CN101748037A - Special grade edible alcohol six-tower difference pressure distilling device and process thereof - Google Patents
Special grade edible alcohol six-tower difference pressure distilling device and process thereof Download PDFInfo
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- CN101748037A CN101748037A CN200910194089A CN200910194089A CN101748037A CN 101748037 A CN101748037 A CN 101748037A CN 200910194089 A CN200910194089 A CN 200910194089A CN 200910194089 A CN200910194089 A CN 200910194089A CN 101748037 A CN101748037 A CN 101748037A
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 75
- 238000000034 method Methods 0.000 title claims abstract description 11
- 230000008569 process Effects 0.000 title abstract description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 258
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 108
- 238000011084 recovery Methods 0.000 claims abstract description 65
- 239000002351 wastewater Substances 0.000 claims abstract description 30
- 235000014101 wine Nutrition 0.000 claims description 221
- 238000010992 reflux Methods 0.000 claims description 56
- 241000282326 Felis catus Species 0.000 claims description 35
- 238000004821 distillation Methods 0.000 claims description 21
- 230000005070 ripening Effects 0.000 claims description 18
- 238000009833 condensation Methods 0.000 claims description 17
- 230000005494 condensation Effects 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 14
- 230000008676 import Effects 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000000605 extraction Methods 0.000 claims description 6
- 239000012808 vapor phase Substances 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 4
- 230000001112 coagulating effect Effects 0.000 claims description 2
- 239000007791 liquid phase Substances 0.000 claims description 2
- 238000000855 fermentation Methods 0.000 abstract description 7
- 230000004151 fermentation Effects 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 5
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 230000008901 benefit Effects 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 description 16
- 244000061456 Solanum tuberosum Species 0.000 description 10
- 235000002595 Solanum tuberosum Nutrition 0.000 description 10
- 238000010407 vacuum cleaning Methods 0.000 description 6
- 239000012141 concentrate Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 150000007513 acids Chemical class 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 239000000470 constituent Substances 0.000 description 3
- 238000010010 raising Methods 0.000 description 3
- 230000001131 transforming effect Effects 0.000 description 3
- CJRJTCMSQLEPFQ-UHFFFAOYSA-N 6-cat Chemical compound ClC1=CC=C2CC(N)CCC2=C1 CJRJTCMSQLEPFQ-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000001760 fusel oil Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000003809 water extraction Methods 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
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- 239000012071 phase Substances 0.000 description 1
- 235000015096 spirit Nutrition 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)
Abstract
The invention discloses a special grade edible alcohol six-tower difference pressure distilling device and a process thereof. The device comprises topping stills, a water scrubber, a rectifying tower, a methanol tower, a recovery tower and auxiliary topping stills, wherein outlets in the middle of the topping stills are connected with inlets of the auxiliary topping stills through pipelines; outlets at the top of the auxiliary topping stills are connected with inlets in the middle of the topping stills; the bottoms of the auxiliary topping stills are connected with externally-connected wastewater through pipelines; an outlet at the top of the recovery tower is connected with an inlet at the reboiler shell side of a first auxiliary topping still through a pipeline; an outlet of the reboiler shell side of the first auxiliary topping still is connected with a reflow tank of the recovery tower through a pipeline; a first outlet at the reboiler shell side of a second auxiliary topping still is connected with an inlet at the reboiler shell of the second auxiliary topping still through a pipeline; and an outlet at the reboiler shell side of the second auxiliary topping still is connected with a reflow tank of the methanol tower through a pipeline. The invention has the advantages that: the device is suitable for thick mash fermentation; affluent heat in alcohol steam of the methanol tower and the recovery tower can be used for concentrating rough alcohol; the steam consumption of each ton of products is 2.2 tons which is saved by 0.5-0.6 ton of steam as comparison with 2.7-2.8 tons advanced in the prior art; and in addition, the invention is beneficial to increasing the aldehyde discharge effect and improving the mouthfeel.
Description
Technical field
The present invention relates to a kind of Alcohol Production device and technology, especially relate to six column distillation device and the technologies that superfine edible ethanol is produced.
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, in " alcohol and liquor technology " (Zhang Kechang chief editor China Light Industry Press in September, 2002), all there is detailed argumentation in " corn alcohol production new technology " (Xie Linlvxi army write China Light Industry Press June calendar year 2001) in the document such as " newly organized alcohol technology " (Jia Shubiao etc. write Chemical Industry Press teaching material publishing centre in July, 2004).Along with the raising of country to the edible ethanol standard, the deterioration of domestic water resource situation and the growing tension of global energy, seek a kind ofly can improve the edible ethanol quality, rationally utilizing water resources fully and reducing the novel process of producing the edible ethanol energy consumption becomes the task of top priority.Superfine edible ethanol product standard is carried out GB (GB10343-2008), but for five tower differential distillation technologies of the prior art, generally can only produce high grade edible spirit, the impurity in the alcohol can't further be got rid of, should this can not be owing to producing superfine edible ethanol.
