CN105776268A - Drying firing method taking fly ash as raw material - Google Patents
Drying firing method taking fly ash as raw material Download PDFInfo
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- CN105776268A CN105776268A CN201610083870.9A CN201610083870A CN105776268A CN 105776268 A CN105776268 A CN 105776268A CN 201610083870 A CN201610083870 A CN 201610083870A CN 105776268 A CN105776268 A CN 105776268A
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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
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/14—Aluminium oxide or hydroxide from alkali metal aluminates
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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
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Abstract
The invention provides a drying firing method taking fly ash as a raw material.The method comprises the following steps that limestone powder, the fly ash, soda ash and evaporated and recovered recycle alkaline liquor are used for batching, and the materials subjected to batching enter a mixer to be fully mixed; the mixture is dried and enters a rotary kiln for sintering, water or correction liquor is added to clinker powder for dissolution, slag obtained through dissolution is fully washed and subjected to dealkalization, a solution obtained through dissolution and a sodium aluminate crystal are mixed and dissolved and subjected to desilicication, by means of seed decomposition, Al(OH)3 is obtained through decomposition, and aluminum oxide is obtained through calcination; obtained spent liquor is subjected to evaporation and salt elimination through two steps.According to the drying firing method taking the fly ash as the raw material, on the basis of a traditional sintering technology of aluminum oxide, a drying firing technology is adopted, and by means of the technology integration in the aspects of desilicication, decomposition, evaporation, clinker dry grinding and dissolution and the like, drying firing of the fly ash is achieved in the whole process.
Description
Technical field
The invention belongs to field of smelting, be specifically related to a kind of method that pelletizing method smelts bauxite.
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 distributed mainly on Zhungeer coal field, coalfield, Zhuozi mountain and Daqingshan coalfield, and wherein alumina content reaches 9～13%.In the flyash produced after generating, alumina content is up to 40～50%, is a kind of unconventional bauxite resource.Often it is only Ordos, inner Mongolia area high alumina coal production and just reaches 1.2 hundred million tons, wherein part coal is for producing nearly 30,000,000 tons of aluminous fly-ash after generating, wherein Inner Mongolia of China about 14,000,000 tons, concentrate heap there is Huhehaote, Erdos, have higher economic development value containing bauxite resource.
Flyash extracts the process route of aluminium oxide currently mainly alkaline process, acid system, using acid and alkali combination method and gas chloridising.Alkaline process mainly includes limestone sintering process, soda lime sintering process, pre-desiliconizing+soda lime sintering process etc.；Acid system specifically includes that sulfuric acid process, hydrochloric acid method, nitrate method, hydrogen fluoride etc..
And the process route that China is domestic at present mainly has: limestone sintering process, pre-desiliconizing soda lime sintering process, acid system, ammonium sulfate sintering process.Several schemes compare from process aspect above, all can realize the aluminium oxide in flyash and silicon dioxide extraction and application respectively.There is the shortcomings such as product is single, energy consumption is higher, the quantity of slag is big in limestone sintering process.Pre-desiliconizing soda lime sintering process is according to the production technology of " after first silicon aluminum ", and main chemical depletion material such as sodium carbonate and sodium hydroxide substantially achieve and recycle, but production cost is higher.Acid system and ammonium sulfate method are the production technologies according to " after first aluminum silicon ", recycling of ammonium sulfate and hydrochloric acid can be realized, the product obtained is aluminium oxide, silicon side-product etc., and the waste residue produced in production is only the 50% of pre-desiliconizing soda lime sintering process, and the quantity of slag is relatively fewer.But acid system equipment investment is significantly high, and production maintenance expense is also significantly high, and production process also can cause bigger ambient pressure.Although ammonium sulfate method overcomes the relatively corrosive of equipment and the pressure that environment is caused, but in large-scale production situation, the maximization of equipment there is also difficulty, and production technology is also required to further exploration, and the reliability of technique is also not as determining.Current China is capable of the technique of the industrial flyash extraction aluminium oxide of serialization and only has soda lime sintering process, but owing to cost occupies height, suffers great loss.
How effectively utilizing flyash, the deficiency and the Industrial Solid Waste that solve China's bauxite resource utilize, and are the challenge faced by the enterprise of this area and opportunity.
