CN102787144B - Process for producing acetone and butanol by coupling biomass fermentation and pervaporation membrane - Google Patents
Process for producing acetone and butanol by coupling biomass fermentation and pervaporation membrane Download PDFInfo
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- CN102787144B CN102787144B CN2012102655263A CN201210265526A CN102787144B CN 102787144 B CN102787144 B CN 102787144B CN 2012102655263 A CN2012102655263 A CN 2012102655263A CN 201210265526 A CN201210265526 A CN 201210265526A CN 102787144 B CN102787144 B CN 102787144B
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- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The invention relates to a process for producing acetone and butanol by biomass fermentation and pervaporation membrane coupling, in particular to a production process of coupling a pervaporation membrane and ABE (acetone, butanol and ethanol) fermentation, separating ABE in situ on line and utilizing an extraction tower to obtain an anhydrous solvent. Fermentation liquor in a fermentation tank is pumped out, and is filtered by an ethanol-permselective membrane to obtain a concentrated solution, the concentrated solution is sent into the extraction tower and is separated into an organic phaseand a water phase in the extraction tower, after the water phase is pumped into a water phase storage tank, the organic phase does not pass a mash tower but directly enters a butanol tower and follow-up rectifying tower groups to obtain anhydrous butanol, acetone and ethanol, the water phase in the water phase storage tank passes a pervaporation ethanol-permselective membrane assembly, dialysate is pumped into the extraction tower, and the cycle is repeated. According to the process disclosed by the invention, the fermentation process is coupled with the pervaporation technology, the extraction tower is added behind the pervaporation assembly, the inhibitory action of the butanol in the fermentation process is reduced, energy consumption in the separation process is saved, and the competitiveness of a biomass fermentation method for producing the butanol is improved.
Description
Invention field
The present invention relates to the technique that a kind of biomass ferment-acetone-butanol is produced in the infiltrating and vaporizing membrane coupling, be specifically related to a kind of infiltration vaporization coupling that will ferment and produce the ABE fermenting process, online original position is separated ABE, and utilizes infiltration evaporation alcohol permselective membrane and extraction tower to obtain the technique of anhydrous solvent.
Background technology
Along with world petroleum resource is day by day in short supply, countries in the world are all in the development and use of actively seeking renewable resource.Biofuel has caused the attention of various countries as important renewable energy source, the ratio that expects the year two thousand twenty bio-fuel-oil will rise to 30%, and aggregate demand will reach 87,000,000,000 gallons.
Yet the preparation of propylene synthesis method is mainly adopted in the at present production of butanols, and this method is that the propylene in the oil prepares the butanols product as raw material.Day by day exhaustion along with petroleum resources utilizes the new butanol production method of renewable biomass development of resources to become the focus of international concern.Fermentation method is the production of butanol technique that is expected to replace the propylene synthesis method of generally acknowledging.Yet, the feedback inhibition that two main bugbears that run in the fermentative Production butanols process namely are tunnings with separate the concentrated too high problem of energy consumption.After feedback inhibition refers to that the concentration of some meta-bolites reaches certain limit, because the purpose product has the noncompetitive inhibition effect to microbial growth, thereby cause fermentation reaction to be difficult to normally carry out, the purpose product no longer increases, and the purpose production concentration is crossed low phenomenon in the product fermented liquid.Just because of this, the concentration of ABE only is that the product of 1～2%(butylic fermentation is generally butanols, acetone and ethanol in the butylic fermentation liquid, and the three is abbreviated as ABE, and wherein the ratio of butanols, acetone, ethanol is 6:3:1).It is too high that so low butanol concentration causes the concentrated energy consumption of subsequent product separation.It is reported, adopt traditional distillation method also high to the combustion heat energy that butylic fermentation liquid concentrates required energy loss-rate butanols itself, especially wine with dregs column distillation concentration process is brought up to 500g/L with solvent strength, and consumed energy almost accounts for 50% of whole distillation energy consumption.Just because of this, for many years, the preparation of propylene synthesis method is adopted in the production of butanols always.This shows, the effective isolation technique of development of new, can solve product feedback inhibition and the concentrated too high problem of energy consumption of product in the fermentation to produce biological fuel process, be the key that realize that the industrialization of biofuel butanols is produced, significant to the Technical Economy that improves the fermentative production butanols.
