CN106422388A - Differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and production technology of high-quality alcohol - Google Patents
Differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and production technology of high-quality alcohol Download PDFInfo
- Publication number
- CN106422388A CN106422388A CN201610952207.8A CN201610952207A CN106422388A CN 106422388 A CN106422388 A CN 106422388A CN 201610952207 A CN201610952207 A CN 201610952207A CN 106422388 A CN106422388 A CN 106422388A
- Authority
- CN
- China
- Prior art keywords
- tower
- preheater
- wine
- mash
- coarse
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000004821 distillation Methods 0.000 title claims abstract description 195
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 238000005516 engineering process Methods 0.000 title abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 168
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 79
- 238000011084 recovery Methods 0.000 claims abstract description 70
- 238000005406 washing Methods 0.000 claims abstract description 60
- 239000002699 waste material Substances 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 239000001760 fusel oil Substances 0.000 claims description 34
- 238000010992 reflux Methods 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 12
- 238000000605 extraction Methods 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 4
- 238000004065 wastewater treatment Methods 0.000 claims description 4
- 238000010790 dilution Methods 0.000 claims description 3
- 239000012895 dilution Substances 0.000 claims description 3
- 238000000855 fermentation Methods 0.000 claims description 3
- 230000004151 fermentation Effects 0.000 claims description 3
- 238000010025 steaming Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 12
- 238000010168 coupling process Methods 0.000 abstract description 5
- 230000008878 coupling Effects 0.000 abstract description 3
- 238000005859 coupling reaction Methods 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract 1
- 230000006866 deterioration Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 235000016735 Manihot esculenta subsp esculenta Nutrition 0.000 description 1
- 241000658379 Manihot esculenta subsp. esculenta Species 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000013339 cereals Nutrition 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 235000000346 sugar Nutrition 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
- B01D3/003—Rectification of spirit
- B01D3/004—Rectification of spirit by continuous methods
- B01D3/005—Combined distillation and rectification
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a differential pressure distillation energy-saving device for producing high-quality alcohol through double crude distillation towers and a production technology of the high-quality alcohol. The device comprises a first crude distillation tower, a second crude distillation tower, a water washing tower, a rectifying tower, a methanol tower, a recovery tower and a heat exchanger which are communicated through pipelines. The alcohol vapor at the top of the first crude distillation tower, the alcohol vapor at the top of the recovery tower and the waste fermented liquid at the bottom of the first crude distillation tower are used for preheating the mature fermented liquor in a first fermented liquor preheater, the mature fermented liquor in a second fermented liquor preheater and the mature fermented liquor in a third fermented liquor preheater respectively, the waste fermented liquid at the bottom of the second crude distillation tower passes through a fourth fermented liquor preheater and then can be used for preheating the mature fermented liquor in the fourth fermented liquor. By arranging two crude distillation towers to produce the high-quality edible alcohol, the heat of the alcohol vapor at the tops of the first crude distillation tower and the recovery tower and the heat of the waste fermented liquid at the bottoms of the first crude distillation tower and the second crude distillation tower can be fully used for preheating the mature fermented liquor, and by means of the differential pressure multiple-effect thermal coupling technology, energy consumption of a distillation system is optimized, and the steam heating energy consumption of the device can be remarkably reduced.
Description
Technical Field
The invention relates to the production field of superior alcohol, in particular to a differential pressure distillation energy-saving device for producing the superior alcohol by double coarse towers and a production process thereof.
Background
The edible alcohol can be prepared by fermenting and distilling cereal, cassava and sugar materials. With the national improvement of the standards of edible alcohol, the deterioration of domestic water resource conditions and the increasing shortage of global energy, it is urgent to find a new process which can improve the quality of edible alcohol, reasonably and fully utilize water resources and reduce the energy consumption for producing edible alcohol. Chinese patent CN200710030550.8 relates to a five-tower two-stage differential pressure distillation device and a process thereof for high-grade edible alcohol, the process adopts a multi-stage differential pressure thermal coupling energy matching technology, the steam consumption of a ton of high-grade edible alcohol product is 2.2-2.5 tons, the cooling water consumption of a ton of product is 90-120 tons, and all technical indexes of the produced high-grade alcohol meet the national high-grade edible alcohol standard. However, the conventional top grade alcohol production device, such as the top grade alcohol production device in chinese patent CN200710030550.8, generally has large energy consumption, and with the deterioration of national energy and water resource status and the increasing shortage of global energy, it is necessary to further optimize the energy consumption for producing edible alcohol and find a new process with more reasonable energy and water resource utilization.
Disclosure of Invention
Based on the above, there is a need for a differential pressure distillation energy-saving device for producing superior alcohol by using double crude towers, which can reduce energy consumption, and a production process thereof.
A differential pressure distillation energy-saving device for producing high-grade alcohol by double coarse towers comprises a coarse distillation tower, a water washing tower, a rectifying tower, a methanol tower and a recovery tower which are communicated through pipelines, wherein the coarse distillation tower comprises a first coarse distillation tower and a second coarse distillation tower, and the differential pressure distillation energy-saving device further comprises a first mash preheater, a second mash preheater, a third mash preheater and a fourth mash preheater; wherein,
the cold end inlet of the first mash preheater is a mature mash inlet, the cold end outlet of the first mash preheater is communicated with the cold end inlet of the second mash preheater, the cold end outlet of the second mash preheater is communicated with the cold end inlet of the third mash preheater, and the cold end outlet of the third mash preheater is communicated with the feed inlet of the first coarse distillation tower; a hot end inlet of the first mash preheater is communicated with a top wine vapor pipeline of the first coarse distillation tower; a hot end inlet of the second mash preheater is communicated with a top wine vapor pipeline of the recovery tower, and a hot end outlet is communicated with a reflux port of the recovery tower; the hot end inlet of the third mash preheater is communicated with the bottom outlet pipeline of the first coarse distillation tower; and a side line extraction pipe orifice of the first coarse distillation tower is communicated with a cold end inlet of the fourth mash preheater, a cold end outlet of the fourth mash preheater is communicated with a feed inlet of the second coarse distillation tower, a hot end inlet of the fourth mash preheater is communicated with a bottom waste mash pipeline of the second coarse distillation tower, and a hot end outlet of the fourth mash preheater is communicated with a bottom tower kettle of the first coarse distillation tower.
