CN111807931A - Energy-conserving apparatus for producing of top grade edible alcohol - Google Patents
Energy-conserving apparatus for producing of top grade edible alcohol Download PDFInfo
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- CN111807931A CN111807931A CN202010687659.4A CN202010687659A CN111807931A CN 111807931 A CN111807931 A CN 111807931A CN 202010687659 A CN202010687659 A CN 202010687659A CN 111807931 A CN111807931 A CN 111807931A
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- preheater
- rectifying
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 78
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 138
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 238000011084 recovery Methods 0.000 claims abstract description 58
- 238000004821 distillation Methods 0.000 claims abstract description 56
- 238000005406 washing Methods 0.000 claims abstract description 39
- 238000010438 heat treatment Methods 0.000 claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 claims abstract description 25
- 238000009833 condensation Methods 0.000 claims description 16
- 230000005494 condensation Effects 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 8
- 238000001704 evaporation Methods 0.000 claims description 7
- 230000008020 evaporation Effects 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 claims description 4
- 239000001760 fusel oil Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000012535 impurity Substances 0.000 description 3
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
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.
Description
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.
Example 1
The embodiment provides an energy-saving production device for top-grade edible alcohol, as shown in fig. 1, comprising a rough distillation tower 1, a rectifying tower 2, a negative pressure rectifying tower 5, a water washing tower 3, a methanol tower 4 and a recovery tower 6; the crude distillation tower 1 is connected with the water washing tower 3, and the water washing tower 3 is respectively connected with the rectifying tower 2 and the negative pressure rectifying tower 5; the rectifying tower 2 and the negative pressure rectifying tower 5 are both connected to the recovery tower 6;
the reboiler 7 of the crude distillation tower receives the alcohol vapor from the top of the methanol tower 4, the treated secondary vapor of other processes, and the steam-condensed water flash vapor of the distillation process and other processes for indirect heating of the crude distillation tower; the alcohol steam at the top of the methanol tower 4 exchanges heat in a reboiler 7 of the crude distillation tower and then flows back to the top of the methanol tower 4;
in this embodiment, the reboiler 7 of the crude distillation tower includes three reboilers, which are respectively used for receiving the alcohol steam at the top of the methanol tower, the treated secondary steam in other processes, and the flash steam of the steam condensate in the distillation process and other processes.
A reboiler 8 of the rectifying tower receives primary steam for indirectly heating the rectifying tower 2; the steam in a reboiler 8 of the rectifying tower exchanges heat and then enters a steam condensate flash tank 20, and flash evaporation is carried out to generate steam condensate flash steam;
the reboiler 9 of the water scrubber receives the alcohol vapor from the top of the rectifying tower 2 and is used for indirectly heating the water scrubber 3, and the alcohol vapor at the top of the rectifying tower 2 exchanges heat in the reboiler 9 of the water scrubber and then flows back to the top of the rectifying tower 2;
a reboiler 10 of the methanol tower receives the alcohol vapor at the top of the rectifying tower 2 and is used for indirectly heating the methanol tower 4; the alcohol vapor at the top of the rectifying tower 2 exchanges heat in a reboiler 10 of the methanol tower and then flows back to the top of the rectifying tower 2;
the reboiler 11 of the negative pressure rectifying tower receives the alcohol vapor from the top of the water scrubber 3 and is used for indirectly heating the negative pressure rectifying tower 5, and the alcohol vapor at the top of the water scrubber 3 exchanges heat in the reboiler 11 of the negative pressure rectifying tower and then flows back to the top of the water scrubber 3;
the recovery column 6 receives the condensate flash steam from the condensate flash tank 20 for heating the recovery column.
Further, the secondary steam and the steam condensation water flash steam enter a steam condensation water flash tank 20 after heat exchange in a reboiler 7 of the coarse distillation tower, and the steam condensation water flash steam is generated after flash evaporation.
Further, the recovery tower 6 can also receive the generated steam for performing supplementary heating on the recovery tower when the flash steam of the steam condensate is insufficient.
