CN201850234U - Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production - Google Patents
Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production Download PDFInfo
- Publication number
- CN201850234U CN201850234U CN2010206085956U CN201020608595U CN201850234U CN 201850234 U CN201850234 U CN 201850234U CN 2010206085956 U CN2010206085956 U CN 2010206085956U CN 201020608595 U CN201020608595 U CN 201020608595U CN 201850234 U CN201850234 U CN 201850234U
- Authority
- CN
- China
- Prior art keywords
- outlet
- wine
- mash
- inlet
- alcohol
- 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.)
- Expired - Lifetime
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production, which comprises a molecular sieve adsorption/resolution tower, a topping still, a complex tower, a rectifying tower, a methyl alcohol tower and mash preheaters, wherein the alcohol steam at the top of the complex tower is used as the heat source and the raw material alcohol steam of the topping still and the methyl alcohol tower after being compressed by an alcohol gas compressor; the alcohol steam of the rectifying tower is the heat source of the complex tower; and the alcohol steam of the topping still , absolute alcohol steam and the alcohol steam of the methyl alcohol tower are respectively the heat source of the first mash preheater, the second mash preheater and the third mash preheater. The device not only can be used for simultaneously producing fuel alcohol and ordinary edible alcohol but also can be used for independently producing the fuel alcohol or the ordinary edible alcohol. Due to the fact that a multiple-effect energy coupling mode is adopted by the distillation dehydration device, the energy consumption is greatly reduced compared with the original process, the steam consumption of each ton of fuel alcohol is reduced to 1.1-1.5t/t and is reduced by 25-35 percent compared with 1.5-2.0 t/t of the original process, and more than 0.7MPag high-grade steam does not need to be consumed; the steam consumption of each ton of ordinary edible alcohol is reduced to 1.2-1.4t/t and is reduced by 35-50 percent compared with 1.9-2.5t/t of the original process.
Description
Technical field
The utility model relates to a kind of alcohol distillation device, relates in particular to the distillation dehydration device of a kind of alcohol fuel and the coproduction of general level edible ethanol.
Background technology
Uncontrolled use along with fossil energy has caused problems such as serious environmental pollution, climate warming, has also caused the exhausted day by day of fossil energy.Countries in the world are development the important component part of the renewable energy source of representative as the future source of energy strategy with the biomass energy one after another.With reproducible non-grain biomass is the raw material production dehydrated alcohol, and then adds effective substitute that alcohol fuel that auxiliary makes can be used as fuel such as gasoline.
Traditional alcohol fuel distillation dehydration unit roughly is divided into double tower differential distillation liquid phase punishment in advance dewatering process flow, double tower differential distillation gas phase punishment in advance dewatering process flow and multitower differential distillation gas phase punishment in advance dewatering process flow etc.Wherein, double tower distil liquid phase punishment in advance process energy consumption height, poor product quality, useless wine with dregs quantity discharged can't reclaim the waste water of cleaning greatly; Though slightly reduce on the double tower gas phase punishment in advance energy consumption, fail to solve a quality product and a useless wine with dregs quantity discharged difficult problem.Publication number be CN101580457A, name to be called " a kind of is the device and the technology of raw material production dehydrated alcohol with the fermentation liquid " and publication number be that CN101157890A, the Chinese patent application that is called " fuel ethanol production equipment and method " have all adopted multitower differential distillation and gas phase punishment in advance dewatering process, there is following defective in they:
(1) to steam grade requirement height:, distill main device and form by negative pressure tower, medium pressure column and high-pressure tower because the technology that adopts is the triple effect distillation.Wherein the high-pressure tower working pressure reaches 450～550kPa (gauge pressure), and column bottom temperature reaches 155～165 ℃, vapor pressure is required to reach 0.7～0.9MPa (gauge pressure), thereby make the generated energy minimizing of heat power plant reduce total economic benefit;
(2) the combined column column bottom temperature is higher, especially be the device of raw material with the corn fermentation wine with dregs, because column bottom temperature reaches 115～125 ℃, Maillard reaction at high temperature takes place in amino acid and carbohydrate in the useless mash, make the color and luster of feed deepen, influence the class and the price of feeds product;
(3) main heat-exchange equipment investment is big, and the heat exchange weak effect: owing to contain the solid substance of a large amount of viscosity higher in ripe wine with dregs and the useless wine with dregs, interchanger often stops up, and has a strong impact on the heat exchange effect; The temperature of crude wine preheater waste water end reaches about 160 ℃, and is higher to the resistant to elevated temperatures requirement of the pad of plate-type heat exchanger, and the phenomenon of leakage takes place easily, and these all make whole energy consumption increase greatly;
(4) the negative pressure tower top exists full gear section (tower) to reflux in the technology that provides of patent application CN 101580457A, needs to consume a large amount of cold general facilitiess and come condensation, has increased steam consumption.
The production of traditional general level edible ethanol, especially with the general level edible ethanol of cassava raw material production,, generally adopt topping still, rectifying tower, methanol column technology because of the methanol content of fermentation liquid is very high, steam consumption is higher, the about 1.9-2.5t/t of steam consumption of the general level of ton edible ethanol product
In addition, traditional alcohol distillation (dehydration) device can only be realized the production of single products such as general level edible ethanol, alcohol fuel, and can not produce general level edible ethanol and two kinds of products of alcohol fuel simultaneously, can not realize that the convenient of two kinds of products switches according to the market requirement, and build two distillation (dehydration) appliance arrangements that overlap products and invest bigger.
Summary of the invention
The shortcoming that the purpose of this utility model is to overcome prior art provides the distillation dehydration device of a kind of alcohol fuel and the coproduction of general level edible ethanol with not enough.
