WO2016181673A1 - 鉱石スラリーの前処理方法、鉱石スラリーの製造方法 - Google Patents
鉱石スラリーの前処理方法、鉱石スラリーの製造方法 Download PDFInfo
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- WO2016181673A1 WO2016181673A1 PCT/JP2016/053626 JP2016053626W WO2016181673A1 WO 2016181673 A1 WO2016181673 A1 WO 2016181673A1 JP 2016053626 W JP2016053626 W JP 2016053626W WO 2016181673 A1 WO2016181673 A1 WO 2016181673A1
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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
- C22B23/005—Preliminary treatment of ores, e.g. by roasting or by the Krupp-Renn process
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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
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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
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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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- 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
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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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- 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 pretreatment method for ore slurry, and more particularly to a pretreatment method for ore slurry to be subjected to a leaching treatment in a wet smelting method of nickel oxide ore, and a method for producing an ore slurry to be used for the leaching treatment. .
- leaching process In the process of leaching metal from nickel oxide ore by such high-temperature pressure acid leaching method (hereinafter also simply referred to as “leaching process”), in addition to nickel and cobalt, which are to be recovered, iron, magnesium, manganese, aluminum Since an impurity element such as leaching was also leached by sulfuric acid, an excess of sulfuric acid was required for the treatment.
- nickel and cobalt are selectively recovered as sulfides, but most of impurity elements such as iron, magnesium, manganese, and aluminum leached in the leaching process in the leaching process. Does not form sulfides and remains in the poor solution after separating the sulfides. In order to discharge this poor solution, it is necessary to precipitate and remove metal ions remaining in the poor solution by a neutralization treatment in the final neutralization step.
- the pH of the poor solution is increased to about 5 by adding the limestone slurry to the poor solution obtained through the sulfiding step, and after removing iron and aluminum, the slaked lime slurry is added.
- a method of removing magnesium and manganese by adding and raising the pH to about 9 is generally performed. Therefore, since the required amount (addition amount) of slaked lime slurry is determined by the amount of magnesium ions and manganese ions remaining in the poor liquid, if the content of magnesium and manganese in the nickel oxide ore is large, a large amount Slaked lime slurry was required.
- Patent Document 1 in a hydrometallurgical method based on high-temperature pressure leaching for recovering nickel from nickel oxide ore, simplification of the leaching step and the solid-liquid separation step, consumption of neutralizing agent and amount of starch in the neutralization step A technique for providing a simple and highly efficient smelting method as a whole process by reducing the amount of water and using the water repeatedly and efficiently is disclosed.
- Patent Document 1 does not disclose a technical idea for reducing the amount of sulfuric acid used in the leaching process in the leaching step or reducing the amount of slaked lime used in the final neutralization step described above.
- it is naturally required to reduce the actual yield of nickel when reducing the amount of acid or neutralizing agent used.
- the present invention has been proposed in view of such circumstances, and in the hydrometallurgical method of nickel oxide ore, the amount of sulfuric acid used in the leaching process and the final amount are reduced while more effectively suppressing the decrease in nickel yield. It aims at providing the method which can reduce the usage-amount of neutralizing agents, such as slaked lime, in a sum process effectively.
- the present inventors have made extensive studies to solve the above-described problems. As a result, sulfuric acid, slaked lime, etc., while suppressing the decrease in nickel yield to a very low level by applying a specific pretreatment to the ore slurry used in the leaching process in the leaching process of the hydrometallurgical method of nickel oxide ore
- the present inventors have found that the amount of chemicals used in the smelting process can be reduced and completed the present invention. That is, the present invention provides the following.
- the first invention of the present invention is a pretreatment method of ore slurry to be subjected to leaching treatment in a nickel oxide ore hydrometallurgy method, wherein the ore slurry is treated with at least one of a hydrocyclone and a density separator.
- a first separation step in which the fine grain portion is separated into a coarse grain portion and a fine grain portion using three stages, and the fine grain portion is supplied to the leaching process, and the coarse grain portion separated in the first separation step Is separated into a heavy specific gravity part and a light specific gravity part using at least a spiral concentrator, and the heavy specific gravity part is separated in the leaching process and separated in the second separation process.
- An ore slurry pretreatment method comprising a vibration sieving step of separating the light specific gravity portion into a sieve top and a sieve under a vibrating sieve and supplying the ore slurry under the sieve to the leaching treatment.
- the second invention of the present invention is the pretreatment method for ore slurry according to the first invention, wherein the opening of the vibrating sieve is 300 ⁇ m or more.
- the coarse part separated in the first separation step has a particle size of less than 45 ⁇ m in the ore slurry.
- This is a pretreatment method for an ore slurry in which particles are 35% by mass or less in the solid content.
- the first separation step includes a classification separation step in which the ore slurry is supplied to the hydrocyclone and classified. And a specific gravity separation step of supplying an underflow classified by the hydrocyclone in the classification separation step to the density separator to separate the specific gravity.
- the fifth invention of the present invention is the ore slurry according to any one of the first to fourth inventions, wherein the nickel oxide ore wet smelting method forms the nickel oxide ore slurry (ore slurry).
- a leaching process in which sulfuric acid is added to the ore slurry and leaching is performed under high temperature and high pressure, and the residue is separated while the obtained leaching slurry is washed in multiple stages.
- a pretreatment method for ore slurry comprising a sulfidation step for producing a sulfide containing nickel and a poor solution by performing a treatment, and a final neutralization step for recovering and detoxifying the poor solution discharged in the sulfidation step It is.
- a sixth invention of the present invention is a method for producing an ore slurry for use in a leaching treatment in a nickel oxide ore hydrometallurgy method, wherein the ore slurrying step obtains a crude ore slurry from the nickel oxide ore.
- a vibration sieving step that separates the upper and lower sieving portions by a vibrating sieve, the ore slurry of the fine-grained portion separated in the first separation step, and the heavy specific gravity portion separated in the second separation step of
- An ore slurry concentration step of charging the stone slurry and the ore slurry under the sieve separated in the vibration sieving step into a solid-liquid separator, separating and removing moisture contained in the ore slurry, and concentrating the ore components Is a method for producing an ore slurry.
