CN109735452A - Airlift bioreactor for membrane tube gas distribution and application thereof - Google Patents
Airlift bioreactor for membrane tube gas distribution and application thereof Download PDFInfo
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- CN109735452A CN109735452A CN201910225398.1A CN201910225398A CN109735452A CN 109735452 A CN109735452 A CN 109735452A CN 201910225398 A CN201910225398 A CN 201910225398A CN 109735452 A CN109735452 A CN 109735452A
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- 239000012528 membrane Substances 0.000 title claims abstract description 149
- 239000007788 liquid Substances 0.000 claims abstract description 48
- 238000000855 fermentation Methods 0.000 claims abstract description 19
- 230000004151 fermentation Effects 0.000 claims abstract description 19
- 230000000630 rising effect Effects 0.000 claims description 31
- 239000002184 metal Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000011521 glass Substances 0.000 claims description 4
- 239000012510 hollow fiber Substances 0.000 claims description 4
- -1 polyethylene Polymers 0.000 claims description 4
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 4
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims description 4
- 241000195493 Cryptophyta Species 0.000 claims description 2
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 claims description 2
- 239000004698 Polyethylene Substances 0.000 claims description 2
- 210000004102 animal cell Anatomy 0.000 claims description 2
- 238000004113 cell culture Methods 0.000 claims description 2
- 229940113088 dimethylacetamide Drugs 0.000 claims description 2
- 230000000813 microbial effect Effects 0.000 claims description 2
- 229920000573 polyethylene Polymers 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 149
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 31
- 229910052760 oxygen Inorganic materials 0.000 abstract description 31
- 239000001301 oxygen Substances 0.000 abstract description 31
- 238000012546 transfer Methods 0.000 abstract description 9
- 238000000034 method Methods 0.000 abstract description 7
- 238000003756 stirring Methods 0.000 abstract description 7
- 238000010008 shearing Methods 0.000 abstract description 5
- 230000001965 increasing effect Effects 0.000 abstract description 3
- 230000036284 oxygen consumption Effects 0.000 abstract description 2
- 230000003519 ventilatory effect Effects 0.000 description 11
- 238000005273 aeration Methods 0.000 description 10
- 230000001954 sterilising effect Effects 0.000 description 6
- NAOLWIGVYRIGTP-UHFFFAOYSA-N 1,3,5-trihydroxyanthracene-9,10-dione Chemical compound C1=CC(O)=C2C(=O)C3=CC(O)=CC(O)=C3C(=O)C2=C1 NAOLWIGVYRIGTP-UHFFFAOYSA-N 0.000 description 4
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 4
- KDXKERNSBIXSRK-YFKPBYRVSA-N L-lysine Chemical compound NCCCC[C@H](N)C(O)=O KDXKERNSBIXSRK-YFKPBYRVSA-N 0.000 description 4
- 230000002708 enhancing effect Effects 0.000 description 4
- 239000008103 glucose Substances 0.000 description 4
- 239000001963 growth medium Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000002609 medium Substances 0.000 description 4
- 125000004122 cyclic group Chemical group 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 241000588724 Escherichia coli Species 0.000 description 2
- 239000007836 KH2PO4 Substances 0.000 description 2
- AYFVYJQAPQTCCC-GBXIJSLDSA-N L-threonine Chemical compound C[C@@H](O)[C@H](N)C(O)=O AYFVYJQAPQTCCC-GBXIJSLDSA-N 0.000 description 2
- 239000004472 Lysine Substances 0.000 description 2
- KDXKERNSBIXSRK-UHFFFAOYSA-N Lysine Natural products NCCCCC(N)C(O)=O KDXKERNSBIXSRK-UHFFFAOYSA-N 0.000 description 2
- 241000209149 Zea Species 0.000 description 2
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 2
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 235000005822 corn Nutrition 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002054 inoculum Substances 0.000 description 2
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 238000009923 sugaring Methods 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 210000004027 cell Anatomy 0.000 description 1
- 229910010293 ceramic material Inorganic materials 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011534 incubation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
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- Apparatus Associated With Microorganisms And Enzymes (AREA)
Abstract
The invention belongs to the field of bioreactors, and particularly relates to an airlift bioreactor for membrane tube gas distribution and application thereof. The bioreactor can be used for fermentation through external circulation and internal circulation, has a simple structure, and solves the problems of low gas-liquid mass transfer efficiency and large shearing force of the stirring bioreactor in the gas-liquid mass transfer process. Especially in high oxygen consumption culture, shear sensitive systems. The membrane tube is better applied to the bioreactor, the bubbles can reach below 1000 mu m, the generation of tiny bubbles is realized, the gas distribution is uniform, the gas-liquid mass transfer of gas and liquid is improved, the volume dissolved oxygen coefficient is improved, the gas content is increased, the volume dissolved oxygen coefficient is improved by 30 percent compared with the traditional annular gas distribution airlift bioreactor, and the membrane tube has good application prospect.
