TWI868610B - Continuous Airlift Double Chamber Bioreactor - Google Patents

Abstract

The present invention discloses a continuous gas-lift double-chamber bioreactor, which includes an inner tank, an upper cover and an outer tank, wherein a liquid horizontal distributor is arranged inside the inner tank, so that the inner tank is divided into an anaerobic reaction chamber and an aerated reaction chamber, and the liquid horizontal distributor has a horizontal distribution plate and a plurality of hole covers, wherein the horizontal distribution plate is provided with a plurality of overflow pipes, and the upper end of each overflow pipe is provided with a plurality of fixing columns, and the upper end of each hole cover is provided with a plurality of fixing holes, and the inner part is provided with a groove, and the fixing hole of the hole cover can be sleeved on the upper end of the fixing column of the overflow pipe, so that the overflow pipe is accommodated in the groove of the hole cover to form an overflow port and an opening. The continuous airlift double-chamber bioreactor of the present invention is equipped with a liquid horizontal distributor to divide the inner tank into two different reaction spaces, upper and lower, to ensure that the upper and lower reaction spaces do not exchange liquids, to achieve the conditions of anaerobic lower layer and aerobic upper layer, to reduce PHA production costs and operating expenses, and to achieve industrial production effects.

Description

Continuous airlift double chamber bioreactor

The present invention relates to a technical field for producing polyhydroxyalkanoate (PHA), and in particular to a continuous gas-lift double-chamber bioreactor for producing polyhydroxyalkanoate (PHA) by anaerobic hydrogenation followed by aerobic production in the same reactor.

Polyhydroxyalkanoate (PHA) is a polyester produced by bio-based microorganisms. It is a natural thermoplastic plastic synthesized by many microorganisms under unbalanced growth conditions and used as an intracellular storage material. It has the characteristics of being completely biodegradable into oligomers and monomers, and then degraded into _CO2 and water. Due to its non-toxicity and high biocompatibility, it is harmless to the environment. Together with many conventional polyolefins, polylactic acid (PLA) and polybutylene succinate (PBS), it is considered to be the green polymer of the future. Due to their similar thermoplastic properties, they are expected to gradually replace polypropylene (PP) and low-density polyethylene (LDPE). They are very promising bulk materials that can be used in a large number of industrial applications and have considerable market potential. Among them, the most common PHAs synthesized by microorganisms are PHB (polyhydroxybutyrate) and PHV (polyhydroxyvalerate).

According to the conventional method of synthesizing polyhydroxyalkanoate (PHA), glucose is used as a substrate to ferment with microorganisms in an aerobic environment to produce polyhydroxyalkanoate (PHA), as shown in FIG1 , which is a schematic diagram of a polyhydroxyalkanoate (PHA) production system in an aeration reactor. In the figure, the polyhydroxyalkanoate (PHA) production system mainly includes a feed tank 11, an alkali tank 12 and an aeration reactor 10, wherein the feed tank 11 uses glucose as a feed source, and then the alkali solution and microorganisms in the alkali tank 12 are placed in the aeration reactor 0, and then air is injected to perform an aeration fermentation reaction to produce polyhydroxyalkanoate (PHA). The production cost of polyhydroxyalkanoates (PHA) remains high due to the high price of high-purity substrates such as glucose and production in discontinuous batch feeding and batch culture modes.

In order to reduce production costs, there is a method for synthesizing polyhydroxyalkanoate (PHA) using organic waste as a matrix. The method is shown in the schematic diagram of a double-tank system for producing polyhydroxyalkanoate (PHA) in FIG2 . The system mainly utilizes organic matter to carry out anaerobic reaction in an anaerobic reactor to produce volatile fatty acids (VFA), which are then provided to another aeration reactor for an aerobic reaction to produce polyhydroxyalkanoate (PHA). The system in FIG. 2 mainly includes an anaerobic reactor 20 and an aeration reactor 30, wherein the aeration reactor 30 is connected to the alkaline solution tank 31 and the anaerobic reactor 20 respectively, and the anaerobic reactor 20 is connected to the feed tank 21. The feed tank 21 uses organic waste as a substrate to provide the anaerobic reactor 20 with anaerobic reaction to produce volatile fatty acids (VFA) such as acetic acid, propionic acid, butyric acid, valeric acid, isovaleric acid, etc., and then the volatile fatty acids (VFA) are sent to the aeration reactor 30 together with the alkaline solution in the alkaline solution tank 31 to perform an aerobic reaction to produce polyhydroxyalkanoate (PHA). Since organic waste contains a large amount of nutrients, it is considered to be an ideal substrate for synthesizing polyhydroxyalkanoate (PHA). In the system diagram of FIG. 2 , the organic waste in the feed tank 21 undergoes fermentation in the anaerobic reactor 20 for acidification reaction to produce volatile fatty acids (VFA), and then enters the aeration reactor 30 (batch fermentation aeration reactor SBR) to react with microorganisms, and at the same time, the alkaline solution and sterile oxygen are sent to the alkaline solution tank 31 to produce polyhydroxyalkanoate (PHA). This method requires passing through two tank reactors (anaerobic reactor 20 and aeration reactor 30), and the volatile fatty acids (VFA) produced in the first stage are used as the raw materials for producing polyhydroxyalkanoate (PHA) in the second stage. However, it has the disadvantages of having more steps, large equipment space, and complex bioreactors. Using this method, such as the invention patent No. 092100912 (application No. 092100912) of the Republic of China applied by the University of Hawaii, the patent disclosed in the "Technology for producing biodegradable thermoplastic materials from organic waste" includes: a first compartment for acid production of organic waste; and a second compartment for polymer synthesis by intensive cultivation of microbial species that produce polyhydroxy fatty acid esters (PHA) including R.eutropha, P.oleovoran or a mixture thereof, wherein the fermentative acid passes from the first compartment to the second compartment through a partition.

