WO2024031789A1 - 还原硫化冶炼红土镍矿生产高冰镍的方法 - Google Patents

还原硫化冶炼红土镍矿生产高冰镍的方法 Download PDF

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WO2024031789A1
WO2024031789A1 PCT/CN2022/120357 CN2022120357W WO2024031789A1 WO 2024031789 A1 WO2024031789 A1 WO 2024031789A1 CN 2022120357 W CN2022120357 W CN 2022120357W WO 2024031789 A1 WO2024031789 A1 WO 2024031789A1
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nickel
slag
matte
cobalt
smelting
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PCT/CN2022/120357
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English (en)
French (fr)
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唐时健
李长东
岳雄
刘云涛
阮丁山
陈绪林
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广东邦普循环科技有限公司
湖南邦普循环科技有限公司
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Publication of WO2024031789A1 publication Critical patent/WO2024031789A1/zh

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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
    • C22B23/02—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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/24—Binding; Briquetting ; Granulating
    • C22B1/2406—Binding; Briquetting ; Granulating pelletizing
    • 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 invention belongs to the technical field of non-ferrous metallurgy, and specifically relates to a method for producing high matte nickel by reducing sulfide smelting laterite nickel ore.
  • Nickel metal has excellent physical and chemical properties, such as high melting point, strong magnetism, excellent corrosion resistance, ductility, and oxidation resistance. It is widely used in the chemical industry, machinery manufacturing industry, electrical instrument industry, and new energy vehicle batteries. materials and other fields. Among them, battery materials are another major demand area for nickel applications. As emerging industries such as new energy electric vehicles and new space energy batteries continue to develop in my country, the demand for nickel in the new energy market continues to rise.
  • Laterite nickel ore As nickel sulfide ore resources continue to decrease, laterite nickel ore has gradually become the mainstream nickel resource for the production of nickel and cobalt-containing products.
  • Laterite nickel ore can be divided into limonite, cobaltite, nontronite, serpentine and silico-magnesium nickel ore according to the cross-sectional characteristics. Limonite and cobaltite are generally processed by pressurized acid leaching process and reduction roasting ammonia leaching process. ore and part of nontronite, while nontronite, serpentine and silico-magnesium ore are mainly processed by pyrotechnics.
  • the fire treatment process can be divided into reduction smelting ferronickel process and reduction smelting nickel matte process according to the different products produced.
  • the reduction smelting nickel matte process is as follows: the ore is dried, screened, and crushed, and then a sulfiding agent is added for sulfurization and smelting.
  • the obtained low-nickel matte enters the converter and is blown to produce high-nickel matte.
  • the high-nickel matte can be further processed to obtain different products. Nickel products.
  • the reduction smelting nickel matte process is a process developed through continuous exploration and innovation based on the reduction smelting nickel-iron process.
  • a sulfiding agent is added for reduction sulfidation to produce matte nickel.
  • the reduction sulfidation process is rarely used to produce high-ice nickel.
  • the supply of ternary materials exceeds the demand.
  • the supply of nickel sulfate and cobalt sulfate raw materials is insufficient, and it is necessary to comprehensively extract it from nickel and cobalt resources. Produce cobalt-rich high matte nickel.
  • the existing reduction smelting nickel matte process generally has problems such as high energy consumption, low safety, low thermal efficiency, and low nickel and cobalt yield.
  • Direct use of side-blown furnaces for reduction sulfurization generally requires large amounts of vulcanizing agents and reducing agents, and reduces the sulfurization time. Problems such as long time, poor reductive vulcanization reaction effect, and low yield.
  • Nickel metal has excellent physical and chemical properties, such as high melting point, strong magnetism, excellent corrosion resistance, ductility, and oxidation resistance. It is widely used in the chemical industry, machinery manufacturing industry, electrical instrument industry, and new energy vehicle batteries. materials and other fields. Among them, battery materials are another major demand area for nickel applications. As emerging industries such as new energy electric vehicles and new space energy batteries continue to develop in my country, the demand for nickel in the new energy market continues to rise.
  • Laterite nickel ore As nickel sulfide ore resources continue to decrease, laterite nickel ore has gradually become the mainstream nickel resource for the production of nickel and cobalt-containing products.
  • Laterite nickel ore can be divided into limonite, cobaltite, nontronite, serpentine and silico-magnesium nickel ore according to the cross-sectional characteristics. Limonite and cobaltite are generally processed by pressurized acid leaching process and reduction roasting ammonia leaching process. ore and part of nontronite, while nontronite, serpentine and silico-magnesium ore are mainly processed by pyrotechnics.
  • the fire treatment process can be divided into reduction smelting ferronickel process and reduction smelting nickel matte process according to the different products produced.
  • the reduction smelting nickel matte process is as follows: the ore is dried, screened, and crushed, and then a sulfiding agent is added for sulfurization and smelting.
  • the obtained low-nickel matte enters the converter and is blown to produce high-nickel matte.
  • the high-nickel matte can be further processed to obtain different products. Nickel products.
  • the reduction smelting nickel matte process is a process developed through continuous exploration and innovation based on the reduction smelting nickel-iron process.
  • a sulfiding agent is added for reduction sulfidation to produce matte nickel.
  • the reduction sulfidation process is rarely used to produce high-ice nickel.
  • the supply of ternary materials exceeds the demand.
  • the supply of nickel sulfate and cobalt sulfate raw materials is insufficient, and it is necessary to comprehensively extract it from nickel and cobalt resources. Produce cobalt-rich high matte nickel.
  • the existing reduction smelting nickel matte process generally has problems such as high energy consumption, low safety, low thermal efficiency, and low nickel and cobalt yield.
  • Direct use of side-blown furnaces for reduction sulfurization generally requires a large amount of vulcanizing agent and reducing agent, and reduces the sulfurization time. Problems such as long time, poor reductive vulcanization reaction effect, and low yield.
  • Figure 1 is a process flow diagram of the present invention.
  • a method of using a rotary kiln and a side-blown furnace to continuously reduce sulfide smelting laterite nickel ore to produce high matte nickel Refer to Figure 1.
  • the specific process is:
  • Laterite nickel ore Preliminarily dry 10 tons of laterite nickel ore through a drying kiln. After drying and dehydration, the moisture content of the laterite nickel ore is 13%; then use a jaw crusher to crush the laterite nickel ore. After crushing, the laterite nickel ore is 95% The particle size of the above ore is less than 2mm.
  • the main components of laterite nickel ore are Ni 1.76wt%, Co 0.07wt%, Fe 34.67wt%, MgO 13.20wt%, and SiO 2 40.22wt%.
  • the first reducing agent is anthracite coal and the amount of the first reducing agent is laterite nickel ore. 3% of the mass, the first sulfiding agent is gypsum, the dosage is 6% of the laterite nickel ore mass, the first flux is limestone, the dosage is 5% of the laterite nickel ore mass.
  • the internal temperature of the laterite nickel ore pellets is pre-reduced and sulfurized and roasted at 1150°C for 1.5 hours, and the first reducing agent, the first sulfiding agent and the first flux are appropriately added according to the actual production conditions, in which the first reducing agent is added
  • the added amount is 1% of the mass of laterite nickel ore pellets
  • the first sulfiding agent added amount is 2% of the laterite nickel ore pellet mass
  • the first flux added amount is 1% of the laterite nickel ore pellet mass
  • part of the presulfurized roasting material is directly put into the side-blown furnace, and part is stored in the silo in the form of solid particles through the water quenching system, and then
  • the material system is put into the side-blowing furnace for reduction sulfurization smelting, which can ensure that the high-temperature melted pre-s
  • the high-temperature melted pre-sulfurized roasting materials can be After the water quenching system, they are stored in the form of solid particles in the batching bin; among them, the main reaction equation of pre-reduction sulfurization in the rotary kiln is as follows:
  • Fe 2 O 3 +CO Fe 3 O 4 +CO 2 ;
  • Fe 2 O 3 +CO FeO+CO 2 ;
  • FeO+CO Fe+CO 2 ;
  • NiO+CO Ni+CO 2 ;
  • FeO+CO+S 2 FeS 2 , CaSO 4 ) ⁇ FeS+CO 2 ;
  • the content of Fe 2 O 3 and the content of FeS in the obtained presulfurized roasted material were 10 wt% and 6 wt%, respectively.
  • the amount of pulverized coal added is 30% of the mass of the pre-sulfurized roasting material
  • the oxygen purity in the oxygen-rich gas is controlled to be 92%
  • the concentration of oxygen-rich air in the furnace is 60%
  • the air excess coefficient is 88%
  • the smelting temperature is controlled to 1500°C
  • the second reducing agent is anthracite coal
  • the dosage is 5% of the mass of the pre-sulfurized roasting material.
  • the second vulcanizing agent is The amount of gypsum added is 8% of the mass of the pre-sulfided roasting material.
  • the second flux is limestone.
  • the amount of added is 6% of the mass of the pre-sulfided roasting material.
  • the reduction sulfidation of valuable metals nickel and cobalt is completed to obtain low Nickel matte, smelting slag and flue gas.
  • the main chemical reaction formula of reduction and sulfurization in the side-blown furnace is as follows:
  • Fe 2 O 3 +CO Fe 3 O 4 +CO 2 ;
  • Fe 2 O 3 +CO FeO+CO 2 ;
  • FeO+CO Fe+CO 2 ;
  • NiO+CO Ni+CO 2 ;
  • FeO+CO+S 2 FeS 2 , CaSO 4 ) ⁇ FeS+CO 2 ;
  • CaO+SiO 2 CaO ⁇ SiO 2 ;
  • MgO+SiO 2 MgO ⁇ SiO 2 ;
  • the chemical composition of the obtained low matte nickel Ni 20.38wt%, Co 0.94wt%, Fe 53.69wt%, S 18.61wt%
  • the main chemical composition of the smelting slag Ni 0.16wt%, Co 0.005wt%, Fe 45.38wt%
  • the smelting slag Medium iron mainly exists in the form of FeS, FeO, and Fe 3 O 4 .
