CN104232455A - Common and superior edible alcohol co-production distillation energy-saving device and energy-saving process thereof - Google Patents
Common and superior edible alcohol co-production distillation energy-saving device and energy-saving process thereof Download PDFInfo
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- CN104232455A CN104232455A CN201410505451.0A CN201410505451A CN104232455A CN 104232455 A CN104232455 A CN 104232455A CN 201410505451 A CN201410505451 A CN 201410505451A CN 104232455 A CN104232455 A CN 104232455A
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Abstract
The invention discloses a common and superior edible alcohol co-production distillation energy-saving device and an energy-saving process thereof. The common and superior edible alcohol co-production distillation energy-saving device comprises a coarse distillation tower, a combined tower, a water scrubbing tower, a rectification tower, a methanol tower and a mash preheating device, wherein the mash preheating device, the coarse distillation tower and the combined tower are sequentially communicated with one another; the rectification tower, the water scrubbing tower and the methanol tower are sequentially communicated with one another; the mash preheating device is further communicated with the water scrubbing tower; the mash preheating device is communicated with a mature fermented mash feeding pipeline; the combined tower is provided with a common alcohol outlet, and the methanol tower is provided with a superior alcohol outlet. The common and superior edible alcohol co-production distillation energy-saving device provided by the invention can ensure flexible adjustment between common edible alcohol and superior edible alcohol, can rapidly meet market demands, and lowers steam consumption and water consumption of a whole set of distillation system.
Description
Technical field
The present invention relates to retort field, particularly relate to a kind of general level and high grade edible spirit coproduction energy-saving distillation device and energy-saving technique thereof.
Background technology
In current edible ethanol production technique, ordinary alcohol and top grade Alcohol Production be respective independently a set of Distallation systm often, when ordinary alcohol is produced separately, and the Distallation systm steam consumption about 1.8 tons of/ton of finished product alcohol, when top grade alcohol is produced separately, the Distallation systm steam consumption about 2.3 tons of/ton of finished product alcohol.Ordinary alcohol Distallation systm can not produce top grade alcohol product, and plant factor can be caused not high with top grade alcohol distillation system production ordinary alcohol product.Therefore, build the alcohol distillation device of a set of single product, can not switch product fast flexibly, and build the water distilling apparatus of two cover products according to the market requirement, its facility investment is larger again.Further, along with the growing tension of global energy and water resources, finding a kind of novel process reducing edible ethanol energy consumption and water consumption becomes the task of top priority.
Summary of the invention
Based on this, be necessary that provide one to realize product production capacity regulates flexibly between general level and high grade edible spirit, meeting the market requirement rapidly, and reduce the steam consumption of a whole set of Distallation systm and the general level of water consumption and high grade edible spirit coproduction energy-saving distillation device.
A kind of general level and high grade edible spirit coproduction energy-saving distillation device, comprise topping still, combined column, water wash column, rectifying tower, methanol column and mash primary heater unit;
Described mash primary heater unit, topping still, combined column are communicated with successively, and described rectifying tower, water wash column, methanol column are communicated with successively, and described mash primary heater unit is also communicated in described water wash column;
Described mash primary heater unit is communicated in ripe wine with dregs feed pipe, and described combined column has ordinary alcohol outlet, and described methanol column has the outlet of top grade alcohol.
Wherein in an embodiment, mash primary heater unit has mash one-level preheater, mash secondary preheater and mash three grades of preheaters, described mash one-level preheater, mash secondary preheater and mash three grades of preheaters all have cold-side inlet, cold side outlet, hot-side inlet and hot junction outlet, and the top of described topping still, combined column, water wash column, methanol column and recovery tower all has wine steam pipe road, top;
The cold-side inlet of the cold-side inlet of the cold-side inlet of ripe wine with dregs feed pipe, mash one-level preheater, the cold side outlet of mash one-level preheater, mash secondary preheater, the cold side outlet of mash secondary preheater, mash three grades of preheaters, the cold side outlet of mash three grades of preheaters and the top entry pipeline of topping still are communicated with successively;
The hot-side inlet of described mash one-level preheater also with the top wine vapour pipeline communication of topping still, the hot junction outlet of mash one-level preheater is communicated with water wash column;
The hot-side inlet of described mash three grades of preheaters is communicated with the bottom of topping still, and the hot junction outlet of described mash three grades of preheaters has wastewater treatment equipment.
Wherein in an embodiment, also comprise recovery tower, the hot-side inlet of described mash secondary preheater and the top wine vapour pipeline communication of recovery tower, the hot junction outlet of described mash secondary preheater is communicated in the overhead reflux mouth of pipe of industrial spirit discharge tube and recovery tower respectively;
Described combined column is communicated in described recovery tower, and described recovery tower is also communicated in described water wash column.
