CN201668968U - Energy-saving system for five-tower three-stage differential-pressure distilling production of edible alcohol - Google Patents
Energy-saving system for five-tower three-stage differential-pressure distilling production of edible alcohol Download PDFInfo
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- CN201668968U CN201668968U CN2010202017235U CN201020201723U CN201668968U CN 201668968 U CN201668968 U CN 201668968U CN 2010202017235 U CN2010202017235 U CN 2010202017235U CN 201020201723 U CN201020201723 U CN 201020201723U CN 201668968 U CN201668968 U CN 201668968U
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- 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
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Abstract
The utility model discloses an energy-saving system for the five-tower three-stage differential-pressure distilling production of edible alcohol. The system mainly comprises a rectifying tower (1), a water scrubbing tower (13), a crude distillation tower (26), a methanol tower (35) and an impurity tower (42); in the energy-saving system, the rectifying tower (1) is heated by using primary steam; alcohol steam at the tower top of the rectifying tower (1) heats the water scrubbing tower (13), the methanol tower (35) and the crude distillation tower (26) sequentially and progressively; alcohol steam at the tower tops of the water scrubbing tower (13) and the methanol tower (35) heats the crude distillation tower (26) respectively; alcohol steam at the tower top of the crude distillation tower (26) is used as a first-stage preheating heat source of fermented liquor; lees at the bottom of the crude distillation tower (26) are used as a second-stage preheating heat source of the fermented liquor; and secondary steam after the flash distillation of the condensed water of the primary steam heats the impurity tower (42).
Description
Technical field
The utility model belongs to the alcohol preparation field, relates to the alcohol distillation power-saving technology, particularly a kind of energy conserving system of producing edible ethanol by five-tower three-stage differential distillation.
Background technology
At present, the distillation technique of domestic representative production edible alcohol is to introduce French SPEICHIM technology the nineties, and this technology steam consumption is a 2.9t/t alcohol.But, along with country to the carrying forward vigorously of energy-saving and emission-reduction principles and policies, and the demand of Alcohol Production enterprise to increasing economic efficiency reduces energy resource consumption and becomes the research emphasis that edible ethanol is produced in distillation.
Summary of the invention
The purpose of this utility model is to provide a kind of five column distillations to produce the edible ethanol energy conserving system, and the utilizable energy source that can make full use of in the Alcohol Production makes its abundant coupling, thereby distillation is significantly reduced with vapour, to reach energy-saving and cost-reducing effect.
In order to reach above-mentioned utility model purpose, the utility model is achieved by the following technical solutions.
A kind of energy conserving system of producing edible ethanol by five-tower three-stage differential distillation, based on above-mentioned power-economizing method, this energy conserving system comprises that rectifying column, rectifying column reboiler, rectifying column return tank, rectifying column coagulate water pot, water scrubber, water scrubber reboiler, water scrubber return tank, topping still, topping still first reboiler, topping still second reboiler, topping still the 3rd reboiler, methanol column, methanol column reboiler, methanol column return tank, impurity tower, flash tank;
It is characterized in that,
The shell side inlet of described rectifying column reboiler is communicated with primary steam, its outlet is coagulated water pot, flash tank by the pipeline rectifying column of connecting successively, the top exit of described flash tank enters the mouth by the middle and lower part that pipeline is communicated with the impurity tower, and the middle and upper part outlet of impurity tower is communicated with the water scrubber return tank by pipeline;
The top wine vapor outlet of described rectifying column is by pipeline connect the successively shell side of water scrubber reboiler, the shell side of methanol column reboiler, the shell side of topping still first reboiler, the wine vapour condensate outlet of the shell side of the shell side of the shell side of described water scrubber reboiler, methanol column reboiler, topping still first reboiler is communicated with the rectifying column return tank by pipeline respectively, and the rectifying column return tank is communicated with the middle and upper part inlet of rectifying column by pipeline; The outlet at bottom of described rectifying column enters the mouth by first middle and upper part that pipeline is communicated with water scrubber, and the centre exit of described rectifying column is communicated with the centre entrance of impurity tower by pipeline;
The top wine vapor outlet of described water scrubber is communicated with the shell side inlet of topping still second reboiler by pipeline, and the shell side outlet of topping still second reboiler is by connect successively second middle and upper part inlet of water scrubber return tank, water scrubber of pipeline; The outlet at bottom of water scrubber is communicated with the centre entrance of rectifying column by pipeline;
The top wine vapor outlet of described methanol column is communicated with the shell side inlet of topping still the 3rd reboiler by pipeline, and the shell side outlet of topping still the 3rd reboiler is by connect the successively middle and upper part inlet of methanol column return tank, methanol column of pipeline.
