KR100981413B1 - Method for manufacturing spherical high purity nickel powder - Google Patents

Abstract

PURPOSE: A method for manufacturing spherical high purity Nickel powder is provided to reduce the manufacturing cost by using only a small amount of hydrogen as a reducing agent or a chip reducing agent instead of hydrogen. CONSTITUTION: A method for manufacturing spherical high purity Nickel powder comprises the steps of: mixing urea or ammonium hydroxide reducing agent into Nickel sulfate solvent extract; producing the reductant mixture into liquid droplets; putting the liquid droplets together with a carrier gas into a reactor; subjecting the liquid droplet mixture to evaporation, drying, and pyrolysis; and washing and drying the resultant material. In the reducing agent mixing step, urea is mixed in the nickel sulfate solvent extract at a volume ratio of 1:1~1:3.

Description

Method for manufacturing spherical high purity Nickel powder

The present invention relates to a method for producing a spherical high purity nickel metal powder from a mineral product. More specifically, the nickel sulfate solvent extract obtained after leaching from a mineral product and solvent extraction is reduced by using a reducing agent without hydrogen to form spherical high purity nickel metal powder. It relates to a production method for producing a metal powder.

In the age of fierce international competition, the international competitiveness of semiconductors, steel, automobiles, and ships, such as the basic industries, is strengthening, but the material industry, which is the core of these industries, is much weaker than the US and Japan.

In particular, the metal material industry should be developed into a higher value-added industry, but in Korea, many metal materials depend on imports. Particularly, fine powders are used for materials that require excellent physical properties and functionality such as superconducting materials, amorphous alloys, electronic materials, and nanomaterials, which have made much progress in recent material development trends. The demand for is increasing rapidly.

Among these, nickel metal powder has attracted attention as a material for forming hollow porous electrodes of fuel cells, internal electrodes of multilayer ceramic capacitors, porous electrodes of batteries, and electrodes of various electronic components. In this field, in order for nickel metal fine powder to have good characteristics, it is necessary to have a uniform size distribution between submicrons and microns, and in order to increase the dispersibility of the powder, it is important that the metal powder has a spherical shape.

On the other hand, the metal powder is prepared by mechanical grinding of metals, reduction of liquid compounds, electrolysis of compounds, spray pyrolysis, and the like. In the mechanical grinding method, impurities may be mixed during grinding, and the reduction method of the liquid compound shows agglomeration, difficult to control the shape, and has a disadvantage of being a multi-process (precipitation, drying, filtration, sintering) process.

The conventional spray pyrolysis is a method of preparing metal powder by reducing with hydrogen, which is a reducing gas, in a high temperature reactor. This sprays a solution of the appropriate concentration of the solute in the form of droplets and loads it in a carrier gas and transfers it to the reactor, where hydrogen, which is required, is introduced at an appropriate position. The reactor is mainly a tubular reactor, which is externally heated by an electric furnace. In the reactor, the solute is dried together with the evaporation of the solvent and the reaction with the reaction gas occurs continuously.

In the spray pyrolysis method, the droplet-to-metal powder particles change only in the droplets of the solution, and thus each droplet serves as a microreactor. Can be.

In the case of manufacturing nickel metal powder, which is important as a basic raw material for electronic parts by using this conventional spray pyrolysis method, hydrogen is mostly used for reduction, but it is economical and safe in mass production due to high price and risk of explosion. There is a problem.

In order to solve the above problems, an object of the present invention is to provide a method for producing a spherical high purity nickel metal powder having a uniform particle size in a short reaction time by reducing using a reducing agent by spray pyrolysis.

Another object of the present invention is to provide a method for producing spherical high purity nickel metal powder using inexpensive minerals as a starting material using little hydrogen as a reducing agent or a cheap reducing agent without hydrogen.

Still another object of the present invention is to provide a method for producing a spherical high purity nickel metal powder, which can produce a large amount of nickel powder, and low cost.

In order to achieve the above object, the present invention provides a spherical nickel metal powder manufacturing method comprising: a reducing agent mixing step of mixing a urea (Urea) reducing agent in 6 g / L to 60 g / L nickel sulfate solvent extract; A droplet forming step of generating the reducing agent mixture in a droplet state by an ultrasonic apparatus; A reactor input step of introducing the generated droplets into the reactor together with a carrier gas; A particle conversion step of evaporating, drying, and pyrolysing the mixture in the droplet state introduced into the reactor; And it provides a spherical high purity nickel metal powder manufacturing method comprising a powder forming step of washing and drying the evaporated, dried and pyrolytically reacted material.

