CN117757595A - Gas-lift type bioreactor for strengthening liquid flow circulation - Google Patents
Gas-lift type bioreactor for strengthening liquid flow circulation Download PDFInfo
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- CN117757595A CN117757595A CN202311758510.0A CN202311758510A CN117757595A CN 117757595 A CN117757595 A CN 117757595A CN 202311758510 A CN202311758510 A CN 202311758510A CN 117757595 A CN117757595 A CN 117757595A
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- rim propeller
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- guide cylinder
- tank body
- gas distributor
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention relates to a gas-lift bioreactor for enhancing liquid flow circulation, comprising: the tank body is internally provided with at least one guide cylinder coaxially arranged with the tank body or at least one outer circulating pipe in fluid conduction connection with the tank body is arranged on the outer wall of the tank body; the rim thrusters are at least one in number and are arranged at the upper end of the guide cylinder, suspended in the tank body or arranged in the outer circulation pipe. The rim propeller disclosed by the invention does not need transmission mechanisms such as a complex and heavy shaft system, a shaft seal system and a speed reducer, and is compact in structure, high in integration level, small in size, light in weight, low in noise, small in vibration and high in efficiency. An air bag is arranged in the reactor to adjust and stabilize the height of the liquid level. Therefore, the reactor of the invention keeps the advantages of no dynamic seal, good sealing performance, difficult bacteria contamination and the like of the airlift bioreactor, strengthens the liquid flow circulation and mass transfer, and has stronger process adaptability.
Description
Technical Field
The invention relates to a gas-lift bioreactor for strengthening liquid flow circulation, and belongs to the technical field of bioreactors.
Background
The large bioreactor is core equipment for biological industrial production, provides a good reaction environment for cells or enzymes, and plays an important role in the biological industry. With the enlargement of the reactor, the heterogeneity of the reaction system is more prominent. In general, exposure of cells to fluctuating environments often negatively affects the productivity of a biological process, but in some cases controlled environmental heterogeneity may improve biological process performance. The effect of mixing is an important factor affecting the uniformity of the reaction system, and therefore, the stirred mixing system of the reactor is critical to providing the desired reaction environment for the cells or enzymes.
Most industrial fermentations are aerobic fermentations, the reaction being carried out under aerobic conditions. In the aerobic liquid submerged fermentation, a mechanical stirring type ventilation bioreactor occupies the dominant position of the bioreactor, the dissolved oxygen concentration in the culture solution and the circulation of the liquid phase are controlled by two modes of stirring rotation speed and ventilation quantity, the dispersion of gas and materials in the reactor is uniform, and the average oxygen mass transfer efficiency is high. However, mechanically stirred ventilated bioreactors also have some drawbacks to be solved, such as: (1) Generally, a plurality of stages of stirring paddles are needed, and the energy consumption of stirring is positively related to the stages of the stirring paddles, so that the operation energy consumption is high, and the energy consumption of a mechanical stirring device accounts for about half of the energy consumption in the fermentation process. (2) the structure is complex, and the manufacturing, installation and maintenance costs are high. (3) the potential risk of contamination at the stirring shaft seal is large. (4) The flow field is complex, and to achieve rational amplification, efficient theoretical guidance and technical means for optimizing and amplifying the fermentation process of the bioreactor are still lacking. (5) The stirring rotation speed is higher, and for the fermentation culture of plant cells and microorganism mycelium, the cells and the mycelium are damaged by the rotation shearing force of a stirring blade, and the metabolism and the productivity can be influenced. (6) For large diameter reactors, a stagnant zone is formed near the tank wall away from the paddles, where aeration is limited. (7) For the reaction liquid with high viscosity, the reaction liquid far away from the stirring paddle has poor mixing effect, even is almost in a static state, and shows serious dissolved oxygen limitation, when the ventilation quantity is too large, the stirring paddle is wrapped by gas, the stirring paddle generates a phenomenon of 'flooding', and the volume oxygen transfer coefficient (K) La ) No further increase occurs. (8) With the development of the large-scale bioreactor, the volume and the power of the tank top motor are larger and larger, the occupied space is occupied, and the size and the strength of the stirring system are also increased.
Thus, the operating costs of using mechanically stirred vented bioreactors tend to be economically prohibitive for certain very cost sensitive products and slower reaction rates and weaker production processes.
The air-lift bioreactor has low energy consumption and is used for microbial fermentation, animal and plant cell culture, enzyme catalytic reaction, wastewater treatment and the like. The airlift bioreactor has no mechanical stirring system, does not need a stirring shaft seal, has good sealing performance and small probability of bacteria contamination, also avoids the damage of shearing force of stirring blades to cells and hyphae, has a simple structure, is easy to amplify, has a larger height-diameter ratio, has longer retention time of bubbles in reaction liquid, and has higher utilization rate of gas. Airlift bioreactors are much less costly to manufacture, install, operate and maintain than mechanically stirred ventilated bioreactors. However, the conventional large airlift bioreactor has disadvantages, which make it limited in application: (1) It is generally considered that the airlift bioreactor has no mechanical stirring system, long mixing time, poor gas-liquid mixing and gas dispersing effects, and the mixing limitation of the large-scale reactor causes a plurality of heterogeneities of the reaction environment, which has negative influence on the profitability of the process. (2) The periodic fluctuation of dissolved oxygen and cell oxygen uptake of the reaction liquid is large in amplitude, the culture liquid at the bottom of the reactor is fully supplied with oxygen and enters the liquid lifting zone, but in the liquid lowering zone, although the fermentation liquid is entrained with bubbles, the liquid lowering zone is still in an anoxic state and CO in the whole because no fresh air is input 2 The concentration is too high. (3) The operation elasticity is small, and the airlift bioreactor can only adjust the dissolved oxygen concentration in the reaction liquid, the circulation period of the liquid phase and the mixing time in one mode of adjusting the ventilation amount, but cannot be controlled respectively. (4) When the efficiency of cells and enzymes is increased to some extent, mass transfer becomes a limiting factor in increasing the efficiency of the bioreactor. The introduced compressed gas is a single energy source for mixing and circulating the reaction liquid in the airlift bioreactor, a large amount of ventilation input momentum is needed to promote mass transfer and circulation of the reaction liquid, and the mixing and circulation effect is poor at low gas speed, so that the ventilation amount of the reaction liquid per unit volume is always higher than that of the mechanical stirring type ventilation bioreactor, and the ventilation energy consumption is high. For some ofFor the cells which are very sensitive to the concentration of oxygen in the reaction solution, the dissolved oxygen level needs to be strictly monitored, and the reduction of ventilation volume leads to serious defects of mass transfer and heat transfer of the fluid. In addition, excessive aeration drives off carbon dioxide and ethylene in the reaction solution, which is disadvantageous for the cultivation of plant cells. (5) Is not suitable for the reaction liquid with high solid content and high viscosity. (6) The guide cylinder of the internal circulation airlift bioreactor is fixed, the outer circulation pipe of the external circulation airlift bioreactor is also fixed, and the gas content of the reaction liquid and the operations of inoculation, feeding, sampling, discharging, continuous reaction and the like in the reaction process influence the apparent volume of the reaction liquid in the reactor and the liquid level height of the reaction liquid, and the fluctuation of the liquid level height of the reaction liquid influences the flowing circulation of the reaction liquid, thereby influencing the whole flow field in the reactor.
