CN100337921C - Method for preparing alumina - Google Patents
Method for preparing alumina Download PDFInfo
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- CN100337921C CN100337921C CNB2005100707386A CN200510070738A CN100337921C CN 100337921 C CN100337921 C CN 100337921C CN B2005100707386 A CNB2005100707386 A CN B2005100707386A CN 200510070738 A CN200510070738 A CN 200510070738A CN 100337921 C CN100337921 C CN 100337921C
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- Prior art keywords
- sodium aluminate
- aluminate solution
- decomposition
- aluminium hydroxide
- stripping
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title abstract description 53
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229910001388 sodium aluminate Inorganic materials 0.000 claims abstract description 50
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims abstract description 47
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 41
- 239000013078 crystal Substances 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 239000003513 alkali Substances 0.000 claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 229910001570 bauxite Inorganic materials 0.000 claims abstract description 6
- 229910021502 aluminium hydroxide Inorganic materials 0.000 claims description 44
- 239000002002 slurry Substances 0.000 claims description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 229910052799 carbon Inorganic materials 0.000 claims description 13
- 239000003518 caustics Substances 0.000 claims description 10
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 8
- 229910052708 sodium Inorganic materials 0.000 claims description 8
- 239000011734 sodium Substances 0.000 claims description 8
- 238000009413 insulation Methods 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 7
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- 229910052782 aluminium Inorganic materials 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 3
- 238000005245 sintering Methods 0.000 abstract description 42
- 238000005516 engineering process Methods 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 2
- 230000029087 digestion Effects 0.000 abstract 1
- 238000001914 filtration Methods 0.000 abstract 1
- 239000012452 mother liquor Substances 0.000 abstract 1
- 230000001590 oxidative effect Effects 0.000 abstract 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 20
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 12
- 239000001569 carbon dioxide Substances 0.000 description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 description 10
- 239000000126 substance Substances 0.000 description 7
- 239000000377 silicon dioxide Substances 0.000 description 6
- 238000004131 Bayer process Methods 0.000 description 5
- 229910000503 Na-aluminosilicate Inorganic materials 0.000 description 5
- 239000000429 sodium aluminium silicate Substances 0.000 description 5
- 235000012217 sodium aluminium silicate Nutrition 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- 238000010129 solution processing Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000004411 aluminium Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 210000000582 semen Anatomy 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 229960001866 silicon dioxide Drugs 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Abstract
The present invention discloses an alumina producing method, which relates to an alumina producing method through raw materials of bauxite by a sintering method, particularly to an improvement on the treating process of coarse sodium aluminate solution output after clinker digestion in the production process. The present invention is characterized in that the deep carbonation decomposition, namely the filtration of the coarse sodium aluminate solution, leads to the obtainment of aluminum hydroxide and mother liquor of carbonation decomposition; after solid-liquid separation, aluminum hydroxide is loaded into a digester; digesting desiliconization is carried out by alkali liquor under the condition of the temperature of 110 to 150 DEG C and the addition of crystal seeds of 20 g/L to 100 g/L; the decomposition of the crystal seeds is then carried out, and a finished product of aluminum hydroxide is produced. Compared with the existing treating technology for coarse sodium aluminate solutions, the alumina output rate of the coarse sodium aluminate solution of the present invention can be increased by about 20%, the rate of first-grade products for alumina products through a sintering method can reach 100%, and the oxidizing productivity of a sintering method system can be increased by 10% to 20%.
Description
Technical field
A kind of production method of aluminium hydroxide, relating to a kind of is that raw material adopts sintering process production method of alumina, the particularly improvement of the crude sodium aluminate solution-treated process of output after the grog stripping in the production process with bauxite.
Background technology
In existing alumina by sintering production process, the crude sodium aluminate solution of output (being called for short thick liquid) after the grog stripping, the general sintering process kind that at first adds some amount divides the white residue seed of mother liquid evaporation (or seed precipitation solution) and some amount to be mixed with the desiliconization slurries, the adding of wherein planting the branch mother liquid evaporation is in order to improve the caustic ratio of crude sodium aluminate solution, to increase its stability at desiliconization process; The adding of white residue seed is in order to improve the desiliconization index of sodium aluminate solution.The desiliconization slurries through press in one section boil desiliconization and two sections add make behind the milk of lime deep desilication (or one section atmospheric silicon removing and two sections add the milk of lime deep desilication) desiliconization index greater than 300 seminal fluid and desiliconization index greater than 600 seminal fluid, the former is used for the sintering process decomposition of crystal seed, the latter is used for the sintering process carbonating and decomposes the two kinds of equal output finished product of decomposition technique aluminium hydroxides.There is following problem in existing sintering process crude sodium aluminate solution processing craft:
(1) sintering process crude sodium aluminate solution oxide aluminium output capacity is low: owing to must adopt decomposition of crystal seed technology in the existing crude sodium aluminate solution processing craft, and the rate of decomposition of decomposition of crystal seed lower (usually less than 60%); In order to guarantee the alumina product quality of carbonating decomposition output, the carbonating rate of decomposition is controlled at below 92%, thereby causes existing crude sodium aluminate solution processing craft aluminum oxide quantum of output lower simultaneously.
