CN204058301U - A kind of production equipment of biomass dehydrated alcohol - Google Patents
A kind of production equipment of biomass dehydrated alcohol Download PDFInfo
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- CN204058301U CN204058301U CN201420547076.1U CN201420547076U CN204058301U CN 204058301 U CN204058301 U CN 204058301U CN 201420547076 U CN201420547076 U CN 201420547076U CN 204058301 U CN204058301 U CN 204058301U
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- tower
- heat exchange
- atmospheric distillation
- infiltrating
- rectifying
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 174
- 229960000935 dehydrated alcohol Drugs 0.000 title claims abstract description 32
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 239000002028 Biomass Substances 0.000 title claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 101
- 238000004821 distillation Methods 0.000 claims abstract description 74
- 239000012528 membrane Substances 0.000 claims abstract description 68
- 230000006835 compression Effects 0.000 claims abstract description 60
- 238000007906 compression Methods 0.000 claims abstract description 60
- 230000008016 vaporization Effects 0.000 claims abstract description 46
- 239000002994 raw material Substances 0.000 claims abstract description 40
- 239000000463 material Substances 0.000 claims description 38
- 239000012466 permeate Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 7
- 230000008676 import Effects 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 25
- 230000018044 dehydration Effects 0.000 abstract description 10
- 238000006297 dehydration reaction Methods 0.000 abstract description 10
- 239000003960 organic solvent Substances 0.000 abstract description 3
- 229960004756 ethanol Drugs 0.000 description 41
- 239000000047 product Substances 0.000 description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 19
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 12
- 239000000203 mixture Substances 0.000 description 10
- 238000000926 separation method Methods 0.000 description 10
- 239000007864 aqueous solution Substances 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 238000010992 reflux Methods 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 8
- 238000000855 fermentation Methods 0.000 description 8
- 230000004151 fermentation Effects 0.000 description 8
- 238000002156 mixing Methods 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 239000011259 mixed solution Substances 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 230000000149 penetrating effect Effects 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 150000001298 alcohols Chemical class 0.000 description 3
- 238000010533 azeotropic distillation Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000002131 composite material Substances 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000000895 extractive distillation Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000001764 infiltration Methods 0.000 description 3
- -1 military project Substances 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- FKNQCJSGGFJEIZ-UHFFFAOYSA-N 4-methylpyridine Chemical compound CC1=CC=NC=C1 FKNQCJSGGFJEIZ-UHFFFAOYSA-N 0.000 description 2
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical class CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 2
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- 239000004642 Polyimide Substances 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 description 2
- 230000008595 infiltration Effects 0.000 description 2
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 238000005373 pervaporation Methods 0.000 description 2
- 229920001721 polyimide Polymers 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- DHKHKXVYLBGOIT-UHFFFAOYSA-N 1,1-Diethoxyethane Chemical compound CCOC(C)OCC DHKHKXVYLBGOIT-UHFFFAOYSA-N 0.000 description 1
- HNAGHMKIPMKKBB-UHFFFAOYSA-N 1-benzylpyrrolidine-3-carboxamide Chemical compound C1C(C(=O)N)CCN1CC1=CC=CC=C1 HNAGHMKIPMKKBB-UHFFFAOYSA-N 0.000 description 1
- BSKHPKMHTQYZBB-UHFFFAOYSA-N 2-methylpyridine Chemical compound CC1=CC=CC=N1 BSKHPKMHTQYZBB-UHFFFAOYSA-N 0.000 description 1
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical group [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 244000061456 Solanum tuberosum Species 0.000 description 1
- 235000002595 Solanum tuberosum Nutrition 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 150000001241 acetals Chemical class 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- OBNCKNCVKJNDBV-UHFFFAOYSA-N butanoic acid ethyl ester Natural products CCCC(=O)OCC OBNCKNCVKJNDBV-UHFFFAOYSA-N 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000004310 lactic acid Substances 0.000 description 1
- 235000014655 lactic acid Nutrition 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 238000011176 pooling Methods 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000005382 thermal cycling Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Classifications
-
- 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
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a kind of production equipment of biomass dehydrated alcohol, belongs to dehydration of organic solvent technical field.At least one compression rectification tower (1), at least one atmospheric distillation tower (2), at least one vacuum rectification tower (3), infiltrating and vaporizing membrane (4); Compression rectification tower (1), atmospheric distillation tower (2) are connected with the entrance of infiltrating and vaporizing membrane (4) respectively with the tower top of vacuum rectification tower (3); Fermented liquid raw material pipeline (6) carries out with the escape route of the feed liquid side of infiltrating and vaporizing membrane (4) and the escape route of tower bottom of rectifying tower liquid after heat exchange is connected, entering to respectively in rectifying tower respectively.This production equipment considers intrasystem energy-optimised configuration at different levels, thus realizes the object of energy saving of system, and the steam mono-consumption of whole system can be saved steam and reach more than 30 ~ 50% compared with traditional technique.
Description
Technical field
The utility model relates to a kind of production equipment of biomass dehydrated alcohol, belongs to dehydration of organic solvent technical field.
Background technology
Dehydrated alcohol widely uses in food, chemical industry, fuel, military project, medicine and other fields.Biomass ferment alcohol concn is out generally 3 ~ 20wt%, when the ethanol maximum concentration after common distillation workshop section removes most of water, aldehyde and fusel wet goods impurity reaches 95% and water define azeotrope, be difficult to separate by the method for common distillation.For obtaining dehydrated alcohol, above-mentioned ethanol must be carried out further processed.
