CN117187030B - Fermentation reaction kettle, corresponding fermentation system and application thereof - Google Patents
Fermentation reaction kettle, corresponding fermentation system and application thereof Download PDFInfo
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- Apparatus Associated With Microorganisms And Enzymes (AREA)
Abstract
The invention provides a fermentation reaction kettle, a corresponding fermentation system and application thereof, and belongs to the field of bioengineering. The fermentation reaction kettle comprises a reaction kettle body and a gas distributor accommodated in the reaction kettle body, wherein the gas distributor comprises an annular pipe body, and a plurality of nozzles with upward openings and a plurality of gas distribution holes with downward openings are arranged on the annular pipe body. By the aid of the gas distributor, fermentation liquid can be continuously replaced and circulated in the diffusion accelerating area, gas-liquid contact area is increased, liquid drop particle size is refined, gas-liquid mass transfer effect is enhanced, input of ventilation and stirring work and foaming problems caused by the input of ventilation and stirring work are reduced, fermentation efficiency and yield are improved, and the gas distributor has a good application prospect.
Description
Technical Field
The invention belongs to the field of bioengineering, and particularly relates to a fermentation reaction kettle, a fermentation system comprising the fermentation reaction kettle and application of the fermentation system.
Background
Rhamnolipid has been widely used in the fields of cosmetics, foods, pharmacy, petrochemical industry, agriculture and the like by virtue of the advantages of excellent surface/interfacial activity, good emulsifying, dispersing and solubilizing capabilities, no toxicity, biodegradability and the like, and becomes one of the biosurfactants with the most application prospects at present.
At present, the industrial rhamnolipid is produced mainly by taking vegetable oil as a carbon source and carrying out aerobic fermentation on pseudomonas aeruginosa. Because the fermentation process is a gas-liquid reaction, in order to meet the high dissolved oxygen and good dispersion performance of oil-water two phases required by pseudomonas aeruginosa, higher ventilation and stirring conditions need to be maintained. The stirring speed is increased, so that the liquid dispersion performance can be improved, and the gas exchange frequency can be improved, but when the stirring speed is too high, stronger shearing stress can be generated, and damage to microorganisms is caused. The ventilation volume is increased, so that the disturbance of fermentation liquid is increased, the oxygen transfer is facilitated, but rhamnolipid is used as an anionic surfactant, a large amount of foam can be generated in a fermentation system under the addition of ventilation and stirring, and various negative effects can be generated on the fermentation process if the foam is not eliminated in time; on one hand, the utilization rate of the fermentation tank can be greatly reduced due to excessive foaming, foam escape can be caused due to untimely defoaming, and the problem of bacteria contamination is easy to occur; on the other hand, excessive aeration can cause the growth rate of the thallus to increase, gel with the microbubbles, generate structural viscosity, influence the metabolism of the thallus and cause fermentation failure.
At present, the foaming problem in the production process of rhamnolipid is relieved by a physical defoaming method, a mechanical defoaming method and a chemical defoaming method in industry, but the material defoaming and mechanical defoaming effects are not obvious; the chemical defoaming such as adding a defoaming agent is more applied at present, but the defoaming agent is unreasonable to be used, so that bacteria are easy to be dyed, the problem of removing the defoaming agent needs to be considered, and the requirement on the subsequent separation flow is relatively high. The scholars consider that the fermentation raw material vegetable oil can be used as a carbon source and has a certain defoaming effect, but when the system is provided with a large number of bubbles, the defoaming effect of the vegetable oil is not obvious, and the use of a large number of vegetable oils can cause vegetable oil residues in the later stage of fermentation, so that emulsification phenomenon is generated, and the subsequent separation and extraction of rhamnolipid are not facilitated. In the chinese patent document CN111118088B, a manner of adjusting pH and pressure of the fermentation tank in stages is adopted to slow down bubble generation, and although the manner can slow down bubble problem to a certain extent, in the fermentation process, as concentration of rhamnolipid in the system increases, particle size of bubbles gradually decreases, and becomes fine small bubbles, stability of bubbles continuously increases, and efficient defoaming cannot be achieved simply by adjusting pH and pressure of the fermentation tank. In addition, the partial pressure of carbon dioxide in the system is increased at the same time due to the increase of the tank pressure, and the pH of the fermentation liquor is reduced due to the fact that the solubility of the carbon dioxide in water is far higher than that of oxygen, so that the carbon dioxide is toxic to microorganisms. Still other scholars adopt adding hemoglobin to fermentation broth to enhance oxygen mass transfer or rich or pure oxygen fermentation, and although the degree of dependence on aeration and stirring is reduced, the hemoglobin is unfavorable for thallus growth and product accumulation, and has amplification effect; in addition, the ideas of low-oxygen fermentation, solid state fermentation and the like are sequentially proposed, but the yield is very low, the amplification is difficult, and the fermentation efficiency is very low.
Although rhamnolipid has more advantages compared with other traditional surfactants, the method has many problems in the industrialized amplification process, such as dissolved oxygen demand, low yield, serious foaming, difficult control and the like, and how to design an efficient fermentation system to ensure high dissolved oxygen, inhibit foaming and improve yield is a problem which needs to be solved rapidly in the industrialized amplification of rhamnolipid at present.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a fermentation reaction kettle, a corresponding fermentation system and application thereof. In the fermentation reaction kettle, the gas distributor with a specific structure is adopted, so that the replacement circulation of fermentation liquid can be realized, the gas-liquid contact area can be increased, the ventilation capacity can be reduced, and the yield can be improved.
In a first aspect, the present invention provides a fermentation reactor.
The fermentation reaction kettle comprises: the reaction kettle comprises a reaction kettle body and a gas distributor accommodated in the reaction kettle body, wherein the gas distributor comprises an annular pipe body, and a plurality of nozzles with upward openings and a plurality of gas distribution holes with downward openings are arranged on the annular pipe body.
In some embodiments, the diameter of the gas distribution holes is less than the diameter of the nozzles.
