CN1896253A - Production of alcohol during non-distilling process - Google Patents
Production of alcohol during non-distilling process Download PDFInfo
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- CN1896253A CN1896253A CNA2006100178847A CN200610017884A CN1896253A CN 1896253 A CN1896253 A CN 1896253A CN A2006100178847 A CNA2006100178847 A CN A2006100178847A CN 200610017884 A CN200610017884 A CN 200610017884A CN 1896253 A CN1896253 A CN 1896253A
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- alcohol
- vaporizer
- flasher
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Production of alcohol during non-distilling process is carried out by fermenting for raw material bacterium in normal-pressure fermenter, entering the fermented material into vacuum flash evaporator, flash evaporating and separating, delivering the separated mixed gas of alcohol and water into condenser, condensing to obtain alcohol solution, vaporizing by vaporizer, removing water-content by adsorptive tower to obtain high-concentration alcohol, returning the separated liquid to fermenter to re-ferment, returning the liquid flash-evaporated and separated to fermenter, heating partly, returning it to the second-stage flash evaporator, extracting material from vaporizer bottom, heating and returning to vaporizer to vaporize. It is simple and has less consumption.
Description
Technical field
The invention belongs to the alcohol production technical field, particularly a kind of alcohol production technology of non-distilling.
Background technology
Existing ethanol and fuel ethanol production process are: feedstock production-→ fermentation-→ distillation-→ ethanol-→ dehydration-→ dehydrated alcohol-→ alcohol fuel.Feedstock production is divided into the preparation of starchiness, molasses and fibrous material.Starchy material need carry out pre-treatment such as removal of impurities, pulverizing, ferments after the saccharification liquefaction processing again.After need diluting, molasses raw material ferments again.Fibrous material need carry out acid hydrolysis or enzymic hydrolysis is fermented then.Zymamsis comprises preparation, enlarged culturing and the industrial fermentation of distillery yeast, obtains sophisticated karusen at last.
In alcohol industry is produced, need through distillation workshop section as single-minded from the fermenting-ripening wine with dregs to finished wine, distillation workshop section was divided into for two steps: the first is separated alcohol and all volatile impunties-still-process (claiming again slightly to heat up in a steamer) from the fermenting-ripening wine with dregs.The distillatory result obtains crude alcohol and vinasse (comprising water and non-volatility impurity), and used equipment is called distillation tower (wine with dregs tower or topping still); It two is the impurity of removing in the crude alcohol, further improves the process of ethanol concn.Used equipment is rectifying tower, can obtain finished product and fusel wet goods byproduct.Alcohol production all adopts continuous still battery, rectification process both at home and abroad, and this technology is divided into two tower flow processs, three-column process flow and multitower flow process again.Rectifying tower is wherein most important operating equipment, and whether its stable operation is directly connected to the height of quality product.Distillation workshop section is the workshop section of energy consumption maximum, accounts for alcohol (this moment, 95% (W) alcohol was finished product) and produces about 60% of total energy consumption.
The method of dehydrated alcohol preparation can reduce two big classes: rectification method and absorption method.Rectification method is divided into azeotropic dehydration, ion-exchange evaporation again and adds dehydration of salt method etc.The used energy consumption of this azeotropic distillation accounts for about 1/3 of whole dehydrated alcohol production process total energy consumption, and therefore this method energy consumption is too high, also has pollutant emission simultaneously; Absorption method is different because of the sorbent material that adopts, and is that sorbent material dewaters with lime, sodium Metal 99.5, silica gel, molecular sieve, cereal generally.This method has the advantages that energy consumption is low, production process does not have the three wastes and production cost is low, uses more and more widely.In the majority in the alcohol production factory both at home and abroad with the molecular sieve adsorption application, but exist the defective that sorbent material is on the high side, the finished product yield is on the low side; The cereal absorption method is used in the majority with the U.S., compare with sieve method, and cheap, application prospect is fine, but fluid by the time sorbent material resistance big, energy consumption is higher during regeneration.
Alcohol fuel adds denaturing agent and obtains in dehydrated alcohol, the production of fuel ethanol cost depends primarily on the height of dehydrated alcohol production energy consumption.
Summary of the invention
The object of the invention is to provide the alcohol production technology of the low non-distilling of a kind of energy consumption.
For reaching above-mentioned purpose, the present invention adopts following technical scheme: the alcohol production technology of non-distilling, comprise raw material and the bacterial classification fermenting process in the normal pressure fermentor tank, material after the fermentation enters vacuum flasher and carries out flash separation, enter condenser condenses through the isolated ethanol of flasher, water mixed gas, condensation gained aqueous ethanolic solution is vaporized and is removed moisture through adsorption tower through vaporizer and gets high concentration ethanol; Returning fermentor tank through the isolated liquid of flash separator further ferments.
The flash separation step comprises the above flash separation of two-stage, and the liquid portion that the final stage flash separation goes out returns fermentor tank, part and return final stage flasher continuation flash separation after heating.
