CN1792802A - Process for extracting aluminium hydroxide from flyash - Google Patents
Process for extracting aluminium hydroxide from flyash Download PDFInfo
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- CN1792802A CN1792802A CN 200510048274 CN200510048274A CN1792802A CN 1792802 A CN1792802 A CN 1792802A CN 200510048274 CN200510048274 CN 200510048274 CN 200510048274 A CN200510048274 A CN 200510048274A CN 1792802 A CN1792802 A CN 1792802A
- Authority
- CN
- China
- Prior art keywords
- flyash
- extracting
- aluminium
- filter residue
- alumina
- Prior art date
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- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000010881 fly ash Substances 0.000 title claims description 47
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 title claims description 12
- 229910021502 aluminium hydroxide Inorganic materials 0.000 title claims description 6
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims abstract description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 13
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims abstract description 13
- 238000001354 calcination Methods 0.000 claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000013078 crystal Substances 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 37
- 239000002253 acid Substances 0.000 claims description 33
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 17
- 229910052782 aluminium Inorganic materials 0.000 claims description 17
- 239000004411 aluminium Substances 0.000 claims description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 239000000706 filtrate Substances 0.000 claims description 12
- 238000002425 crystallisation Methods 0.000 claims description 9
- 230000008025 crystallization Effects 0.000 claims description 9
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 claims description 6
- 239000003546 flue gas Substances 0.000 claims description 6
- 239000000376 reactant Substances 0.000 claims description 6
- 229910001388 sodium aluminate Inorganic materials 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 5
- 230000008020 evaporation Effects 0.000 claims description 5
- 230000018044 dehydration Effects 0.000 claims description 4
- 238000006297 dehydration reaction Methods 0.000 claims description 4
- 238000001994 activation Methods 0.000 claims description 2
- 230000004913 activation Effects 0.000 claims description 2
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 claims 1
- 238000001816 cooling Methods 0.000 abstract description 4
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000010883 coal ash Substances 0.000 abstract description 3
- 238000009835 boiling Methods 0.000 abstract 1
- 238000000227 grinding Methods 0.000 abstract 1
- 238000002156 mixing Methods 0.000 abstract 1
- 235000011149 sulphuric acid Nutrition 0.000 abstract 1
- 229910003158 γ-Al2O3 Inorganic materials 0.000 abstract 1
- 238000010792 warming Methods 0.000 description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 8
- 239000000284 extract Substances 0.000 description 7
- 239000007787 solid Substances 0.000 description 7
- 239000004568 cement Substances 0.000 description 6
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 229910052742 iron Inorganic materials 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- 208000005156 Dehydration Diseases 0.000 description 3
- 230000003213 activating effect Effects 0.000 description 3
- 239000006184 cosolvent Substances 0.000 description 3
- 238000004090 dissolution Methods 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000005245 sintering Methods 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000010306 acid treatment Methods 0.000 description 2
- 159000000013 aluminium salts Chemical class 0.000 description 2
- 229910000329 aluminium sulfate Inorganic materials 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 239000006210 lotion Substances 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 238000007885 magnetic separation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 229910004261 CaF 2 Inorganic materials 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 230000000536 complexating effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000004567 concrete Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000012633 leachable Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
Landscapes
- Processing Of Solid Wastes (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
A process for extracting aluminum oxide from powdered coal ash includes such steps as grinding, calcining, mixing with H2SO4 solution, heating while reaction for extracting aluminum oxide, boiling in water, concentrating, cooling while educing out aluminum sulfate crystals, heating for dewatering, heating for decomposing to obtain gamma-Al2O3, and further preparing metallurgy-class aluminum oxide.
Description
Affiliated technical field
The invention belongs to the comprehensive utilization that becomes more meticulous of flyash, specifically relate to a kind of method of alumina of from flyash, extracting.
Background technology
A large amount of flyash of coal-burning power plant's discharging have caused serious pollution to agricultural production and living environment on every side, and comprehensive regulation flyash has become the environmental problem that an exigence solves.In China, the flyash amount of the annual discharging in coal-burning power plant is up to more than one hundred million tons, and volume of cargo in storage is very big.Al in the flyash
2O
3Content is higher, is about 20～40%, because volume of cargo in storage is big, is one and has the resource treasure-house that the comprehensive development and utilization that becomes more meticulous is worth.
