WO2019102652A1 - 硫酸ニッケル水溶液の脱亜鉛システム、及びその方法 - Google Patents
硫酸ニッケル水溶液の脱亜鉛システム、及びその方法 Download PDFInfo
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- WO2019102652A1 WO2019102652A1 PCT/JP2018/029091 JP2018029091W WO2019102652A1 WO 2019102652 A1 WO2019102652 A1 WO 2019102652A1 JP 2018029091 W JP2018029091 W JP 2018029091W WO 2019102652 A1 WO2019102652 A1 WO 2019102652A1
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- nickel
- zinc
- aqueous solution
- concentration
- hydrogen sulfide
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- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 title claims abstract description 34
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims description 83
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 223
- 239000011701 zinc Substances 0.000 claims abstract description 134
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 130
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 127
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 110
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 59
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 57
- 239000007789 gas Substances 0.000 claims abstract description 47
- 229910017052 cobalt Inorganic materials 0.000 claims abstract description 36
- 239000010941 cobalt Substances 0.000 claims abstract description 36
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 238000004364 calculation method Methods 0.000 claims abstract description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 102
- 239000007864 aqueous solution Substances 0.000 claims description 70
- 230000008569 process Effects 0.000 claims description 38
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 25
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 25
- 239000012535 impurity Substances 0.000 claims description 20
- 238000001514 detection method Methods 0.000 claims description 12
- 239000002253 acid Substances 0.000 claims description 8
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 claims description 6
- 229910000368 zinc sulfate Inorganic materials 0.000 claims description 6
- 229960001763 zinc sulfate Drugs 0.000 claims description 6
- 238000003723 Smelting Methods 0.000 claims description 5
- XOPRVBNTVOBBMM-UHFFFAOYSA-J S(=O)(=O)([O-])[O-].[Zn+2].[Ni+2].S(=O)(=O)([O-])[O-] Chemical compound S(=O)(=O)([O-])[O-].[Zn+2].[Ni+2].S(=O)(=O)([O-])[O-] XOPRVBNTVOBBMM-UHFFFAOYSA-J 0.000 claims 1
- 238000006477 desulfuration reaction Methods 0.000 claims 1
- 230000023556 desulfurization Effects 0.000 claims 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract description 43
- 230000000717 retained effect Effects 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 57
- QXZUUHYBWMWJHK-UHFFFAOYSA-N [Co].[Ni] Chemical compound [Co].[Ni] QXZUUHYBWMWJHK-UHFFFAOYSA-N 0.000 description 49
- 238000006386 neutralization reaction Methods 0.000 description 38
- 238000002386 leaching Methods 0.000 description 37
- 239000002002 slurry Substances 0.000 description 30
- 239000007788 liquid Substances 0.000 description 27
- 238000007726 management method Methods 0.000 description 26
- 239000000047 product Substances 0.000 description 23
- 238000000926 separation method Methods 0.000 description 21
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 18
- 238000011084 recovery Methods 0.000 description 15
- 238000003908 quality control method Methods 0.000 description 12
- 238000005406 washing Methods 0.000 description 12
- 239000005083 Zinc sulfide Substances 0.000 description 11
- 238000005486 sulfidation Methods 0.000 description 11
- 229910052984 zinc sulfide Inorganic materials 0.000 description 11
- 229910052742 iron Inorganic materials 0.000 description 10
- 239000003795 chemical substances by application Substances 0.000 description 9
- 238000009854 hydrometallurgy Methods 0.000 description 9
- 239000012452 mother liquor Substances 0.000 description 9
- 238000005987 sulfurization reaction Methods 0.000 description 9
- 239000002244 precipitate Substances 0.000 description 8
- 238000002360 preparation method Methods 0.000 description 8
- 239000002562 thickening agent Substances 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 7
- DRDVZXDWVBGGMH-UHFFFAOYSA-N zinc;sulfide Chemical compound [S-2].[Zn+2] DRDVZXDWVBGGMH-UHFFFAOYSA-N 0.000 description 7
- 239000002184 metal Substances 0.000 description 6
- 238000007664 blowing Methods 0.000 description 5
- -1 iron ions Chemical class 0.000 description 5
- 230000001603 reducing effect Effects 0.000 description 5
- 229910052782 aluminium Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000706 filtrate Substances 0.000 description 4
- 239000011572 manganese Substances 0.000 description 4
- 150000002739 metals Chemical class 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- 229910001710 laterite Inorganic materials 0.000 description 3
- 239000011504 laterite Substances 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 229910052748 manganese Inorganic materials 0.000 description 3
- 229910052976 metal sulfide Inorganic materials 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 230000003472 neutralizing effect Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 229910052595 hematite Inorganic materials 0.000 description 2
- 239000011019 hematite Substances 0.000 description 2
- 150000004679 hydroxides Chemical class 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000004886 process control Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 241000080590 Niso Species 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 1
- MYYPUXZNVLDNLK-UHFFFAOYSA-N [Ni].[Co].S(O)(O)(=O)=O Chemical compound [Ni].[Co].S(O)(O)(=O)=O MYYPUXZNVLDNLK-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004993 emission spectroscopy Methods 0.000 description 1
- 230000008570 general process Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 229910000358 iron sulfate Inorganic materials 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 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
- 229910052919 magnesium silicate Inorganic materials 0.000 description 1
- 235000019792 magnesium silicate Nutrition 0.000 description 1
- 239000000391 magnesium silicate Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 150000004763 sulfides Chemical class 0.000 description 1
- 239000013589 supplement Substances 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/043—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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
-
- 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
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
- C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
-
- 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 dezincification system for removing a trace amount of zinc contained in a cobalt-containing aqueous nickel sulfate solution, and a method therefor.