Description
Technical field
The invention belongs to bioreactor fields, and in particular to a kind of airlift bioreactor of membrane tube gas distribution and its answer
With.
Background technique
In biofermentation and incubation, bioreactor is played an important role, he is connection raw material and product
Bridge manufactures and designs a kind of high-performance bioreactor, can simplify production procedure in terms of engineering production, can also reduce life
Cost is produced, raw material availability is increased.There are three types of traditional forms for bioreactor at present: mechanical agitation type, gas-lifting type, bubble tower
Formula.With the development of engineering technology, researchers gradually develop the reactor of a variety of aeration forms, such as self-priming,
Venturi jetting type etc..The main target of research be reduce gas in a liquid bubble diameter increase gas liquid interfacial area；Also
Have and increases the residence time of gas in a liquid, mass transfer enhancement process；Improve gas effciency.
Microvesicle bioreactor is a kind of by different gas distribution modes, and gas is scattered in micro-bubble, Lai Zengjia oxygen
A kind of reactor of mass transfer effect.Purpose is by increasing gas liquid interfacial area, and Lai Zengqiang oxygen transfer keeps oxygen in air abundant
It utilizes, reduces energy consumption.The research biological culture high for oxygen demand plays the role of positive.There are many mode for generating microvesicle at present
Kind, have through shearing force to bubble formation microvesicle, such as self-priming gas distribution, jetting type etc.；Micro-pore aeration is also a kind of principal mode,
The poromerics studied at present is varied, and aperture can arrive micron and Nano grade.Micro-pore aeration generates microvesicle phase
It is more suitable for the culture of biological cell for the microvesicle that shearing force form is formed.
Summary of the invention
The object of the present invention is to provide a kind of airlift bioreactor of membrane tube gas distribution and its applications, and it is raw to solve stirring-type
Object reactor is in mass-transfer progress, gas-liquid mass transfer low efficiency, and shearing force is big.It is quick to shearing force especially in high oxygen consumption culture
In the system of sense.The present invention is preferably to be applied to membrane tube in bioreactor, realizes that micro-bubble generates, uniform air distribution,
Gas-liquid gas-liquid mass transfer is improved, volume dissolved oxygen coefficient is improved, increases gas holdup.
To solve prior art problem, the technical scheme adopted by the invention is as follows:
The top of a kind of membrane tube gas distribution formula bioreactor, including tank body, the tank body is equipped with liquid inlet, gas access, gas
Body outlet, tank base are equipped with liquid outlet, further include gas distribution when the bioreactor is that outer circulation mode is fermented
Device and U-tube guide tube, the upper end of the gas distributor are flexibly connected with tank body, and lateral opening hole and the U-tube of the tank body are led
Cylinder connection, the other end of the U-tube guide tube and the lower end of gas distributor connect to form circulation line；The gas distributor
Including gas distribution membrane tube and membrane tube fixed frame, the gas distribution membrane tube is fixed on the inside of membrane tube fixed frame；The intracorporal top of tank
Cavity is flow field body rising area, and flow field rises flowing wherein, and the lower cavity in the U-tube guide tube is flow field descending area,
Flow field until the bottom of gas distributor, and is again introduced into gas distributor by guide tube flow down, forms circulation flow field；
Further include gas distributor and guide tube when the bioreactor is that interior circulation pattern ferments, the gas distributor it is upper
After end is flexibly connected with guide tube, it is movably connected on the center of tank interior, the cavity area in the guide tube is on flow field
Area is risen, the outer cavity tank body tank body between of guide tube is flow field descending area, gas and liquid by the rising of guide tube inside, then from leading
Cylinder outer loop forms circulation flow field in the bottom of gas distributor.
