CN1217295A - Process for producing aluminium oxide by carbonating decomposation - Google Patents
Process for producing aluminium oxide by carbonating decomposation Download PDFInfo
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- CN1217295A CN1217295A CN 97106190 CN97106190A CN1217295A CN 1217295 A CN1217295 A CN 1217295A CN 97106190 CN97106190 CN 97106190 CN 97106190 A CN97106190 A CN 97106190A CN 1217295 A CN1217295 A CN 1217295A
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Abstract
The present invention selates to a technological process for producing sand-like alumina by means of continuous carbonization and decomposition in the production of alumina by using soda-lime sintering method. Said technological process includes three procedures of carbonization decomposition of refined sodium aluminate solution, filtering and washing the decomposed serous fluid and calcining aluminium hydroxide, and is mainly characterized by that the refined sodium aluminate can be continuously introduced into series-connected decomposition cell group to implement decomposition, and the decomposed serous fluid is discharged from final decomposition cell. Said technological process can continuously make decomposition to raise equipment utilization rate and simplify operation.
Description
The present invention relates to process for making alumina.
In the bayer's process aluminum oxide production process, generally adopt crystal seed to stir and decompose the preparation sandy alumina.In alkali-lime sinter process alumina producing, adopt the data of producing sandish aluminium oxide by carbonating decomposition, abroad still be not reported.Domestic No. 85102276 patent applications disclose a kind of method of this respect, add aluminium hydroxide crystal seed to the sintering process sodium aluminate refined liquid, and this crystal seed is special by the carbonating decomposition method.In other words, this technology will be provided with a cover crystal seed preparation flow.It is thermopositive reaction that carbonating is decomposed, and must keep slurry temperature constant in 73 ℃-77 ℃ in this decomposition course all the time.Be that decomposition course need be set up the slurries cooling system, more be pointed out that it is discontinuity technology that this carbonating is decomposed, be that slurries inject decomposer, after reaching specified amount, promptly stop to pump into, carry out carbonating and decompose, after decomposing end, slurries pump into filtration unit, and after the decomposer emptying, row injects another batch slurries to be decomposed again, carry out next groove and decompose, carry out so discontinuously.To sum up, make this technical process complexity, particularly discontinuity technology, efficient is low, cost height, trivial operations.
The objective of the invention is, the method for continuous carbonation decomposition for producing sand-like alumina in a kind of alkali-lime sinter process alumina producing is provided.This method is uninterruptedly carried out decomposition technique, does not need to establish in addition the aluminium hydroxide crystal seed preparation flow, and decomposition course also need not the slurries cooling system.
Process for producing sandish aluminium oxide by carbonating decomposition of the present invention divides three operations, the refined sodium aluminate solution carbonating is decomposed, the filtration of decomposing rear slurry and washing, Aluminium hydroxide roasting, the major technology characteristics are that carbonation decomposition course is a continuity technology, continuous first groove that feeds placed in-line decomposer group down of refined sodium aluminate solution to be decomposed disconnectedly, after after each decomposer finishes carbonating and decomposes in the middle of flowing through successively, slurries are discharged by the last step decomposer.
Accompanying drawing is a process flow sheet of the present invention.Details are as follows with technical process of the present invention in conjunction with the accompanying drawings:
The alumina content 85-125 gram of sintering process refined sodium aluminate solution to be decomposed (1)/ Liter, causticization coefficient 1.35-1.65,80 ℃-90 ℃ of temperature. By lime The concentration of stove production is that the carbon dioxide (2) of 35%-40% passes into the series connection carbonating continuously In first, second, and third groove of decomposer group (3), owing to pass in the carbonation decomposition course Great amount of carbon dioxide gas, and be aided with mechanical agitation (4), the groove endoparticle is abundant fluidized state, Decomposition slurries in first groove are promoted to second groove from trench bottom by compressed air, and follow-up each groove successively Flow into next groove, series connection carbon divides groove series to be made up of 4-6 groove. Decomposition is refining with sodium aluminate It is 2-4 hour that liquid divides the mean residence time in the groove at the serial carbon of series connection, and resolution ratio is according to refining Liquid siliceous modulus (A/S) difference can be between 85%-95%, decompose slurries by pump ( 5) deliver to separation tank (6), the underflow of (6) is delivered to filter (8) by pump (7) , filter cake is delivered to flash roaster (9), makes after 1000 ℃ of-1050 ℃ of roastings Sandy alumina, filter (8) filtrate send the material process batching after evaporation.