In order to produce superfine alcohol, several six-column differential-pressure distil process are arranged at present, existing division is as follows:
1, a kind of six-column differential-pressure distillation device that comprises wine with dregs tower, topping still, water extraction tower, rectifying tower, eparating methanol tower and contain assorted fraction treating column, can be used for producing superfine edible ethanol, but the steam consumption of its ton wine is more than 2.7～2.8 tons, need to extract a large amount of industrial spirit simultaneously, extract (the production of general top grade alcohol more than 15% approximately, getting industrial spirit is being normal below 3%), and produce unstable;
2, a kind of six-column differential-pressure distillation device that comprises wine with dregs tower, water extraction tower, rectifying tower, eparating methanol tower, potato spirit tower and industrial spirit tower, though can produce superfine edible ethanol, steam consumption is often up to 3.3～3.4 tons more than the steam, energy consumption is higher.
3, a kind of topping still, dealdehyder tower, water wash column, rectifying tower, methanol column and recovery tower of comprising.This six-column differential-pressure technology is comparatively complicated, so also difficulty relatively of technology controlling and process, and water coolant and energy consumption are also bigger.
Summary of the invention
The purpose of this invention is to provide a kind of superfine edible ethanol six-column differential-pressure distillation device that improves the edible ethanol quality and reduce water and energy consumption.
Another object of the present invention provides a kind of superfine edible ethanol six-column differential-pressure distilling producing process.
Technical solution of the present invention is: a kind of superfine edible ethanol six-column differential-pressure distillation device, comprise topping still, water wash column, rectifying tower, methanol column, recovery tower and thick auxilliary tower, wherein ripe wine with dregs import connects first ripening wine with dregs preheater tube side in turn by pipeline and links to each other with the second ripe wine with dregs preheater tube side and with the topping still import, the topping still top links to each other with first mash preheater shell-side inlet through pipeline, the first mash preheater shell-side vapor phase exit links to each other with the topping still condenser inlet, the outlet of topping still condenser liquid phase, the outlet of first ripening wine with dregs preheater shell-side links to each other with thick wine jar through pipeline, thick wine pot bottom is communicated with the crude wine preheater import by pipeline through thick wine pump, the crude wine preheater outlet is by pipe connection water wash column inlet, the water wash column top links to each other with first topping still reboiler shell-side inlet through pipeline, the first topping still reboiler shell-side has two outlets, link to each other with water wash column return tank inlet with the cold inlet in water wash column end through pipeline respectively, the water wash column cold outlet in end links to each other with water wash column return tank inlet, water wash column return tank top links to each other with vacuum system through pipeline, water wash column return tank bottom links to each other with water wash column reflux pump inlet end through pipeline, and water wash column reflux pump exit end links to each other with water wash column top refluxing opening through pipeline; The water wash column bottom links to each other with light wine preheater inlet through the light wine pump, the outlet of light wine preheater links to each other with the rectifying tower inlet, the rectifying tower top links to each other with water wash column reboiler shell-side inlet through pipeline, water wash column reboiler shell-side is provided with two outlets, link to each other with rectifying tower return tank inlet with methanol column reboiler shell-side inlet through pipeline respectively, methanol column reboiler shell-side is established two outlets, respectively through pipeline and rectifying tower return tank inlet and rectifying tower cold linking to each other of end, the rectifying tower cold outlet in end links to each other with the rectifying tower return tank, link to each other with rectifying tower reflux pump inlet through pipeline at the bottom of the rectifying tower return tank, rectifying tower reflux pump exit end links to each other with rectifying tower top refluxing opening through pipeline, the outlet of rectifying tower heavy wine enters the mouth through the pipe connection methanol column, the methanol column top links to each other with second topping still reboiler shell-side inlet through pipeline, first outlet of the second topping still reboiler shell-side links to each other with methanol column return tank inlet through pipeline, methanol column return tank outlet at bottom links to each other with methanol column reflux pump inlet end through pipeline, methanol column reflux pump exit end links to each other with methanol column top refluxing opening through pipeline, enters the mouth through the pipe connection discharge pump at the bottom of the methanol column; Vacuum system refluxes, the assorted wine of water wash column return tank exports, the assorted wine of rectifying tower exports and the assorted wine outlet of rectifying tower return tank is connected with assorted wine jar through pipeline respectively, assorted wine pot bottom connects assorted wine preheater inlet through assorted wine pump, and assorted wine preheater outlet is through the pipe connection recovery tower; The topping still centre exit is through the slightly auxilliary tower inlet of pipe connection, and slightly auxilliary top of tower outlet is through pipe connection topping still centre entrance, and slightly auxilliary tower bottom is through the external waste water of pipe connection; Described recovery tower top exit links to each other with the first thick auxilliary tower reboiler shell-side inlet through pipeline, the first thick auxilliary tower reboiler shell-side has two outlets, through pipeline and recovery tower return tank and recovery tower cold linking to each other of end, the recovery tower cold outlet in end links to each other with the recovery tower return tank through pipeline respectively; Second outlet of the described second topping still reboiler shell-side links to each other with the second thick auxilliary tower reboiler shell-side inlet through pipeline, and the second thick auxilliary tower reboiler shell-side outlet links to each other with the methanol column return tank through pipeline.
Owing to mostly be thick mash fermentation at present, ripe raw spirit degree improves, the corresponding reduction of the thermal load of topping still, thick auxilliary tower is set, can further alleviate the load of topping still, recycle rich heat and be used for concentrating thick wine, improve row's aldehyde effect and improve finished product alcohol mouthfeel, thick simultaneously auxilliary tower can reclaim the water that the full gear section refluxes in the topping still, contain the heavy constituent of part acids in the waste water of discharging, further improved the quality of edible ethanol, improved the concentration of useless wine with dregs, help alleviating the follow-up steam consumption that distills workshop section, improve the effect that the alcohol grade reduces steam and water consumption simultaneously thereby reach.
