and cobalt was charged into a thickener, which is a coagulating sedimentation apparatus, and separated into an overflow and an underflow. As an underflow, a mixed sulfide slurry of nickel and cobalt was recovered.
- a thickener which is a coagulating sedimentation apparatus
- the overflow liquid obtained by overflowing from the thickener was collected and subjected to microfiltration using a hollow fiber membrane having a pore diameter of 0.1 ⁇ m.
- the microfiltration treatment was performed using a filtration apparatus in which a filtration membrane composed of a hollow fiber membrane was mounted in an outer container.
- a filtration membrane composed of a hollow fiber membrane was mounted in an outer container.
- the filtrate is discharged and the filtration membrane is washed. What provided the supply / discharge port B which supplies an acidic solution, and the air outlet C was used.
- the inside of the outer container is pressurized by closing the air outlet C,
- the overflow liquid was passed from the outer surface of the hollow fiber membrane mounted in the container toward the inside.
- the filtrate obtained by passing through the hollow fiber membrane passed through the hollow part inside the hollow fiber membrane and was collected from the supply / discharge port B of the outer container.
- the above-described operation was performed such that the pressure in the outer container (filtration pressure) was maintained at 100 kPaG or less and the average flow rate of the overflow liquid per unit membrane area was 0.07 m 3 / Hr or less. .
- the supply of the overflow liquid was temporarily stopped, and a back washing process was performed in which the clarified liquid was passed from the back side of the hollow fiber membrane through the supply / discharge port B.
- the start of the backwashing treatment was taken as a guide when the average flow rate could not be maintained below 0.07 m 3 / Hr even when the filtration pressure was 190 kPaG.
- the mixed sulfide of nickel and cobalt trapped on the surface of the hollow fiber membrane was discharged as a slurry from the supply / discharge port A together with the passed liquid.
- the quantity of the clarified liquid passed from the back side of the hollow fiber membrane was 0.4 L per unit membrane area.