The purpose of this utility model is achieved through the following technical solutions: the distillation dehydration device of a kind of alcohol fuel and the coproduction of general level edible ethanol, comprise molecular sieve adsorption/Analytic Tower, topping still, combined column, rectifying tower, the placed in-line successively first mash preheater of methanol column, tube side, the second mash preheater and the 3rd mash preheater;
Wherein, the mash of first mash preheater inlet is connected with fermenting-ripening mash inlet, and the mash outlet of the first mash preheater is connected with the mash inlet of the second mash preheater, and the fermenting-ripening mash is through the first and second mash preheaters, and temperature raises; The hot junction inlet of the first mash preheater is connected with the wine vapor outlet of topping still, and the hot junction outlet is connected with the inlet of thick wine jar; The hot junction outlet more preferably is set to gaseous phase outlet and liquid phase outlet, gaseous phase outlet is connected successively with topping still condenser, topping still last condenser stage, and the liquid phase outlet of liquid phase outlet, topping still condenser, the liquid phase outlet of topping still last condenser stage are connected by the inlet of pipeline with thick wine jar respectively; The topping still last condenser stage is provided with gaseous phase outlet, is used to discharge not condensing;
The hot junction inlet of the second mash preheater is connected with the alcohol steam outlet at molecular sieve adsorption/Analytic Tower top; The hot junction outlet of the second mash preheater is connected with dehydrated alcohol finished product jar, wherein the hot junction outlet preferably is set to dehydrated alcohol gaseous phase outlet and the outlet of dehydrated alcohol liquid phase, the dehydrated alcohol gaseous phase outlet is connected with dehydrated alcohol finished product condenser, and the outlet of dehydrated alcohol liquid phase is connected with the hot junction liquid phase inlet of dehydrated alcohol water cooler by pipeline respectively with the liquid phase outlet of dehydrated alcohol finished product condenser; The hot junction liquid phase outlet of dehydrated alcohol water cooler is connected with dehydrated alcohol finished product jar; The mash outlet of the second mash preheater is connected with the mash inlet of the 3rd mash preheater, the mash inlet of topping still respectively;
The hot junction inlet of the 3rd mash preheater is connected with the wine vapor outlet of methanol column, the hot junction outlet preferably is set to gaseous phase outlet and liquid phase outlet, gaseous phase outlet is connected with the methanol column last condenser stage, the liquid phase outlet of methanol column last condenser stage is connected with methanol column return tank inlet, and the liquid phase outlet is connected with the top refluxing opening of methanol column return tank and methanol column successively; The mash outlet of the 3rd mash preheater is connected with the mash inlet of topping still;
The topping still outer setting is used for the side line extraction device of the ripe mash after the extraction degassing, side line extraction pipeline is connected with the mash inlet of wine with dregs wine with dregs interchanger, the ripe mash outlet of wine with dregs wine with dregs interchanger is connected with the combined column opening for feed, enters combined column after the preheating of ripe mash process wine with dregs wine with dregs interchanger; The useless wine with dregs inlet of wine with dregs wine with dregs interchanger preferably is connected with combination Tata still, and useless wine with dregs outlet is connected with topping still tower still; Topping still be used to provide the topping still reboiler of heat to be connected, the inlet of topping still reboiler is connected successively with the wine vapor outlet of ethanol vapor gas compressor, combined column, the wine vapour of combined column is origin of heat, the liquid phase outlet of topping still reboiler is connected with the wine liquid inlet of combined column return tank, and the outlet of combined column return tank is connected with combined column top layer column plate refluxing opening;
The combined column outer setting be used to compress the combined column preparation wine vapour the ethanol vapor gas compressor and be used to provide the combined column reboiler of heat, wherein: the ethanol vapor gas compressor is connected with topping still reboiler, methanol column reboiler, raw wine vapour superheater respectively; The combined column reboiler is provided with hot junction inlet and hot junction outlet, and the hot junction inlet is connected with the wine vapor outlet of rectifying tower, and the hot junction outlet is connected with the rectifying tower return tank, and the rectifying tower return tank is connected with the refluxing opening of rectifying tower, the top tray opening for feed of combined column respectively; Combined column is connected with rectifying tower by the light wine extraction mouth that is arranged on the rectifying section bottom; Combined column is connected with methanol column by the wine liquid outlet that is arranged on the top; Wine with dregs wine with dregs interchanger also is provided with the useless wine with dregs inlet and the wine with dregs outlet of giving up, useless wine with dregs inlet is connected with the useless wine with dregs outlet of combined column, the useless wine with dregs outlet of wine with dregs wine with dregs interchanger preferably is connected with topping still tower still, after being the useless wine with dregs process wine with dregs wine with dregs interchanger heat exchange cooling of combined column, enter the flash distillation of topping still tower still, unification is discharged by topping still tower still again;
Rectifying tower be used to provide the rectifying tower reboiler of heat to be connected; The opening for feed of rectifying tower is connected successively with the extraction mouth of crude wine preheater, thick wine jar, after the thick wine process crude wine preheater preheating in the thick wine jar, enters in the rectifying tower; The waste pipe that the hot junction inlet and the rectifier bottoms of crude wine preheater are discharged is connected; The potato spirit alcohol extraction mouth of rectifying tower charging layer top is connected with the inlet of potato spirit separator, wherein preferably between rectifying tower and potato spirit separator the potato spirit water cooler is set; The potato spirit separator is provided with dilution water inlet, potato spirit extraction mouth and light wine outlet, and the light wine outlet is connected with the inlet of thick wine jar;
Methanol column be used to provide the methanol column reboiler of heat to be connected, the hot junction of methanol column reboiler inlet is connected with the outlet of ethanol vapor gas compressor, the hot junction exports to enter the mouth with the wine liquid of combined column return tank and is connected; Methyl alcohol Tata still is connected with general level edible ethanol finished product jar, and general level edible ethanol finished product water cooler preferably is set between the two;
The alcohol gas inlet of molecular sieve adsorption/Analytic Tower bottom is connected successively with the outlet of raw wine vapour superheater, ethanol vapor gas compressor; The alcohol steam outlet at molecular sieve adsorption/Analytic Tower top forms loop structure with regeneration wine vapour superheater; The light wine vapor outlet of molecular sieve adsorption/Analytic Tower bottom is connected with light wine vapour condenser, thick wine jar successively.
The utility model has following advantage and effect with respect to prior art:
(1) the full gear section that needs backflow has been cancelled at the topping still top in the utility model, has reduced the required thermal load of topping still; Because of the operating pressure difference between combined column and the rectifying tower reduces, cancelled the light wine preheater, reduced facility investment.
