CN117069130A - Method for reducing new steam consumption in alumina production - Google Patents
Method for reducing new steam consumption in alumina production Download PDFInfo
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- CN117069130A CN117069130A CN202310849262.4A CN202310849262A CN117069130A CN 117069130 A CN117069130 A CN 117069130A CN 202310849262 A CN202310849262 A CN 202310849262A CN 117069130 A CN117069130 A CN 117069130A
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- Prior art keywords
- dissolution
- new steam
- sent
- alumina production
- temperature
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Links
- 238000000034 method Methods 0.000 title claims abstract description 67
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 30
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 238000004090 dissolution Methods 0.000 claims abstract description 45
- 238000001704 evaporation Methods 0.000 claims abstract description 41
- 230000008020 evaporation Effects 0.000 claims abstract description 37
- 230000008569 process Effects 0.000 claims abstract description 37
- 239000012452 mother liquor Substances 0.000 claims abstract description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 33
- 238000002156 mixing Methods 0.000 claims abstract description 12
- 230000009467 reduction Effects 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 238000010790 dilution Methods 0.000 claims abstract description 8
- 239000012895 dilution Substances 0.000 claims abstract description 8
- 239000003513 alkali Substances 0.000 claims abstract description 7
- 238000000227 grinding Methods 0.000 claims abstract description 7
- 230000001172 regenerating effect Effects 0.000 claims abstract description 7
- 238000011143 downstream manufacturing Methods 0.000 claims abstract description 6
- 238000005406 washing Methods 0.000 claims description 6
- 210000000582 semen Anatomy 0.000 claims description 4
- 238000007865 diluting Methods 0.000 claims description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 12
- 238000001816 cooling Methods 0.000 description 7
- 230000029087 digestion Effects 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000010413 mother solution Substances 0.000 description 5
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 4
- 239000011550 stock solution Substances 0.000 description 4
- 229910001570 bauxite Inorganic materials 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
Classifications
-
- 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
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
- C01F7/0606—Making-up the alkali hydroxide solution from recycled spent liquor
-
- 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
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
- C01F7/062—Digestion
Abstract
A method for reducing new steam consumption in alumina production belongs to the technical field of alumina production, and comprises the following steps: the low-temperature mother liquor is sent to an alkali liquor blending process after heat exchange and temperature rise with refined liquid, the blended circulating mother liquor is respectively sent to a raw ore pulp grinding process and a pre-desilication process, the raw ore pulp is also sent to the pre-desilication process after grinding, the pre-desilication ore pulp is mixed with the circulating mother liquor and then sent to a dissolution process, the dissolution process is sequentially heated to dissolution temperature by using dissolution exhaust steam, new steam condensate water and new steam, the dissolution ore pulp is sent to a downstream process after flash evaporation and pressure reduction and dilution, the new steam condensate water is sent to a regenerative power plant after flash evaporation and temperature reduction, and flash steam is merged into a low-pressure steam pipe network. The invention can reduce the comprehensive steam consumption of alumina production, simplify the production flow and reduce the circulating water consumption of alumina production.
Description
Technical Field
The invention belongs to the technical field of alumina production, and particularly relates to a method for reducing new steam consumption in alumina production.
Background
The digestion process and the mother liquor evaporation process are both important processes in the production of alumina. The leaching step is to heat the leached ore pulp to make it react at certain temperature. The mother liquor evaporation procedure is to make the mother liquor meet the alkali concentration requirement of the circulating mother liquor at the selected dissolution temperature by evaporating and thickening the mother liquor.
The mother liquor evaporation procedure generally adopts the following production process (taking a seven-effect falling film evaporator as an example): a part of the evaporation stock solution sequentially enters a VII and VI effect evaporator for heating evaporation, and VI effect discharging is used as a section of evaporation mother solution; and the other part of the evaporation stock solution sequentially enters a V-IV-III-II-I effect evaporator for heating and evaporating step by step, the I effect discharging material is subjected to flash evaporation, cooling and evaporation through a first-fifth-stage self-evaporator, the fifth-stage self-evaporator discharging material is used as a second-stage evaporation mother solution, and the second-stage evaporation mother solution and the first-stage evaporation mother solution are sent to an evaporation mother solution tank. The low-pressure steam from the pipe network heats the I-effect evaporator, the generated secondary steam is heated step by the II-VII-effect evaporators, and the final-effect secondary steam is condensed by a water cooler.
