CN102732416A - Airlift type loop reactor and method for penicillin fermentation by using the same - Google Patents
Airlift type loop reactor and method for penicillin fermentation by using the same Download PDFInfo
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- 238000000855 fermentation Methods 0.000 title claims abstract description 80
- 230000004151 fermentation Effects 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 36
- 229930182555 Penicillin Natural products 0.000 title claims abstract description 28
- JGSARLDLIJGVTE-MBNYWOFBSA-N Penicillin G Chemical compound N([C@H]1[C@H]2SC([C@@H](N2C1=O)C(O)=O)(C)C)C(=O)CC1=CC=CC=C1 JGSARLDLIJGVTE-MBNYWOFBSA-N 0.000 title claims abstract description 28
- 229940049954 penicillin Drugs 0.000 title claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 238000009423 ventilation Methods 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 8
- 230000008569 process Effects 0.000 claims description 24
- 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 claims description 13
- 239000002253 acid Substances 0.000 claims description 13
- 239000008103 glucose Substances 0.000 claims description 13
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical group N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 12
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 12
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 239000002243 precursor Substances 0.000 claims description 6
- 125000002791 glucosyl group Chemical group C1([C@H](O)[C@@H](O)[C@H](O)[C@H](O1)CO)* 0.000 claims description 4
- 239000002054 inoculum Substances 0.000 claims description 4
- 238000011218 seed culture Methods 0.000 claims description 4
- 230000001580 bacterial effect Effects 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 241000228150 Penicillium chrysogenum Species 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 18
- 241000228143 Penicillium Species 0.000 description 10
- 238000013461 design Methods 0.000 description 7
- 238000010008 shearing Methods 0.000 description 7
- 238000013019 agitation Methods 0.000 description 6
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000001914 filtration Methods 0.000 description 4
- 238000000386 microscopy Methods 0.000 description 4
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000013467 fragmentation Methods 0.000 description 2
- 238000006062 fragmentation reaction Methods 0.000 description 2
- 238000010907 mechanical stirring Methods 0.000 description 2
- 230000004060 metabolic process Effects 0.000 description 2
- 238000011169 microbiological contamination Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000003828 vacuum filtration Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- FRXSZNDVFUDTIR-UHFFFAOYSA-N 6-methoxy-1,2,3,4-tetrahydroquinoline Chemical compound N1CCCC2=CC(OC)=CC=C21 FRXSZNDVFUDTIR-UHFFFAOYSA-N 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- 241001052560 Thallis Species 0.000 description 1
- 238000010564 aerobic fermentation Methods 0.000 description 1
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 1
- 238000010364 biochemical engineering Methods 0.000 description 1
- 230000003570 biosynthesizing effect Effects 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000000050 nutritive effect Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000024053 secondary metabolic process Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000000967 suction filtration Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
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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
- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/18—Flow directing inserts
- C12M27/24—Draft tube
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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
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
- C12M29/08—Air lift
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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
- C12M45/00—Means for pre-treatment of biological substances
- C12M45/04—Phase separators; Separation of non fermentable material; Fractionation
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Abstract
The present invention discloses an airlift type loop reactor and a method for penicillin fermentation by using the airlift type loop reactor. The lower part of the tower body of the airlift type loop reactor is the reaction section, and the upper part is the expanded gas-liquid separation section, wherein a height ratio of the gas-liquid separation section to the reaction section is 0.15-0.25, a diameter ratio is 1.25-1.42, a ratio of the total height of the tower body to the inner diameter of the reaction section is 4.5-8, a ratio of the inner diameter of a draft tube to the inner diameter of the tower body is 0.5-0.78, and a height ratio of the draft tube to the reaction section is 0.9-0.65. In the airlift type loop reactor, air is introduced, and a strain producing penicillium chrysogenum is adopted to produce penicillin, wherein the fermentation temperature is 20-30 DEG C, the pH value is 6.0-7.0, the fermentation pressure is 0.08-0.1 MPa, the ventilation ratio is controlled to 0.8-3 vvm, and the fermentation time is 160-170 hours.
