CN101831382A - Bubble-free air supply and solid-liquid separation integrated membrane biomembrane reactor taking indissoluble gases as fermentation raw materials - Google Patents
Bubble-free air supply and solid-liquid separation integrated membrane biomembrane reactor taking indissoluble gases as fermentation raw materials Download PDFInfo
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- 239000007788 liquid Substances 0.000 title claims abstract description 72
- 238000000926 separation method Methods 0.000 title claims abstract description 40
- 239000007789 gas Substances 0.000 title abstract description 100
- 238000000855 fermentation Methods 0.000 title abstract description 38
- 230000004151 fermentation Effects 0.000 title abstract description 38
- 239000002994 raw material Substances 0.000 title abstract description 8
- 239000012510 hollow fiber Substances 0.000 claims abstract description 62
- 239000000835 fiber Substances 0.000 claims abstract description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000004593 Epoxy Substances 0.000 claims description 12
- -1 polyethylene Polymers 0.000 claims description 6
- 229920005989 resin Polymers 0.000 claims description 6
- 239000011347 resin Substances 0.000 claims description 6
- 238000007789 sealing Methods 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 4
- 239000004698 Polyethylene Substances 0.000 claims description 3
- 239000004743 Polypropylene Substances 0.000 claims description 3
- 230000000712 assembly Effects 0.000 claims description 3
- 238000000429 assembly Methods 0.000 claims description 3
- 230000002209 hydrophobic effect Effects 0.000 claims description 3
- 229920002492 poly(sulfone) Polymers 0.000 claims description 3
- 229920000573 polyethylene Polymers 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 abstract description 17
- 239000001963 growth medium Substances 0.000 abstract description 9
- 230000015572 biosynthetic process Effects 0.000 abstract description 5
- 239000012263 liquid product Substances 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 abstract 1
- 239000006052 feed supplement Substances 0.000 abstract 1
- 238000001179 sorption measurement Methods 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
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- 238000005516 engineering process Methods 0.000 description 5
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- 241000894006 Bacteria Species 0.000 description 4
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 4
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- 238000005755 formation reaction Methods 0.000 description 4
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- 238000005842 biochemical reaction Methods 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
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- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000012262 fermentative production Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
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- 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
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/04—Filters; Permeable or porous membranes or plates, e.g. dialysis
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- C12M29/16—Hollow fibers
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Abstract
The invention provides a bubble-free air supply and solid-liquid separation integrated membrane biomembrane reactor comprising a gas distribution pipe, a hollow bubble-free air supply fiber membrane module, a water distribution pipe and a solid-liquid separation membrane module which are arranged in a tank body of the reactor, wherein the top ends of the hollow bubble-free air supply fiber membrane module and the solid-liquid separation membrane module are lower than the liquid level in the tank body; the hollow bubble-free air supply fiber membrane module is communicated with a feed gas storage tank through the gas distribution pipe, the water distribution pipe is communicated with a culture medium storage tank through a feeding pump, and the solid-liquid separation membrane module is communicated with a liquid product outlet through a sorption pump; the tank body is also provided with a circulating water outlet, a gas product outlet, a feed supplement hole, a thermometer, a pH meter and a pressure gage; and partial pressure of gas in the cavity of a hollow fiber membrane is lower than the pressure of a bubble point so as to ensure that the hollow bubble-free air supply fiber membrane module realizes bubble-free air supply. The reactor has higher fermentation reaction rate and product concentration, and can enhance economic feasibility of fermentation of synthesis gas and other indissoluble gases, thereby being suitable for a biological fermentation process taking various indissoluble gases as raw materials.
Description
Technical field
The present invention relates to biological technical field, more particularly, the present invention relates to a kind of is the still air feed-solid-liquid separation integrated membrane biomembrane reactor of fermentation raw material with the indissoluble gases.
