CN101117228A - Method for extracting aluminium oxide from coal ash - Google Patents
Method for extracting aluminium oxide from coal ash Download PDFInfo
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- CN101117228A CN101117228A CNA2007101186794A CN200710118679A CN101117228A CN 101117228 A CN101117228 A CN 101117228A CN A2007101186794 A CNA2007101186794 A CN A2007101186794A CN 200710118679 A CN200710118679 A CN 200710118679A CN 101117228 A CN101117228 A CN 101117228A
- Authority
- CN
- China
- Prior art keywords
- flyash
- ammonium sulfate
- extracting
- alumina
- solid
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 62
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims description 39
- 239000010883 coal ash Substances 0.000 title 1
- 239000010881 fly ash Substances 0.000 claims abstract description 60
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 36
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 36
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims abstract description 36
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000007787 solid Substances 0.000 claims abstract description 31
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims abstract description 29
- 229910021502 aluminium hydroxide Inorganic materials 0.000 claims abstract description 29
- 238000005245 sintering Methods 0.000 claims abstract description 25
- WZUKKIPWIPZMAS-UHFFFAOYSA-K Ammonium alum Chemical compound [NH4+].O.O.O.O.O.O.O.O.O.O.O.O.[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O WZUKKIPWIPZMAS-UHFFFAOYSA-K 0.000 claims abstract description 22
- 239000007791 liquid phase Substances 0.000 claims abstract description 8
- 235000011124 aluminium ammonium sulphate Nutrition 0.000 claims description 20
- 238000005406 washing Methods 0.000 claims description 17
- 229910021529 ammonia Inorganic materials 0.000 claims description 16
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 15
- 239000007790 solid phase Substances 0.000 claims description 15
- 239000002253 acid Substances 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 11
- FOJJCOHOLNJIHE-UHFFFAOYSA-N aluminum;azane Chemical compound N.[Al+3] FOJJCOHOLNJIHE-UHFFFAOYSA-N 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 238000002425 crystallisation Methods 0.000 claims description 9
- 230000008025 crystallization Effects 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 8
- 230000008020 evaporation Effects 0.000 claims description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 239000003245 coal Substances 0.000 claims description 7
- 229910052717 sulfur Inorganic materials 0.000 claims description 7
- 239000011593 sulfur Substances 0.000 claims description 7
- 239000006229 carbon black Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 3
- 239000001117 sulphuric acid Substances 0.000 claims description 3
- 235000011149 sulphuric acid Nutrition 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 230000002378 acidificating effect Effects 0.000 abstract description 2
- 230000007797 corrosion Effects 0.000 abstract description 2
- 238000005260 corrosion Methods 0.000 abstract description 2
- HSEYYGFJBLWFGD-UHFFFAOYSA-N 4-methylsulfanyl-2-[(2-methylsulfanylpyridine-3-carbonyl)amino]butanoic acid Chemical compound CSCCC(C(O)=O)NC(=O)C1=CC=CN=C1SC HSEYYGFJBLWFGD-UHFFFAOYSA-N 0.000 abstract 1
- 230000009286 beneficial effect Effects 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 239000012535 impurity Substances 0.000 description 6
- 238000004090 dissolution Methods 0.000 description 5
- 238000000605 extraction Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000035484 reaction time Effects 0.000 description 5
- 239000000377 silicon dioxide Substances 0.000 description 5
- 229960001866 silicon dioxide Drugs 0.000 description 5
- 235000012239 silicon dioxide Nutrition 0.000 description 5
- 229910004298 SiO 2 Inorganic materials 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 229910001570 bauxite Inorganic materials 0.000 description 3
- 239000000284 extract Substances 0.000 description 3
- 238000003672 processing method Methods 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000004131 Bayer process Methods 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000012633 leachable Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000001953 recrystallisation Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
Abstract
The invention provides a method to extract aluminum oxide from a fly ash, and relates to a technological method which is to extract aluminum oxide from the fly ash and comprehensively utilize the residue after extracting aluminum oxide. The invention is characterized in the method which is as follows: ammonium sulfate is mixed into the fly ash to sintering, and the solid is dissolved to obtain the solution containing aluminum-ammonium sulfate; the solution is crystallized to form solid aluminium-ammonium sulfate; solid aluminium-ammonium sulfate reacts with ammonia gas to obtain aluminium hydroxide and ammonium sulfate, and aluminium hydroxide and ammonium sulfate are washed and filtrated to obtain solid aluminium hydroxide; solid aluminium hydroxide is calcined to obtain aluminum oxide; ammonium sulfate can be circularly used after being evaporated in the liquid phase. The ammonium sulfate which is used by the method of the invention is weak acidic, the corrosiveness on the equipment is small, and the ammonium sulfate can be used circularly. The whole process is easy to industrial application. The requirement of the corrosion resistance on the equipment is low. The amount of the residue is small which is beneficial to the comprehensive utilization of the residue after extracting the aluminum oxide.
