WO2016157629A1 - ニッケル及びコバルトの混合硫化物の製造方法、ニッケル酸化鉱石の湿式製錬方法 - Google Patents
ニッケル及びコバルトの混合硫化物の製造方法、ニッケル酸化鉱石の湿式製錬方法 Download PDFInfo
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- WO2016157629A1 WO2016157629A1 PCT/JP2015/084427 JP2015084427W WO2016157629A1 WO 2016157629 A1 WO2016157629 A1 WO 2016157629A1 JP 2015084427 W JP2015084427 W JP 2015084427W WO 2016157629 A1 WO2016157629 A1 WO 2016157629A1
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/16—Hydrogen sulfides
- C01B17/165—Preparation from sulfides, oxysulfides or polysulfides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D13/00—Compounds of sodium or potassium not provided for elsewhere
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G53/00—Compounds of nickel
- C01G53/006—Compounds containing, besides nickel, two or more other elements, with the exception of oxygen or hydrogen
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- 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
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- 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
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- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Definitions
- the present invention relates to a method for producing a mixed sulfide of nickel and cobalt, and more specifically, a method for producing a mixed sulfide of nickel and cobalt by a sulfidation reaction from an acidic sulfuric acid solution containing nickel and cobalt, and sulfiding the method.
- the present invention relates to a method for hydrometallizing nickel oxide ore applied to a process.
- a leaching solution containing nickel and cobalt is used as a sulfidation reaction starter to cause a sulfidation reaction under pressure, and mixing of nickel and cobalt while separating impurities Processing to produce sulfides is performed.
- a sulfurization reaction under pressure in particular, separation of zinc, copper and the like is possible, and it has been put into practical use.
- the nickel ions in the end solution increase as the iron concentration increases. That is, it means that the nickel recovery rate decreases as the iron concentration increases. Since the iron concentration in the sulfidation reaction start liquid depends on the operating parameters of the process prior to the sulfidation process in the hydrometallurgical method of nickel oxide ore, the iron concentration in the start liquid at the start of the sulfidation process is not constant. , "The state is scattered". Therefore, in this sulfidation step, in order to suppress a decrease in nickel recovery rate, it is required to cope with the “variation state” of the iron concentration in the sulfidation reaction starting solution.
- Patent Document 1 an alkali sulfide is added to an acidic aqueous solution containing nickel and / or cobalt to precipitate and recover nickel and / or cobalt sulfide.
- the S / (Ni + Co) molar ratio uses hydrogen sulfide.
- a method for recovering sulfide precipitates which is controlled to a value close to 1 which is the stoichiometric composition of NiS and CoS, which is 1.05 or less of the amount of sulfides produced in this manner.
- alkali sulfide is added to the aqueous solution, and the sulfide is removed while maintaining the oxidation-reduction potential (Ag / AgCl electrode standard) at ⁇ 300 mV to 100 mV.
- a method for precipitation is disclosed.
- An object of the present invention is to provide a method for producing a mixed sulfide of nickel and cobalt, which can stabilize the concentration of nickel and cobalt in the sulfidation reaction final solution at a low level and can suppress a decrease in the recovery rate of nickel and cobalt.
- the present inventors have made extensive studies to solve the above-described problems. As a result, hydrogen sulfide gas was blown into the sulfuric acid acidic solution containing nickel and cobalt containing iron at a rate of 1.0 to 4.0 g / L, and the exhaust gas containing hydrogen sulfide gas generated by the sulfurization reaction was discharged.
- a sodium hydrogen sulfide (NaHS) solution obtained by absorption in an alkaline solution to cause a sulfurization reaction, the concentration of nickel and cobalt in the sulfurization reaction final solution is stabilized at a low level.
- NaHS sodium hydrogen sulfide
- the inventors have found that a reduction in recovery rate can be suppressed, and have completed the present invention. That is, the present invention provides the following.
- the first aspect of the present invention is a method for producing a mixed sulfide of nickel and cobalt by causing a sulfurization reaction by blowing hydrogen sulfide gas into a sulfuric acid acidic solution containing nickel and cobalt, wherein the sulfuric acid
- the acidic solution contains iron at a rate of 1.0 to 4.0 g / L, and the hydrogen sulfide gas is blown into the sulfuric acid acidic solution and exhaust gas containing the hydrogen sulfide gas generated by the sulfidation reaction.
