CN114524446A - Two-stage evaporation low-temperature-section independent operation process for aluminum oxide production - Google Patents
Two-stage evaporation low-temperature-section independent operation process for aluminum oxide production Download PDFInfo
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- CN114524446A CN114524446A CN202011323839.0A CN202011323839A CN114524446A CN 114524446 A CN114524446 A CN 114524446A CN 202011323839 A CN202011323839 A CN 202011323839A CN 114524446 A CN114524446 A CN 114524446A
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- 238000001704 evaporation Methods 0.000 title claims abstract description 50
- 230000008020 evaporation Effects 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 28
- 230000008569 process Effects 0.000 title claims abstract description 28
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 title claims abstract description 10
- 238000004519 manufacturing process Methods 0.000 title description 10
- 230000000694 effects Effects 0.000 claims abstract description 95
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000011550 stock solution Substances 0.000 claims description 36
- 238000010438 heat treatment Methods 0.000 claims description 23
- 238000009835 boiling Methods 0.000 claims description 13
- 230000001965 increasing effect Effects 0.000 claims description 13
- 230000009467 reduction Effects 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 239000012153 distilled water Substances 0.000 claims 2
- 238000012423 maintenance Methods 0.000 description 12
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 11
- 238000004140 cleaning Methods 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
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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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a two-section evaporation low-temperature section independent operation process for producing aluminum oxide, wherein operation equipment comprises an evaporator first-effect evaporator, an evaporator second-effect evaporator, an evaporator third-effect evaporator and an evaporator fourth-effect evaporator which are connected by a pipeline, a pump and a valve, wherein the evaporator first-effect evaporator, the evaporator second-effect evaporator, the evaporator third-effect evaporator and the evaporator fourth-effect evaporator are arranged on one side of a boundary of the two-section evaporator; a water cooler is connected to an output pipeline of the seven-effect evaporator; a primary flash evaporator is arranged on a pipeline between the first effect of the evaporator and the third effect of the evaporator; a secondary flash evaporator is connected to the primary flash evaporator output pipeline, a tertiary flash evaporator is arranged on the secondary flash evaporator output pipeline, and a quaternary flash evaporator is arranged on the tertiary flash evaporator output pipeline; the evaporator is provided with a high-temperature section feeding flowmeter in four effects. When the invention operates according to actual parameters, when the five-effect, six-effect and seven-effect evaporators work, the feeding amount of the evaporators can reach 65 percent, and the concentration can be ensured.
Description
Technical Field
The invention relates to a two-stage evaporation low-temperature section independent operation process for producing aluminum oxide, belonging to the technical field of aluminum oxide production.
Background
With the continuous improvement of the alumina production technology, equipment gradually becomes large-scale, regular maintenance of the equipment is also a regulated action of each large alumina enterprise, and the compression maintenance time is also one of the measures for improving the yield and enhancing the efficiency of each large alumina enterprise. At present, the unit maintenance time of the single unit capacity of the domestic alumina enterprise within 50 ten thousand tons of annual capacity is controlled within 18 hours in the shortest way, and the cleaning and maintenance time of an evaporator can not break through 22 hours. The maintenance time of a single unit with 80 ten thousand tons of annual production is controlled within 30 hours, which provides a new challenge for the cleaning and maintenance of the evaporator.
At present, because the carbon emission is strictly controlled by China, various energy-saving measures are adopted by various alumina production enterprises to reduce energy consumption as much as possible, as the alumina enterprises, the steam consumption of an evaporation process accounts for one third of the energy consumption of alumina, the energy-saving measure of the evaporation process is a key process for developing energy conservation and consumption reduction of the alumina enterprises, the energy-saving measure of the evaporation process is also a key process for increasing the effect number of an evaporator, namely a six-effect evaporator in the previous year is increased into a seven-effect evaporator, but when the effect number of the evaporator is increased, because of the particularity of sodium aluminate solution, a boiling point is increased in the evaporation process, so that the effect number of the evaporator is increased, the steam consumption is reduced, but the capacity of the evaporator is reduced, and in order to obtain the same capacity as the six-effect evaporator, the heat exchange area of the evaporator is increased by 40%, therefore, the area of the evaporator is increased, and the maintenance and cleaning time required by the evaporator in the off-production maintenance time is greatly increased, if other measures are not taken into consideration, the upsizing of the evaporator is difficult to realize, or the cleaning and overhauling time of the whole alumina production is determined by the cleaning and overhauling time of the evaporation process, so the production is influenced to a large extent.
