CN101580457B - Device and process for preparing absolute ethyl alcohol by taking fermented liquor as the raw material - Google Patents
Device and process for preparing absolute ethyl alcohol by taking fermented liquor as the raw material Download PDFInfo
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- CN101580457B CN101580457B CN2008100280473A CN200810028047A CN101580457B CN 101580457 B CN101580457 B CN 101580457B CN 2008100280473 A CN2008100280473 A CN 2008100280473A CN 200810028047 A CN200810028047 A CN 200810028047A CN 101580457 B CN101580457 B CN 101580457B
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Abstract
The invention discloses a device and a process for preparing absolute ethyl alcohol by taking the fermented liquor as the raw material. The device comprises a dealdehyding tower, a degassing tower anda first crude distillation tower which are vertically overlapped in sequence, a first fine distillation tower, a second crude distillation tower and a second fine distillation tower which are vertica lly overlapped, a molecular sieve A and a molecular sieve B which are arranged in parallel, and a fermented liquor preheater, a second fermented liquor preheater and a third fermented liquor preheaterwhich are in series connected through tube passes in sequence; and the mutual matching and utilization of energy of all the towers at the distillation section can be realized by adopting the differen tial-pressure thermal coupling technology, the micro positive pressure operation of a molecular sieve is realized through a pressure control system, and the service life of the molecular sieve is prolonged, therefore, the overall steam consumption for preparing each ton of finished absolute ethyl alcohol by a fermentation method is reduced to 1.5-2.0 ton, and compared with the present normally-used fermentation process for preparing the absolute ethyl alcohol with 2.2-3.0 ton steam/tone edible alcohol in China, the process saves the steam consumption by 30-40 percent and the circulating water by 15 ton when each ton of finished absolute ethyl alcohol is prepared.
Description
Technical field
The present invention relates to a kind of technology and device thereof of producing absolute ethyl alcohol with fermentation liquid.
Technical background
Depleted day by day along with Nonrenewable energy resources such as global oil and raw coal is the raw material production absolute ethyl alcohol with reproducible biomass, and then adds effective substitute that alcohol fuel that auxiliary makes can be used as fuel such as gasoline.The maturing fermentation mash that biomass material obtains by fermentation can make absolute ethyl alcohol through distillation, dehydration; Traditional raw spirit distillation dehydration technology mainly contains following several kinds:
1, two tower air distillations, conventional dehydration technology:
Two towers are topping still and rectifying tower, and two towers all adopt air distillation to obtain the alcohol in high concentration about concentration 95% (v/v); Dewatering process adopts azeotropic distillation or molecular sieve dehydration technology more.Distil process is not owing to adopt differential pressure thermal coupling technology, so energy consumption is big, recirculated cooling water consumes highly, basically passes into disuse now.Azeotropic distillation adopts benzene or hexanaphthene for taking off the band agent, and is prone to cause environmental pollution with benzene for taking off the band agent time, and this dewatering process exists energy consumption more greatly, once to drop into bigger shortcoming equally, present application also less.Applying high voltage absorption caused the loss of molecular sieve higher when traditional molecular sieve dehydration was used absorption, and energy consumption is also taught greatly.
2, two tower differential distillations, conventional dehydration technology:
Two towers are similarly topping still and rectifying tower, and topping still is a decompression operation, and rectifying tower is a pressurized operation.Two tower differential distillations obtain the laggard dehydration of alcohol in high concentration workshop section and comprise laggard dehydration workshop section of liquid phase vaporization and the vapour phase two kinds of technologies of workshop section of directly advancing to dewater again.Dewatering process adopts azeotropic distillation or molecular sieve dehydration technology equally.Energy consumption and recirculated water consumption in the time of partly reducing distillation through differential pressure thermal coupling distillation technique, but there have energy to utilize equally to be insufficient, and the recirculated cooling water consumption does not have significantly reduced shortcoming; The shortcoming of dehydration workshop section does not solve equally.
3, three-tower differential pressure distillation, conventional dehydration technology:
Three towers are topping still, and water wash column and rectifying tower, topping still are decompression operation, and water wash column is a micro-negative pressure operation, and rectifying tower is a pressurized operation.For the limited minimizing impurity of workshop section that advances to dewater, this technology spy has increased water wash column.Dewatering process also adopts smart stream of azeotropic or molecular sieve dehydration technology.Because distillation workshop section is that the quality that has improved raw spirit has been set up tower, although also adopt differential pressure technology energy consumption and recirculated cooling water consumption higher equally.And the problem that dewatering process exists still.
Summary of the invention
The purpose of this invention is to provide a kind of is the device and the technology of raw material production absolute ethyl alcohol with the fermentation liquid, can reach to improve the raw spirit quality, reduces the effect of polluting, and effectively cuts down the consumption of energy and reduces the consumption of recirculated cooling water.
