CN1736527A - Alcohol quinque-towel differential pressure distilling arrangement and technique thereof - Google Patents
Alcohol quinque-towel differential pressure distilling arrangement and technique thereof Download PDFInfo
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- CN1736527A CN1736527A CN 200510035598 CN200510035598A CN1736527A CN 1736527 A CN1736527 A CN 1736527A CN 200510035598 CN200510035598 CN 200510035598 CN 200510035598 A CN200510035598 A CN 200510035598A CN 1736527 A CN1736527 A CN 1736527A
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 17
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 123
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 120
- 238000004821 distillation Methods 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- 238000007701 flash-distillation Methods 0.000 claims abstract description 5
- 238000011084 recovery Methods 0.000 claims description 39
- 238000010992 reflux Methods 0.000 claims description 30
- 241000282326 Felis catus Species 0.000 claims description 21
- 238000005516 engineering process Methods 0.000 claims description 21
- 238000000855 fermentation Methods 0.000 claims description 11
- 230000004151 fermentation Effects 0.000 claims description 10
- 239000003517 fume Substances 0.000 claims description 9
- 239000000047 product Substances 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 239000011265 semifinished product Substances 0.000 claims description 4
- 238000005292 vacuum distillation Methods 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 5
- 239000012153 distilled water Substances 0.000 abstract 1
- 239000012535 impurity Substances 0.000 description 14
- 238000007599 discharging Methods 0.000 description 13
- 230000008569 process Effects 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000005406 washing Methods 0.000 description 4
- 230000008676 import Effects 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 2
- 239000001760 fusel oil Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a five-tower differential pressure distilling apparatus and the technique for alcohol: the fractionating tower operating with positive pressure, some alcohol vapor in the head tower flowing into the reboiler of crude distillation column, and the other into the reboiler of water scrubber; the leaving distilled water in the still of fractionating tower preheating the weak alcohol liquid from the bottom of water scrubber, then partly inpouring to crude alcohol preheater to preheat crude alcohol, and partly inpouring to water scrubber according to the requirement of flowmeter; by flash distillation the condensate water in the reboiler of fractionating tower generating indirect steam which enters directly into the still of water scrubber; the water scrubber operating with negative pressure, and the alcohol vapor in the head into the reboiler of the methanol heating tower. The significance effect is that: the energy saving effect is perfect when used to produce excellent edible alcohol and the vapor consuming index approaching the advanced lever of 2.3- 2.6 t/ t.
Description
Technical field
The present invention relates to a kind of biomass to alcohol conversion process and device thereof, especially relate to a kind of five tower differential distillation technology and devices thereof of Alcohol Production.
Background technology
Alcohol Production differential distillation technology is the distillation technique that grows up of alcohol industry in recent years, the differential distillation technology of existing main flow is in " alcohol and Spirit technology " (--Zhang Kechang chief editor China Light Industry Press in September, 2002), the publication of " newly organized alcohol technology " Beijing Chemical Industry Press university teaching publishing centre (--in July, 2004) in detailed argumentation is all arranged.Domestic existing how tame Alcohol Plant adopts five tower differential distillation flow processs.For five tower differential distillation technologies of prior art, generally all be topping still under condition of negative pressure, with the malleation fume (secondary steam) of rectifying column cat head, remove to heat the recycle stock of topping still reboiler; Water scrubber is an atmospheric operation, and its cat head wine vapour (secondary steam) goes the methanol column reboiler heat supply to negative-pressure operation.Utilized the heat energy of the cat head fume (secondary steam) of rectifying column and water scrubber two towers so once more, reach the effect of energy-saving distilling, produce high grade edible spirit consumption steam 3.0～4.2t/t wine, go a step further than the steam consumption of the original traditional air-distillation technology 4.5～5.4t/t wine of China.But there is gap apart from advanced international standard, still has the potential to be tapped.In addition, fouling, precipitation, obstruction often take place and the maintenance that stops production causes economic loss in the topping still reboiler of existing mainstream technology.