Description
Technical field
The present invention relates to a kind ofly be used for the reactor drum of penicillin fermentation and utilize this reactor drum to carry out the method for penicillin fermentation, particularly relate to a kind of Airlift circulating reactor and utilize Airlift circulating reactor to carry out the method for penicillin fermentation.
Background technology
The aerobic fermentation of the thread fungus system of HV non-Newtonian fluid, the typical case is like penicillin fermentation, and general the employing has churned mechanically pot type fermentation reactor; Produce under the condition of bubbling air, mechanical stirring makes being distributed in the tank body of even air, with the needs of the growth metabolism that guarantees thalline; But there are two important problem in this method: on the one hand, the energy consumption of agitator motor and compressed-air actuated energy consumption make the energy consumption of fermenting process generally higher, and general power consumption accounts for the 30-50% of cost; In penicillin fermentation is produced; Adopt the mechanical agitation type fermentor tank to ferment, power consumption average out to 20～25Kwh/BOU (BOU penicillium mould activity unit, down together); On the other hand, churned mechanically shearing force constitutes influence to the silk thalli growth equally.Penicillin fermentation belongs to second order fermentation, is divided into the penicillium spp growth and breeding and produces anti-two stages; In first stage of fermentation of penicillium mould, mechanical shearing is favourable, and it can promote mycelial vegetative propagation; But produce the anti-stage in the later stage, mechanical shearing has quickened mycelial self-dissolving, and then influences the penicillium mould biosynthesizing, and is unfavorable for the processing of downstream production process.In addition, there is shortcomings such as being prone to microbiological contamination, maintenance cost height in mechanical stir-reactor.
The exploitation of non-stirring-type fermentation reactor is the developing direction of fermentation reactor always, and Airlift circulating reactor is the fermentation reactor that wherein is hopeful most to replace stirred reactor.Airlift circulating reactor utilizes the inside and outside gas-liquid density difference of reactor drum inner draft tube to be impellent, and produces the guide shell circulation that centers on, and is one type of efficient solution-air; Gas-liquid-solid or solution-air-liquid heterophase reactor; It is simple in structure, and mass-transfer performance is good, and energy consumption is lower; Be easy to engineering and amplify, in chemical industry, petroleum industry, environmental engineering, biochemical engineering and other commercial run, have a wide range of applications.
At present, both at home and abroad be applied to low-viscosity newton or intend the research that the fermenting process of Newtonian fuid is widely used at Airlift circulating reactor, typical in citric acid fermentation; 100m
3And 250m
3Adopt the gas lift cyclic part to substitute the semi-air-lift formula fermentor tank application in the citric acid fermentation process of stirring, can make total power consumption practice thrift 30～40%.In gas lift type common loop reactor, directly cultivate the Penicllium chrysogenum bacterial strain and ferment correlation technique then do not appear in the newspapers.
The major cause that Airlift circulating reactor is difficult to be applied to penicillin fermentation is:
(1) because the circulation impellent of Airlift circulating reactor (density difference of the inside and outside gas-liquid of guide shell) is less, often do not reach the needs to dissolved oxygen of fermenting process; Perhaps need excessive gas speed to keep circulation, make the economy decline of process and make reactor drum be difficult to operation.
(2) hydrodynamic shear of Airlift circulating reactor is little, and in the elementary metabolism stage, under the situation of competent gas and nutritive substance supply, if extraneous shearing force is little, penicillium spp is prone to clump together, and is unfavorable at the product in secondary metabolism stage anti-at penicillium spp.
Summary of the invention
First purpose of the present invention is exploitation and proposes a kind of gas lift type common loop reactor that is used for penicillin fermentation.
Second purpose of the present invention is to provide a kind of method of utilizing gas lift type common loop reactor to carry out penicillin fermentation, to reduce the energy consumption of process, improves fermentation efficiency.