- the second invention of the present invention is characterized in that, in the first invention, the addition amount of the sodium hydrogen sulfide is an amount equal to or more than an equivalent amount necessary for sulfurization of the iron contained in the sulfuric acid acidic solution. And producing a mixed sulfide of nickel and cobalt.
- the third invention of the present invention is the first or second invention, wherein the sodium hydrogen sulfide is added in an amount of 20 to 35 mass% of the solution containing the sodium hydrogen sulfide in the sulfuric acid acidity.
- a method for producing a mixed sulfide of nickel and cobalt characterized in that a proportion of 1.7 ⁇ 3.8m 3 / H to a solution 1000 m 3 / H.
- the amount of the hydrogen sulfide gas blown is necessary for sulfiding nickel and cobalt contained in the sulfuric acid acidic solution.
- This is a method for producing a mixed sulfide of nickel and cobalt, characterized in that the amount is 1.5 to 2.5 times the theoretical equivalent.
- a fifth invention of the present invention is the method for producing a mixed sulfide of nickel and cobalt according to any one of the first to fourth inventions, wherein the alkaline solution is a sodium hydroxide solution. is there.
- the sixth invention of the present invention is a nickel oxide ore which performs a leaching treatment using sulfuric acid on nickel oxide ore and produces a mixed sulfide of nickel and cobalt from the obtained leachate containing nickel and cobalt.
- the method includes a sulfurization step in which a sulfide reaction is caused by blowing hydrogen sulfide gas into the leachate to obtain a mixed sulfide of nickel and cobalt, and the leachate is 1.0 to 4.0 g / L.
- hydrogen sulfide gas obtained by blowing the hydrogen sulfide gas into the leachate and absorbing exhaust gas containing hydrogen sulfide gas generated by the sulfidation reaction in an alkaline solution is contained in the sulfiding step.
- the nickel and cobalt concentrations in the sulfurization reaction final solution are stabilized at a low level without increasing the cost, even when the sulfurization reaction initial solution having a high iron concentration is processed. And the fall of the recovery rate of cobalt can be suppressed.
- the method for producing a mixed sulfide of nickel and cobalt is a method for obtaining a mixed sulfide of nickel and cobalt by causing a sulfurization reaction by blowing hydrogen sulfide gas into a sulfuric acid acidic solution containing nickel and cobalt.
- the mixed sulfide refers to a mixture of nickel sulfide and cobalt sulfide.
- the mixed sulfide of nickel and cobalt is also simply referred to as “mixed sulfide”.
- this mixed sulfide manufacturing method is a solution in which an acidic sulfuric acid solution containing nickel and cobalt as a sulfurization reaction starting solution contains iron at a rate of 1.0 to 4.0 g / L, Sodium hydrogen sulfide (NaHS) obtained by injecting hydrogen sulfide (H 2 S) gas as a sulfiding agent into the sulfuric acid acidic solution and absorbing exhaust gas containing hydrogen sulfide gas generated by the sulfidation reaction in an alkaline solution Is added to cause a sulfurization reaction.
- NaHS Sodium hydrogen sulfide
- This mixed sulfide production method can be applied, for example, to a treatment in a sulfidation process in a wet smelting method of nickel oxide ore as described later.
- a sulfuric acid acidic solution containing nickel and cobalt a leachate obtained by subjecting nickel oxide ore to a leaching treatment using sulfuric acid can be used.
- a neutralized final solution obtained by neutralizing a leachate obtained through the leaching treatment with a neutralizer may be used.
- the nickel oxide ore contains iron, and the leachate obtained by leaching the nickel oxide ore could not be fixed as hematite (Fe 2 O 3 ) during the leaching process. Iron is included as an impurity element. Moreover, since the root of the plant is mixed in the nickel oxide ore used as a raw material, if the carbon (C) grade in the nickel oxide ore exceeds 0.2%, the ORP of the leachate obtained by the leaching process is lowered. As a result, iron is leached and the iron concentration in the leachate exceeds 1.0 g / L. In addition, even if this iron is neutralized with respect to the leachate, it is difficult to separate compared with other impurity elements. Therefore, even in the neutralized final solution obtained by performing neutralization, the iron has a predetermined concentration. Included.