- Patent Document 1 As disclosed in the following Patent Document 1 as a dezincification treatment plant and an operation method of the dezincification plant, and a wet refining method of nickel oxide ore, sulfuric acid is used as a wet refining method of nickel oxide ore in recent years.
- High pressure acid leaching (HPAL) has attracted attention.
- the hydrometallurgical process is advantageous in terms of energy and cost because it does not include dry processing steps such as drying and roasting steps, but consists of a consistent wet step.
- the hydro-smelting method using the HPAL method is also advantageous in that a nickel-cobalt mixed sulfide in which the nickel grade is concentrated to about 50% by weight can be obtained. Therefore, a process of recovering valuable metals from low grade nickel oxide ore by a hydrometallurgical process using the HPAL process has been commercialized commercially.
- nickel sulfate aqueous solution containing cobalt leached from nickel oxide ore By adding a sulfiding agent such as hydrogen sulfide gas to a nickel sulfate aqueous solution containing cobalt leached from nickel oxide ore by the HPAL method (hereinafter also referred to as “nickel / cobalt mixed sulfuric acid aqueous solution” or simply “sulfuric acid aqueous solution”) A method of recovering nickel-cobalt mixed sulfide is generally used.
- a sulfiding agent such as hydrogen sulfide gas
- the nickel-cobalt mixed sulfide recovered in this way is used as a raw material for purifying high purity nickel and nickel sulfate.
- High purity refers to the quality in which the content of impurities including zinc is controlled to a predetermined level or less. Therefore, there is a need for nickel-cobalt mixed sulfides of low zinc grade, ie, quality guaranteed in the range of predetermined standard (zinc grade ⁇ 250 ppm by weight).
- the dezincification step requires general process control to remove even a slight amount of zinc in an aqueous sulfuric acid solution by reacting a hydrogen sulfide gas with a nickel-cobalt mixed aqueous sulfuric acid solution under a constant pressure.
- the process control required here means control for keeping the zinc concentration in the aqueous sulfuric acid solution at a constant value or less.
- the aqueous solution after the dezincification step is analyzed, and controlled so as to keep the zinc concentration below a certain level.
- the zinc concentration is controlled to be maintained below a certain level, there is a problem that the zinc grade in the nickel-cobalt mixed sulfide fluctuates and exceeds the control standard. Therefore, a new quality control method capable of more stably controlling the zinc quality in the nickel-cobalt mixed sulfide has been required.
- the aqueous solution (final solution) after the dezincification step is analyzed (final solution analysis) every two hours, and management is carried out by maintaining the zinc concentration in the final solution below a certain value. It had been. That is, the quality control of feedback processing the result of the above-described final solution analysis has been implemented. However, it has been difficult to spread quality control to products only by maintaining the zinc concentration in the final solution below a certain value.
- the hydrogen sulfide gas blown into excess removes nickel together with zinc up to the recovery object. That is, under the conventional quality control system, as a result of thorough quality control so as to lower the product defect rate for zinc grade, it is inevitable that a considerable amount of nickel loss occurs.
- the present invention has been proposed in view of such circumstances, and an object thereof is to use nickel in a dezincification step of removing zinc from a nickel sulfate aqueous solution containing a small amount of zinc using hydrogen sulfide gas.
- An object of the present invention is to provide a zinc sulfate aqueous solution dezincification system capable of stably maintaining a low zinc grade in cobalt mixed sulfide, and a method therefor.
- the present inventors focused on the fact that in the nickel-cobalt mixed sulfuric acid aqueous solution, the zinc grade of the nickel-cobalt mixed sulfide fluctuates in conjunction with the fluctuation of the nickel concentration as well as the fluctuation of the zinc concentration.
- conventionally only zinc concentration was generally applied to the control index, and it was found that it is effective to add nickel concentration to the control index, and the present invention was completed.
- one aspect of the present invention is a nickel sulfate aqueous solution dezincing system (100) for removing zinc from a nickel sulfate aqueous solution containing cobalt and zinc as an impurity using hydrogen sulfide gas.
- Another aspect of the present invention is the use of hydrogen sulfide gas from an aqueous nickel sulfate solution containing high pressure acid leached (HPAL) cobalt with sulfuric acid and zinc as an impurity in a hydrometallurgical process of nickel oxide ore Dezincification of an aqueous solution of nickel sulfate to remove zinc
- a zinc sulfate aqueous solution dezincification system capable of stably maintaining a low zinc grade in a nickel-cobalt mixed sulfide, and a method therefor.
- FIG. 1 is a simplified flow chart for explaining a process of producing a nickel-cobalt mixed sulfide from low grade nickel oxide ore as a premise technology of the present invention.
- FIG. 2 is a block diagram for explaining a system for removing zinc sulfate aqueous solution (hereinafter also referred to as “the present system”) according to an embodiment of the present invention.
- FIG. 3 is a potential-pH diagram of the MSH 2 O system for illustrating the ease of formation of metal sulfide with respect to a reducing atmosphere.
- FIG. 4 is a graph showing the relation of nickel loss to zinc grade in the nickel-cobalt mixed sulfide obtained in the sulfurizing step of FIG.
- FIG. 5 is a flowchart for explaining the process of FIG. 1 in more detail.
- a dezincification system (the present system) of a nickel-cobalt mixed sulfuric acid aqueous solution and a method (the present method) according to an embodiment of the present invention will be described with reference to the drawings.
- this invention is not limited to the following example, In the range which does not deviate from the summary of this invention, it can change arbitrarily.
- a wet smelting method of nickel oxide ore including the present method (hereinafter, also referred to simply as a “wet smelting method”) will be described as a prerequisite technology thereof.
- the hydrosmelting method is a hydrosmelting method in which nickel and cobalt are leached and recovered from nickel oxide ore by, for example, the HPAL method.
- the underlying technology of the present invention will be described with reference to FIG.
