CN110698325A - Production device and process for co-producing fuel ethanol and special grade edible alcohol - Google Patents
Production device and process for co-producing fuel ethanol and special grade edible alcohol Download PDFInfo
- Publication number
- CN110698325A CN110698325A CN201911215057.2A CN201911215057A CN110698325A CN 110698325 A CN110698325 A CN 110698325A CN 201911215057 A CN201911215057 A CN 201911215057A CN 110698325 A CN110698325 A CN 110698325A
- Authority
- CN
- China
- Prior art keywords
- tower
- rectifying
- alcohol
- methanol
- distillation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12H—PASTEURISATION, STERILISATION, PRESERVATION, PURIFICATION, CLARIFICATION OR AGEING OF ALCOHOLIC BEVERAGES; METHODS FOR ALTERING THE ALCOHOL CONTENT OF FERMENTED SOLUTIONS OR ALCOHOLIC BEVERAGES
- C12H6/00—Methods for increasing the alcohol content of fermented solutions or alcoholic beverages
- C12H6/02—Methods for increasing the alcohol content of fermented solutions or alcoholic beverages by distillation
Abstract
A production device and process for co-producing fuel ethanol and special grade edible alcohol comprises a first preheater, a second preheater, a light alcohol preheater, a crude distillation tower, a rectifying tower A, a formaldehyde-removing tower, a water washing tower, a rectifying tower B, a methanol tower, an industrial alcohol tower, a light alcohol tower and a molecular sieve dehydration system; operating a coarse distillation tower, a rectifying tower A, a light wine tower and a molecular sieve dehydration system for producing fuel ethanol; operating the crude distillation tower, the rectifying tower A, the aldehyde removing tower, the water washing tower, the rectifying tower B, the methanol tower, the industrial alcohol tower and the light alcohol tower to produce the special grade edible alcohol; the crude distillation tower, the rectifying tower A, the aldehyde removing tower, the water washing tower, the rectifying tower B, the methanol tower, the industrial alcohol tower, the light alcohol tower and the molecular sieve dehydration system are operated to co-produce the special grade edible alcohol and the fuel ethanol. The invention can flexibly adjust the product structure according to market demands, switch production or co-produce special grade edible alcohol and fuel ethanol, reasonably optimize and match energy efficiency, facilitate impurity removal and ensure the product quality.
Description
Technical Field
The invention relates to the technical field of alcohol production, in particular to a production device and a production process for co-producing fuel ethanol and special grade edible alcohol.
Background
Fermented alcohol is a renewable important basic raw material and product, and is divided into edible alcohol and fuel alcohol products according to different requirements on use functions and purity. The fuel ethanol product is mainly used as fuel, chemical production raw material and the like; the edible alcohol product is mainly used for preparing alcoholic beverages, chemical production raw materials and the like.
However, the existing fuel ethanol and special grade edible alcohol device and process method can only produce single products, the fuel ethanol device can only produce fuel ethanol, and the special grade edible alcohol device can produce fuel ethanol, but the process energy consumption is high, the product quality is poor, and the convenient switching of the two products can not be realized according to market demands. A new process method is provided, not only can produce fuel ethanol, but also can produce super-special edible alcohol, and can also co-produce two products, and the product quality is better when the special grade is produced.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a production device and a process for co-producing fuel ethanol and special grade edible alcohol, which can flexibly adjust the product structure according to market demands, switch production or co-produce special grade edible alcohol and fuel ethanol, reasonably optimize and match energy efficiency, facilitate impurity removal and ensure the product quality.
In order to achieve the purpose, the invention adopts the following technical scheme: the utility model provides a coproduction fuel ethanol and special grade edible alcohol's apparatus for producing, includes first preheater, second preheater, light wine preheater, thick distillation column, rectifying column A, dealdehyding tower, water scrubber, rectifying column B, methanol column, industrial spirit tower, light wine tower and molecular sieve dewatering system, thick distillation column pan feeding mouth is equipped with first preheater, rectifying column A's pan feeding mouth is connected to the thick distillation column discharge gate, light wine tower, dealdehyding tower and second preheater's pan feeding mouth is connected to rectifying column A's discharge gate, the discharge gate of light wine tower is connected to the pan feeding mouth of second preheater and industrial spirit tower, molecular sieve dewatering system pan feeding mouth is connected to the second preheater discharge gate, water scrubber feeding mouth is connected to the discharge gate of dealdehyding tower, light wine preheater feed inlet is connected to the water scrubber discharge gate, light wine preheater discharge gate rectifying column B's pan feeding mouth, rectifying column B discharge gate is connected the methanol column pan feeding mouth, industry alcohol column pan feeding mouth is connected to the methanol column discharge gate, second pre-heater pan feeding mouth is connected to industry alcohol column discharge gate.
