CN105565352A - Method for producing aluminium oxide with high-alumina fly ash - Google Patents
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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
- C01F7/44—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water
- C01F7/441—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
- C01B33/24—Alkaline-earth metal silicates
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- C—CHEMISTRY; METALLURGY
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- 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
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Abstract
The invention provides a method for producing aluminium oxide with high-alumina fly ash. The method comprises the steps of adding the fly ash, sodium carbonate and alkali liquor to limestone for material blending, conducting granulation with a roller granulator, then conducting sintering, adding adjusting liquid to clinker for dissolution, conducting sufficient washing on slag which is dissolved out with hot water, using washing water as dissolution adjusting liquid, adding dilute lye to the slag for dealkalization, conducting desilication on coarse liquid obtained after dissolution of clinker, adding aluminium hydroxide seed crystals to a solution obtained after desilication for seed precipitation decomposition, and conducting evaporation and salt drainage on seed precipitation mother liquor in two steps. By means of the method, efficient and comprehensive utilization of the fly ash is achieved, calcium silicate byproducts of different specifications can be produced by controlling the material blending formula, the sintering conditions and dealkalization conditions, the volume weight can be controlled to be 300-800 kg/m<3>, the method is applicable to building material and soil conditioning, the light characteristic of a building material and soil can be guaranteed, and it can be guaranteed that transportation cost is lowered.
Description
Technical field
The invention belongs to trade waste and utilize field, be specifically related to a kind of method using aluminous fly-ash to produce aluminum oxide.
Background technology
Due to special Mineralizing setting, in the part coal resources of China's Middle-west Inner Mongolia, compose and deposit the aluminum-containing minerals such as a large amount of boehmite and kaolinite.These coal resources are mainly distributed in Zhungeer coal field, coalfield, Zhuozi mountain and Daqingshan coalfield, and wherein alumina content reaches 9 ~ 13%.In the flyash produced after generating, alumina content can reach 40 ~ 50%, is a kind of unconventional bauxite resource.
Often be only Ordos, inner Mongolia area high alumina coal production and just reach 1.2 hundred million tons, wherein part coal produces nearly 3,000 ten thousand tons of aluminous fly-ashs after generating electricity, wherein about 1,400 ten thousand tons, Inner Mongolia of China, there is Huhehaote, Erdos in concentrated heap, what have higher economic development value contains bauxite resource.
The operational path that flyash extracts aluminum oxide mainly contains alkaline process, acid system, using acid and alkali combination method and gas chlorination process at present.Alkaline process mainly comprises limestone sintering process, soda-lime sintering process, pre-desiliconizing+soda-lime sintering process etc.; Acid system mainly comprises: sulfuric acid process, hydrochloric acid method, nitrate method, hydrogen fluoride etc.
And the operational path that China is domestic at present mainly contains: limestone sintering process, pre-desiliconizing soda-lime sintering process, acid system, ammonium sulfate sintering process.Several scheme compares from process aspect above, all can realize the aluminum oxide in flyash and silicon-dioxide extraction and application respectively, and limestone sintering process exists the shortcomings such as product is single, energy consumption is higher, the quantity of slag is large.Pre-desiliconizing soda-lime sintering process is according to the production technique of " after first silicon aluminium ", and main chemical depletion material such as sodium carbonate and sodium hydroxide achieve recycle substantially, but production cost is higher.Acid system and ammonium sulfate method are the production technique according to " after first aluminium silicon ", the recycle of ammonium sulfate and hydrochloric acid can be realized, the product obtained is aluminum oxide, silicon byproduct etc., and the waste residue produced in production is only 50% of pre-desiliconizing soda-lime sintering process, and the quantity of slag is relatively less.But acid system facility investment is very high, and production maintenance expense is also very high, and production process also can cause larger environmental stress.Although the relative corrosion that ammonium sulfate method overcomes equipment and the pressure caused environment, in large-scale production situation, the maximization of equipment also has difficulties, and production technique also needs further exploration, and the reliability of technique is not also determine very much.Current China can realize the technique that the industrial flyash of serialization extracts aluminum oxide and only have soda-lime sintering process, but occupies high due to cost, suffers great loss.