In one embodiment, the differential pressure distillation energy saving device further comprises a crude wine tank; the outsides of the first coarse distillation tower, the second coarse distillation tower, the water washing tower, the methanol tower and the recovery tower are respectively connected with a reboiler for providing heat, and the reboilers are respectively a first coarse distillation tower reboiler, a second coarse distillation tower reboiler, a water washing tower reboiler, a methanol tower reboiler and a recovery tower reboiler; wherein,
a hot end inlet of the reboiler of the first coarse distillation tower is communicated with a liquor steam pipeline at the top of the second coarse distillation tower, and a hot end outlet of the reboiler of the first coarse distillation tower is communicated with the crude liquor tank;
the top wine vapor pipeline of the rectifying tower is sequentially connected in series with the hot end inlet of the second coarse distillation tower reboiler, the hot end inlet of the recovery tower reboiler and the hot end inlet of the water scrubber reboiler; the hot end outlet of the second coarse distillation tower reboiler, the hot end outlet of the water scrubber reboiler and the hot end outlet of the recovery tower reboiler are respectively communicated with the reflux port of the rectifying tower;
a hot end inlet of the methanol tower reboiler is communicated with a top liquor steam pipeline of the water washing tower, one part of a hot end outlet is communicated with a reflux port of the water washing tower, and one part of the hot end outlet outputs miscellaneous liquor;
the recovery tower is communicated with the crude wine tank.
In one embodiment, the differential pressure distillation energy-saving device further comprises a first coarse distillation tower condenser, a coarse wine preheater, a weak wine preheater, a miscellaneous wine tank and a miscellaneous wine preheater; wherein,
a hot end outlet of the first mash preheater is provided with a gas phase outlet and a liquid phase outlet, wherein the gas phase outlet is communicated with the first coarse distillation tower condenser, and the first coarse distillation tower condenser and the liquid phase outlet are both communicated with an inlet pipeline of the coarse wine tank;
an outlet pipeline of the crude wine tank is sequentially connected with the crude wine preheater and the water washing tower in series;
the outlet pipeline at the bottom of the water washing tower is sequentially connected with the light wine preheater and the rectifying tower in series;
the bottom outlet pipeline of the rectifying tower is communicated with a hot end inlet of the weak liquor preheater, and a hot end outlet of the weak liquor preheater is communicated with the water washing tower and the crude liquor preheater;
an outlet pipeline of the miscellaneous wine tank is sequentially connected with the miscellaneous wine preheater and the recovery tower in series, and a hot end inlet of the miscellaneous wine preheater is communicated with a bottom outlet pipeline of the recovery tower.
In one embodiment, the differential pressure distillation energy-saving device further comprises a fusel oil cooler and a fusel oil separator; the recovery tower, the fusel oil cooler and the fusel oil separator are sequentially and circularly connected through pipelines.
In one embodiment, the differential pressure distillation energy saving device further comprises a methanol tower condenser; and the top alcohol steam pipeline and the reflux inlet of the methanol tower are communicated with the methanol tower condenser in a circulating way.
A production process of superior alcohol uses the differential pressure distillation energy-saving device for producing the superior alcohol by using the double crude towers in any embodiment to produce the superior alcohol.
In one embodiment, the top of the first coarse distillation tower adopts negative pressure operation, the top of the second coarse distillation tower adopts micro-negative pressure or micro-positive pressure operation, the top of the water washing tower adopts micro-negative pressure or micro-positive pressure operation, the top of the rectification tower adopts positive pressure operation, the top of the methanol tower adopts negative pressure operation, and the top of the recovery tower adopts normal pressure operation.
In one embodiment, the operation pressure at the top of the first crude distillation tower is-50 to-20 kPa, the temperature at the top of the tower is 50 to 60 ℃, and the temperature at the bottom of the tower is 70 to 85 ℃;
the operation pressure at the top of the second coarse distillation tower is-20-30 kPa, the temperature at the top of the second coarse distillation tower is 90-100 ℃, and the temperature at the bottom of the second coarse distillation tower is 95-108 ℃;
the operation pressure at the top of the water washing tower is-10-20 kPa, the temperature at the top of the tower is 90-105 ℃, and the temperature at the bottom of the tower is 90-105 ℃;
the operation pressure at the top of the rectifying tower is 180-320 kPa, the temperature at the top of the rectifying tower is 105-120 ℃, and the temperature at the bottom of the rectifying tower is 130-155 ℃;
the operating pressure at the top of the methanol tower is-50-10 kPa, the temperature at the top of the tower is 60-80 ℃, and the temperature at the bottom of the tower is 70-100 ℃;
the operation pressure at the top of the recovery tower is 0-30 kPa, the temperature at the top of the tower is 70-80 ℃, and the temperature at the bottom of the tower is 100-115 ℃.
