CN114685246B - System and method for co-production of fuel ethanol and alcohol - Google Patents
System and method for co-production of fuel ethanol and alcohol Download PDFInfo
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- CN114685246B CN114685246B CN202011595725.1A CN202011595725A CN114685246B CN 114685246 B CN114685246 B CN 114685246B CN 202011595725 A CN202011595725 A CN 202011595725A CN 114685246 B CN114685246 B CN 114685246B
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- 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
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- 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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/542—Adsorption of impurities during preparation or upgrading of a fuel
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention relates to the field of ethanol production, and discloses a system and a method for co-producing fuel ethanol and alcohol, wherein the system adopts a three-tower process, and a distillation main device comprises a crude distillation tower, a primary distillation tower and a secondary distillation tower. The refining tower is a pressurizing tower, from which the alcohol of the wine is extracted; the second rectifying tower is an atmospheric tower and is used for obtaining fuel alcohol. Compared with the traditional seven-tower process, the system process is simple, the equipment is few, the ethanol yield is high, the energy consumption is reduced by more than 20%, the equipment investment is reduced by about 30%, the production cost is greatly reduced, and the obtained ethanol product meets the related ethanol standard.
Description
Technical Field
The invention relates to the field of ethanol production, in particular to a system and a method for co-producing fuel ethanol and alcohol.
Background
As the key point of renewable fuel, the development of fuel ethanol is significant in adjusting the energy structure of China, developing petroleum alternative resources, improving the proportion of clean fuel, improving the automobile exhaust emission and the atmospheric environment quality, developing low-carbon economy, promoting virtuous circle and sustainable development of agricultural production and consumption, and realizing agricultural efficiency and income increase of farmers. In the process for producing fuel ethanol by taking corn starch as a raw material, a starch raw material liquefying section, a fermenting section, a distillation dehydration section and a waste mash treatment section are generally included, wherein the distillation dehydration section is the source with the largest energy consumption (up to 45%).
In the distillation section of the common alcohol and fuel alcohol co-production project, a 7-tower differential pressure distillation process is adopted: the distillation main device comprises a negative pressure tower, a medium pressure tower, a high pressure tower, a water washing tower, a methanol tower, an industrial wine tower and a recovery tower. The process adopts a thermal coupling process, and because the water washing tower is arranged, the dilute wine of the negative pressure tower is diluted by the water washing tower, the dilute wine is diluted from 40-50% of ethanol concentration to 10-15% of ethanol concentration, and then enters the high pressure tower for rectification to produce plain wine, so that the energy consumption of fresh steam is high; the methanol tower is arranged, the steam stripping at the top of the water washing tower is used as a heat source for the methanol tower, the heat required by the methanol tower is large, the water washing tower is not in the optimal process condition in order to meet the requirement of methanol, and the tower bottom of the methanol tower is used for producing common wine; the arrangement of the industrial wine tower and the recovery tower has the problems of long flow, complex process, high investment and the like.
Disclosure of Invention
The invention aims to solve the problems of complex process and high energy consumption in a distillation section of a fuel ethanol and alcohol ethanol co-production project, and provides a system and a method for co-production of fuel ethanol and alcohol ethanol.
To achieve the above object, in one aspect, the present invention provides a system for co-producing fuel ethanol and privately alcohol, the system comprising: a crude distillation column, a primary rectifying column, a secondary rectifying column and a molecular sieve adsorption and desorption column;
the external part of the crude distillation column is provided with a crude distillation column top gas outlet, a crude distillation column reflux port, a crude distillation column feed inlet, a light wine extraction outlet, a crude distillation column bottom liquid extraction outlet and a crude distillation column reboiler from top to bottom, wherein the crude distillation column feed inlet is connected with a first heat exchange device and is used for preheating fermented mature mash and conveying the preheated fermented mature mash into the crude distillation column; the top gas outlet of the crude distillation column is sequentially connected with the second heat exchange device and the reflux port of the crude distillation column; the light wine extraction outlet is connected with a first feed inlet of the second rectifying tower, and the crude distillation tower bottom liquid extraction outlet is sequentially connected with a third heat exchange device and a second feed inlet of the second rectifying tower;
the outer part of the second rectifying tower is provided with a second rectifying tower top gas outlet, a second rectifying tower top liquid extraction outlet, a second rectifying tower reflux inlet, a first feed inlet, a second rectifying tower kettle liquid extraction outlet, a second feed inlet and a second rectifying tower reboiler from top to bottom, wherein one path of the second rectifying tower top gas outlet is connected with a raw material wine steam heater and a molecular sieve adsorption and desorption tower in sequence; one path of a tower top gas outlet of the second rectifying tower is sequentially connected with a crude rectifying tower reboiler and a reflux port of the second rectifying tower, a tower top liquid extraction outlet of the second rectifying tower is connected with a reflux port of the first rectifying tower, and a tower bottom liquid extraction outlet of the second rectifying tower is sequentially connected with a fourth heat exchange device and a feeding port of the first rectifying tower;
the outer part of the rectifying tower is provided with a rectifying tower top gas outlet, a rectifying tower reflux port, an edible alcohol extraction port, a fusel oil extraction port, a rectifying tower feed port and a rectifying tower reboiler from top to bottom, wherein the fusel oil extraction port is connected with a fuel alcohol tank, and the edible alcohol extraction port is connected with a plain alcohol tank;
the molecular sieve adsorption and desorption tower is provided with a back flush gas phase outlet, a finished product wine gas outlet, a liquid phase outlet and a gas phase inlet from top to bottom, and the gas phase inlet is sequentially connected with a raw material wine gas heater and a top gas outlet of the secondary rectifying tower; one path of the finished product wine gas outlet is connected with the back flushing gas phase outlet, and the other path of the finished product wine gas outlet is connected with the fuel ethanol storage tank; the liquid phase outlet is connected with the light wine tank and the reflux port of the crude distillation column in sequence.