(2) the useless wine with dregs of combined column directly enters the flash distillation of topping still tower still to reclaim used heat in the utility model after the cooling of wine with dregs wine with dregs interchanger, can further reduce the power loss of technological process.
(3) the former technology of energy loss-rate of device described in the utility model reduces greatly.The steam consumption of ton alcohol fuel is reduced to 1.1～1.5t/t, reduces about 25～35% than former technology 1.5～2.0, and need not consume the above higher-grade steam of 0.7MPag, only needs to consume the low-grade steam of 0.4～0.5MPag.
(4) working pressure of combined column is generally 60～120kPa in the prior art, and the top temperature is generally 90～100 ℃.The alcohol steam of the high density at combined column top is through ethanol vapor gas compressor pressurize in the utility model, and the ethanol gas after the compression is as the thermal source of topping still, and is a part of simultaneously as the raw wine vapour charging of raw wine vapour extraction as adsorbing tower with molecular sieve.Thereby the working pressure of combined column is reduced to normal pressure, and column bottom temperature is reduced to 100～115 ℃, on the one hand, is being in the device of raw material with the corn fermentation mash, and the occurrence probability of Maillard reaction reduces greatly in the mash, makes the color and luster of feed be significantly improved; On the other hand, along with the reduction of feeding temperature, the thermal load of wine with dregs wine with dregs interchanger significantly reduces, and can reduce the facility investment of this wine with dregs wine with dregs interchanger.
(5) rectifying tower 200～350kPa in the utility model, 108～120 ℃ of tower top temperatures, 130～150 ℃ of column bottom temperatures; On the one hand the temperature in crude wine preheater hot junction reduces greatly, the resistance to elevated temperatures of pad is required to reduce, thereby reduce the facility investment and the maintenance cost of this interchanger; On the other hand, the requirement of steam grade is reduced to 0.4～0.5MPag, can saves high-grade steam consumption, increase the generated energy of power plant.
Description of drawings
Fig. 1 is a setting drawing of the present utility model:
The 1-first mash preheater; The 2-second mash preheater; 3-the 3rd mash preheater; The 4-topping still; 5-topping still condenser; 6-topping still last condenser stage; 7-wine with dregs wine with dregs interchanger; The 8-combined column; 9-ethanol vapor gas compressor; 10-topping still reboiler; 11-raw wine vapour superheater; 12-molecular sieve adsorption/Analytic Tower; 13-regeneration wine vapour superheater; 14-light wine vapour condenser; The thick wine jar of 15-; The 16-crude wine preheater; The 17-rectifying tower; 18-combined column reboiler; 19-combined column return tank; 20-rectifying tower return tank; 21-potato spirit water cooler; 22-potato spirit separator; 23-rectifying tower reboiler; 24-dehydrated alcohol finished product condenser; 25-dehydrated alcohol finished product water cooler; 26-dehydrated alcohol finished product jar; The 27-methanol column; 28-methanol column last condenser stage; 29-methanol column reboiler; 30-methanol column return tank; The general level of 31-edible ethanol water cooler; The general level of 32-edible ethanol finished product jar.
Embodiment
Below in conjunction with embodiment and accompanying drawing the utility model is described in further detail, but embodiment of the present utility model is not limited thereto.
Embodiment 1
The distillation dehydration device (as shown in Figure 1) of a kind of alcohol fuel and the coproduction of general level edible ethanol, comprise molecular sieve adsorption/Analytic Tower 12, topping still 4, combined column 8, rectifying tower 17, the placed in-line successively first mash preheater 1 of methanol column 27, tube side, the second mash preheater 2 and the 3rd mash preheater 3;
Wherein, the mash of the first mash preheater 1 inlet is connected with fermenting-ripening mash inlet, and the mash outlet is connected with the mash inlet of the second mash preheater 2; The hot junction inlet of the first mash preheater 1 is connected with the wine vapor outlet of topping still 4; The hot junction outlet comprises gaseous phase outlet and liquid phase outlet, gaseous phase outlet is connected successively with topping still condenser 5, topping still last condenser stage 6, and the liquid phase outlet of liquid phase outlet, topping still condenser 5, the liquid phase outlet of topping still last condenser stage 6 are connected by the inlet of pipeline with thick wine jar respectively; Topping still last condenser stage 6 is provided with gaseous phase outlet, is used to discharge not condensing;
The hot junction inlet of the second mash preheater 2 is connected with the alcohol steam outlet at molecular sieve adsorption/Analytic Tower 12 tops; The hot junction outlet of the second mash preheater 2 comprises dehydrated alcohol gaseous phase outlet and the outlet of dehydrated alcohol liquid phase, the dehydrated alcohol gaseous phase outlet is connected with dehydrated alcohol finished product condenser 24, and the outlet of dehydrated alcohol liquid phase is connected with the hot junction liquid phase inlet of dehydrated alcohol water cooler 25 by pipeline respectively with the liquid phase outlet of dehydrated alcohol finished product condenser 24; The hot junction liquid phase outlet of dehydrated alcohol water cooler 25 is connected with dehydrated alcohol finished product jar 26; The mash outlet of the second mash preheater 2 is connected with the mash inlet of the 3rd mash preheater 3, the mash inlet of topping still 4 respectively;
The hot junction inlet of the 3rd mash preheater 3 is connected with the wine vapor outlet of methanol column 27; The hot junction outlet comprises gaseous phase outlet and liquid phase outlet, gaseous phase outlet is connected with methanol column last condenser stage 28, the liquid phase outlet of methanol column last condenser stage 28 is connected with methanol column return tank 30 inlets, and the liquid phase outlet is connected with the top refluxing opening of methanol column return tank 30, methanol column 27 successively; The mash outlet of the 3rd mash preheater 3 is connected with the mash inlet of topping still 4;
Topping still 4 outer setting are used for the side line extraction device of the ripe mash after the extraction degassing, side line extraction pipeline is connected with the mash inlet of wine with dregs wine with dregs interchanger 7, the ripe mash outlet of wine with dregs wine with dregs interchanger 7 is connected with combined column 8 opening for feeds, enters combined column 8 after 7 preheatings of ripe mash process wine with dregs wine with dregs interchanger; The useless wine with dregs inlet of wine with dregs wine with dregs interchanger 7 is connected with combined column 8 tower stills, and useless wine with dregs outlet is connected with topping still 4 tower stills; Topping still 4 be used to provide the topping still reboiler 10 of heat to be connected, the inlet of topping still reboiler 10 is connected successively with the wine vapor outlet of ethanol vapor gas compressor 9, combined column 8, the wine vapour of combined column 8 is origin of heat, the liquid phase outlet of topping still reboiler 10 is connected with the wine liquid inlet of combined column return tank 19, and 19 outlets of combined column return tank are connected with combined column 8 top layer column plate refluxing openings (being arranged at several from top to down the 2nd～6 column plates);