For realizing above-mentioned purpose; Production equipment of the present invention is: a kind of is the device of raw material production absolute ethyl alcohol with the fermentation liquid; It comprises stacked in order up and down dealdehyder tower, degassing tower and first topping still, the first stacked up and down rectifying tower and second topping still, and second rectifying tower; Molecular sieve-4 A and molecular sieve B that parallel connection is provided with, the placed in-line successively first ripening wine with dregs of tube side preheater, the second ripe wine with dregs preheater, the 3rd ripe wine with dregs preheater; Wherein first ripening wine with dregs preheater tube side entrance connects ripe beer feed(raw material)inlet; The 3rd ripe wine with dregs preheater tube side outlet pipe connection degassing tower top inlet; The dealdehyder tower top links to each other with first ripening wine with dregs preheater shell-side inlet through pipeline, and the outlet of first ripening wine with dregs preheater shell-side links to each other with dealdehyder tower top refluxing opening through dealdehyder tower return tank, dealdehyder tower reflux pump; The first topping still top vapor phase exit links to each other with the second ripe wine with dregs preheater shell-side inlet through pipeline; The second ripe wine with dregs preheater shell-side outlet conduit connects thick wine jar; Thick wine pot bottom outlet connects crude wine preheater first inlet through thick wine pump line road, crude wine preheater first outlet links to each other with second rectifying tower middle part opening for feed through pipeline; The first topping still top liquid phase outlet conduit connects ripe wine with dregs extraction pump intake; Ripe wine with dregs extraction pump discharge pipeline connects into ripe wine with dregs preheater first inlet; Ripe wine with dregs preheater first outlet links to each other with second topping still top inlet through pipeline; The second topping still outlet at bottom links to each other with ripe wine with dregs preheater second inlet through pipeline, and ripe wine with dregs preheater second outlet links to each other with the wastewater treatment tubing system through pipeline; First outlet of the first rectifying tower top links to each other with first topping still, first reboiler shell-side inlet through pipeline; First topping still, first reboiler shell-side outlet is through the first rectifying tower return tank, the first rectifier reflux inlet that links to each other with the first rectifying tower reflux pump pipeline; Second outlet of the first rectifying tower top is through suphtr tube side and parallelly connected molecular sieve-4 A and molecular sieve B absorption inlet pipe connection; The molecular sieve-4 A of parallel connection and the absorption of molecular sieve B outlet are connected the 3rd ripe wine with dregs preheater shell-side inlet and regeneration vapour superheater tube side entrance respectively; The 3rd ripe wine with dregs preheater shell-side outlet connects the finished product jar; Regeneration vapour superheater tube side outlet connects the molecular sieve-4 A of parallel connection and the regeneration inlet of molecular sieve B; The regeneration outlet of molecular sieve-4 A and molecular sieve B is connected thick wine jar through light wine condensing surface tube side respectively, and suphtr is connected steam system respectively with the shell-side inlet of regeneration vapour suphtr; The outlet of the second rectifying tower top links to each other with second topping still reboiler shell-side inlet through pipeline; The outlet of the second topping still reboiler shell-side links to each other with the second rectifying tower reflux pump inlet end through the second rectifying tower return tank; The second rectifying tower reflux pump exit end links to each other with the second rectifier reflux inlet and light wine preheater first inlet respectively through pipeline; Light wine preheater first outlet conduit connects the first rectifier refluxing opening; The first rectifier bottoms light wine outlet conduit connects light wine preheater second inlet, and light wine preheater second outlet conduit connects thick wine jar; The outlet of second rectifier bottoms links to each other with crude wine preheater second inlet through pipeline, and crude wine preheater second outlet is through the pipe connection Waste Water Treatment, and the second rectifying tower reboiler shell-side inlet duct connects steam system.
To slightly saute in the device of the present invention with rectifying and be arranged to two sections operations respectively, being equivalent to slightly heat up in a steamer with rectifying is respectively two to imitate operation, and distilling effect is good, and the quality product of production is high; Dealdehyder tower, degassing tower and first topping still is stacked up and down, first rectifying tower and second topping still is stacked up and down, make full use of the space, cost is practiced thrift in minimizing equipment and pipeline setting, can make full use of down the heat of tower simultaneously, improves energy utilization efficiency; The second rectifying tower top wine vapour is through first rectifying tower and second rectifying tower of refluxing respectively after the condensation; Promptly can conveniently control the load of two rectifying tower; Simultaneously also can reduce influence mutual between two towers, improve device traveling comfort and ease for operation, help further reducing system energy consumption; The first rectifying tower top wine vapour is drawn to molecular sieve dehydration, make the working pressure of molecular sieve obviously reduce, reduced system energy consumption, prolonged the work-ing life of molecular sieve.
As a kind of improvement; Outlet links to each other with the flash tank inlet through pipeline respectively with regeneration vapour suphtr shell-side for the shell-side outlet of the said second rectifying tower reboiler, the shell-side outlet of suphtr; The flash drum overhead outlet links to each other with first topping still, second reboiler shell-side inlet through pipeline; Flash tank outlet at bottom and the outlet of first topping still, the second reboiler shell-side are respectively through pipe connection back boiler tubing system; The heat of steam condensate in the device be can make full use of, steam consumption and recirculated water consumption further saved.
