CN101538532B - External loop air lift type membrane bioreactor - Google Patents

External loop air lift type membrane bioreactor Download PDF

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Publication number
CN101538532B
CN101538532B CN 200910026442 CN200910026442A CN101538532B CN 101538532 B CN101538532 B CN 101538532B CN 200910026442 CN200910026442 CN 200910026442 CN 200910026442 A CN200910026442 A CN 200910026442A CN 101538532 B CN101538532 B CN 101538532B
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gas
air
reaction kettle
main body
liquid
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CN101538532A (en
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邢卫红
景文珩
李国玲
张峰
申屠佩兰
徐南平
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Nanjing Tech University
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Nanjing Tech University
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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
    • C12M33/00—Means for introduction, transport, positioning, extraction, harvesting, peeling or sampling of biological material in or from the apparatus
    • C12M33/14—Means for introduction, transport, positioning, extraction, harvesting, peeling or sampling of biological material in or from the apparatus with filters, sieves or membranes
    • 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
    • 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
    • C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate

Abstract

The invention relates to a novel air lift type membrane bioreactor, in particular to an external loop air lift type membrane bioreactor which comprises a reaction kettle body 10, a circulating pipe 15and air lifting pipe 2. The external loop air lift type membrane bioreactor is characterized in that a return nozzle of the air lifting pipe is positioned under the liquid level and is connected with a return pipe 8 extending into the reaction kettle body 10; an air distributor 9 replaces the air lifting return pipe 8 to be used for distributing confluent gas, and an inorganic membrane module 10 is packaged in the air lifting pipe 2 to be used as a liquid/solid separator. The invention has simple structure, flexible operation and lower energy consumption, is easy to realize the industrial expansion, and has huge prospect especially in the biochemical reaction.

Description

A kind of external loop air lift type membrane bioreactor
Technical field
The present invention relates to a kind of external loop air lift type membrane bioreactor, is to develop according to the unit coupling and the thought of process intensification.Gas collection rises that circulating reaction, gas are carried, the biphase gas and liquid flow membrane sepn is in the external loop air lift type membrane bioreactor of one, Gu be used to relate to gas/liquid, gas/liquid/etc. contain heterogeneous reaction, the especially biological fermentation process of gas-liquid two-phase.
Technical background
In biochemical reaction process, often exist product inhibition.Fermentative Production ethanol, butanols are exactly typical example.Want to improve raw material availability, reaction efficiency, just must constantly remove reaction product.
Membrane separation technique has obtained swift and violent development as a kind of novel stripping technique efficiently of generally acknowledging in recent years, is widely applied to industries such as chemical industry, food, biology, medicine.The membrane bioreactor that ultrafiltration, microfiltration process and fermenting process coupling are formed is used for improving fermentation efficiency and has also received extensive studies.In this process; Fermented liquid is through after the membrane filtration; Tunning is shifted out fermentor tank effectively, alleviate even eliminated the restraining effect of product, and remaining raffinate continues to turn back in the fermentor tank with the cell that is trapped; Thereby kept high cell concentration in the fermentor tank, realized a jar interior liquid level equilibrium simultaneously very easily.But in this process, feed liquid is separated on the film surface after pump delivery, and the pollution of film is very serious, and production concentration is the same in the product concentration of coming out through membrane sepn and the retort, and subsequent disposal is cumbersome; Simultaneously, because the existence of pump, this process energy consumption is higher, and the violent deteriorative reaction condition easily of fluidic turbulence, is unfavorable for the growth of thalline.In order to overcome these problems; ZL01108189.9 and ZL200520075139.9 have successively proposed to replace traditional supply of power person---pump with the power of pressurized gas as membrane bioreactor, but the former is connected reactor drum through common pipe with membrane module; Cause structure of reactor comparatively to disperse; The fluid recycle circuit is longer, thereby makes that the gas-liquid mass transfer effect is bad, the difficult demand that satisfies extensive reaction.The latter has proposed the outside circulation gas lift type membrane bioreactor on the former basis, in this reactor drum, and membrane module and reactor drum one integrated mass; The advantage that has well combined airlift reactor and membrane sepn; Overcome membrane sepn and the existing a series of problems of fermentation coupling preferably, in this reactor drum, membrane module both can be used for separating simultaneously; Can be used as radially aeration unit again, produce trickle bubble.But refluxing opening is positioned at reactor drum kettle upper extension section place in this reactor drum; Refluxing opening is positioned on the liquid level or to be positioned at the subsurface degree of depth very little; The refluxing opening place does not have thrust-augmenting nozzle simultaneously, and a large amount of pressurized gass are directly leaning on the effusion of wall place to drain after the loop ends on the liquid level or under liquid level, and pressurized gas has only played the effect of circulation power; Can not rationally be utilized, caused power loss.