Carbon dioxide gas passes into series connection carbon, and to divide the ratio of each groove of groove series be the important of output aluminium hydroxide Condition. Limestone kiln furnace gas carbonated 35%-40%, after compression pressure 1.0-1.5 kilograms per centimeter2, according to 20-40m3 CO
2/hm
3The speed of refined liquid, logical The speed that enters carbon dioxide is successively decreased from first groove, and last groove does not pass into carbon dioxide. Refined liquid Dividing the time of staying of groove series at series connection carbon is 2-4 hour. Decompose slurries when the stop of last groove Between be 0.5-1.0 hour. After the carbon branch was finished, slurries namely obtained sand behind separating, washing Shape aluminium hydroxide obtains aluminium oxide after the roasting.
Technology of the present invention will be interrupted carbon and be divided the production aluminum oxide to be improved to continuous carbon method, increase substantially plant factor, simplify operation, suitable industrial application.
Example: decompose and use industrial sodium aluminate solution, composition is: alumina content 90-100 gram/liter, and causticization coefficient 1.35-1.65, A/S600 decomposes 85 ℃ of initial temperature, used limestone kiln furnace gas carbonated 35%-40%, pressure 1.2 kilograms per centimeter after compression
2, according to 30m
3CO
2/ hm
3The speed of refined liquid, feeding amount feed first, second and third groove respectively, 3 hours resolving times, aluminum oxide rate of decomposition 90% in 50 ± 5%, 30 ± 5%, 20 ± 5% ratio successively.
Claims (3)
1. process for producing aluminium oxide by carbonating decomposation, carbonating by refined sodium aluminate solution is decomposed, filtration and washing, three operations of Aluminium hydroxide roasting of decomposing rear slurry constitute, it is characterized in that, the refined sodium aluminate solution that described carbonating is decomposed continuously feeds series connection carbon and divides first groove of groove group, each decomposer of then flowing through successively, after finishing decomposition, slurries are discharged by the last step decomposer.
2. according to the described technology of claim 1, it is characterized in that the alumina content of refined sodium aluminate solution to be decomposed is a 85-125 gram/liter, causticization coefficient 1.35-1.65, temperature is 80 ℃-95 ℃, the gas concentration lwevel of feeding is 20m
3-40m
3/ hour, feeding speed is successively decreased by groove since first groove, and last groove does not feed carbonic acid gas, and the residence time of refined liquid in decomposer is 2-4 hour, and wherein in the end the residence time of a groove is 0.5-1.0 hour.
3. according to claim 1 or 2 described technologies, it is characterized in that described series connection decomposer is made up of 4-6 groove.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 97106190 CN1217295A (en) | 1997-11-07 | 1997-11-07 | Process for producing aluminium oxide by carbonating decomposation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 97106190 CN1217295A (en) | 1997-11-07 | 1997-11-07 | Process for producing aluminium oxide by carbonating decomposation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1217295A true CN1217295A (en) | 1999-05-26 |
Family
ID=5168455
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 97106190 Pending CN1217295A (en) | 1997-11-07 | 1997-11-07 | Process for producing aluminium oxide by carbonating decomposation |
Country Status (1)
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|---|---|
| CN (1) | CN1217295A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326511A (en) * | 2014-10-17 | 2015-02-04 | 石河子大学 | Nano metal oxide powder and preparation method thereof |
| CN108455640A (en) * | 2018-01-31 | 2018-08-28 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | A kind of preparation facilities and preparation method of aluminium hydroxide |
-
1997
- 1997-11-07 CN CN 97106190 patent/CN1217295A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326511A (en) * | 2014-10-17 | 2015-02-04 | 石河子大学 | Nano metal oxide powder and preparation method thereof |
| CN108455640A (en) * | 2018-01-31 | 2018-08-28 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | A kind of preparation facilities and preparation method of aluminium hydroxide |
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