It is that the diameter ratio of the gas-liquid rising area and gas-liquid descending area is 1-10:1-10 as improved.
Be as improved, the gas distribution membrane tube be micropore membrane tube, the micropore membrane tube be ceramic-film tube, metal film pipe,
Glass membrane tube, polyethylene membrane tube, polytetrafluoroethylene (PTFE) membrane tube, ps hollow fiber uf membrane pipe or dimethyl acetamide hollow fiber membrane tube.
Further improved to be, the 10 nm-100000 nm of micro-pore diameter of the micropore membrane tube, the shape of micropore is circle
Hole, square hole or polygonal hole, the number of micropore are 1-50；The length of membrane tube is 20 mm-10000 mm, the diameter of membrane tube
For 0.1 mm-100 mm.
It is that the shape of the bioreactor is round, quadrangle or polygon as improved.
It is that membrane tube quantity is 1-5000 root, the arrangement side of the membrane tube in the membrane tube gas distributor as improved
Formula is vertical or horizontal.
The airlift bioreactor of above-mentioned membrane tube gas distribution is in microbial fermentation, animal cell culture, algae culture, fixation
Application in one-carbon compound or gas-liquid chemical reaction.
The utility model has the advantages that
The present invention in conjunction with airlift bioreactor, establishes a kind of biological respinse of new gas distribution mode using micropore membrane tube
Device, bubble is up to 1000 μm hereinafter, the traditional cyclic annular gas distribution airlift bioreactor of its volume dissolved oxygen coefficient ratio improves 30%.
This method improves oxygen utilization rate in gas well, reduces air usage amount.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of outer circulation bioreactor of the present invention, 1- gas distributor, the flow field 2- rising area；3-
Flow field descending area；4-U type pipe guide tube；5- gas vent；The liquid inlet 6-；The gas access 7-；8- liquid outlet；11- tank body,
Fig. 2 is the structural schematic diagram of internal circulation biological reactor of the present invention, 1- gas distributor, the flow field 2- rising area；The flow field 3-
Descending area；12- guide tube；5- gas vent；The liquid inlet 6-；The gas access 7-；8- liquid outlet；11- tank body；
Fig. 3 is the top view of gas distributor of the present invention, wherein 9- gas distribution membrane tube；10- membrane tube fixed frame.
Specific embodiment
Embodiment 1
Bioreactor is built according to the structure of Fig. 1, endless form used is outer circulation mode.
The top of a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body is equipped with liquid inlet 6, gas
Entrance 7, gas vent 5, tank base are equipped with liquid outlet 8, when the bioreactor is that outer circulation mode is fermented, also wrap
Gas distributor 1 and U-tube guide tube 4 are included, the upper end of the gas distributor 1 is flexibly connected with tank body 11, the tank body 11
Lateral opening hole is connect with U-tube guide tube 4, and the other end of the U-tube guide tube 4 connect to be formed with the lower end of gas distributor 1 to follow
Endless tube road.The gas distributor 1 includes gas distribution membrane tube 9 and membrane tube fixed frame 10, and it is solid that the gas distribution membrane tube 9 is fixed on membrane tube
Determine the inside of frame 10；Upper cavity in the tank body 11 is flow field body rising area 2, and flow field rises flowing wherein, described to lead
Lower cavity in cylinder 4 is flow field descending area 3, and flow field is by 4 flow down of guide tube, until the bottom of gas distributor 1, and again
It is secondary to enter gas distributor 1, form circulation flow field.