Summary of the invention
For this ore dressing field ore grinding Problems existing, the object of the invention is to provide a kind of wet method roll-type disintegrator, relate to a kind of wet method grinding apparatus and a kind of grading technology supporting for this wet method grinding apparatus, be mainly used in wet method comminution and the classification of ore, also may be used for the solid materials that other needs wet method comminution.
The concrete technical scheme realizing above-mentioned purpose of the present invention is:
1, aluminous fly-ash produces a method for aluminum oxide, comprises step:
(1) Wingdale adds flyash, soda ash and alkali lye and prepares burden, described alkali lye is circulation sodium aluminate solution, and proportion scale is flyash 38 ~ 43 weight part, Wingdale 32 ~ 37 weight part, soda ash 20 ~ 25 weight part, coke powder 8 ~ 12 weight part, moisture after batching is 23 ~ 30%
(2) material prepared is added mixer together with the alkali lye that volume is 85 ~ 90% fully to mix, with roller granulating machine granulation again, granulation particle diameter is 1 ~ 8mm;
(3) sintered on sinter machine by finished product grain, sintering temperature 1400 ~ 1500 DEG C, sintering negative pressure is greater than 8KPa.Then grog adopts Vertical Mill to dry grind, and is milled down to the grog powder (particle of below 0.074mm accounts for more than 90%) that-0.074mm accounts for more than 90%.
(4) chamotte powder is added adjustment liquid and carry out stripping, liquid-solid ratio is 3 ~ 4:1, and dissolution time is 15 ~ 20 minutes, and temperature is 70 ~ 75 DEG C.
(5) after fully being washed by the slag hot water that step (4) chamotte powder stripping obtains, washing water are with adjusting liquid, and the slag after washing adds sig water and carries out dealkalize, control Na in the solution of dealkalize
2o is 90g/L, dealkalize temperature 160 ~ 200 DEG C, 1 hour time, obtains byproduct Calucium Silicate powder, may be used for building materials and soil conditioning after the complete slag of dealkalize fully washs.
(6) carry out desiliconization after solution step (4) chamotte powder stripping obtained and sodium aluminate crystallization mixed dissolution, desiliconization condition is: temperature 160 ~ 180 DEG C, 1 ~ 2 hour time;
(7) the solution hydrogenation alumina seed that step (6) obtains is carried out kind point to decompose, decompose and obtain Al (OH)
3, then roasting obtains aluminum oxide;
(8) carried out in two steps evaporating and salt discharge by the seed precipitation solution that step (7) obtains, it is Na that the first step is evaporated to concentration of lye
2o280 ~ 300g/L, and then carry out second step evaporation, obtaining concentration of lye is Na
2o500 ~ 600g/L; Dealkalize liquid step (5) obtained carries out two steps evaporations too, and to obtain concentration of lye be Na
2o500 ~ 600g/L, is used for the raw material of alumina industry as liquid caustic soda byproduct;
(9) seed precipitation solution after being evaporated by second step carries out seed addition decrease temperature crystalline, and obtain sodium aluminate crystal, sodium aluminate crystal joins in step (6) again and carries out dissolving circulation; Crystallization condition is: first temperature 80 ~ 110 DEG C, end temperature 40 ~ 50 DEG C, 6 ~ 8 hours time;
(10) salt that mother liquor step (9) obtained and step (8) obtain and the white residue that step (6) obtains mix, and then turn back in step (1) as batching alkali lye, realize alkali lye circulation.
Wherein, in described flyash, alumina content is 40 ~ 50%.
Wherein, in described step (1), first limestone mine is crushed to 2 ~ 5mm, then it is levigately accounted for more than 85% for-0.074mm to granularity; By levigate for coke powder to 1 ~ 3mm; Then for batching.
Wherein, in described step (1), concentration of lye is Na
2o500 ~ 600g/L, α k=12 ~ 30.
