KR102178219B1 - Economical Smelting Method for Nickel from Nickel Sulfide ore, combined Hydrometallurgical and Pyrometallurgical Process - Google Patents

Abstract

Separating the sulfide concentrate containing nickel into a leachate and a leach cake by leaching with a strong acid; Introducing oxygen into the leachate to separate the first filtrate and the first impurity containing iron; Separating a second filtrate and a second impurity containing cobalt by adding an extractant to the first filtrate; Adding sodium carbonate to the second filtrate to separate the third filtrate and a precipitate containing nickel; And calcining the precipitate to produce a nickel product. An economical nickel smelting method that combines a wet and dry process from a nickel concentrate comprising: is introduced.

Description

Economical Smelting Method for Nickel from Nickel Sulfide ore, combined Hydrometallurgical and Pyrometallurgical Process}

The present invention relates to an economical nickel smelting method combining wet and dry processes from sulfide nickel concentrates.

The world's nickel resources fall into two main categories: sulfide ores and laterite ores. They are usually found in quite different places, and these types of ores are usually treated independently.

The development process of sulfide ore includes open pit or underground mining, and beneficiation of ore in which impurities are separated by flotation to beneficate the ore after the ore is first crushed. It is essentially a dry metallurgical process.

The beneficiated sulfide concentrate is subjected to a nickel matte smelting (Smelt) and a refining process for nickel recovery (Refining process). However, the base metal sulfide smelting process is inefficient in terms of energy use due to incomplete oxidation of sulfide and heat loss through gas, slag and output.

Another inefficiency is the high loss of cobalt value in the slag from smelted nickel ore or concentrate. The smelting process also generates sulfur dioxide and often presents the problem of complicating sulfuric acid facility extensions to prevent the release of sulfur dioxide into the atmosphere.

In order to solve some of the problems associated with sulfide refining, many wet metallurgical methods for treating nickel sulfide concentrates have been discussed academically, and these methods generally include sulfide by sulfuric acid in the leaching process after grinding or fine grinding of the concentrate. It relies on Oxidative Pressure Leaching.

The biological treatment of nickel sulfide is also described, followed by solution purification, metal separation and electrowinning after bacterial assisted leaching.

The long residence times required for this type of process require very large reactors in the leaching step, and thus these processes require large capital and thus cannot achieve commercial success.

The present invention provides an economical nickel smelting method combining a wet and dry process from a nickel concentrate capable of obtaining a nickel product containing nickel oxide from a nickel sulfide concentrate.

An economical nickel smelting method combining a wet and dry process from a nickel concentrate according to an embodiment of the present invention comprises the steps of leaching a sulfide concentrate containing nickel with a strong acid to separate it into a leachate and a leaching cake; Introducing oxygen into the leachate to separate the first filtrate and the first impurity containing iron; Separating a second filtrate and a second impurity containing cobalt by adding an extractant to the first filtrate; Adding sodium carbonate to the second filtrate to separate the third filtrate and a precipitate containing nickel; And calcining the precipitate to prepare a nickel product.

After the leaching step, the step of recovering the pressurized leachate by pressurizing the leaching cake with a strong acid, and in the leaching step, the pressurized leachate may be leached with the concentrate with a strong acid.

The pressurized leaching may include pressing and leaching the leaching cake with a strong acid to separate the leaching liquid and the intermediate cake; And separating the intermediate cake into the pressurized leachate and the leaching residue by pressing and leaching the intermediate cake with a strong acid.

After the step of adding sodium carbonate to the second filtrate, adding sodium carbonate to the third filtrate to separate the nickel recovery filtrate and the nickel cake; may be further included.

After the step of adding sodium carbonate to the third filtrate, adding calcium hydroxide to the nickel recovery filtrate and separating it into a gypsum filtrate and a residue may be further included.

In the leaching step, the concentrate may be leached with a strong acid at a temperature of 75 to 95°C.

The leaching may include reducing iron in the leaching liquid; Dissolving nickel in the leachate; And removing hydrogen sulfide generated in the process of dissolving nickel in the leachate in a strong acid.

In the pressurized leaching step, the leaching cake may be pressurized with a strong acid at a temperature of 170 to 190°C.

In the pressure leaching step, the leaching cake may be pressure leached with a strong acid at a pressure of 13 to 20 bar using an autoclave.