The present invention is that the production technique of raw material production absolute ethyl alcohol is with the fermentation liquid: the ripe wine with dregs that the workshop section of fermenting certainly gets into the degassing tower top successively after first ripening wine with dregs preheater, the second ripe wine with dregs preheater and the 3rd ripe wine with dregs preheater preheating; The thick wine vapour that comes out in the degassing tower top directly gets into the dealdehyder tower full gear;, the wine vapour that the full gear top of tower comes gets into the dealdehyder tower return tank after getting into the condensation of first ripening wine with dregs preheater; Pump into dealdehyder tower by the dealdehyder tower reflux pump again; Get into the second ripe wine with dregs preheater from the thick wine vapour of the first topping still top extraction; After condensation, get into thick wine jar, the ripe wine with dregs after the first topping still top extraction partly degassed full gear gets into second topping still with the extraction of ripe wine with dregs extraction pump after post-mature wine with dregs preheater is with the useless mash preheating in second topping still bottom; Thick wine vapour after second topping still concentrates directly gets into first rectifying tower; The concentrated wine vapour part that the first rectifying tower cat head goes out gets into the overheated back of suphtr and gets into molecular sieve-4 A or molecular sieve B dehydration, after a no watery wine vapour part gets into the 3rd ripe wine with dregs preheater condensation after molecular sieve-4 A or the molecular sieve B dehydration, gets into the finished product temporary storage jar and exports as finished product; Another part does not have watery wine vapour and after the revivifier suphtr is overheated, uses vapour as the regeneration of molecular sieve B or molecular sieve-4 A, and the regeneration vapour of molecular sieve B or molecular sieve-4 A gets into thick wine jar after the light wine condenser condenses; Another part that the first rectifying tower cat head goes out concentrates wine vapour and gets into first topping still, the first reboiler shell-side condensation; Condensation wine liquid pump is gone into first rectifying tower and is refluxed; Light wine from first rectifier bottoms is come out gets into thick wine jar after the preheating of light wine preheater;, the thick wine that thick wine pot bottom comes gets into second rectifying tower after pumping into the crude wine preheater preheating by thick wine pump; The concentrated wine vapour that comes out from the second rectifying tower top gets into the second topping still reboiler shell-side condensation, and condensation wine liquid gets into the second rectifying tower return tank, pumps a part by the second rectifying tower reflux pump and gets into the backflow of second rectifying tower; Another part gets into the first rectifying tower top and refluxes after the cooling of light wine preheater, the second rectifying tower reboiler, suphtr and revivifier suphtr use steam heating respectively.
Steam condensate after the said second rectifying tower reboiler, suphtr and the heating of revivifier suphtr gets into the flash tank flash distillation respectively; The top flash steam gets into first topping still, the second reboiler shell-side and uses as thermal source; So that further utilize heat, reduce system energy consumption.
In the technology of the present invention, the service temperature of controlling at the bottom of each column overhead working pressure, cat head and the tower is respectively:
Dealdehyder tower (5) absolute pressure 0.25～0.35atm, 50～60 ℃ of tower top temperatures, 55～65 ℃ of column bottom temperatures;
Degassing tower (6) absolute pressure 0.3～0.4atm, 60～70 ℃ of tower top temperatures, 65～75 ℃ of column bottom temperatures;
First topping still (7) absolute pressure 0.3～4atm, 65～75 ℃ of tower top temperatures, 80～90 ℃ of column bottom temperatures;
First rectifying tower (24) absolute pressure 1.2～2.2atm, 85～95 ℃ of tower top temperatures, 100～115 ℃ of column bottom temperatures;
Second topping still (25) absolute pressure 1.5～2.5atm, 100～120 ℃ of tower top temperatures, 110～125 ℃ of column bottom temperatures;
Second rectifying tower (32) absolute pressure 4.8～6.0atm, 120～135 ℃ of tower top temperatures, 150～165 ℃ of column bottom temperatures;
Molecular sieve working pressure, service temperature are respectively during the control adsorption and desorption:
Absolute pressure 1.0～2.0atm during absorption, 100～120 ℃ of temperature;
Absolute pressure 0.3～0.4atm during desorb, 110～140 ℃ of temperature.
Dealdehyder tower, degassing tower, first topping still all adopt decompression operation, and the thick wine vapour that dealdehyder tower comes is used to supply with first ripening wine with dregs preheater energy, and the thick wine vapour that first topping still comes is used to supply with the second ripe wine with dregs preheater energy.Second topping still adopts positive pressure operation, and thick wine vapour directly gets into first rectifying tower; First rectifying tower adopts positive pressure operation, and the concentrated wine vapour that comes out from the first rectifying tower cat head partly gets into first topping still, first reboiler and supplies with the first topping still energy, and another part wine vapour gets into molecular sieve and carries out adsorption dewatering after suphtr is overheated; Second rectifying tower adopts positive pressure operation; The concentrated wine vapour that comes out from the second rectifying tower cat head gets into the second topping still reboiler and supplies with the second topping still energy; Through the condensed wine liquid of the second topping still reboiler reflux respectively first rectifying tower and second rectifying tower; Reduce operating influence mutual between each tower, improved system's traveling comfort.The useless mash that comes at the bottom of the second topping still tower goes useless poor treatment system through the useless mash that comes at the bottom of the first topping still tower after the ripe wine with dregs heat exchange after ripe wine with dregs preheater and the degassing; Through after crude wine preheater and the thick wine liquid heat exchange from the second rectifying Tata at the bottom of the useless surplus water that heats up in a steamer that comes remove Waste Water Treatment.Molecular sieve adsorption pressure adopts pressure-fired, thereby can prolong the work-ing life that guarantees molecular sieve.
Advantage of the present invention is: adopt differential pressure thermal coupling technology to realize that the energy of each tower of distillation workshop section matees utilization each other; Realize that through pressure control system the micro-pressure operation of molecular sieve prolongs the work-ing life of molecular sieve; Thereby the steam wastage in bulk or weight that makes the fermentative Production absolute ethyl alcohol drops to 1.5～2.0 tons of/ton finished product absolute ethyl alcohols; More about 30%～40% than the steam consumption saving steam of 2.2～3.0 tons of steam/ton edible ethanol of at present domestic fermentative Production absolute ethyl alcohol commonly used, about 15 tons of/ton finished product absolute ethyl alcohols of economized cycle water consumption.