The further characteristics of technique scheme are: the top wine vapor outlet of described topping still is communicated with the thermal source inlet of a mash wine vapour preheater, and the thermal source outlet of mash wine vapour preheater is communicated with the shell side inlet of a topping still condenser; The outlet at bottom of described topping still is communicated with the thermal source inlet of a mash vinasse preheater, and the mash vinasse are discharged in the thermal source outlet of mash vinasse preheater; Fermenting-ripening wine with dregs raw material feeds the refrigerant inlet of mash wine vapour preheater, and the refrigerant exit of mash wine vapour preheater is communicated with the refrigerant inlet of mash vinasse preheater, and the refrigerant exit of mash vinasse preheater is communicated with the middle and upper part inlet of topping still; The wine vapour condensate outlet of described mash wine vapour preheater, the outlet of the shell side of topping still condenser are communicated with thick wine jar by pipeline respectively, the top outlet of thick wine jar is communicated with the shell side inlet of topping still condenser, and the lower part outlet of thick wine jar is communicated with the centre entrance of water scrubber.
The further characteristics of technique scheme are: the lower part outlet of described thick wine jar is by being communicated with the centre entrance of water scrubber behind the crude wine preheater, and the thermal source inlet of crude wine preheater is serially connected between first middle and upper part inlet of the outlet at bottom of rectifying column and water scrubber.The shell side outlet of described topping still condenser is provided with scrubbing tower.
Because in the utility model, rectifying column uses the primary steam heating; Rectifying column cat head wine vapour heats water scrubber, methanol column and topping still step by step successively; Water scrubber and methanol column cat head wine vapour heat topping still respectively; Topping still cat head wine vapour is as the first order preheating thermal source of fermentation liquid; Topping still bottom vinasse are as the second level preheating thermal source of fermentation liquid; The indirect steam heating impurity tower of the condensate water of primary steam after flash distillation.The various energy are coupled effective and reasonablely, thereby make edible ethanol distillation steam consumption, reduce to 2.3 tons of steam/ton ethanol by 2.9 tons of steam of present advanced international level/ton ethanol, steam consumption saves 21%.Calculate to produce 100000 tons of Alcohol Plants per year, 60,000 tons of year saving steam are equivalent to save 9,000,000 yuan of Alcohol Production costs (150 yuan of/ton steam).
Description of drawings
Below in conjunction with the drawings and specific embodiments the utility model is described in further detail.
Fig. 1 is the principle schematic of the energy conserving system of a kind of producing edible ethanol by five-tower three-stage differential distillation of the present utility model;
Wherein: 1, rectifying column; 2, rectifying column reboiler; 3, rectifying column coagulates water pot; 4, rectifying column condensate pump; 5, rectifying column waste water pump; 6, thick wine jar; 7, thick wine pump; 8, crude wine preheater; 9, rectifying column condenser; 10, rectifying column return tank; 11, rectifying column reflux pump; 12, water scrubber reboiler; 13, water scrubber; 14, rectifying column feed pump; 15, vinasse pump; 16, water scrubber reflux pump; 17, water scrubber return tank; 18, water scrubber condenser; 19, topping still second reboiler; 20, mash vinasse preheater; 21, mash wine vapour preheater; 22, topping still condenser; 23, scrubbing tower; 24, vavuum pump; 25, topping still second circulating pump; 26, topping still; 27, topping still the 3rd circulating pump; 28, topping still the 3rd reboiler; 29, methanol column return tank; 30, methanol column condenser; 31, methanol column reflux pump; 32, topping still first circulating pump; 33, topping still first reboiler; 34, methanol column reboiler; 35, methanol column; 36, alcohol pump; 37, impurity tower return tank; 38, impurity tower condenser; 39, impurity tower reflux pump; 40, impurity tower condensate pump; 41, flash tank; 42, impurity tower; 43, impurity tower waste water pump.