Disclosure of Invention
The invention aims to provide a two-stage evaporation low-temperature section independent operation process for producing alumina, so as to better perform alumina production organization, reduce cost, save energy and overcome the defects in the background technology.
In order to achieve the above object, the present invention has the following technical means.
A two-section evaporation low-temperature section independent operation process for producing aluminum oxide is characterized in that an evaporator first-effect evaporator, an evaporator second-effect evaporator, an evaporator third-effect evaporator and an evaporator fourth-effect evaporator are arranged on one side of a boundary line of two sections of evaporators and connected through pipelines, pumps and valves, and an evaporator fifth-effect evaporator, an evaporator sixth-effect evaporator and an evaporator seventh-effect evaporator are connected through pipelines, pumps and valves; a water cooler is connected to an output pipeline of the seven-effect evaporator; a primary flash evaporator is arranged on a pipeline between the first effect of the evaporator and the third effect of the evaporator; a secondary flash evaporator is connected to the primary flash evaporator output pipeline, a tertiary flash evaporator is arranged on the secondary flash evaporator output pipeline, and a quaternary flash evaporator is arranged on the tertiary flash evaporator output pipeline; a high-temperature section feeding flowmeter is arranged on the evaporator in four effects; a low-temperature section feeding flowmeter is arranged on the five-effect evaporator; a heat exchanger is arranged on a pipeline between the four-stage flash evaporator and the seven-effect evaporator.
The two-stage evaporation low-temperature section independent operation process for producing the aluminum oxide based on the equipment comprises the following specific flows:
(1) the heating heat source of the first effect of the evaporator is new steam, stock solution in the first effect of the evaporator is boiled after obtaining heat through heat exchange to realize evaporation, the obtained steam is used as the heating heat source of the second effect of the evaporator and is used for heating the stock solution in the second effect of the evaporator to boil the stock solution in the second effect of the evaporator, the steam generated by the second effect of the evaporator is used as the heating heat source of the third effect of the evaporator to heat the stock solution in the third effect of the evaporator to boil the stock solution in the third effect of the evaporator, the secondary steam generated by the third effect of the evaporator is used as the heating heat source of the fourth effect of the evaporator to heat the stock solution in the fourth effect of the evaporator to boil the stock solution in the fourth effect of the evaporator to generate evaporation, and the like in turn until the seventh effect of the evaporator, and the secondary steam generated by the seventh effect of the evaporator enters the heat exchanger to directly condense circulating water to generate vacuum.
(2) Because the temperature of the new steam condensate water generated by the first effect of the evaporator is higher, the condensate water flash evaporator is utilized to carry out pressure reduction flash evaporation, the generated steam is also used as a part of heat source of the second effect of the evaporator, the condensate water of the second effect of the evaporator is also subjected to flash evaporation by the same flash evaporation principle, the generated steam is used as a part of heat source of the third effect of the evaporator, and the like is repeated until the seventh effect of the evaporator, and the condensate water of the seventh effect of the evaporator is sent away by a pump.