Summary of the invention
The objective of the invention is existing alcohol quinque-towel differential pressure distilling arrangement is made improvements the alcohol quinque-towel differential pressure distilling arrangement and the technology thereof that provide a kind of and cut down the consumption of energy, save cost.
For achieving the above object, the technical solution that the present invention adopts is: alcohol quinque-towel differential pressure distilling arrangement, comprise topping still, rectifying column, water scrubber, methanol column and recovery tower, wherein rectifying tower top is connected with topping still reboiler shell-side arrival end and water scrubber reboiler shell-side arrival end respectively through pipeline, and the topping still reboiler shell-side port of export and the water scrubber reboiler shell-side port of export are connected with rectifying column reflux pump arrival end through pipeline respectively; Be connected with the shell-side arrival end of light wine preheater through pipeline at the bottom of the rectifying column, the light wine preheater shell-side port of export is connected with the surplus pump entrance end that heats up in a steamer through pipeline, and the surplus pump outlet that heats up in a steamer is connected with crude wine preheater shell-side arrival end and water scrubber top water inlet respectively through pipeline; Rectifying column reboiler steam condensation-water drain end is connected with the flash tank arrival end through pipeline, and the flash distillation tank deck is connected through the top of pipeline with washing Tata still, is communicated with the net thermal water recovery system through pipeline at the bottom of the flash tank; The washing cat head is connected with methanol column reboiler shell-side arrival end through pipeline, the methanol column reboiler shell-side port of export is connected with water scrubber return tank arrival end through pipeline, water scrubber backflow tank deck is connected with pumped vacuum systems through pipeline, be connected with water scrubber reflux pump arrival end through pipeline at the bottom of the water scrubber return tank, the water scrubber reflux pump port of export is connected with water scrubber top reflux inlet end through pipeline.
Recovery cat head of the present invention is connected with the second mash preheater shell-side arrival end through pipeline, the second mash preheater shell-side port of export is connected with recovery tower reflux pump arrival end through pipeline, and the recovery tower reflux pump port of export is connected with recovery tower top refluxing opening through pipeline; The second mash preheater tube side entrance end is connected with the first mash preheater tube side outlet end through pipeline, and the second mash preheater tube side outlet end is connected with the topping still middle-end through pipeline.The raw material that topping still enters--fermentation liquid utilizes the fume preheater preheating on topping still top earlier, through reclaiming the further preheating of wine vapour of cat head, heat energy is reclaimed as far as possible again, thereby reduces energy consumption.
Be connected with assorted wine preheater shell-side arrival end through pipeline at the bottom of the recovery tower of the present invention, the assorted wine preheater shell-side port of export is connected with the spent hot water system through pipeline, assorted wine preheater tube side entrance end is communicated with assorted wine inlet, and assorted wine preheater tube side outlet end is communicated with recovery tower middle part charging layer through pipeline.Can make assorted wine reclaim spent hot water's heat like this, behind the feed recovery tower, save the steam consumption of recovery tower.
Be connected with pump entry end at the bottom of useless poor system and the tower respectively through pipeline at the bottom of the topping still of the present invention, the outlet of circulating pump end is connected with topping still reboiler pipe side entrance end through pipeline, and topping still reboiler pipe side outlet end is connected with topping still tower still top through pipeline.The topping still reboiler adopts the forced circulation technology, improves heat exchange efficiency, can also reduce reboiler because of fouling, precipitation, obstruction stopping production maintenance times.
Quinque-towel differential pressure distilling arrangement of the present invention is provided with automatic control system, comprise sensors such as being located at on-the-spot temperature, pressure, liquid level and be provided with the active station of PLC system, each sensor can be handled signal and be input to the PLC system, and carries out communication by MPI port and PLC; Active station also is provided with respective display unit, print unit and form unit.