Description
Technical field
A kind of method of alumina of extracting from flyash relates to a kind of processing method that residue behind the aluminum oxide is extracted in aluminum oxide and comprehensive utilization of extracting from flyash.
Background technology
At present, the production of aluminum oxide is raw material with bauxite mainly, and the production method of aluminum oxide is mainly alkaline process, comprises Bayer process, sintering process and integrated process.In recent years, China's aluminum oxide output constantly increases fast, become second-biggest-in-the-world alumina producing state, and China is the poor relatively country of bauxite resource, at present the whole nation is found out and the bauxite resource reserves of inferring guarantee that to China's aluminum oxide industry degree is low, so resource problem has become one of subject matter of restriction China aluminium industrial sustainable development.
China is coal big country, and the flyash quantity discharged in every year is big, and development and use flyash is produced aluminum oxide, not only China's aluminium industrial expansion is had great importance, and the dirty reduction of discharging of falling of the electric industry of China's coal is waited also to have great significance simultaneously.
From flyash, extract Al
2O
3Method can be divided into alkaline process and acid system two big classes.Alkaline process comprises that Wingdale burns method and soda-lime sintering process, is doing a lot of researchs aspect the alkaline process processing flyash both at home and abroad, and the principal feature that alkaline process is handled flyash production aluminum oxide is that technical process is long, and the inventory of running is big, and facility investment is also bigger.And the level of residue that is produced behind the extraction aluminum oxide is the several times of flyash amount, need the supporting a large amount of residues that have corresponding cement production system to handle and produced behind the extraction aluminum oxide, therefore, the somewhere utilizes the industrial scale of flyash extraction aluminum oxide to have to be subjected to the restriction in local cement market to a certain extent.With alkaline process relatively, handle flyash with acid system and effectively extracting in the flyash in the aluminum oxide, the silicon-dioxide in the flyash does not enter wet method system, can not produce new solid materials in process of production, level of residue is less, thereby the inventory of running is little, and facility investment is less relatively.But the main weak point of acid system is that the reaction equipment of using must be acidproof, and spent acid reclaims comparatively difficulty; Secondly, when the leaching aluminum oxide, also bring into solution such as many leachable impurity such as iron, magnesium etc. in the flyash, need increase the postorder treatment process.These weak points all can restrict scale and the economic results in society thereof that acid system extracts aluminum oxide in the flyash to a certain extent.
Summary of the invention
Purpose of the present invention is exactly in order to overcome the existing deficiency of extracting the processing method of aluminum oxide from flyash, provide a kind of processing method simple, to the erosion resistance of equipment require low, be easy to that large-scale industrialization uses from flyash, extract method of alumina.
The objective of the invention is to be achieved through the following technical solutions.
A kind of method of alumina of from flyash, extracting, it is characterized in that its method is to allocate ammonium sulfate into flyash to carry out sintering, the gained solid obtains the solution of sulfur acid aluminium ammonium after stripping, this solution obtains the solid exsiccated ammonium alum by the crystalline method, solid sulphuric acid aluminium ammonium and ammonia get aluminium hydroxide and ammonium sulfate, by washing and filtering, obtain solid aluminium hydroxide, aluminium hydroxide can obtain alumina product after roasting; The ammonium sulfate that enters liquid phase continues to recycle after evaporation.
A kind of method of alumina of from flyash, extracting of the present invention, it is characterized in that ammonium sulfate allocates flyash into and carry out the agglomerating ratio of components and count 3-12 with the molecular ratio of aluminum oxide in ammonium sulfate/flyash, sintering temperature is 240-900 ℃, and sintering reaction is 0.1～5 hour.
A kind of method of alumina of extracting from flyash of the present invention is characterized in that water normal pressure stripping sintered clinker, and the solid phase residue adopts filtration or settlement separate after the stripping.
A kind of method of alumina of extracting from flyash of the present invention is characterized in that the washing water stripping sintered clinker of solid phase residue after water or the stripping.
A kind of method of alumina of extracting from flyash of the present invention is characterized in that the solution for the sulfur acid aluminium ammonium that obtains after the sintered clinker stripping, is to obtain the solid exsiccated ammonium alum by the method for evaporative crystallization or the method for cooling post crystallization.