Technical background
Indissoluble gases refers to the lower gas of solubleness in water, for example carbon monoxide (CO) and hydrogen (H
2).Be that example is introduced the insoluble gaseous fermentation with synthetic gas fermentation and carbon monoxide ferment for hydrogen production below.(be mainly CO, H about synthetic gas
2And CO
2) history in existing more than 10 year of research of chemicals such as fermentative production of ethanol, acetate, butanols and butyric acid or liquid fuel and carbon monoxide ferment for hydrogen production, its biochemical reaction is seen formula (1-9).
6CO+3H
2O→CH
3CH
2OH+4CO
2 (1)
2CO
2+6H
2→CH
3CH
2OH+3H
2O (2)
4CO+2H
2O→CH
3COOH+2CO
2 (3)
4H
2+2CO
2→CH
3COOH+2H
2O (4)
10CO+4H
2O→CH
3CH
2CH
2COOH+6CO
2 (5)
12CO+5H
2O→CH
3CH
2CH
2CH
2OH+86CO
2 (6)
10H
2+4CO
2→CH
3CH
2CH
2COOH+6H
2O (7)
12H
2+4CO
2→CH
3CH
2CH
2CH
2OH+7H
2O (8)
CO+H
2O→H
2+CO
2 (9)
Yet slower fermentation reaction speed and lower production concentration have limited the commercialized running of this technology.Trace it to its cause, cause reason to be mainly following three than long response time speed and low production concentration:
(1) lower gas-liquid mass transfer speed.The fermenting process that with the gas raw material is substrate relates to following steps: gaseous diffusion is diffused into microorganism cells film, gas to liquid-gas interface, gas at liquid-gas interface mass transfer, gas and passes cytolemma and utilized by microorganism in liquid phase.For indissoluble gases, because of its gas Liquid Mass Transfer Coefficient is extremely low, gas-liquid mass transfer is the rate-limiting step of whole biological fermentation process.Though adopt measures such as increasing gas-liquid flow velocity, raising stirring velocity and increase gaseous tension can improve gas Liquid Mass Transfer Coefficient, can not fundamentally avoid the gas-liquid mass transfer step, therefore, the increase rate of fermentation reaction speed is very limited.
Therefore, a kind of mode of raising the efficiency is that unstripped gas is directly delivered on the microorganism cells, fundamentally avoids the gas-liquid mass transfer step.
(2) lower gas utilising efficiency.For traditional reactor, continuous stirred tank reactor (CSTR) for example, provide gas raw material by the submerged bubble diffuser to reactor, the bubble of diffusion enters main body solution (culture medium solution that contains suspension cell), part gas is absorbed the generation product by microorganism cells, and a part of gas is because the buoyancy of bubble is risen and fled from main body solution and enter upper gaseous phase, and bubble is big more, climbing speed is fast more, and gas-liquid contact time is short more.In fact, about 80% gas also has little time to be delivered to just flees from main body solution by the form of bubble on the microorganism cells and enters upper gaseous phase, and the utilising efficiency of gas is lower.
Therefore, the another kind of mode of raising the efficiency is that unstripped gas is transmitted under the situation that does not form bubble, and promptly still air feed avoids unstripped gas to flee from main body solution with the form of bubble, thereby improves the gas utilising efficiency.
(3) lower microorganism cells concentration.Belong to autotrophic bacteria owing to carry out the microorganism major part of gaseous fermentation, as the synthetic gas that ferments is produced acetate and alcoholic acid Clostridium ljungdahlii, fermentation synthetic gas generate acetate, ethanol, butyric acid and the Clostridium carboxidivorans of butanols and the bacteriums such as Carboxydothermushydrogenoformans of carbon monoxide ferment for hydrogen production, and they utilize CO, CO
2And H
2When growing, all belong to autotrophic bacteria as carbon source, electron donor and the energy.In general, autotrophic bacteria is not so good as heterotrophic organism aspect cumulative efficient, thereby growth and breeding is slower, causes the microorganism concn in the reactor lower.In addition, for the common continuous stirred tank reactor (CSTR) of picture, microorganism cells is in suspended state, when discharging, microorganism cells and product solution is outflow reactor together, its solid (microorganism) residence time can not effectively separate with hydraulic detention time, and microorganism cells runs off serious.Therefore, reactor can not move under higher microorganism cells concentration conditions, also just can not obtain higher fermentation reaction speed and production concentration.