Described topping still centre exit and centre entrance lay respectively at the 25th layer of column plate place, are the full gear section more than the 25th layer of column plate, and full gear section and thick auxilliary tower can be used for the heat of affluence the concentrated of thick wine, help increasing row's aldehyde effect and improving mouthfeel.
Another technical solution of the present invention is: ripe wine with dregs is through first ripening wine with dregs preheater, enter topping still after the second ripe wine with dregs preheater preheating, the thick wine vapour at topping still top is successively through entering thick wine jar after first ripening wine with dregs preheater and the topping still condenser condenses, thick wine in the thick wine jar is through crude wine preheater, the waste water preheating is laggard at the bottom of the part rectifying tower that comes with rectifying tower waste water pump pump goes into water wash column, thick wine passes through the washing of rectifying tower waste water in water wash column after, the light wine of water wash column bottom enters the preheating of light wine preheater through the light wine pump, by entering rectifying tower after the waste water preheating at the bottom of the rectifying tower, water wash column top wine vapour is after the first topping still reboiler condensation, phlegma enters in the water wash column return tank, deliver to the water wash column internal reflux through the water wash column reflux pump, non-condensable gas enters vacuum system, the light wine that enters in the rectifying tower enters methanol column through the concentrated back of distillation from rectifier heavy wine outlet extraction, rectifying tower top wine vapour passes through water wash column reboiler and the condensation of methanol column reboiler successively, phlegma enters in the rectifying tower return tank, sends rectifying tower back to by the rectifying tower reflux pump and refluxes; After entering the heavy wine discharge methyl alcohol of methanol column, bottom wine liquid is sent through discharge pump, methanol column top wine vapour is successively through after the second topping still reboiler, the second thick auxilliary tower reboiler condensation, phlegma enters the methanol column return tank, send the methyl alcohol trim the top of column back to through the methanol column reflux pump, enter assorted wine jar respectively from the assorted wine of the assorted wine of vacuum system backflow, the assorted wine of water wash column return tank backflow, rectifying tower and the assorted wine of rectifying tower return tank, the wine pump enters recovery tower after the waste water preheating at the bottom of assorted wine preheater is by recovery tower by mixing; Recovery cat head wine vapour is after the first thick auxilliary tower reboiler condensation, and phlegma enters the recovery tower return tank, and condensing is not sent into last cold the coagulating of recovery tower through the first thick auxilliary tower reboiler shell-side vapor phase exit, and phlegma enters the recovery tower return tank.Send the recovery tower backflow by the recovery tower reflux pump, the topping still middle part is taken out wine liquid and is entered interior the concentrating of thick auxilliary tower, and the wine vapour after concentrating returns the topping still middle part, and the nonalcoholic waste water after concentrating is discharged out-of-bounds at the bottom of slightly auxilliary tower.
Taking out volumetric concentration from the 25th layer of column plate of topping still is that the wine liquid of 20-25% enters thick auxilliary tower and concentrates, and the wine liquid after concentrating returns the 25th layer of column plate place of topping still.
Described topping still, water wash column, rectifying tower, methanol column, recovery tower and slightly cat head working pressure, cat head and the column bottom temperature of auxilliary tower be respectively:
Topping still cat head absolute pressure 0.3-0.6kg/cm
2, tower top temperature 50-70 ℃, column bottom temperature 70-90 ℃;
Water wash column cat head absolute pressure 0.9-1.2kg/cm
2, tower top temperature 90-105 ℃, column bottom temperature 90-110 ℃;
Rectifying tower cat head absolute pressure 2.5-3.5kg/cm
2, tower top temperature 102-112 ℃, column bottom temperature 130-145 ℃;
Methanol column cat head absolute pressure 1.5-2.5kg/cm
2, tower top temperature 85-105 ℃, column bottom temperature 90-110 ℃;
Recovery tower cat head absolute pressure 1.0-1.1kg/cm
2, tower top temperature 85-95 ℃, column bottom temperature is 110-120 ℃;
Thick auxilliary column overhead absolute pressure 0.35-0.5kg/cm
2, tower top temperature 65-75 ℃, column bottom temperature is 75-85 ℃.
Advantage of the present invention is: 1. the present situation that is fit to present thick mash fermentation.Because the raising of ripe raw spirit degree, the corresponding reduction of the thermal load of topping still has increased thick auxilliary tower this moment, the heat of affluence can be used for concentrating of thick wine, help increasing row's aldehyde effect and improving mouthfeel, slightly the waste water of auxilliary tower can be got rid of the heavy constituent of a part of acids.These raisings to quality product are helpful.2. because thick auxilliary tower has reclaimed a part of waste water, improve the concentration of useless wine with dregs, helped reducing the steam consumption of subsequent disposal workshop section.3. realize the mutual coupling utilization of energy, guaranteed the stability of technological operation, be convenient to be provided with online remote centralized control, can also save steam consumption and cooling-water consumption, environmental protection and energy saving by robot control system(RCS).The ton product steam consumption of this technology is about 2.2 tons.