As a further improvement of the invention: rectifying column B and weak liquor tower are by the indirect heating of live steam, rectifying column B top of the tower steam passes through reboiler indirect heating aldehyde tower, washing tower, coarse distillation column, washing tower top of the tower steam passes through reboiler indirect heating methanol column, the aldehyde tower passes through reboiler indirect heating industry spirit tower.
As a further improvement of the invention: the weak liquor tower is indirectly heated by raw steam, the liquor steam at the top of the weak liquor tower heats the rough distillation tower through a reboiler, the dehydrated finished product liquor steam heats the rough distillation tower through the reboiler, and the insufficient heat of the rough distillation tower is supplemented by the raw steam through the reboiler.
As a further improvement of the invention: the operation pressure at the top of the coarse distillation tower is-90 to-20 kPa, the temperature at the top of the coarse distillation tower is 45 to 85 ℃, and the temperature at the bottom of the coarse distillation tower is 50 to 90 ℃;
the operation pressure at the top of the rectifying tower A is-90-10 kPa, the temperature at the top of the rectifying tower A is 45-75 ℃, and the temperature at the bottom of the rectifying tower A is 55-85 ℃;
the operation pressure at the top of the rectifying tower B is 50-300 kPa, the temperature at the top of the rectifying tower B is 90-115 ℃, and the temperature at the bottom of the rectifying tower B is 120-145 ℃;
the operation pressure of the top of the dealdehyding tower is-50-100 kPa, the temperature of the top of the dealdehyding tower is 70-90 ℃, and the temperature of the bottom of the dealdehyding tower is 80-100 ℃;
the operation pressure of the top of the washing tower is-50 kPa, the temperature of the top of the washing tower is 85-105 ℃, and the temperature of the bottom of the washing tower is 90-110 ℃;
the operating pressure of the top of the methanol tower is-90-50 kPa, the temperature of the top of the methanol tower is 45-95 ℃, and the temperature of the bottom of the methanol tower is 50-100 ℃;
the operation pressure of the top of the light wine tower is 50-300 kPa, the temperature of the top of the light wine tower is 90-115 ℃, and the temperature of the bottom of the light wine tower is 120-145 ℃;
the operating pressure of the molecular sieve dehydration system is-90-300 kPa, and the temperature is 60-130 ℃.
As a further improvement of the invention: the rectifying tower B and the weak liquor tower indirectly supply heat through a reboiler by using primary steam of a boiler, and the rectification tower B and the weak liquor tower are operated at positive pressure.
As a further improvement of the invention: the crude distillation tower, the light wine tower and the industrial alcohol tower are all provided with impurity discharging outlets, the methanol and molecular sieve dehydration system is provided with a finished product outlet, the impurity discharging outlet of the light wine tower is also connected with a fusel oil separator, and the outlet of the crude distillation tower is connected to a DDGS removing section.
A process for co-producing fuel ethanol and special grade edible alcohol by using the device comprises the following steps:
operating a rough distillation tower, a rectifying tower A, a light wine tower and a molecular sieve dehydration system to produce fuel ethanol;
operating the crude distillation tower, the rectifying tower A, the aldehyde removing tower, the water washing tower, the rectifying tower B, the methanol tower, the industrial alcohol tower and the light alcohol tower to produce the special grade edible alcohol;
the crude distillation tower, the rectifying tower A, the aldehyde removing tower, the water washing tower, the rectifying tower B, the methanol tower, the industrial alcohol tower, the light alcohol tower and the molecular sieve dehydration system are operated to co-produce the special grade edible alcohol and the fuel ethanol.
As a further improvement of the invention: the method for producing the special grade edible alcohol comprises the steps of preheating mature mash from fermentation by a first preheater, feeding the mature mash into a degassing section of a rough distillation tower, and feeding the degassed mash into a stripping section of the rough distillation tower; gas-phase crude wine vapor after distillation in the crude distillation tower enters a rectifying tower A, and 95% of wine liquid extracted from the upper area of the rectifying tower A enters an aldehyde removing tower; the wine liquid after the aldehyde removal in the aldehyde removal tower enters a water washing tower, and the light wine liquid after impurity extraction through water washing enters a rectifying tower B after being preheated by a light wine preheater; in the rectifying tower B, more than 96% of liquor is extracted from the upper region of the rectifying tower B and enters a methanol tower to further remove methanol impurities, and special grade edible alcohol is extracted from the bottom region of the methanol tower.
