CN110404285A - Four column distillations and UF membrane integrated system and its method for distilling ethyl alcohol - Google Patents
Four column distillations and UF membrane integrated system and its method for distilling ethyl alcohol Download PDFInfo
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- CN110404285A CN110404285A CN201910648880.6A CN201910648880A CN110404285A CN 110404285 A CN110404285 A CN 110404285A CN 201910648880 A CN201910648880 A CN 201910648880A CN 110404285 A CN110404285 A CN 110404285A
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- prefractionator
- tower
- wine
- membrane module
- alcohol
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 102
- 239000012528 membrane Substances 0.000 title claims abstract description 97
- 235000019441 ethanol Nutrition 0.000 title claims abstract description 83
- 238000004821 distillation Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000007872 degassing Methods 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000003517 fume Substances 0.000 claims abstract description 9
- 238000003825 pressing Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 7
- 238000013021 overheating Methods 0.000 claims abstract description 3
- 238000003795 desorption Methods 0.000 claims description 26
- 239000000446 fuel Substances 0.000 claims description 15
- 238000009833 condensation Methods 0.000 claims description 14
- 230000005494 condensation Effects 0.000 claims description 14
- 230000018044 dehydration Effects 0.000 claims description 13
- 238000006297 dehydration reaction Methods 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 8
- 239000000919 ceramic Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 4
- 238000005202 decontamination Methods 0.000 claims description 3
- 230000003588 decontaminative effect Effects 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 238000007710 freezing Methods 0.000 claims description 2
- 230000008014 freezing Effects 0.000 claims description 2
- 238000001704 evaporation Methods 0.000 claims 1
- 230000008020 evaporation Effects 0.000 claims 1
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000002808 molecular sieve Substances 0.000 description 10
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 10
- 230000000694 effects Effects 0.000 description 9
- 229960004756 ethanol Drugs 0.000 description 8
- 239000001760 fusel oil Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000000605 extraction Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 208000024756 faint Diseases 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 206010042772 syncope Diseases 0.000 description 2
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 229960000935 dehydrated alcohol Drugs 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
- B01D3/003—Rectification of spirit
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
- B01D3/003—Rectification of spirit
- B01D3/004—Rectification of spirit by continuous methods
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/145—One step being separation by permeation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/225—Multiple stage diffusion
- B01D53/226—Multiple stage diffusion in serial connexion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
Abstract
The invention discloses four column distillations and UF membrane integrated system, including the smart tower of mash preheater, negative pressure prefractionator, normal pressure prefractionator, middle pressure and high pressure essence tower；High pressure essence tower is sequentially connected fume superheater and membrane separation device by pipeline；The membrane separation device includes concatenated low vacuum membrane module and high vacuum membrane module.The method of above-mentioned system distillation ethyl alcohol, comprising the following steps: A, fermenting-ripening wine with dregs slough gas and form degassing wine with dregs；B, wine vapour is separated with useless mash in degassing wine with dregs；C, wine vapour forms crude alcohol after condensing, and crude alcohol enters high pressure essence tower after pressing smart column distillation in；D, into the alcohol steam of high pressure essence tower, partially sequentially enter low vacuum membrane module and high vacuum membrane module after overheating and separate ethyl alcohol and water.The invention avoids the race wine phenomenons in distillation process, reduce the consumption of chilled water and steam, energy conservation and environmental protection.
Description
Technical field
The present invention relates to ethyl alcohol production technical fields, and in particular to four column distillations and UF membrane integrated system and its distillation second
The method of alcohol.
Background technique
The patent No. 201810719237.3 disclose double thick double smart four tower quadruple effect energy-saving distillings production alcohol fuel systems and
Its application method, mainly includes negative pressure prefractionator, degassing stages, normal pressure prefractionator, the smart tower of middle pressure and high pressure essence tower, middle pressure essence column overhead
Alcohol fuel steam of the alcohol steam extraction after molecular sieve dehydration is for heating negative pressure prefractionator.
Had the following problems by molecular sieve dehydration: 1. the charging of molecular sieve and desorption process are that interval carries out, and are caused
Combined column tower top pressure is fluctuated, and vapour phase is not easily accomplished automation control into molecular sieve dehydration, and distillation procedure is unstable, holds
Easily run wine；2. light the holding a lot of liquor of molecular sieve dehydration process generation, the alcohol amount in light wine accounts for about the 25% of output, causes to distill
System light wine amount to be treated increases, and increases steam consumption.
