CN101851641B - Method and device for producing biological butanol by continuous pervaporation coupling fermentation - Google Patents
Method and device for producing biological butanol by continuous pervaporation coupling fermentation Download PDFInfo
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- CN101851641B CN101851641B CN 201010162856 CN201010162856A CN101851641B CN 101851641 B CN101851641 B CN 101851641B CN 201010162856 CN201010162856 CN 201010162856 CN 201010162856 A CN201010162856 A CN 201010162856A CN 101851641 B CN101851641 B CN 101851641B
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- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
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- C12M23/58—Reaction vessels connected in series or in parallel
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
Abstract
The invention belongs to the technical field of producing biological butanol by fermentation, and relates to a method and a device for producing biological butanol by continuous pervaporation coupling fermentation. The method comprises the following steps of: delivering fermented mash discharged from a previous fermentation tank to a next fermentation tank to perform continuous fermentation in turn, wherein before the fermented mash is delivered to the next fermentation tank from the previous fermentation tank, butanol is vaporized and separated from a liquid phase part in the fermented mash through a pervaporation film separation device and the fermented mash after the butanol is separated is delivered to the next fermentation tank. The method continuously separates the generated butanol from the fermented mash during fermenting by adopting a pervaporation film separation method so as to avoid inhibiting fermentation strains due to over-high butanol concentration, perform continuous fermentation, obtain maximum yield of the butanol, save one half vapor, reduce over 60 percent of wastewater discharge and bring very considerable economic benefit to biological butanol production enterprises.
Description
Technical field
The invention belongs to fermentation to produce biological butanols technical field, relate to a kind of method and apparatus of producing biological butanol by continuous pervaporation coupling fermentation.
Background technology
Biological butanol is meant and utilizes the prior biological resource, the butanols of producing through biological fermentation production.Butanols is widely used in organic synthesis plastics, resin, paint, medicine and national defense industry.Butanols still is that a kind of potential is combined power fuel greatly except that can be used as solvent, and its fuel value and gasoline are suitable, are the substitutes of gasoline.Prior biological production of butanol technology is through to the glucide behind starchy material or the cellulose hydrolysis; High Temperature Sterilization; Inoculation clostridium acetobutylicum, acetone Clostridium butylicum, clostridium saccharobutyricum or the fermentation of Pasteur's gemma clostridium; Technologies such as fractionation by distillation are produced and are obtained, because butanols generates the increase of concentration in the fermenting process, when surpassing 10g/l fermented bacterium are had restraining effect.Mash with the W-Gum preparation is an example; In existing field; If the W-Gum mass concentration is greater than 8.5%, because it is many to produce the butanols amount, butanol concentration reaches peak 10-13g/l, and just generation suppresses to continue fermentation to fermented bacterium; So unnecessary fermentation substrate can not thoroughly utilize, and causes wastage of material.Too low like mash concentration proportioning fermentation substrate concentration, although fermentation energy thoroughly carries out,, cause a large amount of steam of waste for downstream fractionation by distillation workshop section because the butanol concentration that generates is too low, be unfavorable for energy-saving and emission-reduction.
Summary of the invention
The object of the present invention is to provide a kind of method of producing biological butanol by continuous pervaporation coupling fermentation; This method is separated butanols through adopting the method for infiltration evaporation in the fermenting process; Both improved usage ratio of equipment; Reduce the steam output of mash again, reached energy-saving and emission-reduction and the purpose that obtains the maximum production butanols.
Another object of the present invention is to provide a kind of device of realizing producing biological butanol by continuous pervaporation coupling fermentation.
The present invention adopts following technical scheme:
A kind of method of producing biological butanol by continuous pervaporation coupling fermentation; Send into next fermentor tank after fermentation liquid is discharged by last fermentor tank and continue fermentation successively; Fermentation liquid is sent into before next fermentor tank by last fermentor tank; Liquid phase part in the fermentation liquid divides butanol vapour through the infiltration evaporation membrane separation unit earlier and leaves, and the fermentation liquid behind the separating butanol is sent into next fermentor tank again.