Summary of the invention
For the problems referred to above, the present invention provides the method for comprehensive utilization of a kind of flyash, divides and high-concentration alkali liquor evaporation technique in conjunction with dry sintering, full kind, it is achieved the dry method of flyash is burnt till, it is thus achieved that the multi-products such as aluminium oxide, liquid caustic soda.
The technical scheme realizing the object of the invention is:
The dry method firing technology of a kind of flyash, comprises the following steps:
(1) circulation alkali liquor reclaimed with agstone, flyash, soda and evaporation carries out dispensing, and proportion scale is flyash 35～45%, limestone 26～35%, soda 5～15%, and moisture is 12～21%, and alkali ratio is 1, and calcium ratio is 1.
(2) material prepared is entered batch mixer to be sufficiently mixed；
(3) material entrance exsiccator will be blended together be dried, the material dried enters rotary kiln and is sintered, sintering temperature controls at 950～1350 DEG C, the grog cooler that sintering obtains cools down, then adopt Vertical Mill to dry grind, be milled down to-0.074mm and account for the grog powder (granularity granule less than 0.074mm accounts for more than 90%) of more than 90%；
(4) being added water by chamotte powder or adjust liquid and carry out dissolution, liquid-solid ratio is 3～4:1, and dissolution time is 15～20 minutes, and temperature is 75 DEG C.
(5) slag of chamotte powder step (4) obtained carries out dealkalize after carrying out fully washing with 80～95 DEG C of hot water, and the water after washing is for adjusting liquid；Dealkalize temperature 160～200 DEG C, 1 hour time, liquid-solid ratio 3～5:1, the complete slag of dealkalize obtains side-product calcium silicates after carrying out fully washing, it is possible to for building materials and soil conditioning.
(6) desiliconization after the solution that step (4) dissolution is obtained and sodium aluminate crystallization mixed dissolution, desiliconization temperature 160～180 DEG C, 1～2 hour time,
(7) the solution hydrogenation alumina seed that step (6) desiliconization obtains is carried out kind of a point decomposition, decompose and obtain Al (OH)3, then roasting obtains aluminium oxide；
(8) seed precipitation solution that step (7) obtains being undertaken in two steps evaporation and salt discharge, it is Na that the first step is evaporated to concentration of lye2O280～300g/L, then carries out second step evaporation again, and obtaining concentration of lye is Na2O500～600g/L；Dealkalize liquid step (5) obtained carries out two steps evaporations too, and to obtain concentration of lye be Na2O500～600g/L, as liquid caustic soda side-product for alumina industry raw material.
(9) seed precipitation solution after being evaporated by second step carries out seed addition decrease temperature crystalline, obtains sodium aluminate crystal, and sodium aluminate crystal is then added in step (6) to carry out dissolving circulation.Crystallization condition is: first temperature 80～110 DEG C, end temperature 40～50 DEG C, 6～8 hours time.
(10) mother solution step (9) obtained obtains with step (8) salt and the white residue that step (6) obtains mix, and then return in step (1) as dispensing alkali liquor, it is achieved alkali liquor circulates.
Wherein, the flyash in described step (1) is the flyash produced after generating, and wherein alumina content is 40～50%；Described limestone is granularity is the granule of-0.074mm limestone powder that accounts for more than 85%.
The condition that wherein said step (1) dispensing controls is, concentration of lye is Na2O500～600g/L, α k=12～30.
Wherein, the device that the mixed ore deposit of described step (2) adopts is vertical strengthened batch mixer, belongs to dry method mixing technology, and the batch mixing uniformity is up to more than 98%.
Further, in described step (3), dry flue gas is the flue gas of sintering oven, and temperature is 1000～1100 DEG C.
Preferably, the slag of chamotte powder carries out 5～7 back flush with 80～95 DEG C of hot water, carries out dealkalize after washing；In described step (5), the complete slag water of dealkalize fully washs, and the water that washing is discharged is used for preparing dealkalize liquid.
In the dealkalize liquid of the water discharged with washing and slag preparation, Na2O is 80～100g/L.
Wherein, in described step (6), add desiliconization seed and carry out desiliconization.Desiliconization condition is: grain weight 40～60g/L, and desiliconization seed is the crystal (not having seed when just going into operation) that desiliconization step produces.