In the membrane tube gas distributor gas distribution membrane tube be micropore membrane tube, and micropore membrane tube be glass membrane tube when, with organic
Glass multiwell plate compares, and the diameter ratio of 2 diameter of flow field rising area and flow field descending area 3 is 1:1；When ventilatory capacity is 0.6 m3/h
When, the volume dissolved oxygen coefficient of flow field rising area 2 is 25.3, and descending area 3 volume dissolved oxygen coefficient in flow field is 23.42, and gas holdup is
1.8%。
Embodiment 2
The top of a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body is equipped with liquid inlet 6, gas access
7, gas vent 5, tank base is equipped with liquid outlet 8, further includes gas when the bioreactor is that outer circulation mode is fermented
The upper end of body distributor 1 and U-tube guide tube 4, the gas distributor 1 is flexibly connected with tank body 11, the side of the tank body 11
Aperture is connect with U-tube guide tube 4, and the other end of the U-tube guide tube 4 connect to form circulation pipe with the lower end of gas distributor 1
Road.The gas distributor 1 includes gas distribution membrane tube 9 and membrane tube fixed frame 10, and the gas distribution membrane tube 9 is fixed on membrane tube fixed frame
10 inside；Upper cavity in the tank body 11 is flow field body rising area 2, and flow field rises flowing wherein, in the guide tube 4
Lower cavity be flow field descending area 3, flow field is by 4 flow down of guide tube, until the bottom of gas distributor 1, and again into
Enter gas distributor 1, forms circulation flow field.
Gas distribution membrane tube is micropore membrane tube in the membrane tube gas distributor, and micropore membrane tube is ceramic-film tube, with ceramic material
Expect that membrane tube aeration, membrane tube length are 500 mm, membrane micropore aperture is 50 nm；3 mm of film inner hole diameter, fenestra number of aperture 19
It is a；Metal shell is fixed, and membrane tube is 7, and 2 diameter of flow field rising area and flow field descending area diameter ratio are 1:1；When ventilatory capacity is
0.6m3When/h, the volume dissolved oxygen coefficient of flow field rising area 2 is 59.59, and the volume dissolved oxygen coefficient of flow field descending area 3 is 35.03,
Gas holdup is 5%.
Embodiment 3
The top of a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body is equipped with liquid inlet 6, gas access
7, gas vent 5, tank base is equipped with liquid outlet 8, further includes gas when the bioreactor is that outer circulation mode is fermented
The upper end of body distributor 1 and U-tube guide tube 4, the gas distributor 1 is flexibly connected with tank body 11, the side of the tank body 11
Aperture is connect with U-tube guide tube 4, and the other end of the U-tube guide tube 4 connect to form circulation pipe with the lower end of gas distributor 1
Road.The gas distributor 1 includes gas distribution membrane tube 9 and membrane tube fixed frame 10, and the gas distribution membrane tube 9 is fixed on membrane tube fixed frame
10 inside；Upper cavity in the tank body 11 is flow field body rising area 2, and flow field rises flowing wherein, in the guide tube 4
Lower cavity be flow field descending area 3, flow field is by 4 flow down of guide tube, until the bottom of gas distributor 1, and again into
Enter gas distributor 1, forms circulation flow field.
Gas distribution membrane tube is micropore membrane tube in the membrane tube gas distributor, and micropore membrane tube is ceramic-film tube, membrane tube length
For 500 mm, membrane micropore aperture is 500 nm；5 mm of film inner hole diameter, fenestra number of aperture 19；Metal shell is fixed, membrane tube
It is 7, rising area diameter and descending area diameter ratio are 1:1；When ventilatory capacity is 2.1 m3When/h, the volume dissolved oxygen coefficient of rising area
It is 64.03, descending area volume dissolved oxygen coefficient is 40.21, gas holdup 5.5%.