Further, in described step (2), roller nodulizer adds the alkali lye same with step (1) in granulating, and volume is 10 ~ 20%. of step (1) volume
Preferably, in described step (3), ignition temperature is 1050 DEG C, and igniting negative pressure is greater than 4KPa.
Wherein, in described step (5), temperature of washing water is 80 ~ 95 DEG C.
Desiliconization seed is used to be conducive to the separation of crystal.Preferably, add desiliconization seed and carry out desiliconization, grain weight 40 ~ 60g/L in described step (6), desiliconization seed is the solid (the operation initial stage does not have seed) that desiliconization step produces.
The sig water of step (6) preparation dealkalize liquid can be with sodium hydroxide preparation, also can be the washing lotion obtained after the complete slag of dealkalize fully washs.
Preferably, in described step (9), seed precipitation solution carries out seed addition decrease temperature crystalline, grain weight 10 ~ 40g/L.
Beneficial effect of the present invention is:
(1) method of the present invention's proposition, take aluminous fly-ash as raw material, on the basis of aluminum oxide conventional sintering law technology, adopt dry method firing technology, by the Technology Integration in stripping again of first dry grinding at desiliconization, decomposition, evaporation, grog etc., achieve the High-efficient Production of aluminum oxide from whole flow process.
(2) the present invention is on the basis of conventional sintering law technology, propose full kind division technique technology, sintering process technical process is made to reduce more than 1/3rd, COMPREHENSIVE CALCULATING corrosion brings up to more than 90%, the total yield of aluminum oxide reaches more than 90%, reduce operation easier, reduce equipment and personnel's input, reduce energy consumption.
(3) present invention achieves the breakthrough of high density seed precipitation solution evaporation, by two step evaporation salt discharge technology, solve the problem of traditional seed precipitation solution evaporation because of salt discharge difficulty restriction evaporative concn.
(4) present invention achieves the high-efficiency comprehensive utilization of flyash, can produce the Calucium Silicate powder byproduct of different size by controlling batch formula, firing condition and dealkalize condition, unit weight can control at 300 ~ 800kg/m
3, be applicable to building materials and soil conditioning respectively, both can ensure its lightweight nature, can ensure again to reduce transportation cost.
(5) calcined soda for industry that part is cheap can be converted into the high liquid caustic soda of added value by the present invention, and dropped to the cost of the major product of this technology further, economic benefit is obvious.
In a word, the present invention technically achieves important breakthrough conventional sintering method production aluminum oxide, and production cost and investment of founding the factory all significantly reduce, and when processing Industrial Solid Waste flyash, effect is more outstanding, achieves the object of the comprehensive cyclic utilization of aluminium silicon.Simultaneously in lectotype selection, have ripe equipment choice at chemical industry and metallurgy industry, industrialization is very easy to feasible.
Accompanying drawing explanation
Fig. 1 is the schema producing aluminum oxide with aluminous fly-ash.
Embodiment
Following examples for illustration of the present invention, but are not used for limiting the scope of the invention.The following stated is only the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the prerequisite not departing from the technology of the present invention principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
In embodiment, if no special instructions, the technique means used is ordinary skill in the art means.
Raw material powder coal ash adopts the aluminous fly-ash of certain power plant's output of Ordos, inner Mongolia area, and its composition is as shown in table 1.Wingdale adopts Wingdale that Hohhot district produces, and its composition is as table 2.
Table 1: flyash composition
Table 2: Wingdale composition
Embodiment 1
Levigate for the breeze particle being-0.074mm to granularity, see Fig. 1, first by limestone crushing to the 2 ~ 5mm of composition as table 2, is then accounted for more than 85%, coke powder is crushed to 1-3mm by flow process.Then add composition such as the flyash of table 1 and light ash fully to mix: flyash 38 weight part, Wingdale 32 weight part, soda ash 20 weight part, coke powder 8 weight part, then alkali lye is prepared (through the circulating mother liquor of two step evaporation salt discharges, be divided into two portions, allocation proportion is 87:13, this step is with 87%), concentration is Na2O510g/L, causticization factor alpha k=14.Moisture 30% of preparing burden to obtain, alkali ratio is 1, and calcium ratio is 1.
