CN106422388A - Differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and production technology of high-quality alcohol - Google Patents
Differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and production technology of high-quality alcohol Download PDFInfo
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- CN106422388A CN106422388A CN201610952207.8A CN201610952207A CN106422388A CN 106422388 A CN106422388 A CN 106422388A CN 201610952207 A CN201610952207 A CN 201610952207A CN 106422388 A CN106422388 A CN 106422388A
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- preheater
- topping still
- mash
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
- B01D3/003—Rectification of spirit
- B01D3/004—Rectification of spirit by continuous methods
- B01D3/005—Combined distillation and rectification
Abstract
The invention relates to a differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and a production technology of the high-quality alcohol. The device comprises a first crude distillation tower, a second crude distillation tower, a water washing tower, a rectifying tower, a methanol tower, a recovery tower and a heat exchanger which are communicated through pipelines. The alcohol vapor at the top of the first crude distillation tower, the alcohol vapor at the top of the recovery tower and the waste fermented liquid at the bottom of the first crude distillation tower are used for preheating the mature fermented liquor in a first fermented liquor preheater, the mature fermented liquor in a second fermented liquor preheater and the mature fermented liquor in a third fermented liquor preheater respectively, the waste fermented liquid at the bottom of the second crude distillation tower passes through a fourth fermented liquor preheater and then can be used for preheating the mature fermented liquor in the fourth fermented liquor. By arranging two crude distillation towers to produce the high-quality edible alcohol, the heat of the alcohol vapor at the tops of the first crude distillation tower and the recovery tower and the heat of the waste fermented liquid at the bottoms of the first crude distillation tower and the second crude distillation tower can be fully used for preheating the mature fermented liquor, and by means of the differential pressure multiple-effect thermal coupling technology, energy consumption of a distillation system is optimized, and the steam heating energy consumption of the device can be remarkably reduced.
Description
Technical field
The present invention relates to the production field of top grade ethanol, especially relates to a kind of differential pressure of double thick tower production top grade ethanol and steams
Evaporate energy saver and its production technology.
Background technology
Edible ethanol can be obtained by processing to the fermentation of corn, Maninot esculenta crantz. and saccharine material and distillation.As country is right
The raising of edible ethanol standard, the domestic deterioration of water resources situation and the growing tension of global energy, seek one kind and can improve
Edible ethanol quality, the new technology for rationally sufficiently producing edible ethanol energy consumption using water resource and reduction become the task of top priority.
Chinese patent CN200710030550.8 is related to a kind of five-tower two-grade difference pressure distillation equipment for senior edible ethanol and its technique, the work
Skill adopts the steam consumption of multistage differential pressure thermal coupling energy match technology, ton high grade edible spirit product to be 2.2～2.5 tons, ton
Product consumes cooling water and is 90～120 tons, and its top grade ethanol all technical for producing meets the top grade of national regulation and eats
Standards of alcohol.But traditional top grade Alcohol Production device, top grade Alcohol Production dress in such as Chinese patent CN200710030550.8
Put, universal energy consumption is larger, with the deterioration of national energy and water resources situation and the growing tension of global energy, it is necessary to food
Being optimized with Energy Consumption in Alcohol Production further, the energy and water resource is searched out using more rational new technology.
Content of the invention
Based on this, it is necessary to provide a kind of differential distillation energy-conservation dress of the double thick tower production top grade ethanol for being capable of reducing energy consumption
Put and its production technology.
A kind of double thick towers produce the differential distillation energy saver of top grade ethanol, including by the topping still of pipeline communication, water
Tower, rectifying column, methanol column and recovery tower is washed, the topping still includes the first topping still and the second topping still, the differential distillation
Energy saver also includes the first mash preheater, the second mash preheater, the 3rd mash preheater and the 4th mash preheater；Its
In,
The cold-side inlet of the first mash preheater goes out for ripe mash entrance, the cold end of the first mash preheater
Mouthful connect with the cold-side inlet of the second mash preheater, the cold side outlet of the second mash preheater and the 3rd wine with dregs
The cold-side inlet connection of liquid preheater, the cold side outlet of the 3rd mash preheater is connected with the charging aperture of first topping still
Logical；The top wine vapour pipeline communication of the hot-side inlet of the first mash preheater and first topping still；Second wine with dregs
The top wine vapour pipeline communication of the hot-side inlet of liquid preheater and the recovery tower, hot junction exports the refluxing opening with the recovery tower
Connection；The hot-side inlet of the 3rd mash preheater and the outlet at bottom pipeline communication of first topping still；First slightly evaporates
The side take-off mouth of pipe of tower is connected with the cold-side inlet of the 4th mash preheater, and the cold end of the 4th mash preheater goes out
Mouthful connect with the charging aperture of second topping still, the hot-side inlet of the 4th mash preheater and second topping still
Give up mash pipeline communication for bottom, and the hot junction outlet of the 4th mash preheater is with the bottom tower reactor of first topping still even
Logical.