Embodiment 4
The top of a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body is equipped with liquid inlet 6, gas access
7, gas vent 5, tank base is equipped with liquid outlet 8, further includes gas when the bioreactor is that outer circulation mode is fermented
The upper end of body distributor 1 and U-tube guide tube 4, the gas distributor 1 is flexibly connected with tank body 11, the side of the tank body 11
Aperture is connect with U-tube guide tube 4, and the other end of the U-tube guide tube 4 connect to form circulation pipe with the lower end of gas distributor 1
Road.The gas distributor 1 includes gas distribution membrane tube 9 and membrane tube fixed frame 10, and the gas distribution membrane tube 9 is fixed on membrane tube fixed frame
10 inside；Upper cavity in the tank body 11 is flow field body rising area 2, and flow field rises flowing wherein, in the guide tube 4
Lower cavity be flow field descending area 3, flow field is by 4 flow down of guide tube, until the bottom of gas distributor 1, and again into
Enter gas distributor 1, forms circulation flow field.
Gas distribution membrane tube is micropore membrane tube in the membrane tube gas distributor, and micropore membrane tube is ceramic-film tube, membrane tube length
For 500 mm, membrane micropore aperture is 500 nm；5 mm of film inner hole diameter, fenestra number of aperture 19；Metal shell is fixed, membrane tube
It is 7, rising area diameter and descending area diameter ratio are 2:1；When ventilatory capacity is 2.1 m3When/h, the volume dissolved oxygen coefficient of rising area
It is 61.03, descending area volume dissolved oxygen coefficient is 45.21, gas holdup 7.3%.
Embodiment 5
The top of a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body is equipped with liquid inlet 6, gas access
7, gas vent 5, tank base is equipped with liquid outlet 8, further includes gas when the bioreactor is that outer circulation mode is fermented
The upper end of body distributor 1 and U-tube guide tube 4, the gas distributor 1 is flexibly connected with tank body 11, the side of the tank body 11
Aperture is connect with U-tube guide tube 4, and the other end of the U-tube guide tube 4 connect to form circulation pipe with the lower end of gas distributor 1
Road.The gas distributor 1 includes gas distribution membrane tube 9 and membrane tube fixed frame 10, and the gas distribution membrane tube 9 is fixed on membrane tube fixed frame
10 inside；Upper cavity in the tank body 11 is flow field body rising area 2, and flow field rises flowing wherein, in the guide tube 4
Lower cavity be flow field descending area 3, flow field is by 4 flow down of guide tube, until the bottom of gas distributor 1, and again into
Enter gas distributor 1, forms circulation flow field.
Gas distribution membrane tube is micropore membrane tube in the membrane tube gas distributor, and micropore membrane tube is ceramic-film tube, membrane tube length
For 500 mm, membrane micropore aperture is 500 nm；5 mm of film inner hole diameter, fenestra number of aperture 19；Metal shell is fixed, membrane tube
It is 7, flow field rising area diameter and flow field descending area diameter ratio are 2:1；When ventilatory capacity is 2.1 m3When/h, flow field rising area
Volume dissolved oxygen coefficient is 61.03, and flow field descending area volume dissolved oxygen coefficient is 45.21, gas holdup 7.3%.
0.1 m is established with above structure3Practical systems reactor is simultaneously applied, and process is as follows:
Medium sterilization is carried out first, is passed through a small amount of air and enhancing is mixed, be heated evenly culture medium.When temperature is raised to 95 DEG C
It can stop stirring above.The sterilizing of air filter and air pipeline, slightly opened filter and drain valve are carried out again, to guarantee
Air pipeline sterilizing.Final discharge port, sampling valve, steam valve and outlet valve are slightly opened, and guarantee that the pipeline sterilizes.