It is a physical process that gas is carried, and it adopts a kind of gaseous media to break former gas-liquid biphase equilibrium and sets up a kind of new vapor liquid equilibrium state, and a certain component in the solution is desorbed owing to dividing potential drop reduces, thereby reaches the purpose of separate substance.Receive social broad research because the gas formulation has advantages such as simple economy, pollution-free, products obtained therefrom purity height, especially among biological respinse, carry and the legal system ethanol that ferments, butanols coupling like gas.In these coupling process, the most typically be airlift reactor.Gu this reactor drum is the chemical reactor that is used for gas/liquid two phases or gas/liquid/three-phase process that on the basis of bubbling style reactor, grows up; It provides energy through expansion of compressed gas; Dependence contains the lift that the density difference of bubble liquid and neat liquid causes makes fluid circulate along pipeline, belongs to the strength stirred reactor.Advantages such as at present, airlift reactor is simple in structure because of having, shearing force is low, reaction conditions is gentle, air feed efficient high, effectively contact area is big, fluid effect is good receive broad research.But among this process, still exist some shortcomings: as in fermentation system alcoholic acid process, except generating ethanol and CO 2Also can produce succsinic acid, acetaldehyde, formic acid, acetate, lactic acid, glycerine, fusel wet goods by product outward.These by products all can produce restraining effect to fermentation.When acetic acid content reached 0.13% in the fermented liquid, yeast just was difficult to growth.In these by products, except acetaldehyde, formic acid had preferably volatility, acetate, lactic acid, glycerine, fusel wet goods were not volatile, were difficult to remove with the method that gas is carried; Ethanol, CO 2, formic acid, acetaldehyde etc. may put forward effect because of gas and accumulate this inadequately and also can suppress the carrying out of fermenting; In order to keep a jar interior liquid level equilibrium, need constantly drain a part of feed liquid in addition, this has caused a large amount of loss cells again, and some static layering of reporting in the document make the method for cell cycle make the fermenting process microbiological contamination easily.
By on can know; Gas is carried with membrane sepn and in biochemical reaction, is all existed unique advantage, all has bigger application prospect, but exists the shortcoming that can remedy mutually; Therefore; Develop and a kind ofly can make full use of the various energy, membrane sepn and gas are carried the novel reactor that combines, be of great practical significance.
Summary of the invention
The objective of the invention is: for solve membrane sepn, gas is carried and ferment etc. reacted the existing the problems referred to above of coupling; Advantage of carrying according to membrane sepn and gas and the characteristic that remedies shortcoming mutually that they had; And provide a kind of membrane bioreactor and airlift reactor are coupled together; Combine thereby membrane sepn and gas carried, and remedy both insufficient external loop air lift type membrane bioreactors mutually.This reactor drum is introduced membrane module on the basis that does not change airlift reactor substruction; In the advantage that possesses airlift reactor, membrane bioreactor, had the function that gas is put forward again, overcome membrane sepn preferably, gas is carried and the coupled deficiency of fermenting.
Technical scheme of the present invention is: a kind of external loop air lift type membrane reactor drum, form by reaction kettle main body 10, circulation tube 15, air-lift tube 2; It is characterized in that the air-lift tube refluxing opening is positioned at below the liquid level, and be connected with the return line 8 that stretches to reactor drum kettle 10 inside; Gas distributor 9 replaces air lift and return pipe 8 and is used for distribution meeting gas body; Inorganic membrane assembly 3 is encapsulated in the air-lift tube 2, as liquid/solid separator.