From flyash, extract Al both at home and abroad
2O
3Method can be divided into alkaline process and acid system two big classes.In the sixties in last century, Poland just utilizes soda lime sintering process to extract Al in flyash
2O
3, built up and produced 5000 tons of Al per year
2O
3And the pilot plant of 350,000 tons of cement.China Anhui Province Institute of Metallurgical Technology and Hefei cement research institute have declared with limestone sintering, sodium carbonate stripping in the eighties and extracted Al in flyash
2O
3, residue is for the production of the achievement of cement, in March nineteen eighty-two by expert appraisal.The soda lime sintering process of building materials research institute of Ningxia autonomous region research extracts Al in flyash
2O
3, residue produce cement industry in September, 1987 by the Ningxia State Scientific and Technological Commission of autonomous region tissue characterization.In December, 2004, Inner Mongolia Autonomous Region Science and Technology Department has held " flyash extracts the aluminum and coproducing cement industrialization technology " the project appraisal of scientific and technological achievements meeting of covering the research and development of western new and high technology Group Co.,Ltd, and this group has independently finished nearly 5000 tonnes pilot scale.Although extract Al about alkaline process
2O
3Report a lot, adopt above-mentioned process half industrialization and industrialization quantity-produced report but have not yet to see.Its reason is to handle the numerous length of technology that this high silicon contains the aluminium powder coal ash with alkaline process, the inventory of running is big, facility investment is also big, the energy consumption height, the cost height, and also the level of residue that produces is the several times of flyash amount, limited with a large amount of cement market goods locallies that residue is made, overall economic efficiency is poor, and level of comprehensive utilization is low, thereby has hindered the application of alkaline process aspect comprehensive utilization flyash.
Compare with alkaline process, come treated coal ash just to have obvious advantage with acid system.Acid system when the aluminum oxide that effectively extracts in the flyash, silica all can be refused outside liquid, can not produce new solid material in process of production, level of residue is little, thereby the inventory of running is little, equipment investment is little, energy consumption is low, product cost is also low.But the shortcoming of acid system is in leaching during aluminum oxide, has also brought into solution such as the many leachable impurity in the flyash such as iron, titanium, magnesium, must increase the postorder treatment process; The conversion unit manufacturing of Shi Yonging has certain degree of difficulty besides.But compare with alkaline process, use still the most promising method of acid treatment fly ash, therefore, the research of carrying out this respect both at home and abroad is more.
Extract aluminium oxide with acid treatment flyash and mostly adopt sulfuric acid or saline and alkaline technology.Because flyash is the tiny grit that forms through after high temperature (1500 ℃) burning, the glassy phase in the grit accounts for more than 90%, has had a strong impact on the activity of flyash and acid reaction, therefore, need to improve the reactivity of flyash and acid to improve Al
2O
3Dissolution rate.The more practice of data report is to add cosolvent NH in the acidleach negate is answered
4F and CaF
2, by the complexing Si oxide, make Al thereby reach
2O
3The purpose of stripping.Adopt said method in flyash, to reclaim Al
2O
3, Al
2O
3Dissolution rate all lower, generally only have 35～45%, resource utilization is low, and because having added the fluorine element that environment is had pollution, has brought secondary pollution, has hindered the development and use that become more meticulous of flyash.
Summary of the invention
The purpose of this invention is to provide a kind of method of extracting aluminium oxide from flyash, this method adopts sulfuric acid high temperature to leach aluminium oxide under normal pressure, does not add any cosolvent, the rate of recovery height of aluminium oxide.
The present invention extracts aluminum oxide from flyash concrete grammar comprises:
Flyash is ground to 200～400 orders, in 300～760 ℃ of calcination activations 1～1.5 hour;
Flyash after the roasting and 60%～98% H
2SO
4Weight ratio according to 1: 1～6 is mixed, and is heated to 160～330 ℃ of reactions 1～1.5 hour, filters spent acid is separated with the filter residue that contains reactant;
The water that adds 2.5～5 times of amounts in the filter residue boiled under 65～90 ℃ molten 30～45 minutes, and the stripping reactant removes by filter residue, and filtrate concentrates postcooling, separates out the Tai-Ace S 150 crystallization;
Tai-Ace S 150 heats up to dewater and obtains anhydrous slufuric acid aluminium;
Continue to heat up and make the decomposition of anhydrous slufuric acid aluminium obtain γ-Al
2O
3, and reclaim SO
3Flue gas.
Filtration temperature when wherein, spent acid being separated with the filter residue that contains reactant is selected 100～180 ℃.