Summary of the invention
In view of the above shortcomings of the prior art, the object of the present invention is to provide four column distillations and UF membrane integrated system and its
Distill the method for ethyl alcohol.
To achieve the above object, the present invention adopts the following technical scheme:
The first aspect of the present invention provides four column distillations and UF membrane integrated system, including mash preheater, negative pressure wine with dregs
The smart tower of tower, normal pressure prefractionator, middle pressure and high pressure essence tower；High pressure essence tower is sequentially connected fume superheater by pipeline and UF membrane fills
It sets；The membrane separation device includes concatenated low vacuum membrane module and high vacuum membrane module；The import of the low vacuum membrane module
End and fume superheater piping connection, the outlet end of low vacuum membrane module is connect with the input end of high vacuum membrane module；High vacuum
The outlet end of membrane module is connect with normal pressure prefractionator reboiler；The outlet end of low vacuum membrane module, high vacuum membrane module outlet end
Also it is connect respectively by desorption condenser I, desorption condenser II with anhydrous vacuum pump.
Preferably, the low vacuum membrane module and high vacuum membrane module include multiple concatenated shell-and-tube membrane structures, often
A shell-and-tube membrane structure includes shell and the inner tube positioned at interior of shell, and said inner tube includes ceramic tube and overlays on ceramics
The molecular screen membrane of tube outer surface.
Space between shell and inner tube is shell side, and internal tube space is tube side, takes out negative pressure in tube side, leads in shell side
Alcohol steam, alcohol steam after low vacuum membrane module and high vacuum membrane module, the moisture in finished product can achieve 0.5% with
Under, most moisture and a small amount of ethyl alcohol penetrate inner tube, enter distillation workshop section after tube side enters desorption condenser condensation and return
It receives.
The tube side outlet end of low vacuum membrane module with desorption condenser I connect, the tube side outlet end of high vacuum membrane module and
Condenser II is desorbed to connect.The shell-side outlet end of low vacuum membrane module is connect with the shell side input end of high vacuum membrane module, Gao Zhen
The shell-side outlet end of empty membrane module is connect with normal pressure prefractionator reboiler.
Preferably, the normal pressure prefractionator reboiler includes the normal pressure for forming closed circuit with normal pressure prefractionator respectively by pipeline
Prefractionator reboiler I and normal pressure prefractionator reboiler II；The outlet end of high vacuum membrane module is specifically connect with normal pressure prefractionator reboiler II.
Preferably, the mash preheater includes concatenated mash level-one preheater, mash second level preheater and mash three
Grade preheater, the normal pressure prefractionator reboiler II are connect through mash three-level preheater with finished product cooler by pipeline.
Preferably, desorption I outlet end of condenser and the outlet end of desorption condenser II pass through pipeline and connect with thick wine tank.
The second aspect of the present invention provides the method for above-mentioned system distillation ethyl alcohol, which is characterized in that including following step
It is rapid:
A, fermenting-ripening wine with dregs sloughs gas and forms degassing wine with dregs；
B, wine vapour is separated with useless mash in degassing wine with dregs；
C, wine vapour forms crude alcohol after condensing, and crude alcohol enters high pressure essence tower after pressing smart column distillation in；
D, into the alcohol steam of high pressure essence tower be concentrated into tower top wine degree be 95% (v/v) or more alcohol steam, one
Sequentially enter low vacuum membrane module and high vacuum membrane module after lease making overheat to separate ethyl alcohol and water, alcohol fuel steam enters normal
Prefractionator reboiler II is pressed to heat normal pressure prefractionator；Most moisture and a small amount of ethyl alcohol enter desorption condenser I and desorption condensation
Device II enters the recycling of distillation workshop section after condensing；
Wherein low vacuum membrane module vacuum degree is absolute pressure 9-11kpa, desorbs and leads to ordinary cycle water in condenser I；High vacuum
The vacuum degree of membrane module is absolute pressure 2-4kpa, and 1 DEG C of low temperature chilled water is led in desorption condenser II.
Preferably, in step A, fermenting-ripening wine with dregs, in negative pressure prefractionator degassing stages top feed, sloughs gas after preheating
Karusen enter degassing stages bottom rear divide mash by pipe gravity flow pipeline flow into negative pressure prefractionator, remaining it is preheated after enter normal pressure
At the top of prefractionator.