Adopt immobilized biomembrane system and microbial film separation system can avoid microorganism cells to run off, improve the microorganism cells concentration in the reactor.
Therefore, overcome above three kinds of deficiencies, the high efficiency reactor that exploitation has very fast fermentation reaction speed is the key that synthetic gas fermentation and even the fermentation of other indissoluble gases realize commercial applications.
Summary of the invention
The objective of the invention is to overcome the deficiency in the existing indissoluble gases fermentation technique, promptly lower gas-liquid mass transfer speed, lower gas utilising efficiency and lower microorganism cells concentration, a kind of still air feed-solid-liquid separation integrated membrane biomembrane reactor is provided, to improve indissoluble gases is the fermentation reaction speed of raw material, for synthetic gas fermentation and even the fermentation of other indissoluble gases realize that commercial applications lays the foundation.
For realizing above purpose, the present invention takes following technical scheme:
A kind of still air feed-solid-liquid separation integrated membrane biomembrane reactor, comprise the reactor tank body, gas distribution pipe, still air feed hollow fiber film assembly, water distributor, the solid-liquid separation membrane module places in the reactor tank body, and the top of still air feed hollow fiber film assembly and solid-liquid separation membrane module is lower than liquid level in the reactor tank body: still air feed hollow fiber film assembly is communicated to the unstripped gas basin by gas distribution pipe, water distributor is communicated to the substratum basin through fresh feed pump, the solid-liquid separation membrane module is communicated with the product liquid outlet through suction pump, reactor tank body bottom is provided with circulating water outlet, circulating water outlet is communicated with water distributor by recycle pump, reactor tank body top is provided with the gaseous product outlet, on the reactor tank body thermometer is installed, pH meter and tensimeter, be convenient to monitor and the relevant operating parameter of adjusting reactor, material-feeding port also is installed on the reactor tank body, is convenient to add inoculum or other solution.
Described still air feed hollow fiber film assembly can be a curtain formula hollow fiber film assembly, also can be the cartridge type hollow fiber film assembly,, have maximum area/volume ratio because hollow fiber film assembly is compared with the membrane module of other form, therefore, select hollow fiber film assembly.
Described curtain formula hollow fiber film assembly is by some hollow-fibre membranes arranged side by side, two union levers, an inlet pipe, a membrane closure pipe and a hook are formed, two union levers connect parallel inlet pipe and membrane closure pipe respectively, constitute a rectangular frame, hollow-fibre membrane is arranged in the framework side by side, wherein an end is arranged in inlet pipe and fixes with Resins, epoxy, the other end is imbedded membrane closure Guan Bingyong epoxy sealing and is fixed, make gas enter and can not flow out from the other end from hollow-fibre membrane one end, hook is fixed in curtain formula hollow fiber film assembly in the reactor tank body.
Described cartridge type hollow fiber film assembly is made up of some hollow-fibre membranes arranged side by side, inlet mouth, inlet end, membrane closure plate, bracing frame, inlet mouth places circular inlet end center of top position, one end of hollow-fibre membrane is arranged in inlet end and fixes with Resins, epoxy, the other end is imbedded circular membrane closure plate and is fixed with epoxy sealing, make gas enter and can not flow out from the other end from hollow-fibre membrane one end, bracing frame is fixed in the cartridge type hollow fiber film assembly in the reactor tank body.
Described curtain formula hollow fiber film assembly and cartridge type hollow fiber film assembly are the dead end hollow fiber film assembly, and gas can only enter and can not flow out from the other end from hollow-fibre membrane one end, and the gas that enters the film chamber can only spread from fenestra and pass.
Described curtain formula hollow fiber film assembly and cartridge type hollow fiber film assembly, can be according to processing power or reactor tank body size, single or multiple assemblies are set carry out parallel connection, and the quantity of the hollow-fibre membrane of single component also can be selected and be adjusted as required, and the quantity of preferred hollow-fibre membrane is 30～10000.