The specific embodiment
With reference to Fig. 1, be the energy conserving system of a kind of producing edible ethanol by five-tower three-stage differential distillation of the present utility model, comprise that mainly rectifying column 1, rectifying column reboiler 2, rectifying column return tank 10, rectifying column coagulate water pot 3, water scrubber 13, water scrubber reboiler 12, water scrubber return tank 17, topping still 26, topping still first reboiler 33, topping still second reboiler 19, topping still the 3rd reboiler 28, methanol column 35, methanol column reboiler 34, methanol column return tank 29, impurity tower 42, flash tank 41; And with rectifying column return tank 10, water scrubber return tank 17, methanol column return tank 29, impurity tower return tank 37, thick wine jar 6 corresponding rectifying column condensers 9, water scrubber condenser 18, methanol column condenser 30, impurity tower condenser 38, topping still condenser 22 and a plurality of kinetic pumps of matching.
The shell side inlet of rectifying column reboiler 2 is communicated with the primary steam from the boiler room, its outlet is coagulated water pot 3, flash tank 41 by the pipeline rectifying column of connecting successively, the condensate water of flash tank 41 is got back to the boiler room, the top exit of flash tank 41 enters the mouth by the middle and lower part that pipeline is communicated with impurity tower 42, and the indirect steam of flash tank 41 feeds impurity tower 42.The middle and upper part outlet of impurity tower 42 is communicated with water scrubber return tank 17 by pipeline.
The top wine vapor outlet of rectifying column 1 is by pipeline connect the successively shell side of water scrubber reboiler 12, the shell side of methanol column reboiler 34, the shell side of topping still first reboiler 33.The wine vapour condensate outlet of the shell side of the shell side of the shell side of water scrubber reboiler 12, methanol column reboiler 34, topping still first reboiler 33 is connected to the middle and upper part inlet of rectifying column 1 respectively by the pipeline rectifying column return tank 10 that imports in parallel by rectifying column reflux pump 11, pipeline by the wine liquid outlet of rectifying column return tank 10.Rectifying column return tank 10 is connected with rectifying column condenser 9, incoagulability wine vapour is communicated to rectifying column condenser 9 shell sides inlet by rectifying column return tank 10 top exits, the outlet of rectifying column condenser 9 shell sides is connected to rectifying column return tank 10 tops inlet, carries out wine vapour and reclaims.
The tower bottom outlet of rectifying column 1 is connected to the thermal source inlet of crude wine preheater 8 by rectifying column waste water pump 5, pipeline, the surplus water that heats up in a steamer of rectifying column flows out from the thermal source outlet of crude wine preheater 8, a part is removed spice, and another part is back to first middle and upper part inlet of water scrubber 13.The centre exit of rectifying column 1 is communicated with the centre entrance of impurity tower 42 by pipeline.
The top wine vapor outlet of water scrubber 13 is communicated with the shell side inlet of topping still second reboiler 19, the shell side outlet of topping still second reboiler 19 is communicated with the charging aperture of water scrubber return tank 17, and condensation wine liquid is communicated with the second middle and upper part inlet of water scrubber reflux pump 16 to water scrubber 13 through the discharging opening of water scrubber return tank 17.The wine vapor outlet of water scrubber return tank 17 connects the shell side inlet of water scrubber condenser 18, and wine vapour condensate liquid connects back water scrubber return tank 17 through the shell side outlet of water scrubber condenser 18.