Wherein in one embodiment, the differential distillation energy saver also includes thick wine tank；First topping still, institute
The outside for stating the second topping still, the water scrubber, the methanol column and the recovery tower is respectively connected with for providing heat again
Boiling device, respectively the first topping still reboiler, the second topping still reboiler, water scrubber reboiler, methanol column reboiler and recovery
Tower reboiler；Wherein,
The top wine vapour pipeline communication of the hot-side inlet of the first topping still reboiler and second topping still, hot junction
Outlet is connected with the thick wine tank；
The top wine steam pipe road of rectifying column hot-side inlet successively with the second topping still reboiler, the recovery
The hot-side inlet series connection of the hot-side inlet of tower reboiler and the water scrubber reboiler；The hot junction of the second topping still reboiler
Outlet, the water scrubber reboiler hot junction outlet and the recovery tower reboiler hot junction outlet respectively with the rectifying column
Refluxing opening is connected；
The top wine vapour pipeline communication of the hot-side inlet of the methanol column reboiler and the water scrubber, the one of hot junction outlet
Part is connected with the refluxing opening of the water scrubber, the miscellaneous wine of part output；
The recovery tower is connected with the thick wine tank.
Wherein in one embodiment, the differential distillation energy saver also includes that the first topping still condenser, thick wine are pre-
Hot device, light wine preheater, miscellaneous wine tank and miscellaneous wine preheater；Wherein,
The hot junction outlet of the first mash preheater is provided with gaseous phase outlet and liquid-phase outlet, wherein, the gaseous phase outlet
Connect with the first topping still condenser, the first topping still condenser and the liquid-phase outlet all with the thick wine tank
Inlet duct is connected；
The outlet conduit of the thick wine tank is sequentially connected in series with the crude wine preheater and the water scrubber；
The outlet at bottom pipeline of the water scrubber is sequentially connected in series with the light wine preheater and the rectifying column；
The outlet at bottom pipeline of the rectifying column is connected with the hot-side inlet of the light wine preheater, the light wine preheater
Hot junction outlet connect with the water scrubber and the crude wine preheater；
The outlet conduit of the miscellaneous wine tank is sequentially connected in series with the miscellaneous wine preheater and the recovery tower, the miscellaneous wine preheating
The outlet at bottom pipeline communication of the hot-side inlet of device and the recovery tower.
Wherein in one embodiment, the differential distillation energy saver also includes that fusel oil cooler and fusel are separating of oil
Device；Between the recovery tower, the fusel oil cooler and the fusel oil eliminator, connection is circulated successively by pipeline.
Wherein in one embodiment, the differential distillation energy saver also includes methanol column condenser；The methanol column
Top wine steam pipe road and the circulation of reflux inlet and the methanol column condenser connect.
A kind of production technology of top grade ethanol, produces the difference of top grade ethanol using the double thick tower described in any of the above-described embodiment
Pressure energy-saving distillation device is produced.
Wherein in one embodiment, the tower top of first topping still adopts negative-pressure operation, second topping still
Tower top is using tiny structure or micro-pressure operation, and the tower top of the water scrubber is using tiny structure or micro-pressure operation, the rectifying column
Tower top adopt the tower top of positive pressure operation, the methanol column to adopt the tower top of negative-pressure operation, the recovery tower to adopt atmospheric operation.
Wherein in one embodiment, the tower top operating pressure of first topping still is -50～-20kPa, tower top temperature
50～60 DEG C, 70～85 DEG C of column bottom temperature；
The tower top operating pressure of second topping still is -20～30kPa, 90～100 DEG C of tower top temperature, column bottom temperature 95
～108 DEG C；
The tower top operating pressure of the water scrubber is -10～20kPa, 90～105 DEG C of tower top temperature, column bottom temperature 90～
105℃；
The tower top operating pressure of the rectifying column is 180～320kPa, 105～120 DEG C of tower top temperature, column bottom temperature 130
～155 DEG C；
The tower top operating pressure of the methanol column is -50～10kPa, 60～80 DEG C of tower top temperature, column bottom temperature 70～100
℃；
The tower top operating pressure of the recovery tower is 0～30kPa, 70～80 DEG C of tower top temperature, column bottom temperature 100～115
℃.