In some embodiments, the interior of the reaction kettle body is provided with a stirring device positioned above the gas distributor and a heat exchanger fixed on the inner side wall of the reaction kettle body, wherein the stirring device is used for uniformly mixing materials in the reaction kettle body, and in some preferred embodiments, the stirring device is a stirring paddle; the heat exchanger is used for exchanging heat with materials in the fermentation reaction kettle so as to maintain the temperature in the fermentation reaction kettle constant; in some preferred embodiments, the heat exchanger is selected from an inner coil, a coil, or a vertical coil.
In a second aspect, the present invention provides a fermentation system.
The fermentation system comprises the fermentation reaction kettle and a feeding system, wherein the fermentation reaction kettle is connected with the feeding system.
In some embodiments, the feed system comprises a gas phase feed system comprising an air compressor and an air filter, the air compressor connected to the air filter by a conduit, the air filter connected to the gas distributor by a conduit through a gas phase feed port of the fermentation reactor;
In some preferred embodiments, the feed system further comprises a liquid phase feed system comprising a liquid phase injection section, a liquid phase mixing section, a gas-liquid mixing section, and a secondary mixing injection section connected in sequence, wherein:
the liquid phase spraying section comprises a first venturi tube, the liquid phase mixing section comprises a static mixer, and the first venturi tube is connected with the static mixer;
the gas-liquid mixing section comprises a gas-liquid mixing chamber, the gas-liquid mixing chamber comprises a first diameter reduction section connected with the static mixer and a first straight pipe section with the front end connected with the first diameter reduction section, the tail end of the first straight pipe section is connected with the secondary mixing injection section, and in some more preferred embodiments, the distance between the minimum diameter reduction position of the first diameter reduction section and the tail end of the static mixer is 300-400mm; in some further preferred embodiments, the gas-liquid mixing chamber is provided with a gas phase inlet;
the secondary mixing injection section comprises a second diameter-reducing section and a second straight pipe section which are communicated, the front end of the second diameter-reducing section is connected with the gas-liquid mixing chamber, and a plurality of injection holes are arranged at the tail end of the second straight pipe section and are connected with a fermentation raw material feeding port of the fermentation reaction kettle through a pipeline.
In some embodiments, the liquid phase injection section further comprises a first feedstock inlet connected to the top of the first venturi tube and a second feedstock inlet connected to the reduced diameter of the first venturi tube, the first feedstock inlet having a feed direction parallel to the axial direction of the first venturi tube, the second feedstock inlet having a feed direction at an angle to the axial direction of the first venturi tube, in some preferred embodiments in the range of 0 ° -90 °, in some more preferred embodiments the angle is 90 °; the side wall of the gas-liquid mixing chamber is provided with a plurality of gas spray holes, in some preferred embodiments, the gas spray holes are arranged on the side wall of the gas-liquid mixing chamber in a row, and in some more preferred embodiments, the total area of the gas spray holes is 0.5% -2% of the sectional area of the gas phase inlet; one end of the gas phase inlet is connected with the first diameter-reducing section of the gas-liquid mixing chamber, and a gas phase diversion hole is also arranged on the gas phase inlet; the other end of the gas phase inlet is connected with the air filter through a pipeline.
In some embodiments, the fermentation system further comprises a liquid phase circulation on-line separation system, the liquid phase circulation on-line separation system comprises a first circulation pump, a second venturi tube, a first separation device and a second separation device, the fermentation reaction kettle, the first circulation pump, the second venturi tube, the first separation device and the second separation device are sequentially connected through pipelines, and the first separation device is used for separating fermentation thalli from fermentation liquor in the fermentation reaction kettle; in some preferred embodiments, the first separation device is selected from a butterfly centrifuge, a decanter centrifuge, a ceramic membrane, or an organic membrane, in some more preferred embodiments, the first separation device is a ceramic membrane; the second separation device is used for separating the fermentation liquid passing through the first separation device to obtain a fermentation product and a filtrate, and in some preferred embodiments, the second separation device is selected from an adsorption column, a chromatographic column or an extraction device, and in some more preferred embodiments, the second separation device is an adsorption column.
In some embodiments, the liquid phase circulation on-line separation system further comprises a second circulation pump, wherein the middle part of the second venturi tube is connected with the foam outlet of the fermentation reaction kettle through a pipeline, and the second venturi tube is used for crushing foam from the fermentation reaction kettle; one end of the second circulating pump is connected with the first separation device through a pipeline, the other end of the second circulating pump is connected with a circulating liquid reflux port of the fermentation reaction kettle, and the second circulating pump is used for refluxing fermentation thalli separated by the first separation device into the fermentation reaction kettle; the second separation device is connected with the fermentation reaction kettle and is used for refluxing the filtrate separated by the second separation device into the fermentation reaction kettle; the first circulation pump and the second circulation pump are each selected from a centrifugal pump, a canned motor pump, or a diaphragm pump.
In a third aspect, the invention provides the use of a fermentation system as defined in any one of the preceding claims for the preparation of an aerobic fermentation product.
In some preferred embodiments, the aerobic fermentation product is rhamnolipid.
In some embodiments, the application comprises:
inoculating strain seed liquid into a fermentation reaction kettle for continuous aerobic fermentation culture, and under the action of a first circulating pump, sequentially passing fermentation liquor obtained by the continuous aerobic fermentation culture through a second venturi tube, a first separation device and a second separation device, wherein the second venturi tube breaks foam in the fermentation liquor; the first separation device separates fermentation thalli in the fermentation liquor, and the fermentation thalli flows back to the fermentation reaction kettle under the action of a second circulating pump; the second separation device separates aerobic fermentation products in the fermentation liquor, and the obtained filtrate flows back to the fermentation reaction kettle;
optionally, the method further comprises the step of purifying the aerobic fermentation product.
In the present invention, the aerobic fermentation product is a fermentation product which is conventional in the art and can be obtained by aerobic fermentation of a strain, for example, the aerobic fermentation product may be rhamnolipid.
In some embodiments, when the fermentation system is used to produce rhamnolipids, the species is a species that can produce rhamnolipids by fermentation, including, but not limited to, pseudomonas aeruginosa.