Existing dewatering mainly contains adsorption dewatering, azeotropic distillation, extractive distillation with salt, infiltrating and vaporizing membrane dehydration etc.Azeotropic distillation adds benzene, distills in main distillation column, at the bottom of tower, obtain dehydrated alcohol, and tower top obtains alcohol-water-benzene tertiary mixture (boiling point 64.8 DEG C).Two-layer being divided in this tertiary mixture introducing separator, upper strata is imbued with benzene, and lower floor is imbued with ethanol.Supernatant liquid introduces main distillation column again, reclaims benzene.Lower floor's liquid then reclaims ethanol wherein and benzene in secondary rectifying tower.Extractive distillation with salt adds the compound separating agent that solvent (as ethylene glycol) and salt (as calcium chloride) form, then rectifying, tower top obtains dehydrated alcohol, and the water at the bottom of tower and compound separating agent are sent to solvent regeneration tower rectifying except anhydrating, and solvent reclamation utilizes.
Infiltrating and vaporizing membrane dehydration technique is a kind of separation method that the distillation method of thermal drivers combines with embrane method, the mixture of organic solvent and water, under the promotion of component vapor partial pressure difference, utilizes component to realize the sepn process of material by infiltrating and vaporizing membrane absorption and the difference of velocity of diffusion.Adopt inorganic infiltrating and vaporizing membrane dehydration technique to carry out organics dehydration, the separating technology that distillation, absorption etc. are traditional can be substituted, high-quality product can be obtained with lower energy consumption, realize the separation requirement that ordinary method is difficult to maybe cannot realize.This sepn process shows the energy-saving effect of height, is particularly suitable for azeotrope, closely boils the separation of mixture, can save energy more than 50% compared with traditional rectifying, adsorption technology; This process does not need to introduce the third component, avoids the third component pollution on the environment, and a small amount of permeate can recycle and recycle simultaneously; Infiltrating and vaporizing membrane dewatering unit compact construction, floor space is little; Infiltrating and vaporizing membrane dehydration process is simple, and level of automation is high.
Azeotropic distillation and extractive distillation with salt need add and reclaim three components, and energy consumption is high, fluctuation of service, and environment is unfriendly.Molecular sieve adsorption uses 3A molecular sieve, reheat after high concentration ethanol heating and gasifying and pass into molecular sieve adsorption device adsorption dewatering to superheat state and obtain dehydrated alcohol, this method is widely used, there is the advantage of pervaporation membrane, but desorption out light is held a lot of liquor, concentration is low, and steam consumption is large compared with pervaporation membrane.Conventional distillation and further dehydration workshop section adopt different technique and heat reclaiming system, and steam mono-consumption difference is comparatively large, conventional distillation section double tower process unit consumption up to 2.5 tons of steam/ton dehydrated alcohol, multitower technique unit consumption about 2 tons of steam/ton dehydrated alcohols.
Utility model content
Technical problem to be solved in the utility model is: the product energy consumption that biomass ferment is produced in the process of dehydrated alcohol is large, provides a kind of production equipment of biomass dehydrated alcohol.
Technical scheme:
According to an aspect of the present utility model, a kind of production method of biomass dehydrated alcohol, comprise the steps: that fermented liquid is respectively by compression rectification, at least one times atmospheric distillation at least one times with at least one times after rectification under vacuum, the overhead vapours of rectifying tower is dewatered further by infiltrating and vaporizing membrane, obtains finished product ethanol; Fermented liquid, before feeding rectifying tower, carries out heat exchange with the tower bottoms of finished product ethanol and rectifying tower; Described rectifying tower refers at least one in compression rectification tower, atmospheric distillation tower and vacuum rectification tower.
Described rectifying tower refers to compression rectification tower, atmospheric distillation tower and vacuum rectification tower.
Further, the overhead vapours of compression rectification and the tower bottoms of atmospheric distillation carry out heat exchange.
Further, the overhead vapours of atmospheric distillation and the tower bottoms of rectification under vacuum carry out heat exchange.
Further, entering the flow direction of rectifying tower along fermented liquid, fermented liquid passes through following level Four heat exchange successively: the first step: the heat exchange of finished product ethanol; The second stage: the tower bottoms heat exchange of rectifying tower; The third stage: finished product ethanol heat exchange; The fourth stage: the tower bottoms heat exchange of rectifying tower.
Further, the tower bottoms of the rectifying tower of the described second stage refers to the mixed solution of tower bottoms of compression rectification, atmospheric distillation and rectification under vacuum.
Further, the flow direction of finished product ethanol after infiltrating and vaporizing membrane dehydration, finished product ethanol successively with enter the stock liquid of compression rectification, the stock liquid of atmospheric distillation, the stock liquid of rectification under vacuum and the fermented liquid do not shunted carries out heat exchange.
Further, along the discharge direction of kettle material, the kettle material of compression rectification tower successively with enter compression rectification tower, enter the raw material of vacuum rectification tower and carry out heat exchange, obtain still liquid a; The kettle material of atmospheric distillation tower carries out heat exchange with the raw material entering atmospheric distillation tower, obtains still liquid b; After still liquid a, still liquid b mix with the tower bottoms of vacuum rectification tower, then carry out heat exchange with the fermented liquid do not shunted.