(3) When the stock solution enters the five-effect evaporator, the temperature of the stock solution exceeds the boiling point temperature of the five-effect evaporator, the stock solution with the temperature higher than the boiling point is generated by self-evaporation, and steam generated by the self-evaporation is also used as a part of a heating heat source of the six-effect evaporator. The five effects of the evaporator and the six effects of the evaporator are a downstream flow, the material entering the five effects of the evaporator exceeds the boiling point, the heating steam provided by the four effects of the evaporator is completely used for evaporation, the evaporation capacity of the five effects of the evaporator is greatly improved, and thus, the heating heat source capacity of the six effects of the evaporator is also greatly improved, so that the evaporation capacity of the six effects of the evaporator is greatly improved, meanwhile, the stock solution in the five effects of the evaporator enters the six effects of the evaporator downstream, the boiling point of the stock solution in the six effects of the evaporator is also exceeded, and a large amount of self-evaporation is generated, so that the purpose of improving the evaporation capacity is realized until the seven effects of the evaporator are discharged.
The invention has the beneficial effects that: the process scheme that the two-stage seven-effect double-countercurrent process flow and the two-stage seven-effect countercurrent process flow are compared fully, the steam stop cleaning and maintenance of the high-temperature section are realized on the two-stage seven-effect countercurrent process flow, the normal operation of the low-temperature section can be realized, the problem that the evaporator stops steam for a long time, the cleaning and maintenance of the low-temperature section can be effectively solved, the process flow is not changed greatly, only one pipeline (not less than phi 250) is connected onto a four-effect secondary steam pipe from a primary steam pipe, the effective operation of the low-temperature section of the evaporator can be ensured, the shutdown cleaning and maintenance of the high-temperature section evaporator is realized, the operation of a stripping unit is not influenced, and the once-stripped steam exhaust can be normally used by the low-temperature section evaporator. The process can ensure that the cleaning time of the first-effect evaporator, the second-effect evaporator and the third-effect evaporator is within 40 hours, and can completely ensure that the cleaning and maintenance work of the evaporators is finished with quality and quality guarantee. When the operation is carried out according to actual parameters, when the five-effect evaporator, the six-effect evaporator and the seven-effect evaporator work, the feeding amount of the evaporator can reach 65 percent, and the concentration can be ensured.
Drawings
FIG. 1 is a schematic of a process flow used in an embodiment of the present invention.
The notation in the figure is: 1. first effect of an evaporator; 2. the evaporator has two effects; 3. the evaporator has three effects; 4. the evaporator has four effects; 5. the evaporator has five effects; 6. six effects of an evaporator; 7. the evaporator has seven effects; 8. a water cooler; 9. a primary flash evaporator; 10. a secondary flash evaporator; 11. a three-stage flash evaporator; 12. a four-stage flash evaporator; 13. a high temperature section feed flow meter; 14. a low temperature section feed flow meter; 15. a heat exchanger; 16. two sections of evaporator boundaries.
Detailed Description
The following description of specific embodiments of the present invention is provided in order to better understand the present invention with reference to the accompanying drawings.
Examples
The operation equipment of the two-section evaporation low-temperature section independent operation process for producing the aluminum oxide shown in the figure 1 is that an evaporator first-effect 1, an evaporator second-effect 2, an evaporator third-effect 3 and an evaporator fourth-effect 4 are arranged on one side of a boundary line 16 of the two sections of evaporators and are connected by adopting a pipeline, a pump and a valve, and an evaporator fifth-effect 5, an evaporator sixth-effect 6 and an evaporator seventh-effect 7 are arranged on the other side of the boundary line and are connected by adopting a pipeline, a pump and a valve; the output pipeline of the evaporator seven-effect 7 is connected with a water cooler 8; a primary flash evaporator 9 is arranged on a pipeline between the first effect 1 of the evaporator and the third effect 3 of the evaporator; a secondary flash evaporator 10 is connected to an output pipeline of the primary flash evaporator 9, a tertiary flash evaporator 11 is arranged on an output pipeline of the secondary flash evaporator 10, and a quaternary flash evaporator 12 is arranged on an output pipeline of the tertiary flash evaporator 11; a high-temperature section feeding flowmeter 13 is arranged on the evaporator four-effect 4; a low-temperature section feeding flowmeter 14 is arranged on the evaporator five-effect 5; a heat exchanger 15 is arranged on a pipeline between the four-stage flash evaporator 12 and the seven-effect evaporator 7.
