CN103215179A - Internal-circulation airlift type reactor adopting membrane tube aeration - Google Patents
Internal-circulation airlift type reactor adopting membrane tube aeration Download PDFInfo
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- CN103215179A CN103215179A CN2013101660201A CN201310166020A CN103215179A CN 103215179 A CN103215179 A CN 103215179A CN 2013101660201 A CN2013101660201 A CN 2013101660201A CN 201310166020 A CN201310166020 A CN 201310166020A CN 103215179 A CN103215179 A CN 103215179A
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Abstract
The invention relates to an internal-circulation airlift type reactor adopting membrane tube aeration. The internal-circulation airlift type reactor comprises an internal-circulation airlift type reactor body, wherein a gas distributor is arranged on the bottom of the internal-circulation airlift type reactor body; and a membrane tube with a nanoscale pore diameter is connected on the gas distributor. According to the internal-circulation airlift type reactor adopting the membrane tube aeration, the membrane tube is applied to the internal-circulation airlift type reactor, and the nanoscale pore diameter of the membrane tube is adopted, so air bubbles escaped from the membrane tube are small in diameter and large in quantity, and therefore, the problem that the air bubbles of a spray nozzle type distributor and a plate pore type distributor are larger is overcome; moreover, the mass transfer performance is greatly improved, thus facilitating the control of dissolved oxygen in fermentation liquor.
Description
Technical field
The invention belongs to internal circulation gas-lift type reactor field, relate to a kind of internal circulation gas-lift type reactor that adopts film pipe aeration.
Background technology
Airlift reactor mainly is divided into two big class, i.e. internal circulation gas-lift type reactor and outer circulation airlift reactors.Two kinds of reactors mainly are to distinguish according to different fluid circulating paths.When aeration in the up-flow district, because the difference of the apparent fluid density that empty gas holdup difference causes in the ascending, descending stream district finally causes fluid at the reactor internal recycle.The internal circulation gas-lift type reactor is considered to introduce in the gas-liquid bubbling bed upspout or a baffle plate makes fluid at different regional internal recycle.
The solubleness of oxygen in water is lower, and at normal temperatures and pressures, the solubleness of pure water oxygen is 0.2mmol/L, and the solubleness in fermented liquid is then lower.Yet oxygen concentration is the important factor of restriction micro-organisms growth in the fermenting process fermented liquid, so the design of bio-reactor is had relatively high expectations to its mass-transfer performance.Particularly along with the increase of reactor volume, the local gas holdup in its inner each zone and the important content that mass-transfer performance will become reactor design.The reinforcement that oxygen transmits is very important in biological fermentation process, and especially the transmission of oxygen usually becomes restrictive factor in high density fermentation.
Unit volume fermented liquid oxygen-consumption hourly is generally 25-100mmol/ (L*h).Glutamic acid fermentation 18h oxygen consumption rate is 51mmol/ (L*h), the oxygen consumption rate of same quasi-microorganism also is subjected to the influence of temperature, fermented liquid composition and concentration, as working as the oxygen supply deficiency, glucose concn is 1% o'clock, the zymic oxygen consumption rate is 15-18mmol/ (L*h), and the oxygen supply abundance, glucose concn is 15% o'clock, oxygen consumption rate then reaches 342-396mmol/ (L*h).The aerobic speed of microbial fermentation be can improve greatly so improve the reactor mass-transfer performance, growth, the metabolic rate of producing bacterium improved.
Adopt the film pipe of nano aperture to carry out aeration, because the bubble diameter that produces is less, specific surface area is less, causes the gas-to-liquid contact area bigger on the one hand.On the other hand, small bubbles can fall the stream district along with liquid-flow enters, and improve the oxyty of falling the stream district.So the volume transmission quality coefficient that adopts film pipe aeration to obtain is greater than general nozzle-type and orifice-plate type.So both can save energy, also can improve the mass transfer of gas-liquid reactor.For example, in the stirring rake ferment tank process of reality, normally utilize stirring rake to improve mixed effect and raising mass transfer effect, yet the energy consumption of stirring rake is very big, it can account for 1/3 of total energy consumption.