Described hollow-fibre membrane is the microporous hydrophobic air-permeating film that polysulfones, polyethylene, polypropylene or polytetrafluoroethylmaterial material are made, and the external diameter of hollow-fibre membrane is 0.015～4.5mm, the thick 0.005～0.8mm of membranous wall, and membrane pore size is 0.07～0.45 μ m.
Described hollow-fibre membrane has following feature: the ventilation property membranous wall of hollow-fibre membrane is as the Supporting Media of biofilm development on film/liquid interface, it is the microbial film of 10～2000 μ m that the ventilation property membranous wall outside can form a layer thickness, microbial film is a kind of microorganism cells that comprises, the superpolymer that cell produces, the abiotic solid of intercepting and capturing, matrix, the complex set zoarium in metabolite and inner duct, the ventilation property membranous wall provides a bigger surface-area for the transmission and the biomembranous formation of gas, apposition growth has biomembranous hollow-fibre membrane membranous wall to contact with gas closely, gas can be directly delivered on the fixation of microbe in the microbial film with nearest distance by the ventilation property membranous wall, avoided the gas-liquid mass transfer step, and in this transmittance process, can not form bubble, most gases microorganism that is fixed absorbs in the gas transfer process, extremely trace have little time be fixed gas transfer that microorganism absorbs in main body solution (culture medium solution), absorbed by suspension microorganism, therefore, can obtain nearly 100% gas utilising efficiency.
Described still air feed hollow fiber film assembly, for guaranteeing still air feed, hollow-fibre membrane film intracavity gas dividing potential drop should maintain below the bubble point pressure, is the hollow fiber film assembly of 0.07～0.45 μ m for the aperture, and the pilot-gas dividing potential drop is lower than 0.45MPa can guarantee to realize still air feed.This is one of key point that reaches the technology of the present invention purpose.
Compare with existing indissoluble gases fermentation technique, major advantage of the present invention is as follows:
(1) the still air feed hollow fiber film assembly in the reactor of the present invention makes gas be absorbed and used with the fixed cell that nearest distance is directly delivered in the microbial film, has avoided the gas-liquid mass transfer step, has improved fermentation reaction speed.
(2) the still air feed hollow fiber film assembly in the reactor of the present invention, realized that gas transmits air feed under the situation that does not form bubble, be still air feed, avoid unstripped gas to flee from main body solution with the form of bubble and lose, thereby improve the gas utilising efficiency.
(3) the still air feed hollow fiber film assembly in the reactor of the present invention, except having still air feed and gas being directly delivered to function on the microbial film, but also has the function of cell fixation, be immobilized cell attached to the microbial film on the hollow-fibre membrane, the loss of organism of fermentation has been avoided in the immobilization of cell.
(4) organism of fermentation in the reactor that when the discharge liquid product, can dam of the solid-liquid separation membrane module in the reactor of the present invention, further avoid microorganism cells to run off, reactor is moved under higher organism of fermentation cell concn condition all the time, thereby further improve fermentation reaction speed.
(5) the present invention's application is wider, and tunning can be gas, also can be liquid.If be gas then discharge from the outlet of the gaseous product of reactor head, if be liquid, auxiliary in solid-liquid separation membrane module and suction pump then down from product liquid outlet discharge.
(6) because membrane module is modular design, the reactor scale is changeable, to satisfy different industrial scales.
Still air feed-the solid-liquid separation integrated membrane biomembrane reactor of the present invention has higher fermentation reaction speed and production concentration, can improve the economic feasibility of synthetic gas fermentation and even the fermentation of other indissoluble gases.Be applicable to that various indissoluble gases are the biological fermentation process of raw material, including, but not limited to synthetic gas fermentation production of organic acid and alcohols, carbon monoxide ferment for hydrogen production, and biological desulphurization (for the metabolism of desulfurization microorganism growth provides the carbon source and the energy).