A kind of method of alumina of from flyash, extracting of the present invention, the solid phase exsiccated ammonium alum reaction that it is characterized in that logical ammonia and obtain is decomposed the solid phase exsiccated ammonium alum and is generated aluminium hydroxide; Obtain aluminium hydroxide through washing, obtain aluminum oxide after the roasting, the liquid phase behind the washing aluminium hydroxide is through evaporation, and the ammonium sulfate that obtains returns the sintering circuit batching.
A kind of method of alumina of extracting from flyash of the present invention is characterized in that the sintering circuit of the ammonia of its process use from ammonium sulfate and flyash.
A kind of method of alumina of extracting from flyash of the present invention is characterized in that extracting that the main component of residue is SiO behind the aluminum oxide
2, can be used for producing white carbon black or structure material etc.
A kind of method of alumina of extracting from flyash of the present invention is characterized in that used raw material also can be a coal gangue.
Method of the present invention, based on the following principles of chemistry:
Sintering reaction: 4 (NH
4)
2SO
4+ Al
2O
3=2NH
4Al (SO
4)
2+ 6NH
3+ 3H
2O
Decomposition reaction: NH
4Al (SO
4)
212H
2O+3NH
3=Al (OH)
3+ 2 (NH
4)
2SO
4+ 9H
2O
Adopt ammonium sulfate and flyash to burn till by certain proportioning, the gained solid obtains the solution of sulfur acid aluminium ammonium after stripping, solution obtains the solid exsiccated ammonium alum by the crystalline method, after logical ammonia and the reaction of solid phase exsiccated ammonium alum, obtain aluminium hydroxide and ammonium sulfate, by washing and filtering, can obtain solid aluminium hydroxide, aluminium hydroxide can obtain alumina product after calcining; The ammonium sulfate that enters liquid phase continues to recycle after evaporation.
Adopt method of the present invention, the residue from flyash behind the extraction aluminum oxide can be reused, as is used to produce white carbon black or structure material etc.; The ammonium sulfate that uses is slightly acidic, and is little to the corrodibility of equipment, and ammonium sulfate can recycle, and integrated artistic is easy to industrial applications.Corrosion resistance nature to equipment requires low; Residue obtained amount is little, helps extracting the comprehensive utilization of residue behind the aluminum oxide.
Description of drawings]
Fig. 1 is the principle process flow sheet of method of the present invention.
Embodiment]
A kind of method of alumina of from flyash, extracting, adopt flyash and ammonium sulfate to burn till by certain proportioning, the gained solid obtains the solution of sulfur acid aluminium ammonium after stripping, this solution obtains the solid exsiccated ammonium alum by the crystalline method, solid sulphuric acid aluminium ammonium and react (in case of necessity except that ammonia from sintering process from the ammonia of sintering process, can also replenish a certain amount of ammonia), can get aluminium hydroxide and ammonium sulfate, pass through washing and filtering, can obtain solid aluminium hydroxide, aluminium hydroxide can obtain alumina product after roasting; The ammonium sulfate that enters liquid phase continues to recycle after evaporation.And the main component of solid phase residue is SiO after the stripping
2, be convenient to comprehensive utilization, as produce white carbon black etc.Carry out sintering after using ammonium sulfate and flyash by the proper proportion batching, sintering temperature is at 240-900 ℃, and the sintering reaction time is 0.1～5 hour, and ratio of components is 3-12 in the molecular ratio of aluminum oxide in ammonium sulfate/flyash.Water normal pressure stripping sintered clinker can have higher digesting efficiency of alumina.The leaching condition that control is suitable, in the sintered clinker solubility rate of aluminum oxide can 〉=95%.The separation of solid phase residue can adopt filtering separation or settlement separate method to realize after the stripping.The water that is used for the stripping sintered clinker can be new water, also can be the washing water of solid phase residue after the stripping.Solution for the sulfur acid aluminium ammonium that obtains after the sintered clinker stripping obtains the solid exsiccated ammonium alum by the crystalline method, effectively separates the impurity such as iron in the dissolution fluid simultaneously.Such as can the exsiccated ammonium alum crystallization being separated out by the way of evaporation.Logical ammonia and the reaction of solid phase exsiccated ammonium alum are decomposed the solid phase exsiccated ammonium alum and are generated aluminium hydroxide.Obtain aluminium hydroxide through washing, obtain aluminum oxide after the roasting.Liquid phase behind the washing aluminium hydroxide is through evaporation, and the ammonium sulfate that obtains returns the sintering circuit batching.Ammonia is from the sintering circuit of ammonium sulfate and flyash.Need to replenish a certain amount of new ammonia in case of necessity.Residue from flyash behind the extraction aluminum oxide can be reused, as is used to produce white carbon black and structure material etc.Used raw material also can be a coal gangue.
