CN220176078U - Distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermented mash - Google Patents
Distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermented mash Download PDFInfo
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- CN220176078U CN220176078U CN202321728939.0U CN202321728939U CN220176078U CN 220176078 U CN220176078 U CN 220176078U CN 202321728939 U CN202321728939 U CN 202321728939U CN 220176078 U CN220176078 U CN 220176078U
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 190
- 238000004821 distillation Methods 0.000 title claims abstract description 32
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 305
- 239000002253 acid Substances 0.000 claims description 59
- 235000013405 beer Nutrition 0.000 claims description 47
- 238000007872 degassing Methods 0.000 claims description 44
- 239000006096 absorbing agent Substances 0.000 claims description 35
- 238000010992 reflux Methods 0.000 claims description 21
- 238000007599 discharging Methods 0.000 claims description 20
- 238000000855 fermentation Methods 0.000 claims description 11
- 230000004151 fermentation Effects 0.000 claims description 11
- 238000003795 desorption Methods 0.000 claims description 10
- 235000019441 ethanol Nutrition 0.000 abstract description 56
- 238000000034 method Methods 0.000 abstract description 11
- 230000018044 dehydration Effects 0.000 abstract description 7
- 238000006297 dehydration reaction Methods 0.000 abstract description 7
- 230000008569 process Effects 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 208000028659 discharge Diseases 0.000 description 32
- 239000007789 gas Substances 0.000 description 23
- 239000012535 impurity Substances 0.000 description 14
- 239000007788 liquid Substances 0.000 description 14
- 239000000463 material Substances 0.000 description 11
- 239000002994 raw material Substances 0.000 description 11
- 238000009833 condensation Methods 0.000 description 10
- 230000005494 condensation Effects 0.000 description 10
- 238000009835 boiling Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000001760 fusel oil Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 230000001174 ascending effect Effects 0.000 description 5
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000001913 cellulose Substances 0.000 description 4
- 229920002678 cellulose Polymers 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 239000004458 spent grain Substances 0.000 description 3
- 239000010902 straw Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 108010059892 Cellulase Proteins 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 229940106157 cellulase Drugs 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermented mash, which comprises a mature mash preheater, a negative pressure fermented mash tower, a normal pressure fermented mash tower, a rectifying tower and a superheater which are sequentially connected, wherein the outlet of the superheater is connected with the inlet of an adsorber set, the adsorber set is formed by sequentially connecting three adsorbers, the outlet of the adsorber set is connected with a positive pressure methanol removal tower through a positive pressure methanol removal tower reboiler, the positive pressure methanol removal tower is connected with the normal pressure methanol removal tower through the normal pressure methanol removal tower reboiler, and the outlet of the positive pressure methanol removal tower and the outlet of the normal pressure methanol removal tower are both connected with a finished product metering tank. The first tower of the rectifying tower is used for feeding steam, the five towers and the adsorber set work simultaneously, and the energy consumption of the processes of fermenting mash distillation concentration, hydrous ethanol dehydration and absolute ethanol methanol removal is reduced to the maximum extent.
Description
Technical Field
The utility model relates to the technical field of alcohol production, in particular to a distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermented mash.
Background
At present, domestic ethanol mainly has the following production modes: (1) The traditional production method for preparing the ethanol by taking the starch or the sugar as the raw material through fermentation. (2) The method is characterized by adopting cellulose such as straw and the like as raw materials, decomposing the raw materials by cellulase and fermenting the decomposed raw materials to prepare the ethanol. (3) The method is characterized in that coal is used as a raw material to prepare ethanol through chemical reaction. (4) The method is to prepare the ethanol by taking the waste gas of the steel mill as the raw material through fermentation. (5) The method is to prepare ethanol by taking synthesis gas as a raw material through fermentation.
The synthesis gas is generally prepared by gasifying coal at present, and can be prepared by gasifying cellulose raw materials such as straw and the like in future. Compared with the mode of preparing ethanol by fermenting cellulose such as straw and the like serving as raw materials after cellulose is decomposed, the method has great cost advantage and market prospect. The patent is a distillation system for preparing high-quality absolute ethyl alcohol by taking synthesis gas as a raw material and utilizing carbon dioxide, carbon monoxide and hydrogen in the synthesis gas to carry out biological fermentation.