Wherein in an embodiment, the bottom of described topping still, combined column, water wash column, methanol column and recovery tower is connected to topping still reboiler, combined column reboiler, water wash column reboiler, methanol column reboiler and recovery tower reboiler for providing heat;
Described topping still reboiler, combined column reboiler, water wash column reboiler, methanol column reboiler and recovery tower reboiler all have hot-side inlet and hot junction outlet;
The hot-side inlet of described topping still reboiler and the top wine vapour pipeline communication of described combined column, the hot junction outlet of described topping still reboiler is communicated with the overhead reflux mouth of pipe of described combined column, the hot-side inlet of described combined column reboiler and the top wine vapour pipeline communication of described rectifying tower, the hot junction outlet of described combined column reboiler is communicated with the hot-side inlet of described recovery tower reboiler, the hot junction outlet of described recovery tower reboiler is communicated with the hot-side inlet of described water wash column reboiler, the hot junction outlet of described water wash column reboiler is communicated with the overhead reflux mouth of pipe of described rectifying tower, the hot-side inlet of described methanol column reboiler and the top wine vapour pipeline communication of water wash column, the hot junction outlet of described methanol column reboiler is communicated with the overhead reflux mouth of pipe of water wash column, described combined column reboiler is communicated with the overhead reflux mouth of pipe of described rectifying tower with recovery tower reboiler hot junction liquid-phase outlet.
Wherein in an embodiment, described topping still top is provided with de-gassing vessel and the side take-off device for the ripe mash of extraction;
Described mash primary heater unit has mash level Four preheater, and described mash level Four preheater has cold-side inlet, cold side outlet, hot-side inlet and hot junction outlet;
The outlet conduit of described side take-off device with the cold-side inlet of described mash level Four preheater, the cold junction of mash level Four preheater goes out and combined column is communicated with successively.
Wherein in an embodiment, also comprise assorted wine tank, assorted wine preheater, the bottom of described topping still, combined column, water wash column, methanol column and recovery tower all has outlet at bottom pipeline, the hot-side inlet of described mash three grades of preheaters and the outlet at bottom pipeline communication of topping still, the outlet at bottom pipeline of described combined column with the hot-side inlet of described mash level Four preheater, the hot junction of mash level Four preheater exports and the bottom of topping still is communicated with successively;
Described assorted wine tank, serial communication is between described combined column, recovery tower successively for assorted wine preheater, and the outlet at bottom pipeline of described recovery tower is also communicated in described assorted wine preheater, and described assorted wine preheater also has the outer relief outlet for outer row;
Middle part, the water wash column backflow mouth of pipe of described rectifying tower are also connected to the recovery of described assorted wine tank for assorted wine.
Wherein in an embodiment, also comprise topping still condenser, thick wine tank, crude wine preheater, light wine preheater and methanol column condenser, described topping still condenser, thick wine tank and crude wine preheater are series between the hot junction outlet of described mash one-level preheater and water wash column successively;
Described mash one-level preheater is also communicated in described thick wine tank, and the top of described recovery tower is also communicated in described thick wine tank;
The outlet at bottom pipeline of described rectifying tower is also communicated in described crude wine preheater, and described crude wine preheater is also communicated in the top of described water wash column;
Described light wine preheater serial communication between the outlet at bottom pipeline and described crude wine preheater of described rectifying tower, described light wine preheater also serial communication between the outlet at bottom pipeline and described rectifying tower of described water wash column;
Described methanol column condenser circulation is connected to the top of described methanol column.
Wherein in an embodiment, also comprise general level finished product water cooler, top grade finished product water cooler, potato spirit condenser and potato spirit separator;
The middle and upper part of described combined column has the middle and upper part extraction mouth of pipe, and the middle and upper part extraction mouth of pipe of described combined column is communicated with described general level finished product water cooler, and the outlet at bottom pipeline of described methanol column is communicated with top grade finished product water cooler;
To be circulated successively connection by pipeline between described recovery tower, potato spirit condenser, potato spirit separator.
The object of the present invention is to provide a kind of general level and high grade edible spirit coproduction energy-saving distillation technique.
A kind of general level and high grade edible spirit coproduction energy-saving distillation technique, comprise following steps:
Come from the ripe mash of fermentation workshop section, topping still is entered degassed after the preheating of mash primary heater unit, ripe mash after degassed is by entering combined column after the preheating of a topping still extraction part, top wine vapour condensation in mash primary heater unit of topping still, enter thick wine tank after the wine vapour condensation of topping still, the bottom of the topping still mash that gives up is disposed to wastewater treatment working section after preheating in mash primary heater unit;
Combined column top is back to after phlegma extraction part industrial spirit after the top wine vapour condensation of combined column, give up after mash preheating and enter topping still flash distillation in the bottom of combined column, from the general level finished product edible ethanol that the middle and upper part extraction of combined column is qualified, after cooling, send into finished product tank field;
From the thick wine in thick wine tank, water wash column is entered after preheating, after the top wine vapour condensation of water wash column, phlegma extraction part is assorted is back to water wash column top after drinking, weak liquor out bottom water wash column, rectifying tower is entered after preheating, after the top wine vapour condensation of rectifying tower, phlegma is back to the top of rectifying tower, methanol column is entered from the middle and upper part extraction work in-process alcohol of rectifying tower, the top of methanol column is back to after phlegma extraction part industrial spirit after the top wine vapour condensation of methanol column, from the top grade finished product alcohol that the bottom extraction of methanol column is qualified, finished product tank field is sent into after cooling.