Combined column 8 outer setting be used to compress the combined column preparation wine vapour ethanol vapor gas compressor 9 and be used to provide the combined column reboiler 18 of heat, wherein: ethanol vapor gas compressor 9 is connected with topping still reboiler 10, methanol column reboiler 29, raw wine vapour superheater 11 respectively; Combined column reboiler 18 is provided with hot junction inlet and hot junction outlet, the hot junction inlet is connected with the wine vapor outlet of rectifying tower 17, the hot junction outlet is connected with rectifying tower return tank 20, and rectifying tower return tank 20 is connected with the refluxing opening of rectifying tower 17, the top tray opening for feed of combined column 8 (being arranged at several from top to down the 1st～6 column plates) respectively; Combined column 8 is connected with rectifying tower 17 by the light wine extraction mouth that is arranged on the rectifying section bottom; Combined column 8 is connected with methanol column 27 by the wine liquid outlet that is arranged on the top; Wine with dregs wine with dregs interchanger 7 also is provided with the useless wine with dregs inlet and the wine with dregs outlet of giving up, useless wine with dregs inlet is connected with the useless wine with dregs outlet of combined column 8, the useless wine with dregs outlet of wine with dregs wine with dregs interchanger 7 is connected with topping still 4 tower stills, after being the useless wine with dregs process wine with dregs wine with dregs interchanger 7 heat exchange cooling of combined column 8, enter topping still 4 tower still flash distillations, unification is discharged by topping still 4 tower stills again;
Rectifying tower 17 be used to provide the rectifying tower reboiler 23 of heat to be connected; The opening for feed of rectifying tower 17 is connected successively with crude wine preheater 16, thick wine jar 15, after thick wine process crude wine preheater 16 preheatings in the thick wine jar 15, enters in the rectifying tower 17; The waste pipe that the hot junction inlet and the rectifier bottoms of crude wine preheater 16 are discharged is connected; The potato spirit alcohol extraction mouth of rectifying tower 17 charging layers top is connected successively with the inlet of potato spirit water cooler 21, potato spirit separator 22; Potato spirit separator 22 is provided with dilution water inlet, potato spirit extraction mouth and light wine outlet, and the light wine outlet is connected with the inlet of assorted thick wine jar 15;
The alcohol gas inlet of molecular sieve adsorption/Analytic Tower 12 bottoms is connected successively with the outlet of raw wine vapour superheater 11 and ethanol vapor gas compressor 9; The alcohol steam outlet at molecular sieve adsorption/Analytic Tower 12 tops forms loop structure with regeneration wine vapour superheater 13; The light wine vapor outlet of molecular sieve adsorption/Analytic Tower 12 bottoms is connected with light wine vapour condenser 14, thick wine jar 15 successively.
Utilize embodiment 1 described device to produce alcohol fuel, Ipomoea batatas fermenting-ripening mash is a raw material:
From the next 13%V/V fermenting-ripening mash of fermentation workshop section, temperature is 30 ℃, flow is 144t/h, be preheating to 45 ℃, the second mash preheater 2 through the first mash preheater 1 successively and enter topping still 4 after being preheating to 70 ℃, the wine vapour at topping still 4 tops (55 ℃ of temperature, pressure-70kPa) through entering thick wine jar 15 after mash first preheater 1 and topping still condenser 5 and 6 condensations of topping still last condenser stage.Simultaneously also enter thick wine jar 15 from the light wine of molecular sieve dehydration device light wine vapour condenser 14 with from the light wine of potato spirit separator 22.Enter rectifying tower 17 after thick wine is preheating to 90 ℃ by crude wine preheater 16 and carry out concentration, thermal source is the waste water that discharge rectifying tower 17 bottoms.The fermenting-ripening mash outgases after entering combined column, partly degassed mash (67 ℃ of temperature, flow 100t/h, account for total mash amount 70%) extract out from the topping still side line, enter combined column 8 stripping sections after wine with dregs wine with dregs interchanger 7 is preheating to 91 ℃, the thermal source of wine with dregs wine with dregs interchanger 7 is useless wine with dregs that combined column 8 tower stills are discharged.The light wine of combined column 8 rectifying sections bottom extraction (95 ℃ of temperature, flow 10.1t/h), enter rectifying tower 17 further concentration.The useless wine with dregs of combined column 8 bottoms enters topping still tower still after wine with dregs wine with dregs interchanger 7 cooling, remove effluent treatment plant from the useless wine with dregs of topping still 4 tower still extraction.The top extraction of rectifying tower 17 charging layers is rich in the alcohol of potato spirit after 21 coolings of potato spirit water cooler, enters potato spirit separator 22, adds dilution water and dilutes layering, isolates potato spirit.Light wine is sent to thick wine jar 15.Rectifying tower waste water is by process water or the potato spirit diluting water of crude wine preheater 16 cooling backs as other workshops.
Combined column top 95%V/V wine vapour (78 ℃ of temperature, pressure 0kPa) compressed machine 9 is divided into two strands after being compressed to 80kPa, first strand of wine vapour (accounting for volume percent 35% ratio) is as the thermal source of topping still reboiler 10, and condensation wine liquid enters combined column return tank 19, returns combined column (8) top again.Second strand of wine vapour (accounting for volume percent 65% ratio) is superheated to 120 ℃ through raw wine vapour superheater 11, from bottom to top sieve adsorpting bed 12 dehydrations by being in adsorbed state.The product alcohol vapour of volume percent 25% enters regeneration wine vapour superheater 13, enters into the moisture in another molecular sieve tower 12 desorbed molecules sieve then, and after taking moisture 14 condensations of to light wine vapour condenser, phlegma closes at thick wine jar 15.Alcohol steam after the dehydration does not wherein coagulate wine vapour through the 24 further condensations of dehydrated alcohol finished product condenser as the thermal source of the second mash preheater 2, and condensed dehydrated alcohol finished wine liquid enters dehydrated alcohol jar 26 through 25 coolings of dehydrated alcohol water cooler.The dehydrated alcohol finished product obtains alcohol fuel after adding the denaturing agent sex change.
