WO2019045161A1 - 니켈 산화광으로부터 습식 및 건식 공정을 조합한 경제적 니켈 제련 공법 - Google Patents
니켈 산화광으로부터 습식 및 건식 공정을 조합한 경제적 니켈 제련 공법 Download PDFInfo
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- WO2019045161A1 WO2019045161A1 PCT/KR2017/009900 KR2017009900W WO2019045161A1 WO 2019045161 A1 WO2019045161 A1 WO 2019045161A1 KR 2017009900 W KR2017009900 W KR 2017009900W WO 2019045161 A1 WO2019045161 A1 WO 2019045161A1
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- Prior art keywords
- nickel
- wet
- economical
- smelting
- solution
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0476—Separation of nickel from cobalt
- C22B23/0484—Separation of nickel from cobalt in acidic type solutions
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/06—Refining
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/02—Obtaining nickel or cobalt by dry processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/043—Sulfurated acids or salts thereof
-
- 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
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/38—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
- C22B3/384—Pentavalent phosphorus oxyacids, esters thereof
- C22B3/3842—Phosphinic acid, e.g. H2P(O)(OH)
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Definitions
- the present invention relates to a method for producing nickel using a latex ore, which is one of the nickel raw materials.
- a typical dry smelting method of producing nickel by processing a commercially operated lateion ore is a method of producing ferronickel through drying, reduction roasting, electric furnace smelting and refining processes.
- the method of precipitating nickel is a method of producing Mixed Sulfide Precipitation (MSP) by injecting H 2 S gas, precipitating it as nickel sulfide, and producing Mixed Hydroxide Precipitate (MHP) by using a vaporization method.
- MSP Mixed Sulfide Precipitation
- MHP Mixed Hydroxide Precipitate
- the latite ore mainly used in the nickel dry smelting is saprolite (Ni: 1.8-3.0%, Fe: 10-25%, MgO: 15-35%), and the calcite which is mainly used in the nickel wet smelting
- the iron content is low and the MgO content is higher than that of iron, nitrite, limonite, Ni: 0.8 to 1.5%, Fe: 40 to 50%, MgO: 0.5 to 5%
- the most unreasonable point in the oxidative light dry smelting process is the low nickel content and the relatively large amount of slag generated by the gangue component. In order to remove the nickel of about 3% or less, all of the remaining gangue components must be removed by using heat.
- the most unreasonable point of the oxidative light wet smelting process is that the pure nickel metal is used for the most demanded stainless steel manufacturing (about 10 ⁇ 14% Ni alloy), and thus it is refined to an excessive purity unnecessarily.
- the future nickel smelting business requires the development of a method that can produce nickel metal which is higher in purity than the current ferronickel and which is suitable for manufacturing stainless steel, but can simplify the process and lower the manufacturing cost.
- the present invention relates to a method for producing nickel metal by treating a laterite ore, which is one of nickel raw materials.
- An economical nickel smelting method in which wet and dry processes are combined from nickel oxidation light includes the steps of: dissolving a fused hydroxide containing nickel and impurities in a strong acid to prepare a solution; Introducing an organic material into the solution to separate impurities; Introducing a first neutralizing agent into the post-liquid after the impurities are separated, and calcining to obtain a nickel oxide; And reducing the nickel oxide to produce a nickel product.
- the method may further include the step of leaching a raw material containing ore into a strong acid and neutralizing the raw material to prepare the refined hydroxide.
- the step of separating the impurities comprises the steps of: injecting an organic material into the solution to prepare an organic compound containing the impurities; And separating the organic compound to prepare a post-liquid.
- Na 2 CO 3 is added to the dissolution solution into which the organic matter is introduced, 6 < / RTI >
- Preparing a stripping solution by adding sulfuric acid to the organic compound; And adding a second neutralizing agent to the stripping solution to form a cobalt precipitate.
- the second neutralizing agent is Na 2 CO 3 , and a first cobalt product containing CoCo 3 can be obtained.
- the second neutralizing agent is NaSH and a second cobalt product containing CoS can be obtained.
- the pH of the stripping solution into which NaSH is added can be adjusted to 4 to 5.
- the step of obtaining the nickel oxide may include the steps of countering the latex and the first thickening agent at a temperature of 70 [ deg.] C or higher to prepare a reaction product; Washing the water with water to reduce sulfur content in the water; And a step of calcining the reduced sulfur-containing solution to obtain a nickel oxide.
- the first neutralizing agent is Na 2 CO 3 , and the pH of the solution containing the water is adjusted to 7 to 9.
- the reaction product may be repeatedly washed with water and repeatedly washed with aqueous NaOH solution.