Film in the said infiltration evaporation membrane separation unit is divided into upstream side and downstream side with this device; It is 100-600Pa that the downstream side keeps vacuum tightness; The liquid phase part of fermentation liquid is heated to the upstream side of sending into the infiltration evaporation membrane separation unit after 40-60 ℃; To the downstream side, under vacuum environment, vaporize is drawn out of butanols through membrane permeation, and the liquid phase part of the fermentation liquid behind the separating butanol is directly discharged from upstream side and sent into next fermentor tank continuation fermentation.
When containing solid phase in the said fermentation liquid, separate through solid-liquid separating equipment earlier, send into next fermentor tank behind the liquid phase part entering infiltration evaporation membrane separation unit removal butanols and continue fermentation, the solid phase part is directly sent into next fermentor tank continuation and is fermented.
Said infiltration evaporation membrane separation unit, heat-processed, solid-liquid separating equipment are arranged in the sealing oxygen-free atmosphere that last fermentor tank expellant gas is provided.
The butanols of said vaporization is discharged after cooling apparatus is cooled to liquid state, rectifying then.
The saccharic amount that contains per-cent when beginning to ferment in the said last fermentation cylinder for fermentation mash is 10%-25%, carries out infiltrating and vaporizing membrane after 12-45 hour after last fermentation cylinder for fermentation mash begins to ferment and separates; Fermentation liquid behind the separating butanol is sent into next fermentor tank, in next fermentor tank, replenishes original mash, and making mixed mash contain saccharic amount per-cent is 10%-24%, and control pH value is 4.3-7.
Establishing film in the said infiltration evaporation membrane separation unit is alcohol permselective membrane, and the material of alcohol permselective membrane is Zylox or YSR 3286 etc.
A kind of device of realizing producing biological butanol by continuous pervaporation coupling fermentation comprises last fermentor tank and next fermentor tank, is provided with the infiltration evaporation membrane separation unit between last fermentor tank and next fermentor tank.
Be provided with well heater between said last fermentor tank and the infiltration evaporation membrane separation unit, the outlet of well heater is connected with the upstream side import of infiltration evaporation membrane separation unit, and the outlet of upstream side is connected with the import of back one fermentor tank; The downstream side of infiltration evaporation membrane separation unit is connected with vacuum system, is provided with cooling apparatus between downstream side and the vacuum system, and the liquid exit of cooling apparatus is connected with rectifier unit.
Be provided with solid-liquid separating equipment between said last fermentor tank and the well heater, the liquid phase outlet of solid-liquid separating equipment is connected with the import of well heater, and the solid phase outlet of solid-liquid separating equipment is connected with next fermentor tank; Said solid-liquid separating equipment, well heater and infiltration evaporation membrane separation unit are positioned at enclosed hood, and the inlet mouth of enclosed hood is connected with the air outlet of last fermentor tank, and the air outlet of enclosed hood is connected with the collection and confinement of gases jar.
Original mash among the present invention refers to starchy material and/or the glucide mash after batching, sterilization, before the fermentation; Fermentation liquid refers to starchy material and/or the mash of glucide behind batching, sterilization, entering fermentation stage.
Method of the present invention is to adopt the isolating method of infiltrating and vaporizing membrane that fermenting process is continuously separated the butanols that has generated from fermentation liquid, lets fermentation carry out continuously, thereby obtains the maximum production of butanols.Concrete grammar is to produce in the process of butanols in fermentation; Preferably be chosen in and carry out separating butanol after beginning to ferment in the last fermentor tank 12-45 hour; This be because this moment butanols volumetric concentration reach the 10-13 grams per liter, begin fermented bacterium is produced restraining effect, adopt liquid glucose to generate the upstream side that directly after heating, is pressed into the infiltration evaporation membrane separation unit when not having solid substance in the fermentation liquid of butanols as fermentation substrate; Having generated when containing solid substance in the fermentation liquid of butanols needs carry out solid-liquid separation through solid-liquid separating equipment earlier; Liquid phase part is pressed into infiltration evaporation membrane separation unit upstream side after heating, the butanols in the fermentation liquid of entering upstream side infiltrates into the downstream side through alcohol permselective membrane, and the butanols vaporization is drawn out of under the vacuum environment in downstream side; The butanols of vaporization is cooled to liquid state through cooling apparatus, rectifying then; Fermentation liquid behind the separating butanol is discharged through upstream side and is sent into next fermentor tank continuation fermentation; Solid phase after solid-liquid separation is partly sent into next fermentor tank and is continued fermentation; Look the fermentation liquid concentration behind the separating butanol, in next fermentor tank, replenish original mash, the saccharic amount that the contains per-cent that keeps mixing in the mash of back is 10%-24%; Continue to repeat fermentation, sepn process; The acetone concentration superelevation that finally produces to fermentation liquid suppresses till the fermentation, and acetone content can adopt gas chromatography to measure, also can be according to the speed observation of fermenting process gas production rate.