The present invention carries out the processing of distinct methods to concentrating the aluminum sulfate crystallization of separating out after the cooling, can produce aluminium salt and the aluminum oxide of many kinds, specifically:
The Tai-Ace S 150 crystallization being no more than dehydration fully under 400 ℃ the temperature, is generated anhydrous slufuric acid aluminium.
In calcining below 900 ℃, aluminum sulfate is decomposed fully in anhydrous slufuric acid aluminium, all generate active strong γ-Al
2O
3
γ-the Al for preparing
2O
3Boil moltenly at 120～190 ℃ of lower NaOH solution with 150g/L～200g/L, make sodium aluminate solution.Owing to the impurity such as iron contained in the aluminium oxide, calcium, magnesium can not be dissolved by alkali, be present in the solid phase, can remove by filter, after the Separation of Solid and Liquid, form the high sodium aluminate solution of purity.Add aluminium hydroxide crystal seed in solution, the sodium aluminate in the solution is separated out with the form crystallization of aluminium hydroxide, the crystalline aluminum hydroxide that obtains can obtain metallurgical-grade aluminum oxide at 1100 ℃ of temperature lower calcinations.
Anhydrous slufuric acid aluminium decomposes preparation γ-Al
2O
3The time SO that produces
3Flue gas directly passes in the spent acid that filters to isolate and produces sulfuric acid, produces the leaching that the sulfuric acid that obtains is used further to aluminium oxide in the flyash, realizes recycling of sulfate system.
The present invention adopts new flyash activating technology, does not use any cosolvent at normal pressure, with sulfuric acid the aluminium oxide in the flyash is effectively leached, and the dissolution rate of aluminium oxide can reach more than 85%.
Any waste water, waste liquid, waste residue and obnoxious flavour are not discharged in all effectively recycles such as the spent acid that produces in the technical process of the present invention, waste water in the whole process.
The present invention adopts different processing methods, the alumina preparation that leaches from flyash can be become aluminium salt and the aluminum oxide of many kinds.
Technological process of the present invention is simple, invests for a short time, and cost is low, and the added value of product height is a flyash that has the prospect comprehensive utilization industrialization method that becomes more meticulous.
Embodiment
Embodiment 1
Get salic 40% flyash 1t, grind to form 300 purpose fine powders, behind the iron removal by magnetic separation,, obtain activatory flyash in 400 ℃ of following roasting 1.5h.
The H of adding 72% in activating fly ash
2SO
44t is warming up to 300 ℃ and leaches reaction 1h, and aluminum oxide is fully leached, and reacting rear material is used further to after the spent acid that filters out reclaims leach operation next time 150 ℃ of solid-liquid separation, recycles.
Add 4t water in solid slag, be warming up to 80 ℃ and boil molten 40min, filter, filter residue washes with water 2 times, the reverse use of washing lotion.
With the filtrate evaporation concentration, return the stripping operation behind the water vapor condensation that steams, separate out the Tai-Ace S 150 crystallization after the concentrated solution cooling, filter, collect solid crystal 2200Kg.The filtrate evaporation concentration is returned the stripping operation behind the water vapor condensation, concentrated solution returns and leaches the use that is mixed of operation and concentrated acid.
The Tai-Ace S 150 solid crystal that obtains is warming up to 350 ℃ of dehydrations gradually, obtains 1500Kg anhydrous slufuric acid aluminium, returns the stripping operation behind the water vapor condensation of generation.
Anhydrous slufuric acid aluminium continues to be warming up to 453 ℃ and begins to decompose, heating direct to 870 ℃ again, and calcining 6h decomposes anhydrous slufuric acid aluminium fully, generates 350Kg γ-Al
2O
3, the SO that calcining produces
3Flue gas is passed in the spent acid for the production of H
2SO
4
γ-Al
2O
3Join in the NaOH solution of 150g/L, be warming up to 150 ℃ and boil moltenly, remove by filter residue, add a small amount of aluminium hydroxide crystal seed in the filtrate, the sodium aluminate in the filtrate is separated out with the form of crystalline aluminum hydroxide, filter, filtrate cycle is used.
The crystalline aluminum hydroxide that obtains is warming up to 1100 ℃ of calcinings obtains the 350Kg metallurgical-grade aluminum oxide.
Embodiment 2
Get salic 40% flyash 1t, grind to form 200 purpose fine powders, behind the iron removal by magnetic separation,, obtain activatory flyash in 600 ℃ of following roasting 1h.