For the scale of plant cell culture, photosynthetic fermentation, gas fermentation, electrofermentation, enzyme electrocatalysis, photo-enzyme catalysis and other emerging reactions, the existing airlift bioreactor still needs to be improved greatly.
Disclosure of Invention
Aiming at the technical problems, the invention provides a gas-lift type bioreactor for strengthening liquid flow circulation, which overcomes the defects of the traditional mechanical stirring type ventilation bioreactor and the gas-lift type bioreactor and has strong adaptability to the process.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
a gas-lift bioreactor for enhanced circulation of a liquid stream comprising:
the tank body is internally provided with at least one guide cylinder which is coaxially arranged with the tank body or uniformly distributed by taking the axle center of the tank body as the center, or at least one outer circulating pipe which is connected with the tank fluid in a conducting way is arranged on the outer wall of the tank body;
the rim thrusters are at least one in number and are arranged at the upper end of the guide cylinder or hung in the tank body or arranged in the outer circulation pipe;
the air bags are at least one in number and are arranged in the tank body, and the air bags are connected with an external pipeline and are used for introducing fluid.
The airlift bioreactor preferably comprises a rim thruster stator, a rim thruster rotor and rim thruster paddles, wherein the rim thruster stator is provided with a cavity for accommodating the rim thruster rotor, and the rim thruster rotor and the rim thruster paddles are integrally designed or detachably connected; or,
the rim propeller comprises a rim propeller stator, a rim propeller rotor and rim propeller blades, wherein the rim propeller rotor is sleeved outside the rim propeller stator, and the rim propeller rotor and the rim propeller blades are integrally designed or detachably connected.
Preferably, the guide cylinder is an integral cylinder or is formed by coaxially arranging a plurality of sectional cylinders, an annular gap is arranged between two adjacent sectional cylinders, and the rim propeller stator is connected with the guide cylinder or the rim propeller stator is connected with the pipe wall of the outer circulation pipe, or the rim propeller stator is fixed in the tank body through a fixing piece.
In the airlift bioreactor, preferably, a jacket or a guide cylinder heat exchange tube is arranged on the inner wall and/or the outer wall of the guide cylinder;
The guide cylinder heat exchange tubes extend along the axial direction of the guide cylinder on the inner wall and/or the outer wall of the guide cylinder and are uniformly distributed in the circumferential direction of the guide cylinder heat exchange tubes; or,
the guide cylinder heat exchange tube is coiled on the inner wall or the outer wall of the guide cylinder; or,
and the guide cylinder heat exchange tubes are longitudinally and/or transversely spliced to form the guide cylinder.
The airlift bioreactor preferably further comprises a gas distributor, wherein the gas distributor comprises an upper end gas distributor and/or a lower end gas distributor, the upper end gas distributor is suspended on the inner tank top of the tank body or is arranged between the rim propeller stator and the rim propeller rotor, and the lower end gas distributor is arranged at the inner bottom of the tank body.
Preferably, the air lift bioreactor is characterized in that the lower-end air distributor is a cyclone propulsion type air distributor and comprises a lower-end breather pipe and a cyclone propulsion type air distributor turbine arranged at an air outlet of the lower-end breather pipe.
In the airlift bioreactor, preferably, radial opening rotary blades are uniformly distributed in the cyclone propulsion type gas distributor turbine, and the upper end of the cyclone propulsion type gas distributor turbine is connected with cyclone propulsion type gas distributor blades for pushing fluid to ascend axially; or,
The gas distributor turbine consists of several tangential flow gas distributor nozzles.
Preferably, the air lift type bioreactor is characterized in that the cyclone propulsion type gas distributor is a magnetic suspension type gas distributor.
In the airlift bioreactor, preferably, the rim propeller is a magnetic levitation propeller.
In the airlift bioreactor, preferably, a diversion cone is arranged at the bottom of the tank body, and/or,
a plurality of porous sieve plates are arranged in the tank body.
In the airlift bioreactor, preferably, a plurality of vortex deflectors are arranged in the liquid lifting area and the liquid lowering area of the tank body, and/or,
a spoiler is arranged above the guide cylinder.
In the airlift bioreactor, preferably, the rim propeller is an outer rotor rim propeller, the rim propeller rotor is sleeved outside the rim propeller stator, and the rim propeller blades are defoaming paddles.
Preferably, the rim propeller rotor and the rim propeller stator form an impeller together, the inside of the impeller is designed into a cavity to form a self-priming impeller, the internal cavity of the impeller is communicated with the lower end of a rim propeller fixing pipe, the upper end of the rim propeller fixing pipe is provided with an air suction hole, and the upper end of the rim propeller fixing pipe is fixed at the inner top of the tank body.
In the airlift bioreactor, preferably, a light source or a light source array is arranged in the tank body and used for light fermentation, and the light source or the light source array is arranged on the guide plate, the inner wall and the outer wall of the guide cylinder, the inner wall of the outer circulation pipe or the inner wall of the tank body; or,
an electrode is arranged in the tank body and used for electric fermentation.