  • the high-temperature smelting slag produced in the above step (4) flows into the melting oxidation furnace through the chute, and the laterite nickel ore wet leaching slag and flux 4 are added to adjust the smelting slag composition.
  • the amount of laterite nickel ore wet leaching slag is: 10% of the mass of the smelting slag.
  • the main chemical components of the laterite nickel ore wet leaching slag are: Ni 0.07wt%, Fe 48wt%, Cr 1.97wt%, S 2wt%.
  • the fourth flux is limestone, and the amount added is the mass of the smelting slag.
  • the fuel is pulverized coal
  • the amount added is 10% of the mass of the slag
  • the iron elements in the smelting slag and leaching slag are massively oxidized to produce ferric oxide.
  • the temperature is first raised to 1480°C for 1.2 hours, and then the temperature is lowered to 1200°C at a cooling rate of 5°C/min. After the crystallization process Generate nickel-cobalt-rich magnetite.
  • the nickel-cobalt-rich magnetite is first separated by 6000Gs strong magnetic separation to separate nickel-cobalt-rich magnetite concentrate and waste 1.
  • the nickel-cobalt-rich magnetite concentrate is separated by 2000Gs weak magnetic separation to separate iron concentrate. 1 and nickel-rich cobalt matte slag 1.
  • the high-temperature molten low-matte nickel produced in step (4) is quenched by the water quenching system and stored in the nickel matte silo in the form of low-matte nickel particles. It is added to the bottom blowing furnace through a belt conveyor and 25000Nm 3 / h compressed air, add the third flux, the third flux is quartz stone, the dosage is 5% of the mass of low nickel matte, carry out deironing, desulfurization and slag making blowing operation at 1270°C for 2 hours, and produce high cobalt, high nickel matte, blown nickel matte Refining slag and soot.
  • low nickel matte blowing mainly converts low nickel matte into high nickel matte by adding quartz stone.
  • the blowing reaction of low nickel matte is an exothermic reaction, and the iron in low nickel matte is in the form of iron silicate.
  • the main chemical reactions of slagging and high matte separation and blowing are as follows:
  • Fe+1/2O 2 FeO
  • Ni 3 S 2 +7/2O 2 3NiO+2SO 2 ;
  • Ni 3 S 2 +2O 2 3Ni+2SO 2 ;
  • CoS+O 2 Co+SO 2 ;
  • the main components of the obtained high cobalt and high matte nickel Ni 75.67wt%, Co 2.34wt%, S 8.64wt%
  • the main chemical components of the blowing slag Ni 1.9wt%, Co 0.16wt%, Fe51.76wt%
  • iron in the blowing slag Mainly exists in the form of Fe 3 O 4 , FeS, FeO.
  • the high-temperature blowing slag produced in the above (6) flows into the melting oxidation furnace through the chute, and the laterite nickel ore wet leaching slag and the fourth flux are added to adjust the smelting slag composition.
  • the amount of laterite nickel ore wet leaching slag is added It is 12% of the mass of the smelting slag.
  • the main chemical components of the laterite nickel ore wet leaching slag are: Ni 0.07%, Fe 48%, Cr 1.97%, S 2%.
  • the fourth flux is limestone, and the amount added is 3% of the mass of the smelting slag.
  • the fuel is pulverized coal
  • the amount added is 5% of the mass of the smelting slag
  • the iron elements in the slag and leached slag are oxidized in large quantities to produce ferric oxide. Specifically, the temperature is first raised to 1520°C for 1.5 hours, and then the temperature is lowered to 1100°C at a cooling rate of 10°C/min, and the product is formed through the crystallization process.
  • the nickel-cobalt-rich magnetite is first separated by 6000Gs strong magnetic separation to separate the nickel-cobalt-rich magnetite concentrate and waste 2.
  • the nickel-cobalt-rich magnetite concentrate is separated by 2000Gs weak magnetic separation to separate the iron concentrate2. and nickel-rich cobalt matte slag2.
  • High-temperature melting of high-cobalt and high-matte nickel is cast into high-cobalt and high-matte nickel blocks.
  • nickel sulfate and cobalt sulfate are obtained;
  • the nickel-rich cobalt matte slag 1 and the nickel-rich cobalt matte slag 2 are returned to the bottom blowing furnace for blowing to recover nickel and cobalt. and other valuable metals;
  • iron concentrate 1 and iron concentrate 2 are directly sold for steelmaking or electromagnetic functional materials;
  • the flue gas generated by the rotary kiln, side blowing furnace, bottom blowing furnace and melting oxidation furnace collects smoke and dust through the dust collection system.
  • the desulfurization system's desulfurization meets emission standards, and the collected smoke and dust can be returned to the mixing and granulation process to participate in batching and granulation, or directly returned to the side-blown furnace to participate in reduction and sulfurization smelting.
  • the specific process is:
  • laterite nickel ore Preliminarily dry 10 tons of laterite nickel ore through a drying kiln. After drying and dehydration, the moisture content of the laterite nickel ore is 20%; then use a jaw crusher to crush the laterite nickel ore. After crushing, the laterite nickel ore is 94% The particle size of the above ore is less than 5mm.
  • the main components of laterite nickel ore are Ni 1.76wt%, Co 0.07wt%, Fe 34.67wt%, MgO 13.20wt%, and SiO 2 40.22wt%.
  • the first reducing agent is anthracite coal
  • the dosage is 7% of the mass of laterite nickel ore.
  • the first sulfiding agent is gypsum
  • the dosage is 9% of the mass of laterite nickel ore
  • the first flux is limestone, and the dosage is 6% of the mass of laterite nickel ore.
  • the high-temperature melted pre-sulfurized roasting material can be passed through
  • the water quenching system is stored in the batching bin in the form of solid particles.
  • the content of Fe 2 O 3 and FeS in the obtained pre-sulfurized roasting material is 2wt% and 12wt%.
  • the amount of pulverized coal added is 35% of the mass of the pre-sulfurized roasting material
  • the oxygen purity in the oxygen-rich gas is controlled to be 93%
  • the oxygen-rich air concentration in the furnace is 70%
  • the air excess coefficient is 87%
  • the smelting temperature is controlled. 1550°C
  • a second reducing agent is anthracite coal
  • the amount added is 5.6% of the mass of the pre-sulfurized roasting material.
  • the second vulcanizing agent It is gypsum, and the dosage is 10% of the mass of the pre-sulfurized roasting material.
  • the second flux is limestone, and the dosage is 6.5% of the mass of the pre-sulfurized roasting material.
  • the reduction sulfidation reaction the reduction sulfidation of valuable metals nickel and cobalt is completed, and we obtain Low matte nickel, smelting slag and flue gas, the chemical composition of the obtained low matte nickel: Ni 19.56wt%, Co 1.27wt%, Fe 55.61wt%, S 18.69wt%, the main chemical composition of the smelting slag: Ni 0.17wt%, Co 0.006 wt%, Fe 42.87wt%, iron in the smelting slag mainly exists in the form of FeS, FeO, Fe 3 O 4 .
  • the high-temperature smelting slag produced in the above step (4) flows into the melting oxidation furnace through the chute, and the laterite nickel ore wet leaching slag and the fourth flux are added to adjust the smelting slag composition, in which the amount of laterite nickel ore wet leaching slag is added It is 15% of the smelting slag mass.
  • the main chemical components of laterite nickel ore wet leaching slag are: Ni 0.05wt%, Fe 50.27wt%, Cr 1.65wt%, S 2.43wt%.
  • the fourth flux is limestone, and the added amount is smelting 3% of the mass of the slag. Inject the fuel to control the temperature to 1530°C.
  • the fuel is pulverized coal.
  • the added amount is 13% of the mass of the slag.
  • Blow in air to control the melting oxidation atmosphere so that the oxygen level of the smelting slag is lgpO2 10-3Pa.
  • a large amount of iron elements in the smelting slag and leaching slag are oxidized to produce ferric oxide.
  • the temperature is first raised to 1530°C and reacted for 2 hours, and then the temperature is lowered to 1230°C at a cooling rate of 10°C/min, and the crystallization process is carried out.
  • the nickel-cobalt-rich magnetite is first separated by 5000Gs strong magnetic separation to separate nickel-cobalt-rich magnetite concentrate and waste 1.
  • the nickel-cobalt-rich magnetite concentrate is separated by 2000Gs weak magnetic separation to separate iron concentrate. 1 and nickel-rich cobalt matte slag 1.
  • step (4) The high-temperature molten low-matte nickel produced in step (4) is quenched by the water quenching system, stored in the form of low-matte nickel particles in the nickel matte warehouse, and added to the bottom blowing furnace through a belt conveyor, and 26000Nm 3 / h compressed air, add the third flux, the third flux is quartz stone, the dosage is 8.5% of the mass of low nickel matte, carry out deironization, desulfurization and slag making blowing operation at 1230°C for 2 hours, producing high cobalt and high nickel matte, blowing Refining slag and soot.
  • low nickel matte blowing mainly converts low nickel matte into high nickel matte by adding quartz stone.
  • the blowing reaction of low nickel matte is an exothermic reaction, and the iron in low nickel matte is in the form of iron silicate.
  • the slagging and high matte nickel are separated.
  • the main components of the obtained high cobalt and high matte nickel are: Ni 72.29wt%, Co 2.37wt%, S 9.21wt%.
