CN101851149A - Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation - Google Patents
Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation Download PDFInfo
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Abstract
The invention discloses an energy-saving method and an energy-saving system for producing edible ethanol by five-tower three-stage differential distillation. The system mainly comprises a rectifying tower (1), a water washing tower (13), a coarse distillation tower (26), a methanol tower (35) and an impurity tower (42). In the energy-saving method, the rectifying tower (1) is heated by using primary steam; the tower top alcohol steam of the rectifying tower (1) gradually heats the water washing tower (13), the methanol tower (35) and the coarse distillation tower (26) in turn; the tower top alcohol steam of the water washing tower (13) and the tower top alcohol steam of the methanol tower (35) heat the coarse distillation tower (26) respectively; the tower top alcohol steam of the coarse distillation tower (26) is used as a primary pre-heating heat source for fermented liquor; the bottom vinasse of the coarse distillation tower (26) is used as a secondary pre-heating heat source for the fermented liquor; and the secondary steam after the condensed water of the primary steam is flashed heats the impurity tower (42).
Description
Technical field
The invention belongs to the alcohol preparation field, relate to the alcohol distillation power-saving technology, particularly a kind of power-economizing method of producing edible ethanol by five-tower three-stage differential distillation and energy conserving system.
Background technology
At present, the distillation technique of domestic representative production edible ethanol 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 consumption and becomes the research emphasis that edible ethanol is produced in distillation.
Summary of the invention
The object of the present invention is to provide a kind of five column distillations to produce the power-economizing method and the energy conserving system of edible ethanol, 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 the foregoing invention purpose, the present invention is achieved by the following technical solutions.
Technical scheme one:
A kind of power-economizing method of producing edible ethanol by five-tower three-stage differential distillation, wherein five towers comprise rectifying tower, water wash column, topping still, methanol column and impurity tower, it is characterized in that, in this power-economizing method, rectifying tower uses the primary steam heating; Rectifying tower cat head wine vapour heats water wash column, methanol column and topping still step by step successively; Water wash column and methanol column cat head wine vapour heat topping still respectively; Topping still cat head wine vapour is as the first step preheating thermal source of fermentation liquid; Topping still bottom vinasse are as the second stage preheating thermal source of fermentation liquid; The secondary steam heating impurity tower of the condensed water of primary steam after flash distillation.
The further characteristics of this technical scheme are: 165-170 ℃ of described primary steam temperature, pressure 0.65-0.8Mpa; 157-159 ℃ of rectifier bottoms temperature, head temperature 133-135 ℃; 123-125 ℃ of water wash column bottom temp, head temperature 93-95 ℃; 83-85 ℃ of topping still bottom temp, head temperature 69-71 ℃; 117-119 ℃ of methanol column bottom temp, head temperature 93-95 ℃; 103-105 ℃ of impurity column bottom temperature, head temperature 78-80 ℃.
Technical scheme two:
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 tower, rectifying tower reboiler, rectifying tower return tank, rectifying tower coagulate water pot, water wash column, water wash column reboiler, water wash column 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 tower reboiler is communicated with primary steam, its outlet is coagulated water pot, flash tank by the pipeline rectifying tower 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 wash column return tank by pipeline;
The top wine vapor outlet of described rectifying tower is by pipeline connect the successively shell side of water wash column 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 wash column reboiler, methanol column reboiler, topping still first reboiler is communicated with the rectifying tower return tank by pipeline respectively, and the rectifying tower return tank is communicated with the middle and upper part inlet of rectifying tower by pipeline; The outlet at bottom of described rectifying tower enters the mouth by first middle and upper part that pipeline is communicated with water wash column, and the centre exit of described rectifying tower is communicated with the centre entrance of impurity tower by pipeline;
The top wine vapor outlet of described water wash column 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 wash column return tank, water wash column of pipeline; The outlet at bottom of water wash column is communicated with the centre entrance of rectifying tower 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 wash column.
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 wash column 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 tower and water wash column.The shell side outlet of described topping still condenser is provided with scrubbing tower.