First purpose of the present invention is implemented by following technical scheme, a kind of gas lift type common loop reactor that is used for penicillin fermentation, it comprise tower body, with the coaxial mounted guide shell of tower body, gas distributor; Wherein guide shell is a single hop or multistage, it is characterized in that, the tower body bottom of said Airlift circulating reactor is a conversion zone; The gas-liquid separation section of top for enlarging; The aspect ratio of gas-liquid separation section and conversion zone is 0.15～0.25, and the diameter ratio is 1.25～1.42, and the tower body height overall is 4.5～8 with the ratio of conversion zone internal diameter; Guide shell internal diameter and conversion zone internal diameter ratio are 0.5～0.78, and guide shell height and conversion zone aspect ratio are 0.9～0.65.
The bottom of going up of said guide shell is the jagged edges that is made up of vee, the degree of depth 10～20mm of each breach, width 10～20mm, distance 5～15mm between breach.
The design of air-distributor guarantees that air edge and axial angle are 30 °～60 ° conical surface ejection, and egress line speed is not less than 2m/s.
Second purpose of the present invention is to provide a kind of method of utilizing Airlift circulating reactor to carry out penicillin fermentation, after Penicllium chrysogenum bacterial strain seed culture is accomplished, begins fermentation in the inoculum size access Airlift circulating reactor according to 8～10% (v/v).Leavening temperature is 20～30 ℃; PH is 6.0～7.0; The ventilation of fermentation whole process is than being controlled at 0.8～3vvm, and through regulating the ventilation ratio, the control dissolved oxygen is more than 30%; Fermentation pressure is 0.08～0.1Mpa; Fermentation period is 160～170h; Whole fermentation process control fermented liquid mycelial concentration is 35～45%.
Fermenting process need be added carbon source, nitrogenous source and precursor, and it is glucose that stream adds carbon source, and glucose concn is controlled at 70～85% (v/v), and glucose stream dosage is 1～2L/h; It is ammonium sulfate that stream adds nitrogenous source, and the concentration of ammonium sulfate is controlled at 30～40% (v/v), and the ammonium sulfate stream dosage is 0.1～0.2L/h; It is toluylic acid that stream adds precursor substance, and toluylic acid concentration is controlled at 30～40% (v/v), and toluylic acid stream dosage is 0.1～0.2L/h.
The present invention realizes above-mentioned target from the angle of optimizing structure of reactor, adjustment and optimization for fermentation technology parameter, the invention has the advantages that
(1) gas-liquid separation section diameter can spread greater than other gases that make to producing in reactant gases and the fermenting process that relate to of conversion zone diameter rapidly; Guarantee the good operation of reaction; The design of guide shell breach and gas distributor and help increasing a certain amount of shearing force overcomes problems such as penicillium spp is prone to clump together.
(3) utilize the Airlift multi-stage loop reactor drum to carry out penicillin fermentation, fermentation efficiency is higher than the fermentation of mechanical agitation type fermentor tank, and fermentation period can be from shortening about 20%, and fermentation unit can improve more than 10%;
(4) with respect to the mechanical type fermentor tank, fermenting process is little to mycelial shearing force, and the ratio of mycelium self-dissolving is little, can not cause difficulty for the processing of postorder;
(5) the power consumption average out to 20～25Kwh/BOU of mechanical agitating fermentation tank utilizes loop reactor to carry out the penicillium spp fermentation, and power consumption average out to 10～21Kwh/BOU in the fermenting process only is equivalent to 50% of tool stirred fermentor power consumption loss.
(6) because there are not utility appliance such as shaft coupling and the bearing of mechanical agitation type fermentor tank in the Airlift multi-stage loop reactor drum, greatly reduce the microbiological contamination rate.