In one embodiment, the production process specifically comprises the following steps:
mature mash from a fermentation section enters a first coarse distillation tower after being preheated by a first mash preheater, a second mash preheater and a third mash preheater, the mature mash is partially extracted by a top side line extraction device of the first coarse distillation tower, the mature mash enters a second coarse distillation tower after being preheated by a fourth mash preheater, wine vapor at the top of the first coarse distillation tower is condensed in the first mash preheater, uncondensed wine vapor is fully condensed in a first coarse distillation tower condenser, wine vapor condensate in the first coarse distillation tower condenser enters a coarse wine tank, and waste mash at the bottom of the first coarse distillation tower is used for preheating the mature mash in the third mash preheater and then enters a wastewater treatment section; the top wine vapor of the second coarse distillation tower is condensed in the reboiler of the first coarse distillation tower, the condensate enters the coarse wine tank, and the waste mash at the bottom of the second coarse distillation tower is used for preheating the mature mash in the fourth mash preheater and then enters the tower kettle of the first coarse distillation tower, and is discharged together with the waste mash at the tower kettle of the first coarse distillation tower; preheating crude wine in a crude wine tank by a crude wine preheater, then feeding the preheated crude wine into a water washing tower, condensing wine vapor at the top of the water washing tower in a methanol tower reboiler, extracting partial miscellaneous wine from condensate, then refluxing the extracted miscellaneous wine to the top of the water washing tower, preheating weak wine from the bottom of the water washing tower by a weak wine preheater, and then feeding the weak wine into a rectifying tower; the top alcohol vapor of the rectifying tower is condensed in a second rough distillation tower reboiler, a recovery tower reboiler and a water washing tower reboiler in sequence, the condensate liquid flows back to the top of the rectifying tower, and semi-finished alcohol is extracted from a tower plate at the middle upper part of the rectifying tower and enters a methanol tower; condensing the alcohol vapor at the top of the methanol tower by circulating cooling water, extracting partial industrial alcohol from the condensate, refluxing to the top of the methanol tower, extracting qualified high-grade finished alcohol from the bottom of the methanol tower, cooling and then sending into a finished product tank area; the miscellaneous wine extracted from the reflux of the water washing tower and the middle part of the rectifying tower enters an miscellaneous wine tank, is preheated by an miscellaneous wine preheater and then enters a recovery tower; alcohol rich in fusel oil is extracted from the middle part of the recovery tower, the alcohol is cooled by a fusel oil cooler and then enters a fusel oil separator, the fusel oil is separated in the fusel oil separator by adding dilution water, light wine after the fusel oil is separated enters the recovery tower for steaming, and wine liquid extracted from the top of the recovery tower enters a wine roughing tank.
In one embodiment, the rectification column provides a thermal load from the primary steam from the boiler.
The differential pressure distillation energy-saving device for producing the top-grade alcohol by the double coarse towers and the production process thereof use the double coarse towers, the top alcohol steam of the first coarse tower, the top alcohol steam of the recovery tower and the bottom waste mash of the first coarse tower can be respectively used for preheating mature mash in the first mash preheater, the second mash preheater and the third mash preheater, the bottom waste mash of the second coarse tower can be used for preheating the mature mash in the fourth mash preheater after passing through the fourth mash preheater, and enters the tower kettle of the first coarse tower after being cooled, and is discharged after passing through the third mash preheater together with the waste mash in the tower kettle of the first coarse tower. The device and the production process produce the top grade edible alcohol by configuring the two coarse distillation towers, can fully utilize the top wine steam of the first coarse distillation tower and the recovery tower and the heat of the bottom waste mash of the first coarse distillation tower and the second coarse distillation tower to preheat the mature mash, adopt a differential pressure multiple-effect thermal coupling process to optimize the energy consumption of a distillation system, can obviously reduce the energy consumption of the device, and have the beneficial effect of saving energy.
In addition, alcohol steam at the top of the rectifying tower indirectly heats the second coarse distillation tower, the recovery tower and the water washing tower through a second coarse distillation tower reboiler, a recovery tower reboiler and a water washing tower reboiler in sequence; the wine steam at the top of the second crude distillation tower indirectly heats the first crude distillation tower through a reboiler of the first crude distillation tower; the alcohol steam of the water washing tower indirectly heats the methanol tower through a reboiler of the methanol tower; the rectification tower waste water is preheated by the weak liquor preheater to feed weak liquor into the rectification tower, and is divided into two parts, one part is used as washing water of the washing tower, and the other part is used as process water or discharged outside of other workshops after the crude liquor is preheated by the washing tower, so that the heat of liquor steam and the like can be further fully utilized to heat other parts, and the purpose of saving energy consumption is achieved.
Compared with the traditional high-grade alcohol production device, the device and the production process can reduce the energy consumption to 1.8 tons of steam/ton of finished alcohol and reduce the circulating water consumption to 80 tons of finished alcohol, and the device and the production process can save about 20 percent of energy compared with the existing distillation process for producing high-grade edible alcohol by only configuring a single crude tower and adopting five tower differential pressure.
Drawings
FIG. 1 is a schematic diagram of an embodiment of a differential pressure distillation energy-saving device for producing high-grade alcohol by using double crude towers, wherein arrows indicate the flow direction of liquid and/or steam.
The reference numerals are explained below:
1: a first mash preheater; 2: a second mash preheater; 3: a third mash preheater; 4: a first coarse distillation column; 5: a first coarse distillation column reboiler; 6: a first coarse distillation column condenser; 7: a fourth mash preheater; 8: a second coarse distillation column; 9: a second coarse distillation column reboiler; 10: a crude wine tank; 11: a crude wine preheater; 12: washing the tower with water; 13: a water scrubber reboiler; 14: a light wine preheater; 15: a rectifying tower; 16: a methanol tower; 17: a methanol tower reboiler; 18: a methanol tower condenser; 19: a mixed wine tank; 20: a miscellaneous wine preheater; 21: a recovery tower; 22: a recovery column reboiler; 23: a fusel oil condenser; 24: fusel oil separator.
Detailed Description
To facilitate an understanding of the invention, the invention will now be described more fully with reference to the accompanying drawings. Preferred embodiments of the present invention are shown in the drawings. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.
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 invention belongs. The terminology used in the description of the invention herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.
As shown in fig. 1, the differential pressure distillation energy-saving device for producing high-grade alcohol by using double rough towers of an embodiment comprises a first mash preheater 1, a second mash preheater 2, a third mash preheater 3, a first rough distillation tower 4, a first rough distillation tower reboiler 5, a first rough distillation tower condenser 6, a fourth mash preheater 7, a second rough distillation tower 8, a second rough distillation tower reboiler 9, a rough wine tank 10, a rough wine preheater 11, a water washing tower 12, a water washing tower reboiler 13, a weak wine preheater 14, a rectification tower 15, a methanol tower 16, a methanol tower reboiler 17, a methanol tower condenser 18, a miscellaneous wine tank 19, a miscellaneous wine preheater 20, a recovery tower 21, a recovery tower reboiler 22, a miscellaneous alcohol oil condenser 23 and a miscellaneous alcohol oil separator 24. The first mash preheater 1, the second mash preheater 2 and the third mash preheater 3 of this example constitute a three-stage mash preheating system. The two crude distillation columns are the first crude distillation column 4 and the second crude distillation column 8. The corresponding devices of the differential pressure distillation energy-saving device of the embodiment are communicated through connecting mechanisms such as pipelines.