- FIG. 1 is a simplified flow chart for explaining a process of producing a nickel-cobalt mixed sulfide from low grade nickel oxide ore as a premise technology of the present invention.
- FIG. 5 is a flowchart for explaining the process of FIG. 1 in more detail.
- the hydrometallurgical method including the present method comprises a slurry preparation step (S1), a high pressure acid leaching step (hereinafter, also simply referred to as "leaching step") (S2), It has a sum process (S3), a solid-liquid separation process (S4), a neutralization process (S5), a dezincification process (S6), a sulfurization process (S7), and a final neutralization process (S8).
- This method is based on the HPAL leaching step (S2), and in particular, in the dezincification step (S6), an aqueous nickel-cobalt mixed sulfuric acid solution capable of stably keeping the zinc grade in the nickel-cobalt mixed sulfide low. It is a dezincing method.
- the slurry preparation step (S1) several types of nickel oxide ore are mixed, mixed with water and classified to prepare an ore slurry.
- the leaching step (S2) sulfuric acid is added to the obtained slurry of nickel oxide ore, and leaching treatment is performed under high temperature and high pressure.
- the preliminary neutralization step (S3) the pH of the leached slurry obtained in the leaching step (S2) is adjusted to a predetermined range.
- the solid-liquid separation step (S4) the residue is separated while washing the pH-adjusted leached slurry in multiple stages to obtain a leachate containing an impurity element together with nickel and cobalt.
- the neutralization step (S5) the pH of the leachate solid-liquid separated in the solid-liquid separation step (S4) is adjusted, the neutralization precipitate containing the impurity element is separated, and the neutralization final solution containing zinc together with nickel and cobalt
- a zinc sulfide is formed by adding a sulfurizing agent such as hydrogen sulfide gas to the final solution after neutralization, and the zinc sulfide is separated and removed to obtain a nickel and cobalt-containing mother liquor containing nickel and cobalt.
- a sulfiding agent is added to the nickel recovery mother liquor to form a mixed sulfide containing nickel and cobalt.
- a leaching residue containing free sulfuric acid transferred from the solid-liquid separation step (S4) and a filtrate containing impurities such as magnesium, aluminum, iron transferred from the sulfurization step (S7) ( Neutralize the poor solution).
- FIG. 2 is a block diagram for explaining a dezincification system (the present system) of a nickel-cobalt mixed sulfuric acid aqueous solution according to an embodiment of the present invention.
- the present system 100 shown in FIG. 2 efficiently performs dezincification of a nickel-cobalt mixed sulfuric acid aqueous solution in which zinc is removed from a sulfuric acid aqueous solution containing nickel and cobalt using hydrogen sulfide gas.
- the present system 100 includes a reaction vessel 50, a hydrogen sulfide supply means 40, a zinc concentration detection means 10, a nickel concentration detection means 20, and a control unit 90, and the processing of the dezincing step (S6) It is for the zinc concentration detection means 10 and the nickel concentration detection means 20, for example, ICP emission spectrometry or atomic absorption analysis can be used.
- the reaction vessel 50 introduces a nickel-cobalt mixed sulfuric acid aqueous solution, blows in hydrogen sulfide gas, and discharges the zinc sulfide (ZnS) and the nickel recovery mother liquor after the treatment of the zinc removal step (S6).
- the hydrogen sulfide supply means 40 supplies hydrogen sulfide gas to the reaction vessel 50 so as to blow an appropriate amount.
- the zinc concentration detection means 10 detects the zinc concentration Z contained in the sulfuric acid aqueous solution.
- the nickel concentration detection means 20 detects the nickel concentration N contained in the sulfuric acid aqueous solution.
- the control unit 90 controls the hydrogen sulfide supply means 40 to adjust the flow rate P of the hydrogen sulfide gas supplied to the sulfuric acid solution.
- the control unit 90 further includes a management index calculation unit 91.
- the present system 100 and the present method have a problem that it is inevitable that a considerable amount of nickel loss occurs as a result of thorough quality control so as to lower the product defect rate for zinc quality under the conventional quality control system. Solve the problem. Specifically, in the dezincification process of a process of producing a nickel-cobalt mixed sulfide from low grade nickel oxide ore, even if the zinc concentration in the sulfuric acid aqueous solution causing the failure is at a level that causes no problem, In order to remove the excess hydrogen sulfide gas in excess of the necessary minimum to remove, it has been done routinely to improve.
- the blowing amount of hydrogen sulfide gas is suppressed, the zinc to be removed, ie, the absolute amount of dezincification decreases, and even if the zinc concentration Z value remains high, the nickel concentration N is sufficient to compensate for it. If secured, the zinc quality of the target product can be maintained at the pass level.
- the nickel loss is suppressed by appropriately adjusting the amount P supplied to the
- the present system 100 and the present method aim at the following.
- First to improve the recovery efficiency of valuable metals from low grade nickel oxide ore. In particular, to control nickel loss.
- FIG. 3 is a potential-pH diagram of the MSH 2 O system for illustrating the ease of formation of metal sulfide with respect to a reducing atmosphere.
- the source of this figure is the introductory metal chemistry series 3 "Metal Smelting Engineering" (The Japan Institute of Metals).
- the horizontal axis of the graph shown in FIG. 3 indicates the pH of the aqueous solution, and the vertical axis indicates the redox potential of the aqueous solution.
- Hydrogen sulfide (H 2 S) gas produces metal sulfide with strong reducing action on metal ions in the contacting aqueous solution.
- the main metal ions tend to precipitate out as sulfide in the order of Cu 2+ , Cd 2+ , Pb 2+ , Sn 2+ , Zn 2+ , Co 2+ , Ni 2+ , Fe 2+ , Mn 2+ .
- the following formulas [1] and [2] show the sulfurization reaction of Zn and Ni by hydrogen sulfide, but since the following formulas [1] and [2] are hydrogen ion generation reactions, the higher the pH, The reaction is easy to proceed. In other words, when comparing Zn and Ni, Zn tends to form sulfide at a lower pH. According to FIG.
