WO2017038589A1 - Procédé de fabrication d'une poudre de nickel - Google Patents

Procédé de fabrication d'une poudre de nickel Download PDF

Info

Publication number
WO2017038589A1
WO2017038589A1 PCT/JP2016/074694 JP2016074694W WO2017038589A1 WO 2017038589 A1 WO2017038589 A1 WO 2017038589A1 JP 2016074694 W JP2016074694 W JP 2016074694W WO 2017038589 A1 WO2017038589 A1 WO 2017038589A1
Authority
WO
WIPO (PCT)
Prior art keywords
nickel
nickel powder
reduction
solution
powder
Prior art date
Application number
PCT/JP2016/074694
Other languages
English (en)
Japanese (ja)
Inventor
佳智 尾崎
伸一 平郡
Original Assignee
住友金属鉱山株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from JP2016100070A external-priority patent/JP6610425B2/ja
Application filed by 住友金属鉱山株式会社 filed Critical 住友金属鉱山株式会社
Priority to AU2016314002A priority Critical patent/AU2016314002B2/en
Priority to US15/755,147 priority patent/US20180250752A1/en
Priority to CN201680049552.9A priority patent/CN107921544A/zh
Priority to CA2996277A priority patent/CA2996277C/fr
Priority to EP16841621.2A priority patent/EP3345701A4/fr
Publication of WO2017038589A1 publication Critical patent/WO2017038589A1/fr
Priority to PH12018500435A priority patent/PH12018500435A1/en