In some embodiments, when the above fermentation system is used to produce rhamnolipids, the fermentation reactor is added with a fermentation medium and a fermentation feedstock; preferably, the fermentation raw material is continuously added through a liquid phase feeding system in the continuous aerobic fermentation culture process; more preferably, the fermentation feedstock is preferably a liquid phase feedstock, preferably a carbon source and a nitrogen source; even more preferably, the carbon source is preferably a vegetable oil and the nitrogen source is preferably a yeast powder; and/or the number of the groups of groups,
the parameters of the continuous aerobic fermentation culture include: the fermentation temperature is 20-45 ℃, the initial ventilation is 0.1-2vvm, the stirring rotation speed is 50-300rpm, and the fermentation time is 18-24 hours; then, the feeding amount of air and the feeding amount of fermentation raw materials in the fermentation reaction kettle need to be adjusted; wherein, air enters the fermentation reaction kettle and the gas-liquid mixing chamber, after fermentation raw materials are sprayed by a first venturi tube and mixed in a static mixer in sequence, the mixed gas enters a gas-liquid mixing chamber, is mixed with air in the gas-liquid mixing chamber, and is sprayed into a stirring device in the middle of the fermentation reaction kettle through a secondary mixing spraying section; and/or the number of the groups of groups,
And after fermenting for 8-10 days, stopping feeding, and stopping the continuous aerobic fermentation to obtain rhamnolipid.
In some embodiments, the total feed of the fermentation feedstock is 0.48kg/h, wherein the feed ratio of the carbon source to the nitrogen source is 1:0.5 to 1:2, and in some more preferred embodiments, the feed ratio is 1:1; the said spaceThe gas feed amount is 4-7Nm 3 And/h, wherein the air feed to the gas distributor is 70-90% of the total air feed, and in some more preferred embodiments, 80% of the total air feed; the temperature during fermentation is from 20 to 45 ℃, and in some more preferred embodiments, the temperature during fermentation is from 25 to 35 ℃.
Compared with the prior art, the invention has the following beneficial effects:
1) The improved gas distributor is adopted, and through the cooperation of the nozzles and the gas distribution holes on the improved gas distributor, the fermentation liquid can be continuously circulated in the diffusion accelerating zone, so that the gas-liquid contact area is increased, the particle size of liquid drops is thinned, the gas-liquid mass transfer effect is enhanced, and the ventilation capacity, the input of stirring work and the foaming problem generated by the process are reduced;
2) In some preferred embodiments, the invention adopts a liquid phase feeding system, utilizes a mode of combining static mixing and Venturi effect to fully mix non-intersoluble raw materials to form small liquid drops, and further enhances the contact of gas phase and liquid phase through uniform gas atomization to strengthen mass transfer in the fermentation process;
3) In some preferred embodiments, a low-flow fermentation liquor circulation system is adopted, on one hand, the online separation of products is realized, the foaming rate and the foam stability of a fermentation system are reduced, and the foaming problem of the system is relieved; on the other hand, the venturi suction realizes automatic elimination of top-layer foam, accelerates the foam breaking rate of the foam, realizes online foam separation, and avoids low utilization rate of the fermentation reaction kettle caused by untimely foaming and defoaming;
4) In some preferred embodiments, the technology of coupling foam on-line separation and fermentation is adopted, so that the problems of foaming and product inhibition are reduced, the yield is improved, the production integration is realized, and the production cost is reduced.
Drawings
FIG. 1 is a schematic diagram of a fermentation system of the present invention;
FIG. 2 is a schematic diagram of the gas distributor in the fermentation system of the present invention;
FIG. 3 is a schematic diagram of the liquid phase feed system in the fermentation system of the present invention;
FIG. 4 is a schematic view of a conventional loop distributor in a fermentation system of the present invention;
wherein the reference numerals have the following meanings: 1. a reaction kettle body; 2. an air compressor; 3. an air filter; 4. a liquid phase feed system; 41. a liquid phase injection section; 411. a first venturi tube; 412. a first feedstock inlet; 413. a second feedstock inlet; 42. a liquid phase mixing section; 421. a static mixer; 43. a gas-liquid mixing section; 431. a gas-liquid mixing chamber; 4311. a first reduced diameter section; 4312. a first straight pipe section; 4313. a gas jet orifice; 432. a gas phase inlet; 4321. a gas phase diversion hole; 44. a secondary mixing and spraying section; 441. a second reduced diameter section; 442. a second straight tube section; 4421. an injection hole; 5. a heat exchanger; 6. a gas distributor; 61. a nozzle; 62. gas distribution holes; 7. a stirring device; 8. a first circulation pump; 9. a second venturi tube; 10. a first separation device; 11. a second circulation pump; 12. a second separation device; 13. defoaming electrodes; 14. a circulating water supply pipe; 15. and a circulating water return pipe.
Detailed Description
Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative and intended to explain the present invention and should not be construed as limiting the invention.
In the description of the present invention, it should be noted that the positional or positional relationship indicated by the terms such as "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", "bottom", "top", etc. are based on the positional or positional relationship shown in the drawings, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the apparatus or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Unless specifically stated or limited otherwise, the terms "mounted," "connected," and "fixed" are to be construed broadly, and may be, for example, either fixed or removable; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
The experimental methods for which specific conditions are not specified in the examples are generally commercially available according to conventional conditions and those described in handbooks, or according to conditions recommended by the manufacturer, using general-purpose equipment, materials, reagents, etc., unless otherwise specified.
As shown in fig. 1-3, the invention provides a fermentation reaction kettle, which comprises a reaction kettle body 1 and a gas distributor 6 accommodated in the reaction kettle body 1, wherein the gas distributor 6 comprises an annular pipe body, and a plurality of nozzles 61 with upward openings and a plurality of gas distribution holes 62 with downward openings are arranged on the annular pipe body.
Specifically, through the cooperation of the nozzles 61 with upward openings and the gas distribution holes 62 with downward openings, the fermentation liquid is promoted to continuously circulate in the diffusion accelerating zone, so that the fermentation liquid is fully contacted with air, and the gas-liquid mass transfer effect is enhanced. In addition, in the present invention, the annular tube body is provided with 4 nozzles 61 with upward openings, but is not limited thereto, and the number of the nozzles 61 and the gas distribution holes 62 on the annular tube body may be adjusted according to actual use requirements.
Further, the diameter of the gas distribution holes 62 is smaller than the diameter of the nozzles 61.
