CN101792865A - Method for drying and prereducing laterite-nickel ores - Google Patents
Method for drying and prereducing laterite-nickel ores Download PDFInfo
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- CN101792865A CN101792865A CN200910095198A CN200910095198A CN101792865A CN 101792865 A CN101792865 A CN 101792865A CN 200910095198 A CN200910095198 A CN 200910095198A CN 200910095198 A CN200910095198 A CN 200910095198A CN 101792865 A CN101792865 A CN 101792865A
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Abstract
The invention relates to a method for drying and prereducing laterite-nickel ores with low energy consumption, belonging to the technical field of metallurgy. The method is especially suitable for drying and prereducing low grade laterite-nickel ores. The method is characterized by the technological processes as follows: grinding the laterite-nickel ores until the grain size is less than 1mm by a vertical mill, ensuring the ground laterite-nickel ores to enter into a multistage suspension drying and calcining device and a prereducer in sequence, simultaneously introducing the flue gas generated by the suspension drying and calcining device into the vertical mill; spraying the coal, coke, carbon black solid reducing agents or vulcanizer powder into the prereducer, reducing, calcining or vulcanizing the materials in the suspension state, ensuring the tail gas from the prereducer to directly enter into the final drying and calcining device to produce prereduced or vulcanized thermal state materials. The method is simple in process, easy to operate, low in investment, high in thermal efficiency and low in smelting cost.
Description
Technical field
The present invention relates to a kind of red soil nickel ore method for drying and prereducing of less energy-consumption, be specially adapted to the drying and the prereduction of low-grade red soil nickel ore, belong to metallurgical technology field.
Background technology:
Nickel (Ni) is a rare precious metal, and its purposes is very extensive, space flight, aviation, navigation, national defence, scientific research, industry, agricultural, medical treatment, automobile, iron and steel and every profession and trade such as civilian all lack bound it.Nickel-containing mineral is more and more rare on the earth's crust, and grade is also more and more lower.To from low-grade red soil nickel ore, extract nickel, technical difficulty is very big, conventional wet processing, the high environmental pollution of production cost is big, there is red soil nickel ore crystal water content height in conventional pyrometallurgical smelting, with rotary kiln drying energy consumption height, the production cost height, in a word Chang Gui pyrogenic process, still all there is the high difficult problem of cost in wet processing.The nickel oxide mineral deposit be nickeliferous peridotites in the torrid zone or the subtropics rotten and form through long-term weathering leaching.Because the oxidation of iron after the weathering of mineral deposit, ore takes on a red color, so be commonly referred to as red soil nickel ore (Laterite).Because the result of weathering leaching, top, mineral deposit iron content is many, and silicon, magnesium are few, and the nickel grade is lower, and cobalt is high slightly, and nickel minerals takes on a red color, and belongs to the nickel-containing limonite type.The bottom, mineral deposit is because the weathering enrichment, and nickel ores is siliceous, magnesium is higher, and the nickel grade is than top height and iron content is low is garnirite (Garnierite) type, sometimes because geological change often has two kinds of ores to mix existence in same mineral deposit.
Develop the history in existing more than 80 year of red soil nickel ore in the world, mainly be divided into pyrogenic process and hydrometallurgy at present, nickeliferous metamorphic peridotite of high grade is mainly handled in pyrometallurgy, contains Ni1.5～3%, Co0.02～0.1%, Fe10～40%, MgO5～35%, Cr
2O
31～2%.Smelting technology mainly contains rotary kiln---electric furnace process (RKEF), its product is mainly ferronickel, contain Ni2.5～3% as the raw material grade, also available this method output contains the nickel matte of Ni78%, its main manufacturer is as many Ni Anbo factory of many Buddhist nuns Asia in newly coughing up, the Henry David Thoreau A Ke nickel smeltery of Indonesia, the Han Na company of the U.S. etc.The big rivers and mountains factory of Japan then adopts rotary kiln high temperature reduction roasting output granulated iron, through magnetic separation, jigging enrichment output Rhometal.Mainly for producing stainless steel, its nickel price is by the 90-95% of electric nickel price for the ferronickel product.The main drawback of this products scheme is that contained valency is planted higher cobalt and can not be reclaimed and enter stainless steel, though do not influence stainless performance, does not improve the effect of performance also.