Wherein in one embodiment, the production technology specifically includes following steps：
From the ripe mash that fermentation workshop section comes, pre- through the first mash preheater, the second mash preheater and the 3rd mash
The first topping still is entered after hot device preheating, a top side take-off device extraction part of the ripe mash by the first topping still,
The second topping still is entered after the preheating of the 4th mash preheater, the first topping still top wine vapour is cold in the first mash preheater
Solidifying, uncooled wine vapour is all condensed in the first topping still condenser, and in the first topping still condenser, wine vapour condensed fluid enters thick
Wine tank, the first topping still bottom is given up after mash is used in the 3rd mash preheater preheating ripe mash and goes wastewater treatment working section；
The top wine vapour of the second topping still is condensed in the first topping still reboiler, and condensed fluid enters thick wine tank, the second topping still bottom
Tower of the useless mash in the 4th mash preheater for going the tower reactor of the first topping still after preheating ripe mash, with the first topping still
Kettle gives up, and mash is outer together to be arranged；Thick wine in thick wine tank enters water scrubber after crude wine preheater preheating, and washing top of tower wine vapour exists
Condense in methanol column reboiler, part is miscellaneous is back to washing top of tower after drinking for condensed fluid extraction, from washing tower bottom out light
Wine, enters in rectifying column after the preheating of light wine preheater；Rectifying column top wine vapour is successively in the second topping still reboiler, recovery tower
Condense in reboiler and water scrubber reboiler, condensed fluid is back to rectifying column top, partly become from the extraction of rectifying column middle and upper part column plate
Sample wine and progress greatly into methanol column；Methanol top of tower wine vapour is flowed back after the industrial alcohol of condensed fluid extraction part through circulating cooling water condensation
To methanol top of tower, from the qualified top grade finished product ethanol of methanol tower bottom extraction, finished product tank field is sent into after cooling；From water scrubber
The miscellaneous wine for producing in the middle part of backflow, rectifying column enters miscellaneous wine tank, enters recovery tower after the preheating of miscellaneous wine preheater；From in the middle part of recovery tower
Ethanol of the extraction rich in Alcohols,fusel, enters Alcohols,fusel separator after the cooling of fusel oil cooler, leads in fusel oil eliminator
Cross addition dilution water and Alcohols,fusel is separated, the light wine after separation Alcohols,fusel then enters recovery tower and steaming is returned, and produces from top of tower is reclaimed
Wine liquid enter thick wine tank.
Wherein in one embodiment, the rectifying column provides thermic load by the primary steam from boiler.
Above-mentioned double thick towers produce the differential distillation energy saver of top grade ethanol and its production technology by using double topping stills,
The top wine vapour of the first topping still, the top wine vapour of recovery tower, the first topping still bottom give up mash can be respectively used to the first wine with dregs
Ripe mash in liquid preheater, the second mash preheater and the 3rd mash preheater is preheated, the bottom of the second topping still
Useless mash can be used for the ripe mash in the 4th mash preheater after the 4th mash preheater and be preheated, and it is laggard to lower the temperature
Enter the tower reactor of the first topping still, discharge after the 3rd mash preheater together with the useless mash in the first topping still tower reactor.Should
Device and production technology produce high grade edible spirit by configuring two topping stills, can make full use of the first topping still and recovery
The give up heat of mash of the top wine vapour of tower and the first topping still, the bottom of the second topping still is preheated to ripe mash, is adopted
With differential pressure multiple-effect thermal coupling process optimization Distallation systm energy expenditure, plant energy consumption can be significantly reduced, with save energy
Beneficial effect.
Additionally, the alcohol steam of rectifying column tower top passes sequentially through the second topping still reboiler, recovery tower reboiler, water scrubber
The second topping still of reboiler indirectly heat, recovery tower, water scrubber；Second topping still top wine vapour passes through the first topping still reboiler
The first topping still of indirectly heat；Water scrubber wine vapour passes through methanol column reboiler indirectly heat methanol column；Rectifying column waste water is first passed through
The preheating rectifying column light wine charging of light wine preheater, is further divided into two parts, and a part is used as water scrubber slurry, and remainder is pre-
After the charging of hot water wash tower thick wine as other workshops process water or outer arrange, the heats pair such as wine vapour can be made full use of further
Miscellaneous part is heated, and reaches the purpose for saving energy consumption.
The device and production technology are than traditional top grade Alcohol Production device, and its energy expenditure can be reduced to 1.8 tons of steamings
Vapour/ton finished product ethanol, circulation water consumption can be reduced to 80 ton/ton finished product ethanol, than only configuring five tower differential pressures of single thick tower at present
The distillation technique saving energy 20% of production high grade edible spirit.
Description of the drawings
Fig. 1 is the structural representation of the differential distillation energy saver of the double thick tower production top grade ethanol of an embodiment, in figure
Arrow represents the flow direction of liquid and/or steam.
Description of reference numerals is as follows：
1：First mash preheater；2：Second mash preheater；3：3rd mash preheater；4：First topping still；5：The
One topping still reboiler；6：First topping still condenser；7：4th mash preheater；8：Second topping still；9：Second topping still
Reboiler；10：Thick wine tank；11：Crude wine preheater；12：Water scrubber；13：Water scrubber reboiler；14：Light wine preheater；15：Essence
Evaporate tower；16：Methanol column；17：Methanol column reboiler；18：Methanol column condenser；19：Miscellaneous wine tank；20：Miscellaneous wine preheater；21：Return
Receive tower；22：Recovery tower reboiler；23：Fusel oil condenser；24：Fusel oil eliminator.