The H of adding 98% in activating fly ash
2SO
42t is warming up to 250 ℃ and leaches reaction 1.5h, and aluminum oxide is fully leached, and reacting rear material is used further to after the spent acid that filters out reclaims leach operation next time 180 ℃ of solid-liquid separation, recycles.
Add 6t water in solid slag, be warming up to 75 ℃ and boil molten 45min, filter, filter residue washes with water 2 times, the reverse use of washing lotion.
With the filtrate evaporation concentration, return the stripping operation behind the water vapor condensation that steams, separate out the Tai-Ace S 150 crystallization after the concentrated solution cooling, filter, collect solid crystal 2200Kg.The filtrate evaporation concentration is returned the stripping operation behind the water vapor condensation, concentrated solution returns and leaches the use that is mixed of operation and concentrated acid.
The Tai-Ace S 150 solid crystal that obtains is warming up to 400 ℃ of dehydrations gradually, obtains 1480Kg anhydrous slufuric acid aluminium, returns the stripping operation behind the water vapor condensation of generation.
Anhydrous slufuric acid aluminium continues to be warming up to 850 ℃, and calcining 8h decomposes anhydrous slufuric acid aluminium fully, generates 350Kg γ-Al
2O
3, the SO that calcining produces
3Flue gas is passed in the spent acid for the production of H
2SO
4
γ-Al
2O
3Join in the NaOH solution of 150g/L, be warming up to 150 ℃ and boil moltenly, remove by filter residue, add a small amount of aluminium hydroxide crystal seed in the filtrate, the sodium aluminate in the filtrate is separated out with the form of crystalline aluminum hydroxide, filter, filtrate cycle is used.
The crystalline aluminum hydroxide that obtains is warming up to 1100 ℃ of calcinings obtains the 350Kg metallurgical-grade aluminum oxide.
Claims (6)
1, a kind of method of alumina of extracting from flyash comprises:
Flyash is ground to 200～400 orders, in 300～760 ℃ of calcination activations 1～1.5 hour;
Flyash after the roasting and 60%～98% H
2SO
4Weight ratio according to 1: 1～6 is mixed, and is heated to 160～330 ℃ of reactions 1～1.5 hour, filters spent acid is separated with the filter residue that contains reactant;
The water that adds 2.5～5 times of amounts in the filter residue boiled under 65～90 ℃ molten 30～45 minutes, and the stripping reactant removes by filter residue, and filtrate evaporation concentration postcooling is separated out the Tai-Ace S 150 crystallization;
The Tai-Ace S 150 crystallization heats up to dewater and obtains anhydrous slufuric acid aluminium;
Continue to heat up and make the decomposition of anhydrous slufuric acid aluminium obtain γ-Al
2O
3, and reclaim SO
3Flue gas.
2, according to the described method of alumina of from flyash, extracting of claim 1, it is characterized in that, spent acid is separated with the filter residue that contains reactant 100～180 ℃ of filtrations.
3, the method for alumina of extracting from flyash according to claim 1 is characterized in that dehydration generates anhydrous slufuric acid aluminium under 400 ℃ the temperature being no more than with the Tai-Ace S 150 crystallization.
4, the method for extracting aluminium oxide from flyash according to claim 1 is characterized in that anhydrous slufuric acid aluminium is prepared γ-Al at the temperature lower calcination that is no more than 900 ℃
2O
3
5, the method for alumina of extracting from flyash according to claim 1 is characterized in that the SO that reclaims
3Flue gas is produced the vitriol oil with sulfuric acid absorption.