Patent CN211522068U discloses a system for producing fuel ethanol by distilling low concentration fermented mash with double coarse and single refined three towers, comprising a mash preheater, a degassing section, a negative pressure mash tower, a normal pressure mash tower and a rectifying tower, wherein the concentration of the produced ethanol can reach 95% (v/v), but the ethanol also contains more methanol and more impurities. At present, a distillation device with high ethanol concentration and less impurities is needed to prepare the synthetic gas fermented mash serving as a raw material.
Disclosure of Invention
The present utility model aims to provide a distillation system for producing high quality absolute ethanol from syngas beer, in view of the above prior art.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
the utility model provides a distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermented mash, which comprises a mature mash preheater, a negative pressure fermented mash tower, a normal pressure fermented mash tower, a rectifying tower and a superheater which are sequentially connected, wherein the outlet of the superheater is connected with the inlet of an adsorber set, the adsorber set is formed by sequentially connecting three adsorbers, the outlet of the adsorber set is connected with a positive pressure methanol removal tower through a positive pressure methanol removal tower reboiler, the positive pressure methanol removal tower is connected with the normal pressure methanol removal tower through the normal pressure methanol removal tower reboiler, the positive pressure methanol removal tower reboiler is also connected with the normal pressure methanol removal tower, and the outlet of the positive pressure methanol removal tower and the outlet of the normal pressure methanol removal tower are both connected with a finished product metering tank.
Because the ethanol content in the mature mash of the biological fermentation of the synthetic gas is lower and is only 3-5% (v/v), the distillation and concentration of the fermented mash adopts a double-coarse-tower single-fine-tower distillation and concentration scheme, a negative pressure mash tower, a normal pressure mash tower and a rectifying tower are arranged, and a three-tower three-effect thermal coupling distillation process is formed among the three towers. Meanwhile, in order to obtain high-quality absolute ethyl alcohol, two absolute ethyl alcohol methanol removing towers are arranged, an absorber group is formed by three molecular sieve absorbers, a three-effect thermal coupling distillation process is formed between the absorber group and the two methanol removing towers, only one rectifying tower is used for steam inlet, and five towers and the absorber group work simultaneously, so that the energy consumption of the whole system is reduced to the greatest extent. In order to enable the absolute alcohol to reach GB/T678 high-grade pure alcohol standard, reduce the methanol content (less than or equal to 200 ppm) in a finished product, and simultaneously realize energy conservation, the system adopts two methanol removing towers for carrying out methanol removing treatment on dehydrated absolute alcohol, wherein a positive pressure methanol removing tower uses semi-finished absolute alcohol steam from an absorber group as a heat source, and a normal pressure methanol removing tower uses positive pressure methanol removing tower top steam as a heat source.
Preferably, the top part of the negative pressure mash tower is provided with an acid discharging section and a degassing section, and the acid discharging section is positioned above the degassing section; the mature mash preheater is connected with a degassing section, the degassing section is connected with a primary preheater of the normal pressure mash tower, a secondary preheater of the normal pressure mash tower and the normal pressure mash tower in sequence, and the degassing section is also connected with a degassing section condenser; the acid discharge section is connected with the acid discharge section condenser and the acid discharge section reflux tank in sequence, and the acid discharge section reflux is connected with the acid discharge section; the degassing section condenser is also connected with an acid discharge section reflux tank. The top of the negative pressure mash tower is provided with a degassing section and an acid discharging section, so that CO in the fermentation liquid can be effectively removed 2 And the volatile acid and part of low-boiling impurities can improve the oxidation time of the finished absolute ethyl alcohol and reduce the acidity of the finished absolute ethyl alcohol.
Preferably, the normal pressure beer column is connected with the negative pressure beer column reboiler, the crude wine tank, the crude wine preheater and the rectifying column in sequence.
Preferably, the negative pressure beer column reboiler is connected with the negative pressure beer column; the acid discharging section is connected with the crude wine tank; the normal pressure mash tower is also connected with the rectifying tower through a reboiler of the normal pressure mash tower.