Wherein in an embodiment, the tower top working pressure of topping still is-50 ~-20kPa, tower top temperature 50 ~ 60 DEG C, column bottom temperature 70 ~ 85 DEG C;
The tower top working pressure of combined column is-10 ~ 50kPa, tower top temperature 75 ~ 95 DEG C, column bottom temperature 100 ~ 115 DEG C;
The tower top working pressure of water wash column is-10 ~ 20kPa, tower top temperature 90 ~ 105 DEG C, column bottom temperature 90 ~ 105 DEG C;
The tower top working pressure of rectifying tower is 200 ~ 350kPa, tower top temperature 105 ~ 120 DEG C, column bottom temperature 130 ~ 150 DEG C;
The tower top working pressure of methanol column is-50 ~ 10kPa, tower top temperature 60 ~ 80 DEG C, column bottom temperature 70 ~ 100 DEG C.
The Energy Coupling mode of the general level that the present invention relates to and high grade edible spirit coproduction energy-saving distillation device is: topping still is negative-pressure operation, and combined column is normal pressure or micro-pressure operation, water wash column is normal pressure or micro-pressure operation, rectifying tower are pressurized operation, methanol column is negative-pressure operation, recovery tower is atmospheric operation.Rectifying tower provides thermal load by the primary steam from boiler; The alcohol steam of rectifying tower tower top is successively by combined column reboiler, recovery tower reboiler, water wash column reboiler indirect heating combined column, recovery tower, water wash column; Combined column wine vapour is by topping still reboiler indirect heating topping still; Water wash column wine vapour is by methanol column reboiler indirect heating methanol column; Topping still top wine vapour, recovery tower top wine vapour, the rectifying tower mash that gives up carries out one-level, secondary, three grades of preheatings to ripe wine with dregs, combined column gives up wine with dregs by mash level Four preheater preheats combined column charging mash, go topping still tower reactor after cooling, useless wine with dregs unification discharges wastewater treatment working section from topping still tower reactor; Rectifying tower waste water by the charging of light wine preheater preheats rectifying tower light wine, as water wash column bath water after cooling, remainder as other workshops process water or arrange outward.
Advantage and the effect of the general level that the present invention relates to and high grade edible spirit coproduction energy-saving distillation device are: this device can produce general level and high grade edible spirit simultaneously, can according to the Productivity Allocation of the general level of market demand flexible and high grade edible spirit.The production technique of this device adopts differential pressure multiple-effect thermal coupling mode, the general level of observable index and high grade edible spirit reduce when independently producing greatly, steam consumption is reduced to 1.4 ~ 1.6 tons of/ton of finished product alcohol, when independently producing than general level and high grade edible spirit energy-conservation 25 ~ 40%.And facility investment when independently producing than general level and high grade edible spirit greatly reduces.
The rectifying tower column bottom temperature 130 ~ 150 DEG C of the general level that the present invention relates to and high grade edible spirit coproduction energy-saving distillation device, is reduced to 0.4 ~ 0.5MPag to the requirement of steam grade, can saves high-grade steam consumption.
Accompanying drawing explanation
Fig. 1 is the general level of the embodiment of the present invention and high grade edible spirit coproduction energy-saving distillation device schematic diagram.
Description of reference numerals:
1, mash one-level preheater; 2, mash secondary preheater; 3, mash three grades of preheaters; 4, topping still; 5, topping still reboiler; 6, topping still condenser; 7, mash level Four preheater; 8, combined column; 9, combined column reboiler; 10, thick wine tank; 11, crude wine preheater; 12, water wash column; 13, water wash column reboiler; 14, light wine preheater; 15, rectifying tower; 16, methanol column; 17, methanol column reboiler; 18, methanol column condenser; 19, assorted wine tank; 20, assorted wine preheater; 21, recovery tower; 22, recovery tower reboiler; 23, potato spirit condenser; 24, potato spirit separator; 25, general level finished product water cooler; 26, top grade finished product water cooler; 27, industrial spirit pipeline; 28, assorted wine pipeline; 30, outer discharge pipe; 31, dilution water pipeline; 32, ripe wine with dregs feed pipe; 33, steam-pipe; 34, potato spirit pipeline.
Embodiment
For the ease of understanding the present invention, below with reference to relevant drawings, the present invention is described more fully.Preferred embodiment of the present invention is given in accompanying drawing.But the present invention can realize in many different forms, is not limited to embodiment described herein.On the contrary, provide the object of these embodiments be make the understanding of disclosure of the present invention more comprehensively thorough.
It should be noted that, when equipment is called as " being fixed on " another equipment, directly can there is equipment placed in the middle in it on another or also.When an equipment is considered to " connection " another equipment, it can be directly connected to another equipment or may there is equipment placed in the middle simultaneously.
Unless otherwise defined, all technology used herein and scientific terminology are identical with belonging to the implication that those skilled in the art of the present invention understand usually.The object of term used in the description of the invention herein just in order to describe specific embodiment, is not intended to be restriction the present invention.Term as used herein "and/or" comprises arbitrary and all combinations of one or more relevant Listed Items.
A kind of general level and high grade edible spirit coproduction energy-saving distillation device, comprise topping still 4, combined column 8, water wash column 12, rectifying tower 15, methanol column 16 and mash primary heater unit;
Described mash primary heater unit, topping still 4, combined column 8 are communicated with successively, and described rectifying tower 15, water wash column 12, methanol column 16 are communicated with successively, and described mash primary heater unit is also communicated in described water wash column 12;
Described mash primary heater unit is communicated in ripe wine with dregs feed pipe 32, and described combined column 8 has ordinary alcohol outlet, and described methanol column 16 has the outlet of top grade alcohol.
