CN104250016A - Method for preparation of alumina by use of ammonia gas for decomposition of aluminum sulfate solution - Google Patents
Method for preparation of alumina by use of ammonia gas for decomposition of aluminum sulfate solution Download PDFInfo
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- CN104250016A CN104250016A CN201310260605.XA CN201310260605A CN104250016A CN 104250016 A CN104250016 A CN 104250016A CN 201310260605 A CN201310260605 A CN 201310260605A CN 104250016 A CN104250016 A CN 104250016A
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- ammonia
- aluminum oxide
- decomposition
- aluminium hydroxide
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 132
- 238000000034 method Methods 0.000 title claims abstract description 61
- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 26
- 238000002360 preparation method Methods 0.000 title claims abstract description 6
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical group [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 title abstract description 9
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title abstract description 7
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 63
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims abstract description 47
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000010881 fly ash Substances 0.000 claims abstract description 29
- 239000013078 crystal Substances 0.000 claims abstract description 19
- 229910052742 iron Inorganic materials 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052598 goethite Inorganic materials 0.000 claims abstract description 10
- AEIXRCIKZIZYPM-UHFFFAOYSA-M hydroxy(oxo)iron Chemical compound [O][Fe]O AEIXRCIKZIZYPM-UHFFFAOYSA-M 0.000 claims abstract description 10
- 238000001354 calcination Methods 0.000 claims abstract description 7
- -1 iron ions Chemical class 0.000 claims abstract description 3
- 229910021502 aluminium hydroxide Inorganic materials 0.000 claims description 43
- 229940037003 alum Drugs 0.000 claims description 36
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 28
- 239000007787 solid Substances 0.000 claims description 14
- 238000003756 stirring Methods 0.000 claims description 14
- 239000012065 filter cake Substances 0.000 claims description 12
- 239000000047 product Substances 0.000 claims description 12
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 9
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 9
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 9
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 9
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 9
- 235000011124 aluminium ammonium sulphate Nutrition 0.000 claims description 8
- FOJJCOHOLNJIHE-UHFFFAOYSA-N aluminum;azane Chemical compound N.[Al+3] FOJJCOHOLNJIHE-UHFFFAOYSA-N 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 8
- 230000003292 diminished effect Effects 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 9
- 238000000926 separation method Methods 0.000 abstract description 2
- 230000001105 regulatory effect Effects 0.000 abstract 3
- 229910001570 bauxite Inorganic materials 0.000 description 7
- 238000011085 pressure filtration Methods 0.000 description 5
- 238000005245 sintering Methods 0.000 description 5
- 239000002893 slag Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000378 calcium silicate Substances 0.000 description 1
- 229910052918 calcium silicate Inorganic materials 0.000 description 1
- OYACROKNLOSFPA-UHFFFAOYSA-N calcium;dioxido(oxo)silane Chemical compound [Ca+2].[O-][Si]([O-])=O OYACROKNLOSFPA-UHFFFAOYSA-N 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention relates to a method for preparation of alumina, and in particular relates to a method for preparation of the alumina by use of ammonia gas for decomposition of aluminum sulfate solution; the method includes the following steps: a product obtained by ammonia method calcination of fly ash is leached with water at 60 to 95 DEG C and separated; iron ions in the solution are removed by goethite method; ammonia gas produced by calcination is used for decomposition of the aluminum sulfate solution, the ammonia gas is used for pH regulating of a pre-stage solution; a crystal seed is added; pH regulating of a secondary-stage solution is performed; terminal point pH regulating is performed; after remaining, aluminum hydroxide is obtained; and metallurgical grade alumina is obtained by calcinations of the prepared aluminum hydroxide. The method has the advantages that: the ammonia gas produced by calcination is used for decomposition of the de-ironed liquid, so that the ammonia gas produced by the whole ammonia method calcination process can be recycled, the aluminum hydroxide produced by decomposition is easy in solid-liquid separation, process is simple, and industrialization is facilitated.
Description
Technical field
The present invention is a kind of method of aluminum oxide, particularly relates to a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide.
