CN1156399C - Alumina producing process with hydraulic duralumin-type bauxite concentrate - Google Patents
Alumina producing process with hydraulic duralumin-type bauxite concentrate Download PDFInfo
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- CN1156399C CN1156399C CNB001134388A CN00113438A CN1156399C CN 1156399 C CN1156399 C CN 1156399C CN B001134388 A CNB001134388 A CN B001134388A CN 00113438 A CN00113438 A CN 00113438A CN 1156399 C CN1156399 C CN 1156399C
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- concentrate
- alumina
- bauxite
- lime
- aluminium
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Abstract
The present invention relates to a method for producing alumina by diasporic bauxite. In the present invention, aluminium concentrate (with the alumina-silica ratio larger than that 10) is used as raw materials, wherein the aluminium concentrate is obtained through the direct flotation desiliconization of diasporic bauxite with a medium and low alumina-silica ratio (between 4 and 8); a single Bayer method is used for producing alumina. The method comprises the technical processes of slurry preparation, dissolution by a Bayer method, the settling separation and the washing of red mud, the crystal seed decomposition of a sodium aluminate solution, etc. Compared with a combined method, the present invention reduces investment in engineering construction by 16.4%, saves energy consumption by more than 50%, and reduces the manufacturing cost of alumina by 8.86%. The present invention provides an effective method for reasonably developing and using diasporic bauxite with a medium and low alumina-silica ratio.
Description
[technical field] the present invention relates to a kind of is raw material with diaspore type bauxite through the aluminium concentrate that direct-flotation desiliconisation obtains, and adopts single bayer process production method of alumina.
[background technology] uses alumina producing Bayer process, requires raw material alumina silica ratio (A/S) greater than 10.In the diaspore type bauxite of low alumina silica ratio (average alumina silica ratio is 4～8) can not adopt alumina producing Bayer process in direct economy ground, this type of ore generally adopts soda-lime sintering process or Bayer process one sintering integrated process production aluminum oxide.Relatively there is following shortcoming in these two kinds of methods with the single Bayer process of handling high aluminium silicon ratio (A/S＞10) bauxite: (1) production energy consumption height is 2～4 times of Bayer process production method, and energy consumption cost accounts for 50% in direct operating cost; (2) technical process is long, and construction investment is big, and for large and medium-sized alumina producer, the construction investment of integrated process unit product is higher more than 20% than single Bayer process; (3) deficiency in economic performance, the unit product manufacturing cost is higher more than 8% than Bayer process.
[summary of the invention] in order to address the above problem, the invention provides a kind of with in the bauxite concentrate (alumina silica ratio is greater than 10) that obtains through direct-flotation desiliconisation of the diaspore type bauxite of low alumina silica ratio (A/S 4～8) be raw material, the production method of alumina.
The present invention---diaspore type bauxite preparing alumina from concentrate method mainly comprises the preparation of bauxite concentrate ore pulp, the Bayer process stripping, settlement separate washing, technological processs such as sodium aluminate solution crystal seed decomposition, its process is: aluminium concentrate and circulation alkali liquor, milk of lime adds pulp tank in proportion to carry out ore pulp and is mixed with qualified ore pulp, after pre-desiliconization is handled, send into the high pressure digester and carry out the high pressure stripping, dissolved mineral slurry enters settlement separate groove and carries out the red mud separation after dilution, the solid phase red mud effluxes after washing, foam settlement separate and that washing process produces enters foam chute to carry out returning original system behind the mechanical defoaming, sodium aluminate solution obtains aluminium hydroxide through decomposition of crystal seed, aluminium hydroxide obtains the finished product aluminum oxide through high-temperature roasting, and decomposition nut liquid returns aluminium concentrate pulp batching after evaporation concentration.The technical parameter of each technological process is as follows:
The bauxite concentrate that diaspore type bauxite adopts direct-flotation desiliconisation to obtain is a raw material, and its fineness is-0.074mm 74.4%～94.5%, contains Al
2O
367%～71%, SiO
25.8%～6.7%, moisture content 8%～14%, A/S 10, batching alkali lye Na
2O
K220g/L～230g/L, alkali lye molecular ratio (α
K) 3.0～3.3, ingredients molecular ratio (α
K) 1.45～1.55, the lime addition is 9～10% of a dried concentrate weight.