  • the main chemical components of the blowing slag are: Ni 1.54wt%, Co 0.13wt%, Fe 53.49wt %, iron in blowing slag mainly exists in the form of Fe 3 O 4 , FeS, and FeO.
  • the high-temperature blowing slag produced in the above (6) flows into the melting oxidation furnace through the chute, and the laterite nickel ore wet leaching slag and the fourth flux are added to adjust the smelting slag composition.
  • the amount of laterite nickel ore wet leaching slag is added It is 15% of the smelting slag mass.
  • the main chemical components of laterite nickel ore wet leaching slag are: Ni 0.05wt%, Fe 50.27wt%, Cr 1.65wt%, S 2.43wt%.
  • the fourth flux is limestone, and the added amount is smelting 4% of the mass of the slag. Inject the fuel to control the temperature to 1500°C.
  • the fuel is pulverized coal.
  • High-temperature melting of high-cobalt and high-matte nickel is cast into high-cobalt and high-matte nickel blocks.
  • nickel sulfate and cobalt sulfate are obtained;
  • the nickel-rich cobalt matte slag 1 and the nickel-rich cobalt matte slag 2 are returned to the bottom blowing furnace for blowing to recover nickel and cobalt. and other valuable metals;
  • iron concentrate 1 and iron concentrate 2 are directly sold for steelmaking or electromagnetic functional materials;
  • the flue gas generated by the rotary kiln, side blowing furnace, bottom blowing furnace and melting oxidation furnace collects smoke and dust through the dust collection system.
  • the desulfurization system's desulfurization meets emission standards, and the collected smoke and dust can be returned to the mixing and granulation process to participate in batching and granulation, or directly returned to the side-blown furnace to participate in reduction and sulfurization smelting.
  • the specific process is:
  • laterite nickel ore Preliminarily dry 10 tons of laterite nickel ore through a drying kiln. After drying and dehydration, the moisture content of the laterite nickel ore is 20%; then use a jaw crusher to crush the laterite nickel ore. After crushing, the laterite nickel ore is 96% The particle size of the above ore is less than 4.5mm.
  • the main components of laterite nickel ore are Ni 1.76wt%, Co 0.07wt%, Fe 34.67wt%, MgO 13.20wt%, and SiO 2 40.22wt%.
  • the first reducing agent is anthracite coal, and the dosage is 8.5% of the mass of laterite nickel ore.
  • the first sulfiding agent is gypsum, and the dosage is 10% of the mass of laterite nickel ore, and the first flux is limestone, and the dosage is 7.5% of the mass of laterite nickel ore.
  • the internal temperature of the laterite nickel ore pellets is pre-reduced and sulfurized and roasted at 1250°C for 1 hour, and the first reducing agent, the first sulfiding agent and the first flux are appropriately added according to the actual production conditions, of which the first reducing agent is added
  • the amount is 2.2% of the mass of laterite nickel ore pellets
  • the first sulfiding agent addition amount is 2.6% of the laterite nickel ore pellet mass
  • the first flux addition amount is 2.8% of the laterite nickel ore pellet mass
  • part of the presulfurized roasting material is directly put into the side-blown furnace, and part is stored in the silo in the form of solid particles through the water quenching system, and then fed
  • the system is put into the side-blown furnace for reduction sulfurization smelting, which ensures that the side-blown furnace can directly receive the high-temperature
  • the high-temperature melted pre-sulfurized roasting material can be passed through
  • the water quenching system is stored in the batching bin in the form of solid particles.
  • the content of Fe 2 O 3 and FeS in the obtained pre-sulfurized roasting material is 5wt% and 10wt%.
  • the amount of pulverized coal added is 38% of the mass of the pre-sulfurized roasting material
  • the oxygen purity in the oxygen-rich gas is controlled to be 95%
  • the oxygen-rich air concentration in the furnace is 73%
  • the air excess coefficient is 86%
  • the smelting temperature is controlled. 1530°C
  • a second reducing agent is anthracite coal
  • the dosage is 5.7% of the mass of the pre-sulfurized roasting material.
  • the second vulcanizing agent is The amount of gypsum added is 11% of the mass of the pre-sulfided roasting material.
  • the second flux is limestone.
  • the amount of added is 7.6% of the mass of the pre-sulfided roasting material.
  • the reduction sulfidation of valuable metals nickel and cobalt is completed to obtain low Nickel matte, smelting slag and flue gas, the chemical composition of low nickel matte obtained: Ni 23.87wt%, Co 1.38wt%, Fe 52.49wt%, S 16.74wt%, the main chemical composition of smelting slag: Ni 0.12wt%, Co 0.007wt %, Fe 46.31wt%, iron in the smelting slag mainly exists in the form of FeS, FeO, Fe 3 O 4 .
  • the high-temperature smelting slag produced in the above step (4) flows into the melting oxidation furnace through the chute, and the laterite nickel ore wet leaching slag and the fourth flux are added to adjust the smelting slag composition, in which the amount of laterite nickel ore wet leaching slag is added It is 20% of the smelting slag mass.
  • the main chemical components of laterite nickel ore wet leaching slag are: Ni 0.12wt%, Fe 47.69wt%, Cr 1.82wt%, S 1.45wt%.
  • the fourth flux is limestone, and the added amount is smelting 5% of the mass of the slag. Inject the fuel to control the temperature to 1550°C.
  • the fuel is pulverized coal.
  • the added amount is 15% of the mass of the slag.
  • Blow in air to control the melting oxidation atmosphere so that the oxygen level of the smelting slag is lgpO 2 10 -2.5 Pa, a large amount of iron elements in the smelting slag and leaching slag are oxidized to produce ferric oxide.
  • the temperature is first raised to 1550°C and reacted for 0.5h, and then the temperature is lowered to 1260°C at a cooling rate of 20°C/min.
  • the crystallization process generates nickel-cobalt-rich magnetite.
  • the nickel-cobalt-rich magnetite is first separated by 7000Gs strong magnetic separation to separate nickel-cobalt-rich magnetite concentrate and waste 1.
  • the nickel-cobalt-rich magnetite concentrate is separated by 3000Gs weak magnetic separation. Iron concentrate 1 and nickel-rich cobalt matte slag 1.
  • step (4) The high-temperature molten low-ice nickel produced in step (4) is quenched by the water quenching system and stored in the nickel-ice warehouse in the form of low-ice nickel particles. It is added to the bottom blowing furnace through a belt conveyor and 26500Nm 3 / h compressed air, add the third flux, the third flux is quartz stone, the dosage is 7.2% of the mass of low nickel matte, carry out deironization, desulfurization and slag making blowing operation at 1260°C for 3 hours, producing high cobalt and high nickel matte, blowing Refining slag and soot.
  • low nickel matte blowing mainly converts low nickel matte into high nickel matte by adding quartz stone.
  • the blowing reaction of low nickel matte is an exothermic reaction, and the iron in low nickel matte is in the form of iron silicate.
  • the slagging and high matte nickel are separated.
  • the main components of the high cobalt and high matte nickel are: Ni 76.48wt%, Co 2.82wt%, S 7.66wt%.
  • the main chemical components of the blowing slag are: Ni 1.71wt%, Co 0.19wt%, Fe 49.81wt %, iron in blowing slag mainly exists in the form of Fe 3 O 4 , FeS, and FeO.
  • the high-temperature blowing slag produced in the above (6) flows into the melting oxidation furnace through the chute, and the laterite nickel ore wet leaching slag and the fourth flux are added to adjust the smelting slag composition.
  • the amount of laterite nickel ore wet leaching slag is added It is 16% of the smelting slag mass.
  • the main chemical components of laterite nickel ore wet leaching slag are: Ni 0.12wt%, Fe 47.69wt%, Cr 1.82wt%, S 1.45wt%.
  • the fourth flux is limestone, and the added amount is smelting 7% of the mass of the slag. Inject the fuel to control the temperature to 1490°C.
  • the fuel is pulverized coal.
  • the nickel-cobalt-rich magnetite first undergoes 6000Gs of strong magnetic separation to separate the nickel-cobalt-rich magnetite concentrate and waste 2.
  • the nickel-cobalt-rich magnetite concentrate undergoes 2500Gs. Weak magnetic separation separates iron concentrate 2 and nickel-rich cobalt matte slag 2.
  • High-temperature melting of high-cobalt and high-matte nickel is cast into high-cobalt and high-matte nickel blocks.
  • nickel sulfate and cobalt sulfate are obtained;
  • the nickel-rich cobalt matte slag 1 and the nickel-rich cobalt matte slag 2 are returned to the bottom blowing furnace for blowing to recover nickel and cobalt. and other valuable metals;
  • iron concentrate 1 and iron concentrate 2 are directly sold for steelmaking or electromagnetic functional materials;
  • the flue gas generated by the rotary kiln, side blowing furnace, bottom blowing furnace and melting oxidation furnace collects smoke and dust through the dust collection system.
  • the desulfurization system's desulfurization meets emission standards, and the collected smoke and dust can be returned to the mixing and granulation process to participate in batching and granulation, or directly returned to the side-blown furnace to participate in reduction and sulfurization smelting.
  • the specific process is:
  • laterite nickel ore Preliminarily dry 10 tons of laterite nickel ore through a drying kiln. After drying and dehydration, the moisture content of the laterite nickel ore is 21%; then use a jaw crusher to crush the laterite nickel ore. After crushing, the laterite nickel ore is 90% The particle size of the above ore is less than 9mm.
  • the main components of laterite nickel ore are Ni 1.76wt%, Co 0.07wt%, Fe 34.67wt%, MgO 13.20wt%, and SiO 2 40.22wt%.