Because fermented bacterium belongs to anaerobic species; Need avoid becoming sour of bacterial classification contact with oxygen generation in the fermenting process; Therefore can the equipment of infiltrating and vaporizing membrane sepn process, heat-processed, solid-liquid separation process be placed oxygen-free atmosphere; This oxygen-free atmosphere can be provided by the carbonic acid gas of fermenting process generation and the gas mixture of hydrogen, also can adopt extraneous gas to provide.Solid-liquid separating equipment, well heater and infiltration evaporation membrane separation unit are placed in the enclosed hood; This enclosed hood is connected with the air outlet of last fermentor tank gets final product; Can make the blanketing gas in the enclosed hood is carbonic acid gas and the hydrogen mixed gas that last fermentor tank produces, and carbonic acid gas and hydrogen reclaim after discharging enclosed hood.
Present method is exactly this characteristic according to the fermentation to produce biological butanols; Adopt the isolating method of infiltrating and vaporizing membrane that the butanols that produces in the fermenting process is separated; Avoid the too high inhibition to fermented bacterium of butanol concentration, the highest 3 times of the biological butanol productive rates that improve are saved 1/2nd steam; Reduce the discharge of wastewater more than 60 percent, for biological production of butanol enterprise brings considerable economic benefit.
Description of drawings
Fig. 1 is the structural representation that embodiment 1 realizes the device of producing biological butanol by continuous pervaporation coupling fermentation;
Fig. 2 is the structural representation that embodiment 2 realizes the device of producing biological butanol by continuous pervaporation coupling fermentation;
Fig. 3 is the structural representation that embodiment 3 realizes the device of producing biological butanol by continuous pervaporation coupling fermentation.
Embodiment
Embodiment 1; The device of realization producing biological butanol by continuous pervaporation coupling fermentation as shown in Figure 1; Comprise last fermentor tank 1 and next fermentor tank 6; Be provided with well heater 3 and infiltration evaporation membrane separation unit 4 between last fermentor tank 1 and next fermentor tank 6, the outlet of well heater 3 is connected with upstream side 41 imports of infiltration evaporation membrane separation unit 4, and the outlet of upstream side 41 is connected with the import of back one fermentor tank 6; The downstream side 42 of infiltration evaporation membrane separation unit 4 is connected with vacuum system 13, is provided with cooling apparatus 5 between downstream side 42 and the vacuum system 13, and the liquid exit of cooling apparatus 5 is connected with rectifier unit 51.Next fermentor tank 6 is provided with feed supplement device 8, adder-subtractor 9 and pH value and detects mouth 7.
It is that 12% liquid glucose is during as fermentation substrate that employing contains saccharic amount per-cent; The fermentation liquid that ferments after 45 hours is heated to 60 ℃ by last fermentor tank 1 discharge back heater via 3; Be pressed into the upstream side 41 of infiltration evaporation membrane separation unit 4 then, butanols is that the butanols vaporization is drawn out of under the 600Pa environment through membrane permeation to downstream side 42 in the vacuum tightness that vacuum system 13 provides; Fermentation liquid behind the separating butanol is directly discharged from upstream side 41 and is sent into next fermentor tank 6 continuation fermentation; In next fermentor tank 6, replenish original mash by feed supplement device 8, making mixed mash contain saccharic amount per-cent is 10%, detects mouthful 7 detection pH values through the pH value; Adding alkali control pH value through adder-subtractor 9 is 7, and fermentation is normally carried out; The butanols of vaporization is cooled to liquid state through cooling apparatus 5, send rectifier unit 51 rectifying then, thereby realizes continuously butanols being separated in the fermenting process.The film of establishing in the infiltration evaporation membrane separation unit 4 is an alcohol permselective membrane, and the material of alcohol permselective membrane is a Zylox.