- the zinc concentration Z of the neutralization final solution that is, the dezincing initial solution
- the nickel concentration N are generally linked in the vertical movement. That is, when the zinc concentration Z increases, the nickel concentration N also increases in conjunction.
- the prescribed quality level can be regarded as a trace amount of zinc with respect to the amount of nickel which is the main component contained about 50% by weight. Therefore, if both the amount of nickel and the amount of zinc increase, the amount of zinc relative to the amount of nickel does not rapidly increase just because the concentration of zinc Z increases, so the H 2 S flow rate often does not necessarily need to increase rapidly .
- nickel loss in order to reduce the nickel loss, it is effective to appropriately manage with less fluctuation without excessively reducing the zinc grade of the product. For these reasons, nickel loss can be suppressed by maintaining the zinc quality of the product nickel-cobalt mixed sulfide within the standard ( ⁇ 250 ppm by weight) at a level not exceeding excess quality, for example, around 150 ppm by weight. .
- FIG. 4 is a graph showing the relationship between the nickel loss and the zinc grade of the nickel-cobalt mixed sulfide obtained in the process of FIG.
- the horizontal axis of the graph shown in FIG. 4 represents the zinc grade (weight ppm) of the product nickel-cobalt mixed sulfide, and the vertical axis represents nickel loss (t / month).
- the present system 100 and the present method aim at quality control such that good production efficiency can be obtained at a prescribed quality level while avoiding excessive quality.
- nickel oxide ore is subjected to high pressure acid leaching (HPAL) using sulfuric acid (S2).
- HPAL high pressure acid leaching
- S2 sulfuric acid
- S2 An aqueous solution of sulfuric acid containing nickel and cobalt is obtained by HPAL (S2).
- Zinc is removed from the obtained nickel-cobalt mixed sulfuric acid aqueous solution using hydrogen sulfide gas (S6).
- S6 dezincification step (S6), a slight amount of zinc contained in a nickel-cobalt mixed sulfuric acid aqueous solution is reacted with hydrogen sulfide (H 2 S) gas as a sulfiding agent to remove and recover as zinc sulfide (ZnS) (Fig. 1, see Figure 5).
- the ratio (Z / N) of the nickel concentration N contained in the nickel-cobalt mixed sulfuric acid aqueous solution and the zinc concentration Z contained in the nickel-cobalt mixed sulfuric acid aqueous solution is applied to the management index W.
- the ratio of the control reference value 0.30 to 0.35% by weight is maintained (see FIG. 2).
- the zinc quality of the product nickel-cobalt mixed sulfide can be maintained within the standard ( ⁇ 250 ppm by weight) range, and the variation of the zinc quality of the product is reduced, and an extremely low zinc quality product is produced. Can be prevented. As a result, nickel loss can be reduced.
- FIG. 5 is a flowchart for explaining the process of FIG. 1 in more detail.
- the hydrometallurgical process of this nickel oxide ore is a hydrometallurgical process having a slurry preparation process (S1) to a final neutralization process (S8).
- the present system and the present method are capable of stably keeping the zinc grade in the nickel-cobalt mixed sulfide low in the dezincification step (S6) therein.
- the management method in the dezincification step (S6) the conventional example is taken as comparative example 1, examples 1 to 4 according to an embodiment of the present invention are listed, and their results will be described later.
- ⁇ Slurry preparation process> In the slurry preparation step (S1), using nickel oxide ore which is a raw material ore, several kinds of nickel oxide ore are mixed so as to obtain predetermined Ni grade and impurity grade, they are mixed with water and slurried, and sieved After classification at a predetermined classification point to remove oversized ore particles, only undersized ore is used.
- Nickel oxide ores used in the slurry preparation step (S1) are mainly so-called laterite ores such as limonite or saprolite ore.
- the nickel content of laterite ore is usually from 0.8 to 2.5% by weight and is contained as hydroxide or siliceous earth (magnesium silicate) mineral.
- the iron content is 10 to 50% by weight, and is mainly in the form of a trivalent hydroxide (gesite), but a part of divalent iron is contained in the clay-mass earth mineral.
- the nickel oxide ore used in this slurry preparation step (S1) includes not only such laterite ore but also oxide ores containing valuable metals such as nickel, cobalt, manganese and copper, such as manganese lumps present in the deep sea floor May be used.
- the classification method of the nickel oxide ore is not particularly limited as long as the ore can be classified based on the desired particle size, and for example, it can be performed by sieving using a general vibrating sieve or the like. Further, the classification point is not particularly limited, and the classification point for obtaining an ore slurry composed of ore particles having a particle diameter value or less desired can be appropriately set.
- the nickel oxide ore is leached using the HPAL method. Specifically, sulfuric acid is added to the ore slurry obtained by pulverizing nickel oxide ore as a raw material, and added under high temperature conditions of 220 to 280 ° C. using, for example, a high-temperature pressure vessel (autoclave). By pressure, nickel, cobalt and the like are leached from the ore to form a leach slurry consisting of a leachate and a leach residue.
- a high-temperature pressure vessel autoclave
- the addition amount of sulfuric acid in the leaching step (S2) is not particularly limited, and an excessive amount such that iron in the ore is leached is used.
- the pH of the obtained leachate is 0.1 to 1.0 from the viewpoint of solid-liquid separation of the leaching residue containing hematite produced in the solid-liquid separation step (S4) of the next step. It is preferable to adjust so that
- the pH of the leached slurry obtained in the leaching step (S2) is adjusted to a predetermined range.
- the leaching step (S2) in which the above-described HPAL leaching treatment is performed excess sulfuric acid is added from the viewpoint of improving the leaching rate. Therefore, the obtained leaching slurry contains excess sulfuric acid which did not participate in the leaching reaction, and its pH is very low.