Further, mash primary heater unit has mash one-level preheater 1, mash secondary preheater 2 and mash three grades of preheaters 3, described mash one-level preheater 1, mash secondary preheater 2 and mash three grades of preheaters 3 all have cold-side inlet, cold side outlet, hot-side inlet and hot junction outlet, and the top of described topping still 4, combined column 8, water wash column 12, methanol column 16 and recovery tower 21 all has wine steam pipe road, top;
The wine steam pipe road, top of the cold-side inlet of the cold-side inlet of ripe wine with dregs feed pipe, mash one-level preheater 1, the cold side outlet of mash one-level preheater 1, mash secondary preheater 2, the cold side outlet of mash secondary preheater 2, the cold-side inlet of mash three grades of preheaters 3, the cold side outlet of mash three grades of preheaters 3 and topping still 4 is communicated with successively;
The hot-side inlet of described mash one-level preheater 1 also with the top wine vapour pipeline communication of topping still 4, the hot junction outlet of mash one-level preheater 1 is communicated with water wash column 12;
The hot-side inlet of described mash three grades of preheaters 3 is communicated with the bottom of topping still 4, and the hot junction outlet of described mash three grades of preheaters 3 has wastewater treatment equipment.
Further, also comprise recovery tower 21, the hot-side inlet of described mash secondary preheater 2 and the top wine vapour pipeline communication of recovery tower 21, the hot junction outlet of described mash secondary preheater 2 is communicated in the overhead reflux mouth of pipe of industrial spirit discharge tube and recovery tower 21 respectively; The hot junction of described mash secondary preheater 2 exports the pipeline be communicated with the overhead reflux mouth of pipe of recovery tower 21 and is also communicated with industrial spirit pipeline 27.
Described combined column 8 is communicated in described recovery tower 21, and described recovery tower 21 is also communicated in described water wash column 12.
Further, the bottom of described topping still 4, combined column 8, water wash column 12, methanol column 16 and recovery tower 21 is connected to topping still reboiler 5, combined column reboiler 9, water wash column reboiler 13, methanol column reboiler 17 and the recovery tower reboiler 22 for providing heat;
Described topping still reboiler 5, combined column reboiler 9, water wash column reboiler 13, methanol column reboiler 17 and recovery tower reboiler 22 all have hot-side inlet and hot junction outlet;
The hot-side inlet of described topping still reboiler 5 and the top wine vapour pipeline communication of described combined column 8, the hot junction outlet of described topping still reboiler 5 is communicated with the overhead reflux mouth of pipe of described combined column 8, the hot-side inlet of described combined column reboiler 9 and the top wine vapour pipeline communication of described rectifying tower 15, the hot junction outlet of described combined column reboiler 9 is communicated with the hot-side inlet of described recovery tower reboiler 22, the hot junction outlet of described recovery tower reboiler 22 is communicated with the hot-side inlet of described water wash column reboiler 13, the hot junction outlet of described water wash column reboiler 13 is communicated with the overhead reflux mouth of pipe of described rectifying tower 15, the hot-side inlet of described methanol column reboiler 17 and the top wine vapour pipeline communication of water wash column 12, the hot junction outlet of described methanol column reboiler 17 is communicated with the overhead reflux mouth of pipe of water wash column 12, described combined column reboiler 9 is communicated with the overhead reflux mouth of pipe of described rectifying tower 15 with recovery tower reboiler 22 hot junction liquid-phase outlet.Industrial spirit pipeline 27 is also communicated with between the hot junction outlet of described topping still reboiler 5 and the overhead reflux inlet duct of combined column 8.Assorted wine pipeline 28 is also communicated with, for being communicated to described assorted wine tank 19 between the hot junction outlet of described methanol column reboiler 17 and the overhead reflux inlet duct of water wash column 12.
Further, described topping still 4 top is provided with de-gassing vessel and the side take-off device for the ripe mash of extraction;
Described mash primary heater unit has mash level Four preheater 7, and described mash level Four preheater 7 has cold-side inlet, cold side outlet, hot-side inlet and hot junction outlet;
The outlet conduit of described side take-off device with the cold-side inlet of described mash level Four preheater 7, the cold junction of mash level Four preheater 7 goes out and combined column 8 is communicated with successively.
Further, also comprise assorted wine tank 19, assorted wine preheater 20, the bottom of described topping still 4, combined column 8, water wash column 12, methanol column 16 and recovery tower 21 all has outlet at bottom pipeline, the hot-side inlet of described mash three grades of preheaters 3 and the outlet at bottom pipeline communication of topping still 4, the outlet at bottom pipeline of described combined column 8 with the hot-side inlet of described mash level Four preheater 7, the hot junction of mash level Four preheater 7 exports and the bottom of topping still 4 is communicated with successively;
Described assorted wine tank 19, assorted wine preheater 20 successively serial communication between described combined column 8, recovery tower 21, the outlet at bottom pipeline of described recovery tower 21 is also communicated in described assorted wine preheater 20, and described assorted wine preheater 20 also has the outer discharge pipe 30 for outer row;
The middle part of described rectifying tower 15, water wash column 12 mouth of pipe that refluxes also is connected to the recovery of described assorted wine tank 19 for assorted wine.