The technology that the present invention adopts is: from the next maturing fermentation mash of fermentation procedure, earlier through the first mash preheater again through reclaiming the second mash preheater preheating of cat head wine vapour, enter topping still, the fume on topping still top is through the first mash preheater, condenser condenses becomes thick wine, thick wine enters thick wine temporary storage jar, divide two-way to see off through thick wine pump, one the tunnel squeezes into the topping still top refluxes, crude wine preheater 1 is sent on another road, enter the charging layer of water scrubber, after the operation of water scrubber negative pressure extraction, light wine comes out to remove the light wine preheater by light wine pump pump from tower bottom, enters rectifying column charging layer after the preheating; After the rectifying of rectifying column malleation, the alcohol semi-finished product draw to methanol column from the wine fetch port of cat head, further get rid of methyl alcohol through the methanol column vacuum distillation, draw the high grade edible spirit finished product from tower bottom and remove basin;
Rectifying column adopts positive pressure operation, the wine vapour of its cat head, and one the tunnel removes to heat the topping still reboiler; The water scrubber reboiler is removed to heat in another road; Topping still and water scrubber all adopt negative-pressure operation; The steam condensate (SC) of rectifying column reboiler directly enters washing Tata still and uses through the indirect steam that flash distillation produces; The surplus water that heats up in a steamer of rectifying Tata still is earlier through the light wine preheater, and preheating is from the next weak liquor in water scrubber bottom; Light wine charging rectifying column behind the absorption heat; From the surplus water that heats up in a steamer that the light wine preheater comes out, the one tunnel through crude wine preheater, the thick wine liquid that the thick wine pump of preheating comes, charging water scrubber behind the thick wine absorption heat; The surplus water that heats up in a steamer in another road enters the backflow of water scrubber top by the flowmeter requirement;
The wine vapour of washing cat head removes the reboiler of heating methanol tower; The methanol column negative-pressure operation, its absolute pressure is less than the absolute pressure of water scrubber;
Maturing fermentation wine with dregs elder generation, uses through the second mash preheater and reclaims the further preheating of cat head wine vapour with the fume preheating of topping still top through the first mash preheater;
Assorted wine is the charging recovery tower behind the assorted wine preheater recovery spent hot water's of recovery tower bottom heat;
Regulate the negative pressure value of topping still, water scrubber, methanol column by the pipeline control valve;
Draff liquid at the bottom of the topping still enters reboiler by circulating pump, and being heated boils again enters at the bottom of the tower, realizes forced circulation;
Absolute pressure is 5kg/cm
2Primary steam, the reboiler of mainly supplying with smart tower uses, the indirect steam of condensed water flash is for water scrubber still usefulness, net thermal water back boiler.
In the technology of the present invention, control each column overhead operating pressure, temperature is respectively:
Topping still absolute pressure 0.35～0.4kg/cm
2, 50～60 ℃ of tower top temperatures, 78～86 ℃ of column bottom temperatures;
Rectifying column absolute pressure 2.0～2.5kg/cm
2, 96～105 ℃ of tower top temperatures, 125～135 ℃ of column bottom temperatures;
Water scrubber absolute pressure 0.6～0.8kg/cm
2, 82～92 ℃ of tower top temperatures, 85～95 ℃ of column bottom temperatures;
Methanol column absolute pressure 0.3～0.4kg/cm
2, 50～60 ℃ of tower top temperatures, 58～70 ℃ of column bottom temperatures;
Recovery tower absolute pressure 1.00kg/cm
2, 79 ℃ of tower top temperatures, 106 ℃ of column bottom temperatures.