- the pre-neutralization step (S3) the pH of the leached slurry is adjusted to a predetermined range so that washing can be efficiently performed in multistage washing in the solid-liquid separation step (S4) of the next step.
- the pH of the leached slurry to be subjected to the solid-liquid separation step (S4) is adjusted to about 2 to 6, preferably 2.5 to 3.4. If the pH is lower than 2, the cost for making the post-process equipment acid resistant is required. On the other hand, if the pH is higher than 6, nickel leached into the leachate (slurry) may precipitate in the course of washing and remain as a residue, thereby reducing the recovery of nickel and lowering the washing efficiency. There is sex.
- Solid-liquid separation process In the solid-liquid separation step (S4), the leached slurry pH-adjusted in the preliminary neutralization step (S3) is washed in multiple stages to obtain a leachate containing zinc as an impurity element in addition to nickel and cobalt and a leaching residue.
- a thickener is provided in multiple stages as a solid-liquid separation device to perform solid-liquid separation treatment. Specifically, the leaching slurry is first diluted by the washing solution, and then the leaching residue in the slurry is concentrated as a thickener of thickener. Thereby, the nickel content adhering to the leaching residue can be reduced according to the degree of its dilution. In addition, by connecting and using thickeners in multiple stages in this way, it is possible to improve the recovery of nickel and cobalt.
- a continuous countercurrent washing method (CCD method: Counter Current Decantation method) in which a nickel-free washing solution is brought into contact with a countercurrent is used.
- CCD method Counter Current Decantation method
- the amount of cleaning solution newly introduced into the system can be reduced, and the recovery of nickel and cobalt can be improved.
- the cleaning solution is not particularly limited, but a cleaning solution which does not contain nickel and does not affect the process can be used. Among them, it is preferable to use an aqueous solution having a pH of 1 to 3. When the pH of the washing solution is high, if aluminum is contained in the leaching solution, a bulky aluminum hydroxide is formed, which causes poor settling of the leaching residue in the thickener. From this, it is preferable to repeatedly use the poor solution of low pH (pH is about 1 to 3) obtained in the subsequent step, the sulfurizing step (S7), as the washing solution.
- pH pH is about 1 to 3
- the neutralization step (S5) while suppressing the oxidation of the separated leachate, the neutralization final solution serving as the source of the mother liquor for nickel recovery, and the neutralized precipitate slurry containing trivalent iron as an impurity element Form.
- a neutralizing agent such as calcium carbonate is added to the leachate. The addition amount of the neutralizing agent is adjusted so that the pH of the neutralization final solution obtained by neutralization is 4 or less, preferably 3.0 to 3.5, more preferably 3.1 to 3.2.
- the leaching solution is subjected to the neutralization treatment in this manner to neutralize the excess acid used in the leaching treatment by the HPAL method, and to neutralize the final solution serving as the mother liquor for nickel recovery. Generate At this time, the final solution of neutralization is formed and simultaneously impurities are removed as neutralization precipitate.
- the neutralized precipitate is one in which an impurity such as trivalent iron ion or aluminum ion remaining in the solution is formed as a hydroxide.
- the neutralized precipitate may be returned to the solid-liquid separation step (S4) again.
- a sulfurizing agent such as hydrogen sulfide gas is added to the neutralized final solution obtained from the neutralization step (S5) to form a zinc sulfide by sulfurization treatment, and the zinc sulfide The product is separated and removed to obtain a nickel recovery mother liquor (dezinced final solution) containing nickel and cobalt. More specifically, it is as follows.
- zinc is selectively sulfided relative to nickel and cobalt by introducing a neutralization final solution containing zinc together with nickel and cobalt into a pressurized container, and blowing hydrogen sulfide gas into a gas phase, A zinc sulfide and a nickel recovery mother liquor are formed.
- the sulfurization reaction is caused by blowing hydrogen sulfide gas as a sulfurizing agent into the initial solution of the sulfurization reaction with the dezincification final solution, which is the mother liquid for recovering nickel, as the initial solution of the sulfurization reaction, thereby causing a nickel / cobalt mixed sulfide Produce an object and a poor solution.
- the sulfidation treatment in the sulfidation step (S7) can be carried out using a sulfidation reaction tank or the like, and hydrogen sulfide gas is introduced into the gas phase portion in the reaction vessel with respect to the sulfurization reaction start solution charged in the sulfidation reaction tank.
- a sulfidation reaction is generated by blowing in and dissolving hydrogen sulfide gas in the solution.
- nickel and cobalt contained in the initial solution of the sulfidation reaction are immobilized as a mixed sulfide.
- the obtained slurry containing nickel and cobalt mixed sulfide is charged into a solid-liquid separation device such as thickener and subjected to sedimentation separation treatment, and only the mixed sulfide is separated and recovered from the bottom of the thickener. .
- the aqueous solution component separated through the sulfiding step (S7) overflows from the top of the thickener and is recovered as a poor solution.
- the collected poor liquid is a solution having a very low concentration of valuable metals such as nickel, and contains impurity elements such as iron, magnesium and manganese remaining without being sulfurized.
- the poor solution is transferred to the final neutralization step (S8) to be detoxified. Alternatively, it may be returned to the solid-liquid separation step (S4) and used again for nickel recovery.
- the final neutralization step (S8) a leaching residue containing free sulfuric acid transferred from the above-mentioned solid-liquid separation step (S4) and a filter containing impurities such as magnesium, aluminum, iron transferred from the sulfidation step (S7) Neutralize the liquid (poor liquid).
- the final neutralization step (S8) is the neutralization performed to discard the slurry from the hydrometallurgical process to the outside, and refers to the neutralization process performed at the end of the hydrometallurgical process.