By the material prepared together with 87% alkali lye add mixer carry out first time mixing, a material mixed enters rerolling machine, sprays into the alkali lye of remaining 13% simultaneously, granulate in roller pelletizer in rerolling machine, and size distribution is 1 ~ 8mm.The permeability index of corning is 50k.
Finished pellets and grate-layer material and rim charge are distributed on sinter machine and sinter, control ignition temperature 1050 DEG C, igniting negative pressure 4KPa, sintering temperature 1400 ~ 1500 DEG C, sintering negative pressure 8 ~ 8.5KPa.Then agglomerate is milled down to the grog grinding that-0.074mm accounts for more than 90%.
The chamotte powder ground is added adjustment liquid (elutant after hot water washery slag) and carry out stripping in stripping groove, liquid-solid ratio is 4:1, to add after adjustment liquid Na in mixture
2o50g/L, α k=1.2, dissolution time is 15 ~ 20 minutes, and temperature is 75 DEG C.
The hot water of slag after chamotte powder stripping with 90 DEG C is fully washed, then adds sig water and control Na in dealkalize liquid
2o90g/L carries out dealkalize, dealkalize temperature 200 DEG C, 1 hour time, liquid-solid ratio 4:1, and obtain byproduct Calucium Silicate powder after the complete slag of dealkalize fully washs, Volume-weight Determination is 310kg/m
3, for making light building material.
After the solution that chamotte powder stripping obtains and sodium aluminate crystallization mixed dissolution, dividing mother liquid evaporation to adjust α k by one section of kind is 1.5, AL
2o
3concentration controls as 140g/L, adds desiliconization seed (solid that desiliconization step produces) and carry out desiliconization in desilicator.Desiliconization condition is: grain weight 60g/L, temperature 160 DEG C, and 1 hour time, after desiliconization completes, slurries leaf filter is refined, and seminal fluid carries out kind point and decomposes, and desiliconization slag mixes with circulating mother liquor later prepares burden.
The seminal fluid adding aluminum hydroxide crystal seed that desiliconization obtains carries out kind point and decomposes, and decompose and obtain Al (OH) 3, then roasting obtains aluminum oxide.
Decompose the seed precipitation solution obtained to carry out in two steps evaporating and salt discharge, it is Na that the conventional 6 effect falling-film evaporators of the first step are evaporated to concentration of lye
2o280 ~ 300g/L, and then carry out second step evaporation with nickel material vaporizer, obtaining concentration of lye is Na
2o510g/L.The dealkalize liquid dealkalize of stripping slag obtained carries out two steps evaporations too, and to obtain concentration of lye be Na
2o500 ~ 600g/L, is used for alumina industry as raw material as a kind of liquid caustic soda byproduct.
Seed precipitation solution after being evaporated by second step carries out seed addition decrease temperature crystalline, and obtain sodium aluminate crystal, sodium aluminate crystal joins in the thick liquid of stripping again and carries out dissolving circulation.Crystallization condition is: first temperature 80 DEG C, end temperature 50 DEG C, grain weight 20g/L, 6 hours time.
Circulating mother liquor crystallization obtained and evaporation are discharged the white residue that salt and desiliconization obtain and are mixed, and then return as batching alkali lye and prepare burden, realize alkali lye and circulate.
By the Decomposition Cycle mother liquor COMPREHENSIVE CALCULATING that kind point decomposition step and two steps evaporation salt discharge step obtain, corrosion reaches 92%.
Embodiment 2
First by limestone crushing to the 2 ~ 5mm of composition as table 2, then account for more than 85% to granularity for-0.074mm by levigate for breeze, coke powder is crushed to 1 ~ 3mm., then add composition such as the flyash of table 1 and light ash and fully mix: flyash 40 weight part, Wingdale 35 weight part, soda ash 22 weight part, coke powder 10 weight part, then adds alkali lye, and concentration is Na2O550g/L, α k=20.The batching moisture 28% obtained, alkali ratio is 1, and calcium ratio is 1.Circulating mother liquor alkali lye is by volume divided into two portions, and allocation proportion is 87:13, batching 87% wherein.