Preferably, the rectifying tower is connected with the superheater, and the adsorber group comprises a first adsorber, a second adsorber and a third adsorber which are sequentially connected; the superheater is respectively connected with the first absorber, the second absorber and the third absorber, and the first absorber, the second absorber and the third absorber are all connected with the reboiler of the positive pressure methanol removal tower. And the dehydrated absolute ethanol vapor of the first adsorber, the second adsorber and the third adsorber supplies heat to a reboiler of the positive pressure methanol removal tower. The alcohol vapor extracted from the gas phase at the top of the rectifying tower is adsorbed and dehydrated by an adsorber set, wherein the adsorber set adopts three adsorbers, one adsorber is used for adsorption, one adsorber is used for pressurizing and the other adsorber is used for analysis, and the pressure fluctuation is small during switching, so that the stable operation of the device and the normal thermal coupling with the methanol removing tower are ensured. Compared with the dehydration process of the two adsorbers, the dehydration process of the two adsorbers has great change in operating pressure, and particularly no anhydrous alcohol vapor is output in the pressure equalizing process of the two adsorbers, so that the dehydration process of the two adsorbers cannot be thermally coupled with the methanol removal tower.
More preferably, the first adsorber, the second adsorber, and the third adsorber are each connected to a desorption condenser, and the desorption condenser is connected to a raw wine tank.
More preferably, the rectifying tower reboiler is connected with a steam pipeline, the rectifying tower reboiler is connected with a rectifying tower, and the rectifying tower reboiler is also connected with a raw wine preheater.
Preferably, the atmospheric demethanizer is connected to an atmospheric demethanizer condenser.
Mature mash from a fermentation section is preheated by a mature mash preheater and then enters a degassing section of a negative pressure mash tower, carbon dioxide, volatile acid and partial low boiling impurities in the mature mash enter the tower and are separated from the fermentation mash under the action of negative pressure, and the impurity-containing crude ethanol steam enters a degassing section condenser for condensation, and condensate of the degassing section condenser enters an acid discharge section reflux tank. The uncondensed gas was discharged to the atmosphere by a distillation vacuum pump. After the gas-removed fermented mash enters the bottom of the degassing section, a part (about 45 percent) of the fermented mash enters the negative pressure mash tower through a self-flow pipeline, and the rest of the fermented mash (about 55 percent) is sequentially sent into the normal pressure mash tower through the first-stage preheater of the normal pressure mash tower and the second-stage preheater of the normal pressure mash tower.
The deaerated fermented mash enters the negative pressure mash tower through a gravity flow pipeline, and is heated by the steam rising at the bottom of the tower while descending in the negative pressure mash tower, and the wine steam is separated from the vinasse liquid in an ascending manner. The vinasse liquid is discharged from the bottom of the tower, heated by a mature mash preheater and sent to a vinasse liquid subsequent treatment section. The part of the negative pressure crude distillation wine gas goes upward and enters the bottom of the degassing section, and the rest enters the bottom of the acid discharging section. The crude ethanol vapor at the top of the acid discharge section enters an acid discharge section condenser for condensation, condensate of the acid discharge section condenser enters an acid discharge section reflux tank, and uncondensed gas enters a distillation vacuum pump and is discharged into the atmosphere. The crude ethanol in the acid discharge section reflux tank is refluxed to the top of the acid discharge section through a reflux pump. Crude alcohol at the bottom of the acid discharging section automatically flows into the crude wine tank.
After the fermented mash extracted from the degassing section of the negative pressure mash tower is preheated in sequence by a primary preheater of the normal pressure mash tower and a secondary preheater of the normal pressure mash tower, the fermented mash is fed from the top of the normal pressure mash tower, enters the tower, descends in the normal pressure mash tower and is heated by steam ascending from the bottom of the tower, and ethanol steam ascends and is separated from the vinasse liquid. The vinasse liquid is discharged from the bottom of the tower, and after being heated by a primary preheater of the normal pressure mash tower, the vinasse liquid goes to a subsequent treatment working section; and the alcohol gas of the normal pressure beer still enters a reboiler of the negative pressure beer still for condensation, and simultaneously provides heat for the negative pressure beer still, and the condensed crude alcohol enters a crude alcohol tank.
The crude alcohol from the crude alcohol tank is preheated by the crude alcohol preheater and enters a 16 th layer tower plate of the rectifying tower, ethanol is gradually concentrated after entering the tower until the concentration of the ethanol at the top of the tower can reach more than 95% (v/v), and medium-grade impurities (fusel oil) are retained on a plurality of layers of plates above the feeding plate, are extracted and cooled, and enter a fusel oil separator to separate fusel oil. The ethanol vapor at the top of the rectifying tower enters an atmospheric pressure mash tower reboiler to be condensed, and simultaneously provides heat for the atmospheric pressure mash tower, and the condensate flows back into the top of the rectifying tower. And heating the wastewater at the bottom of the rectifying tower by a secondary preheater of the normal pressure mash tower, and then removing a sewage treatment section.
