CN116568831A - Method for extracting nickel sulfate from high nickel matte - Google Patents
Method for extracting nickel sulfate from high nickel matte Download PDFInfo
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- CN116568831A CN116568831A CN202180081614.5A CN202180081614A CN116568831A CN 116568831 A CN116568831 A CN 116568831A CN 202180081614 A CN202180081614 A CN 202180081614A CN 116568831 A CN116568831 A CN 116568831A
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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
- C22B11/00—Obtaining noble metals
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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
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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
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention discloses a method for extracting nickel sulfate from high nickel matte, which comprises the following steps: pulping the treated high nickel matte by adopting the pressure leached liquid produced by the back-end process; then, purifying and impurity-removing the pulpified high nickel matte slurry, and carrying out solid-liquid separation to obtain a nickel cobalt sulfate solution and purified and impurity-removing slag; pulping the purified impurity-removed slag by adopting normal-pressure nickel-leaching precursor solution; then, sequentially carrying out normal-pressure nickel leaching and pressure nickel leaching on the pulpified purified and impurity-removed slag slurry; finally, carrying out solid-liquid separation to obtain a pressure leaching solution and pressure leaching residues; the normal pressure nickel-immersing front liquid is obtained by mixing the pressure leached liquid of the back-end process, sulfuric acid and copper sulfate, wherein Cu in the normal pressure nickel-immersing front liquid 2+ The concentration is 1-20 g/L. The method can realize no three-waste discharge, the leaching rate of nickel and cobalt reaches more than 98 percent, and the pressurized leaching slag can be used as the export of iron raw materials.
Description
The invention belongs to the technical field of nonferrous metal hydrometallurgy, and particularly relates to a method for extracting nickel sulfate from high nickel matte.
In recent years, new energy automobiles rapidly develop, the energy density required by automobile power batteries is continuously improved, and the mature positive electrode in the current market can only be met by ternary materials, and high nickel is the development direction of the ternary materials in the future. Therefore, nickel sulfate is required to be used as a new energy battery material, and the productivity and the yield of the nickel sulfate are also increased in an explosive manner.
At present, the traditional nickel sulfate production process mainly comprises the steps of producing high nickel matte by adopting a nickel sulfide ore pyrometallurgy method and then producing nickel sulfate by adopting a wet process, wherein the retained reserves of the nickel sulfide ore are drastically reduced, the exploitation difficulty is increased, the nickel grade is reduced, the exploitation cost is increased, and the international nickel industry has changed from the nickel sulfide ore to the nickel laterite ore. The nickel laterite is mainly used for producing nickel sulfate by adopting a pressurized acid leaching process, and then nickel sulfate solution is produced after the procedures of acid dissolution, extraction, impurity removal and the like.
Along with the gradual maturity of the technology for smelting high nickel matte by a nickel laterite fire method, the large-scale production of the high nickel matte by the nickel laterite smelting is started, and the high nickel matte material produced by the nickel laterite has different mineral characteristics from the high nickel matte produced by the traditional sulphide ore, so that the method for producing nickel sulfate by the high nickel matte by the nickel laterite is required to be provided in a targeted manner, the current situation that the productivity of the nickel sulfate produced by the traditional nickel laterite is low is changed, and the rapidly-growing requirement of the nickel sulfate market in the battery industry is met.
In order to solve the problem of low productivity in the existing method for extracting nickel sulfate from high nickel matte, the invention provides a method for extracting nickel sulfate from high nickel matte.
The invention provides a method for extracting nickel sulfate from high nickel matte, which comprises the following steps:
pulping the treated high nickel matte by adopting the pressure leached liquid produced by the back-end process; then, purifying and impurity-removing the pulpified high nickel matte slurry, and carrying out solid-liquid separation to obtain a nickel cobalt sulfate solution and purified and impurity-removing slag;
pulping the purified impurity-removed slag by adopting normal-pressure nickel-leaching precursor solution; then, sequentially carrying out normal-pressure nickel leaching and pressure nickel leaching on the pulpified purified and impurity-removed slag slurry; finally, carrying out solid-liquid separation to obtain a pressure leaching solution and pressure leaching residues;
the normal pressure nickel-immersing front liquid is obtained by mixing the pressure leached liquid of the back-end process, water, sulfuric acid and copper sulfate, wherein Cu in the normal pressure nickel-immersing front liquid 2+ The concentration is 1-20 g/L.