Description of drawings:
Accompanying drawing 1 is a technical process schematic diagram of the present invention;
1. first ripening wine with dregs preheater, 2. the dealdehyder tower end is cold, 3. dealdehyder tower return tank, 4. dealdehyder tower reflux pump, 5. dealdehyder tower; 6. degassing tower, 7. first topping still, the 8. second ripe wine with dregs preheater, 9. the first topping still end is cold, 10. thick wine jar; 11. the 3rd ripe wine with dregs preheater, 12. finished wine vapour ends are cold, 13. finished wine temporary storage jars, 14. first topping still recycle pumps, 15. first topping stills, first reboiler; 16. the first rectifying tower end is cold, 17. first rectifying tower return tanks, 18. first rectifying tower recycle pumps, 19. first topping stills, second recycle pump, 20. first topping stills, second reboiler; 21. flash tank, 22. ripe wine with dregs extraction pumps, 23. ripe wine with dregs preheaters, 24. first rectifying tower, 25. second topping stills; 26. the second topping still recycle pump, 27. second topping still reboilers, 28. second rectifying tower return tanks, 29. second rectifying tower reflux pumps, 30. thick wine pumps; 31. crude wine preheater, 32. second rectifying tower, 33. light wine preheaters, 34. potato spirit separators, 35. second rectifying tower reboilers; 36. suphtr, 37. molecular sieve-4 As, 38. molecular sieve B, 39. desorb vapour suphtrs, 40. light wine condensing surfaces
Embodiment:
Embodiment: shown in accompanying drawing 1, a kind of is that the device of raw material production absolute ethyl alcohol includes dealdehyder tower 5, degassing tower 6, first topping still 7, first rectifying tower 24, second topping still 25, second rectifying tower 32, molecular sieve-4 A 37, molecular sieve B38 with the fermentation liquid.Wherein second rectifying tower, 32 top exits link to each other with the second topping still reboiler, 27 shell-sides inlet through pipeline; The outlet of the second topping still reboiler, 27 shell-sides links to each other with the second rectifying tower return tank, 28 inlets through pipeline; The second rectifying tower return tank, 28 outlet at bottoms link to each other with the second rectifying tower reflux pump, 29 inlet ends through pipeline; The second rectifying tower reflux pump, 29 exit end link to each other with second rectifying tower, 32 top refluxing openings through pipeline; Tell one on second rectifying tower, 32 reflux lines and link to each other with light wine preheater 33 first inlet, 33 first outlets of light wine preheater link to each other with first rectifying tower, 24 tops inlet through pipeline; Second rectifying tower, 32 outlet at bottoms link to each other with crude wine preheater 31 second inlets through pipeline; Crude wine preheater 31 second outlets link to each other with Waste Water Treatment through pipeline; First outlet of first rectifying tower, 24 cats head links to each other with first topping still, first reboiler, 15 shell-sides inlet through pipeline; Cold 16 inlets link to each other first topping still, first reboiler, 15 shell-side vapor phase exits through pipeline and first rectifying tower end; Cold 16 outlets in first rectifying tower end link to each other with the first rectifying tower return tank, 17 inlets through pipeline; The outlet of first topping still, first reboiler, 15 shell-side liquid phases links to each other with the first rectifying tower return tank, 17 inlets through pipeline, and the first rectifying tower return tank, 17 outlet at bottoms link to each other with the first rectifying tower reflux pump, 18 inlet ends through pipeline, and the first rectifying tower reflux pump, 18 exit end link to each other with first rectifying tower, 24 top refluxing openings through pipeline; First rectifying tower, 24 outlet at bottoms link to each other with light wine preheater 33 second inlets through pipeline, and 33 second outlets of light wine preheater link to each other with thick wine jar 10 inlet ends through pipeline; Second topping still, 25 outlet at bottom parts are extracted out through the second topping still recycle pump 26; Get into second topping still, 27 tower stills through the second topping still reboiler, 27 tube sides heating back; Another part links to each other with ripe wine with dregs preheater 23 second inlets through pipeline, and ripe wine with dregs preheater 23 second outlets link to each other with useless poor treatment system through pipeline; Dealdehyder tower 5 top exits link to each other with first ripening wine with dregs preheater 1 shell-side inlet duct through pipeline; Cold 2 inlets link to each other first ripening wine with dregs preheater 1 vapor phase exit through pipeline and dealdehyder tower end; Cold 2 outlets in dealdehyder tower end link to each other with dealdehyder tower return tank 3 inlets through pipeline; The outlet of first ripening wine with dregs preheater 1 liquid phase also links to each other with dealdehyder tower return tank 3 inlets through pipeline; Dealdehyder tower return tank 3 outlet at bottoms link to each other with dealdehyder tower reflux pump 4 inlet ends through pipeline, and dealdehyder tower reflux pump 4 exit end link to each other with dealdehyder tower 5 top refluxing openings through pipeline; First topping still, 7 top vapor phase exits link to each other with the second ripe wine with dregs preheater 8 shell-sides inlet through pipeline; Cold 9 inlets link to each other the second ripe wine with dregs preheater 8 shell-side vapor phase exits through pipeline and first topping still end; Cold 9 outlets in first topping still end link to each other with thick wine jar 10 inlets through pipeline; Cold 9 vapor phase exits of dealdehyder tower cold 2 vapor phase exits in end and first topping still end remove vacuum cleaning system pipeline inlet through pipeline; Vacuum cleaning system outlet at bottom links to each other with thick wine jar 10 inlets through pipeline; Thick wine jar 10 outlet at bottoms link to each other with thick wine pump 30 inlet ends through pipeline, and thick wine pump 30 exit end link to each other with crude wine preheater 31 first inlets through pipeline, and crude wine preheater 31 first outlets link to each other with second rectifying tower, 32 centre entrances through pipeline; The second ripe wine with dregs preheater 8 liquid phases outlet also links to each other with thick wine jar 10 inlets through pipeline; The 7 top liquid phase outlets of first topping still link to each other with ripe wine with dregs extraction pump 22 inlet ends through pipeline, and ripe wine with dregs extraction pump 22 exit end warps link to each other with ripe wine with dregs preheater 23 first inlets, and ripe wine with dregs preheater 23 second outlets link to each other with second topping still top inlet through pipeline.