Because the present invention is coupled the various energy 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 grain distillerys 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 present invention 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 invention;
Wherein: 1, rectifying tower; 2, rectifying tower reboiler; 3, rectifying tower coagulates water pot; 4, rectifying tower water extraction pump; 5, rectifying tower waste water pump; 6, thick wine jar; 7, thick wine pump; 8, crude wine preheater; 9, rectifying tower condenser; 10, rectifying tower return tank; 11, rectifying tower reflux pump; 12, water wash column reboiler; 13, water wash column; 14, rectifying tower feeding pump; 15, vinasse pump; 16, water wash column reflux pump; 17, water wash column return tank; 18, water wash column condenser; 19, topping still second reboiler; 20, mash vinasse preheater; 21, mash wine vapour preheater; 22, topping still condenser; 23, scrubbing tower; 24, vacuum pump; 25, topping still second recycle pump; 26, topping still; 27, topping still the 3rd recycle 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 recycle 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 water extraction pump; 41, flash tank; 42, impurity tower; 43, impurity tower waste water pump.
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 invention, comprise that mainly rectifying tower 1, rectifying tower reboiler 2, rectifying tower return tank 10, rectifying tower coagulate water pot 3, water wash column 13, water wash column reboiler 12, water wash column 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 tower return tank 10, water wash column return tank 17, methanol column return tank 29, impurity tower return tank 37, thick wine jar 6 corresponding rectifying tower condensers 9, water wash column condenser 18, methanol column condenser 30, impurity tower condenser 38, topping still condenser 22 and a plurality of power-driven pumps of matching.
The shell side inlet of rectifying tower reboiler 2 is communicated with the primary steam from the boiler house, its outlet is coagulated water pot 3, flash tank 41 by the pipeline rectifying tower of connecting successively, the condensed water of flash tank 41 is got back to the boiler house, 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 secondary steam of flash tank 41 feeds impurity tower 42.The middle and upper part outlet of impurity tower 42 is communicated with water wash column return tank 17 by pipeline.
The top wine vapor outlet of rectifying tower 1 is by pipeline connect the successively shell side of water wash column 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 wash column reboiler 12, methanol column reboiler 34, topping still first reboiler 33 is respectively by the pipeline rectifying tower return tank 10 that imports in parallel, by the wine liquid outlet of rectifying tower return tank 10 by rectifying tower reflux pump 11, pipe connection middle and upper part inlet to rectifying tower 1.Rectifying tower return tank 10 is connected with rectifying tower condenser 9, incoagulability wine vapour is communicated to rectifying tower condenser 9 shell sides inlet by rectifying tower return tank 10 top exits, the outlet of rectifying tower condenser 9 shell sides is connected to rectifying tower return tank 10 tops inlet, carries out wine vapour and reclaims.
The tower bottom outlet of rectifying tower 1 enters the mouth by rectifying tower waste water pump 5, pipe connection to the thermal source of crude wine preheater 8, the surplus water that heats up in a steamer of rectifying tower 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 wash column 13.The centre exit of rectifying tower 1 is communicated with the centre entrance of impurity tower 42 by pipeline.
The top wine vapor outlet of water wash column 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 opening for feed of water wash column return tank 17, and condensation wine liquid is communicated with the second middle and upper part inlet of water wash column reflux pump 16 to water wash column 13 through the discharge port of water wash column return tank 17.The wine vapor outlet of water wash column return tank 17 connects the shell side inlet of water wash column condenser 18, and wine vapour phlegma connects back water wash column return tank 17 through the shell side outlet of water wash column condenser 18.
The top wine vapor outlet of methanol column 35 is by the shell side inlet of pipe connection to topping still the 3rd reboiler 28, the shell side outlet of topping still the 3rd reboiler 28 is by the wine liquid inlet of pipe connection to methanol column return tank 29, and the wine liquid outlet of methanol column return tank 29 enters the mouth through methanol column reflux pump 31, pipe connection to the middle and upper part of methanol column 35.The wine vapor outlet of methanol column return tank 29 is by the shell side inlet of pipe connection 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 phlegma.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 is by the refrigerant inlet of thick wine pump 7, pipe connection crude wine preheater 8, and crude wine preheater 8 refrigerant exits are communicated with the centre entrance of water wash column 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 is by pipe connection vacuum pump 24.
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 wash column 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 tower 1 is by the centre entrance of pipeline connection impurity tower, impurity tower 42 centre exit extraction potato spirit.Impurity tower 42 centre exit pipe connection are not to potato spirit separator (drawing).