Preferably, in step B, degassing wine with dregs is in negative pressure prefractionator and normal pressure prefractionator by the steam of tower bottom rising while downlink
Heating, wine vapour uplink are separated with useless mash, and vinasse are discharged in tower bottom, send to vinasse processing system.
Preferably, in step C, the wine vapour of negative pressure prefractionator and normal pressure prefractionator tower top enters thick wine tank, thick wine tank after condensing
Crude alcohol it is preheated after enter in press smart tower lower part, the smart column overhead wine vapour of middle pressure all returns after normal pressure prefractionator reboiler condenses
Stream enters high pressure essence tower after tower bottom alcohol is preheated.
Preferably, in step D, into high pressure essence tower after carry out vapour-liquid mass friendship with overhead reflux liquid after the vaporized alcohol of part
Change, be gradually concentrated, until tower top wine degree be 95% (v/v) or more alcohol steam part after overheating striping dehydration device, pass through
The device separates ethyl alcohol and water；Remaining whole goes normal pressure prefractionator reboiler to heat normal pressure prefractionator, high pressure essence tower tower reactor spent hot water
Decontamination water treatment system after preheating crude alcohol；
Mash three-level preheater preheating karusen is entered back into after the condensation of alcohol fuel steam, it is most cooling through finished product cooler afterwards
After obtain alcohol fuel finished product；The ordinary cycle water is 26 DEG C -28 DEG C.
Beneficial effects of the present invention:
(1) wine vapour of the present invention enters the shell side of membrane separation device, and tube side is desorbed, and the process for separating and desorbing is continuous
Stable, dehydrating effect is good, and occupation area of equipment is few, small investment, energy conservation and environmental protection；Film dehydration is continuous process, work pressure
Power is stablized, and will not have any impact to distillation, avoids and runs wine phenomenon.
(2) inventive film dehydration meets Dalton's law (of partial pressures), the moisture in membrane separation device shell side alcohol steam
Lower, the vacuum level requirements of tube side inlet side are relatively high, and vacuum degree is higher, and condensation temperature is lower, according to this principle, to reduce
The condensation of the light wine steam of the inlet side of film dehydration is divided into two sections by the consumption of chilled water, and membrane separation device includes mutual
Concatenated low vacuum membrane module and high vacuum membrane module, the faints steam in low vacuum membrane module pass through ordinary cycle water cooling
But, the faints steam in high vacuum membrane module is cooling by low temperature chilled water, by the improvement of this structure, with conventional molecular
Sieve dehydration is compared, and 2/3 freezing water consumption is reduced.
(3) dehydration device is light holds a lot of liquor for conventional molecular sieve, and the alcohol amount in light wine accounts for about the 25% of finished product, UF membrane dress
It sets and is carried out simultaneously due to desorbing and separating, light wine amount is very low, and the alcohol amount in light wine accounts for about the 5 ‰ of finished product, distills workshop section
Light wine amount to be treated substantially reduces, and reduces steam consumption；
Alcohol steam is produced from high pressure essence tower vapour phase in the present invention simultaneously, is used for through the dewatered alcohol fuel steam of film
Normal pressure prefractionator is heated, smart column overhead vapour phase extraction is therefrom pressed with alcohol steam, the alcohol fuel steam after molecular sieve dehydration is used
It is compared in the traditional handicraft of heating negative pressure prefractionator, because an effect is utilized in alcohol steam more, to reduce steam consumption, this hair
It is bright more energy saving；
Every production one ton of alcohol fuel whole set process consumption vapour is no more than 1.0 tons, can be reduced compared with traditional handicraft 30% with
Upper steam.
Both (4) four column distillations and membrane separation device are not independent, nor simple combination, there is heats for the two
Coupling, combination both not is not achieved energy-saving effect, is in particular in, 1. from the high pressure essence tower vapour phase of four column distillation workshop sections
Alcohol is produced, alcohol steam returns again to distillation workshop section and heats normal pressure prefractionator after being dehydrated by membrane module, realize the repetition of heat
It utilizes；2. after the two combination, light wine amount is reduced to 1% to distill the negative of workshop section's recovered alcohol hereinafter, reducing by original 25%
Lotus, to reduce steam consumption；3. energy-saving effect is more significant after combination, than traditional three tower triple effect distillation techniques+molecular sieve
Dehydration device is compared with " double thick double smart four tower quadruple effects distillations produce alcohol fuel technologies and device ", is saved steam and is existed
20% or more.