Wherein, in described step (6), it is 1.4～1.8 that the causticization index α k of desiliconization solution controls, AL2O3It is 120～160g/L that concentration controls.
Further, in described step (9), seed addition decrease temperature crystalline in seed precipitation solution, grain weight 10～40g/L, described seed is kind of point sodium aluminate crystal produced.
The present invention compared with prior art advantage is in that:
(1) present invention is on the basis of aluminium oxide conventional sintering law technology, adopts dry method firing technology, and by the Technology Integration in first dry grinding dissolution again etc. at desiliconization, decomposition, evaporation, grog, the dry method achieving flyash whole flow process is burnt till.
(2) present invention is on the basis of conventional sintering law technology, invent complete kind of division technique technology, sintering process technological process is made to reduce more than 1/3rd, COMPREHENSIVE CALCULATING corrosion brings up to more than 90%, the overall recovery of aluminium oxide reaches more than 90%, reduce operation easier, reduce equipment and personnel put into, reduce energy consumption.
(3) the inventive method achieves the high-efficiency comprehensive utilization of flyash, can produce the calcium silicates side-product of different size by controlling batch formula, firing condition and dealkalize condition, and unit weight can control at 300～800kg/m3, it is respectively suitable for building materials and soil conditioning, both can ensure that its lightweight nature, can ensure that again reduction cost of transportation.
(4) calcined soda for industry cheap for part can be converted into the liquid caustic soda that added value is high by the present invention, falls below the cost of the major product of this technology further, and economic benefit is obvious.
Accompanying drawing explanation
Fig. 1: dry method is burnt till flyash and produced the flow chart of aluminium oxide.
Detailed description of the invention
Now with following most preferred embodiment, the present invention is described, but does not limit the scope of the present invention with this.
Following by different embodiments, the present invention is described.The present invention is not limited in these embodiments, it is possible to adjusted enforcement within the scope of afore mentioned chemical composition with manufacture method.
Embodiment 1
The raw material powder coal ash that the present embodiment adopts is the aluminous fly-ash of certain power plant's output of Ordos, inner Mongolia area, and its composition is as shown in table 1.Limestone adopts the produced limestone of Hohhot district, its composition such as table 2.
Table 1: flyash composition
Table 2: limestone composition
| Composition | AL2O3 | SiO2 | Fe2O3 | MgO | K2O | CaO | Igloss | Total amount |
| Limestone | 0.57 | 1.32 | 0.31 | 1.56 | 0.19 | 51.98 | 54.93 | 100 |
First by the limestone crushing of composition such as table 2 to 2～5mm, then more than 85% is accounted for for-0.074mm by levigate for breeze to granularity.The flyash and the light ash that are subsequently adding composition such as table 1 are sufficiently mixed, and proportion scale is flyash 35 mass parts, limestone 26 mass parts, soda 5 mass parts, is subsequently adding the circulation alkali liquor obtained through double evaporation-cooling, and its concentration is Na2O530g/L, α k=14.Moisture 26% in the dispensing obtained, alkali ratio is 1, and calcium ratio is 1.
The material prepared being added vertical strengthened batch mixer be sufficiently mixed, mixing homogeneity reaches more than 98%.
To blend together material entrance exsiccator to be dried, dry flue gas is the flue gas of sintering oven, and temperature is 1000～1100 DEG C, and the material dried enters rotary kiln and is sintered, and sintering temperature controls at 950～1050 DEG C, and sintered clinker cooler cools down.Then grog adopts Vertical Mill to dry grind, and is milled down to-0.074mm and accounts for the grog powder of more than 90%.
The chamotte powder ground adding adjustment liquid and carries out dissolution in dissolution groove, liquid-solid ratio is 4:1, and the leaching condition of the chamotte powder mixed liquor of preparation is: concentration of lye Na2O50g/L, α k=1.2, dissolution time 20 minutes, temperature is 75 DEG C.
Add dealkalize wash heat liquid after the slag of the chamotte powder after dissolution is carried out fully washing with 90 DEG C of hot water and carry out dealkalize (water that washing is discharged is as adjusting liquid), Na in dealkalize mixture2O90g/L, dealkalize temperature 200 DEG C, 1 hour time, liquid-solid ratio 4:1, the complete slag of dealkalize obtains side-product calcium silicates (the dealkalize wash heat liquid after washing returns dealkalize step and uses) after carrying out fully washing, Volume-weight Determination is 310kg/m3, it is used for making light building material.