Rectifying tower 1 and rectifying tower reboiler 2, water wash column 13 and water wash column 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 this power-economizing method of the present invention, rectifying tower 1 uses the primary steam heating; Rectifying tower 1 cat head wine vapour heats water wash column 13, methanol column 35 and topping still 26 step by step successively; Water wash column 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 step preheating thermal source of fermentation liquid; Topping still 26 bottom vinasse are as the second stage preheating thermal source of fermentation liquid; The secondary steam heating impurity tower 42 of the condensed water of primary steam after flash distillation; Wherein: 165-170 ℃ of primary steam temperature, pressure 0.65-0.8Mpa; Rectifying tower 1 bottom temp 157-159 ℃, head temperature 133-135 ℃; Water wash column 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 non-condensable gas is through vacuum 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 tower waste water pump 5 and carry out heat exchange with heat up in a steamer water from rectifying tower 1 bottom surplus, the thick wine after the heat exchange enters water wash column 13 middle parts.The surplus water part of heating up in a steamer after the heat exchange is gone to water wash column 13 middle and upper parts, and another part removes spice between alcohol-fueled car.Rectifying tower 1 top wine vapour is connected successively by water wash column reboiler 12 heating water wash columns 13, again by methanol column reboiler 34 heating methanol towers 35, again by topping still first reboiler 33 heating topping stills 26.
Rectifying tower 1 adopts the primary steam from boiler to heat by rectifying tower reboiler 2, the primary steam condensed water enters rectifying tower and coagulates water pot 3, enter flash tank 41 by rectifying tower water extraction pump 4, flash tank 41 secondary steams heating impurity tower 42, the secondary condensed water is sent boiler back to through impurity tower water extraction pump 40.
Water wash column 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 phlegma 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 wash column reboiler 12, methanol column reboiler 34, topping still first reboiler 33 flows into rectifying tower return tank 10, send into rectifying tower 1 middle and upper part by rectifying tower reflux pump 11, the wine vapour in the rectifying tower return tank 10 is by flowing into rectifying tower return tank 10 after 9 condensations of rectifying tower condenser.Water wash column 13 bottom light wine are sent into rectifying tower 1 centre entrance by rectifying tower feeding pump 14.
Topping still 26 bottom alcohol tank liquids constitute closed circuit circulatory system one by topping still first recycle pump 32, topping still first reboiler 33 with topping still 26; Topping still 26 bottom alcohol tank liquids constitute closed circuit circulatory system two by topping still second recycle pump 25, topping still second reboiler 19 with topping still 26.Topping still 26 bottom alcohol tank liquids constitute closed circuit circulatory system three by topping still the 3rd recycle 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 wash column return tank 17 is delivered in the 42 middle and upper part alcohol quantitative extraction of impurity tower.Rectifying tower 1 middle part is rich in potato spirit alcohol and is flowed into impurity tower 42 centre entrances.Impurity tower 42 centre exit extraction potato spirit.
In the present embodiment, 165-170 ℃ of primary steam temperature, pressure 0.65-0.8Mpa; About 158 ℃ of rectifying tower 1 bottom temp, about 134 ℃ of head temperature; About 124 ℃ of water wash column 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 grain distillerys 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 (6)
1. the power-economizing method of a producing edible ethanol by five-tower three-stage differential distillation, wherein five towers comprise rectifying tower (1), water wash column (13), topping still (26), methanol column (35) and impurity tower (42), it is characterized in that in this power-economizing method, rectifying tower (1) uses the primary steam heating; Rectifying tower (1) cat head wine vapour heats water wash column (13), methanol column (35) and topping still (26) step by step successively; Water wash column (13) and methanol column (35) cat head wine vapour heat topping still (26) respectively; Topping still (26) cat head wine vapour is as the first step preheating thermal source of fermentation liquid; Topping still (26) bottom vinasse are as the second stage preheating thermal source of fermentation liquid; The secondary steam heating impurity tower (42) of the condensed water of primary steam after flash distillation.
2. the power-economizing method of producing edible ethanol by five-tower three-stage differential distillation according to claim 1 is characterized in that, 165-170 ℃ of described primary steam temperature, pressure 0.65-0.8Mpa; Bottom temp 157-159 ℃ on rectifying tower (1), head temperature 133-135 ℃; Bottom temp 123-125 ℃ of water wash column (13), head temperature 93-95 ℃; Bottom temp 83-85 ℃ of topping still (26), head temperature 69-71 ℃; Bottom temp 117-119 ℃ of methanol column (35), head temperature 93-95 ℃; Bottom temp 103-105 ℃ in impurity tower (42), head temperature 78-80 ℃.