(5) advanced quadruple effect thermal coupling distillation technique is utilized, only high pressure essence tower needs raw steam to provide heat by reboiler
The wine vapour of amount, high pressure essence tower provides heat to the smart tower of middle pressure by reboiler, and the middle wine vapour for pressing smart tower and finished product dehydrated alcohol steam
Vapour passes through reboiler respectively and provides heat to normal pressure prefractionator, and the wine vapour of normal pressure prefractionator provides heat to negative pressure prefractionator by reboiler
Amount is truly realized a tower into vapour, and four towers work, and heat is fully used, and reduce steam consumption.
Detailed description of the invention
Fig. 1 is flow chart of the present invention；
Fig. 2 is the schematic cross-sectional view of shell-and-tube membrane structure of the present invention；
In figure: 101, mash level-one preheater, 102, mash second level preheater, 103, mash three-level preheater, 2, degassing
Section, 3, degassing stages condenser group, 4, thick wine tank, 5, distillation vacuum pump, 6, negative pressure prefractionator condenser group, 7, finished product cooler, 8,
Negative pressure prefractionator, 9, normal pressure prefractionator feed preheater, 10, normal pressure prefractionator, 11, negative pressure prefractionator reboiler, 12, vinasse processing system,
13, crude alcohol preheater, 14, the smart tower of middle pressure, 15, the smart tower reboiler of middle pressure, 16, normal pressure prefractionator reboiler I, 17, high pressure essence tower
Feed preheater, 18, high pressure essence tower, 19, fusel oil eliminator, 20, sewage disposal system, 21, smart tower reboiler, 22, condensation
Water tank, 23, boiler room, 24, normal pressure prefractionator reboiler II, 25, fume superheater, 26, low vacuum membrane module, 27, high vacuum film
Component, 28, desorption condenser I, 29, desorption condenser II, 30, anhydrous vacuum pump, 31, shell, 32, ceramic tube, 33, molecular sieve
Film, 34, shell side, 35, tube side.
Specific embodiment
It is noted that following detailed description is all illustrative, it is intended to provide further instruction to the application.Unless another
It indicates, all technical and scientific terms used herein has usual with the application person of an ordinary skill in the technical field
The identical meanings of understanding.
In order to enable those skilled in the art can clearly understand the technical solution of the application, below with reference to tool
The technical solution of the application is described in detail in the embodiment of body.
Four column distillations and UF membrane integrated system include mash preheater, degassing stages 2, degassing stages condenser group 3, thick wine tank
4, vacuum pump 5, negative pressure prefractionator condenser group 6 and finished product cooler 7 are distilled.Mash preheater passes through pipeline and the formation of degassing stages 2
Closed circuit.In order to obtain better pre-heat effect, production efficiency is improved, the mash preheater includes concatenated mash level-one
Preheater 101, mash second level preheater 102 and mash three-level preheater 103.
The outlet end of mash three-level preheater 103 is connect with finished product cooler 7, degassing stages 2 respectively, the outlet of degassing stages 2
End by pipeline successively after mash level-one preheater 101, degassing stages condenser group 3 respectively with thick wine tank 4 and distillation vacuum pump 5
Successively distinguished after mash second level preheater 102, negative pressure prefractionator condenser group 6 by pipeline the outlet end of connection, negative pressure prefractionator 8
It is connect with thick wine tank 4 and distillation vacuum pump 5.
Its further include negative pressure prefractionator 8, normal pressure prefractionator feed preheater 9, normal pressure prefractionator 10, negative pressure prefractionator reboiler 11, often
Prefractionator reboiler and vinasse processing system 12 are pressed, the outlet end of degassing stages 2 is connect by pipeline with negative pressure prefractionator 8, degassing stages 2
Outlet end is connect after normal pressure prefractionator feed preheater 9 with normal pressure prefractionator 10 by pipeline, and the outlet end of normal pressure prefractionator 10 passes through
Pipeline connects thick wine tank 4 after negative pressure prefractionator reboiler 11.