The ethanol steam with the concentration of more than 95% (v/v) is extracted from the gas phase at the top of the rectifying tower, is overheated by a superheater and then enters three molecular sieve adsorbers, namely a first adsorber, a second adsorber and a third adsorber, respectively for adsorption and dehydration, the three adsorbers alternately and circularly work, the dehydrated absolute ethanol steam enters a positive pressure methanol removal tower reboiler for condensation, and simultaneously provides heat for the positive pressure methanol removal tower, and the condensate is the semi-finished absolute ethanol and enters the middle upper part of the positive pressure methanol removal tower and the normal pressure methanol removal tower respectively in two paths. The bottoms of the first absorber, the second absorber and the third absorber are respectively connected with an analysis condenser, and the dilute ethanol generated by analysis enters a crude wine tank.
Part (about 52%) of the semi-finished absolute ethyl alcohol enters the middle part of the positive pressure methanol removal tower, after entering the tower, methanol and low boiling impurities in the semi-finished absolute ethyl alcohol enter the tower top, the ethanol vapor at the tower top is totally refluxed after being condensed by a reboiler of the normal pressure methanol removal tower, non-condensable tail gas containing a large amount of methanol enters the upper part of the normal pressure methanol removal tower, and high-quality absolute ethyl alcohol at the tower bottom is pumped out from the tower bottom, cooled and then sent into a finished product metering tank.
The rest part (about 48%) of the semi-finished absolute ethyl alcohol enters the middle part of an atmospheric pressure methanol removal tower, methanol and low boiling point impurities in the absolute ethyl alcohol enter the tower top after entering the tower, the ethanol vapor at the tower top enters a methanol removal tower condenser for condensation, and a small amount of wine heads are extracted from the methanol removal tower condenser and enter an aldehyde wine tank. And extracting high-quality absolute ethyl alcohol from the bottom of the tower, cooling, and delivering the cooled absolute ethyl alcohol into a finished product metering tank.
The steam pipeline is connected with a rectifying tower reboiler, the fresh steam heats the rectifying tower through the rectifying tower reboiler, and the fresh steam also heats the superheater. The condensation water of the rectifying tower reboiler provides heat for the crude wine preheater; ethanol steam at the top of the rectifying tower enters an atmospheric pressure mash tower reboiler and simultaneously provides heat for the atmospheric pressure mash tower; and heating the wastewater at the bottom of the rectifying tower by a secondary preheater of the normal pressure mash tower. Discharging the vinasse liquid of the normal pressure mash tower from the bottom of the tower and heating the vinasse liquid by a primary preheater of the normal pressure mash tower; and (3) feeding the crude ethanol steam at the top of the normal pressure beer still into a negative pressure beer still reboiler, and heating the negative pressure beer still. The vinasse liquid at the bottom of the negative pressure mash tower heats the mature mash preheater. And the absolute ethanol steam from the first absorber, the second absorber and the third absorber enters a reboiler of the positive pressure methanol removal tower, and the positive pressure methanol removal tower is heated. The alcohol steam at the top of the positive pressure methanol removing tower is heated by a reboiler of the normal pressure methanol removing tower.
The utility model has the beneficial effects that:
the utility model adopts a three-tower distillation concentration, molecular sieve dehydration and two-tower methanol removal process flow. A negative pressure mash tower, a normal pressure mash tower, a rectifying tower, three molecular sieve adsorbers, a positive pressure methanol removing tower and a normal pressure methanol removing tower are arranged. The whole system has one rectifying tower with one steam inlet, five towers and adsorber set to operate simultaneously, and this can reduce the energy consumption of fermenting mash distillation and concentration, dewatering water-containing alcohol and eliminating methanol of anhydrous alcohol.
The absolute ethyl alcohol obtained by the utility model reaches the standard of high-grade purity in GB/T678-2002 chemical reagent ethanol (absolute ethyl alcohol), the mass fraction of the ethanol is more than or equal to 99.8%, and the mass fraction of the methanol is less than or equal to 0.02%.