As a further improvement of the invention: the miscellaneous wine rich in fusel oil extracted from the rectifying tower A, the rectifying tower B and the water washing tower enters a weak liquor tower for treatment, and fusel oil is extracted; and the miscellaneous wine rich in methanol impurities and extracted by the final-stage condenser of each tower enters an industrial alcohol tower to extract industrial alcohol.
As a further improvement of the invention: the method for producing the fuel ethanol comprises the steps of enabling mature mash from fermentation to enter a degassing section of a coarse distillation tower through a first preheater, and enabling the degassed mash to enter a stripping section of the coarse distillation tower; gas-phase crude wine vapor after distillation in the crude distillation tower enters a rectifying tower A, and light wine is extracted from the bottom of the rectifying tower A and enters a light wine tower after being preheated; and after the liquor extracted from the rectifying tower A and the weak liquor tower is heated in a liquid phase by a second preheater, the liquor enters a molecular sieve dehydration system for dehydration to obtain the finished product fuel ethanol.
As a further improvement of the invention: the method for co-producing the special grade edible alcohol and the fuel ethanol comprises the steps of enabling mature mash from fermentation to enter a degassing section of a rough distillation tower through a first preheater, enabling the degassed mash to enter a stripping section of the rough distillation tower, and enabling gas-phase crude wine steam after distillation in the rough distillation tower to enter a rectifying tower A; part of the liquid phase extracted from the rectifying tower A is sent to an aldehyde removal tower, the alcohol liquid after aldehyde removal enters a water washing tower, and the light alcohol liquid after impurity extraction through water washing enters a rectifying tower B; extracting more than 96% liquor from the upper region of the rectifying tower B, introducing the liquor into a methanol tower, further removing methanol impurities, and extracting special grade edible alcohol from the bottom region of the methanol tower; the aldehyde removing tower, the water washing tower, the rectifying tower B and the methanol tower system generate special grade edible alcohol; and respectively extracting the other part of the liquid phase extracted from the rectifying tower A to a second preheater and a light wine tower, heating the liquid phase extracted from the rectifying tower A and the light wine tower in the second preheater, and then dehydrating the liquid phase in a molecular sieve dehydration system to obtain a finished product of fuel ethanol, wherein the finished product of fuel ethanol is obtained after dehydration in the molecular sieve dehydration system.
The invention has the beneficial technical effects that:
1. the invention uses the rough distillation tower, the rectification tower A, the light wine tower and the molecular sieve dehydration system to produce the fuel ethanol, uses the rough distillation tower, the rectification tower A, the aldehyde removal tower, the water washing tower, the rectification tower B, the methanol tower, the industrial alcohol tower and the light wine tower to produce the special grade edible alcohol, uses the rough distillation tower, the rectification tower A, the aldehyde removal tower, the water washing tower, the rectification tower B, the methanol tower, the industrial alcohol tower, the light wine tower and the molecular sieve dehydration system to co-produce the special grade edible alcohol and the fuel ethanol, can realize the switchable production or the co-production of the special grade edible alcohol and the fuel ethanol of a set of devices, can flexibly adjust the product structure according to market demands, further improve the quality of the special grade edible alcohol and improve the market adaptability of the production devices.
2. The rough distillation tower and the rectifying tower A can directly transfer mass energy under the negative pressure condition, the rectifying tower B and the light wine tower indirectly supply heat by primary steam of a boiler through a reboiler in an energy coupling mode, the process is positive pressure operation, and the energy efficiency can be reasonably optimized and matched, so that the energy conservation is realized.
3. When the fuel ethanol is produced by the method, the liquid-phase material passing is adopted, so that the quality of the product is further ensured.
4. When the invention is used for producing special grade edible alcohol, the coarse distillation tower, the weak wine tower and the industrial alcohol tower are all provided with impurity discharging outlets, and due to adoption of multi-point impurity discharging, the functions of the towers are specific, and the working conditions are different, thereby being more beneficial to impurity discharging and having better product quality.
Drawings
FIG. 1 is a schematic view of the connection structure of the device of the present invention.
Detailed Description
The present invention will be further described with reference to the accompanying drawings, and it should be noted that the present embodiment is based on the technical solution, and the detailed implementation and the specific operation process are provided, but the protection scope of the present invention is not limited to the present embodiment.