Wherein said air-lift tube refluxing opening is positioned under the liquid level, and the refluxing opening upper liquid degree of depth is 2～8 with the ratio of the refluxing opening lower liquid degree of depth; Return line length is 1/3～2/3 of reaction kettle main body 10 internal diameters; Gas distributor 9 is outer end sealing tubular type gas distributor, and length is 1/3～1 of return line.
Above-mentioned mineral membrane element 3 is tubular type ultrafiltration or micro-filtration mineral membrane.So just can avoid the high-temperature sterilization in the biochemical reaction to give the destruction that organic membrane caused; Admittedly mineral membrane is carrying out liquid/carry out positive press filtration when separating, transmembrane pressure is 0.01～1MPa or negative pressure-pumping, and transmembrane pressure is 0.01～0.1MPa, operates more flexible.
Reaction kettle main body 10 of the present invention contains contraction section and amplifying sections.Contraction section is positioned at the lower end of reaction kettle main body.In application process, liquid level can not arrive amplifying sections.Reaction kettle main body 10 upper ends are equipped with tensimeter; And having opening for feed 14 and venting port 12, kettle has form 11, and TM, pH meter, oxygen measuring instrument are installed; So that in time the feed liquid situation in the observing response device has discharge opening 16 on the circulation tube bottom; Venting port 12 places are equipped with valve 13, thereby through regulating the pressure in the free air delivery conditioned reaction still main body 10; Valve 13 connects condensation of gas pipeline E, is connected with condensation of gas collection device E-1, vacuum pump E-2, carrier gas circulating line F in turn, through condensation of gas collection device E-1, obtains the purity high product thereby product obtains condensation; Gas among the carrier gas circulating line F recycles or discharges along pipeline (G) through T-valve F-1 through valve H-1, gas meter H-2, aeration head 1 entering air-lift tube 2 successively through pipeline H through T-valve F-1.
Characteristic of the present invention is that also the air-lift tube lower end is equipped with aeration head 1, and aeration head 1 links to each other with compressed gas source B, and compressed gas source B is nitrogen, ammonia, oxygen or the helium that the pressurized air that provides of air (B-1) or pressure gas cylinder (B-2) provide.
Characteristic of the present invention is that also pressurized gas just begins to play gas afterwards through aeration head (1) entering air-lift tube (2) and proposes effect; Effusion along with carrier gas; Volatile product finally makes the removal of volatile product to propose common control by membrane sepn and gas also along with the effusion reactor drum.
Beneficial effect:
1, adopt aeration head in reactor drum, to feed pressurized gas in the air-lift tube bottom with certain initial velocity; Under the drive of this initial velocity; Liquid upwards is flowing in the membrane module place with gas and carries out membrane sepn; Because the existence of bubble has improved the environment on film surface, helps to alleviate film and pollutes, and improves the strainability of membrane module; Under equal operational condition, membrane flux can improve 50%～200%.
2, pressurized gas has just played the effect that gas is proposed after getting into reactor drum; The gas distributor that in reactor body, is provided with carries out quadratic distribution to gas and produces trickle bubble; More help to make full use of resource, improve gas stripping efficiency; Carry through gas and can obtain the higher product of purity, product can be purified 4～10 times.
3, pressurized gas has played the effect of stirring in reactor drum, and produces bubble relatively uniformly, and the mass-and heat-transfer effect is better, helps the carrying out that react, and reaction effect can improve 10～100 times.
4, the mineral membrane element adopts positive pressure operation when separating, and perhaps carries out negative pressure-pumping; When carrying out positive press filtration, can turn place, the air outlet valve (13) of reaction kettle upper end down, thereby increase the still internal pressure, realize membrane sepn; When the still internal pressure is normal pressure or negative pressure, then open vacuum pump and carry out negative-pressure operation.