Further, the overhead product of compression rectification, atmospheric distillation, after heat exchange, is partly refluxed in respective tower respectively.
Further, the tower top absolute pressure 0.4 ~ 0.45MPa of compression rectification, tower top temperature 115 ~ 125 DEG C, column bottom temperature 140 ~ 150 DEG C.
Further, the tower top absolute pressure 0.10 ~ 0.15MPa of atmospheric distillation, tower top temperature 80 ~ 90 DEG C, column bottom temperature 105 ~ 115 DEG C.
Further, the tower top absolute pressure 0.015 ~ 0.020MPa of rectification under vacuum, tower top temperature 35 ~ 45 DEG C, column bottom temperature 65 ~ 75 DEG C.
Further, ethanol 3 ~ 20wt.% is contained in fermented liquid.
Further, the water content in the overhead product of rectifying tower is 15 ~ 20wt.%.
Further, the per-meate side feed liquid of infiltrating and vaporizing membrane is back to vacuum rectification tower and reclaims.
According to another aspect of the present utility model, the production equipment of biomass dehydrated alcohol, includes: at least one compression rectification tower, at least one atmospheric distillation tower, at least one vacuum rectification tower, infiltrating and vaporizing membrane; Compression rectification tower, atmospheric distillation tower are connected with the entrance of infiltrating and vaporizing membrane respectively with the tower top of vacuum rectification tower; Fermented liquid raw material pipeline carries out with the escape route of the feed liquid side of infiltrating and vaporizing membrane and the tower bottoms escape route of rectifying tower after heat exchange is connected, entering to respectively in rectifying tower respectively; Described rectifying tower refers at least one in compression rectification tower, atmospheric distillation tower and vacuum rectification tower.
Further, between the discharging pipeline of the tower top of compression rectification tower and the tower reactor of atmospheric distillation tower for heat exchange is connected; Connect preferably by reboiler.
Further, along the tower top material discharge direction of compression rectification tower, the tower top of compression rectification tower after carrying out heat exchange connection, then is connected to the tower top of compression rectification tower by the first part flow arrangement.
Further, between the discharging pipeline of the tower top of atmospheric distillation tower and the tower reactor of vacuum rectification tower for heat exchange is connected; Connect preferably by reboiler.
Further, along the tower top material discharge direction of atmospheric distillation tower, the tower top of atmospheric distillation tower after carrying out heat exchange connection, then is connected to the tower top of atmospheric distillation tower by the first part flow arrangement.
Further, entering the flow direction of rectifying tower along fermented liquid, fermented liquid raw material pipeline carries out level Four heat exchange with such as lower pipeline successively and is connected: the first step, the escape route of the feed liquid side of infiltrating and vaporizing membrane; The second stage, the escape route of tower bottom of rectifying tower liquid; The third stage, the escape route of the feed liquid side of infiltrating and vaporizing membrane; The fourth stage, the escape route of tower bottom of rectifying tower liquid.
Further, the escape route of the tower bottom of rectifying tower liquid of the above-mentioned second stage refers to the mutual mixed escape route of the tower bottoms of compression rectification tower, atmospheric distillation tower and vacuum rectification tower.
Further, the flow direction of finished product ethanol after infiltrating and vaporizing membrane dehydration, the escape route of the feed liquid side of infiltrating and vaporizing membrane successively with enter the pipeline of stock liquid of compression rectification tower, the pipeline entering the stock liquid of atmospheric distillation tower, the pipeline entering the stock liquid of rectification under vacuum and the pipeline of fermented liquid do not shunted and carry out heat exchange and be connected.
Further, along the discharge direction of kettle material, the escape route of compression rectification tower successively with enter compression rectification tower, enter after the raw material pipeline heat exchange of vacuum rectification tower is connected, and after the escape route of atmospheric distillation tower is connected with the raw material pipeline heat exchange entering atmospheric distillation tower, mutually collect with the tower bottoms escape route of vacuum rectification tower again, collect pipeline and carry out heat exchange with the pipeline of the fermented liquid do not shunted again and be connected.
Further, the per-meate side of infiltrating and vaporizing membrane is connected with the import of vacuum rectification tower.
Beneficial effect
1, the utility model dewaters further and adopts infiltration evaporation membrane separation unit, and do not limit by azeotropic, simply, level of automation is high, easy and simple to handle, and occupation area of equipment is few for technological process; This process does not need to introduce the third component, avoids the third component pollution on the environment, simultaneously does not need to reclaim three components and energy-conservation; One time yield is high, and penetrating fluid returns to distillation tower recycling simultaneously, decreases the quantity discharged of ethanol, adds the total recovery of ethanol;
2, the utility model adopts 3 tower differential pressure rectifying, only need to provide steam to the raw materials evaporate of boiling again at the bottom of high-pressure tower tower and enter membrane separation unit, the whole recycle of other heats, the steam mono-consumption of whole system is 1.35 tons of steam/ton dehydrated alcohol product, can save steam and reach more than 30 ~ 50% compared with traditional technique.
3, the utility model energy-optimised configuration at different levels, multiple preheater, reboiler are equivalent to condenser, decrease the fixture investment of whole system.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the wood-based composites dewatering unit adopted in embodiment 1.
Fig. 2 is the schematic flow sheet of the wood-based composites dewatering unit adopted in embodiment 2.