Specifically, in this embodiment, the cold end inlet of the first mash preheater 1 is a mature mash inlet, the cold end outlet of the first mash preheater 1 is communicated with the cold end inlet of the second mash preheater 2, the cold end outlet of the second mash preheater 2 is communicated with the cold end inlet of the third mash preheater 3, and the cold end outlet of the third mash preheater 3 is communicated with the feed inlet of the first coarse distillation tower 4. The hot end inlet of the first mash preheater 1 is communicated with the top wine steam pipeline of the first coarse distillation tower 4. The hot end inlet of the second mash preheater 2 is communicated with the top wine steam pipeline of the recovery tower 21, and the hot end outlet is communicated with the return port of the recovery tower 21 and used for outputting part of industrial alcohol. The hot end inlet of the third mash preheater 3 is communicated with the bottom outlet pipeline of the first coarse distillation tower 4. A side line extraction pipe orifice of the first coarse distillation tower 4 is communicated with a cold end inlet of a fourth mash preheater 7, a cold end outlet of the fourth mash preheater 7 is communicated with a feed inlet of a second coarse distillation tower 8, a hot end inlet of the fourth mash preheater 7 is communicated with a waste mash pipeline at the bottom of the second coarse distillation tower 8, and a hot end outlet of the fourth mash preheater 7 is communicated with a tower kettle at the bottom of the first coarse distillation tower 4.
The first coarse distillation tower reboiler 5, the second coarse distillation tower reboiler 9, the water scrubber reboiler 13, the methanol tower reboiler 17 and the recovery tower reboiler 22 are respectively connected to the outside of the first coarse distillation tower 4, the second coarse distillation tower 8, the water scrubber 12, the methanol tower 16 and the recovery tower 21 to provide reboiling heat for corresponding equipment. In this embodiment, the first topping still reboiler 5 corresponds to an alcohol condenser of the second topping still 8, the second topping still reboiler 9 and the recovery tower reboiler 21 stages of the water scrubber reboilers 13 correspond to a first condenser, a second condenser and a third condenser of the alcohol of the rectifying tower 15, respectively, and the methanol tower reboiler 17 corresponds to an alcohol condenser of the water scrubber 12.
Specifically, a hot end inlet of the first coarse distillation tower reboiler 5 is communicated with a top wine steam pipeline of the second coarse distillation tower 8, and a hot end outlet is communicated with the coarse wine tank 10. The top wine steam pipeline of the rectifying tower 15 is connected with the hot end inlet of the second coarse distillation tower reboiler 9, the hot end inlet of the recovery tower reboiler 22 and the hot end inlet of the water washing tower reboiler 13 in series in sequence. The hot end outlet of the second coarse distillation tower reboiler 9, the hot end outlet of the water scrubber reboiler 13 and the hot end outlet of the recovery tower reboiler 22 are respectively communicated with the reflux port of the rectifying tower 15. The hot end inlet of the methanol tower reboiler 17 is communicated with the top liquor steam pipeline of the water washing tower 12, one part of the hot end outlet is communicated with the reflux port of the water washing tower 12, and one part of the hot end outlet outputs miscellaneous liquor. The top of the recovery tower 21 is communicated with the crude wine tank 10. The middle outlet of the rectifying tower 15 is also used for outputting the miscellaneous wine.
The hot end outlet of the first mash preheater 1 is provided with a gas phase outlet and a liquid phase outlet, wherein the gas phase outlet is communicated with the first rough distillation tower condenser 6, and the first rough distillation tower condenser 6 and the liquid phase outlet are both communicated with the inlet pipeline of the crude wine tank 10. The outlet pipeline of the crude wine tank 10 is connected with a crude wine preheater 11 and a water washing tower 12 in series in sequence. The outlet pipeline at the bottom of the water washing tower 12 is connected with a light wine preheater 14 and a rectifying tower 15 in series in sequence. The outlet pipeline at the bottom of the rectifying tower 15 is communicated with the hot end inlet of the weak liquor preheater 14, and the hot end outlet of the weak liquor preheater 14 is communicated with the water washing tower 12 and the crude liquor preheater 11. The outlet pipeline of the miscellaneous liquor tank 19 is sequentially connected with the miscellaneous liquor preheater 20 and the recovery tower 21 in series, and the hot end inlet of the miscellaneous liquor preheater 20 is communicated with the outlet pipeline at the bottom of the recovery tower 21.
The recovery tower 21, the fusel oil condenser 23 and the fusel oil separator 24 are sequentially connected in a circulating way through pipelines. Specifically, a middle extraction pipe orifice of the recovery tower 21 is communicated with a hot end inlet of the fusel oil condenser 23, a hot end outlet of the fusel oil condenser 23 is communicated with the fusel oil separator 24, and a bottom outlet pipeline of the fusel oil separator 24 is communicated with the recovery tower 21.
The top alcohol steam pipeline of the methanol tower 16 is circularly communicated with the reflux inlet through the methanol tower condenser 18, and the condensate liquid from the methanol tower condenser 18 can output partial industrial alcohol and then reflux to the methanol tower 16.