Adopting film pipe aeration is a kind of technique means, than nozzle-type and orifice-plate type, adopt that the advantage of film pipe aeration is that mass-transfer performance is good, energy consumption is low, adaptability is big, good economy performance etc., but present the report that the film pipe is applied to the internal circulation gas-lift type reactor do not arranged as yet.
Summary of the invention
The purpose of this invention is to provide a kind of internal circulation gas-lift type reactor that adopts film pipe aeration, it is lower to solve the volume transmission quality coefficient that adopts nozzle-type and orifice-plate type gas distribution to obtain in the existing internal circulation gas-lift type reactor, is unfavorable for aerobic microbiological fermentation, restriction thalli growth, metabolic problem.
The present invention is achieved through the following technical solutions: the internal circulation gas-lift type reactor that adopts film pipe aeration, comprise the internal circulation gas-lift type reactor, described internal circulation gas-lift type reactor internal upper part is provided with plate-fin heat exchanger, there are steam inlet and cooling water outlet flange in the plate-fin heat exchanger upper end, there are vapor condensation water out and entrance of cooling water flange in the lower end, wherein, steam inlet and cooling water outlet flange are linked to be an integral body to plate wing heat exchanger fin by pipeline one, and vapor condensation water out and entrance of cooling water flange are linked to be an integral body to plate wing heat exchanger fin by pipeline two; Gas distributor is equipped with in the bottom of described internal circulation gas-lift type reactor, is connected with many film pipes with nano level aperture on the gas distributor.
Between described gas distributor and the film pipe for being threaded.
The plate wing heat exchanger fin of described plate-fin heat exchanger is a plate shape, and pipeline one and pipeline two are straight tube.
The plate wing heat exchanger fin of described plate-fin heat exchanger is fan-shaped, and pipeline one and pipeline two are endless tube.
Be flexible connection between described plate-fin heat exchanger and the internal circulation gas-lift type reactor.
Described flexible connection is that strut member is connected with bolt.
Adopt the positively effect of technique scheme: the present invention is applied to the internal circulation gas-lift type reactor with the film pipe, utilize the nano level aperture of film pipe, make that the bubble diameter of overflowing is little from the film pipe, quantity is many, overcome nozzle-type and plate hole formula sparger bubble is bigger, make mass-transfer performance improve greatly, help control dissolved oxygen in the fermented liquid; In addition, be connected by screw thread between film pipe and the gas distributor, can maintenance for convenience detach greatly.
Description of drawings
Fig. 1 is a structural representation of the present invention;
Fig. 2 be among Fig. 1 A-A to vertical view;
Among the figure, 1 internal circulation gas-lift type reactor, 2 plate-fin heat exchangers, 3 steam inlets and cooling water outlet flange, 4 pipelines, one, 5 strut member, 6 vapor condensation water outs and entrance of cooling water flange, 7 pipelines, two, 8 gas distributors, 9 film pipes.
Embodiment
Below in conjunction with embodiment and Comparative Examples technical scheme of the present invention is described further, but should not be construed as limitation of the present invention:
Embodiment 1
Fig. 1 is a structural representation of the present invention, Fig. 2 be among Fig. 1 A-A to vertical view, in conjunction with Fig. 1, shown in Figure 2, adopt the internal circulation gas-lift type reactor of film pipe aeration, comprise internal circulation gas-lift type reactor 1, internal circulation gas-lift type reactor 1 internal upper part is provided with plate-fin heat exchanger 2, there are steam inlet and cooling water outlet flange 3 in plate-fin heat exchanger 2 upper ends, there are vapor condensation water out and entrance of cooling water flange 6 in the lower end, wherein, steam inlet and cooling water outlet flange 3 are linked to be an integral body to plate wing heat exchanger fin by pipeline 1, vapor condensation water out and entrance of cooling water flange 6 are linked to be an integral body to plate wing heat exchanger fin by pipeline 27, are convenient to steam or cooling-water flow.Gas distributor 8 is equipped with in the bottom of internal circulation gas-lift type reactor 1, is connected with many film pipes 9 with nano level aperture on the gas distributor 8.Gas distributor 8 is used for aeration, is connected with pump-up device, and gas is overflowed from the nano level aperture of film pipe 9, strengthens the dissolved oxygen in the fermented liquid.