- FIG. 1 is a graph showing the relationship between the pH of a solution and the solubility of various metal sulfides. From the graph of FIG. 1, it can be seen that the solubility of nickel sulfide (NiS) and cobalt sulfide (CoS) depends on pH. Therefore, the higher the pH is, the sulfide form is maintained in the final sulfurization reaction solution, and the concentration of nickel ions and cobalt ions decreases. That is, the recovery rate as a mixed sulfide of nickel and cobalt is improved.
- NiS nickel sulfide
- CoS cobalt sulfide
- FIG. 2 is a graph showing the relationship between the iron concentration in the sulfurization reaction start solution and the nickel concentration in the sulfurization reaction end solution. As shown in FIG. 2, the higher the iron concentration in the sulfurization reaction start solution, the lower the pH of the solution as described above to promote NiS redissolution, and as a result, in the sulfurization reaction final solution. It can be clearly seen that the nickel concentration tends to increase.
- a sulfurization reaction is performed on a sulfuric acid acidic solution containing nickel and cobalt and containing iron at a concentration of 1.0 to 4.0 g / L.
- a predetermined amount of hydrogen sulfide gas is blown in, an exhaust gas containing hydrogen sulfide gas generated by the sulfurization reaction is alkali-treated, and a solution containing sodium hydrogen sulfide obtained by the alkali treatment ( Hereinafter, it is also referred to as “NaHS solution”) to cause a sulfurization reaction.
- the reaction shown in the following reaction formulas (ii) and (iii) proceeds by adding the NaHS solution obtained by alkali treatment of the exhaust gas generated by the sulfidation reaction to the sulfidation reaction starting solution.
- the acid produced in the reaction shown in i) is neutralized.
- the fall of pH of a solution is suppressed, the density
- the sulfurization reaction can be promoted based on the reaction formula (iii), and the utilization efficiency of the hydrogen sulfide gas can be improved by reusing the excessively added hydrogen sulfide gas as described later. .
- the necessary theory is obtained in order to obtain a desired recovery rate and to use the surplus as exhaust gas for alkali treatment.
- An excess of 1.5 to 2.5 times the equivalent is added.
- the present embodiment is characterized in that NaHS is generated by subjecting excess hydrogen sulfide gas to alkali treatment, a solution containing the NaHS is recovered, and repeatedly added in the sulfurization reaction.
- FIG. 3 schematically shows a flow in which surplus hydrogen sulfide gas is recovered and subjected to detoxification treatment with an alkaline solution (hereinafter simply referred to as “alkali treatment”), and the obtained NaHS solution is supplied to the sulfurization reaction.
- alkali treatment an alkaline solution
- FIG. 3 shows a flow in which surplus hydrogen sulfide gas is recovered and subjected to detoxification treatment with an alkaline solution (hereinafter simply referred to as “alkali treatment”), and the obtained NaHS solution is supplied to the sulfurization reaction.
- alkali treatment an alkaline solution
- the NaHS solution 13 obtained in this way is added to the sulfurization reaction starting liquid 10 charged in the sulfurization reaction tank 1 using a pump or the like. It is characterized by.
- the repeatedly added NaHS solution is also used for the sulfurization reaction, and the decrease in pH in the reaction system accompanying the sulfurization reaction is suppressed.
- the re-dissolution of the produced NiS and CoS is reduced, and even when the sulfurization reaction initial solution 10 having a high iron concentration is processed, the nickel concentration in the resulting sulfurization reaction final solution 14 is stabilized at a low level. Can do.
- the system for adding the NaHS solution obtained by alkali treatment of the hydrogen sulfide gas discharged from the sulfidation reaction tank to the sulfidation reaction starting solution is not particularly limited, but as described above, a circulation system as shown in FIG. be able to. That is, the exhaust gas 12 containing the surplus hydrogen sulfide gas 11a is used as the NaHS solution 13 in the H 2 S gas cleaning tower 2 in which the alkali solution is circulated, and the obtained NaHS solution 13 is discharged into the sulfurization reaction tank.