In the pressure leaching step, the nickel is dissolved in the form of nickel sulfate, and the dissolution rate of the nickel may be 98% by weight or more based on 100% by weight of the total nickel.

In the step of introducing oxygen into the leachate, a neutralizing agent is added together with the oxygen to separate the first filtrate and the first impurity.

After the step of introducing oxygen into the leachate, washing the first impurity with water and separating the first impurity into a washing filtrate and a washing residue containing iron oxide; may further include.

In the step of adding an extractant to the first filtrate, sodium carbonate may be added together with the extractant to separate the second filtrate and the second impurity.

The extractant may be PC88A (2-Ethylhexyl phosphonic acid mono-2-ethylhexyl ester).

In the step of adding sodium carbonate to the second filtrate, the second filtrate and the sodium carbonate may be reacted at a temperature of 70 to 90°C.

In the step of adding sodium carbonate to the second filtrate, the pH may be adjusted to 6 to 8 by adding the sodium carbonate.

In the step of adding sodium carbonate to the second filtrate, a reaction including the following reaction formula may be performed.

[Reaction Scheme]

5NiSO ₄ + 5Na ₂ CO ₃ + 7H ₂ O → 2NiCO ₃ 3Ni(OH) ₂ 4H ₂ O↓ + 5Na ₂ SO ₄ + 3CO ₂

After the step of adding sodium carbonate to the second filtrate, adding sodium hydroxide to the precipitate and washing with water; may be further included.

In the step of adding sodium hydroxide to the precipitate, the amount of sulfur in the precipitate may be adjusted to 0.2% by weight or less by performing the washing with water a plurality of times.

In the step of adding sodium carbonate to the third filtrate, the third filtrate and the sodium carbonate may be reacted at a temperature of 70 to 90°C.

In the step of adding sodium carbonate to the third filtrate, the pH may be adjusted to 6 to 8 by adding the sodium carbonate.

The precipitate is calcined at a temperature of 700 to 900°C, and the precipitate may contain nickel oxide.

Based on 100% by weight of the total nickel product, sulfur may be 0.1% by weight or less.

According to an economical nickel smelting method combining a wet and dry process from a nickel concentrate according to an embodiment of the present invention, it is possible to obtain a nickel product including high purity nickel oxide from a nickel sulfide concentrate.

1 is a view showing a process chart of an economical nickel smelting method combining a wet and dry process from a nickel concentrate according to an embodiment of the present invention.
2 is a view showing a process chart of an economical nickel smelting method combining a wet and dry process from a nickel concentrate according to an embodiment of the present invention.
3 is a view showing the composition of a sulfide concentrate containing nickel.

Terms such as first, second and third are used to describe various parts, components, regions, layers, and/or sections, but are not limited thereto. These terms are only used to distinguish one part, component, region, layer or section from another part, component, region, layer or section. Accordingly, a first part, component, region, layer or section described below may be referred to as a second part, component, region, layer or section without departing from the scope of the present invention.

The terminology used herein is for referring only to specific embodiments and is not intended to limit the present invention. Singular forms as used herein also include plural forms unless the phrases clearly indicate the opposite. As used in the specification, the meaning of “comprising” specifies a specific characteristic, region, integer, step, action, element and/or component, and the presence of another characteristic, region, integer, step, action, element and/or component It does not exclude additions.

When a part is referred to as being "on" or "on" another part, it may be directly on or on another part, or other parts may be involved in between. In contrast, when a part is referred to as being “directly above” another part, no other part is intervened.

Although not defined differently, all terms including technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which the present invention belongs.

Terms defined in a commonly used dictionary are additionally interpreted as having a meaning consistent with the related technical literature and the presently disclosed content, and are not interpreted in an ideal or very formal meaning unless defined.

Hereinafter, embodiments of the present invention will be described in detail so that those of ordinary skill in the art can easily implement the present invention. However, the present invention may be implemented in various different forms and is not limited to the embodiments described herein.

Economical nickel smelting method combining wet and dry processes from nickel concentrate

In the economical nickel smelting method combining a wet and dry process from a nickel concentrate according to an embodiment of the present invention, referring to FIG. Separating into a first filtrate and a first impurity containing iron by introducing oxygen into the first filtrate and separating into a second filtrate and a second impurity containing cobalt by introducing an extractant into the first filtrate, sodium carbonate in the second filtrate And separating the precipitate into a third filtrate and a precipitate containing nickel, and calcining the precipitate to prepare a nickel product.