Description of drawings
Fig. 1 is the still air feed of the present invention-solid-liquid separation integrated membrane biomembrane reactor structural representation;
Description of reference numerals: 1-unstripped gas basin, 2-inlet mouth, 3-tensimeter, 4-gas meter, the 5-gas distribution pipe, the still air feed hollow fiber film assembly of 6-, 7-reactor tank body, 8-substratum basin, the 9-fresh feed pump, 10-water distributor, 11-recycle pump, 12-solid-liquid separation membrane module, 13-tensimeter, 14-suction pump, the 15-liquid meter, the outlet of 16-product liquid, the outlet of 17-gaseous product, the 18-thermometer, 19-pH meter, 20-material-feeding port.
Fig. 2 is a curtain formula hollow fiber film assembly structural representation;
Description of reference numerals: 21-hook, 22-inlet pipe, 23-union lever, the still air feed hollow-fibre membrane of 24-, 25-membrane closure pipe.
Fig. 3 is a cartridge type hollow fiber film assembly structural representation;
Description of reference numerals: 26-inlet mouth, 27-inlet end, the still air feed hollow-fibre membrane of 28-, 29-membrane closure plate, 30-bracing frame.
Fig. 4 is the still air feed membrane biomembrane of a present invention fundamental diagram;
Description of reference numerals: 31-hollow-fibre membrane, 32-film chamber, 33-membranous wall, 34-microbial film, 35-culture medium solution, 36-suspension microorganism, 37-fixation of microbe, 38-unstripped gas, 39-tunning.
Embodiment
Below in conjunction with the drawings and specific embodiments content of the present invention is described in further details.It should be noted, the invention is not restricted to following examples, many distortion can also be arranged, all distortion that every those of ordinary skill in the art can directly derive or associate from content disclosed by the invention all should be thought protection scope of the present invention.
Still air feed-solid-liquid separation integrated membrane biomembrane reactor (referring to Fig. 1) in the present embodiment, comprise reactor tank body 7, gas distribution pipe 5, still air feed hollow fiber film assembly 6, water distributor 10, solid-liquid separation membrane module 12 place in the reactor tank body 7, and the top of still air feed hollow fiber film assembly 6 and solid-liquid separation membrane module 12 is lower than liquid level 30～50cm in the reactor tank body 7; Still air feed hollow fiber film assembly 6 is communicated with gas distribution pipe 5, gas meter 4, inlet mouth 2, unstripped gas basin 1 successively; Water distributor 10 is communicated with fresh feed pump 9, substratum basin 8 successively; Solid-liquid separation membrane module 12 is communicated with suction pump 14, liquid meter 15, product liquid outlet 16 successively; Reactor tank body 7 bottoms are provided with circulating water outlet and are communicated with water distributor 10 by recycle pump 11, reactor tank body 7 tops are provided with gaseous product outlet 17, thermometer 18, pH meter 19 and tensimeter are installed on the reactor tank body 7, be convenient to monitor and the relevant operating parameter of adjusting reactor, also be provided with material-feeding port 20 on the reactor tank body 7, convenient inoculum or other solution of adding.For ease of the adjusting process parameter, in a plurality of positions of reactor pipeline variable valve is set, gas meter 4 and suction pump 14 front ends are provided with tensimeter 3 and tensimeter 13 respectively.
Above-mentioned still air feed hollow fiber film assembly 6 can be a curtain formula hollow fiber film assembly, also can be the cartridge type hollow fiber film assembly,, have maximum area/volume ratio because hollow fiber film assembly is compared with the membrane module of other form, therefore, select hollow fiber film assembly.
Above-mentioned curtain formula hollow fiber film assembly (referring to Fig. 2), by some hollow-fibre membranes arranged side by side 24, two union levers 23, an inlet pipe 22, a membrane closure pipe 25 and a hook 21 are formed, two union levers 23 connect parallel inlet pipe 22 and rectangular frame of membrane closure pipe 25 formations respectively, hollow-fibre membrane 24 is arranged in the framework side by side, wherein an end is arranged in inlet pipe 22 and fixes with Resins, epoxy, the other end is imbedded membrane closure pipe 25 and is fixed with epoxy sealing, make gas enter and can not flow out from the other end from hollow-fibre membrane 24 1 ends, hook 21 is used for curtain formula hollow fiber film assembly is fixed in the reactor tank body 7.