Further, the wine vapor at the top of the negative pressure rectifying tower 5 is conveyed to a condenser 16 of the negative pressure rectifying tower, and is condensed and then refluxed to the top of the negative pressure rectifying tower 5.
Further, the energy-saving production device for the high-grade edible alcohol further comprises a first-grade preheater 12, a second-grade preheater 13 and a third-grade preheater 14; the preheating medium of the primary preheater 12 is wine steam from the top of the crude distillation tower 1; the preheating medium of the secondary preheater 13 is wine vapor from the top of the recovery tower 6; the preheating medium of the three-stage preheater 14 is steam condensate flash steam from the steam condensate flash tank 20.
Further, the steam condensation water in the three-stage preheater 14 exchanges heat with flash steam and is condensed and then flows back to the boiler.
Furthermore, the liquor vapor at the top of the recovery tower 6 is subjected to heat exchange and condensation by the secondary preheater 13, then the condensate liquid flows back to the top of the recovery tower, the uncondensed liquor vapor enters the condenser 17 of the recovery tower for further condensation, and the condensate liquid flows back to the top of the recovery tower.
Furthermore, the energy-saving production device for the high-grade edible alcohol further comprises a crude wine preheater 18, after the wine vapor of the crude distillation tower exchanges heat in the primary preheater 12, the condensed crude wine enters the water washing tower 3 through the crude wine preheater 18, the uncondensed wine vapor enters a condenser 15 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 18; the preheating medium of the crude alcohol preheater 18 is from waste water discharged from the rectifying tower and high-grade edible alcohol finished products.
Further, energy-conserving apparatus for producing of high-grade edible alcohol still includes weak liquor preheater 19, weak liquor preheater connects in scrubbing tower 3 and rectifying column 2 respectively, and weak liquor preheater 19's preheating medium is rectifying column tower bottom liquid.
Example 2
The embodiment provides a method for producing high-grade edible alcohol by using the high-grade edible alcohol energy-saving production device in embodiment 1, as shown in fig. 1, the specific process is as follows:
mature mash from fermentation sequentially passes through a primary preheater 12, a secondary preheater 13 and a tertiary preheater 14 to be preheated in three stages, wherein the preheating medium of the primary preheater 12 is the top alcohol steam of a rough distillation tower, the preheating medium of the secondary preheater 13 is the top alcohol steam of a recovery tower, and the preheating medium of the tertiary preheater 14 is steam condensate flash steam;
the preheated mature mash enters a degassing section of the coarse distillation tower 1, the mash after removing carbonic acid gas and low-boiling-point impurities enters a stripping section of the coarse distillation tower 1, and distilled liquor steam enters a primary preheater 12 from the top of the tower to be used as a preheating medium for preheating the mature mash; the reboiler 7 of the crude distillation tower receives the alcohol steam from the top of the methanol tower 4, the processed secondary steam of other processes and/or the steam condensate flash steam of the distillation process and other processes, and the substances to be heated in the crude distillation tower are sent into the reboiler 7 of the crude distillation tower to exchange heat with the alcohol steam from the top of the methanol tower 4, the processed secondary steam of other processes and/or the steam condensate flash steam of the distillation process and other processes, so that the heating of the crude distillation tower is realized; the alcohol vapor at the top of the methanol tower 4 is condensed and then flows back to the top of the methanol tower 4; the secondary steam and the steam condensate flash steam enter a steam condensate flash tank 20 after exchanging heat in a reboiler 7 of the crude distillation tower, and the steam condensate flash steam is generated after flash evaporation;
after the wine vapor of the rough distillation tower exchanges heat in the primary preheater 12, condensed crude wine enters the water washing tower through the crude wine preheater 18, the uncondensed wine vapor enters the condenser 15 of the rough distillation tower and is condensed by cooling water, and the condensed crude wine enters the water washing tower 3 through the crude wine preheater 18; the preheating medium of the crude alcohol preheater 18 is from the waste water discharged from the rectifying tower and the finished product of the high-grade edible alcohol;
