阅读说明：本技术 一种优级食用酒精节能生产装置 (Energy-conserving apparatus for producing of top grade edible alcohol ) 是由 周宏才 姜新春 黎进英 刘慧生 张慧婷 姚磊 陆树浩 于 2020-07-16 设计创作，主要内容包括：本发明公开了一种优级食用酒精节能生产装置,包括粗馏塔、精馏塔、负压精馏塔、水洗塔、甲醇塔和回收塔；所述粗馏塔的再沸器接收来自甲醇塔塔顶的酒汽、二次蒸汽和/或汽凝水闪蒸汽,用于粗馏塔的间接加热；所述精馏塔的再沸器接收一次蒸汽,用于对精馏塔进行间接加热；所述水洗塔的再沸器接收来自精馏塔塔顶的酒汽,用于对水洗塔进行间接加热；所述甲醇塔的再沸器接收精馏塔塔顶的酒汽,用于对甲醇塔进行间接加热；所述负压精馏塔的再沸器接收来自水洗塔塔顶的酒汽,用于对负压精馏塔进行间接加热；回收塔接收来自汽凝水闪蒸罐的汽凝水闪蒸汽,用于对回收塔进行加热。利用本发明生产优级食用酒精,能够有效利用热源,减少蒸汽消耗。(The invention discloses a high-grade edible alcohol energy-saving production device, which comprises a rough distillation tower, a rectifying tower, a negative pressure rectifying tower, a water washing tower, a methanol tower and a recovery tower, wherein the rough distillation tower is connected with the rectifying tower; a reboiler of the crude distillation tower receives alcohol steam, secondary steam and/or steam condensate flash steam from the top of the methanol tower and is used for indirectly heating the crude distillation tower; a reboiler of the rectifying tower receives primary steam and is used for indirectly heating the rectifying tower; the reboiler of the water scrubber receives the wine vapor from the top of the rectifying tower and is used for indirectly heating the water scrubber; a reboiler of the methanol tower receives the alcohol vapor at the top of the rectifying tower and is used for indirectly heating the methanol tower; a reboiler of the negative pressure rectifying tower receives the wine vapor from the top of the water washing tower and is used for indirectly heating the negative pressure rectifying tower; the recovery tower receives the steam condensate flash steam from the steam condensate flash tank and is used for heating the recovery tower. The invention can be used for producing high-grade edible alcohol, effectively utilize heat source and reduce steam consumption.)

1. An energy-saving production device for top-grade edible alcohol is characterized by comprising a rough distillation tower, a rectifying tower, a negative pressure rectifying tower, a water washing tower, a methanol tower and a recovery tower; the rough distillation tower is connected with the water washing tower, and the water washing tower is respectively connected with the rectifying tower and the negative pressure rectifying tower; the rectifying tower and the negative pressure rectifying tower are both connected to the recovery tower;

a reboiler of the crude distillation tower receives alcohol steam, secondary steam and/or steam condensate flash steam from the top of the methanol tower and is used for indirectly heating the crude distillation tower; the alcohol vapor at the top of the methanol tower exchanges heat in a reboiler of the crude distillation tower and then flows back to the top of the methanol tower;

a reboiler of the rectifying tower receives primary steam and is used for indirectly heating the rectifying tower; the method comprises the following steps that (1) primary steam in a reboiler of a rectifying tower exchanges heat and then enters a steam condensate flash tank, and steam condensate flash steam is generated through flash evaporation;

the reboiler of the water scrubber receives the alcohol vapor from the top of the rectifying tower and is used for indirectly heating the water scrubber, and the alcohol vapor at the top of the rectifying tower exchanges heat in the reboiler of the water scrubber and then flows back to the top of the rectifying tower;

a reboiler of the methanol tower receives the alcohol vapor at the top of the rectifying tower and is used for indirectly heating the methanol tower; the alcohol vapor at the top of the rectifying tower exchanges heat in a reboiler of the methanol tower and then flows back to the top of the rectifying tower;

the reboiler of the negative pressure rectifying tower receives the alcohol vapor from the top of the water scrubber and is used for indirectly heating the negative pressure rectifying tower, and the alcohol vapor at the top of the water scrubber exchanges heat in the reboiler of the negative pressure rectifying tower and then flows back to the top of the water scrubber;

the recovery tower receives the steam condensate flash steam from the steam condensate flash tank and is used for heating the recovery tower.

2. The energy-saving production device of superior edible alcohol according to claim 1, wherein the secondary steam and the flash steam of the steam condensate enter the steam condensate flash tank after heat exchange in a reboiler of the coarse distillation tower, and the flash steam of the steam condensate is generated after flash evaporation.

3. The energy-saving production device of superior edible alcohol according to claim 1, wherein the recovery tower is further capable of receiving the generated steam for performing supplementary heating on the recovery tower when flash steam of the steam condensate is insufficient.