Bauxite concentrate Bayer process leaching condition is: the stripping temperature is 250 ℃～270 ℃, dissolution time 30～90 minutes.
Exsolution red mud settlement separate with the washing operation parameter be 95 ℃～110 ℃ of settlement separate temperature, sedimentation slurries liquid-solid ratio (L/S) 19～21, slurry specific gravity 1.38～1.65, average liquid composition Al
2O
3145g/L～160g/L, α
K1.50～1.60.
The sodium aluminate solution crystal seed decomposition condition is for decomposing 64 ℃～70 ℃ of initial temperature, and temperature is 42 ℃～46 ℃ eventually, resolving time 55h～70h, and seed is than 2.5～3.0.
Set up header tank and foam receiving tank in red-mud settlement separation and washing system, carry out mechanical defoaming, the slurries behind the froth breaking return sedimenting system.
The lime addition is 5%～15% (weight percent) that accounts for dried concentrate in the aluminium concentrate pulp allocation process of the present invention, allocates into the milk of lime that the circulation alkali liquor ashing obtains.In mechanical stirring ashing groove, with circulation alkali liquor lime is carried out ashing and handle, effectively calcium contains admittedly and reaches 150g/L～170g/L in milk of lime.
Fineness is-the single alumina producing Bayer process of aluminium concentrate of 0.074mm 74.4%～94.5%, and Al
2O
3Relative solubility rate be 96.0%～99.0%, dissolution fluid α
K1.50～1.55, exsolution red mud alumina silica ratio (A/S) is 1.10～1.60, sodium-silicon-rate (N/S) 0.05～0.40, and subsider underflow liquid-solid ratio (L/S)＜3.0, decomposition of crystal seed rate are 45%～55%.
At raw ore alumina silica ratio 4～8, through aluminium concentrate alumina silica ratio that flotation desilication obtains greater than 10 condition under, calculate with the industrial scale of producing 600000 tons of aluminum oxide per year, the present invention compares with integrated process, the engineering construction gross investment reduces by 16.4%, and energy consumption is saved more than 50%, and manufacturing cost reduces by 8.86%.The present invention is a low alumina silica ratio diaspore type bauxite resources effective method in the rational exploitation and utilization.
[description of drawings]
Fig. 1: process flow diagram of the present invention
[embodiment]
Embodiment 1: fineness is-0.074mm 74.4%～94.5% that alumina silica ratio is 11.25 direct flotation aluminium concentrate, at circulation alkali liquor concentration Na
2O
K220g/L (α
K1.38), the batching α
K1.55,255 ℃ of stripping temperature, 60 minutes time, lime addition be under the condition of 10% (weight percent) of dried concentrate, through the Al that obtains after the Bayer process stripping
2O
3Relative solubility rate be 98.24%, the red mud alumina silica ratio is 1.41, the red mud sodium-silicon-rate is 0.20.
Embodiment 2: fineness is-0.074mm 74.4%～94.5% that alumina silica ratio is 11.31 direct flotation aluminium concentrate, at circulation alkali liquor concentration Na
2O
K221g/L (α
K1.38), the batching α
K1.50,260 ℃ of stripping temperature, 90 minutes time, lime addition be under 9.01% the condition of dried concentrate, through the Al that obtains after the Bayer process stripping
2O
3Relative solubility rate be 99.0%, the red mud alumina silica ratio is 1.10, the red mud sodium-silicon-rate is 0.36.