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B22—CASTING; POWDER METALLURGY
    • B22F—WORKING METALLIC POWDER; MANUFACTURE OF ARTICLES FROM METALLIC POWDER; MAKING METALLIC POWDER; APPARATUS OR DEVICES SPECIALLY ADAPTED FOR METALLIC POWDER
    • B22F9/00—Making metallic powder or suspensions thereof
    • B22F9/16—Making metallic powder or suspensions thereof using chemical processes
    • B22F9/18—Making metallic powder or suspensions thereof using chemical processes with reduction of metal compounds
    • B22F9/24—Making metallic powder or suspensions thereof using chemical processes with reduction of metal compounds starting from liquid metal compounds, e.g. solutions
    • B22F9/26—Making metallic powder or suspensions thereof using chemical processes with reduction of metal compounds starting from liquid metal compounds, e.g. solutions using gaseous reductors
    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating
    • 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
    • C22B3/44—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 obtaining high-purity nickel powder having a low sulfur quality and briquettes obtained by solidifying it from a nickel sulfate ammine complex solution.
  • it can be applied to the treatment of an intermediate product solution generated in a wet nickel smelting process.
  • nickel powder As a method of industrially producing nickel powder using a hydrometallurgical process, after dissolving the raw material in a sulfuric acid solution, through a step of removing impurities, ammonia is added to the obtained nickel sulfate solution, and an nickel ammine complex is formed. There is a method for producing nickel powder by supplying hydrogen gas to a nickel sulfate ammine complex solution formed and reducing nickel.
  • Non-Patent Document 1 describes a nickel powder manufacturing process in which an iron compound is added as a seed crystal during a reduction reaction, and nickel is deposited on the iron compound. Have problems with the resulting points
  • Patent Document 1 is inexpensive and excellent in weather resistance, has low electrical resistance in a kneaded state with a resin, reduces initial electrical resistance and electrical resistance during use, and can be used stably over a long period of time.
  • a nickel powder suitable as conductive particles for a paste and a conductive resin, and a method for providing a method for producing the same are disclosed.
  • the nickel powder disclosed in Patent Document 1 is a nickel powder containing secondary particles in which cobalt is contained in an amount of 1 to 20% by mass, the balance is made of nickel and inevitable impurities, and primary particles are aggregated. The amount is 0.8% by mass or less. Cobalt is contained only in the surface layer portion of the secondary particles, and the cobalt content in the surface layer portion is preferably 1 to 40% by mass. Cobalt coexists when trying to obtain this nickel powder by the disclosed manufacturing method. For example, nickel and cobalt coexist like nickel oxide ore, and these are separated to increase the amount. It is not suitable for use in purifying and economically.
  • Patent Document 2 provides a method for producing metal powder by a liquid phase reduction method, which is improved so as not to easily generate particle aggregates.
  • this production method by dissolving a metal compound, a reducing agent, a complexing agent, and a dispersant, a first step of preparing an aqueous solution containing metal ions derived from the metal compound, and adjusting the pH of the aqueous solution And a second step of reducing metal ions with a reducing agent and precipitating the metal powder.
  • this production method is expensive using an expensive chemical and is not economically advantageous when applied to a process that operates on a large scale as the nickel smelting.
  • the object is to provide a production method for producing coarse particles.
  • the first invention of the present invention for solving the above-mentioned problems is characterized in that in the production process for producing nickel powder from a nickel sulfate solution, the following treatment steps (1) to (4) are performed. It is a manufacturing method of powder.
  • a hydroxylation step in which an alkali is added to a nickel sulfate solution to form a nickel hydroxide precipitate.
  • a reduction final solution obtained from the solid-liquid separation step (4) and nickel powder as seed crystals are added, and the hydroxylation is performed.
  • the nickel powder recovered in the solid-liquid separation step (4) according to the first aspect is sieved according to particle size, and nickel powder having a particle size smaller than a preset particle size is used as a seed crystal.
  • a nickel powder production method characterized by obtaining a nickel powder coarser than the grain size of the seed crystal nickel powder by repeatedly adding to either or both of the crystallization step (2) and the reduction step (3) It is.
  • the average particle size of the seed crystals added to either or both of the complexing step (2) and the reduction step (3) in the second invention is as large as 0.1 to 100 ⁇ m. This is a method for producing nickel powder.
  • the complexing step (2) in the first to third aspects forms a mixed slurry containing a nickel sulfate ammine complex solution, a seed crystal and nickel hydroxide
  • the mixed slurry further comprises adding a dispersant to the nickel powder production method.
  • the amount of the seed crystal added in the complexing step (2) in the first to fourth aspects is 1 to 100% with respect to the weight of nickel in the nickel sulfate ammine complex solution. It is a manufacturing method of nickel powder characterized by being.
  • the reducing slurry according to the first to fifth aspects is sieved, and the under-sieving nickel powder and the reducing end solution under-sieving reduced slurry are combined in the complexing step (2).
  • It is a nickel powder manufacturing method characterized by being repeatedly used as part of a liquid and seed crystal nickel powder.
  • the complexing step (2) in the sixth aspect comprises a dissolution step of adding a reduction final solution to obtain a nickel sulfate ammine complex solution, a nickel powder or nickel powder and a reduction final solution. It is the manufacturing method of nickel powder characterized by being comprised by two processes of the seed crystal addition process which adds the mixed slurry containing.
  • the nickel sulfate solution in the first aspect is a mixed sulfide, nickel sulfide, crude nickel sulfate, nickel oxide, nickel hydroxide of nickel and cobalt recovered by leaching nickel oxide ore.
  • a nickel powder production method characterized in that it is obtained by dissolving at least one of nickel carbonate and metal nickel powder in an acidic sulfuric acid solution.
  • the nickel sulfate solution according to the first aspect is a leaching step for dissolving a nickel-containing material containing cobalt as an impurity, and the pH of the leaching solution containing nickel and cobalt obtained in the leaching step is adjusted.