Outlet links to each other with flash tank 21 inlets through pipeline respectively with regeneration vapour suphtr 39 shell-sides for the shell-side outlet of the second rectifying tower reboiler 35, the shell-side outlet of suphtr 36; Flash tank 21 top exits link to each other with first topping still, second reboiler, 20 shell-sides inlet through pipeline, and flash tank 21 outlet at bottoms and the outlet of first topping still, second reboiler, 20 shell-sides are respectively through pipe connection back boiler tubing system.The useless mash in first topping still, 7 bottoms is divided into three parts; A part is extracted out through the first topping still recycle pump 14; Be heated the back through first topping still, first reboiler, 15 pipe sides and get into first topping still, 7 tower stills; Second section is extracted out through first topping still, second recycle pump 19, gets into first topping still, 7 tower stills through first topping still, second reboiler, 20 pipe side heating backs, and third part directly links to each other with useless poor treatment system through pipeline.From second rectifying tower, 32 middle part extracting mouth pipe connection potato spirit separators 34, add primary water flushing wine liquid simultaneously, from the recovered overhead potato spirit, separator 34 bottom pipe connect thick wine jar 10, reclaim weak liquor.
Molecular sieve-4 A 37 links to each other with the 3rd ripe wine with dregs preheater 11 shell-sides inlet through pipeline with molecular sieve B38 top exit; Cold 12 inlets link to each other the 3rd ripe wine with dregs preheater 11 shell-side vapor phase exits through pipeline and finished wine vapour end; Cold 12 outlets in finished wine vapour end link to each other with finished wine temporary storage jar 13 inlets through pipeline; The 3rd ripe wine with dregs preheater 11 shell-side liquid phases outlet also links to each other with finished wine temporary storage jar 13 inlets through pipeline; On molecular sieve A37 and molecular sieve B38 top exit pipeline, draw another pipeline and link to each other with regeneration vapour suphtr 39 pipe side entrances, the regeneration vapour suphtr 39 pipe side outlets vapour of regenerating through pipeline and molecular sieve-4 A 37 and molecular sieve B38 top enters the mouth and links to each other; Molecular sieve-4 A 37 links to each other with light wine condensing surface 40 inlets through pipeline with molecular sieve B38 bottom regeneration vapor outlet, and 40 outlets of light wine condensing surface link to each other with thick wine jar 10 inlets through pipeline.
The process flow of material is to being: the beer that the workshop section of fermenting certainly comes; After first ripening wine with dregs preheater 1, second ripe wine with dregs preheater 8 and the 3rd ripe wine with dregs preheater 11 preheatings, get into degassing tower 6 tops; The thick wine vapour that comes from dealdehyder tower 5 tops gets into dealdehyder tower return tank 3 after last cold 2 condensations of first ripening wine with dregs preheater 1 and dealdehyder tower; Pumping into dealdehyder tower 5 tops by dealdehyder tower reflux pump 4 again refluxes; The thick wine vapour that is come by first topping still, 7 tops gets into thick wine jar 10 after the second ripe wine with dregs preheater 8 and cold 9 condensations in end of first topping still; Not condensing from cold 2 and first topping still end, dealdehyder tower end cold 9 gets into the vacuum cleaning system; The washing light wine that comes from the vacuum cleaning system gets into thick wine jar 10, and the ripe wine with dregs after the next degassing in first topping still, 7 tops pumps into ripe wine with dregs preheater 23 by ripe wine with dregs extraction pump 22, after the useless mash preheating that comes at the bottom of second topping still, 25 towers, gets into second topping still, 25 tops; The a part of wine vapour that comes out from first rectifying tower, 24 tops gets into the first rectifying tower return tank 17 after first topping still, first reboiler 15 and cold 16 condensations in end of first rectifying tower, pump into first rectifying tower 24 by the first rectifying tower reflux pump 18 then and reflux; Another part wine vapour that comes out by first rectifying tower, 24 tops by suphtr 36 overheated after again after molecular sieve-4 A 37 or molecular sieve B38 dehydration; Part wine vapour gets into finished product temporary storage jar 13 after the 3rd ripe wine with dregs preheater 11 and cold 12 condensations in end of finished wine vapour; Another part wine vapour is regenerated through regeneration vapour suphtr 39 overheated back entering molecular sieve-4 As 37 or molecular sieve B38, and the light wine vapour after the regeneration gets into thick wine jar 10 after 40 condensations of light wine condensing surface; Thick wine liquid from thick wine jar 10 is pumped into crude wine preheater 31 entering second rectifying tower 32 after the waste water preheating that comes at the bottom of second rectifying tower, 32 towers by thick wine pump 30; The wine vapour that comes from the second rectifying tower cat head gets into the second rectifying tower return tank 28 after 27 condensations of the second topping still reboiler; Pumping into second rectifying tower 32 by the second rectifying tower reflux pump 29 again refluxes; After light wine preheater 33 and the light wine heat exchange that at the bottom of first rectifying tower, 24 towers, comes, get into first rectifying tower, 24 tops from extraction part wine liquid on second rectifying tower, 32 reflux lines, the light wine after the heat exchange that comes from first rectifying tower, 24 bottoms gets into thick wine jar 10; The useless mash after the heat exchange that comes at the bottom of mash, second topping still, 25 towers of giving up at the bottom of first topping still, 7 towers converges and gets into useless poor treatment system, the useless surplus water entering Waste Water Treatment that heats up in a steamer after the heat exchange that comes at the bottom of second rectifying tower, 32 towers; Import flash tank 21 together from the water of condensation of the second rectifying tower reboiler 35, the water of condensation of suphtr 36, the water of condensation of desorb vapour suphtr 39; The flash steam that flashes off gets into first topping still, second reboiler 20, and condensed flash steam is got back to boiler with flash distillation water.