Drawings
Fig. 1: a flow chart of the present utility model;
the figure shows: 1. a rectifying tower; 2. an atmospheric beer column; 3. a negative pressure mash tower; 4. a positive pressure methanol removing tower; 5. a normal pressure methanol removing tower; 6. a rectifying column reboiler; 7. a superheater; 8. a first adsorber; 9. a second adsorber; 10. a third adsorber; 11. a crude wine preheater; 12. a second-stage preheater of the normal pressure mash tower; 13. a reboiler of the normal pressure mash tower; 14. a parse condenser; 15. an anhydrous vacuum pump; 16. a primary preheater of the normal pressure mash tower; 17. a crude wine tank; 18. a negative pressure beer column reboiler; 19. a degassing section; 20. an acid discharging section; 21. an acid discharge section condenser; 22. a distillation vacuum pump; 23. a reflux tank of an acid discharge section; 24. a degassing section condenser; 25. a matured mash preheater; 26. a positive pressure methanol removal tower reboiler; 27. a reboiler of the normal pressure methanol removing tower; 28. a condenser of the normal pressure methanol removing tower.
Detailed Description
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the utility model. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this utility model belongs.
As described in the background art, the ethanol concentration of the current ethanol production device can reach 95% (v/v), but the ethanol also contains more methanol and more impurities.
Based on the above, the utility model provides a distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermentation mash, which comprises a negative pressure mash tower 3, wherein the top part of the negative pressure mash tower 3 is provided with an acid discharging section 20 and a degassing section 19, and the acid discharging section 20 is positioned above the degassing section 19; the mature mash preheater 25 is connected with the degassing section 19 through a material pipeline, the degassing section 19 is connected with the normal pressure mash tower primary preheater 16, the normal pressure mash tower secondary preheater 12 and the normal pressure mash tower 2 in sequence through material pipelines, and the degassing section 19 is also connected with the degassing section condenser 24; the acid discharge section 20 is connected with an acid discharge section condenser 21 and an acid discharge section reflux tank 23 in sequence through a material pipeline, and the acid discharge section 20 reflux is connected with the acid discharge section 20; the degassing stage condenser 24 is also connected to an acid discharge stage reflux drum 23.
The normal pressure beer column 2 is connected with the negative pressure beer column reboiler 18, the crude wine tank 17, the crude wine preheater 11 and the rectifying column 1 in sequence through material pipelines. The negative pressure beer column reboiler 18 is connected with the negative pressure beer column 3; the acid discharging section 20 is connected with the crude wine tank 17; the normal pressure mash tower 2 is also connected with the rectifying tower 1 through a normal pressure mash tower reboiler 13.
The rectifying tower 1 is connected with the superheater 7 through a material pipeline, the superheater 7 is respectively connected with the first absorber 8, the second absorber 9 and the third absorber 10, and the first absorber 8, the second absorber 9 and the third absorber 10 are all connected with the reboiler 26 of the positive pressure methanol removal tower. The rectifying tower reboiler 6 is connected with a steam pipeline, the rectifying tower reboiler 6 is connected with the rectifying tower 1, and the rectifying tower reboiler 6 is also connected with the raw wine preheater 11. The first adsorber 8, the second adsorber 9, and the third adsorber 10 are each connected to a desorption condenser 14, and the desorption condenser 14 is connected to a raw wine tank 17.
The positive pressure methanol removal tower reboiler 26 is connected with the positive pressure methanol removal tower 4, and the positive pressure methanol removal tower reboiler 26 is also connected with the normal pressure methanol removal tower 5. The positive pressure methanol removal tower 4 is connected with the normal pressure methanol removal tower 5 through the normal pressure methanol removal tower reboiler 27. The atmospheric demethanizer 5 is connected to an atmospheric demethanizer condenser 28.
In order to enable those skilled in the art to more clearly understand the technical scheme of the present utility model, the technical scheme of the present utility model will be described in detail with reference to specific embodiments.
The test materials used in the examples of the present utility model are all conventional in the art and are commercially available.