It is that 25% W-Gum solid matter is during as fermentation substrate that employing contains saccharic amount per-cent; The fermentation liquid that ferments after 12 hours is discharged the back earlier through solid-liquid separating equipment 2 solid-liquid separation by last fermentor tank 1; Isolating liquid phase part heater via 3 is heated to 40 ℃; Be pressed into the upstream side 41 of infiltration evaporation membrane separation unit 4 then, butanols is that the butanols vaporization is drawn out of under the 100Pa environment through membrane permeation to downstream side 42 in the vacuum tightness that vacuum system 13 provides; Fermentation liquid behind the separating butanol that upstream side 41 is discharged and solid-liquid separating equipment 2 isolating solid phase parts are all sent into next fermentor tank 6 and are continued fermentation; In next fermentor tank 6, replenish original mash by feed supplement device 8, making mixed mash contain saccharic amount per-cent is 24%, detects mouthful 7 detection pH values through the pH value; Adding alkali control pH value through adder-subtractor 9 is 4.3, and fermentation is normally carried out; The butanols of vaporization is cooled to liquid state through cooling apparatus, send rectifier unit 51 rectifying then, thereby realizes continuously butanols being separated in the fermenting process.
Infiltration evaporation membrane separation unit 4, well heater 3, solid-liquid separating equipment 2 are arranged in the carbonic acid gas of last fermentor tank 1 discharge and seal closure 10 oxygen-free atmospheres that hydrogen gas mixture provides; The equipment that prevents is airtight sternly not to cause becoming sour that the contact with oxygen of fermented bacterium produces, and guarantees the cleaning of mash.The film of establishing in the infiltration evaporation membrane separation unit 4 is an alcohol permselective membrane, and the material of alcohol permselective membrane is a YSR 3286.
Claims (5)
1. the method for a producing biological butanol by continuous pervaporation coupling fermentation; It is characterized in that: send into next fermentor tank after fermentation liquid is discharged by last fermentor tank and continue fermentation successively; Fermentation liquid is sent into before next fermentor tank by last fermentor tank; Liquid phase part in the fermentation liquid divides butanol vapour through the infiltration evaporation membrane separation unit earlier and leaves, and the fermentation liquid behind the separating butanol is sent into next fermentor tank again; Film in the said infiltration evaporation membrane separation unit is divided into upstream side and downstream side with this device; It is 100-600Pa that the downstream side keeps vacuum tightness; The liquid phase part of fermentation liquid is heated to the upstream side of sending into the infiltration evaporation membrane separation unit after 40-60 ℃; To the downstream side, under vacuum environment, vaporize is drawn out of butanols through membrane permeation, and the liquid phase part of the fermentation liquid behind the separating butanol is directly discharged from upstream side and sent into next fermentor tank continuation fermentation; When containing solid phase in the said fermentation liquid, separate through solid-liquid separating equipment earlier, send into next fermentor tank behind the liquid phase part entering infiltration evaporation membrane separation unit removal butanols and continue fermentation, the solid phase part is directly sent into next fermentor tank continuation and is fermented; Said infiltration evaporation membrane separation unit, heat-processed, solid-liquid separating equipment are arranged in the sealing oxygen-free atmosphere that last fermentor tank expellant gas is provided.
2. the method for producing biological butanol by continuous pervaporation coupling fermentation as claimed in claim 1 is characterized in that: the butanols of said vaporization is discharged after cooling apparatus is cooled to liquid state, rectifying then.
3. according to claim 1 or claim 2 the method for producing biological butanol by continuous pervaporation coupling fermentation; It is characterized in that: the saccharic amount that the contains per-cent when said last fermentation cylinder for fermentation mash begins to ferment is 10%-25%, carries out infiltrating and vaporizing membrane after 12-45 hour after last fermentation cylinder for fermentation mash begins to ferment and separates; Fermentation liquid behind the separating butanol is sent into next fermentor tank, in next fermentor tank, replenishes original mash, and making mixed mash contain saccharic amount per-cent is 10%-24%, and control pH value is 4.3-7.