The invention has the beneficial effects as follows: the technical combinations that adopts multinomial recycling heat, add the forced circulation technology that adopts the topping still reboiler, and match with the Automatic Control technology, the energy-saving effect that makes this invention is when producing high grade edible spirit, steam consumption index reaches the advanced level of 2.3～2.6t/t wine, the steam consumption than existing main flow differential distillation technology 3.0～4.2t/t wine saves nearly 20～30%, the steam consumption than the original traditional air-distillation technology 4.5～5.4t/t wine of China saves nearly 50%, and prevented the reboiler fouling, precipitation, stop up, improved the heat exchange effect.Thick tower reboiler can use for a long time, has guaranteed the serialization production of alcohol.
Description of drawings
Accompanying drawing 1 is a technological process schematic diagram of the present invention
1, topping still, 2, rectifying column, 3, water scrubber, 4, methanol column, 5, recovery tower, 6, the first mash preheater, 7, the second mash preheater, 8, condenser, 9, temporary jar of thick wine, 10, crude wine preheater, 11, the light wine preheater, 12, the topping still reboiler, 13, the rectifying column reboiler, 14, the water scrubber reboiler, 15, the methanol column reboiler, 16, flash tank, 17, assorted wine preheater, 18, the water scrubber return tank, 19, the methanol column condenser, 201, thick wine pump, 202, the recovery tower reflux pump, 203, circulating pump, 204, the rectifying column reflux pump, 205, the surplus water pump that heats up in a steamer, 206, the light wine pump, 207, the water scrubber reflux pump, a1, impurity discharging port, a2, impurity discharging port, a3, impurity discharging port, a4, impurity discharging port, a5, impurity discharging port, a6, impurity discharging port, a7, impurity discharging port, a8, impurity discharging port, b, assorted wine import, c, get hydraulic fluid port, z, primary steam.
The specific embodiment
Embodiment: as shown in Figure 1, quinque-towel differential pressure distilling arrangement, comprise topping still 1, rectifying column 2, water scrubber 3, methanol column 4 and recovery tower 5, wherein rectifying column 2 tops are connected with topping still reboiler 12 shell-side arrival ends and water scrubber reboiler 14 shell-side arrival ends respectively through pipeline, and the topping still reboiler 12 shell-side ports of export and the water scrubber reboiler 14 shell-side ports of export are connected with rectifying column reflux pump 204 arrival ends through pipeline respectively; 2 ends of rectifying column, be connected with the shell-side arrival end of light wine preheater 11 through pipeline, the light wine preheater 11 shell-side ports of export are connected with surplus water pump 205 arrival ends that heat up in a steamer through pipeline, and surplus water pump 205 ports of export that heat up in a steamer are connected with crude wine preheater 10 shell-side arrival ends and water scrubber 3 top water inlets respectively through pipeline; The rectifying column reboiler 13 steam condensate (SC) ports of export are connected with flash tank 16 arrival ends through pipeline, and flash tank 16 tops are connected through pipeline and water scrubber 3 bottoms backflow end, and 16 ends of flash tank are communicated with the net thermal water recovery system through pipeline; Water scrubber 3 tops are connected with methanol column reboiler 15 shell-side arrival ends through pipeline, the methanol column reboiler 15 shell-side ports of export are connected with water scrubber return tank 18 arrival ends through pipeline, water scrubber return tank 18 tops are connected with pumped vacuum systems through pipeline, 18 ends of water scrubber return tank, be connected with water scrubber reflux pump 207 arrival ends through pipeline, and water scrubber reflux pump 207 ports of export are connected with water scrubber 3 top reflux inlet ends through pipeline.
1 end of topping still, be connected with circulating pump 203 arrival ends at the bottom of useless poor system and the tower respectively through pipeline, the port of export of circulating pump 203 is connected with topping still reboiler 12 pipe side entrance ends through pipeline, and topping still reboiler 12 pipe side outlet ends are connected with topping still 1 lower end through pipeline.