- the system can be repeated to 1.
- a detoxifying facility such as a scrubber in order to efficiently contact the alkali solution and the hydrogen sulfide gas.
- the alkali solution used for alkali treatment in H 2 S gas washing tower 2 is not particularly limited, industrially has high alkali strength, it is preferable to handle using easy sodium hydroxide (NaOH) solution as a solution.
- the concentration of the sodium hydroxide solution is preferably about 20 to 30% by mass. If the concentration of sodium hydroxide is less than 20%, the concentration decreases and the amount of sodium hydroxide solution increases. On the other hand, if the concentration exceeds 30%, unreacted sodium hydroxide may remain.
- the NaHS solution obtained by this alkali treatment is, for example, a 20 to 35% by mass NaHS solution.
- this NaHS solution is repeatedly added to the sulfidation reaction vessel to cause a sulfidation reaction.
- the amount of addition is sulfuric acid containing nickel and cobalt which are the sulfidation reaction starting liquid. it is preferably added in an amount of about 1.7 ⁇ 3.8m 3 / H to acidic solution 1000 m 3 / H.
- Amount of NaHS is less than 1.7 m 3 / H with respect to sulfuric acid solution 1000 m 3 / H, increase the effect of pH is the desired effect, the effect of suppressing pH decrease sufficiently obtained in other words There is no possibility.
- the sulfuric acid acidic solution exceeds 3.8 m 3 / H with respect to 1000 m 3 / H, not only the recovery rate of nickel or cobalt is increased, but also the mixing of Fe into the product is promoted due to excessive increase in pH. This is not preferable.
- a sulfuric acid acidic solution containing nickel and cobalt is used as a sulfurization reaction starting solution, and hydrogen sulfide gas and a NaHS solution obtained by alkali treatment are added to this solution. This causes a sulfurization reaction.
- the sulfuric acid acidic solution containing nickel and cobalt for example, a leachate obtained by leaching nickel oxide ore with sulfuric acid can be used. And a mixed sulfide of cobalt.
- the mixed sulfide manufacturing method according to the present embodiment can be applied to a sulfiding step in a hydrometallurgical method for recovering nickel from nickel oxide ore.
- FIG. 4 is a process diagram showing an example of the flow of a method for hydrometallizing nickel oxide ore.
- the hydrometallurgical method of nickel oxide ore is a leaching step S1 in which sulfuric acid is added to a raw material nickel oxide ore slurry and leaching is performed under high temperature and high pressure, and the residue is separated from the leached slurry.
- Leaching step S1 sulfuric acid is added to a slurry of nickel oxide ore (hereinafter also referred to as “ore slurry”) using a high-temperature pressure reaction tank such as an autoclave, and the pressure is about 230 to 270 ° C.
- the mixture is stirred under a condition of about 3 to 5 MPa to produce a leaching slurry comprising a leaching solution and a leaching residue.
- Nickel oxide ores 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 weight and is contained as a hydroxide or magnesium silicate mineral.
- the iron content is 10 to 50% by weight and is mainly in the form of a trivalent hydroxide, but a part of the divalent iron is contained in the siliceous clay.
- oxide ores containing valuable metals such as nickel, cobalt, manganese, and copper, such as manganese nodules existing in the deep sea floor, can be used.
- the leaching process in the leaching step S1 for example, a leaching reaction represented by the following formulas (a) to (e) and a high-temperature thermal hydrolysis reaction occur, leaching as sulfates such as nickel and cobalt, and leached iron sulfate. Is fixed as hematite. However, since the immobilization of iron ions does not proceed completely, the leaching slurry obtained usually contains divalent and trivalent iron ions in addition to nickel, cobalt and the like.
- the pH of the obtained leachate is 0.1 to 1.0 from the viewpoint of the filterability of the leaching residue containing hematite produced in the subsequent solid-liquid separation step S2. It is preferable to adjust.
- the amount of sulfuric acid added to the autoclave charged with the ore slurry is not particularly limited, but an excessive amount such that iron in the ore is leached is used.