Negative pressure prefractionator reboiler 11 forms closed circuit by pipeline and negative pressure prefractionator 8, and the outlet end of negative pressure prefractionator 8 passes through
Pipeline is connect with vinasse processing system 12.
The normal pressure prefractionator reboiler includes the normal pressure prefractionator for forming closed circuit with normal pressure prefractionator 10 respectively by pipeline
Reboiler I 16 and normal pressure prefractionator reboiler II 24；Normal pressure prefractionator 10 by pipeline respectively with normal pressure prefractionator reboiler I 16 and normal pressure
Prefractionator reboiler II 24 forms closed circuit, and the outlet end of normal pressure prefractionator 10 is by pipeline after normal pressure prefractionator feed preheater 9
It is connect with vinasse processing system 12.
It further includes crude alcohol preheater 13, the smart tower 14 of middle pressure, the smart tower reboiler 15 of middle pressure and normal pressure prefractionator reboiler I
16, high pressure essence tower feed preheater 17, high pressure essence tower 18, fusel oil eliminator 19, sewage disposal system 20, smart tower reboiler
21, condensate tank 22 and boiler room 23.
The outlet end of thick wine tank 4 by pipeline connect after crude alcohol preheater 13 in press smart tower 14, middle pressure essence tower 14 leads to
It crosses pipeline and forms closed circuit with the smart tower reboiler 15 of middle pressure and normal pressure prefractionator reboiler I 16 respectively；Normal pressure prefractionator reboiler I 16
Also pass through piping connection with high pressure essence tower 18.
The middle outlet end for pressing smart tower 14 is connect after high pressure essence tower feed preheater 17 with high pressure essence tower 18 by pipeline, high
Smart tower 18 is pressed to form closed circuit with the smart tower reboiler 15 of middle pressure, smart tower reboiler 21 respectively by pipeline；Smart tower reboiler 21
Outlet end successively connect after condensate tank 22 and high pressure essence tower feed preheater 17 with boiler room 23 by pipeline.
The outlet end of high pressure essence tower 18 is connect by pipeline with fusel oil eliminator 19, and the outlet end of high pressure essence tower 18 is also logical
It crosses pipeline and is connect through crude alcohol preheater 13 with sewage disposal system 20.
High pressure essence tower 18 is sequentially connected fume superheater 25 and membrane separation device by pipeline；The membrane separation device includes
The low vacuum membrane module 26 and high vacuum membrane module 27 being serially connected；The input end and fume of the low vacuum membrane module 26 overheat
The outlet end of 25 piping connection of device, low vacuum membrane module 26 is connect with the input end of high vacuum membrane module 27；High vacuum membrane module
27 outlet end is connect with normal pressure prefractionator reboiler II 24；The outlet end of low vacuum membrane module 26, high vacuum membrane module 27 go out
Mouth end is also connect by desorption condenser I 28, desorption condenser II 29 with anhydrous vacuum pump 30 respectively.The normal pressure prefractionator is boiled again
Device II 24 is connect through mash three-level preheater 103 with finished product cooler 7 by pipeline.Desorb I 28 outlet end of condenser and desorption
The outlet end of condenser II 29 passes through pipeline and connect with thick wine tank 4.
The low vacuum membrane module 26 and high vacuum membrane module 27 include multiple concatenated shell-and-tube membrane structures, such as Fig. 2
Shown, each shell-and-tube membrane structure includes shell 31 and the inner tube inside shell 31, and said inner tube includes ceramic tube
32 and overlay on the molecular screen membrane 33 of 32 outer surface of ceramic tube.
Space between shell 31 and inner tube is shell side 34, and internal tube space is tube side 35, takes out negative pressure, In in tube side 35
Lead to alcohol steam, moisture of the alcohol steam after low vacuum membrane module 26 and high vacuum membrane module 27, in finished product in shell side 34
0.5% be can achieve hereinafter, most moisture and a small amount of ethyl alcohol enter desorption condenser condensation through tube side 35 through inner tube
Enter the recycling of distillation workshop section afterwards.