At present, utilize the patent of infiltration vaporization coupling original position acetone, butanols and ethanol to have 201010136813.5,201010162856.0.Patent 201010136813.5 optionally arranges a microfiltration membrane separator before infiltrating and vaporizing membrane, the suspended solid in microorganism cells and the fermented liquid is held back, thereby the pollution of reduction infiltrating and vaporizing membrane improves separation efficiency.Patent 201010162856.0, fermentation liquid are sent into by last fermentor tank before next fermentor tank, and the liquid phase part in the fermentation liquid separates butanols by the infiltration evaporation membrane separation unit first, and the fermentation liquid behind the separating butanol is sent into next fermentor tank again.There is bibliographical information utilization fermentation-infiltration vaporization coupling technique to alleviate inhibition both at home and abroad, improve the butanols productive rate, Heitmann et al. (2012) for example, Wouter et al. (2012) utilizes respectively the solvent in ionic liquid supporting liquid sheet and the PDMS membrane sepn fermented liquid.But these reports all do not relate to the application of the phenomenon of phase separation of acetone-butanol solvent.The characteristics that the present invention utilizes the ABE concentrated solution to occur being separated increase extraction tower after infiltration evaporation technique, be separated at the solvent of extraction tower middle and high concentration.The concentration of organic phase solvent wherein, can reach the concentration (500g/L) after the wine with dregs tower concentrates, thereby in follow-up rectifying, omit the wine with dregs tower, and extraction tower does not increase energy consumption, so with respect to CN101805754A and CN101851641A, this technique can reduce energy consumption and water consumption, and then obtains anhydrous solvent.
Summary of the invention
The object of the present invention is to provide a kind of technique of producing acetone-butanol with fermentation infiltration vaporization coupling technology, removed that ABE improves the productive rate of acetone-butanol to the restraining effect of thalline in the fermenting process.
Another object of the present invention is to provide a kind of infiltration evaporation and extraction tower of utilizing, obtain the method for high density acetone-butanol ethanol, reduced follow-up distillation procedure step, fall low-energy consumption, realize energy-saving and emission-reduction.
The invention provides a kind of continuously fermenting and produce the technique of anhydrous solvent with the infiltrating and vaporizing membrane separation coupling, it is characterized in that technological process is as follows:
(1) will be through pretreated biomass as fermentation substrate, inoculation butanol acetone alcohol production bacterial classification ferments;
(2) fermented liquid in the fermentor tank is inputed to the evaporation alcohol permselective membrane separator by pump, see through liquid and collect the concentrated solution that obtains acetone, butanols and ethanol through condenser, trapped fluid is back in the fermentor tank;
(3) penetrating fluid of acetone, butanols and ethanol is by in the pump input extraction tower, and penetrating fluid is divided into organic phase and water in extraction tower;
(4) above-mentioned water is by pump input water basin, and above-mentioned organic phase directly enters a fourth tower and follow-up rectifying tower group without the wine with dregs tower, and a small amount of water removes acquisition anhydrous propanone, butanols and ethanol in the realization organic phase; Water in the water basin is realized the concentrated of a small amount of acetone of aqueous phase, butanols and alcohol mixeding liquid through the evaporation alcohol permselective membrane separator, enters subsequently extraction tower again, carries out subsequent operations.
Evaporation alcohol permselective membrane separator of the present invention is comprised of one or more evaporation alcohol permselective membrane separator, and the per-meate side of each unit evaporation alcohol permselective membrane separator is passed through the pipeline serial or parallel connection in the vacuum pump main pipe rail.
Evaporation alcohol permselective membrane of the present invention is organic membrane, mineral membrane or hybrid organic-inorganic film; Its membrane module form is rolling, tubular type, plate and frame or tubular fibre formula.