Fermented and cultured and result: the Escherichia coli for producing L- lysine (are bought from CGMCC, strain by 10% inoculum concentration
Deposit number is CGMCC1.0281) (1L fermentation medium contains: glucose 20 ~ 40 g/L, (NH in reactor4)2SO4 1.5~
1.8 g, KH2PO41.2 g, 1 ~ 2 g of corn pulp, g), starting ventilatory capacity is 0.6 m to L- threonine 0.2 ~ 0.43/ h ventilation
Amount, then gradually promotes ventilatory capacity according to dissolved oxygen, 35 ~ 37 DEG C of fermentation temperature, Feeding ammonia water is to control pH 6.5 ~ 6.8, often
Detect remaining sugar concentration every 2 ~ 4 h, cocurrent adds the glucose of 500 g/L, maintain remaining sugar concentration 4 before 3-5 g/L, fermentation ends ~
5 h stop stream sugaring liquid, when residual sugar is down to 5 ~ 7g/L, i.e. fermentation ends, and about 50 h of entire fermentation period.Fermentation process
In, gas is escaped from membrane tube nanoscale aperture, is passed through in atmosphere from outlet valve after gas membrane tube distributor.It is fermenting
Peak period improves air inflow to maximum, and the solubility of oxygen is enabled to reach 2.5-3.2 ppm, but should be noted that because
To manually control tank pressure in fermentation process, so outlet valve must be adjusted simultaneously when adjusting air mass flow, so that tank
It presses and constant is greater than 0.03 Mpa.
Comparison does not have membrane tube aeration structure, the bioreactor of cyclic annular aeration stirring formula, 0.1 m of reactor size3, hair
Ferment mode is consistent with culture medium with the present embodiment.As follows by fermentation results: reactor of the invention uses micropore ceramics membrane tube
Being aerated obtained dissolved oxygen is 3.3 ppm, and saccharic acid conversion ratio is 62 %, and the dissolved oxygen data for comparing conventional reactor are 2.8 ppm, carbon
Sour conversion ratio 53%.From the above data, it can be seen that the reactor of the invention using membrane tube aeration, which raises oxyty,
Improve reactor totality mass tranfer coefficient.Energy consumption needed for reducing stirring, the saccharic acid conversion ratio of enhancing lysine production.
Embodiment 6
Bioreactor, a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body are built in the way of Fig. 2
Top be equipped with liquid inlet 6, gas access 7, gas vent 5, tank base be equipped with liquid outlet 8, when the biological respinse
It further include gas distributor 1 and guide tube 12, upper end and the guide tube 12 of the gas distributor 1 when device is that interior circulation pattern ferments
After flexible connection, it is movably connected on the center inside tank body 1, the cavity area in the guide tube 12 is flow field rising area 2,
The outer cavity tank body 11 between of guide tube 4 is flow field descending area 3, and gas and liquid pass through to be risen inside guide tube 4, then from guide tube 4
Outer loop forms circulation flow field in the bottom of gas distributor 1.
Gas distribution membrane tube is micropore membrane tube in the membrane tube gas distributor, and micropore membrane tube is ceramic-film tube, membrane tube length
For 200 mm, membrane micropore aperture is 50 nm；3 mm of film inner hole diameter, fenestra number of aperture 19；Metal shell is fixed, membrane tube
It is 16, rising area diameter and descending area diameter ratio are 1:1；When ventilatory capacity is 2.1 m3When/h, the volume dissolved oxygen system of rising area
Number is 60.53, and descending area volume dissolved oxygen coefficient is 36.21, gas holdup 5.7%.
Embodiment 7
Bioreactor, a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body are built in the way of Fig. 2
Top be equipped with liquid inlet 6, gas access 7, gas vent 5, tank base be equipped with liquid outlet 8, when the biological respinse
It further include gas distributor 1 and guide tube 12, upper end and the guide tube 12 of the gas distributor 1 when device is that interior circulation pattern ferments
After flexible connection, it is movably connected on the center inside tank body 1, the cavity area in the guide tube 12 is flow field rising area 2,
The outer cavity tank body 11 between of guide tube 4 is flow field descending area 3, and gas and liquid pass through to be risen inside guide tube 4, then from guide tube 4
Outer loop forms circulation flow field in the bottom of gas distributor 1.