First, in the leaching step, an Atmospheric Leaching (ATM) process is performed in which a sulfide concentrate containing nickel is leached with a strong acid and separated into a leaching liquid and a leaching cake.

Based on 100% of the total weight of the concentrate, 25% or more of nickel may be included. Nickel contained in the concentrate may exist in the form of nickel sulfide (Ni ₃ S ₂ ). In addition to nickel, the concentrate may further include magnesium (Mg), iron (Fe), cobalt (Co), manganese (Mn), and silicon (Si). The concentrate can be leached with a strong acid at a temperature of 75 to 95°C. Strong acids may consist of sulfuric acid.

Specifically, the step of leaching may include reducing iron in the leachate, dissolving nickel in the leachate, and removing hydrogen sulfide generated during the dissolution of nickel in the leachate in a strong acid.

In the step of reducing iron in the leachate, +3valent iron may be reduced to +2valent through reaction with nickel sulfide, and a reaction including the following formula (1) may be performed. In this way, by reducing iron, iron can be removed in the form of Ferric Oxide using oxygen later.

[Formula 1]

Ni ₃ S ₂ + 3Fe ₂ (SO ₄ ) ₃ = 3NiSO ₄ + 6FeSO ₄ + 2S

In the step of dissolving nickel in the leachate, nickel sulfide may be dissolved in sulfuric acid, and a reaction including the following formula (2) may be performed.

[Formula 2]

Ni ₃ S ₂ + 3H ₂ SO ₄ = 3NiSO ₄ + 2H ₂ S + H ₂

In the step of removing hydrogen sulfide, hydrogen sulfide generated in the process of dissolving nickel in the leachate in a strong acid as in Chemical Formula 2 may be removed by scrubbing. At this time, sodium hydroxide (NaOH) may be used.

Specifically, after the leaching step, the step of recovering the pressurized leachate by pressurizing the leaching cake with strong acid is further performed, and in the leaching step, the pressurized leachate may be leached with a strong acid together with the concentrate.

In the pressure leaching step, a high pressure acid leaching (HPAL, Autoclave) process may be performed in which the leaching cake is pressurized with strong acid to recover the pressurized leachate.

Specifically, the step of pressurized leaching may include separating the leaching cake into an intermediate leachate and an intermediate cake by pressurizing the leaching cake with a strong acid, and separating the intermediate cake into a pressurized leachate and a leaching residue by pressurizing the intermediate cake with a strong acid.

In the pressure leaching step, the leaching cake can be pressure leached with strong acid at a pressure of 13 to 20 bar and a temperature of 170 to 190°C using an autoclave. Strong acids may consist of sulfuric acid.

Nickel is dissolved in the form of nickel sulfate by pressure leaching, and the dissolution rate of nickel may be 98% by weight or more based on 100% by weight of the total nickel. More specifically, it may be 99.8% by weight or more. The dissolution rate of nickel under normal pressure conditions may be only 50% by weight or less. Nickel dissolution rate can be increased by two-stage pressurized leaching using an autoclave.

Nickel may be dissolved in the form of nickel sulfate (NiSO ₄ ), and a reaction including the following Chemical Formulas 3 to 6 may be performed.

[Formula 3]

Ni ₃ S ₂ + 3H ₂ SO ₄ + 0.5O ₂ = 3NiSO ₄ + 2H ₂ S + H ₂ O

[Formula 4]

Ni ₃ S ₂ + H ₂ SO ₄ + 4.5 O ₂ = 3 NiSO ₄ + H ₂ O

[Formula 5]

2FeS + 2H ₂ SO ₄ + O ₂ = 2FeSO ₄ + 2H ₂ O + 2S

[Formula 6]

2FeS + H ₂ SO ₄ + 4.5O ₂ = Fe ₂ (SO ₄ ) ₃ + H ₂ O

The leaching residue subjected to two-stage pressure leaching may contain 2% by weight or less of nickel. More specifically, 0.2% by weight or less of nickel may be included. In addition, 20 to 30% by weight of iron and 10 to 20% by weight of silicon may be further included, and may be replaced with a cast sand or a removable material of DRS.

In addition, noble metals including at least one of gold, silver, platinum, and palladium may exist in a concentrated state without dissolving in the leaching residue.