The material of hybrid organic-inorganic film of the present invention is a kind of among PDMS-Silicalite-1, PDMS-ZSM-5 or the PTMSP-Silicalite; The material of organic membrane is silicon rubber, poly-trimethyl silicane propine, polypropylene, polyvinylidene difluoride (PVDF) or tetrafluoroethylene; The material of mineral membrane can be Silicalite-1 or ZSM-5.
Extraction tower of the present invention is a kind of in extraction spray column, sieve-tray tower, rotating disc contactor and the pulse-column.
Biomass of the present invention can be lignocellulose (stalk, careless class and deciduous tree or the acerose wood chips of various farm crop such as wheat stalk, maize straw, bagasse), also can be starchy material (for example one or both in corn, cassava, Ipomoea batatas, potato, the root of kudzu vine), also can be saccharide raw material (for example molasses, Chinese sorghum juice).The pretreatment process of lignocellulose adopts the physics and chemistry pre-treatment such as the Chemical Pretreatment such as conventional diluted acid or steam explosion to get final product.The hydrolysis temperature of lignocellulose is 45-50 ℃, and the temperature of acetone butanol fermentation is 37-40 ℃.Preferred acetone butanol fermentation microorganism is C.acetobutylicum ATCC824, C.butylicum23592, C.acetobutylicum170, C.acetobutylicum P260, C.beijerinckii ATCC55025.
Provided by the inventionly a kind ofly utilize the technique of fermentation infiltration vaporization coupling explained hereafter acetone-butanol ferment, evaporation alcohol permselective membrane separator and rectifying combination, realized the original position separation of tunning acetone-butanol ethanol, reduce the restraining effect of acetone-butanol ethanol to organism of fermentation, improved butylic fermentation intensity; While also is provided with extraction tower after the evaporation alcohol permselective membrane separator, fully effectively utilized by the phenomenon of phase separation that sees through liquid after the evaporation alcohol permselective membrane separator, has reduced the separation costs of follow-up solvent.Technique provided by the invention has been saved energy consumption and the water consumption in the production process with zymotechnique and the infiltrating and vaporizing membrane sepn process close-coupled of glucose acetone-butanol in the hydrolyzed solution, has reduced the production cost of being produced the fuel butanols by biomass.
Description of drawings
Fig. 1 is that fermentation infiltration evaporation rectification integrated technique is produced the process flow diagram of acetone-butanol scheme one;
Reference numeral
1. feed supplement tank 2. fresh feed pumps 3. fermentor tanks 4. fresh feed pumps 5. evaporation alcohol permselective membrane assemblies 6. condensers 7. tensimeters 8. vacuum pumps 9. fresh feed pumps 10. extraction towers 11. fresh feed pumps 12. valves 13. water basins 14. fresh feed pumps 15. evaporation alcohol permselective membrane assemblies 16. condensers 17. tensimeters 18. vacuum pumps 19. fresh feed pumps 20. 1 fourth towers
Embodiment
The present invention will be further described below in conjunction with embodiment, and theme protection domain involved in the present invention is not limited only to these embodiment.