Examples
The distillation system for preparing high-quality absolute ethyl alcohol from the synthetic gas fermented mash comprises a negative pressure mash tower 3, wherein the top part of the negative pressure mash tower 3 is provided with an acid discharging section 20 and a degassing section 19, and the acid discharging section 20 is positioned above the degassing section 19; the mature mash preheater 25 is connected with the degassing section 19 through a material pipeline, the degassing section 19 is connected with the normal pressure mash tower primary preheater 16, the normal pressure mash tower secondary preheater 12 and the normal pressure mash tower 2 in sequence through material pipelines, and the degassing section 19 is also connected with the degassing section condenser 24; the acid discharge section 20 is connected with an acid discharge section condenser 21 and an acid discharge section reflux tank 23 in sequence through a material pipeline, and the acid discharge section 20 reflux is connected with the acid discharge section 20; the degassing stage condenser 24 is also connected to an acid discharge stage reflux drum 23.
The normal pressure beer column 2 is connected with the negative pressure beer column reboiler 18, the crude wine tank 17, the crude wine preheater 11 and the rectifying column 1 in sequence through material pipelines. The negative pressure beer column reboiler 18 is connected with the negative pressure beer column 3; the acid discharging section 20 is connected with the crude wine tank 17; the normal pressure mash tower 2 is also connected with the rectifying tower 1 through a normal pressure mash tower reboiler 13.
The rectifying tower 1 is connected with the superheater 7 through a material pipeline, the superheater 7 is respectively connected with the first absorber 8, the second absorber 9 and the third absorber 10, and the first absorber 8, the second absorber 9 and the third absorber 10 are all connected with the reboiler 26 of the positive pressure methanol removal tower. The rectifying tower reboiler 6 is connected with a steam pipeline, the rectifying tower reboiler 6 is connected with the rectifying tower 1, and the rectifying tower reboiler 6 is also connected with the raw wine preheater 11. The first adsorber 8, the second adsorber 9, and the third adsorber 10 are each connected to a desorption condenser 14, and the desorption condenser 14 is connected to a raw wine tank 17.
The positive pressure methanol removal tower reboiler 26 is connected with the positive pressure methanol removal tower 4, and the positive pressure methanol removal tower reboiler 26 is also connected with the normal pressure methanol removal tower 5. The positive pressure methanol removal tower 4 is connected with the normal pressure methanol removal tower 5 through the normal pressure methanol removal tower reboiler 27. The atmospheric demethanizer 5 is connected to an atmospheric demethanizer condenser 28.
Mature mash from the fermentation section is preheated to 65 ℃ by a mature mash preheater 25 and then enters a degassing section 19 of a negative pressure mash tower 3, carbon dioxide, volatile acid and partial low boiling impurities in the mature mash after entering the tower are separated from the fermented mash under the action of negative pressure, and the impurity-containing crude ethanol steam enters a degassing section condenser 24 for condensation, and condensate of the degassing section condenser 24 enters an acid discharge section reflux tank 23. The uncondensed gases are discharged to the atmosphere by a distillation vacuum pump 22. After the gas-removed fermented mash enters the bottom of the degassing section 19, a part (about 45%) of the fermented mash enters the negative pressure mash tower 3 through a self-flow pipeline, and the rest of the fermented mash (about 55%) is sequentially sent into the normal pressure mash tower 2 through the normal pressure mash tower primary preheater 16 and the normal pressure mash tower secondary preheater 12.
The deaerated fermented mash enters the negative pressure mash tower 3 through a gravity flow pipeline, and is heated to 80 ℃ by the steam rising from the bottom of the tower while descending in the negative pressure mash tower 3, and the wine steam is separated from the vinasse liquid in an ascending manner. The spent grain is removed at the bottom of the column and the mature beer preheater 25 is heated to 65 ℃ and sent to the spent grain post-treatment section. The part of the negative pressure crude distillation wine gas after ascending enters the bottom of the degassing section 19, and the rest enters the bottom of the acid discharging section 20. The crude ethanol vapor at the top of the acid discharge section 20 enters an acid discharge section condenser 21 for condensation, condensate of the acid discharge section condenser 21 enters an acid discharge section reflux tank 23, and uncondensed gas enters a distillation vacuum pump 22 and is discharged into the atmosphere. The crude ethanol in the acid-stage reflux drum 23 is refluxed to the top of the acid-stage 20 by a reflux pump. The crude alcohol at the bottom of the acid discharging section 20 automatically flows into the crude wine tank 17.