Cu 2+ The concentration of 1-20 g/L is that copper can accelerate leaching reaction, and simultaneously prevent hydrogen sulfide from being emitted from ore pulp to damage equipment and human body. Cu in normal pressure nickel immersion liquid 2+ The concentration may be 1g/L, 20g/L, or any concentration of 1 to 20g/L, and the specific concentration is determined according to the actual situation.
Further, the purifying and impurity removing process comprises the following steps: adding compressed air or oxygen-enriched air into the pulpified high nickel matte slurry, and controlling the pH value of the reaction end point of the purification and impurity removal to be 4.0-6.5. The purpose of adding the oxidant is to oxidize ferrous iron in the slurried high nickel matte slurry, so as to prepare for iron precipitation in the purification process. The purpose of controlling the pH of the end point of the purification and impurity removal reaction to be 4.0-6.5 is to completely precipitate iron and copper as much as possible.
Controlling the reaction end point pH of the purification and the impurity removal to be 4.0 to 6.5 means that in a specific embodiment, the reaction end point pH of the purification and the impurity removal can be 4.0, can be 6.5, can be any value in the range of 4.0 to 6.5, and the specific pH is determined according to practical situations, and can be a dynamic pH value, but the dynamic pH is also in the range of 4.0 to 6.5.
Further, the reaction temperature is controlled to be 60-90 ℃ and the ventilation rate is controlled to be 500-2500 NM in the purification and impurity removal process 3 And/t material, and the reaction time is 3-h-8 h. In a specific embodiment, the reaction temperature may be 60 ℃, may be 90 ℃, or may be any temperature value in the range of 60 to 90 ℃. In a particular embodiment, the ventilation may be 500NM 3 The material/t is 2500NM 3 The material/t can also be 500-2500 NM 3 And (3) any ventilation quantity value in the material. In a specific embodiment, the reaction time may be 3 hours, may be 8 hours, or may be any time point from 3 to 8 hours according to actual conditions.
Further, adding an oxidant into the pulpified high nickel matte slurry specifically comprises: and (3) introducing compressed air or oxygen-enriched air into the pulpified high nickel matte slurry.
Further, the process of normal pressure nickel leaching comprises the following steps: compressed air or oxygen-enriched air is introduced into the pulpified purified and impurity-removed slag slurry, and the pH value of the reaction end point is controlled to be 0.5-3.5 by controlling the addition amount of sulfuric acid, at the moment, the purpose of controlling the reaction pH is to provide proper acidity for normal-pressure nickel leaching and pressure nickel leaching, and the pressure nickel leaching can completely react metal nickel within the acidity, so that hydrogen is prevented from generating during pressurization. At this time, a small part of the introduced compressed air or oxygen-enriched air participates in the reaction, and a large part of the compressed air or oxygen-enriched air is discharged out of the reaction system.
By controlling the amount of sulfuric acid added to control the pH of the reaction end point to be 0.5 to 3.5 is meant that in a specific example, the pH of the reaction end point can be controlled to be 0.5, the pH of the reaction end point can be controlled to be 3.5, or the pH of the reaction end point can be any value in the range of 0.5 to 3.5.
Further, the reaction temperature is controlled to be 60-90 ℃ and the ventilation rate is controlled to be 500-2500 NM in the normal pressure nickel leaching process 3 And/t material for 3-8 h.
Further, the pressure leaching process includes: adding oxidant into ore pulp after normal pressure nickel leaching, controlling the temperature to be 130-220 ℃, the reaction time to be 2-8 h, the oxygen partial pressure to be 0.1-1.5 Mpa, and the pH value at the end of the reaction to be 1.0-3.5. The aim of controlling the reaction temperature, the reaction time, the oxygen partial pressure and the reaction end pH is to completely leach the nickel as much as possible, reduce the nickel content in the pressure leaching slag as much as possible and avoid nickel waste in the pressure leaching process.
In a specific embodiment, the reaction temperature of the pressure leaching may be 130 ℃, 220 ℃ or any temperature value in the range of 130-220 ℃. In a specific embodiment, the reaction time may be 2h, may be 8h, or may be any time point value from 2h to 8h. In a specific embodiment, the partial pressure of oxygen may be 0.1Mpa, may be 1.0 Mpa, may be 1.2 Mpa, may be 1.5 Mpa, and may be any value in the range of 0.1 to 1.5 Mpa. Oxygen partial pressure lower than 0.1Mpa affects the leaching rate of nickel; however, an oxygen partial pressure higher than 1.5 Mpa does not bring about an effective increase in nickel leaching rate, but has higher requirements for the apparatus of the present invention, which leads to an increase in the cost of the entire process. In particular embodiments, the reaction endpoint pH may be 1.0, may be 3.5, or may be any value in the range of 1.0 to 3.5.