  • the nickel powder solution is a nickel sulfate solution obtained through a solvent extraction step of separating into a nickel sulfate solution and a cobalt recovery solution by a solvent extraction method.
  • the ammonium sulfate concentration in the nickel sulfate ammine complex solution in the first invention is 100 to 500 g / L, and the ammonium concentration is 1 in molar ratio to the nickel concentration in the complex solution. It is a manufacturing method of nickel powder characterized by being 9 or more.
  • the hydrogen gas blowing in the reduction step (3) in the first aspect is performed while maintaining the temperature at 100 to 200 ° C. and the pressure within the range of 0.8 to 4.0 MPa. This is a method for producing nickel powder.
  • the twelfth invention of the present invention is a nickel powder manufacturing method, wherein the dispersant according to the fourth invention contains a polyacrylate.
  • the thirteenth invention of the present invention is a nickel dust ore step for processing the nickel powder obtained through the reduction step (3) in the first invention into a massive nickel briquette using a briquetting machine.
  • a nickel powder characterized by including a briquette sintering step in which a massive nickel briquette is sintered under a holding condition at a temperature of 500 to 1200 ° C. in a hydrogen atmosphere to form a sintered nickel briquette It is a manufacturing method.
  • the fourteenth invention of the present invention includes an ammonium sulfate recovery step of concentrating the reduction final solution of the solid-liquid separation step (4) in the first invention and crystallizing ammonium sulfate to recover ammonium sulfate crystals. It is a manufacturing method of nickel powder.
  • the fifteenth aspect of the present invention includes an ammonia recovery step in which an alkali is added to the final reduction liquid in the solid-liquid separation step (4) in the first invention and heated to volatilize and recover the ammonia gas. It is a manufacturing method of nickel powder.
  • the production method for obtaining nickel powder from a nickel sulfate ammine complex solution by applying the steps shown in the following (1) to (4) to the process liquid of the hydrometallurgical process, It is characterized by producing high-purity nickel powder with few impurities.
  • the leaching step is a starting material, such as nickel or cobalt mixed sulfide, crude nickel sulfate, nickel oxide, nickel hydroxide, nickel carbonate, nickel powder, industrial intermediate made of one or more mixtures, etc.
  • a known method disclosed in Japanese Patent Application Laid-Open No. 2005-350766 is used. Done.
  • (1) Hydroxidation Step an alkali is added to the nickel sulfate solution obtained through the above-described steps to produce a nickel hydroxide precipitate, and the solid component precipitate and the liquid component are separated.
  • the alkali to be added it is preferable to use an industrially inexpensive one that can be procured in large quantities, such as sodium hydroxide and calcium hydroxide.
  • This complexation step is specifically composed of two steps, a dissolution step and a seed crystal addition step.
  • the dissolution step (1) the precipitate nickel hydroxide obtained in the hydroxylation step is converted into nickel hydroxide.
  • a nickel sulfate ammine complex which is a nickel ammine complex is formed by performing a heat treatment, and a nickel sulfate ammine complex solution is formed.
  • ammonia gas or aqueous ammonia can be added to adjust the ammonium concentration.
  • ammonia is added so that the ammonium concentration is 1.9 or more in molar ratio with respect to the nickel concentration in the solution.
  • the ammonium concentration of the ammonia to be added is less than 1.9, nickel does not form an ammine complex, and nickel hydroxide precipitates are generated.
  • ammonium sulfate can be added in this step.
  • the ammonium sulfate concentration at this time is preferably 100 to 500 g / L, and if it is 500 g / L or more, the solubility is exceeded, crystals are precipitated, and it is difficult to achieve less than 100 g / L because of the metal balance of the process. .
  • ammonia gas or ammonia water produced in the ammonia recovery step described later can also be used for ammonia gas or ammonia water used in this step.
  • nickel powder having an average particle size of 0.1 to 5 ⁇ m is added as a seed crystal in the form of a nickel powder slurry to the resulting nickel sulfate ammine complex solution.
  • a seed crystal addition step for forming a mixed slurry containing nickel hydroxide is performed.
  • the weight of the seed crystal added at this time is preferably 1 to 100% with respect to the weight of nickel in the nickel sulfate ammine complex solution. If it is less than 1%, the reaction efficiency at the time of reduction in the next step will be significantly reduced. On the other hand, if it is 100% or more, the amount used is large, and the seed crystal production costs high, which is not economical.
  • the dispersant used here is not particularly limited as long as it has a sulfonate, but lignin sulfonate is preferred as it can be obtained industrially at low cost.
  • Reduction step In this step, hydrogen gas is blown into the obtained mixed slurry to reduce the nickel component in the solution and form a reduced slurry containing nickel powder formed by precipitation on the seed crystal.
  • the reaction temperature is preferably 100 to 200 ° C. When the temperature is less than 100 ° C., more preferably less than 150 ° C., the reduction efficiency is lowered.
  • the pressure during the reaction is preferably 0.8 to 4.0 MPa. If it is less than 0.8 MPa, the reaction efficiency decreases, and even if it exceeds 4.0 MPa, the reaction is not affected and the loss of hydrogen gas increases.
  • magnesium ions, sodium ions, calcium ions, sulfate ions, and ammonium ions are mainly present as impurities, but all of them remain in the solution. Can be generated.
  • nickel hydroxide in the mixed slurry reacts with ammonium ions produced by the reduction reaction, dissolves as a nickel ammine complex in the solution, is reduced by reacting with hydrogen gas, and nickel is deposited on the seed crystal. To do.
  • the recovered high-purity nickel powder with few impurities is reduced in diameter by pulverization or the like, and is repeatedly supplied to the (2) complexing step as a seed crystal. Furthermore, (2) nickel sulfate is added to the nickel sulfate ammine complex solution obtained in the complexing step, and (3) nickel is further reduced and deposited on the high-purity nickel powder by supplying hydrogen gas in the reduction step. Therefore, the particles can be grown. Further, by repeating the supply to the reduction step a plurality of times, it is possible to produce high-purity nickel powder having a higher bulk density and a larger particle size. Furthermore, the obtained high-purity nickel powder may be finished into a briquette shape that is coarser, less oxidizable, and easy to handle through the following nickel powder ore step and briquette firing step. Further, an ammonia recovery step may be provided.