The material prepared is added mixer and carry out first time mixing, a material mixed enters roll-type nodulizer machine, and the alkali lye simultaneously spraying into remaining 13% is granulated, and size distribution is 1 ~ 8mm.The permeability index of granulating is 50k.
Finished pellets and grate-layer material and rim charge are distributed on sinter machine and sinter, control ignition temperature 1050 DEG C, igniting negative pressure is greater than 4KPa, sintering temperature 1400 ~ 1500 DEG C, sintering negative pressure 8 ~ 8.5KPa.Then agglomerate is milled down to the grog grinding that-0.074mm accounts for more than 90%.
The chamotte powder ground is added adjustment liquid and carry out stripping in stripping groove, leaching condition is: concentration of lye Na
2o50g/L, α k=1.2, liquid-solid ratio is 3:1, and dissolution time is 20 minutes, and temperature is 75 DEG C.
Add sig water after fully being washed with 90 DEG C of hot water by slag after chamotte powder stripping and carry out dealkalize, dealkalize liquid composition Na
2o90g/L, temperature 180 DEG C, 1 hour time, liquid-solid ratio 4:1, obtain byproduct Calucium Silicate powder after the complete slag of dealkalize fully washs, Volume-weight Determination is that 450kg/m3 is for making building materials.
After the solution that chamotte powder stripping obtains and sodium aluminate crystallization mixed dissolution, dividing mother liquid evaporation to adjust α k by one section of kind is 1.5, AL
2o
3concentration controls, for 140g/L, to add desiliconization seed and carry out desiliconization in desilicator.Desiliconization condition is: grain weight 60g/L, temperature 160 DEG C, and 1 hour time, after desiliconization completes, slurries leaf filter is refined, and seminal fluid carries out kind point and decomposes, and desiliconization slag mixes with circulating mother liquor later prepares burden.
Repeat the decomposition in example 1, evaporation and crystallization mode, realize technological cycle.
By the Decomposition Cycle mother liquor COMPREHENSIVE CALCULATING that kind point decomposition step and two steps evaporation salt discharge step obtain, corrosion reaches 95%.
Embodiment 3
First by limestone crushing to the 2 ~ 5mm of composition as table 2, then account for more than 85% to granularity for-0.074mm by levigate for breeze, coke powder is crushed to 1 ~ 3mm.Then add composition such as the flyash of table 1 and light ash fully to mix, flyash 43 weight part, Wingdale 37 weight part, soda ash 25 weight part, coke powder 12 weight part, then add alkali lye batching, concentration of lye is Na
2o600g/L, α k=30.Alkali lye is by volume divided into two portions, and allocation proportion is 87:13.The batching moisture 26% obtained, alkali ratio is 1, and calcium ratio is 1, and coke powder ratio is 12%.
The material prepared is added mixer and carry out first time mixing, a material mixed enters roll-type nodulizer machine, and the alkali lye simultaneously spraying into remaining 13% is granulated, and size distribution is 1 ~ 8mm.The permeability index of granulating is 55k.
Finished pellets and grate-layer material and rim charge are distributed on sinter machine and sinter, control ignition temperature 1050 DEG C, igniting negative pressure is greater than 4KPa, sintering temperature 1400 ~ 1500 DEG C, sintering negative pressure 8 ~ 8.5KPa.Then agglomerate is milled down to the grog grinding that-0.074mm accounts for more than 90%.
The chamotte powder ground is added adjustment liquid and carry out stripping in stripping groove, leaching condition is: concentration of lye Na
2o50g/L, α k=1.2, liquid-solid ratio is 4:1, and dissolution time is 20 minutes, and temperature is 75 DEG C.
