CN102070401B - Energy-saving process for preparing absolute ethanol from bioethanol aqueous solution - Google Patents
Energy-saving process for preparing absolute ethanol from bioethanol aqueous solution Download PDFInfo
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Abstract
The invention relates to a production method for preparing absolute ethanol from bioethanol aqueous solution. In the method, main equipment comprises vacuum rectifying tower, a return tank, a heat exchanger, an air source heat pump system, a refrigeration system, a vacuum system and the like; and the absolute ethanol with mass concentration of 99.5 to 99.9 percent is obtained after 15 to 25 percent ethanol-aqueous solution subjected to biological fermentation passes through three gradually pressure-reducing rectifying towers. In the process, a heat source is provided to the next level rectifying tower by utilizing heat of the materials in the preceding level rectifying tower; and the insufficient part is supplemented by the air source heat pump system. The ethanol aqueous solution raw material is preheated by utilizing the unused waste heat of the materials discharged from the rectifying towers to form a thermally coupled network, so that energy consumption in the process for producing unit mass of absolute ethanol is reduced by 30 to 48 percent compared with that in other process. The process has the prominent advantages of low energy consumption, high efficiency, small pollution and the like.
Description
Invention field
The present invention relates to be produced by the bio-ethanol aqueous solution new energy-saving process of dehydrated alcohol.
Background technology
Bio-ethanol refers to the ethanol that the fermentation by microorganism obtains various Wood Adhesives from Biomass, is a kind of renewable resources; Dehydrated alcohol refers to that water content is not higher than the ethanol of 0.3-0.5%wt, and its relative density is 0.7893(20 ℃), fusing point is :-114.5 ℃, boiling point is 78.32 ℃, and specific refractory power is 1.3614,14 ℃ of flash-points.Dehydrated alcohol is widely used in chemical reagent, agricultural chemicals, medicine, in all conglomeraties such as biology, paint, pigment, makeup, spices, electronics, especially under current petroleum resources situation in short supply, dehydrated alcohol has been joined in gasoline the fuel of making oil engine in a large number.Because the ethanol burning only produces carbonic acid gas and water, can not produce other obnoxious flavour, therefore use ethanol petrol to be conducive to reduce the pollution to environment.
The production of dehydrated alcohol initial twenties in last century, the excessive moisture adsorbed in industrial alcohol (95%) with CaO is produced dehydrated alcohol, utilizes again afterwards salt effect to produce, and is about to CaCl
2Add in industrial alcohol the vapor-liquid equilibrium that changes aqueous ethanolic solution Deng salt.The method for preparing at present dehydrated alcohol mainly contains unslaked lime evaporation, extraction fractional distillation, rectification under vacuum method, ion exchange method, azeotropic distillation, the molten rectification method of salt, anhydrous calciumsulphate method, molecular sieve adsorption and membrane separation process etc.Wherein azeotropic distillation, extraction fractional distillation and molecular sieve adsorption are the main method of current industrial production dehydrated alcohol, and obtained in practice application as the novel molecular sieve adsorption of producing dehydrated alcohol and membrane separation process, there is good development prospect.