The working pressure of each distillation tower and molecular sieve adsorption Analytic Tower, cat head and column bottom temperature are respectively:
The operation of topping still cat head is pressed and is-70kPa 55 ℃ of tower top temperatures, 70 ℃ of column bottom temperatures;
Combined column cat head working pressure is 0kPa, 78 ℃ of tower top temperatures, 105 ℃ of column bottom temperatures;
Rectifying tower cat head working pressure is 220kPa, 110 ℃ of tower top temperatures, 138 ℃ of column bottom temperatures;
The adsorbing tower with molecular sieve working pressure is 0kPa, and molecular sieve Analytic Tower working pressure is-80kPa.
This technology is produced 100000 tons of alcohol fuels (year production time 7920h) per year, and the distillation rate is more than 99%.Ton product steam (0.5MPa gauge pressure) consumption is the 1.29t/t alcohol fuel, and end product quality satisfies alcohol fuel standard GB 18350-2001.
Embodiment 3
Utilize embodiment 1 described device to produce general level edible ethanol, cassava fermenting-ripening mash is a raw material:
From the next 13.5%V/V fermenting-ripening mash of fermentation workshop section, temperature is 30 ℃, flow is 135t/h, be preheating to 54 ℃, the 3rd mash preheater 3 through the first mash preheater 1 successively and enter topping still after being preheating to 75 ℃, the wine vapour at topping still top (75 ℃ of temperature, pressure-30kPa) through entering thick wine jar 15 after mash first preheater 1 and topping still condenser 5 and 6 condensations of topping still last condenser stage.Light wine from potato spirit separator 22 also enters thick wine jar 15 simultaneously.Enter rectifying tower 17 after thick wine is preheating to 88 ℃ by crude wine preheater 16 and carry out concentration, thermal source is the waste water that discharge rectifying tower 17 bottoms.Ripe wine with dregs (68 ℃ of the temperature of part after the degassing, flow 79t/h, account for total mash 58%) extract out from the topping still side line, after 7 preheatings of wine with dregs wine with dregs interchanger, enter combined column 8 stripping sections, the light wine of combined column 8 rectifying sections bottom extraction enters rectifying tower 17 further concentration.The useless wine with dregs of combined column 8 bottoms enters topping still tower still after wine with dregs wine with dregs interchanger 7 cooling, remove effluent treatment plant from the useless wine with dregs of topping still 4 tower still extraction.The alcohol that the extraction of rectifying tower 17 charging layers top contains potato spirit is cooled to 28 ℃ through potato spirit water cooler 21, enters potato spirit separator 22, adds process water and dilutes and isolate potato spirit (flow 41kg/h, 28 ℃ of temperature).Potato spirit light wine is sent to thick wine jar 15.Rectifying tower 17 bottom waste water are by process water or the potato spirit diluting water of crude wine preheater 16 cooling backs as other workshops.
Combined column 8 top wine vapour (78.5 ℃ of temperature, pressure 3kPa) after 9 compressions (top hole pressure 115kPa) of ethanol vapor gas compressor, is divided into two strands, first strand of wine vapour (accounting for volume percent 48% ratio) is as the thermal source of methanol column reboiler 29, the wine liquid of condensation enters combined column return tank 19, and it refluxes as combined column 8 tops; Entering methanol column 27 from the wine liquid of combined column 8 tops the 2nd laminate extraction carries out separating methanol and handles, methanol column 27 cat head wine vapour are as the thermal source of the 3rd mash preheater 3, the industrial spirit (flow 205kg/h) of methyl alcohol partly is rich in 28 extraction of methanol column last condenser stage, the remaining methanol column return tank 30 that enters is returned methanol column (27) top refluxing opening then; The few general level edible ethanol of extraction methanol content at the bottom of methanol column (27) tower; Second strand of wine vapour (accounting for volume percent 52% ratio) is as the thermal source of topping still reboiler (10), and condensation wine liquid is sent combined column (8) top refluxing opening back to.
The working pressure of each distillation tower and molecular sieve adsorption Analytic Tower, cat head and column bottom temperature are respectively:
The operation of topping still cat head is pressed and is-30kPa 70 ℃ of tower top temperatures, 95 ℃ of column bottom temperatures;
Combined column cat head working pressure is 3kPa, 78.5 ℃ of tower top temperatures, 105 ℃ of column bottom temperatures;
Rectifying tower cat head working pressure is 220kPa, 110 ℃ of tower top temperatures, 138 ℃ of column bottom temperatures;
Methyl alcohol cat head working pressure is-50kPa 62 ℃ of tower top temperatures, 72 ℃ of column bottom temperatures;
This technology is produced 100000 tons of general level edible ethanols (year production time 7920h) per year, and the distillation rate is more than 99%.Ton product steam (0.5MPa gauge pressure) consumption is the general level of a 1.21t/t edible ethanol, and quality product satisfies the general level edible ethanol standard among the GB/T10343-2008.