The first mash preheater, 6 shell-side arrival ends are connected with topping still 1 top through pipeline, the first mash preheater, the 6 shell-side ports of export are connected with temporary jar 9 of thick wine and condenser 8 respectively through pipeline, condenser 8 tops are connected with pumped vacuum systems, its bottom is connected for temporary jar 9 through pipeline and thick wine, temporary jar 9 top of thick wine is communicated with pumped vacuum systems through pipeline, and its bottom links to each other with thick wine pump 201; Be respectively equipped with impurity discharging port a1, a2, a3 on condenser 8,201 outlets of thick wine pump and topping still 1 top.
For guaranteeing product quality, must get rid of impurity, top and middle part at rectifying column 2 are respectively equipped with impurity discharging port a4 and a5, and the outlet conduit of rectifying column reflux pump 204 is provided with impurity discharging port a6, are respectively equipped with impurity discharging port a7 and a8 on the outlet conduit of water scrubber reflux pump 207 and recovery tower reflux pump 202.After the assorted wine that each impurity discharging port is discharged is concentrated, be collected to assorted wine import b place.
5 ends of recovery tower, be connected with assorted wine preheater 17 shell-side arrival ends through pipeline, the assorted wine preheater 17 shell-side ports of export are connected with the spent hot water system through pipeline, assorted wine preheater 17 pipe side entrance ends are communicated with assorted wine import b, and assorted wine preheater 17 pipe side outlet ends are communicated with recovery tower 5 middle part charging layers through pipeline.The recovery tower middle part is provided with gets hydraulic fluid port c, extracts the oily wine liquid that contains fusel, goes conventional fusel oil piece-rate system to separate fusel oil.
Quinque-towel differential pressure distilling arrangement of the present invention is provided with automatic control system, comprise sensors such as being located at on-the-spot temperature, pressure, liquid level and be provided with the active station of PLC system, each sensor can be handled signal and be input to the PLC system, and carries out communication by MPI port and PLC; Active station also is provided with respective display unit, print unit and form unit.The various data of active station in showing production procedure, also warning message is classified, picture shows all is with menu mode, this control system possesses functions such as Monitoring and Controlling, demonstration, printing, form, simultaneously can directly utilize mouse start and stop motor on display, guarantee the stable operation of new technological process.Above technical combinations flow process is obviously outstanding than existing main flow difference distillation technique flow process, has increased a plurality of conservation measures and has reduced fault.
The trend of material is: from the next maturing fermentation mash of fermentation procedure, earlier through the first mash preheater 6 again through reclaiming the second mash preheater, 7 preheatings of cat head wine vapour, enter topping still 1, the fume on topping still 1 top is through the first mash preheater 6, condenser 8 is condensed into thick wine, thick wine enters thick wine temporary storage jar 9, see off through thick 201 fens two-way of wine pump, one the tunnel squeezes into topping still 1 top refluxes, crude wine preheater 10 is sent on another road, enter the charging layer of water scrubber 3, after the operation of water scrubber 3 negative pressure extractions, light wine comes out to remove light wine preheater 11 by light wine pump 206 pumps from tower bottom, enters rectifying column 2 charging layers after the preheating.After rectifying column 2 malleation rectifying, the alcohol semi-finished product draw to methanol column 4 from the wine fetch port of cat head, further get rid of methyl alcohol through methanol column 4 vacuum distillations, draw the high grade edible spirit finished product from tower bottom and remove basin.
Rectifying column 2 adopts positive pressure operation, the wine vapour of its cat head, and one the tunnel removes to heat topping still reboiler 12; Water scrubber reboiler 14 is removed to heat in another road.Topping still 1 and water scrubber 3 all adopt negative-pressure operation; The steam condensate (SC) of rectifying column reboiler 13 directly enters water scrubber 3 tower stills and uses through the indirect steam that flash distillation produces.Rectifying Tata still surplus heats up in a steamer water earlier through light wine preheater 11, and the weak liquor that preheating comes from water scrubber 3 bottoms absorbs the light wine charging rectifying column 2 behind the heat; From the surplus water that heats up in a steamer that light wine preheater 11 comes out, the one tunnel through crude wine preheater 10, the thick wine liquid of the thick wine pump 201 of preheating, charging water scrubber 3 behind the thick wine absorption heat; The surplus water that heats up in a steamer in another road enters the backflow of water scrubber 3 tops by the flowmeter requirement.