Producing 80000 tons of absolute ethyl alcohols per year with maize raw material is example, specifies technological process of the present invention:
103.2 tons/hour of come from fermentation workshop section 30 ℃ beers that contain wine 12.0% (v/v);, first ripening wine with dregs preheater 1, the second ripe wine with dregs preheater 8 and the 3rd ripe wine with dregs 11 preheaters get into after being preheating to about 67 ℃ by degassing tower 6 tops; About the 50 ℃ thick wine vapour that contain about wine 91% (v/v) that come out from dealdehyder tower 5 tops get into dealdehyder tower return tank 3 after last cold 2 condensations of first ripening wine with dregs preheater 1 and dealdehyder tower; Pumping into dealdehyder tower 5 tops by dealdehyder tower reflux pump 4 again refluxes; About 70 ℃ that come from first topping still, 7 tops contain the thick wine vapour of wine 60% (v/v) and after the second ripe wine with dregs preheater 8 and cold 9 condensations in end of first topping still, get into thick wine jar 10; The ripe wine with dregs after the degassing gets into second topping still, 25 tops for 67.9 tons/hour about wine 12% (v/v) after ripe wine with dregs preheater 23 is preheated to about 102 ℃ from containing about 70 ℃ of degree of first topping still, 7 top extraction; The thick wine vapour that comes out from second topping still, 25 tops directly gets into about the 90 ℃ concentrated wine vapour that contain wine 95% (v/v) more than of first rectifying tower 24 after rectifying concentrates and partly gets into first topping still, first reboiler 15; After first topping still, first reboiler 15 and cold 16 condensations in end of first rectifying tower, get into the first rectifying tower return tank 17; Pumping into first rectifying tower, 24 tops by the first rectifying tower reflux pump 18 again refluxes; About 90 ℃ concentrated wine vapour that contain more than the wine 95% (v/v) of the another part that comes from first rectifying tower, 24 tops get into molecular sieve-4 A 37 or molecular sieve B38 dehydration after suphtr 36 heating; Come out from first rectifying tower, 24 bottoms about 102 ℃ light wine after 33 preheatings of light wine preheater, get into thick wine jar 10; Thick wine liquid from thick wine jar 10 gets into second rectifying tower, 32 opening for feeds after thick wine pump 30 pumps into crude wine preheater 31 preheatings; 128 ℃ of concentrated wine vapour that contain more than the wine 95% (v/v) that come out from second rectifying tower, 32 tops get into the second rectifying tower return tank 28 after 27 condensations of the second topping still reboiler; Pumping into second rectifying tower, 32 tops through the second rectifying tower reflux pump 29 again refluxes; After 33 coolings of light wine preheater, get into first rectifying tower, 24 tops from extraction partially concd wine liquid on second rectifying tower, 32 reflux lines; Raw spirit vapour part more than 99.5% (v/v) after the dehydration of coming out from molecular sieve A37 or molecular sieve B38 top after the 3rd ripe wine with dregs preheater 11 and cold 12 condensations in end of finished wine vapour as finished product entering finished product temporary storage jar 13; Another part does not have watery wine vapour and gets into perhaps molecular sieve B38 top of molecular sieve-4 A 37 through desorb vapour suphtr 39 heating back, and the light wine vapour that comes out from molecular sieve A37 or molecular sieve B38 bottom gets into thick wine jar 10 after 40 condensations of light wine condensing surface.
Producing 30000 tons of absolute ethyl alcohols per year with the cassava raw material again is example, further specifies technology of the present invention:
47.8 tons/hour of come from fermentation workshop section 30 ℃ beers that contain wine 10.0% (v/v);, first ripening wine with dregs preheater 1, the second ripe wine with dregs preheater 8 and the 3rd ripe wine with dregs 11 preheaters get into after being preheating to about 67 ℃ by degassing tower 6 tops; About the 50 ℃ thick wine vapour that contain about wine 89% (v/v) that come out from dealdehyder tower 5 tops get into dealdehyder tower return tank 3 after last cold 2 condensations of first ripening wine with dregs preheater 1 and dealdehyder tower; Pumping into dealdehyder tower 5 tops by dealdehyder tower reflux pump 4 again refluxes; About the 70 ℃ thick wine vapour that contain wine 57% (v/v) that come from first topping still, 7 tops get into thick wine jar 10 after the second ripe wine with dregs preheater 8 and cold 9 condensations in end of first topping still; The ripe wine with dregs after the degassing gets into second topping still, 25 tops for 30.6 tons/hour about wine 11% (v/v) after ripe wine with dregs preheater 23 is preheated to about 102 ℃ from containing about 70 ℃ of degree of first topping still, 7 top extraction; The thick wine vapour that comes out from second topping still, 25 tops directly gets into about the 90 ℃ concentrated wine vapour that contain wine 95% (v/v) more than of first rectifying tower 24 after rectifying concentrates and partly gets into first topping still, first reboiler 15; After first topping still, first reboiler 15 and cold 16 condensations in end of first rectifying tower, get into the first rectifying tower return tank 17; Pumping into first rectifying tower, 24 tops by the first rectifying tower reflux pump 18 again refluxes; About 90 ℃ concentrated wine vapour that contain more than the wine 95% (v/v) of the another part that comes from first rectifying tower, 24 tops get into molecular sieve-4 A 37 or molecular sieve B38 dehydration after suphtr 36 heating; Come out from first rectifying tower, 24 bottoms about 102 ℃ light wine after 33 preheatings of light wine preheater, get into thick wine jar 10; Thick wine liquid from thick wine jar 10 gets into second rectifying tower, 32 opening for feeds after thick wine pump 30 pumps into crude wine preheater 31 preheatings; 128 ℃ of concentrated wine vapour that contain more than the wine 95% (v/v) that come out from second rectifying tower, 32 tops get into the second rectifying tower return tank 28 after 27 condensations of the second topping still reboiler; Pumping into second rectifying tower, 32 tops through the second rectifying tower reflux pump 29 again refluxes; After 33 coolings of light wine preheater, get into first rectifying tower, 24 tops from extraction partially concd wine liquid on second rectifying tower, 32 reflux lines; Raw spirit vapour part more than 99.5% (v/v) after the dehydration of coming out from molecular sieve A37 or molecular sieve B38 top after the 3rd ripe wine with dregs preheater 11 and cold 12 condensations in end of finished wine vapour as finished product entering finished product temporary storage jar 13; Another part raw spirit vapour gets into perhaps molecular sieve B38 top of molecular sieve-4 A 37 through desorb vapour suphtr 39 heating back, and the light wine vapour that comes out from molecular sieve A37 or molecular sieve B38 bottom gets into thick wine jar 10 after 40 condensations of light wine condensing surface.