- the supply pressure of the clarified liquid during backwashing was 100 PaG to 200 kPaG, and the average flow rate at that time was 0.06 m / Hr.
- Table 1 shows the 80-day average values of the SS concentration in the overflow solution supplied to the hollow fiber membrane used for microfiltration and the SS concentration in the filtrate recovered from the filtration device.
- the fine mixture of nickel and cobalt in the overflow liquid overflowing in the sedimentation process is performed by performing microfiltration on the overflow liquid using a hollow fiber membrane having a predetermined pore size. It was found that sulfide can be recovered efficiently. From this, it is considered that the recovery loss of nickel and cobalt, which are valuable metals, can be effectively reduced by returning the recovered mixed sulfide again to the sulfiding treatment again.
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Abstract
Description
本発明に係る金属酸化物の製錬方法は、ニッケル及びコバルトを含む金属酸化鉱の製錬方法である。具体的には、ニッケル及びコバルトを含有する金属酸化鉱を加圧酸浸出してニッケル及びコバルトの酸性溶液を得る工程と、酸性溶液に対して中和処理を施す程と、得られた中和終液に硫化剤を添加して硫化処理を施し、ニッケル及びコバルトの混合硫化物のスラリーを得る工程と、混合硫化物のスラリーからその混合硫化物を沈降分離する沈降分離工程と、を有する。そして、この製錬方法においては、混合硫化物を分離した後のオーバーフロー液を精密ろ過して、そのオーバーフロー液に残存する混合硫化物の微粒子とろ液とを得る工程を有することを特徴としている。
図1は、本実施の形態に係るニッケル酸化鉱の湿式製錬方法の流れの一例を示す工程図である。図1に示すように、この湿式製錬方法は、ニッケル及びコバルトを含有する金属酸化鉱を加圧酸浸出してニッケル及びコバルトの酸性溶液を得る浸出工程S1と、酸性溶液に対して中和処理を施す中和工程S2と、得られた中和終液に硫化剤を添加して硫化処理を施し、ニッケル及びコバルトの混合硫化物のスラリーを得る硫化工程S3と、混合硫化物のスラリーからその混合硫化物を沈降分離する沈降分離工程S4と、混合硫化物を分離した後のオーバーフロー液を精密ろ過して、そのオーバーフロー液に残存する混合硫化物の微粒子とろ液とを得る精密ろ過工程S5と、を有する。
浸出工程S1では、ニッケル及びコバルトを含有するニッケル酸化鉱を加圧酸浸出してニッケル及びコバルトの酸性溶液(浸出液)を得る。具体的には、例えば高温加圧容器(オートクレーブ)等を用いて、ニッケル酸化鉱のスラリーに硫酸等の酸を添加し、240℃~260℃の温度下で加圧しながら撹拌処理を施し、浸出液と浸出残渣とからなる浸出スラリーを生成する。なお、浸出工程S1における処理は、従来知られているHPALプロセスに従って行うことができる。
中和工程S2では、浸出工程S1により得られた酸性溶液である浸出液に対して中和処理を施す。具体的には、浸出液に中和剤を添加してpHを調整し、不純物元素を含む中和澱物と中和終液とを得る工程である。この中和処理により、ニッケルやコバルト、スカンジウム等の有価金属は中和終液に含まれるようになり、鉄、アルミニウムをはじめとした不純物の大部分が中和澱物となる。
硫化工程S3は、中和工程S2により得られた中和終液に硫化剤を添加して硫化処理を施し、ニッケル及びコバルトの混合硫化物のスラリーを得る。
沈降分離工程S4では、硫化工程S3により得られた混合硫化物のスラリーから、ニッケル及びコバルトの混合硫化物を沈降分離する。この沈降分離工程S4における沈降分離処理は、例えばシックナー等の沈降分離装置により行われ、混合硫化物のスラリーに対して凝集剤を添加することによってニッケル及びコバルトの混合硫化物を凝集沈降させる。
精密ろ過工程S5では、沈降分離工程S4にて分離排出されたオーバーフロー液を精密ろ過して、そのオーバーフロー液に残存する混合硫化物の微粒子とろ液とを得る。
