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WO2019049593A1 - Procédé de métallurgie par voie humide pour du minerai d'oxyde de nickel - Google Patents

Procédé de métallurgie par voie humide pour du minerai d'oxyde de nickel Download PDF

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Publication number
WO2019049593A1
WO2019049593A1 PCT/JP2018/029778 JP2018029778W WO2019049593A1 WO 2019049593 A1 WO2019049593 A1 WO 2019049593A1 JP 2018029778 W JP2018029778 W JP 2018029778W WO 2019049593 A1 WO2019049593 A1 WO 2019049593A1
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WIPO (PCT)
Prior art keywords
neutralization
liquid
solid
slurry
nickel oxide
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Ceased
Application number
PCT/JP2018/029778
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English (en)
Japanese (ja)
Inventor
雄大 田中
二郎 早田
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sumitomo Metal Mining Co Ltd
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Sumitomo Metal Mining Co Ltd
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Priority to PH1/2020/500279A priority Critical patent/PH12020500279B1/en
Publication of WO2019049593A1 publication Critical patent/WO2019049593A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
    • 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
    • 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
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • 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 method for hydrometallurgical refining of nickel oxide ore, more specifically, the leaching solution obtained by adding sulfuric acid to nickel oxide ore is subjected to neutralization treatment, and the slurry after neutralization is converted to solid-liquid
  • the present invention relates to a method for hydrous smelting of nickel oxide ore in which nickel and cobalt are recovered by subjecting a solution obtained after separation to neutralization treatment by sulfidation treatment.
  • HPAL high pressure acid leaching
  • the amount of hydrogen sulfide gas that can be dissolved in the process liquid in the sulfurization treatment that causes a sulfurization reaction can be calculated by the acid dissociation constant of hydrogen sulfide shown in the following formulas (4) and (5).
  • dissolved in a process liquid can be shown by the following (6) Formula.
  • [S 2- ] (K 1 K 2 ⁇ [H 2 S]) ⁇ [H + ] 2 (6)
  • a method of adding a polymer such as a coagulant or a coagulant which captures fine particles generated by the neutralization reaction to a reaction solution is generally used.
  • a polymer such as a coagulant or a coagulant which captures fine particles generated by the neutralization reaction
  • Patent Document 1 discloses that in the hydrometallurgical process of nickel oxide ore, in order to improve the filterability in the separation of zinc sulfide formed in the dezincification treatment and extend the life of the filter cloth, There is disclosed a method of adding a coagulant to the slurry after the sum reaction. However, this patent document 1 does not show anything about raising the pH in the sulfurization reaction, and enhancing the efficiency of the sulfurization reaction by the pH increase to improve the yield of sulfide.
  • Patent Document 2 discloses a leaching solution containing nickel and cobalt in order to effectively separate and remove neutralized precipitates by suppressing poor filtration and a decrease in filtration rate in a hydrometallurgical process of nickel oxide ore.
  • a method is disclosed in which a neutralization treatment is performed using magnesium oxide as a neutralizing agent, and a cationic flocculant is added to the neutralized slurry to separate and remove the neutralized precipitate.
  • Patent Document 2 there is no indication that the pH is increased in the sulfurization reaction, and the efficiency of the sulfurization reaction is enhanced by the pH increase to improve the yield of sulfide.
  • the present invention has been proposed in view of such circumstances, and it is an object of the present invention to provide a method of hydrorefining a nickel oxide ore without deteriorating the solid-liquid separability of the slurry after the neutralization reaction against the leachate. It is an object of the present invention to provide a method capable of effectively raising the pH and using the process solution to efficiently promote the sulfurization reaction.
  • an aggregating agent is added to the liquid feed line for feeding the neutralized slurry obtained by the neutralization treatment from the neutralization reaction tank to the solid-liquid separator, and the slurry after neutralization passed through the feed line. It has been found that solid-liquid separation can improve solid-liquid separation while effectively raising the pH, and the present invention has been completed.