- the nickel oxide in the process of calcining the nickel hydroxide to obtain nickel oxide, the nickel oxide can be calcined and thermally decomposed for 30 minutes or more at a temperature of 400 ° C or more.
- the strong acid is sulfuric acid
- the pH of the dissolution liquid can be adjusted to 1 to 2.
- the step of preparing the fused hydroxide may include: a step of pressurizing and leaching the raw material into sulfuric acid to prepare an extract; 'Process for producing a neutralized filtrate was charged into the CaO or CaC0 3 in the leachate; And adding MgO to the filtrate to produce the condensed hydroxide.
- the nickel oxide may be charged into an electric furnace and reduced at a temperature of 1500 to 170CTC.
- the nickel production process is simplified, and nickel of purity suitable for the production of stainless steel can be produced instead of unnecessarily excessive purity.
- the manufacturing cost can be reduced and the productivity can be improved.
- FIG. 1 is a view showing an entire process of an economical nickel smelting process in which a wet process and a dry process are combined from the nickel oxidation light according to the present invention.
- FIG. 2 is a graph showing a selective metal extraction ratio according to pH in the step of separating impurities in an economical nickel smelting process in which wet and dry processes are combined from nickel oxidation light according to the present invention.
- FIG. 3 is a graph showing the solubility of metal sulfides according to the pH of the stripping solution in the process of producing cobalt products in an economical nickel smelting process in which wet and dry processes are combined from nickel oxidation light according to the present invention.
- FIG. 4 shows the XRD measurement results of the second cobalt product in the economical nickel smelting process in which the wet and dry processes are combined from the nickel oxidation light according to the present invention.
- FIG. 5 is a graph showing a thermal decomposition graph according to a calcination temperature in the step of obtaining a nickel oxide in an economical nickel smelting process in which a wet process and a dry process are combined from the nickel oxidation light according to the present invention.
- FIG. 6 shows the results of XRD measurement of water after washing in an economical nickel smelting process in which a wet process and a dry process were combined from the nickel oxidation light according to the present invention.
- FIG. 7 shows XRD measurement results of nickel oxide in an economical nickel smelting process in which a wet process and a dry process are combined from the nickel oxide light according to the present invention.
- an economical nickel smelting process combining wet and dry processes from nickel oxidation light comprises steps of producing a fused hydroxide, , Separating the impurities, obtaining a nickel oxide, and producing the nickel product.
- a raw material containing ore is leached into strong acid and neutralized to produce a fused hydroxide.
- the process may include a process of producing the leached liquid by pressurized leaching of the raw material into sulfuric acid, a process of producing a neutralized filtrate by adding CaO or CaC0 3 to the leached liquid, and a process of producing the purified hydroxide by adding MgO to the neutralized filtrate have.
- the ores included in the raw material may be nickel oxide light, among which are laerite ores.
- the components of the lateite ores can be expressed as follows.
- the total weight is expressed in terms of 10OT, and the remainder is composed of other unavoidable impurities.
- Ni 0.8 to 3.0%
- Co 0.01 to 0.15%
- Fe 14 to 48%
- Mg 1.0 to 15%
- Zn 0.01 to 0.05%
- the raw material containing the above-mentioned latex ore can be pressurized and leached into sulfuric acid. Pressurized leaching can be achieved at a pressure of 33 to 55 atm, at a silver of 240 to 270 ° C.
- the amount of sulfuric acid used may be 200 to 500 kg / T Ni.
- the reaction at this time can be expressed as follows.
- Ni (0H) 2 (s) + H 2 S0 4 (1) NiS0 4 (aq) + 2H 2 0 (1)
- Some of the iron (Fe) present in the Fe 2 (SO 4 ) 3 (aq) state together with the antimony may be precipitated in the form of hematite or jarosite,
- Fe 2 (S0 4) 3 ( aq) + 3H 2 0 (1) Fe 2 0 3 (s) + 2H 2 S0 4 (aq)
- 3Fe 2 (SO 4 ) 3 (aq) + 14H 2 0 (1) 2 [3 ⁇ 40Fe 3 (SO 4 ) 2 (OH) 6 ] (s) + 6H 2 SO 4 (aq)
- CaO or CaCO 3 may be added to the reaction mixture to prepare a neutralized filtrate. At this time, the pH can be controlled to 3 to 4.
- Part of the iron (Fe) present in the Fe 2 (SO 4 ) 3 (aq) state in the leach solution can counteract CaO or CaCO 3, and can be expressed in the following equation.