This method has the following disadvantages: the last effect secondary steam enters the water cooler and needs a vacuum pump to be vacuumized, and meanwhile, a large amount of circulating water is needed for cooling the secondary steam. About 20 to 25 percent of water enters the water cooler after each 1t of water is evaporated from the evaporation stock solution, the heat carried by the steam is about 520 to 650MJ, and 9 to 11t of circulating water is consumed to condense the water. The heat carried by the final-effect secondary steam is not effectively utilized, and the transportation and cooling of the circulating water also need additional consumption of electric energy.
Disclosure of Invention
In order to solve the problems, the invention provides a method for reducing the steam consumption, which can not only reduce the comprehensive steam consumption in the production of aluminum oxide, but also simplify the production flow and reduce the circulating water consumption in the production of aluminum oxide.
In order to achieve the above purpose, the main technical scheme adopted by the invention comprises the following steps:
a method for reducing new steam consumption in alumina production, comprising the following steps: the low-temperature mother liquor is sent to an alkali liquor blending process after heat exchange and temperature rise with refined liquid, the blended circulating mother liquor is respectively sent to a raw ore pulp grinding process and a pre-desilication process, the pre-desilication ore pulp is mixed with the circulating mother liquor and then sent to a dissolution process, the dissolution process is sequentially heated to a dissolution temperature by using dissolution exhaust steam, new steam condensate water and new steam, the dissolution ore pulp is sent to a downstream process after flash evaporation, depressurization, temperature reduction and dilution, the new steam condensate water is sent to a regenerative power plant after flash evaporation, temperature reduction, and flash steam is integrated into a low-pressure steam pipe network.
Further, the concentration of the circulating mother liquor is 145-170 g/L.
Further, the concentration of the semen is 140-160g/L.
Further, the dissolution step adopts high-temperature dissolution, and the dissolution temperature is 260-300 ℃.
Further, the flash evaporation stage number of the ore pulp is 10-14.
Further, the pulp molecular ratio after the dissolution in the dissolution process is 1.25-1.40.
Further, the pre-desilication temperature is in the range of 75-95 ℃.
Further, the dilution is mixed with the washing liquid and diluted to Na 2 O k The concentration range is 140-160g/L.
Further, the molecular ratio of the pulp after dilution is 1.30-1.32.
And further, the new steam condensate is subjected to flash evaporation and temperature reduction to 150-170 ℃ and then is sent to a regenerative power plant.
The beneficial effects of the invention are as follows:
the invention omits the mother liquor evaporation process, reduces the concentration of circulating mother liquor by increasing the dissolution temperature, reduces the amount of evaporation water required by the system, and reduces the unit consumption of alumina steam and the consumption of circulating water by evaporating all the evaporation water through the dissolution process. The method solves the problem of high comprehensive steam consumption of the aluminum oxide produced by the prior high-temperature dissolution, can reduce the steam consumption of the aluminum oxide production, reduce the consumption of circulating water, improve the dissolution feeding temperature, and avoid the increase of new dissolution steam consumption caused by the increase of the dissolution feeding quantity.
Drawings
Fig. 1 is a schematic process diagram of embodiment 1 and embodiment 2 of the present invention.
Detailed Description
The invention will be better explained by the following detailed description of the embodiments with reference to the drawings.
The invention provides a method for reducing new steam consumption in alumina production, which is shown in figure 1 and comprises the following steps: the low-temperature mother liquor 1 (namely raw evaporation stock solution) is cooled by seminal fluid 2 to be heated to obtain high-temperature mother liquor 3, the high-temperature mother liquor is sent to an alkali liquor preparation 4 process, the prepared circulating mother liquor 5 is respectively sent to an original ore pulp grinding 7 and a pre-desilication 9 process, ore pulp 8 of bauxite 6 after being ground by the original ore pulp is also sent to the pre-desilication 9 process, the pre-desilication ore pulp is mixed with the circulating mother liquor and then sent to a dissolution 10 process, the dissolution process is sequentially heated to a dissolution temperature by using dissolution exhaust steam, new steam condensate water and new steam, the dissolution ore pulp is sent to a downstream process after flash evaporation, depressurization and dilution, the new steam condensate water is sent to a regenerative power plant after flash evaporation and cooling, and flash steam is merged into a low-pressure steam pipe network.