Embodiment 3: average fineness is-0.074mm 74.4% that alumina silica ratio is 11.12 direct flotation aluminium concentrate, is 8～10m at mineral slurry flux
3/ h, lime addition account for do the ore deposit amount 10%, circulation alkali liquor concentration Na
2O
K227g/L, ingredients molecular ratio (α
K) 1.50, under 260 ℃～265 ℃ of the stripping temperature, the condition of 60～90 minutes time, be 1.52 through the stripping molecular ratio that obtains after the Bayer process stripping, Al
2O
3Relative solubility rate be 97.0%～98%, the red mud alumina silica ratio is 1.40, the red mud sodium-silicon-rate is 0.40.
At about 105 ℃ of temperature, diluent alumina concentration 150 ± 5g/L, α
K1.57 condition under, subsider underflow liquid-solid ratio is less than 2.2.
The sodium aluminate decomposition of crystal seed is being decomposed 64 ℃ of initial temperature, and temperature is 44 ℃ eventually, and resolving time 60h, seed are than under 2.5～3.0 the condition, and rate of decomposition is 48.6%, decomposition nut liquid α
K3.08 product aluminium hydroxide amount reaches international first grade standard.
Claims (4)
1, a kind of diaspore type bauxite preparing alumina from concentrate method, comprise the preparation of aluminium concentrate pulp, the Bayer process stripping, settlement separate washing, sodium aluminate solution crystal seed decomposes, it is characterized in that: aluminium concentrate and circulation alkali liquor, milk of lime is mixed and made into ore pulp, after pre-desiliconization is handled, send into the high pressure digester and carry out the high pressure stripping, dissolved mineral slurry enters settlement separate groove and carries out the red mud separation after dilution, the solid phase red mud effluxes after washing, foam settlement separate and that washing process produces enters foam chute to carry out returning original system behind the mechanical defoaming, sodium aluminate solution obtains aluminium hydroxide through decomposition of crystal seed, aluminium hydroxide obtains the finished product aluminum oxide through high-temperature roasting, decomposition nut liquid returns aluminium concentrate pulp batching after evaporation concentration, the technical parameter of each technological process is as follows:
A: direct flotation bauxite concentrate fineness is-0.074mm 74.4%～94.5% batching alkali lye Na
2O
K220g/L～230g/L, the alkali lye molecular ratio is 1.45～1.55, and ingredients molecular ratio is 1.45～1.55, and the lime addition is 9～10% of a dried concentrate weight;
B: in the bauxite concentrate Bayer process process in leaching, the stripping temperature is 250 ℃～270 ℃, dissolution time 30～90 minutes;
C: 95 ℃～110 ℃ of the settlement separate temperature of exsolution red mud, sedimentation slurries liquid-solid ratio 19～21, slurry specific gravity 1.38～1.65, average liquid composition Al
2O
3145g/L～160g/L, α
K1.50～1.60;
D: sodium aluminate solution crystal seed decomposes 64 ℃～70 ℃ of initial temperature, and temperature is 42 ℃～46 ℃ eventually, resolving time 55h～70h, and seed is than 2.5～3.0.
2, method according to claim 1 is characterized in that: lime is after handling through the circulation alkali liquor ashing, adds in the mode of milk of lime.
3, method according to claim 1 is characterized in that; Bauxite concentrate does not need ore grinding, directly carries out Bayer process with circulation alkali liquor and milk of lime and prepares burden.