Above-mentioned cartridge type hollow fiber film assembly (referring to Fig. 3), by some hollow-fibre membranes arranged side by side 28, inlet mouth 26, inlet end 27, membrane closure plate 29, bracing frame 30 is formed, inlet mouth 26 places circular inlet end 27 center of top positions, one end of hollow-fibre membrane 28 is arranged in inlet end 27 inside and fixes with Resins, epoxy, the other end is imbedded circular membrane closure plate 29 and is fixed with epoxy sealing, make gas enter and can not flow out from the other end from hollow-fibre membrane 28 1 ends, bracing frame 30 is used for the cartridge type hollow fiber film assembly is fixed in the reactor tank body 7.
Above-mentioned curtain formula hollow fiber film assembly and cartridge type hollow fiber film assembly are the dead end hollow fiber film assembly, and gas can only enter and can not flow out from the other end from hollow-fibre membrane one end, and the gas that enters the film chamber can only spread from fenestra and pass.
Above-mentioned curtain formula hollow fiber film assembly and cartridge type hollow fiber film assembly, can be according to processing power and reactor tank body size, single or multiple assemblies are set carry out parallel connection, and the quantity of the hollow-fibre membrane of single component also can be selected to adjust as required, and the quantity of preferred hollow-fibre membrane is 30～10000.
Above-mentioned hollow-fibre membrane is the microporous hydrophobic air-permeating film that polysulfones, polyethylene, polypropylene or polytetrafluoroethylmaterial material are made, and the external diameter of hollow-fibre membrane is 0.015～4.5mm, the thick 0.005～0.8mm of membranous wall, and membrane pore size is 0.07～0.45 μ m.
The principle of work of still air feed membrane biomembrane (referring to Fig. 4) is: the ventilation property membranous wall 33 of hollow-fibre membrane 31 is as the Supporting Media of 34 growths of microbial film on film/liquid interface, and ventilation property membranous wall 33 outsides can form the microbial film 34 that a layer thickness is 10～2000 μ m.Microbial film 34 is a kind of complex set zoariums that comprise abiotic solid, matrix, metabolite and the inner duct of superpolymer that microorganism cells, cell produce, intercepting and capturing.Ventilation property membranous wall 33 provides a bigger surface-area for the transmission of gas 38 and the formation of microbial film 34 in the film chamber 32.Apposition growth has the membranous wall 33 of microbial film 34 to contact with gas 38 closely, gas 38 can be directly delivered on the fixation of microbe 37 in the microbial film 34 with nearest distance by ventilation property membranous wall 33, avoid the gas-liquid mass transfer step, and in this transmittance process, can not form bubble.Most gases microorganism 37 that is fixed absorbs in the gas transfer process, extremely trace have little time be fixed gas transfer that microorganism 37 absorbs in main body solution (culture medium solution 35), absorbed by suspension microorganism 36, therefore, can obtain nearly 100% gas utilising efficiency.The tunning 39 that fixation of microbe 37 utilizes gas to generate is delivered to microbial film 34 surfaces by diffusion, under the waterpower stirring action from top to bottom that recycle pump 11 is carried out, rapidly the tunning 39 on microbial film 34 surfaces is taken away, thereby the concentration gradient that guarantees tunning 39 is beneficial to mass transfer.
For the plenum system of guaranteeing hollow fiber film assembly is still air feed, hollow-fibre membrane film intracavity gas dividing potential drop should maintain below the bubble point pressure, for aperture among the present invention is the hollow fiber film assembly of 0.07～0.45 μ m, and the pilot-gas dividing potential drop is lower than 0.45MPa can guarantee to realize still air feed.