The embodiment also provides a process for producing superior alcohol by using the differential pressure distillation energy-saving device for producing superior alcohol by using the double crude towers, and the production process specifically comprises the following steps in the operation process:
mature mash from a fermentation section enters a first coarse distillation tower 4 after being preheated by a first mash preheater 1, a second mash preheater 2 and a third mash preheater 3, the mature mash is partially extracted by a side line extraction device at the top of the first coarse distillation tower 4 and enters a second coarse distillation tower 8 after being preheated by a fourth mash preheater 7, wine vapor at the top of the first coarse distillation tower 4 is condensed in the first mash preheater 1, the uncondensed wine vapor is completely condensed in a first coarse distillation tower condenser 6, a wine vapor condensate in the first coarse distillation tower condenser 6 enters a coarse wine tank 10, and waste mash at the bottom of the first coarse distillation tower 4 is used for preheating the mature mash in the third mash preheater 3 and then enters a waste water treatment section. The top wine steam of the second coarse distillation tower 8 is condensed in the first coarse distillation tower reboiler 5, the condensate enters the coarse wine tank 10, and the waste mash at the bottom of the second coarse distillation tower 8 is used for preheating mature mash in the fourth mash preheater 7, then enters the tower kettle of the first coarse distillation tower 4, and is discharged together with the tower kettle waste mash of the first coarse distillation tower 4. Crude wine in a crude wine tank 10 enters a water washing tower 12 after being preheated by a crude wine preheater 11, wine vapor at the top of the water washing tower 12 is condensed in a methanol tower reboiler 17, partial miscellaneous wine is extracted from the condensate and then flows back to the top of the water washing tower 12, and light wine coming out from the bottom of the water washing tower 12 enters a rectifying tower 15 after being preheated by a light wine preheater 14. The liquor steam on the top of the rectifying tower 15 is condensed in the second rough distillation tower reboiler 9, the recovery tower reboiler 22 and the water washing tower reboiler 13 in sequence, the condensate liquid flows back to the top of the rectifying tower 15, and semi-finished alcohol is extracted from a tower plate on the middle upper part of the rectifying tower 15 and enters the methanol tower 16. The alcohol steam at the top of the methanol tower 16 is condensed by circulating cooling water in a methanol tower condenser 18, partial industrial alcohol is extracted from the condensate and flows back to the top of the methanol tower 16, qualified high-grade finished alcohol is extracted from the bottom of the methanol tower 16 and is sent to a finished product tank area after being cooled. The mixed liquor which flows back from the water washing tower 12 (flows back through a methanol reboiler 17), is extracted from the middle part of the rectifying tower 15 and enters a mixed liquor tank 19, and enters a recovery tower 21 after being preheated by a mixed liquor preheater 20. Alcohol rich in fusel oil is extracted from the middle part of the recovery tower 21, the alcohol is cooled by a fusel oil condenser 23 and then enters a fusel oil separator 24, the fusel oil is separated in the fusel oil separator 24 by adding dilution water, light wine after the fusel oil is separated enters the recovery tower 21 for re-steaming, and wine liquid extracted from the top of the recovery tower 21 enters a crude wine tank 10.
In this embodiment, the first crude distillation column 4 is operated at a negative pressure at the top, the second crude distillation column 8 is operated at a slight negative pressure or slight positive pressure at the top, the water washing column 12 is operated at a slight negative pressure or slight positive pressure at the top, the rectification column 15 is operated at a positive pressure at the top, the methanol column 16 is operated at a negative pressure at the top, and the recovery column 21 is operated at a normal pressure at the top.
In particular, the rectifying column 15 provides a thermal load from the primary steam from the boiler. The operation pressure of the top of the first crude distillation tower 4 is-50 to-20 kPa, the temperature of the top of the tower is 50 to 60 ℃, and the temperature of the bottom of the tower is 70 to 85 ℃. The operation pressure at the top of the second crude distillation tower 8 is-20 to 30kPa, the temperature at the top of the tower is 90 to 100 ℃, and the temperature at the bottom of the tower is 95 to 108 ℃. The operation pressure at the top of the water washing tower 12 is-10 to 20kPa, the temperature at the top of the tower is 90 to 105 ℃, and the temperature at the bottom of the tower is 90 to 105 ℃. The operation pressure at the top of the rectifying tower 15 is 180-320 kPa, the temperature at the top of the tower is 105-120 ℃, and the temperature at the bottom of the tower is 130-155 ℃. The operation pressure at the top of the methanol tower 16 is-50-10 kPa, the temperature at the top of the tower is 60-80 ℃, and the temperature at the bottom of the tower is 70-100 ℃. The operation pressure at the top of the recovery tower 21 is 0-30 kPa, the temperature at the top of the tower is 70-80 ℃, and the temperature at the bottom of the tower is 100-115 ℃.
The energy coupling mode of the differential pressure distillation energy-saving device for producing superior alcohol by using the double coarse towers and the production process thereof is as follows: the rectifying column 15 provides a heat load from the primary steam from the boiler; alcohol steam at the top of the rectifying tower 15 indirectly heats the second coarse distillation tower 8, the recovery tower 21 and the water scrubber 12 through a second coarse distillation tower reboiler 9, a recovery tower reboiler 22 and a water scrubber reboiler 13 in sequence; the second crude distillation tower 8 indirectly heats the first crude distillation tower 4 through a first crude distillation tower reboiler 5; the alcohol steam in the water washing tower 12 indirectly heats the methanol tower 16 through a methanol tower reboiler 17; wine steam at the top of the first coarse distillation tower 4, wine steam at the top of the recovery tower 21 and waste mash at the bottom of the first coarse distillation tower 4 can preheat mature mash in a first-stage, a second-stage and a third-stage manner, waste mash at the bottom of the second coarse distillation tower 8 is preheated by a fourth mash preheater 7, the mash enters the second coarse distillation tower 8 and is conveyed to a tower kettle of the first coarse distillation tower 4 after being cooled, and the waste mash is discharged from the tower kettle of the first coarse distillation tower 4 to a wastewater treatment section; the wastewater in the rectifying tower 15 is preheated by the weak liquor preheater 14 and enters the weak liquor in the rectifying tower 15, and is divided into two parts, wherein one part is used as washing water for the washing tower 12, and the other part is used as process water for other workshops or discharged after the crude liquor in the preheating washing tower 12 is fed.