Embodiment 1
Flyash salic 33%, silicon-dioxide 49% is levigate, by the molecular ratio of the aluminum oxide in ammonium sulfate/flyash is 5 to join the ore deposit, 530 ℃ of sintering temperatures, reaction times is 2 hours, sintered clinker stripping under 98 ℃ condition, and dissolution fluid gained exsiccated ammonium alum solid after crystallization uses ammonia to decompose, obtain the aluminium hydroxide solid, after washing, filtration, roasting, obtain alumina product, gained alumina product impurity chemical ingredients is: Fe
2O
3: 0.02%, SiO
2: 0.08%.
Embodiment 2
Flyash salic 40%, silicon-dioxide 48% is levigate, by the molecular ratio of the aluminum oxide in ammonium sulfate/flyash is 4 to join the ore deposit, 500 ℃ of sintering reaction temperature, reaction times is 2 hours, sintered clinker stripping under 85 ℃ condition, and dissolution fluid gained exsiccated ammonium alum solid after crystallization uses ammonia to decompose, obtain the aluminium hydroxide solid, after washing, filtration, roasting, obtain alumina product, gained alumina product impurity chemical ingredients is: Fe
2O
3: 0.05%, SiO
2: 0.05%.
Embodiment 3
Flyash salic 38%, silicon-dioxide 47% is levigate, by the molecular ratio of the aluminum oxide in ammonium sulfate/flyash is 4.5 to join the ore deposit, 460 ℃ of sintering reaction temperature, the reaction times is 3 hours, sintered clinker stripping under 90 ℃ condition, exsiccated ammonium alum solid through stripping after the recrystallization of dissolution fluid through obtaining after the crystallization, re-use ammonia and decompose, obtain the aluminium hydroxide solid, after washing, filtration, roasting, obtain alumina product, gained alumina product impurity chemical ingredients is: Fe
2O
3: 0.04%, SiO
2: 0.04%.
Embodiment 4
With coal gangue pulverizing and jevigating salic 38%, silicon-dioxide 46%, by the molecular ratio of the aluminum oxide in ammonium sulfate/coal gangue is 5 to join the ore deposit, 460 ℃ of sintering reaction temperature, reaction times is 3 hours, sintered clinker stripping under 95 ℃ condition, and the exsiccated ammonium alum solid that dissolution fluid obtains after crystallization re-uses ammonia and decomposes, obtain the aluminium hydroxide solid, after washing, filtration, roasting, obtain alumina product, gained alumina product impurity chemical ingredients is: Fe
2O
3: 0.05%, SiO
2: 0.05%.
Claims (9)
1. one kind is extracted method of alumina from flyash, it is characterized in that its method is to allocate ammonium sulfate into flyash to carry out sintering, the gained solid obtains the solution of sulfur acid aluminium ammonium after stripping, this solution obtains the solid exsiccated ammonium alum by the crystalline method, solid sulphuric acid aluminium ammonium and ammonia gas react obtain aluminium hydroxide and ammonium sulfate, by washing and filtering, obtain solid aluminium hydroxide, aluminium hydroxide can obtain alumina product after roasting; The ammonium sulfate that enters liquid phase continues to recycle after evaporation.
2. a kind of method of alumina of from flyash, extracting according to claim 1, it is characterized in that ammonium sulfate allocates flyash into and carry out the agglomerating ratio of components and count 3-12 with the molecular ratio of aluminum oxide in ammonium sulfate/flyash, sintering temperature is 240-900 ℃, and sintering reaction is 0.1～5 hour.
3. a kind of method of alumina of extracting from flyash according to claim 1 is characterized in that water normal pressure stripping sintered clinker, and the solid phase residue adopts filtration or settlement separate after the stripping.
4. a kind of method of alumina of extracting from flyash according to claim 1 is characterized in that the washing water stripping sintered clinker of solid phase residue after water or the stripping.
5. a kind of method of alumina of from flyash, extracting according to claim 1, it is characterized in that the solution for the sulfur acid aluminium ammonium that obtains after the sintered clinker stripping, is to obtain the solid exsiccated ammonium alum by the method for evaporative crystallization or the method for cooling post crystallization.