The top wine vapor outlet of methanol column 35 is connected to the shell side inlet of topping still the 3rd reboiler 28 by pipeline, the shell side outlet of topping still the 3rd reboiler 28 enters the mouth by the wine liquid that pipeline is connected to methanol column return tank 29, and the wine liquid outlet of methanol column return tank 29 is connected to the middle and upper part inlet of methanol column 35 through methanol column reflux pump 31, pipeline.The wine vapor outlet of methanol column return tank 29 enters the mouth by the shell side that pipeline is connected to methanol column condenser 30, and the shell side outlet of methanol column condenser 30 is communicated to methanol column return tank 29 by pipeline with wine vapour condensate liquid.The outlet of methanol column 35 middle and lower parts connects alcohol pump 36, extracts the edible ethanol finished product out.
The top wine vapor outlet of topping still 26 is communicated with the thermal source inlet of mash wine vapour preheater 21, and the thermal source outlet of mash wine vapour preheater 21 is communicated with the shell side inlet of topping still condenser 22; The outlet at bottom of topping still 26 is communicated with the thermal source inlet of mash vinasse preheater 20, and the thermal source outlet of mash vinasse preheater 20 is discharged the mash vinasse to the DDGS workshop; Feed the refrigerant inlet of mash wine vapour preheater 21 from the fermenting-ripening wine with dregs raw material of fermentation workshop section, the refrigerant exit of mash wine vapour preheater 21 is communicated with the refrigerant inlet of mash vinasse preheater 20, and the refrigerant exit of mash vinasse preheater 20 is communicated with the middle and upper part inlet of topping still 26; The wine vapour condensate outlet of mash wine vapour preheater 21, the outlet of the shell side of topping still condenser 22 are respectively by the thick wine jar 6 of pipeline remittance in parallel, the top outlet of thick wine jar 6 is communicated with the shell side inlet of topping still condenser 22, the lower part outlet of thick wine jar 6 enters the mouth by the refrigerant that thick wine pump 7, pipeline connect crude wine preheater 8, and crude wine preheater 8 refrigerant exits are communicated with the centre entrance of water scrubber 13.The shell side outlet of topping still condenser 22 is provided with scrubbing tower 23, and the middle and upper part inlet of scrubbing tower 23 feeds a water, and the top exit of scrubbing tower 23 connects vavuum pump 24 by pipeline.
Impurity tower 42 top wine vapor outlets are communicated with the shell side inlet of impurity tower condenser 38, the shell side outlet of impurity tower condenser 38 is communicated with impurity tower return tank 37 inlets, 37 outlets of impurity tower return tank are communicated with impurity tower 42 middle and upper parts inlet by impurity tower reflux pump 39, pipeline, and the middle and upper part outlet of impurity tower 42 is communicated with water scrubber return tank 17 by pipeline.Impurity tower 42 outlet at bottoms connect impurity tower waste water pump 43, and its waste water is sent to spice.The centre exit of rectifying column 1 is by the centre entrance of pipeline connection impurity tower, impurity tower 42 centre exit extraction fusel oil.Impurity tower 42 centre exit pipelines are connected to fusel oil separator (not drawing).
Rectifying column 1 and rectifying column reboiler 2, water scrubber 13 and water scrubber reboiler 12, topping still 26, with topping still first reboiler 33, topping still second reboiler 19, topping still the 3rd reboiler 28, be known connection, be specially: an end of the tube side of reboiler is communicated with a middle and lower part inlet of corresponding column, and the other end of tube side is communicated with an outlet at bottom of corresponding column.