In a second aspect the invention provides a method for co-producing fuel ethanol and privately usable ethanol using a system as described above, the method comprising:
(1) In a crude distillation column, carrying out crude distillation treatment on preheated fermented mature mash to obtain crude distillation column top gas, light wine and crude distillation column bottom liquid; performing first condensation treatment on the top gas of the crude distillation column to obtain crude distillation column condensate, wherein the crude distillation column condensate is refluxed and subjected to crude distillation treatment;
(2) Rectifying the light wine and the tower bottom liquid of the crude distillation tower after the first heat exchange treatment in a secondary rectifying tower at normal pressure to obtain secondary rectifying tower top gas, secondary rectifying tower top liquid and secondary rectifying tower bottom liquid; performing second condensation on part of the tower top gas of the second rectifying tower to obtain condensate of the second rectifying tower, and performing normal pressure rectification on condensate reflux of the second rectifying tower;
(3) In a first rectifying tower, pressurizing and rectifying tower top liquid of the second rectifying tower and tower bottom liquid of the second rectifying tower after the second heat exchange treatment to obtain alcohol and fusel oil;
(4) And in the molecular sieve adsorption and desorption tower, dehydrating the rest of the tower top gas of the second rectifying tower after the third heat exchange to obtain fuel ethanol.
The system of the invention has the advantages that the light wine directly enters the second rectifying tower to strip impurities in the light wine, the second rectifying tower laterally extracts the light wine and then enters the first rectifying tower, the first rectifying tower laterally extracts the common alcohol, the second rectifying tower produces the fuel alcohol, and the main distillation device in the whole process is 3 towers (namely the crude rectifying tower, the first rectifying tower and the second rectifying tower), so that the process is simple and the energy and material consumption is low.
Compared with fuel ethanol, the edible wine has the characteristics of oxidation time requirement, high impurity requirement and high ethanol purity requirement. Aiming at different product requirements of edible general wine and fuel ethanol, in the process of co-producing the fuel ethanol and the general wine in a 3-tower process, the light wine in a crude distillation tower directly enters a secondary distillation tower through the adjustment and optimization of the process flow, and aldehydes in the light wine are removed through the stripping action of the tower, so that components affecting the oxidation time are mainly discharged from the top of the crude distillation tower and the top of the secondary distillation tower or enter fuel ethanol products, and the fuel ethanol products can be mixed after fusel oil containing n-propanol and the like is extracted, and the impurities enter the fuel ethanol products, but meet the product requirements of the fuel ethanol; and (3) carrying out process adjustment on the side line of a rectifying tower to obtain the plain wine, thereby meeting the requirements of plain wine products.
Drawings
FIG. 1 is a flow chart of a system for co-production of fuel ethanol and privately-used alcohol according to the present invention.
Fig. 2 is a flow chart of a seven-tower system for co-production of conventional fuel ethanol and privately-distilled ethanol.
Description of the reference numerals
1. A first mash preheater; 2. a second mash preheater; 3. a crude distillation column; 4. a first condenser of the crude distillation column; 5. a second condenser of the crude distillation column; 6. a first mash heat exchanger; 7. a second mash heat exchanger; 8. a crude distillation column reboiler; 9. a second rectifying tower; 10. a second rectifying tower reboiler; 11. a third mash heat exchanger; 12. a fourth mash heat exchanger; 13. a rectifying tower; 14. a raw material wine steam heater; 15. a rectifying tower reboiler; 16. molecular sieve adsorption and desorption towers; 17. a regenerated wine steam superheater; 18. a light wine tank;
t1', a crude distillation column; t2', a combined tower; t3', rectifying tower; t4', methanol column; t5', industrial alcohol tower; t6', recovery tower; t7' water scrubber.
Detailed Description
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
In the invention, the product quality of the common grade edible alcohol accords with the common grade edible alcohol standard in edible alcohol national standard GB/T10343-2008; the quality of the fuel ethanol product accords with the national fuel ethanol standard GB18350-2001.
In one aspect, the present invention provides a system for co-production of fuel ethanol and privately-used alcohol, the system comprising: a crude distillation column 3, a primary rectifying column 13, a secondary rectifying column 9 and a molecular sieve adsorption and desorption column 16;
the outer part of the crude distillation column 3 is provided with a crude distillation column top gas outlet, a crude distillation column reflux port, a crude distillation column feed inlet, a light wine extraction outlet, a crude distillation column bottom liquid extraction outlet and a crude distillation column reboiler 8 from top to bottom, wherein the crude distillation column feed inlet is connected with a first heat exchange device and is used for preheating fermented mature mash and conveying the preheated fermented mature mash into the crude distillation column 3; the top gas outlet of the crude distillation column is sequentially connected with the second heat exchange device and the reflux port of the crude distillation column; the light wine extraction outlet is connected with a first feed inlet of the second rectifying tower, and the crude distillation tower bottom liquid extraction outlet is sequentially connected with a third heat exchange device and a second feed inlet of the second rectifying tower;
the outer part of the second rectifying tower 9 is provided with a second rectifying tower top gas outlet, a second rectifying tower top liquid outlet, a second rectifying tower reflux inlet, a first feed inlet, a second rectifying tower bottom liquid outlet, a second feed inlet and a second rectifying tower reboiler 10 from top to bottom, wherein one path of the second rectifying tower top gas outlet is sequentially connected with a raw material wine steam heater 14 and a molecular sieve adsorption and desorption tower 16; one path of gas outlet at the top of the second rectifying tower is sequentially connected with the reboiler 8 of the crude rectifying tower and the reflux port of the second rectifying tower, liquid outlet at the top of the second rectifying tower is connected with the reflux port of the first rectifying tower, and liquid outlet at the bottom of the second rectifying tower is sequentially connected with the fourth heat exchange device and the feed port of the first rectifying tower;
the outer part of the rectifying tower 13 is provided with a rectifying tower top gas outlet, a rectifying tower reflux port, an edible alcohol extraction port, a fusel oil extraction port, a rectifying tower feed port and a rectifying tower reboiler 15 from top to bottom, wherein the fusel oil extraction port is connected with a fuel alcohol tank, and the edible alcohol extraction port is connected with a general alcohol tank;
the molecular sieve adsorption and desorption tower 16 is provided with a back flushing gas phase outlet, a finished product wine gas outlet, a liquid phase outlet and a gas phase inlet from top to bottom, and the gas phase inlet is sequentially connected with the raw material wine gas heater 14 and a top gas outlet of the two-rectifying tower; one path of the finished product wine gas outlet is connected with the back flushing gas phase outlet, and the other path of the finished product wine gas outlet is connected with the fuel ethanol storage tank; the liquid phase outlet is connected with the light wine tank 18 and the reflux port of the crude distillation column in sequence.