Specifically, the openings of the gas distribution holes 62 are arranged downwards, and the diameter of the gas distribution holes is smaller than that of the nozzles 61, so that the problem that the materials in the fermentation liquid fall into the gas distribution holes 62 to cause hole blockage can be avoided.
Further, a stirring device 7 positioned above the gas distributor 6 and a heat exchanger 5 fixed on the inner side wall of the reaction kettle body 1 are arranged in the reaction kettle body 1, wherein the stirring device 7 is used for uniformly mixing materials in the reaction kettle body 1, preferably, the stirring device 7 is a stirring paddle, and the heat exchanger 5 is used for exchanging heat with the materials in the reaction kettle body 1 so as to maintain the temperature in the reaction kettle body 1 constant; preferably, the heat exchanger 5 is selected from an inner coil, a coil or a vertical coil.
Specifically, the stirring device 7 ensures that the fermentation liquid is uniformly mixed, thereby facilitating fermentation and improving yield; the heat exchanger 5 can remove the fermentation heat in time, and maintain the constant fermentation temperature.
In addition, the upper end socket of the reaction kettle body 1 in the fermentation reaction kettle is provided with a stirring device port, a defoaming electrode port and an exhaust port, the lower end socket is provided with a fermentation liquid outlet, a straight cylinder section of the tank body is respectively provided with a circulating water return pipe orifice, a circulating water upper water pipe orifice, a foam outlet, a circulating liquid return port, a fermentation raw material feed port and a gas phase feed port from top to bottom, wherein the stirring device port is used for fixedly mounting the stirring device, the defoaming electrode port is used for fixedly mounting the defoaming electrode, the exhaust port is used for timely exhausting gas in the reaction kettle body 1, the fermentation liquid outlet is used for exhausting small-flow fermentation liquid, and the circulating water return pipe orifice and the circulating water upper water pipe orifice are used for introducing water into the heat exchanger 5 and exchanging heat with the fermentation liquid to maintain the temperature in the reaction kettle body 1 constant. And the reaction kettle body 1 is also provided with instrument monitoring pipe orifices such as temperature, liquid level, pH, dissolved oxygen and the like. The above-mentioned settings are all conventional in the art, and in addition, other necessary settings may be performed to meet the fermentation requirements according to actual use needs.
Further, the invention provides a fermentation system. The fermentation system comprises any one of the fermentation reaction kettles and a feeding system, and the fermentation reaction kettles are connected with the feeding system.
Further, the feeding system comprises a gas-phase feeding system, the gas-phase feeding system comprises an air compressor 2 and an air filter 3, the air compressor 2 is connected with the air filter 3 through a pipeline, and the air filter 3 is connected with the gas distributor 6 through a pipeline through a gas-phase feeding port of a reaction kettle body 1 in the fermentation reaction kettle.
Specifically, air is compressed by the air compressor 2, filtered in the air filter 3, and then is introduced into the gas distributor 6 through a pipeline, and is ejected from the gas distribution holes 62 and the nozzles 61 on the modified gas distributor 6, so as to provide oxygen demand of fermentation bacteria.
Further, the feeding system further comprises a liquid phase feeding system 4, the liquid phase feeding system 4 comprises a liquid phase injection section 41, a liquid phase mixing section 42, a gas-liquid mixing section 43 and a secondary mixing injection section 44 which are connected in sequence, wherein: the liquid-phase spraying section 41 includes a first venturi tube 411, the liquid-phase mixing section 42 includes a static mixer 421, and the first venturi tube 411 is connected to the static mixer 421;
The gas-liquid mixing section 43 comprises a gas-liquid mixing chamber 431, the gas-liquid mixing chamber 431 comprises a first diameter-reducing section 4311 connected with the static mixer 421 and a first straight pipe section 4312 with the front end connected with the first diameter-reducing section 4311, and the tail end of the first straight pipe section 4312 is connected with the secondary mixing injection section 44; more preferably, the minimum diameter reduction of the first diameter reduction section 4311 is 300-400mm from the end of the static mixer 421, which may be 300mm, 310mm, 320mm, 330mm, 340mm, 350mm, 360mm, 370mm, 380mm, 390mm, 400mm or other values within this range, for example; further preferably, the gas-liquid mixing chamber 431 is provided with a gas phase inlet 432;
the secondary mixing injection section 44 comprises a second diameter-reducing section 441 and a second straight pipe section 442 which are communicated, the front end of the second diameter-reducing section 441 is connected with a gas-liquid mixing chamber 431, and the tail end of the second straight pipe section 442 is provided with a plurality of injection holes 4421 and is connected with a fermentation raw material feed inlet of the reaction kettle body 1 in the fermentation reaction kettle through a pipeline.
Specifically, the fermentation raw materials are primarily mixed in the first venturi 411, after passing through the static mixer 421, the fermentation raw materials are further fully dispersed and mixed, and then enter the gas-liquid mixing chamber 431, and after being mixed with the air entering from the gas phase inlet 432, enter the second diameter reducing section 441 of the secondary mixing injection section 44 from the gas-liquid mixing chamber 431, at this time, the flow speed of the gas-liquid mixture is changed, the shearing is enhanced, the remixing is realized, the gas-liquid mixture is sprayed out through the spraying hole 4421 on the second straight pipe section 442 and enters the reaction kettle body 1 in the fermentation reaction kettle, and when the gas-liquid mixture passes through the spraying hole 4421, the particle size of the material is further reduced due to the pressure change, and the materialized particles with smaller and uniform particle size are obtained.
Further, the liquid-phase injection section 41 further includes a first raw material inlet 412 and a second raw material inlet 413, the first raw material inlet 412 is connected to the top of the first venturi 411, the second raw material inlet 413 is connected to the diameter-reduced portion of the first venturi 411, the feeding direction of the first raw material inlet 412 is parallel to the axial direction of the first venturi 411, and the feeding direction of the second raw material inlet 413 forms a certain angle with the axial direction of the first venturi 411, preferably, the angle ranges from 0 ° to 90 °, for example, may be 10 °, 20 °, 30 °, 40 °, 50 °, 60 °, 70 °, 80 °, 90 ° or other values within the range. More preferably, the angle is 90 °; a plurality of gas spray holes 4313 are arranged on the side wall of the gas-liquid mixing chamber 431, preferably, the gas spray holes 4313 are arranged on the side wall of the gas-liquid mixing chamber 431 in a row, and more preferably, the total area of the gas spray holes 4313 is 0.5% -2% of the sectional area of the gas phase inlet 432; one end of the gas phase inlet 432 is connected with a first diameter-reducing section 4311 of the gas-liquid mixing chamber 431, and a gas phase diversion hole 4321 is also arranged on the gas phase inlet 432; the other end of the gas phase inlet 432 is connected to the air filter 3 by a pipe.