(2) the alumina by sintering quality product is relatively poor: because carbonating is decomposed the alumina product ratio big (being that the sintering process kind is divided more than 1.5 times of alumina product) that obtains, the chemistry percentage of product is lower, cause whole alumina by sintering product chemical quality amount relatively poor, being generally is two, three grades of product, and the ratio of first-grade products is lower.(3) because the sodium white residue and the calcium-silicon slag of a desiliconization and secondary desiliconization output all turn back to the sintering process feed proportioning system, reduced the treatment capacity of sintering process system bauxite, thereby reduced sintering process system aluminum oxide production capacity.(4) pressure-off silicon in the employing, the desiliconization temperature is 155-165 ℃, the live steam consumption is bigger.
Summary of the invention
The present invention be directed to the deficiency that above-mentioned existing crude sodium aluminate solution processing techniques exists, propose a kind of production method that can effectively improve sintering process crude sodium aluminate solution aluminium hydroxide output capacity, raising sintering process product aluminium hydroxide chemistry grade amount, the whole sintering process system aluminium hydroxide production capacity of raising, simplification sintering process desiliconization flow process, reduce the aluminium hydroxide of desiliconization system live steam consumption.
The objective of the invention is to be achieved through the following technical solutions.
A kind of production method of aluminium hydroxide comprises that bauxite is added the alkali knot to be burnt, prepare the crude aluminum acid solution with the dilute alkaline soln stripping, it is characterized in that it being crude sodium aluminate solution to be filtered promptly carry out the decomposition of degree of depth carbonating, obtains aluminium hydroxide and carbon mother liquid; After the solid-liquid separation aluminium hydroxide is sent in the digester, carried out stripping with alkali lye under the crystal seed condition of 110-150 ℃ of temperature and interpolation 20g/L-100g/L, the alkali lye caustic sodium concentration is 100～250g/L; With stripping slurries insulation 1～5 hour, the desiliconization index that makes liquid phase was greater than 200; The stripping slurries being adjusted to alumina concentration then is 100g/L-200g/L; Solid-liquid separation obtains sodium aluminate solution, carries out decomposition of crystal seed, output finished product aluminium hydroxide.
Method of the present invention is removed most red mud suspended substances with filter plant.The aluminum oxide that to make with extra care in the crude sodium aluminate solution decomposes out as much as possible again, and output contains silicon-dioxide higher thick aluminium hydroxide and carbon mother liquid.The thick aluminium hydroxide of output is purified with bayer process, obtain satisfactory finished product aluminium hydroxide.Where necessary, implement the carbon mother liquid causticization, output caustic alkali is used for mending alkali to the bayer process flow process.Filter by sintering process crude sodium aluminate solution, output contains red mud suspended substance refining crude sodium aluminate solution seldom.Refining crude sodium aluminate solution deep carbonating is decomposed output siliceous high thick aluminium hydroxide and carbon mother liquid.Thick aluminium hydroxide is purified output finished product aluminium hydroxide with bayer process.The finished product Aluminium hydroxide roasting, output finished product aluminum oxide.Carbon mother liquid all send the grog stripping generally speaking and prepares burden after evaporation concentration, and in case of necessity with part carbon mother liquid causticization, output caustic alkali send bayer process to mend alkali.Effectively improve sintering process crude sodium aluminate solution oxide aluminium output capacity, improved sintering process product aluminum oxide chemistry grade amount, improved whole sintering process system aluminum oxide production capacity, simplified sintering process desiliconization flow process, reduced the live steam consumption of desiliconization system.
Because the rate of decomposition that the product aluminum oxide quantum of output of crude sodium aluminate solution is decomposed by degree of depth carbonating is mainly controlled, because of degree of depth carbon branch rate of decomposition can reach 90%-100%, thus method of the present invention, aluminum oxide output capacity height; The thick aluminium hydroxide because the use bayer process is purified makes the whole sintering process product aluminum oxide ratio of first-grade products can reach 100%; Because the 4A-zeolite of output can be used as production marketing, thus the white residue that returns burden process can not produced in the novel process, thus improve sintering system aluminum oxide production capacity greatly.Compare with existing crude sodium aluminate solution processing craft, crude sodium aluminate solution oxide aluminium output capacity can improve about 20%; The sintering process product aluminum oxide ratio of first-grade products can reach 100%; Sintering process system oxidation production capacity can improve 10%-20%.