In the present invention, the system employs a three column process, and the distillation main unit includes a crude distillation column, a primary distillation column and a secondary distillation column, wherein the equipment used is equipment conventionally used in the art, and is commercially available. The locations of the various outlets and inlets of the crude, primary and secondary columns are well known in the art.
In the present invention, the system for preparing a fermented beer may be a system conventional in the art, and in a preferred embodiment of the present invention, the system for preparing a fermented beer is a system for preparing a fermented beer from a starchy material, the system comprising:
the crushing unit is used for crushing the starchy raw material to obtain a crushed starchy raw material product;
the pulp mixing unit is used for mixing the crushed product of the starchiness raw material to obtain starch pulp;
the liquefaction unit is used for carrying out enzymolysis on the starch slurry to obtain liquefied liquid;
and the fermentation unit is used for fermenting the liquefied liquid to obtain fermented mature mash.
The specific manner and conditions of operation of each unit are common general knowledge in the art and will not be described in detail herein.
In the invention, the waste liquid at the tower bottom of the crude distillation tower is discharged from the bottom of the crude distillation tower, the discharged waste liquid at the tower bottom can be separated by a separation unit to obtain byproducts (such as DDGS) and separated waste liquid, and the separated waste liquid can be conveyed to a sewage treatment unit for treatment.
Preferably, the first heat exchange means comprises a first mash preheater 1 and a second mash preheater 2.
Preferably, the second heat exchange means comprises a crude distillation column first condenser 4 and a crude distillation column second condenser 5.
Preferably, the first mash preheater 1 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; the mash outlet is connected with a mash inlet of the second mash preheater 2, the hot end inlet is connected with a top gas outlet of the crude distillation column, the hot end outlet comprises a gas phase outlet and a liquid phase outlet, the gas phase outlet is sequentially connected with a first condenser 4 of the crude distillation column and a second condenser 5 of the crude distillation column, and the liquid phase outlet of the first mash preheater 1, the liquid phase outlet of the first condenser 4 of the crude distillation column and the liquid phase outlet of the second condenser 5 of the crude distillation column are respectively connected with a reflux port of the crude distillation column through pipelines; the second condenser 5 of the crude distillation column is provided with a gas phase outlet for discharging non-condensed steam.
Preferably, the second mash preheater 2 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash outlet is connected with the feed inlet of the crude distillation column, the hot end inlet is connected with the outlet of the finished product alcohol gas of the molecular sieve adsorption and desorption column, and the hot end outlet is connected with the fuel alcohol tank.
Preferably, the system further comprises a finished product aftercooler, and the hot end outlet of the second mash preheater 2, the finished product aftercooler and the fuel alcohol tank are connected in sequence. The finished product wine vapor from the molecular sieve adsorption and desorption tower is subjected to heat exchange condensation through a second mash preheater 2, and the uncondensed wine vapor is further condensed through a finished product aftercooler and then is conveyed into a fuel alcohol tank.
Preferably, the third heat exchange means comprises a first mash heat exchanger 6 and a second mash heat exchanger 7.
Preferably, the first mash heat exchanger 6 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with the liquid extraction outlet of the tower bottom of the crude distillation tower, the mash outlet is connected with the second feeding port of the second rectifying tower 9, and the hot end inlet is connected with the hot end outlet of the fourth mash heat exchanger 12.
Preferably, the warm end outlet of the first mash heat exchanger 6 is connected with the size mixing unit.
Preferably, the second mash heat exchanger 7 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with the liquid extraction outlet of the tower bottom of the crude distillation tower, the mash outlet is connected with the second feeding port of the secondary rectifying tower 9, and the hot end inlet is connected with the outlet of the secondary rectifying tower reboiler 10.
Preferably, the hot end outlet of the second mash heat exchanger 7 is connected to a separation unit. The separation unit is used to separate, for example, crude distillation column waste mash to obtain DDGS.
Preferably, the fourth heat exchange means comprises a third mash heat exchanger 11 and a fourth mash heat exchanger 12.
Preferably, the third mash heat exchanger 11 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with a tower bottom liquid side extraction outlet of the second rectifying tower 9, and the mash outlet is connected with a rectifying tower feed inlet.
Preferably, the warm end inlet of the third mash heat exchanger 11 is connected to the bottom outlet of a rectifying tower 13.
Preferably, the warm end outlet of the third mash heat exchanger 11 is connected with the size mixing unit.
Preferably, the fourth mash heat exchanger 12 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with a tower bottom liquid side extraction outlet of the second rectifying tower 9, the mash outlet is connected with a rectifying tower feed inlet, and the hot end inlet is connected with a hot end outlet of a rectifying tower reboiler 15.
Preferably, the crude distillation column reboiler 8 is provided with a hot end inlet and a hot end outlet, the hot end inlet is connected with a top gas outlet of the secondary rectifying column, and the hot end outlet is connected with a reflux port of the secondary rectifying column.
Preferably, the two rectifying towers reboiler 10 is provided with a hot end inlet and a hot end outlet, the hot end inlet is connected with a rectifying tower top gas outlet, and the hot end outlet is connected with a rectifying tower reflux port.
Preferably, a rectifying tower reboiler 15 is provided with a hot end inlet and a hot end outlet, the hot end inlet is connected with the steam source outlet, and the hot end outlet is connected with the fourth heat exchange device.
The first rectifying tower reboiler is heated by using external steam, and the source of the external steam can be a steam generator conventional in the field, and the fresh steam is preferably 0.7-0.9MPa.
In the invention, the system can also comprise a regenerated wine steam superheater 17, and one path of a finished wine steam outlet is sequentially connected with the regenerated wine steam superheater 17 and a back flushing gas phase outlet.