Description of drawings
Accompanying drawing 1 is the device schema of the embodiment of the invention;
1, first ripening wine with dregs preheater, 2, the second ripe wine with dregs preheater, 3, the topping still condenser, 4, the vacuum cleaning tower, 5, vacuum pump, 6, topping still, 7, useless wine with dregs pump, 8, the first topping still reboiler, 9, the first topping still recycle pump, 10, the second topping still reboiler, 11, the second topping still recycle pump, 12, thick wine jar, 13, thick wine pump, 14, crude wine preheater, 15, water wash column, 16, the water wash column end is cold, and 17, the water wash column return tank, 18, the water wash column reflux pump, 19, the light wine pump, 20, the light wine preheater, 21, rectifying tower, 22, the water wash column reboiler, 23, the methanol column reboiler, 24, the rectifying tower end is cold, and 25, the rectifying tower return tank, 26, the rectifying tower reflux pump, 27, the rectifying tower reboiler, 28, the rectifying tower waste water pump, 29, methanol column, 30, thick auxilliary tower, 31, the methanol column return tank, 32, the methanol column reflux pump, 33, discharge pump, 34, the finished product water cooler, 35, the finished product jar, 36, the finished product volume pump, 37, assorted wine jar, 38, assorted wine pump, 39, assorted wine preheater, 40, recovery tower, 41, the recovery tower end is cold, 42, the recovery tower return tank, 43, the recovery tower reflux pump, 44, the recovery tower waste water pump, 45, the potato spirit water cooler, 46, the potato spirit separator, 47, the potato spirit basin, 48, the fusel oil pump, 49, flash tank, 50, the second thick auxilliary tower reboiler, 51, the first thick auxilliary tower reboiler.
Embodiment
Embodiment:
Consult Fig. 1, a kind of superfine edible ethanol six-column differential-pressure distillation device is: comprise topping still 6, water wash column 15, rectifying tower 21, methanol column 29, recovery tower 40 and thick auxilliary tower 30, wherein ripe wine with dregs import connects first ripening wine with dregs preheater 1 pipe side in turn by pipeline and links to each other with the second ripe wine with dregs preheater 2 pipe sides and with topping still 6 imports, topping still 6 tops link to each other with the first mash preheater, 1 shell-side inlet through pipeline, the outlet of first ripening wine with dregs preheater 1 shell-side links to each other with thick wine jar 12 through pipeline, first ripening wine with dregs preheater 1 shell-side vapor phase exit connects the shell-side inlet of topping still condenser 3, the shell-side outlet of topping still condenser 3 connects thick wine jar 12, the shell-side gaseous phase outlet pipe connection vacuum cleaning tower 4 of topping still condenser 3, the top of vacuum cleaning tower 4 connects emptying by vacuum pump 5; Thick wine jar 12 bottoms are communicated with crude wine preheater 14 imports by pipeline through thick wine pump 13, crude wine preheater 14 outlets are by pipe connection water wash column 15 inlets, water wash column 15 tops link to each other with the first topping still reboiler, 8 shell-sides inlet through pipeline, the first topping still reboiler, 8 shell-sides have two outlets, link to each other through the cold 16 pipe side entrances in pipeline and water wash column return tank 17 inlets and water wash column end respectively, the cold 16 pipe side outlets in water wash column end link to each other with water wash column return tank 17 inlets through pipeline, water wash column return tank 17 tops link to each other with vacuum cleaning tower 4 through pipeline, water wash column return tank 17 bottoms link to each other with water wash column reflux pump 18 inlet ends through pipeline, and water wash column reflux pump 18 exit end link to each other with water wash column 15 top refluxing openings through pipeline; Water wash column 15 bottoms link to each other with light wine preheater 20 inlets through light wine pump 19,20 outlets of light wine preheater link to each other with rectifying tower 21 inlets, rectifying tower 21 tops link to each other with water wash column reboiler 22 shell-sides inlet through pipeline, water wash column reboiler 22 shell-sides are provided with two outlets, link to each other with rectifying tower return tank 25 inlets with methanol column reboiler 23 shell-sides inlet through pipeline respectively, methanol column reboiler 23 shell-sides are provided with two outlets, link to each other through the cold 24 pipe side entrances in pipeline and rectifying tower return tank 25 inlets and rectifying tower end respectively, the cold 24 pipe side outlets in rectifying tower end link to each other with rectifying tower return tank 25 through pipeline; 25 ends of rectifying tower return tank, link to each other with rectifying tower reflux pump 26 inlets through pipeline, rectifying tower reflux pump 26 exit end link to each other with rectifying tower 21 top refluxing openings through pipeline, rectifying tower 21 bottoms connect rectifying tower reboiler 27 inlets and light wine preheater 20 second inlets respectively by pipeline, 20 second outlets of light wine preheater are through pipe connection rectifying tower waste water pump 28 inlets, 28 outlets of rectifying tower waste water pump connect crude wine preheater 14 second inlets and water wash column 15 tops inlet respectively through pipeline, and second of crude wine preheater 14 exports out the battery limit (BL); The outlet of rectifying tower 21 heavy wines is through pipe connection methanol column 29 inlets, methanol column 29 tops link to each other with the second topping still reboiler, 10 shell-sides inlet through pipeline, first outlet of the second topping still reboiler, 10 shell-sides links to each other with methanol column return tank 31 inlets through pipeline, methanol column return tank 31 outlet at bottoms link to each other with methanol column reflux pump 32 inlet ends through pipeline, methanol column reflux pump 32 exit end link to each other with methanol column 29 top refluxing openings through pipeline, and methanol column return tank 31 is provided with industrial spirit extraction mouth; 29 ends of methanol