The wine vapour on water scrubber 3 tops removes the reboiler 15 of heating methanol tower 4.
Regulate the negative pressure value of thick tower 1, water scrubber 3, methanol column 4 by the pipeline control valve.The absolute pressure of methanol column 4 is less than the absolute pressure of water scrubber 3.After methanol column 4 cat head vapour process methanol column condenser 19 water-cooleds, condensate liquid backflow methanol column 4 tops.
The draff liquid at 1 end of topping still enters reboiler 12 by circulating pump 203, and being heated boils again enters at the bottom of the tower, realizes forced circulation.
Absolute pressure is 5kg/cm
2Primary steam z, most of rectifying column reboiler 13 of supplying with uses, the indirect steam of condensed water flash is for water scrubber 3 tower still usefulness, net thermal water back boiler; Small part is supplied with recovery tower 5 heating and is used, and the spent hot water goes to handle.
To produce 60000 tons of devices of high grade edible spirit per year is example, further specifies technical process of the present invention:
Operating pressure, the temperature of controlling each column overhead are:
Topping still 1 absolute pressure 0.35kg/cm
2, 55 ℃ of tower top temperatures, 82 ℃ of column bottom temperatures;
Rectifying column 2 absolute pressure 2.30kg/cm
2, 100 ℃ of tower top temperatures, 128.5 ℃ of column bottom temperatures;
Water scrubber 3 absolute pressure 0.68kg/cm
2, 87 ℃ of tower top temperatures, 89 ℃ of column bottom temperatures;
Methanol column 4 absolute pressure 0.35kg/cm
2, 54 ℃ of tower top temperatures, 63 ℃ of column bottom temperatures;
108.5 tons of come from fermentation procedure 30 ℃ maturing fermentation wine with dregs that contain wine 9.5% (V/V)/time, earlier be preheating to 48 ℃ through the first mash preheater 6, the second mash preheater 7 through reclaiming cat head wine vapour is preheating to 65 ℃ again, enters the charging layer of topping still 1, and topping still 1 top is provided with enriching section.55 ℃ of the fume temperature on topping still 1 top, operating pressure is absolute pressure 0.35kg/cm
2, being condensed into thick wine through the first mash preheater 6, condenser 8, thick wine enters thick wine temporary storage jar 9, see off through thick 201 fens two-way of wine pump, one the tunnel squeezes into thick top of tower refluxes, and reflux ratio is 2.2～2.5, and crude wine preheater 10 is sent on another road, be preheating to 75 ℃, enter the charging layer of water scrubber 3, after water scrubber 3 negative-pressure operations extractions, light wine is from tower bottom come out (89 ℃), remove light wine preheater 11 by light wine pump 206 pumps, be preheating to 120 ℃ and enter rectifying column 2 charging layers.After rectifying column 2 malleation rectifying, alcohol semi-finished product 95.5% (V/V), 100 ℃, draw to methanol column 4 methanol column 4 vacuum distillations from the wine fetch port of cat head, further get rid of methyl alcohol, draw high grade edible spirit finished product 95.5% (V/V) from tower bottom, 63 ℃, remove the smart cooler of finished wine, 8.386 tons of normal temperature finished products/time, the high-quality edible alcohol advances the alcohol basin.