5, in the process of fermentation, can regulate the amount of shifting out that aeration rate and membrane flux are regulated product, thereby can adjust accordingly according to speed of reaction, operation has more handiness.
In a word, this external loop air lift type membrane bioreactor gas collection rises reaction, membrane sepn, gas and carries in one, and the required energy of whole process is all provided by pressurized gas, has advantages such as energy consumption is low, simple in structure, flexible operation, reaction conditions gentleness.
Description of drawings
Fig. 1 is an outer circulation air lift type membrane bioreactor synoptic diagram.
Fig. 2 is an outer circulation air lift type membrane bioreactor process flow diagram.
A is the feed liquid main flow among the figure, and B is a compressed gas source, and C is recoil or micro-pore aeration compressed gas source, and D is that filtration product is collected main flow, and E is that gas is put forward the product main flow; 1 is aeration head, and 2 is air-lift tube, and 3 is the mineral membrane element, and 4 are recoil or micro-pore aeration inlet mouth; 5 are recoil or micro-pore aeration air intake control valve, and 6 are the filtered liq outlet, and 7 is the filtered liq valve, and 8 is the air-lift tube return line; 9 is gas distributor, and 10 is the reactor drum kettle, and 11 is visor, and 12 is venting port; 13 is the venting port valve, and 14 is opening for feed, and 15 is discharge opening; B-1 is an air compressor, and B-2 is a steel cylinder dress pressurized gas, and B-3 is a gas meter, and B-4 is the tolerance valve; D-1 is a filtrate tanks, and D-2 is a vacuum pump, and E-1 is the condensation and collection jar, and E-2 is a vacuum pump; F-1 is a T-valve, and H-1 is a gas meter, and H-2 is the tolerance valve.
Embodiment
Embodiment 1
Below in conjunction with accompanying drawing 1 explanation embodiment of the present invention
External loop air lift type membrane bioreactor provided by the present invention mainly is made up of reaction kettle main body 10, circulating line 15, air-lift tube 2, aeration head 1, the mineral membrane original paper 3 air lift and return pipes 8, the gas distributor 9 that are encapsulated in the air-lift tube, and is as shown in Figure 1.Reaction kettle main body 10 comprises contraction section and amplifying sections two portions, and required ratio was confirmed when two sections internal diameter compared by gas-liquid separation, was about 1.5～8; Reaction kettle main body 10 tops have opening for feed 14 and venting port 12, and exhaust ports is equipped with valve 13, thereby so that regulate free air delivery conditioned reaction still internal pressure, the reaction kettle top also is equipped with tensimeter, so that the pressure change of observing response still; Have form on the kettle and be used for the reacting phenomenon in the observing response still, and TM, pH meter, oxygen measuring instrument are installed are used to observe reaction conditions; Circulating line 15 lower ends have discharge opening 16; Aeration head 1 lower end links to each other with compressed gas source and by valve, under meter control survey flow; Return line and gas distributor carry out quadratic distribution with reflux gas, carry out gas and carry thereby make full use of pressurized gas, obtain the higher product of purity.
The operating method of external loop air lift type membrane bioreactor provided by the present invention is following: in reaction kettle, add feed liquid through pipeline A, to wherein blasting pressurized gas, gas gets into air-lift tube 2 through aeration head 1 through pipeline B.Owing to have the entering of the pressurized gas of certain initial velocity, between circulation tube 15 and air-lift tube 2, produce density difference, under the two effect, air-lift tube 2 inner fluids move upward, and open controlling diaphragm by valve 7 when arriving mineral membrane element 3 and separate.Liquid concentrator continues upwards to be circulated to the refluxing opening place, turns back to reaction kettle main body 10 through return line 8, and reflux gas is upwards overflowed after gas distributor 9 carries out quadratic distribution, in the process of overflowing, plays gas and proposes effect.Bring about the desired sensation and carry product and get rid of product is carried out in the back in pipeline E condensation and collection at venting port, obtain the higher product of purity.Uncooled carrier gas then recycles through aeration head 1 through circulating line H.