The fermented mash extracted from the degassing section 19 of the negative pressure mash tower 3 is heated to 95 ℃ through the primary preheater 16 of the normal pressure mash tower, is heated to 100 ℃ through the secondary preheater 12 of the normal pressure mash tower, is fed from the top of the normal pressure mash tower 2, is fed into the normal pressure mash tower 2 and is heated to 105 ℃ by the steam rising from the bottom of the tower while descending in the normal pressure mash tower 2, and the ethanol steam is separated from the waste liquid in an ascending mode. The vinasse liquid is discharged from the bottom of the tower, is heated to 95 ℃ by a primary preheater 16 of the normal pressure mash tower, and goes to a subsequent treatment working section; the alcohol vapor in the normal pressure beer column 2 enters a negative pressure beer column reboiler 18 to be condensed, and meanwhile, the negative pressure beer column 3 is heated to 80 ℃, and the condensed crude alcohol enters a crude alcohol tank 17.
The crude alcohol from the crude alcohol tank 17 is preheated to 120 ℃ by the crude alcohol preheater 11, enters the 16 th layer tower plate of the rectifying tower 1, is gradually concentrated after entering the tower, and is gradually concentrated until the concentration of the alcohol at the top of the tower can reach more than 95% (v/v), and medium-grade impurities (fusel oil) are retained on a plurality of layers of plates above the feeding plate, are extracted and cooled, and enter the fusel oil separator to separate fusel oil. The ethanol vapor at the top of the rectifying tower 1 enters an atmospheric beer tower reboiler 13 to be condensed, and meanwhile, the atmospheric beer tower 2 is heated to 105 ℃, and the condensate flows back into the top of the rectifying tower 1. The wastewater at the bottom of the rectifying tower 1 heats the secondary preheater 12 of the normal pressure mash tower and then decontaminates the water treatment section.
The ethanol vapor with the concentration of more than 95% (v/v) is extracted from the gas phase at the top of the rectifying tower 1, is overheated by a heater 7, and then enters three molecular sieve adsorbers, namely a first adsorber 8, a second adsorber 9 and a third adsorber 10, respectively from bottom to top for adsorption and dehydration, the three adsorbers alternately and circularly work, the dehydrated absolute ethanol vapor enters a positive pressure methanol removal tower reboiler 26 for condensation, and meanwhile, the positive pressure methanol removal tower 4 is heated to 95 ℃, the condensate is the semi-finished absolute ethanol and enters the middle upper part of the positive pressure methanol removal tower 4 at 95 ℃ and the normal pressure methanol removal tower 5 at 80 ℃ respectively. The bottoms of the first adsorber 8, the second adsorber 9 and the third adsorber 10 are respectively connected with a desorption condenser 14, and the diluted ethanol generated by desorption enters a raw wine tank 17.
Part (about 52%) of the semi-finished absolute ethyl alcohol enters the middle part of the positive pressure methanol removal tower 4, after entering the tower, methanol and low boiling impurities in the semi-finished absolute ethyl alcohol enter the tower top, and the tower top ethanol vapor is condensed by the normal pressure methanol removal tower reboiler 27 and then flows back completely, and meanwhile, the normal pressure methanol removal tower is heated to 80 ℃; non-condensable tail gas containing a large amount of methanol enters the upper part of the normal pressure methanol removal tower 5, and high-quality absolute ethyl alcohol at the bottom of the tower is pumped out from the bottom of the tower and is cooled and then sent into a finished product metering tank.
The rest part (about 48%) of the semi-finished absolute ethyl alcohol enters the middle part of the normal pressure methanol removal tower 5, after entering the tower, methanol and low boiling point impurities in the absolute ethyl alcohol enter the tower top, the ethanol vapor at the tower top enters a methanol removal tower condenser for condensation, and a small amount of wine heads are extracted from the methanol removal tower condenser and enter an aldehyde wine tank. And extracting high-quality absolute ethyl alcohol from the bottom of the tower, cooling, and delivering the cooled absolute ethyl alcohol into a finished product metering tank.