- H 2 SO 4 (aq) + CaCOs (s) + H 2 O (1) CaSO 4 * 2H 2 O (s) + CO 2 (g)
- iron (Fe) with the same banung is a component such as aluminum which is treated with an impurity (A1), silica (Si0 2), keureum (Cr), and gypsum can be removed through precipitation, filtration.
- A1 impurity
- Si0 2 silica
- Cr keureum
- gypsum gypsum
- MgO may be added to the neutralized filtrate to produce a condensed hydroxide.
- the pH can be controlled to 7 to 8.
- Co Co
- Ni (S0) 4 (aq) and nickel (Ni) and Co (S0) 4 (aq) in the neutralized filtrate can counteract with MgO, .
- NiS0 4 (aq) + MgO ( s) + 3 ⁇ 40 (1) Ni (0H) 2 (s) + MgS0 4 (aq)
- Cobalt hydroxide, magnes hydroxides, manganese hydroxides and zinc hydroxides can conveniently be treated as impurity metal hydroxides. have.
- Nickel and impurities can be made. This can be expressed as Mixed Hydroxide Precipitates (MHP) Cake.
- MHP Mixed Hydroxide Precipitates
- the composition of the fused hydroxide can be expressed as follows.
- the total amount is expressed on the basis of 100%, and the remainder is composed of other unavoidable impurities.
- the dissolving hydroxide containing nickel and impurities is dissolved in strong acid.
- the strong acid is sulfuric acid
- the pH of the dissolution liquid can be adjusted to 1 to 2.
- a step of preparing a solution for about 3 hours at a reaction temperature of 60 to 70 ° C can be performed, and the reaction of cobalt hydroxide and sulfuric acid among nickel hydroxide and impurity metal hydroxide can be represented by the following equation.
- Ni (0H) 2 (s) + H 2 S0 4 (1) NiS0 4 (aq) + 2H 2 0 (1)
- organic substances are added to the dissolution liquid to separate the impurities.
- the method may include a step of adding an organic substance to the solution to prepare an organic compound containing the impurity, and a step of separating the organic compound to prepare a post-solution.
- the method may further include a step of adding a sulfuric acid to the organic compound to prepare a stripping solution, and a step of adding a second neutralizing agent to the stripping solution to form a cobalt precipitate.
- Cobalt, magnesium, manganese and zinc present in the solution are counteracted by organic solvent extraction (S / X).
- the organic matter is cyanex 272, and Na 2 CO 3 is added to the above solution and
- the pH of the solution in which organic matters are mixed can be adjusted to 5 to 6.
- the reaction of cobalt and organic matter can be expressed by the following equation.
- NiR 2 (RH) 2 (org ) + CoS0 4 (aq) CoR 2 (RH) 2 (org) + NiS0 4 (aq)
- the selective extraction rate by cyanex 272 varies depending on the pH of the solution containing the organic compound.
- the extractability of nickel is low in the range of pH 5 to 6, while the extraction rate of cobalt, magnesium, It can be seen that the extraction rate is 70% or more. In this case, the extraction rate of cobalt, magnes and manganese is more than 95%.
- cobalt products can be prepared from separated organic compounds to produce cobalt, which is a valuable metal, as a product.
- a str ipping filtrate can be prepared by adding sulfuric acid to the organic compound.
- the stripping solution may include a cobalt organic compound, a magnesium organic compound, a manganese organic compound, and a zinc organic compound.
- CoR 2 (RH) 2 (org ) + H 2 S0 4 (aq) 2 (RH) 2 (org) + CoS0 4 (aq)
- a second neutralizing agent in the stripping solution containing the CoS0 4 may be formed of a cobalt precipitate.
- the pH of the stripping solution to which Na 2 CO 3 is added can be adjusted to 8 to 10 and can be carried out at a reaction temperature of 70 to 90 ° C.
- a first cobalt product is generally that in a not in a pure CoC0 3 are mixed with Co (0H) 2 state, i.e. Bas ic Cobal t car bona te ( CoC0 3. YCo (OH) 2. ZH 2 0) state .
- CoC0 3 and Co more than a first product of cobalt present in the state heunjae and (0H) 2 may be sold as product without refining.
- a second cobalt product comprising CoS can be obtained through the following countercurrent reaction.
- the pH of the stripping solution to which NaSH is added can be adjusted to 4 to 5 and can be carried out at a reaction temperature of 70 to 90 ° C for about 3 hours.
- the pH of the stripping solution can be adjusted to take advantage of the solubility differences of cobalt sulfide, magnesulfide, manganese sulfide and zinc sulfide.
- the solubility of cobalt sulphide and zinc sulphide is very low as 0.01 mg / L or less, while the solubility of magnesium sulphide and manganese sulphide is very high in the range of pH 4 to 5, so that NaSH can not be precipitated in the loaded stripping solution and can be separated.