Due to the adoption of the technical scheme, the invention has the following advantages:
1. the liquid level of the reaction liquid is regulated and stabilized through the inflation degree of the air bag in the reactor, the mixing and circulation of the top reaction liquid are controlled and stabilized, and the whole flow field is prevented from being out of control due to the out of control of the height of the top reaction liquid.
2. The rim propeller provides a second kinetic energy source for mixing and circulating the reaction liquid in the airlift bioreactor, and the rim propeller and the ventilation volume of the lower-end gas distributor can jointly regulate the liquid speed, the circulation period and the mixing time of the reaction liquid, so that the fluctuation period and the fluctuation degree of the reaction liquid pressure and the gas content can be regulated and controlled to a certain extent.
3. The rim propeller does not need transmission mechanisms such as a complex and heavy shaft system, a shaft seal system and a speed reducer, and has the advantages of compact structure, high integration level, small volume, light weight, low noise, small vibration and high efficiency. Therefore, the reactor of the invention keeps the advantages of no dynamic seal, good sealing performance and difficult bacteria contamination of the airlift bioreactor.
4. Compared with a multistage stirrer of a mechanical stirring type ventilation bioreactor, the rim propeller drives liquid flow to axially circulate, so that the axial mixing performance is good, and the multistage stirring type ventilation bioreactor can adapt to reaction liquid with high viscosity or containing a large amount of solids; the reaction liquid can be driven by the lower rotating speed of the rim propeller, so that the energy consumption is low, and the shearing force of the blades on cells and hyphae is small.
5. Fresh gas is introduced into the liquid-reducing area of the culture solution, so that the gas content and dissolved oxygen concentration (DO) of the liquid-reducing area can be improved, the amplitude of periodic fluctuation of the gas and DO in the reaction solution can be reduced, the fermentation device can adapt to fermentation with high respiratory intensity, and the reaction uniformity in the reactor can be improved.
6. The mixing intensity of the fluid, the gas content of the liquid rising area and the liquid falling area and DO are regulated and controlled by the rotating speed of the rim propeller, the ventilation quantity of the upper gas distributor and the ventilation quantity of the lower gas distributor, so that the elasticity of the process operation is increased, and the possibility is provided for implementing new regulation and control modes such as flow field environment control, temperature field control, concentration field control and the like.
7. The flow field is simpler and is easy to amplify. The turbulence of the flow field is increased by adding a spoiler, a flow guide plate, a porous sieve plate and the like, so that bubbles are further dispersed, and the radial mixing of the fluid is enhanced.
8. The uniformity of the reaction system is improved, and the negative influence on the reaction due to the heterogeneity of the reaction system is reduced.
9. The reactor of the invention can be used for gas fermentation and anaerobic fermentation. The reactor is easy to reform so as to adapt to the emerging large-scale biological reactions such as photosynthetic fermentation, electrofermentation, enzyme-electrocatalytic, photo-enzyme catalysis, plant cell culture and the like, and can also be used for other chemical reactions.
Drawings
FIG. 1 is a schematic view of an internal circulation airlift reactor according to the present invention;
FIG. 2 is a schematic view of another internal recycle airlift reactor provided by the invention;
FIG. 3 is a schematic view of a third internal recycle gas lift reactor provided by the present invention;
fig. 4 is a cross-sectional view of the inner rotor rim mover of fig. 1, 2, 6, 7, 8, 9, 12, 13, 14, 15;
FIG. 5 is a top view of the outer rotor rim propeller of FIGS. 3 and 16;
FIG. 6 is a schematic illustration of an external circulation airlift reactor with a single circulation tube provided by the present invention;
FIG. 7 is a schematic diagram of an external circulation airlift reactor with multiple circulation tubes provided by the invention;
FIG. 8 is a schematic top view of another multi-circulation loop external circulation airlift reactor provided by the invention;
FIG. 9 is a schematic illustration of a third multi-cycle tube external circulation airlift reactor provided by the present invention;
FIG. 10 is a top view of a cyclonic propulsion gas distributor in a airlift reactor provided by the present invention;
FIG. 11 is a top view of a jet cyclonic propulsion gas distributor in a airlift reactor provided by the present invention;
FIG. 12 is a schematic view of an external circulation airlift reactor with perforated screen plates provided by the present invention;
FIG. 13 is a schematic view of an internal circulation airlift reactor with baffles provided by the present invention;
FIG. 14 is a schematic view of an internal circulation airlift reactor with multiple guide barrels provided by the present invention;
FIG. 15 is a schematic view of a gas lift reactor with spherical tanks according to the present invention;
FIG. 16 is a schematic view of an airlift reactor of a tank top suspended rim propeller provided by the present invention;
FIG. 17 is a schematic view of a self-priming impeller according to the present invention;
FIG. 18 is a schematic diagram of a tank top airflow cycle provided by the present invention;
FIG. 19 is a schematic longitudinal section of a heat exchange flow guide cylinder according to the present invention;
FIG. 20 is a schematic cross-sectional view of a heat exchange flow guide cylinder according to the present invention;
the figures are marked as follows:
100-tank body; 101-an outer circulation tube; 112-manhole; 113-an exhaust port; 114-a discharge port;
200-a guide cylinder; 201-annular gap; 202-a guide cylinder heat exchange tube; 210-a lower vent pipe; 211-a lower gas distributor; 212-a cyclonic propulsion gas distributor; 213-cyclonic propulsion gas distributor blades; 214-a cyclonic propulsion gas distributor turbine; 215-cyclonic propulsion gas distributor nozzles; 216-upper vent pipe; 217-upper gas distributor; 218-vent pipe a; 219-an air suction hole; 220-defoaming paddles; 221-defoaming paddle bracket;
300-reaction solution; 301-a gas-liquid separation zone; 302-a liquid lifting zone; 303-a liquid dropping area; 304-direction of flow; 305-direction of air flow;
400-rim propeller; 401-rim propeller blades; 402-rim propeller stator; 403-rim propeller rotor; 404-rim propeller end cap; 405-rim pusher securing ribs; 406-rim propeller securing tube; 407-self priming impeller;
500-balloon; 501-an air bag fixing rib;
600-spoiler; 601-a deflector; 602-a porous screen plate; 603-diversion cone.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present invention more apparent, the technical solutions in the present invention will be clearly and completely described below, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by one of ordinary skill in the art without undue burden from the present disclosure, are intended to be within the scope of the present disclosure.
Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs. The terms "first," "second," "third," "fourth," and the like as used herein do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that elements or items preceding the word are included in the element or item listed after the word and equivalents thereof, but does not exclude other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect.
For ease of description, spatially relative terms, such as "inner," "outer," "lower," "upper," and the like, may be used herein to describe one element or feature's relationship to another element or feature as illustrated in the figures. Such spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures.
The traditional large airlift bioreactor has the defects that the application is limited: (1) It is generally considered that the airlift bioreactor has no mechanical stirring system, long mixing time, poor gas-liquid mixing and gas dispersing effects, and the mixing limitation of the large-scale reactor causes a plurality of heterogeneities of the reaction environment, which has negative influence on the profitability of the process. (2) The periodic fluctuation of dissolved oxygen and cell oxygen uptake of the reaction liquid is large in amplitude, the culture liquid at the bottom of the reactor is fully supplied with oxygen and enters the liquid lifting zone, but in the liquid lowering zone, although the fermentation liquid is entrained with bubbles, the liquid lowering zone is still in an anoxic state and CO in the whole because no fresh air is input 2 The concentration is too high. (3) The operation elasticity is small, and the airlift bioreactor can only adjust the dissolved oxygen concentration in the reaction liquid, the circulation period of the liquid phase and the mixing time in one mode of adjusting the ventilation amount, but cannot be controlled respectively (the mechanical stirring type ventilation bioreactor is controlled by two parameters of the ventilation amount and the stirring rotating speed). (4) When the efficiency of cells and enzymes is increased to some extent, mass transfer becomes a limiting factor in increasing the efficiency of the bioreactor. The introduced compressed gas is a single energy source for mixing and circulating the reaction liquid in the airlift bioreactor, a large amount of ventilation input momentum is needed to promote mass transfer and circulation of the reaction liquid, and the mixing and circulation effect is poor at low gas speed, so that the ventilation amount of the reaction liquid per unit volume is always higher than that of the mechanical stirring type ventilation bioreactor, and the ventilation energy consumption is high. For some cells which are very sensitive to the concentration of oxygen in the reaction solution, the dissolved oxygen level is strictly monitored, and the reduction of ventilation volume leads to serious defects of mass transfer and heat transfer of the fluid. In addition, excessive aeration drives off carbon dioxide and ethylene in the reaction solution, which is disadvantageous for the cultivation of plant cells. (5) Is not suitable for the reaction liquid with high solid content and high viscosity. (6) The guide cylinder of the internal circulation airlift bioreactor is fixed in position, the outer circulation pipe of the external circulation airlift bioreactor is also fixed in position, and the gas content of the reaction solution and the reaction are carried out The operations of inoculation, feeding, sampling, discharging, continuous reaction and the like in the process all influence the apparent volume of the reaction liquid in the reactor and the liquid level height of the reaction liquid, and the fluctuation of the liquid level height of the reaction liquid influences the flow circulation of the reaction liquid, so that the whole flow field in the reactor is influenced.
Aiming at the technical problems, the invention provides the airlift bioreactor for strengthening the circulation of liquid flow, which overcomes the defects of the traditional mechanical stirring type ventilation bioreactor and the airlift bioreactor, and has strong adaptability to the process and strong expandability.
Some terms involved in the present invention are explained as follows.
The reaction solution: the liquid, gas-liquid mixture, gas-liquid-solid mixture and liquid-solid mixture in the reactor are collectively called as fermentation liquid, culture liquid, enzyme catalytic reaction liquid and chemical reaction liquid.
Photosynthetic fermentation: light energy driven biocatalytic reactions, including cultivation of plant cells, microalgae, photosynthetic bacteria, artificially constructed photosynthetic cells, autotrophic by photosynthesis, the photogenerated electrons entering the oxidative respiratory chain of the cells, providing energy for the metabolism of the cells to obtain organic chemicals and/or Biomass (Biomass). Photosynthetic fermentation also includes light culture.
Hydrogen energy fermentation: fermentation or biochemical reactions with hydrogen gas to provide reducing power.
Photo-enzyme catalysis: combining photocatalytic and enzymatic reactions.
Gas content: the gas phase is a percentage of the volume of the gas-liquid mixture.
Electrofermentation (Electro-Fermentation, EF): the electric energy supplied by the electrodes provides reducing power, and microorganisms change their fermentation in the energized environment to produce and provide the target product. The electrode in electrofermentation may act as an electron acceptor (i.e. anodic electrofermentation, AEF) or donor (i.e. cathodic electrofermentation, CEF), or simply as a means of controlling the redox potential.
And (3) gas fermentation: and (3) taking one or more substances which are gas under normal temperature and normal pressure as a carbon source or energy source, and generating one or more compounds or/and biological reaction processes of cell biomass through one or more organisms or/and enzymes.
Sunlight tunnel: light outside the reactor can be introduced into the cylindrical structure inside the reactor by reflection.
The technical scheme of the invention is described in detail below with reference to the accompanying drawings.
As shown in fig. 1, 2 and 3, the rim propeller 400 is also called as a rim driving propeller (Rim Driven Thruster, RDT), a shaftless propeller and an integrated motor propeller, wherein a rotor of the propeller and a blade are integrated into a whole, a shaft is not used for transmitting torque, and the torque generated by the motor is directly transmitted to the rim part of the rim blade through the rotor to drive the rim blade to rotate, so that a stirring shaft system and a shaft seal system penetrating through a tank body in a traditional stirrer are completely eliminated. Rim thrusters 400 are classified into an inner rotor rim thruster (see fig. 4 for details) and an outer rotor rim thruster (see fig. 5 for details) according to the position of the rotor. Compared with the traditional shaft stirring system, the shaft system is not required, so that the weight is much lighter, the noise source is reduced, and the vibration is very low; the device has the advantages of high efficiency, compact structure and small volume; in addition, the motor efficiency is higher, and the rotating speed range is larger. The stator and rotor of rim propeller 400 may employ magnetic levitation technology.