For convenience of field-strip, for being threaded, simultaneously, be flexible connection between plate-fin heat exchanger 2 and the internal circulation gas-lift type reactor 1 between gas distributor 8 and the film pipe 9, as long as can realize easy-to-mount flexible connection all can, be connected with bolt for strut member 5 in the present embodiment.
In actual applications, the plate wing heat exchanger fin of plate-fin heat exchanger 2 is a plate shape, and corresponding pipeline 1 and pipeline 27 are straight tube; The plate wing heat exchanger fin that also can be plate-fin heat exchanger 2 is fan-shaped, and corresponding pipeline 1 and pipeline 27 are endless tube.
When needs heated, steam entered from the steam inlet of the upper end of plate-fin heat exchanger 2, and template or fan-shaped heat exchanger fin by pipeline one 4 arrival plate-fin heat exchangers 2 enter pipeline 27 behind the heat-shift, discharged from the vapor condensation water out of lower end then; When needs cool off, water coolant enters from the entrance of cooling water of the lower end of plate-fin heat exchanger 2, template or fanning strip wing heat exchanger fin by pipeline 27 arrival plate-fin heat exchangers 2 enter pipeline 1 behind the heat-shift, discharge from the cooling water outlet of upper end then to get final product.Simultaneously, gas is through behind the gas distributor 8, from the nano level aperture of film pipe 9, overflow, because the nano level aperture of film pipe 9, the bubble diameter that make to produce is little, and quantity is many, has overcome nozzle-type and plate hole formula sparger bubble is bigger, make mass-transfer performance improve greatly, help control dissolved oxygen in the fermented liquid.
Embodiment 2
Present embodiment is used for explanation and utilizes 10 m
3Reactor adopt the method for film pipe aeration mode fermentation production of L-lysine.
At first carry out medium sterilization, open agitator motor, rotating speed is heated evenly fermented liquid at 100r/min.When being raised to more than 95 degree, temperature can stop to stir.Carry out the sterilization of air filter and air line again, opened filter and water discharge valve slightly, thus guarantee the air line sterilization.Final discharge port, sampling valve, steam valve and outlet valve are opened slightly, guarantee this pipeline sterilization.
Fermentation culture and result: 5 m are equipped with in intestinal bacteria (buy from CGMCC, culture presevation the is numbered CGMCC1.0281) access that will produce L-Methionin by 10% inoculum size
310 m of fermention medium
3Adopt the film pipe to carry out that (the 1L fermention medium contains: glucose 20 ~ 40 g/L, (NH in the stirring reactor of aeration
4)
2SO
41.5 ~ 1.8 g, KH
2PO
41.2 g, corn steep liquor 1 ~ 2 g, L-Threonine 0.2 ~ 0.4 g), air flow is 200 ~ 250 m
3/ h, mixing speed 100 ~ 200 r/min, 35 ~ 37 ℃ of leavening temperatures, stream add ammoniacal liquor to control pH 6.5 ~ 6.8, detect remaining sugar concentration every 2 ~ 4 h, and stream adds the glucose of 700 g/L, keeps remaining sugar concentration at 10 ~ 15 g/L, preceding 4 ~ 5 h of fermentation ends, stop stream with liquid glucose, when residual sugar is reduced to 5 ~ 7 g/L, i.e. fermentation ends, about 72 h of whole fermentation period.In the fermenting process, gas is overflowed from the nano level aperture of film pipe 9 through behind the gas distributor 8, feeds the atmosphere from outlet valve.In the fermentation peak period air input is increased to maximum, makes the solubleness of oxygen can reach 3-4ppm, but it should be noted that, manually control tank pressure because in the fermenting process be, so when regulating air flow quantity, must regulate outlet valve simultaneously, thereby make tank pressure constant greater than 0.03Mpa.