A second aspect of the present invention is a method for co-producing fuel ethanol and praline ethanol using the system described above, the method comprising:
(1) In a crude distillation column 3, carrying out crude distillation treatment on the preheated fermented mature mash to obtain crude distillation column top gas, light wine and crude distillation column bottom liquid; performing first condensation treatment on the top gas of the crude distillation column to obtain crude distillation column condensate, wherein the crude distillation column condensate is refluxed and subjected to crude distillation treatment;
(2) In a secondary rectifying tower 9, rectifying the light wine and the tower bottom liquid of the crude rectifying tower after the first heat exchange treatment at normal pressure to obtain secondary rectifying tower top gas, secondary rectifying tower top liquid and secondary rectifying tower bottom liquid; performing second condensation on part of the tower top gas of the second rectifying tower to obtain condensate of the second rectifying tower, and performing normal pressure rectification on condensate reflux of the second rectifying tower;
(3) In a rectifying tower 13, pressurizing and rectifying tower top liquid of the rectifying tower and tower bottom liquid of the rectifying tower after the second heat exchange treatment to obtain alcohol and fusel oil;
(4) In the molecular sieve adsorption and desorption tower 16, the rest of the tower top gas of the second rectifying tower after the third heat exchange is dehydrated to obtain fuel ethanol.
In the present invention, the fermented beer can be prepared by methods conventional in the art, such as sequentially pulverizing, slurrying, liquefying, and fermenting the starchy material to obtain the fermented beer.
In the present invention, the ethanol content in the fermented beer can be selected within a wide range, preferably 13-17 vol%.
The fermented mature mash is preheated by a first heat exchange device so as to facilitate the rough distillation process. Preferably, the temperature of the pre-heat treated fermented beer is 63-88 ℃.
Preferably, the first mash preheater is preheated to 45-55deg.C and the second mash preheater is preheated to 63-88deg.C.
The crude distillation column is operated at a negative pressure, preferably, in step (1), the conditions of the crude distillation include: the temperature of the tower kettle is 65-85 ℃; the pressure of the tower kettle is between-0.06 and-0.03 MPa; the temperature of the tower top is 40-60 ℃; the pressure at the top of the tower is-0.05 to-0.08 MPa; the reflux ratio is 0.5-5.
In the present invention, the reflux ratio means a ratio of the amount of the extracted material to the amount of the material returned to the column.
And discharging the waste liquid from the tower bottom of the crude distillation tower, wherein the ethanol content in the waste liquid is preferably less than 0.04 wt%, and conveying the waste liquid to a post-treatment unit for post-treatment, such as separating to obtain DDGS byproducts.
And (3) carrying out first condensation treatment on the top gas of the crude distillation column to obtain crude distillation column condensate, wherein the condition of the first condensation treatment is that the temperature of the crude distillation column condensate is 40-50 ℃.
In the invention, in the step (2), the condition of the first heat exchange treatment is that the temperature of the tower bottom liquid of the crude distillation tower after the first heat exchange treatment is 65-85 ℃.
Preferably, in the step (2), the conditions of the atmospheric rectification include: the temperature of the tower kettle is 105-125 ℃; the pressure of the tower kettle is 0.07 to 0.3MPa; the temperature of the tower top is 85-98 ℃; the pressure at the top of the tower is 0.05 to 0.2MPa; the reflux ratio is 0.5-8.
And (3) performing second condensation on part of the tower top gas of the second rectifying tower to obtain second rectifying tower condensate, and performing normal pressure rectification on reflux of the second rectifying tower condensate, wherein the condition of the second condensation treatment is preferably that the temperature of the second rectifying tower condensate is 60-80 ℃.
And heating the second tower top gas to a required temperature by a raw material wine heater, and dehydrating by a molecular sieve adsorption and desorption tower from bottom to top. And (3) adsorbing in the tower A of the molecular sieve adsorption tower and regenerating in the tower B. The material enters A, and the alcohol gas after adsorption is extracted from a finished alcohol gas outlet to obtain fuel ethanol; and part of the adsorbed wine gas enters a regenerated wine gas superheater, the overheated wine gas enters the tower B from a backwashing gas phase outlet, and the obtained light wine liquid enters a light wine tank from a liquid phase outlet. The tower A and the tower B are used in a switching way.
After the dehydrated alcohol vapor is used as a heat source to exchange heat and condense with the second mash preheater, the uncondensed alcohol vapor preferably enters a finished product aftercooler to be further condensed, and the obtained condensate is preferably further cooled by an absolute ethyl alcohol cooler and enters a fuel alcohol tank.
Preferably, in step (3), the conditions of the pressure rectification include: the temperature of the tower kettle is 140-170 ℃; the pressure of the tower kettle is 0.4 to 0.8MPa; the temperature of the tower top is 110-140 ℃; the pressure at the top of the tower is 0.2 to 0.4MPa; the reflux ratio is 1-5.
In the present invention, preferably, in the step (3), the condition of the second heat exchange treatment is such that the temperature of the second rectifying tower bottom liquid after the second heat exchange treatment is 105-125 ℃.
The extraction temperature of the privet ethanol is conventional in the art, and preferably, the extraction temperature of the privet ethanol is 115-120 ℃.
The amount of ethanol recovered from the wine varies depending on the scale of production of ethanol, and is preferably 50% by volume or less based on the amount of ethanol fed to the fermented beer.
The fusel oil is produced at a temperature conventional in the art, preferably 130-160 ℃.
The amount of fusel oil withdrawn varies depending on the scale of production of ethanol, and is preferably 0.5 to 3% by volume based on the amount of ethanol fed to the fermented beer.
In the present invention, preferably, in the step (4), the condition of the third heat exchange treatment is that the temperature of the top gas of the remaining second rectifying tower after the third heat exchange is 60-80 ℃.
Preferably, in step (4), the conditions for dehydration include: the adsorption pressure is 0 to 0.5MPa; the desorption pressure is-0.05 to-0.09 MPa.
In the present invention, the pressures are gauge pressures.
It will be appreciated that in order to save energy and steam consumption, in addition to circulating the heat-containing material through the pipeline according to the first aspect, the person skilled in the art may also perform multiple heat exchanges on the heat-containing material or transfer it to other units than the co-production system according to the present invention, such as a pulp mixing unit in an ethanol fermentation production system, etc., as required, to reduce heat energy losses.
The present invention will be described in detail by examples.