Embodiment
A kind of production method of aluminium hydroxide comprises bauxite is added the alkali knot to be burnt, prepare the crude aluminum acid solution with the dilute alkaline soln stripping, is characterized in that it being crude sodium aluminate solution to be filtered to red mud suspension content＜0.1g/L make with extra care; Sodium aluminate solution after will making with extra care again feeds carbon dioxide and carries out the decomposition of degree of depth carbonating, and wherein density of carbon dioxide gas is 30%～40%, and the carbonating rate of decomposition is 90%～100%.Obtaining silica weight content after the decomposition is thick aluminium hydroxide and the carbon mother liquid of 1%-5%; Thick aluminium hydroxide is sent in the digester, carried out stripping with alkali lye under the crystal seed condition of 110-150 ℃ of temperature and interpolation 20g/L-100g/L, the alkali lye caustic sodium concentration is 100～250g/L; With stripping slurries insulation 1～5 hour, the desiliconization index that makes liquid phase was greater than 200; The stripping slurries being adjusted to alumina concentration then is 100g/L-200g/L; Solid-liquid separation goes out sodium aluminate solution and delivers to the decomposition of crystal seed system; What obtain contains sodium aluminosilicate of water or sale or returns the sintering process feed proportioning system; Add aluminium hydroxide crystal seed and decompose in sodium aluminate solution, the decomposition of crystal seed rate is 45%～60%, output finished product aluminium hydroxide.
Embodiment 1
With leaf filter filter sintering process crude sodium aluminate solution is filtered, obtaining the red mud suspended substance is the crude sodium aluminate solution of 0.012g/l, sodium aluminate solution after will making with extra care again feeds carbon dioxide and carries out the decomposition of degree of depth carbonating, and wherein density of carbon dioxide gas is 30%, and the carbonating rate of decomposition is 90.Obtain silica weight content after the decomposition and be 5% thick aluminium hydroxide and carbon mother liquid; Thick aluminium hydroxide is sent in the digester, carried out stripping with alkali lye under the crystal seed condition of 110 ℃ of temperature and interpolation 20g/L, the alkali lye caustic sodium concentration is 100g/L; With stripping slurries insulation 1 hour, the desiliconization index that makes liquid phase was greater than 200; The stripping slurries being adjusted to alumina concentration then is 100g/L; Solid-liquid separation goes out sodium aluminate solution and delivers to the decomposition of crystal seed system; What obtain contains sodium aluminosilicate of water or sale or returns the sintering process feed proportioning system; Add aluminium hydroxide crystal seed and decompose in sodium aluminate solution, the decomposition of crystal seed rate is 45%, output finished product aluminium hydroxide.The sintering process product aluminum oxide ratio of first-grade products can reach 100%; Sintering process system oxidation production capacity can improve 10%.
Embodiment 2
With leaf filter filter sintering process crude sodium aluminate solution is filtered, obtaining the red mud suspended substance is the crude sodium aluminate solution of 0.08g/l, sodium aluminate solution after will making with extra care again feeds carbon dioxide and carries out the decomposition of degree of depth carbonating, and wherein density of carbon dioxide gas is 34%, and the carbonating rate of decomposition is 95%.Obtain silica weight content after the decomposition and be 3% thick aluminium hydroxide and carbon mother liquid; Thick aluminium hydroxide is sent in the digester, carried out stripping with alkali lye under the crystal seed condition of 130 ℃ of temperature and interpolation 60g/L, the alkali lye caustic sodium concentration is 100～200g/L; With stripping slurries insulation 3 hours, the desiliconization index that makes liquid phase was greater than 200; The stripping slurries being adjusted to alumina concentration then is 150g/L; Solid-liquid separation goes out sodium aluminate solution and delivers to the decomposition of crystal seed system; What obtain contains sodium aluminosilicate of water or sale or returns the sintering process feed proportioning system; Add aluminium hydroxide crystal seed and decompose in sodium aluminate solution, the decomposition of crystal seed rate is 50%, output finished product aluminium hydroxide.The sintering process product aluminum oxide ratio of first-grade products can reach 100%; Sintering process system oxidation production capacity can improve 20%.