The differential pressure distillation energy-saving device for producing high-grade alcohol by using the double coarse towers is provided with the two coarse distillation towers to produce high-grade edible alcohol, the energy consumption of a distillation system is optimized by adopting a differential pressure multiple-effect thermal coupling process, the energy consumption can be reduced to 1.8 tons of steam/ton of finished alcohol, the circulating water consumption can be reduced to 80 tons of finished alcohol, and the energy-saving device is about 20 percent more energy-saving than the conventional distillation process for producing high-grade edible alcohol by using five towers only provided with a single coarse tower under differential pressure.
The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.
The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.
Claims (10)
1. A differential pressure distillation energy-saving device for producing superior alcohol by double coarse towers comprises a coarse distillation tower, a water washing tower, a rectifying tower, a methanol tower and a recovery tower which are communicated through pipelines, and is characterized in that the coarse distillation tower comprises a first coarse distillation tower and a second coarse distillation tower, and the differential pressure distillation energy-saving device further comprises a first mash preheater, a second mash preheater, a third mash preheater and a fourth mash preheater; wherein,
the cold end inlet of the first mash preheater is a mature mash inlet, the cold end outlet of the first mash preheater is communicated with the cold end inlet of the second mash preheater, the cold end outlet of the second mash preheater is communicated with the cold end inlet of the third mash preheater, and the cold end outlet of the third mash preheater is communicated with the feed inlet of the first coarse distillation tower; a hot end inlet of the first mash preheater is communicated with a top wine vapor pipeline of the first coarse distillation tower; a hot end inlet of the second mash preheater is communicated with a top wine vapor pipeline of the recovery tower, and a hot end outlet is communicated with a reflux port of the recovery tower; the hot end inlet of the third mash preheater is communicated with the bottom outlet pipeline of the first coarse distillation tower; and a side line extraction pipe orifice of the first coarse distillation tower is communicated with a cold end inlet of the fourth mash preheater, a cold end outlet of the fourth mash preheater is communicated with a feed inlet of the second coarse distillation tower, a hot end inlet of the fourth mash preheater is communicated with a bottom waste mash pipeline of the second coarse distillation tower, and a hot end outlet of the fourth mash preheater is communicated with a bottom tower kettle of the first coarse distillation tower.
2. The differential pressure distillation energy-saving device for producing superior alcohol by using the double crude towers according to claim 1, which is characterized by further comprising a crude wine tank; the outsides of the first coarse distillation tower, the second coarse distillation tower, the water washing tower, the methanol tower and the recovery tower are respectively connected with a reboiler for providing heat, and the reboilers are respectively a first coarse distillation tower reboiler, a second coarse distillation tower reboiler, a water washing tower reboiler, a methanol tower reboiler and a recovery tower reboiler; wherein,
a hot end inlet of the reboiler of the first coarse distillation tower is communicated with a liquor steam pipeline at the top of the second coarse distillation tower, and a hot end outlet of the reboiler of the first coarse distillation tower is communicated with the crude liquor tank;
the top wine vapor pipeline of the rectifying tower is sequentially connected in series with the hot end inlet of the second coarse distillation tower reboiler, the hot end inlet of the recovery tower reboiler and the hot end inlet of the water scrubber reboiler; the hot end outlet of the second coarse distillation tower reboiler, the hot end outlet of the water scrubber reboiler and the hot end outlet of the recovery tower reboiler are respectively communicated with the reflux port of the rectifying tower;
a hot end inlet of the methanol tower reboiler is communicated with a top liquor steam pipeline of the water washing tower, one part of a hot end outlet is communicated with a reflux port of the water washing tower, and one part of the hot end outlet outputs miscellaneous liquor;
the recovery tower is communicated with the crude wine tank.
3. The differential pressure distillation energy-saving device for producing high-grade alcohol by using double crude towers according to claim 2, further comprising a first crude distillation tower condenser, a crude wine preheater, a weak wine preheater, a miscellaneous wine tank and a miscellaneous wine preheater; wherein,
a hot end outlet of the first mash preheater is provided with a gas phase outlet and a liquid phase outlet, wherein the gas phase outlet is communicated with the first coarse distillation tower condenser, and the first coarse distillation tower condenser and the liquid phase outlet are both communicated with an inlet pipeline of the coarse wine tank;
an outlet pipeline of the crude wine tank is sequentially connected with the crude wine preheater and the water washing tower in series;
the outlet pipeline at the bottom of the water washing tower is sequentially connected with the light wine preheater and the rectifying tower in series;
the bottom outlet pipeline of the rectifying tower is communicated with a hot end inlet of the weak liquor preheater, and a hot end outlet of the weak liquor preheater is communicated with the water washing tower and the crude liquor preheater;
an outlet pipeline of the miscellaneous wine tank is sequentially connected with the miscellaneous wine preheater and the recovery tower in series, and a hot end inlet of the miscellaneous wine preheater is communicated with a bottom outlet pipeline of the recovery tower.
4. The differential pressure distillation energy-saving device for producing superior alcohol by using the double crude towers according to claim 3, which is characterized by further comprising a fusel oil cooler and a fusel oil separator; the recovery tower, the fusel oil cooler and the fusel oil separator are sequentially and circularly connected through pipelines.
5. The differential pressure distillation energy-saving device for producing superior alcohol by using the double crude towers as claimed in claim 4, which is characterized by further comprising a methanol tower condenser; and the top alcohol steam pipeline and the reflux inlet of the methanol tower are communicated with the methanol tower condenser in a circulating way.
6. A production process of superior alcohol is characterized in that the differential pressure distillation energy-saving device for producing the superior alcohol by using the double crude tower according to any one of claims 1 to 5 is used for production.
7. The process for producing premium grade alcohol according to claim 6, wherein the top of the first crude distillation tower is operated at negative pressure, the top of the second crude distillation tower is operated at slight negative pressure or slight positive pressure, the top of the water washing tower is operated at slight negative pressure or slight positive pressure, the top of the rectification tower is operated at positive pressure, the top of the methanol tower is operated at negative pressure, and the top of the recovery tower is operated at normal pressure.