Further, also comprise topping still condenser 6, thick wine tank 10, crude wine preheater 11, light wine preheater 14 and methanol column condenser 18, described topping still condenser 6, thick wine tank 10 and crude wine preheater 11 are series between the hot junction outlet of described mash one-level preheater 1 and water wash column 12 successively;
Described mash one-level preheater 1 is also communicated in described thick wine tank 10, and the top of described recovery tower 21 is also communicated in described thick wine tank 10;
The outlet at bottom pipeline of described rectifying tower 15 is also communicated in described crude wine preheater 11, and described crude wine preheater 11 is also communicated in the top of described water wash column 12; The middle part of described rectifying tower 15 has assorted wine pipeline 28, is communicated in described assorted wine tank 19, and the bottom of described rectifying tower 15 has steam-pipe 33 for passing into steam.
Described light wine preheater 14 serial communication is between the outlet at bottom pipeline and described crude wine preheater 11 of described rectifying tower 15, and described light wine preheater 14 goes back serial communication between the outlet at bottom pipeline and described rectifying tower 15 of described water wash column 12;
Described methanol column condenser 18 circulation is connected to the top of described methanol column 16, and the pipeline entering the top of methanol column 16 from methanol column condenser 18 is also communicated with industrial spirit pipeline 27 for taking industrial spirit.Described light wine preheater 14 also has the outer discharge pipe 30 for outer row.
Further, general level finished product water cooler 25, top grade finished product water cooler 26, potato spirit condenser 23 and potato spirit separator 24 is also comprised;
The middle and upper part of described combined column 8 has the middle and upper part extraction mouth of pipe, and the middle and upper part extraction mouth of pipe of described combined column 8 is communicated with described general level finished product water cooler 25, and the outlet at bottom pipeline of described methanol column 16 is communicated with top grade finished product water cooler 26;
To be circulated successively connection by pipeline between described recovery tower 21, potato spirit condenser 23, potato spirit separator 24.Described potato spirit separator 24 also has potato spirit pipeline 34 for separating of potato spirit, and described potato spirit separator 24 also has dilution water pipeline 31 for entering dilution water.
The general level that the present invention relates to and high grade edible spirit coproduction energy-saving distillation device, the process flow that the general level related in process of production and high grade edible spirit coproduction energy-saving distillation technique have a following logistics to:
From the ripe mash that fermentation workshop section comes, through mash one-level preheater 1, mash secondary preheater 2, mash three grades of preheaters 3 enter topping still 4 after preheating successively, after ripe mash removes non-condensable gas by topping still 4 tower top de-gassing vessel, by a topping still 4 tower top side take-off device extraction part, combined column 8 is entered after the preheating of mash level Four preheater 7, the condensation in mash one-level preheater 1 of topping still 4 top wine vapour, heat of condensation is used for preheating mash, uncooled wine vapour is whole condensation in topping still condenser 6, thick wine vapour phlegma enters thick wine tank 10, concentrated wine liquid simultaneously from recovery tower 21 top extraction also enters thick wine tank 10, bottom topping still 4, useless mash goes wastewater treatment working section after the charging of preheating mash in mash three grades of preheaters 3,
The condensation in topping still reboiler 5 of combined column 8 top wine vapour, heat of condensation is for heating topping still 4, combined column 8 top is back to after phlegma extraction part industrial spirit, bottom combined column 8, useless mash goes topping still 4 tower reactor after the charging of preheating mash in mash level Four preheater 7, from the general level finished product edible ethanol that the column plate extraction of combined column 8 middle and upper part is qualified, after general level finished product water cooler 25 cooling, send into finished product tank field;
From the thick wine in thick wine tank 10, enter after crude wine preheater 11 preheating in water wash column 12, the condensation in methanol column reboiler 17 of water wash column 12 top wine vapour, heat of condensation is used for heating methanol tower 16, phlegma extraction part is assorted is back to water wash column 12 top after drinking, weak liquor out bottom water wash column 12, enters in rectifying tower 15 after light wine preheater 14 preheating; The condensation in combined column reboiler 9, recovery tower reboiler 22, water wash column reboiler 13 successively of rectifying tower 15 top wine vapour, heat of condensation is used for heating in combination tower 8, recovery tower 21, water wash column 12, phlegma is back to rectifying tower 15 top, enters methanol column 16 from rectifying tower 15 middle and upper part column plate extraction work in-process alcohol; Methanol column 16 top wine vapour in methanol column condenser 18 through circulating cooling water condensation, methanol column 16 top is back to after phlegma extraction part industrial spirit, the top grade finished product alcohol that extraction is qualified bottom methanol column 16, sends into finished product tank field after top grade finished wine essence water cooler 26 cools;
In the middle part of combined column 8, water wash column 12 refluxes, impurity is rich in extraction in the middle part of rectifying tower 15 assorted wine enters assorted wine tank 19, and assorted wine enters recovery tower 21 after wine preheater 20 preheating of mixing; In the middle part of recovery tower 21, the assorted wine of potato spirit is rich in extraction, potato spirit separator 24 is entered after potato spirit condenser 23 cools, in potato spirit separator 24, separate potato spirit by adding dilution water, the light wine be separated after potato spirit then enters recovery tower and steams for 21 times.