in a water washing tower 3, the crude wine is washed and extracted to remove impurities from the top of the tower, and the washed light wine enters the tower kettle of the water washing tower and is respectively conveyed to feed layers of a rectifying tower 2 and a negative pressure rectifying tower 5 through a pump, wherein the light wine conveyed to the rectifying tower 2 is preheated by a light wine preheater 19, and a preheating medium of the light wine preheater 19 is tower kettle liquid of the rectifying tower; the reboiler 9 of the water scrubber receives the alcohol vapor from the top of the rectifying tower 2, the substances to be heated in the water scrubber 3 are sent into the reboiler 9 of the water scrubber to exchange heat with the alcohol vapor at the top of the rectifying tower 2, and the alcohol vapor at the top of the rectifying tower 2 exchanges heat in the reboiler 9 of the water scrubber and then flows back to the top of the rectifying tower 2;
extracting miscellaneous wine rich in fusel oil from the middle parts of the rectifying tower 2 and the negative pressure rectifying tower 5, and sending the miscellaneous wine into a recovery tower 6; semi-finished liquor extracted from the top regions of the rectifying tower and the negative pressure rectifying tower enters a methanol tower 4, methanol impurities are removed through the methanol tower 4, and a top-grade edible alcohol finished product is extracted from the bottom region of the methanol tower 4;
a reboiler 8 of the rectifying tower receives primary steam, substances to be heated in the rectifying tower 2 are sent into the reboiler 8 of the rectifying tower to exchange heat with the primary steam, and the primary steam enters a steam condensate flash evaporator 20 after heat exchange; a reboiler 11 of the negative pressure rectifying tower receives the wine vapor from the top of the water washing tower 3, substances to be heated in the negative pressure rectifying tower 5 are sent into the reboiler 11 of the negative pressure rectifying tower to exchange heat with the wine vapor at the top of the water washing tower 3, and the wine vapor is condensed and then flows back to the top of the water washing tower 3; the wine vapor at the top of the negative pressure rectifying tower 5 is conveyed to a condenser 16 of the negative pressure rectifying tower, and is condensed and then reflows to the top of the negative pressure rectifying tower 5;
the steam condensate flash steam generated by the steam condensate flash tank 20 enters the recovery tower 6 and heats the recovery tower; when the flash steam of the steam condensate is insufficient, the recovery tower is subjected to supplementary heating by using the raw steam; the reboiler 10 of methanol tower receives the steam at the top of the rectifying tower 2, the substance that needs heating in the methanol tower is sent into the reboiler 10 of methanol tower and exchanges heat with the steam at the top of the rectifying tower 2, and the steam at the top of the rectifying tower 2 exchanges heat and is condensed and then flows back to the top of the rectifying tower 2.
The fusel wine rich in fusel oil extracted from the recovery tower 6 and the water washing tower 3 enters a fusel oil separator to extract fusel oil, and the light wine after extracting the fusel oil returns to the recovery tower 6.
High-concentration alcohol is extracted from the top area of the recovery tower 6 and sent to the washing tower 3 for recovery, condensate liquid generated after the alcohol vapor at the top of the recovery tower 6 is subjected to heat exchange and condensation through the secondary preheater 13 flows back to the top of the recovery tower, the uncondensed alcohol vapor enters the condenser 17 of the recovery tower for further condensation, and the condensate liquid is conveyed by a pump to flow back to the top of the recovery tower.
The rough distillation tower and the negative pressure rectifying tower operate under negative pressure.
Operating parameters of each tower:
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 ℃.
Various corresponding changes and modifications can be made by those skilled in the art based on the above technical solutions and concepts, and all such changes and modifications should be included in the protection scope of the present invention.
Claims (10)
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 ℃.
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| CN202010687659.4A CN111807931A (en) | 2020-07-16 | 2020-07-16 | Energy-conserving apparatus for producing of top grade edible alcohol |
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| CN202010687659.4A CN111807931A (en) | 2020-07-16 | 2020-07-16 | Energy-conserving apparatus for producing of top grade edible alcohol |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN109876486A (en) * | 2019-04-03 | 2019-06-14 | 广东中科天元新能源科技有限公司 | A kind of eight column differential-pressure distillation device of superfine alcohol and energy-saving processing technique |
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