The two-stage evaporation low-temperature section independent operation process for producing the aluminum oxide based on the equipment comprises the following specific flows:
(1) the heating heat source of the first-effect evaporator 1 is new steam, stock solution in the first-effect evaporator is boiled after obtaining heat through heat exchange to realize evaporation, the obtained steam is used as the heating heat source of the second-effect evaporator 2 to heat the stock solution in the second-effect evaporator 2 so as to boil the stock solution in the second-effect evaporator 2, the steam generated by the second-effect evaporator 2 is used as the heating heat source of the third-effect evaporator 3 to heat the stock solution in the third-effect evaporator 3 so as to boil the stock solution in the third-effect evaporator 3, the secondary steam generated by the third-effect evaporator 3 is used as the heating heat source of the fourth-effect evaporator 4 to heat the stock solution in the fourth-effect evaporator 4 so as to boil the stock solution in the fourth-effect evaporator 4 to generate evaporation, and the rest is done until the seventh-effect evaporator 7, and the secondary steam generated by the seventh-effect evaporator 7 enters the heat exchanger 15 to generate vacuum through direct condensation of circulating water.
(2) Because the temperature of the new steam condensate water generated by the first-effect evaporator 1 is higher, the condensate water flash evaporator is used for pressure reduction flash evaporation, the generated steam is also used as a part of heat source of the second-effect evaporator 2, the condensate water of the second-effect evaporator 2 is also subjected to flash evaporation by the same flash evaporation principle, the generated steam is used as a part of heat source of the third-effect evaporator 3, and so on until the seventh-effect evaporator 7, and the condensate water of the seventh-effect evaporator 7 is pumped away.
(3) When the stock solution enters the five-effect evaporator 5, the temperature of the stock solution exceeds the boiling point temperature in the five-effect evaporator 5, the stock solution with the temperature higher than the boiling point is generated by self-evaporation, and steam generated by the self-evaporation is also used as a part of a heating heat source of the six-effect evaporator 6. The five-effect evaporator 5 and the six-effect evaporator 6 are downstream flows, the material entering the five-effect evaporator 5 exceeds the boiling point, the heating steam provided by the four-effect evaporator 4 is completely used for evaporation, the evaporation capacity of the five-effect evaporator 5 is greatly increased, and thus the heating heat source capacity of the six-effect evaporator 6 is also greatly increased, so that the evaporation capacity of the six-effect evaporator 6 is greatly increased, meanwhile, the stock solution in the five-effect evaporator 5 enters the six-effect evaporator 6 downstream, the boiling point of the stock solution in the six-effect evaporator 6 is also exceeded, a large amount of self-evaporation is generated, the purpose of increasing the evaporation capacity is achieved, and the same process is carried out until the seven-effect evaporator is discharged.
The following table is a list of evaporator parameters from which it can be seen that when operating according to the actual parameters in the list, the feed rate to the evaporator can reach 65% and the concentration can be guaranteed when the five, six or seven effect evaporators are operating.
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention.
Claims (2)
1. A two-stage evaporation low-temperature section independent operation process for producing aluminum oxide is characterized in that: the operation equipment is characterized in that a first evaporator effect, a second evaporator effect, a third evaporator effect and a fourth evaporator effect are arranged on one side of a boundary of two sections of evaporators and are connected through a pipeline, a pump and a valve, and a fifth evaporator effect, a sixth evaporator effect and a seventh evaporator effect are arranged on the other side of the boundary of the two sections of evaporators and are connected through a pipeline, a pump and a valve; a water cooler is connected to an output pipeline of the seven-effect evaporator; a primary flash evaporator is arranged on a pipeline between the first effect of the evaporator and the third effect of the evaporator; the primary flash evaporator output pipeline is connected with a secondary flash evaporator, a tertiary flash evaporator is arranged on the secondary flash evaporator output pipeline, and a quaternary flash evaporator is arranged on the tertiary flash evaporator output pipeline; a high-temperature section feeding flowmeter is arranged on the evaporator in four effects; a low-temperature section feeding flowmeter is arranged on the five-effect evaporator; and a heat exchanger is arranged on a pipeline between the four-stage flash evaporator and the seven-effect evaporator.