The method of above system distillation ethyl alcohol, comprising the following steps:
A, fermenting-ripening wine with dregs enters degassing stages 2, carbon dioxide and part in mature wine with dregs after the preheating of mash preheater
Low boiling impurity separates under the action of 2 negative pressure of degassing stages with karusen, enters 101 He of mash level-one preheater containing miscellaneous thick wine vapour
Degassing stages condenser group 3 condenses, and then condensate liquid enters thick wine tank 4；Slough gas karusen enter 2 bottom of degassing stages after,
Part mash (about 47%) flows into negative pressure prefractionator 8 by pipe gravity flow pipeline, remaining (about 53%) passes through normal pressure prefractionator feed preheater 9
Enter normal pressure prefractionator 10 after preheating；
Wherein: the steam that degassing wine with dregs is risen while from degassing stages 2 to negative pressure 8 downlink of prefractionator by 8 tower bottom of negative pressure prefractionator
Heating, wine vapour uplink are separated with useless mash；Useless mash is discharged in the tower bottom of negative pressure prefractionator 8, sends to the processing of vinasse processing system 12；
After 8 wine vapour of negative pressure prefractionator rises, partially enter 2 bottom of degassing stages, remaining thick wine vapour reaches negative pressure prefractionator after mash preheater
Condenser group 6 condenses, and condensate liquid enters thick wine tank 4；It is uncooled to be discharged containing miscellaneous gas by distillation vacuum pump 5.
Mash preheater includes the mash level-one preheater 101 for passing sequentially through piping connection, 102 and of mash second level preheater
Mash three-level preheater 103, fermenting-ripening wine with dregs are preheated to 45 DEG C, mash second level preheater 102 by mash level-one preheater 101
Be preheated to 55 DEG C, mash three-level preheater 103 enter degassing stages 2 after preheating about 61 DEG C, carbon dioxide and part in mature wine with dregs
Low boiling impurity separates under the action of 2 negative pressure of degassing stages with karusen, enters mash level-one preheater 101 containing miscellaneous thick wine vapour；
Thick wine vapour enters second level preheater 102 and negative pressure prefractionator condenser group 6 condenses, and condensate liquid enters thick wine tank 4.
B, into the partly degassed wine with dregs of normal pressure prefractionator 10 in normal pressure prefractionator 10 while downlink by 10 tower bottom of normal pressure prefractionator
The steam of rising heats, and wine vapour uplink is separated with useless mash；Useless mash is discharged in 10 tower bottom of normal pressure prefractionator, after preheating karusen
Send to the processing of vinasse processing system 12；Negative pressure prefractionator reboiler 11 is advanced on 10 wine vapour of normal pressure prefractionator to heat to negative pressure prefractionator 8,
Condensed crude alcohol enters thick wine tank 4；10 tower top vapour of normal pressure prefractionator heats negative pressure prefractionator 8 by negative pressure prefractionator reboiler 11.
8 tower bottom operation temperature of negative pressure prefractionator is 80 DEG C, and head temperature is 65 DEG C, and 2 head temperature of degassing stages is 60 DEG C.
C, crude alcohol from thick wine tank 4 after the preheating of crude alcohol preheater 13 (with 18 tower bottom spent hot water of high pressure essence tower into
Row heat exchange) enter in press smart tower 14, enter to carry out vapour-liquid mass with overhead reflux liquid after the vaporized alcohol of part after tower and exchange, it is gradually dense
Contracting, until the alcohol steam that tower top wine degree is 95% (v/v) or more, which enters normal pressure prefractionator reboiler I 16, heats normal pressure prefractionator 10, it is cold
Partial reflux after solidifying, remaining enters 18 top of high pressure essence tower.
The smart tower 14 of middle pressure works under positive pressure, operating pressure 0.25MPa, the middle heating method for pressing smart tower 14:
18 tower top alcohol steam of high pressure essence tower is by pressing smart tower 14 in the smart heating of tower reboiler 15 of middle pressure.Smart 14 tower bottom of the tower operation temperature of middle pressure
Degree is 121 DEG C, and head temperature is 113 DEG C.
D, the light wine from 14 tower bottom of the middle smart tower of pressure is after the preheating of high pressure essence tower feed preheater 17 (with steam condensate water
Exchange heat) enter the middle part of high pressure essence tower 18, alcohol is gradually concentrated after entering tower, until tower top alcohol concentration up to 95% (v/v) with
On, intermediate impurity (fusel iol) then more than feedboard it is several layers of it is stiff stay, after producing and cooling down enter fusel oil separator 19
Separate fusel oil.18 overhead vapor phase of high pressure essence tower extraction wine degree is the alcohol steam of 95% (v/v) or more through fume superheater 25
It is dehydrated into membrane separation device, remaining alcohol steam all flows back after pressing smart tower reboiler 15 to condense in.18 tower of high pressure essence tower
Kettle spent hot water preheats decontamination water treatment system 20 after crude alcohol.