column, are through pipe connection methanol column reboiler 23 and discharge pump 33 inlets, discharge pump 33 outlet conduits connect finished product water cooler 34 pipe side entrances, finished product water cooler 34 pipe side outlet pipe connection finished product jars 35, the superfine edible ethanol of the finished product in the finished product jar 35 is sent the battery limit (BL) by finished product volume pump 36.Reflux in 4 ends of vacuum cleaning tower, the 17 assorted wine outlets of water wash column return tank, the assorted wine outlet of rectifying tower 21 and the assorted wine outlet of rectifying tower return tank 25 are connected with assorted wine jar 37 through pipeline respectively, assorted wine jar 37 bottoms connect assorted wine preheater 39 inlets through assorted wine pump 38, assorted wine preheater 39 outlets are through pipe connection recovery tower 40,6 ends of topping still, connect the first topping still recycle pump 9 respectively by pipeline, the second topping still recycle pump, 11 inlets and useless wine with dregs pump 7 inlets, 9 outlets of the first topping still recycle pump connect the first topping still reboiler, 8 pipe side entrances, the second topping still recycle pump, 11 inlet ducts connect the second topping still reboiler, 10 pipe side entrances, and useless wine with dregs pump 7 outlets connect outside the battery limit (BL).Topping still 6 centre exits are through slightly auxilliary tower 30 inlets of pipe connection, thick auxilliary tower 30 top exit inlet pipe roads connect topping still 6 centre entrances, thick auxilliary tower 30 bottoms are through the external waste water of pipe connection, recovery tower 40 top exits link to each other with the first thick auxilliary tower reboiler 51 shell-sides inlet through pipeline, first thick auxilliary tower reboiler 51 shell-sides are provided with two outlets, link to each other through the cold 41 pipe sides in pipeline and recovery tower return tank 42 and recovery tower end respectively, the cold 41 pipe side outlets in recovery tower end connect recovery tower return tank 42, second outlet of the second topping still reboiler, 10 shell-sides links to each other with the second thick auxilliary tower reboiler 50 shell-sides inlet through pipeline, and the second thick auxilliary tower reboiler 50 shell-sides outlet links to each other with methanol column return tank 31 through pipeline.The outlet of recovery tower 40 fusels connects potato spirit water cooler 45 pipe side entrances, potato spirit water cooler 45 pipe side outlet pipe connection potato spirit separators 46, potato spirit separator 46 tops feed a water, the oil phase side connects potato spirit basin 47, the aqueous phase side pipe connection wine jar 37 of mixing, potato spirit basin 47 bottom pipe connect fusel oil pump 48.Rectifying tower reboiler 27 shell-sides inlet connects steam system, and outlet conduit connects flash tank 49, and flash tank 49 top ducts connect recovery tower 40, and bottom pipe connects second ripe wine with dregs preheater 2 shell-sides.
Superfine edible ethanol six-column differential-pressure distil process of the present invention is: ripe wine with dregs is through first ripening wine with dregs preheater 1, enter topping still 6 after second ripe wine with dregs preheater 2 preheatings, the thick wine vapour at topping still 6 tops is successively through entering thick wine jar 12 after first ripening wine with dregs preheater 1 and 3 condensations of topping still condenser, thick wine in the thick wine jar 12 is through crude wine preheater 14,21 end of the part rectifying tower waste water preheating that comes with rectifying tower waste water pump 28 pumps is laggard goes into water wash column 15, thick wine is washed through rectifying tower 21 waste water in water wash column 15, the light wine of water wash column 15 bottoms enters 20 preheatings of light wine preheater through light wine pump 19, by entering rectifying tower 21 after the waste water preheating of 21 end of rectifying tower, water wash column 15 top wine vapour are after 8 condensations of the first topping still reboiler, phlegma enters in the water wash column return tank 17 and returns, deliver to water wash column 15 internal reflux through water wash column reflux pump 18, non-condensable gas enters vacuum cleaning tower 4, the light wine that enters in the rectifying tower 21 enters methanol column 29 through the concentrated back of distillation from rectifying tower 21 top heavy wine outlet extraction, rectifying tower 21 top wine vapour pass through water wash column reboiler 22 and 23 condensations of methanol column reboiler successively, phlegma enters in the rectifying tower return tank 25, sends rectifying tower 21 back to by rectifying tower reflux pump 26 and refluxes; The heavy wine that enters methanol column 29 is got rid of methyl alcohol, bottom wine liquid is sent through discharge pump 33, methanol column 29 top wine vapour are successively through after 10, second thick auxilliary tower reboiler 50 condensations of the second topping still reboiler, phlegma enters methanol column return tank 31, send methanol column 29 tops back to through methanol column reflux pump 32 and reflux, methanol column return tank 31 proposes industrial spirit; From the assorted wine of vacuum system backflow, the assorted wine of water wash column return tank 17 backflows, the assorted wine that assorted wine that rectifying tower 21 takes out and rectifying tower return tank 25 take out enters assorted wine jar 37 respectively, after assorted wine preheater 39 is by the waste water preheating of 40 end of recovery tower, enter recovery tower 40 by assorted wine pump 38, recovery tower 40 top wine vapour are after first thick auxilliary tower reboiler 51 condensations, phlegma enters recovery tower return tank 42, send recovery tower 40 to reflux by recovery tower reflux pump 43, topping still 6 middle parts are taken out wine liquid and are entered in the thick auxilliary tower 30 concentrated, wine vapour after concentrating returns topping still 6 middle parts, and the nonalcoholic waste water after concentrating was discharged out-of-bounds from thick auxilliary 30 ends of tower.