Referring to fig. 1, a device for co-producing fuel ethanol and special grade edible alcohol, comprising a first preheater, a second preheater, a light alcohol preheater, a crude distillation tower, a rectification tower A, a formaldehyde-removing tower, a water washing tower, a rectification tower B, a methanol tower, an industrial alcohol tower, a light alcohol tower and a molecular sieve dehydration system, wherein the feed inlet of the crude distillation tower is provided with the first preheater, the discharge outlet of the crude distillation tower is connected with the feed inlet of the rectification tower A, the discharge outlet of the rectification tower A is connected with the feed inlets of the light alcohol tower, the formaldehyde-removing tower and the second preheater, the discharge outlet of the light alcohol tower is connected with the feed inlets of the second preheater and the industrial alcohol tower, the discharge outlet of the second preheater is connected with the feed inlet of the molecular sieve dehydration system, the discharge outlet of the formaldehyde-removing tower is connected with the feed inlet of the water washing tower, the discharge outlet of the water washing tower is connected with the feed inlet of the light alcohol preheater, the discharge outlet of the rectification tower B is connected with the discharge outlet of the methanol tower, the discharge port of the industrial alcohol tower is connected with the feeding port of the second preheater.
The coarse distillation tower, the light wine tower and the industrial alcohol tower are all provided with impurity discharging outlets, the methanol and molecular sieve dehydration systems are all provided with finished product outlets, the impurity discharging outlet of the light wine tower is connected with a fusel oil separator for separating fusel oil in the discharged fusel wine, the discharging port of the coarse distillation tower is connected with a DDGS (Distillers Dried Grains with Solubles, which is abbreviated as Dried Distillers Grains and soluble substances thereof, in the invention, mature mash enters a degassing section of the coarse distillation tower through a first preheater, the Dried Distillers Grains of soluble solid substances left in the degassed mash are removed), the impurity discharging port of the industrial alcohol tower is used for discharging industrial alcohol, the finished product outlet of the molecular sieve dehydration system is used for discharging fuel ethanol, and the methanol finished product outlet is used for discharging special edible alcohol.
The column parameters were as follows:
the operation pressure at the top of the coarse distillation tower is-90 to-20 kPa, the temperature at the top of the coarse distillation tower is 45 to 85 ℃, and the temperature at the bottom of the coarse distillation tower is 50 to 90 ℃;
the operation pressure at the top of the rectifying tower A is-90-10 kPa, the temperature at the top of the rectifying tower A is 45-75 ℃, and the temperature at the bottom of the rectifying tower A is 55-85 ℃;
the operation pressure at the top of the rectifying tower B is 50-300 kPa, the temperature at the top of the rectifying tower B is 90-115 ℃, and the temperature at the bottom of the rectifying tower B is 120-145 ℃;
the operation pressure at the top of the dealdehyding tower is-50-100 kPa, the temperature at the top of the tower is 70-90 ℃, and the temperature at the bottom of the tower is 80-100 ℃;
the operation pressure of the top of the washing tower is-50 kPa, the temperature of the top of the washing tower is 85-105 ℃, and the temperature of the bottom of the washing tower is 90-110 ℃;
the operating pressure of the top of the methanol tower is-90-50 kPa, the temperature of the top of the methanol tower is 45-95 ℃, and the temperature of the bottom of the methanol tower is 50-100 ℃;
the operation pressure of the top of the light wine tower is 50-300 kPa, the temperature of the top of the wine tower is 90-115 ℃, and the temperature of the bottom of the wine tower is 120-145 ℃;
the operating pressure of the molecular sieve dehydration system is-90-300 kPa, and the temperature is 60-130 ℃.
The energy coupling mode of the production device for co-producing the fuel ethanol and the special grade edible alcohol is as follows: the rectifying tower B and the weak liquor tower indirectly supply heat through a reboiler by using primary steam of a boiler, and are operated at positive pressure.
The first embodiment is as follows:
the method is characterized in that a crude distillation tower, a rectifying tower A, a weak liquor tower and a molecular sieve dehydration system are operated for producing fuel ethanol, and the specific method comprises the following steps:
feeding fermented mature mash into a degassing section of a coarse distillation tower through a first preheater, and feeding the degassed mash into a stripping section of the coarse distillation tower; gas-phase crude wine vapor after distillation in the crude distillation tower enters a rectifying tower A, and light wine is extracted from the bottom of the rectifying tower A and enters a light wine tower after being preheated; and after the liquor extracted from the rectifying tower A and the weak liquor tower is heated in a liquid phase by a second preheater, the liquor enters a molecular sieve dehydration system for dehydration to obtain the finished product fuel ethanol.
In the process, a light wine tower is indirectly heated by raw steam, wine steam at the top of the light wine tower heats a coarse distillation tower through a reboiler, dehydrated finished wine steam heats the coarse distillation tower through the reboiler, and insufficient heat of the coarse distillation tower is supplemented by heat sources such as the raw steam through the reboiler.