The material extraction of vaporizer bottom is returned vaporizer again through heating and is vaporized.
The heating thermal source is the low-grade heat source that produces in the production process.
Alcohol production device among the present invention comprises the normal pressure fermentor tank, and the fermentor tank material outlet is connected with the vacuum flasher material inlet by pipeline, and flasher gaseous state material outlet is connected with interchanger, vaporizer, dehydration tower by pipeline successively; The outlet of flasher liquid material is connected with fermentor tank by the pipeline that is serially connected with suction pump.
Flasher comprises that the top connects the one-level flasher of vacuum pump, one-level flasher discharge port is connected with the secondary flash vessel opening for feed by pipeline, final stage flasher gaseous state material outlet is connected with vacuum interchanger opening for feed by pipeline, and vacuum interchanger discharge port is connected with vaporizer top opening for feed; The outlet of final stage flasher liquid material is connected with fermentor tank by the pipeline that is serially connected with suction pump.
Final stage flasher bottom discharge mouth is connected with the opening for feed of described discharge port top by the pipeline that is serially connected with suction pump and interchanger.
Vaporizer bottom discharge mouth is connected with the opening for feed of described discharge port top by the pipeline that is serially connected with suction pump and interchanger.
Thereby the invention provides a kind of dewatering integrated alcohol production technology of ethanol fermentation of removing the meta-bolites feedback inhibition of separating while fermenting, removed the still-process of energy consumption maximum in the dehydrated alcohol production process, realized the alcohol production of no rectifying, can significantly reduce production energy consumption, reduce the production of fuel ethanol cost.Utilize the present invention the concentration of fermentor tank intracellular metabolite product can be controlled at below 4% (wt), mash is after flasher separates, and the alcohol concn of getting back in the fermentor tank is lower than 1 ‰ (wt), removes the feedback inhibition of meta-bolites with this, improves fermentation production rate; By separating obtained product after two-stage or the above flash distillation of two-stage, revaporization enters the adsorption dewatering tower product that obtains that dewaters and meets national alcohol fuel standard GB18350-2001; Flasher uses the low-grade heat (40 ℃-90 ℃) of a large amount of existence in the factory to keep the vacuum separation process, can be energy-conservation significantly, realize that waste heat utilizes again.
The present invention is applicable to all alcohol production raw materials, and basic material can adopt continuous interpolation, realizes continuous production.
Description of drawings
Fig. 1 is an apparatus structure synoptic diagram among the embodiment 1;
Fig. 2 is an apparatus structure synoptic diagram among the embodiment 2;
Fig. 3 is an apparatus structure synoptic diagram among the embodiment 3.
Embodiment
The alcohol production technology of embodiment 1, non-distilling, comprise raw material and the bacterial classification fermenting process in the normal pressure fermentor tank, material after the fermentation enters the two-stage vacuum flasher and carries out flash separation, enter condenser condenses through the isolated ethanol of flasher, water mixed gas, condensation gained aqueous ethanolic solution is vaporized and is removed moisture through adsorption tower through vaporizer and gets high concentration ethanol; Returning fermentor tank through the isolated liquid of flash separator further ferments.The heating thermal source is the low-grade heat source that produces in the production process.The present embodiment equipment therefor comprises fermentor tank 1, fermentor tank 1 is the normal pressure fermentor tank, fermentor tank 1 material outlet connects with one-level flasher 2 opening for feeds that are connected vacuum pump 3 by pipeline, one-level flasher 2 bottom discharge mouths are connected with two-stage flash device 5 opening for feeds by pipeline, the gaseous state material outlet at two-stage flash device 5 tops is connected by interchanger 6 opening for feeds of pipeline with band vacuum pump 7, interchanger 6 discharge ports are connected with vaporizer 8 top opening for feeds, the outlet of vaporizer 8 top materials is connected with dehydration tower 11 opening for feeds by pipeline, and dehydration tower 11 tops are provided with the product outlet.The outlet of two-stage flash device 5 liquid materials is connected with fermentor tank 1 bottom by the pipeline that is serially connected with suction pump 4.
In embodiment 2, the present embodiment, the liquid portion that the final stage flash separation goes out returns fermentor tank, part is returned the final stage flasher after heating.In the present embodiment equipment therefor, two-stage flash device 5 bottom discharge mouths are connected with the opening for feed of described discharge port top by the pipeline that is serially connected with suction pump 12 and interchanger 13, can utilize by interchanger 13 that low grade heat energy heats material in the ethanol production process, quicken feed separation.Other are with embodiment 1.
In embodiment 3, the present embodiment, the material extraction of vaporizer bottom is returned vaporizer again through heating and is vaporized.In the present embodiment in the equipment therefor, vaporizer 8 bottom discharge mouths are connected with the opening for feed of described discharge port top by the pipeline that is serially connected with suction pump 10 and interchanger 9, can utilize by interchanger 9 that low grade heat energy heats material in the ethanol production process, quicken the material vaporization.Other are with embodiment 2.
