CN102009991A - Method for producing aluminum oxide by Bayer process - Google Patents
Method for producing aluminum oxide by Bayer process Download PDFInfo
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- CN102009991A CN102009991A CN 201010614016 CN201010614016A CN102009991A CN 102009991 A CN102009991 A CN 102009991A CN 201010614016 CN201010614016 CN 201010614016 CN 201010614016 A CN201010614016 A CN 201010614016A CN 102009991 A CN102009991 A CN 102009991A
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- Prior art keywords
- bauxite
- alkali
- aluminum oxide
- reduced
- liquor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Links
- 238000004131 Bayer process Methods 0.000 title claims abstract description 23
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 title abstract description 32
- 238000004519 manufacturing process Methods 0.000 title abstract description 12
- 229910001570 bauxite Inorganic materials 0.000 claims abstract description 40
- 238000000034 method Methods 0.000 claims abstract description 26
- 239000002002 slurry Substances 0.000 claims abstract description 25
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 14
- 238000005406 washing Methods 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 50
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 21
- 239000011707 mineral Substances 0.000 claims description 21
- 238000010790 dilution Methods 0.000 claims description 16
- 239000012895 dilution Substances 0.000 claims description 16
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 13
- 238000007701 flash-distillation Methods 0.000 claims description 9
- 239000006210 lotion Substances 0.000 claims description 8
- 239000003513 alkali Substances 0.000 abstract description 67
- 238000007670 refining Methods 0.000 abstract description 11
- 238000005516 engineering process Methods 0.000 abstract description 10
- 238000001704 evaporation Methods 0.000 abstract description 5
- 230000008020 evaporation Effects 0.000 abstract description 5
- 239000012452 mother liquor Substances 0.000 abstract description 4
- 230000029087 digestion Effects 0.000 abstract 4
- 238000003113 dilution method Methods 0.000 abstract 1
- 239000007787 solid Substances 0.000 abstract 1
- 239000000203 mixture Substances 0.000 description 27
- 239000003518 caustics Substances 0.000 description 21
- 229910001648 diaspore Inorganic materials 0.000 description 11
- 239000012071 phase Substances 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000013055 pulp slurry Substances 0.000 description 6
- 229910052814 silicon oxide Inorganic materials 0.000 description 6
- 239000007790 solid phase Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000035515 penetration Effects 0.000 description 4
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000012065 filter cake Substances 0.000 description 3
- 229910001679 gibbsite Inorganic materials 0.000 description 3
- 229910021502 aluminium hydroxide Inorganic materials 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 210000000582 semen Anatomy 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000012795 verification Methods 0.000 description 2
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 230000001925 catabolic effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000005432 seston Substances 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
Landscapes
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention discloses a method for producing aluminum oxide by a Bayer process and relates to improvement of increasing slurry concentration with back feeding bauxite digestion technology during an aluminum oxide production process. The method is characterized by comprising the following steps: adding gibbsite-type bauxite to a flash evaporation process; increasing Rp of the digested bauxite slurry after the convergence to 1.30-1.35; adding decomposition mother liquor or flat plate washing liquor with Rp of 0.10-0.60 in the dilution process; reducing the Rp of the crude liquor to 1.15-1.18; and refining the crude liquor. In the method provided by the invention, a method of adding alkali after bauxite sweetening is adopted, thus the solid content of back feeding bauxite is effectively increased; and as the alkali liquor is added after the digestion, so that the amount of the alkali liquor involved in the back feeding bauxite digestion is remarkably reduced, and the bauxite slurry reduced ratio of a back feeding bauxite system is effectively reduced, thus the steam consumption of the back feeding bauxite digestion is reduced. Through the invention, the capacity of a single system of the Bayer process can be further increased, a system of the Bayer process is maximized, the power consumption and the evaporation steam consumption are reduced, and the high-quality operation of the system is maintained; and besides, the sustainable stable operation of the high-yield situation is ensured while the system capacity is increased.
Description
Technical field
A kind of method of alumina producing Bayer process, relate in the aluminum oxide production process after add the improvement of ore deposit enrichment dissolving-out process.