The second embodiment:
the method comprises the following steps of operating a crude distillation tower, a rectifying tower A, an aldehyde removing tower, a water washing tower, a rectifying tower B, a methanol tower, an industrial alcohol tower and a light alcohol tower, wherein a molecular sieve dehydration system does not operate and is used for producing special edible alcohol, and the specific method comprises the following steps:
preheating mature mash from fermentation by a first preheater, feeding the preheated mash into a degassing section of a coarse distillation tower, and feeding the degassed mash into a stripping section of the coarse distillation tower; gas-phase crude wine vapor after distillation in the crude distillation tower enters a rectifying tower A, and 95% of wine liquid extracted from the upper area of the rectifying tower A enters an aldehyde removing tower; the wine liquid after the aldehyde removal in the aldehyde removal tower enters a water washing tower, and the light wine liquid after impurity extraction through water washing enters a rectifying tower B after being preheated by a light wine preheater; in the rectifying tower B, more than 96% of liquor is extracted from the upper region of the rectifying tower B and enters a methanol tower to further remove methanol impurities, and special grade edible alcohol is extracted from the bottom region of the methanol tower.
The miscellaneous wine rich in fusel oil extracted from the rectifying tower A, the rectifying tower B and the water washing tower enters a weak liquor tower for treatment, and fusel oil is extracted; and the miscellaneous wine rich in methanol impurities and extracted by the final-stage condenser of each tower enters an industrial alcohol tower to extract industrial alcohol.
In the process, a rectifying tower B and a light wine tower are indirectly heated by raw steam, the tower top alcohol steam of the rectifying tower B indirectly heats an aldehyde removing tower, a water washing tower and a coarse distillation tower through reboilers, the tower top alcohol steam of the water washing tower indirectly heats a methanol tower through the reboilers, and the aldehyde removing tower indirectly heats an industrial alcohol tower through the reboilers.
The third embodiment is as follows:
referring to the first and second embodiments, the heating mode of each tower is that a crude distillation tower, a rectifying tower A, an aldehyde removal tower, a water washing tower, a rectifying tower B, a methanol tower, an industrial alcohol tower, a light alcohol tower and a molecular sieve dehydration system are operated to co-produce special grade edible alcohol and fuel ethanol, and the specific method comprises the following steps:
mature mash from fermentation enters a degassing section of a coarse distillation tower through a first preheater, the degassed mash enters a stripping section of the coarse distillation tower, and gas-phase crude wine vapor obtained after distillation in the coarse distillation tower enters a rectifying tower A.
Part of the liquid phase extracted from the rectifying tower A is sent to an aldehyde removal tower, the alcohol liquid after aldehyde removal enters a water washing tower, and the light alcohol liquid after impurity extraction through water washing enters a rectifying tower B; in the rectifying tower B, more than 96% of liquor is extracted from the upper region of the rectifying tower B and enters a methanol tower to further remove methanol impurities, and special grade edible alcohol is extracted from the bottom region of the methanol tower.
And respectively extracting the other part of the liquid phase extracted from the rectifying tower A to a second preheater and a light wine tower, heating the liquid phase extracted from the rectifying tower A and the light wine tower in the second preheater, and then dehydrating the liquid phase in a molecular sieve dehydration system to obtain a finished product of fuel ethanol, wherein the finished product of fuel ethanol is obtained after dehydration in the molecular sieve dehydration system.
The fourth embodiment is as follows:
the molecular sieve dehydration system comprises a granular molecular sieve system and a membrane molecular sieve system, the membrane molecular sieve system comprises a membrane molecular sieve, a membrane molecular sieve superheater and a membrane molecular sieve evaporator, the membrane molecular sieve evaporator is connected with the membrane molecular sieve superheater, and the membrane molecular sieve superheater is connected with the membrane molecular sieve; the granular molecular sieve system comprises a granular molecular sieve, a granular molecular sieve superheater and a granular molecular sieve evaporator, wherein a steam outlet section of the membrane type molecular sieve is connected with the granular molecular sieve evaporator through a steam pipe, and the granular molecular sieve superheater is connected with the granular molecular sieve.
Various corresponding changes and modifications can be made by those skilled in the art based on the above technical solutions and concepts, and all such changes and modifications should be included in the protection scope of the present invention.