Wherein the concentration of the circulating mother liquor is 145-170 g/L; the concentration of the semen is 140-160g/L; the dissolution process adopts high-temperature dissolution, and the dissolution temperature is 260-300 ℃; the flash evaporation stage number of the ore pulp is 10-14; the molecular ratio of ore pulp after the dissolution in the dissolution step is 1.25-1.40; the temperature range of the pre-desilication is 75-95 ℃; the dilution is carried out by mixing with washing liquid and diluting to Na 2 O k The concentration range is 140-160g/L; the molecular ratio of the diluted ore pulp is 1.30-1.32; and the new steam condensate is subjected to flash evaporation and temperature reduction to 150-170 ℃ and then is sent to a regenerative power plant.
Example 1
A method for reducing new steam consumption in alumina production comprises the following steps: selecting bauxite in a mining area of Guinea, heating seed precipitation mother liquor by heat exchange with refined liquor, delivering to alkali liquor blending procedure, and blending to obtain circulating mother liquor Na 2 O k The concentration was 152g/L. The circulating mother liquor is respectively sent to the grinding and pre-desilication working procedures of raw ore pulp, and the pre-desilication temperature is 75 ℃. Mixing the pre-desilication ore pulp and the circulating mother liquor, pumping to a dissolution process by using a diaphragm pump, heating to a dissolution temperature of 280 ℃ by using dissolved exhaust steam, new steam condensate water and new steam in sequence,the leached ore pulp is subjected to 11-stage flash evaporation, depressurization and temperature reduction, and then is mixed with red mud washing liquid to be diluted to Na 2 O k The slurry a with the concentration of about 143g/L is sent to the downstream process k And 1.32, carrying out flash evaporation on the new steam condensate water, cooling to 158 ℃, and then sending the new steam condensate water back to the heat recovery power plant, wherein the flash steam is merged into a low-pressure steam pipe network. The new steam consumption of the stripping process is 1.521t/t-Al 2 O 3 Can provide 158 ℃ steam of 0.297t/t-Al 2 O 3 Reduced steam consumption of 1.224t/t-Al 2 O 3 . Compared with the conventional process, the steam consumption is reduced by 0.295t/t-Al 2 O 3 The consumption of circulating water is reduced by 11.2t/t-Al 2 O 3 。
Example 2
A method for reducing new steam consumption in alumina production comprises the following steps: selecting bauxite in a certain mining area in Australia, heating seed precipitation mother liquor by heat exchange with refined liquor, delivering to alkali liquor blending procedure, and blending to obtain circulating mother liquor Na 2 O k The concentration was 159g/L. The circulating mother liquor is respectively sent to the grinding and pre-desilication working procedures of raw ore pulp, and the pre-desilication temperature is 95 ℃. Mixing pre-desilication ore pulp and circulating mother liquor, pumping to a digestion process by using a diaphragm pump, sequentially heating the digestion process to a digestion temperature of 290 ℃ by using digestion exhaust steam, new steam condensate water and new steam, and mixing and diluting the digestion ore pulp with red mud washing liquid and aluminum hydroxide washing liquid to Na after 12-level flash evaporation, depressurization and cooling 2 O k The mixture with the concentration of 147g/L is sent to the downstream process, and the pulp a is leached k And 1.30, carrying out flash evaporation on the new steam condensate water, cooling to 158 ℃, and then sending the new steam condensate water back to the heat recovery power plant, wherein the flash steam is merged into a low-pressure steam pipe network. The new steam consumption of the stripping procedure is 1.611t/t-Al 2 O 3 Can provide 158 ℃ steam of 0.357t/t-Al 2 O 3 Reduced steam consumption of 1.254t/t-Al 2 O 3 . Compared with the conventional process, the steam consumption is reduced by 0.366t/t-Al 2 O 3 The consumption of circulating water is reduced by 10.8t/t-Al 2 O 3 。
The invention aims to solve the problem of high steam consumption in alumina production caused by energy loss caused by the fact that the final-effect secondary steam of a mother liquor evaporation process enters a water cooler, and reduces the concentration of circulating mother liquor by increasing the dissolution temperature and the steam quantity required by a system, and the whole steam quantity passes through dissolutionEvaporating in the working procedure, further eliminating the mother liquor evaporating working procedure, and reducing the unit consumption of alumina steam by 0.2-0.5 t/t-Al 2 O 3 The consumption of circulating water is reduced by 10 to 25t/t-Al 2 O 3 。
While embodiments of the present invention have been shown and described above, it should be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that alterations, modifications, substitutions and variations may be made by those of ordinary skill in the art without departing from the scope of the invention.