  • the first reducing agent is anthracite coal and the dosage is 13% of the mass of laterite nickel ore.
  • the first sulfiding agent is gypsum, and the dosage is 8% of the mass of laterite nickel ore, and the first flux is limestone, and the dosage is 12% of the mass of laterite nickel ore.
  • the laterite nickel ore pellets Feed the laterite nickel ore pellets into the rotary kiln through the feeding device, and introduce pulverized coal and oxygen-rich air for heating.
  • the amount of pulverized coal added is 46% of the quality of the laterite nickel ore pellets, and the monitoring furnace is strictly controlled.
  • Internal temperature the laterite nickel ore pellets are pre-reduced and sulfurized roasted at 350°C for 0.4h, so that the nickel and cobalt in the laterite nickel ore can fully react with the vulcanizing agent, reduce the volatilization loss of the vulcanizing agent, improve the vulcanizing efficiency, and then quickly heat up Secondary reduction and sulfurization roasting is carried out at a temperature of 600°C for 3 hours.
  • the main purpose is to aggregate and grow the nickel sulfide and cobalt sulfide grains, which facilitates subsequent smelting, sedimentation, separation and enrichment of nickel and cobalt in the side-blown furnace.
  • the first reducing agent, the first vulcanizing agent and the first flux are appropriately added.
  • the first reducing agent is added in an amount of 5% of the laterite nickel ore pellet mass
  • the first vulcanizing agent is added in an amount of 5% of the laterite nickel ore pellet mass.
  • the first flux supplement is 8% of the mass of laterite nickel ore pellets
  • reduced sulfide roasted sand is generated.
  • the particle size of the roasted sand after cooling is about 12mm; Fe 2 in the obtained reduced sulfide roasted sand
  • the content of O3 is 60wt%.
  • the reduced sulfurized roasting sand After the reduced sulfurized roasting sand is cooled, it is stored in the silo. When feeding, the ingredients can be weighed through the feeding belt and then added to the side-blown furnace. According to the material balance and heat balance calculation, the air volume per ton of reduced sulfurized roasting sand is 700Nm 3 , using a special spray gun to simultaneously spray pulverized coal, oxygen-rich gas, and compressed air into the molten pool of the side-blown furnace. The amount of pulverized coal added is 45% of the quality of the reduced sulfide roasting sand, and the content of the oxygen-rich gas is controlled.
  • the oxygen purity is 60%
  • the concentration of oxygen-rich air in the furnace is 45%
  • the air excess coefficient is 70%
  • the smelting temperature is controlled to 1300°C
  • the second reducing agent, the second vulcanizing agent and the second flux are added to perform a 3-hour reduction sulfurization reaction.
  • the second reducing agent is anthracite
  • the dosage is 10% of the quality of the reduced sulfide roasted sand.
  • the second sulfiding agent is gypsum, and the dosage is 7% of the quality of the reduced sulfide roasted sand.
  • the second flux is limestone, and the dosage is The amount is 13% of the quality of the reduction sulfide roasting sand.
  • the chemical composition of the obtained low matte nickel is: Ni 16.53wt%, Co 0.24 wt%, Fe 63.75wt%, S 19.10wt%
  • the main chemical composition of the smelting slag Ni 0.42wt%, Co 0.16wt%, Fe 36.78wt%
  • the iron in the smelting slag mainly exists in the form of FeS, FeO, Fe 3 O 4 .
  • step (4) The high-temperature molten low-ice nickel produced in step (4) is quenched by the water quenching system and stored in the nickel ice warehouse in the form of low-ice nickel particles. It is added to the converter through a belt conveyor and pumped into 29000Nm 3 /h compression air, add the third flux, the third flux is quartz stone, the dosage is 12% of the mass of low nickel matte, carry out deironization, desulfurization and slag making blowing operation at 1300°C for 3.5 hours to produce high cobalt, high nickel matte and blowing slag and soot.
  • low nickel matte blowing mainly converts low nickel matte into high nickel matte by adding quartz stone.
  • the blowing reaction of low nickel matte is an exothermic reaction, and the iron in low nickel matte forms slag in the form of iron silicate.
  • the main components of the obtained high cobalt and high matte nickel are: Ni 56.71wt%, Co 0.92wt%, S 10.57wt%.
  • the main chemical components of the blowing slag are: Ni 3.94wt%, Co 0.34wt%, Fe 61.79wt%.
  • Iron in blowing slag mainly exists in the form of Fe 3 O 4 , FeS, and FeO.
  • High-temperature melting of high-matte nickel is cast into high-cobalt and high-matte nickel blocks, and nickel sulfate and cobalt sulfate are obtained through subsequent wet processing; the blowing slag can be returned to the side-blown furnace to recover valuable metals such as nickel and cobalt after water quenching; converter flue gas, The flue gas collected from the side-blown furnace and the rotary furnace after dust collection and desulfurization can be returned to the mixed laterite nickel ore for granulation; the smelting slag produced by the side-blown furnace is directly sold externally.
  • Table 1 shows the main element contents of high cobalt and high nickel matte products produced in Examples 1, 2, 3 and Comparative Examples. The specific data are obtained by chemical methods.
  • Table 2 is a statistical table comparing the nickel recovery rate and cobalt recovery rate of the entire system of Examples 1, 2, 3 and the comparative example. The specific data is obtained through ingredient calculation, material balance calculation and heat balance calculation.
  • Example 1 Example 2
  • Example 3 Comparative ratio Nickel recovery rate (%) 97.21 96.53 97.91 80.27
  • Cobalt recovery rate (%) 95.71 94.78 95.88 70.36
  • the nickel recovery rate and cobalt recovery rate in the overall system in the embodiment are obviously better than those in Comparative Example 1, especially in Example 3.
  • the main reasons are: (1) The reduction sulfurization effect of the embodiment is better, the degree of enrichment of nickel and cobalt is high, and the obtained low matte nickel has a higher grade of nickel and cobalt.
  • the main factors affecting the grade of low nickel matte are the different pre-reduction temperatures and sulfurization degrees of the rotary kiln.
  • the comparative roasting temperature is lower, which does not provide the energy required for material reactions, making the reduction sulfurization reaction difficult, and the amount of additives is unreasonable.
  • the reducing agent and sulfurizing agent required for the reaction cannot be provided, making the reduction and sulfurization reaction incomplete and affecting the quality of low nickel matte.
  • the oxygen-rich air concentration in the side-blown furnace of the comparative example is 45%
  • the air excess coefficient is 70%
  • the smelting temperature is controlled at 1300°C, which results in poor smelting reaction, poor removal of impurities, and poor quality of the obtained low nickel matte.
  • the smelting slag and blowing slag of the comparative example did not further recycle the Ni and Co valuable metals in the slag, while the examples effectively recycled the nickel and cobalt in the slag through the melting oxidation furnace, so that the examples The recovery rates of nickel and cobalt were higher than in the comparative example.

