CN104512917A - Method of decomposing fly ash dissolution solution by ammonia water to prepare aluminum hydroxide - Google Patents
Method of decomposing fly ash dissolution solution by ammonia water to prepare aluminum hydroxide Download PDFInfo
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- CN104512917A CN104512917A CN201310450817.4A CN201310450817A CN104512917A CN 104512917 A CN104512917 A CN 104512917A CN 201310450817 A CN201310450817 A CN 201310450817A CN 104512917 A CN104512917 A CN 104512917A
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- ammoniacal liquor
- aluminium hydroxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/20—Preparation of aluminium oxide or hydroxide from aluminous ores using acids or salts
- C01F7/26—Preparation of aluminium oxide or hydroxide from aluminous ores using acids or salts with sulfuric acids or sulfates
Abstract
Relating to the aluminum hydroxide production field, the invention specifically discloses a method of decomposing a fly ash dissolution solution by ammonia water to prepare aluminum hydroxide. The method includes: subjecting fly ash to ammonia process roasting, dissolving the product in water at 50-95DEG C and performing separation so as t o obtain an aluminum sulfate solution containing iron ions; removing the iron ions from the solution by a cation exchange resin technique to obtain an aluminum sulfate refined solution; absorbing the roasting generated ammonia with water to obtain ammonia water for decomposition of the iron removed aluminum sulfate solution, firstly using ammonia water to adjust the pH of an early stage solution, then adding a seed crystal to adjust the pH of a second-stage solution, and finally adjusting the end point pH value; and remaining the state for certain time, thus obtaining aluminum hydroxide with a large particle size. The method provided by the invention adopts the ammonia water obtained by absorption of ammonia produced in the roasting process to decompose the iron removed solution, the pH of the solution is easy to control, the aluminum hydroxide produced by decomposition is easy to realize solid-liquid separation, and the process is simple and is in favor of industrialization.
Description
Technical field
The present invention is production of aluminum hydroxide field, is specially a kind of method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide.
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.
Summary of the invention
The invention provides a kind of method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide, object to make the aluminum hydroxide particles of decomposition comparatively large, and water ratio is low, is easy to be separated.
In order to solve the problem, the present invention is achieved in that
Utilize ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare a method for aluminium hydroxide, the products in water roasting of flyash ammonia process obtained stripping being separated at 50 ~ 95 DEG C, obtains the alum liquor containing iron ion; Adopt the iron ion in cation exchange resin processes removing solution, obtain Tai-Ace S 150 refined soln; The ammonia water that roasting produces absorbs the ammoniacal liquor obtained, and is used for decomposing alum liquor after deironing, first carries out the adjustment of pH value of solution in earlier stage with ammoniacal liquor, then adds crystal seed, then carry out the adjustment of two sections of pH value of solution, finally carry out the adjustment of endpoint pH; After stop, obtain the larger aluminium hydroxide of granularity.
Described flyash ammonia process roasting and stripping are after being mixed by weight 1:3 ~ 1:7 with ammonium sulfate by flyash, be 300 ~ 600 DEG C in temperature and carry out roasting 1 ~ 6 hour, be that 1:1 ~ 5:1 carries out stripping by water and sintered product weight ratio at 50 ~ 95 DEG C, obtain the alum liquor containing iron ion.
Described ammoniacal liquor is that the ammonia water that ammonia process roasting produces absorbs, and obtains the ammoniacal liquor that concentration is 15wt% ~ 28wt%, is used for decomposing the alum liquor after deironing.
The concentration of described Tai-Ace S 150 refined soln is 160 ~ 280g/L, and the pH value of Tai-Ace S 150 refined soln is 0.8 ~ 1.6.
Described early stage, the adjustment of pH value of solution was at 50 ~ 95 DEG C, with the ammoniacal liquor obtained in 30 ~ 60min regulator solution pH value to 2 ~ 3, and to stir under stir speed (S.S.) is 200 ~ 400r/min.