  • the high-purity nickel powder produced according to the present invention is molded into a product form after drying using a briquetting machine or the like to obtain a massive nickel briquette.
  • a substance that does not contaminate the product quality such as water may be added to the nickel powder as a binder.
  • the nickel briquette produced in the briquetting process is roasted and sintered in a hydrogen atmosphere to produce a briquette sintered body.
  • This treatment increases strength and removes trace amounts of ammonia and sulfur components, and the roasting and sintering temperature is preferably 500 to 1200 ° C. If it is less than 500 degreeC, sintering will become inadequate and even if it exceeds 1200 degreeC, efficiency will hardly change and the loss of energy will become large.
  • ammonium sulfate recovery process (3) Separating nickel powder as a solid phase after the reduction step (4)
  • the reduction final solution generated by the solid-liquid separation step contains ammonium sulfate and ammonia. Therefore, ammonium sulfate can be recovered as ammonium sulfate crystals by subjecting the solution after the reaction to heat concentration to crystallize ammonium sulfate by performing an ammonium sulfate recovery step.
  • ammonia recovery process In addition, ammonia can be recovered by volatilizing ammonia gas by adding alkali to the final reduction solution and adjusting the pH to 10 to 13 and then heating.
  • the alkali used here is not particularly limited, but caustic soda, slaked lime and the like are industrially inexpensive and suitable.
  • the recovered ammonia gas can be brought into contact with water to generate ammonia water, and the obtained ammonia water can be used repeatedly in the process.
  • nickel hydroxide By adding 800 ml of slaked lime adjusted to a slurry concentration of 200 g / L to 1000 ml of nickel sulfate solution having a nickel concentration of 120 g / L, 116 g of nickel hydroxide was obtained.
  • the nickel hydroxide was added to 1700 ml of a mixed solution of nickel sulfate solution having a nickel concentration of 30 g / L and ammonium sulfate solution having an ammonia concentration of 40 g / L together with 12.8 g of nickel powder having an average particle diameter of 2 ⁇ m as a seed crystal, and stirred. A mixed slurry was prepared.
  • Example 1 Using the reduction final solution obtained in the solid-liquid separation step of Example 1 as a part of the ammonia source, a mixed slurry is prepared, subjected to the reduction step under the same conditions as in Example 1, and after passing through the solid-liquid separation step, The grown nickel powder was collected. The same nickel powder as in Example 1 was recovered.
  • the nickel powder prepared under the same conditions as in Example 1 was added to a solution containing 336 g of nickel sulfate and 330 g of ammonium sulfate. Through the reduction process and solid-liquid separation process under the same conditions as in Example 1, grain-grown nickel powder was produced. Using this produced nickel powder, the same operation was repeated 10 times to grow nickel powder. The average particle diameter of the collected nickel powder was 111 ⁇ m, which was 1.7 times larger than that of the nickel powder of Example 1.
  • the sulfur quality in the nickel powder obtained by this repeated operation was 0.04%. Further, sodium and magnesium were below the lower limit of quantification as in Table 1. Furthermore, the obtained nickel powder was heated to 1000 ° C. in a 2% hydrogen atmosphere and held for 60 minutes. The sulfur grade in the obtained nickel powder after holding was 0.008%, and the sulfur grade could be further reduced by roasting.
  • nickel sulfate ammine solution prepared by mixing 135 g of nickel sulfate hexahydrate, 191 ml of 25% aqueous ammonia, 169 g of ammonium sulfate and pure water, 75 g of nickel hydroxide was added, and pure water was added so that the liquid volume became 1000 ml. Then, 15 g of nickel powder having an average particle diameter of 1 ⁇ m was added as a seed crystal to prepare a mixed slurry.
  • the mixed slurry was heated to 100 ° C. while being stirred in an autoclave, and hydrogen powder was supplied so that the pressure in the autoclave was 3.5 MPa to perform nickel powder generation treatment.
  • One hour after the supply of hydrogen gas the supply of hydrogen gas was stopped and the autoclave was cooled.
  • the reduced slurry obtained after cooling was subjected to solid-liquid separation treatment by filtration to recover high-purity small-diameter nickel powder.
  • the nickel reduction rate at this time was 58%.
  • Example 6 Using the same mixed slurry as in Example 6, the same operation as in Example 6 was performed under the conditions of a temperature of 100 ° C. and a pressure in the autoclave of 0.8 MPa. The nickel reduction rate at this time was 56%.
  • Example 6 Using the same mixed slurry as in Example 6, the same operation as in Example 6 was performed under the conditions of a temperature of 120 ° C. and a pressure in the autoclave of 3.5 MPa. The nickel reduction rate at this time was 74%.
  • Example 6 Using the same mixed slurry as in Example 6, the same operation as in Example 6 was performed under the conditions of a temperature of 120 ° C. and a pressure in the autoclave of 2.0 MPa. The nickel reduction rate at this time was 74%.
  • Example 6 Using the same mixed slurry as in Example 6, the same operation as in Example 6 was performed under the conditions of a temperature of 120 ° C. and a pressure in the autoclave of 1.5 MPa. The nickel reduction rate at this time was 74%.
  • Example 1 A solution prepared by adding 191 ml of 25% aqueous ammonia to a solution containing nickel sulfate 75 g containing nickel 75 g and ammonium sulfate 330 g without performing the hydroxylation step in Example 1 so that the total liquid volume becomes 1000 ml.
  • nickel powder was prepared under the same conditions as in Example 1 except that 7.5 g was added as a seed crystal of nickel powder having an average particle diameter of 1 ⁇ m to prepare a mixed slurry. After the recovered nickel powder was washed with pure water, the impurity quality of the nickel powder was analyzed. The results are shown in Table 4. The mixing of Mg and Na into the nickel powder resulted in more results than in Example 1. The average particle diameter and the recovered amount were almost the same as in Example 1.
  • Comparative Example 2 Using the same method as in Comparative Example 1, nickel powder was produced without performing a hydroxylation step. This nickel powder was repeated 10 times in the same manner as in Example 3 to grow grains. The sulfur quality in the nickel powder obtained by this repetitive operation was 0.1%, and it was not possible to obtain a high-purity nickel powder having a sulfur quality of about 0.04% obtained in Example 3 of the present invention. .