8. The process for producing premium alcohol according to claim 7, wherein the first topping tower has an operating pressure of-50 to-20 kPa at a top temperature of 50 to 60 ℃ and a bottom temperature of 70 to 85 ℃;
the operation pressure at the top of the second coarse distillation tower is-20-30 kPa, the temperature at the top of the second coarse distillation tower is 90-100 ℃, and the temperature at the bottom of the second coarse distillation tower is 95-108 ℃;
the operation pressure at the top of the water washing tower is-10-20 kPa, the temperature at the top of the tower is 90-105 ℃, and the temperature at the bottom of the tower is 90-105 ℃;
the operation pressure at the top of the rectifying tower is 180-320 kPa, the temperature at the top of the rectifying tower is 105-120 ℃, and the temperature at the bottom of the rectifying tower is 130-155 ℃;
the operating pressure at the top of the methanol tower is-50-10 kPa, the temperature at the top of the tower is 60-80 ℃, and the temperature at the bottom of the tower is 70-100 ℃;
the operation pressure at the top of the recovery tower is 0-30 kPa, the temperature at the top of the tower is 70-80 ℃, and the temperature at the bottom of the tower is 100-115 ℃.
9. The process for producing superior alcohol according to claim 8, wherein the differential pressure distillation energy-saving device for producing superior alcohol by using the double crude tower according to claim 5 comprises the following steps:
mature mash from a fermentation section enters a first coarse distillation tower after being preheated by a first mash preheater, a second mash preheater and a third mash preheater, the mature mash is partially extracted by a top side line extraction device of the first coarse distillation tower, the mature mash enters a second coarse distillation tower after being preheated by a fourth mash preheater, wine vapor at the top of the first coarse distillation tower is condensed in the first mash preheater, uncondensed wine vapor is fully condensed in a first coarse distillation tower condenser, wine vapor condensate in the first coarse distillation tower condenser enters a coarse wine tank, and waste mash at the bottom of the first coarse distillation tower is used for preheating the mature mash in the third mash preheater and then enters a wastewater treatment section; the top wine vapor of the second coarse distillation tower is condensed in the reboiler of the first coarse distillation tower, the condensate enters the coarse wine tank, and the waste mash at the bottom of the second coarse distillation tower is used for preheating the mature mash in the fourth mash preheater and then enters the tower kettle of the first coarse distillation tower, and is discharged together with the waste mash at the tower kettle of the first coarse distillation tower; preheating crude wine in a crude wine tank by a crude wine preheater, then feeding the preheated crude wine into a water washing tower, condensing wine vapor at the top of the water washing tower in a methanol tower reboiler, extracting partial miscellaneous wine from condensate, then refluxing the extracted miscellaneous wine to the top of the water washing tower, preheating weak wine from the bottom of the water washing tower by a weak wine preheater, and then feeding the weak wine into a rectifying tower; the top alcohol vapor of the rectifying tower is condensed in a second rough distillation tower reboiler, a recovery tower reboiler and a water washing tower reboiler in sequence, the condensate liquid flows back to the top of the rectifying tower, and semi-finished alcohol is extracted from a tower plate at the middle upper part of the rectifying tower and enters a methanol tower; condensing the alcohol vapor at the top of the methanol tower by circulating cooling water, extracting partial industrial alcohol from the condensate, refluxing to the top of the methanol tower, extracting qualified high-grade finished alcohol from the bottom of the methanol tower, cooling and then sending into a finished product tank area; the miscellaneous wine extracted from the reflux of the water washing tower and the middle part of the rectifying tower enters an miscellaneous wine tank, is preheated by an miscellaneous wine preheater and then enters a recovery tower; alcohol rich in fusel oil is extracted from the middle part of the recovery tower, the alcohol is cooled by a fusel oil cooler and then enters a fusel oil separator, the fusel oil is separated in the fusel oil separator by adding dilution water, light wine after the fusel oil is separated enters the recovery tower for steaming, and wine liquid extracted from the top of the recovery tower enters a wine roughing tank.
10. The process for producing super alcohol according to claim 9, wherein the rectifying tower provides a heat load from primary steam from a boiler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610952207.8A CN106422388B (en) | 2016-10-26 | 2016-10-26 | The differential distillation energy saver and its production technology of double thick tower production top grade alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610952207.8A CN106422388B (en) | 2016-10-26 | 2016-10-26 | The differential distillation energy saver and its production technology of double thick tower production top grade alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106422388A true CN106422388A (en) | 2017-02-22 |
| CN106422388B CN106422388B (en) | 2019-02-19 |
Family
ID=58179298
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610952207.8A Active CN106422388B (en) | 2016-10-26 | 2016-10-26 | The differential distillation energy saver and its production technology of double thick tower production top grade alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106422388B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107858254A (en) * | 2017-10-12 | 2018-03-30 | 广东省阳春酒厂有限公司 | A kind of energy-saving distilling equipment |
| CN107954837A (en) * | 2017-11-22 | 2018-04-24 | 广东中科天元新能源科技有限公司 | Produce neutral alcohol, the device and its production technology of superneutrality alcohol |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
| CN110981696A (en) * | 2019-12-30 | 2020-04-10 | 肥城金塔机械科技有限公司 | Process and system for producing fuel ethanol by using double-coarse single-fine three-tower distillation low-concentration fermented mash |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59196833A (en) * | 1983-04-21 | 1984-11-08 | Res Assoc Petroleum Alternat Dev<Rapad> | Method and apparatus for producing anhydrous methanol |
| CN1880435A (en) * | 2006-04-30 | 2006-12-20 | 广东中科天元再生资源工程有限公司 | Six-column differential-pressure distillation device for extra edible alcohol and process therefor |