In the following examples and comparative examples, reagents used were commercially available unless otherwise specified.
The steam consumption and the energy consumption were calculated as the weight of steam and the energy consumption, respectively, consumed per 1t of ethanol produced (in ethanol concentration of 99.5%).
A steam generator is adopted to generate fresh steam of 0.80MPaG, and a heat source is provided for a reboiler of the first rectifying tower, a raw material wine steam heater and a regenerated wine steam superheater.
In the following examples, the fuel ethanol scale was 16 ten thousand tons and the food grade wine co-production scale was 9 ten thousand tons/year.
Preparation example 1
This preparation example is used to illustrate the process of preparing a fermented beer from corn starch.
The system for preparing the fermented mature mash by using the corn starch comprises a crushing unit, a crushing unit and a processing unit, wherein the crushing unit is used for crushing the starchy raw material to obtain a starchy raw material crushed product;
the pulp mixing unit is used for mixing the crushed product of the starchiness raw material to obtain starch pulp;
the liquefaction unit is used for carrying out enzymolysis on the starch slurry to obtain liquefied liquid;
the fermentation unit is used for fermenting the liquefied liquid to obtain fermented mature mash;
an activation unit for activating the strain.
The specific operation is as follows:
(1) Crushing and size mixing
In the pulverizing unit, corn is pulverized to obtain corn flour, wherein the average particle size of the corn flour is 20 meshes. In the size mixing unit, the sieved corn flour is sent to a size mixing tank to be mixed with size mixing water for size mixing, so as to obtain starch size, the size mixing temperature is 80 ℃, and the amount of size mixing water is such that the solid content in the obtained corn size is 30 wt%.
(2) Liquefaction process
Uniformly mixing the corn steep liquor obtained in the step (1) with alpha-amylase (high temperature resistant alpha-amylase, purchased from Jewelry company) in a liquefaction unit, and liquefying to obtain liquefied liquid; wherein the alpha-amylase is used in an amount of 20U/g dry basis starchy material relative to 1 g corn flour under liquefaction conditions of: the temperature of liquefaction was 90 ℃, the time of liquefaction was 90 minutes, and the pH of liquefaction was 5.6.
(3) Fermentation and distillation
Saccharomyces cerevisiae (Angel super high activity dry yeast, hubei Angel Yeast Co.) is added into a spreading unit, and mixed with water for activation for 10 hr at pH of 4.2 and activation temperature of 32deg.C.
Delivering the liquefied liquid and activated Saccharomyces cerevisiae to a fermentation unit for fermentation, wherein the inoculation amount of the Saccharomyces cerevisiae is 10 relative to 1 g of the liquefied liquid 5 cfu, and carrying out stirring culture, wherein the fermentation conditions are as follows: the fermentation temperature is 32 ℃, the pH is 4.2, the fermentation time is 65 hours, and the fermented mature mash is obtained, and the ethanol concentration is 15-16 vol%.
Example 1
This example is presented to illustrate the system and method of co-production of fuel ethanol and praline ethanol of the present invention.
The fermented beer prepared in preparation example 1 was used as a raw material for co-production of fuel ethanol and praline ethanol, and was operated in the system described below (flow chart see fig. 1) in the manner described below to co-produce fuel ethanol and praline ethanol.
(1) The system mainly comprises a crude distillation column 3, a primary rectifying column 13, a secondary rectifying column 9 and a molecular sieve adsorption and desorption column 16.
The outer part of the crude distillation column 3 is provided with a crude distillation column top gas outlet, a crude distillation column reflux port, a crude distillation column feed inlet, a light wine extraction outlet, a crude distillation column bottom liquid extraction outlet and a crude distillation column reboiler 8 from top to bottom, wherein the crude distillation column feed inlet is connected with a first heat exchange device and is used for preheating fermented mature mash and conveying the preheated fermented mature mash into the crude distillation column 3; the top gas outlet of the crude distillation column is sequentially connected with the second heat exchange device and the reflux port of the crude distillation column; the light wine extraction outlet is connected with the first feed inlet of the second rectifying tower, and the crude distillation tower bottom liquid extraction outlet is sequentially connected with the third heat exchange device and the second feed inlet of the second rectifying tower.
The outer part of the second rectifying tower 9 is provided with a second rectifying tower top gas outlet, a second rectifying tower top liquid outlet, a second rectifying tower reflux inlet, a first feed inlet, a second rectifying tower bottom liquid outlet, a second feed inlet and a second rectifying tower reboiler 10 from top to bottom, wherein one path of the second rectifying tower top gas outlet is sequentially connected with a raw material wine steam heater 14 and a molecular sieve adsorption and desorption tower 16; one path of gas outlet at the top of the second rectifying tower is sequentially connected with the reboiler 8 of the crude rectifying tower and the reflux port of the second rectifying tower, liquid outlet at the top of the second rectifying tower is sequentially connected with the reflux port of the first rectifying tower, and liquid outlet at the bottom of the second rectifying tower is sequentially connected with the fourth heat exchange device and the feed port of the first rectifying tower.
The outer top-down of a rectifying tower 13 is provided with a rectifying tower top gas outlet, a rectifying tower reflux port, an edible alcohol extraction port, a fusel oil extraction port, a rectifying tower feed inlet and a rectifying tower reboiler 15, wherein the fusel oil extraction port is connected with a fuel alcohol tank, and the edible alcohol extraction port is connected with a general alcohol tank.
The molecular sieve adsorption and desorption tower 16 is provided with a back flushing gas phase outlet, a finished product wine gas outlet, a liquid phase outlet and a gas phase inlet from top to bottom, and the gas phase inlet is sequentially connected with the raw material wine gas heater 14 and a top gas outlet of the two-rectifying tower; one path of the finished product wine steam outlet is sequentially connected with the regenerated wine steam superheater 17 and the back flush gas phase outlet, and one path of the finished product wine steam outlet is connected with the fuel ethanol storage tank; the liquid phase outlet is connected with the light wine tank 18 and the reflux port of the crude distillation column in sequence.
Wherein the first heat exchange device comprises a first mash preheater 1 and a second mash preheater 2, and the second heat exchange device comprises a first condenser 4 of the crude distillation column and a second condenser 5 of the crude distillation column.