6, the method for extracting aluminium oxide from flyash according to claim 1 is characterized in that the γ-Al for preparing
2O
3Can also boil at 120～190 ℃ of lower NaOH solution with 150g/L～200g/L moltenly, make sodium aluminate solution, remove by filter residue after, the adding aluminium hydroxide crystal seed makes solution separate out crystalline aluminum hydroxide, prepares metallurgical-grade aluminum oxide at 1100 ℃ of temperature lower calcinations.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100482749A CN1329301C (en) | 2005-12-31 | 2005-12-31 | Process for extracting aluminium hydroxide from flyash |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100482749A CN1329301C (en) | 2005-12-31 | 2005-12-31 | Process for extracting aluminium hydroxide from flyash |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1792802A true CN1792802A (en) | 2006-06-28 |
| CN1329301C CN1329301C (en) | 2007-08-01 |
Family
ID=36804475
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100482749A Expired - Fee Related CN1329301C (en) | 2005-12-31 | 2005-12-31 | Process for extracting aluminium hydroxide from flyash |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1329301C (en) |
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404423C (en) * | 2006-09-15 | 2008-07-23 | 平朔煤炭工业公司 | Method for preparing alumina from fly ash |
| CN100410174C (en) * | 2006-08-29 | 2008-08-13 | 神华准格尔能源有限责任公司 | Method for preparing aluminum oxide |
| CN100413981C (en) * | 2006-09-14 | 2008-08-27 | 北京矿冶研究总院 | Method for extracting aluminum from high-silicon aluminum-containing mineral raw material by acid process |
| CN101254933B (en) * | 2008-04-02 | 2010-06-23 | 潘爱芳 | Method for extracting high-purity alumina and silica gel from coal ash |
| CN101306826B (en) * | 2008-06-20 | 2011-05-25 | 北京世纪地和科技有限公司 | Process for extracting metallurgy-level aluminum oxide from fly ash or slag |
| CN102557091A (en) * | 2011-12-30 | 2012-07-11 | 西安航天科技工业公司 | Method for subsequent treatment of aluminum sulfate generated in technical process of extracting alumina from fly ash |
| CN101327944B (en) * | 2008-07-16 | 2012-11-28 | 孙志昂 | Production process for preparing superfine crystal alpha-aluminum oxide by directly using aluminum sulfate |
| DE112011101459T5 (en) | 2010-04-27 | 2013-03-07 | China Shenhua Energy Company Limited | A method of providing metallurgical grade aluminum using fluid bed ash |
| CN103042160A (en) * | 2012-12-25 | 2013-04-17 | 马鞍山市万鑫铸造有限公司 | Zircon sand contained moulding sand and preparation method thereof |
| CN103042156A (en) * | 2012-12-25 | 2013-04-17 | 马鞍山市万鑫铸造有限公司 | Bauxite contained moulding sand and preparation method thereof |
| CN103042158A (en) * | 2012-12-25 | 2013-04-17 | 马鞍山市万鑫铸造有限公司 | High crush-resistance moulding sand and preparation method thereof |
| CN103305686A (en) * | 2013-05-30 | 2013-09-18 | 华东理工大学 | Method for realizing separation of aluminium, iron and calcium by activating coal gasification ash |
| CN103738972A (en) * | 2013-12-27 | 2014-04-23 | 中国神华能源股份有限公司 | Method for preparing silicon micropowder by using pulverized fuel ash aluminum extraction residues |
| CN104445308A (en) * | 2013-09-16 | 2015-03-25 | 贵阳铝镁设计研究院有限公司 | Method for extracting alumina from fly ash in circulating fluidized bed |
| CN104591244A (en) * | 2014-12-23 | 2015-05-06 | 贵州师范大学 | Method for extracting high-purity aluminum oxide by adsorbing impurities with molecular sieve |
| CN104591245A (en) * | 2014-12-23 | 2015-05-06 | 贵州师范大学 | Method for extracting high-purity alumina by adsorbing impurities with activated carbon |
| CN104591239A (en) * | 2014-12-23 | 2015-05-06 | 贵州师范大学 | Method for extracting high-purity aluminum oxide from bauxite |
| CN104831074A (en) * | 2015-05-19 | 2015-08-12 | 河北工程大学 | Method for extracting aluminum from fly ash |
| US9517965B2 (en) | 2012-11-27 | 2016-12-13 | National Institute Of Clean-And-Low-Carbon Energy | Method for preparing a soda-lime-silica glass basic formulation and a method for extracting aluminum from coal ash for co-production of glass |
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| JPS59227760A (en) * | 1983-06-08 | 1984-12-21 | 富士不燃建材工業株式会社 | Manufacture of hardened body from such as blast furnace slag |
| CN1003277B (en) * | 1986-12-29 | 1989-02-15 | 陕西省农垦科技教育中心 | Three-line Hybrid Seed Production Technology of Brassica napus |
| WO1989004811A1 (en) * | 1987-11-24 | 1989-06-01 | Northern States Power Company | Method for the processing of fly ash, scrubber sludge and the like; and products recovered therefrom |
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| CN1059880C (en) * | 1995-10-24 | 2000-12-27 | 何志强 | Treatment of flyash |
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