Background technology
In alumina producing Bayer process technology, by after add ore deposit enrichment dissolving-out technology and handle gibbsitic bauxite, can make Al in the dissolved mineral slurry Rp(sodium aluminate solution
2O
3With Na
2The mass ratio of O) be increased to more than 1.30 by about 1.10, experiment shows: add the import gibbsitic bauxite at stripping Na
2The balance Rp that can reach when 0k concentration is 180 ~ 220g/l is 1.30 ~ 1.36.But the thick liquid Rp that can pass through smoothly owing to thick liquid refining system in the subsequent production process is up to 1.18 ~ 1.20.Because at present, thick liquid refining system major equipment is a leaf filter, when thick liquid Rp greater than 1.18 the time, filter cakes of leaf filter is hard, the difficulty of unloading, the filter cloth cycle is short, and the brush car is frequent, influences system's throughput.For guaranteeing system stable operation, require to control about dissolved mineral slurry Rp1.20, limited system's production capacity.
Summary of the invention
Purpose of the present invention is exactly the deficiency that exists at above-mentioned prior art, provide a kind of and can solve effectively that filter cakes of leaf filter is hard, the difficulty of unloading, filter cloth cycle be short, and the brush car is frequent, the method for the alumina producing Bayer process of restriction system production capacity problem.
The objective of the invention is to be achieved through the following technical solutions.
A kind of method of alumina producing Bayer process, it is characterized in that formerly adding gibbsitic bauxite in the flash distillation operation, the Rp of back, interflow dissolved mineral slurry is carried to 1.30-1.35, again in dilution, adding Rp is decomposition nut liquid or the square position washing lotion of 0.10-0.60, the Rp of thick liquid is reduced to 1.15-1.18, carry out thick liquid again and make with extra care.
A kind of alumina producing Bayer process method of the present invention, add the Process configuration that the ore deposit adds alkali again after the employing, promptly in alumina producing Bayer process technology, find a suitable point of penetration, earlier by after add ore deposit enrichment stripping dissolved mineral slurry Rp carried to 1.30-1.35, by behind the dilution pit, adding part decomposition nut liquid or the square position washing lotion that Rp is 0.10-0.60 thick liquid Rp is reduced to 1.15-1.18 again, overcome at follow-up thick liquid refining system and just pass through difficult bottleneck problem greater than 1.18, the high quality operation of assurance Bayer process system because of thick liquid Rp.The add-on that adds alkali in the alkali process after the adjusting guarantees that thick liquid Rp will take into account thick liquid refining system when can not shine into negative impact to thick liquid refining system operating mode liquid measure passes through, and really accomplishes sustainable stable the carrying out of system's high yield situation.
Experiment of the present invention shows that during bauxite stripping Na20k concentration 180g/l, dissolved mineral slurry balance Rp is 1.30, and during stripping Na20k concentration 220g/l, dissolved mineral slurry balance Rp is 1.36, and stripping balance Rp improves along with the raising of stripping Na20k concentration.Add experimental verification by calculating and stripping Rp can be reduced to 1.15-1.18 at dilution pit interpolation part decomposition nut liquid.Add after the employing and add the alkali technology behind the ore deposit and can bring following benefit:
(1) add the ore deposit after can further improving and contain admittedly, alkali lye adds after stripping simultaneously, and the alkali lye amount that adds the ore deposit stripping after the participation significantly reduces, and adds system ore pulp reduced ratio in ore deposit after effectively reducing, thereby adds the ore deposit stripping steam consumption after reducing.
(2) production capacity of Bayer process individual system further improves, and has realized the maximization of Bayer process system, reduces the power consumption and the evaporation steam consumption, has kept the high quality operation of system.
(3) add the ore deposit system after and steam the about 2t/t-Al of the water yield
2O
3, the about 0.65 t/t-Al of the low pressure steam consumption
2O
3, add the alkali technology and add the ore deposit after adopting after again, by control washing amount of water, after add the ore deposit system and steam the water yield and can be reduced to 1.4 ~ 1.5 t/t-Al
2O
3, the low pressure steam consumption can reduce by 0.15 ~ 0.20 t/t-Al
2O
3
A kind of method of alumina producing Bayer process, add the Process configuration that the ore deposit adds alkali again after the employing: promptly in alumina producing Bayer process technology, find a suitable point of penetration, earlier by after add ore deposit enrichment stripping dissolved mineral slurry Rp carried to 1.30 ~ 1.36, be that 0.10 ~ 0.60 part decomposition nut liquid or square position washing lotion are reduced to 1.15-1.18 with thick liquid Rp by add Rp behind the pit in dilution again, overcome at follow-up thick liquid refining system and just pass through difficult bottleneck problem greater than 1.18, the high quality operation of assurance Bayer process system because of thick liquid Rp.After add alkali in the alkali process add-on need suitably to adjust according to dissolved mineral slurry Rp, guarantee that thick liquid Rp will take into account thick liquid refining system when can not shine into negative impact to thick liquid refining system operating mode liquid measure passes through, really accomplish sustainable stable the carrying out of system's high yield situation.