Specific embodiment
For the ease of understanding the present invention, below with reference to relevant drawings, the present invention is described more fully.In accompanying drawing
Give presently preferred embodiments of the present invention.But, the present invention can be realized in many different forms, however it is not limited to this paper institute
The embodiment of description.On the contrary, the purpose for providing these embodiments is to make the understanding to the disclosure more thorough
Comprehensively.
Unless otherwise defined, all of technology used herein and scientific terminology and the technical field for belonging to the present invention
The implication that technical staff is generally understood that is identical.The term for being used in the description of the invention herein is intended merely to description tool
The purpose of the embodiment of body, it is not intended that in the restriction present invention.Term as used herein "and/or" includes one or more phases
The arbitrary and all of combination of the Listed Items of pass.
As shown in figure 1, the differential distillation energy saver of the double thick tower production top grade ethanol of an embodiment includes the first mash
Preheater 1, the second mash preheater 2, the 3rd mash preheater 3, the first topping still 4, the first topping still reboiler 5, first are thick
Evaporate tower condenser 6, the 4th mash preheater 7, the second topping still 8, the second topping still reboiler 9, thick wine tank 10, crude wine preheater
11st, water scrubber 12, water scrubber reboiler 13, light wine preheater 14, rectifying column 15, methanol column 16, methanol column reboiler 17, methanol
Tower condenser 18, miscellaneous wine tank 19, miscellaneous wine preheater 20, recovery tower 21, recovery tower reboiler 22, fusel oil condenser 23 and fusel
Oil eliminator 24.The first mash preheater 1 of the present embodiment, the second mash preheater 2, the 3rd mash preheater 3 constitute three-level
Mash pre-heating system.Topping still has two, respectively above-mentioned first topping still 4 and the second topping still 8.The differential pressure of the present embodiment is steamed
Evaporate between the relevant device of energy saver and all connected by bindiny mechanisms such as pipelines.
Specifically, in the present embodiment, the cold-side inlet of the first mash preheater 1 is ripe mash entrance, the first mash
The cold side outlet of preheater 1 is connected with the cold-side inlet of the second mash preheater 2, the cold side outlet of the second mash preheater 2 with
The cold-side inlet connection of the 3rd mash preheater 3, the charging aperture of the cold side outlet of the 3rd mash preheater 3 and the first topping still 4
Connection.The top wine vapour pipeline communication of the hot-side inlet of the first mash preheater 1 and the first topping still 4.Second mash preheater 2
Hot-side inlet and recovery tower 21 top wine vapour pipeline communication, hot junction outlet is connected with the refluxing opening of recovery tower 21, for defeated
Go out part industrial alcohol.The hot-side inlet of the 3rd mash preheater 3 and the outlet at bottom pipeline communication of the first topping still 4.First
The side take-off mouth of pipe of topping still 4 is connected with the cold-side inlet of the 4th mash preheater 7, and the cold end of the 4th mash preheater 7 goes out
Mouthful connect with the charging aperture of the second topping still 8, the useless wine with dregs in the bottom of the hot-side inlet of the 4th mash preheater 7 and the second topping still 8
Liquid pipeline communication, the hot junction outlet of the 4th mash preheater 7 is connected with the bottom tower reactor of the first topping still 4.
First topping still reboiler 5, the second topping still reboiler 9, water scrubber reboiler 13, methanol column reboiler 17 and return
Receive tower reboiler 22 and be connected to the outer of the first topping still 4, the second topping still 8, water scrubber 12, methanol column 16 and recovery tower 21
Portion, to provide boiling hot amount again to corresponding equipment.In the present embodiment, the first topping still reboiler 5 is equivalent to the second topping still 8
Wine vapour condenser, the second topping still reboiler 9,21 grades of water scrubber reboilers 13 of recovery tower reboiler are respectively equivalent to rectifying column
First condenser of 15 wine vapour, the second condenser and the 3rd condenser, methanol column reboiler 17 is equivalent to the wine vapour of water scrubber 12
Condenser.