- the leaching residue and the filtrate are adjusted to a predetermined pH range by a neutralizing agent to be a waste slurry (tailing).
- the tailing generated in this reaction tank is transferred to a tailing dam (waste reservoir).
- the final neutralization step (S8) the free sulfuric acid contained in the leaching residue is completely neutralized, the impurities contained in the filtrate are fixed as hydroxides, and a slurry containing hydroxides of impurities is obtained. Discharge to the tailing dam.
- Example 1 When the ratio of zinc concentration to nickel concentration in the nickel-cobalt mixed sulfuric acid aqueous solution is used as a control index, the zinc grade variation (standard deviation ⁇ ) of nickel-cobalt mixed sulfide is 29 weight ppm over 3 months Met. The results of Example 1 with respect to Comparative Example 1 are shown in Table 1.
- Table 1 is a table showing the variation of the zinc grade with respect to the control distinction in the dezincification process by the standard deviation ⁇ . More specifically, the upper part of Table 1 shows the case where only the zinc concentration is used as a management index by the conventional management method, and the lower part of Table 1 shows the ratio of zinc concentration to nickel concentration by the management method of this method. Is used as a control index, and in each case, the variation value of the zinc grade in the nickel-cobalt mixed sulfide is indicated by the standard deviation ⁇ .
- Example 1 with respect to Comparative Example 1 are as shown in Table 1, and Example 1 with a circle is better than Comparative Example 1 with a cross.
- Example 2 When the ratio of zinc concentration to nickel concentration in a nickel-cobalt mixed sulfuric acid aqueous solution is controlled as 0.25 to 0.30% by weight for one month using the same control index as in Example 1, nickel-cobalt mixed The average value of the zinc grade of the sulfide was 132 ppm by weight, the zinc acceptance rate was 100%, and the nickel loss was 10.7 t / month.
- Example 3 When the ratio of the zinc concentration to the nickel concentration in the nickel-cobalt mixed sulfuric acid aqueous solution is controlled at 0.30 to 0.35 wt% for one month, using the same control index as in Examples 1 and 2, The average zinc grade of the cobalt mixed sulfide was 152 ppm by weight, the zinc acceptance rate was 100%, and the nickel loss was 9.6 t / month.
- Example 4 When the ratio of zinc concentration to nickel concentration in a nickel-cobalt mixed sulfuric acid aqueous solution is controlled at 0.35 to 0.40% by weight for one month using the same control index as in Examples 1 and 2, The average value of the zinc grade in the cobalt mixed sulfide was 171 ppm by weight, the zinc acceptance rate was 98%, and the nickel loss was 8.4 t / month. Even if the average value is 171 ppm by weight and within the range of the specification ( ⁇ 250 ppm by weight), the result of Example 4 is unacceptable because the rejection rate deviated from the range is 2%.
- Table 2 shows the average of the zinc grades when setting and managing three control reference values using the ratio of the zinc concentration to the nickel concentration as a control index as in Example 1 shown at the bottom of Table 1 It is the table which showed the relationship between the value, the zinc grade passing rate, and the amount of nickel loss.
- Example 2 The results of Examples 2 to 4 are as shown in Table 2.
- Example 2 and 3 were circled, and Example 4 was marked with x.
- Example 4 was marked with x.
- nickel loss round marks were given to Examples 3 and 4 and X marks were given to Example 2.
- Example 3 the pass rate and the nickel loss were both marked with a circle, while in Examples 2 and 4, either the nickel loss or the pass rate was marked with a cross. That is, the conclusion that Example 3 is the best was obtained.
- Example 3 of Table 2 it is best that the ratio of zinc concentration to nickel concentration in the nickel-cobalt sulfuric acid solution is controlled to 0.30 to 0.35% by weight as a control index. I understood.
- the average value of the zinc grade in the nickel-cobalt mixed sulfide was 152 ppm by weight, the zinc acceptance rate was 100%, and the nickel loss was 9.6 t / month.
- Example 1 it is confirmed in Example 1 using the same management index that the variation is also stable as compared with Comparative Example 1 that the average value of the zinc quality of Example 3 is 152 ppm by weight. .
- the variation since the variation is small and stable, it is possible to solve the problem that the zinc grade in the nickel-cobalt mixed sulfide fluctuates and exceeds the control standard. Furthermore, since the addition of excess hydrogen sulfide gas does not lower the zinc grade more than necessary, nickel loss can be reduced. This means that the amount of expensive hydrogen sulfide gas used has also been reduced. According to the present invention, it is possible to realize a new management method capable of more stably controlling the zinc grade in the nickel-cobalt mixed sulfide.
- the terms described together with the broader or synonymous different terms at least once can be replaced with the different terms anywhere in the specification or the drawings.
- the configuration of the dezincification system of the nickel-cobalt mixed sulfuric acid aqueous solution is not limited to those described in the embodiment and each example of the present invention, and various modifications can be made.