Further, adding an oxidant into the ore pulp after normal pressure nickel leaching comprises: oxygen is introduced into the ore pulp after nickel leaching under normal pressure.
Further, in the process of pulping the treated high nickel matte by adopting the pressure leached liquid produced by the back-end process, the pulping solid-liquid ratio is controlled to be 4-10: 1, the slurrying time is 0.5-2 h. In a specific embodiment, the solid-to-liquid ratio may be 4:1, may be 10:1, or may be 4 to 10:1, the purpose of which is to thoroughly mix the high nickel matte with the pressure leached liquor.
Further, in the process of pulping the purified and impurity-removed slag by adopting normal-pressure nickel-leaching precursor solution, the pulping solid-liquid ratio is controlled to be 4-10: 1, the slurrying time is 0.5-2 h. In a specific embodiment, the solid-to-liquid ratio may be 4:1, may be 10:1, or may be 4 to 10:1, and aims to fully mix the purified and impurity-removed slag with the normal-pressure nickel-immersing precursor solution.
Compared with the prior art, the invention has the beneficial effects that by adopting the scheme, the invention has the following advantages:
nickel in high nickel matte exists in two forms, one is metallic phase nickel and the other is nonmetallic phase nickel; the content of the nonmetallic phase nickel is large, only partial metallic phase nickel and impurities are leached out by displacement reaction through pulping and purifying and impurity removal, and a large amount of nonmetallic phase nickel and the rest of metallic phase nickel exist in the purifying and impurity removal slag; in order to realize the recovery of nickel in the purified and impurity-removed slag, the purified and impurity-removed slag is further required to be pulpified, and then nickel is leached into a pressure leaching liquid in a mode of normal pressure nickel leaching and pressure nickel leaching in sequence, so that the recovery of nickel in the high nickel matte is realized, the waste liquid is avoided, and the leaching rate of nickel and cobalt is up to more than 98 percent; ni in the nickel cobalt sulfate solution generated by purifying and removing impurities is more than or equal to 90g/L, cu is less than or equal to 0.01g/L, fe and less than or equal to 0.01g/L; the pressure leaching slag contains less than 1% of nickel and the iron content reaches more than 55%, so that the pressure leaching slag can be used as an iron raw material for sale, and waste slag is avoided. Meanwhile, no waste gas is generated in the whole preparation process.
FIG. 1 is a flow chart of a method for extracting nickel sulfate from high nickel matte provided by the invention.
In order that the above-recited objects, features and advantages of the invention will be more clearly understood, a more particular description of the invention will be rendered by reference to specific embodiments thereof. It should be noted that, in the case of no conflict, the embodiments of the present application and the features in the embodiments may be combined with each other.
As shown in fig. 1, the present invention provides a method for extracting nickel sulfate from nickel matte, the method comprising:
pulping the treated high nickel matte by adopting the pressure leaching liquid produced by the back-end process, so as to fully mix the treated high nickel matte with the pressure leaching liquid; then, purifying and impurity-removing the pulpified high nickel matte slurry, and carrying out solid-liquid separation to obtain a nickel cobalt sulfate solution and purified and impurity-removed slag, wherein the separation of nickel cobalt and impurities is realized;
pulping the purified and impurity-removed slag by adopting normal-pressure nickel-immersing precursor liquid; then, sequentially carrying out normal-pressure nickel leaching and pressure nickel leaching on the pulpified purified and impurity-removed slag slurry; finally, carrying out solid-liquid separation to obtain a pressure leaching solution and pressure leaching residues;
the normal pressure nickel-immersing front liquid is obtained by mixing the pressure leached front liquid of the back-end process, water, sulfuric acid and copper sulfate, wherein Cu in the normal pressure nickel-immersing front liquid 2+ The concentration is 1-20 g/L.