- an excessive amount such that iron in the ore is leached is used.
- a solid-liquid separation process is performed using a solid-liquid separation apparatus such as a thickener.
- the leaching slurry is first diluted with a cleaning liquid, and then the leaching residue in the leaching slurry is concentrated as a thickener sediment.
- the nickel part adhering to a leaching residue can be reduced according to the dilution degree.
- the recovery rate of nickel can be improved by using thickeners having such functions connected in multiple stages.
- Neutralization step S3 a neutralizing agent such as magnesium oxide or calcium carbonate is added so that the pH becomes 4 or less while suppressing oxidation of the leachate, and trivalent iron is contained.
- a Japanese starch slurry and a neutralized final solution which is a mother liquor for nickel recovery are obtained.
- the pH of the resulting neutralized final solution is adjusted to 4 or less, preferably 3.0 to 3.5, more preferably 3.1 to 3.2 while suppressing oxidation of the separated leachate.
- a neutralizing agent such as calcium carbonate is added to the leachate to form a neutralized final solution that becomes a mother liquor for nickel and cobalt recovery, and a neutralized starch slurry that contains trivalent iron as an impurity element. To do.
- the neutralization step S3 by performing the neutralization treatment on the leachate in this way, the excess acid used in the leaching treatment by the HPAL method is neutralized to form a neutralized final solution, and also remains in the solution 3 Impurities such as valent iron ions and aluminum ions are removed as neutralized starch.
- the neutralized final solution is a solution based on a leaching solution obtained by leaching the raw material nickel oxide ore with sulfuric acid in the leaching step S1, and is a sulfuric acid acidic solution containing nickel. is there.
- This neutralized final solution is a reaction start solution for the sulfurization reaction in the sulfurization step S4 described later, and has a nickel concentration in the range of about 0.5 to 5.0 g / L.
- the neutralized final solution contains cobalt as a valuable metal in addition to nickel.
- iron, manganese, magnesium, aluminum, chromium, lead, etc. may be contained. Specifically, iron is contained at a rate of 1.0 to 4.0 g / L.
- a neutralization final solution which is a mother liquor for nickel and cobalt recovery is used as a sulfidation reaction start solution, and a sulfidation reaction is caused by blowing hydrogen sulfide gas as a sulfiding agent into the sulfidation reaction start solution.
- a mixed sulfide of nickel and cobalt with a small amount of components and a sulfurization reaction final solution which is a poor solution in which the concentrations of nickel and cobalt are stabilized at a low level are generated.
- the sulfidation treatment in the sulfidation step S4 can be performed using a sulfidation reaction tank or the like, and hydrogen sulfide gas is blown into the gas phase portion in the reaction tank with respect to the sulfidation reaction starting liquid introduced into the sulfidation reaction tank.
- a sulfurization reaction is caused by dissolving hydrogen sulfide gas therein.
- the obtained slurry containing mixed sulfide of nickel and cobalt is charged into a settling separator such as thickener and subjected to settling separation, and only the mixed sulfide is separated from the bottom of the thickener. to recover.
- the aqueous solution component overflows from the upper part of the thickener and is recovered as a poor solution.
- hydrogen sulfide gas is blown into the neutralized final solution that is an acidic solution containing nickel and cobalt and that has an iron concentration of 1.0 to 4.0 g / L.
- a solution of NaHS obtained by absorbing an exhaust gas containing hydrogen sulfide gas generated by the sulfurization reaction into an alkaline solution is added to cause a sulfurization reaction.
- nickel is used as the hydrogen sulfide gas.
- An excess amount of 1.5 to 2.5 times the theoretical equivalent required for sulfurization treatment of cobalt and cobalt is blown, and excess hydrogen sulfide gas that has not been used for the sulfurization reaction is brought into contact with an alkaline solution by alkali treatment to form NaHS. Become.
- the solution containing NaHS obtained by alkali treatment of excess hydrogen sulfide gas in this way is repeatedly used for the sulfurization reaction.