High pressure essence tower 18 works under positive pressure, operating pressure 0.45MPa, the heating method of high pressure essence tower 18:
Live steam from boiler room heats high pressure essence tower 18 by 18 reboiler 21 of high pressure essence tower.18 tower bottom of high pressure essence tower operation temperature
Degree is 155 DEG C, and head temperature is 126 DEG C.
Into the alcohol steam of membrane separation device, it is introduced into low vacuum membrane module 26, the vacuum degree of low vacuum membrane module 26
For absolute pressure 9-11kpa, it is only necessary to which (28 DEG C) of ordinary cycle water are condensed by desorption condenser I 28, and low vacuum membrane module 26 can
Remove in raw material alcohol 65% or more moisture；Enter through the dewatered alcohol steam of low vacuum membrane module 26 into high vacuum film
Component 27, the vacuum degree of high vacuum membrane module 27 are absolute pressure 2-4kpa, and 1 DEG C of low temperature chilled water is needed to pass through desorption condenser II
29 condensations, high vacuum membrane module 27 can only remove in raw material alcohol 35% moisture.Ethyl alcohol and water are separated by the device, most
Alcohol fuel is obtained eventually.Divide the condensation of condensed in two stages device, saves the demand of chilled water.
Dewatered alcohol fuel steam enters normal pressure prefractionator reboiler II 24 and heats normal pressure prefractionator 10, enters back into after condensation
Mash three-level preheater 103 preheats karusen, most obtains alcohol fuel finished product after finished product cooler 7 is cooling afterwards.
The foregoing is merely preferred embodiment of the present application, are not intended to limit this application, for the skill of this field
For art personnel, various changes and changes are possible in this application.Within the spirit and principles of this application, made any to repair
Change, equivalent replacement, improvement etc., should be included within the scope of protection of this application.
Claims (10)
1. four column distillations and UF membrane integrated system, including mash preheater, negative pressure prefractionator (8), normal pressure prefractionator (10), middle pressure essence
Tower (14) and high pressure essence tower (18)；It is characterized by: high pressure essence tower (18) by pipeline be sequentially connected fume superheater (25) and
Membrane separation device；The membrane separation device includes concatenated low vacuum membrane module (26) and high vacuum membrane module (27)；It is described low
The input end and fume superheater (25) piping connection, the outlet end of low vacuum membrane module (26) and Gao Zhen of vacuum membrane module (26)
The input end of empty membrane module (27) connects；The outlet end of high vacuum membrane module (27) is connect with normal pressure prefractionator reboiler；Low vacuum
The outlet end of membrane module (26), the outlet end of high vacuum membrane module (27) also pass through desorption condenser I (28), desorption condensation respectively
Device II (29) is connect with anhydrous vacuum pump (30).
2. system according to claim 1, it is characterised in that: the low vacuum membrane module (26) and high vacuum membrane module
(27) include multiple concatenated shell-and-tube membrane structures, each shell-and-tube membrane structure include shell (31) and be located at shell
(31) internal inner tube, said inner tube includes ceramic tube (32) and the molecular screen membrane (33) for overlaying on ceramic tube (32) outer surface.
3. system according to claim 1, it is characterised in that: the normal pressure prefractionator reboiler include by pipeline respectively with
The normal pressure prefractionator reboiler I (16) and normal pressure prefractionator reboiler II (24) of normal pressure prefractionator (10) formation closed circuit；High vacuum film
The outlet end of component (27) is specifically connect with normal pressure prefractionator reboiler II (24).
4. system according to claim 3, it is characterised in that: the mash preheater includes mash level-one preheater
(101), mash second level preheater (102) and mash three-level preheater (103), the normal pressure prefractionator reboiler II (24) pass through pipe
Road is connect through mash three-level preheater (103) with finished product cooler (7).
5. system according to claim 1, it is characterised in that: desorption condenser I (28) outlet end and desorption condenser II
(29) outlet end passes through pipeline and connect with thick wine tank (4).