4. The energy-saving production device of the top-grade edible alcohol according to claim 1, wherein the alcohol vapor at the top of the negative pressure rectifying tower is conveyed to a condenser of the negative pressure rectifying tower and condensed and then flows back to the top of the negative pressure rectifying tower.

5. The energy-saving production device of superior edible alcohol according to claim 1, further comprising a primary preheater, a secondary preheater and a tertiary preheater; the preheating medium of the primary preheater is wine steam at the top of the crude distillation tower; the preheating medium of the secondary preheater comes from the wine vapor at the top of the recovery tower; the preheating medium of the three-stage preheater is steam condensate flash steam of the steam condensate flash tank.

6. The energy-saving production device of superior edible alcohol according to claim 5, wherein the flash steam of the steam condensation water in the tertiary preheater exchanges heat and then flows back to the boiler.

7. The energy-saving production device of superior edible alcohol according to claim 5, wherein after the alcohol vapor at the top of the recovery tower passes through the secondary preheater, the condensate after the heat exchange and condensation of the alcohol vapor flows back to the top of the recovery tower, the uncondensed alcohol vapor enters the condenser of the recovery tower for further condensation, and the condensate flows back to the top of the recovery tower.

8. The energy-saving production device of superior edible alcohol according to claim 5, further comprising a crude wine preheater, wherein after the wine vapor in the crude distillation tower exchanges heat in the primary preheater, the condensed crude wine enters the water washing tower through the crude wine preheater, the uncondensed wine vapor enters the condenser of the crude distillation tower and is condensed by cooling water, and the condensed crude wine enters the water washing tower through the crude wine preheater; the preheating medium of the crude alcohol preheater is from waste water discharged from the rectifying tower and high-grade edible alcohol finished products.

9. The energy-saving production device of high-grade edible alcohol according to claim 1, further comprising a light wine preheater, wherein the light wine preheater is respectively connected to the water washing tower and the rectifying tower, and light wine collected by the water washing tower enters the rectifying tower after being preheated by the light wine preheater; the preheating medium of the light wine preheater is the tower bottom liquid of the rectifying tower.

10. The energy-saving production device of top grade edible alcohol according to claim 1, wherein the operation pressure at the top of the coarse distillation tower is-85 to-10 kPa, the temperature at the top of the coarse distillation tower is 40 to 90 ℃, and the temperature at the bottom of the coarse distillation tower is 55 to 95 ℃;

the operation pressure at the top of the rectifying tower is 150-400 kPa, the temperature at the top of the rectifying tower is 100-125 ℃, and the temperature at the bottom of the rectifying tower is 120-155 ℃;

the operation pressure at the top of the negative pressure rectifying tower is-90 to-10 kPa, the temperature at the top of the tower is 45 to 75 ℃, and the temperature at the bottom of the tower is 80 to 100 ℃;

the operation pressure of the top of the washing tower is 0-100 kPa, the temperature of the top of the washing tower is 90-110 ℃, and the temperature of the bottom of the washing tower is 95-115 ℃;

the operating pressure of the top of the methanol tower is 50-150 kPa, the temperature of the top of the methanol tower is 90-105 ℃, and the temperature of the bottom of the methanol tower is 95-110 ℃;

the operation pressure at the top of the recovery tower is 0-100 kPa, the temperature at the top of the recovery tower is 80-95 ℃, and the temperature at the bottom of the recovery tower is 105-115 ℃.

Technical Field

The invention relates to the technical field of alcohol production, in particular to a high-grade edible alcohol energy-saving production device.

Background

Aiming at thick mash fermentation, the existing high-grade edible alcohol production process has limitations, heat sources cannot be reasonably utilized well, heat source waste among working procedures is caused, and steam consumption is high. Therefore, the novel process capable of reasonably utilizing redundant heat sources in other workshops is provided, and the novel process has great practical value.

Disclosure of Invention

Aiming at the defects of the prior art, the invention aims to provide a high-grade edible alcohol energy-saving production device which can effectively utilize a heat source and reduce steam consumption.

In order to achieve the purpose, the invention adopts the following technical scheme:

an energy-saving production device for high-grade edible alcohol comprises a coarse distillation tower, a rectifying tower, a negative pressure rectifying tower, a water washing tower, a methanol tower and a recovery tower; the rough distillation tower is connected with the water washing tower, and the water washing tower is respectively connected with the rectifying tower and the negative pressure rectifying tower; the rectifying tower and the negative pressure rectifying tower are both connected to the recovery tower;

a reboiler of the crude distillation tower receives alcohol steam, secondary steam and/or steam condensate flash steam from the top of the methanol tower and is used for indirectly heating the crude distillation tower; the alcohol vapor at the top of the methanol tower exchanges heat in a reboiler of the crude distillation tower and then flows back to the top of the methanol tower;

a reboiler of the rectifying tower receives primary steam and is used for indirectly heating the rectifying tower; the method comprises the following steps that (1) primary steam in a reboiler of a rectifying tower exchanges heat and then enters a steam condensate flash tank, and steam condensate flash steam is generated through flash evaporation;