- the use of a neutralizing agent such as slaked lime in the amount of sulfuric acid used in the leaching process and the final neutralization process while more effectively suppressing the decrease in nickel yield can be effectively reduced.
- the present embodiment a specific embodiment of the present invention (hereinafter referred to as “the present embodiment”) will be described in detail.
- 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 pretreatment method of the ore slurry according to the present embodiment is a pretreatment method of a nickel oxide ore slurry that is subjected to a leaching treatment by high-temperature high-pressure acid leaching, for example, in a nickel oxide ore hydrometallurgy method.
- the nickel oxide ore ore slurry is, for example, 35% by mass of particles having a particle size of less than 45 ⁇ m in the solid content.
- the amount of sulfuric acid used in the leaching process of the leaching process and the amount of neutralizing agent such as slaked lime used in the neutralization process of the final neutralization process are raw material ores. It is known to increase due to the presence of elements such as iron, magnesium, manganese, and aluminum which are metal components other than nickel and cobalt contained in a certain nickel oxide ore. Such a metal element is mainly mixed as a gangue component in a nickel oxide ore slurry (ore slurry) used for leaching treatment. The present inventor has found that the gangue component is coarse particles in the ore slurry, for example, coarse particles having a particle diameter of 45 ⁇ m or more, and further exists as light specific gravity particles.
- the light specific gravity particles ore is removed by a vibrating sieve. Pre-processing is performed. This makes it possible to effectively reduce the amount of sulfuric acid used in the leaching step and the amount of slaked lime used in the final neutralization step while minimizing the decrease in the actual yield of nickel.
- each step will be described.
- First separation step In the first separation step, the ore slurry of nickel oxide ore is separated into a “coarse part” and a “fine part” in which particles having a particle size of less than 45 ⁇ m, for example, are 35% by mass or less in the solid content. To do. The fine-grained part obtained by the separation becomes the ore slurry supplied to the leaching process as it is.
- the proportion of particles having a particle size of less than 45 ⁇ m in the ore slurry is 35% by mass or less. And the fine-grained portion can be separated.
- the separation process in the first separation step is performed using 1 to 3 stages of at least one of a hydrocyclone and a density separator.
- a separation treatment using a hydrocyclone or a density separator is preferable because the ore slurry can be accurately separated into an underflow and an overflow depending on the particle size.
- the ore slurry is first supplied to the hydrocyclone for classification and separation (this treatment process is also referred to as “classification separation process”), and then classified in the classification and separation process by the hydrocyclone. More preferably, the underflow is supplied to a density separator for specific gravity separation (this treatment step is also referred to as “specific gravity separation step”).
- a large amount of nickel oxide ore (ore slurry) is processed by the hydrometallurgical method, and the particles of the ore slurry are fine, for example, the ratio of 80% to 95% of the particles is less than 45 ⁇ m. Therefore, in the first separation step, first, a classification separation process using a hydrocyclone that is suitable for the treatment of a large amount of ore slurry and suitable for the treatment when there are many distributions to the fine-grained portion, that is, the overflow is performed. preferable.
- the ore slurry whose amount to be treated is greatly reduced is subjected to a specific gravity separation treatment with a density separator suitable for treatment when the treatment amount is relatively small and the distribution ratio to the underflow and the overflow is almost the same. Is preferred.
- the separability in the spiral concentrator used in the second separation step is increased. It deteriorates and many particles having a particle size of less than 45 ⁇ m remain in the light specific gravity portion obtained by specific gravity separation. Then, in the vibration sieving step, which is the next step, particles having a particle size of less than 45 ⁇ m in the light specific gravity portion adhere to the coarse low nickel-containing particles, and together with the low nickel-containing particles, Will be removed.
- the ratio of particles having a particle diameter of less than 45 ⁇ m in the ore slurry is closer to 0%.
- the ratio of particles having a particle diameter of less than 45 ⁇ m is lowered, the coarse particles are separated from the coarse particles in the first separation step.
- Coarse particles of low nickel content are mixed in the fine particles.
- coarse low-nickel-containing particles begin to be mixed in the fine particle portion.
- Second separation step> the coarse particle portion in which the proportion of particles having a particle size of less than 45 ⁇ m in the ore slurry separated in the first separation step is 35% by mass or less is supplied to the spiral concentrator, and the specific gravity is increased.
- the particles are separated into particles having a heavy specific gravity (also referred to as “heavy specific gravity part”) and light specific gravity particles having a light specific gravity (also referred to as “light specific gravity part”).
- the specific gravity part obtained by the separation becomes ore slurry supplied to the leaching process.
- this second separation step specific gravity separation by a spiral concentrator is performed in order to selectively remove a gangue component having a high magnesium to nickel ratio and a light specific gravity.
- the coarse-grained and fine-grained parts are separated by hydrocyclone and density separator, and the gangue components with light specific gravity are preferentially separated and removed from the separated coarse-grained parts by a spiral concentrator.
- the low nickel-containing particles containing the gangue component in the ore slurry can be separated and removed more efficiently. This makes it possible to effectively reduce the amount of sulfuric acid used in the leaching step and the amount of slaked lime used in the final neutralization step while suppressing the decrease in the actual yield of nickel to a very low level.
- the number of necessary spiral concentrators can be reduced by supplying the ore slurry to the spiral concentrator having a small equipment capacity in a state where the processing amount is reduced in the first separation step described above.
- Vibration sieve process Next, the ore slurry of the light specific gravity part separated in the second separation step is separated into a sieve top and a sieve bottom using a vibrating sieve, and the ore slurry under the sieve is supplied to the leaching process in the leaching process. .
- the vibration sieve By performing the treatment with the vibration sieve in this way, it is possible to separate the ore grains of low nickel grade and dehydrate the ore grains, so that the ore grains can be deposited as they are without providing a dehydration step or the like. .