Specifically, the top wine vapour pipeline communication of the hot-side inlet of the first topping still reboiler 5 and the second topping still 8, heat
Bring out mouth to connect with thick wine tank 10.The top wine steam pipe road of rectifying column 15 hot-side inlet successively with the second topping still reboiler 9,
The hot-side inlet series connection of the hot-side inlet of recovery tower reboiler 22 and water scrubber reboiler 13.The heat of the second topping still reboiler 9
Bring out mouth, the hot junction outlet of water scrubber reboiler 13 and the hot junction outlet of recovery tower reboiler 22 backflow respectively with rectifying column 15
Mouth connection.The top wine vapour pipeline communication of the hot-side inlet of methanol column reboiler 17 and water scrubber 12, a part for hot junction outlet
Connect with the refluxing opening of water scrubber 12, the miscellaneous wine of part output.The tower top of recovery tower 21 is connected with thick wine tank 10.Rectifying column 15
Centre exit is also used for exporting miscellaneous wine.
The hot junction outlet of the first mash preheater 1 is provided with gaseous phase outlet and liquid-phase outlet, and wherein, gaseous phase outlet is thick with first
Evaporate tower condenser 6 to connect, the first topping still condenser 6 is all connected with the inlet duct of thick wine tank 10 with liquid-phase outlet.Thick wine tank
10 outlet conduit is sequentially connected in series with crude wine preheater 11 and water scrubber 12.The outlet at bottom pipeline of water scrubber 12 is preheated with light wine
Device 14 and rectifying column 15 are sequentially connected in series.The outlet at bottom pipeline of rectifying column 15 is connected with the hot-side inlet of light wine preheater 14, light
The hot junction outlet of wine preheater 14 is connected with water scrubber 12 and crude wine preheater 11.The outlet conduit of miscellaneous wine tank 19 is preheated with miscellaneous wine
Device 20 and recovery tower 21 are sequentially connected in series, the hot-side inlet of miscellaneous wine preheater 20 and the outlet at bottom pipeline communication of recovery tower 21.
Between recovery tower 21, fusel oil condenser 23 and fusel oil eliminator 24, connection is circulated successively by pipeline.Specifically
, the middle part extraction mouth of pipe of recovery tower 21 is connected with the hot-side inlet of fusel oil condenser 23, the heat of fusel oil condenser 23
Bring out mouth to be connected with fusel oil eliminator 24, the outlet at bottom pipeline of fusel oil eliminator 24 is connected with recovery tower 21.
By the circulation connection of methanol column condenser 18 between the top wine steam pipe road of methanol column 16 and reflux inlet, from methanol
The condensed fluid out of tower condenser 18 can be to be back in methanol column 16 after output par, c industrial alcohol.
The present embodiment additionally provides a kind of differential distillation energy saver using above-mentioned double thick tower production top grade ethanol and carries out
The technique of top grade Alcohol Production, the production technology in operation, specifically includes following steps：
From the ripe mash that fermentation workshop section comes, through the first mash preheater 1, the second mash preheater 2 and the 3rd mash
Preheater 3 enters the first topping still 4 after preheating, and ripe mash produces one by the top side take-off device of the first topping still 4
Part, enters the second topping still 8 after preheating through the 4th mash preheater 7, and 4 top wine vapour of the first topping still is preheated in the first mash
Condense in device 1, uncooled wine vapour is all condensed in the first topping still condenser 6, wine vapour condensation in the first topping still condenser 6
Liquid enters thick wine tank 10, and 4 bottom of the first topping still is given up after mash is used in the 3rd mash preheater 3 preheating ripe mash and goes to give up
Water process workshop section.The top wine vapour of the second topping still 8 is condensed in the first topping still reboiler 5, and condensed fluid enters thick wine tank 10,
Mash is given up for removing the tower of the first topping still 4 after preheating ripe mash in the 4th mash preheater 7 in second topping still, 8 bottom
Kettle, is given up outside together with mash with the tower reactor of the first topping still 4 and arranges.Thick wine in thick wine tank 10 is entered after the preheating of crude wine preheater 11
Water scrubber 12,12 top wine vapour of water scrubber is condensed in methanol column reboiler 17, and part is miscellaneous is back to water after drinking for condensed fluid extraction
12 top of tower is washed, from 12 bottom of water scrubber light wine out, is entered in rectifying column 15 after preheating through light wine preheater 14.Rectifying column
15 top wine vapour are condensed successively in the second topping still reboiler 9, recovery tower reboiler 22 and water scrubber reboiler 13, condensed fluid
15 top of rectifying column is back to, and methanol column 16 is entered from 15 middle and upper part column plate extraction semi-finished product ethanol of rectifying column.Methanol column 16 is pushed up
Portion's wine vapour is back to methanol column through the circulating cooling water condensation in methanol column condenser 18 after the industrial alcohol of condensed fluid extraction part
16 tops, from the qualified top grade finished product ethanol of 16 bottom of methanol column extraction, send into finished product tank field after cooling.From water scrubber 12 times
Stream (flowing back via in methanol reboiler 17), the miscellaneous wine of 15 middle part extraction of rectifying column enter miscellaneous wine tank 19, through miscellaneous wine preheater 20
Recovery tower 21 is entered after preheating.From ethanol of the 21 middle part extraction of recovery tower rich in Alcohols,fusel, after cooling down through fusel oil condenser 23
Fusel oil eliminator 24 is entered, and Alcohols,fusel is separated by adding dilution water in fusel oil eliminator 24, after separating Alcohols,fusel
Light wine then enter the steaming of recovery tower 21 times, enter thick wine tank 10 from the wine liquid of 21 top of recovery tower extraction.