4. the method for described producing biological butanol by continuous pervaporation coupling fermentation as claimed in claim 3, it is characterized in that: establishing film in the said infiltration evaporation membrane separation unit is alcohol permselective membrane.
5. a device of realizing producing biological butanol by continuous pervaporation coupling fermentation comprises last fermentor tank and next fermentor tank, it is characterized in that: be provided with the infiltration evaporation membrane separation unit between last fermentor tank and next fermentor tank; Be provided with well heater between said last fermentor tank and the infiltration evaporation membrane separation unit, the outlet of well heater is connected with the upstream side import of infiltration evaporation membrane separation unit, and the outlet of upstream side is connected with the import of back one fermentor tank; The downstream side of infiltration evaporation membrane separation unit is connected with vacuum system, is provided with cooling apparatus between downstream side and the vacuum system, and the liquid exit of cooling apparatus is connected with rectifier unit; Be provided with solid-liquid separating equipment between said last fermentor tank and the well heater, the liquid phase outlet of solid-liquid separating equipment is connected with the import of well heater, and the solid phase outlet of solid-liquid separating equipment is connected with next fermentor tank; Said solid-liquid separating equipment, well heater and infiltration evaporation membrane separation unit are positioned at enclosed hood, and the inlet mouth of enclosed hood is connected with the air outlet of last fermentor tank, and the air outlet of enclosed hood is connected with the collection and confinement of gases jar.
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| CN 201010162856 CN101851641B (en) | 2010-05-05 | 2010-05-05 | Method and device for producing biological butanol by continuous pervaporation coupling fermentation |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101979615B (en) * | 2010-11-25 | 2013-01-09 | 南京工业大学 | Method for continuously producing biological butanol by fermentation, separation and coupling of static bed |
| CN102787144B (en) * | 2012-07-27 | 2013-10-16 | 中国科学院过程工程研究所 | Process for producing acetone and butanol by coupling biomass fermentation and pervaporation membrane |
| CN106987523B (en) * | 2017-03-06 | 2019-05-14 | 上海交通大学 | A kind of method and system continuously fermented |
| CN115232708B (en) * | 2022-07-18 | 2023-03-28 | 鲍兴权 | Sewage discharge system for edible alcohol saccharified mash and fermented mash |
| CN115921496A (en) * | 2022-11-18 | 2023-04-07 | 安徽省蓝天能源环保科技有限公司 | Fermentation treatment device capable of realizing solid-liquid separation of kitchen waste |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1634820A (en) * | 2004-11-22 | 2005-07-06 | 上海蓝景膜技术工程有限公司 | Process for producing high concentration tert-butyl alcohol by permeation vaporization method and products therefrom |
| CN101235389A (en) * | 2008-03-04 | 2008-08-06 | 南京工业大学 | Fermentation and infiltration vaporization coupling technique for producing ethanol |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1634820A (en) * | 2004-11-22 | 2005-07-06 | 上海蓝景膜技术工程有限公司 | Process for producing high concentration tert-butyl alcohol by permeation vaporization method and products therefrom |
| CN101235389A (en) * | 2008-03-04 | 2008-08-06 | 南京工业大学 | Fermentation and infiltration vaporization coupling technique for producing ethanol |
Non-Patent Citations (3)
| Title |
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| N Qureshi et al..Butanol Production Using Clostridium beijerinckii BA101 Hyper-Butanol Producing Mutant Strain and Recovery by Pervaporation.《Applied Biochemistry and Biotechnology》.1999,第226页第3段，图4. * |
| 童灿灿等.丙酮-丁醇发酵分离耦合技术的研究进展.《化工进展》.2008,第27卷(第11期),第1782页左栏第2段,第1785页第1.4节以及图3. * |
| 金万勤.渗透汽化在丙酮- 丁醇发酵制备燃料丁醇中的研究进展.《膜科学与技术》.2011,第31卷(第3期),第25-30页. * |
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