Embodiment 4
Utilize embodiment 1 described device to produce alcohol fuel and general level edible ethanol, the ripe mash of corn fermentation is a raw material:
From the next 13%V/V fermenting-ripening mash of fermentation workshop section, temperature is 30 ℃, flow is 167t/h, being preheating to 45 ℃, the second mash preheater 2 through the first mash preheater 1 successively is preheating to and enters topping still after 65 ℃ and the 3rd mash preheater 3 are preheating to 75 ℃, the wine vapour at topping still top enters thick wine jar 15 through mash first preheater 1 and topping still condenser 5 after 6 condensations of topping still last condenser stage.Also enter thick wine jar 15 from the light wine of molecular sieve pressure-swing absorption apparatus generation and the potato spirit light wine of potato spirit separator 22 simultaneously.The waste water (139 ℃ of temperature) that thick wine is discharged through rectifying tower 17 bottoms is preheating to 114 ℃ and enters rectifying tower 17 and carry out concentration.The ripe wine with dregs of part after the degassing (67 ℃ of temperature, flow 96.8t/h) is extracted out from the topping still side line, enters combined column 8 stripping sections after wine with dregs wine with dregs interchanger 7 is preheating to 96 ℃, and the light wine of combined column 8 rectifying sections bottom extraction enters rectifying tower 17 further concentration.The useless wine with dregs of combined column bottom enters topping still tower still after the heat exchange of wine with dregs wine with dregs, go between feed carriage concentrate drying to handle from the useless wine with dregs of topping still tower still extraction, and it is golden yellow that the feed color and luster is, and color and luster improves greatly than the chocolate of former technology (publication number is CN101580457A).The extraction of rectifying tower 17 charging layers top contains the alcohol of potato spirit after 21 coolings of potato spirit water cooler, enters potato spirit separator 22, adds process water and dilutes and isolate potato spirit, and potato spirit light wine is sent to thick wine jar 15.Rectifying tower waste water is by process water or the potato spirit diluting water of crude wine preheater 16 cooling backs as other workshops.
Combined column 8 top wine vapour (79 ℃ of temperature, pressure 6.5kPa) after 9 compression of ethanol vapor gas compressor (top hole pressure 82kPa), be divided into three strands, first strand of wine vapour (accounting for 31% ratio) is as the thermal source of methanol column reboiler 29, the wine liquid of condensation enters combined column return tank 20, being re-used as combined column 8 tops refluxes, entering methanol column 27 behind the 3rd layer of column plate extraction wine liquid of combined column 8 tops carries out separating methanol and handles, cat head wine vapour is as the thermal source of the 3rd mash preheater 3, industrial spirit (72 ℃ of the temperature of methyl alcohol partly are rich in 28 extraction of methanol column last condenser stage, flow 240kg/h), remaining wine liquid enters methanol column return tank 30, returns methanol column top refluxing opening then; The general level edible ethanol (flow 8334kg/h) that the extraction methanol content is few at the bottom of methanol column 27 towers enters general level edible ethanol finished product jar 32 after general level edible ethanol finished product water cooler 31 is cooled to 30 ℃; Second strand of wine vapour (accounting for 34% ratio) is as the thermal source of topping still reboiler 10, and condensation wine liquid enters combined column return tank 19, sends combined column 8 tops back to by the combined column reflux pump.The 3rd strand of wine vapour (accounting for 35% ratio) is superheated to 118 ℃ through raw wine vapour superheater 11, by sieve adsorpting bed 12 dehydrations that are in adsorbed state.The product alcohol vapour that accounts for the total volume of exports 18% enters regeneration wine vapour superheater 13, enters into the moisture in another molecular sieve tower 12 desorbed molecules sieve then, and after taking moisture 14 condensations of to light wine vapour condenser, phlegma closes at thick wine jar 15.Alcohol steam after the dehydration does not coagulate wine vapour through the 24 further condensations of dehydrated alcohol finished product condenser as the thermal source of the 3rd mash preheater 3, and condensation wine liquid enters dehydrated alcohol finished product jar 26 through 25 coolings of dehydrated alcohol water cooler.The dehydrated alcohol finished product obtains alcohol fuel after adding the denaturing agent sex change.
The working pressure of each distillation tower and molecular sieve adsorption Analytic Tower, cat head and column bottom temperature are respectively:
The operation of topping still cat head is pressed and is-70kPa 55 ℃ of tower top temperatures, 75 ℃ of column bottom temperatures;
Combined column cat head working pressure is 6.5kPa, 79 ℃ of tower top temperatures, 105 ℃ of column bottom temperatures;
Rectifying tower cat head working pressure is 220kPa, 110 ℃ of tower top temperatures, 139 ℃ of column bottom temperatures;
Methyl alcohol cat head working pressure is-40kPa 65 ℃ of tower top temperatures, 75 ℃ of column bottom temperatures;
The adsorbing tower with molecular sieve working pressure is 30kPa, and molecular sieve Analytic Tower working pressure is-60kPa.
This technology is produced 60000 tons of alcohol fuels of 60,000 tons of general level edible ethanol coproduction (year production time 7920h) per year, and the distillation rate is more than 99%.Ton product steam (0.5MPa gauge pressure) consumption is 1.39t/t alcohol fuel+general level edible ethanol, and quality product satisfies the general level edible ethanol standard among alcohol fuel standard GB 18350-2001 and the GB/T 10343-2008 respectively.
The foregoing description is the utility model preferred implementation; but embodiment of the present utility model is not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present utility model and the principle, substitutes, combination, simplify; all should be the substitute mode of equivalence, be included within the protection domain of the present utility model.