The pressurized leachate can be leached again with a strong acid along with the concentrate to minimize the nickel loss rate.

Next, in the step of introducing oxygen to the leachate, an iron removal process is performed in which oxygen is added to the leachate to separate the first filtrate and the first impurity containing iron.

Specifically, in the step of introducing oxygen to the leachate, a neutralizing agent together with oxygen may be added to separate the first filtrate and the first impurity. As the neutralizing agent, a nickel cake obtained in the Ni Recovery process can be used. Nickel cake may contain nickel carbonate (NiCO ₃ ).

A reaction including the following Chemical Formula 7 and Chemical Formula 8 may be performed.

[Formula 7]

2FeSO ₄ + 2NiCO ₃ + H ₂ O + 0.5O ₂ = 2FeOOH + 2NiSO ₄ + 2CO ₂

[Formula 8]

2FeSO ₄ + 2H ₂ O + 0.5O ₂ = Fe ₂ O ₃ + 2H ₂ SO ₄

After the step of introducing oxygen to the leachate, the first impurity may be washed with water to separate the first impurity into a washing filtrate and a washing residue containing iron oxide.

Next, in the step of adding the extractant to the first filtrate, a Co S/X process is performed in which the extractant is added to the first filtrate to separate the second filtrate and the second impurity containing cobalt.

At this time, the extractant may be PC88A (2-Ethylhexyl phosphonic acid mono-2-ethylhexyl ester). Accordingly, cobalt in the second impurity may exist in a precipitated state as cobalt carbonate (CoCO ₃ ). In addition, copper in the second impurity may exist in a precipitated state as copper carbonate (CuCO ₃ ).

Next, in the step of adding sodium carbonate to the second filtrate, a Selective Nickel Precipitation (SNP) process in which sodium carbonate is added to the second filtrate and separated into a third filtrate and a precipitate containing nickel is performed.

Through this, it is possible to selectively precipitate and then recover only nickel in the second filtrate. The second filtrate and sodium carbonate may be reacted at a temperature of 70 to 90° C., and the pH may be adjusted to 6 to 8 by adding sodium carbonate.

Nickel can be precipitated in the form of Basic Nickel Carbonate, which can be expressed as 2NiCO ₃ ·3Ni(OH) ₂ ·4H ₂ O as shown in the following reaction formula.

[Reaction Scheme]

5NiSO ₄ + 5Na ₂ CO ₃ + 7H ₂ O → 2NiCO ₃ 3Ni(OH) ₂ 4H ₂ O↓ + 5Na ₂ SO ₄ + 3CO ₂

Specifically, after the step of adding sodium carbonate to the second filtrate, the step of washing with water by adding sodium hydroxide to the precipitate may be further performed. The amount of sulfur in the precipitate can be adjusted to 0.2% by weight or less by removing unreacted nickel sulfate as shown in Formula 9 below by performing water washing a plurality of times.

[Formula 9]

NiSO ₄ + 2NaOH = Ni(OH) ₂ + Na ₂ SO ₄

Specifically, after the step of adding sodium carbonate to the second filtrate, sodium carbonate may be added to the third filtrate to prepare a nickel recovery filtrate and a nickel cake to be separated into a nickel cake.

Specifically, in the step of adding sodium carbonate to the third filtrate, the third filtrate and the sodium carbonate may be reacted at a temperature of 70 to 90° C., and the pH may be adjusted to 6 to 8 by adding sodium carbonate. By adjusting the pH, 25% by weight or more of magnesium can be incorporated into the nickel cake based on the total 100% by weight of magnesium. Accordingly, it is possible to increase the amount of magnesium recovered. If the pH is too high, magnesium, an impurity, may be mixed into the nickel cake, and if the pH is too low, the nickel recovery rate may decrease.

In addition, as mentioned above, as a neutralizing agent, a nickel cake can be added together with oxygen to separate the first filtrate and the first impurity. Nickel cake may contain nickel carbonate (NiCO ₃ ). Accordingly, the nickel loss rate can be minimized.

Specifically, after the step of adding sodium carbonate to the third filtrate, calcium hydroxide is added to the nickel recovery filtrate to separate the gypsum filtrate and the residue, and discharge the waste water treatment (WWT) process may be performed.