Fig. 3 is the schematic flow sheet of the wood-based composites dewatering unit adopted in embodiment 3.
Wherein, 1, compression rectification tower; 2, atmospheric distillation tower; 3, vacuum rectification tower; 4, infiltrating and vaporizing membrane; 5, vacuum pump; 6, fermented liquid raw material pipeline; 7, the first part flow arrangement; 8, the second part flow arrangement; 18, penetrating fluid condenser; 19, well heater; 20, overhead condenser.The parts being labeled as R in figure are reboiler, and the parts being labeled as E in figure are interchanger.
Embodiment
Below by embodiment, the utility model is described in further detail.But it will be understood to those of skill in the art that the following example only for illustration of the utility model, and should not be considered as limiting scope of the present utility model.Unreceipted concrete technology or condition person in embodiment, according to the technology described by the document in this area or condition (" chemical engineering handbook " (second edition) that such as Shi Jun etc. write, Chemical Industry Press, 1996) or carry out according to product description.Agents useful for same or the unreceipted production firm person of instrument, being can by the conventional products of commercial acquisition.
Approximate language used herein can be used for modifying the statement of any quantity in whole specification sheets and claims, and it can permit changing under the condition not causing its relevant basic function to change.Therefore, the value of being modified by the term of such as " about " is not limited to specified exact value.In at least some cases, approximate language can be corresponding with the precision of the instrument for measuring this value.Unless separately pointed out in context or statement, otherwise range limit can carry out combining and/or exchanging, and this scope is confirmed as and comprises included all subranges herein.Except in operation embodiment or except indicating in elsewhere, the numeral of the amount, reaction conditions etc. of all expression compositions used in specification sheets and claims or express the modification that all should be understood to be subject to word " about " in all cases.
In the utility model, dehydrated alcohol represents that purity of alcohol is 99% or more by weight, preferably 99.5% or more, further preferably 99.7% or more, particularly preferably 99.8% or more.
Succinct in order to describe, in the utility model, term " rectifying tower ", when without specified otherwise, is to refer to compression rectification tower, atmospheric distillation tower and vacuum rectification tower respectively.
In the utility model, term " heat exchange connection " refers to the mode of connection of a kind of pipeline and pipeline, feed liquid between pipeline and pipeline is not interconnected, and refer to that the outer wall of these two pipelines is interconnected and can exchange heat each other and the mixing being unlikely to make feed liquid, this mode of connection can be interconnected by interchanger usually.Interchanger can be chosen according to practical situation, is not particularly limited, and can exemplify: tubular heat exchanger, plate-type heat exchanger, finned heat exchanger, hot tube heat exchanger etc.
First fermented liquid is carry in a fermented liquid raw material pipeline, then becomes multiply feed liquid to enter to respectively in each rectifying tower after shunting again, therefore, in the utility model, term " fermented liquid do not shunted " refer to shunting before fermented liquid.
In the utility model, " the feed liquid side " of infiltrating and vaporizing membrane refers to the side at the feed liquid place to be separated entering infiltrating and vaporizing membrane, also referred to as retaining side.
In the utility model, the fermenting alcohol aqueous solution is not particularly limited.Such as, the fermenting alcohol aqueous solution can be from fermentation asccharin, obtains in starch and/or cellulose materials.These raw materials obtain the aqueous solution of fermenting alcohol in fermentation cylinder for fermentation.The alcohol concn of the fermenting alcohol aqueous solution is typically about 3 ~ 20% by weight, and preferably 5 ~ 12%.The aqueous solution of fermenting alcohol, except water and ethanol are as main component, also includes yeast and bacterium, and various byproduct comprises alcohol as methyl alcohol, lipid acid as formic acid, acetic acid, succsinic acid, lactic acid and butyric acid, aldehydes is as acetaldehyde and formaldehyde, ester class as ethyl acetate, ethyl butyrate, acetals is as diethyl acetal, ketone as acetone and methyl ethyl ketone, amine as pyridine, picoline, 3-methylamine and 4-picoline, and the mixture of higher alcohols and high-grade aliphatic ester, so-called potato spirit.Usually, unfermentable raw material remains as insoluble composition, forms suspension.
The aqueous solution of fermenting alcohol is directly input in rectifying tower by fermented liquid raw material pipeline 6 from fermentor tank, or is stored in a tank and inputs rectifying tower again.The aqueous solution of preferred fermenting alcohol removes large insoluble composition by coarse filtration before input rectifying tower.In addition, the aqueous solution of the fermenting alcohol after fermentation cylinder for fermentation, due to the existence of fatty acid by-products, possible pH is 3 ~ 5.Therefore, the acidic component preferably and in the fermenting alcohol aqueous solution, such as, by adding a kind of alkaline components.This neutralization is useful, because effectively can prevent acid pollution dehydrated alcohol after purification.The alkaline components being suitable for adding comprises water-soluble alkaline compound, as sodium hydroxide, and potassium hydroxide and potassium permanganate.
In infiltrating and vaporizing membrane 4, ethanol/water mixing steam selectivity is by separatory membrane, and the water vapour containing a small amount of ethanol is collected into the per-meate side of separatory membrane.The alcohol concn of per-meate side is 0.05 ~ 20% (such as, the ethanol of 1% by weight), and in order to improve the rate of recovery of ethanol, this penetrant can be got back in rectifying tower and reclaim further.On the other hand, in the feed side of separatory membrane, water is removed, and therefore can obtain high-purity dehydrated alcohol.