  • the leaching solution obtained by adding sulfuric acid to nickel oxide ore and leaching is subjected to neutralization treatment in a neutralization reaction tank, and the slurry after neutralization is subjected to solid-liquid
  • It is a wet refining method of nickel oxide ore including a treatment of recovering nickel and cobalt by subjecting a solution after neutralization obtained by solid-liquid separation with a separation device to a sulfurization treatment, and the neutralization reaction tank
  • a coagulant is added to the solid-liquid separator from the feed line for feeding the slurry after neutralization and a flocculant is added, and the slurry passed through the feed line is solid-liquid separated, wet smelting nickel oxide ore It is a method.
  • the second invention of the present invention is, in the first invention, a method for hydrosmelting nickel oxide ore, wherein a coagulant is further added to the liquid feed line.
  • the third invention of the present invention is the method for hydrosmelting nickel oxide ore according to the first or second invention, wherein the coagulant is a cationic coagulant.
  • the pH of the obtained post-neutralization solution is 3.2 or more and 3.5 or less. It is a hydrometallurgical method of nickel oxide ore.
  • a fifth invention of the present invention is the method of hydrosmelting nickel oxide ore according to any one of the first to fourth inventions, wherein calcium carbonate is used as the neutralizing agent in the neutralization treatment.
  • the sixth invention of the present invention is the method according to the fourth or fifth invention, wherein the turbidity of the supernatant liquid in the solid-liquid separator is 50 NTU or less. .
  • the process liquid can be used to provide a method capable of efficiently promoting the sulfidation reaction.
  • the present embodiment will be described in detail with reference to the drawings.
  • this invention is not limited to the following embodiment, A various change is possible in the range which does not change the summary of this invention.
  • the notation “x to y” (x and y are arbitrary numerical values) has the meaning of “x or more and y or less” unless otherwise specified.
  • wet smelting method of nickel oxide ore In the wet refining method of nickel oxide ore according to the present embodiment, the raw material nickel oxide ore is leached with sulfuric acid under high temperature and high pressure conditions, and the obtained leachate is neutralized After removing impurities, nickel and cobalt contained in the leachate are recovered as sulfides.
  • the following wet refining processes show the form which collect
  • HPAL method high temperature pressure acid leaching method
  • FIG. 1 is a process diagram showing an example of the flow of the hydrometallurgical method of nickel oxide ore.
  • a leaching process S1 is carried out in which sulfuric acid is added to a slurry of raw material nickel oxide ore under high temperature and high pressure to leach out, and a leachate obtained by the leaching process
  • a sulfiding step S3 for obtaining a mixed sulfide of nickel and cobalt by adding a sulfiding agent to the obtained solution after the neutralization and subjecting the solution to a sulfiding treatment.
  • Stir treatment is performed in a high pressure atmosphere to produce a leached slurry consisting of leachate and leachate residue.
  • the treatment in the leaching step S1 may be performed in accordance with the conventionally known HPAL process.
  • laterite ores such as limonite ore and saprolite ore can be used.
  • the nickel content of laterite ore is about 0.8% by weight to 2.5% by weight, and is contained as a hydroxide or siliceous earth (magnesium silicate) mineral.
  • solid-liquid separation is performed into a leachate containing nickel, cobalt and the like, and a leachate mainly composed of hematite.
  • a leaching slurry is mixed with a washing solution, and subjected to a solid-liquid separation process by a solid-liquid separation facility such as a thickener.
  • 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.
  • solid-liquid separation tanks such as thickeners connected in multiple stages and perform solid-liquid separation while washing the leached slurry in multiple stages.
  • the leaching solution obtained by solid-liquid separation of the leaching slurry is transferred to the neutralization step S2 of the next step, while the leaching residue is subjected to washing treatment and the like and discharged out of the system.
  • neutralizing agent conventionally known ones can be used.
  • calcium carbonate, calcium hydroxide, sodium hydroxide and the like can be used, and calcium carbonate is particularly preferable.
  • the treatment in the neutralization step S2 is performed in a neutralization treatment plant.
  • the neutralization processing plant includes a neutralization reaction tank that performs processing (neutralization processing) based on the neutralization reaction, and a solid-liquid separation device that separates the obtained post-neutralization slurry into a post-neutralization solution and neutralization sediment. And have.