The technique of 1 one kinds of maize straw fermentation-infiltration vaporization couplings of embodiment explained hereafter acetone-butanol
Maize straw is made slip and is entered feed supplement tank 1 after steam explosion processing, acid hydrolysis, enzymic hydrolysis, open fresh feed pump 2 and enter fermentor tank 3, behind the microbe inoculation 37 ℃ the fermentation 72h after, when total solvent concentration reaches 18g/L after testing in the liquid phase in the tank, open fresh feed pump 4, fermented liquid is delivered into evaporation alcohol permselective membrane assembly 5, be composed in series by two plate and frame evaporation alcohol permselective membrane separators in the infiltration evaporation assembly, the infiltrating and vaporizing membrane of employing is hybrid organic-inorganic film (PDMS-Silicalite-1).Simultaneously, open vacuum pump 8, tensimeter 7 vacuum tightnesss maintain 500Pa, and the penetrating fluid device 6 that is condensed is collected, and acetone, butanols and the total ethanol concentration of collecting gained reach 150g/L, and the feed liquid of holding back is returned in the fermentor tank 3; Through behind the integrated separation 12h, suspend integrated separation, stream adds the identical stalk hydrolysis sugar liquid of penetrating fluid volume that obtains with the infiltration evaporation membrane sepn in the fermentor tank from feed supplement tank 1, continues fermentation.Open simultaneously fresh feed pump 9, collect the penetrating fluid that obtains in the condenser 6 and enter extraction tower 10, extraction tower is extraction spray column, is divided into organic phase and water in extraction tower; Aqueous-phase concentration is about 100g/L in the extraction tower, by fresh feed pump 11, opens valve 12 and enters water basin 13 paths; Organic phase concentration in the extraction tower reaches 500g/L, by fresh feed pump 11, opens valve 12 and enters a fourth tower 20 paths, obtains anhydrous butanols, acetone and ethanol; Water in the water basin 13 is by fresh feed pump 14 input evaporation alcohol permselective membrane assemblies 15, open vacuum pump 18, tensimeter pressure 500pa, treat that the extraction tower organic phase all enters a fourth tower 20, condenser 16 is collected penetrating fluid and is entered extraction tower 12 by fresh feed pump 19, so circulation obtains anhydrous butanols, acetone and ethanol at last.Behind the integrated separation 12h, suspend integrated separation, stream adds the identical stalk hydrolysis sugar liquid of penetrating fluid volume that obtains with the infiltration evaporation membrane sepn in the fermentor tank from feed supplement tank 1, continues fermentation.When reaching 18g/L to the concentration of total solvent in the fermentor tank 2, open vacuum pump, again carry out integrated separation, penetrating fluid enters condenser and is collected, and so circulates 10 times.
This example has realized maize straw hydrolysis sugar liquid semicontinuous fermentation production acetone-butanol, not only greatly reduced the acetone-butanol solvent of fermentation generation to the restraining effect of microorganism cells, and owing to behind the evaporation alcohol permselective membrane assembly, having increased extraction tower, take full advantage of the phase separation property of evaporation alcohol permselective membrane penetrating fluid, effectively reduce the energy consumption of concentration process, compare with traditional batch fermentation-still-process, the production intensity of butanols improves, owing to omitting the wine with dregs tower, can save the rectifying energy consumption.
The technique of 2 one kinds of fermentation of corn starch of embodiment-infiltration vaporization coupling explained hereafter acetone-butanol
Take Semen Maydis powder as the preparation of raw material substratum, 121 ℃ of boiling gelatinizations 90 minutes, obtain maize powder medium, enter feed supplement tank 1, open fresh feed pump 2 and enter fermentor tank 3, behind the microbe inoculation 37 ℃ the fermentation 60h after, when total solvent concentration reaches 20g/L after testing in the liquid phase in the tank, open fresh feed pump 4, fermented liquid is delivered into evaporation alcohol permselective membrane assembly 5, membrane module is comprised of a tubular fibre evaporation alcohol permselective membrane separator, and the infiltrating and vaporizing membrane of selecting is mineral membrane Silicalite-1 or ZSM-5.Simultaneously, open vacuum pump 8, tensimeter 7 vacuum tightnesss maintain 500Pa, and the penetrating fluid device 6 that is condensed is collected, and acetone, butanols and the total ethanol concentration of collecting gained reach 400g/L, and the feed liquid of holding back is returned in the fermentor tank 3; After separating 12h, suspend infiltration evaporation and separate, stream adds the identical stalk hydrolysis sugar liquid of penetrating fluid volume that obtains with the infiltration evaporation membrane sepn in the fermentor tank from feed supplement tank 1, continues fermentation.Open simultaneously fresh feed pump 9, collect the penetrating fluid that obtains in the condenser 6 and enter extraction tower 10, extraction tower is sieve-tray tower, is divided into organic phase and water in extraction tower; Aqueous-phase concentration is about 280g/L in the extraction tower, by fresh feed pump 11, opens valve 12 and enters water basin 13 paths; Organic phase concentration in the extraction tower reaches 700g/L, by fresh feed pump 11, opens valve 12 and enters a fourth tower 20 paths, obtains anhydrous butanols, acetone and ethanol; Water in the water basin 13 is by fresh feed pump 14 input evaporation alcohol permselective membrane assemblies 15, open vacuum pump 18, tensimeter pressure 500pa, treat that the extraction tower organic phase all enters a fourth tower 20, condenser 16 is collected penetrating fluid and is entered extraction tower 12 by fresh feed pump 19, so circulation obtains anhydrous butanols, acetone and ethanol at last.Through behind the integrated separation 12h, suspend integrated separation, stream adds the identical stalk hydrolysis sugar liquid of penetrating fluid volume that obtains with the infiltration evaporation membrane sepn in the fermentor tank from feed supplement tank 1, continues fermentation.When reaching 20g/L to the concentration of total solvent in the fermentor tank 2, open vacuum pump, again carry out integrated separation, penetrating fluid enters condenser and is collected, and so circulates 10 times.