The conventional reactor of contrast does not possess film pipe aeration structure, and other structure is identical with reactor of the present invention, by making the Zhenjiang Oriental Bio-engineering Technology Co., Ltd reactor size 10m
3, fermentation mode is consistent with present embodiment with substratum.The result is as follows by fermentation: the dissolved oxygen that reactor of the present invention adopts film pipe aeration to obtain is 4.3ppm, and the dissolved oxygen data of contrast popular response device are 2.6ppm.By above-mentioned data as can be seen, the reactor of employing film pipe aeration of the present invention, it has improved oxyty, has improved the overall reactor mass transfer coefficient.
Embodiment 3
Present embodiment is used for explanation and utilizes 50 m
3Reactor adopts the method for film pipe aeration mode fermentation production of citric acid.
At first carry out medium sterilization, open agitator motor, rotating speed is heated evenly fermented liquid at 100r/min.When being raised to more than 95 degree, temperature can stop to stir.Carry out the sterilization of air filter and air line again, opened filter and water discharge valve slightly, thus guarantee the air line sterilization.Final discharge port, sampling valve, steam valve and outlet valve are opened slightly, guarantee this pipeline sterilization.
Fermentation culture and result: will produce citric acid aspergillus niger (buy from CGMCC, the deposit number of aspergillus niger is CGMCC5343) access by 10% inoculum size 35m is housed
3The 50m of fermention medium
3Employing film pipe carry out that (the 1L fermention medium contains: potato is done 50 ~ 70 g, α-Dian Fenmei 80 U/g raw materials, (NH in the reactor of aeration
4)
2SO
445 ~ 65 g), air flow is 2500 ~ 4000 m
3/ h, mixing speed 100 ~ 150 r/min, 28 ~ 30 ℃ of leavening temperatures, about 65 h of whole fermentation period.In the fermenting process, gas is overflowed from the nano level aperture of film pipe 9 through behind the gas distributor 8, feeds the atmosphere from outlet valve.In the fermentation peak period air input is increased to maximum, makes the solubleness of oxygen can reach 3-4ppm, but it should be noted that, manually control tank pressure because in the fermenting process be, so when regulating air flow quantity, must regulate outlet valve simultaneously, thereby make tank pressure constant greater than 0.03Mpa.
The conventional reactor of contrast does not possess film pipe aeration structure, and other structure is identical with reactor of the present invention, by making the Zhenjiang Oriental Bio-engineering Technology Co., Ltd reactor size 50m
3, fermentation mode is consistent with present embodiment with substratum.The result is as follows by fermentation: the dissolved oxygen that reactor of the present invention adopts film pipe aeration to obtain is 3.9ppm, and the dissolved oxygen data of contrast popular response device are 2.3ppm.By above-mentioned data as can be seen, the reactor of employing film pipe aeration of the present invention, it has improved oxyty, has improved the overall reactor mass transfer coefficient.
Embodiment 4
Present embodiment is used for explanation and utilizes 20 m
3Reactor adopts the method for film pipe aeration mode fermentative production ARA
At first carry out medium sterilization, open agitator motor, rotating speed is heated evenly fermented liquid at 100r/min.When being raised to more than 95 degree, temperature can stop to stir.Carry out the sterilization of air filter and air line again, opened filter and water discharge valve slightly, thus guarantee the air line sterilization.Final discharge port, sampling valve, steam valve and outlet valve are opened slightly, guarantee this pipeline sterilization.
Fermentation culture and result: the Mortierella alpina (the bacterial strain code name is ME-AA01, available from Chinese industrial microbial strains preservation administrative center) that the inoculum size by 10% will be produced ALA inserts 12m is housed
3The 20m of fermention medium
3Employing film pipe carry out in the reactor of aeration (the fermentation culture based component is a 80g/L glucose, 20g/L yeast powder, 500mg/L phosphoric acid salt adds the 500mg/L sodium glutamate), air flow is 400 ~ 500 m
3/ h, mixing speed 100 ~ 150 r/min, 28 ~ 30 ℃ of leavening temperatures, about 180 h of whole fermentation period.In the fermenting process, gas is overflowed from the nano level aperture of film pipe 9 through behind the gas distributor 8, feeds the atmosphere from outlet valve.In the fermentation peak period air input is increased to maximum, makes the solubleness of oxygen can reach 3-4ppm, but it should be noted that, manually control tank pressure because in the fermenting process be, so when regulating air flow quantity, must regulate outlet valve simultaneously, thereby make tank pressure constant greater than 0.03Mpa.