In another aspect, the present invention provides a spherical high-purity nickel metal powder manufacturing method, characterized in that the concentration of the urea (Urea) in the reducing agent mixing step is 3M to 7M.

In addition, the present invention is the amount of the urea (Urea) reducing agent is mixed in the reducing agent mixing step is urea (Urea) of the spherical high purity nickel metal, characterized in that mixed in a volume ratio of 1: 1 to 1: 3 It provides a powder manufacturing method.

In another aspect, the present invention provides a spherical high purity nickel metal powder manufacturing method characterized in that the carrier gas carried to the reactor in the droplet forming step is argon (Ar).

In another aspect, the present invention is the carrier gas transported to the reactor in the droplet formation step of producing a spherical high purity nickel metal powder, characterized in that the mixture of hydrogen (H ₂ ) and argon (Ar) in a volume ratio of 15:85 to 1:99. Provide a method.

In another aspect, the present invention provides a method for producing a spherical high purity nickel metal powder, characterized in that the droplet is processed at a rate of 1 to 7 L / min in the reactor input step.

In another aspect, the present invention provides a method for producing a spherical high purity nickel metal powder, characterized in that the thermal decomposition reaction is carried out at 1000 ℃ to 1400 ℃ during the particle conversion step in the droplets.

The spherical nickel metal powder manufacturing method according to the present invention has the effect of providing a spherical high purity nickel metal powder having a uniform spherical particle size in a short reaction time by spray pyrolysis.

In addition, the method for producing spherical nickel metal powder according to the present invention has the effect of significantly reducing the production cost when producing spherical nickel metal powder by using little expensive hydrogen as a reducing agent or using urea, which is a cheap reducing agent without hydrogen. There is.

In addition, the spherical high purity nickel metal powder production method according to the present invention has the effect of producing a large amount of high purity nickel metal powder.

DETAILED DESCRIPTION Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings. First, it should be noted that in the drawings, the same components or parts denote the same reference numerals as much as possible. In describing the present invention, detailed descriptions of related well-known functions or configurations are omitted in order not to obscure the subject matter of the present invention.

The terms "about "," substantially ", etc. used to the extent that they are used herein are intended to be taken to mean an approximation of, or approximation to, the numerical values of manufacturing and material tolerances inherent in the meanings mentioned, Accurate or absolute numbers are used to help prevent unauthorized exploitation by unauthorized intruders of the referenced disclosure.

The present invention is a method for producing a spherical nickel metal powder from the nickel sulfate sulfate extract containing nickel by spray pyrolysis, Urea can be used as a reducing agent for the reduction. The urea (Urea) plays a role in allowing the nickel sulfate solvent extract to be directly involved in causing a reduction reaction to be made of nickel metal powder.

1 is a manufacturing process diagram of the nickel metal powder particles according to an embodiment of the present invention, Figure 2 is a block diagram of a pyrolysis apparatus for producing a nickel metal powder according to an embodiment of the present invention.

Spherical nickel metal powder production method according to a preferred embodiment of the present invention comprises a reducing agent mixing step of mixing a urea (Urea) reducing agent in the nickel sulfate solvent extract; A droplet forming step of generating the reducing agent mixture in a droplet state by an ultrasonic apparatus; A reactor input step of introducing the generated droplets into the reactor together with a carrier gas; A particle conversion step of evaporating, drying, and pyrolysing the mixture in the droplet state introduced into the reactor; And spherical high purity nickel metal powder is prepared through a powder forming step of washing and drying the evaporated, dried and pyrolyzed materials.

In the present invention, a nickel sulfate solvent extract is used to obtain a nickel metal powder, and the particle size of the finally produced spherical nickel metal powder varies depending on the concentration of the nickel sulfate solvent extract. That is, when the nickel sulfate solvent extract is high concentration, the particle size is increased, and when the nickel sulfate solvent extract is low concentration, the particle size is characterized. The concentration of the nickel sulfate solvent extract is preferably 6g / L to 60 g / L. Spherical nickel metal powder particles are formed evenly within the above range. When the concentration of the liquid is less than 6g / L concentration is too low to cause problems in the production per hour, when the concentration of the liquid exceeds 60 g / L spraying is not made smoothly not only productivity problems but also the size of the particles very Since it becomes large, it is preferable that it is the said range of 6g / L-60g / L.