Add sig water after fully being washed by slag hot water after stripping and carry out dealkalize, dealkalize liquid composition Na
2o90g/L, temperature 160 DEG C, 1 hour time, liquid-solid ratio 4:1, obtain byproduct Calucium Silicate powder after the complete slag of dealkalize fully washs, Volume-weight Determination is 760kg/m
3.For making building materials and soil conditioner.
After the solution that stripping obtains and sodium aluminate crystallization mixed dissolution, dividing mother liquid evaporation to adjust α k by one section of kind is 1.5, AL
2o
3concentration controls, for 140g/L, to add desiliconization seed and carry out desiliconization in desilicator.Desiliconization condition is: grain weight 60g/L, temperature 160 DEG C, and 1 hour time, after desiliconization completes, slurries leaf filter is refined, and seminal fluid carries out kind point and decomposes, and desiliconization slag mixes with circulating mother liquor later prepares burden.
Repeat the decomposition in example 1, evaporation and crystallization mode, realize technological cycle.
By the Decomposition Cycle mother liquor COMPREHENSIVE CALCULATING that kind point decomposition step and two steps evaporation salt discharge step obtain, corrosion reaches 91%.
Embodiment that is disclosed or that require can make or implement in the scope being no more than existing disclosed laboratory facilities above.All products described by the preferred embodiment of the present invention and/or method, refer to expressly those do not violate concept of the present invention, scope and spirit may be used for this product and/or experimental technique and following step.To all changes and the improvement of technique means in described technique, all belong to concept, the scope and spirit of the claims in the present invention definition.
Claims (9)
1. produce a method for aluminum oxide with aluminous fly-ash, it is characterized in that, comprise step:
(1) Wingdale adds flyash, soda ash and alkali lye and prepares burden, described alkali lye is circulation sodium aluminate solution, proportion scale is flyash 38 ~ 43 weight part, Wingdale 32 ~ 37 weight part, soda ash 20 ~ 25 weight part, coke powder 8 ~ 12 weight part, and the moisture after batching is 23 ~ 30%;
(2) material prepared is added mixer fully to mix, granulate with roller granulating machine, granulation particle diameter is 1 ~ 8mm;
(3) sintered on sinter machine by finished product grain, sintering temperature 1400 ~ 1500 DEG C, sintering negative pressure is greater than 8KPa.Then grog adopts Vertical Mill to dry grind, and is milled down to the grog powder that-0.074mm accounts for more than 90%;
(4) chamotte powder is added adjustment liquid and carry out stripping, liquid-solid ratio is 3-4:1, and dissolution time is 15 ~ 20 minutes, and temperature is 70 ~ 75 DEG C;
(5) after fully being washed by the slag water that step (4) chamotte powder stripping obtains, washing water are with adjusting liquid, and the slag after washing adds sig water and carries out dealkalize, control Na in the solution of dealkalize
2o is 90g/L, dealkalize temperature 160 ~ 200 DEG C, 1 hour time, obtains byproduct Calucium Silicate powder after the complete slag of dealkalize fully washs;
(6) carry out desiliconization by after the solution of step (4) chamotte powder stripping and sodium aluminate crystallization mixed dissolution, desiliconization condition is: temperature 160 ~ 180 DEG C, 1 ~ 2 hour time;
(7) the solution hydrogenation alumina seed that step (6) desiliconization obtains is carried out kind point to decompose, decompose and obtain Al (OH)
3, then roasting obtains aluminum oxide;
(8) carried out in two steps evaporating and salt discharge by the seed precipitation solution that step (7) obtains, it is Na that the first step is evaporated to concentration of lye
2o280 ~ 300g/L, and then carry out second step evaporation, obtaining concentration of lye is Na
2o500 ~ 600g/L; Dealkalize liquid step (5) obtained carries out two steps evaporations too, and to obtain concentration of lye be Na
2o500 ~ 600g/L, is used for alumina industry as raw material as a kind of liquid caustic soda byproduct;
(9) seed precipitation solution after being evaporated by second step carries out seed addition decrease temperature crystalline, and obtain sodium aluminate crystal, sodium aluminate crystal joins in step (6) again and carries out dissolving circulation; Crystallization condition is: first temperature 80 ~ 110 DEG C, end temperature 40 ~ 50 DEG C, 6 ~ 8 hours time;
(10) salt that mother liquor step (9) obtained and step (8) obtain and the white residue that step (6) obtains mix, and then turn back in step (1) as batching alkali lye, realize alkali lye circulation.