Experiment of the present invention shows that during bauxite stripping Na20k concentration 180g/l, dissolved mineral slurry balance Rp is 1.30, and during stripping Na20k concentration 220g/l, dissolved mineral slurry balance Rp is 1.36, and stripping balance Rp improves along with the raising of stripping Na20k concentration.Add experimental verification by calculating and stripping Rp can be reduced to 1.15-1.18 at dilution pit interpolation part decomposition nut liquid.Add after the employing and add the alkali technology behind the ore deposit and can bring following benefit:
(1) add the ore deposit after can further improving and contain admittedly, alkali lye adds after stripping simultaneously, and the alkali lye amount that adds the ore deposit stripping after the participation significantly reduces, and adds system ore pulp reduced ratio in ore deposit after effectively reducing, thereby adds the ore deposit stripping steam consumption after reducing.
(2) production capacity of Bayer process individual system further improves, and has realized the maximization of Bayer process system, reduces the power consumption and the evaporation steam consumption, has kept the high quality operation of system.
(3) add the ore deposit system after and steam the about 2t/t-Al of the water yield
2O
3, the about 0.65 t/t-Al of the low pressure steam consumption
2O
3, add the alkali technology and add the ore deposit after adopting after again, by control washing amount of water, after add the ore deposit system and steam the water yield and can be reduced to 1.4 ~ 1.5 t/t-Al
2O
3, the low pressure steam consumption can reduce by 0.15 ~ 0.20 t/t-Al
2O
3
Embodiment
A kind of method of alumina producing Bayer process, it is characterized in that formerly adding gibbsitic bauxite in the flash distillation operation, the Rp of back, interflow dissolved mineral slurry is carried to 1.30-1.35, again in dilution, adding Rp is decomposition nut liquid or the square position washing lotion of 0.10-0.60, the Rp of thick liquid is reduced to 1.15-1.18, carry out thick liquid again and make with extra care.
The method of a kind of alumina producing Bayer process of the present invention, its concrete operations step of producing alumina process comprises that (1) utilizes the grinding machine equipment bauxite that broken homogenizing is good (comprising diaspore bauxite and gibbsite bauxite) to grind respectively and makes ore pulp; (2) by ore pulp allotment means ore pulp and circulation alkali liquor are mixed with concentration, contain admittedly and proportioning meets the qualified ore pulp of stripping requirement; (3) the qualified ore pulp of diaspore bauxite carries out stripping in digester.(4) the follow-up connection flash process of stripping reclaims the heat that process in leaching produces; Flash distillation operation in the suitable gibbsite stripping of temperature, pressure is a point of penetration, adds gibbsite bauxite ore pulp, and two kinds of ores are at this point of penetration interflow, and last step flash distillation discharging is as dissolved mineral slurry; (5) dissolved mineral slurry through the dilution become the dilution ore pulp enter the settlement separate stage.(6) isolating overflow is referred to as thick liquid and enters thick liquid refining step and utilize leaf filter to remove most of seston to make it to become qualified seminal fluid; (7) seminal fluid enters the seed decomposition process and obtains aluminum hydroxide slurry.Obtain the required seed of catabolic phase, aluminium hydroxide and mother liquor through separation means; (8) Aluminium hydroxide roasting obtains aluminum oxide, and mother liquor becomes next Bayer process round-robin circulating mother liquor by evaporation and alkali liquor preparing means.
The thick liquid refining system of step (6) is strict to thick liquid Rp's, when thick liquid Rp greater than 1.18 the time, can unload firmly because of leaf filter filter cake and frequently cause liquid measure to pass through difficulty.Influence the further raising of total system output.
Method of the present invention (is the gibbsitic bauxite that step 4) adds volume in the flash distillation operation earlier, the Rp of back, interflow dissolved mineral slurry is carried to 1.30-1.35, again by in dilution, adding Rp is that decomposition nut liquid or the square position washing lotion of 0.10-0.60 reduced to 1.15-1.18 with thick liquid Rp, carries out thick liquid again and makes with extra care.