This example has realized Semen Maydis powder semicontinuous fermentation production acetone-butanol, not only greatly reduced the acetone-butanol solvent of fermentation generation to the restraining effect of microorganism cells, and owing to behind evaporation alcohol permselective membrane, having increased extraction tower, take full advantage of the phase separation property of high density penetrating fluid, effectively reduce the energy consumption of concentration process, compare with traditional batch fermentation-still-process, the production intensity of butanols improves.
3 one kinds of maize straws of embodiment continuously ferment-technique of infiltration vaporization coupling explained hereafter acetone-butanol
Maize straw is made slip and is entered feed supplement tank 1 after steam explosion processing, acid hydrolysis, enzymic hydrolysis, open fresh feed pump 2 and enter fermentor tank 3, behind the microbe inoculation 37 ℃ the fermentation 20h after, when total solvent concentration reaches 5g/L after testing in the liquid phase in the tank, open fresh feed pump 4, fermented liquid is delivered into evaporation alcohol permselective membrane assembly 5, and membrane module is composed in parallel by two rolling evaporation alcohol permselective membrane separators, uses infiltrating and vaporizing membrane to be the polyvinylidene difluoride (PVDF) organic membrane.Simultaneously, open vacuum pump 8, tensimeter 7 vacuum tightnesss maintain 500Pa, collect the penetrating fluid that obtains in the condenser 6 and enter extraction tower 10, and extraction tower is rotating disc contactor, is divided into organic phase and water in extraction tower; Aqueous-phase concentration is about 80g/L in the extraction tower, by fresh feed pump 11, opens valve 12 and enters water basin 13 paths; Organic phase concentration in the extraction tower reaches 500g/L, by fresh feed pump 11, opens valve 12 and enters a fourth tower 20 paths, directly enters a fourth tower, obtains anhydrous butanols, acetone and ethanol; Water in the water basin 13 is by fresh feed pump 14 input evaporation alcohol permselective membrane assemblies 15, open vacuum pump 18, tensimeter pressure 500pa, treat that the extraction tower organic phase all enters a fourth tower 20, condenser 16 is collected penetrating fluid and is entered extraction tower 12 by fresh feed pump 19, so circulation obtains anhydrous butanols, acetone and ethanol at last.
This example has realized the maize straw production acetone-butanol that continuously ferments, not only greatly reduced the acetone-butanol solvent of fermentation generation to the restraining effect of microorganism cells, and owing to behind evaporation alcohol permselective membrane, having increased extraction tower, take full advantage of the phase separation property of evaporation alcohol permselective membrane penetrating fluid, effectively reduce the energy consumption of concentration process, compare with traditional batch fermentation-still-process, the production intensity of butanols is improved simultaneously.