The each tower operational condition of alcohol distillation is:
Topping still 4 tower top working pressure is-50 ~-20kPa, tower top temperature 50 ~ 60 DEG C, column bottom temperature 70 ~ 85 DEG C;
Combined column 8 tower top working pressure is-10 ~ 50kPa, tower top temperature 75 ~ 95 DEG C, column bottom temperature 100 ~ 115 DEG C;
Water wash column 12 tower top working pressure is-10 ~ 20kPa, tower top temperature 90 ~ 105 DEG C, column bottom temperature 90 ~ 105 DEG C;
Rectifying tower 15 tower top working pressure is 200 ~ 350kPa, tower top temperature 105 ~ 120 DEG C, column bottom temperature 130 ~ 150 DEG C;
Methanol column 16 tower top working pressure is-50 ~ 10kPa, tower top temperature 60 ~ 80 DEG C, column bottom temperature 70 ~ 100 DEG C;
Recovery tower 21 tower top working pressure is 0 ~ 30kPa, tower top temperature 70 ~ 80 DEG C, column bottom temperature 100 ~ 115 DEG C.
The Energy Coupling mode of the general level that the present invention relates to and high grade edible spirit coproduction energy-saving distillation device is: topping still is negative-pressure operation, and combined column is normal pressure or micro-pressure operation, water wash column is normal pressure or micro-pressure operation, rectifying tower are pressurized operation, methanol column is negative-pressure operation, recovery tower is atmospheric operation.Rectifying tower provides thermal load by the primary steam from boiler; The alcohol steam of rectifying tower tower top is successively by combined column reboiler, recovery tower reboiler, water wash column reboiler indirect heating combined column, recovery tower, water wash column; Combined column wine vapour is by topping still reboiler indirect heating topping still; Water wash column wine vapour is by methanol column reboiler indirect heating methanol column; Topping still top wine vapour, recovery tower top wine vapour, the rectifying tower mash that gives up carries out one-level, secondary, three grades of preheatings to ripe wine with dregs, combined column gives up wine with dregs by mash level Four preheater preheats combined column charging mash, go topping still tower reactor after cooling, useless wine with dregs unification discharges wastewater treatment working section from topping still tower reactor; Rectifying tower waste water by the charging of light wine preheater preheats rectifying tower light wine, as water wash column bath water after cooling, remainder as other workshops process water or arrange outward.
Advantage and the effect of the general level that the present invention relates to and high grade edible spirit coproduction energy-saving distillation device are: this device can produce general level and high grade edible spirit simultaneously, can according to the Productivity Allocation of the general level of market demand flexible and high grade edible spirit.The production technique of this device adopts differential pressure multiple-effect thermal coupling mode, the general level of observable index and high grade edible spirit reduce when independently producing greatly, steam consumption is reduced to 1.4 ~ 1.6 tons of/ton of finished product alcohol, when independently producing than general level and high grade edible spirit energy-conservation 25 ~ 40%.And facility investment when independently producing than general level and high grade edible spirit greatly reduces.
The rectifying tower column bottom temperature 130 ~ 150 DEG C of the general level that the present invention relates to and high grade edible spirit coproduction energy-saving distillation device, is reduced to 0.4 ~ 0.5MPag to the requirement of steam grade, can saves high-grade steam consumption.
The above embodiment only have expressed several embodiment of the present invention, and it describes comparatively concrete and detailed, but therefore can not be interpreted as the restriction to the scope of the claims of the present invention.It should be pointed out that for the person of ordinary skill of the art, without departing from the inventive concept of the premise, can also make some distortion and improvement, these all belong to protection scope of the present invention.Therefore, the protection domain of patent of the present invention should be as the criterion with claims.
Claims (10)
1. general level and a high grade edible spirit coproduction energy-saving distillation device, is characterized in that, comprise topping still, combined column, water wash column, rectifying tower, methanol column and mash primary heater unit;
Described mash primary heater unit, topping still, combined column are communicated with successively, and described rectifying tower, water wash column, methanol column are communicated with successively, and described mash primary heater unit is also communicated in described water wash column;
Described mash primary heater unit is communicated in ripe wine with dregs feed pipe, and described combined column has ordinary alcohol outlet, and described methanol column has the outlet of top grade alcohol.
2. general level according to claim 1 and high grade edible spirit coproduction energy-saving distillation device, it is characterized in that, mash primary heater unit has mash one-level preheater, mash secondary preheater and mash three grades of preheaters, described mash one-level preheater, mash secondary preheater and mash three grades of preheaters all have cold-side inlet, cold side outlet, hot-side inlet and hot junction outlet, and the top of described topping still, combined column, water wash column, methanol column and recovery tower all has wine steam pipe road, top;
The cold-side inlet of the cold-side inlet of the cold-side inlet of ripe wine with dregs feed pipe, mash one-level preheater, the cold side outlet of mash one-level preheater, mash secondary preheater, the cold side outlet of mash secondary preheater, mash three grades of preheaters, the cold side outlet of mash three grades of preheaters and the top entry pipeline of topping still are communicated with successively;
The hot-side inlet of described mash one-level preheater also with the top wine vapour pipeline communication of topping still, the hot junction outlet of mash one-level preheater is communicated with water wash column;
The hot-side inlet of described mash three grades of preheaters is communicated with the bottom of topping still, and the hot junction outlet of described mash three grades of preheaters has wastewater treatment equipment.