After the solution obtained after dealkalize and sodium aluminate crystallization mixed dissolution, dividing mother liquid evaporation to adjust α k by one section of kind is 1.5, AL2O3Concentration controls to be 140g/L, adds desiliconization seed (crystal that namely desiliconization produces) and carries out desiliconization in desilicator.Desiliconization condition is: grain weight 60g/L, temperature 160 DEG C, and 1 hour time, after desiliconization completes, serosity leaf filter is refined, and seminal fluid carries out kind of a point decomposition, and desiliconization slag is for later dispensing.
The seminal fluid adding aluminum hydroxide crystal seed that desiliconization obtains carries out kind of a point decomposition, decomposes and obtains Al (OH)3, then roasting obtains aluminium oxide.
Decomposing the seed precipitation solution obtained and be undertaken in two steps evaporation and salt discharge, it is Na that the conventional six effect falling film evaporators of the first step are evaporated to concentration of lye2O280～300g/L, then carries out second step evaporation with nickel material vaporizer again, and obtaining concentration of lye is Na2O530g/L.Dealkalize liquid dissolution slag dealkalize obtained carries out two steps evaporations too, and to obtain concentration of lye be Na2O550g/L, as a kind of liquid caustic soda side-product for alumina industry as raw material.
Seed precipitation solution after being evaporated by second step carries out seed addition decrease temperature crystalline, obtains sodium aluminate crystal, and sodium aluminate crystal is then added in dissolution rough liquid to carry out dissolving circulation.Crystallization condition is: first temperature 80 DEG C, end temperature 50 DEG C, grain weight 20g/L, 6 hours time.
The white residue that circulating mother liquor crystallization obtained obtains with evaporation discharge salt and desiliconization mixes, and then comes back for dispensing as dispensing alkali liquor, it is achieved alkali liquor circulates.Decomposition Cycle mother solution COMPREHENSIVE CALCULATING kind point decomposition step and two steps evaporation salt discharge step obtained, corrosion can reach more than 90%.
Embodiment 2
First by the limestone crushing of composition such as table 2 to 2～5mm, then more than 85% is accounted for for-0.074mm by levigate for breeze to granularity.The flyash and the light ash that are subsequently adding composition such as table 1 are sufficiently mixed, wherein 40 parts of flyash, limestone 30 parts, soda 10 parts, be subsequently adding alkali liquor, concentration is Na2O550g/L, α k=20.Batching control index, moisture 25%, alkali ratio is 1, and calcium ratio is 1.
Together with alkali liquor, the material prepared being added powerful batch mixer be sufficiently mixed, mixing homogeneity requires more than more than 98%.
To blend together material entrance exsiccator to be dried, dry flue gas is the flue gas of sintering oven, and temperature is 1000～1100 DEG C, and the material dried enters rotary kiln and is sintered, and sintering temperature controls at 1150～1250 DEG C, and sintered clinker cooler cools down.Then grog adopts Vertical Mill to dry grind, and is milled down to-0.074mm and accounts for the grog powder of more than 90%.
The chamotte powder ground adding adjustment liquid and carries out dissolution in dissolution groove, leaching condition is: concentration of lye Na2O50g/L, α k=1.2, and liquid-solid ratio is 4:1, and dissolution time is 15 minutes, and temperature is 75 DEG C.
Add dealkalize wash heat liquid after slag after dissolution is carried out fully washing and carry out dealkalize, washing liquid liquid composition Na2O90g/L, temperature 180 DEG C, 1 hour time, liquid-solid ratio 4:1, the complete slag of dealkalize obtains side-product calcium silicates after carrying out fully washing, and Volume-weight Determination is 450kg/m3For making building materials.
After the solution that dissolution obtains and sodium aluminate crystallization mixed dissolution, dividing mother liquid evaporation to adjust α k by one section of kind is 1.5, AL2O3Concentration controls to be 140g/L, adds desiliconization seed and carries out desiliconization in desilicator.Desiliconization condition is: grain weight 60g/L, temperature 160 DEG C, and 1 hour time, after desiliconization completes, serosity leaf filter is refined, and seminal fluid carries out kind of a point decomposition, and desiliconization slag mixes later dispensing with circulating mother liquor.