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Abstract

一种还原硫化冶炼红土镍矿生产高冰镍的方法，将红土镍矿与还原剂、硫化剂和熔剂混合制成球团进行选择性预还原硫化焙烧，预硫化焙烧料进入侧吹炉，再添加还原剂、硫化剂和熔剂进行还原硫化反应，得到低冰镍和熔炼渣，低冰镍进行吹炼造渣处理得到高冰镍和吹炼渣，熔炼渣和/或吹炼渣进行熔融氧化生成四氧化三铁，再降温得到富镍钴磁铁矿，经分级磁选得铁精矿和富镍钴锍渣。采用回转窑和侧吹炉连续还原硫化熔炼红土镍矿产出低冰镍，能有效富集提取镍、钴等有价金属，流程工艺简单，安全性、环保性好，热效率高，综合能耗低，整个系统镍回收率为90-98％、钴回收率为90-97％，经济价值高。

Description

还原硫化冶炼红土镍矿生产高冰镍的方法 技术领域
本发明属于有色冶金技术领域，具体涉及一种还原硫化冶炼红土镍矿生产高冰镍的方法。
背景技术
金属镍具有优越的物理化学性质，具有熔点高、磁性强、优异的耐腐蚀性、延展性、抗氧化性等特点，被广泛应用于化学工业、机械制造工业、电器仪表工业、新能源汽车电池材料等多个领域。其中，电池材料是镍应用的又一大需求领域，随着我国新能源电动汽车、太空新型能源电池等新兴产业持续发展，新能源市场对镍的需求量持续上涨。
随着硫化镍矿资源不断降低，红土镍矿逐渐成为生产含镍、钴产品的主流镍资源。红土镍矿按照断面特点可分为褐铁矿、钴土矿、绿脱石、蛇纹石及硅镁镍矿，一般采用加压酸浸工艺和还原焙烧氨浸工艺处理褐铁矿、钴土矿及部分绿脱石，而绿脱石、蛇纹石及硅镁镍矿主要以火法工艺处理。
火法处理工艺按照生产产品的不同可分为还原熔炼镍铁工艺和还原熔炼镍锍工艺。其中还原熔炼镍锍工艺流程为：矿石经干燥、筛分、破碎后加入硫化剂硫化熔炼，得到的低镍锍进入转炉吹炼产出高镍锍，高镍锍通过进一步处理，可得到不同的镍产品。
还原熔炼镍锍工艺是在还原熔炼镍铁工艺基础上不断探索创新发展出的工艺，红土镍矿还原熔炼过程中加入硫化剂进行还原硫化生产冰镍。红土镍矿火法冶炼工艺中，较少采用还原硫化工艺生产高冰镍，随着新能源电池产业快速发展，三元材料供不应求，硫酸镍、硫酸钴原料供量不足，需从镍钴资源中综合提取生产出富钴高冰镍。但现有还原熔炼镍锍工艺普遍存在能耗高、安全性低、热效率低、镍钴收率低等问题，直接使用侧吹炉还原硫化，普遍存在硫化剂和还原剂用量多、还原硫化时间长、还原硫化反应效果较差、产量低等问题。
发明内容
金属镍具有优越的物理化学性质，具有熔点高、磁性强、优异的耐腐蚀性、延展性、抗氧化性等特点，被广泛应用于化学工业、机械制造工业、电器仪表工业、新能源汽车电池材料等多个领域。其中，电池材料是镍应用的又一大需求领域，随着我国新能源电动汽车、太空新型能源电池等新兴产业持续发展，新能源市场对镍的需求量持续上涨。
随着硫化镍矿资源不断降低，红土镍矿逐渐成为生产含镍、钴产品的主流镍资源。红土镍矿按照断面特点可分为褐铁矿、钴土矿、绿脱石、蛇纹石及硅镁镍矿，一般采用加压酸浸工艺和还原焙烧氨浸工艺处理褐铁矿、钴土矿及部分绿脱石，而绿脱石、蛇纹石及硅镁镍矿主要以火法工艺处理。
火法处理工艺按照生产产品的不同可分为还原熔炼镍铁工艺和还原熔炼镍锍工艺。其中还原熔炼镍锍工艺流程为：矿石经干燥、筛分、破碎后加入硫化剂硫化熔炼，得到的低镍锍进入转炉吹炼产出高镍锍，高镍锍通过进一步处理，可得到不同的镍产品。
还原熔炼镍锍工艺是在还原熔炼镍铁工艺基础上不断探索创新发展出的工艺，红土镍矿还原熔炼过程中加入硫化剂进行还原硫化生产冰镍。红土镍矿火法冶炼工艺中，较少采用还原硫化工艺生产高冰镍，随着新能源电池产业快速发展，三元材料供不应求，硫酸镍、硫酸钴原料供量不足，需从镍钴资源中综合提取生产出富钴高冰镍。但现有还原熔炼镍锍工艺普遍存在能耗高、安全性低、热效率低、镍钴收率低等问题，直接使用侧吹炉还原硫化，普遍存在硫化剂和还原剂用量多、还原硫化时间长、还原硫化反应效果较差、产量低等问题。
附图说明
下面结合附图和实施例对本发明做进一步的说明，其中：
图1为本发明的工艺流程图。
具体实施方式
以下将结合实施例对本发明的构思及产生的技术效果进行清楚、完整地描述，以充分地理解本发明的目的、特征和效果。显然，所描述的实施例只是本发明的一部分实施例，而不是全部实施例，基于本发明的实施例，本领域的技术人员在不付出创造性劳动的前提下所获得的其他实施例，均属于本发明保护的范围。
实施例1
一种利用回转窑和侧吹炉连续还原硫化冶炼红土镍矿生产高冰镍的方法，参照图1，具体过程为：
(1)通过干燥窑对10吨红土镍矿进行初步干燥，干燥脱水后红土镍矿的含水率为13％；再用颚式破碎机将红土镍矿进行破碎处理，破碎后红土镍矿95％以上矿粒度小于2mm，红土镍矿的主要成分为Ni 1.76wt％、Co 0.07wt％、Fe 34.67wt％、MgO 13.20wt％、SiO 2 40.22wt％。
(2)将干燥破碎后的红土镍矿通过皮带输送机送入圆盘制粒机，同时配入第一还原剂、第一硫化剂、第一熔剂，将红土镍矿与第一还原剂、第一硫化剂及第一熔剂进行混合制成球团，成球率为98％，球团直径为10-30mm，其中，第一还原剂为无烟煤，第一还原剂配入量为红土镍矿质量的3％，第一硫化剂为石膏，配入量为红土镍矿质量的6％，第一熔剂是石灰石，配入量为红土镍矿质量的5％。
(3)将红土镍矿球团通过进料装置送入回转窑，并通入粉煤和富氧空气供热，粉煤配入量为红土镍矿球团质量的30％，严格控制监测炉内温度，使红土镍矿球团在1150℃温度下预还原硫化焙烧1.5h，并根据实际生产情况，适当补加第一还原剂、第一硫化剂和第一熔剂，其中第一还原剂补加量为红土镍矿球团质量的1％，第一硫化剂补加量为红土镍矿球团质量的 2％，第一熔剂补加量为红土镍矿球团质量的1％，产出部分还原硫化焙砂和部分低镍锍的预硫化焙烧料(固液混合物)；预硫化焙烧料部分直接投入侧吹炉，部分经过水淬系统以固体颗粒形态堆存于料仓，再经进料系统投入侧吹炉进行还原硫化熔炼，便可保证侧吹炉正常熔炼时，可直接接收高温熔融的预硫化焙烧料，而侧吹炉停炉检修时，可将高温熔融的预硫化焙烧料经过水淬系统以固体颗粒形式堆存于配料仓；其中，回转窑预还原硫化主要反应方程式如下：
C+CO 2＝2CO；
Fe 2O 3+CO＝Fe 3O 4+CO 2；
Fe 2O 3+CO＝FeO+CO 2；
FeO+CO＝Fe+CO 2；
NiO+CO＝Ni+CO 2；
CoO+CO＝Co+CO 2；
Fe+S 2(FeS 2、CaSO 4)→FeS；
Ni+S 2(FeS 2、CaSO 4)→Ni 3S 2；
Co+S 2(FeS 2、CaSO 4)→CoS；
FeO+CO+S 2(FeS 2、CaSO 4)→FeS+CO 2；
NiO+CO+S 2(FeS 2、CaSO 4)→Ni 3S 2+CO 2；
CoO+CO+S 2(FeS 2、CaSO 4)→CoS+CO 2；
所得预硫化焙烧料中Fe 2O 3的含量为10wt％、FeS的含量为6wt％。
(4)回转窑出来的高温熔融的预硫化焙烧料通过具有称重功能的铜体溜槽均匀地淌入侧吹炉进行还原硫化熔炼，而配料仓的固体颗粒可通过进料皮带称量配料后加入侧吹炉内，根据物料平衡和热平衡计算，每吨预硫化焙烧料配入风量为260Nm 3，采用特制的喷枪将粉煤、富氧气体、压缩空气同时喷吹到侧吹炉的熔池中，粉煤配入量是预硫化焙烧料质量的30％，控制富氧气体中的氧气纯度为92％，炉内富氧空气浓度为60％，空气过剩系数为88％，控制冶炼温度为1500℃，并添加第二还原剂、第二硫化剂和第二熔剂进行3h还原硫化反应，其中第二还原剂为无烟煤，配入量是预硫化焙烧料质量的5％，第二硫化剂为石膏，配入量是预硫化焙烧料质量的8％，第二熔剂为石灰石，配入量是预硫化焙烧料质量的6％，经还原硫化反应完成有价金属镍、钴还原硫化，得到低冰镍、熔炼渣和烟气，其中，侧吹炉内还原硫化主要化学反应式如下：
C+CO 2＝2CO；
Fe 2O 3+CO＝Fe 3O 4+CO 2；
Fe 2O 3+CO＝FeO+CO 2；
FeO+CO＝Fe+CO 2；
NiO+CO＝Ni+CO 2；
CoO+CO＝Co+CO 2；
Fe+S 2(FeS 2、CaSO 4)→FeS；
Ni+S 2(FeS 2、CaSO 4)→Ni 3S 2；
Co+S 2(FeS 2、CaSO 4)→CoS；
FeO+CO+S 2(FeS 2、CaSO 4)→FeS+CO 2；