| CN101153257A (en) * | 2007-09-27 | 2008-04-02 | 广州保捷机电有限公司 | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof |
| CN101717802A (en) * | 2009-12-18 | 2010-06-02 | 天津大学 | Energy-saving production method of bio-ethanol |
| CN203256177U (en) * | 2013-05-23 | 2013-10-30 | 肥城金塔机械有限公司 | Alcohol preparation device |
| CN104232455A (en) * | 2014-09-26 | 2014-12-24 | 广东中科天元新能源科技有限公司 | Common and superior edible alcohol co-production distillation energy-saving device and energy-saving process thereof |
| CN204310984U (en) * | 2014-12-17 | 2015-05-06 | 广东中科天元新能源科技有限公司 | Seven tower multiple-effect differential distillation technology coproduction top grade alcohol and fuel alcohol plants |
-
2016
- 2016-10-26 CN CN201610952207.8A patent/CN106422388B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59196833A (en) * | 1983-04-21 | 1984-11-08 | Res Assoc Petroleum Alternat Dev<Rapad> | Method and apparatus for producing anhydrous methanol |
| CN1880435A (en) * | 2006-04-30 | 2006-12-20 | 广东中科天元再生资源工程有限公司 | Six-column differential-pressure distillation device for extra edible alcohol and process therefor |
| CN101153257A (en) * | 2007-09-27 | 2008-04-02 | 广州保捷机电有限公司 | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof |
| CN101717802A (en) * | 2009-12-18 | 2010-06-02 | 天津大学 | Energy-saving production method of bio-ethanol |
| CN203256177U (en) * | 2013-05-23 | 2013-10-30 | 肥城金塔机械有限公司 | Alcohol preparation device |
| CN104232455A (en) * | 2014-09-26 | 2014-12-24 | 广东中科天元新能源科技有限公司 | Common and superior edible alcohol co-production distillation energy-saving device and energy-saving process thereof |
| CN204310984U (en) * | 2014-12-17 | 2015-05-06 | 广东中科天元新能源科技有限公司 | Seven tower multiple-effect differential distillation technology coproduction top grade alcohol and fuel alcohol plants |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107858254A (en) * | 2017-10-12 | 2018-03-30 | 广东省阳春酒厂有限公司 | A kind of energy-saving distilling equipment |
| CN107954837A (en) * | 2017-11-22 | 2018-04-24 | 广东中科天元新能源科技有限公司 | Produce neutral alcohol, the device and its production technology of superneutrality alcohol |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
| CN110981696A (en) * | 2019-12-30 | 2020-04-10 | 肥城金塔机械科技有限公司 | Process and system for producing fuel ethanol by using double-coarse single-fine three-tower distillation low-concentration fermented mash |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106422388B (en) | 2019-02-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101153257B (en) | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof | |
| CN106422388B (en) | The differential distillation energy saver and its production technology of double thick tower production top grade alcohol | |
| CN101748037B (en) | Special grade edible alcohol six-tower difference pressure distilling device and process thereof | |
| CN204310984U (en) | Seven tower multiple-effect differential distillation technology coproduction top grade alcohol and fuel alcohol plants | |
| CN110404285B (en) | Four-tower distillation and membrane separation integrated system and method for distilling ethanol | |
| CN111116317B (en) | Five-tower four-effect methanol rectification process and equipment | |
| CN102126920B (en) | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration | |
| CN111437619B (en) | Multi-tower differential pressure energy-saving absolute alcohol distillation system and absolute alcohol energy-saving production method | |
| CN109908616B (en) | Energy-saving distillation system for preparing ethanol from carbon monoxide and distillation method thereof | |
| CN101580457A (en) | Device and process for preparing absolute ethyl alcohol by taking fermented liquor as the raw material | |
| CN114031580B (en) | Refining device and refining method for low-energy PBAT byproduct tetrahydrofuran | |
| CN106635706B (en) | Differential pressure distillation energy-saving production device and method for white spirit with double distillation retorts | |
| CN216536963U (en) | Separation system of sulfuric acid alkylation reaction product | |
| CN108421274B (en) | Low-pressure double-coarse double-fine eight-tower distillation device and method for preparing high-grade alcohol | |
| CN218653048U (en) | Heat pump rectifying device | |
| CN207667178U (en) | The double thick double smart eight column distillation devices of low-pressure process for producing top grade alcohol | |
| CN104232455B (en) | General level and high grade edible spirit coproduction energy-saving distillation device and energy-saving technique thereof | |
| CN101851149A (en) | Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation | |
| CN111072454B (en) | System and process for producing fuel ethanol by double-coarse and double-fine distillation with low pressure method | |
| CN201668968U (en) | An energy-saving system for the production of edible ethanol by five-tower three-stage differential pressure distillation | |
| CN212818177U (en) | Multi-tower differential pressure energy-saving anhydrous alcohol distillation system | |
| CN102126923B (en) | Three-tower differential pressure distillation method for preparing azeotropic ethanol | |
| CN110483248B (en) | Method for refining fuel ethanol by coupling and strengthening three towers and two membranes | |
| CN210495282U (en) | Four-tower distillation and membrane separation integrated system | |
| CN111821712B (en) | Seven-tower differential pressure distillation energy-saving production system and method for top-grade edible alcohol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 510640 Unit 210, Second Floor, Comprehensive Service Building of Guangzhou Science and Technology Innovation Base, No. 80 Lanyue Road, Science City, Guangzhou High-tech Industrial Development Zone, Guangdong Province Applicant after: Guangdong Zhongke Tianyuan New Energy Science & Technology Co., Ltd. Address before: 510640 Technology Integration Building, Guangzhou Institute of Energy, Chinese Academy of Sciences, No. 4 Wushan Energy Road, Tianhe District, Guangzhou City, Guangdong Province Applicant before: Guangdong Zhongke Tianyuan New Energy Science & Technology Co., Ltd. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CB03 | Change of inventor or designer information |
Inventor after: Jiang Xinchun Inventor after: Li Jing Inventor after: Zhou Hongcai Inventor after: Tang Zhaoxing Inventor after: Li Jinying Inventor after: Gao Zhigui Inventor after: Chen Liuxin Inventor before: Li Jing Inventor before: Zhou Hongcai Inventor before: Jiang Xinchun Inventor before: Tang Zhaoxing Inventor before: Li Jinying Inventor before: Gao Zhigui Inventor before: Chen Liuxin |
|
| CB03 | Change of inventor or designer information |