Claims (11)
1. The utility model provides a coproduction fuel ethanol and special grade edible alcohol's apparatus for producing, includes first preheater, second preheater, light wine preheater, thick distillation column, rectifying column A, takes off aldehyde tower, water scrubber, rectifying column B, methanol column, industry spirit tower, light wine tower and molecular sieve dewatering system, its characterized in that: the coarse distillation tower pan feeding mouth is equipped with first pre-heater, rectifying column A's pan feeding mouth is connected to the coarse distillation tower discharge gate, light wine tower, the pan feeding mouth of dealdehyding tower and second pre-heater are connected to rectifying column A's discharge gate, the discharge gate of light wine tower is connected to the pan feeding mouth of second pre-heater and industry spirit tower, molecular sieve dewatering system pan feeding mouth is connected to the second pre-heater discharge gate, the discharge gate of dealdehyding tower connects the washing tower pan feeding mouth, light wine pre-heater pan feeding mouth is connected to the washing tower discharge gate, light wine pre-heater discharge gate rectifying column B's pan feeding mouth, methanol tower pan feeding mouth is connected to rectifying column B discharge gate, industry alcohol tower pan feeding mouth is connected to the methanol tower discharge gate, second pre-heater pan feeding mouth is connected to industry spirit tower discharge gate.
2. The apparatus for co-producing ethanol fuel and super grade edible alcohol as claimed in claim 1, wherein: rectifying column B and weak liquor tower are by the indirect heating of live steam, rectifying column B top of the tower steam passes through reboiler indirect heating aldehyde tower, washing tower, coarse distillation column, washing tower top of the tower steam passes through reboiler indirect heating methanol column, the aldehyde tower passes through reboiler indirect heating industry spirit tower.
3. The apparatus for co-producing ethanol fuel and super grade edible alcohol as claimed in claim 1, wherein: the weak liquor tower is indirectly heated by raw steam, the liquor steam at the top of the weak liquor tower heats the rough distillation tower through a reboiler, the dehydrated finished product liquor steam heats the rough distillation tower through the reboiler, and the insufficient heat of the rough distillation tower is supplemented by the raw steam through the reboiler.
4. The apparatus for co-producing ethanol fuel and super grade edible alcohol as claimed in claim 1, wherein:
the operation pressure at the top of the coarse distillation tower is-90 to-20 kPa, the temperature at the top of the coarse distillation tower is 45 to 85 ℃, and the temperature at the bottom of the coarse distillation tower is 50 to 90 ℃;
the operation pressure at the top of the rectifying tower A is-90-10 kPa, the temperature at the top of the rectifying tower A is 45-75 ℃, and the temperature at the bottom of the rectifying tower A is 55-85 ℃;
the operation pressure at the top of the rectifying tower B is 50-300 kPa, the temperature at the top of the rectifying tower B is 90-115 ℃, and the temperature at the bottom of the rectifying tower B is 120-145 ℃;
the operation pressure of the top of the dealdehyding tower is-50-100 kPa, the temperature of the top of the dealdehyding tower is 70-90 ℃, and the temperature of the bottom of the dealdehyding tower is 80-100 ℃;
the operation pressure of the top of the washing tower is-50 kPa, the temperature of the top of the washing tower is 85-105 ℃, and the temperature of the bottom of the washing tower is 90-110 ℃;
the operating pressure of the top of the methanol tower is-90-50 kPa, the temperature of the top of the methanol tower is 45-95 ℃, and the temperature of the bottom of the methanol tower is 50-100 ℃;
the operation pressure of the top of the light wine tower is 50-300 kPa, the temperature of the top of the light wine tower is 90-115 ℃, and the temperature of the bottom of the light wine tower is 120-145 ℃;
the operating pressure of the molecular sieve dehydration system is-90-300 kPa, and the temperature is 60-130 ℃.
5. The apparatus for co-producing ethanol fuel and super grade edible alcohol as claimed in claim 1, wherein: the rectifying tower B and the weak liquor tower indirectly supply heat through a reboiler by using primary steam of a boiler, and the rectification tower B and the weak liquor tower are operated at positive pressure.
6. The apparatus for co-producing ethanol fuel and super grade edible alcohol as claimed in claim 1, wherein: the crude distillation tower, the light wine tower and the industrial alcohol tower are all provided with impurity discharging outlets, the methanol and molecular sieve dehydration system is provided with a finished product outlet, the impurity discharging outlet of the light wine tower is also connected with a fusel oil separator, and the outlet of the crude distillation tower is connected to a DDGS removing section.
7. A process for co-producing fuel ethanol and special grade edible alcohol by using the device of any one of claims 1 to 6, which is characterized in that:
operating a rough distillation tower, a rectifying tower A, a light wine tower and a molecular sieve dehydration system to produce fuel ethanol;
operating the crude distillation tower, the rectifying tower A, the aldehyde removing tower, the water washing tower, the rectifying tower B, the methanol tower, the industrial alcohol tower and the light alcohol tower to produce the special grade edible alcohol;
the crude distillation tower, the rectifying tower A, the aldehyde removing tower, the water washing tower, the rectifying tower B, the methanol tower, the industrial alcohol tower, the light alcohol tower and the molecular sieve dehydration system are operated to co-produce the special grade edible alcohol and the fuel ethanol.