- the opening of the vibration sieve used for the vibration sieve treatment is not particularly limited, but is preferably 300 ⁇ m or more, and more preferably about 300 ⁇ m to 500 ⁇ m. If the aperture of the vibrating sieve is less than 300 ⁇ m, the proportion of ore grains remaining on the sieve increases, and as a result, fine particles with high nickel content that adhere to the ore grains and remain on the sieve increase. There is a possibility that. On the other hand, when the aperture of the vibrating sieve exceeds 500 ⁇ m, low nickel grade ore grains may be mixed under the sieve.
- the pretreatment method of the ore slurry according to the present embodiment is such that particles having a particle size of less than 45 ⁇ m are contained in the solid content with respect to the ore slurry supplied to the leaching treatment of the wet smelting method of nickel oxide ore.
- gangue components such as iron, magnesium, manganese, and aluminum can be efficiently separated on the sieve of the vibratory sieve obtained through the vibratory sieve process.
- other separation components that is, a fine granule portion separated in the first separation step, a heavy specific gravity portion separated in the second separation step, and a component under the sieve of the vibration sieve in the vibration sieve step Is supplied to the leaching treatment as ore slurry, while suppressing the decrease in the actual yield of nickel extremely low, the amount of sulfuric acid used in the leaching process in the hydrometallurgical method, slaked lime in the final neutralization process, etc.
- the amount of neutralizing agent used can be effectively reduced.
- Nickel oxide ore hydrometallurgical process is a smelting process in which nickel is leached and recovered from nickel oxide ore using, for example, a high-pressure acid leaching method (HPAL method).
- HPAL method high-pressure acid leaching method
- FIG. 2 is a process diagram showing an example of the flow of a hydrometallurgical smelting process by high pressure acid leaching of nickel oxide ore.
- the hydrometallurgical process of nickel oxide ore includes ore slurrying step S1 for slurrying nickel oxide ore and ore for removing water contained in the ore slurry and concentrating ore components.
- a solid-liquid separation step S5 for obtaining a leachate containing a neutralization step S6 for adjusting the pH of the leachate to separate a neutralized starch containing an impurity element to obtain a neutralized final solution containing nickel, and sulfidizing the neutralized final solution
- this hydrometallurgy method has a final neutralization step S8 for recovering and detoxifying the leaching residue separated in the solid-liquid separation step S5 and the poor liquid discharged in the sulfurization step S7.
- Ore slurrying step S1 the nickel oxide ore that is the raw ore is classified at a predetermined classification point to remove the oversized ore particles, and then the undersized ore particles are washed with water. To make a coarse ore slurry.
- the nickel oxide ore as the raw material ore is an ore containing nickel and cobalt, and so-called laterite ores such as limonite or saprolite ore are mainly used.
- Laterite ore generally has a nickel content of 0.8% to 2.5% by weight, and is contained as a hydroxide or siliceous clay (magnesium silicate) mineral.
- the iron content is 10% to 50% by weight and is mainly in the form of trivalent hydroxide (goethite), but partly 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, are used.
- the nickel oxide ore classification method is not particularly limited as long as it can classify the ore based on the desired particle size, and can be performed, for example, by sieving using a general grizzly or vibrating sieve.
- the classification point is not particularly limited, and a classification point for obtaining an ore slurry composed of ore particles having a desired particle size or less can be appropriately set.
- Pretreatment process S2 before performing the leaching process with respect to an ore slurry, it has pretreatment process S2 which pretreats the ore slurry obtained through the ore slurrying process S1.
- Pretreatment process S2 isolate
- the detailed description of the pretreatment in the pretreatment step S2 is the same as described above, and is omitted here.
- the ore slurry divided below is supplied to the leaching process in the leaching step S4 through the ore slurry concentration step S3 described later.
- each ore slurry is charged into a solid-liquid separation device such as thickener, for example, and the solid components are settled and taken out from the lower part of the device.
- Solid-liquid separation is performed to overflow from the top of the tube.
- the pretreatment step S2 including the ore slurrying step S1, the first separation step S21, the second separation step S22, and the vibrating sieve step S23, and the ore slurry concentration step S3 are performed.
- an ore slurry to be subjected to the leaching process in the leaching step S4 described later can be manufactured, and a method including these steps can be defined as a method for manufacturing the ore slurry.
- a leaching process using, for example, a high-pressure acid leaching method is performed on the produced ore slurry. Specifically, sulfuric acid is added to an ore slurry containing nickel oxide ore as a raw material, and the ore slurry is stirred while being pressurized under a high temperature condition of 220 ° C. to 280 ° C., and a leach consisting of a leachate and a leach residue. A slurry is produced.
- a leaching reaction represented by the following formulas (i) to (iii) and a high-temperature thermal hydrolysis reaction represented by the following formulas (iv) and (v) occur, and nickel, cobalt, etc.
- Leaching as sulfate and immobilization of leached iron sulfate as hematite are performed.
- an excessive amount of sulfuric acid in the leaching step S4 an excessive amount is generally used conventionally.
- nickel oxide ore also contains impurities such as iron, magnesium, manganese, and aluminum, and these impurities are also leached by sulfuric acid, so as to increase the actual yield of nickel and cobalt recovery targets.
- An excessive amount of sulfuric acid was added to the leaching treatment.
- the ore slurry subjected to the leaching process in the leaching step S4 is subjected to a specific pretreatment in the above-described pretreatment step S2, so that the ore slurry is subjected to the ore slurry.
- the concentration of impurities contained can be reduced, and the amount of sulfuric acid used for the leaching treatment can be effectively reduced while suppressing the decrease in the actual yield of nickel or the like to a very low level.
- Solid-liquid separation process In the solid-liquid separation process S5, the leaching liquid containing the impurity element in addition to nickel and cobalt is separated from the leaching residue while washing the leaching slurry obtained through the leaching process S4 in multiple stages.