3. the energy conserving system of a producing edible ethanol by five-tower three-stage differential distillation, based on the described power-economizing method of claim 1, this energy conserving system comprises rectifying tower (1), rectifying tower reboiler (2), rectifying tower return tank (10), rectifying tower coagulates water pot (3), water wash column (13), water wash column reboiler (12), water wash column 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 tower reboiler (2) is communicated with primary steam, its outlet is coagulated water pot (3), flash tank (41) by the pipeline rectifying tower 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 wash column return tank (17) by pipeline;
The top wine vapor outlet of described rectifying tower (1) is by pipeline connect the successively shell side of water wash column 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 wash column reboiler (12), methanol column reboiler (34), topping still first reboiler (33) is communicated with rectifying tower return tank (10) by pipeline respectively, and rectifying tower return tank (10) is communicated with the middle and upper part inlet of rectifying tower (1) by pipeline; The outlet at bottom of described rectifying tower (1) enters the mouth by first middle and upper part that pipeline is communicated with water wash column (13), and the centre exit of described rectifying tower (1) is communicated with the centre entrance of impurity tower (42) by pipeline;
The top wine vapor outlet of described water wash column (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 wash column return tank (17), water wash column (13) of pipeline; The outlet at bottom of water wash column (13) is communicated with the centre entrance of rectifying tower (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.
4. the energy conserving system of producing edible ethanol by five-tower three-stage differential distillation according to claim 3, 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 wash column.
5. the energy conserving system of producing edible ethanol by five-tower three-stage differential distillation according to claim 4, it is characterized in that, the lower part outlet of described thick wine jar (6) is communicated with the centre entrance of water wash column (13) by a crude wine preheater (8) back, and the thermal source gangway of crude wine preheater (8) is serially connected between first middle and upper part inlet of the outlet at bottom of rectifying tower (1) and water wash column (13).
6. the energy conserving system of producing edible ethanol by five-tower three-stage differential distillation according to claim 4 is characterized in that, the shell side outlet of described topping still condenser (22) is provided with scrubbing tower (3).
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| CN102716596A (en) * | 2012-07-06 | 2012-10-10 | 广东高科生物工程有限公司 | Five-tower differential-pressure energy-saving alcohol distillation device |
| CN106334327A (en) * | 2016-08-30 | 2017-01-18 | 安徽安特食品股份有限公司 | Alcohol distilling production method |
| CN107954837A (en) * | 2017-11-22 | 2018-04-24 | 广东中科天元新能源科技有限公司 | Produce neutral alcohol, the device and its production technology of superneutrality alcohol |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
| CN110016425A (en) * | 2017-12-18 | 2019-07-16 | 江苏醉开心酒业有限公司 | A kind of energy-saving brewing device |
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| CN201668968U (en) * | 2010-05-24 | 2010-12-15 | 中国轻工业西安设计工程有限责任公司 | Energy-saving system for five-tower three-stage differential-pressure distilling production of edible alcohol |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102716596A (en) * | 2012-07-06 | 2012-10-10 | 广东高科生物工程有限公司 | Five-tower differential-pressure energy-saving alcohol distillation device |
| CN102716596B (en) * | 2012-07-06 | 2014-08-06 | 广东高科生物工程有限公司 | Five-tower differential-pressure energy-saving alcohol distillation device |
| CN106334327A (en) * | 2016-08-30 | 2017-01-18 | 安徽安特食品股份有限公司 | Alcohol distilling production method |
| CN106334327B (en) * | 2016-08-30 | 2018-05-04 | 安徽安特食品股份有限公司 | A kind of alcohol distillation production method |
| CN107954837A (en) * | 2017-11-22 | 2018-04-24 | 广东中科天元新能源科技有限公司 | Produce neutral alcohol, the device and its production technology of superneutrality alcohol |
| CN110016425A (en) * | 2017-12-18 | 2019-07-16 | 江苏醉开心酒业有限公司 | A kind of energy-saving brewing device |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
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Application publication date: 20101006 |