Usually, through the impellent of separatory membrane be the partial pressure difference of film both sides water vapour.Therefore, in the utility model, be suitable for making the ethanol/water mixing steam in well heater 20 to produce a relatively high pressure, about 200kPa (absolute pressure) or higher, preferably 250 ~ 700kPa (absolute pressure), then inputs membrane separation apparatus.Also the suitable pressure simultaneously reducing separatory membrane per-meate side.Specifically, separatory membrane per-meate side to be connected with vacuum pump 5 by penetrating fluid condenser 18 and to make this space by vacuum pumping, and through vapor permeable condensation in penetrating fluid condenser 18 of separatory membrane, produce phlegma, this phlegma is preferably recovered to rectifying tower.
Here it infiltrating and vaporizing membrane 4 is had no particular limits, as long as can isolate water vapour from the mixing steam of the water vapor separatory membrane and alcohol vapour.In addition, separatory membrane is had no particular limits, if it can from ethanol water mixing steam optionally infiltration water steam.Film can by polymkeric substance as polyimide, high molecular weight polyvinyl alcohol class, or inorganic materials such as zeolite and aluminum oxide are made.About the type of membrane separation apparatus, conventionally known type is just passable, the hollow fiber separation membrane component be made up of asymmetric polyimide hollow-fibre membrane of such as shell-tube type component assembling, or the organic zeolite membrane assembly of tubular separation membrane component assembling.
After obtaining ethanol fermentation liquid (or after corresponding pre-removal of impurities process has been carried out to it), the device provided by the utility model carries out processed to it, as shown in Figure 1, on the whole, three rectifying tower are included in the technique adopted, compression rectification tower 1 is respectively from left to right from figure, atmospheric distillation tower 2 and vacuum rectification tower 3, rectifying tower realizes the preliminary rectifying and dewatering of fermented liquid, water content in the material of tower top is reduced to about 15 ~ 20%, the tower top material of rectifying tower will be fed through in infiltrating and vaporizing membrane 4 and dewater further, infiltrating and vaporizing membrane 4 is preferential water permeable membrane, water in feed liquid can enter to per-meate side through rete, what feed liquid side obtained is dehydrated alcohol, be parallel with one another between rectifying tower in the utility model, separately the tower top material after rectifying is sent into infiltrating and vaporizing membrane 4 and dewater further, the material at the bottom of tower is water and other impurity mainly, and the processing unit can sending into other carries out subsequent disposal.
Because the dewater temperature of the finished product ethanol obtained of infiltrating and vaporizing membrane is higher, it can be used to carry out heat exchange to the raw material inputing to intrasystem fermented liquid, to reduce energy consumption, as shown in fig. 1, the alcohol vapour obtained by being dewatered by infiltrating and vaporizing membrane is directly connected by the mutual heat exchange of interchanger with fermented liquid raw material pipeline 6 without condensation, the heat of alcohol vapour can be passed to raw material, and avoid use condenser product is cooled.
Because the temperature in compression rectification tower 1 is generally higher than atmospheric distillation tower 2, and the temperature in atmospheric distillation tower 2 is also generally higher than the temperature in vacuum rectification tower 3, at the tower top absolute pressure 0.4 ~ 0.45MPa of the present embodiment compression rectification, tower top temperature 115 ~ 125 DEG C, column bottom temperature 140 ~ 150 DEG C, the tower top absolute pressure 0.10 ~ 0.15MPa of atmospheric distillation, tower top temperature 80 ~ 90 DEG C, column bottom temperature 105 ~ 115 DEG C, the tower top absolute pressure 0.015 ~ 0.020MPa of rectification under vacuum, tower top temperature 35 ~ 45 DEG C, column bottom temperature 65 ~ 75 DEG C, the utility model is connected by the overhead vapours escape route of compression rectification tower 1 is carried out heat exchange with the still liquid liquid of atmospheric distillation tower 2 by reboiler, the boiling hot amount again that can to realize at the bottom of the tower of atmospheric distillation tower 2 is provided by the overhead product of compression rectification tower 1 completely, similarly, the overhead vapours escape route of atmospheric distillation tower 2 carries out heat exchange with the still liquid of vacuum rectification tower 3 by reboiler and is connected, the boiling hot amount again that can to realize at the bottom of the tower of vacuum rectification tower 3 is provided by the overhead product of atmospheric distillation tower 2 completely, heat is provided only to need to carry out heat supply with the reboiler of steam to the tower bottom of compression rectification tower 1 to all rectifying tower.
In addition, because the still liquid at the bottom of the tower of each rectifying tower is mainly containing a large amount of water, also containing more heat in still liquid, carry out heat exchange by still liquid and input raw material, also can reduce energy consumption further.In order to utilize the heat in finished product ethanol, tower bottoms better, the heat exchange order of fermented liquid raw material is preferably through level Four preheating, in a preferred implementation of the present utility model, fermented liquid raw material is by following level Four heat exchange: the first step: the heat exchange of finished product ethanol; The second stage: the tower bottoms heat exchange of rectifying tower; The third stage: finished product ethanol heat exchange; The fourth stage: the tower bottoms heat exchange of rectifying tower.As shown in Figure 1 like this, the mode that pipeline connects is: fermented liquid raw material pipeline carries out level Four heat exchange with such as lower pipeline successively and is connected: the first step, the escape route of the feed liquid side of infiltrating and vaporizing membrane; The second stage, the escape route of tower bottom of rectifying tower liquid; The third stage, the escape route of the feed liquid side of infiltrating and vaporizing membrane; The fourth stage, the escape route of tower bottom of rectifying tower liquid.