The described crystal seed that adds adds aluminium hydroxide crystal seed in the solution to make the solid content of solution reach 130 ~ 280g/L.
The adjustment of two sections of described pH value of solution adds after crystal seed through 20 ~ 60min, continue to pass into obtained ammoniacal liquor in solution, make the pH value of solution reach 3.5 ~ 4.5 at 50 ~ 90min to stop adding ammoniacal liquor, the solid now generated in solution some be aluminium ammonium alum, obtain the mixture of aluminium ammonium alum and aluminium hydroxide; Afterwards, while continuing to add ammoniacal liquor adjust ph, aluminium ammonium alum will generate aluminium hydroxide.
The described adjustment carrying out endpoint pH is after the adjustment of two sections of pH value of solution, continues to pass into ammoniacal liquor to solution for continuous, make solution reach endpoint pH 5 ~ 5.8 at 10 ~ 40min through 30 ~ 60min.
Obtaining aluminium hydroxide after described stop is stop 2 ~ 5h, and adopt pressurization or filtration under diminished pressure to obtain aluminium hydroxide, rate of decomposition more than 99%, filter cake moisture content is 10wt% ~ 30wt%, and aluminium hydroxide particle diameter D50 reaches 40 ~ 70 μm.
Advantage of the present invention and effect as follows:
The present invention adopts the ammonia produced in roasting process, the ammoniacal liquor obtained is absorbed with water, deironing liquid is decomposed, the product circulation produced in whole ammonia process roasting process can be made to utilize, be easy to control pH value of solution with ammoniacal liquor, 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.
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.
As shown in Figure 1, the present invention utilizes ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare the method for aluminium hydroxide, and its technical process is:
(1) ammonia process roasting and stripping, the roasting of flyash ammonia process and stripping are after being mixed by weight 1:3 ~ 1:7 with ammonium sulfate by flyash, be 300 ~ 600 DEG C in temperature and carry out roasting 1 ~ 6 hour, be that 1:1 ~ 5:1 carries out stripping by water and sintered product weight ratio at 50 ~ 95 DEG C, obtain the alum liquor containing a small amount of iron ion;
(2) deironing, adopts the iron ion in cation exchange resin processes removing solution, obtains Tai-Ace S 150 refined soln;
(3) decompose, the ammonia water that ammonia process roasting produces absorbs and obtains the ammoniacal liquor that concentration is 15wt% ~ 28wt%, is used for decomposing the alum liquor after deironing; Wherein, the concentration of Tai-Ace S 150 refined soln is 160 ~ 280g/L, and the pH value of Tai-Ace S 150 refined soln is 0.8 ~ 1.6.
First carry out the adjustment of pH value of solution in early stage with ammoniacal liquor, then add crystal seed, then carry out the adjustment of two sections of pH value of solution, finally carry out the adjustment of endpoint pH; After stop, obtain the aluminium hydroxide that granularity is larger.
Described early stage pH value of solution adjustment, be at 50 ~ 95 DEG C, with the ammoniacal liquor obtained in 30 ~ 60min regulator solution pH value to 2 ~ 3, and to stir under stir speed (S.S.) is 200 ~ 400r/min;
Described adds crystal seed, is to add aluminium hydroxide crystal seed in the solution to make the solid content of solution reach 130 ~ 280g/L;
The adjustment of described two sections of pH value of solution, add after crystal seed through 20 ~ 60min, continue to pass into obtained ammoniacal liquor in solution, make the pH value of solution reach 3.5 ~ 4.5 at 50 ~ 90min to stop adding ammoniacal liquor, the solid now generated in solution some be aluminium ammonium alum, obtain the mixture of aluminium ammonium alum and aluminium hydroxide.Afterwards, while continuing to add ammoniacal liquor adjust ph, aluminium ammonium alum will generate aluminium hydroxide.