さて、上述したように、製錬対象となるニッケル酸化鉱は、ニッケル及びコバルトと共に、スカンジウムを含有するものである。スカンジウムは、その挙動がニッケル等と類似しており、湿式製錬プロセスにおける浸出処理(浸出工程S1)にて浸出液中に浸出され、硫化工程S3にて混合硫化物を生成させる母液となる中和終液に含まれるようになる。一方で、このスカンジウムは、硫化工程S3における硫化処理によっては硫化物の形態とはならず、貧液(オーバーフロー液)中に移行する。したがって、スカンジウムと、ニッケル及びコバルトとは、上述した湿式製錬プロセスによって効果的に分離される。
図3は、スカンジウム回収工程S6の流れの一例を示す工程図である。図3に示すように、例えば、スカンジウム回収工程S6としては、精密ろ過工程S5により得られたろ液をイオン交換樹脂に通液するイオン交換工程S61と、イオン交換樹脂から溶離した溶離液に対して濃縮処理を施す濃縮工程S62と、濃縮処理を経て得られた溶液に対して溶媒抽出処理を施す溶媒抽出工程S63と、溶媒抽出処理を経て得られたスカンジウムを含む溶液から酸化スカンジウムを回収する酸化スカンジウム回収工程S64と、を含むものとすることができる。
イオン交換工程S61は、キレート樹脂を使用したイオン交換反応によりスカンジウムを他の不純物成分と分離して、スカンジウム溶離液を得る工程である。
濃縮工程S62は、イオン交換工程S61を経て得られたスカンジウム溶離液に対して中和等の濃縮処理を施すことによって不純物成分を除去してスカンジウムを濃縮させる工程である。濃縮工程S62としては、例えば図3に示すように、2段階の中和処理を行うものを例示することができる。
溶媒抽出工程S63は、濃縮工程S62を経て得られた溶解液(スカンジウム含有溶液)を抽出始液として、これを抽出剤に接触させて溶媒抽出処理を施し、スカンジウムを含有する抽出残液を得る工程である。
酸化スカンジウム回収工程S64は、溶媒抽出工程S63における抽出工程S81にて得られた抽出残液、及び、スクラビング工程S82にてスクラビングを行った場合にはそのスクラビング後の洗浄後液から、スカンジウムを酸化スカンジウムの形態で回収する。
S2 中和工程
S3 硫化工程
S4 沈降分離工程
S5 精密ろ過工程
S6 スカンジウム回収工程
Claims (8)
- ニッケル及びコバルトを含有する金属酸化鉱の製錬方法であって、
前記金属酸化鉱を加圧酸浸出してニッケル及びコバルトの酸性溶液を得る浸出工程と、
前記酸性溶液に対して中和処理を施す中和工程と、
得られた中和終液に硫化剤を添加して硫化処理を施し、ニッケル及びコバルトの混合硫化物のスラリーを得る硫化工程と、
前記混合硫化物のスラリーから該混合硫化物を沈降分離する沈降分離工程と、
前記混合硫化物を分離した後のオーバーフロー液を精密ろ過して、該オーバーフロー液に残存する混合硫化物の微粒子とろ液とを得る精密ろ過工程と、
を有する、金属酸化鉱の製錬方法。 - 前記精密ろ過工程にて精密ろ過して得られた前記混合硫化物の微粒子を、前記硫化工程において硫化処理される前記中和終液に添加する
請求項1に記載の金属酸化鉱の製錬方法。 - 前記精密ろ過工程では、孔径が0.2μm以下の中空糸膜を使用して精密ろ過する
請求項1又は2に記載の金属酸化鉱の製錬方法。 - 前記浸出工程では、硫酸を用いて加圧酸浸出する
請求項1乃至3のいずれか1項に記載の金属酸化鉱の製錬方法。 - 前記硫化工程で得られた前記混合硫化物のスラリーを減圧し、前記硫化処理に用いた硫化剤を回収する
請求項1乃至4のいずれか1項に記載の金属酸化鉱の製錬方法。 - 前記硫化剤は、硫化水素ガスである
請求項1乃至5のいずれか1項に記載の金属酸化鉱の製錬方法。 - 前記金属酸化鉱は、スカンジウムを含有するニッケル酸化鉱であり、
前記精密ろ過工程で得られたろ液を、スカンジウムを回収する原料とする
請求項1乃至6のいずれか1項に記載の金属酸化鉱の製錬方法。 - 前記金属酸化鉱は、スカンジウムを含有するニッケル酸化鉱であり、
前記精密ろ過工程で得られたろ液からスカンジウムを回収するスカンジウム回収工程をさらに有し、
前記スカンジウム回収工程は、
前記ろ液をイオン交換樹脂に通液するイオン交換工程と、
前記イオン交換樹脂から溶離した溶離液に対して濃縮処理を施す濃縮工程と、
濃縮処理を経て得られた溶液に対して溶媒抽出処理を施す溶媒抽出工程と、
溶媒抽出処理を経て得られたスカンジウムを含む溶液から酸化スカンジウムを回収する酸化スカンジウム回収工程と、を含む
請求項1乃至6のいずれか1項に記載の金属酸化鉱の製錬方法。
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WO2012098924A1 (ja) * | 2011-01-20 | 2012-07-26 | 三菱レイヨン株式会社 | 廃水の処理装置、処理方法、および廃水処理システム |
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WO2012098924A1 (ja) * | 2011-01-20 | 2012-07-26 | 三菱レイヨン株式会社 | 廃水の処理装置、処理方法、および廃水処理システム |
JP2013043996A (ja) | 2011-08-22 | 2013-03-04 | Sumitomo Metal Mining Co Ltd | ニッケル回収ロスの低減方法、ニッケル酸化鉱石の湿式製錬方法、並びに硫化処理システム |
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