- 10 zinc concentration detection means 10 zinc concentration detection means, 20 nickel concentration detection means, 40 hydrogen sulfide supply means, 50 reaction vessel, 90 control unit, 91 management index calculation means, 100 nickel-cobalt mixed sulfuric acid aqueous solution dezincification system (this system), Z ( Zinc concentration contained in sulfuric acid aqueous solution, N nickel concentration (containing in sulfuric acid aqueous solution), P amount of supplied hydrogen sulfide gas (supplied to sulfuric acid aqueous solution), Q (for management index W) management reference value, S1 Slurry preparation process, S2 high pressure acid leaching (HPAL) process (leaching process), S3 preliminary neutralization process, S4 solid-liquid separation process, S5 neutralization process, S6 dezincification process, S7 sulfurization process, S8 final neutralization process
- HPAL high pressure acid leaching
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Abstract
Description
前記硫酸ニッケル水溶液を貯留する反応容器(50)と、
該反応容器(50)に硫化水素ガスを供給する硫化水素供給手段(40)と、
前記硫酸ニッケル水溶液中に含有される亜鉛濃度(Z)を検出する亜鉛濃度検出手段(10)と、
前記硫酸ニッケル水溶液中に含有されるニッケル濃度(N)を検出するニッケル濃度検出手段(20)と、
前記硫化水素ガスを前記反応容器に供給する量(P)を前記硫化水素供給手段(40)に調整させる制御部(90)と、
を備え、
前記制御部(90)は、
前記硫酸ニッケル水溶液中に含有されるニッケル濃度(N)に対する硫酸ニッケル水溶液中に含有される亜鉛濃度(Z)の比率を管理指標(W=Z/N)として算出する管理指標算出手段(91)をさらに備え、
該管理指標算出手段(91)により算出された前記管理指標(W)を管理基準値内(Q1≦W≦Q2)に維持するように調整するようにしたものである。
前記硫酸ニッケル水溶液中に含有されるニッケル濃度(N)に対する前記硫酸ニッケル水溶液中に含有される亜鉛濃度(Z)の比率を管理指標(W=Z/N)に適用し、
前記硫化水素ガスを前記反応容器に供給する量(P)を調整することにより前記管理指標(W=Z/N)を管理基準値内(Q1≦W≦Q2)に維持するようにした、
硫酸ニッケル水溶液の脱亜鉛方法である。
NiSO4 + H2S → NiS + H2SO4・・・[2]
脱亜鉛始液Zn濃度×始液流量×反応当量×係数(補正値)=H2S流量・・・[3]
初期設定後は、分析されたニッケル濃度Nと亜鉛濃度Zにより算出された管理指標Wをフィードバックして、管理基準値Q内に管理指標Wが維持されるように硫化水素ガスの供給量を調整する。
スラリー調製工程(S1)では、原料鉱石であるニッケル酸化鉱石を用いて、数種類のニッケル酸化鉱石を所定のNi品位、不純物品位となるように混合し、それらを水と混合してスラリー化し、篩にかけて所定の分級点で分級してオーバーサイズの鉱石粒子を除去した後に、アンダーサイズの鉱石のみを使用する。
浸出工程(S2)では、ニッケル酸化鉱石に対して、HPAL法を用いた浸出処理を施す。具体的には、原料となるニッケル酸化鉱石を粉砕等して得られた鉱石スラリーに硫酸を添加し、例えば高温加圧容器(オートクレーブ)を用いて、220~280℃の高い温度条件下で加圧することによって鉱石からニッケル、コバルト等を浸出し、浸出液と浸出残渣とからなる浸出スラリーを形成する。
予備中和工程(S3)では、浸出工程(S2)にて得られた浸出スラリーのpHを所定範囲に調整する。上述したHPAL法による浸出処理を行う浸出工程(S2)では、浸出率を向上させる観点から過剰の硫酸を加えるようにしている。そのため、得られた浸出スラリーには浸出反応に関与しなかった余剰の硫酸が含まれており、そのpHは非常に低い。このことから、予備中和工程(S3)では、次工程の固液分離工程(S4)における多段洗浄時に効率よく洗浄が行われるように、浸出スラリーのpHを所定の範囲に調整する。
固液分離工程(S4)では、予備中和工程(S3)にてpH調整された浸出スラリーを多段洗浄して、ニッケル及びコバルトのほか不純物元素として亜鉛を含む浸出液と浸出残渣とを得る。
中和工程(S5)では、固液分離工程(S4)にて分離された浸出液のpHを調整し、不純物元素を含む中和澱物を分離して、ニッケル及びコバルトと共に亜鉛を含む中和終液を得る。より具体的には以下のとおりである。
脱亜鉛工程(S6)では、中和工程(S5)から得られた中和終液に硫化水素ガス等の硫化剤を添加して硫化処理を施すことにより亜鉛硫化物を生成させ、その亜鉛硫化物を分離除去してニッケル及びコバルトを含むニッケル回収用母液(脱亜鉛終液)を得る。より具体的には、以下のとおりである。
硫化工程(S7)では、ニッケル回収用母液に対し、不純物成分の少ないニッケル・コバルト混合硫化物と、ニッケル及びコバルトの濃度を低い水準で安定させた貧液と、を生成させる。ここでは、ニッケル回収用母液である脱亜鉛終液を硫化反応始液として、その硫化反応始液に対して硫化剤としての硫化水素ガスを吹き込むことによって硫化反応を生じさせ、ニッケル・コバルト混合硫化物と、貧液と、を生成させる。
最終中和工程(S8)は、上述した固液分離工程(S4)から移送された遊離硫酸を含む浸出残渣と、硫化工程(S7)から移送されたマグネシウムやアルミニウム、鉄等の不純物を含むろ液(貧液)の中和を行う。最終中和工程(S8)とは、湿式製錬プロセスから外部にスラリーを廃棄するために行う中和であり、湿式製錬プロセスの最後に行う中和工程のことをいう。
従来の一般的な亜鉛濃度のみを管理指標に用いて脱亜鉛工程を管理した場合、製品であるニッケル・コバルト混合硫化物の亜鉛品位のバラツキ(標準偏差σ)は35重量ppmであった。