The conventional reactor of contrast does not possess film pipe aeration structure, and other structure is identical with reactor of the present invention, by making the Zhenjiang Oriental Bio-engineering Technology Co., Ltd reactor size 20m
3, fermentation mode is consistent with present embodiment with substratum.The result is as follows by fermentation: the dissolved oxygen that reactor of the present invention adopts film pipe aeration to obtain is 4.1ppm, and the dissolved oxygen data of contrast popular response device are 2.5ppm.By above-mentioned data as can be seen, the reactor of employing film pipe aeration of the present invention, it has improved oxyty, has improved the overall reactor mass transfer coefficient.
Claims (6)
1. internal circulation gas-lift type reactor that adopts film pipe aeration, comprise internal circulation gas-lift type reactor (1), described internal circulation gas-lift type reactor (1) internal upper part is provided with plate-fin heat exchanger (2), there are steam inlet and cooling water outlet flange (3) in plate-fin heat exchanger (2) upper end, there are vapor condensation water out and entrance of cooling water flange (6) in the lower end, wherein, steam inlet and cooling water outlet flange (3) are linked to be an integral body to plate wing heat exchanger fin by pipeline one (4), vapor condensation water out and entrance of cooling water flange (6) are linked to be an integral body to plate wing heat exchanger fin by pipeline two (7), it is characterized in that: gas distributor (8) is equipped with in the bottom of described internal circulation gas-lift type reactor (1), is connected with many film pipes (9) with nano level aperture on the gas distributor (8).
2. the internal circulation gas-lift type reactor of employing film pipe aeration according to claim 1 is characterized in that: between described gas distributor (8) and the film pipe (9) for being threaded.
3. the internal circulation gas-lift type reactor of employing film pipe aeration according to claim 1 is characterized in that: the plate wing heat exchanger fin of described plate-fin heat exchanger (2) is a plate shape, and pipeline one (4) and pipeline two (7) are straight tube.
4. the internal circulation gas-lift type reactor of employing film pipe aeration according to claim 1 is characterized in that: the plate wing heat exchanger fin of described plate-fin heat exchanger (2) is fan-shaped, and pipeline one (4) and pipeline two (7) are endless tube.
5. the internal circulation gas-lift type reactor of employing film pipe aeration according to claim 1 is characterized in that: be flexible connection between described plate-fin heat exchanger (2) and the internal circulation gas-lift type reactor (1).
6. the internal circulation gas-lift type reactor of employing film pipe aeration according to claim 5 is characterized in that: described flexible connection is that strut member (5) is connected with bolt.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106629958A (en) * | 2017-01-20 | 2017-05-10 | 南京工业大学 | Closed continuous high-pressure gas dissolving apparatus and method |
| CN108138107A (en) * | 2015-10-23 | 2018-06-08 | Gg科里奥利思公司 | Including establishing the fermentor for rising cycle volume and declining the automatic device of the fluid communication between cycle volume, the fluid nutrient medium stirred using gas circulation according to the height of fluid nutrient medium |
| CN109735452A (en) * | 2019-03-25 | 2019-05-10 | 南京工业大学 | A kind of airlift bioreactor of membrane tube gas distribution and its application |
| CN110042046A (en) * | 2019-05-07 | 2019-07-23 | 南京工业大学 | The built-in stirring mocromembrane of continuous immobilization is aerated internal circulation gas-lift type bioreactor |
| CN110963641A (en) * | 2019-11-20 | 2020-04-07 | 安徽舜禹水务股份有限公司 | Small-size self-loopa sewage treatment device |
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Application publication date: 20130724 |