Claims (10)
1. A method for reducing new steam consumption in alumina production, comprising the steps of: the low-temperature mother liquor is sent to an alkali liquor blending process after heat exchange and temperature rise with refined liquid, the blended circulating mother liquor is respectively sent to a raw ore pulp grinding process and a pre-desilication process, the pre-desilication ore pulp is mixed with the circulating mother liquor and then sent to a dissolution process, the dissolution process is sequentially heated to a dissolution temperature by using dissolution exhaust steam, new steam condensate water and new steam, the dissolution ore pulp is sent to a downstream process after flash evaporation, depressurization, temperature reduction and dilution, the new steam condensate water is sent to a regenerative power plant after flash evaporation, temperature reduction, and flash steam is integrated into a low-pressure steam pipe network.
2. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the concentration of the circulating mother liquor is 145-170 g/L.
3. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the concentration of the semen is 140-160g/L.
4. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the dissolution process adopts high-temperature dissolution, and the dissolution temperature is 260-300 ℃.
5. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the flash evaporation stage number of the ore pulp is 10-14.
6. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the molecular ratio of ore pulp after the dissolution in the dissolution step is 1.25-1.40.
7. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the temperature range of the pre-desilication is 75-95 ℃.
8. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the dilution is carried out by mixing with washing liquid and diluting to Na 2 O k The concentration range is 140-160g/L.
9. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: the molecular ratio of the diluted ore pulp is 1.30-1.32.
10. A method for reducing new steam consumption in alumina production as defined in claim 1, wherein: and the new steam condensate is subjected to flash evaporation and temperature reduction to 150-170 ℃ and then is sent to a regenerative power plant.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310849262.4A CN117069130A (en) | 2023-07-12 | 2023-07-12 | Method for reducing new steam consumption in alumina production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310849262.4A CN117069130A (en) | 2023-07-12 | 2023-07-12 | Method for reducing new steam consumption in alumina production |
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|---|---|
| CN117069130A true CN117069130A (en) | 2023-11-17 |
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| CN202310849262.4A Pending CN117069130A (en) | 2023-07-12 | 2023-07-12 | Method for reducing new steam consumption in alumina production |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101638240A (en) * | 2008-07-29 | 2010-02-03 | 贵阳铝镁设计研究院 | Process for dissolving alkali and adding alkali for aluminium oxide plant |
| CN103101940A (en) * | 2011-11-14 | 2013-05-15 | 沈阳铝镁设计研究院有限公司 | Method for reducing water evaporating volume of system |
| CN103101938A (en) * | 2011-11-14 | 2013-05-15 | 沈阳铝镁设计研究院有限公司 | Method for reducing steam consumption in evaporation process |
| CN103101947A (en) * | 2013-03-11 | 2013-05-15 | 茌平信发华宇氧化铝有限公司 | Digesting process for aluminum oxide production process |
| WO2015165152A1 (en) * | 2014-04-30 | 2015-11-05 | 东北大学 | Calcification-carbonization process-based method for producing aluminum oxide without evaporation |
| CN107915243A (en) * | 2017-12-30 | 2018-04-17 | 贵阳铝镁设计研究院有限公司 | The hybrid technique equipment and its technological process of evaporation and twin driving composition |
| CN110817915A (en) * | 2019-11-25 | 2020-02-21 | 沈阳铝镁设计研究院有限公司 | Method and device for reducing steam consumption in alumina production |
| CN111661859A (en) * | 2020-07-10 | 2020-09-15 | 中铝山东工程技术有限公司 | Evaporation and dissolution integrated process equipment and process flow thereof |
-
2023
- 2023-07-12 CN CN202310849262.4A patent/CN117069130A/en active Pending
Patent Citations (8)
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| CN101638240A (en) * | 2008-07-29 | 2010-02-03 | 贵阳铝镁设计研究院 | Process for dissolving alkali and adding alkali for aluminium oxide plant |
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| WO2015165152A1 (en) * | 2014-04-30 | 2015-11-05 | 东北大学 | Calcification-carbonization process-based method for producing aluminum oxide without evaporation |
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| CN110817915A (en) * | 2019-11-25 | 2020-02-21 | 沈阳铝镁设计研究院有限公司 | Method and device for reducing steam consumption in alumina production |
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