The accompanying drawing summary description
Accompanying drawing 1 has shown Airlift circulating reactor of the present invention
Accompanying drawing 2 has shown the breach design of guide shell in the Airlift circulating reactor
Accompanying drawing 3 has shown a kind of design of gas distributor in the Airlift circulating reactor
Accompanying drawing 4 has shown the concrete design that is used to flow the Airlift circulating reactor that adds fermentation
Embodiment
Airlift circulating reactor
Explanation for each parts among the accompanying drawing 1-4 is following:
The 1-conversion zone, 2-gas-liquid separation section, 3-reactor head, 4-reactor drum bottom (head), 5-heat exchange jacket, 6-guide shell; The perforate of 7-guide shell, 8-opening for feed, 9-recirculated water inlet, 10-circulating water outlet, 11-visor liquidometer; Locating support on the 2-guide shell, 13-gas distributor, 14-guide shell lower bracket, 15-inlet pipe, 16-discharge gate; 17-stream adds mouth, and 18-stream adds a mouthful steam protection, 19-venting port, 20-SV, the design of 21-breach
The present invention has made concrete improvement to the design between each parts of Airlift circulating reactor, and is consistent with general Airlift circulating reactor for the concrete operation of retort.
Embodiment 2
A kind of 200L of utilization Airlift circulating reactor carries out the method for penicillin fermentation, after seed culture is accomplished, begins fermentation in the inoculum size access gas lift type common loop reactor according to 8～10% (v/v).Leavening temperature is 26 ℃; PH is 6.5 ± 0.1; The fermenting process ventilation is than 2.8vvm, and the control dissolved oxygen is more than 30%; Fermentation pressure is 0.1Mpa; Fermentation period is 165h; Whole fermentation process control fermented liquid mycelial concentration is about 40%.
Utilize the 200L Airlift circulating reactor to carry out in the penicillin fermentation process, adding carbon source is glucose, and glucose concn is 83% (w/v), and operation process glucose additional amount is 1.8L/h; Adding nitrogenous source is ammonium sulfate, and the concentration of ammonium sulfate is 37% (w/v), and operation process ammonium sulfate additional amount is 0.19L/h; Adding precursor substance is toluylic acid, and toluylic acid concentration is 36% (w/v), and operation process toluylic acid additional amount is 0.19L/h.Fermentation is put tank volume 152L after stopping; Microscopy mycelia complete form, self-dissolving is less; Fermented liquid is through vacuum filtration, and filtering velocity is 1.70mL/s, and obtaining penicillin fermentation unit is 106880u/mL.
Utilize 200L mechanical agitation type fermentor tank to compare experiment.After seed culture is accomplished, begin fermentation in the inoculum size access stirred-tank fermenter according to 8～10% (v/v).Leavening temperature is 25 ℃; PH is 6.4 ± 0.1; Mixing speed 380r/min; The fermenting process ventilation is than 1.3vvm, and the control dissolved oxygen is more than 30%; Fermentation pressure is 0.08Mpa; Fermentation period is 192h; Whole fermentation process control fermented liquid mycelial concentration is about 40%.Utilize 200L mechanical agitation type fermentor tank to carry out in the penicillin fermentation process, adding carbon source is glucose, and glucose concn is 83% (w/v), and operation process glucose additional amount is 1.7L/h; Adding nitrogenous source is ammonium sulfate, and the concentration of ammonium sulfate is 36% (w/v), and operation process ammonium sulfate additional amount is 0.21L/h; Adding precursor substance is toluylic acid, and toluylic acid concentration is 36% (w/v), and operation process toluylic acid additional amount is 0.20L/h.Fermentation is put tank volume 155L after stopping; The most mycelia fractures of microscopy, fragmentation, self-dissolving is more, and fermented liquid is through vacuum filtration, and filtering velocity is 1.32mL/s, and obtaining penicillin fermentation unit is 98643u/mL.
According to embodiment 2 embodiments, to 10 batches of Airlift circulating reactor continuous operation.After fermentation stopped, microscopy mycelia form was intact; Average filtration speed 1.73mL/s; The average fermentation cycle is 163h; Obtaining penicillium mould average fermentation unit is 106320u/mL.