Background technology
Flyash is the solid waste that coal-burning power plant discharges.At present, the more than one hundred million ton of China's flyash annual emissions, total volume of cargo in storage of China's flyash has tens00000000 tons.A large amount of soil is is not only occupied in the discharge of a large amount of flyash, and serious environment pollution, constitutes the dual destruction to ecosystem environment.Therefore the comprehensive utilization carrying out flyash has Great significance and long-range strategic importance.Equally, China is the country that a bauxite resource is not rich in, and bauxite can not meet the following demand to mineral products.By the rate of growth of current aluminum oxide output and bauxite exploitation, utilize in waste, even if consider prospective reserves, the guarantee time limit of the bauxite of China is also difficult to reach 50 years.So the method solving this crisis of resource has two kinds: one to be the existing bauxite resource of Appropriate application, prolongs length of service; Two is actively look for and utilize other to contain bauxite resource.And aluminum oxide is one of main component of flyash, the alumina content in some local flyash can reach 40% ~ 50%, has and can extract economic worth.Therefore, carry out the pollution that the research work of extracting aluminum oxide from flyash both can solve flyash, bauxite resource shortage problem can be alleviated again.
At present, that from flyash, extracts the research comparative maturity of aluminum oxide has limestone sintering process and soda-lime sintering process, is commonly referred to as alkaline process both this.In this alkalinity extraction flyash also there are some problems in aluminum oxide, the calcium silicate slag that sintering process produces, and can only be used as cement raw material, and the quantity of slag produced is larger, can cause more pollution; The facility investment of sintering process treated coal ash is large, and energy consumption is high, and cost is high.Have now Some Enterprises to adopt sulfuric acid process and hydrochloric acid method, these two kinds of methods require high to the erosion resistance of equipment, the large and poor reliability of facility investment; And only having ammonium sulfate sintering process preparation process to be decrement process, the quantity of slag is little; Reaction system is weak acid system, and equipment is easier to solve, and is beneficial to industrialization.
The mixing grog that ammonium sulfate mixes with flyash, compressing tablet, roasting obtain Tai-Ace S 150, ferric sulfate, grog obtains the alum liquor containing a small amount of ferric sulfate after leaching, adopt iron ore method to enter and deironing is carried out to solution, obtain iron content at the comparatively pure alum liquor of below 20mg/L.Adopt ammonia to decompose and obtain aluminium hydroxide, in order to last roasting obtains the larger alumina product of granularity, the process of decomposing alum liquor just seems particularly important, and ammonia passes into too fast easy generation colloid, not easily separated, and the alumina product of back is had a great impact.Therefore a kind of suitable decomposition method is invented very important.
Summary of the invention
In order to solve the problem, the invention provides a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide, object to make the aluminum hydroxide particles of decomposition comparatively large, and water ratio is low, is easy to be separated.
A kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide of the present invention, comprises the steps: that the products in water roasting of flyash ammonia process obtained leaches and is separated at 60 ~ 95 DEG C for achieving the above object; Adopt the iron ion in goethite process removing solution; The ammonia produced with roasting decomposes alum liquor, carries out the adjustment of pH value of solution in early stage with ammonia; Add crystal seed; Carry out the adjustment of two sections of pH value of solution; Then the adjustment of endpoint pH is carried out; Aluminium hydroxide is obtained after stop; The aluminium hydroxide of preparation carries out calcining and obtains metallurgical-grade aluminum oxide.
The roasting of flyash ammonia process and stripping are after being mixed with ammonium sulfate by flyash, be 300 ~ 570 DEG C in temperature and carry out roasting, leach than for 2:1 ~ 4:1 by water and sintered product at 60 ~ 95 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in goethite process removing solution at 60 DEG C ~ 90 DEG C, obtain the alum liquor of iron concentration at below 20mg/L.
Described early stage, the adjustment of pH value of solution was at 70 ~ 95 DEG C, with ammonia in 40 ~ 60min regulator solution pH value to 2 ~ 2.8, and to stir under stir speed (S.S.) is 300 ~ 400r/min.
The described crystal seed that adds adds aluminium hydroxide crystal seed in the solution to make the solid containing reaching 130 ~ 200g/L of solution.
Being adjusted to of described two sections of pH value of solution to add after crystal seed through 30 ~ 50min, continues to pass into ammonia in solution, makes the pH value of solution reach 3.5 ~ 4.5 at 60 ~ 90min and stop logical ammonia, the solid now generated in solution some be aluminium ammonium alum.