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Geochemistry & Mineralogy (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Manufacture Of Metal Powder And Suspensions Thereof (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

L'invention concerne un procédé de production d'une poudre de nickel dite de grande pureté, constituée de grosses particules et dont la teneur en impuretés est réduite, en particulier la teneur en soufre, ladite poudre de nickel étant produite à partir d'une solution de complexe d'ammine de sulfate de nickel à l'aide d'une fine poudre de nickel. Ce procédé sert à produire une poudre de nickel à partir d'une solution de sulfate de nickel, et est caractérisé par la mise en oeuvre des étapes de traitement (1) à (4) suivantes : (1) une étape d'hydroxylation, dans laquelle un sédiment d'hydroxyde de nickel est produit ; (2) une étape de complexation, dans laquelle une suspension mixte comprenant une solution de complexe d'ammine de sulfate de nickel, des cristaux d'ensemencement et l'hydroxyde de nickel est formée ; (3) une étape de réduction, dans laquelle une suspension de réduction contenant une poudre de nickel formée par le dépôt d'une matière de nickel sur les cristaux d'ensemencement est formée ; et (4) une étape de séparation solide-liquide dans laquelle la suspension de réduction formée à l'étape de réduction (3) est soumise à une séparation solide-liquide pour récupérer la poudre de nickel et un liquide de fin de réduction.
PCT/JP2016/074694 2015-08-31 2016-08-24 Procédé de fabrication d'une poudre de nickel WO2017038589A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
AU2016314002A AU2016314002B2 (en) 2015-08-31 2016-08-24 Process for producing nickel powder
US15/755,147 US20180250752A1 (en) 2015-08-31 2016-08-24 Method for producing nickel powder
CN201680049552.9A CN107921544A (zh) 2015-08-31 2016-08-24 镍粉的制造方法
CA2996277A CA2996277C (fr) 2015-08-31 2016-08-24 Procede de fabrication d'une poudre de nickel
EP16841621.2A EP3345701A4 (fr) 2015-08-31 2016-08-24 Procédé de fabrication d'une poudre de nickel
PH12018500435A PH12018500435A1 (en) 2015-08-31 2018-02-28 Method for producing nickel powder