Produced the traditional technology of dehydrated alcohol by biological fermentation process as shown in accompanying drawing one, biomass are joined in fermentation vat V-1 and fermented, after having fermented, the material in V-1 is carried out to wherein fermentation residue of filter at low temperature separation, obtain containing under normal temperature the fermented liquid of ethanol 15-25%, fermented liquid being obtained to the feed liquid of 85-90 ℃ after by transferpump P-1 and interchanger E-4 enters into rectifying tower T-1 by pipeline 3 and carries out initial gross separation, the pressure of rectifying tower T-1 is 1-1.2 normal atmosphere, the temperature of reboiler E-4 is 105-110 ℃, heating medium is 2-5 kilogram low-pressure steam, tower top obtains the mixing solutions containing ethanol 85-90%, be mainly water and high-boiling-point impurity at the bottom of tower, obtain high temperature at the bottom of tower and containing the water of minute quantity ethanol, this part water is used for to preheating material.The mixing solutions of tower top is entered to rectifying tower T-2 by pipeline 7 and make with extra care separation, the working pressure of rectifying tower T-2 is generally normal pressure, the temperature of reboiler E-5 is 100-105 ℃, heating medium is 2-5 kilogram low-pressure steam, tower top obtains the azeotropic liquid of alcohol-water, and its ethanol quality percentage composition is 95.57%.The azeotropic liquid of the alcohol-water of T-2 tower top is entered to adsorbing tower with molecular sieve T-3 through piping 11, remove moisture wherein.Obtain the dehydrated alcohol that ethanol content is 99.5%-99.7% after absorption.Make regenerating molecular sieve with dry warm air dehydration afterwards.
The energy consumption that this traditional technology is produced dehydrated alcohol mainly comprises: the hear rate used of the low-pressure steam that the tower reactor reboiler of rectifying tower T-1, T-2 consumes and molecular sieve dehydration regeneration.
Summary of the invention
The purpose of this invention is to provide a kind of more energy-conservation novel process and device of being produced dehydrated alcohol by the bio-ethanol aqueous solution, as shown in accompanying drawing two.The present invention adopts three tower variable-pressure rectification techniques, and is equipped with air source heat pump system, at the bottom of utilizing tower simultaneously and the used heat of tower top feed liquid form thermal coupling with reboiler and feed preheater, thereby realize the purpose of saving energy and reduce the cost by a relatively large margin.
Purpose of the present invention can realize by following technical solution:
A kind of technique of being produced dehydrated alcohol by the bio-ethanol aqueous solution, it comprises the following steps:
Step 1. is transported to interchanger E-6 and E-8 heat exchange to 40-55 ℃ from will the ferment bio-ethanol feed liquid containing the about 15-25% of ethanol that obtains of storage tank V-2 with pump P-2, the mixed liquor of discharging feed liquid at the bottom of discharging feed liquid and Second distillation column T-5 tower at the bottom of the tower that heating medium is the first rectifying tower T-4 after the first rectifying tower T-4 overhead vapours and heating Second distillation column T-5 tower bottom reboiler E-11, then the bio-ethanol feed liquid being transported to the first rectifying tower T-4 by pipeline 15 is separated, the operation absolute pressure of the first rectifying tower T-4 is 0.3-0.35 normal atmosphere, tower top temperature is 50-55 ℃, the temperature of the first rectifying tower T-4 tower bottom reboiler E-10 is 65-72 ℃, and can provide the air source heat pump system E-13 of hot water more than 80 ℃ to heat the first rectifying tower T-4 tower bottom reboiler E-10 by one,
Step 2. is after the first rectifying tower T-4 distillation, in the alcohol mixed solution of tower top, ethanol content reaches 80-90%, its part is refluxed by pipeline 18, part enters into Second distillation column T-5 by pipeline 19 and carries out rectifying, the operation absolute pressure of Second distillation column T-5 is 0.15-0.25 normal atmosphere, reflux ratio is selected 0.8-1.2, tower top temperature is 40-45 ℃, the temperature of Second distillation column T-5 tower bottom reboiler E-11 is 50-55 ℃, Second distillation column T-5 tower bottom reboiler E-11(arranges two of A/B in case of necessity) mainly by T-4 tower reactor discharging (for the aqueous solution of 65-72 ℃), heated, the shortage of heat part is by hot water more than air source heat pump system E-13(80 ℃) provide, can obtain purity from Second distillation column T-5 top is the aqueous ethanolic solution more than 95%, it will be as the charging of the 3rd rectifying tower T-6,
The tower bottom reboiler E-12 that the alcohol vapour that step 3. Second distillation column T-5 tower top is 40-45 ℃ enters the 3rd rectifying tower T-6 by pipeline 20 is heated the feed liquid in E-12 as thermal source, Partial Liquid Phase after the alcohol vapour condensation is delivered to Second distillation column T-5 tower top as backflow by reflux pump P-5 after metering, the rest part liquid phase is admitted in the 3rd rectifying tower T-6 carries out high vacuum rectification, the operation absolute pressure of the 3rd rectifying tower T-6 is 0.03-0.05 normal atmosphere, reflux ratio is determined (being generally between 1-3) according to the product purity requirement, the tower top vapor phase temperature is 12-20 ℃, at the bottom of tower, liquidus temperature is 25-32 ℃.The 3rd rectifying tower T-6 tower bottom reboiler E-12(arranges two of A/B in case of necessity) insufficient section of heat is by hot water more than air source heat pump system E-13(80 ℃) dehydrated alcohol that rectifying tower T-6 tower top can continuously extraction mass concentration is 99.5-99.9% is provided.