Claims (7)
1, a kind of alcohol quinque-towel differential pressure distilling arrangement, comprise topping still (1), rectifying column (2), water scrubber (3), methanol column (4) and recovery tower (5), it is characterized in that: wherein rectifying column (2) top is connected with topping still reboiler (12) shell-side arrival end and water scrubber reboiler (14) shell-side arrival end respectively through pipeline, and topping still reboiler (12) the shell-side port of export and water scrubber reboiler (14) the shell-side port of export are connected with rectifying column reflux pump (204) arrival end through pipeline respectively; Rectifying column (2) end, be connected through the shell-side arrival end of pipeline with light wine preheater (11), light wine preheater (11) the shell-side port of export is connected with surplus water pump (205) arrival end that heats up in a steamer through pipeline, and surplus water pump (205) port of export that heats up in a steamer is connected with crude wine preheater (10) shell-side arrival end and water scrubber (3) top water inlet respectively through pipeline; Rectifying column reboiler (13) the steam condensate (SC) port of export is connected with flash tank (16) arrival end through pipeline, and flash tank (16) top is connected through the top of pipeline with water scrubber (3) tower still, and flash tank (16) end is communicated with the net thermal water recovery system through pipeline; Water scrubber (3) top is connected with methanol column reboiler (15) heating arrival end through pipeline, methanol column reboiler (15) the shell-side port of export is connected with water scrubber return tank (18) arrival end through pipeline, water scrubber return tank (18) top is connected with pumped vacuum systems through pipeline, water scrubber return tank (18) end, be connected with water scrubber reflux pump (207) arrival end through pipeline, and water scrubber reflux pump (207) port of export is connected with water scrubber (3) top reflux inlet end through pipeline.
2, alcohol quinque-towel differential pressure distilling arrangement according to claim 1, it is characterized in that: described recovery tower (5) top is connected with second mash preheater (7) the shell-side arrival end through pipeline, second mash preheater (7) the shell-side port of export is connected with recovery tower reflux pump (202) arrival end through pipeline, and recovery tower reflux pump (202) port of export is connected through pipeline and recovery tower (5) top backflow end; The second mash preheater (7) pipe side entrance end is connected with the first mash preheater (6) pipe side outlet end through pipeline, and the second mash preheater (7) pipe side outlet end is connected with topping still (1) middle part charging layer through pipeline.
3, alcohol quinque-towel differential pressure distilling arrangement according to claim 1, it is characterized in that: described topping still (1) end, be connected with circulating pump (203) arrival end at the bottom of useless poor system and the tower respectively through pipeline, the port of export of circulating pump (203) is connected with topping still reboiler (12) pipe side entrance end through pipeline, and topping still reboiler (12) pipe side outlet end is connected with topping still (1) tower still top through pipeline.
4, alcohol quinque-towel differential pressure distilling arrangement according to claim 1, it is characterized in that: described quinque-towel differential pressure distilling arrangement is provided with automatic control system, comprise sensors such as being located at on-the-spot temperature, pressure, liquid level and be provided with the active station of PLC system, each sensor can be handled signal and be input to the PLC system, and carries out communication by MPI port and PLC; Active station also is provided with respective display unit, print unit and form unit.