4 one kinds of Semen Maydis powder of embodiment continuously ferment-technique of infiltration vaporization coupling explained hereafter acetone-butanol
Take Semen Maydis powder as the preparation of raw material substratum, 121 ℃ of boiling gelatinizations 90 minutes, obtain maize powder medium, enter feed supplement tank 1, open fresh feed pump 2 and enter fermentor tank 3, behind the microbe inoculation 37 ℃ the fermentation 20h after, when total solvent concentration reaches 5g/L after testing in the liquid phase in the tank, open fresh feed pump 4, fermented liquid is delivered into evaporation alcohol permselective membrane assembly 5, membrane module is composed in parallel by three tubular type evaporation alcohol permselective membrane separators, and used infiltrating and vaporizing membrane is organic membrane polypropylene or hybrid organic-inorganic film PTMSP-Silicalite-1.Simultaneously, open vacuum pump 8, tensimeter 7 vacuum tightnesss maintain 500Pa, and the penetrating fluid device 6 that is condensed is collected, and acetone, butanols and the total ethanol concentration of collecting gained reach 200g/L, and the feed liquid of holding back is returned in the fermentor tank 3; Simultaneously from feed supplement tank 1 in the fermentor tank stream add the identical stalk hydrolysis sugar liquid of penetrating fluid volume that obtains with the infiltration evaporation membrane sepn, continue fermentation.Open simultaneously fresh feed pump 9, collect the penetrating fluid that obtains in the condenser 6 and enter extraction tower 10, extraction tower is pulse-column, is divided into organic phase and water in extraction tower; Aqueous-phase concentration is about 100g/L in the extraction tower, by fresh feed pump 11, opens valve 12 and enters water basin 13 paths; Organic phase concentration in the extraction tower reaches 520g/L, by fresh feed pump 11, opens valve 12 and enters a fourth tower 20 paths, obtains anhydrous butanols, acetone and ethanol; Water in the water basin 13 is by fresh feed pump 14 input evaporation alcohol permselective membrane assemblies 15, open vacuum pump 18, tensimeter pressure 500pa, treat that the extraction tower organic phase all enters a fourth tower 20, condenser 16 is collected penetrating fluid and is entered extraction tower 12 by fresh feed pump 19, so circulation obtains anhydrous butanols, acetone and ethanol at last.
This example has realized the Semen Maydis powder production acetone-butanol that continuously ferments, not only greatly reduced the acetone-butanol solvent of fermentation generation to the restraining effect of microorganism cells, and owing to behind evaporation alcohol permselective membrane, having increased extraction tower, take full advantage of the phase separation property of evaporation alcohol permselective membrane penetrating fluid, omitted the large wine with dregs tower of energy consumption, effectively reduce the energy consumption of concentration process, compare with traditional batch fermentation-still-process, the production intensity of butanols improves.
Claims (8)
1. the technique that biomass ferment-acetone-butanol is produced in the infiltrating and vaporizing membrane coupling is characterized in that, this technique key step comprises:
(1) will be through pretreated biomass as fermentation substrate, inoculation butanol acetone alcohol production bacterial classification ferments;
(2) fermented liquid in the fermentor tank is inputed to the evaporation alcohol permselective membrane separator by pump, penetrating fluid is collected the concentrated solution that obtains acetone, butanols and ethanol through condenser; Trapped fluid is back to fermentor tank;
(3) with the concentrated solution of the acetone, butanols and the ethanol that obtain in the step (2) by in the pump input extraction tower, concentrated solution is divided into organic phase and water in extraction tower;
(4) water that obtains in the step (3) is drained in the water basin by pump, organic phase directly enters a fourth tower and follow-up rectifying tower group without the wine with dregs tower, and a small amount of water removes acquisition anhydrous propanone, butanols and ethanol in the realization organic phase; Water in the water basin is concentrated through infiltration evaporation alcohol permselective membrane assembly, and concentrated solution enters extraction tower and re-starts and be separated so circulation.
2. technique according to claim 1 is characterized in that, in the fermented liquid of extracting out in the fermentor tank described in the step (2), the concentration of acetone, butanols and total ethanol solvent reaches 18-20g/L.
3. technique according to claim 1 is characterized in that, the total solvent mass concentration of acetone, butanols and the ethanol concentrated solution that obtains through the condenser collection described in the step (2) reaches 100-400g/L.
4. technique according to claim 1 is characterized in that, the total solvent mass concentration reaches 500-700g/L in the organic phase that extraction tower obtains described in the step (3), and aqueous phase total solvent mass concentration reaches 80-280g/L.