The above-mentioned technique of producing dehydrated alcohol, the negative pressure of described the first rectifying tower T-4, Second distillation column T-5 and the 3rd rectifying tower T-6 is by vacuum system VS-1, VS-2 and VS-3, to be provided respectively, before vacuum system, all need to be equipped with vacuum buffer device, to maintain the stable of pressure.
The above-mentioned technique of producing dehydrated alcohol, step 3, because the 3rd rectifying tower T-6 overhead product steam is 12-20 ℃, so the chilled brine of 0-5 ℃ provided by a refrigeration system R-1 as refrigerant with condensation tower top vapour phase, while is in the exit of three vacuum pump VS-1, VS-2 and VS-3, the cold-trap device that interchanger E-14 and cold-trap V-6 form is set, as the organism that will not yet be condensed in vacuum outlet gas again deep cooling trap among cold-trap V-6.So, the ethanol loss can be avoided on the one hand, the environmental pollution caused thus can be prevented on the other hand.
The above-mentioned technique of producing dehydrated alcohol, the refrigerant of described deep-cooling heat exchanger E-14 is also the chilled brine of 0-5 ℃ provided by refrigeration system R-1.
The present invention is optimized the purifying production process of traditional bio-ethanol, the reboiler E-10 of rectifying tower T-4 is heated by an air source heat pump system E-13, feed liquid and T-5 overhead vapours that the tower bottom reboiler E-11 of rectifying tower T-5 and the tower bottom reboiler E-12 of rectifying tower T-6 discharge by the T-4 tower reactor are respectively heated, not enough heat part is supplemented by air source heat pump system E-13, makes the heat of whole flow process consumption greatly reduce.With conventional art, compare, it is low that the present invention has energy consumption, pollutes littlely, and do not need to carry out the outstanding advantages that azeotropic distillation or extracting rectifying or molecular sieve adsorbing and dewatering can obtain the dehydrated alcohol product.
Technique of the present invention has the following advantages: used heat and reboiler and feed preheater formation thermal coupling at the bottom of tower top and tower between the three-tower rectification system that (1) utilization is reduced pressure step by step, and energy utilization is more scientific and reasonable; (2) application of vacuum system reduces rectifying tower T-4, T-5, T-6 service temperature greatly, for the use of air source heat pump system provide may, thereby significantly saved the high-grade energy that must adopt in the traditional technology--give birth to steam; (3) rectifying utilizes the thermodynamics ultimate principle--and system pressure exerts an influence to the vapor-liquid equilibrium of system, thereby breaks the normal pressure azeotropic point of alcohol-water, and then can directly obtain dehydrated alcohol by the rectification under vacuum mode; (4) through theoretical and experimental study, confirm, the present invention produces the required total energy consumption of dehydrated alcohol per ton and reduces 33～48% than traditional technology, and relatively low to the grade requirement of the energy.The energy consumption that the present invention produces dehydrated alcohol mainly comprises: vacuum system energy consumption, air source heat pump system energy consumption and refrigeration system energy consumption, and the energy consumption of material-handling pump.