- Example 1 A sulfuric acid acidic solution having a nickel concentration of 1.0 to 3.0 g / L, a cobalt concentration of 1.0 to 3.0 g / L, and an iron concentration of 1.0 to 2.0 g / L is used as a sulfurization reaction starting solution. Then, it was charged into a sulfurization reactor, and a sulfurization reaction was caused while blowing hydrogen sulfide gas.
- the amount of hydrogen sulfide gas blown was 0.30 to 0.85 Nm 3 / kg ⁇ Ni, and a solution containing sodium hydrogen sulfide (NaHS) was added to the sulfuric acid acidic solution.
- Amount of NaHS solution was a ratio of 1.7 ⁇ 3.8m 3 / H with respect to sulfuric acid solution 1000 m 3 / H.
- This NaHS was obtained by bringing an exhaust gas containing excess hydrogen sulfide gas generated by the sulfidation reaction into contact with a sodium hydroxide solution, and this was repeatedly added to the sulfuric acid acidic solution in the sulfidation reaction tank.
- mixed sulfides were obtained in which nickel and cobalt in the sulfuric acid acidic solution, which is a sulfurization reaction starting solution, were respectively sulfides.
- the obtained mixed sulfide was separated from the aqueous solution component by sedimentation treatment using a thickener, and then the nickel concentration in the sulfurization reaction final solution as the aqueous solution component was analyzed.
- the nickel concentration in the sulfurization reaction final solution was less than 0.10 g / L, and could be stabilized at a low level.
- Example 1 As in Example 1, a sulfuric acid acidic solution containing nickel and cobalt and containing iron at a rate of 1.0 to 2.0 g / L was used as a sulfurization reaction starting solution to cause a sulfurization reaction.
- Comparative Example 1 with blowing hydrogen sulfide gas was added at a ratio of 1.0 ⁇ 1.5m 3 / H the NaHS solution in an acidic sulfuric acid solution relative to the sulfuric acid solution 1000 m 3 / H.
- this NaHS used what was obtained by making the waste gas containing the surplus hydrogen sulfide gas produced by the sulfurization reaction contact with a sodium hydroxide solution.
- mixed sulfides were obtained in which nickel and cobalt in the sulfuric acid acidic solution, which is a sulfurization reaction starting solution, were respectively sulfides.
- the obtained mixed sulfide was separated from the aqueous solution component by sedimentation treatment using a thickener, and then the nickel concentration in the sulfurization reaction final solution as the aqueous solution component was analyzed.