Recovery tower 40 top wine vapour enter first thick auxilliary tower reboiler 51 condensations, and condensing is not sent into recovery tower cold 41 condensations in end through the first thick auxilliary tower reboiler 51 shell-side vapor phase exits, and phlegma enters recovery tower return tank 42.
Taking out volumetric concentration from the 25 layer of column plate of topping still 6 is that the wine liquid of 20-25% enters thick auxilliary tower 30 and concentrates, and the wine liquid after concentrating returns the 25 layer of column plate place of topping still,
Topping still 6, water wash column 15, rectifying tower 21, methanol column 29, recovery tower 40 and slightly cat head working pressure, cat head and the column bottom temperature of auxilliary tower 30 be respectively:
Topping still 6 cat head absolute pressure 0.3-0.6kg/cm
2, tower top temperature 50-70 ℃, column bottom temperature 70-90 ℃;
Water wash column 15 cat head absolute pressure 0.9-1.2kg/cm
2, tower top temperature 90-105 ℃, column bottom temperature 90-110 ℃;
Rectifying tower 21 cat head absolute pressure 2.5-3.5kg/cm
2, tower top temperature 102-112 ℃, column bottom temperature 130-145 ℃;
Methanol column 29 cat head absolute pressure 1.5-2.5kg/cm
2, tower top temperature 85-105 ℃, column bottom temperature 90-110 ℃;
40 recovery tower cat head absolute pressure 1.0-1.1kg/cm
2, tower top temperature 85-95 ℃, column bottom temperature is 110-120 ℃;
Thick auxilliary tower 30 cat head absolute pressure 0.35-0.5kg/cm
2, tower top temperature 65-75 ℃, column bottom temperature is 75-85 ℃.
To produce 50000 tons of edible ethanol plant modifications per year is example, further specifies beneficial effect of the present invention:
This device such as application number are 2007100305508 and are called disclosed device in " five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technology thereof " before transforming, and it produces high grade edible spirit, and each tower operating parameters is respectively:
Topping still cat head absolute pressure 0.3-0.6kg/cm
2, tower top temperature 50-70 ℃, column bottom temperature 70-90 ℃;
Water wash column cat head absolute pressure 0.7-1.0kg/cm
2, tower top temperature 90-105 ℃, column bottom temperature 90-110 ℃;
Rectifying tower cat head absolute pressure 2.5-3.5kg/cm
2, tower top temperature 102-112 ℃, column bottom temperature 127-142 ℃;
Methanol column cat head absolute pressure 1.5-2.5kg/cm
2, tower top temperature 85-105 ℃, column bottom temperature 90-110 ℃;
Recovery tower cat head absolute pressure 1.0-1.1kg/cm
2, tower top temperature 78-85 ℃, column bottom temperature is 102-115 ℃.
215.8 tons/hour of come from fermentation workshop section 30 ℃ maturing fermentation wine with dregs that contain wine 10.5% (v/v), after being preheating to 52 ℃, first ripening wine with dregs preheater 1 is preheating to 62 ℃ by the second ripe wine with dregs preheater 2 again, enter by the topping still top then, come out from the topping still top 66 ℃ contain thick wine vapour about wine 58% (v/v) after first ripening wine with dregs preheater and topping still condenser condenses, again by sending into water wash column after the crude wine preheater preheating, after the preheating of light wine preheater, send into rectifying tower from the 95 ℃ of light wine that contain about wine 15% (v/v) after washing that come out in the water wash column bottom, after rectifying concentrates 108 ℃ contain the concentrated wine of wine 95% or more and send into methanol column after by the rectifier extraction and make with extra care, after the refining liquor liquid that after refining 98 ℃ contain wine 95.5% is discharged by the methanol column bottom, be cooled to 30 ℃, promptly obtain 18.9 tons/hour of finished product high grade edible spirits, the ton product steam consumption of this technology is about 2.3 tons.
Improved device is a superfine edible ethanol six-column differential-pressure distillation device of the present invention, and its each column overhead working pressure, cat head and column bottom temperature are respectively:
Topping still 6 cat head absolute pressure 0.3-0.6kg/cm
2, tower top temperature 50-70 ℃, column bottom temperature 70-90 ℃;
Water wash column 15 cat head absolute pressure 0.9-1.2kg/cm
2, tower top temperature 90-105 ℃, column bottom temperature 90-110 ℃;
Rectifying tower 21 cat head absolute pressure 2.5-3.5kg/cm
2, tower top temperature 102-112 ℃, column bottom temperature 130-145 ℃;
Methanol column 29 cat head absolute pressure 1.5-2.5kg/cm
2, tower top temperature 85-105 ℃, column bottom temperature 90-110 ℃;
Recovery tower 40 cat head absolute pressure 1.0-1.1kg/cm
2, tower top temperature 85-95 ℃, column bottom temperature is 110-120 ℃;
Thick auxilliary tower 30 cat head absolute pressure 0.35-0.5kg/cm
2, tower top temperature 65-75 ℃, column bottom temperature is 75-85 ℃.