The first mash preheater 1 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; the mash outlet is connected with a mash inlet of the second mash preheater 2, the hot end inlet is connected with a top gas outlet of the crude distillation column, the hot end outlet comprises a gas phase outlet and a liquid phase outlet, the gas phase outlet is sequentially connected with a first condenser 4 of the crude distillation column and a second condenser 5 of the crude distillation column, and the liquid phase outlet of the first mash preheater 1, the liquid phase outlet of the first condenser 4 of the crude distillation column and the liquid phase outlet of the second condenser 5 of the crude distillation column are respectively connected with a reflux port of the crude distillation column through pipelines; the second condenser 5 of the crude distillation column is provided with a gas phase outlet for discharging non-condensed steam.
The second mash preheater 2 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash outlet is connected with the feed inlet of the crude distillation column, the hot end inlet is connected with the outlet of the finished product alcohol gas of the molecular sieve adsorption and desorption column, and the hot end outlet is connected with the fuel alcohol tank.
The third heat exchange device comprises a first mash heat exchanger 6 and a second mash heat exchanger 7, wherein the first mash heat exchanger 6 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with the liquid extraction outlet of the tower bottom of the crude distillation tower, the mash outlet is connected with the second feed inlet of the second rectifying tower 9, the hot end inlet is connected with the hot end outlet of the fourth mash heat exchanger 12, and the hot end outlet is connected with the slurry mixing unit.
The second mash heat exchanger 7 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with the liquid extraction outlet of the tower bottom of the crude distillation tower, the mash outlet is connected with the second feed inlet of the second rectifying tower 9, the hot end inlet is connected with the outlet of the tower bottom of the reboiler 10 of the second rectifying tower, and the hot end outlet is connected with the separation unit.
The fourth heat exchange means comprises a third mash heat exchanger 11 and a fourth mash heat exchanger 12.
The third mash heat exchanger 11 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with a tower bottom liquid side extraction outlet of the second rectifying tower 9, the mash outlet is connected with a rectifying tower feed inlet, the hot end inlet is connected with a tower bottom outlet of the first rectifying tower 13, and the hot end outlet is connected with the pulp mixing unit.
The fourth mash heat exchanger 12 is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with a tower bottom liquid side extraction outlet of the second rectifying tower 9, the mash outlet is connected with a rectifying tower feed inlet, and the hot end inlet is connected with a hot end outlet of a rectifying tower reboiler 15.
The system also comprises a finished product aftercooler, and the hot end outlet of the second mash preheater 2, the finished product aftercooler and the fuel alcohol tank are connected in sequence. The finished product wine vapor from the molecular sieve adsorption and desorption tower is subjected to heat exchange condensation through a second mash preheater 2, and the uncondensed wine vapor is further condensed through a finished product aftercooler and then is conveyed into a fuel alcohol tank.
(2) Method for co-producing fuel ethanol and alcohol
The fermented mature mash with the flow rate of 190t/h is preheated to 45 ℃ by a first mash preheater, the second mash preheater is preheated to 65 ℃, and enters a crude distillation tower from an inlet at the middle upper part of the crude distillation tower to carry out crude distillation treatment, so as to obtain crude distillation tower top gas, light wine and crude distillation tower bottom liquid; condensing the top gas of the crude distillation column to obtain crude distillation column condensate at 45 ℃, wherein the crude distillation column condensate is refluxed and subjected to crude distillation. And discharging the waste liquid at the tower bottom of the crude distillation tower from the bottom of the crude distillation tower, wherein the ethanol content is less than 0.04 weight percent, and conveying the waste liquid to sewage treatment equipment.
Rectifying the light wine and the tower bottom liquid of the coarse distillation tower at 83 ℃ under normal pressure to obtain gas at the top of the secondary rectifying tower, tower top liquid of the secondary rectifying tower and tower bottom liquid of the secondary rectifying tower; heating part of the tower top gas of the second rectifying tower to about 125 ℃ through a raw material wine heater, and then conveying the tower top gas to a molecular sieve adsorption and desorption tower for dehydration treatment (the adsorption pressure is 0.05MPa and the desorption pressure is-0.06 MPa) to obtain fuel ethanol; condensing the rest part of the tower top gas of the secondary rectifying tower to obtain secondary rectifying tower condensate at 70 ℃, and rectifying the secondary rectifying tower condensate at normal pressure.
Pressurizing and rectifying tower top liquid of the second rectifying tower and tower bottom liquid of the second rectifying tower at 110 ℃, and laterally extracting the alcohol and fusel oil of the wine, wherein the extraction temperature of the alcohol of the wine is 128 ℃; the extraction temperature of the fusel oil was 133.8 ℃.
The operating conditions of the crude distillation column, the primary rectification column and the secondary rectification column are shown in Table 1.
TABLE 1
| Project | Crude distillation column | Two smart towers | Refining tower |
| Overhead pressure MPaG | -0.068 | 0.07 | 0.3 |
| Tower bottom pressure MPaG | -0.048 | 0.0935 | 0.445 |
| Temperature of the top of the tower at DEG C | 52.4 | 93.0 | 126.6 |
| Tower bottom temperature °c | 83.0 | 119.5 | 155.4 |
| Reflux ratio | 1 | 2.5 | 3 |
In the system, the fuel ethanol and the common alcohol are co-produced by the method (the product quality of the common edible alcohol accords with common edible alcohol standards in edible alcohol national standard GB/T10343-2008; the product quality of the fuel ethanol accords with fuel ethanol national standard GB 18350-2001), the yield of the obtained fuel ethanol is 16 ten thousand tons/year, the yield of the common alcohol is 9 ten thousand tons/year, and the yield is 99 percent.
The steam consumption is 1.7T/T ethanol (99.5%), the energy consumption is 6397MJ/T ethanol (general rule is calculated according to GB/T2589-2008 comprehensive energy consumption).
Example 2
The procedure of example 1 was followed except that the fermented beer was preheated to 43℃in sequence by the first beer preheater and to 63℃by the second beer preheater, and the operating conditions of the crude distillation column, the primary distillation column and the secondary distillation column were as shown in Table 2.