The accompanying drawing explanation
Figure mono-is the conventional process flow schematic diagram.Wherein:
V-1 is raw material feed liquid storage tank, and T-1, T-2 are rectifying tower, and T-3 is molecular sieve water separation tower, E-1, E-2, E-3 are interchanger, and P-1, P-2 are fluid delivery pump, and E-4, E-5 are tower bottom reboiler, F1-1, F1-2 are valve, and 1,2,3,4,5,6,7,8,9,10,11,12 is pipeline.
Figure bis-is schematic flow sheet of the present invention.Wherein:
P-2 is fluid delivery pump, V-2 is raw material feed liquid storage tank, V-3, V-5 is snubber assembly, V-4, V-6 is cold-trap, T-4, T-5, T-6 is vacuum rectifying tower, E-6, E-7, E-8, E-9, E-14, E-15 is interchanger, E-10, E-11A, B, E-12A, B is tower bottom reboiler, E-13 is air source heat pump system, F2-1, F2-2, F2-3, F2-4, F2-5, F2-6, F2-7, F2-8, F2-9, F2-10, F2-11, F2-12, F2-13, F2-14, F2-15 is valve, VS-1, VS-2, VS-3 is vacuum system, R-1 is refrigeration system, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, 24, 25, 26, 27, 28, 29, 30, 31, 32 is fluid-transporting tubing, 33 is drain, 34, 35, 36, 37, 38, 39, 40, 41 is the air source heat pump system pipeline, 42, 43, 44, 45, 46, 47 is the refrigeration system pipeline, 48, 49, 50, 51, 52, 53, 54 is the vacuum system pipeline.
Embodiment
Further illustrate by the following examples the present invention.
Embodiment 1: the rectification under vacuum method is produced 10000 ton/years of dehydrated alcohols
The production method operation steps of dehydrated alcohol as shown in Figure 2.This system mainly is comprised of equipment such as rectifying tower, return tank, interchanger, air source heat pump system, refrigeration system, vacuum systems.Be provided with metering and control instruments and pipeline at each equipment room.To after being preheated to 45 ℃, interchanger E-6 enter rectifying tower T-4 containing the bio-ethanol of ethanol 22%, the theoretical plate number of rectifying tower T-4 tower is 35, tower diameter is 1.2 meters, adopt regular packing without wall flow in tower, the operation absolute pressure is 0.32 normal atmosphere, it is 70.6 ℃ that reflux ratio is selected 1.0, the first rectifying tower T-4 bottom liquid temperature.Adopt the air source heat pump system E13 that a hot water temperature is 83 ℃ to provide thermal source for rectifying tower T-4 reboiler.After distillation, the content of the alcohol mixture ethanol of the first rectifying tower T-4 tower top reaches 90.3%.The condensation rear section is as backflow, and part is sent to Second distillation column T-5 by pipeline 19 and carries out rectifying.
Second distillation column T-5 theoretical plate number is 40,1.3 meters of tower diameters, working pressure is 0.2 normal atmosphere, reflux ratio selects 1.2, the temperature of tower bottom reboiler E-11 is about 54.1 ℃, the heating medium of tower bottom reboiler E-11A is the discharging (aqueous solution, temperature is 70.6 ℃) of the first rectifying tower T-4 tower reactor, and the heating medium of tower bottom reboiler E-11B is the hot water that air source heat pump system E13 provides.Second distillation column T-5 top can obtain the alcohol vapour more than 95.5%, this steam is introduced in the 3rd rectifying tower T-6 tower bottom reboiler E-12A shell as heat source, condensed feed liquid enters storage tank V-4, the steam be not condensed rises to the further condensation of interchanger E-15 by tower bottom reboiler E-12A upper pipe, 2 ℃ of icy salt solutions that the refrigerant of E-15 provides for refrigeration system R-1.Also drop to storage tank V-4 by the liquid phase obtained after the E-15 condensation.Feed liquid in storage tank V-4 (ethanol content is more than 95.5%) is by transferpump P-3, and the tower top that its part is sent to Second distillation column T-5 after metering is as backflow, and another part is transported to the 3rd rectifying tower T-6 after metering as charging.The shortage of heat part of the 3rd rectifying tower T-6 is passed through tower bottom reboiler E-12B by air source heat pump system E-13 heat make-up.