The described adjustment carrying out endpoint pH continues to pass into ammonia to solution for continuous through 30 ~ 60min after the adjustment of two sections of pH value of solution, makes solution reach endpoint pH 5.5 ~ 5.8 at 20 ~ 40min.
Obtaining aluminium hydroxide after described stop is stop 3 ~ 5h, and adopt pressurization or filtration under diminished pressure to obtain aluminium hydroxide, rate of decomposition more than 98%, filter cake moisture content is 15% ~ 25%, and aluminium hydroxide particle diameter 40 ~ 60 μm accounts for 75% ~ 85%.
Described aluminium hydroxide is calcined at 1000 DEG C ~ 1200 DEG C, obtains metallurgical-grade aluminum oxide.
Advantageous effect of the present invention: the present invention adopts the ammonia produced in roasting process to decompose deironing liquid, the ammonia recycle produced in whole ammonia process roasting process can be made to utilize, and decompose the aluminium hydroxide generated and be easy to solid-liquid separation, technique is simple, is beneficial to industrialization.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
1, ammonia process roasting; 2, leaching, deironing; 3, ammonia decomposes; 4, aluminium ammonium alum and aluminium hydroxide; 5, ammonia; 6, aluminium hydroxide; 7, calcine; 8, aluminum oxide.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in detail, but protection scope of the present invention not limit by schematic diagram.
embodiment 1
The roasting of flyash ammonia process and stripping are after being mixed with ammonium sulfate by flyash, be 450 DEG C in temperature and carry out roasting, leach than for 3:1 by water and sintered product at 80 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in goethite process removing solution at 70 DEG C, obtaining iron concentration in 18mg/L Tai-Ace S 150 concentration is the alum liquor of 190g/L, alum liquor pH value is 1.4, measure the deironing liquid of 800ml, at 75 DEG C early stage pH value of solution adjustment, with ammonia in 45min regulator solution pH value to 2.2, and stir under stir speed (S.S.) is 350r/min, add 160g aluminium hydroxide crystal seed and make the solid containing reaching 180g/L of solution.
To add after crystal seed through 35min, continue to pass into ammonia in solution, make the pH value of solution reach 3.8 stoppings at 70min and lead to ammonia, the solid now generated in solution some be aluminium ammonium alum.
Continue to pass into ammonia to solution for continuous through 40min after the adjustment of two sections of pH value of solution, make solution reach endpoint pH 5.6 at 25min.
Obtain aluminium hydroxide after described stop for stopping 3.5h, adopt pressure filtration to obtain aluminium hydroxide, disengaging time is 52 seconds, and filter cake thickness is 8.2mm, rate of decomposition 98%, and filter cake moisture content is 20%, and aluminium hydroxide particle diameter 40 ~ 60 μm accounts for 80%.
Aluminium hydroxide is calcined at 1100 DEG C, obtains metallurgical-grade aluminum oxide.
embodiment 2
The roasting of flyash ammonia process and stripping are after being mixed with ammonium sulfate by flyash, be 300 DEG C in temperature and carry out roasting, leach than for 4:1 by water and sintered product at 95 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in goethite process removing solution at 90 DEG C, obtaining iron concentration in 19mg/L Tai-Ace S 150 concentration is the alum liquor of 200g/L, alum liquor pH value is 1.6, measure the deironing liquid of 1000ml, at 95 DEG C early stage pH value of solution adjustment, with ammonia in 60min regulator solution pH value to 2.8, and stir under stir speed (S.S.) is 400r/min, add 150g aluminium hydroxide crystal seed and make the solid containing reaching 200g/L of solution.
To add after crystal seed through 50min, continue to pass into ammonia in solution, make the pH value of solution reach 4.5 stoppings at 90min and lead to ammonia, the solid now generated in solution some be aluminium ammonium alum.
Continue to pass into ammonia to solution for continuous through 60min after the adjustment of two sections of pH value of solution, make solution reach endpoint pH 5.8 at 40min.
Obtain aluminium hydroxide after described stop for stopping 5h, adopt pressure filtration to obtain aluminium hydroxide, disengaging time is 60 seconds, and filter cake thickness is 8.2mm, rate of decomposition 99%, and filter cake moisture content is 25%, and aluminium hydroxide particle diameter 40 ~ 60 μm accounts for 78%.