Nickel in high nickel matte exists in two forms, one is metallic phase nickel and the other is nonmetallic phase nickel; the content of the nonmetallic phase nickel is large, only partial metallic phase nickel and impurities are leached out by displacement reaction through pulping and purifying and removing impurities, and a large amount of nonmetallic phase nickel and the rest of metallic phase nickel exist in the purifying and removing impurities slag; in order to realize the recovery of nonmetallic phase nickel, the invention also needs to continuously slurry the purified and impurity-removed slag, then sequentially adopts the modes of normal pressure nickel leaching and pressure nickel leaching to separate nickel from other impurities, nickel enters the liquid after pressure leaching, the liquid after pressure leaching returns to the extraction process of the invention, and the recovery of nickel in high nickel matte is realized by cyclic reciprocation, so that the nickel cobalt leaching rate is over 98 percent while the waste liquid is avoided; ni in the nickel cobalt sulfate solution generated by purifying and removing impurities is more than or equal to 90g/L, cu is less than or equal to 0.01g/L, fe and less than or equal to 0.01g/L; the pressure leaching slag contains less than 1% of nickel and the iron content reaches more than 55%, so that the pressure leaching slag can be used as an iron raw material for sale, and waste slag is avoided. Meanwhile, no waste gas is generated in the whole preparation process. Copper sulfate is added into the normal pressure nickel-leaching precursor liquid, and copper ions can be recycled in the whole production system.
Examples
1
The embodiment provides a method for extracting nickel sulfate from high nickel matte, wherein the high nickel matte is from nickel laterite, and the components (%) are as follows: ni-78, fe-1, co-1, S-20.
The method for extracting nickel sulfate from the high nickel matte specifically comprises the following steps:
s1, ball milling is carried out on high nickel matte to obtain 90% of materials with particle sizes below 200 meshes for later use;
the pressure leached liquid produced by the back-end process of the embodiment is mixed with the materials obtained by ball milling, and pulpified, wherein the pulpified solid-to-liquid ratio is 8:1, pulping for 1h to obtain high nickel matte slurry;
s2, adding the high nickel matte slurry into a purifying and impurity removing tank, introducing compressed air or oxygen-enriched air into the purifying and impurity removing tank, controlling the temperature to 80 ℃ in the whole purifying and impurity removing reaction process, and controlling the ventilation rate to 1500NM 3 Material/t, time 6h, end point pH 6.0. Carrying out solid-liquid separation on the ore pulp after purifying and removing impurities to obtain nickel-cobalt sulfate solution and purifying and removing impurities;
s3, firstly, mixing the pressure leaching solution produced by the back-end process with sulfuric acid, copper sulfate and water to prepare normal-pressure nickel leaching precursor solution, and carrying out normal-pressure nickel leaching on Cu in the normal-pressure nickel leaching precursor solution 2+ The concentration is 8g/L;
then, mixing and stirring the normal pressure nickel-immersing precursor solution and the purified impurity-removing slag for slurrying, and controlling the solid-liquid ratio of slurrying to be 9:1, pulping for 1h to obtain purified and impurity-removed slag slurry;
s4, adding the purified and impurity-removed slag slurry into an ordinary pressure nickel leaching tank, introducing compressed air or oxygen-enriched air into the ordinary pressure nickel leaching tank, controlling the temperature to be 80 ℃ and the ventilation rate to be 1500NM in the whole ordinary pressure nickel leaching process 3 Material/t, time 5h, pH value of reaction end point 1.8, wherein the nickel is immersed under normal pressure by controlling the adding amount of sulfuric acidThe reaction end point pH;
s5, adding the mineral aggregate subjected to normal-pressure nickel leaching into a pressurized nickel leaching kettle, introducing oxygen as an oxidant for reaction, controlling the reaction temperature to 165 ℃, the reaction time to 6 hours, the oxygen partial pressure to 0.5 Mpa, and the reaction end-point pH value to 1.5; and then carrying out solid-liquid separation on the pulp after pressure leaching to obtain pressure leached liquid and pressure leached slag, wherein the pressure leached liquid is returned to purify the impurity-removing slurrying ingredients and the normal-pressure nickel-leaching slurrying ingredients, and the pressure leached slag is used as an iron raw material for sale.
After the treatment in the process, the material components of each section are as follows:
nickel cobalt sulfate solution (g/L): ni 96.38,Cu 0.006,Fe 0.003,Co 1.26.
Pressurized leaching residue (%): fe 57.29, ni 0.81
The leaching rate of Ni and Co is more than or equal to 98 percent
Slag rate is 3.5 percent.