Therefore, by adjusting the concentration of the nickel sulfate solvent extract it can be produced by adjusting the particle size of the spherical nickel metal powder to the desired size.

In addition, it is preferable to use urea (Urea) as the reducing agent in the reducing agent mixing step. When the reducing agent urea (Urea) is mixed, by directly involved in the reduction reaction, the nickel sulfate solution can be reduced with little or no hydrogen in the course of the reaction so that nickel metal can be produced as a result. do. This is an advantage that can significantly reduce the production cost by eliminating or saving the use of expensive hydrogen.

In the urea (Urea) which is the reducing agent, the concentration to be mixed is preferably 3 to 7M. Pure nickel metal powder can be obtained within the above range, and a nickel metal powder having a constant particle size and sphericity can be prepared. When the concentration is less than 3M, pure nickel is not easily produced, and mainly nickel oxide (NiO) is produced. When the concentration exceeds 7M, the manufacturing cost increases, and it is preferable that it is 3 to 7M.

3 to 5 are shown by electron micrographs of the particle powder prepared by adjusting the concentration of the urea (Urea) reducing agent according to an embodiment of the present invention. Figure 6 shows the X-ray diffraction analysis of the particles prepared by adjusting the concentration of the urea (Urea) reducing agent according to an embodiment of the present invention.

3 to 5 show photographs of nickel metal powders prepared by using a concentration of urea (Urea) of 1M, 3M, and 7M, respectively, when the concentration of the nickel sulfate solvent is 12 g / L at a pyrolysis temperature of 1000 ° C. Referring to Figure 3, when urea (Urea) 1M, it can be seen that the size of the nickel particles is uneven and there are many aggregated particles in the shape as well. In contrast, it can be observed that nickel particles made of 3M and 7M have a uniform surface and almost constant particle size and sphericity.

6 is an X-ray diffraction analysis of the particle powder prepared by reducing the concentration of urea (Urea) from 1M to 7M, the concentration of the nickel sulfate solvent extraction solution at a thermal decomposition temperature of 1000 ℃ 12g / L, urea Particle powder produced when the concentration of (Urea) is 1M, it can be seen that the nickel oxide is produced rather than the nickel metal powder is formed. On the other hand, when the concentration of urea (Urea) is 3M, 4M, 5M, 6M, 7M, respectively, it can be confirmed that the nickel metal powder is produced, it is preferable to set it to 3M to 7M.

Table 1 below is an energy dispersive spectroscopy (EDS) result of the powder produced according to the concentration change of urea (Urea) according to an embodiment of the present invention.

density Ni wt (%) S wt (%) O wt (%) 1M 78.83 - 21.17 2M 97.63 2.37 - 3M 99.11 0.89 - 4M 98.90 1.10 - 5M 99.66 0.34 -

Referring to [Table 1], when the urea concentration is 1M, when the produced material is analyzed by an energy dispersive spectroscopy (EDS), about 79% by weight of nickel (Ni) and about 21% by weight of oxygen (O) It was confirmed that the conversion to the oxide, X-ray diffraction also confirms the analysis results. In contrast, when the urea concentration was 3M or higher, nickel (Ni) showed a weight% of about 97.63 to 99.66. Therefore, it can be confirmed that high purity nickel metal powder can be obtained when urea (Urea) is used as the reducing agent in the sulfuric acid solvent extract more than 3M.

In addition, the amount of the urea (Urea) is mixed in the reducing agent mixing step may be mixed in the volume ratio of urea (Urea) 1: 1 to 1: 3 in the nickel sulfate solvent extract. Pure nickel metal powder can be obtained within the above range.

When the urea (Urea) is a volume ratio of 1: 1 to 1: 3 with respect to the nickel sulfate solvent extract of 12g / L it can be observed that only the nickel metal powder is present, the nickel sulfate solvent extract and urea (Urea) If the volume ratio exceeds 1: 3, a problem occurs that other materials coexist in addition to pure nickel. Therefore, it is preferable that the volume ratio of the nickel sulfate solvent extract and the urea (Urea) reducing agent is mixed at 1: 1 to 1: 3.