3. general level according to claim 2 and high grade edible spirit coproduction energy-saving distillation device, it is characterized in that, also comprise recovery tower, the hot-side inlet of described mash secondary preheater and the top wine vapour pipeline communication of recovery tower, the hot junction outlet of described mash secondary preheater is communicated in the overhead reflux mouth of pipe of industrial spirit discharge tube and recovery tower respectively;
Described combined column is communicated in described recovery tower, and described recovery tower is also communicated in described water wash column.
4. general level according to claim 3 and high grade edible spirit coproduction energy-saving distillation device, it is characterized in that, the bottom of described topping still, combined column, water wash column, methanol column and recovery tower is connected to topping still reboiler, combined column reboiler, water wash column reboiler, methanol column reboiler and recovery tower reboiler for providing heat;
Described topping still reboiler, combined column reboiler, water wash column reboiler, methanol column reboiler and recovery tower reboiler all have hot-side inlet and hot junction outlet;
The hot-side inlet of described topping still reboiler and the top wine vapour pipeline communication of described combined column, the hot junction outlet of described topping still reboiler is communicated with the overhead reflux mouth of pipe of described combined column, the hot-side inlet of described combined column reboiler and the top wine vapour pipeline communication of described rectifying tower, the hot junction outlet of described combined column reboiler is communicated with the hot-side inlet of described recovery tower reboiler, the hot junction outlet of described recovery tower reboiler is communicated with the hot-side inlet of described water wash column reboiler, the hot junction outlet of described water wash column reboiler is communicated with the overhead reflux mouth of pipe of described rectifying tower, the hot-side inlet of described methanol column reboiler and the top wine vapour pipeline communication of water wash column, the hot junction outlet of described methanol column reboiler is communicated with the overhead reflux mouth of pipe of water wash column, described combined column reboiler is communicated with the overhead reflux mouth of pipe of described rectifying tower with recovery tower reboiler hot junction liquid-phase outlet.
5. general level according to claim 2 and high grade edible spirit coproduction energy-saving distillation device, is characterized in that, described topping still top is provided with de-gassing vessel and the side take-off device for the ripe mash of extraction;
Described mash primary heater unit has mash level Four preheater, and described mash level Four preheater has cold-side inlet, cold side outlet, hot-side inlet and hot junction outlet;
The outlet conduit of described side take-off device with the cold-side inlet of described mash level Four preheater, the cold junction of mash level Four preheater goes out and combined column is communicated with successively.
6. general level according to claim 4 and high grade edible spirit coproduction energy-saving distillation device, it is characterized in that, also comprise assorted wine tank, assorted wine preheater, the bottom of described topping still, combined column, water wash column, methanol column and recovery tower all has outlet at bottom pipeline, the hot-side inlet of described mash three grades of preheaters and the outlet at bottom pipeline communication of topping still, the outlet at bottom pipeline of described combined column with the hot-side inlet of described mash level Four preheater, the hot junction of mash level Four preheater exports and the bottom of topping still is communicated with successively;
Described assorted wine tank, serial communication is between described combined column, recovery tower successively for assorted wine preheater, and the outlet at bottom pipeline of described recovery tower is also communicated in described assorted wine preheater, and described assorted wine preheater also has the outer relief outlet for outer row;
Middle part, the water wash column backflow mouth of pipe of described rectifying tower are also connected to the recovery of described assorted wine tank for assorted wine.
7. general level according to claim 6 and high grade edible spirit coproduction energy-saving distillation device, it is characterized in that, also comprise topping still condenser, thick wine tank, crude wine preheater, light wine preheater and methanol column condenser, described topping still condenser, thick wine tank and crude wine preheater are series between the hot junction outlet of described mash one-level preheater and water wash column successively;
Described mash one-level preheater is also communicated in described thick wine tank, and the top of described recovery tower is also communicated in described thick wine tank;
The outlet at bottom pipeline of described rectifying tower is also communicated in described crude wine preheater, and described crude wine preheater is also communicated in the top of described water wash column;
Described light wine preheater serial communication between the outlet at bottom pipeline and described crude wine preheater of described rectifying tower, described light wine preheater also serial communication between the outlet at bottom pipeline and described rectifying tower of described water wash column;
Described methanol column condenser circulation is connected to the top of described methanol column.
8. general level according to claim 6 and high grade edible spirit coproduction energy-saving distillation device, is characterized in that, also comprises general level finished product water cooler, top grade finished product water cooler, potato spirit condenser and potato spirit separator;
The middle and upper part of described combined column has the middle and upper part extraction mouth of pipe, and the middle and upper part extraction mouth of pipe of described combined column is communicated with described general level finished product water cooler, and the outlet at bottom pipeline of described methanol column is communicated with top grade finished product water cooler;
To be circulated successively connection by pipeline between described recovery tower, potato spirit condenser, potato spirit separator.