6. a kind of method of alumina of from flyash, extracting according to claim 1, the solid phase exsiccated ammonium alum reaction that it is characterized in that logical ammonia and obtain is decomposed the solid phase exsiccated ammonium alum and is generated aluminium hydroxide; Obtain aluminium hydroxide through washing, obtain aluminum oxide after the roasting, the liquid phase behind the washing aluminium hydroxide is through evaporation, and the ammonium sulfate that obtains returns the sintering circuit batching.
7. a kind of method of alumina of extracting from flyash according to claim 1 is characterized in that the sintering circuit of the ammonia of its solid phase exsiccated ammonium alum decomposition course use from ammonium sulfate and flyash.
8. a kind of method of alumina of extracting from flyash according to claim 1 is characterized in that extracting that the main component of residue is SiO behind the aluminum oxide
2, be used to produce white carbon black or structure material etc.
9. a kind of method of alumina of extracting from flyash according to claim 1 is characterized in that used raw material is a coal gangue.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007101186794A CN100572279C (en) | 2007-07-12 | 2007-07-12 | A kind of method of alumina of from flyash, extracting |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007101186794A CN100572279C (en) | 2007-07-12 | 2007-07-12 | A kind of method of alumina of from flyash, extracting |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101117228A true CN101117228A (en) | 2008-02-06 |
| CN100572279C CN100572279C (en) | 2009-12-23 |
Family
ID=39053519
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2007101186794A Active CN100572279C (en) | 2007-07-12 | 2007-07-12 | A kind of method of alumina of from flyash, extracting |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100572279C (en) |
Cited By (19)
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| CN102275964A (en) * | 2011-07-25 | 2011-12-14 | 北京世纪地和科技有限公司 | Method for extracting high-purity superfine aluminum oxide from coal ash |
| CN102344155A (en) * | 2010-07-30 | 2012-02-08 | 沈阳铝镁设计研究院有限公司 | Method for preparing alumina from fly ash |
| CN102351251A (en) * | 2011-07-25 | 2012-02-15 | 北京世纪地和科技有限公司 | Method for extracting ferrotitanium from aluminum oxide dissolution liquid extracted by low-temperature ammonium process |
| CN102358623A (en) * | 2011-09-24 | 2012-02-22 | 沈阳铝镁设计研究院有限公司 | Method for producing aluminum oxide by treating fly ash through ammonia process |
| CN102381723A (en) * | 2011-07-25 | 2012-03-21 | 北京世纪地和科技有限公司 | Method for extracting aluminium oxide from pulverized fuel ash |
| CN102424412A (en) * | 2011-09-24 | 2012-04-25 | 沈阳铝镁设计研究院有限公司 | Method of producing alumina from fly ash |
| CN102689915A (en) * | 2012-06-06 | 2012-09-26 | 清华大学 | Process method for producing high-purity aluminum oxide and co-producing silicate from coal ash |
| CN102120600B (en) * | 2010-01-08 | 2012-11-07 | 北京世纪地和科技有限公司 | Method for purifying aluminum ammonium sulfate |
| CN102120593B (en) * | 2010-01-08 | 2012-11-07 | 北京世纪地和科技有限公司 | Method for extracting aluminum oxide from pulverized flue ash |
| CN103086412A (en) * | 2013-02-28 | 2013-05-08 | 山东科院天力节能工程有限公司 | Method for extracting alumina through coal ash |
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| CN104860338A (en) * | 2014-02-20 | 2015-08-26 | 中国科学院过程工程研究所 | Method for extracting alumina from fly ash through sulfo ammonium salt mixing medium system |
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|---|---|---|---|---|
| ES482881A1 (en) * | 1979-07-27 | 1980-04-01 | Consejo Superior Investigacion | A method of obtaining alumina from clay and other alumino-silicates and alumina obtained by this method. |
| CN100457628C (en) * | 2006-06-02 | 2009-02-04 | 李禹� | Method of extracting aluminium oxide from fly ash and simultaneously producing white carbon black |
| CN100410174C (en) * | 2006-08-29 | 2008-08-13 | 神华准格尔能源有限责任公司 | Preparation method of alumina |
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2007
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| CN102120593B (en) * | 2010-01-08 | 2012-11-07 | 北京世纪地和科技有限公司 | Method for extracting aluminum oxide from pulverized flue ash |
| CN102344155A (en) * | 2010-07-30 | 2012-02-08 | 沈阳铝镁设计研究院有限公司 | Method for preparing alumina from fly ash |
| CN102381723A (en) * | 2011-07-25 | 2012-03-21 | 北京世纪地和科技有限公司 | Method for extracting aluminium oxide from pulverized fuel ash |
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