In the utility model, rectifying column 1 uses the primary steam heating; Rectifying column 1 cat head wine vapour heats water scrubber 13, methanol column 35 and topping still 26 step by step successively; Water scrubber 13 and methanol column 35 cat head wine vapour heat topping still 26 respectively; Topping still 26 cat head wine vapour are as the first order preheating thermal source of fermentation liquid; Topping still 26 bottom vinasse are as the second level preheating thermal source of fermentation liquid; The indirect steam heating impurity tower 42 of the condensate water of primary steam after flash distillation; Wherein: 165-170 ℃ of primary steam temperature, pressure 0.65-0.8Mpa; Rectifying column 1 bottom temp 157-159 ℃, head temperature 133-135 ℃; Water scrubber 13 bottom temp 123-125 ℃, head temperature 93-95 ℃; Topping still 26 bottom temp 83-85 ℃, head temperature 69-71 ℃; Methanol column 35 bottom temp 117-119 ℃, head temperature 93-95 ℃; Impurity tower 42 bottom temp 103-105 ℃, head temperature 78-80 ℃.
The concrete technology of present embodiment is: fermenting-ripening wine with dregs (30 ℃) is pumped into mash wine vapour preheater 21, carry out the one-level heat exchange with the wine vapour that comes from topping still 26.Mash after the heat exchange enters mash vinasse preheater 20 and carries out the secondary heat exchange, and the thermal source of secondary heat exchange comes from the vinasse at the bottom of topping still 26 towers, and vinasse are sent into mash vinasse preheater 20 through vinasse pump 15, and the vinasse after the heat exchange are sent into the DDGS workshop.Be about 78 ℃ through the mash temperature after the two-stage heat exchange and enter the topping still middle and upper part.The uncooled gas of mash wine vapour preheater 21 wine vapour enters the 22 further condensations of topping still condenser together with the wine vapour of thick wine jar 6, and final uncooled gas enters scrubbing tower 23 by after the direct condensation of water, and fixed gas is through vavuum pump 24 emptyings.The wine liquid that mash wine vapour preheater 21, mash topping still condenser 22 and scrubbing tower 23 are discharged flows into thick wine jar 6, thick wine pumps into crude wine preheater 8 through thick wine pump 7, pump into crude wine preheater 8 by rectifying column waste water pump 5 and carry out heat exchange with heat up in a steamer water from rectifying column 1 bottom surplus, the thick wine after the heat exchange enters water scrubber 13 middle parts.The surplus water part of heating up in a steamer after the heat exchange is gone to water scrubber 13 middle and upper parts, and another part removes spice between alcohol-fueled car.Rectifying column 1 top wine vapour is connected successively by water scrubber reboiler 12 heating water scrubbers 13, again by methanol column reboiler 34 heating methanol towers 35, again by topping still first reboiler 33 heating topping stills 26.
Rectifying column 1 adopts the primary steam from boiler to heat by rectifying column reboiler 2, the primary steam condensate water enters rectifying column and coagulates water pot 3, enter flash tank 41 by rectifying column condensate pump 4, flash tank 41 indirect steams heating impurity tower 42, the secondary condensate water is sent boiler back to through impurity tower condensate pump 40.
Water scrubber 13 top wine vapour are by topping still second reboiler 19 heating topping stills 26.Methanol column 35 top wine vapour are by topping still the 3rd reboiler 28 heating topping stills 26, its alcohol condensate liquid flows into methanol column return tank 29, pass back into methanol column 35 tops by methanol column reflux pump 31, wine vapour in the methanol column return tank 29 is back to methanol column return tank 29 again by after 30 condensations of methanol column condenser.
The wine liquid of being discharged by water scrubber reboiler 12, methanol column reboiler 34, topping still first reboiler 33 flows into rectifying column return tank 10, send into rectifying column 1 middle and upper part by rectifying column reflux pump 11, the wine vapour in the rectifying column return tank 10 is by flowing into rectifying column return tank 10 after 9 condensations of rectifying column condenser.Water scrubber 13 bottom light wine are sent into rectifying column 1 centre entrance by rectifying column feed pump 14.