ニッケル・コバルト混合硫酸水溶液中のニッケル濃度に対する亜鉛濃度の比率を管理指標に用いて管理した場合、3か月間の、ニッケル・コバルト混合硫化物の亜鉛品位のバラツキ(標準偏差σ)は29重量ppmであった。比較例1に対する実施例1の成績を表1に示す。
実施例1と同様の管理指標を用いて、1ヶ月間、ニッケル・コバルト混合硫酸水溶液中のニッケル濃度に対する亜鉛濃度の比率を0.25~0.30重量%として管理した場合、ニッケル・コバルト混合硫化物の亜鉛品位の平均値は132重量ppm、亜鉛合格率は100%であり、ニッケルロスは10.7t/月であった。
実施例1,2と同様の管理指標を用いて、1ヶ月間、ニッケル・コバルト混合硫酸水溶液中のニッケル濃度に対する亜鉛濃度の比率を0.30~0.35重量%で管理した場合、ニッケル・コバルト混合硫化物の亜鉛品位の平均値は152重量ppm、亜鉛合格率は100%であり、ニッケルロスは9.6t/月であった。
実施例1,2と同様の管理指標を用いて、1ヶ月間、ニッケル・コバルト混合硫酸水溶液中のニッケル濃度に対する亜鉛濃度の比率を0.35~0.40重量%で管理した場合、ニッケル・コバルト混合硫化物における亜鉛品位の平均値は171重量ppm、亜鉛合格率は98%であり、ニッケルロスは8.4t/月であった。平均値は171重量ppmで規格(≦250重量ppm)の範囲内であっても、その範囲から逸脱した不合格率が2%のため、実施例4の結果は許容できない。
Claims (4)
- コバルト、および不純物として亜鉛を含有する硫酸ニッケル水溶液から硫化水素ガスを用いて亜鉛を除去する硫酸ニッケル水溶液の脱亜鉛システムであって、
前記硫酸ニッケル水溶液を貯留する反応容器と、
該反応容器に硫化水素ガスを供給する硫化水素供給手段と、
前記硫酸ニッケル水溶液中に含有される亜鉛濃度(Z)を検出する亜鉛濃度検出手段と、
前記硫酸ニッケル水溶液中に含有されるニッケル濃度(N)を検出するニッケル濃度検出手段と、
前記硫化水素ガスを前記反応容器に供給する量(P)を前記硫化水素供給手段に調整させる制御部と、
を備え、
前記制御部は、
前記硫酸ニッケル水溶液中に含有されるニッケル濃度(N)に対する硫酸ニッケル水溶液中に含有される亜鉛濃度(Z)の比率を管理指標(W=Z/N)として算出する管理指標算出手段をさらに備え、
該管理指標算出手段により算出された前記管理指標(W)を管理基準値内(Q1≦W≦Q2)に維持するように調整する、
硫酸ニッケル水溶液の脱亜鉛システム。 - 前記管理指標(W=Z/N)の管理基準範囲を0.30~0.35重量%の比率に維持する、
請求項1に記載の硫酸ニッケル水溶液の脱亜鉛システム。 - ニッケル酸化鉱石の湿式製錬プロセスの中で硫酸を用いて高圧酸浸出(HPAL)したコバルト、および不純物として亜鉛を含有する硫酸ニッケル水溶液から硫化水素ガスを用いて亜鉛を除去する硫酸ニッケル水溶液の脱亜鉛方法であって、
前記硫酸ニッケル水溶液中に含有されるニッケル濃度(N)に対する前記硫酸ニッケル水溶液中に含有される亜鉛濃度(Z)の比率を管理指標(W=Z/N)に適用し、
前記硫化水素ガスを前記反応容器に供給する量(P)を調整することにより前記管理指標(W=Z/N)を管理基準値内(Q1≦W≦Q2)に維持する、
硫酸ニッケル水溶液の脱亜鉛方法。 - 前記管理指標(W=Z/N)の管理基準範囲を0.30~0.35重量%の比率に維持する、
請求項3に記載の硫酸ニッケル水溶液の脱亜鉛方法。
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JP2002121624A (ja) * | 2000-10-13 | 2002-04-26 | Sumitomo Metal Mining Co Ltd | 硫酸ニッケル溶液からの亜鉛の分離除去方法 |
JP2003313617A (ja) * | 2002-02-25 | 2003-11-06 | Sumitomo Metal Mining Co Ltd | 硫化反応の制御方法 |
JP2013185179A (ja) * | 2012-03-06 | 2013-09-19 | Sumitomo Metal Mining Co Ltd | 中和処理方法及び中和処理プラント |
JP2013185178A (ja) | 2012-03-06 | 2013-09-19 | Sumitomo Metal Mining Co Ltd | 脱亜鉛処理プラント及び脱亜鉛プラントの操業方法、並びにニッケル酸化鉱石の湿式製錬方法 |
JP2017226237A (ja) | 2016-06-20 | 2017-12-28 | 株式会社 34 | ベルト型ライフジャケットに用いられるストッパー |
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US7018605B2 (en) * | 2002-02-25 | 2006-03-28 | Sumitomo Metal Mining Co., Ltd. | Sulfidation reaction control method |
JP2004305917A (ja) * | 2003-04-07 | 2004-11-04 | Sumitomo Metal Mining Co Ltd | 硫酸ニッケル水溶液からの亜鉛の除去方法 |
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JP2002121624A (ja) * | 2000-10-13 | 2002-04-26 | Sumitomo Metal Mining Co Ltd | 硫酸ニッケル溶液からの亜鉛の分離除去方法 |
JP2003313617A (ja) * | 2002-02-25 | 2003-11-06 | Sumitomo Metal Mining Co Ltd | 硫化反応の制御方法 |
JP2013185179A (ja) * | 2012-03-06 | 2013-09-19 | Sumitomo Metal Mining Co Ltd | 中和処理方法及び中和処理プラント |
JP2013185178A (ja) | 2012-03-06 | 2013-09-19 | Sumitomo Metal Mining Co Ltd | 脱亜鉛処理プラント及び脱亜鉛プラントの操業方法、並びにニッケル酸化鉱石の湿式製錬方法 |
JP2017226237A (ja) | 2016-06-20 | 2017-12-28 | 株式会社 34 | ベルト型ライフジャケットに用いられるストッパー |
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JP2019094544A (ja) | 2019-06-20 |
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AU2018372226A1 (en) | 2020-06-18 |
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