From 30 ℃ of next maturing fermentation wine with dregs that contain wine 10.5% (v/v) of fermentation workshop section, after being preheating to 51 ℃, first ripening wine with dregs preheater 1 is preheating to 61 ℃ by the second ripe wine with dregs preheater 2 again, enter by the 25th layer of column plate place of topping still 6 then, establish a upflow tube at thick the 25th layer of column plate place of tower, making 22% (v/v) low-concentration ethanol of backflow enter thick auxilliary tower further concentrates, 60% (v/v) wine vapour after concentrating returns 25 layers in thick tower again, come out from topping still 6 tops 55 ℃ contain thick wine vapour about wine 87% (v/v) after first ripening wine with dregs preheater 1 and 3 condensations of topping still condenser, again by sending into water wash column 15 after crude wine preheater 14 preheatings, the 97 ℃ of light wine that contain about wine 15% (v/v) after washing that come out from water wash column 15 bottoms are sent into rectifying tower 21 after 20 preheatings of light wine preheater, after rectifying concentrates 108 ℃ contain the concentrated wine of wine 96% or more and send into methanol column 29 after by rectifying tower 21 top extraction and make with extra care, after the refining liquor liquid that after refining 98 ℃ contain wine 96.2% is discharged by methanol column 29 bottoms, be cooled to 30 ℃, promptly obtain the superfine edible ethanol of finished product, the ton product steam consumption of this technology is about 2.2 tons.Than 2.7-2.8 ton advanced in the prior art, also save 0.5-0.6 ton steam.
The contrast before and after transforming as can be seen, use device of the present invention can adapt to the higher ripe mash of concentration, the thick auxilliary tower that increases can reclaim more waste water, useless wine with dregs concentration improves, help reducing the steam consumption of subsequent disposal workshop section, discharge more acids heavy constituent simultaneously, the thick wine in the topping still is concentrated, the corresponding thermal load that reduces topping still has reduced the consumption of steam on the whole.
The quality product of device production edible ethanol is as shown in the table before and after transforming:
As can be seen from the above table, for indexs such as very important in the industry ethanol content, methyl alcohol, n-propyl alcohol, oxidation test, sulfuric acid test and total acids, meet or exceed superfine edible ethanol standard.
Above-listed detailed description is at the specifying of one of the present invention embodiment, and this embodiment is not in order to limiting claim of the present invention, and the equivalence that all the present invention of disengaging do is implemented or change, all should be contained in the claim of this case.
Claims (5)
1. superfine edible ethanol six-column differential-pressure distillation device, comprise topping still, water wash column, rectifying tower, methanol column, recovery tower and thick auxilliary tower, wherein ripe wine with dregs import connects first ripening wine with dregs preheater tube side in turn by pipeline and links to each other with the second ripe wine with dregs preheater tube side and with the topping still import, the topping still top links to each other with first mash preheater shell-side inlet through pipeline, the first mash preheater shell-side vapor phase exit links to each other with the topping still condenser inlet, the outlet of topping still condenser liquid phase, the outlet of first ripening wine with dregs preheater shell-side links to each other with thick wine jar through pipeline, thick wine pot bottom is communicated with the crude wine preheater import by pipeline through thick wine pump, the crude wine preheater outlet is by pipe connection water wash column inlet, the water wash column top links to each other with first topping still reboiler shell-side inlet through pipeline, the first topping still reboiler shell-side has two outlets, link to each other with water wash column return tank inlet with the cold inlet in water wash column end through pipeline respectively, the water wash column cold outlet in end links to each other with water wash column return tank inlet, water wash column return tank top links to each other with vacuum system through pipeline, water wash column return tank bottom links to each other with water wash column reflux pump inlet end through pipeline, and water wash column reflux pump exit end links to each other with water wash column top refluxing opening through pipeline; The water wash column bottom links to each other with light wine preheater inlet through the light wine pump, the outlet of light wine preheater links to each other with the rectifying tower inlet, the rectifying tower top links to each other with water wash column reboiler shell-side inlet through pipeline, water wash column reboiler shell-side is provided with two outlets, link to each other with rectifying tower return tank inlet with methanol column reboiler shell-side inlet through pipeline respectively, methanol column reboiler shell-side is established two outlets, respectively through pipeline and rectifying tower return tank inlet and rectifying tower cold linking to each other of end, the rectifying tower cold outlet in end links to each other with the rectifying tower return tank, link to each other with rectifying tower reflux pump inlet through pipeline at the bottom of the rectifying tower return tank, rectifying tower reflux pump exit end links to each other with rectifying tower top refluxing opening through pipeline, the outlet of rectifying tower heavy wine enters the mouth through the pipe connection methanol column, the methanol column top links to each other with second topping still reboiler shell-side inlet through pipeline, first outlet of the second topping still reboiler shell-side links to each other with methanol column return tank inlet through pipeline, methanol column return tank outlet at bottom links to each other with methanol column reflux pump inlet end through pipeline, methanol column reflux pump exit end links to each other with methanol column top refluxing opening through pipeline, enters the mouth through the pipe connection discharge pump at the bottom of the methanol column; Vacuum system refluxes, the assorted wine of water wash column return tank exports, the assorted wine of rectifying tower exports and the assorted wine outlet of rectifying tower return tank is connected with assorted wine jar through pipeline respectively, assorted wine pot bottom connects assorted wine preheater inlet through assorted wine pump, assorted wine preheater outlet is through the pipe connection recovery tower, it is characterized in that: described topping still centre exit is through the described thick auxilliary tower inlet of pipe connection, described thick auxilliary top of tower outlet is through the described topping still centre entrance of pipe connection, and described thick auxilliary tower bottom is through the external waste water of pipe connection; Described recovery tower top exit links to each other with the first thick auxilliary tower reboiler shell-side inlet through pipeline, the first thick auxilliary tower reboiler shell-side has two outlets, through pipeline and described recovery tower return tank and described recovery tower cold linking to each other of end, the described recovery tower cold outlet in end links to each other with described recovery tower return tank through pipeline respectively; Second outlet of the described second topping still reboiler shell-side links to each other with the second thick auxilliary tower reboiler shell-side inlet through pipeline, and the second thick auxilliary tower reboiler shell-side outlet links to each other with described methanol column return tank through pipeline.