Embodiment 2
The system process of external loop air lift type membrane bioreactor provided by the present invention is as shown in Figure 2; Specific as follows: as in reaction kettle, to add feed liquid through pipeline A; Through pipeline B to wherein blasting pressurized gas; Pressurized gas is pressurized air B-1 or steel cylinder dress gas B-2; Pressurized gas is through getting into air-lift tube 2 through aeration head 1 after under meter B-3 and the valve B-4 control survey, and liquid carries out micro-filtration at arrival inorganic ceramic film separation unit 3 drive of the pressurized gas with initial velocity under and the promotion of density difference under, controls whether carry out membrane sepn by valve 7.When under the drive of reacting kettle inner pressure or vacuum pump D-2, carrying out membrane sepn, open valve 7, gained filtrating is collected in storage tank D-1.Liquid concentrator then continues circulation and arrives in the reaction kettle main body 10 through return line 8; The pipe range that wherein refluxes is 1/2 of reaction kettle main body 10 internal diameters, reflux gas then pass through gas distributor 9 (gas distributor 9 is single tube inorganic ceramic film support, length be return line length 3/4) form trickle bubble after the quadratic distribution and upwards overflow; Play gas simultaneously and propose effect; Gas is through venting port 12 effusion reaction kettle under the control of valve 13, through piping E, under the condensation of condensation of gas collection device E-1; Obtain the higher product of purity, vacuum pump E-1 then is used for controlling reacting kettle inner pressure.Uncooled carrier gas then continues perhaps to be discharged by T-valve F-1 Control Circulation along pipeline F, continues circulation time, and gas, is restored in the reaction kettle through aeration head 1 under the control survey of valve H-2 through under meter H-1.
In fermentative Production alcoholic acid process; To volume is to add the 3L substratum in 10 liters the external loop air lift type membrane biological fermentation tank (effective volume is 6.5 liters) under 120 ℃, to sterilize; Add 2g wine brewing active yeast after being cooled to 38 ℃, in fermentor tank, feed aseptic pressurized air through aeration head and carry out activation.Being 12g/L with 2L concentration after half hour adds fermentor tank through the glucose solution of high-temperature sterilization, under 31 ℃, ferments and continues in reaction kettle, to feed the pressurized air of purification.Under the drive of pressurized gas, under the promotion of fluid density difference, pot liquid arrives membrane element, opens vacuum pump, regulates transmembrane pressure, carries out negative pressure-pumping, makes membrane flux consistent with feed rate, with maintenance tank level balance.Under the drive of pressurized gas, the liquid concentrator that contains a large amount of cells returns the reaction kettle main body, makes jar contain higher cell concn.In jar gas after accomplishing a circulation with jar in volatile substances take out of, after venting port is discharged, collect, can obtain concentration is the ethanol extract of 5 times of feed concentrations.At the feed liquid alcohol concn is 10%, and when aeration rate was 11L/min, unit hour unit's effective volume alcoholic acid gas is put forward the amount of shifting out can reach 10g/ (L.h).When adopting mean pore size simultaneously is the membrane element of 50nm when carrying out membrane sepn, and under the same operation condition, transmembrane pressure is under the 0.03MPa, and the ethanol of unit time unit's effective volume shifts out speed can reach 17g/ (L.h).
This embodiment also can be used for the process that butylic fermentation, wastewater treatment etc. include volatile substances.
In the process of fermentative Production L-glutamic acid, in this external loop air lift type membrane biological respinse still, add the 6L substratum 120 ℃ of sterilizations 15 minutes down, be cooled to 34～35 ℃ after to wherein adding 0.7gS 9114Number bacterial classification, and open aeration head and ferment to wherein blasting sterile air.When glutamic in the feed liquid is 7%, begin in fermentor tank, to add concentration and be 35% glucose feed liquid, the venting port valve of conditioned reaction still main body upper end, when the jar internal pressure increased to required pressure, membrane module upper end valve carried out positive press filtration.Through this method, glutamic maintains about 8% in the fermentor tank, and the employing mean pore size is that the inorganic ceramic film of 200nm filters, and thalline is held back by 100%.