Meanwhile, in the production of nickel metal powder, a carrier gas is also an important factor for powder formation. In the present invention, an inert gas of argon (Ar) is used. In addition, hydrogen (H ₂ ) and argon (Ar) may be mixed and used as a carrier gas, and the amount of the mixture may be used by mixing hydrogen (H ₂ ) and argon (Ar) in a volume ratio of 15:85 to 1:99. It is desirable to. The hydrogen (H ₂ ) may serve as a reducing agent for reduction, and may additionally serve as a reducing agent of urea (Urea) mixed in the reducing agent mixing step. Accordingly, there is an advantage that the reaction temperature can be lowered as compared with not adding hydrogen (H ₂ ) when the reaction occurs. However, although hydrogen (H ₂ ) is mainly used as a carrier gas for reduction, it is expensive and there is a risk of explosion when a large amount is used. Therefore, in the present invention, it is possible to reduce without using hydrogen, and even in the case of using hydrogen (H ₂ ), it is preferable to use it in a small amount and mix with argon, and the amount of hydrogen used is hydrogen in the above range (H ₂ ) and argon (Ar) are preferably used by mixing in a volume ratio of 15:85 to 1:99.

In addition, the treatment rate of the reducing agent mixture in the tubular reactor 500 may be treated at 1 to 7 L / min. When treated at a rate of less than 1 L / min has the advantage that the particles can be sufficiently treated in the reactor, but the production speed is low, there may be a problem in productivity. In addition, when the process proceeds at a rate exceeding 7 L / min, there is a problem that the mixed droplets can not properly perform the treatment, such as drying. The flow rate of the carrier gas is highly correlated with the residence time of the droplets in the reactor. When the flow rate of the carrier gas exceeds 7L / min, it can be seen that the particles are largely crushed or large particles appear. This is because when the flow rate of the carrier gas in the reactor is high, the liquid droplet stays in the chamber for a short time. As a result, the droplets appear to occur due to insufficient evaporation, drying and pyrolysis in the reactor or overlapping. In addition, an electric furnace 600 is formed around the reactor 500 to provide respective suitable heat to the reactor partitioned into the first to third chambers.

The reducing agent mixture in which the nickel sulfate solvent extract and the urea reducing agent are mixed is converted into droplets under the influence of a specific frequency band (1.67 MHz) formed in the ultrasonic generator 400. Various attempts can be made to increase the amount of droplets generated, such as ultrasonic nozzles and two-fluid spraying methods. However, the above methods do not have a great advantage in terms of yield because the size of the droplets produced is so large that the concentration of the starting material should be relatively low in order to obtain particles of a small size. Therefore, ultrasonic spraying capable of generating droplets within 5 to 20 μm may be desirable. On the other hand, the carrier gas supply unit 100 in which a carrier gas of argon (Ar) is stored to the left side of the ultrasonic generator 400 to transport the mixture in the droplet state into the high temperature tubular reactor 500 is connected to the flow meter 200.

The conveyed mixture is converted into particles through evaporation, drying and pyrolysis in the tubular reactor 500. The mixture and the carrier gas flow into the reactor 500, and are made of a quartz concentric tube. The reactor 500 may be composed of three chambers suitable for evaporation, drying, and pyrolysis conditions. Preferably, the reactor 500 does not overlap evaporation, drying, and pyrolysis in the first chamber 510, the second chamber 520, and the third chamber 530, respectively. It can be done sequentially without.

As the preferred temperature of the chamber in the reactor, the first chamber 510 may be treated with 100 to 500 ° C., the second chamber 520 with 600 to 900 ° C., and the third chamber 530 with 1000 ° C. to 1400 ° C. to be evaporated, dried, and pyrolyzed. .

In particular, temperature control is important to obtain nickel metal powder when pyrolysis occurs in the third chamber 530. Preferably, the temperature in the third chamber 530, which is a reactor, is 1000 to 1400 ° C. If the temperature is less than 1000 ℃, more nickel oxide is produced than nickel metal, and the production of nickel metal powder may occur well above 1400 ℃, but there is no remarkable difference from the above range of 1000 ℃ to 1400 ℃ and the production cost There is a problem that only rises. Analyzing the product prepared according to an embodiment of the present invention, when the pyrolysis temperature is 1000 ℃ to 1400 ℃, it can be seen that the nickel represents 96 to 98% by weight. However, when the material was analyzed at a decomposition temperature of about 800 ° C., it was confirmed that nickel represented 82 to 88 wt% and other impurities were mixed. Therefore, the reaction temperature at the time of pyrolysis is preferably 1000 ℃ to 1400 ℃.