Examples
2
The embodiment provides a method for extracting nickel sulfate from high nickel matte, wherein the high nickel matte is from nickel laterite, and the components (%) are as follows: ni-75, fe-1, co-1, S-22.
The method for extracting nickel sulfate from the high nickel matte specifically comprises the following steps:
s1, ball milling is carried out on high nickel matte to obtain 90% of materials with particle sizes below 200 meshes for later use;
the pressure leached liquid produced by the back-end process of the embodiment is mixed with the materials obtained by ball milling, and pulpified, wherein the pulpified solid-to-liquid ratio is 7:1, pulping for 1h to obtain high nickel matte slurry;
s2, adding the high nickel matte slurry into a purifying and impurity removing tank, introducing compressed air or oxygen-enriched air into the purifying and impurity removing tank, controlling the temperature to be 85 ℃ in the whole purifying and impurity removing reaction process, and controlling the ventilation quantity to be 1800NM 3 Material/t, time 6.5h, end point pH 6.2. Carrying out solid-liquid separation on the ore pulp after purifying and removing impurities to obtain nickel-cobalt sulfate solution and purifying and removing impurities;
s3, firstly, mixing the pressure leaching solution produced by the back-end process with sulfuric acid, copper sulfate and water to prepare normal-pressure nickel leaching precursor solution, and carrying out normal-pressure nickel leaching on Cu in the normal-pressure nickel leaching precursor solution 2+ The concentration is 10g/L;
then, mixing and stirring the normal pressure nickel-immersing precursor solution and the purified impurity-removing slag for pulping, and controlling the solid-liquid ratio of pulping to be 8:1, pulping for 1h to obtain purified and impurity-removed slag slurry;
s4, adding the purified and impurity-removed slag slurry into an ordinary pressure nickel leaching tank, introducing compressed air or oxygen-enriched air into the ordinary pressure nickel leaching tank, controlling the temperature to be 85 ℃ and the ventilation quantity to be 1800NM in the whole ordinary pressure nickel leaching process 3 Material/t, time 5.5. 5.5 h, reaction end point pH value 2.0, wherein the normal pressure nickel leaching reaction end point pH is controlled by controlling the addition amount of sulfuric acid;
s5, adding the mineral aggregate subjected to normal pressure nickel leaching into a pressurized nickel leaching kettle, introducing oxygen as an oxidant for reaction, controlling the reaction temperature to 170 ℃, controlling the reaction time to 6 hours, controlling the oxygen partial pressure to 0.4 Mpa, and controlling the pH value at the end of the reaction to 1.8; and then carrying out solid-liquid separation on the pulp after pressure leaching to obtain pressure leached liquid and pressure leached slag, wherein the pressure leached liquid is returned to purify the impurity-removing slurrying ingredients and the normal-pressure nickel-leaching slurrying ingredients, and the pressure leached slag is used as an iron raw material for sale.
After the treatment in the process, the material components of each section are as follows:
nickel cobalt sulfate solution (g/L): ni 101.65,Cu 0.0001,Fe 0.001,Co 1.48.
Pressurized leaching residue (%): fe 59.68, ni 0.85
The leaching rate of Ni and Co is more than or equal to 98 percent
Slag rate is 3.0 percent.
The present invention is not limited to the above-mentioned embodiments, and any changes or substitutions that can be easily understood by those skilled in the art within the technical scope of the present invention are intended to be included in the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the claims.
Claims (10)
- A method for extracting nickel sulfate from high nickel matte, the method comprising:pulping the treated high nickel matte by adopting the pressure leached liquid produced by the back-end process; then, purifying and impurity-removing the pulpified high nickel matte slurry, and carrying out solid-liquid separation to obtain a nickel cobalt sulfate solution and purified and impurity-removing slag;pulping the purified impurity-removed slag by adopting normal-pressure nickel-leaching precursor solution; then, sequentially carrying out normal-pressure nickel leaching and pressure nickel leaching on the pulpified purified and impurity-removed slag slurry; finally, carrying out solid-liquid separation to obtain a pressure leaching solution and pressure leaching residues;the normal pressure nickel-immersing front liquid is obtained by mixing the pressure leached liquid of the back-end process, water, sulfuric acid and copper sulfate, wherein Cu in the normal pressure nickel-immersing front liquid 2+ The concentration is 1-20 g/L.