The rim impeller 400 is immersed in the reaction liquid in three ways: (1) A rim propeller 400 is fixed to the upper end of the inner circulation airlift reactor guide cylinder 200, and a cylindrical stator of the rim propeller 400 is connected to the guide cylinder 200 as shown in fig. 1, 2 and 3. (2) The rim impeller 400 is fixed on the pipe wall of the outer circulation pipe 101 or the upper part of the tank body 100 of the outer circulation airlift reactor, as shown in fig. 6, 7, 8, 9 and 12, the cylindrical stator of the rim impeller 400 in the outer circulation pipe 101 is connected to the pipe wall of the outer circulation pipe 101 or as a part of the outer circulation pipe 101, and the stator of the rim impeller 400 in the tank body 100 is connected to the tank wall by a fixing rib (rim impeller fixing rib 405). (3) Rim impeller 400 is suspended from the tank top by a securing rod or hollow rim impeller securing tube 406, as shown in fig. 16.
The invention refers to an integrated rotor and blade as an "impeller", which can be of various designs. The blades of rim propeller 400 are preferably pitched blades or approximately helicoidal blades, two or more of which are symmetrically distributed. When the rim propeller 400 operates, the blades press down the fluid in the corresponding region, strengthen the flow rate of the reaction liquid in the liquid-dropping region, accelerate the circulation and mixing of the reaction liquid, and break up the bubbles gathered at the upper part of the reaction liquid.
Rim impeller 400 may be an electrically powered rim impeller or a compressed gas powered pneumatic rim impeller. The pneumatic rim propeller drives the rotor to rotate by compressed gas and simultaneously introduces gas into the reaction liquid, so that the compressed gas can fully utilize the kinetic energy of the compressed gas and can introduce fresh gas into the liquid dropping area. The rim propeller is driven by compressed gas, so that the difficulty that the electric drive is difficult to make the fermentation tank form a potential difference with the outside is avoided. The electric cable of the electric rim propeller and the compressed gas pipeline of the pneumatic rim propeller are easy to arrange in the reactor, easy to seal and small in occupied space.
The upper part of rim propeller 400 may not need a "baffle" because at rest the rotor falls on the stator; on the other hand, when the paddle rotates, the culture solution is pressed downwards, and an upward force can be generated to lift the rotor. The defoaming paddle bracket 221 can be erected on the rotor ring of the rim propeller 400 to support and connect the defoaming paddles 220, as shown in fig. 3, the defoaming paddles 220 rotate along with the rotor, and perform the defoaming function in the gas-liquid separation area 301.
The outer rotor rim propeller can be hung down from the tank top, the blades of the outer rotor rim propeller are replaced by the defoaming paddles 220, as shown in fig. 13, the defoaming paddles 220 are started according to the condition of foam, the rotating speed of the defoaming paddles 220 is regulated, no starting is performed when no foam exists, electric energy is saved, when more foam exists, the defoaming paddles 220 are started, and even the foam can be rotated at a higher speed to be centrifuged to the tank wall, so that quick defoaming is realized. The independently controlled rotational speed defoaming paddles 220 may take a variety of forms including, but not limited to: rake, scraper, turbine, centrifugal, disk.
The rotation speed of the rim propeller 400 at the upper end of the guide cylinder 200 in the internal circulation airlift reactor is increased to a certain degree, vortex generated by the rim propeller 400 reaches the upper part of the impeller, gas above the liquid level is entrained into the reaction liquid 300, and part of the gas in the top space of the reactor reenters the reaction liquid 300 to participate in the reaction. Another benefit of this approach is: foam floating on the liquid surface of the reaction liquid 300 is entrained back into the reaction liquid 300, and plays a role in defoaming.
As shown in fig. 1, 2 and 3, the guide cylinder 200 for guiding the circulation of the reaction liquid in the internal circulation airlift reactor is a cylinder coaxial with the tank 100, and the guide cylinder 200 may be a single body or may be two or more coaxial cylinders in sections. The gap between two adjacent cylinders of a segment is referred to as the annulus 201. There may be no annular space 201 or an annular space 201 between the cylindrical stator of rim impeller 400 and guide cylinder 200. The guide cylinder 200 may be a regular cylinder or a spiral cylinder, and guides the reaction liquid to rise or fall spirally, increases tangential flow and turbulence of a flow field, prolongs residence time and flow path of bubbles in the reactor, and breaks up large bubbles.
As shown in fig. 14 and 15, a plurality of guide cylinders 200 uniformly distributed around the axis of the tank 100 are disposed in the internal circulation airlift reactor.
The outer wall of the tank 100 and the outer wall of the outer circulation pipe 101 are provided with a jacket or a coil pipe for heat exchange of the reaction liquid, preferably a semicircular coil pipe structure. To increase the heat exchange area of the reactor, the guide cylinder 200 also has the function of a heat exchanger by arranging a jacket or a guide cylinder heat exchange tube 202.
The guide cylinder 200 can be provided with a guide cylinder heat exchange tube 202 which is hollow inside; the heat exchange tube 202 of the guide cylinder can be a coil on the inner wall and/or the outer wall of the guide cylinder 200 (fig. 19A is a semicircular coil on the inner wall of the guide cylinder 200) or a vertical tube (fig. 20A is a circular vertical tube on the inner wall of the guide cylinder 200, fig. 20B is a square vertical tube on the inner wall of the guide cylinder 200, and fig. 20C is a semicircular vertical tube on the outer wall of the guide cylinder 200); the heat exchange tube 202 may be directly connected to the outside of the guide tube longitudinally and/or transversely (fig. 19B is the outside of the guide tube 200 formed by horizontally and spirally connecting square tubes, and fig. 20D is the outside of the guide tube 200 formed by vertically connecting square tubes). The hollow jacket of the guide cylinder 200 or the inner part of the guide cylinder heat exchange tube 202 is filled with fluid for heat exchange, so that the guide cylinder 200 has the function of a heat exchanger, and is used for heating and cooling reaction liquid, improving the temperature control performance of the internal circulation airlift reactor, and having faster heating and cooling, saving the heating and cooling time of sterilization, improving the equipment utilization rate and being suitable for fermentation with large heat release.