Hydrometallurgy is mainly handled and is contained Ni0.8～1.8%, Co0.02～0.2%, Fe25～50%, MgO 0.5～15% raw material.Hydrometallurgy has two kinds of technologies, and a kind of is the reduction roasting-ammonia leaching method, and another kind is the pressurized acid leaching method.Ammonia leaching process is with nickel oxide ore reducing roasting NH
3-CO
2-H
2O system selectivity leaches the nickel cobalt, and product is a basic nickel carbonate, can be for producing metallic nickel.The main advantage of this method is that reagent corrodibility is less, can be recycled, and suitable treatment contains the higher nickel oxide ore of MgO, and Ca, Mg, Fe still are retained in the slag.Its shortcoming is that nickel cobalt leaching yield is on the low side, Ni75-85%, Co40-60%.This is because NH
3---CO
2-H
2The O system determined the ligand complex ability of nickel cobalt, adopts the factory of ammonia leaching process to have high factory in Cuba Ni Jialuo factory, Albanian Ai Erbasang Steel Complex, the Xie Liede factory of Czech, the Filipine Soviet Union (this factory then adopt the pressurized acid leaching method) and the copper precipice iron ore of Canadian INCO to reclaim factory etc.
Pressurized acid leaching method (HPAL) mainly be applicable to handle low MgO content (laterite of＜6%=, too high to avoid acid consumption.This method is to leach nickel minerals with sulfuric acid under high temperature (230-260 ℃) high pressure (4-5MPa), and leaching yield is up to Ni95%, Co90-92%.Leach liquor H
2The S precipitation can obtain nickel cobalt mixture (Ni-55%) intermediates.What adopt this technology the earliest is Cuba hair A Wan (MaoBay) factory of nineteen ninety-five by the research and development of U.S. sulphur company, late nineteen nineties in last century, Australia built three factories on the basis of Mao A factory production technology: Mu Linmulin factory (MurrinMurrin), Cowes factory (Cawse) and Bu Long factory (BuLong).At present your gulf (Coral Bay) factory of Philippines's cola, newly cough up in the Ge Luo factory (GoRo) and Australian La Wensuopu (Raven Sthorpe) factory of many Buddhist nuns Asia build with this method, 7-8 country is in the resource of oneself studied the preparatory stage in addition.Plan to produce about 3.2 ten thousand tons of nickel, the nickelous sulfide cobalt mixture that cobalt is about 3000 tons per year comprising Chinese metallurgical construction group company in the construction of Papua New Guinea RAMU nickel minerals.Adopt the pressurized acid leaching method owing to the metal recovery rate height as can be seen, process structure is simple relatively, and nickelous sulfide cobalt product grade height is convenient to be transported to the local preferably refining of condition, and this method more and more is much accounted of.
Because red soil nickel ore moisture is higher, time of drying is long, and the external general rotary kiln drying that adopts when smelting red soil nickel ore becomes behind the diffusing shape material sintering again.But the general investment of rotary kiln is bigger, and thermo-efficiency is low, the dry energy that need be a large amount of, and smelting cost is higher.
Summary of the invention:
The method for drying and prereducing that the purpose of this invention is to provide a kind of red soil nickel ore, its technology is simple, processing ease, invest less, the thermo-efficiency height, smelting cost is lower.
Realize that the technical scheme that the object of the invention adopts is: technological process is that the employing Vertical Mill is crushed to red soil nickel ore below the 1mm, enters multistage suspension drying and calcining device and prereduction device successively, simultaneously the flue gas of suspension drying and calcining device output is introduced Vertical Mill; Coal, coke or carbon black solid reductant or vulcanizing agent powder enter the prereduction device in the mode of spraying into, material is carried out suspended state reduction calcining or sulfuration, prereduction device tail gas directly enters last step drying and calcining device, the hot state material after output prereduction or the sulfuration.
Technical scheme of the present invention also comprises:
Drying and calcining device of the present invention and prereduction device output temperature of charge are 300 ℃～1000 ℃.
Add coal, coke, the carbon black solid reductant that accounts for material gross weight 1～16% in the described prereduction device.
The progression of suspension drying and calcining device of the present invention is 3～7 grades.
The invention has the beneficial effects as follows: based on drying and dehydrating, prereduction is time during technology of the present invention, and therefore the technology that requires is simple, and processing ease is invested less.
Description of drawings
Fig. 1 is a process flow sheet of the present invention;
Fig. 2 is a processing unit interface chart of the present invention.