The pressure that this embodiment utilizes gas to produce provides membrane filtration power, can be used for that products such as Methionin, Streptomycin sulphate are difficult to the evaporable biological fermentation and some relate among the chemical reaction of gas/liquid/solid phase.

Claims (7)

1. an external loop air lift type membrane bioreactor is made up of reaction kettle main body (10), circulation tube (15), air-lift tube (2); It is characterized in that the air-lift tube refluxing opening is positioned at below the reaction kettle main body liquid level and is connected with stretches to the inner air lift and return pipe (8) of reaction kettle main body (10); Gas distributor (9) replaces air lift and return pipe (8) and is used to the reflux gas that distributes; Inorganic membrane assembly (3) is encapsulated in the air-lift tube (2), as liquid/solid separator; Wherein said return line length is 1/3～2/3 of reaction kettle main body (10) internal diameter; Gas distributor (9) is the tubular gas sparger of outer end sealing, and length is 1/3～1 of return line length.
2. reactor drum according to claim 1 is characterized in that described air-lift tube refluxing opening is positioned under the liquid level, and the refluxing opening upper liquid degree of depth is 2～8 with the ratio of the refluxing opening lower liquid degree of depth.
3. reactor drum according to claim 1 is characterized in that described inorganic membrane assembly (3) is tubular type ultrafiltration or micro-filtration inorganic membrane assembly; Admittedly inorganic membrane assembly is carrying out liquid/carry out positive press filtration when separating, transmembrane pressure is 0.01～1MPa; Perhaps negative pressure-pumping, transmembrane pressure is 0.01～0.1MPa.
4. reactor drum according to claim 1 is characterized in that reaction kettle main body (10) contains contraction section and amplifying sections, and contraction section is positioned at the lower end of reaction kettle main body; In application process, liquid level can not arrive amplifying sections.
5. reactor drum according to claim 1 is characterized in that reaction kettle main body (10) upper end is equipped with tensimeter, and has opening for feed (14) and venting port (12); The reaction kettle main body has form (11), and TM, pH meter, oxygen measuring instrument are installed, so that the feed liquid situation in the timely observing response device has discharge opening (16) on the circulation tube bottom.
6. reactor drum according to claim 5 is characterized in that venting port (12) locates to be equipped with valve (13), thereby through regulating the pressure in the free air delivery conditioned reaction still main body (10); Valve (13) connects condensation of gas pipeline (E), is connected with condensation of gas collection device (E-1), vacuum pump (E-2), carrier gas circulating line (F) in turn, and through condensation of gas collection device E-1, product obtains condensation, thereby obtains the higher product of purity; Gas in the carrier gas circulating line (F) passes through valve (H-1), gas meter (H-2) successively, aeration head (1) entering air-lift tube (2) recycles or passes through three-way valve (F-1) along second pipeline (G) discharging through first pipeline (H) through T-valve (F-1).
7. reactor drum according to claim 1 is characterized in that the air-lift tube lower end is equipped with aeration head (1), and aeration head (1) links to each other with compressed gas source (B); Nitrogen, ammonia, hydrogen, oxygen or helium that pressurized air that compressed gas source (B) provides for air (B-1) or high-pressure gas tank (B-2) provide.
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SI2751255T1 (en) * 2011-09-01 2021-04-30 Gicon Grossmann Ingenieur Consult Gmbh Method and device for feeding gases or gas mixtures into a liquid, suspension, or emulsion in a photobioreactor in a specific manner
CN104403937B (en) * 2014-12-17 2016-08-17 大连大学 Rotate internal circulation gas-lift type membrane bioreactor and process system thereof
CN106629958B (en) * 2017-01-20 2023-02-14 南京工业大学 Closed continuous high-pressure gas dissolving device and method
CN106916727A (en) * 2017-03-31 2017-07-04 江南大学 Assemble the airlift reactor of baffling sieve plate
CN111286442A (en) * 2018-12-07 2020-06-16 国投生物科技投资有限公司 Device for culturing microorganisms to obtain volatile products, method and application thereof

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