- The method for extracting nickel sulfate from high nickel matte according to claim 1, wherein the purifying and impurity removing process comprises: and adding an oxidant into the pulpified high nickel matte slurry, and controlling the pH value of the reaction end point of the purification and impurity removal to be 4.0-6.5.
- The method for extracting nickel sulfate from high nickel matte according to claim 2, wherein the reaction temperature is controlled to be 60-90 ℃ and the ventilation rate is controlled to be 500-2500 NM in the purification and impurity removal process 3 And/t material, and the reaction time is 3-8 h.
- The method for extracting nickel sulfate from high nickel matte according to claim 2, wherein adding an oxidizing agent to the slurried high nickel matte slurry specifically comprises: and (3) introducing compressed air or oxygen-enriched air into the pulpified high nickel matte slurry.
- The method for extracting nickel sulfate from high nickel matte according to claim 1, wherein the process of atmospheric pressure nickel leaching comprises: compressed air or oxygen-enriched air is introduced into the pulpified purified and impurity-removed slag slurry, and the pH value of the reaction end point is controlled to be 0.5-3.5 by controlling the addition amount of sulfuric acid.
- The method for extracting nickel sulfate from high nickel matte according to claim 5, wherein the reaction temperature is controlled to be 60-90 ℃ and the ventilation rate is controlled to be 500-2500 NM in the normal pressure nickel leaching process 3 And/t material for 3-8 h.
- The method of extracting nickel sulfate from high grade nickel matte of claim 1 wherein the pressure leaching process comprises: adding oxidant into ore pulp after normal pressure nickel leaching, controlling the temperature to be 130-220 ℃, the reaction time to be 2-8 h, the oxygen partial pressure to be 0.1-1.5 Mpa, and the pH value at the end of the reaction to be 1.0-3.5.
- The method for extracting nickel sulfate from high grade nickel matte of claim 7 wherein adding an oxidizer to the slurry after the atmospheric pressure nickel leaching comprises: oxygen is introduced into ore pulp after nickel is immersed under normal pressure.
- The method for extracting nickel sulfate from high nickel matte according to any one of claims 1-8, wherein in the process of pulping the treated high nickel matte by adopting the pressure leached liquid produced by the back-end process, the pulping solid-liquid ratio is controlled to be 4-10: 1, the slurrying time is 0.5-2 h.
- The method for extracting nickel sulfate from high nickel matte according to any one of claims 1-8, wherein in the process of pulping the purified and impurity-removed slag by adopting a normal pressure nickel leaching pre-liquid, the pulping solid-liquid ratio is controlled to be 4-10: 1, the slurrying time is 0.5-2 h.
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| PCT/CN2021/133610 WO2023092480A1 (en) | 2021-11-26 | 2021-11-26 | Method for extracting nickel sulfate from nickel matte |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6428604B1 (en) * | 2000-09-18 | 2002-08-06 | Inco Limited | Hydrometallurgical process for the recovery of nickel and cobalt values from a sulfidic flotation concentrate |
| CN101195858B (en) * | 2007-12-20 | 2010-08-25 | 金川集团有限公司 | Method for extracting nickel with pressure leaching of non-metal high nickel sulfonium material |
| KR101412462B1 (en) * | 2013-12-19 | 2014-06-30 | 주식회사 에너텍 | Highly Purified Nickel Sulfate from Nickel and Cobalt Mixed hydroxide precipitation and the Manufacturing Method of the Same |
| CN104630464A (en) * | 2014-12-31 | 2015-05-20 | 金川集团股份有限公司 | Method for extracting nickel and cobalt from laterite-nickel ores by atmospheric-pressure acid leaching |
| CN106399682A (en) * | 2016-09-23 | 2017-02-15 | 中国恩菲工程技术有限公司 | Method for extracting valuable metal from copper, cobalt and nickel sulfide |
| CN110241310B (en) * | 2019-06-18 | 2021-10-01 | 深圳市坤鹏冶金工程技术有限公司 | Method for enriching noble metals by selective oxygen pressure leaching of high-iron high-copper nickel-containing material |
| CN112342377B (en) * | 2020-11-13 | 2022-12-09 | 中国恩菲工程技术有限公司 | Treatment process of nickel concentrate |
| CN112779419B (en) * | 2020-12-24 | 2022-09-13 | 浙江华友钴业股份有限公司 | Method for removing iron, aluminum and silicon from nickel, cobalt, manganese and copper solution under normal pressure |
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