Specifically, a part of the air entering the gas phase inlet 432 directly enters the first diameter-reducing section 4311 of the gas-liquid mixing chamber 431 and is mixed with the liquid-phase material entering the gas-liquid mixing chamber 431; the other part enters the hollow cavity in the gas-liquid mixing section 43 through the gas-phase diversion hole 4321, and enters the gas-liquid mixing chamber 431 through the gas spray hole 4313 on the side wall of the gas-liquid mixing chamber 431 to further enhance the mixing between the gas and the liquid phase materials. In addition, the gas spraying holes 4313 in the invention can be round or square, and a person skilled in the art can perform corresponding arrangement according to actual use requirements.
Further, the fermentation system further comprises a liquid-phase circulation on-line separation system, the liquid-phase circulation on-line separation system comprises a first circulation pump 8, a second venturi tube 9, a first separation device 10 and a second separation device 12, the reaction kettle body 1, the first circulation pump 8, the second venturi tube 9, the first separation device 10 and the second separation device 12 in the fermentation reaction kettle are sequentially connected through pipelines, the first separation device 10 is used for separating fermentation thalli from fermentation broth in the reaction kettle body 1 in the fermentation reaction kettle, preferably, the first separation device 10 is selected from a butterfly centrifuge, a horizontal decanter centrifuge, a ceramic membrane or an organic membrane, more preferably, the first separation device 10 is a ceramic membrane; the second separation device 12 is used for separating the fermentation liquid passing through the first separation device 10 to obtain a fermentation product and a filtrate, preferably the second separation device 12 is selected from an adsorption column, a chromatographic column or an extraction device, more preferably the second separation device 12 is an adsorption column.
Specifically, under the action of the first circulating pump 8, the fermentation liquor with small flow passes through the first separating device 10, the second venturi tube 9 and the second separating device 12 in sequence through the fermentation liquor outlet on the lower seal head of the reaction kettle body 1 in the fermentation reaction kettle, and then the fermentation products in the fermentation liquor are separated to a certain extent, so that the stability contribution of the fermentation liquor to foam is reduced, and the foaming generation is reduced.
Further, the liquid phase circulation on-line separation system also comprises a second circulation pump 11, the middle part of a second venturi tube 9 is connected with a foam outlet of the reaction kettle body 1 in the fermentation reaction kettle through a pipeline, and the second venturi tube 9 is used for crushing foam from the reaction kettle body 1 in the fermentation reaction kettle; one end of a second circulating pump 11 is connected with the first separating device 10 through a pipeline, the other end of the second circulating pump 11 is connected with a circulating liquid reflux port of the reaction kettle body 1 in the fermentation reaction kettle, and the second circulating pump 11 is used for refluxing the fermentation thalli separated by the first separating device 10 to the reaction kettle body 1 in the fermentation reaction kettle for reuse; the second separation device 12 is connected with the reaction kettle body 1 in the fermentation reaction kettle, and is used for refluxing the filtrate separated by the second separation device 12 into the reaction kettle body 1 in the fermentation reaction kettle for reuse; the first circulation pump 8 and the second circulation pump 11 are each selected from a centrifugal pump, a canned motor pump, or a diaphragm pump.
Specifically, through the effect of second venturi 9, the foam layer is sucked to the inside of sprayer and broken bubble in the reation kettle body 1 top in the fermentation reaction kettle, has played the defoaming effect, reduces the foam layer height in the reation kettle body 1 in the fermentation reaction kettle, makes the utilization ratio of reation kettle body 1 in the fermentation reaction kettle further promote.
Furthermore, the invention also provides application of the fermentation system in preparation of an aerobic fermentation product, preferably rhamnolipid.
Further, the application includes:
inoculating the strain seed liquid into a reaction kettle body 1 in a fermentation reaction kettle added with a fermentation medium and fermentation raw materials for continuous aerobic fermentation culture, wherein the fermentation raw materials are preferably continuously added through a liquid phase feeding system 4 in the continuous aerobic fermentation culture process; under the action of a first circulating pump 8, the fermentation liquor obtained by continuous aerobic fermentation culture sequentially passes through a second venturi tube 9, a first separation device 10 and a second separation device 12, wherein the second venturi tube 9 breaks foam in the fermentation liquor; the first separation device 10 separates fermentation thalli in the fermentation broth, and the fermentation thalli flows back to the reaction kettle body 1 in the fermentation reaction kettle under the action of the second circulating pump 11; the second separating device 12 separates the aerobic fermentation product in the fermentation broth, and the obtained filtrate flows back to the reaction kettle body 1 in the fermentation reaction kettle;
optionally, the method further comprises the step of purifying the aerobic fermentation product.
Specifically, when the above fermentation system is used for producing rhamnolipids, the fermentation raw material is preferably a liquid-phase raw material, and the liquid-phase raw material is preferably a carbon source and a nitrogen source; the carbon source is preferably vegetable oil, and the nitrogen source is preferably yeast powder; and parameters of the continuous aerobic fermentation culture include: the fermentation temperature is 20-45 ℃, the initial ventilation is 0.1-2vvm, the stirring rotation speed is 50-300rpm, and the fermentation time is 18-24 hours; then, adjusting the feeding amount of air and the feeding amount of fermentation raw materials in the reaction kettle body 1 entering the fermentation reaction kettle; wherein, after air passes through the air compressor 2 and the air filter 3, part of the air enters the reaction kettle body 1 of the fermentation reaction kettle and the gas-liquid mixing chamber 431, the fermentation raw material sequentially passes through the first venturi tube 411 to be sprayed and mixed with the static mixer 421, then enters the gas-liquid mixing chamber 431, is mixed with the air in the gas-liquid mixing chamber 431, and is sprayed into the middle stirring device 7 of the reaction kettle body 1 of the fermentation reaction kettle through the secondary mixing spraying section 44; and after fermenting for 8-10 days, stopping feeding, and stopping the continuous aerobic fermentation to obtain rhamnolipid.