  • an aggregating agent is added in the liquid feed line for feeding the slurry after neutralization from the neutralization reaction tank to the solid-liquid separator in the neutralization treatment plant, and the fluid passes through the liquid feed line. After neutralization, the slurry is subjected to a solid-liquid separation treatment.
  • the pH of the obtained solution after neutralization is in the range of 3.2 or more and 3.5 or less.
  • the pH exceeds 3.5 hydroxides of nickel may occur, resulting in a recovery loss of nickel.
  • solid-liquid separation may be reduced.
  • the pH of the post-neutralization solution is less than 3.2, the amount of hydrogen sulfide gas that can be dissolved in the subsequent sulfurization step S3 decreases, which may reduce the efficiency of the sulfurization reaction.
  • a sulfiding agent such as hydrogen sulfide gas, sodium sulfide, sodium hydrosulfide or the like is added to the obtained neutralized solution, and a sulfide containing nickel and cobalt with few impurity components (Silver-cobalt mixed sulfide) and a post-sulfiding solution stabilized at a low level of nickel concentration.
  • the slurry of the nickel-cobalt mixed sulfide produced by the sulfidation reaction is subjected to separation treatment using a solid-liquid separation device (sedimentation separation device) such as thickener, etc. Separately from the bottom of the thickener.
  • a solid-liquid separation device such as thickener, etc. Separately from the bottom of the thickener.
  • the post-sulfiding solution which is an aqueous solution component is overflowed and recovered.
  • the recovered after-sulfiding solution is subjected to washing treatment, (final) neutralization treatment and the like together with the leaching residue and the like and discharged out of the system.
  • This neutralization treatment is performed, for example, in a neutralization treatment plant provided with a neutralization reaction tank for performing a neutralization reaction and a solid-liquid separation device for solid-liquid separation of the obtained slurry after neutralization.
  • a neutralization treatment plant provided with a neutralization reaction tank for performing a neutralization reaction and a solid-liquid separation device for solid-liquid separation of the obtained slurry after neutralization.
  • the post-neutralization slurry is sent from the neutralization reaction tank to the solid-liquid separator.
  • a flocculant is added in the feed line, and the neutralized slurry which has passed through the feed line is subjected to solid-liquid separation.
  • the neutralization treatment such that the pH of the obtained solution after neutralization is in a relatively high range, specifically in the range of about 3.2 to 3.5.
  • the deterioration of the solid-liquid separation property of the obtained slurry after neutralization can be prevented.
  • the pH of the obtained solution after neutralization can be set in the range of about 3.2 or more and 3.5 or less, it is possible to dissolve the hydrogen sulfide gas and the like added in the sulfurization treatment using the solution after neutralization as the initial solution. The amount can be increased, the sulfurization reaction efficiency can be improved, and nickel can be recovered with a high recovery rate.
  • FIG. 2 is a figure which shows an example of a structure of the neutralization process plant used at neutralization process S2.
  • the neutralization processing plant 10 includes a neutralization reaction tank 11 that performs neutralization processing based on the neutralization reaction, and a solid-liquid separation device 12 that separates the obtained post-neutralization slurry into a post-neutralization solution and neutralization sediment. And have.
  • the neutralization reaction tank 11 and the solid-liquid separation device 12 are connected by the liquid feed line 13, and the slurry after neutralization generated in the neutralization reaction tank 11 is the liquid feed line 13. It passes through and is charged into the solid-liquid separator 12.
  • the neutralization reaction vessel 11 is, for example, a cylindrical vessel, and the leachate obtained through the leaching step S1 is charged into the vessel, and a neutralizing agent for neutralization treatment is added to the neutralization reaction vessel 11.
  • a stirring apparatus is installed in the neutralization reaction tank 11, and causes the neutralization reaction to occur while stirring the leachate charged in the tank.
  • FIG. 2 the example of the stirring apparatus provided with the stirring shaft 11a and the stirring blade 11b is shown.
  • a liquid feed line 13 is connected to the neutralization reaction tank 11, and the neutralized slurry generated in the tank is transferred to the solid-liquid separator 12 through the liquid feed line 13.