In the present embodiment, the tower top of the first topping still 4 adopts negative-pressure operation, and the tower top of the second topping still 8 is using micro- negative
Pressure or micro-pressure operation, the tower top of water scrubber 12 is using tiny structure or micro-pressure operation, and the tower top of rectifying column 15 is grasped using malleation
Make, the tower top of methanol column 16 adopts the tower top of negative-pressure operation, recovery tower 21 to adopt atmospheric operation.
Specifically, rectifying column 15 provides thermic load by the primary steam from boiler.The tower top operation pressure of the first topping still 4
Power is -50～-20kPa, 50～60 DEG C of tower top temperature, 70～85 DEG C of column bottom temperature.The tower top operating pressure of the second topping still 8
For -20～30kPa, 90～100 DEG C of tower top temperature, 95～108 DEG C of column bottom temperature.The tower top operating pressure of water scrubber 12 is -10
～20kPa, 90～105 DEG C of tower top temperature, 90～105 DEG C of column bottom temperature.The tower top operating pressure of rectifying column 15 be 180～
320kPa, 105～120 DEG C of tower top temperature, 130～155 DEG C of column bottom temperature.The tower top operating pressure of methanol column 16 be -50～
10kPa, 60～80 DEG C of tower top temperature, 70～100 DEG C of column bottom temperature.The tower top operating pressure of recovery tower 21 is 0～30kPa, tower
70～80 DEG C of the temperature in top, 100～115 DEG C of column bottom temperature.
The double thick tower production differential distillation energy saver of top grade ethanol of the present embodiment and its energy coupling of production technology
Mode is：Rectifying column 15 provides thermic load by the primary steam from boiler；The alcohol steam of 15 tower top of rectifying column is passed sequentially through
Second topping still reboiler 9, recovery tower reboiler 22,13 the second topping still of indirectly heat 8, recovery tower 21 of water scrubber reboiler,
Water scrubber 12；Second topping still, 8 wine vapour passes through 5 the first topping still of indirectly heat 4 of the first topping still reboiler；12 wine vapour of water scrubber
By 17 indirectly heat methanol column 16 of methanol column reboiler；First topping still, 4 top wine vapour, 21 top wine vapour of recovery tower, first
4 bottom of the topping still mash that gives up can carry out one-level, two grades, three-level preheating to ripe mash, and wine with dregs is given up by the in 8 bottom of the second topping still
Four mash preheater 7 preheats the mash for entering the second topping still 8, is delivered to the tower reactor of the first topping still 4, useless mash system after cooling
One discharges wastewater treatment working section from 4 tower reactor of the first topping still；15 waste water of rectifying column first passes through the preheating of light wine preheater 14 and enters
The light wine of rectifying column 15, is further divided into two parts, and a part is used as 12 slurry of water scrubber, and remainder preheating water scrubber 12 is thick
As the process water in other workshops or outer arrange after wine charging.
The differential distillation energy saver of the double thick tower production top grade ethanol of the present embodiment configures two topping stills and produces top grade
Edible ethanol, using differential pressure multiple-effect thermal coupling process optimization Distallation systm energy expenditure, energy expenditure can be reduced to 1.8 tons of steamings
Vapour/ton finished product ethanol, circulation water consumption can be reduced to 80 ton/ton finished product ethanol, than only configuring five tower differential pressures of single thick tower at present
The distillation technique saving energy 20% of production high grade edible spirit.
Each technical characteristic of embodiment described above arbitrarily can be combined, for making description succinct, not to above-mentioned reality
Apply all possible combination of each technical characteristic in example to be all described, as long as however, the combination of these technical characteristics is not deposited
In contradiction, the scope of this specification record is all considered to be.
Embodiment described above only have expressed the several embodiments of the present invention, and its description is more concrete and detailed, but simultaneously
Therefore can not be construed as limiting the scope of the patent.It should be pointed out that coming for one of ordinary skill in the art
Say, without departing from the inventive concept of the premise, can also make some deformation and improve, these belong to the protection of the present invention
Scope.Therefore, the protection domain of patent of the present invention should be defined by claims.