Further, the total feed amount of the fermentation raw material is 0.48kg/h, wherein the feed ratio of the carbon source to the nitrogen source is 1:0.5-1:2, and more preferably, the feed ratio of the carbon source to the nitrogen source is 1:1; if the carbon source is excessively added, the pH is reduced, the metabolism of thalli is not facilitated, the residual oil content is increased, and the fermentation liquid is emulsified; if the nitrogen source content is high, the overall pH is higher, so that the viscosity of the system is increased, and the fermentation and post-treatment processes are not facilitated.
The air feed amount was 4-7Nm 3 And/h, wherein the air feed amount entering the gas distributor 6 accounts for 70-90% of the total air feed amount, and more preferably, the air feed amount entering the gas distributor 6 accounts for 80% of the total air feed amount; the temperature during fermentation is 20-45 ℃, more preferably 25-35 ℃. If the temperature is low, the metabolism of thalli becomes slow, and the fermentation period is prolonged; if the temperature is high and exceeds the suitable growth environment for the cells, the cells tend to die.
Specifically, in the continuous aerobic fermentation culture process, the heat exchanger 5 is timely opened according to actual needs, heat generated in the fermentation process is timely removed, and the fermentation temperature is kept constant.
The fermentation system of the present invention will be further described with specific examples of the preparation of rhamnolipids.
Example 1
1) Inoculating pseudomonas aeruginosa KT1115 (purchased from China Center for Type Culture Collection (CCTCC) M2016686) into a seed culture medium (10 g/L of peptone, 5g/L, naCl g/L of yeast powder and the balance of water) by using an inoculating loop, and culturing for 20 hours at a fermentation temperature of 35 ℃ and a rotating speed of 180rpm to obtain seed liquid;
2) Inoculating the seed solution obtained in step 1) to 310L containingFermentation medium (vegetable oil 80.0g/L, KH) 2 PO 4 4.0g/L、K 2 HPO 4 6.0g/L、NaNO 3 3g/L、NaCl 1.1g/L、KCl 1.1g/L、MgSO 4 ·7H 2 O0.2 g/L, pH:7.0, microelement solution 5ml/L (microelement solution composition (g/L): feSO) 4 ·7H 2 O 12、 ZnSO 4 ·7H 2 O 3.0、CoSO 4 ·7H 2 O 1.0、MnSO 4 ·2H 2 O3.0)), the fermentation culture is carried out in the reaction kettle body 1 (liquid loading amount 40%), the fermentation temperature is 35 ℃, the initial ventilation amount is 1.5vvm, the stirring rotation speed is 200rpm, the fermentation culture is carried out for 24 hours, and the yeast powder and the vegetable oil are continuously added through the liquid phase feeding system 4 in the fermentation culture process; under the action of a first circulating pump 8, fermentation liquor obtained through continuous aerobic fermentation culture sequentially passes through a second venturi tube 9, a first separation device 10 and a second separation device 12, wherein the second venturi tube 9 breaks foam in the fermentation liquor; the first separation device 10 separates fermentation thalli in the fermentation liquor, and the fermentation thalli flows back to the reaction kettle body 1 under the action of the second circulating pump 11; the second separating device 12 separates and discharges rhamnolipid, a fermentation product, in the fermentation broth from the bottom of the reaction kettle body 1, and the obtained filtrate flows back to the reaction kettle body 1;
3) The total feeding amount of vegetable oil and yeast powder is regulated to be 0.48kg/h, the feeding ratio of the vegetable oil to the yeast powder is 1:1, and the air feeding amount is regulated to be 4Nm 3 And/h, wherein the air feed amount entering the gas distributor 6 accounts for 80% of the total air feed amount, the fermentation temperature is 35 ℃, and the stirring rotation speed is 150rpm;
4) And (3) no antifoaming agent is added in the fermentation process, continuous fermentation is carried out for 9 days under the condition, feeding is stopped, and fermentation is stopped after the residual oil is basically consumed.
The liquid level of the fermentation end point is observed to be 70%, and the yield of the rhamnolipid reaches 92g/L through detection.
Example 2
The fermentation process was basically the same as in example 1, except that the liquid phase feed was not conducted by the liquid phase feed system 4, but directly fed from the fermentation raw material feed port on the reaction vessel body 1 in the fermentation reaction vessel, the fermentation temperature was 35 ℃, aeration and stirring were adjusted according to dissolved oxygen and residual oil, and the other fermentation processes were the same as in example 1.
The aeration rate required to maintain the same dissolved oxygen and residual oil level during the feeding stage of vegetable oil and yeast powder was 6Nm 3 And/h, the stirring speed is 200rpm, the fermentation end point liquid level height is 70%, and the yield of the rhamnolipid reaches 91g/L through detection.
Example 3
The fermentation process was essentially identical to example 1, except that the gas phase feed was not fed by means of a gas distributor 6, but instead by means of a conventional loop distributor (see fig. 4, in which the gas distribution holes were open in the upward direction), the fermentation temperature was 35 ℃, aeration and stirring were adjusted according to dissolved oxygen and residual oil, defoamer was added selectively according to the foam layer height, and the other fermentation processes were identical to example 1.
The aeration rate required for the vegetable oil and yeast powder feeding stage to maintain the same dissolved oxygen and residual oil level in the process was 8Nm 3 And/h, stirring at 200rpm, and adding an antifoaming agent (bubble enemy, available from Nantong Jinlai chemical industry Co., ltd., product catalog number FAG 375) to the mixture to obtain about 0.1kg/kg rhamnolipid, wherein the fermentation end point liquid level is 65%, and the yield of rhamnolipid reaches 90.5g/L.
Example 4
The fermentation process was essentially identical to example 1, except that no liquid-phase circulation on-line separation system was employed, the fermentation temperature was 35 ℃, aeration and stirring were adjusted according to dissolved oxygen and residual oil, defoamer was selectively added according to the foam layer height, and the other fermentation processes were identical to example 1.