- the solid-liquid separation processing is performed by solid-liquid separation equipment such as a thickener. Specifically, the leaching slurry is first diluted with a cleaning liquid, and then the leaching residue in the slurry is concentrated as a thickener sediment. Thereby, the nickel content adhering to the leaching residue can be reduced according to the degree of dilution.
- an anionic flocculant may be added.
- the solid-liquid separation step S5 it is preferable to perform solid-liquid separation while washing the leach slurry in multiple stages.
- the multistage cleaning method for example, a continuous countercurrent cleaning method in which the cleaning liquid is brought into contact with the leaching slurry in a countercurrent flow can be used. Thereby, the cleaning liquid newly introduced into the system can be reduced, and the recovery rate of nickel and cobalt can be improved to 95% or more.
- the cleaning liquid (cleaning water) is not particularly limited, but it is preferable to use a liquid that does not include nickel and does not affect the process.
- the cleaning liquid preferably, the poor liquid obtained in the subsequent sulfurization step S7 can be used repeatedly.
- Neutralization step S6 the pH of the leachate separated in the solid-liquid separation step S5 is adjusted, the neutralized starch containing impurity elements is separated, and the neutralization finish containing nickel and cobalt is completed. Obtain a liquid.
- the pH of the resulting neutralized final solution is 4 or less, preferably 3.0 to 3.5, more preferably 3.1 to 3, while suppressing oxidation of the separated leachate.
- a neutralizing agent such as calcium carbonate is added to the leachate so as to be 3.2, and a neutralized final slurry and a neutralized starch slurry containing trivalent iron, aluminum, or the like as an impurity element are generated.
- the impurities are removed as neutralized starch in this way, and a neutralized final solution serving as a mother liquor for nickel recovery is generated.
- a sulfide containing nickel (and cobalt) is generated by injecting a sulfiding agent such as hydrogen sulfide gas into the neutralized final solution which is a mother liquor for nickel recovery to cause a sulfidation reaction. (Hereinafter also simply referred to as “nickel sulfide”) and a poor solution.
- a sulfiding agent such as hydrogen sulfide gas
- the neutralization final solution which is the mother liquor for nickel recovery, is a sulfuric acid solution in which impurity components are reduced from the leachate through the neutralization step S6.
- the nickel recovery mother liquor may contain about several g / L of iron, magnesium, manganese, etc. as impurity components, but these impurity components have low stability as sulfides (recovery). (As opposed to nickel and cobalt), it is not contained in the resulting nickel sulfide.
- the sulfidation process in the sulfidation step S7 is performed in a nickel recovery facility.
- the nickel recovery facility includes, for example, a sulfurization reaction tank that performs a sulfurization reaction by blowing hydrogen sulfide gas or the like into a neutralized final liquid that is a mother liquid, and a solid-liquid separation tank that separates and recovers nickel sulfide from the liquid after the sulfurization reaction.
- the solid-liquid separation tank is constituted by, for example, a thickener or the like, and precipitates and precipitates nickel sulfide from the bottom of the thickener by subjecting the slurry after the sulfurization reaction containing nickel sulfide to sedimentation separation. .
- the aqueous solution component overflows and is recovered as a poor solution.
- the recovered poor solution 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 sulfided. This poor solution is transferred to a final neutralization step S8, which will be described later, and detoxified.
- Final neutralization step S8 the poor pH containing impurity elements such as iron, magnesium and manganese discharged in the sulfurization step S7 described above is within a predetermined pH range that satisfies the discharge standard. Apply neutralization treatment (detoxification treatment) to be adjusted. In this final neutralization step S8, the leaching residue discharged from the solid-liquid separation process in the solid-liquid separation process S5 can also be processed.
- the method of detoxification treatment in the final neutralization step S8, that is, the pH adjustment method is not particularly limited, but for example, by adding a neutralizing agent such as calcium carbonate (limestone) slurry or calcium hydroxide (slaked lime) slurry. It can be adjusted to a predetermined range.
- a neutralizing agent such as calcium carbonate (limestone) slurry or calcium hydroxide (slaked lime) slurry. It can be adjusted to a predetermined range.
- the first stage neutralization treatment (first final neutralization step S81) using limestone as a neutralizer and the second stage using slaked lime as a neutralizer. It is possible to carry out a stepwise neutralization process consisting of a neutralization process (second final neutralization step S82). By performing stepwise neutralization treatment in this way, efficient and effective neutralization treatment can be performed.
- the poor liquid discharged from the sulfurization step S7 and the leach residue separated in the solid-liquid separation step S5 are charged into the neutralization treatment tank, and limestone slurry is added. Then, a stirring process is performed.
- the pH of the solution to be treated such as a poor solution is adjusted to 4 to 5 by adding a limestone slurry.
- the slaked lime slurry is added to the solution that has been subjected to the neutralization treatment in the first stage by adding the limestone slurry, and the stirring treatment is performed.
- the pH of the solution to be treated is raised to 8-9 by adding slaked lime slurry.
- a neutralization treatment residue is generated and stored in a tailing dam (tailing residue).
- the neutralized solution satisfies the discharge standard and is discharged out of the system.
- the amount of neutralizing agent such as slaked lime is determined according to the amount of impurity element ions such as magnesium ions and manganese ions remaining in the poor solution.
- magnesium or manganese contained in the ore slurry is obtained by performing a specific pretreatment in the above-described pretreatment step S2 on the ore slurry to be subjected to the leaching treatment in the leaching step S4. Impurity elements such as can be reduced. Thereby, the concentration of these elements contained in the poor solution can be reduced, and the amount of neutralizing agent used for the neutralization treatment in the final neutralization step can be effectively reduced.
- Example 1 As shown below, a hydrometallurgical treatment of nickel oxide ore consisting of the process diagram shown in FIG. 2 was performed. That is, first, as an ore slurry pretreatment step, an ore slurry obtained by slurrying nickel oxide ore having the composition shown in Table 1 below is supplied to a hydrocyclone (SC1030-P type manufactured by Salter Cyclone). Then, classification separation treatment was performed, and subsequently, the underflow discharged from the hydrocyclone was supplied to a density separator (CFS Corp., 6 ⁇ 6 type) to perform specific gravity separation treatment. Note that these separation processing steps are referred to as a first separation step. By the separation process in the first separation step, an ore slurry (coarse portion) in which the content of particles having a particle size of less than 45 ⁇ m in the underflow solid content of the density separator is 25% by mass was obtained.