NiO+CO+S 2(FeS 2、CaSO 4)→Ni 3S 2+CO 2；
CoO+CO+S 2(FeS 2、CaSO 4)→CoS+CO 2；
3NiO+FeS＝Ni 3S 2+3FeO+1/2S 2；
CoO+FeS＝CoS+FeO；
2FeO+SiO 2＝2FeO·SiO 2；
CaO+SiO 2＝CaO·SiO 2；
MgO+SiO 2＝MgO·SiO 2；
所得低冰镍化学成分：Ni 20.38wt％、Co 0.94wt％、Fe 53.69wt％、S 18.61wt％，熔炼渣主要化学成分：Ni 0.16wt％、Co 0.005wt％、Fe 45.38wt％，熔炼渣中铁主要以FeS、FeO、Fe 3O 4形式存在。
(5)上述步骤(4)产出的高温熔炼渣通过溜槽淌入熔融氧化炉，加入红土镍矿湿法浸出渣和熔剂4调节熔炼渣组分，其中红土镍矿湿法浸出渣加入量为熔炼渣质量的10％，红土镍矿湿法浸出渣主要化学成分为：Ni 0.07wt％、Fe 48wt％、Cr 1.97wt％、S 2wt％，第四熔剂为石灰石，加入量为熔炼渣质量的2％，通入燃料控制温度至1480℃，燃料为粉煤，加入量为熔炼渣质量的10％，鼓入空气控制熔融氧化气氛，使熔炼渣氧位为lgpO 2＝10 -1Pa，使熔炼渣和浸出渣里的铁元素大量氧化生产四氧化三铁，具体为，先升温至1480℃反应1.2h，再以5℃/min的降温速率，将温度降至1200℃，经过析晶过程生成富镍钴磁铁矿，富镍钴磁铁矿先经过6000Gs的强磁选分离出富镍钴磁铁精矿和弃渣1，富镍钴磁铁精矿经过2000Gs弱磁选分离出铁精矿1和富镍钴锍渣1。
(6)步骤(4)产出的高温熔融的低冰镍经过水淬系统水淬后，以低冰镍粒形态储存于冰镍仓，并通过皮带运输机加入底吹炉，鼓入25000Nm 3/h压缩空气，加入第三熔剂，第三熔剂为石英石，用量为低冰镍质量的5％，在1270℃温度条件下进行脱铁脱硫造渣吹炼作业2h，产出高钴高冰镍、吹炼渣和烟尘，其中，低冰镍吹炼主要是通过添加石英石将低冰镍吹炼成 高冰镍，低冰镍吹炼反应为放热反应，低冰镍中的铁以硅酸铁的形式造渣与高冰镍分离，吹炼主要的化学反应如下：
3FeS 2+8O 2＝Fe 3O 4+6SO 2；
Fe+1/2O 2＝FeO；
Ni 3S 2+7/2O 2＝3NiO+2SO 2；
Ni 3S 2+2O 2＝3Ni+2SO 2；
CoS+O 2＝Co+SO 2；
2CoS+3O 2＝2CoO+2SO 2；
2FeS+3O 2＝2FeO+2SO 2；
2FeO+SiO 2＝2FeO·SiO 2；
所得高钴高冰镍的主要成分：Ni 75.67wt％、Co 2.34wt％、S 8.64wt％，吹炼渣的主要化学成分：Ni 1.9wt％、Co 0.16wt％、Fe51.76wt％，吹炼渣中铁主要以Fe 3O 4、FeS、FeO形式存在。
(7)上述(6)产出的高温吹炼渣通过溜槽淌入熔融氧化炉，加入红土镍矿湿法浸出渣和第四熔剂调节熔炼渣组分，其中红土镍矿湿法浸出渣加入量为熔炼渣质量的12％，红土镍矿湿法浸出渣主要化学成分为：Ni 0.07％、Fe 48％、Cr 1.97％、S 2％，第四熔剂为石灰石，加入量为熔炼渣质量的3％，通入燃料控制温度至1520℃，燃料为粉煤，加入量为熔炼渣质量的5％，鼓入空气控制熔融氧化气氛，使熔炼渣氧位为lgpO 2＝10 -4Pa，使熔炼渣和浸出渣里的铁元素大量氧化生产四氧化三铁，具体为，先升温至1520℃反应1.5h，再以10℃/min的降温速率，将温度将至1100℃，经过析晶过程生成富镍钴磁铁矿，富镍钴磁铁矿先经过6000Gs的强磁选分离出富镍钴磁铁精矿和弃渣2，富镍钴磁铁精矿经过2000Gs弱磁选分离出铁精矿2和富镍钴锍渣2。
(8)高温熔融高钴高冰镍浇铸成高钴高冰镍块，经过后续湿法处理得到硫酸镍和硫酸钴；富镍钴锍渣1和富镍钴锍渣2返回底吹炉吹炼回收镍、钴等有价金属；铁精矿1、铁精矿2直接外售炼钢或做电磁功能材料；回转窑、侧吹炉、底吹炉和熔融氧化炉产生的烟气经过收尘系统收集烟尘，脱硫系统脱硫达标排放，而收集的烟尘可返回混合制粒工序参与配料制粒，或直接返回侧吹炉配料参与还原硫化熔炼。
(9)通过配料计算、物料平衡计算和热平衡计算得出：本实施例整个系统镍回收率为97.21％、钴回收率为95.71％。
实施例2
一种利用回转窑和侧吹炉连续还原硫化冶炼红土镍矿生产高冰镍的方法，具体过程为：
(1)通过干燥窑对10吨红土镍矿进行初步干燥，干燥脱水后红土镍矿的含水率为20％；再用颚式破碎机将红土镍矿进行破碎处理，破碎后红土镍矿94％以上矿粒度小于5mm，红土镍矿的主要成分为Ni 1.76wt％、Co 0.07wt％、Fe 34.67wt％、MgO 13.20wt％、SiO 2 40.22wt％。
(2)将干燥破碎后的红土镍矿通过皮带输送机送入圆盘制粒机，同时配入第一还原剂、第一硫化剂、第一熔剂，将红土镍矿与第一还原剂、第一硫化剂及第一熔剂进行混合制成球团，成球率为95％，球团直径为10-30mm，其中，第一还原剂为无烟煤，配入量为红土镍矿质量的7％，第一硫化剂为石膏，配入量为红土镍矿质量的9％，第一熔剂是石灰石，配入量为红土镍矿质量的6％。
(3)将红土镍矿球团通过进料装置送入回转窑，并通入粉煤和富氧空气供热，粉煤配入量为红土镍矿球团质量的25％，严格控制监测炉内温度，使红土镍矿球团在1200℃温度下预还原硫化焙烧2h，并根据实际生产情况，适当补加第一还原剂、第一硫化剂和第一熔剂，其中第一还原剂补加量为红土镍矿球团质量的1.2％，第一硫化剂补加量为红土镍矿球团质量的2.3％，第一熔剂补加量为红土镍矿球团质量的2.5％，产出部分还原硫化焙砂和部分低镍锍的预硫化焙烧料(固液混合物)；预硫化焙烧料部分直接投入侧吹炉，部分经过水淬系统以固体颗粒形态堆存于料仓，再经进料系统投入侧吹炉进行还原硫化熔炼，便可保证侧吹炉正常熔炼时，可直接接收高温熔融的预硫化焙烧料，而侧吹炉停炉检修时，可将高温熔融的预硫化焙烧料经过水淬系统以固体颗粒形式堆存于配料仓，所得预硫化焙烧料中Fe 2O 3的含量为2wt％、FeS的含量为12wt％。
(4)回转窑出来的高温熔融的预硫化焙烧料通过具有称重功能的铜体溜槽均匀地淌入侧吹炉进行还原硫化熔炼，而配料仓的固体颗粒可通过进料皮带称量配料后加入侧吹炉内，根据物料平衡和热平衡计算，每吨预硫化焙烧料配入风量为300Nm 3，采用特制的喷枪将粉煤、富氧气体、压缩空气同时喷吹到侧吹炉的熔池中，粉煤配入量是预硫化焙烧料质量的35％，控制富氧气体中的氧气纯度为93％，炉内富氧空气浓度为70％，空气过剩系数为87％，控制冶炼温度为1550℃，并添加第二还原剂、第二硫化剂和第二熔剂进行3.5h还原硫化反应，其中第二还原剂为无烟煤，配入量是预硫化焙烧料质量的5.6％，第二硫化剂为石膏，配入量是预硫化焙烧料质量的10％，第二熔剂为石灰石，配入量是预硫化焙烧料质量的6.5％，经还原硫化反应完成有价金属镍、钴还原硫化，得到低冰镍、熔炼渣和烟气，所得低冰镍化学成分：Ni 19.56wt％、Co 1.27wt％、Fe 55.61wt％、S 18.69wt％，熔炼渣主要化学成分：Ni 0.17wt％、Co 0.006wt％、Fe 42.87wt％，熔炼渣中铁主要以FeS、FeO、Fe 3O 4形式存在。
(5)上述步骤(4)产出的高温熔炼渣通过溜槽淌入熔融氧化炉，加入红土镍矿湿法浸出渣和第四熔剂调节熔炼渣组分，其中红土镍矿湿法浸出渣加入量为熔炼渣质量的15％，红土镍矿湿法浸出渣主要化学成分为：Ni 0.05wt％、Fe 50.27wt％、Cr 1.65wt％、S 2.43wt％，第四熔剂为石灰石，加入量为熔炼渣质量的3％，通入燃料控制温度至1530℃，燃料为粉煤， 加入量为熔炼渣质量的13％，鼓入空气控制熔融氧化气氛，使熔炼渣氧位为lgpO2＝10-3Pa，使熔炼渣和浸出渣里的铁元素大量氧化生产四氧化三铁，具体为，先升温至1530℃反应2h，再以10℃/min的降温速率，将温度将至1230℃，经过析晶过程生成富镍钴磁铁矿，富镍钴磁铁矿先经过5000Gs的强磁选分离出富镍钴磁铁精矿和弃渣1，富镍钴磁铁精矿经过2000Gs弱磁选分离出铁精矿1和富镍钴锍渣1。