The described adjustment carrying out endpoint pH is after the adjustment of two sections of pH value of solution, continues to pass into ammoniacal liquor to solution for continuous, make solution reach endpoint pH 5 ~ 5.8 at 10 ~ 40min through 30 ~ 60min.
Obtaining aluminium hydroxide after described stop is stop 2 ~ 5h, and adopt pressurization or filtration under diminished pressure to obtain aluminium hydroxide, rate of decomposition more than 99%, filter cake moisture content is 10wt% ~ 30wt%, and aluminium hydroxide particle diameter D50 reaches 40 ~ 70 μm.In the present invention, disengaging time and filter cake thickness are specifically determined according to the amount that will decompose.
Embodiment 1
The roasting of flyash ammonia process and stripping are after being mixed by weight 1:4 with ammonium sulfate by flyash, be 350 DEG C in temperature and carry out roasting 5 hours, the ammonia absorbing roasting generation with water obtains the ammoniacal liquor that concentration is 20wt%, be that 3:1 carries out stripping by water and sintered product weight ratio at 60 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron ion in cation exchange resin processes removing solution, obtain the alum liquor that concentration is 190g/L, alum liquor pH value is 1.3, measure the deironing liquid of 800ml, at 70 DEG C early stage pH value of solution adjustment, with ammoniacal liquor in 45min regulator solution pH value to 2.1, and stir under stir speed (S.S.) is 300r/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 ammoniacal liquor in solution, make the pH value of solution reach 4.0 stoppings at 70min and lead to ammoniacal liquor, the solid now generated in solution some be aluminium ammonium alum.Afterwards, while continuing to add ammoniacal liquor adjust ph, aluminium ammonium alum will generate aluminium hydroxide.
After the adjustment of two sections of pH value of solution, continue to pass into ammoniacal liquor to solution for continuous through 40min, make solution reach endpoint pH 5.6 at 25min.
Stop 2.5h, adopt vacuum filtration to obtain aluminium hydroxide, disengaging time is 52 seconds, and filter cake thickness is 8.2mm, rate of decomposition 99%, and filter cake moisture content is 20wt%, and aluminium hydroxide particle diameter D50 is 55 μm.
Embodiment 2
The roasting of flyash ammonia process and stripping are after being mixed by weight 1:5 with ammonium sulfate by flyash, be 400 DEG C in temperature and carry out roasting 4 hours, the ammonia absorbing roasting generation with water obtains the ammoniacal liquor that concentration is 25wt%, be that 2.5:1 carries out stripping by water and sintered product weight ratio at 95 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron ion in cation exchange resin processes removing solution, obtain the alum liquor that concentration is 200g/L, alum liquor pH value is 1.6, measure the deironing liquid of 1000ml, the adjustment of pH value of solution in early stage is carried out at 95 DEG C, with ammoniacal liquor in 60min regulator solution pH value to 2.8, and stir under stir speed (S.S.) is 400r/min, add 210g 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 ammoniacal liquor in solution, make the pH value of solution reach 4.5 stoppings at 90min and pass into ammoniacal liquor, the solid now generated in solution some be aluminium ammonium alum.Afterwards, while continuing to add ammoniacal liquor adjust ph, aluminium ammonium alum will generate aluminium hydroxide.
Continue to pass into ammoniacal liquor 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.
After stopping reaction 3h, adopt vacuum filtration to obtain aluminium hydroxide, disengaging time is 60 seconds, and filter cake thickness is 7.6mm, rate of decomposition 99%, and filter cake moisture content is 18wt%, and aluminium hydroxide particle diameter D50 is 58 μm.
Embodiment 3
The roasting of flyash ammonia process and stripping are after being mixed by weight 1:5.5 with ammonium sulfate by flyash, be 570 DEG C in temperature and carry out roasting 3.5 hours, the ammonia absorbing roasting generation with water obtains the ammoniacal liquor that concentration is 22wt%, be that 2:1 carries out stripping by water and sintered product weight ratio at 60 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron ion in cation exchange resin processes removing solution, obtain the alum liquor that concentration is 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 ammoniacal liquor in 45min regulator solution pH value to 2.5, and stir under stir speed (S.S.) is 300r/min, add 160g aluminium hydroxide crystal seed and make the solid containing reaching 140g/L of solution.