The pH can be adjusted to 9.5 or higher by adding calcium hydroxide. In order to meet the effluent standard (nickel content less than 1mg/L), calcium hydroxide can be added to adjust the pH to 9.5 or higher. In Table 1 below, when the temperature is 40°C, the change in nickel content according to pH can be confirmed.

pH 8.0 pH 9.0 pH 9.5 Nickel content (mg/L) 16 3.5 0.1

As shown in Table 1, when the pH is 9.5, it can be confirmed that the content of nickel is 0.1 mg/L, which satisfies the effluent standard.

On the other hand, when the pH is 9.5, as shown in Formula 10 below, 3.4 mg/L of magnesium remains, and the remainder is precipitated as magnesium hydroxide (Mg(OH) ₂ ), and since gypsum is produced together, the residual amount increases significantly. Disposal may be required.

[Formula 10]

MgSO ₄ + Ca(OH) ₂ + 2H ₂ O = Mg(OH) ₂ + CaSO ₄ 2H ₂ O

Next, in the step of preparing a nickel product, a calcination process of producing a nickel product by calcining the precipitate is performed.

Specifically, the precipitate is calcined at 700 to 900°C, and the precipitate may include nickel oxide.

Moisture and crystal water evaporate above 120°C, nickel hydroxide is decomposed to nickel oxide at 230°C or higher, and nickel carbonate may be decomposed to nickel oxide at 400°C or higher. At 800° C. or higher, the sulfur content may be 0.1 wt% or less based on 100 wt% of the nickel product.

Hereinafter, specific examples of the present invention will be described. However, the following examples are only specific examples of the present invention, and the present invention is not limited to the following examples.

Example

An embodiment will be described with reference to FIG. 2.

(1) Concentrate leaching with strong acid (Atmospheric Leaching)

Components of the sulfide concentrate containing nickel are shown in FIG. 3. The sulfide concentrate containing nickel oxide was leached at 85° C. for 8 hours. The final pH of the leachate was 2.0.

ATM lea, the leachate. The composition of o/f Sol'n was shown in Table 2 below, and the composition of the leaching cake was shown in Table 3 below. The composition of HPAL o/f Sol'n, a pressurized leachate, was shown in Table 4 below.

division Ni Fe Mg Si Co Cr Cu Mn g/L 55.6 32.1 16.9 0.27 1.65 0.29 0.79 0.08

division Ni Fe Mg Si Co Cr Cu Mn weight% 24.1 23.6 4.52 6.68 0.74 0.04 0.50 0.04

Ni Fe Mg Si Co Cr Cu Mn H ₂ SO ₄ g/L 58.0 34.3 14.1 0.32 1.73 0.20 1.00 0.08 58.2

(2) High Pressure Acid Leaching by adding strong acid to the leaching cake

Sulfuric acid, oxygen, and steam were added to the leaching cake and leached under pressure with an autoclave at 180°C and 15 bar for 3 hours. Pressurized leaching in two stages. The intermediate cake #1 HPAL Cake and the leaching residue #2 HPAL Residue are shown in Tables 5 and 6 below.

Ni Fe Mg Si Content (% by weight) 3.24 19.8 0.07 22.2

Ni Fe Mg Si Co Cr Cu Mn Pt Pd T.S content 0.17Wt% 25.2
Wt% 0.05
Wt% 18.7
Wt% 0.02
Wt% 0.002Wt% 0.01
Wt% 0.02
Wt% 8.6
g/t 17
g/t 1.28
Wt%

(3) Oxygen is added to the leachate to separate the first impurity (Iron Removal)

ATM Lea, the leachate. In o/f Sol'n, oxygen, steam, and nickel cake as a neutralizing agent were added to separate the first filtrate, Iron Removal Sol'n, and the first impurity. Thereafter, the first impurity was washed with water and steam to separate Ferric Oxide.

The first filtrate, HYD Sol'n and Ferric Oxide, were shown in Tables 7 and 8 below.

Ni Fe Mg Si Co Cr Cu Mn g/L 53.6 0.15 18.3 0.15 1.40 0.001 0.65 0.06

Ni Fe Mg Si Co Cr Cu Mn weight% 0.30 40.0 0.02 0.10 0.003 0.03 0.001 0.004

(4) Separating the second impurity by adding an extractant to the first filtrate (Co S/X)

Sodium carbonate and PC88A (2-Ethylhexyl phosphonic acid mono-2-ethylhexyl ester) as an extractant were added to HYD Sol'n, the first filtrate, and the second filtrate, Co Rec. Sol'n and the second impurity were separated. Accordingly, a second impurity containing cobalt carbonate containing 40 wt% or more of cobalt and copper carbonate containing 40 wt% or more of copper was separated.