9. general level and a high grade edible spirit coproduction energy-saving distillation technique, is characterized in that, comprise following steps:
Come from the ripe mash of fermentation workshop section, topping still is entered degassed after the preheating of mash primary heater unit, ripe mash after degassed is by entering combined column after the preheating of a topping still extraction part, top wine vapour condensation in mash primary heater unit of topping still, enter thick wine tank after the wine vapour condensation of topping still, the bottom of the topping still mash that gives up is disposed to wastewater treatment working section after preheating in mash primary heater unit;
Combined column top is back to after phlegma extraction part industrial spirit after the top wine vapour condensation of combined column, give up after mash preheating and enter topping still flash distillation in the bottom of combined column, from the general level finished product edible ethanol that the middle and upper part extraction of combined column is qualified, after cooling, send into finished product tank field;
From the thick wine in thick wine tank, water wash column is entered after preheating, after the top wine vapour condensation of water wash column, phlegma extraction part is assorted is back to water wash column top after drinking, weak liquor out bottom water wash column, rectifying tower is entered after preheating, after the top wine vapour condensation of rectifying tower, phlegma is back to the top of rectifying tower, methanol column is entered from the middle and upper part extraction work in-process alcohol of rectifying tower, the top of methanol column is back to after phlegma extraction part industrial spirit after the top wine vapour condensation of methanol column, from the top grade finished product alcohol that the bottom extraction of methanol column is qualified, finished product tank field is sent into after cooling.
10. general level according to claim 9 and high grade edible spirit coproduction energy-saving distillation technique, is characterized in that:
The tower top working pressure of topping still is-50 ~-20kPa, tower top temperature 50 ~ 60 DEG C, column bottom temperature 70 ~ 85 DEG C;
The tower top working pressure of combined column is-10 ~ 50kPa, tower top temperature 75 ~ 95 DEG C, column bottom temperature 100 ~ 115 DEG C;
The tower top working pressure of water wash column is-10 ~ 20kPa, tower top temperature 90 ~ 105 DEG C, column bottom temperature 90 ~ 105 DEG C;
The tower top working pressure of rectifying tower is 200 ~ 350kPa, tower top temperature 105 ~ 120 DEG C, column bottom temperature 130 ~ 150 DEG C;
The tower top working pressure of methanol column is-50 ~ 10kPa, tower top temperature 60 ~ 80 DEG C, column bottom temperature 70 ~ 100 DEG C.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106422388A (en) * | 2016-10-26 | 2017-02-22 | 广东中科天元新能源科技有限公司 | Differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and production technology of high-quality alcohol |
| 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 |
| CN108504526A (en) * | 2018-05-18 | 2018-09-07 | 广东省九江酒厂有限公司 | A kind of energy-efficient liquid distillate wine continuous distillation plant and distillating method |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1880435A (en) * | 2006-04-30 | 2006-12-20 | 广东中科天元再生资源工程有限公司 | Six-column differential-pressure distillation device for extra edible alcohol and process therefor |
| CN101153257A (en) * | 2007-09-27 | 2008-04-02 | 广州保捷机电有限公司 | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof |
| CN101717802A (en) * | 2009-12-18 | 2010-06-02 | 天津大学 | Energy-saving production method of bio-ethanol |
| CN203256177U (en) * | 2013-05-23 | 2013-10-30 | 肥城金塔机械有限公司 | Alcohol preparation device |
-
2014
- 2014-09-26 CN CN201410505451.0A patent/CN104232455B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1880435A (en) * | 2006-04-30 | 2006-12-20 | 广东中科天元再生资源工程有限公司 | Six-column differential-pressure distillation device for extra edible alcohol and process therefor |
| CN101153257A (en) * | 2007-09-27 | 2008-04-02 | 广州保捷机电有限公司 | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof |
| CN101717802A (en) * | 2009-12-18 | 2010-06-02 | 天津大学 | Energy-saving production method of bio-ethanol |
| CN203256177U (en) * | 2013-05-23 | 2013-10-30 | 肥城金塔机械有限公司 | Alcohol preparation device |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106422388A (en) * | 2016-10-26 | 2017-02-22 | 广东中科天元新能源科技有限公司 | Differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and production technology of high-quality alcohol |
| CN106422388B (en) * | 2016-10-26 | 2019-02-19 | 广东中科天元新能源科技有限公司 | The differential distillation energy saver and its production technology of double thick tower production top grade alcohol |
| 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 |
| CN107903148B (en) * | 2017-10-13 | 2020-11-10 | 广东中科天元新能源科技有限公司 | Production device and production process of superior alcohol, fuel ethanol and electronic grade absolute ethanol |
| CN108504526A (en) * | 2018-05-18 | 2018-09-07 | 广东省九江酒厂有限公司 | A kind of energy-efficient liquid distillate wine continuous distillation plant and distillating method |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
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|---|---|
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Denomination of invention: Common-grade and premium-grade edible alcohol co-production distillation energy-saving device and its energy-saving process Effective date of registration: 20220914 Granted publication date: 20160203 Pledgee: Guangdong Development Bank Limited by Share Ltd. Guangzhou branch Pledgor: GUANGDONG ZHONGKE TIANYUAN NEW ENERGY SCIENCE & TECHNOLOGY Co.,Ltd. Registration number: Y2022980015192 |