Gas distribution membrane tube is micropore membrane tube in the membrane tube gas distributor, and micropore membrane tube is ceramic-film tube, membrane tube length
For 100 mm, membrane micropore aperture is 500 nm；5 mm of film inner hole diameter, fenestra number of aperture 19；Metal shell is fixed, membrane tube
It is 16, rising area diameter and descending area diameter ratio are 2:1；When ventilatory capacity is 2.1 m3When/h, the volume dissolved oxygen system of rising area
Number is 70.32, and descending area volume dissolved oxygen coefficient is 50.43, and gas holdup is 8.9 %.
Embodiment 8
Bioreactor, a kind of membrane tube gas distribution formula bioreactor, including tank body 11, the tank body are built in the way of Fig. 2
Top be equipped with liquid inlet 6, gas access 7, gas vent 5, tank base be equipped with liquid outlet 8, when the biological respinse
It further include gas distributor 1 and guide tube 12, upper end and the guide tube 12 of the gas distributor 1 when device is that interior circulation pattern ferments
After flexible connection, it is movably connected on the center inside tank body 1, the cavity area in the guide tube 12 is flow field rising area 2,
The outer cavity tank body 11 between of guide tube 4 is flow field descending area 3, and gas and liquid pass through to be risen inside guide tube 4, then from guide tube 4
Outer loop forms circulation flow field in the bottom of gas distributor 1.
Gas distribution membrane tube is micropore membrane tube in the membrane tube gas distributor, and micropore membrane tube is ceramic-film tube, membrane tube length
For 100 mm, membrane micropore aperture is 500 nm；5 mm of film inner hole diameter, fenestra number of aperture 19；Metal shell is fixed, membrane tube
It is 16, rising area diameter and descending area diameter ratio are 2:1, about 0.5 m of total volume3, establish hotting mask reactor.
Medium sterilization is carried out first, is passed through a small amount of air and enhancing is mixed, be heated evenly culture medium.When temperature is raised to
95 DEG C or more can stop stirring.The sterilizing of air filter and air pipeline, slightly opened filter and drain valve are carried out again, thus
Guarantee air pipeline sterilizing.Final discharge port, sampling valve, steam valve and outlet valve are slightly opened, and guarantee that the pipeline sterilizes.
Fermented and cultured and result: the Escherichia coli for producing L- lysine (are bought from CGMCC, strain by 10% inoculum concentration
Deposit number is CGMCC1.0281) (1L fermentation medium contains: glucose 20 ~ 40 g/L, (NH in reactor4)2SO4 1.5~
1.8 g, KH2PO41.2 g, 1 ~ 2 g of corn pulp, g), starting ventilatory capacity is 0.6 m to L- threonine 0.2 ~ 0.43/ h ventilation
Amount, then gradually promotes ventilatory capacity according to dissolved oxygen, 35 ~ 37 DEG C of fermentation temperature, Feeding ammonia water is to control pH 6.5 ~ 6.8, often
Detect remaining sugar concentration every 2 ~ 4 h, cocurrent adds the glucose of 500 g/L, maintain remaining sugar concentration 4 before 3-5 g/L, fermentation ends ~
5 h stop stream sugaring liquid, when residual sugar is down to 5 ~ 7g/L, i.e. fermentation ends, and about 50 h of entire fermentation period.Fermentation process
In, gas is escaped from membrane tube nanoscale aperture, is passed through in atmosphere from outlet valve after gas membrane tube distributor.It is fermenting
Peak period improves air inflow to maximum, and the solubility of oxygen is enabled to reach 3-4ppm, but should be noted that because of fermentation
Tank pressure is manually controlled in the process, so outlet valve must be adjusted simultaneously when adjusting air mass flow, so that tank pressure is constant
Greater than 0.03 Mpa.