Embodiment:
Embodiment 1: step is as follows:
The red soil nickel ore Chemical Composition such as the following table of A, employing:
| Element | ??Ni | ??Co | ??FeO | ??MgO | ??Al2O3 | ??SiO2 | ??CaO |
| Content % | ??1.03 | ??0.039 | ??17.22 | ??27.3 | ??4.84 | ??35.72 | ??0.32 |
The ore of the direct extraction of stope is moisture 25%, gets rid of＞massive ore (entering Vertical Mill again with crusher in crushing＜100mm) of 100mm with the bar shaped sieve, and screen underflow enters the dry fragmentation of Vertical Mill.
B, feed Vertical Mill with the flue gas of 300 ℃ of 3 grades of suspension drying and calcining device output temperature and carry out drying, raw meal particle size 0.2mm, material moisture content 10% after the Vertical Mill fragmentation are with entering 3 grades of suspension drying and calcining devices after whirlwind and the bagroom collection.
C, in 3 grades of suspension drying and calcining devices, the high-temperature flue gas that material and coal dust firing produce 1100 ℃ of temperature carries out adverse current suspension heat exchange, residence time of material 2 minutes, enter the prereduction device from the material of 650 ℃ of third stage suspension device output temperature, enter Vertical Mill from the flue gas of 300 ℃ of first step output temperature.
D, spray into the bituminous coal powder of the granularity＜0.1mm that accounts for material (butt) 6%, the high-temperature flue gas that feeds 1100 ℃ of coal dust fuel combustion generation temperature carries out suspended state reduction calcining in the prereduction device, control prereduction device tail gas CO content 0.5～1%, 850 ℃ of output temperature of charge, nickel degree of metalization 95%, iron are reduced into Armco magnetic iron rate 60%, directly enter melting facility output Rhometal with hot state material, prereduction device tail gas directly enters third stage suspension device.
Embodiment 2 steps are as follows:
The first step is identical with example 1 steps A.
A, feed Vertical Mill with the flue gas of 250 ℃ of 5 grades of suspension drying and calcining device output temperature and carry out drying, raw meal particle size 0.6mm, material moisture content 15% after the Vertical Mill fragmentation are with entering 5 grades of suspension drying and calcining devices after whirlwind and the bagroom collection.
B, in 5 grades of suspension drying and calcining devices, the high-temperature flue gas that material and coal dust firing produce 1100 ℃ of temperature carries out adverse current suspension heat exchange, residence time of material 4 minutes, enter the prereduction device from the material of 750 ℃ of level V suspension device output temperature, enter Vertical Mill from the flue gas of 250 ℃ of first step output temperature.
C, spray into the coke powder of the granularity＜0.1mm that accounts for material (butt) 3%, the high-temperature flue gas that feeds 1100 ℃ of coal dust fuel combustion generation temperature carries out suspended state reduction calcining in the prereduction device, control prereduction device tail gas CO content 0.5～1%, 950 ℃ of output temperature of charge, nickel degree of metalization 90%, iron are reduced into Armco magnetic iron rate 50%, directly enter melting facility output Rhometal with hot state material, prereduction device tail gas directly enters the level V suspension device.
Embodiment 3 steps are as follows:
The first step is identical with example 1 steps A.
A, feed Vertical Mill with the flue gas of 200 ℃ of 7 grades of suspension drying and calcining device output temperature and carry out drying, raw meal particle size 0.8mm, material moisture content 17% after the Vertical Mill fragmentation are with entering 7 grades of suspension drying and calcining devices after whirlwind and the bagroom collection.
B, in 7 grades of suspension drying and calcining devices, the high-temperature flue gas that material and coal dust firing produce 1100 ℃ of temperature carries out adverse current suspension heat exchange, residence time of material 6 minutes, enter the prereduction device from the material of 800 ℃ of the 7th grade of suspension device output temperature, enter Vertical Mill from the flue gas of 200 ℃ of first step output temperature.
C, spray into the carbon black powder of the granularity＜0.1mm that accounts for material (butt) 1.5% and account for the SULPHUR POWDER of material (butt) 1.0% granularity＜0.1mm, the high-temperature flue gas that feeds 1100 ℃ of coal dust fuel combustion generation temperature carries out the calcining of suspended state reduction-sulfurization in the prereduction device, control prereduction device tail gas CO content 0.5～1%, 1000 ℃ of output temperature of charge, nickel metal sulfuration rate 95%, iron sulfuration rate 20%, directly enter melting facility output nickel matte product with hot state material, prereduction device tail gas directly enters the level V suspension device.