Topping still 26 bottom alcohol distiller's solutions constitute closed circuit circulatory system one by topping still first circulating pump 32, topping still first reboiler 33 with topping still 26; Topping still 26 bottom alcohol distiller's solutions constitute closed circuit circulatory system two by topping still second circulating pump 25, topping still second reboiler 19 with topping still 26.Topping still 26 bottom alcohol distiller's solutions constitute closed circuit circulatory system three by topping still the 3rd circulating pump 27, topping still the 3rd reboiler 28 with topping still 26.
Edible ethanol is extracted out from methanol column 35 middle and lower parts by finished wine sperm pump 36.Impurity tower 42 cat head wine vapour are sent into impurity tower 42 middle and upper parts through impurity tower reflux pump 39 again by flowing into impurity tower return tank 37 after 38 condensations of impurity tower condenser.Impurity tower 42 bottom waste water are sent to spice through impurity tower waste water pump 43.Water scrubber return tank 17 is delivered in the 42 middle and upper part alcohol quantitative extraction of impurity tower.Rectifying column 1 middle part is rich in fusel oil alcohol and is flowed into impurity tower 42 centre entrances.Impurity tower 42 centre exit extraction fusel oil.
In the present embodiment, 165-170 ℃ of primary steam temperature, pressure 0.65-0.8Mpa; About 158 ℃ of rectifying column 1 bottom temp, about 134 ℃ of head temperature; About 124 ℃ of water scrubber 13 bottom temps, about 94 ℃ of head temperature; About 84 ℃ of topping still 26 bottom temps, about 70 ℃ of head temperature; About 118 ℃ of methanol column 35 bottom temps, about 94 ℃ of head temperature; About 104 ℃ of impurity tower 42 bottom temps, about 79 ℃ of head temperature.Because present embodiment is coupled the various energy effective and reasonablely, thereby edible ethanol distillation steam consumption is reduced, reduce to 2.3 tons of steam/ton ethanol by 2.9 tons of steam of present advanced international level/ton ethanol, steam consumption saves 21%.Calculate to produce 100000 tons of Alcohol Plants per year, 60,000 tons of year saving steam are equivalent to save 9,000,000 yuan of Alcohol Production costs (150 yuan of/ton steam).
Claims (4)
1. the energy conserving system of a producing edible ethanol by five-tower three-stage differential distillation comprises that rectifying column (1), rectifying column reboiler (2), rectifying column return tank (10), rectifying column coagulate water pot (3), water scrubber (13), water scrubber reboiler (12), water scrubber return tank (17), topping still (26), topping still first reboiler (33), topping still second reboiler (19), topping still the 3rd reboiler (28), methanol column (35), methanol column reboiler (34), methanol column return tank (29), impurity tower (42), flash tank (41);
It is characterized in that,
The shell side inlet of described rectifying column reboiler (2) is communicated with primary steam, its outlet is coagulated water pot (3), flash tank (41) by the pipeline rectifying column of connecting successively, the top exit of described flash tank (41) enters the mouth by the middle and lower part that pipeline is communicated with impurity tower (42), and the middle and upper part outlet of impurity tower (42) is communicated with water scrubber return tank (17) by pipeline;
The top wine vapor outlet of described rectifying column (1) is by pipeline connect the successively shell side of water scrubber reboiler (12), the shell side of methanol column reboiler (34), the shell side of topping still first reboiler (33), the wine vapour condensate outlet of the shell side of the shell side of the shell side of described water scrubber reboiler (12), methanol column reboiler (34), topping still first reboiler (33) is communicated with rectifying column return tank (10) by pipeline respectively, and rectifying column return tank (10) is communicated with the middle and upper part inlet of rectifying column (1) by pipeline; The outlet at bottom of described rectifying column (1) enters the mouth by first middle and upper part that pipeline is communicated with water scrubber (13), and the centre exit of described rectifying column (1) is communicated with the centre entrance of impurity tower (42) by pipeline;
The top wine vapor outlet of described water scrubber (13) is communicated with the shell side inlet of topping still second reboiler (19) by pipeline, and the shell side outlet of topping still second reboiler (19) is by connect successively second middle and upper part inlet of water scrubber return tank (17), water scrubber (13) of pipeline; The outlet at bottom of water scrubber (13) is communicated with the centre entrance of rectifying column (1) by pipeline;
The top wine vapor outlet of described methanol column (35) is communicated with the shell side inlet of topping still the 3rd reboiler (28) by pipeline, and the shell side outlet of topping still the 3rd reboiler (28) is by connect the successively middle and upper part inlet of methanol column return tank (29), methanol column (35) of pipeline.