Hollow-fibre membrane described in the present invention is the conventional fibre film, can buy from market.
Solid-liquid separation membrane module and cell separation technology, the product and the mature technology that are a commercialization, all there are sale in many enterprises such as membrane science technical institute of Nanjing University of Technology, Wuxi City Ultrafilter Equipment Factory, Yuyao membrane separation plant factory, Zhaoyuan, Shandong membrane separation plant factory, the bright utmost point in Shanghai Chemical Industry Science Co., Ltd, Hangzhou Kaihong Membrane Technology Co., Ltd., Motian Film Science and Technology Co., Ltd., Tianjin etc. both at home and abroad.Ultra-filtration membrane or microfiltration membrane are housed in the solid-liquid separation membrane module, allow materials such as water, small molecular organic acid, alcohol to pass through, particulate matter such as fermentation cell can not be passed through, thereby the fermentation cell is retained in the reactor, and tunning can be discharged from reactor.Therefore, solid-liquid separation membrane module of the present invention directly adopts prior art.
The operational process of the still air feed-solid-liquid separation integrated membrane biomembrane reactor in the present embodiment is as follows:
When reactor start-up, feeding steam from material-feeding port 20 to reactor tank body 7 sterilizes, sterilization time 30min, and then pump into aseptic culture medium by fresh feed pump 9 to reactor tank body 7 from substratum basin 8, be higher than still air feed hollow fiber film assembly and solid-liquid separation membrane module top 30～50cm up to the substratum liquid level, assisting down of thermometer 18 and pH meter 19, regulating also, controlling reactor tank body 7 interior temperature and pH are desirable value.Add inoculation liquid and organic carbon source (as glucose solution) from material-feeding port 20, liquid in 11 pairs of reactors of ON cycle pump stirs, but the Control Circulation amount can not be too big, internal circulating load is crossed conference and is slowed down biomembranous formation, cultivation through 10～20 days, can form a layer thickness above the membranous wall 33 of hollow-fibre membrane 31 in the still air feed hollow fiber film assembly 6 is the microbial film 34 of 10～2000 μ m, microbial film 34 mainly is made up of fixation of microbe 37, in the main body solution (culture medium solution 35) suspension microorganism 36 is arranged still simultaneously.Open unstripped gas basin 1 from inlet mouth 2 to still air feed hollow fiber film assembly 6 air feed, and regulate intake valves control intake pressures according to tensimeter 3 and be lower than 0.45MPa to guarantee still air feed.Unstripped gas 38 enters the film chamber 32 of hollow-fibre membrane 31, and from the fenestra of membranous wall 33, spread and be delivered on the microbial film 34, overwhelming majority gas is absorbed by the fixation of microbe 37 in the microbial film 34 and generates tunning 39, tunning 39 is diffused into culture medium solution 35 immediately, the gas that the microorganism 37 that has little time to be fixed utilizes enters culture medium solution 35, is further utilized the generation tunning by suspension microorganism.If tunning is gas (a for example carbon monoxide ferment for hydrogen production), open gaseous product outlet 17, collect the gaseous product that fermentation produces.If tunning is liquid (for example synthetic gas fermentation system ethanol and an acetate), and when tunning concentration reaches desired value, open product liquid outlet 16 and start suction pump 14, under the membrane sepn effect of solid-liquid separation membrane module 12, the liquid that contains tunning but do not contain microorganism cells flows out from product liquid outlet 16, and microorganism cells is trapped within the reactor tank body 7, thereby avoids microorganism cells to run off, and reactor is moved under higher microorganism cells concentration conditions all the time.Regularly pass through fresh feed pump 9 supplemental medium in reactor tank body 7 during the fermentation, to guarantee the required nutritive ingredient of organism of fermentation normal growth metabolism from substratum basin 8.