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
JP2015170115 2015-08-31
JP2015-170115 2015-08-31
JP2016-032519 2016-02-23
JP2016032519 2016-02-23
JP2016-100070 2016-05-19
JP2016100070A JP6610425B2 (ja) 2015-08-31 2016-05-19 ニッケル粉の製造方法

Publications (1)

Publication Number Publication Date
WO2017038589A1 true WO2017038589A1 (fr) 2017-03-09

Family

ID=58187350

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2016/074694 WO2017038589A1 (fr) 2015-08-31 2016-08-24 Procédé de fabrication d'une poudre de nickel

Country Status (1)

Country Link
WO (1) WO2017038589A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2018178232A (ja) * 2017-04-20 2018-11-15 住友金属鉱山株式会社 ニッケル粉の製造方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2003147570A (ja) * 2001-11-08 2003-05-21 Sumitomo Electric Ind Ltd 微細金属部品の製造方法
JP2005194156A (ja) * 2004-01-09 2005-07-21 Ishikawajima Harima Heavy Ind Co Ltd 水酸化ニッケル粉末の製造方法
JP2015140480A (ja) * 2014-01-30 2015-08-03 国立大学法人高知大学 ニッケル粉の製造方法

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2003147570A (ja) * 2001-11-08 2003-05-21 Sumitomo Electric Ind Ltd 微細金属部品の製造方法
JP2005194156A (ja) * 2004-01-09 2005-07-21 Ishikawajima Harima Heavy Ind Co Ltd 水酸化ニッケル粉末の製造方法
JP2015140480A (ja) * 2014-01-30 2015-08-03 国立大学法人高知大学 ニッケル粉の製造方法

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP3345701A4 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2018178232A (ja) * 2017-04-20 2018-11-15 住友金属鉱山株式会社 ニッケル粉の製造方法

Similar Documents

Publication Publication Date Title
JP5828923B2 (ja) ニッケル粉の製造方法
JP6610425B2 (ja) ニッケル粉の製造方法
JP2017150063A5 (fr)
CA2980440C (fr) Procede de production de poudre de cobalt
AU2017223933B2 (en) Method for producing nickel powder
JP2017150002A5 (fr)
JP6531913B2 (ja) ニッケル粉の製造方法
WO2017038589A1 (fr) Procédé de fabrication d'une poudre de nickel
JP6624464B2 (ja) ニッケル粉の製造方法
JP2019065345A (ja) ニッケル粉の製造方法
WO2020183728A1 (fr) Procédé de production de poudre de nickel

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 16841621

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
ENP Entry into the national phase

Ref document number: 2996277

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 15755147

Country of ref document: US

WWE Wipo information: entry into national phase

Ref document number: 12018500435

Country of ref document: PH

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2016314002

Country of ref document: AU

Date of ref document: 20160824

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 2016841621

Country of ref document: EP