In order to multi-method carries out the problem of thermal cycling utilization, finding the interflow by changing charging fermented liquid and shunting, the interflow of still underflow and the arrangement situation of shunting in the utility model, can heat be effectively utilized.In improvement embodiment of the present utility model, when heat exchange is carried out in fermented liquid charging and kettle base solution, second stage heat exchange is by after being mixed by the kettle base solution of compression rectification tower 1, atmospheric distillation tower 2, vacuum rectification tower 3, to carry out heat exchange as mixed solution with it; In addition, when the fourth stage heat exchange for fermented liquid raw material, the utility model find by by fermented liquid raw material shunt after, respectively with pressurization and atmospheric distillation tower tower at the bottom of liquid carry out separately heat exchange time, energy consumption can be reduced further, because the temperature of the tower bottoms of vacuum rectification tower 3 is lower, can not fourth stage heat exchange be carried out and only carry out second stage heat exchange; As shown in Figure 1, more preferably heat exchange mode is: along the discharge direction of kettle material, the kettle material of compression rectification tower 1 successively with enter separately compression rectification tower 1, enter the raw material of vacuum rectification tower 3 and carry out heat exchange, obtain still liquid a, the kettle material of atmospheric distillation tower 2 carries out heat exchange with the raw material entering separately atmospheric distillation tower 2, obtains still liquid b; After still liquid a, still liquid b mix with the tower bottoms of vacuum rectification tower 3, then carry out heat exchange with the fermented liquid do not shunted.In addition, improve in embodiment at one of the present utility model, above-mentioned third stage heat exchange is carried out for fermenting raw materials liquid, when namely raw material and finished product ethanol carry out heat exchange, preferably raw material is divided into the material of multiple flow to each rectifying tower, and finished product ethanol carries out heat exchange with these materials successively, as shown in Figure 1, fermented liquid raw material is after the second stage heat exchange of mixed solution at the bottom of still, divide into the material that multiply flows to each rectifying tower respectively, and finished product ethanol is after outflow, first heat exchange is carried out with the material entering compression rectification tower 1, heat exchange is carried out successively again with the material flowing into atmospheric distillation tower 2 and vacuum rectification tower 3, finally carry out heat exchange with the fermented liquid do not shunted again, in actually operating, although also the heat exchange of finished product ethanol order can be changed, such as: first carry out heat exchange with the fermentation raw material do not shunted, then carry out heat exchange with the material of decompression, normal pressure, compression rectification successively, but energy consumption a kind of afterwards can be higher than front one.
Embodiment is improved as one of the present utility model, the overhead product of compression rectification tower, atmospheric distillation tower respectively with the still liquid liquid heat exchange of normal pressure, decompression after, partial reflux enters in each tower, these materials can form trim the top of column liquid, make the pneumatic separation better effects if in rectifying, this also avoids and use condenser at tower top, reduce energy consumption, and solidifying gas can directly be sent into infiltrating and vaporizing membrane and is separated, if when temperature is lower slightly, also certain heating can be carried out before it enters infiltrating and vaporizing membrane.As illustrated in figures 1-3 like this, along the tower top material discharge direction of compression rectification tower, for heat exchange is connected between the discharging pipeline of the tower top of compression rectification tower and the tower reactor of atmospheric distillation tower, then the tower top of compression rectification tower is connected to by the first part flow arrangement; Along the tower top material discharge direction of atmospheric distillation tower, for heat exchange is connected between the discharging pipeline of the tower top of atmospheric distillation tower and the tower reactor of vacuum rectification tower, then be connected to the tower top of atmospheric distillation tower by the second part flow arrangement; First, second part flow arrangement 7,8 role is that the tower top material through heat exchange of part is back to respective rectifying tower, realizes backflow.
Conventional condenser can be adopted to carry out condensation rear section at the tower top material of vacuum rectification tower to be back in vacuum distillation tower.
Embodiment 1
As Fig. 1, the equipment that the isolation technique in production technology of absolute alcohol by zeolite molecular sieve described in the utility model embodiment uses comprises: compression rectification tower 1, atmospheric distillation tower 2, vacuum rectification tower 3, infiltrating and vaporizing membrane 4, vacuum pump 5, reboiler; Interchanger; Penetrating fluid condenser 18; Well heater 19; Overhead condenser 20, is connected with valve by pipeline between each equipment.