Claims (7)
1. still air feed-solid-liquid separation-body formula membrane biomembrane reactor, comprise the reactor tank body, it is characterized in that: gas distribution pipe, still air feed hollow fiber film assembly, water distributor, solid-liquid separation membrane module place in the reactor tank body, the top of still air feed hollow fiber film assembly and solid-liquid separation membrane module is lower than liquid level in the reactor tank body: still air feed hollow fiber film assembly is communicated to the unstripped gas basin by gas distribution pipe, water distributor is communicated to the substratum basin through fresh feed pump, and the solid-liquid separation membrane module is communicated with the product liquid outlet through suction pump; Reactor tank body bottom is provided with circulating water outlet, and circulating water outlet is communicated with water distributor by recycle pump; Reactor tank body top is provided with the gaseous product outlet, and thermometer, pH meter and tensimeter are installed on the reactor tank body, and material-feeding port also is installed on the reactor tank body; Hollow-fibre membrane film intracavity gas dividing potential drop is lower than bubble point pressure, realizes still air feed to guarantee still air feed hollow fiber film assembly.
2. still air feed-solid-liquid separation integrated membrane biomembrane reactor as claimed in claim 1 is characterized in that described still air feed hollow fiber film assembly is the dead end hollow fiber film assembly, is curtain formula hollow fiber film assembly or cartridge type hollow fiber film assembly.
3. still air feed-solid-liquid separation as claimed in claim 2-body formula membrane biomembrane reactor, it is characterized in that described curtain formula hollow fiber film assembly is by some hollow-fibre membranes arranged side by side, two union levers, an inlet pipe, a membrane closure pipe and a hook are formed, two union levers connect parallel inlet pipe and membrane closure pipe respectively, constitute a rectangular frame, hollow-fibre membrane is arranged in the framework side by side, wherein an end is arranged in inlet pipe and fixes with Resins, epoxy, the other end is imbedded membrane closure Guan Bingyong epoxy sealing and is fixed, make gas enter and can not flow out from the other end from hollow-fibre membrane one end, hook is fixed in curtain formula hollow fiber film assembly in the reactor tank body.
4. still air feed-solid-liquid separation as claimed in claim 2-body formula membrane biomembrane reactor, it is characterized in that described cartridge type hollow fiber film assembly is by some hollow-fibre membranes arranged side by side, inlet mouth, inlet end, the membrane closure plate, bracing frame is formed, inlet mouth places circular inlet end center of top position, one end of hollow-fibre membrane is arranged in inlet end and fixes with Resins, epoxy, the other end is imbedded circular membrane closure plate and is fixed with epoxy sealing, make gas enter and can not flow out from the other end from hollow-fibre membrane one end, bracing frame is fixed in the cartridge type hollow fiber film assembly in the reactor tank body.
5. still air feed-solid-liquid separation integrated membrane biomembrane reactor as claimed in claim 2, it is characterized in that described curtain formula hollow fiber film assembly and cartridge type hollow fiber film assembly, can single or multiple assemblies be set carry out parallel connection according to processing power or reactor tank body size.
6. still air feed-solid-liquid separation integrated membrane biomembrane reactor as claimed in claim 1 or 2, it is characterized in that described hollow-fibre membrane is the microporous hydrophobic air-permeating film that polysulfones, polyethylene, polypropylene or polytetrafluoroethylmaterial material are made, the external diameter of hollow-fibre membrane is 0.015～4.5mm, thick 0.005～the 0.8mm of membranous wall, membrane pore size is 0.07～0.45 μ m.
7. still air feed-solid-liquid separation integrated membrane biomembrane reactor as claimed in claim 6 is characterized in that hollow-fibre membrane film intracavity gas dividing potential drop is lower than 0.45MPa.
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Inventor after: Yuan Zhenhong Inventor after: Li Dong Inventor after: Sun Yongming Inventor after: Kong Xiaoying Inventor after: Li Lianhua Inventor after: Xu Jingliang Inventor after: Xu Huijuan Inventor before: Li Dong Inventor before: Yuan Zhenhong Inventor before: Sun Yongming Inventor before: Kong Xiaoying Inventor before: Li Lianhua Inventor before: Xu Jingliang Inventor before: Xu Huijuan |
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Application publication date: 20100915 |