- the nickel concentration in the sulfurization reaction final solution exceeded 0.10 g / L, and the nickel concentration became high. This is considered to be because the decrease in pH of the solution could not be suppressed, and the re-dissolution of the produced NiS was promoted.
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Abstract
Description
H2S+NiSO4→H2SO4+NiS ・・(i)
H2S+FeSO4→H2SO4+FeS ・・(ii)
本実施の形態に係るニッケル及びコバルトの混合硫化物の製造方法は、ニッケル及びコバルトを含む硫酸酸性溶液に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てニッケル及びコバルトの混合硫化物を得る方法である。ここで、混合硫化物とは、ニッケル硫化物とコバルト硫化物の混合物をいう。以下では、ニッケル及びコバルトの混合硫化物を、単に「混合硫化物」ともいう。
H2S+NiSO4⇔H2SO4+NiS ・・(i)
2NaHS+H2SO4→Na2SO4+2H2S ・・(ii)
2NaHS+NiSO4
→Na2SO4+NiS+H2S ・・(iii)
NaOH+H2S→NaHS+H2O ・・(iv)
本実施の形態に係る混合硫化物の製造方法では、硫化反応始液としてニッケル及びコバルトを含む硫酸酸性溶液を用い、この溶液に対して硫化水素ガス及びアルカリ処理により得られたNaHS溶液を添加して硫化反応を生じさせる。ここで、ニッケル及びコバルトを含む硫酸酸性溶液としては、例えば、ニッケル酸化鉱石に対して硫酸により浸出処理を施して得られる浸出液を用いることができ、その浸出液に対して硫化反応を生じさせてニッケル及びコバルトの混合硫化物を得る。
図4は、ニッケル酸化鉱石の湿式製錬方法の流れの一例を示した工程図である。図4に示すように、ニッケル酸化鉱石の湿式製錬方法は、原料のニッケル酸化鉱石のスラリーに硫酸を添加して高温高圧下で浸出処理を施す浸出工程S1と、浸出スラリーから残渣を分離してニッケル及びコバルトを含む浸出液を得る固液分離工程S2と、浸出液のpHを調整して浸出液中の不純物元素を中和澱物スラリーとして分離して中和終液を得る中和工程S3と、中和終液に硫化剤としての硫化水素ガスを添加することでニッケル及びコバルトの混合硫化物を生成させる硫化工程S4とを有する。
浸出工程S1では、オートクレーブ等の高温加圧反応槽を用い、ニッケル酸化鉱石のスラリー(以下、「鉱石スラリー」ともいう)に硫酸を添加して温度230~270℃程度、圧力3~5MPa程度の条件下で攪拌し、浸出液と浸出残渣とからなる浸出スラリーを生成する。
MO+H2SO4⇒MSO4+H2O ・・(a)
(なお、式中Mは、Ni、Co、Fe、Zn、Cu、Mg、Cr、Mn等を表す)
2Fe(OH)3+3H2SO4⇒Fe2(SO4)3+6H2O ・・(b)
FeO+H2SO4⇒FeSO4+H2O ・・(c)
・高温熱加水分解反応
2FeSO4+H2SO4+1/2O2⇒Fe2(SO4)3+H2O・・(d)
Fe2(SO4)3+3H2O⇒Fe2O3+3H2SO4 ・・(e)
固液分離工程S2では、浸出工程S1で生成した浸出スラリーを多段洗浄して、ニッケルやコバルト等の有価金属を含む浸出液と浸出残渣とを得る。
中和工程S3では、浸出液の酸化を抑制しながら、pHが4以下となるように酸化マグネシウムや炭酸カルシウム等の中和剤を添加して、3価の鉄を含む中和澱物スラリーとニッケル回収用母液である中和終液とを得る。
硫化工程S4では、ニッケル及びコバルト回収用母液である中和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、不純物成分の少ないニッケル及びコバルトの混合硫化物と、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である硫化反応終液とを生成させる。
ここで、硫化工程S4での処理、つまりニッケル及びコバルトを含む硫酸酸性溶液である中和終液からニッケル及びコバルトの混合硫化物を生成させる硫化処理においては、その中和終液を硫化反応始液として、上述した混合硫化物の製造方法を適用できる。
ニッケル濃度が1.0~3.0g/L、コバルト濃度が1.0~3.0g/L、鉄濃度が1.0~2.0g/Lである硫酸酸性溶液を硫化反応始液として用いて、それを硫化反応槽に装入し、硫化水素ガスを吹き込みながら硫化反応を生じさせた。
実施例1と同じ、ニッケル及びコバルトを含み、また1.0~2.0g/Lの割合で鉄を含有する硫酸酸性溶液を硫化反応始液として用いて、硫化反応を生じさせた。
2 H2Sガス洗浄塔
10 硫化反応始液
11 硫化水素ガス
11a 余剰の硫化水素ガス
12 排ガス
13 NaHS溶液
14 硫化反応終液
Claims (6)
- ニッケル及びコバルトを含む硫酸酸性溶液に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てニッケル及びコバルトの混合硫化物を得る方法であって、
前記硫酸酸性溶液は、1.0~4.0g/Lの割合で鉄を含有し、
前記硫酸酸性溶液に対して、前記硫化水素ガスを吹き込むとともに、前記硫化反応により生じた硫化水素ガスを含む排ガスをアルカリ溶液に吸収させて得られる硫化水素ナトリウム(NaHS)を添加して硫化反応を生じさせる
ことを特徴とするニッケル及びコバルトの混合硫化物の製造方法。 - 前記硫化水素ナトリウムの添加量は、前記硫酸酸性溶液に含まれる前記鉄の硫化に必要な当量以上の量であることを特徴とする請求項1に記載のニッケル及びコバルトの混合硫化物の製造方法。