Embodiment 1
The qualified pulp slurry phase composition of diaspore type bauxite: full alkali: the 127.4g/l aluminum oxide: 29.6g/l caustic alkali: 98.0g/l contains 792g/l solid phase composition admittedly: aluminum oxide: 58.60% silicon oxide: 7.73%
Circulation alkali liquor composition: full alkali: 265.0g/l aluminum oxide: 125.98g/l caustic alkali: 234.0g/l Rp:0.538
The qualified ore pulp of circulation alkali liquor and diaspore type bauxite is carried out stripping, ore pulp after the diaspore type bauxite stripping (promptly adding before the gibbsitic bauxite) composition by 2.90 proportioning configuration: full alkali: 227.0g/l aluminum oxide: 211.51g/l caustic alkali: 198.0g/l Rp:1.068
The qualified pulp slurry phase composition of gibbsitic bauxite: full alkali: the 144.20g/l aluminum oxide: 78.29g/l caustic alkali: 125g/l contains 618g/l solid phase composition admittedly: aluminum oxide: 47.20% silicon oxide: 10.37%
In the stripping flash distillation flow process of qualified ore pulp by the per hour flow adding running at full capacity of 80m3 with gibbsitic bauxite, the dissolved mineral slurry liquid composition behind the interflow is: full alkali: 220.7g/l aluminum oxide: 249.60g/l caustic alkali: 192.0g/l Rp:1.300
Decomposition nut liquid composition: full alkali: 187.0g/l aluminum oxide: 86.84g/l caustic alkali: the flow that 163.0g/l Rp:0.533 presses decomposition nut liquid per hour 35m3 adds in the dilution ore pulp in the dissolved mineral slurry dilution, and the final thick liquid composition of gained is: full alkali: 171.4g/l aluminum oxide: 175.00g/l caustic alkali: 150.0g/l Rp:1.167.Leaf filter throughput satisfies the production demand.
Embodiment 2
The qualified pulp slurry phase composition of diaspore type bauxite: full alkali: the 143.2g/l aluminum oxide: 45.4g/l caustic alkali: 106.0g/l contains 762g/l solid phase composition admittedly: aluminum oxide: 59.40% silicon oxide: 7.80%
Circulation alkali liquor composition: full alkali: 264.8g/l aluminum oxide: 122.36g/l caustic alkali: 230.0g/l Rp:0.532
The qualified ore pulp of circulation alkali liquor and diaspore type bauxite is carried out stripping, ore pulp after the diaspore type bauxite stripping (promptly adding before the gibbsitic bauxite) composition by 2.91 proportioning configuration: full alkali: 224.2g/l aluminum oxide: 203.61g/l caustic alkali: 192.0g/l Rp:1.060
The qualified pulp slurry phase composition of gibbsitic bauxite: full alkali: the 163.2g/l aluminum oxide: 86.18g/l caustic alkali: 132.0g/l contains 593g/l solid phase composition admittedly: aluminum oxide: 47.20% silicon oxide: 15.30%
In the stripping flash distillation flow process of qualified ore pulp by the per hour flow adding running at full capacity of 90m3 with gibbsitic bauxite, the dissolved mineral slurry liquid composition behind the interflow is: full alkali: 223.0g/l aluminum oxide: 249.01g/l caustic alkali: 188.0g/l Rp:1.325
Decomposition nut liquid composition: full alkali: 190.2g/l aluminum oxide: 94.20g/l caustic alkali: the flow that 157.0g/l Rp:0.600 presses decomposition nut liquid per hour 42m3 adds in the dilution ore pulp in the dissolved mineral slurry dilution, and the final thick liquid composition of gained is: full alkali: 184.0g/l aluminum oxide: 184.1g/l caustic alkali: 156.0g/l Rp:1.180.Leaf filter throughput satisfies the production demand.