TABLE 2
In the system, the fuel ethanol and the common alcohol are co-produced by the method (the product quality of the common edible alcohol accords with the common edible alcohol standard in edible alcohol national standard GB/T10343-2008; the product quality of the fuel ethanol accords with the fuel ethanol national standard GB 18350-2001), and the yield of the obtained fuel ethanol and the common alcohol are basically consistent with those of the embodiment 1. The steam consumption is 1.8t/t of ethanol, and the energy consumption is 6733MJ/t of ethanol.
Example 3
The procedure of example 1 was followed except that the fermented beer was preheated to 50℃in sequence by the first beer preheater and to 88℃by the second beer preheater, and the operating conditions of the crude distillation column, the primary distillation column and the secondary distillation column were as shown in Table 3.
TABLE 3 Table 3
| Project | Crude distillation column | Two smart towers | Refining tower |
| Overhead pressure MPaG | -0.08 | 0.05 | 0.2 |
| Tower bottom pressure MPaG | -0.06 | 0.07 | 0.4 |
| Temperature of the top of the tower at DEG C | 40 | 85 | 110 |
| Tower bottom temperature °c | 65 | 105 | 140 |
| Reflux ratio | 5 | 8 | 5 |
In the system, the fuel ethanol and the common alcohol are co-produced by the method (the product quality of the common edible alcohol accords with the common edible alcohol standard in edible alcohol national standard GB/T10343-2008; the product quality of the fuel ethanol accords with the fuel ethanol national standard GB 18350-2001), and the yield of the obtained fuel ethanol and the common alcohol are basically consistent with those of the embodiment 1. The steam consumption is 1.6t/t ethanol, and the energy consumption is 6021MJ/t ethanol.
Comparative example 1
This comparative example is used to illustrate the conventional seven column process for co-production of fuel ethanol and privately owned ethanol.
The seven-tower process is used for co-producing the fuel ethanol and the alcohol, and the seven-tower system comprises a crude distillation tower T1', a combined tower T2', a water washing tower T7', a rectifying tower T3', a methanol tower T4', a recovery tower T6' and an industrial alcohol tower T5', wherein the connection mode and the material flow direction are shown in figure 2.
The specific operating parameters for each column are shown in tables 4 and 5.
TABLE 4 Table 4
| Project | Crude distillation column | Combined tower | Rectifying tower |
| The ethanol content of the tower kettle is wt% | <0.06 | <0.04 | <0.04 |
| Overhead pressure MPaG | -0.065 | 0.05 | 0.38 |
| Tower bottom pressure MPaG | -0.050 | 0.08 | 0.42 |
| Temperature of the top of the tower at DEG C | 50 | 95 | 130 |
| Tower bottom temperature °c | 80 | 120 | 156 |
| Reflux ratio | 1 | 3 | 4 |
TABLE 5
The yield of the prepared fuel ethanol is 16 ten thousand tons/year, the yield of the general wine ethanol is 8.7 ten thousand tons/year, the yield is 97 percent, and the byproduct is about 0.3 ten thousand tons/year of industrial wine.
The steam consumption was 2.35 tons of steam/t ethanol and the energy consumption was 8843MJ/t ethanol.
Compared with the traditional seven-tower process, the equipment investment of the system and the method is reduced by about 30 percent, and the energy consumption is reduced by more than 20 percent.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (12)
1. A method for co-production of fuel ethanol and privately owned ethanol, characterized in that the method is carried out in an apparatus comprising: a crude distillation column (3), a primary rectifying column (13), a secondary rectifying column (9) and a molecular sieve adsorption and desorption column (16);
the external part of the crude distillation column (3) is provided with a crude distillation column top gas outlet, a crude distillation column reflux port, a crude distillation column feed inlet, a light wine extraction outlet, a crude distillation column bottom liquid extraction outlet and a crude distillation column reboiler (8) from top to bottom, wherein the crude distillation column feed inlet is connected with a first heat exchange device and is used for preheating fermented mature mash and conveying the preheated fermented mature mash into the crude distillation column (3); the top gas outlet of the crude distillation column is sequentially connected with the second heat exchange device and the reflux port of the crude distillation column; the light wine extraction outlet is connected with a first feed inlet of the second rectifying tower, and the crude distillation tower bottom liquid extraction outlet is sequentially connected with a third heat exchange device and a second feed inlet of the second rectifying tower;
the outer part of the second rectifying tower (9) is provided with a second rectifying tower top gas outlet, a second rectifying tower top liquid outlet, a second rectifying tower reflux inlet, a first feed inlet, a second rectifying tower kettle liquid outlet, a second feed inlet and a second rectifying tower reboiler (10) from top to bottom, wherein one path of the second rectifying tower top gas outlet is sequentially connected with a raw material wine steam heater (14) and a molecular sieve adsorption and desorption tower (16); one path of gas outlet at the top of the second rectifying tower is sequentially connected with a reboiler (8) of the crude rectifying tower and a reflux port of the second rectifying tower, liquid outlet at the top of the second rectifying tower is sequentially connected with a reflux port of the first rectifying tower, and liquid outlet at the bottom of the second rectifying tower is sequentially connected with a fourth heat exchange device and a feed port of the first rectifying tower;
the outer part of the rectifying tower (13) is provided with a rectifying tower top gas outlet, a rectifying tower reflux port, an edible alcohol extraction port, a fusel oil extraction port, a rectifying tower feed port and a rectifying tower reboiler (15) from top to bottom, wherein the rectifying tower top gas outlet is sequentially connected with the two rectifying tower reboilers 10 and the rectifying tower reflux port; the fusel oil extraction outlet is connected with the fuel alcohol tank, and the edible alcohol extraction outlet is connected with the common alcohol tank;
the molecular sieve adsorption and desorption tower (16) is provided with a back flushing gas phase outlet, a finished product wine gas outlet, a liquid phase outlet and a gas phase inlet from top to bottom, and the gas phase inlet is sequentially connected with the raw material wine gas heater (14) and a gas outlet at the top of the second rectifying tower; one path of the finished product wine gas outlet is connected with the back flushing gas phase outlet, and the other path of the finished product wine gas outlet is connected with the fuel ethanol storage tank; the liquid phase outlet is sequentially connected with a light wine tank (18) and a reflux port of the crude distillation column;
the method comprises the following steps:
(1) In a crude distillation column (3), carrying out crude distillation treatment on the preheated fermented mature mash to obtain crude distillation column top gas, light wine and crude distillation column bottom liquid; performing first condensation treatment on the top gas of the crude distillation column to obtain crude distillation column condensate, wherein the crude distillation column condensate is refluxed and subjected to crude distillation treatment;
(2) In a secondary rectifying tower (9), rectifying the light wine and the crude rectifying tower bottom liquid subjected to the first heat exchange treatment at normal pressure to obtain secondary rectifying tower top gas, secondary rectifying tower top liquid and secondary rectifying tower bottom liquid; performing second condensation on part of the tower top gas of the second rectifying tower to obtain condensate of the second rectifying tower, and performing normal pressure rectification on condensate reflux of the second rectifying tower;
(3) In a rectifying tower (13), pressurizing and rectifying tower top liquid of the rectifying tower and tower bottom liquid of the rectifying tower after the second heat exchange treatment to obtain alcohol and fusel oil;
(4) And in the molecular sieve adsorption and desorption tower (16), dehydrating the rest part of the second rectifying tower overhead gas after the third heat exchange to obtain fuel ethanol.