Claims (7)
1. the distillation dehydration device of alcohol fuel and the coproduction of general level edible ethanol, comprise molecular sieve adsorption/Analytic Tower (12), topping still (4), combined column (8), rectifying tower (17), methanol column (27), the placed in-line successively first mash preheater (1) of tube side, the second mash preheater (2) and the 3rd mash preheater (3); It is characterized in that:
The first mash preheater (1) is provided with mash inlet, mash outlet, hot junction inlet and hot junction outlet, wherein: the mash inlet is connected with fermenting-ripening mash inlet, the mash outlet is connected with the mash inlet of the second mash preheater (2), the hot junction inlet is connected with the wine vapor outlet of topping still (4), and the hot junction outlet is connected with thick wine jar (15);
The second mash preheater (2) is provided with mash inlet, mash outlet, hot junction inlet and hot junction outlet, wherein: the mash outlet is connected with the mash inlet of the 3rd mash preheater (3), the mash inlet of topping still (4) respectively, the hot junction inlet is connected with the alcohol steam outlet at molecular sieve adsorption/Analytic Tower (12) top, and the hot junction outlet is connected with dehydrated alcohol finished product jar (26);
The 3rd mash preheater (3) is provided with mash inlet, mash outlet, hot junction inlet and hot junction outlet, wherein: the mash outlet is connected with the mash inlet of topping still (4), the hot junction inlet is connected with the wine vapor outlet of methanol column (27), and the hot junction outlet is connected with the top refluxing opening of methanol column (27);
Topping still (4) outer setting is used for the side line extraction device of the ripe mash after the extraction degassing and is used to provide the topping still reboiler (10) of heat, and wherein: the mash outlet of side line extraction device is connected successively with wine with dregs wine with dregs interchanger (7), combined column (8); Topping still reboiler (10) is provided with hot junction inlet and hot junction outlet, and the hot junction inlet is connected with the outlet of ethanol vapor gas compressor (9), and the hot junction outlet is connected successively with combined column return tank (19), combined column (8) top layer column plate refluxing opening;
Combined column (8) outer setting be used to compress combined column (8) preparation wine vapour ethanol vapor gas compressor (9) and be used to provide the combined column reboiler (18) of heat, wherein: ethanol vapor gas compressor (9) is connected with topping still reboiler (10), methanol column reboiler (29), raw wine vapour superheater (11) respectively; Combined column reboiler (18) is provided with hot junction inlet and hot junction outlet, the hot junction inlet is connected with the wine vapor outlet of rectifying tower (17), the hot junction outlet is connected with rectifying tower return tank (20), and rectifying tower return tank (20) is connected with the refluxing opening of rectifying tower (17), the top tray opening for feed of combined column (8) respectively; Combined column (8) is connected with rectifying tower (17) by the light wine extraction mouth that is arranged on the rectifying section bottom; Combined column (8) is connected with methanol column (27) by the wine liquid outlet that is arranged on the top; Wine with dregs wine with dregs interchanger (7) also is provided with the useless wine with dregs inlet and the wine with dregs outlet of giving up, and useless wine with dregs inlet is connected with the useless wine with dregs outlet of combined column (8);
The opening for feed of rectifying tower (17) is connected successively with the extraction mouth of crude wine preheater (16), thick wine jar (15), and the hot junction inlet of crude wine preheater (16) is connected with the wastewater outlet of rectifier bottoms; Rectifying tower (17) is connected with the rectifying tower reboiler (23) that is used to provide heat, potato spirit separator (22) respectively; Potato spirit separator (22) is provided with dilution water inlet, potato spirit extraction mouth and light wine outlet, and the light wine outlet is connected with the inlet of thick wine jar (15);
Methanol column (27) tower still is connected with general level edible ethanol finished product jar (32); Methanol column (27) be used to provide the methanol column reboiler (29) of heat to be connected, the hot junction of methanol column reboiler (29) inlet is connected with the outlet of ethanol vapor gas compressor (9), the hot junction exports to enter the mouth with the wine liquid of combined column return tank (19) and is connected;
The alcohol gas inlet of molecular sieve adsorption/Analytic Tower (12) bottom is connected successively with the outlet of raw wine vapour superheater (11), ethanol vapor gas compressor (9); The alcohol steam outlet and the regeneration wine vapour superheater (13) at molecular sieve adsorption/Analytic Tower (12) top form loop structure; The light wine vapor outlet of molecular sieve adsorption/Analytic Tower (12) bottom is connected with light wine vapour condenser (14), thick wine jar (15) successively.
2. according to the distillation dehydration device of described alcohol fuel of claim 1 and the coproduction of general level edible ethanol, it is characterized in that: between described first mash preheater (1) and the described thick wine jar (15) topping still condenser (5) and topping still last condenser stage (6) are set also; The hot junction outlet of the described first mash preheater (1) comprises gaseous phase outlet and liquid phase outlet, gaseous phase outlet is connected successively with topping still condenser (5), topping still last condenser stage (6), and the liquid phase outlet of liquid phase outlet, topping still condenser (5), the liquid phase outlet of topping still last condenser stage (6) are connected by the inlet of pipeline with thick wine jar respectively; Topping still last condenser stage (6) is provided with gaseous phase outlet.
3. according to the distillation dehydration device of described alcohol fuel of claim 2 and the coproduction of general level edible ethanol, it is characterized in that: between described second mash preheater (2) and the described dehydrated alcohol finished product jar (26) dehydrated alcohol finished product condenser (24) and dehydrated alcohol water cooler (25) are set also; The hot junction outlet of the described second mash preheater (2) comprises dehydrated alcohol gaseous phase outlet and the outlet of dehydrated alcohol liquid phase, the dehydrated alcohol gaseous phase outlet is connected with dehydrated alcohol finished product condenser (24), and the outlet of dehydrated alcohol liquid phase is connected with the hot junction liquid phase inlet of dehydrated alcohol water cooler (25) by pipeline respectively with the liquid phase outlet of dehydrated alcohol finished product condenser (24); The hot junction liquid phase outlet of dehydrated alcohol water cooler (25) is connected with dehydrated alcohol finished product jar (26).
4. according to the distillation dehydration device of described alcohol fuel of claim 3 and the coproduction of general level edible ethanol, it is characterized in that: between described the 3rd mash preheater (3) and the described methanol column (27) methanol column last condenser stage (28) and methanol column return tank (30) are set also; The hot junction outlet of described the 3rd mash preheater (3) comprises gaseous phase outlet and liquid phase outlet, gaseous phase outlet is connected with methanol column last condenser stage (28), the liquid phase outlet of methanol column last condenser stage (28) is connected with methanol column return tank (30) inlet, and the liquid phase outlet is connected with the top refluxing opening of methanol column return tank (30), methanol column (27) successively.
5. according to the distillation dehydration device of described alcohol fuel of claim 4 and the coproduction of general level edible ethanol, it is characterized in that: the useless wine with dregs outlet of described wine with dregs wine with dregs interchanger (7) is connected with topping still (4) tower still.
6. according to the distillation dehydration device of described alcohol fuel of claim 5 and the coproduction of general level edible ethanol, it is characterized in that: between described rectifying tower (17) and the potato spirit separator (22) potato spirit water cooler (21) is set also.