In order to increase the gas content of the liquid drop zone 303 and overcome the anoxic phenomenon of the liquid drop zone 303, a gas distributor, that is, an upper gas distributor 217 may be provided at the upper portion of the liquid drop zone 303, and fresh gas may be introduced. The gas introduced from the upper gas distributor 217 is broken up by the rim propeller 400 and descends with the reaction liquid, so that the problem of insufficient fresh gas content or DO in the liquid-lowering region 303 is solved. The upper gas distributor 217 may also be between the stator and rotor of the rim propeller 400. The ventilation amounts of the upper gas distributor 217 and the lower gas distributor 211 may be controlled separately, and the upper gas distributor and the lower gas distributor may be used for ventilation at the same time, or the upper gas distributor or the lower gas distributor may be used alone for ventilation of only a single stage of gas distributors.
The gas distributor can have various forms such as single tube type, umbrella cover type, small hole coil type, jet flow type, rotational flow type and the like. The gas outlet of the gas distributor can be a micro-filtration membrane, preferably a ceramic membrane and a metal sintering membrane, and has the advantages that: (1) the bubbles are smaller; (2) The gas distributor may withdraw filtrate from the reactor in reverse.
The lower gas distributor 211 is preferably a cyclone propulsion gas distributor 212 (as shown in fig. 10) and can fully utilize the injection kinetic energy of the compressed gas to increase the flow rate of the liquid phase rising. The cyclone propulsion type gas distributor 212 (shown in fig. 3) has a hollow turbine (cyclone propulsion type gas distributor turbine 214) rotating around the air outlet as an axis at the air outlet of the lower ventilation pipe 210, the uniformly distributed rotary blades in the hollow turbine extend along radial openings, and the upper part of the hollow turbine is connected with blades (cyclone propulsion type gas distributor blades 213) for pushing the fluid to rise upwards axially. When the lower gas distributor 211 sprays gas into the reactor, the gas is guided by the rotary vane in the turbine, the kinetic energy of the gas pushes the turbine to rotate reversely, and the blades on the turbine rotate along with the turbine, so that the reaction liquid is pushed to move upwards, the flow speed of the fluid in the liquid lifting area is enhanced, and the bubbles are further broken. The turbine of the cyclonic propelled gas distributor 212 may also be formed of a plurality of tangential flow gas nozzles (cyclonic propelled gas distributor nozzles 215) as shown in fig. 11. The stator and rotor of the cyclonic propulsion gas distributor 212 may employ magnetic levitation technology to reduce friction between the rotating disk and the breather tube, reduce energy consumption, and extend life.
Dissolved oxygen concentration (DO) in the aerobic fermentation reaction liquid and corresponding gas concentration in the gas fermentation reaction liquid are important operation variables in the reaction process, and the regulation level of the operation variables directly influences the change of a plurality of other variable parameters. The invention can regulate and control DO, gas content, apparent liquid velocity, liquid phase circulation time and mixing strength in the reaction liquid through the ventilation volume of the upper end gas distributor 217, the ventilation volume of the lower end gas distributor 211 and the rotating speed of the rim propeller 400, thereby providing possibility for implementing new control modes of flow field environment, temperature field, concentration field and the like.
As shown in fig. 3, 7, 9, 15 and 16, a diversion cone 603 can be arranged at the bottom of the tank to guide the mixing and circulation of the materials at the bottom of the tank, so that the materials at the central part of the tank bottom are prevented from becoming a flowing dead zone and the retention of particles is prevented. Porous screen plates 602 may be added to the reactor to further disperse the bubbles and increase the turbulence of the flow field, as shown in fig. 12. Vortex deflectors 601 may be provided in the liquid lifting zone 302 and the liquid lowering zone 303, as shown in fig. 13, to enhance the rotational mixing of the liquid streams, and the deflectors 601 may be porous and have the function of dispersing bubbles by a porous plate. A spoiler 600 may be provided above the guide cylinder 200 to enhance mixing of the reaction solution top materials.
The liquid phase height above the guide cylinder 200 or the outer circulation pipe of the airlift bioreactor greatly affects the mixing circulation of the reaction liquid, and the part consists of a gas-liquid or gas-liquid-solid disperse phase, and the height of the gas-liquid or gas-liquid-solid disperse phase changes along with the volume of the liquid in the tank and the spraying amount of the gas. The gas content of the reaction solution 300, and the operations of inoculation, feeding, sampling, discharging, continuous fermentation and the like in the reaction process affect the volume of the reaction solution in the reactor and the liquid level thereof. In order to stabilize and adjust the height of the liquid level in the reactor, the invention installs the air bag 500 below the liquid level in the reactor, the air bag 500 is connected with a pipeline leading to the outside of the tank, the air bag 500 is filled with fluid through the pipeline or the fluid is discharged from the air bag 500, the filling degree of the air bag 500 is controlled to change the volume of the air bag 500, and then the liquid level of the reaction liquid in the reactor is adjusted. The balloon 500 may be inflated with gas and liquid, preferably compressed air. A level sensor may be provided to feedback control the filling level of the bladder 500.
The balloon 500 has a longitudinal cross-section in the form of a shuttle and the balloon wall is composed of an elastic polymer material capable of withstanding the fermentation sterilization temperatures and pressures. For the internal circulation airlift bioreactor, the air bag 500 can be enclosed into a cylinder shape, and replace a part of the internal guide cylinder 200, the position of the air bag 500 is preferably in the middle section of the internal guide cylinder 200, and the upper and lower ends of the air bag 500 are preferably fixed on the guide cylinder 200 above and below the air bag 500, as shown in fig. 1, 3, 13 and 18; the balloon 500 may also be positioned in other suitable locations as shown in fig. 15. For the external circulation airlift bioreactor, the air bag 500 is preferably disposed at the central axis of the tank 100, as shown in fig. 6, 7, 9, 12 and 16. The position of the air bag 500 can be fixed by the air bag fixing rib 501, the air bag fixing rib 501 is preferably of a tubular structure, and the pipeline of the air bag fixing rib 501 is communicated with the inner pipeline and the outer pipeline of the reactor of the air bag 500. One reactor may have one or more airbags 500, as shown in fig. 6, 7, and 15.