40 DEG C of stock liquids that 10900kg/h from fermentation workshop section contains ethanol 11.4wt% input rectifying-infiltration evaporation system by pipeline.The tower top absolute pressure 0.42MPa of compression rectification tower 1, tower top temperature 119 DEG C, column bottom temperature 146 DEG C, the heat of the reboiler at the bottom of tower is provided by primary steam, and reflux ratio is 0.58, the tower top absolute pressure 0.13MPa of atmospheric distillation tower 2, tower top temperature 85 DEG C, column bottom temperature 109 DEG C, the tower top material of compression rectification tower 1 carries out heat exchange by pipeline with the reboiler at the bottom of atmospheric distillation tower 2 tower and is connected, the heat boiled again at the bottom of the tower of atmospheric distillation tower 2 is all provided by high-pressure tower overhead product, after the tower top material of compression rectification tower 1 carries out heat exchange, be partly refluxed to compression rectification tower 1 by the first reflux 7, reflux ratio was 0.58 (can be called the reflux ratio of compression rectification tower 1), described rectification under vacuum column overhead absolute pressure 0.02MPa, tower top temperature 41 DEG C, column bottom temperature 67 DEG C, the tower top material of atmospheric distillation tower 2 carries out heat exchange by pipeline with vacuum rectification tower 3 tower bottom reboiler and is connected, the heat boiled again at the bottom of tower is all provided by atmospheric tower overhead product, after the tower top material of atmospheric distillation tower carries out heat exchange, atmospheric distillation tower is partly refluxed to by the second reflux 8, reflux ratio was 0.61 (can be called the reflux ratio of atmospheric distillation tower), the material of the tower top of vacuum rectification tower is after overhead condenser 20 condensation, be partly refluxed to vacuum rectification tower, reflux ratio is 1.4.
Dehydrated alcohol after infiltrating and vaporizing membrane 4 dewaters is preheating to 45 DEG C to raw material, after fermented liquid raw material inputs to system, first one-level preheating is carried out through dehydrated alcohol, next, the mixed solution of the tower bottoms of three rectifying tower carries out secondary to it again and is preheating to 65 DEG C, then 1.33:1:1 partition ratio is shunted in mass ratio, enter pressurization respectively, normal pressure, vacuum rectification tower, and through three grades of preheatings of dehydrated alcohol, as shown in Figure 1, the dehydrated alcohol carrying out preheating to these three strands of materials is positioned at the upper reaches that dehydrated alcohol flows out direction, and be first 97 DEG C are preheating to the raw material entering compression rectification tower, then successively 85 DEG C and 80 DEG C are preheating to the material entering normal pressure and vacuum rectification tower.Next these raw materials need the preheating through tower bottoms, these tower bottomss are the upstreams being positioned at tower reactor mixed solution, as shown in Figure 1, three strands of materials are before pooling together and carrying out secondary preheating to raw material, independently discharge, first the tower bottoms flowed out from compression rectification tower is carry out level Four preheating 122 DEG C to the raw material entering compression rectification tower, again 100 DEG C are preheated to the material entering vacuum rectification tower, and then collect with other still liquid, and the tower bottoms of discharging from atmospheric distillation tower first carries out level Four preheating 100 DEG C to the raw material entering atmospheric distillation tower, and then collect with other still liquid, and preheating do not participated in by the tower bottoms of vacuum rectification tower, because its temperature is lower, after directly mixing with other tower bottoms, secondary preheating is carried out to fermented liquid raw material.
The ethanol evaporation of the rear moisture 17wt% of 1630kg/h of ethanol mixing of the ethanol of the moisture 14.6wt% of compression rectification column overhead 580kg/h, the ethanol of the moisture 16.6wt% of atmospheric distillation column overhead 450kg/h, the moisture 19.5wt% of rectification under vacuum column overhead 600kg/h becomes 115 DEG C of saturation steams and enters infiltrating and vaporizing membrane dewatering unit, adopts 200M
2molecular screen membrane, membrane permeation wall pressure is 1500Pa, and finished product is that the penetrant of 99.7wt%, 300kg/h is preheating to 57 DEG C through still raffinate and enters vacuum rectification tower again and reclaim after low temperature secondary refrigerant condenses to 0 DEG C.
This technique skill is adopted to need the reboiler at the bottom of tower for compression rectification tower 1 and the well heater 19 (for heating the steam entering infiltrating and vaporizing membrane) of steam heating, other heat supplies all carry out heat reuse, and the quantity of steam obtaining the ethanol needs per ton of 99.7% is 1.35 ~ 1.40 tons.The utility model production method considers intrasystem energy-optimised configuration at different levels, thus realizes the object of energy saving of system, can save steam and reach more than 30 ~ 50% compared with traditional technique.
Embodiment 2
The device adopted as shown in Figure 2, be with the difference of embodiment 1: the heat exchange order of the dewatered ethanol of infiltrating and vaporizing membrane 4 there occurs change, first it be carry out first step heat exchange with total feed liquid of fermented liquid raw material, next, the mixed solution of the tower reactor of stock liquid and rectifying tower carries out the heat exchange of the second stage, then dewatered ethanol successively with enter to separately reduce pressure, the material of normal pressure, compression rectification tower carries out heat exchange, the quantity of steam obtaining the ethanol needs per ton of 99.7% is 1.40 ~ 1.45 tons.
Embodiment 3
As shown in Figure 3, be with the difference of embodiment 1: the heat exchange mode of the dewatered ethanol of infiltrating and vaporizing membrane 4 there occurs change, first it carry out three grades of heat exchange with the fermented liquid that have passed through secondary heat exchange, not be successively heat exchange is carried out to the stock liquid entering three rectifying tower respectively as in embodiment 1 when three grades of heat exchange, but directly heat exchange is carried out to the total feed liquid of the fermented liquid coming from interchanger 16, carry out again afterwards branching to three rectifying tower, feed liquid after shunting carries out level Four heat exchange with the tower bottoms of rectifying tower more respectively, the quantity of steam obtaining the ethanol needs per ton of 99.7% is 1.4 ~ 1.5 tons.