5, a kind of alcohol five tower differential distillation technologies of alcohol quinque-towel differential pressure distilling arrangement as claimed in claim 1, it is characterized in that: from the next maturing fermentation mash of fermentation procedure, earlier through the first mash preheater (6) again through reclaiming second mash preheater (7) preheating of cat head wine vapour, enter topping still (1), the fume on topping still (1) top is through the first mash preheater (6), condenser (8) is condensed into thick wine, thick wine enters thick wine temporary storage jar (9), divide two-way to see off through thick wine pump (201), one the tunnel squeezes into topping still (1) top refluxes, crude wine preheater (10) is sent on another road, enter the charging layer of water scrubber (3), after the operation of water scrubber (3) negative pressure extraction, light wine comes out to remove light wine preheater (11) by light wine pump (206) pump from tower bottom, enters rectifying column (2) charging layer after the preheating; After rectifying column (2) malleation rectifying, the alcohol semi-finished product draw to methanol column (4) from the wine fetch port of cat head, further get rid of methyl alcohol through methanol column (4) vacuum distillation, draw the high grade edible spirit finished product from tower bottom and remove basin; Rectifying column (2) adopts positive pressure operation, the wine vapour of its cat head, and one the tunnel removes to heat topping still reboiler (12); Water scrubber reboiler (14) is removed to heat in another road; Topping still (1) and water scrubber (3) all adopt negative-pressure operation; The steam condensate (SC) of rectifying column reboiler (13) directly enters water scrubber (3) tower still and uses through the indirect steam that flash distillation produces; The surplus water that heats up in a steamer of rectifying Tata still is earlier through light wine preheater (11), and preheating is from the next weak liquor in water scrubber (3) bottom; Light wine charging rectifying column (2) behind the absorption heat; From the surplus water that heats up in a steamer that light wine preheater (11) comes out, the one tunnel through crude wine preheater (10), the thick wine liquid that the thick wine pump of preheating (201) comes, charging water scrubber (3) behind the thick wine absorption heat; The surplus water that heats up in a steamer in another road enters the backflow of water scrubber (3) top by the flowmeter requirement; The wine vapour on water scrubber (3) top removes the reboiler (15) of heating methanol tower (4); Methanol column (4) is used negative-pressure operation, and its absolute pressure is less than the absolute pressure of water scrubber;
Maturing fermentation wine with dregs elder generation, uses through the second mash preheater (7) and reclaims the further preheating of cat head wine vapour with the fume preheating of topping still top through the first mash preheater (6);
Assorted wine is charging recovery tower (5) behind assorted wine preheater (17) the recovery spent hot water's of recovery tower (5) bottom heat;
The draff liquid at topping still (1) end enters topping still reboiler (12) by circulating pump (20-3), and being heated boils again enters at the bottom of the tower;
Absolute pressure is 5kg/cm
2Primary steam, the reboiler (13) of mainly supplying with smart tower uses, the indirect steam of condensed water flash is for water scrubber still usefulness, net thermal water back boiler.
6, alcohol five tower differential distillation technologies according to claim 5 is characterized in that: control each column overhead operating pressure, temperature is respectively:
Topping still (1) absolute pressure 0.35～0.4kg/cm
2, 50～60 ℃ of tower top temperatures, 78～86 ℃ of column bottom temperatures;
Rectifying column (2) absolute pressure 2.0～2.5kg/cm
2, 96～105 ℃ of tower top temperatures, 125～135 ℃ of column bottom temperatures;
Water scrubber (3) absolute pressure 0.6～0.8kg/cm
2, 82～92 ℃ of tower top temperatures, 85～95 ℃ of column bottom temperatures;
Methanol column (4) absolute pressure 0.3～0.4kg/cm
2, 50～60 ℃ of tower top temperatures, 58～70 ℃ of column bottom temperatures;
Recovery tower (5) absolute pressure 1.00kg/cm
2, 79 ℃ of tower top temperatures, 106 ℃ of column bottom temperatures.
7, alcohol five tower differential distillation technologies according to claim 6 is characterized in that: control each column overhead operating pressure, temperature is respectively:
Topping still (1) absolute pressure 0.35kg/cm
2, 55 ℃ of tower top temperatures, 82 ℃ of column bottom temperatures;
Rectifying column (2) absolute pressure 2.30kg/cm
2, 100 ℃ of tower top temperatures, 128.5 ℃ of column bottom temperatures;
Water scrubber (3) absolute pressure 0.68kg/cm
2, 87 ℃ of tower top temperatures, 89 ℃ of column bottom temperatures;
Methanol column (4) absolute pressure 0.35kg/cm
2, 54 ℃ of tower top temperatures, 63 ℃ of column bottom temperatures;
Recovery tower (5) absolute pressure 1.00kg/cm
2, 79 ℃ of tower top temperatures, 106 ℃ of column bottom temperatures.
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