  • the solid-liquid separator 12 is, for example, a device such as a thickener.
  • the solid-liquid separator 12 is charged with a slurry after neutralization reaction (slurry after neutralization) generated by the neutralization reaction in the neutralization reaction tank 11, and the slurry is neutralized to be a mother liquor for nickel recovery.
  • the solution is separated into a post-liquid and a neutralized precipitate slurry consisting of impurity components.
  • the solid-liquid separation device 12 overflows and transfers the post-neutralization solution separated from the neutralization precipitate by the solid-liquid separation and the feed well portion 12 a to which the slurry after neutralization, which is the solid-liquid separation target, is supplied And 12 b.
  • the other end of the liquid feed line 13 connected to the neutralization reaction tank 11 is connected to the feed well 12a, and the neutralized slurry transferred from the neutralization reaction tank 11 is solidified via the feed well 12a. It is charged into the liquid separation device 12.
  • the liquid phase (phase of the solution after neutralization) is on the top and the phase of the solid phase (neutralization slurry is on the bottom) by solid-liquid separation processing. ) Is formed, and the neutralization final solution constituting the liquid phase overflows and is transferred to, for example, an attached reservoir etc., while the neutralization precipitate slurry constituting the solid phase is the bottom of the solid-liquid separator 12 Taken from
  • the neutralized sediment slurry extracted from the bottom portion is transferred by the transfer pump 12c, and appropriately repeated in a predetermined reaction tank or the like in the system.
  • the liquid transfer line 13 is a liquid transfer line connecting the neutralization reaction tank 11 and the solid-liquid separator 12 in the neutralization processing plant 10, and the slurry after neutralization generated in the neutralization reaction tank 11 is solid-liquid The liquid is sent to the separation device 12.
  • the liquid transfer line 13 is constituted by a weir, piping and the like.
  • the liquid feed line 13 connects, for example, the neutralization reaction tank 11 located on the upper side at the position in the height direction, and the solid-liquid separation device 12 located on the lower side, and is installed in an inclined state due to the difference in height position. It is done. Therefore, the post-neutralization slurry transferred from the neutralization reaction tank 11 is sent to flow downstream along the inclined liquid feed line 13.
  • the liquid feed line 13 is connected to the feedwell portion 12a of the solid-liquid separator 12, and the neutralized slurry is charged into the solid-liquid separator 12 through the feedwell portion 12a.
  • a flocculant is added in the liquid feeding line 13 for feeding the slurry after neutralization from the neutralization reaction tank 11 to the solid-liquid separator 12.
  • the slurry which has passed through the liquid feed line 13 is separated into solid and liquid.
  • a chemical agent such as a coagulant and a coagulant made of a polymer is added.
  • a coagulant and a coagulant are added to the inside of the neutralization reaction tank 11 and to the feed well portion 12a of the solid-liquid separator 12, and the neutralization treatment and solid-liquid separation are performed while stirring. I was processing.
  • coagulants and coagulants made of high-molecular polymers have the property of capturing fine particles by their functional groups, it is advantageous to lower the drug concentration from the viewpoint of polymer dispersibility, and also high-molecular An aggregate substance formed by combining the polymer and the fine particles is easily destroyed by physical force by a stirring device or the like.
  • the generated aggregate substance is hard to be destroyed since it is not affected by the power of the stirring device, and the solid-liquid separation property is improved. It can be enhanced.
  • the coagulant When a coagulant is added in the liquid feed line 13, the coagulant is added to the neutralized slurry which passes through the liquid feed line 13 at a stage where the slurry is fed after neutralization in the liquid feed line 13. Can be added. Alternatively, a predetermined amount of coagulant is placed on the liquid feed line 13 before the slurry passes through the liquid feed line 13 after neutralization, and thereafter, on the liquid feed line 13 on which the coagulant is placed. The slurry may pass after neutralization.
  • the addition position of the coagulant in the liquid delivery line 13 is not particularly limited as long as it is on the liquid delivery line 13, but it is relatively upstream from the viewpoint of effectively producing an aggregate substance in the liquid delivery line 13. It is preferable to add on the side (the side of the neutralization reaction tank 11). In addition, a coagulant may be added in multiple stages on the liquid feed line 13.