Through above embodiment contrast, utilize gas lift type common loop reactor to carry out penicillin fermentation, fermentation period can shorten 15%; Fermentation unit can improve about 10%; Fermentation equipment is little to mycelial shearing force, and mycelial self-dissolving ratio is little; Fermented liquid suction filtration speed has improved more than 40%; Saved mechanical stirring, the power cost in the fermenting process significantly reduces.
Be the better penicillin fermentation effect that obtains, the parameter sectional of fermenting process of the present invention is controlled: after ferment-seeded is cultivated mycelial concentration to 20～40% (v/v), change Airlift circulating reactor over to and begin fermentation, fermentating liquid volume 168L.Leavening temperature is 25 ℃, and pressure is 0.08Mpa.Whole fermentation period 170h, preceding 0～60h air flow 8.5m
3/ h (the mark condition is equivalent to empty tower gas velocity 4cm/s), ventilation is than being 0.84vvm; Back 60～90h air flow 13m
3/ h (the mark condition is equivalent to empty tower gas velocity 6cm/s), ventilation is than being 1.29vvm; Behind the 90h, air flow is controlled at 20m
3/ h, (the mark condition is equivalent to empty tower gas velocity 9.5cm/s), ventilation is than being 1.98vvm.Supplementary carbon source is a glucose, and sugared concentration is at 82% (w/v), and stream dosage 0～60h is at 1L/h; 60～100h, the stream dosage is at 1.5L/h; Behind the 100h, the stream dosage is at 1.8L/h; The sulphur ammonium concentration is at 35% (w/v), and 0～60h flows dosage at 0.11L/h; 60～100h, the stream dosage is at 0.14L/h; Behind the 100h, the stream dosage is at 0.17L/h; Toluylic acid concentration is at 38% (w/v), and at 0～60h, the stream dosage is at 0.10L/h; 60～100h, the stream dosage is at 0.14L/h; Behind the 100h, the stream dosage is at 0.19L/h; The highest mycelial concentration 40% in the fermenting process, dissolved oxygen concentration maintains more than 35%.During fermentation ends, obtaining penicillin fermentation unit is 100943u/ml.
Claims (5)
1. Airlift circulating reactor that is used for penicillin fermentation, it comprise tower body, with the coaxial mounted guide shell of tower body, air-distributor, wherein guide shell is a single hop or multistage; It is characterized in that; The tower body bottom of said Airlift circulating reactor is a conversion zone, the gas-liquid separation section of top for enlarging, and the aspect ratio of gas-liquid separation section and conversion zone is 0.15～0.25; The diameter ratio is 1.25～1.42; The tower body height overall is 4.5～8 with the ratio of conversion zone internal diameter, and guide shell internal diameter and conversion zone internal diameter ratio are 0.5～0.78, and guide shell height and conversion zone aspect ratio are 0.9～0.65.
2. a kind of Airlift circulating reactor that is used for penicillin fermentation according to claim 1; It is characterized in that the bottom of going up of said guide shell is the jagged edges that is made up of vee, the degree of depth 10～20mm of each breach; Width 10～20mm, distance 5～15mm between breach.
3. Airlift circulating reactor according to claim 1 and 2, wherein air-distributor guarantees that air edge and axial angle are 30 °～60 ° conical surface ejection, and egress line speed is not less than 2m/s.
4. an Airlift circulating reactor that utilizes claim 1-3 carries out the method for penicillin fermentation; It is characterized in that; After Penicllium chrysogenum bacterial strain seed culture is accomplished, begin fermentation in the inoculum size access Airlift circulating reactor according to 8～10% (v/v), leavening temperature is 20～30 ℃; PH is 6.0～7.0; The ventilation of fermentation whole process is than being controlled at 0.8～3vvm, and through regulating the ventilation ratio, the control dissolved oxygen is more than 30%; Fermentation pressure is 0.08～0.1Mpa; Fermentation period is 160～170h; Whole fermentation process control fermented liquid mycelial concentration is 35～45%.