5. technique according to claim 1, it is characterized in that, evaporation alcohol permselective membrane separator described in the step (2) is comprised of one or more evaporation alcohol permselective membrane separator, and the per-meate side of each unit evaporation alcohol permselective membrane separator is passed through the pipeline serial or parallel connection in the vacuum pump main pipe rail.
6. the technique described in according to claim 1 is characterized in that, evaporation alcohol permselective membrane is organic membrane, mineral membrane or hybrid organic-inorganic film described in the step (2); Its membrane module form is rolling, tubular type, plate and frame or tubular fibre formula.
7. the technique described in according to claim 6 is characterized in that, the material of hybrid organic-inorganic film is a kind of among PDMS-Silicalite-1, PDMS-ZSM-5 and the PTMSP-Silicalite-1; The material of organic membrane is silicon rubber, poly-trimethyl silicane propine, polypropylene, polyvinylidene difluoride (PVDF) or tetrafluoroethylene; The material of mineral membrane is Silicalite-1 or ZSM-5.
8. the technique described in according to claim 1 is characterized in that, extraction tower described in the step (3) is a kind of in extraction spray column, sieve-tray tower, rotating disc contactor and the pulse-column.
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| CN102911854B (en) * | 2012-09-29 | 2014-06-25 | 大连理工大学 | Separation and purification device and separation and purification method for butanol and acetone |
| CN103910605B (en) * | 2013-12-27 | 2016-04-27 | 江苏九天高科技股份有限公司 | The technique of a kind of infiltration evaporation system and refined biological propyl carbinol thereof |
| CN103695301B (en) * | 2013-12-30 | 2016-06-22 | 南京九思高科技有限公司 | A kind of device improving biomass fuel alcohol fermentation efficiency and technique |
| CN105482998A (en) * | 2016-01-12 | 2016-04-13 | 广西新天德能源有限公司 | High-efficiency and environment-friendly alcoholic fermentation coupling film separating system device |
| CN108265083A (en) * | 2017-01-04 | 2018-07-10 | 北京化工大学 | The method that ethyl alcohol, acetone and butanol are prepared using ligno-cellulose hydrolysate segmentation |
| CN106754259A (en) * | 2017-02-14 | 2017-05-31 | 中国科学院过程工程研究所 | A kind of synthesis gas that ferments produces the system and its processing method of alcohols |
| CN107904265A (en) * | 2017-12-21 | 2018-04-13 | 北京首钢朗泽新能源科技有限公司 | The utilization technique and device of product in a kind of legal system alcohol that ferments |
| CN111766191B (en) * | 2020-08-10 | 2023-11-24 | 江苏钦宇建设工程有限公司 | Environment-friendly material cylinder penetration testing machine and working method thereof |
| CN111948112A (en) * | 2020-08-10 | 2020-11-17 | 盐城新海川机电科技有限公司 | Penetrating fluid constant-pressure quantitative supply method and device |
| WO2024058081A1 (en) * | 2022-09-14 | 2024-03-21 | 日東電工株式会社 | Membrane separation system and method for operating membrane separation system |
| CN115925515A (en) * | 2022-11-25 | 2023-04-07 | 青岛科技大学 | Energy-saving process for separating n-butyl alcohol-vinyl butyl ether-water by coupling ethylene glycol extractive distillation-pervaporation |
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| CN102666867A (en) * | 2009-11-23 | 2012-09-12 | 布特马斯先进生物燃料有限责任公司 | Method for producing butanol using extractive fermentation with osmolyte addition |
| CN101805754B (en) * | 2010-03-31 | 2012-06-27 | 南京工业大学 | Process for separating acetone, butanol and ethanol in situ by coupling biomass fermentation and pervaporation |
| CN101851641B (en) * | 2010-05-05 | 2012-10-24 | 王建设 | Method and device for producing biological butanol by continuous pervaporation coupling fermentation |
| CN102304106B (en) * | 2011-08-11 | 2013-10-16 | 北京化工大学 | Method for producing butanol, acetone, butyric acid and furfural by fermentation of hemicellulose-rich biomass |
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