2. method according to claim 1, is characterized in that, in described flyash, alumina content is 40 ~ 50%.
3. method according to claim 1, is characterized in that, in described step (1), first limestone mine is crushed to 2 ~ 5mm, then it is levigately accounted for more than 85% for-0.074mm to granularity; By levigate for coke powder to 1 ~ 3mm, then for batching.
4. method according to claim 1, is characterized in that, in described step (1), concentration of lye is Na2O500 ~ 600g/L, α k=12 ~ 30.
5. method according to claim 1, is characterized in that, in described step (2), roller nodulizer adds the alkali lye same with step (1) in granulating, and volume is 10 ~ 20% of step (1) volume.
6. method according to claim 1, is characterized in that, in described step (3), ignition temperature is 1050 DEG C, and igniting negative pressure is greater than 4KPa.
7. method according to claim 1, is characterized in that, in described step (5), temperature of washing water is 80 ~ 95 DEG C.
8. method according to claim 1, is characterized in that, adds desiliconization seed and carries out desiliconization, grain weight 40 ~ 60g/L in described step (6), and desiliconization seed is the solid that desiliconization step produces.
9. method according to claim 1, is characterized in that, in described step (9), seed precipitation solution carries out seed addition decrease temperature crystalline, grain weight 10 ~ 40g/L.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106348380A (en) * | 2016-09-08 | 2017-01-25 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing water purifying agent by using carbide furnace gas dust |
| CN107416874A (en) * | 2016-05-24 | 2017-12-01 | 中国科学院过程工程研究所 | A kind of dealkalization method of coal ash lifting aluminium slag |
| CN112500864A (en) * | 2020-12-16 | 2021-03-16 | 华南理工大学 | Multi-element soil conditioner produced by using fly ash and preparation method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434403A (en) * | 2008-12-16 | 2009-05-20 | 重庆市博赛矿业（集团）有限公司 | Novel method for processing calx sodica sintered alumina by dry method |
| CN102502740A (en) * | 2011-09-26 | 2012-06-20 | 北京亿维德曼科技发展有限公司 | Method for preparing high-alkali high-causticity-ratio solution and improving traditional seed precipitation efficiency |
| CN102627305A (en) * | 2012-03-28 | 2012-08-08 | 中国铝业股份有限公司 | Method using alkaline process to extract alumina in coal ash |
-
2016
- 2016-02-06 CN CN201610083890.6A patent/CN105565352B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434403A (en) * | 2008-12-16 | 2009-05-20 | 重庆市博赛矿业（集团）有限公司 | Novel method for processing calx sodica sintered alumina by dry method |
| CN102502740A (en) * | 2011-09-26 | 2012-06-20 | 北京亿维德曼科技发展有限公司 | Method for preparing high-alkali high-causticity-ratio solution and improving traditional seed precipitation efficiency |
| CN102627305A (en) * | 2012-03-28 | 2012-08-08 | 中国铝业股份有限公司 | Method using alkaline process to extract alumina in coal ash |
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| CN107416874A (en) * | 2016-05-24 | 2017-12-01 | 中国科学院过程工程研究所 | A kind of dealkalization method of coal ash lifting aluminium slag |
| CN106348380A (en) * | 2016-09-08 | 2017-01-25 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing water purifying agent by using carbide furnace gas dust |
| CN112500864A (en) * | 2020-12-16 | 2021-03-16 | 华南理工大学 | Multi-element soil conditioner produced by using fly ash and preparation method thereof |
| CN112500864B (en) * | 2020-12-16 | 2022-04-22 | 华南理工大学 | Multi-element soil conditioner produced by using fly ash and preparation method thereof |
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