5. the method for penicillin fermentation according to claim 4 is characterized in that, fermenting process need be added carbon source, nitrogenous source and precursor, and it is glucose that stream adds carbon source, and glucose concn is controlled at 70～85% (w/v), and glucose stream dosage is 1～2L/h; It is ammonium sulfate that stream adds nitrogenous source, and the concentration of ammonium sulfate is controlled at 30～40% (w/v), and the ammonium sulfate stream dosage is 0.1～0.2L/h; It is toluylic acid that stream adds precursor, and toluylic acid concentration is controlled at 30～40% (w/v), and toluylic acid stream dosage is 0.1～0.2L/h.
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| WO2015091455A1 (en) * | 2013-12-17 | 2015-06-25 | Dpx Holdings B.V. | Bioreactor |
| WO2017068265A1 (en) * | 2015-10-23 | 2017-04-27 | Gg Coriolis | Liquid-medium digester with gas-flow-based agitation, comprising an automatic device for establishing a fluid communication between the upflow and downflow spaces according to the height of the medium |
| CN106916727A (en) * | 2017-03-31 | 2017-07-04 | 江南大学 | Assemble the airlift reactor of baffling sieve plate |
| EP3766982A1 (en) * | 2019-07-18 | 2021-01-20 | Delft Advanced Biofuels B.V. | Integrated system for biocatalytically producing and recovering an organic substance |
| CN117757595A (en) * | 2023-12-20 | 2024-03-26 | 中国科学院天津工业生物技术研究所 | Gas-lift type bioreactor for strengthening liquid flow circulation |
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|---|---|---|---|---|
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| WO2017068265A1 (en) * | 2015-10-23 | 2017-04-27 | Gg Coriolis | Liquid-medium digester with gas-flow-based agitation, comprising an automatic device for establishing a fluid communication between the upflow and downflow spaces according to the height of the medium |
| FR3042795A1 (en) * | 2015-10-23 | 2017-04-28 | Gg Coriolis | CLOSER FOR LIQUID ENVIRONMENT WITH AUTOMATIC FLUID COMMUNICATION BETWEEN ASCENDING AND DESCENDING CIRCULATIONS IN RELATION TO THE LEVEL OF THE LIQUID ENVIRONMENT |
| CN108138107A (en) * | 2015-10-23 | 2018-06-08 | Gg科里奥利思公司 | Including establishing the fermentor for rising cycle volume and declining the automatic device of the fluid communication between cycle volume, the fluid nutrient medium stirred using gas circulation according to the height of fluid nutrient medium |
| US10975347B2 (en) | 2015-10-23 | 2021-04-13 | Biorea | Fermenter for a liquid medium with gas circulation stirring, comprising an automatic device for establishing a fluid communication between the ascending circulation and the descending circulation volumes depending on the height of the medium |
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| EP3766982A1 (en) * | 2019-07-18 | 2021-01-20 | Delft Advanced Biofuels B.V. | Integrated system for biocatalytically producing and recovering an organic substance |
| WO2021010822A1 (en) * | 2019-07-18 | 2021-01-21 | Delft Advanced Biofuels B.V. | Integrated system for biocatalytically producing and recovering an organic substance |
| CN114502738A (en) * | 2019-07-18 | 2022-05-13 | 代尔夫特先进生物燃料有限公司 | Integrated system for biocatalytic production and recovery of organic matter |
| AU2020315676B2 (en) * | 2019-07-18 | 2023-09-21 | Delft Advanced Biofuels B.V. | Integrated system for biocatalytically producing and recovering an organic substance |
| CN117757595A (en) * | 2023-12-20 | 2024-03-26 | 中国科学院天津工业生物技术研究所 | Gas-lift type bioreactor for strengthening liquid flow circulation |
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