7 to 10 show X-ray diffraction analysis and electron micrographs according to pyrolysis temperature of nickel powder prepared according to an embodiment of the present invention.

7 to 9 shows that when the concentration of the nickel sulfate solvent extract is 12 g / L, the concentration of urea (Urea) is 4M and the sulfuric acid solvent extract and the urea (Urea) are mixed in the same volume, and the pyrolysis temperature is 800 ° C., 1000. Electron micrograph of the nickel metal powder prepared by changing to ℃ and 1200 ℃ and Figure 10 shows the X-ray diffraction results of pyrolysis temperature at 800 ℃, 1000 ℃, 1200 ℃ and 1400 ℃ for the prepared nickel metal powder It is shown.

7 to 9, the particles are large and uneven at 800 ° C. at a relatively low temperature of pyrolysis, but above 1000 ° C., the particles are small in size, have a uniform spherical shape, and have a very good surface state. You can check it.

[Table 2] below is an energy dispersive spectroscopy (EDS) result of the powder produced according to the temperature change according to the embodiment of the present invention.

Temperature Ni wt (%) S wt (%) O wt (%) 800 ℃ 60.01 - 39.99 1000 ℃ 100 - - 1200 ℃ 92.96 7.04 - 1400 ℃ 94.05 5.95 -

Referring to FIG. 10 and [Table 2], it can be seen that nickel oxide is produced rather than nickel metal at a pyrolysis temperature of 800 ° C. Analysis of the resulting powder with an energy dispersive spectroscopy showed that the pyrolysis temperature was about 60 wt% nickel (Ni) and about 40 wt% oxygen (O) at 800 ° C. Nickel metal powders were obtained, and the energy dispersion spectroscopy analysis showed that nickel (Ni) was about 100% by weight. S appears when the pyrolysis temperature rises to 1200 ° C and 1400 ° C. Specifically, the sulfur (S) component is found to be 5.95 to 7.04%. X-ray diffraction also shows that the pure nickel phase only at 1000 ℃ and a small amount of oxides and impurities at other temperatures, the thermal decomposition temperature is about 1000 ℃ is the most preferred.

Meanwhile, the droplet mixture is converted into nickel particles and filtered, which is processed by a collecting device 700 formed at the end of the reactor 500, and the collecting device 700 is connected to a Pyrex cup holder. ring is inserted. In order to collect the particles reacted in the reactor, filter paper (Advantec, 5C) having a pore size of 1 μm and a diameter of 9 cm is used. In order to make a filter device for the use of filter paper, the flow rate of the aerosol containing particles can be lowered to increase the collection efficiency and lower the pressure drop, but the temperature drop is severe, which increases the risk of water condensation. In order to prevent this, the condensation of water is removed by external heating to increase the collection efficiency.

In addition, the prepared particles are washed 1-5 times in a magnetic stirrer with deionized water, and then obtained by using a filtration apparatus, and then treated in a drying oven to prepare spherical nickel particle powder.

Meanwhile, after obtaining the particles from which the solvent component passed through the high temperature tubular reactor 500 is removed, and collecting and recovering the particles from the gas exiting the reactant, the gas including water vapor and acid generated is caustic soda solution in the gas treatment apparatus 800. Neutralize and discharge to outside.

The spherical nickel powder prepared by the above method can obtain a spherical powder having a uniform spherical particle size even if an expensive hydrogen reducing agent is hardly used.

Hereinafter, embodiments of the present invention will be described in detail.

Example  One

Using nickel in Ambatoby mine, leaching with sulfuric acid, solvent extraction to make nickel sulfate solvent extract. Dilute the nickel sulfate solvent extract to a concentration of 12 g / L. 3 M of urea is mixed with nickel sulfate in the same volume as a reducing agent to the nickel sulfate.

The reducing agent mixture in which the urea reducing agent was mixed was converted into droplet state using an ultrasonic atomizer, and moved into a high temperature tubular reactor using argon (Ar) as a carrier gas. At this time, the high temperature tubular reactor changed the temperature step by step so that the droplets can be evaporated, dried and pyrolyzed sequentially. That is, since the evaporation in the droplet occurs at the part where the droplet enters, the temperature is maintained at a relatively low temperature of 300 ° C., and the temperature is maintained at 700 ° C. in the next step of drying the solute in the droplet. The temperature was kept at 1000 ° C. to allow sufficient reaction to occur. At this time, the flow rate of argon (Ar) was flowed at 3L / min. Thus, the nickel material collected in the collecting device was washed 1-5 times with deionized water and then obtained by using a filtration device using a membrane filter, and then dried in a dryer to obtain a powdery product. X-ray diffraction analysis of the prepared powder is shown in FIG. 6, and the electron micrograph of FIG. 4 shows the prepared particle powder.