Aluminium hydroxide is calcined at 1200 DEG C, obtains metallurgical-grade aluminum oxide.
embodiment 3
The roasting of flyash ammonia process and stripping are after being mixed with ammonium sulfate by flyash, be 570 DEG C in temperature and carry out roasting, leach than for 2:1 by water and sintered product at 60 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in goethite process removing solution at 60 DEG C, obtaining iron concentration in 15mg/L Tai-Ace S 150 concentration is the alum liquor of 210g/L, alum liquor pH value is 1.3, measure the deironing liquid of 700ml, at 70 DEG C early stage pH value of solution adjustment, with ammonia in 45min regulator solution pH value to 2.7, and stir under stir speed (S.S.) is 300r/min, add 160g aluminium hydroxide crystal seed and make the solid containing reaching 130g/L of solution.
To add after crystal seed through 30min, continue to pass into ammonia in solution, make the pH value of solution reach 3.5 stoppings at 60min and lead to ammonia, the solid now generated in solution some be aluminium ammonium alum.
Continue to pass into ammonia to solution for continuous through 30min after the adjustment of two sections of pH value of solution, make solution reach endpoint pH 5.5 at 20min.
Obtain aluminium hydroxide after described stop for stopping 3h, adopt pressure filtration to obtain aluminium hydroxide, disengaging time is 50 seconds, and filter cake thickness is 8.2mm, rate of decomposition 98%, and filter cake moisture content is 15%, and aluminium hydroxide particle diameter 40 ~ 60 μm accounts for 85%.
Aluminium hydroxide is calcined at 1150 DEG C, obtains metallurgical-grade aluminum oxide.
embodiment 4
The roasting of flyash ammonia process and stripping are after being mixed with ammonium sulfate by flyash, be 500 DEG C in temperature and carry out roasting, leach than for 3:1 by water and sintered product at 70 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in goethite process removing solution at 70 DEG C, obtaining iron concentration in 18mg/L Tai-Ace S 150 concentration is the alum liquor of 190g/L, alum liquor pH value is 1.4, measure the deironing liquid of 800ml, at 80 DEG C early stage pH value of solution adjustment, with ammonia in 55min regulator solution pH value to 2.5, and stir under stir speed (S.S.) is 380r/min, add 160g aluminium hydroxide crystal seed and make the solid containing reaching 170g/L of solution.
To add after crystal seed through 40min, continue to pass into ammonia in solution, make the pH value of solution reach 3.9 stoppings at 75min and lead to ammonia, the solid now generated in solution some be aluminium ammonium alum.
Continue to pass into ammonia to solution for continuous through 50min after the adjustment of two sections of pH value of solution, make solution reach endpoint pH 5.6 at 30min.
Obtain aluminium hydroxide after described stop for stopping 4.5h, adopt pressure filtration to obtain aluminium hydroxide, disengaging time is 52 seconds, and filter cake thickness is 8.2mm, rate of decomposition 98%, and filter cake moisture content is 20%, and aluminium hydroxide particle diameter 40 ~ 60 μm accounts for 80%.
Aluminium hydroxide is calcined at 1100 DEG C, obtains metallurgical-grade aluminum oxide.
embodiment 5
The roasting of flyash ammonia process and stripping are after being mixed with ammonium sulfate by flyash, be 350 DEG C in temperature and carry out roasting, leach than for 3:1 by water and sintered product at 90 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in goethite process removing solution at 80 DEG C, obtaining iron concentration in 18mg/L Tai-Ace S 150 concentration is the alum liquor of 190g/L, alum liquor pH value is 1.6, measure the deironing liquid of 800ml, at 85 DEG C early stage pH value of solution adjustment, with ammonia in 50min regulator solution pH value to 2, and stir under stir speed (S.S.) is 320r/min, add 160g aluminium hydroxide crystal seed and make the solid containing reaching 150g/L of solution.
To add after crystal seed through 45min, continue to pass into ammonia in solution, make the pH value of solution reach 4.3 stoppings at 80min and lead to ammonia, the solid now generated in solution some be aluminium ammonium alum.
Continue to pass into ammonia to solution for continuous through 55min after the adjustment of two sections of pH value of solution, make solution reach endpoint pH 5.7 at 35min.