The aeration rate required for maintaining the same dissolved oxygen and residual oil level during the feeding stage of vegetable oil and yeast powder was 4Nm 3 And/h, the stirring speed is 150rpm, and meanwhile, about 0.05kg/kg of rhamnolipid needs to be supplemented, the fermentation end point liquid level height is 65%, and the yield of rhamnolipid reaches 89g/L through detection.
Comparative example
The traditional fermentation reaction is adopted to produce rhamnolipid, vegetable oil and yeast powder feed respectively enter a reaction kettle body 1 in a fermentation reaction kettle through an insertion pipe, an air distributor is a common ring-tube distributor (see fig. 4, wherein the opening direction of a gas distribution hole is upward), after fermentation is carried out for 9 days, the feeding is stopped, and after residual oil is consumed, the fermentation process is finished. The fermentation temperature was 35 ℃, aeration and agitation were adjusted according to dissolved oxygen and residual oil, defoamer was selectively added according to the foam layer height, and other fermentation processes were consistent with example 1.
The aeration rate required to maintain the same dissolved oxygen and process summary resid level during the vegetable oil and yeast powder feeding stage was 10Nm 3 And/h, stirring at 250rpm, and adding about 0.2kg/kg of rhamnolipid with a defoaming dosage, wherein the liquid level of the fermentation end point is 60%, and detecting that the yield of rhamnolipid reaches 85g/L.
As can be seen from the above examples and comparative examples, in example 2, the liquid phase feed was not fed by the liquid phase feed system 4 but directly fed through the raw material feed port, and as a result, it was found that to maintain the same dissolved oxygen and residual oil level in the process, it was necessary to increase the aeration rate and increase the stirring rotation speed, and the yield of rhamnolipid was slightly lowered; in example 3, the gas phase feed was not fed by gas distributor 6, but by a conventional loop distributor, and as a result, it was found that, in order to maintain the same dissolved oxygen and residual oil level in the process, not only was the aeration rate increased and the stirring speed increased, but also an antifoaming agent was added, and the yield of rhamnolipid was further lowered; in example 4, no liquid phase recycle on-line separation system was employed, and as a result, it was found that the addition of an antifoaming agent was required to maintain the same dissolved oxygen and in-process residuum level; as is clear from comparative examples 1 and examples 2-4, when the fermentation system of the present invention is used for the production of rhamnolipid, the need for aeration and stirring can be reduced, the problem of foaming can be solved, and the yield of rhamnolipid can be increased. Compared with the traditional fermentation system of the comparative example, the foaming problem of the fermentation system provided by the invention is obviously improved, the consumption of the defoaming agent is obviously reduced, the requirements on ventilation and stirring are also reduced, the product yield is improved to a certain extent, and the utilization rate of the fermentation reaction kettle is obviously increased.
The above examples are only specific embodiments of the present invention for illustrating the technical solution of the present invention, but not for limiting the scope of the present invention, and although the present invention has been described in detail with reference to the foregoing examples, it will be understood by those skilled in the art that the present invention is not limited thereto: any person skilled in the art may modify or easily conceive of the technical solution described in the foregoing embodiments, or perform equivalent substitution of some of the technical features, while remaining within the technical scope of the present disclosure; such modifications, changes or substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present invention, and are intended to be included in the scope of the present invention.
Claims (19)
1. The fermentation system is characterized by comprising a fermentation reaction kettle and a feeding system, wherein the fermentation reaction kettle is connected with the feeding system;
the feeding system comprises a gas phase feeding system, the gas phase feeding system comprises an air compressor and an air filter, the air compressor is connected with the air filter through a pipeline, and the air filter is connected with a gas distributor through a gas phase feeding port of the fermentation reaction kettle through a pipeline;
The feeding system further comprises a liquid-phase feeding system, wherein the liquid-phase feeding system comprises a liquid-phase injection section, a liquid-phase mixing section, a gas-liquid mixing section and a secondary mixing injection section which are sequentially connected, the liquid-phase injection section comprises a first venturi tube, the liquid-phase mixing section comprises a static mixer, and the first venturi tube is connected with the static mixer;
the gas-liquid mixing section comprises a gas-liquid mixing chamber, the gas-liquid mixing chamber comprises a first diameter reduction section connected with the static mixer and a first straight pipe section connected with the first diameter reduction section at the front end, and the tail end of the first straight pipe section is connected with the secondary mixing injection section;
the secondary mixing injection section comprises a second diameter-reducing section and a second straight pipe section which are communicated, the front end of the second diameter-reducing section is connected with the gas-liquid mixing chamber, and the tail end of the second straight pipe section is provided with a plurality of injection holes and is connected with a fermentation raw material feed inlet of the fermentation reaction kettle through a pipeline;
the fermentation reaction kettle comprises a reaction kettle body and a gas distributor accommodated in the reaction kettle body, wherein the gas distributor comprises an annular pipe body, and a plurality of nozzles with upward openings and a plurality of gas distribution holes with downward openings are arranged on the annular pipe body;
The liquid-phase injection section further comprises a first raw material inlet and a second raw material inlet, the first raw material inlet is connected with the top of the first venturi tube, the second raw material inlet is connected with the diameter reduction part of the first venturi tube, the feeding direction of the first raw material inlet is parallel to the axial direction of the first venturi tube, and the feeding direction of the second raw material inlet forms a certain angle with the axial direction of the first venturi tube; the side wall of the gas-liquid mixing chamber is provided with a plurality of gas spray holes, one end of the gas phase inlet is connected with the first diameter reduction section of the gas-liquid mixing chamber, and the gas phase inlet is also provided with a gas phase diversion hole; the other end of the gas phase inlet is connected with the air filter through a pipeline.
2. The fermentation system of claim 1, wherein the gas distribution holes have a diameter that is smaller than a diameter of the nozzle.
3. The fermentation system of claim 1 or 2, wherein the interior of the reactor body is provided with a stirring device located above the gas distributor and a heat exchanger fixed on the inner side wall of the reactor body.
4. A fermentation system according to claim 3, wherein the heat exchanger is selected from an inner coil, a coil or a vertical coil.