Claims (10)
1. a kind of double thick towers produce the differential distillation energy saver of top grade ethanol, including by the topping still of pipeline communication, washing
Tower, rectifying column, methanol column and recovery tower, it is characterised in that the topping still includes the first topping still and the second topping still, described
Differential distillation energy saver also includes the first mash preheater, the second mash preheater, the 3rd mash preheater and the 4th mash
Preheater；Wherein,
The cold-side inlet of the first mash preheater is ripe mash entrance, the cold side outlet of the first mash preheater with
The cold-side inlet connection of the second mash preheater, the cold side outlet of the second mash preheater is pre- with the 3rd mash
The cold-side inlet connection of hot device, the cold side outlet of the 3rd mash preheater is connected with the charging aperture of first topping still；
The top wine vapour pipeline communication of the hot-side inlet of the first mash preheater and first topping still；Second mash is pre-
The top wine vapour pipeline communication of the hot-side inlet of hot device and the recovery tower, hot junction exports with the refluxing opening of the recovery tower even
Logical；The hot-side inlet of the 3rd mash preheater and the outlet at bottom pipeline communication of first topping still；First topping still
The side take-off mouth of pipe connect with the cold-side inlet of the 4th mash preheater, the cold side outlet of the 4th mash preheater
Connect with the charging aperture of second topping still, the hot-side inlet of the 4th mash preheater and the bottom of second topping still
Give up mash pipeline communication in portion, and the hot junction outlet of the 4th mash preheater is connected with the bottom tower reactor of first topping still.
2. double thick towers as claimed in claim 1 produce the differential distillation energy saver of top grade ethanol, it is characterised in that also include
Thick wine tank；First topping still, second topping still, the water scrubber, the outside of the methanol column and the recovery tower
The reboiler being respectively connected with for providing heat, respectively the first topping still reboiler, the second topping still reboiler, water scrubber are again
Boiling device, methanol column reboiler and recovery tower reboiler；Wherein,
The top wine vapour pipeline communication of the hot-side inlet of the first topping still reboiler and second topping still, hot junction exports
Connect with the thick wine tank；
The top wine steam pipe road of rectifying column hot-side inlet successively with the second topping still reboiler, the recovery tower are again
The hot-side inlet series connection of the hot-side inlet of boiling device and the water scrubber reboiler；The hot junction of the second topping still reboiler goes out
Mouthful, the outlet of the hot junction of the water scrubber reboiler and the hot junction outlet of the recovery tower reboiler respectively with the returning of the rectifying column
Head piece is connected；
The top wine vapour pipeline communication of the hot-side inlet of the methanol column reboiler and the water scrubber, a part for hot junction outlet
Connect with the refluxing opening of the water scrubber, the miscellaneous wine of part output；
The recovery tower is connected with the thick wine tank.
3. double thick towers as claimed in claim 2 produce the differential distillation energy saver of top grade ethanol, it is characterised in that also include
First topping still condenser, crude wine preheater, light wine preheater, miscellaneous wine tank and miscellaneous wine preheater；Wherein,
The hot junction outlet of the first mash preheater is provided with gaseous phase outlet and liquid-phase outlet, wherein, the gaseous phase outlet and institute
State the connection of the first topping still condenser, entrance of the first topping still condenser with the liquid-phase outlet all with the thick wine tank
Pipeline communication；
The outlet conduit of the thick wine tank is sequentially connected in series with the crude wine preheater and the water scrubber；
The outlet at bottom pipeline of the water scrubber is sequentially connected in series with the light wine preheater and the rectifying column；
The outlet at bottom pipeline of the rectifying column is connected with the hot-side inlet of the light wine preheater, the heat of the light wine preheater
Bring out mouth to connect with the water scrubber and the crude wine preheater；
The outlet conduit of the miscellaneous wine tank is sequentially connected in series with the miscellaneous wine preheater and the recovery tower, the miscellaneous wine preheater
The outlet at bottom pipeline communication of hot-side inlet and the recovery tower.
4. double thick towers as claimed in claim 3 produce the differential distillation energy saver of top grade ethanol, it is characterised in that also include
Fusel oil cooler and fusel oil eliminator；Between the recovery tower, the fusel oil cooler and the fusel oil eliminator
Connection is circulated successively by pipeline.
5. double thick towers as claimed in claim 4 produce the differential distillation energy saver of top grade ethanol, it is characterised in that also include
Methanol column condenser；The top wine steam pipe road of the methanol column and reflux inlet are connected with methanol column condenser circulation.
6. a kind of production technology of top grade ethanol, it is characterised in that using double thick as any one of Claims 1 to 5
The differential distillation energy saver of tower production top grade ethanol is produced.
7. the production technology of top grade ethanol as claimed in claim 6, it is characterised in that the tower top of first topping still is adopted
Negative-pressure operation, the tower top of second topping still is using tiny structure or micro-pressure operation, and the tower top of the water scrubber is using micro- negative
Pressure or micro-pressure operation, the tower top of the rectifying column adopts the tower top of positive pressure operation, the methanol column to adopt negative-pressure operation, described
The tower top of recovery tower adopts atmospheric operation.