- a hydrocyclone SC1030-P type manufactured by Salter Cyclone
- CFS Corp. 6 ⁇ 6 type
- the coarse-grained ore slurry separated through the first separation step is supplied to a spiral concentrator (manufactured by Autotech Co., Ltd.) at a solid content concentration of 20% for specific gravity separation, and nickel is used as the light specific gravity part.
- a spiral concentrator manufactured by Autotech Co., Ltd.
- nickel is used as the light specific gravity part.
- An ore slurry containing a solid content of 0.86% grade and 5.34% magnesium grade was obtained. This separation process is referred to as a second separation process.
- the separated ore slurry having a light specific gravity part was supplied to a vibrating sieve (VDS27-6, manufactured by Sizetec Co., Ltd.) equipped with a sieve having an opening of 300 ⁇ m, and subjected to a vibrating sieve treatment. Note that.
- This vibration sieving process is referred to as a vibration sieving process.
- solids having a nickel quality of 0.91% and a magnesium quality of 8.40% on the sieve, that is, low nickel-containing particles were obtained.
- the ore slurry under the sieve of the vibration sieve in the vibration sieve process, the fine grain ore slurry separated in the first separation process described above, and the ore of the heavy specific gravity part separated in the second separation process The slurry was supplied to a leaching process for leaching the ore.
- the nickel loss rate on the sieve of the vibrating sieve was 3.7%.
- the sulfuric acid consumption in the leaching process in the leaching process in which the ore slurry was supplied was 278 kg / tone of ore.
- the leachate obtained through the leaching treatment was subjected to sulfidation treatment (sulfurization step), and the final neutralization treatment (final neutralization step) was performed on the poor liquid obtained by the sulfidation treatment,
- the amount of slaked lime used in the neutralization treatment was 41 kg / ton ore.
- Example 2 The same operation as in Example 1 is performed, and in the first separation step, an ore slurry (coarse portion) in which the content of particles having a particle size of less than 45 ⁇ m in the underflow solid content of the density separator is 30% by mass is obtained. It was.
- the obtained coarse-grained ore slurry is supplied to the spiral concentrator at a solid content concentration of 20%, and as the light specific gravity part, the nickel quality is 0.85% and the magnesium quality is 4. An ore slurry containing 99% solids was obtained.
- the obtained ore slurry having a light specific gravity part was supplied to a vibration sieve equipped with a sieve having an opening of 300 ⁇ m to perform a vibration sieving process.
- solids having a nickel quality of 0.91% and a magnesium quality of 8.23% on the sieve, that is, low nickel-containing particles were obtained.
- the ore slurry under the sieve of the vibration sieve in the vibration sieve process, the fine grain ore slurry separated in the first separation process described above, and the ore of the heavy specific gravity part separated in the second separation process The slurry was supplied to a leaching process for leaching the ore.
- the nickel loss rate on the vibrating sieve was 3.8%.
- the sulfuric acid consumption in the leaching process in the leaching process in which the ore slurry was supplied was 278 kg / tone of ore.
- the leachate obtained through the leaching treatment was subjected to sulfidation treatment (sulfurization step), and the final neutralization treatment (final neutralization step) was performed on the poor liquid obtained by the sulfidation treatment,
- the amount of slaked lime used in the neutralization treatment was 41 kg / ton ore.
- Example 3 The same operation as in Example 1 was performed, and in the first separation step, an ore slurry (coarse portion) in which the content of particles having a particle size of less than 45 ⁇ m in the underflow solid content of the density separator was 35% by mass was obtained. It was.
- the obtained coarse-grained ore slurry is supplied to the spiral concentrator at a solid content concentration of 20%, and as the light specific gravity part, the nickel quality is 0.84% and the magnesium quality is 4. An ore slurry containing 36% solids was obtained.
- the obtained ore slurry having a light specific gravity part was supplied to a vibration sieve equipped with a sieve having an opening of 300 ⁇ m to perform a vibration sieving process.
- a solid content having a nickel quality of 0.88% and a magnesium quality of 6.77% on the sieve, that is, low nickel-containing particles was obtained.
- the ore slurry under the sieve of the vibration sieve in the vibration sieve process, the fine grain ore slurry separated in the first separation process described above, and the ore of the heavy specific gravity part separated in the second separation process The slurry was supplied to a leaching process for leaching the ore.
- the nickel loss rate on the sieve of the vibrating sieve was 4.9%, which was slightly increased as compared with Examples 1 and 2, but the decrease in nickel yield could be suppressed at a low level.
- the reason why the nickel loss rate increased compared to Examples 1 and 2 was that the content of particles of less than 45 ⁇ m in the ore slurry supplied to the spiral concentrator was slightly higher, so the separability in the spiral concentrator was This is considered to be because the particles of less than 45 ⁇ m were accompanied by the low-nickel-containing particles and transferred to the sieve and removed in the vibrating sieve.
- the sulfuric acid consumption in the leaching process in the leaching process in which the ore slurry was supplied was 279 kg / tone of ore. Furthermore, when the leachate obtained through the leaching treatment was subjected to sulfidation treatment (sulfurization step), and the final neutralization treatment (final neutralization step) was performed on the poor liquid obtained by the sulfidation treatment, The amount of slaked lime used in the neutralization treatment was 40.5 kg / ton ore.
- Example 3 although the nickel yield was slightly reduced, the amount of sulfuric acid used in the leaching step and the amount of slaked lime used in the final neutralization step could be kept low as in Examples 1 and 2. .
- Example 1 The nickel oxide ore whose composition is shown in Table 1 is slurried, and the same operation as in Example 1 is performed. In the first separation step, the content of particles having a particle size of less than 45 ⁇ m in the underflow solid content of the density separator is 25. An ore slurry (coarse portion) having a mass% was obtained.