In the foregoing description, raw material and bacterial classification join in the fermentor tank and ferment, when the ethanol concn in the fermented liquid reaches 4-5% (wt) (below be mass percent concentration), start two-stage or the above vacuum flashing device of two-stage, the ethanol that the final stage flasher flashes off, the liquid of water gas mixture after condenser condenses are called light wine (ethanol content 〉=20%), enter in the collector, the liquid (ethanol content≤1 ‰) of final stage vacuum flasher bottom returns fermentor tank.Reduced the alcohol accumulation amount in the fermented liquid so on the one hand, reduced the zymic restraining effect; Also played the purpose of fermented liquid pump circulation on the other hand, overcome because the disadvantageous effect of the too high inhibition yeast growth of the local alcohol concn of static fermentation.Utilize in the factory a large amount of 40-90 ℃ of low-grade heat sources heating that exist, light wine is entered in the vaporizer, further vaporization becomes 64.9% alcohol gas, enters dehydration adsorption tower adsorption dewatering again, becomes 〉=99.6% dehydrated alcohol through condenser condenses then.
Claims (4)
1, the alcohol production technology of non-distilling, it is characterized in that, comprise raw material and the bacterial classification fermenting process in the normal pressure fermentor tank, material after the fermentation enters vacuum flasher and carries out flash separation, enter condenser condenses through the isolated ethanol of flasher, water mixed gas, condensation gained aqueous ethanolic solution is vaporized and is removed moisture through adsorption tower through vaporizer and gets high concentration ethanol; Returning fermentor tank through the isolated liquid of flash separator further ferments.
2, the alcohol production technology of non-distilling as claimed in claim 1, it is characterized in that, the flash separation step comprises the above flash separation of two-stage, and the liquid portion that the final stage flash separation goes out returns fermentor tank, part and return final stage flasher continuation flash separation after heating.
3, the alcohol production technology of non-distilling as claimed in claim 2 is characterized in that, the material extraction of vaporizer bottom is returned vaporizer again through heating and vaporized.
As the alcohol production technology of claim 2 or 3 described non-distillings, it is characterized in that 4, the heating thermal source is the low-grade heat source that produces in the production process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006100178847A CN1896253A (en) | 2006-06-02 | 2006-06-02 | Production of alcohol during non-distilling process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006100178847A CN1896253A (en) | 2006-06-02 | 2006-06-02 | Production of alcohol during non-distilling process |
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| CN1896253A true CN1896253A (en) | 2007-01-17 |
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| CNA2006100178847A Pending CN1896253A (en) | 2006-06-02 | 2006-06-02 | Production of alcohol during non-distilling process |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100493620C (en) * | 2007-04-02 | 2009-06-03 | 郑州大学生化工程中心 | Continuously sterilizing two-stage flash vaporization process and equipment |
| FR2949348A1 (en) * | 2009-09-03 | 2011-03-04 | Rhodia Operations | PROCESS FOR CONTINUOUS SEPARATION OF ORGANIC PRODUCTS OF INTEREST OF A FERMENTATION |
| CN101270371B (en) * | 2008-03-31 | 2011-08-17 | 陕西科技大学 | Preprocessing method for biomass |
| WO2013060173A1 (en) * | 2011-10-27 | 2013-05-02 | 中国科学院大连化学物理研究所 | Nickel-based microporous material and preparation and application thereof |
| CN106497986A (en) * | 2016-12-29 | 2017-03-15 | 吉林化工学院 | A kind of method that vacuum fermentation couples production alcohol fuel with rectification |
-
2006
- 2006-06-02 CN CNA2006100178847A patent/CN1896253A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100493620C (en) * | 2007-04-02 | 2009-06-03 | 郑州大学生化工程中心 | Continuously sterilizing two-stage flash vaporization process and equipment |
| CN101270371B (en) * | 2008-03-31 | 2011-08-17 | 陕西科技大学 | Preprocessing method for biomass |
| FR2949348A1 (en) * | 2009-09-03 | 2011-03-04 | Rhodia Operations | PROCESS FOR CONTINUOUS SEPARATION OF ORGANIC PRODUCTS OF INTEREST OF A FERMENTATION |
| WO2011026933A1 (en) * | 2009-09-03 | 2011-03-10 | Rhodia Operations | Method for continuously separating organic materials of interest from fermentation |
| WO2013060173A1 (en) * | 2011-10-27 | 2013-05-02 | 中国科学院大连化学物理研究所 | Nickel-based microporous material and preparation and application thereof |
| CN106497986A (en) * | 2016-12-29 | 2017-03-15 | 吉林化工学院 | A kind of method that vacuum fermentation couples production alcohol fuel with rectification |
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Open date: 20070117 |