8. The process of co-producing fuel ethanol and super grade food alcohol according to claim 7, wherein the method for producing super grade food alcohol comprises:
preheating mature mash from fermentation by a first preheater, feeding the preheated mash into a degassing section of a coarse distillation tower, and feeding the degassed mash into a stripping section of the coarse distillation tower;
gas-phase crude wine vapor after distillation in the crude distillation tower enters a rectifying tower A, and 95% of wine liquid extracted from the upper area of the rectifying tower A enters an aldehyde removing tower;
the wine liquid after the aldehyde removal in the aldehyde removal tower enters a water washing tower, and the light wine liquid after impurity extraction through water washing enters a rectifying tower B after being preheated by a light wine preheater;
in the rectifying tower B, more than 96% of liquor is extracted from the upper region of the rectifying tower B and enters a methanol tower to further remove methanol impurities, and special grade edible alcohol is extracted from the bottom region of the methanol tower.
9. The process of co-producing fuel ethanol and super grade food alcohol according to claim 8, wherein: the miscellaneous wine rich in fusel oil extracted from the rectifying tower A, the rectifying tower B and the water washing tower enters a weak liquor tower for treatment, and fusel oil is extracted; and the miscellaneous wine rich in methanol impurities and extracted by the final-stage condenser of each tower enters an industrial alcohol tower to extract industrial alcohol.
10. A process for co-producing fuel ethanol and super grade food alcohol in accordance with claim 7, wherein the method for producing fuel ethanol comprises:
feeding fermented mature mash into a degassing section of a coarse distillation tower through a first preheater, and feeding the degassed mash into a stripping section of the coarse distillation tower;
gas-phase crude wine vapor after distillation in the crude distillation tower enters a rectifying tower A, and light wine is extracted from the bottom of the rectifying tower A and enters a light wine tower after being preheated;
and after the liquor extracted from the rectifying tower A and the weak liquor tower is heated in a liquid phase by a second preheater, the liquor enters a molecular sieve dehydration system for dehydration to obtain the finished product fuel ethanol.
11. The process of claim 7, wherein the method for co-producing the special grade edible alcohol and the fuel ethanol comprises the following steps:
feeding fermented mature mash into a degassing section of a coarse distillation tower through a first preheater, feeding the degassed mash into a stripping section of the coarse distillation tower, and feeding gas-phase crude wine vapor subjected to distillation in the coarse distillation tower into a rectifying tower A;
part of the liquid phase extracted from the rectifying tower A is sent to an aldehyde removal tower, the alcohol liquid after aldehyde removal enters a water washing tower, and the light alcohol liquid after impurity extraction through water washing enters a rectifying tower B; extracting more than 96% liquor from the upper region of the rectifying tower B, introducing the liquor into a methanol tower, further removing methanol impurities, and extracting special grade edible alcohol from the bottom region of the methanol tower; the aldehyde removing tower, the water washing tower, the rectifying tower B and the methanol tower system generate special grade edible alcohol;
and respectively extracting the other part of the liquid phase extracted from the rectifying tower A to a second preheater and a light wine tower, heating the liquid phase extracted from the rectifying tower A and the light wine tower in the second preheater, and then dehydrating the liquid phase in a molecular sieve dehydration system to obtain a finished product of fuel ethanol, wherein the finished product of fuel ethanol is obtained after dehydration in the molecular sieve dehydration system.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2019107137205 | 2019-08-02 | ||
| CN201910713720 | 2019-08-02 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110698325A true CN110698325A (en) | 2020-01-17 |
Family
ID=69208038
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911215057.2A Pending CN110698325A (en) | 2019-08-02 | 2019-12-02 | Production device and process for co-producing fuel ethanol and special grade edible alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110698325A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111807928A (en) * | 2020-08-14 | 2020-10-23 | 广东中科天元新能源科技有限公司 | Distillation dehydration production device and method for co-producing superior edible alcohol and fuel ethanol |
| CN113072423A (en) * | 2021-04-01 | 2021-07-06 | 天津大学 | Method and equipment for co-producing fuel ethanol and brewed edible alcohol |