6. utilizing the method for the described in any item system distillation ethyl alcohol of claim 1-5, which comprises the following steps:
A, fermenting-ripening wine with dregs sloughs gas and forms degassing wine with dregs；
B, wine vapour is separated with useless mash in degassing wine with dregs；
C, wine vapour forms crude alcohol after condensing, and crude alcohol enters high pressure essence tower (18) after pressing smart tower (14) to distill in；
D, into the alcohol steam of high pressure essence tower (18) be concentrated into tower top wine degree be 95% (v/v) or more alcohol steam, one
Sequentially enter low vacuum membrane module (26) after lease making overheat to separate ethyl alcohol and water with high vacuum membrane module (27), alcohol fuel steams
Vapour enters normal pressure prefractionator reboiler II (24) heating normal pressure prefractionator (10)；It is cold that most moisture and a small amount of ethyl alcohol enter desorption
Enter the recycling of distillation workshop section after condenser I (28) and desorption condenser II (29) condensation；
Wherein low vacuum membrane module (26) vacuum degree is absolute pressure 9kpa-11kpa, leads to ordinary cycle water in desorption condenser I (28)；
The vacuum degree of high vacuum membrane module (27) is absolute pressure 2kpa-4kpa, and 1 DEG C of cryogenic freezing is led in desorption condenser II (29)
Water.
7. according to the method described in claim 6, it is characterized in that, fermenting-ripening wine with dregs is after preheating in negative pressure wine with dregs in step A
Tower (8) degassing stages (2) top feed, the karusen for sloughing gas enter degassing stages (2) bottom rear and mash are divided to pass through gravity line
Road flows into negative pressure prefractionator (8), enters at the top of normal pressure prefractionator (10) after remaining is preheated.
8. according to the method described in claim 6, it is characterized in that, the wine with dregs that deaerates is in negative pressure prefractionator (8) and normal pressure wine with dregs in step B
The steam risen while downlink by tower bottom in tower (10) heats, and wine vapour uplink is separated with useless mash, and vinasse are discharged in tower bottom, send
Go to vinasse processing system (12).
9. according to the method described in claim 6, it is characterized in that, in step C, negative pressure prefractionator (8) and normal pressure prefractionator (10) tower
The wine vapour on top enters thick wine tank (4) after condensing, and presses smart tower (14) lower part after the crude alcohol of thick wine tank (4) is preheated in entrance,
Smart tower (14) the tower top wine vapour of middle pressure all flows back after the condensation of normal pressure prefractionator reboiler, and high pressure essence is entered after tower bottom alcohol is preheated
Tower (18).
10. according to the method described in claim 6, it is characterized in that, in step D, into high pressure essence tower (18) part alcohol afterwards
Vapour-liquid mass is carried out with overhead reflux liquid after evaporation to exchange, is gradually concentrated, until the alcohol that tower top wine degree is 95% (v/v) or more steams
Vapour part striping dehydration device after overheating is separated ethyl alcohol and water by the device；Remaining whole removes normal pressure prefractionator reboiler
It heats normal pressure prefractionator (10), high pressure essence tower (18) tower reactor spent hot water preheats decontamination water treatment system (20) after crude alcohol；
Mash three-level preheater (103) preheating karusen is entered back into after the condensation of alcohol fuel steam, most afterwards through finished product cooler (7)
Alcohol fuel finished product is obtained after cooling；The ordinary cycle water is 26 DEG C -28 DEG C.
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| CN111036083A (en) * | 2019-12-30 | 2020-04-21 | 肥城金塔机械有限公司 | Energy-saving method and device for triple-effect membrane separation dehydration for preparing anhydrous alcohol |
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| CN111072454B (en) * | 2020-01-19 | 2024-02-27 | 肥城金塔机械科技有限公司 | System and process for producing fuel ethanol by double-coarse and double-fine distillation with low pressure method |
| CN112827202A (en) * | 2020-12-30 | 2021-05-25 | 肥城金塔酒精化工设备有限公司 | Method and device for distilling fuel ethanol by using superheated steam fluidized bed dryer secondary steam as partial heat source |
| CN115636728A (en) * | 2021-07-20 | 2023-01-24 | 中国石油天然气股份有限公司 | Treatment method of cellulose ethanol fermentation mash and preparation method of cellulose fuel ethanol |
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