Claims (6)
1. one kind is the device of raw material production absolute ethyl alcohol with the fermentation liquid; It is characterized in that: it comprises stacked in order up and down dealdehyder tower (5), degassing tower (6) and first topping still (7); Stacked up and down first rectifying tower (24) and second topping still (25); And second rectifying tower (32), molecular sieve-4 A (37) and molecular sieve B (38) that parallel connection is provided with, the placed in-line successively first ripening wine with dregs of tube side preheater (1), the second ripe wine with dregs preheater (8), the 3rd ripe wine with dregs preheater (11); Wherein first ripening wine with dregs preheater (1) pipe side entrance connects ripe beer feed(raw material)inlet; The 3rd ripe wine with dregs preheater (11) pipe side outlet pipe connection degassing tower (6) top inlet; Dealdehyder tower (5) top links to each other with first ripening wine with dregs preheater (1) shell-side inlet through pipeline, and the outlet of first ripening wine with dregs preheater (1) shell-side links to each other with dealdehyder tower (5) top refluxing opening through dealdehyder tower return tank (3), dealdehyder tower reflux pump (4); First topping still (7) top vapor phase exit links to each other with second ripe wine with dregs preheater (8) shell-side inlet through pipeline; Second ripe wine with dregs preheater (8) the shell-side outlet conduit connects thick wine jar (10); Thick wine jar (10) outlet at bottom is through thick wine pump (30) pipe connection crude wine preheater (31) first inlets, and crude wine preheater (31) first outlets link to each other with second rectifying tower (32) middle part opening for feed through pipeline; First topping still (7) top liquid phase outlet conduit connects ripe wine with dregs extraction pump (22) inlet; Ripe wine with dregs extraction pump (22) outlet conduit connects ripe wine with dregs preheater (23) first inlets; Ripe wine with dregs preheater (23) first outlets link to each other with second topping still (25) top inlet through pipeline; Second topping still (25) outlet at bottom links to each other with ripe wine with dregs preheater (23) second inlets through pipeline, and ripe wine with dregs preheater (23) second outlets link to each other with the useless poor tubing system of handling through pipeline; First outlet of first rectifying tower (24) top links to each other with first topping still, first reboiler (15) shell-side inlet through pipeline; First topping still, first reboiler (15) shell-side outlet is through the first rectifying tower return tank (17), first rectifying tower (24) the top reflux inlet that links to each other with first rectifying tower reflux pump (18) pipeline; Second outlet of first rectifying tower (24) top is through suphtr (36) tube side and parallelly connected molecular sieve-4 A (37) and molecular sieve B (38) absorption inlet pipe connection; The molecular sieve-4 A (37) of parallel connection and the absorption of molecular sieve B (38) outlet are connected the 3rd ripe wine with dregs preheater (11) shell-side inlet and regeneration vapour suphtr (39) pipe side entrance respectively; The outlet of the 3rd ripe wine with dregs preheater (11) shell-side connects the finished product jar; Regeneration vapour suphtr (39) pipe side outlet connects the molecular sieve-4 A (37) of parallel connection and the regeneration inlet of molecular sieve B (38); The regeneration outlet of molecular sieve-4 A (37) and molecular sieve B (38) is connected thick wine jar (10) through light wine condensing surface (40) tube side respectively, and the shell-side inlet of suphtr (36) and regeneration vapour suphtr (39) is connected steam system respectively; Second rectifying tower (32) top exit links to each other with second topping still reboiler (27) shell-side inlet through pipeline; The outlet of second topping still reboiler (27) shell-side links to each other with second rectifying tower reflux pump (29) inlet end through the second rectifying tower return tank (28); Second rectifying tower reflux pump (29) exit end links to each other with second rectifying tower (32) top reflux inlet and light wine preheater (33) first inlets respectively through pipeline; Light wine preheater (33) first outlet conduits connect first rectifying tower (24) top refluxing opening; First rectifying tower (24) bottom light wine outlet conduit connects light wine preheater (33) second inlets, and light wine preheater (33) second outlet conduits connect thick wine jar (10); Second rectifying tower (32) outlet at bottom links to each other with crude wine preheater (31) second inlets through pipeline, and crude wine preheater (31) second outlets are through the pipe connection Waste Water Treatment, and second rectifying tower reboiler (35) the shell-side inlet duct connects steam system.