Obtain aluminium hydroxide after described stop for stopping 4h, adopt pressure filtration to obtain aluminium hydroxide, disengaging time is 52 seconds, and filter cake thickness is 8.2mm, rate of decomposition 98%, and filter cake moisture content is 20%, and aluminium hydroxide particle diameter 40 ~ 60 μm accounts for 75%.
Aluminium hydroxide is calcined at 1100 DEG C, obtains metallurgical-grade aluminum oxide.
Claims (8)
1. utilize ammonia decomposition alum liquor to prepare a method for aluminum oxide, it is characterized in that the products in water comprising the steps: the roasting of flyash ammonia process to obtain leaches and is separated at 60 ~ 95 DEG C; Adopt the iron ion in goethite process removing solution; The ammonia produced with roasting decomposes alum liquor, carries out the adjustment of pH value of solution in early stage with ammonia; Add crystal seed; Carry out the adjustment of two sections of pH value of solution; Then the adjustment of endpoint pH is carried out; Aluminium hydroxide is obtained after stop; The aluminium hydroxide of preparation carries out calcining and obtains metallurgical-grade aluminum oxide.
2. a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide according to claim 1, it is characterized in that the roasting of flyash ammonia process and stripping are after being mixed with ammonium sulfate by flyash, be 300 ~ 570 DEG C in temperature and carry out roasting, leach than for 2:1 ~ 4:1 by water and sintered product at 60 ~ 95 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in goethite process removing solution at 60 DEG C ~ 90 DEG C, obtain the alum liquor of iron concentration at below 20mg/L.
3. a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide according to claim 1, the adjustment that it is characterized in that pH value of solution in described early stage is at 70 ~ 95 DEG C, with ammonia in 40 ~ 60min regulator solution pH value to 2 ~ 2.8, and to stir under stir speed (S.S.) is 300 ~ 400r/min.
4. a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide according to claim 1, is characterized in that the described crystal seed that adds adds aluminium hydroxide crystal seed in the solution to make the solid containing reaching 130 ~ 200g/L of solution.
5. a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide according to claim 1, it is characterized in that being adjusted to of described two sections of pH value of solution adds after crystal seed through 30 ~ 50min, continue to pass into ammonia in solution, make the pH value of solution reach 3.5 ~ 4.5 at 60 ~ 90min and stop logical ammonia, the solid now generated in solution some be aluminium ammonium alum.
6. a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide according to claim 1, it is characterized in that the described adjustment carrying out endpoint pH continues to pass into ammonia to solution for continuous through 30 ~ 60min after the adjustment of two sections of pH value of solution, make solution reach endpoint pH 5.5 ~ 5.8 at 20 ~ 40min.
7. a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide according to claim 1, obtaining aluminium hydroxide after it is characterized in that described stop is stop 3 ~ 5h, pressurization or filtration under diminished pressure is adopted to obtain aluminium hydroxide, rate of decomposition more than 98%, filter cake moisture content is 15% ~ 25%, and aluminium hydroxide particle diameter 40 ~ 60 μm accounts for 75% ~ 85%.
8. a kind of method utilizing ammonia decomposition alum liquor to prepare aluminum oxide according to claim 1, is characterized in that described aluminium hydroxide is calcined at 1000 DEG C ~ 1200 DEG C, obtains metallurgical-grade aluminum oxide.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107935006A (en) * | 2016-10-12 | 2018-04-20 | 北京矿冶研究总院 | Method for extracting aluminum oxide by mixing and roasting ammonium sulfate and fly ash in reducing atmosphere |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103086408A (en) * | 2013-01-24 | 2013-05-08 | 沈阳铝镁设计研究院有限公司 | Method for producing alumina by mixing and roasting flyash and ammonium sulfate |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103086408A (en) * | 2013-01-24 | 2013-05-08 | 沈阳铝镁设计研究院有限公司 | Method for producing alumina by mixing and roasting flyash and ammonium sulfate |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107935006A (en) * | 2016-10-12 | 2018-04-20 | 北京矿冶研究总院 | Method for extracting aluminum oxide by mixing and roasting ammonium sulfate and fly ash in reducing atmosphere |
| CN107935006B (en) * | 2016-10-12 | 2019-09-03 | 北京矿冶科技集团有限公司 | Ammonium sulfate and the baking mixed method for extracting aluminium oxide of flyash reducing atmosphere |
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Application publication date: 20141231 |