7. according to the distillation dehydration device of each described alcohol fuel of claim 1～6 and the coproduction of general level edible ethanol, it is characterized in that: general level edible ethanol finished product water cooler (31) also is set between described methanol column (27) and the described general level edible ethanol finished product jar (32).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206085956U CN201850234U (en) | 2010-11-16 | 2010-11-16 | Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206085956U CN201850234U (en) | 2010-11-16 | 2010-11-16 | Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201850234U true CN201850234U (en) | 2011-06-01 |
Family
ID=44092634
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010206085956U Expired - Lifetime CN201850234U (en) | 2010-11-16 | 2010-11-16 | Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201850234U (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040471A (en) * | 2010-11-16 | 2011-05-04 | 广东中科天元新能源科技有限公司 | Distillation dehydration device and process for co-producing ethanol fuels and custom grade edible alcohols |
| CN102351644A (en) * | 2011-08-19 | 2012-02-15 | 天津大学 | Method and device for molecular sieve compound rectifying and refining ethanol product from biobutanol apparatus |
| CN103316498A (en) * | 2013-06-28 | 2013-09-25 | 中国轻工业广州工程有限公司 | General distillation unit for edible alcohol and fuel alcohol |
| CN109776266A (en) * | 2019-02-28 | 2019-05-21 | 肥城金塔酒精化工设备有限公司 | A kind of energy-saving equipment and its power-economizing method producing absolute alcohol |
| CN110698325A (en) * | 2019-08-02 | 2020-01-17 | 广东中科天元新能源科技有限公司 | Production device and process for co-producing fuel ethanol and special grade edible alcohol |
| CN110922303A (en) * | 2019-12-30 | 2020-03-27 | 肥城金塔酒精化工设备有限公司 | Negative pressure mash tower degassing and aldehyde-discharging acid-discharging device for fuel ethanol and edible alcohol |
-
2010
- 2010-11-16 CN CN2010206085956U patent/CN201850234U/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040471A (en) * | 2010-11-16 | 2011-05-04 | 广东中科天元新能源科技有限公司 | Distillation dehydration device and process for co-producing ethanol fuels and custom grade edible alcohols |
| CN102040471B (en) * | 2010-11-16 | 2013-07-10 | 广东中科天元新能源科技有限公司 | Distillation dehydration device and process for co-producing ethanol fuels and custom grade edible alcohols |
| CN102351644A (en) * | 2011-08-19 | 2012-02-15 | 天津大学 | Method and device for molecular sieve compound rectifying and refining ethanol product from biobutanol apparatus |
| CN103316498A (en) * | 2013-06-28 | 2013-09-25 | 中国轻工业广州工程有限公司 | General distillation unit for edible alcohol and fuel alcohol |
| CN103316498B (en) * | 2013-06-28 | 2015-05-13 | 中国轻工业广州工程有限公司 | General distillation unit for edible alcohol and fuel alcohol |
| CN109776266A (en) * | 2019-02-28 | 2019-05-21 | 肥城金塔酒精化工设备有限公司 | A kind of energy-saving equipment and its power-economizing method producing absolute alcohol |
| CN110698325A (en) * | 2019-08-02 | 2020-01-17 | 广东中科天元新能源科技有限公司 | Production device and process for co-producing fuel ethanol and special grade edible alcohol |
| CN110922303A (en) * | 2019-12-30 | 2020-03-27 | 肥城金塔酒精化工设备有限公司 | Negative pressure mash tower degassing and aldehyde-discharging acid-discharging device for fuel ethanol and edible alcohol |
| CN110922303B (en) * | 2019-12-30 | 2024-04-19 | 肥城金塔酒精化工设备有限公司 | Negative pressure mash tower degassing, aldehyde and acid discharging device for fuel ethanol and edible alcohol |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102040471B (en) | Distillation dehydration device and process for co-producing ethanol fuels and custom grade edible alcohols | |
| CN201850234U (en) | Distillation dehydration device for fuel alcohol and ordinary edible alcohol co-production | |
| CN101580457B (en) | Device and process for preparing absolute ethyl alcohol by taking fermented liquor as the raw material | |
| CN102126920B (en) | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration | |
| CN108558602B (en) | System for producing fuel ethanol by double-coarse double-fine four-tower four-effect energy-saving distillation and application method thereof | |
| CN104262089B (en) | The method and device that the dehydration of a kind of bio-fuel is refined | |
| CN104788289A (en) | Heat pump coupling process for ethylene glycol rectification | |
| CN101153257A (en) | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof | |
| CN114031580B (en) | Refining device and refining method for low-energy PBAT byproduct tetrahydrofuran | |
| CN110143850A (en) | The not energy-saving methanol multi-effect distillation method of the single column steam drive of by-product fusel oil | |
| CN107418979A (en) | A kind of alcohol fuel energy-saving clean production method | |
| CN109646980B (en) | Fusel-free oil dividing wall tower coupled methanol multi-effect rectification energy-saving device and method | |
| CN101412665A (en) | Apparatus for coproduction of refined methanol and dimethyl ether or production of each of refined methanol and dimethyl ether from coarse methyl alcohol | |
| CN201253496Y (en) | Alcohol three-effect differential pressure distillation equipment | |
| CN211411045U (en) | Methanol distillation tower | |
| CN106675616B (en) | The method for reducing catalytic cracking unit Vapor recovery unit part supplement absorbent dosage | |
| CN110483249A (en) | A kind of six tower quadruple effect rectificating method of single column steam drive type methanol of not by-product fusel oil | |
| CN213085848U (en) | Distillation dehydration production device for co-producing high-grade edible alcohol and fuel ethanol | |
| CN112961033B (en) | Five-tower five-effect rectification process method and device for methanol | |
| CN104016833B (en) | The processing method of the integrated rectifying ethanol of three tower heat | |
| CN104140357A (en) | Method for producing ethanol with acetic acid as raw material | |
| CN111807928A (en) | Distillation dehydration production device and method for co-producing superior edible alcohol and fuel ethanol | |
| CN220176078U (en) | Distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermented mash | |
| CN217794591U (en) | Differential pressure thermal coupling rectifying device for separating light dihydric alcohol from coal-to-ethylene glycol | |
| CN220404864U (en) | Baffle rectifying tower for rectifying methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20110601 Effective date of abandoning: 20130710 |
|
| RGAV | Abandon patent right to avoid regrant |