Embodiment 3
The qualified pulp slurry phase composition of diaspore type bauxite: full alkali: the 126.8g/l aluminum oxide: 32.89g/l caustic alkali: 93.0g/l contains 804g/l solid phase composition admittedly: aluminum oxide: 59.70% silicon oxide: 7.49%
Circulation alkali liquor composition: full alkali: 273.1g/l aluminum oxide: 125.16g/l caustic alkali: 235.0g/l Rp:0.533
The qualified ore pulp of circulation alkali liquor and diaspore type bauxite is carried out stripping, ore pulp after the diaspore type bauxite stripping (promptly adding before the gibbsitic bauxite) composition by 2.86 proportioning configuration: full alkali: 225.0g/l aluminum oxide: 208.88g/l caustic alkali: 191.0g/l Rp:1.094
The qualified pulp slurry phase composition of gibbsitic bauxite: full alkali: the 151.6g/l aluminum oxide: 84.21g/l caustic alkali: 126.0g/l contains 612g/l solid phase composition admittedly: aluminum oxide: 47.60% silicon oxide: 15.46%
In the stripping flash distillation flow process of qualified ore pulp by the per hour flow adding running at full capacity of 86m3 with gibbsitic bauxite, the dissolved mineral slurry liquid composition behind the interflow is: full alkali: 226.0g/l aluminum oxide: 257.39g/l caustic alkali: 189.2g/l Rp:1.357
Square position washing lotion composition: full alkali: 36.0g/l aluminum oxide: 3.4g/l caustic alkali: the flow that 32.3g/l Rp:0.105 presses the square position washing lotion per hour 14m3 adds in the dilution ore pulp in the dissolved mineral slurry dilution, and the final thick liquid composition of gained is: full alkali: 188.0g/l aluminum oxide: 182.0g/l caustic alkali: 158.0g/l Rp:1.152.Leaf filter throughput satisfies the production demand.
Claims (1)
1. the method for an alumina producing Bayer process, it is characterized in that formerly adding gibbsitic bauxite in the flash distillation operation, the Rp of back, interflow dissolved mineral slurry is carried to 1.30-1.35, again in dilution, adding Rp is decomposition nut liquid or the square position washing lotion of 0.10-0.60, the Rp of thick liquid is reduced to 1.15-1.18, carry out thick liquid again and make with extra care.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010614016 CN102009991A (en) | 2010-12-30 | 2010-12-30 | Method for producing aluminum oxide by Bayer process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010614016 CN102009991A (en) | 2010-12-30 | 2010-12-30 | Method for producing aluminum oxide by Bayer process |
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| Publication Number | Publication Date |
|---|---|
| CN102009991A true CN102009991A (en) | 2011-04-13 |
Family
ID=43840351
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|---|---|---|---|
| CN 201010614016 Pending CN102009991A (en) | 2010-12-30 | 2010-12-30 | Method for producing aluminum oxide by Bayer process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106564920A (en) * | 2016-11-07 | 2017-04-19 | 中国铝业股份有限公司 | Method for increasing bayer process seed decomposition rate |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1160679A (en) * | 1996-11-15 | 1997-10-01 | 山西铝厂 | Primary mineral pulp preparation process in Baeyer's alumina producing process |
| CN1775686A (en) * | 2005-12-15 | 2006-05-24 | 中国铝业股份有限公司 | Method for producing alumina by adding ore and concentrating after hydraulic aluminous stone type bauxite stripping |
| CN1865145A (en) * | 2005-05-19 | 2006-11-22 | 贵阳铝镁设计研究院 | Batching process after leaching in alumina production |
| CN101219803A (en) * | 2007-12-11 | 2008-07-16 | 中国铝业股份有限公司 | Bauxite dissolving out technique |
-
2010
- 2010-12-30 CN CN 201010614016 patent/CN102009991A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1160679A (en) * | 1996-11-15 | 1997-10-01 | 山西铝厂 | Primary mineral pulp preparation process in Baeyer's alumina producing process |
| CN1865145A (en) * | 2005-05-19 | 2006-11-22 | 贵阳铝镁设计研究院 | Batching process after leaching in alumina production |
| CN1775686A (en) * | 2005-12-15 | 2006-05-24 | 中国铝业股份有限公司 | Method for producing alumina by adding ore and concentrating after hydraulic aluminous stone type bauxite stripping |
| CN101219803A (en) * | 2007-12-11 | 2008-07-16 | 中国铝业股份有限公司 | Bauxite dissolving out technique |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106564920A (en) * | 2016-11-07 | 2017-04-19 | 中国铝业股份有限公司 | Method for increasing bayer process seed decomposition rate |
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Application publication date: 20110413 |