the reboiler of the water scrubber receives the alcohol vapor from the top of the rectifying tower and is used for indirectly heating the water scrubber, and the alcohol vapor at the top of the rectifying tower exchanges heat in the reboiler of the water scrubber and then flows back to the top of the rectifying tower;

a reboiler of the methanol tower receives the alcohol vapor at the top of the rectifying tower and is used for indirectly heating the methanol tower; the alcohol vapor at the top of the rectifying tower exchanges heat in a reboiler of the methanol tower and then flows back to the top of the rectifying tower;

the reboiler of the negative pressure rectifying tower receives the alcohol vapor from the top of the water scrubber and is used for indirectly heating the negative pressure rectifying tower, and the alcohol vapor at the top of the water scrubber exchanges heat in the reboiler of the negative pressure rectifying tower and then flows back to the top of the water scrubber;

the recovery tower receives the steam condensate flash steam from the steam condensate flash tank and is used for heating the recovery tower.

Further, the secondary steam and the steam condensation water flash steam enter a steam condensation water flash tank after heat exchange in a reboiler of the coarse distillation tower, and the steam condensation water flash steam is generated after flash evaporation.

Further, the recovery tower can also receive raw steam for performing supplementary heating on the recovery tower when flash steam of the steam condensate is insufficient.

Further, the wine vapor at the top of the negative pressure rectifying tower is conveyed to a condenser of the negative pressure rectifying tower, and is refluxed to the top of the negative pressure rectifying tower after being condensed.

Further, the energy-saving production device for the high-grade edible alcohol further comprises a first-grade preheater, a second-grade preheater and a third-grade preheater; the preheating medium of the primary preheater is wine steam at the top of the crude distillation tower; the preheating medium of the secondary preheater comes from the wine vapor at the top of the recovery tower; the preheating medium of the three-stage preheater is steam condensate flash steam of the steam condensate flash tank.

Furthermore, the steam condensate in the three-stage preheater exchanges heat with flash steam and then flows back to the boiler.

Furthermore, after the wine vapor at the top of the recovery tower passes through the secondary preheater, the condensate after the heat exchange and condensation of the wine vapor flows back to the top of the recovery tower, the uncondensed wine vapor enters the condenser of the recovery tower for further condensation, and the condensate flows back to the top of the recovery tower.

Furthermore, the system also comprises a crude wine preheater, wherein after the wine vapor in the crude distillation tower exchanges heat in the primary preheater, the condensed crude wine enters the water washing tower through the crude wine preheater, the uncondensed wine vapor enters a condenser of the crude distillation tower and is condensed by cooling water, and the condensed crude wine enters the water washing tower through the crude wine preheater; the preheating medium of the crude alcohol preheater is from waste water discharged from the rectifying tower and high-grade edible alcohol finished products.

Furthermore, the energy-saving production device for the high-grade edible alcohol further comprises a light wine preheater, the light wine preheater is respectively connected with the water washing tower and the rectifying tower, and light wine extracted from the water washing tower enters the rectifying tower after being preheated by the light wine preheater; the preheating medium of the light wine preheater is the tower bottom liquid of the rectifying tower.

Further, the operation pressure of the top of the coarse distillation tower is-85 to-10 kPa, the temperature of the top of the coarse distillation tower is 40 to 90 ℃, and the temperature of the bottom of the coarse distillation tower is 55 to 95 ℃;

the operation pressure at the top of the rectifying tower is 150-400 kPa, the temperature at the top of the rectifying tower is 100-125 ℃, and the temperature at the bottom of the rectifying tower is 120-155 ℃;

the operation pressure at the top of the negative pressure rectifying tower is-90 to-10 kPa, the temperature at the top of the tower is 45 to 75 ℃, and the temperature at the bottom of the tower is 80 to 100 ℃;

the operation pressure of the top of the washing tower is 0-100 kPa, the temperature of the top of the washing tower is 90-110 ℃, and the temperature of the bottom of the washing tower is 95-115 ℃;

the operating pressure of the top of the methanol tower is 50-150 kPa, the temperature of the top of the methanol tower is 90-105 ℃, and the temperature of the bottom of the methanol tower is 95-110 ℃;

the operation pressure at the top of the recovery tower is 0-100 kPa, the temperature at the top of the recovery tower is 80-95 ℃, and the temperature at the bottom of the recovery tower is 105-115 ℃.

The invention has the beneficial effects that: by improving the thermal coupling mode of the production device, heat sources such as steam, steam condensate flash steam and the like from other workshop processes can be effectively utilized, the heat sources among the towers can be fully utilized, the steam consumption is effectively reduced, and the energy is saved.

Drawings

Fig. 1 is a schematic structural view of a production apparatus in embodiment 1 of the present invention.

Detailed Description

The present invention will be further described with reference to the accompanying drawings, and it should be noted that the present embodiment is based on the technical solution, and the detailed implementation and the specific operation process are provided, but the protection scope of the present invention is not limited to the present embodiment.