(6)步骤(4)产出的高温熔融的低冰镍经过水淬系统水淬后，以低冰镍粒形态储存于冰镍仓，并通过皮带运输机加入底吹炉，鼓入26000Nm 3/h压缩空气，加入第三熔剂，第三熔剂为石英石，用量为低冰镍质量的8.5％，在1230℃温度条件下进行脱铁脱硫造渣吹炼作业2h，产出高钴高冰镍、吹炼渣和烟尘，其中，低冰镍吹炼主要是通过添加石英石将低冰镍吹炼成高冰镍，低冰镍吹炼反应为放热反应，低冰镍中的铁以硅酸铁的形式造渣与高冰镍分离，所得高钴高冰镍的主要成分：Ni 72.29wt％、Co 2.37wt％、S 9.21wt％，吹炼渣的主要化学成分：Ni 1.54wt％、Co 0.13wt％、Fe 53.49wt％，吹炼渣中铁主要以Fe 3O 4、FeS、FeO形式存在。
(7)上述(6)产出的高温吹炼渣通过溜槽淌入熔融氧化炉，加入红土镍矿湿法浸出渣和第四熔剂调节熔炼渣组分，其中红土镍矿湿法浸出渣加入量为熔炼渣质量的15％，红土镍矿湿法浸出渣主要化学成分为：Ni 0.05wt％、Fe 50.27wt％、Cr 1.65wt％、S 2.43wt％，第四熔剂为石灰石，加入量为熔炼渣质量的4％，通入燃料控制温度至1500℃，燃料为粉煤，加入量为熔炼渣质量的6％，鼓入空气控制熔融氧化气氛，使熔炼渣氧位为lgpO 2＝10 -2Pa，使熔炼渣和浸出渣里的铁元素大量氧化生产四氧化三铁，具体为，先升温至1500℃反应1.6h，再以15℃/min的降温速率，将温度降至1150℃，经过析晶过程生成富镍钴磁铁矿，富镍钴磁铁矿先经过5000Gs的强磁选分离出富镍钴磁铁精矿和弃渣2，富镍钴磁铁精矿经过2000Gs弱磁选分离出铁精矿2和富镍钴锍渣2。
(8)高温熔融高钴高冰镍浇铸成高钴高冰镍块，经过后续湿法处理得到硫酸镍和硫酸钴；富镍钴锍渣1和富镍钴锍渣2返回底吹炉吹炼回收镍、钴等有价金属；铁精矿1、铁精矿2直接外售炼钢或做电磁功能材料；回转窑、侧吹炉、底吹炉和熔融氧化炉产生的烟气经过收尘系统收集烟尘，脱硫系统脱硫达标排放，而收集的烟尘可返回混合制粒工序参与配料制粒，或直接返回侧吹炉配料参与还原硫化熔炼。
(9)通过配料计算、物料平衡计算和热平衡计算得出：本实施例整个系统镍回收率为96.53％、钴回收率为94.78％。
实施例3
一种利用回转窑和侧吹炉连续还原硫化冶炼红土镍矿生产高冰镍的方法，具体过程为：
(1)通过干燥窑对10吨红土镍矿进行初步干燥，干燥脱水后红土镍矿的含水率为20％； 再用颚式破碎机将红土镍矿进行破碎处理，破碎后红土镍矿96％以上矿粒度小于4.5mm，红土镍矿的主要成分为Ni 1.76wt％、Co 0.07wt％、Fe 34.67wt％、MgO 13.20wt％、SiO 2 40.22wt％。
(2)将干燥破碎后的红土镍矿通过皮带输送机送入圆盘制粒机，同时配入第一还原剂、第一硫化剂、第一熔剂，将红土镍矿与第一还原剂、第一硫化剂及第一熔剂进行混合制成球团，成球率为96.50％，球团直径为10-30mm，其中，第一还原剂为无烟煤，配入量为红土镍矿质量的8.5％，第一硫化剂为石膏，配入量为红土镍矿质量的10％，第一熔剂是石灰石，配入量为红土镍矿质量的7.5％。
(3)将红土镍矿球团通过进料装置送入回转窑，并通入粉煤和富氧空气供热，粉煤配入量为红土镍矿球团质量的27％，严格控制监测炉内温度，使红土镍矿球团在1250℃温度下预还原硫化焙烧1h，并根据实际生产情况，适当补加第一还原剂、第一硫化剂和第一熔剂，其中第一还原剂补加量为红土镍矿球团质量的2.2％，第一硫化剂补加量为红土镍矿球团质量的2.6％，第一熔剂补加量为红土镍矿球团质量的2.8％，产出部分还原硫化焙砂和部分低镍锍的预硫化焙烧料(固液混合物)；预硫化焙烧料部分直接投入侧吹炉，部分经过水淬系统以固体颗粒形态堆存于料仓，再经进料系统投入侧吹炉进行还原硫化熔炼，便可保证侧吹炉正常熔炼时，可直接接收高温熔融的预硫化焙烧料，而侧吹炉停炉检修时，可将高温熔融的预硫化焙烧料经过水淬系统以固体颗粒形式堆存于配料仓，所得预硫化焙烧料中Fe 2O 3的含量为5wt％、FeS的含量为10wt％。
(4)回转窑出来的高温熔融的预硫化焙烧料通过具有称重功能的铜体溜槽均匀地淌入侧吹炉进行还原硫化熔炼，而配料仓的固体颗粒可通过进料皮带称量配料后加入侧吹炉内，根据物料平衡和热平衡计算，每吨预硫化焙烧料配入风量为350Nm 3，采用特制的喷枪将粉煤、富氧气体、压缩空气同时喷吹到侧吹炉的熔池中，粉煤配入量是预硫化焙烧料质量的38％，控制富氧气体中的氧气纯度为95％，炉内富氧空气浓度为73％，空气过剩系数为86％，控制冶炼温度为1530℃，并添加第二还原剂、第二硫化剂和第二熔剂进行4h还原硫化反应，其中第二还原剂为无烟煤，配入量是预硫化焙烧料质量的5.7％，第二硫化剂为石膏，配入量是预硫化焙烧料质量的11％，第二熔剂为石灰石，配入量是预硫化焙烧料质量的7.6％，经还原硫化反应完成有价金属镍、钴还原硫化，得到低冰镍、熔炼渣和烟气，所得低冰镍化学成分：Ni 23.87wt％、Co 1.38wt％、Fe 52.49wt％、S 16.74wt％，熔炼渣主要化学成分：Ni 0.12wt％、Co 0.007wt％、Fe 46.31wt％，熔炼渣中铁主要以FeS、FeO、Fe 3O 4形式存在。
(5)上述步骤(4)产出的高温熔炼渣通过溜槽淌入熔融氧化炉，加入红土镍矿湿法浸出渣和第四熔剂调节熔炼渣组分，其中红土镍矿湿法浸出渣加入量为熔炼渣质量的20％，红土镍矿湿法浸出渣主要化学成分为：Ni 0.12wt％、Fe 47.69wt％、Cr 1.82wt％、S 1.45wt％，第四熔剂为石灰石，加入量为熔炼渣质量的5％，通入燃料控制温度至1550℃，燃料为粉煤，加入量为熔炼渣质量的15％，鼓入空气控制熔融氧化气氛，使熔炼渣氧位为lgpO 2＝10 -2.5Pa， 使熔炼渣和浸出渣里的铁元素大量氧化生产四氧化三铁，具体为，先升温至1550℃反应0.5h，再以20℃/min的降温速率，将温度降至1260℃，经过析晶过程生成富镍钴磁铁矿，富镍钴磁铁矿先经过7000Gs的强磁选分离出富镍钴磁铁精矿和弃渣1，富镍钴磁铁精矿经过3000Gs弱磁选分离出铁精矿1和富镍钴锍渣1。
(6)步骤(4)产出的高温熔融的低冰镍经过水淬系统水淬后，以低冰镍粒形态储存于冰镍仓，并通过皮带运输机加入底吹炉，鼓入26500Nm 3/h压缩空气，加入第三熔剂，第三熔剂为石英石，用量为低冰镍质量的7.2％，在1260℃温度条件下进行脱铁脱硫造渣吹炼作业3h，产出高钴高冰镍、吹炼渣和烟尘，其中，低冰镍吹炼主要是通过添加石英石将低冰镍吹炼成高冰镍，低冰镍吹炼反应为放热反应，低冰镍中的铁以硅酸铁的形式造渣与高冰镍分离，所得高钴高冰镍的主要成分：Ni 76.48wt％、Co 2.82wt％、S 7.66wt％，吹炼渣的主要化学成分：Ni 1.71wt％、Co 0.19wt％、Fe 49.81wt％，吹炼渣中铁主要以Fe 3O 4、FeS、FeO形式存在。
(7)上述(6)产出的高温吹炼渣通过溜槽淌入熔融氧化炉，加入红土镍矿湿法浸出渣和第四熔剂调节熔炼渣组分，其中红土镍矿湿法浸出渣加入量为熔炼渣质量的16％，红土镍矿湿法浸出渣主要化学成分为：Ni 0.12wt％、Fe 47.69wt％、Cr 1.82wt％、S 1.45wt％，第四熔剂为石灰石，加入量为熔炼渣质量的7％，通入燃料控制温度至1490℃，燃料为粉煤，加入量为熔炼渣质量的8％，鼓入空气控制熔融氧化气氛，使熔炼渣氧位为熔渣氧位为lgpO 2＝10 -1.8Pa，使熔炼渣和浸出渣里的铁元素大量氧化生产四氧化三铁，具体为，先升温至1490℃反应1.4h，再以14℃/min的降温速率，将温度将至1180℃，经过析晶过程生成富镍钴磁铁矿，富镍钴磁铁矿先经过6000Gs的强磁选分离出富镍钴磁铁精矿和弃渣2，富镍钴磁铁精矿经过2500Gs弱磁选分离出铁精矿2和富镍钴锍渣2。
(8)高温熔融高钴高冰镍浇铸成高钴高冰镍块，经过后续湿法处理得到硫酸镍和硫酸钴；富镍钴锍渣1和富镍钴锍渣2返回底吹炉吹炼回收镍、钴等有价金属；铁精矿1、铁精矿2直接外售炼钢或做电磁功能材料；回转窑、侧吹炉、底吹炉和熔融氧化炉产生的烟气经过收尘系统收集烟尘，脱硫系统脱硫达标排放，而收集的烟尘可返回混合制粒工序参与配料制粒，或直接返回侧吹炉配料参与还原硫化熔炼。
(9)通过配料计算、物料平衡计算和热平衡计算得出：本实施例整个系统镍回收率为97.91％、钴回收率为95.88％。
对比例
一种利用回转窑和侧吹炉连续还原硫化冶炼红土镍矿生产高冰镍的方法，具体过程为：
(1)通过干燥窑对10吨红土镍矿进行初步干燥，干燥脱水后红土镍矿的含水率为21％；再用颚式破碎机将红土镍矿进行破碎处理，破碎后红土镍矿90％以上矿粒度小于9mm，红土 镍矿的主要成分为Ni 1.76wt％、Co 0.07wt％、Fe 34.67wt％、MgO 13.20wt％、SiO 2 40.22wt％。