2. according to claim 1 a kind of be the device of raw material production absolute ethyl alcohol with the fermentation liquid; It is characterized in that: outlet links to each other with flash tank (21) inlet through pipeline respectively with regeneration vapour suphtr (39) shell-side for the shell-side outlet of the said second rectifying tower reboiler (35), the shell-side outlet of suphtr (36); Flash tank (21) top exit links to each other with first topping still, second reboiler (20) shell-side inlet through pipeline, and flash tank (21) outlet at bottom and the outlet of first topping still, second reboiler (20) shell-side are respectively through pipe connection back boiler tubing system.
3. one kind is used the described production technique of producing absolute ethyl alcohol with fermentation liquid as the device of raw material production absolute ethyl alcohol of claim 1; It is characterized in that: the ripe wine with dregs that the workshop section of fermenting certainly gets into degassing tower (6) top successively after first ripening wine with dregs preheater (1), the second ripe wine with dregs preheater (8) and the 3rd ripe wine with dregs preheater (11) preheating; The thick wine vapour that comes out in degassing tower (6) top directly gets into dealdehyder tower (5) full gear;, the wine vapour that the full gear top of tower comes gets into dealdehyder tower return tank (3) after getting into first ripening wine with dregs preheater (1) condensation; Pump into dealdehyder tower (5) by dealdehyder tower reflux pump (4) again; Get into the second ripe wine with dregs preheater (8) from the thick wine vapour of first topping still (7) top extraction; After condensation, get into thick wine jar (10); Ripe wine with dregs after first topping still (7) top is with the full gear of ripe wine with dregs extraction pump (22) extraction partly degassed gets into second topping still (25) top after post-mature wine with dregs preheater (23) is with the useless mash preheating in second topping still (25) bottom, the thick wine vapour after second topping still (25) concentrates directly gets into first rectifying tower (24); After the concentrated wine vapour part entering suphtr (36) that first rectifying tower (24) cat head goes out is overheated; Get into molecular sieve-4 A (37) or molecular sieve B (38) dehydration, after molecular sieve-4 A (37) or molecular sieve B (38) dehydration, get into finished product temporary storage jar (13) after no watery wine vapour part entering the 3rd ripe wine with dregs preheater (11) condensation and export as finished product; Another part does not have watery wine vapour and after regeneration vapour suphtr (39) is overheated, uses vapour as the regeneration of molecular sieve B (38) or molecular sieve-4 A (37), and the regeneration vapour of process molecular sieve B (38) or molecular sieve-4 A (37) gets into thick wine jar (10) after light wine condensing surface (40) condensation; Another part that first rectifying tower (24) cat head goes out concentrates wine vapour and gets into first topping still, first reboiler (15) shell-side condensation; Condensation wine liquid pump is gone into first rectifying tower (24) and is refluxed; The light wine that comes out from first rectifying tower (24) bottom gets into thick wine jar (10) after light wine preheater (33) preheating; After pumping into crude wine preheater (31) preheating by thick wine pump (30), the thick wine that comes from thick wine jar (10) bottom gets into second rectifying tower (32); The concentrated wine vapour that comes out from second rectifying tower (32) top gets into second topping still reboiler (27) shell-side condensation; Condensation wine liquid gets into the second rectifying tower return tank (28); Pump a part by the second rectifying tower reflux pump (29) and get into second rectifying tower (32) backflow, another part gets into first rectifying tower (24) top and refluxes after light wine preheater (33) cooling, and the second rectifying tower reboiler (35), suphtr (36) and regeneration vapour suphtr (39) use steam heating respectively.
4. the production technique of production absolute ethyl alcohol according to claim 3; It is characterized in that: the steam condensate after the said second rectifying tower reboiler (35), suphtr (36) and regeneration vapour suphtr (39) heating gets into flash tank (21) flash distillation respectively, and the top flash steam gets into first topping still, second reboiler (20) shell-side and uses as thermal source.
5. the production technique of production absolute ethyl alcohol according to claim 4 is characterized in that: each column overhead working pressure, service temperature are respectively:
Dealdehyder tower (5) absolute pressure 0.25～0.35atm, 50～60 ℃ of temperature;
Degassing tower (6) absolute pressure 0.3～0.4atm, 60～70 ℃ of temperature;
First topping still (7) absolute pressure 0.3～0.4atm, 65～75 ℃ of temperature;
First rectifying tower (24) absolute pressure 1.2～2.2atm, 85～95 ℃ of temperature;
Second topping still (25) absolute pressure 1.5～2.5atm, 100～120 ℃ of temperature;
Second rectifying tower (32) absolute pressure 4.8～6.0atm, 120～135 ℃ of tower top temperatures.
6. the production technique of production absolute ethyl alcohol according to claim 5 is characterized in that: working pressure, the service temperature of molecular sieve-4 A (37) and molecular sieve B (38) are respectively when absorption and regeneration:
Absolute pressure 1.0～2.0atm during absorption, 100～120 ℃ of temperature;
Absolute pressure 0.3～0.4atm during regeneration, 110～140 ℃ of temperature.
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| CN111821712B (en) * | 2020-07-27 | 2022-04-05 | 广东中科天元新能源科技有限公司 | Seven-tower differential pressure distillation energy-saving production system and method for top-grade edible alcohol |
| CN113816834B (en) * | 2021-10-14 | 2022-08-05 | 北京化工大学 | Energy-saving rectification-adsorption combined method for preparing high-purity absolute ethyl alcohol |
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