The proper height of the reaction liquid column is beneficial to prolonging the detention time of the gas in the reaction liquid 300 and improving the utilization rate of the gas. Therefore, the height to diameter ratio of the airlift reactor is usually 4 to 12, and the height of the industrial scale reactor can reach more than 30 m. However, the liquid surface of the reaction solution 300 of the large airlift bioreactor is too high, so that the gas-liquid distribution is uneven, and the periodical variation of the pressure born by the cells during the circulation of the reaction solution 300 is large. In addition, the static pressure of the feed liquid is large, the pressure of the outlet of the gas compressor must be increased, the power consumption of the gas compressor is greatly increased, the pressure bearing of the reactor design is also large, and the manufacturing and installation costs of the tank body 100 are high. Static pressure in the lower part of the reactor may directly affect cell viability or increased gas solubility may affect metabolic activity, thereby affecting productivity and product quality. For this reason, the height of the airlift bioreactor can be reduced and the diameter of the tank 100 can be increased, i.e., the height to diameter ratio of the reactor can be reduced, while the effective volume is ensured. To ensure the liquid flow circulation of the airlift reactor with a smaller height-to-diameter ratio, a plurality of outer circulation pipes 101 can be arranged for the outer circulation airlift reactor, as shown in fig. 7, 8 and 9; for an internal circulation airlift bioreactor, multiple sets of air distributors and draft tubes 200 are provided within the tank 100 as shown in fig. 14. Further, the outer shape of such an internal circulation airlift bioreactor with multiple sets of air distributors and guide barrels 200 may be spherical as shown in fig. 15. With the same volume, the spherical tank body 100 requires the least area of tank wall material, has stronger pressure bearing capability, and can be thinner.
The invention adopts the electrically driven rim propeller 400 to transfer kinetic energy to the reaction liquid 300, and can realize mass transfer and heat transfer of the reaction liquid 300 without introducing gas, so the invention can be used for aerobic reaction without ventilation, also can be used for anaerobic reaction without ventilation, and can be used for reaction divided into an aerobic stage and an anaerobic stage in one reaction period.
The compressed gas required by the ventilation reaction needs an electric gas compressor, the power consumption is very high, and the energy consumption of the air compressor accounts for 30-70% of the total power consumption in the fermentation process. The compressed gas is obtained by utilizing wind energy (the wind power is utilized to drive the wind wheel to rotate, and then the gas compressor is driven to obtain the compressed gas, the compressed gas is stored in the gas storage tank, and the gas is released from the gas storage tank according to the required flow and pressure when in use, the compressed gas is compressed without depending on electric energy, so that the energy consumption cost of the reactor for gas supply can be greatly reduced.
The reactor of the invention can also be filled with hydrogen, low-carbon gas (such as methane, carbon dioxide, carbon monoxide) and NH 3 、H 2 S、SO 2 And synthesis gas (syngas), etc., hydrogen energy fermentation, gas fermentation, biological decarbonization, biological desulfurization, biological purification, etc. The gas fermentation is closely related to the design of the reactor and the control of fermentation process parameters, and the rotating speed of the rim propeller 400 can be independently controlled, so that the adaptability is provided, and the utilization rate of raw material gas can be improved.
The method for improving the utilization rate of the raw material gas comprises the following steps: the impeller is designed into a cavity to become a self-priming impeller, the cavity inside the impeller is communicated with the lower end of the rim impeller fixing tube 406 as shown in fig. 17, and the upper end of the rim impeller fixing tube 406 in the tank is provided with a suction hole 219 as shown in fig. 18. By increasing the rotation speed of the impeller, the gas in the top space of the reactor can be sucked into the reaction liquid from the air suction holes 219, and the recycling of the gas in the top space of the reactor is realized, so that the reaction gas is fully utilized, and the exhaust emission and the exhaust treatment cost are reduced. The mechanism is as follows: the impeller rotates to form liquid flow around the impeller to continuously repel the surrounding reaction liquid, when the impeller rotates at a high speed to reach a critical rotation speed, the pressure of the liquid around the impeller is lower than the pressure in the center of a cavity of the impeller, the impeller with the cavity generates pressure difference at the opening at the tail end of the impeller, when the partial pressure drop overcomes the pressure head of the reaction liquid level, the gas in the hollow rim-impeller fixing pipe 406 reaches the opening at the tail end of the rotor to be ejected at a high speed, and the gas suction hole 219 at the upper end of the rim-impeller fixing pipe 406 sucks the gas in the top space of the reactor to realize the recycling of the gas. The self-priming impeller can have a variety of designs/structures, and the invention is not limited. If the rim propeller fixing tube 406 communicates with the vent tube a 218 outside the canister, as shown in fig. 18, gas inside and outside the canister can be inhaled at the same time.
The airlift bioreactor can be internally provided with light sources such as a light emitting diode, an optical fiber or a light guide rod (light is taken out of a tank), a sunlight tunnel and the like to implement photosynthetic fermentation and photo-enzyme catalytic reaction. The light guide fiber or the light guide rod and the sunlight tunnel can fully utilize sunlight and save electric energy under the cooperation of the automatic sun tracking device. The light source may be disposed at the baffle 601, the inner and outer walls of the guide cylinder 200, the inner wall of the outer circulation pipe 101, and the inner wall of the can 100. Since the light penetration distance is short, attenuation in the reaction liquid is serious, for this purpose, an array of light sources may be arranged in the reactor, such as: a plurality of layers of coaxial guide barrels are arranged in the reactor, and light sources are arranged on the inner wall and the outer wall of the guide barrels. The light source may be arranged only locally in the reactor (e.g. only in the guide cylinder 200 or only outside the guide cylinder 200 or only in the outer circulation pipe 101), so that the reaction liquid flows through the light zone and the dark zone without light in the circulation process, and the light and dark alternate culture is implemented.
The reactor of the present invention is also suitable for use in enzyme-catalyzed reactions, including those requiring the passage of a gas.
After the electrodes are arranged in the reactor, the reactor can be used as an electric energy bioreactor for electric fermentation. The electrodes can be one or more groups, and the electrodes can be plate-shaped or cylindrical and can be spiral in the reactor, and have the functions of diversion and mixing.