- the resulting coarse-grained ore slurry was supplied to a vibration sieve equipped with a sieve having an opening of 300 ⁇ m without performing a treatment with a spiral concentrator, and a vibration sieving treatment was performed.
- a vibration sieve equipped with a sieve having an opening of 300 ⁇ m without performing a treatment with a spiral concentrator, and a vibration sieving treatment was performed.
- a solid content of 0.83% nickel grade and 7.50% magnesium grade was obtained on the sieve.
- the ore slurry under the vibration sieve in the vibration sieving step and the fine ore slurry separated in the first separation step described above were supplied to the leaching step for leaching the ore.
- the nickel loss rate on the vibrating sieve was very high at 6.7%. This is considered to be because the gangue component having a low specific gravity could not be selectively separated and removed because the treatment by the spiral concentrator was not performed.
- the sulfuric acid consumption in the leaching process in the leaching process in which the ore slurry was supplied was 272 kg / tone of ore.
- the leachate obtained through the leaching treatment was subjected to sulfidation treatment (sulfurization step), and the final neutralization treatment (final neutralization step) was performed on the poor liquid obtained by the sulfidation treatment,
- the amount of slaked lime used in the neutralization treatment was 36.0 kg / ton ore.
- Example 2 The nickel oxide ore whose composition is shown in Table 1 is slurried, and the same operation as in Example 1 is performed. In the first separation step, the content of particles having a particle size of less than 45 ⁇ m in the underflow solid content of the density separator is 30. An ore slurry (coarse portion) having a mass% was obtained.
- the resulting coarse-grained ore slurry was supplied to a vibration sieve equipped with a sieve having an opening of 300 ⁇ m without performing a treatment with a spiral concentrator, and a vibration sieving treatment was performed.
- This vibrating sieve provided a solid content of 0.84% nickel grade and 7.39% magnesium grade on the sieve.
- the ore slurry under the vibration sieve in the vibration sieving step and the fine ore slurry separated in the first separation step described above were supplied to the leaching step for leaching the ore.
- the nickel loss rate on the vibrating screen was very high at 6.8%.
- the sulfuric acid consumption in the leaching process in the leaching process in which the ore slurry was supplied was 272 kg / tone of ore.
- the leachate obtained through the leaching treatment was subjected to sulfidation treatment (sulfurization step), and the final neutralization treatment (final neutralization step) was performed on the poor liquid obtained by the sulfidation treatment,
- the amount of slaked lime used in the neutralization treatment was 36.0 kg / ton ore.
- the sulfuric acid consumption in the leaching process in the leaching process in which the ore slurry was supplied was 287 kg / tone of ore.
- the leaching solution obtained through the leaching treatment was subjected to sulfidation treatment (sulfurization step), and the final neutralization treatment (final neutralization step) was performed on the poor liquid obtained by the sulfidation treatment.
- the amount of slaked lime used in the neutralization treatment was 47.5 kg / ton ore.
- Table 2 shows the ore slurry supplied to the spiral concentrator and the vibrating sieve in the operations of Examples 1 to 3 and Comparative Examples 1 to 3, and the recovered particles recovered on the sieve by the treatment with the vibrating sieve.