| CN114685247A (en) * | 2020-12-29 | 2022-07-01 | 国投生物科技投资有限公司 | Method and system for co-producing fuel ethanol and edible alcohol |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040471A (en) * | 2010-11-16 | 2011-05-04 | 广东中科天元新能源科技有限公司 | Distillation dehydration device and process for co-producing ethanol fuels and custom grade edible alcohols |
| CN201850234U (en) * | 2010-11-16 | 2011-06-01 | 广东中科天元新能源科技有限公司 | Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production |
| CN107903148A (en) * | 2017-10-13 | 2018-04-13 | 广东中科天元新能源科技有限公司 | Top grade alcohol, alcohol fuel, electronic grade anhydrous alcohol production device and its production technology |
| CN109876486A (en) * | 2019-04-03 | 2019-06-14 | 广东中科天元新能源科技有限公司 | A kind of eight column differential-pressure distillation device of superfine alcohol and energy-saving processing technique |
-
2019
- 2019-12-02 CN CN201911215057.2A patent/CN110698325A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040471A (en) * | 2010-11-16 | 2011-05-04 | 广东中科天元新能源科技有限公司 | Distillation dehydration device and process for co-producing ethanol fuels and custom grade edible alcohols |
| CN201850234U (en) * | 2010-11-16 | 2011-06-01 | 广东中科天元新能源科技有限公司 | Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production |
| CN107903148A (en) * | 2017-10-13 | 2018-04-13 | 广东中科天元新能源科技有限公司 | Top grade alcohol, alcohol fuel, electronic grade anhydrous alcohol production device and its production technology |
| CN109876486A (en) * | 2019-04-03 | 2019-06-14 | 广东中科天元新能源科技有限公司 | A kind of eight column differential-pressure distillation device of superfine alcohol and energy-saving processing technique |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111807928A (en) * | 2020-08-14 | 2020-10-23 | 广东中科天元新能源科技有限公司 | Distillation dehydration production device and method for co-producing superior edible alcohol and fuel ethanol |
| CN114685247A (en) * | 2020-12-29 | 2022-07-01 | 国投生物科技投资有限公司 | Method and system for co-producing fuel ethanol and edible alcohol |
| CN114685247B (en) * | 2020-12-29 | 2023-06-20 | 国投生物科技投资有限公司 | Method and system for co-producing fuel ethanol and edible alcohol |
| CN113072423A (en) * | 2021-04-01 | 2021-07-06 | 天津大学 | Method and equipment for co-producing fuel ethanol and brewed edible alcohol |
| CN113072423B (en) * | 2021-04-01 | 2022-10-04 | 天津大学 | Method and equipment for co-producing fuel ethanol and brewed edible alcohol |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108103112B (en) | Process for producing fuel ethanol by using corn starch as raw material | |
| CN100525874C (en) | Six-column differential-pressure distillation device for extra edible alcohol and process therefor | |
| CN110698325A (en) | Production device and process for co-producing fuel ethanol and special grade edible alcohol | |
| CN100453137C (en) | Alcohol quinque-towel differential pressure distilling arrangement and technique thereof | |
| CN106928026B (en) | Method for distilling cellulosic ethanol | |
| CN110922302B (en) | Differential pressure distillation dehydration production process of fuel ethanol double-negative-pressure rough distillation tower | |
| CN101088975A (en) | Fuel alcohol dewatering apparatus and process | |
| CN108421274B (en) | Low-pressure double-coarse double-fine eight-tower distillation device and method for preparing high-grade alcohol | |
| CN203677978U (en) | Vapor-compression type alcohol recovery tower | |
| CN101851149A (en) | Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation | |
| CN110981696A (en) | Process and system for producing fuel ethanol by using double-coarse single-fine three-tower distillation low-concentration fermented mash | |
| CN203639370U (en) | Continuous rectification system for m-toluic acid | |
| CN114031580B (en) | Refining device and refining method for low-energy PBAT byproduct tetrahydrofuran | |
| CN106316792B (en) | The device and method of methanol and ethyl alcohol is recycled from stalk sugar hydrocrackates | |
| CN211522068U (en) | System for producing fuel ethanol by using double-coarse single-fine three-tower distillation low-concentration fermented mash | |
| CN213085848U (en) | Distillation dehydration production device for co-producing high-grade edible alcohol and fuel ethanol | |
| CN210495282U (en) | Four-tower distillation and membrane separation integrated system | |
| CN104151273B (en) | Device and the technique of furfural is extracted from paper waste | |
| CN113667700A (en) | Method and system for producing ethanol by fermenting mixed raw materials | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN102492555B (en) | Method and device for high-efficiency energy-saving desolvation of fossilized animal/plant wax-containing solution | |
| CN111807928A (en) | Distillation dehydration production device and method for co-producing superior edible alcohol and fuel ethanol | |
| CN212854692U (en) | Fuel ethanol production device for optimizing heat supply through whole-process heat energy | |
| CN203602599U (en) | Equipment for processing molasses alcohol liquid waste | |
| CN212076901U (en) | Cogeneration device of superior edible alcohol and absolute ethyl alcohol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200117 |