2. The method according to claim 1, wherein the first heat exchange means comprises a first mash preheater (1) and a second mash preheater (2), and/or
The second heat exchange device comprises a first condenser (4) of the crude distillation column and a second condenser (5) of the crude distillation column.
3. The method according to claim 2, wherein the first mash preheater (1) is provided with a mash inlet, a mash outlet, a warm end inlet and a warm end outlet; the mash outlet is connected with a mash inlet of the second mash preheater (2), the hot end inlet is connected with a top gas outlet of the crude distillation column, the hot end outlet comprises a gas phase outlet and a liquid phase outlet, the gas phase outlet is sequentially connected with a first condenser (4) of the crude distillation column and a second condenser (5) of the crude distillation column, and a liquid phase outlet of the first mash preheater (1), a liquid phase outlet of the first condenser (4) of the crude distillation column and a liquid phase outlet of the second condenser (5) of the crude distillation column are respectively connected with a reflux port of the crude distillation column through pipelines; the second condenser (5) of the crude distillation column is provided with a gas phase outlet for discharging non-condensing steam.
4. The method according to claim 2, wherein the second mash preheater (2) is provided with a mash inlet, a mash outlet, a warm end inlet and a warm end outlet; wherein, the mash outlet is connected with the feed inlet of the crude distillation column, the hot end inlet is connected with the outlet of the finished product alcohol gas of the molecular sieve adsorption and desorption column, and the hot end outlet is connected with the fuel alcohol tank.
5. The method according to claim 1, wherein the third heat exchange means comprises a first mash heat exchanger (6) and a second mash heat exchanger (7),
wherein, the first mash heat exchanger (6) is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with the liquid extraction outlet of the tower bottom of the crude distillation tower, the mash outlet is connected with the second feed inlet of the second rectifying tower (9), and the hot end inlet is connected with the hot end outlet of the fourth mash heat exchanger (12);
the second mash heat exchanger (7) is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with the liquid extraction outlet of the tower bottom of the crude distillation tower, the mash outlet is connected with the second feed inlet of the secondary rectifying tower (9), and the hot end inlet is connected with the outlet of the tower bottom of the secondary rectifying tower reboiler (10).
6. The method according to claim 1, wherein the fourth heat exchange means comprises a third mash heat exchanger (11) and a fourth mash heat exchanger (12),
wherein the third mash heat exchanger (11) is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with a tower bottom liquid side extraction outlet of the second rectifying tower (9), the mash outlet is connected with a rectifying tower feed inlet, and the hot end inlet is connected with a tower bottom outlet of the first rectifying tower (13);
the fourth mash heat exchanger (12) is provided with a mash inlet, a mash outlet, a hot end inlet and a hot end outlet; wherein, the mash inlet is connected with a tower bottom liquid side extraction outlet of the second rectifying tower (9), the mash outlet is connected with a rectifying tower feed inlet, and the hot end inlet is connected with a hot end outlet of a rectifying tower reboiler (15).
7. The method according to claim 1, wherein the crude distillation column reboiler (8) is provided with a warm end inlet and a warm end outlet, the warm end inlet is connected with a top gas outlet of the secondary rectifying column, and the warm end outlet is connected with a top tray reflux port of the secondary rectifying column (9); and/or
The two rectifying tower reboilers (10) are provided with a hot end inlet and a hot end outlet, the hot end inlet is connected with a rectifying tower top gas outlet, and the hot end outlet is connected with a rectifying tower reflux port; and/or
A rectifying tower reboiler (15) is provided with a hot end inlet and a hot end outlet, the hot end inlet is connected with the steam source outlet, and the hot end outlet is connected with the fourth heat exchange device.
8. The method of claim 1, wherein the temperature of the pre-heat treated fermented beer is 63-88 ℃.
9. The method of claim 1, wherein in step (1), the conditions of the crude distillation comprise: the temperature of the tower kettle is 65-85 ℃; the pressure of the tower kettle is between-0.06 and-0.03 MPa; the temperature of the tower top is 40-60 ℃; the pressure at the top of the tower is-0.05 to-0.08 MPa; the reflux ratio is 0.5-5.
10. The method of claim 1, wherein in step (2), the atmospheric rectification conditions include: the temperature of the tower kettle is 105-125 ℃; the pressure of the tower kettle is 0.07 to 0.3MPa; the temperature of the tower top is 85-98 ℃; the pressure at the top of the tower is 0.05 to 0.2MPa; the reflux ratio is 0.5-8.
11. The method of claim 1, wherein in step (3), the conditions of the pressure rectification include: the temperature of the tower kettle is 140-170 ℃; the pressure of the tower kettle is 0.4 to 0.8MPa; the temperature of the tower top is 110-140 ℃; the pressure at the top of the tower is 0.2 to 0.4MPa; the reflux ratio is 1-5.
12. The method according to claim 1, wherein in the step (3), the extraction temperature of the privet ethanol is 115-120 ℃; and/or
The extraction temperature of the fusel oil is 130-160 ℃.
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