Embodiment 3
With leaf filter filter sintering process crude sodium aluminate solution is filtered, obtaining the red mud suspended substance is the crude sodium aluminate solution of 0.1g/L, sodium aluminate solution after will making with extra care again feeds carbon dioxide and carries out the decomposition of degree of depth carbonating, and wherein density of carbon dioxide gas is 40%, and the carbonating rate of decomposition is 98%.Obtain silica weight content after the decomposition and be 1% thick aluminium hydroxide and carbon mother liquid; Thick aluminium hydroxide is sent in the digester, carried out stripping with alkali lye under the crystal seed condition of 150 ℃ of temperature and interpolation 100g/L, the alkali lye caustic sodium concentration is 250g/L; With stripping slurries insulation 5 hours, the desiliconization index that makes liquid phase was greater than 200; The stripping slurries being adjusted to alumina concentration then is 200g/L; Solid-liquid separation goes out sodium aluminate solution and delivers to the decomposition of crystal seed system; What obtain contains sodium aluminosilicate of water or sale or returns the sintering process feed proportioning system; Add aluminium hydroxide crystal seed and decompose in sodium aluminate solution, the decomposition of crystal seed rate is 60%, output finished product aluminium hydroxide.
Embodiment 4
With leaf filter filter sintering process crude sodium aluminate solution is filtered, obtaining the red mud suspended substance is the crude sodium aluminate solution of 0.054g/L, sodium aluminate solution after will making with extra care again feeds carbon dioxide and carries out the decomposition of degree of depth carbonating, wherein density of carbon dioxide gas is 38%, and the carbonating rate of decomposition is 97%.Obtain silica weight content after the decomposition and be 3.5% thick aluminium hydroxide and carbon mother liquid; Thick aluminium hydroxide is sent in the digester, carried out stripping with alkali lye under the crystal seed condition of 140 ℃ of temperature and interpolation 80g/L, the alkali lye caustic sodium concentration is 230g/L; With stripping slurries insulation 3.8 hours, the desiliconization index that makes liquid phase was greater than 200; The stripping slurries being adjusted to alumina concentration then is 185g/L; Solid-liquid separation goes out sodium aluminate solution and delivers to the decomposition of crystal seed system; What obtain contains sodium aluminosilicate of water or sale or returns the sintering process feed proportioning system; Add aluminium hydroxide crystal seed and decompose in sodium aluminate solution, the decomposition of crystal seed rate is 55%, output finished product aluminium hydroxide.
Claims (1)
1. the production method of an aluminium hydroxide comprises that bauxite is added the alkali knot to be burnt, prepare the crude aluminum acid solution with the dilute alkaline soln stripping, it is characterized in that it being crude sodium aluminate solution to be filtered promptly carry out the decomposition of degree of depth carbonating, obtains aluminium hydroxide and carbon mother liquid; After the solid-liquid separation aluminium hydroxide is sent in the digester, carried out stripping with alkali lye under the crystal seed condition of 110-150 ℃ of temperature and interpolation 20g/L-100g/L, the alkali lye caustic sodium concentration is 100～250g/L; With stripping slurries insulation 1～5 hour, the desiliconization index that makes liquid phase was greater than 200; The stripping slurries being adjusted to alumina concentration then is 100g/L-200g/L; Solid-liquid separation obtains sodium aluminate solution, carries out decomposition of crystal seed, output finished product aluminium hydroxide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100707386A CN100337921C (en) | 2005-05-18 | 2005-05-18 | Method for preparing alumina |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100707386A CN100337921C (en) | 2005-05-18 | 2005-05-18 | Method for preparing alumina |
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| CN1686810A CN1686810A (en) | 2005-10-26 |
| CN100337921C true CN100337921C (en) | 2007-09-19 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB2005100707386A Active CN100337921C (en) | 2005-05-18 | 2005-05-18 | Method for preparing alumina |
Country Status (1)
| Country | Link |
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| CN (1) | CN100337921C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101328693B (en) * | 2007-06-19 | 2010-08-18 | 郭海军 | Clean production method of chemical pulping paper making and aluminum oxide cogeneration |
| CN101249976B (en) * | 2007-12-04 | 2010-12-22 | 北京化工大学 | Technique for producing aluminum oxide by alkali dissolving carbonation method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1005859B (en) * | 1986-01-04 | 1989-11-22 | 日产自动车株式会社 | Weft testing device for jet loom |
| CN1095444C (en) * | 1999-07-05 | 2002-12-04 | 中国长城铝业公司中州铝厂 | Intensified sintering process for alumina production |
-
2005
- 2005-05-18 CN CNB2005100707386A patent/CN100337921C/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1005859B (en) * | 1986-01-04 | 1989-11-22 | 日产自动车株式会社 | Weft testing device for jet loom |
| CN1095444C (en) * | 1999-07-05 | 2002-12-04 | 中国长城铝业公司中州铝厂 | Intensified sintering process for alumina production |
Non-Patent Citations (2)
| Title |
|---|
| 关于改进烧结法湿法流程的刍议 上官正、杨重愚，轻金属，第2期 1995 * |
| 深度碳分技术在烧结法生产中的应用 冯文洁、赵志英、卜天梅，有色冶金节能，第22卷第1期 2005 * |
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| CN1686810A (en) | 2005-10-26 |
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