Claims (4)
1. the method for drying and prereducing of a red soil nickel ore, it is characterized in that: technological process is, adopt Vertical Mill that red soil nickel ore is crushed to below the 1mm, enter multistage suspension drying and calcining device and prereduction device successively, simultaneously the flue gas of suspension drying and calcining device output is introduced Vertical Mill; Coal, coke or carbon black solid reductant or vulcanizing agent powder enter the prereduction device in the mode of spraying into, material is carried out suspended state reduction calcining or sulfuration, prereduction device tail gas directly enters last step drying and calcining device, the hot state material after output prereduction or the sulfuration.
2. the method for drying and prereducing of red soil nickel ore according to claim 1 is characterized in that: 300 ℃～1000 ℃ of drying and calcining device and prereduction device output temperature of charge.
3. the method for drying and prereducing of red soil nickel ore according to claim 1 is characterized in that: add coal, coke, the carbon black solid reductant that accounts for material gross weight 1～16% in the prereduction device.
4. according to the method for drying and prereducing of the described red soil nickel ore of claim 1, it is characterized in that: the progression of suspension drying and calcining device is 3～7 grades.
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| CN2009100951985A CN101792865B (en) | 2009-11-16 | 2009-11-16 | Method for drying and prereducing laterite-nickel ores |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942558A (en) * | 2010-09-10 | 2011-01-12 | 平安鑫海资源开发有限公司 | Method for drying and reducing low-grade laterite-nickel ore by using bituminous coal |
| CN102021351A (en) * | 2010-10-11 | 2011-04-20 | 云南锡业集团（控股）有限责任公司 | Integrated approach to enriching nickel from nickel oxide laterite ore |
| CN102134656A (en) * | 2011-01-06 | 2011-07-27 | 昆明理工大学 | Method for fluidized drying and synchronous pre-reduction of laterite-nickel ore |
| CN103276224A (en) * | 2013-05-22 | 2013-09-04 | 连云港腾翔金属材料有限公司 | Energy-saving carbothermal reduction method for laterite-nickel ores |
| CN106119574A (en) * | 2016-08-01 | 2016-11-16 | 江苏省冶金设计院有限公司 | Process the method and system of lateritic nickel ore |
| CN110538717A (en) * | 2019-09-11 | 2019-12-06 | 李怀明 | Method for recovering nickel sulfide from nickel slag |
| CN117947261A (en) * | 2024-03-26 | 2024-04-30 | 扬州一川镍业有限公司 | Method for treating laterite-nickel ore leaching slag by using suspension magnetization roasting |
-
2009
- 2009-11-16 CN CN2009100951985A patent/CN101792865B/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942558A (en) * | 2010-09-10 | 2011-01-12 | 平安鑫海资源开发有限公司 | Method for drying and reducing low-grade laterite-nickel ore by using bituminous coal |
| CN102021351A (en) * | 2010-10-11 | 2011-04-20 | 云南锡业集团（控股）有限责任公司 | Integrated approach to enriching nickel from nickel oxide laterite ore |
| CN102134656A (en) * | 2011-01-06 | 2011-07-27 | 昆明理工大学 | Method for fluidized drying and synchronous pre-reduction of laterite-nickel ore |
| CN102134656B (en) * | 2011-01-06 | 2013-07-31 | 昆明理工大学 | Method for fluidized drying and synchronous pre-reduction of laterite-nickel ore |
| CN103276224A (en) * | 2013-05-22 | 2013-09-04 | 连云港腾翔金属材料有限公司 | Energy-saving carbothermal reduction method for laterite-nickel ores |
| CN103276224B (en) * | 2013-05-22 | 2014-12-03 | 连云港腾翔金属材料有限公司 | Energy-saving carbothermal reduction method for laterite-nickel ores |
| CN106119574A (en) * | 2016-08-01 | 2016-11-16 | 江苏省冶金设计院有限公司 | Process the method and system of lateritic nickel ore |
| CN106119574B (en) * | 2016-08-01 | 2018-07-17 | 江苏省冶金设计院有限公司 | Handle the method and system of lateritic nickel ore |
| CN110538717A (en) * | 2019-09-11 | 2019-12-06 | 李怀明 | Method for recovering nickel sulfide from nickel slag |
| CN117947261A (en) * | 2024-03-26 | 2024-04-30 | 扬州一川镍业有限公司 | Method for treating laterite-nickel ore leaching slag by using suspension magnetization roasting |
| CN117947261B (en) * | 2024-03-26 | 2024-05-28 | 扬州一川镍业有限公司 | Method for treating laterite-nickel ore leaching slag by using suspension magnetization roasting |
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| CN101792865B (en) | 2011-11-09 |
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