5. The fermentation system of claim 1, wherein the minimum diameter reduction of the first diameter reduction section is 300-400m from the end of the static mixer.
6. The fermentation system of claim 1, wherein the gas-liquid mixing chamber is provided with a gas phase inlet.
7. A fermentation system according to claim 1, wherein the angle is in the range of 10 ° -90 °.
8. The fermentation system of claim 7, wherein the angle is 90 °.
9. The fermentation system of claim 1, wherein the gas orifices are arranged in a row on a sidewall of the gas-liquid mixing chamber.
10. The fermentation system of claim 9, wherein the total area of the gas orifices is 0.5% -2% of the gas phase inlet cross-sectional area.
11. The fermentation system of claim 1, further comprising a liquid phase circulation on-line separation system comprising a first circulation pump, a second venturi, a first separation device and a second separation device, wherein the fermentation reactor, the first circulation pump, the second venturi, the first separation device and the second separation device are sequentially connected by a pipeline, and the first separation device is used for separating fermentation bacteria from fermentation broth in the fermentation reactor; the second separation device is used for separating the fermentation liquor passing through the first separation device to obtain a fermentation product and filtrate.
12. The fermentation system of claim 11, wherein the first separation device is selected from the group consisting of a butterfly centrifuge, a decanter centrifuge, a ceramic membrane, and an organic membrane.
13. The fermentation system of claim 12, wherein the first separation device is a ceramic membrane.
14. Fermentation system according to claim 11, wherein the second separation device is selected from an adsorption column, a chromatography column or an extraction apparatus.
15. The fermentation system of claim 14, wherein the second separation device is an adsorption column.
16. The fermentation system of claim 11, wherein the liquid phase circulation on-line separation system further comprises a second circulation pump, the middle of the second venturi is connected with the foam outlet of the fermentation reactor through a pipe, and the second venturi is used for crushing foam from the fermentation reactor; one end of the second circulating pump is connected with the first separation device through a pipeline, the other end of the second circulating pump is connected with a circulating liquid reflux port of the fermentation reaction kettle, and the second circulating pump is used for refluxing fermentation thalli separated by the first separation device into the fermentation reaction kettle; the second separation device is connected with the fermentation reaction kettle and is used for refluxing the filtrate separated by the second separation device into the fermentation reaction kettle; the first circulation pump and the second circulation pump are each selected from a centrifugal pump, a canned motor pump, or a diaphragm pump.
17. Use of a fermentation system according to any one of claims 1-16 for the preparation of an aerobic fermentation product.
18. The use according to claim 17, wherein the aerobic fermentation product is rhamnolipid.
19. Use according to claim 17 or 18, characterized in that it comprises:
inoculating strain seed liquid into a fermentation reaction kettle for continuous aerobic fermentation culture, and under the action of a first circulating pump, sequentially passing fermentation liquor obtained by the continuous aerobic fermentation culture through a second venturi tube, a first separation device and a second separation device, wherein the second venturi tube breaks foam in the fermentation liquor; the first separation device separates fermentation thalli in the fermentation liquor, and the fermentation thalli flows back to the fermentation reaction kettle under the action of a second circulating pump; the second separation device separates aerobic fermentation products in the fermentation liquor, and the obtained filtrate flows back to the fermentation reaction kettle;
optionally, the method further comprises the step of purifying the aerobic fermentation product.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2078322U (en) * | 1990-12-13 | 1991-06-05 | 中国科学院化工冶金研究所 | Air-lift biological reactor for high-visco sity fermentation |
| CN1175635A (en) * | 1996-08-29 | 1998-03-11 | 中国科学院化工冶金研究所 | Air lift internal cross-current type bio-reactor |
| CN103614293A (en) * | 2013-11-22 | 2014-03-05 | 南京汇科生物工程设备有限公司 | Internal loop airlift reactor for high-density yeast continuous-fermentation and yeast continuous-fermentation method |
| WO2014060778A1 (en) * | 2012-10-19 | 2014-04-24 | Advanced Technology And Engineering Limited (Atel) | Fermentation apparatus and method of fermentation for protein production |
| CN106552560A (en) * | 2016-10-28 | 2017-04-05 | 江南大学 | A kind of airlift reactor with spiral porous sieve plate |
| CN108795704A (en) * | 2018-09-06 | 2018-11-13 | 辽阳博仕流体设备有限公司 | A kind of oxygen supply fermentation system |
| CN213966481U (en) * | 2020-11-18 | 2021-08-17 | 恒力石化（大连）炼化有限公司 | CO gas distributor device on acetic acid device |
| CN114350480A (en) * | 2022-01-12 | 2022-04-15 | 万华化学(四川)有限公司 | Double-circulation bubbling fermentation tank and method for preparing lactic acid through fermentation |
-
2023
- 2023-11-06 CN CN202311460606.9A patent/CN117187030B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2078322U (en) * | 1990-12-13 | 1991-06-05 | 中国科学院化工冶金研究所 | Air-lift biological reactor for high-visco sity fermentation |
| CN1175635A (en) * | 1996-08-29 | 1998-03-11 | 中国科学院化工冶金研究所 | Air lift internal cross-current type bio-reactor |
| WO2014060778A1 (en) * | 2012-10-19 | 2014-04-24 | Advanced Technology And Engineering Limited (Atel) | Fermentation apparatus and method of fermentation for protein production |
| CN103614293A (en) * | 2013-11-22 | 2014-03-05 | 南京汇科生物工程设备有限公司 | Internal loop airlift reactor for high-density yeast continuous-fermentation and yeast continuous-fermentation method |
| CN106552560A (en) * | 2016-10-28 | 2017-04-05 | 江南大学 | A kind of airlift reactor with spiral porous sieve plate |
| CN108795704A (en) * | 2018-09-06 | 2018-11-13 | 辽阳博仕流体设备有限公司 | A kind of oxygen supply fermentation system |
| CN213966481U (en) * | 2020-11-18 | 2021-08-17 | 恒力石化（大连）炼化有限公司 | CO gas distributor device on acetic acid device |
| CN114350480A (en) * | 2022-01-12 | 2022-04-15 | 万华化学(四川)有限公司 | Double-circulation bubbling fermentation tank and method for preparing lactic acid through fermentation |
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