- the second cobalt product has a high cobalt content and a low impurity content and can be sold as a product.
- the first neutralizing agent is added to the after-liquid after the impurities are separated, and the nickel oxide is obtained by calcination.
- the latex and the first neutralizing agent are repelled at a silver level of 70 ° C or higher
- the first neutralizing agent is added to the post-treatment liquid after the impurities such as cobalt are removed, and the nickel is precipitated in carbonate form at a temperature of 70 ° C or higher.
- the first neutralizing agent is Na 2 CO 3 and the pH of the solution containing the reactants can be adjusted to 7-9.
- the reaction temperature is less than 70 ° C, the filtration time is increased due to the generation of fine particles, so that the removal rate of sulfur in the post-washing step may be reduced.
- the nickel and Na 2 C0 3 in huaek can be expressed as equations which banung banung.
- Banung water it is common that in a not in a pure NiC0 3 heunjae with Ni (0H) 2 state, i.e., Basi c Ni ckel carbonate (xNiC0 3 .yNi (0H) 2. ZH 2 0) state eu
- the sulfur content in the water is high, the sulfur content can be lowered through the washing process.
- the reaction product may be repeatedly washed with water and then with NaOH aqueous solution repeatedly.
- reaction represented by the following reaction formula can be performed.
- NiS0 4 + 2NaOH Ni (0H ) 2 + Na 2 S0 4
- the hydrolysis product can be thermally decomposed by calcination at a temperature of 400 ° C or more for 30 minutes or more. It can be removed with water in the reactants and can be carried out in a rotary kiln.
- the thermal decomposition reaction of water can be expressed in the following manner.
- NiC0 3 NiO + C0 2
- the nickel oxide may be charged into an electric furnace together with cokes, etc., and reduced at a silver of 1500 to 170 CTC. Accordingly, it is possible to produce nickel having a purity of 97% or more.
- the nickel manufacturing process is simplified, and nickel of purity suitable for stainless steel production can be produced, not unnecessarily excessive purity. As a result, the manufacturing cost can be reduced and the productivity can be improved.
- the lateite ore was dissolved in sulfuric acid.
- the temperature at this time was 250 ° C and the pressure was 44 atm.
- About 350 kg / T Ni was added to the sulfuric acid.
- CaO was added to the leaching solution in which lactate ore was leached into sulfuric acid to remove impurities first. Thereafter, MgO was further added to prepare a fused hydroxide containing nickel and impurities.
- the composition of the fused hydroxide was as follows.
- the total weight is expressed as 100%, and the remainder is composed of other unavoidable impurities.
- Ni 40%, Co: 0.04%, Fe: 0.01%, Si: 0. 15%, Mg: 0.55%, Mn: 0.02%, Cu: 0.01%, Zn: 0.01% %, S: 2.0%
- Soluble hydroxide sulfuric acid to prepare a dissolution solution.
- the air temperature was 60 ° C and the reaction was continued for about 3 hours.
- the pH of the solution was adjusted to 1.2.
- cyanex 272 was added to the solution, and Na 2 CO 3 was added thereto to adjust the pH of the solution in which the dissolution solution and organic matter were mixed to 5.2.
- the organic compound was removed from the solution in which the dissolving solution and organic matter were mixed to prepare a post-solution.
- Na 2 CO 3 was added to the reaction solution to form a reaction product.
- the pH of the solution containing the NaOH solution was adjusted to be 8, at which the NaOH silver temperature was 70 ° C and the reaction was continued for about 3 hours.
- the composition of the water is as follows.
- the total weight is expressed as 100%, and the remainder is composed of other unavoidable impurities.
- Ni 45%, Co: 0.044%, Fe: 0.0005%, Si: 0. 15%, Mg: 0.59%, Mn: 0.001%, Cu: 0.006%, Zn: 0.01% : 0.05%
- nickel oxide The composition of nickel oxide is as follows.
- the total weight is expressed in terms of 10OT, and the remainder is composed of other unavoidable impurities.
- Ni 70%, Co: 0.1%, Fe: 0.001%, Si: 0.3%, Mg: 1.0%, Mn: 0.002%, Cu: 0.01%
- the nickel content was increased, and the impurity content was further decreased.
- the previously prepared nickel product was charged into an electric furnace together with coke, Reduction at 1600 [ deg.] C resulted in the preparation of the nickel product.
- the composition of the nickel product is as follows.
- the total weight is expressed as 100%, and the remainder is composed of other unavoidable impurities.