The 3rd rectifying tower T-6 theoretical plate number is 120,1.6 meters of tower diameters, and working pressure is 0.06 normal atmosphere, and tower top temperature is 19.8 ℃, and the temperature of tower bottom reboiler E-12 is 33 ℃.But the dehydrated alcohol that the 3rd rectifying tower T-6 tower top extraction 1251.0 kg/hr concentration are 99.7%wt, in bottom product, ethanol content is lower than 0.013%wt.
Embodiment 2: the rectification under vacuum method is produced 8000 ton/years of dehydrated alcohols
Operating method is as embodiment 1.To after being preheated to 43 ℃, interchanger E-6 enter the first rectifying tower T-4 containing the bio-ethanol of ethanol 18%, the theoretical plate number of the first rectifying tower T-4 tower is 35, tower diameter is 1.2 meters, adopt regular packing without wall flow in tower, working pressure is 0.31 normal atmosphere, it is 68.7 ℃ that reflux ratio is selected 1.1, the first rectifying tower T-4 bottom liquid temperature.Adopt the air source heat pump system E13 that a hot water temperature is 83 ℃ to provide thermal source for the first rectifying tower T-4 reboiler.After distillation, the content of the alcohol mixture ethanol of the first rectifying tower T-4 tower top reaches 88.7%.The condensation rear section is as backflow, and part is sent to Second distillation column T-5 by pipeline 19 and carries out rectifying.
Second distillation column T-5 theoretical plate number is 40,1.3 meters of tower diameters, working pressure is 0.19 normal atmosphere, reflux ratio selects 1.1, the temperature of reboiler E-11 is about 54 ℃, the heating medium of tower bottom reboiler E-11A is the discharging (aqueous solution, temperature is 68.7 ℃) of the first rectifying tower T-4 tower reactor, and the heating medium of tower bottom reboiler E-11B is the hot water that air source heat pump system E13 provides.Second distillation column T-5 top can obtain the alcohol vapour more than 94.8%, this steam is introduced in the 3rd rectifying tower T-6 tower bottom reboiler E-12A shell as heat source, condensed feed liquid enters storage tank V-4, and the steam be not condensed rises to the further condensation of interchanger E-15 by reboiler E-12A upper pipe.2 ℃ of icy salt solutions that the refrigerant of E-15 provides for refrigeration system R-1.Also drop to storage tank V-4 by the liquid phase obtained after the E-15 condensation.Feed liquid in storage tank V-4 (ethanol content is more than 94.8%) is by transferpump P-3, and the tower top that its part is sent to Second distillation column T-5 after metering is as backflow, and another part is transported to the 3rd rectifying tower T-6 after metering as charging.The shortage of heat part of the 3rd rectifying tower T-6 is passed through reboiler E-12B by air source heat pump system E-13 heat make-up.
The 3rd rectifying tower T-6 theoretical plate number is 120,1.6 meters of tower diameters, and working pressure is 0.05 normal atmosphere, and tower top temperature is 19.6 ℃, and the temperature of tower bottom reboiler E-12 is 32.5 ℃.But the dehydrated alcohol that the 3rd rectifying tower T-6 tower top extraction 1111.2 kg/hr concentration are 99.8%wt, in bottom product, ethanol content is lower than 0.011%wt.