To reduce adhesion and corrosion, the inner walls and internal components of the reactor may be coated with a hydrophobic copolymer film, preferably a self-assembled, strongly adhesive copolymer film as disclosed in chinese patent No. CN 02110796270.8.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and are not limiting; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present invention.
Claims (14)
1. A gas-lift bioreactor for enhanced circulation of a liquid stream, comprising:
the tank comprises a tank body (100), wherein at least one guide cylinder (200) which is coaxially arranged with the tank body (100) or uniformly distributed by taking the axle center of the tank body (100) as the center is arranged in the tank body (100), or at least one outer circulating pipe (101) which is in conductive connection with the tank fluid is arranged on the outer wall of the tank body (100);
at least one rim propeller (400) arranged at the upper end of the guide cylinder (200) or suspended in the tank body (100) or arranged in the outer circulation pipe (101);
And at least one air bag (500) is arranged in the tank body (100), and the air bag (500) is connected with an external pipeline and is used for introducing fluid.
2. The airlift bioreactor as claimed in claim 1, characterized in that the rim propeller (400) comprises a rim propeller stator (402), a rim propeller rotor (403) and rim propeller blades (401), wherein a cavity for accommodating the rim propeller rotor (403) is formed in the rim propeller stator (402), and the rim propeller rotor (403) and the rim propeller blades (401) are integrally designed or detachably connected; or,
the rim propeller (400) comprises a rim propeller stator (402), a rim propeller rotor (403) and rim propeller blades (401), wherein the rim propeller rotor (403) is sleeved outside the rim propeller stator (402), and the rim propeller rotor (403) and the rim propeller blades (401) are integrally designed or detachably connected.
3. Airlift bioreactor according to claim 2, characterized in that the guide cylinder (200) is an integral cylinder or is formed by coaxially arranging a plurality of segmented cylinders, an annular gap (201) is arranged between two adjacent segmented cylinders, the rim propeller stator (402) is connected with the guide cylinder (200) or the rim propeller stator (402) is connected with the pipe wall of the outer circulation pipe (101), or the rim propeller stator (402) is fixed in the tank body (100) through a fixing piece.
4. A airlift bioreactor as claimed in claim 3, characterized in that a jacket or a guide cylinder heat exchange tube (202) is provided on the inner wall and/or outer wall of the guide cylinder (200);
the guide cylinder heat exchange tubes (202) extend along the axial direction of the guide cylinder (200) on the inner wall and/or the outer wall of the guide cylinder (200) and are uniformly arranged in the circumferential direction of the guide cylinder; or,
the guide cylinder heat exchange tube (202) is coiled on the inner wall or the outer wall of the guide cylinder (200); or,
the guide cylinder heat exchange tubes (202) are longitudinally and/or transversely spliced into the guide cylinder (200).
5. The airlift bioreactor of claim 1, further comprising a gas distributor comprising an upper gas distributor (217) and/or a lower gas distributor (211), the upper gas distributor (217) suspended from an inner tank top of the tank (100) or disposed between the rim propeller stator (402) and the rim propeller rotor (403), the lower gas distributor (211) disposed at an inner bottom of the tank (100).
6. The airlift bioreactor of claim 5, wherein the lower end gas distributor (211) is a cyclonic propulsion gas distributor (212) comprising a lower end breather pipe (210) and a cyclonic propulsion gas distributor turbine (214) disposed at an outlet of the lower end breather pipe (210).
7. The airlift bioreactor as claimed in claim 6, characterized in that radial opening radial rotary blades are uniformly distributed in the cyclone propulsion type gas distributor turbine (214), and a cyclone propulsion type gas distributor blade (213) for pushing fluid to ascend axially is connected to the upper end of the cyclone propulsion type gas distributor turbine (214); or,
the gas distributor turbine (214) is comprised of several tangential flow gas distributor nozzles (215).
8. The airlift bioreactor of claim 6, wherein the cyclonic propulsion gas distributor (212) is a magnetic levitation gas distributor.
9. Airlift bioreactor as claimed in claim 1, characterized in that the rim propeller (400) is a magnetically levitated propeller.
10. Airlift bioreactor as claimed in claim 1, characterized in that the bottom of the tank (100) is provided with a flow guide cone (603), and/or,
a plurality of porous sieve plates (602) are arranged in the tank body (100).
11. The airlift bioreactor as claimed in claim 10, characterized in that a plurality of vortex deflectors (601) are arranged in the liquid lifting zone (302) and the liquid lowering zone (303) of the tank body (100), and/or,
A spoiler (600) is arranged above the guide cylinder (200).
12. The airlift bioreactor as claimed in claim 2, characterized in that the rim propeller (400) is an outer rotor rim propeller, the rim propeller rotor (403) is sleeved outside the rim propeller stator (402), and the rim propeller blades (401) are defoaming paddles (220).
13. The airlift bioreactor as claimed in claim 2, characterized in that the rim propeller rotor (403) and the rim propeller stator (402) together form an impeller, the inside of the impeller is designed into a cavity and becomes a self-priming impeller, the internal cavity of the impeller is communicated with the lower end of a rim propeller fixing tube (406), the upper end of the rim propeller fixing tube (406) is provided with a suction hole (219), and the upper end of the rim propeller fixing tube (406) is fixed at the inner top of the tank body (100).
14. The airlift bioreactor as claimed in claim 1, characterized in that a light source or an array of light sources is provided within the tank (100) for light fermentation, the light source or the array of light sources being arranged on a baffle (601), an inner and outer wall of the guide cylinder (200), an inner wall of the outer circulation pipe (101) or an inner wall of the tank (100); or,
An electrode is arranged in the tank body (100) and is used for electric fermentation.
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| CN202311758510.0A CN117757595A (en) | 2023-12-20 | 2023-12-20 | Gas-lift type bioreactor for strengthening liquid flow circulation |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202311758510.0A CN117757595A (en) | 2023-12-20 | 2023-12-20 | Gas-lift type bioreactor for strengthening liquid flow circulation |
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| CN117757595A true CN117757595A (en) | 2024-03-26 |
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| CN202311758510.0A Pending CN117757595A (en) | 2023-12-20 | 2023-12-20 | Gas-lift type bioreactor for strengthening liquid flow circulation |
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- 2023-12-20 CN CN202311758510.0A patent/CN117757595A/en active Pending
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