2. a kind of superfine edible ethanol six-column differential-pressure distillation device according to claim 1 and 2 is characterized in that: described topping still centre exit and centre entrance lay respectively at the 25th layer of column plate place.
3. the production technique of a superfine edible ethanol six-column differential-pressure distillation device as claimed in claim 1, it is characterized in that: ripe wine with dregs is through first ripening wine with dregs preheater, enter topping still after the second ripe wine with dregs preheater preheating, the thick wine vapour at topping still top is successively through entering thick wine jar after first ripening wine with dregs preheater and the topping still condenser condenses, thick wine in the thick wine jar is through crude wine preheater, the waste water preheating is laggard at the bottom of the part rectifying tower that comes with rectifying tower waste water pump pump goes into water wash column, thick wine passes through the washing of rectifying tower waste water in water wash column after, the light wine of water wash column bottom enters the preheating of light wine preheater through the light wine pump, by entering rectifying tower after the waste water preheating at the bottom of the rectifying tower, water wash column top wine vapour is after the first topping still reboiler condensation, phlegma enters in the water wash column return tank, deliver to the water wash column internal reflux through the water wash column reflux pump, non-condensable gas enters vacuum system, the light wine that enters in the rectifying tower enters methanol column through the concentrated back of distillation from rectifier heavy wine outlet extraction, rectifying tower top wine vapour passes through water wash column reboiler and the condensation of methanol column reboiler successively, phlegma enters in the rectifying tower return tank, sends rectifying tower back to by the rectifying tower reflux pump and refluxes; After entering the heavy wine discharge methyl alcohol of methanol column, bottom wine liquid is sent through discharge pump, methanol column top wine vapour is successively through the second topping still reboiler, after the second thick auxilliary tower reboiler condensation, phlegma enters the methanol column return tank, send the methyl alcohol trim the top of column back to through the methanol column reflux pump, from the assorted wine of vacuum system backflow, the assorted wine of water wash column return tank backflow, the assorted wine of rectifying tower and the assorted wine of rectifying tower return tank enter assorted wine jar respectively, at the bottom of assorted wine preheater is by recovery tower, enter recovery tower after the waste water preheating by assorted wine pump, reclaim cat head wine vapour after the first thick auxilliary tower reboiler condensation, phlegma enters the recovery tower return tank, send recovery tower to reflux by the recovery tower reflux pump, the topping still middle part is taken out wine liquid and is entered interior the concentrating of thick auxilliary tower, wine vapour after concentrating returns the topping still middle part, nonalcoholic waste water after concentrating is discharged out-of-bounds at the bottom of thick auxilliary tower, reclaim cat head wine vapour and enter the first thick auxilliary tower reboiler condensation, condensing is not sent into last cold the coagulating of recovery tower through the first thick auxilliary tower reboiler shell-side vapor phase exit, and phlegma enters the recovery tower return tank.
4. the production technique of a kind of superfine edible ethanol six-column differential-pressure distillation device according to claim 3, it is characterized in that: taking out volumetric concentration from the 25th layer of column plate of topping still is that the wine liquid of 20-25% enters thick auxilliary tower concentration, and the wine liquid after concentrating returns the 25th layer of column plate place of topping still.
5. the production technique of a kind of superfine edible ethanol six-column differential-pressure distillation device according to claim 4 is characterized in that: described topping still, water wash column, rectifying tower, methanol column, recovery tower and slightly cat head working pressure, cat head and the column bottom temperature of auxilliary tower be respectively:
Topping still cat head absolute pressure 0.3-0.6kg/cm
2, tower top temperature 50-70 ℃, column bottom temperature 70-90 ℃;
Water wash column cat head absolute pressure 0.9-1.2kg/cm
2, tower top temperature 90-105 ℃, column bottom temperature 90-110 ℃;
Rectifying tower cat head absolute pressure 2.5-3.5kg/cm
2, tower top temperature 102-112 ℃, column bottom temperature 130-145 ℃;
Methanol column cat head absolute pressure 1.5-2.5kg/cm
2, tower top temperature 85-105 ℃, column bottom temperature 90-110 ℃;
Recovery tower cat head absolute pressure 1.0-1.1kg/cm
2, tower top temperature 85-95 ℃, column bottom temperature is 110-120 ℃;
Thick auxilliary column overhead absolute pressure 0.35-0.5kg/cm
2, tower top temperature 65-75 ℃, column bottom temperature is 75-85 ℃.
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