4, method according to claim 1 is characterized in that: described aluminium concentrate is that to adopt alumina silica ratio be that 4～8 diaspore type bauxite is a raw material, makes behind direct-flotation desiliconisation, and its aluminum-containing mineral remains diaspore type bauxite.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001134388A CN1156399C (en) | 2000-05-19 | 2000-05-19 | Alumina producing process with hydraulic duralumin-type bauxite concentrate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001134388A CN1156399C (en) | 2000-05-19 | 2000-05-19 | Alumina producing process with hydraulic duralumin-type bauxite concentrate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1324765A CN1324765A (en) | 2001-12-05 |
| CN1156399C true CN1156399C (en) | 2004-07-07 |
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ID=4583222
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB001134388A Expired - Fee Related CN1156399C (en) | 2000-05-19 | 2000-05-19 | Alumina producing process with hydraulic duralumin-type bauxite concentrate |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100396383C (en) * | 2005-09-22 | 2008-06-25 | 贵阳铝镁设计研究院 | Coarse-fine red mud grading method |
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| CN1307105C (en) * | 2004-03-31 | 2007-03-28 | 中国铝业股份有限公司 | Method for separating alumina and vaporizing sodium carbonate in mother liquor |
| CN1772620B (en) * | 2004-11-10 | 2010-12-22 | 赵中伟 | Symmetrical Bayer process of decomposing bauxite |
| CN100398447C (en) * | 2005-01-21 | 2008-07-02 | 中南大学 | Method for extracting alumina from high silicon bauxite |
| CN1332884C (en) * | 2005-04-29 | 2007-08-22 | 华建村 | Method for preparing sodium aluminate solution |
| CN100363262C (en) * | 2005-04-29 | 2008-01-23 | 邓少彬 | Method for producing alumina |
| CN100348492C (en) * | 2005-10-20 | 2007-11-14 | 贵阳铝镁设计研究院 | Method for adjusting dissolved liquid by spieces mother liquid |
| CN100348331C (en) * | 2005-11-28 | 2007-11-14 | 中国铝业股份有限公司 | Flotation selection and desiliconization method for middle and low grade alumyte |
| CN100532262C (en) * | 2007-07-12 | 2009-08-26 | 中国铝业股份有限公司 | Method for producing aluminium oxide by middle-low grade alumyte |
| CN101249976B (en) * | 2007-12-04 | 2010-12-22 | 北京化工大学 | Technique for producing aluminum oxide by alkali dissolving carbonation method |
| CN101264906B (en) * | 2008-04-25 | 2010-06-16 | 河南未来铝业（集团）有限公司 | Method for producing aluminum hydroxide or aluminum oxide by Bayer process |
| CN101746795B (en) * | 2008-12-02 | 2012-04-25 | 中国科学院过程工程研究所 | Method for producing alumina from bauxite |
| CN102146515A (en) * | 2011-01-12 | 2011-08-10 | 虹京环保有限公司 | Method for preparing aluminium oxide by recovery of nickel-aluminium concentrate |
| CN103101941A (en) * | 2011-11-14 | 2013-05-15 | 沈阳铝镁设计研究院有限公司 | Comprehensive energy-saving method for ore grinding, predesilicification and digestion procedures |
| CN102515217A (en) * | 2011-11-18 | 2012-06-27 | 中国铝业股份有限公司 | Method for adding lime to alumina produced by adopting ore-dressing Bayer process |
| CN102674416B (en) * | 2012-05-18 | 2014-02-05 | 义马煤业集团股份有限公司 | Method for producing aluminum oxide-lime blend ores by Bayer process |
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| CN103663517B (en) * | 2013-11-26 | 2016-07-13 | 中国铝业股份有限公司 | A kind of method reducing Liquor of Ore Dressing Bayer process exsolution red mud sodium-silicon-rate |
| CN105435942A (en) * | 2014-09-16 | 2016-03-30 | 沈阳铝镁设计研究院有限公司 | Bauxite coarse-fine separation grinding method |
| CN104528786A (en) * | 2014-12-15 | 2015-04-22 | 沈阳工业大学 | Method for producing aluminum oxide by treating low-grade bauxite with ammonia-alkali combination method |
| CN109179463B (en) * | 2018-11-07 | 2020-10-20 | 沈阳工业大学 | Method for treating aluminum resource by Bayer-red mud alkali-dissolution series process |
-
2000
- 2000-05-19 CN CNB001134388A patent/CN1156399C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100396383C (en) * | 2005-09-22 | 2008-06-25 | 贵阳铝镁设计研究院 | Coarse-fine red mud grading method |
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| CN1324765A (en) | 2001-12-05 |
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