Embodiment 3: the rectification under vacuum method is produced 12000 ton/years of dehydrated alcohols
Operating method is as embodiment 1.To after being preheated to 45 ℃, interchanger E-6 enter the first rectifying tower T-4 containing the bio-ethanol of ethanol 25.2%, the theoretical plate number of the first rectifying tower T-4 tower is 35, tower diameter is 1.2 meters, adopt regular packing without wall flow in tower, working pressure is 0.33 normal atmosphere, it is 70.1 ℃ that reflux ratio is selected 1.2, the first rectifying tower T-4 bottom liquid temperature.Adopt the air source heat pump system E13 that a hot water temperature is 83 ℃ to provide thermal source for the first rectifying tower T-4 tower bottom reboiler.After distillation, the content of the alcohol mixture ethanol of the first rectifying tower T-4 tower top reaches 91.2%.The condensation rear section is as backflow, and part is sent to Second distillation column T-5 by pipeline 19 and carries out rectifying.
Second distillation column T-5 theoretical plate number is 40,1.3 meters of tower diameters, working pressure is 0.2 normal atmosphere, reflux ratio selects 1.05, the temperature of tower bottom reboiler E-11 is about 55 ℃, the heating medium of tower bottom reboiler E-11A is the discharging (aqueous solution, temperature is 70.1 ℃) of the first rectifying tower T-4 tower reactor, and the heating medium of tower bottom reboiler E-11B is the hot water that air source heat pump system E13 provides.Second distillation column T-5 top can obtain the alcohol vapour more than 95.3%, this steam is introduced in the 3rd rectifying tower T-6 tower bottom reboiler E-12A shell as heat source, condensed feed liquid enters storage tank V-4, and the steam be not condensed rises to the further condensation of interchanger E-15 by tower bottom reboiler E-12A upper pipe.2 ℃ of icy salt solutions that the refrigerant of interchanger E-15 provides for refrigeration system R-1.Also drop to storage tank V-4 by the liquid phase obtained after interchanger E-15 condensation.Feed liquid in storage tank V-4 (ethanol content is more than 95.3%) is by transferpump P-3, and the tower top that its part is sent to Second distillation column T-5 after metering is as backflow, and another part is transported to the 3rd rectifying tower T-6 after metering as charging.The shortage of heat part of the 3rd rectifying tower T-6 is passed through tower bottom reboiler E-12B by air source heat pump system E-13 heat make-up.
The 3rd rectifying tower T-6 theoretical plate number is 120,1.6 meters of tower diameters, and working pressure is 0.053 normal atmosphere, and tower top temperature is 20.5 ℃, and the temperature of tower bottom reboiler E-12 is 33.1 ℃.But the dehydrated alcohol that T-6 tower top extraction 1501.7 kg/hr concentration are 99.6%wt, in bottom product, ethanol content is lower than 0.009%wt.
Claims (6)
1. a technique of being produced dehydrated alcohol by the bio-ethanol aqueous solution, is characterized in that it comprises the following steps:
Step 1. from raw material feed liquid storage tank (V-2) will ferment the bio-ethanol containing ethanol 15-25% that obtains for feed liquid pump (P-2) be transported to interchanger (E-6 and E-8) heat exchange to 40-55 ℃, the mixed liquor of discharging feed liquid at the bottom of discharging feed liquid and Second distillation column (T-5) tower at the bottom of the tower that heating medium is the first rectifying tower (T-4) after the first rectifying tower (T-4) overhead vapours and heating Second distillation column (T-5) tower bottom reboiler (E-11), then the bio-ethanol feed liquid being transported to the first rectifying tower (T-4) by pipeline (15) is separated, the operation absolute pressure of the first rectifying tower (T-4) is 0.3-0.35 normal atmosphere, tower top temperature is 50-55 ℃, the temperature of the first rectifying tower (T-4) tower bottom reboiler (E-10) is 65-72 ℃, and can provide the air source heat pump system (E-13) of hot water more than 80 ℃ to heat the first rectifying tower (T-4) tower bottom reboiler (E-10) by one,