The second filtrate, Co Rec. Sol'n was shown in Table 9 below.

Ni Fe Mg Si Co Cr Cu Mn g/L 53.6 0.001 18.3 0.15 0.03 0.0003 0.03 0.0002

(5) In the second filtrate Prepare a precipitate by adding sodium carbonate (Selective Nickel Precipitation)

The second filtrate, Co Rec. Sodium carbonate and steam were added to Sol'n. The temperature was 80°C and the pH was 7.3. Accordingly, it was separated into a third filtrate and a precipitate containing nickel.

Thereafter, the precipitate was washed twice with sodium hydroxide, water and steam to obtain a SNP Cake. The washing temperature was 70° C. and the pH was 10.

The composition of the SNP Cake was shown in Table 10 below.

Ni Fe Mg Si Co Cu Mn T.S weight% 45.0 0.0005 1.94 0.14 0.0265 0.031 0.0002 0.20

(6) Sodium carbonate was added to the third filtrate to prepare a nickel cake (Ni Recovery)

Sodium carbonate and steam were added to the third liquid. The temperature was 80°C and the pH was 7.5. It was reacted for 3 hours. This gave a nickel cake.

The composition of the nickel cake was shown in Table 11 below.

Ni Mg weight% 16.9 11.5

(7) Nickel recovery (Waste Water Treatment) after treatment by adding calcium hydroxide to the filtrate

After the nickel cake was separated, calcium hydroxide and water were added to the remaining nickel recovery filtrate. The temperature was 40°C and the pH was 9.5. It was reacted for 3 hours. Accordingly, Gypsum, a gypsum, and Effluent, a residue, were obtained. The COD of effluent was 49mg/L.

The composition of Gypsum was shown in Table 12 below, and the composition of Effluent was shown in Table 13 below. Through this, it can be confirmed that the discharge standard was satisfied.

Ni Mg CaO SO ₃ moisture weight% 0.05 7.74 11.1 16.7 40.0

As CD Co F Hg Mg Mn N Ni Sb Se Si Zn mg/L 0.1 <0.01 N.D <1 N.D 3.5g/L <1 2.5 <1 <0.1 N.D 1.3 <0.01

(8) Calcination of the precipitate to produce nickel product (Calcination)

The precipitated SNP Cake was calcined to obtain Nickel Oxide, a nickel product. The temperature was 800° C., and it was carried out for 1 hour.

The composition of Nickel Oxide, a nickel product, was shown in Table 14 below.

Ni Fe Mg Si Co Cu Mn T.S weight% 70.0 0.001 3.02 0.22 0.0412 0.048 0.0002 0.05

The present invention is not limited to the above embodiments and/or embodiments, but may be manufactured in various different forms, and those of ordinary skill in the art to which the present invention pertains change the technical spirit or essential features of the present invention. It will be appreciated that it can be implemented in other specific forms without doing so. Therefore, it should be understood that the embodiments and/or embodiments described above are illustrative and non-limiting in all respects.

Claims (23)