- 前記硫化水素ナトリウムの添加量は、該硫化水素ナトリウムを20~35質量%の割合で含む溶液を、前記硫酸酸性溶液1000m3/Hに対して1.7~3.8m3/Hの割合とすることを特徴とする請求項1又は2に記載のニッケル及びコバルトの混合硫化物の製造方法。
- 前記硫化水素ガスの吹き込み量は、前記硫酸酸性溶液に含まれるニッケル及びコバルトを硫化するのに必要な理論当量の1.5~2.5倍の量とすることを特徴とする請求項1乃至3のいずれか1項に記載のニッケル及びコバルトの混合硫化物の製造方法。
- 前記アルカリ溶液は水酸化ナトリウム溶液であることを特徴とする請求項1乃至4のいずれか1項に記載のニッケル及びコバルトの混合硫化物の製造方法。
- ニッケル酸化鉱石に対して硫酸を用いて浸出処理を施し、得られたニッケル及びコバルトを含む浸出液からニッケル及びコバルトの混合硫化物を生成させるニッケル酸化鉱石の湿式製錬方法において、
前記浸出液に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てニッケル及びコバルトの混合硫化物を得る硫化工程を含み、
前記浸出液は、1.0~4.0g/Lの割合で鉄を含有し、
前記硫化工程では、前記浸出液に対して、前記硫化水素ガスを吹き込むとともに、前記硫化反応により生じた硫化水素ガスを含む排ガスをアルカリ溶液に吸収させて得られる硫化水素ナトリウム(NaHS)を添加して硫化反応を生じさせる
ことを特徴とするニッケル酸化鉱石の湿式製錬方法。
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US11186492B2 (en) * | 2019-03-05 | 2021-11-30 | Korea Resources Corporation | Method for recovering valuable metal sulfides |
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Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2005350766A (ja) * | 2004-05-13 | 2005-12-22 | Sumitomo Metal Mining Co Ltd | ニッケル酸化鉱石の湿式製錬方法 |
JP2010126778A (ja) * | 2008-11-28 | 2010-06-10 | Sumitomo Metal Mining Co Ltd | ニッケル及びコバルトを含む硫化物の製造方法 |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4110400A (en) * | 1977-08-01 | 1978-08-29 | Amax Inc. | Selective precipitation of nickel and cobalt sulfides from acidic sulfate solution |
JP3203707B2 (ja) * | 1991-10-09 | 2001-08-27 | 大平洋金属株式会社 | 酸化鉱石から有価金属を回収する方法 |
JP4457864B2 (ja) | 2004-11-24 | 2010-04-28 | 住友金属鉱山株式会社 | ニッケル及び/又はコバルト硫化物の回収方法 |
BRPI0604853B1 (pt) * | 2006-10-27 | 2016-03-08 | Vale Do Rio Doce Co | método para produção de cobalto metálico a partir de refinado de extração por solventes de níquel |
CN101302584A (zh) * | 2008-07-08 | 2008-11-12 | 中南大学 | 一种采用硫化沉淀从红土镍矿浸出液中富集镍钴的方法 |
CN101575676A (zh) * | 2009-06-18 | 2009-11-11 | 中南大学 | 一种红土镍矿沉淀除铁和镍钴富集的方法 |
JP5533700B2 (ja) * | 2011-01-27 | 2014-06-25 | 住友金属鉱山株式会社 | 有価金属の浸出方法及びこの浸出方法を用いた有価金属の回収方法 |
JP5500208B2 (ja) | 2012-06-12 | 2014-05-21 | 住友金属鉱山株式会社 | 中和処理方法 |
CN103173623B (zh) * | 2013-02-28 | 2014-11-05 | 江西铜业股份有限公司 | 一种从多金属酸性水中回收镍钴的方法 |
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Publication number | Priority date | Publication date | Assignee | Title |
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See also references of EP3279344A4 * |
Cited By (2)
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JP2019183189A (ja) * | 2018-04-03 | 2019-10-24 | 住友金属鉱山株式会社 | 低ニッケル品位酸化鉱石からのニッケルコバルト混合硫化物の製造方法 |
JP7035735B2 (ja) | 2018-04-03 | 2022-03-15 | 住友金属鉱山株式会社 | 低ニッケル品位酸化鉱石からのニッケルコバルト混合硫化物の製造方法 |
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