- Ni 97%, Co: 0.1%, Fe: 0.001%, Si: 0.1%, Mg: 0.01%, Mn: 0.002%, Cu: 0.01%
- the content of nickel is 97% . And the impurity content is low.
- composition of the cobalt product is as follows.
- the total weight is expressed as 100%, and the remainder is composed of other unavoidable impurities.
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Abstract
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Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP17923731.8A EP3677695A4 (en) | 2017-08-31 | 2017-09-08 | ECONOMICAL PROCESS FOR MELTING NICKEL FROM NICKEL LATERITE ORE BY COMBINATION OF WET AND DRY PROCESSES |
AU2017430097A AU2017430097B2 (en) | 2017-08-31 | 2017-09-08 | Method for economically smelting nickel from nickel laterite ores by combination of wet and dry processes |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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KR10-2017-0111411 | 2017-08-31 | ||
KR1020170111411A KR101950314B1 (ko) | 2017-08-31 | 2017-08-31 | 니켈 산화광으로부터 습식 및 건식 공정을 조합한 경제적 니켈 제련 공법 |
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WO2019045161A1 true WO2019045161A1 (ko) | 2019-03-07 |
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PCT/KR2017/009900 WO2019045161A1 (ko) | 2017-08-31 | 2017-09-08 | 니켈 산화광으로부터 습식 및 건식 공정을 조합한 경제적 니켈 제련 공법 |
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EP (1) | EP3677695A4 (ko) |
KR (1) | KR101950314B1 (ko) |
AU (1) | AU2017430097B2 (ko) |
WO (1) | WO2019045161A1 (ko) |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2005350766A (ja) * | 2004-05-13 | 2005-12-22 | Sumitomo Metal Mining Co Ltd | ニッケル酸化鉱石の湿式製錬方法 |
KR20070094819A (ko) * | 2004-12-30 | 2007-09-21 | 비에이치피 빌리톤 에스에스엠 테크놀로지 피티와이 엘티디 | 수지 용출 스트림으로부터 니켈 및 코발트의 추출 |
KR20070107787A (ko) * | 2005-02-24 | 2007-11-07 | 비에이치피 빌리톤 에스에스엠 테크놀로지 피티와이 엘티디 | 페로니켈 제조 |
KR20090042996A (ko) * | 2006-08-23 | 2009-05-04 | 비에이치피 빌리톤 에스에스엠 디벨롭먼트 피티와이 엘티디 | 철 함량이 낮은 금속 니켈 제조 |
JP5904459B2 (ja) * | 2011-11-22 | 2016-04-13 | 住友金属鉱山株式会社 | 高純度硫酸ニッケルの製造方法 |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
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US8147782B2 (en) * | 2007-09-28 | 2012-04-03 | Vale Inco Limited | Producing nickel hydroxide suitable for pelletization with iron-containing ore and for stainless steel manufacture |
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2017
- 2017-08-31 KR KR1020170111411A patent/KR101950314B1/ko active IP Right Grant
- 2017-09-08 WO PCT/KR2017/009900 patent/WO2019045161A1/ko unknown
- 2017-09-08 AU AU2017430097A patent/AU2017430097B2/en active Active
- 2017-09-08 EP EP17923731.8A patent/EP3677695A4/en active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2005350766A (ja) * | 2004-05-13 | 2005-12-22 | Sumitomo Metal Mining Co Ltd | ニッケル酸化鉱石の湿式製錬方法 |
KR20070094819A (ko) * | 2004-12-30 | 2007-09-21 | 비에이치피 빌리톤 에스에스엠 테크놀로지 피티와이 엘티디 | 수지 용출 스트림으로부터 니켈 및 코발트의 추출 |
KR20070107787A (ko) * | 2005-02-24 | 2007-11-07 | 비에이치피 빌리톤 에스에스엠 테크놀로지 피티와이 엘티디 | 페로니켈 제조 |
KR20090042996A (ko) * | 2006-08-23 | 2009-05-04 | 비에이치피 빌리톤 에스에스엠 디벨롭먼트 피티와이 엘티디 | 철 함량이 낮은 금속 니켈 제조 |
JP5904459B2 (ja) * | 2011-11-22 | 2016-04-13 | 住友金属鉱山株式会社 | 高純度硫酸ニッケルの製造方法 |
Non-Patent Citations (1)
Title |
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See also references of EP3677695A4 * |
Also Published As
Publication number | Publication date |
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EP3677695A4 (en) | 2021-06-02 |
EP3677695A1 (en) | 2020-07-08 |
AU2017430097B2 (en) | 2021-12-23 |
KR101950314B1 (ko) | 2019-02-20 |
AU2017430097A1 (en) | 2020-04-09 |
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