Step 2. is after the first rectifying tower (T-4) distillation, in the alcohol mixed solution of tower top, ethanol content reaches 80-90%, its part is refluxed by pipeline (18), part enters into Second distillation column (T-5) by pipeline (19) and carries out rectifying, the operation absolute pressure of Second distillation column (T-5) is 0.15-0.25 normal atmosphere, reflux ratio is selected 0.8-1.2, tower top temperature is 40-45 ℃, the temperature of Second distillation column (T-5) tower bottom reboiler (E-11) is 50-55 ℃, Second distillation column (T-5) tower bottom reboiler (E-11) is mainly heated by the discharging of the first rectifying tower (T-4) tower reactor, the shortage of heat part is provided by air source heat pump system (E-13), can obtain purity from Second distillation column (T-5) top is the aqueous ethanolic solution more than 95%, it will be as the charging of the 3rd rectifying tower (T-6),
The tower bottom reboiler (E-12) that the alcohol vapour that step 3. Second distillation column (T-5) tower top is 40-45 ℃ enters the 3rd rectifying tower (T-6) by pipeline (20) is heated the feed liquid in tower bottom reboiler (E-12) as thermal source, Partial Liquid Phase after the alcohol vapour condensation is delivered to Second distillation column (T-5) tower top as backflow by reflux pump (P-5) after metering, the rest part liquid phase is admitted in the 3rd rectifying tower (T-6) carries out high vacuum rectification, the operation absolute pressure of the 3rd rectifying tower (T-6) is 0.03-0.05 normal atmosphere, reflux ratio is 1-3, the tower top vapor phase temperature is 12-20 ℃, at the bottom of tower, liquidus temperature is 25-32 ℃, the insufficient section of the 3rd rectifying tower (T-6) tower bottom reboiler (E-12) heat is provided by air source heat pump system (E-13), the dehydrated alcohol that rectifying tower (T-6) tower top can continuously extraction mass concentration is 99.5-99.9%.
2. the technique of producing dehydrated alcohol according to claim 1, it is characterized in that: the described Second distillation column of step 2 (T-5) arranges two tower bottom reboilers of A/B (E-11) in case of necessity.
3. the technique of producing dehydrated alcohol according to claim 1, it is characterized in that: described the 3rd rectifying tower (T-6) of step 3 arranges two tower bottom reboilers of A/B (E-12) in case of necessity.
4. the technique of producing dehydrated alcohol according to claim 1, it is characterized in that: the reflux ratio of described the 3rd rectifying tower (T-6) of step 3 is 1-3.
5. the technique of producing dehydrated alcohol according to claim 1, it is characterized in that: the negative pressure of described the first rectifying tower (T-4), Second distillation column (T-5) and the 3rd rectifying tower (T-6) is by three vacuum systems (VS-1, VS-2 and VS-3), to be provided respectively, before vacuum system, all need to be equipped with vacuum buffer device, to maintain the stable of pressure.
6. the arbitrary described technique of producing dehydrated alcohol according to claim 1 to 5, it is characterized in that: in step 3, because the 3rd rectifying tower (T-6) overhead product steam is 12-20 ℃, so the chilled brine of 0-5 ℃ provided by refrigeration system (R-1) as refrigerant with condensation tower top vapour phase, while is in the exit of three vacuum systems (VS-1, VS-2 and VS-3), the cold-trap device that interchanger (E-14) and cold-trap (V-6) form is set, as the organism that will not yet be condensed in vacuum outlet gas again deep cooling trap among cold-trap (V-6).
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| CN101225017A (en) * | 2008-01-24 | 2008-07-23 | 复旦大学 | Method and device for producing fuel alcohol by fermentation liquor distillation-free whole molecular sieve adsorptive separation |
| CN101891590A (en) * | 2010-08-05 | 2010-11-24 | 湖南农业大学 | Method for producing anhydrous ethanol from fermentation liquid by gas adsorption |
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