- the quality of magnesium, the content of particles less than 45 ⁇ m in the solid content, and the nickel loss rate are shown together.
- Table 3 summarizes the sulfuric acid consumption in the leaching process and the slaked lime consumption in the final neutralization process in the operations of Examples 1 to 3 and Comparative Examples 1 to 3.
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Abstract
Description
本実施の形態に係る鉱石スラリーの前処理方法は、ニッケル酸化鉱石の湿式製錬方法において、例えば高温高圧酸浸出による浸出処理に供するニッケル酸化鉱石のスラリーの前処理方法である。具体的に、この鉱石スラリーの前処理方法は、図1に示す工程図にあるように、ニッケル酸化鉱石の鉱石スラリーを、例えば、45μm未満の粒径を有する粒子が固形分中の35質量%以下である粗粒部と、細粒部とに分離して、その細粒部を浸出処理に供給する第1の分離工程と、分離した粗粒部を、スパイラルコンセントレーターを用いて重比重部と軽比重部とに比重分離し、重比重部を浸出処理に供給する第2の分離工程と、分離した軽比重部を振動篩によって篩上と篩下とに分離し、その篩下の鉱石スラリーを浸出処理に供給する振動篩工程とを有する。
第1の分離工程では、ニッケル酸化鉱石の鉱石スラリーを、例えば45μm未満の粒径を有する粒子が固形分中の35質量%以下である「粗粒部」と、「細粒部」とに分離する。分離して得られた細粒部は、そのまま、浸出処理に供給する鉱石スラリーとなる。
第2の分離工程では、第1の分離工程にて分離した、鉱石スラリー中の粒径45μm未満の粒子の割合が35質量%以下である粗粒部を、スパイラルコンセントレーターに供給して、比重の重い重比重粒子(「重比重部」ともいう)と比重の軽い軽比重粒子(「軽比重部」ともいう)とに分離する。分離して得られた重比重部は、浸出処理に供給する鉱石スラリーとなる。
次に、第2の分離工程にて分離した、軽比重部の鉱石スラリーを、振動篩を用いて篩上と篩下に分別し、その篩下の鉱石スラリーを浸出工程における浸出処理に供給する。このように振動篩による処理を施すことで、低ニッケル品位の鉱石粒を分離するとともに、鉱石粒を脱水することができるため、脱水工程等を別途設けることなく鉱石粒をそのまま堆積させることができる。
ニッケル酸化鉱石の湿式製錬プロセスは、例えば高圧酸浸出法(HPAL法)を用いて、ニッケル酸化鉱石からニッケルを浸出させて回収する製錬プロセスである。
鉱石スラリー化工程S1では、原料鉱石であるニッケル酸化鉱石に対して、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粒子に水を添加して粗鉱石スラリーとする。
本実施の形態においては、鉱石スラリーに対して浸出処理を施すに先立ち、鉱石スラリー化工程S1を経て得られた鉱石スラリーに前処理を施す前処理工程S2を有する。
鉱石スラリー濃縮工程S3では、上述した前処理工程S2における第1の分離工程S21にて分離した細粒部の鉱石スラリーと、第2の分離工程S22にて分離した重比重部の鉱石スラリーと、振動篩工程S23にて分離した篩下の鉱石粒子を含む鉱石スラリーとを、固液分離装置に装入して、その粗鉱石スラリー中に含まれる水分を分離除去して鉱石成分を濃縮し、鉱石スラリーを得る。この濃縮された鉱石スラリーが、浸出工程S4における浸出処理に供される鉱石スラリーとなる。
浸出工程S4では、製造した鉱石スラリーに対して、例えば高圧酸浸出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含有する鉱石スラリーに硫酸を添加し、220℃~280℃の高い温度条件下で加圧しながら鉱石スラリーを攪拌し、浸出液と浸出残渣とからなる浸出スラリーを生成させる。
MO+H2SO4⇒MSO4+H2O ・・(i)
(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 ・・(ii)
FeO+H2SO4→FeSO4+H2O ・・(iii)
・高温熱加水分解反応
2FeSO4+H2SO4+1/2O2⇒Fe2(SO4)3+H2O ・・(iv)
Fe2(SO4)3+3H2O⇒Fe2O3+3H2SO4 ・・(v)
固液分離工程S5では、浸出工程S4を経て得られた浸出スラリーを多段で洗浄しながら、ニッケル及びコバルトのほか不純物元素を含む浸出液と、浸出残渣とを分離する。
中和工程S6では、固液分離工程S5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、ニッケルやコバルトを含む中和終液を得る。
硫化工程S7では、ニッケル回収用の母液である中和終液に対して、硫化水素ガス等の硫化剤を吹き込んで硫化反応を生じさせ、ニッケル(及びコバルト)を含む硫化物(以下、単に「ニッケル硫化物」ともいう)と貧液とを生成させる。
最終中和工程S8では、上述した硫化工程S7にて排出された鉄、マグネシウム、マンガン等の不純物元素を含む貧液に対して、排出基準を満たす所定のpH範囲に調整する中和処理(無害化処理)を施す。この最終中和工程S8では、固液分離工程S5における固液分離処理から排出された浸出残渣も併せて処理することもできる。
以下に示すように、図2に示す工程図からなるニッケル酸化鉱石の湿式製錬処理を行った。すなわち、先ず、鉱石スラリーの前処理工程として、下記表1に示す組成を有するニッケル酸化鉱石をスラリー化して得られた鉱石スラリーを、ハイドロサイクロン(ソルターサイクロン社製,SC1030-P型)へ供給して分級分離処理を施し、続いて、ハイドロサイクロンから排出されたアンダーフローを、デンシティセパレーター(シーエフエス社製,6×6型)へ供給して比重分離処理を施した。なお、これらの分離処理の工程を第1の分離工程とする。この第1の分離工程における分離処理により、デンシティセパレーターのアンダーフロー固形分中における粒径45μm未満の粒子の含有量が25質量%である鉱石スラリー(粗粒部)を得た。
実施例1と同様の操作を行い、第1の分離工程において、デンシティセパレーターのアンダーフロー固形分中における粒径45μm未満の粒子の含有量が30質量%である鉱石スラリー(粗粒部)を得た。
実施例1と同様の操作を行い、第1の分離工程において、デンシティセパレーターのアンダーフロー固形分中における粒径45μm未満の粒子の含有量が35質量%である鉱石スラリー(粗粒部)を得た。
表1に組成を示したニッケル酸化鉱石をスラリー化し、実施例1と同様の操作を行い、第1の分離工程においてデンシティセパレーターのアンダーフロー固形分中における粒径45μm未満の粒子の含有量が25質量%である鉱石スラリー(粗粒部)を得た。
表1に組成を示したニッケル酸化鉱石をスラリー化し、実施例1と同様の操作を行い、第1の分離工程においてデンシティセパレーターのアンダーフロー固形分中における粒径45μm未満の粒子の含有量が30質量%である鉱石スラリー(粗粒部)を得た。
表1に組成を示したニッケル酸化鉱石をスラリー化し、その鉱石スラリーに対して前処理(第1の分離工程、第2の分離工程、及び振動篩工程)を行わず、浸出処理を施す浸出工程に供給した。
Claims (6)
- ニッケル酸化鉱石の湿式製錬方法における浸出処理に供する鉱石スラリーの前処理方法であって、
鉱石スラリーを、ハイドロサイクロン、デンシティセパレーターの少なくとも1つを1~3段使用して粗粒部と細粒部とに分離し、該細粒部を前記浸出処理に供給する第1の分離工程と、
前記第1の分離工程にて分離した前記粗粒部を、少なくともスパイラルコンセントレーターを使用して重比重部と軽比重部とに分離し、該重比重部を前記浸出処理に供給する第2の分離工程と、
前記第2の分離工程にて分離した前記軽比重部を振動篩によって篩上と篩下とに分離し、該篩下の鉱石スラリーを前記浸出処理に供給する振動篩工程と