  • the coagulant is not particularly limited, and cationic coagulants, non-ionic coagulants, nonionic coagulants, amphoteric coagulants and the like can be used. Among them, it is preferable to use a cationic coagulant from the viewpoint of further enhancing the solid-liquid separation property of the slurry after neutralization. Moreover, it is preferable to use a polymer flocculant from the viewpoint of being excellent in cohesiveness.
  • cationic flocculants include polymer flocculants such as polyaminoalkyl methacrylate, polyethylene imine, halogenated polydiallyl ammonium, chitosan, urea-formalin resin and the like.
  • anionic flocculant include sodium polyacrylate, partially hydrolyzed polyacrylamide, partially sulfomethylated polyacrylamide, poly (2-acrylamido) -2-methylpropane sulfate and the like.
  • flocculant a polyacrylamide, a polyethylene oxide etc. are mentioned, for example.
  • flocculant the copolymer etc. of acrylamide, an aminoalkyl methacrylate, and sodium acrylate are mentioned, for example.
  • the addition amount of the coagulant is not particularly limited, and it is preferable to adjust appropriately according to the solid content contained in the slurry after neutralization, for example, 1 m 3 of the slurry after neutralization passing through the liquid feeding line 13 Therefore, it is preferable to set it to about 0.3 L to 1.0 L, and more preferable to set it to about 0.4 L to 0.7 L.
  • a coagulant can be added together with the coagulant in the liquid feed line 13.
  • a coagulant a cationic coagulant, an anionic coagulant, a nonionic coagulant, an amphoteric coagulant etc. can be used.
  • polydiallyldimethyl ammonium chloride which is a cationic coagulant can be used. Even when a coagulant is added, the addition of the coagulant is performed in the liquid feed line 13.
  • the solid-liquid separation property of the slurry after neutralization can be further enhanced by using the coagulant and the coagulant in combination and adding them in the liquid feed line 13.
  • the reaction efficiency in the sulfidation treatment depends on the amount of the sulfiding agent dissolved in the solution after neutralization.
  • the sulfurization reaction proceeds more efficiently, and nickel etc. in the solution after neutralization are effectively sulfided. can do.
  • the amount of sulfurizing agent that can be dissolved depends on the pH of the solution after neutralization.
  • the neutralization treatment can be performed such that the pH of the solution after neutralization is in the range of 3.2 or more and 3.5 or less. Even if it is, it can prevent effectively that the solid-liquid separation property of the slurry after neutralization deteriorates. That is, in the present embodiment, an aggregating agent is added in the liquid feeding line 13 for feeding the slurry after neutralization from the neutralization reaction tank 11 to the solid-liquid separator 12 and after the neutralization passing through the liquid feeding line 13 Since the slurry is subjected to solid-liquid separation, the solid content is efficiently aggregated and separated even if it is a post-neutralization slurry containing a post-neutralization solution having a pH of 3.2 or more and 3.5 or less. It is possible to obtain a post-neutralization solution with low turbidity.
  • the numerical value measured by a turbidimeter (for example, a 2100P type scattered light turbidimeter manufactured by HACH) Can be less than 50 NTU.
  • the recovery rate of nickel and cobalt recovered by the sulfidation treatment is correlated with the turbidity of the post-neutralization solution which is the starting solution of the sulfidation reaction. From this, the recovery of nickel and cobalt can be managed by the turbidity of the solution after neutralization (sulfurization reaction start solution). The lower the turbidity of the sulfurization reaction start solution (the higher the transparency), the more the aggregation of the solid proceeds and the more the adhesion water is washed. And since it is such a sulfurization reaction starting solution, nickel can be collect
  • the solid content can be efficiently aggregated and separated, it is possible to obtain a post-neutralization solution with low turbidity, and a high recovery rate. Nickel can be recovered.
  • Comparative Example 1 Conventional Method In the wet smelting process of nickel oxide ore, neutralization treatment was carried out using a leaching solution obtained by subjecting nickel oxide ore to leaching treatment with sulfuric acid using a neutralization treatment plant 10 as shown in FIG. .