Repeat the decomposition in example 1, evaporation and crystallization mode, it is achieved process cycles.Decomposition Cycle mother solution COMPREHENSIVE CALCULATING kind point decomposition step and two steps evaporation salt discharge step obtained, corrosion can reach more than 90%.
Embodiment 3
First by the limestone crushing of composition such as table 2 to 2～5mm, then more than 85% is accounted for for-0.074mm by levigate for breeze to granularity.The flyash and the light ash that are subsequently adding composition such as table 1 are sufficiently mixed, wherein flyash 45 mass parts, limestone 35 mass parts, soda 15 mass parts, be subsequently adding alkali liquor, concentration is Na2O600g/L, α k=30.Batching control index, moisture 23%., alkali ratio is 1, and calcium ratio is 1.
Together with alkali liquor, the material prepared being added powerful batch mixer be sufficiently mixed, mixing homogeneity requires more than more than 98%.
To blend together material entrance exsiccator to be dried, dry flue gas is the flue gas of sintering oven, and temperature is 1000～1100 DEG C, and the material dried enters rotary kiln and is sintered, and sintering temperature controls at 1300～1350 DEG C, and sintered clinker cooler cools down.Then grog adopts Vertical Mill to dry grind, and is milled down to-0.074mm and accounts for the grog powder of more than 90%.
The chamotte powder ground adding adjustment liquid and carries out dissolution in dissolution groove, leaching condition is: concentration of lye Na2O50g/L, α k=1.2, liquid-solid ratio is 3.5:1, and dissolution time is 20 minutes, and temperature is 75 DEG C.
Add dealkalize wash heat liquid after slag after dissolution is carried out fully washing and carry out dealkalize, washing liquid liquid composition Na2O90g/L, temperature 160 DEG C, 1 hour time, liquid-solid ratio 4:1, the complete slag of dealkalize obtains side-product calcium silicates after carrying out fully washing, and Volume-weight Determination is 760kg/m3, it is used for making building materials and soil conditioner.
After the solution that dissolution obtains and sodium aluminate crystallization mixed dissolution, dividing mother liquid evaporation to adjust α k by one section of kind is 1.5, AL2O3Concentration controls to be 140g/L, adds desiliconization seed and carries out desiliconization in desilicator.Desiliconization condition is: grain weight 60g/L, temperature 160 DEG C, and 1 hour time, after desiliconization completes, serosity leaf filter is refined, and seminal fluid carries out kind of a point decomposition, and desiliconization slag mixes later dispensing with circulating mother liquor.
Repeat the decomposition in example 1, evaporation and crystallization mode, it is achieved process cycles.
Those skilled in the art in the art will be appreciated that, above-described embodiment is intended merely to the explanation present invention, and it is not limitation of the invention, as long as in the spirit of the present invention, the conversion of above-described embodiment, modification all will be fallen within the scope of the claims.
Claims (10)
1. the dry method process for calcining that a kind is raw material with flyash, it is characterised in that comprise the following steps:
(1) circulation alkali liquor reclaimed with agstone, flyash, soda and evaporation carries out dispensing, and proportion scale is flyash 35～45 mass parts, limestone 26～35 mass parts, soda 5～15 mass parts, moisture 12～21% in dispensing；
(2) material prepared is entered batch mixer to be sufficiently mixed；
(3) material entrance exsiccator will be blended together be dried, the material dried enters rotary kiln and is sintered, sintering temperature controls at 950～1350 DEG C, the grog cooler that sintering obtains cools down, then adopt Vertical Mill to dry grind, be milled down to-0.074mm and account for the grog powder of more than 90%；
(4) being added water by chamotte powder or adjust liquid and carry out dissolution, liquid-solid ratio is 3～4:1, and dissolution time is 15～20 minutes, and temperature is 75 DEG C.