(2)将干燥破碎后的红土镍矿通过皮带输送机送入圆盘制粒机，同时配入第一还原剂、第一硫化剂、第一熔剂，将红土镍矿与第一还原剂、第一硫化剂及第一熔剂进行混合制成球团，成球率为90％，球团直径为10-30mm，其中，第一还原剂为无烟煤，配入量为红土镍矿质量的13％，第一硫化剂为石膏，配入量为红土镍矿质量的8％，第一熔剂是石灰石，配入量为红土镍矿质量的12％。
(3)将红土镍矿球团通过进料装置送入回转窑，并通入粉煤和富氧空气供热，粉煤配入量为红土镍矿球团质量的46％，严格控制监测炉内温度，使红土镍矿球团在350℃温度下预还原硫化焙烧0.4h，使红土镍矿中的镍、钴充分与硫化剂反应，减少硫化剂的挥发损失，提高硫化效率，然后迅速升温至600℃温度下进行二次还原硫化焙烧3h，主要目的是使硫化镍、硫化钴晶粒聚集长大，便于后续侧吹炉熔炼沉降分离富集镍和钴，回转窑还原硫化过程中，可根据实际生产情况，适当补加第一还原剂、第一硫化剂和第一熔剂，其中第一还原剂补加量为红土镍矿球团质量的5％，第一硫化剂补加量为红土镍矿球团质量的7％，第一熔剂补加量为红土镍矿球团质量的8％，最终生成还原硫化焙砂，冷却后焙砂粒度约为12mm；所得还原硫化焙砂中Fe 2O 3的含量为60wt％。
(4)还原硫化焙砂冷却后料仓堆存，进料时，可通过进料皮带称量配料后加入侧吹炉内，根据物料平衡和热平衡计算，每吨还原硫化焙砂配入风量为700Nm 3，采用特制的喷枪将粉煤、富氧气体、压缩空气同时喷吹到侧吹炉的熔池中，粉煤配入量是还原硫化焙砂质量的45％，控制富氧气体中的氧气纯度为60％，炉内富氧空气浓度为45％，空气过剩系数为70％，控制冶炼温度为1300℃，并添加第二还原剂、第二硫化剂和第二熔剂进行3h还原硫化反应，其中第二还原剂为无烟煤，配入量是还原硫化焙砂质量的10％，第二硫化剂为石膏，配入量是还原硫化焙砂质量的7％，第二熔剂为石灰石，配入量是还原硫化焙砂质量的13％，经还原硫化反应完成有价金属镍、钴还原硫化，得到低冰镍、熔炼渣和烟气，所得低冰镍化学成分：Ni 16.53wt％、Co 0.24wt％、Fe 63.75wt％、S 19.10wt％，熔炼渣主要化学成分：Ni 0.42wt％、Co 0.16wt％、Fe 36.78wt％，熔炼渣中铁主要以FeS、FeO、Fe 3O 4形式存在。
(5)步骤(4)产出的高温熔融的低冰镍经过水淬系统水淬后，以低冰镍粒形态储存于冰镍仓，并通过皮带运输机加入转炉，鼓入29000Nm 3/h压缩空气，加入第三熔剂，第三熔剂为石英石，用量为低冰镍质量的12％，在1300℃温度下进行脱铁脱硫造渣吹炼作业3.5h，产出高钴高冰镍、吹炼渣和烟尘，其中，低冰镍吹炼主要是通过添加石英石将低冰镍吹炼成高冰镍，低冰镍吹炼反应为放热反应，低冰镍中的铁以硅酸铁的形式造渣与高冰镍分离，所得高钴高冰镍的主要成分：Ni 56.71wt％、Co 0.92wt％、S 10.57wt％，吹炼渣的主要化学成分：Ni 3.94wt％、Co 0.34wt％、Fe 61.79wt％，吹炼渣中铁主要以Fe 3O 4、FeS、FeO形式存在。
(6)高温熔融高冰镍浇铸成高钴高冰镍块，经过后续湿法处理得到硫酸镍和硫酸钴；而吹炼渣水淬后可返回侧吹炉回收镍、钴等有价金属；转炉烟气、侧吹炉烟气、回转炉烟气经过收尘脱硫后收集的烟尘可返回混合红土镍矿制粒；侧吹炉产出的熔炼炉渣则直接外售。
(7)通过配料计算、物料平衡计算和热平衡计算得出：本实施例整个系统镍回收率为80.27％、钴回收率为70.36％。
高钴高冰镍质量：表1为实施例1、2、3与对比例生产的高钴高冰镍产品的主要元素含量，具体数据是由化学法得到。
表1高钴高冰镍产品中主要元素含量
Figure PCTCN2022120357-appb-000001
由表1可知，实施例中生产的高钴高冰镍产品的主要有价金属含量明显比对比例要高，特别是实施例3。
金属回收率：表2为实施例1、2、3与对比例整个系统的镍回收率和钴回收率对比统计表，具体数据是通过配料计算、物料平衡计算和热平衡计算得到。
表2不同案例中镍钴回收率对比
金属回收率 实施例1 实施例2 实施例3 对比例
镍回收率(％) 97.21 96.53 97.91 80.27
钴回收率(％) 95.71 94.78 95.88 70.36
由表2可知，实施例中整体系统中镍回收率和钴回收率明显比对比例1要好，特别是实施例3。主要原因在于：(1)实施例还原硫化效果更好，对镍钴的富集程度高，所得到的低冰镍中镍钴品位更高。而影响低冰镍品位的主要因素在于回转窑预还原温度、硫化程度不同，对比例焙烧温度较低，提供不了物质反应所需的能量，使还原硫化反应困难，且添加剂配入量不合理，提供不了反应所需的还原剂和硫化剂，使还原硫化反应不完全，影响低冰镍质量。此外对比例的侧吹炉炉内富氧空气浓度为45％，空气过剩系数为70％，控制冶炼温度为1300℃，使得熔炼反应不佳，脱杂效果差，所得低冰镍质量差。(2)对比例的熔炼渣和吹炼渣没有进一步回收利用渣中的Ni、Co有价金属，而实施例通过熔融氧化炉有效地对渣中的镍和钴进行有效回收利用，使得实施例镍和钴的回收率比对比例高。
上面结合附图对本发明实施例作了详细说明，但是本发明不限于上述实施例，在所属技术领域普通技术人员所具备的知识范围内，还可以在不脱离本发明宗旨的前提下作出各种变化。此外，在不冲突的情况下，本发明的实施例及实施例中的特征可以相互组合。

Claims (10)

  1. 一种还原硫化冶炼红土镍矿生产高冰镍的方法，其特征在于，包括以下步骤：
    S1：将干燥破碎后的红土镍矿与第一还原剂、第一硫化剂和第一熔剂混合制成球团；
    S2：将球团置于回转窑中，在1000-1350℃下进行选择性预还原硫化焙烧，得到固液混合态的预硫化焙烧料；所述预硫化焙烧料中Fe 2O 3的含量≤10wt％、FeS的含量为2wt％-20wt％；
    S3：所述预硫化焙烧料进入侧吹炉，并添加第二还原剂、第二硫化剂和第二熔剂，在1350-1600℃下进行还原硫化反应，得到低冰镍和熔炼渣；
    S4：将所述低冰镍和第三熔剂混合，进行吹炼造渣处理，得到高冰镍和吹炼渣；
    S5：将所述熔炼渣和/或所述吹炼渣与第四熔剂混合，在1400-1550℃下进行熔融氧化生成四氧化三铁，再降温至1000-1260℃，得到富镍钴磁铁矿，经分级磁选分离出铁精矿、富镍钴锍渣和弃渣。
  2. 根据权利要求1所述的方法，其特征在于，所述第一还原剂、第二还原剂独立地选自无烟煤、焦炭、兰炭或石墨粉中的至少一种。
  3. 根据权利要求1所述的方法，其特征在于，所述第一硫化剂、第二硫化剂独立地选自石膏、硫磺或含硫矿物中的至少一种。
  4. 根据权利要求1所述的方法，其特征在于，所述第一熔剂、第二熔剂独立地选自石灰石或石英石中的至少一种。
  5. 根据权利要求1所述的方法，其特征在于，步骤S1中，红土镍矿、第一还原剂、第一硫化剂和第一熔剂的质量比为100：(3-10)：(4-10)：(3-10)。
  6. 根据权利要求1所述的方法，其特征在于，步骤S2中，在所述选择性预还原硫化焙烧的过程中，根据实际生产情况，补加第一还原剂、第一硫化剂或第一熔剂。
  7. 根据权利要求6所述的方法，其特征在于，将步骤S3所得的所述预硫化焙烧料趁热加入所述侧吹炉；或者将所述预硫化焙烧料经过水淬处理后，再投入所述侧吹炉。
  8. 根据权利要求1所述的方法，其特征在于，步骤S3中，所述预硫化焙烧料、第二还原剂、第二硫化剂和第二熔剂的质量比为100：(1-9)：(3-12)：(1-10)。
  9. 根据权利要求1所述的方法，其特征在于，所述分级磁选的过程为：所述富镍钴磁铁矿先经过4000-8000Gs的强磁选分离出富镍钴磁铁精矿和所述弃渣，再将所述富镍钴磁铁精矿经过2000-3000Gs的弱磁选分离出所述铁精矿和富镍钴锍渣。
  10. 根据权利要求1所述的方法，其特征在于，所述熔炼渣和/或所述吹炼渣在进行熔融氧化前，还加入红土镍矿湿法浸出渣。
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CN116004936A (zh) * 2022-11-30 2023-04-25 中国恩菲工程技术有限公司 红土镍矿酸浸渣的处理方法
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