Claims (8)
1. a production equipment for biomass dehydrated alcohol, is characterized in that, includes: at least one compression rectification tower (1), at least one atmospheric distillation tower (2), at least one vacuum rectification tower (3), infiltrating and vaporizing membrane (4); Compression rectification tower (1), atmospheric distillation tower (2) are connected with the entrance of infiltrating and vaporizing membrane (4) respectively with the tower top of vacuum rectification tower (3); Fermented liquid raw material pipeline (6) carries out with the escape route of the feed liquid side of infiltrating and vaporizing membrane (4) and the tower bottoms escape route of rectifying tower after heat exchange is connected, entering to respectively in rectifying tower respectively; Described rectifying tower refers at least one in compression rectification tower (1), atmospheric distillation tower (2) and vacuum rectification tower (3).
2. the production equipment of biomass dehydrated alcohol according to claim 1, is characterized in that: for heat exchange is connected between the discharging pipeline of the tower top of compression rectification tower (1) and the tower reactor of atmospheric distillation tower (2).
3. the production equipment of biomass dehydrated alcohol according to claim 2, it is characterized in that: along the tower top material discharge direction of compression rectification tower (1), the tower top of compression rectification tower (1) after carrying out heat exchange connection, then is connected to the tower top of compression rectification tower (1) by the first part flow arrangement (7).
4. the production equipment of biomass dehydrated alcohol according to claim 1, is characterized in that: for heat exchange is connected between the discharging pipeline of the tower top of atmospheric distillation tower (2) and the tower reactor of vacuum rectification tower (3).
5. the production equipment of biomass dehydrated alcohol according to claim 4, it is characterized in that: along the tower top material discharge direction of atmospheric distillation tower (2), the tower top of atmospheric distillation tower (2) after carrying out heat exchange connection, then is connected to the tower top of atmospheric distillation tower (2) by the second part flow arrangement (8).
6. the production equipment of biomass dehydrated alcohol according to claim 1, it is characterized in that: entering the flow direction of rectifying tower along fermented liquid, fermented liquid raw material pipeline (6) carries out level Four heat exchange with such as lower pipeline successively and is connected: the first step, the escape route of the feed liquid side of infiltrating and vaporizing membrane (4); The second stage, the tower bottoms escape route of rectifying tower; The third stage, the escape route of the feed liquid side of infiltrating and vaporizing membrane (4); The fourth stage, the tower bottoms escape route of rectifying tower.
7. the production equipment of biomass dehydrated alcohol according to claim 6, is characterized in that: the escape route of the tower bottom of rectifying tower liquid of the described second stage refers to the mutual mixed escape route of tower bottoms of compression rectification tower (1), atmospheric distillation tower (2) and vacuum rectification tower (3).
8. the production equipment of biomass dehydrated alcohol according to claim 1, is characterized in that: the per-meate side of infiltrating and vaporizing membrane (4) is connected with the import of vacuum rectification tower (3).
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104262090A (en) * | 2014-09-22 | 2015-01-07 | 江苏九天高科技股份有限公司 | Method and device for producing biomass absolute ethyl alcohol |
| CN108409535A (en) * | 2017-09-15 | 2018-08-17 | 江苏九天高科技股份有限公司 | The production technology and device of a kind of reuse method of fusel oil, ammonia from coal |
| CN109704920A (en) * | 2019-02-25 | 2019-05-03 | 天津市新天进科技开发有限公司 | From the energy-saving process method and device of low concentration fermentation liquid production alcohol fuel |
| CN112194567A (en) * | 2020-11-03 | 2021-01-08 | 山东中盛药化设备有限公司 | Process and system for recovering absolute ethyl alcohol by combining rectification, vaporization membrane and MVR (mechanical vapor recompression) technology |
-
2014
- 2014-09-22 CN CN201420547076.1U patent/CN204058301U/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104262090A (en) * | 2014-09-22 | 2015-01-07 | 江苏九天高科技股份有限公司 | Method and device for producing biomass absolute ethyl alcohol |
| CN104262090B (en) * | 2014-09-22 | 2016-06-29 | 江苏九天高科技股份有限公司 | The production method of a kind of biomass dehydrated alcohol and device |
| CN108409535A (en) * | 2017-09-15 | 2018-08-17 | 江苏九天高科技股份有限公司 | The production technology and device of a kind of reuse method of fusel oil, ammonia from coal |
| CN108409535B (en) * | 2017-09-15 | 2024-01-30 | 江苏九天高科技股份有限公司 | Method for recycling fusel oil, production process and device for preparing methanol from coal |
| CN109704920A (en) * | 2019-02-25 | 2019-05-03 | 天津市新天进科技开发有限公司 | From the energy-saving process method and device of low concentration fermentation liquid production alcohol fuel |
| CN109704920B (en) * | 2019-02-25 | 2024-01-30 | 天津市新天进科技开发有限公司 | Energy-saving process and device for producing fuel ethanol from low-concentration fermentation liquor |
| CN112194567A (en) * | 2020-11-03 | 2021-01-08 | 山东中盛药化设备有限公司 | Process and system for recovering absolute ethyl alcohol by combining rectification, vaporization membrane and MVR (mechanical vapor recompression) technology |
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