To add after crystal seed through 30min, continue to pass into ammoniacal liquor in solution, make the pH value of solution reach 3.5 stoppings at 60min and pass into ammoniacal liquor, the solid now generated in solution some be aluminium ammonium alum.Afterwards, while continuing to add ammoniacal liquor adjust ph, aluminium ammonium alum will generate aluminium hydroxide.
Continue to pass into ammoniacal liquor 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 50min.
After stopping reaction 4h, adopt vacuum filtration to obtain aluminium hydroxide, filter cake thickness is 7.5mm, rate of decomposition more than 99%, and filter cake moisture content is 16wt%, and aluminium hydroxide particle diameter D50 can reach 60 μm.
Embodiment 4
The roasting of flyash ammonia process and stripping are after being mixed by weight 1:6 with ammonium sulfate by flyash, be 500 DEG C in temperature and carry out roasting 3 hours, the ammonia absorbing roasting generation with water obtains the ammoniacal liquor that concentration is 23wt%, be that 3:1 carries out stripping by water and sintered product weight ratio at 70 DEG C, obtain the alum liquor containing a small amount of ferric sulfate, with the iron in cation exchange resin processes removing solution, obtain the alum liquor that concentration is 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 ammoniacal liquor 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.Afterwards, while continuing to add ammoniacal liquor adjust ph, aluminium ammonium alum will generate aluminium hydroxide.
To add after crystal seed through 40min, continue to pass into ammoniacal liquor in solution, make the pH value of solution reach 4.2 stoppings at 65min and pass into ammoniacal liquor, the solid now generated in solution some be aluminium ammonium alum.
Continue to pass into ammoniacal liquor 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.
After stopping reaction 3h, adopt filtration under diminished pressure to obtain aluminium hydroxide, disengaging time is 52 seconds, and filter cake thickness is 8.5mm, rate of decomposition 98%, and filter cake moisture content is 20wt%, and aluminium hydroxide particle diameter D50 can reach 65 μm.
Embodiment result shows, ammonium sulfate is mixed with flyash, mixing grog that 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 cation exchange resin processes to enter and deironing is carried out to solution, obtain comparatively pure alum liquor.Adopt ammoniacal liquor to decompose and obtain aluminium hydroxide, in order to the aluminium hydroxide of metallurgical grade can be obtained, the process of decomposing alum liquor just seems particularly important, the too fast ammoniacal liquor that passes into easily produces colloid, not easily separated, and the purity of product is had a great impact, decomposition method of the present invention and with ammoniacal liquor, three sections of pH regulator are carried out to solution and well solve this problem.
Claims (9)
1. utilize ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare a method for aluminium hydroxide, it is characterized in that, the products in water roasting of flyash ammonia process obtained stripping being separated at 50 ~ 95 DEG C, obtains the alum liquor containing iron ion; Adopt the iron ion in cation exchange resin processes removing solution, obtain Tai-Ace S 150 refined soln; The ammonia water that roasting produces absorbs the ammoniacal liquor obtained, and is used for decomposing alum liquor after deironing, first carries out the adjustment of pH value of solution in earlier stage with ammoniacal liquor, then adds crystal seed, then carry out the adjustment of two sections of pH value of solution, finally carry out the adjustment of endpoint pH; After stop, obtain the larger aluminium hydroxide of granularity.
2. according to the method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide according to claim 1, it is characterized in that, described flyash ammonia process roasting and stripping are after being mixed by weight 1:3 ~ 1:7 with ammonium sulfate by flyash, be 300 ~ 600 DEG C in temperature and carry out roasting 1 ~ 6 hour, be that 1:1 ~ 5:1 carries out stripping by water and sintered product weight ratio at 50 ~ 95 DEG C, obtain the alum liquor containing iron ion.