Separating the sulfide concentrate containing nickel into a leachate and a leach cake by leaching with a strong acid;
Adding oxygen to the leachate to separate the first filtrate and the first impurity containing iron;
Separating a second filtrate and a second impurity containing cobalt by adding an extractant to the first filtrate;
Adding sodium carbonate to the second filtrate to separate the third filtrate and a precipitate containing nickel; And
Comprising: calcining the precipitate to prepare a nickel product; and
In the step of adding sodium carbonate to the second filtrate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate in which a reaction including the following reaction formula occurs
[Reaction Scheme]
5NiSO ₄ + 5Na ₂ CO ₃ + 7H ₂ O → 2NiCO ₃ 3Ni(OH) ₂ 4H ₂ O↓ + 5Na ₂ SO ₄ + 3CO ₂ The method of claim 1,
After the leaching step,
The step of recovering the pressurized leachate by pressurizing the leaching cake with a strong acid; further comprising,
In the leaching step,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate in which the pressurized leachate is leached with a strong acid together with the concentrate. The method of claim 2,
The pressure leaching step,
Separating the leaching cake into an intermediate leaching liquid and an intermediate cake by pressing and leaching the leaching cake with a strong acid; And
An economical nickel smelting method combining a wet and dry process from a nickel concentrate comprising a step of separating the intermediate cake into the pressurized leachate and the leaching residue by pressurizing the intermediate cake with strong acid. The method of claim 1,
After the step of adding sodium carbonate to the second filtrate,
An economical nickel smelting method that combines wet and dry processes from a nickel concentrate further comprising a step of separating into a nickel recovery filtrate and a nickel cake by adding sodium carbonate to the third filtrate. The method of claim 4,
After the step of adding sodium carbonate to the third filtrate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate further comprising: separating a gypsum filtrate and a residue by adding calcium hydroxide to the nickel recovery filtrate. The method of claim 1,
In the leaching step,
An economical nickel smelting method that combines wet and dry processes from nickel concentrates in which the concentrates are leached with a strong acid at a temperature of 75 to 95°C. The method of claim 1,
The leaching step,
Reducing iron in the leachate;
Dissolving nickel in the leachate; And
An economical nickel smelting method combining a wet and dry process from a nickel concentrate comprising a step of removing hydrogen sulfide generated in the process of dissolving nickel in the leachate in a strong acid. The method of claim 2,
In the pressure leaching step,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate that pressurizes the leaching cake with a strong acid at a temperature of 170 to 190°C. The method of claim 2,
In the pressure leaching step,
An economical nickel smelting method that combines wet and dry processes from a nickel concentrate that pressurizes the leaching cake with a strong acid at a pressure of 13 to 20 bar using an autoclave. The method of claim 2,
In the pressure leaching step,
The nickel is dissolved in the form of nickel sulfate, and the dissolution rate of the nickel is 98% by weight or more, based on 100% by weight of the total nickel, and an economical nickel smelting method combining a wet and dry process from a nickel concentrate. The method of claim 1,
In the step of introducing oxygen to the leachate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate that separates the first filtrate and the first impurity by adding a neutralizing agent together with oxygen. The method of claim 2,
After the step of introducing oxygen to the leachate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate further comprising the step of separating the first impurity into a washing residue including a washing filtrate and iron oxide by washing with water. The method of claim 1,
In the step of adding an extractant to the first filtrate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate in which sodium carbonate is added together with the extracting agent to separate the second filtrate and the second impurity. The method of claim 13,
The extractant is PC88A (2-Ethylhexyl phosphonic acid mono-2-ethylhexyl ester), an economical nickel smelting method that combines a wet and dry process from a nickel concentrate. The method of claim 1,
In the step of adding sodium carbonate to the second filtrate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate in which the second filtrate and the sodium carbonate are reacted at a temperature of 70 to 90°C. The method of claim 1,
In the step of adding sodium carbonate to the second filtrate,
An economical nickel smelting method combining a wet and dry process from a nickel concentrate that adjusts the pH to 6 to 8 by the addition of the sodium carbonate. delete The method of claim 1,
After the step of adding sodium carbonate to the second filtrate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate further comprising: adding sodium hydroxide to the precipitate and washing with water. The method of claim 18,
In the step of adding sodium hydroxide to the precipitate,
An economical nickel smelting method combining wet and dry processes from nickel concentrates in which the content of sulfur in the precipitate is adjusted to 0.2% by weight or less by performing the washing with water a plurality of times. The method of claim 4,
In the step of adding sodium carbonate to the third filtrate,
An economical nickel smelting method that combines a wet and dry process from a nickel concentrate in which the third filtrate and the sodium carbonate are reacted at a temperature of 70 to 90°C. The method of claim 4,
In the step of adding sodium carbonate to the third filtrate,
An economical nickel smelting method combining a wet and dry process from a nickel concentrate that adjusts the pH to 6 to 8 by the addition of the sodium carbonate. The method of claim 1,
An economical nickel smelting method in which the precipitate is calcined at a temperature of 700 to 900°C, and the precipitate is a combination of a wet and dry process from a nickel concentrate containing nickel oxide. The method of claim 1,
An economical nickel smelting method in which a wet and dry process is combined from a nickel concentrate in which sulfur is 0.1% by weight or less based on 100% by weight of the total nickel product.

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