2. The process of claim 1, wherein the process comprises the following steps: the process is as follows:
(1) the heating heat source of the first effect of the evaporator is new steam, the stock solution in the first effect of the evaporator is boiled after obtaining heat through heat exchange to realize evaporation, the obtained steam is used as the heating heat source of the second effect of the evaporator and is used for heating the stock solution in the second effect of the evaporator to boil the stock solution in the second effect of the evaporator, the steam generated by the second effect of the evaporator is used as the heating heat source of the third effect of the evaporator to heat the stock solution in the third effect of the evaporator to boil the stock solution in the third effect of the evaporator, the secondary steam generated by the third effect of the evaporator is used as the heating heat source of the fourth effect of the evaporator to heat the stock solution in the fourth effect of the evaporator to boil the stock solution in the fourth effect of the evaporator to generate evaporation, and the like in turn until the seventh effect of the evaporator, and the secondary steam generated by the seventh effect of the evaporator enters the heat exchanger to directly condense through circulating water to generate vacuum;
(2) because the temperature of the new steam condensate water generated by the first effect of the evaporator is higher, the condensate water flash evaporator is utilized for pressure reduction flash evaporation, the generated steam is also used as a part of heat source of the second effect of the evaporator, the condensate water of the second effect of the evaporator is also subjected to flash evaporation by the same flash evaporation principle, the generated steam is used as a part of heat source of the third effect of the evaporator, and the like is repeated until the seventh effect of the evaporator is reached, and the condensate water of the seventh effect of the evaporator is sent away by a pump;
(3) when the stock solution enters the five-effect evaporator, the temperature of the stock solution exceeds the boiling point temperature in the five-effect evaporator, the stock solution with the temperature higher than the boiling point is generated by self-evaporation, and steam generated by the self-evaporation is also used as a part of a heating heat source of the six-effect evaporator; the five effects of the evaporator, the six effects of the evaporator and the seven effects of the evaporator are a downstream flow, the material entering the five effects of the evaporator exceeds the boiling point, the heating steam provided by the four effects of the evaporator is completely used for evaporation, the evaporation capacity of the five effects of the evaporator is greatly improved, and thus, the heating heat source capacity of the six effects of the evaporator is also greatly improved, so that the distilled water capacity of the six effects of the evaporator is greatly improved, and similarly, the distilled water capacity of the seven effects of the evaporator is greatly improved. Meanwhile, stock solution in the five effects of the evaporator enters the six effects of the evaporator downstream and exceeds the boiling point of the stock solution in the six effects of the evaporator, and a large amount of self-evaporation is generated, so that the purpose of increasing the evaporation water amount is realized until the seven effects of the evaporator discharge.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011323839.0A CN114524446A (en) | 2020-11-23 | 2020-11-23 | Two-stage evaporation low-temperature-section independent operation process for aluminum oxide production |
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| CN202011323839.0A CN114524446A (en) | 2020-11-23 | 2020-11-23 | Two-stage evaporation low-temperature-section independent operation process for aluminum oxide production |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105080169A (en) * | 2014-06-16 | 2015-11-25 | 瞿虹 | Two stage co-current and countercurrent flow alumina evaporation process flow |
| CN109865305A (en) * | 2017-12-01 | 2019-06-11 | 沈阳铝镁设计研究院有限公司 | One kind seven imitates evaporation technology |
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- 2020-11-23 CN CN202011323839.0A patent/CN114524446A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105080169A (en) * | 2014-06-16 | 2015-11-25 | 瞿虹 | Two stage co-current and countercurrent flow alumina evaporation process flow |
| CN109865305A (en) * | 2017-12-01 | 2019-06-11 | 沈阳铝镁设计研究院有限公司 | One kind seven imitates evaporation technology |
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Application publication date: 20220524 |