3. according to the method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide according to claim 1, it is characterized in that, described ammoniacal liquor is that the ammonia water that ammonia process roasting produces absorbs, and obtains the ammoniacal liquor that concentration is 15wt% ~ 28wt%, is used for decomposing the alum liquor after deironing.
4. prepare the method for aluminium hydroxide according to the ammoniacal liquor decomposed powder coal ash dissolution fluid that utilizes described in claim 1 or 3, it is characterized in that, the concentration of described Tai-Ace S 150 refined soln is 160 ~ 280g/L, and the pH value of Tai-Ace S 150 refined soln is 0.8 ~ 1.6.
5. according to the method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide according to claim 1, it is characterized in that, described early stage, the adjustment of pH value of solution was at 50 ~ 95 DEG C, with obtained ammoniacal liquor in 30 ~ 60min regulator solution pH value to 2 ~ 3, and to stir under stir speed (S.S.) is 200 ~ 400r/min.
6. according to the method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide according to claim 1, it is characterized in that, the described crystal seed that adds adds aluminium hydroxide crystal seed in the solution to make the solid content of solution reach 130 ~ 280g/L.
7. according to the method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide according to claim 1, it is characterized in that, the adjustment of two sections of described pH value of solution adds after crystal seed through 20 ~ 60min, continue to pass into obtained ammoniacal liquor in solution, make the pH value of solution reach 3.5 ~ 4.5 at 50 ~ 90min to stop adding ammoniacal liquor, the solid now generated in solution some be aluminium ammonium alum, obtain the mixture of aluminium ammonium alum and aluminium hydroxide; Afterwards, while continuing to add ammoniacal liquor adjust ph, aluminium ammonium alum will generate aluminium hydroxide.
8. according to the method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide according to claim 1, it is characterized in that, the described adjustment carrying out endpoint pH is after the adjustment of two sections of pH value of solution, continue to pass into ammoniacal liquor to solution for continuous through 30 ~ 60min, make solution reach endpoint pH 5 ~ 5.8 at 10 ~ 40min.
9. according to the method utilizing ammoniacal liquor decomposed powder coal ash dissolution fluid to prepare aluminium hydroxide according to claim 1, it is characterized in that, obtaining aluminium hydroxide after described stop is stop 2 ~ 5h, pressurization or filtration under diminished pressure is adopted to obtain aluminium hydroxide, rate of decomposition more than 99%, filter cake moisture content is 10wt% ~ 30wt%, and aluminium hydroxide particle diameter D50 reaches 40 ~ 70 μm.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109650419A (en) * | 2017-10-10 | 2019-04-19 | 广东科达洁能股份有限公司 | The method and system that a kind of pair of Aluminum sludge is comprehensively utilized |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4242313A (en) * | 1980-03-21 | 1980-12-30 | Extraction Research & Development, Inc. | Processes for the recovery of alumina from fly ash and production of cement constituents |
| CN102502736A (en) * | 2011-11-03 | 2012-06-20 | 沈阳铝镁设计研究院有限公司 | Method for producing alumina by using pulverized fuel ash |
| 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 |
-
2013
- 2013-09-28 CN CN201310450817.4A patent/CN104512917B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4242313A (en) * | 1980-03-21 | 1980-12-30 | Extraction Research & Development, Inc. | Processes for the recovery of alumina from fly ash and production of cement constituents |
| CN102502736A (en) * | 2011-11-03 | 2012-06-20 | 沈阳铝镁设计研究院有限公司 | Method for producing alumina by using pulverized fuel ash |
| 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 |
Non-Patent Citations (1)
| Title |
|---|
| 李来时: "粉煤灰中提取氧化铝研究新进展", 《轻金属》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109650419A (en) * | 2017-10-10 | 2019-04-19 | 广东科达洁能股份有限公司 | The method and system that a kind of pair of Aluminum sludge is comprehensively utilized |
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