Comparison does not have membrane tube aeration structure, the bioreactor of cyclic annular aeration stirring formula, 0.5 m of reactor size3, hair
Ferment mode is consistent with culture medium with the present embodiment.As follows by fermentation results: reactor of the invention uses micropore ceramics membrane tube
Being aerated obtained dissolved oxygen is 4.0 ppm, and saccharic acid conversion ratio is 68%, and the dissolved oxygen data for comparing conventional reactor are 3.5ppm, carbonic acid
Conversion ratio 53%.From the above data, it can be seen that the reactor of the invention using membrane tube aeration, which raises oxytys, mention
High reactor totality mass tranfer coefficient.Energy consumption needed for reducing stirring, the saccharic acid conversion ratio of enhancing lysine production.
Claims (7)
1. a kind of airlift bioreactor of membrane tube gas distribution, it is characterised in that including tank body, the top of the tank body is equipped with liquid
Body entrance, gas access, gas vent, tank base are equipped with liquid outlet, when the bioreactor is outer circulation mode hair
It further include gas distributor and U-tube guide tube when ferment, the upper end of the gas distributor is flexibly connected with tank body, the tank body
Lateral opening hole connect with U-tube guide tube, the other end of the U-tube guide tube and the lower end of gas distributor connect to form circulation
Pipeline；The gas distributor includes gas distribution membrane tube and membrane tube fixed frame, and the gas distribution membrane tube is fixed on the interior of membrane tube fixed frame
Portion；The intracorporal upper cavity of tank is flow field body rising area, and flow field rises flowing, the lower cavity in the guide tube wherein
For flow field descending area, flow field until the bottom of gas distributor, and is again introduced into gas distributor by guide tube flow down,
Form circulation flow field；It further include gas distributor and guide tube, the gas when the bioreactor is that interior circulation pattern ferments
After the upper end of body distributor is flexibly connected with guide tube, it is movably connected on the center of tank interior, the cavity in the guide tube
Region is flow field rising area, and the outer cavity between tank body tank body of guide tube is that flow field descending area, gas and liquid pass through in guide tube
Portion rises, then forms circulation flow field in the bottom of gas distributor from guide tube outer loop.
2. the airlift bioreactor of membrane tube gas distribution according to claim 1, which is characterized in that the gas-liquid rising area
Diameter ratio with gas-liquid descending area is 1-10:1-10.
3. the airlift bioreactor of membrane tube gas distribution according to claim 1, which is characterized in that the gas distribution membrane tube is
Micropore membrane tube, the micropore membrane tube be ceramic-film tube, metal film pipe, glass membrane tube, polyethylene membrane tube, polytetrafluoroethylene (PTFE) membrane tube,
Ps hollow fiber uf membrane pipe or dimethyl acetamide hollow fiber membrane tube.
4. the airlift bioreactor of membrane tube gas distribution according to claim 5, which is characterized in that the micropore membrane tube
10 nm-100000 nm of micro-pore diameter, the shape of micropore are circular hole, square hole or polygonal hole, and the number of micropore is 1-50；
The length of membrane tube is 20 mm-10000 mm, and the diameter of membrane tube is 0.1 mm-100 mm.
5. the airlift bioreactor of membrane tube gas distribution according to claim 1, which is characterized in that the bioreactor
Shape be round, quadrangle or polygon.
6. the airlift bioreactor of membrane tube gas distribution according to claim 1, which is characterized in that the membrane tube gas point
Membrane tube quantity is 1-5000 root in cloth device, and the arrangement mode of the membrane tube is vertical or horizontal.
7. the airlift bioreactor based on membrane tube gas distribution described in claim 1 microbial fermentation, animal cell culture,
Application in algae culture, fixed one-carbon compound or gas-liquid chemical reaction.
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| CN201910225398.1A CN109735452A (en) | 2019-03-25 | 2019-03-25 | Airlift bioreactor for membrane tube gas distribution and application thereof |
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| CN201910225398.1A CN109735452A (en) | 2019-03-25 | 2019-03-25 | Airlift bioreactor for membrane tube gas distribution and application thereof |
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Application publication date: 20190510 |