8. the production technology of top grade ethanol as claimed in claim 7, it is characterised in that the tower top operation of first topping still
Pressure is -50～-20kPa, 50～60 DEG C of tower top temperature, 70～85 DEG C of column bottom temperature；
The tower top operating pressure of second topping still is -20～30kPa, 90～100 DEG C of tower top temperature, column bottom temperature 95～
108℃；
The tower top operating pressure of the water scrubber is -10～20kPa, 90～105 DEG C of tower top temperature, 90～105 DEG C of column bottom temperature；
The tower top operating pressure of the rectifying column is 180～320kPa, 105～120 DEG C of tower top temperature, column bottom temperature 130～155
℃；
The tower top operating pressure of the methanol column is -50～10kPa, 60～80 DEG C of tower top temperature, 70～100 DEG C of column bottom temperature；
The tower top operating pressure of the recovery tower is 0～30kPa, 70～80 DEG C of tower top temperature, 100～115 DEG C of column bottom temperature.
9. the production technology of top grade ethanol as claimed in claim 8, it is characterised in that using as claimed in claim 5 double
Thick tower produces the differential distillation energy saver of top grade ethanol, and the production technology specifically includes following steps：
From the ripe mash that fermentation workshop section comes, through the first mash preheater, the second mash preheater and the 3rd mash preheater
The first topping still is entered after preheating, and a top side take-off device extraction part of the ripe mash by the first topping still, through the
The second topping still is entered after the preheating of four mash preheaters, the first topping still top wine vapour is condensed in the first mash preheater, not
Condensation wine vapour is all condensed in the first topping still condenser, and in the first topping still condenser, wine vapour condensed fluid enters thick wine tank,
First topping still bottom is given up after mash is used in the 3rd mash preheater preheating ripe mash and goes wastewater treatment working section；Second is thick
The top wine vapour for evaporating tower is condensed in the first topping still reboiler, and condensed fluid enters thick wine tank, and give up mash for the second topping still bottom
For going the tower reactor of the first topping still after preheating ripe mash in the 4th mash preheater, with the useless wine with dregs of the tower reactor of the first topping still
Liquid is outer together to be arranged；Thick wine in thick wine tank enters water scrubber after crude wine preheater preheating, and washing top of tower wine vapour is in methanol column
Condense in reboiler, part is miscellaneous is back to washing top of tower after drinking for condensed fluid extraction, from washing tower bottom light wine out, through light
Enter in rectifying column after the preheating of wine preheater；Rectifying column top wine vapour is successively in the second topping still reboiler, recovery tower reboiler
And condense in water scrubber reboiler, condensed fluid is back to rectifying column top, produces semi-finished product ethanol from rectifying column middle and upper part column plate
Enter methanol column；Methanol top of tower wine vapour is back to methanol through circulating cooling water condensation after the industrial alcohol of condensed fluid extraction part
Top of tower, from the qualified top grade finished product ethanol of methanol tower bottom extraction, sends into finished product tank field after cooling；Flow back from water scrubber,
The miscellaneous wine for producing in the middle part of rectifying column enters miscellaneous wine tank, enters recovery tower after the preheating of miscellaneous wine preheater；Produce from the middle part of recovery tower
Ethanol rich in Alcohols,fusel, enters Alcohols,fusel separator, by adding in fusel oil eliminator after the cooling of fusel oil cooler
Enter dilution water and Alcohols,fusel is separated, the light wine after separation Alcohols,fusel then enters recovery tower and steaming is returned, from the wine for reclaiming top of tower extraction
Liquid enters thick wine tank.
10. the production technology of top grade ethanol as claimed in claim 9, it is characterised in that the rectifying column is by from boiler
Primary steam provides thermic load.
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Address after: 510640 Unit 210, Second Floor, Comprehensive Service Building of Guangzhou Science and Technology Innovation Base, No. 80 Lanyue Road, Science City, Guangzhou High-tech Industrial Development Zone, Guangdong Province Applicant after: Guangdong Zhongke Tianyuan New Energy Science & Technology Co., Ltd. Address before: 510640 Technology Integration Building, Guangzhou Institute of Energy, Chinese Academy of Sciences, No. 4 Wushan Energy Road, Tianhe District, Guangzhou City, Guangdong Province Applicant before: Guangdong Zhongke Tianyuan New Energy Science & Technology Co., Ltd. |
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Inventor after: Jiang Xinchun Inventor after: Li Jing Inventor after: Zhou Hongcai Inventor after: Tang Zhaoxing Inventor after: Li Jinying Inventor after: Gao Zhigui Inventor after: Chen Liuxin Inventor before: Li Jing Inventor before: Zhou Hongcai Inventor before: Jiang Xinchun Inventor before: Tang Zhaoxing Inventor before: Li Jinying Inventor before: Gao Zhigui Inventor before: Chen Liuxin |
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