(5) carrying out dealkalize after the slag of the chamotte powder after step (4) dissolution being carried out fully washing with 80～95 DEG C of hot water, the water after washing is for adjusting liquid；Dealkalize condition is: dealkalize temperature 160～200 DEG C, 1 hour time, liquid-solid ratio 3～5:1, and the complete slag of dealkalize obtains side-product calcium silicates after carrying out fully washing；
(6) desiliconization after the solution that step (4) chamotte powder dissolution is obtained and sodium aluminate crystallization mixed dissolution, desiliconization temperature 160～180 DEG C, 1～2 hour time；
(7) the solution hydrogenation alumina seed that step (6) desiliconization obtains is carried out kind of a point decomposition, decompose and obtain Al (OH)3, then roasting obtains aluminium oxide；
(8) seed precipitation solution that step (7) obtains being undertaken in two steps evaporation and salt discharge, it is Na that the first step is evaporated to concentration of lye2O280～300g/L, then carries out second step evaporation again, and obtaining concentration of lye is Na2O500～600g/L；Dealkalize liquid step (5) obtained carries out two steps evaporations too, and to obtain concentration of lye be Na2O500～600g/L, as liquid caustic soda side-product for alumina industry raw material；
(9) seed precipitation solution after being evaporated by second step carries out seed addition decrease temperature crystalline, obtaining sodium aluminate crystal, sodium aluminate crystal is then added in step (6) to carry out dissolving circulation, and crystallization condition is: first temperature 80～110 DEG C, end temperature 40～50 DEG C, 6～8 hours time；
(10) mother solution step (9) obtained obtains with step (8) salt and the white residue that step (6) obtains mix, and then return in step (1) as dispensing alkali liquor, it is achieved alkali liquor circulates.
2. dry method process for calcining according to claim 1, it is characterised in that: the flyash in described step (1) is the flyash produced after generating, and wherein alumina content is 40～50%；Described limestone is granularity is the granule of-0.074mm limestone powder that accounts for more than 85%.
3. dry method process for calcining according to claim 1, it is characterised in that: the condition that described step (1) dispensing controls is, concentration of lye is Na2O500～600g/L, α k=12～30.
4. dry method process for calcining according to claim 1, it is characterised in that: the device that described step (2) batch mixing adopts is vertical strengthened batch mixer.
5. dry method process for calcining according to claim 1, it is characterised in that: in described step (3), dry flue gas is the flue gas of sintering oven, and temperature is 1000～1100 DEG C.
6. dry method process for calcining according to claim 1, it is characterised in that: in described step (5), the complete slag water of dealkalize fully washs, and the water that washing is discharged is used for preparing dealkalize liquid.
7. dry method process for calcining according to claim 6, it is characterised in that: in described step (5), in the water discharged with described washing and the dealkalize liquid of slag preparation, Na2O is 80～100g/L.
8. dry method process for calcining according to claim 1, it is characterised in that: in described step (6), add desiliconization seed and carry out desiliconization.Desiliconization condition is: grain weight 40～60g/L, and desiliconization seed is the crystal that desiliconization step produces.
9. according to the arbitrary described dry method process for calcining of claim 1～8, it is characterised in that: in described step (6), it is 1.4～1.8 that the causticization index α k of desiliconization solution controls, AL2O3It is 120～160g/L that concentration controls.
10. according to the arbitrary described dry method process for calcining of claim 1～8, it is characterised in that: in described step (9), seed addition decrease temperature crystalline in seed precipitation solution after evaporation, grain weight 10～40g/L, described seed is kind of point sodium aluminate crystal produced.
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| CN108545781A (en) * | 2018-07-03 | 2018-09-18 | 贵州大学 | A kind of comprehensive utilization process of high-sulfur bauxite and ardealite |
| CN108658111A (en) * | 2018-08-24 | 2018-10-16 | 中国科学院过程工程研究所 | A method of improving alumina producing Bayer process efficiency |
| CN109516484A (en) * | 2018-12-11 | 2019-03-26 | 王博 | A method of aluminium oxide is produced with carbide slurry flyash and coal gangue sintering method |
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Effective date of registration: 20201224 Address after: 472100 Shanxian Industrial Park, Sanmenxia City, Henan Province Patentee after: KAIMAN ALUMINUM (SANMENXIA) Co.,Ltd. Address before: Hangzhou City, Zhejiang province 310005 111 South Building 20-22, Jinjiang Patentee before: HANGZHOU JINJIANG GROUP Co.,Ltd. |