を有することを特徴とする鉱石スラリーの前処理方法。 - 前記振動篩の目開きが300μm以上であることを特徴とする請求項1に記載の鉱石スラリーの前処理方法。
- 前記第1の分離工程にて分離する前記粗粒部は、
前記鉱石スラリーのうち、45μm未満の粒径を有する粒子が固形分中の35質量%以下のものであることを特徴とする請求項1又は2に記載の鉱石スラリーの前処理方法。 - 前記第1の分離工程は、
前記鉱石スラリーを前記ハイドロサイクロンに供給して分級分離する分級分離工程と、
前記分級分離工程において前記ハイドロサイクロンにより分級されたアンダーフローを前記デンシティセパレーターに供給して比重分離する比重分離工程と
を有することを特徴とする請求項1乃至3のいずれか1項に記載の鉱石スラリーの前処理方法。 - 前記ニッケル酸化鉱石の湿式製錬方法は、
前記ニッケル酸化鉱石のスラリー(鉱石スラリー)を形成する鉱石スラリー化工程と、
前記鉱石スラリーに対して硫酸を添加して高温高圧下で浸出処理を施す浸出工程と、
得られた浸出スラリーを多段洗浄しながら残渣を分離し、ニッケルと共に不純物元素を含む浸出液を得る固液分離工程と、
前記浸出液のpHを調整して前記不純物元素を含む中和澱物を分離し、ニッケルを含む中和終液を得る中和工程と、
前記中和終液に対し硫化処理を施してニッケルを含む硫化物と貧液とを生成させる硫化工程と、
前記硫化工程にて排出された貧液を回収して無害化する最終中和工程と
を有することを特徴とする請求項1乃至4のいずれか1項に記載の鉱石スラリーの前処理方法。 - ニッケル酸化鉱石の湿式製錬方法における浸出処理に供するための鉱石スラリーの製造方法であって、
前記ニッケル酸化鉱石から粗鉱石スラリーを得る鉱石スラリー化工程と、
前記粗鉱石スラリーを、ハイドロサイクロン、デンシティセパレーターの少なくとも1つを1~3段使用して粗粒部と細粒部とに分離する第1の分離工程と、
前記第1の分離工程にて分離した前記粗粒部を、少なくともスパイラルコンセントレーターを使用して重比重部と軽比重部とに分離する第2の分離工程と、
前記第2の分離工程にて分離した前記軽比重部を振動篩によって篩上と篩下とに分離する振動篩工程と、
前記第1の分離工程にて分離した前記細粒部の鉱石スラリーと、前記第2の分離工程にて分離した前記重比重部の鉱石スラリーと、前記振動篩工程にて分離した前記篩下の鉱石スラリーとを固液分離装置に装入し、該鉱石スラリーに含まれる水分を分離除去して鉱石成分を濃縮する鉱石スラリー濃縮工程と
を有することを特徴とする鉱石スラリーの製造方法。
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JP6977458B2 (ja) * | 2017-09-29 | 2021-12-08 | 住友金属鉱山株式会社 | ニッケル酸化鉱石の湿式製錬方法 |
JP2019203152A (ja) * | 2018-05-21 | 2019-11-28 | 住友金属鉱山株式会社 | 鉱石スラリーの濃縮システム、及び鉱石スラリーの濃縮方法 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6075536A (ja) * | 1983-07-22 | 1985-04-27 | カリフオルニア・ニツケル・コ−ポレイシヨン | マグネシウム、ニツケル及びコバルト含有ラテライト鉱石から該金属量を回収する方法 |
WO2010032513A1 (ja) * | 2008-09-18 | 2010-03-25 | 住友金属鉱山株式会社 | サプロライト鉱のニッケル濃縮処理方法 |
WO2010060144A1 (en) * | 2008-11-28 | 2010-06-03 | Bhp Billiton Ssm Development Pty Ltd | Process for separating limonite and saprolite |
WO2014125558A1 (ja) * | 2013-02-12 | 2014-08-21 | 住友金属鉱山株式会社 | ニッケル酸化鉱石の湿式製錬方法 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP4525428B2 (ja) | 2004-05-13 | 2010-08-18 | 住友金属鉱山株式会社 | ニッケル酸化鉱石の湿式製錬方法 |
CN201070597Y (zh) * | 2007-02-08 | 2008-06-11 | 邹强 | 离心桶重选机 |
JP5163387B2 (ja) * | 2007-11-13 | 2013-03-13 | 住友金属鉱山株式会社 | サプロライト鉱のニッケル濃縮処理方法 |
CN101823018B (zh) | 2009-03-05 | 2013-03-06 | 中国恩菲工程技术有限公司 | 红土矿选铬方法 |
CN102172559A (zh) * | 2010-12-29 | 2011-09-07 | 昆明冶金研究院 | 一种离心选矿和浮选相结合的钨、锡回收选矿方法 |
JP5403033B2 (ja) | 2011-11-01 | 2014-01-29 | 住友金属鉱山株式会社 | ニッケル酸化鉱石の湿式製錬方法 |
WO2013150642A1 (ja) | 2012-04-06 | 2013-10-10 | 住友金属鉱山株式会社 | クロマイト回収方法、並びにニッケル酸化鉱石の湿式製錬方法 |
CN102974451A (zh) * | 2012-10-12 | 2013-03-20 | 金川集团股份有限公司 | 一种提高铜镍矿伴生贵金属回收率的方法 |
-
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Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6075536A (ja) * | 1983-07-22 | 1985-04-27 | カリフオルニア・ニツケル・コ−ポレイシヨン | マグネシウム、ニツケル及びコバルト含有ラテライト鉱石から該金属量を回収する方法 |
WO2010032513A1 (ja) * | 2008-09-18 | 2010-03-25 | 住友金属鉱山株式会社 | サプロライト鉱のニッケル濃縮処理方法 |
WO2010060144A1 (en) * | 2008-11-28 | 2010-06-03 | Bhp Billiton Ssm Development Pty Ltd | Process for separating limonite and saprolite |
WO2014125558A1 (ja) * | 2013-02-12 | 2014-08-21 | 住友金属鉱山株式会社 | ニッケル酸化鉱石の湿式製錬方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP3296410A4 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021193424A1 (ja) * | 2020-03-25 | 2021-09-30 | 住友金属鉱山株式会社 | 鉱石スラリーの処理方法、ニッケル酸化鉱石の湿式製錬方法 |
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PH12017502045B1 (en) | 2018-04-23 |
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AU2016261416B2 (en) | 2019-02-14 |
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PH12017502045A1 (en) | 2018-04-23 |
CN107532235B (zh) | 2019-07-09 |
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US10626481B2 (en) | 2020-04-21 |
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