Example  2

The same method as in Example 1, except that a concentration of 7M was used as a urea (Urea) reducing agent. X-ray diffraction analysis of the prepared powder is shown in FIG. 6, and the electron micrograph of FIG. 5 shows the prepared particle powder.

Example  3

In the same manner as in Example 1, but the concentration of the urea (Urea) reducing agent 4M was used. X-ray diffraction analysis of the prepared powder is shown in FIG. 10, and the electron micrograph of FIG. 8 shows the prepared particle powder.

Example  4

It carried out in the same manner as in Example 1, the concentration of the urea (Urea) reducing agent was used 4M, the pyrolysis temperature was set to 1200 ℃. X-ray diffraction analysis of the prepared powder is shown in FIG. 10, and the electron micrograph of FIG. 9 shows the prepared particle powder.

The nickel metal powders prepared in Examples 1 to 4 have smooth and spherical particles, and have almost the same shape and uniform spherical shape.

The present invention described above is not limited to the above-described embodiment and the accompanying drawings, and various substitutions, modifications, and changes are possible within the scope without departing from the technical spirit of the present invention. It will be evident to those who have knowledge of.

Figure 1 shows a manufacturing process diagram of a spherical high purity nickel metal powder according to an embodiment of the present invention.

Figure 2 shows the configuration of a pyrolysis device for producing a nickel metal powder according to an embodiment of the present invention.

3 to 5 are shown by electron micrographs of the particle powder prepared by adjusting the concentration of the urea reducing agent according to an embodiment of the present invention.

Figure 6 shows the X-ray diffraction analysis of the particles prepared by adjusting the concentration of the urea reducing agent according to an embodiment of the present invention.

7 to 9 are shown by electron micrographs of the particle powder prepared according to the pyrolysis temperature according to an embodiment of the present invention.

Figure 10 shows the X-ray diffraction analysis according to the thermal decomposition temperature of the particle powder prepared according to an embodiment of the present invention.

DESCRIPTION OF THE RELATED ART [0002]

100: carrier gas supply unit 200: flow meter

300: reducing agent mixture 400: ultrasonic generator

500: tubular reactors 510, 520, 530: first chamber, second chamber, third chamber

600: electric furnace 700: collecting device

800: gas treatment device

Claims (7)

In the method of producing a spherical nickel metal powder, Reducing agent mixing step of mixing a urea (Urea) reducing agent in 6 g / L to 60 g / L nickel sulfate solvent extract; A droplet forming step of generating the reducing agent mixture in a droplet state by an ultrasonic apparatus; A reactor input step of introducing the generated droplets into the reactor together with a carrier gas; A particle conversion step of evaporating, drying, and pyrolysing the mixture in the droplet state introduced into the reactor; And Including a powder forming step of washing and drying the evaporated, dried and pyrolyzed material, The amount of the urea (Urea) reducing agent is mixed in the reducing agent mixing step is a spherical high purity nickel metal powder manufacturing method, characterized in that the urea (Urea) is mixed in a volume ratio of 1: 1 to 1: 3 nickel sulfate solvent extract. The method of claim 1, Spherical high purity nickel metal powder manufacturing method, characterized in that the concentration of the urea (Urea) in the reducing agent mixing step is 3M to 7M. delete The method of claim 1, The carrier gas conveyed to the reactor in the droplet forming step is argon (Ar) of the spherical high purity nickel metal powder manufacturing method. The method of claim 1, The carrier gas carried to the reactor in the droplet forming step is a spherical high purity nickel metal powder manufacturing method, characterized in that the mixture of hydrogen (H ₂ ) and argon (Ar) in a volume ratio of 15:85 to 1:99. The method of claim 1, In the reactor input step, the droplets are spherical high purity nickel metal powder manufacturing method characterized in that the treatment at a rate of 1 to 7 L / min. The method of claim 1, The pyrolysis reaction temperature during the particle conversion step in the droplets is processed to 1000 ℃ to 1400 ℃ spherical high purity nickel metal powder manufacturing method characterized in that the pyrolysis is made.

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