2. the energy conserving system of producing edible ethanol by five-tower three-stage differential distillation according to claim 1, it is characterized in that, the top wine vapor outlet of described topping still (26) is communicated with the thermal source inlet of a mash wine vapour preheater (21), and the thermal source outlet of mash wine vapour preheater (21) is communicated with the shell side inlet of a topping still condenser (22); The outlet at bottom of described topping still (26) is communicated with the thermal source inlet of a mash vinasse preheater (20), and the mash vinasse are discharged in the thermal source outlet of mash vinasse preheater (20); Fermenting-ripening wine with dregs raw material feeds the refrigerant inlet of mash wine vapour preheater (21), the refrigerant exit of mash wine vapour preheater (21) is communicated with the refrigerant inlet of mash vinasse preheaters (20), and the refrigerant exit of mash vinasse preheater (20) is communicated with the middle and upper part inlet of topping still (26); The wine vapour condensate outlet of described mash wine vapour preheater (21), the outlet of the shell side of topping still condenser (22) are communicated with a thick wine jar (6) by pipeline respectively, the top outlet of thick wine jar (6) is communicated with the shell side inlet of topping still condenser (22), and the lower part outlet of thick wine jar (6) is communicated with the centre entrance of water scrubber.
3. the energy conserving system of producing edible ethanol by five-tower three-stage differential distillation according to claim 2, it is characterized in that, the lower part outlet of described thick wine jar (6) is communicated with the centre entrance of water scrubber (13) by a crude wine preheater (8) back, and the thermal source gateway of crude wine preheater (8) is serially connected between first middle and upper part inlet of the outlet at bottom of rectifying column (1) and water scrubber (13).
4. the energy conserving system of producing edible ethanol by five-tower three-stage differential distillation according to claim 2 is characterized in that, the shell side outlet of described topping still condenser (22) is provided with scrubbing tower (3).
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| CN2010202017235U CN201668968U (en) | 2010-05-24 | 2010-05-24 | Energy-saving system for five-tower three-stage differential-pressure distilling production of edible alcohol |
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| CN2010202017235U CN201668968U (en) | 2010-05-24 | 2010-05-24 | Energy-saving system for five-tower three-stage differential-pressure distilling production of edible alcohol |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101851149A (en) * | 2010-05-24 | 2010-10-06 | 中国轻工业西安设计工程有限责任公司 | Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation |
| CN104262090A (en) * | 2014-09-22 | 2015-01-07 | 江苏九天高科技股份有限公司 | Method and device for producing biomass absolute ethyl alcohol |
| WO2021213552A1 (en) * | 2020-04-21 | 2021-10-28 | 广东高科生物工程有限公司 | Multi-column differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method |
-
2010
- 2010-05-24 CN CN2010202017235U patent/CN201668968U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101851149A (en) * | 2010-05-24 | 2010-10-06 | 中国轻工业西安设计工程有限责任公司 | Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation |
| CN104262090A (en) * | 2014-09-22 | 2015-01-07 | 江苏九天高科技股份有限公司 | Method and device for producing biomass absolute ethyl alcohol |
| WO2021213552A1 (en) * | 2020-04-21 | 2021-10-28 | 广东高科生物工程有限公司 | Multi-column differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method |
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Granted publication date: 20101215 |