  • the neutralization processing plant 10 includes a neutralization reaction tank 11 for neutralizing the leachate, and a solid-liquid separator 12 for solid-liquid separation of the neutralized slurry into a post-neutralization solution and a neutralized precipitate.
  • calcium carbonate was used as a neutralizing agent.
  • Comparative Example 1 a cationic coagulant was added to the neutralization reaction tank 11, and a nonionic coagulant was added to the feedwell portion 12a of the solid-liquid separator (thickener) 12.
  • Example 1 In Example 1, the cationic coagulant and the nonionic coagulant are added to the liquid feeding line 13 for feeding the slurry after neutralization from the neutralization reaction tank 11 to the solid-liquid separator 12. , And treated in the same manner as in Comparative Example 1. Specifically, arrow P in FIG. 2 is the addition position of the cationic coagulant and the nonionic coagulant.
  • the turbidity of the supernatant liquid of the solid-liquid separator 12 was measured using a turbidimeter and was 37 NTU, which was slightly higher than that of Comparative Example 1, but the pH of the solution after neutralization was 3.27 It was possible to raise it.
  • Example 2 In Example 2, the cationic flocculant is added to the feed line 13 (the position of the arrow P in FIG. 2) in the same manner as in Example 1 except that the drug used is changed to only the cationic flocculant. It was made to do.
  • Comparative Example 2 was the same as Comparative Example 1 except that the pH of the post-neutralization solution obtained in the neutralization treatment in the neutralization reaction tank 11 was 3.31. That is, a cationic coagulant was added to the neutralization reaction tank 11, and a nonionic coagulant was added to the feed well portion 12 a of the solid-liquid separator 12.
  • Comparative Example 3 Comparative Example 3 was the same as Example 2 except that the addition position of the cationic coagulant was changed to the inside of the neutralization reaction tank 11 and the inside of the solid-liquid separator 12. No flocculant was added to the liquid delivery line 13.

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Abstract

L'invention concerne un procédé de métallurgie par voie humide pour un minerai d'oxyde de nickel, le procédé permettant d'augmenter efficacement le pH d'un liquide de traitement et permettant de faciliter efficacement une réaction de sulfuration utilisant le liquide de traitement sans provoquer de détérioration des propriétés de séparation solide-liquide d'une bouillie après une réaction de neutralisation d'un lixiviat. Ce procédé de métallurgie par voie humide pour un minerai d'oxyde de nickel consiste à soumettre un lixiviat, qui est obtenu par lixiviation d'un minerai d'oxyde de nickel par addition d'acide sulfurique, à un traitement de neutralisation dans un bac de réaction de neutralisation (11), à soumettre la bouillie neutralisée à une séparation solide-liquide dans un appareil de séparation solide-liquide (12) de manière à obtenir un liquide neutralisé et à soumettre le liquide neutralisé à un traitement de sulfuration de manière à séparer et récupérer du nickel et du cobalt. Un coagulant est ajouté à une conduite d'alimentation en liquide (13) qui alimente l'appareil de séparation solide-liquide (12) en la bouillie neutralisée provenant du bac de réaction de neutralisation (11) et la bouillie neutralisée qui est passée dans la conduite d'alimentation en liquide (13) est soumise à une séparation solide-liquide.
PCT/JP2018/029778 2017-09-11 2018-08-08 Procédé de métallurgie par voie humide pour du minerai d'oxyde de nickel Ceased WO2019049593A1 (fr)

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JP2017174034A JP6551481B2 (ja) 2017-09-11 2017-09-11 ニッケル酸化鉱石の湿式製錬方法

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JP7183503B2 (ja) * 2018-08-30 2022-12-06 住友金属鉱山株式会社 高濃度鉱石スラリーの製造方法
JP7115170B2 (ja) * 2018-09-12 2022-08-09 住友金属鉱山株式会社 ニッケル酸化鉱石の処理方法及び該処理方法を含んだニッケルコバルト混合硫化物の製造方法

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