The heating mode of the utility model: the steam pipe is connected with the rectifying tower reboiler 6, and the 160 ℃ fresh steam heats the rectifying tower reboiler 6 to 150 ℃ and the superheater 7 to 150 ℃. The crude wine preheater 11 is heated to 120 ℃ by the condensed water of the rectifying tower reboiler 6; ethanol steam at the top of the rectifying tower 1 enters an atmospheric pressure mash tower reboiler 13, and the atmospheric pressure mash tower 2 is heated to 105 ℃; the waste water at the bottom of the rectifying tower 1 heats the normal pressure beer column secondary preheater 12 to 100 ℃. Discharging the distilled liquid of the normal pressure beer column 2 from the bottom of the tower to heat the primary preheater 16 of the normal pressure beer column to 95 ℃; the crude ethanol steam at the top of the normal pressure beer column 2 enters a negative pressure beer column reboiler 18, and the negative pressure beer column 3 is heated to 80 ℃. The spent grain at the bottom of the negative pressure beer column 3 heats the mature beer preheater 25 to 65 ℃. The absolute ethanol vapor from the first adsorber 8, the second adsorber 9, and the third adsorber 10 is fed to the positive pressure methanol removal column reboiler 26 while heating the positive pressure methanol removal column 4 to 95 ℃. The alcohol vapor at the top of the positive pressure methanol removal column 4 was heated to 80 c by the atmospheric pressure methanol removal column reboiler 27.
The absolute ethyl alcohol obtained by the utility model reaches the standard of high-grade purity in GB/T678-2002 chemical reagent ethanol (absolute ethyl alcohol), the mass fraction of the ethanol is more than or equal to 99.8%, the mass fraction of the methanol is less than or equal to 0.02%, and the steam consumption per 1 ton of absolute ethyl alcohol produced is not more than 1.2 tons.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (8)
1. A distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermentation mash, including mature mash preheater, negative pressure mash tower, ordinary pressure mash tower, rectifying column, the superheater that connects gradually, its characterized in that, the export of superheater is connected with the entry of adsorber group, the adsorber group is formed by three adsorber connection in proper order, and the export of adsorber group is connected with the malleation and is taken off the methanol tower through malleation and take off the methanol tower reboiler, and the malleation takes off the methanol tower and is connected with ordinary pressure and take off the methanol tower through ordinary pressure and take off the methanol tower reboiler, and malleation takes off the methanol tower reboiler still and is connected with ordinary pressure and take off the methanol tower, and the export of malleation and ordinary pressure that takes off the methanol tower are all connected with the finished product metering tank.
2. The distillation system for producing high quality absolute ethanol from synthetic gas beer according to claim 1, wherein the top portion of the negative pressure beer column is an acid discharging section and a degassing section, the acid discharging section being located above the degassing section; the mature mash preheater is connected with a degassing section, the degassing section is connected with a primary preheater of the normal pressure mash tower, a secondary preheater of the normal pressure mash tower and the normal pressure mash tower in sequence, and the degassing section is also connected with a degassing section condenser; the acid discharge section is connected with the acid discharge section condenser and the acid discharge section reflux tank in sequence, and the acid discharge section reflux is connected with the acid discharge section; the degassing section condenser is also connected with an acid discharge section reflux tank.
3. The distillation system for producing high quality absolute ethanol from synthetic gas beer according to claim 1, wherein the atmospheric beer column is connected with a negative pressure beer column reboiler, a raw wine tank, a raw wine preheater, and a rectifying column in sequence.
4. The distillation system for producing high quality absolute ethanol from syngas beer according to claim 3, wherein the negative pressure beer column reboiler is coupled to a negative pressure beer column; the crude wine tank is connected with the acid discharging section; the normal pressure mash tower is also connected with the rectifying tower through a reboiler of the normal pressure mash tower.
5. The distillation system for producing high quality absolute ethanol from syngas beer according to claim 1, wherein the rectifying tower is connected to a superheater, and the adsorber set comprises a first adsorber, a second adsorber, and a third adsorber connected in sequence; the superheater is respectively connected with the first absorber, the second absorber and the third absorber, and the first absorber, the second absorber and the third absorber are all connected with the reboiler of the positive pressure methanol removal tower.
6. The distillation system for producing high quality absolute ethanol from synthetic gas beer according to claim 5, wherein the first adsorber, the second adsorber, and the third adsorber are each connected to a desorption condenser, and the desorption condenser is connected to a raw wine tank.
7. The distillation system for producing high quality absolute ethanol from synthetic gas beer according to claim 5, wherein the rectifying column reboiler is connected to a steam line, the rectifying column reboiler is connected to a rectifying column, and the rectifying column reboiler is further connected to a raw liquor preheater.
8. The distillation system for producing high quality absolute ethanol from syngas beer according to claim 1, wherein the atmospheric demethanizer is coupled to an atmospheric demethanizer condenser.
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