The high production cost of the dual tank has always been the main factor hindering the popularization of biodegradable materials. In order to reduce the production cost of polyhydroxy fatty acid esters (PHA) and improve its extraction purity, so as to enhance the economic benefits of industrialized production of polyhydroxy fatty acid esters (PHA), there is still a need to continue to develop new polyhydroxy fatty acid esters (PHA) production methods.

The main purpose of the present invention is to provide a continuous gas-lift double-chamber bioreactor for the existing double-tank reactor, which uses the volatile fatty acids (VFA) produced in the first stage (anaerobic reactor) as the raw materials for producing polyhydroxy fatty acid esters (PHA) in the second stage (aeration reactor). The bioreactor has many steps, large equipment space and is complex. The continuous gas-lift double-chamber bioreactor is mainly composed of an anaerobic reaction chamber and an aeration reaction chamber, and a liquid horizontal distributor is arranged between the anaerobic reaction chamber and the aeration reaction chamber, wherein the hydrogen (H ₂ ) and volatile fatty acids (VFA) rise to the upper aeration reaction chamber through a liquid horizontal distributor to serve as the raw materials for the second stage production of polyhydroxy fatty acid esters (PHA). The present invention can simplify the original multi-step and complex bioreactor into a single-tank double-chamber continuous gas-lift double-chamber bioreactor, and use immobilized microbial technology to prevent bacteria from being lost with the outflow of the reaction effluent, which can save and reduce material costs, and adjust the pH and air intake rate at a fixed substrate concentration to produce hydrogen and polyhydroxy fatty acid esters (PHA).

To achieve the above purpose, the present invention provides a continuous airlift double chamber bioreactor, which includes at least an inner tank, an upper cover is provided on the upper part of the inner tank, an outer tank is provided on the outside, and an insulation chamber is formed between the inner tank and the outer tank; the characteristic is that a liquid horizontal distributor is provided inside the inner tank, so that the inner tank is divided into two different reaction spaces, the lower reaction space is an anaerobic reaction chamber, and the upper reaction space is an aerated reaction chamber.

The aforementioned liquid horizontal distributor includes but is not limited to narrow groove type, trough type, disc type, drum disc type, tube type, nozzle type and wall ring type. The liquid horizontal distributor can be selected and designed according to different working conditions. The liquid horizontal distributor applicable to the present invention is in the shape of a disc. The function of the disc-shaped liquid horizontal distributor is to uniformly distribute or redistribute the liquid at the top of the packing or at a certain height, so as to increase the effective surface of mass transfer and heat transfer, improve the phase contact, and thus improve the efficiency of the reactor. In addition, the flow of the liquid in the reactor is not a uniform plug flow, but there may be channel flow, bias flow, and wall flow, which will cause the extreme effect of the amplification effect of the reactor. Poor distribution of liquid in the reactor is caused by the liquid channel in the reactor, which will seriously reduce the efficiency of the entire reactor. The purpose of rationally designing and selecting liquid horizontal distributors and redistributors is to reduce and prevent the amplification effect of the reactor, thereby reducing the cost or operating expenses.

In one embodiment of the present invention, in order to ensure that the upper and lower reaction spaces do not exchange liquids, the lower anaerobic and upper aerobic conditions can be achieved simultaneously in the same reactor, thereby improving the efficiency of the reactor, saving costs and simplifying the process. Therefore, a disk-shaped liquid horizontal distributor is provided inside the reactor to prevent the volatile fatty acids (VFA) that rise to the upper aerobic reaction chamber from flowing back to the lower anaerobic reaction chamber, wherein The liquid horizontal distributor includes a horizontal distribution plate and a plurality of hole covers, wherein the horizontal distribution plate is provided with a plurality of overflow pipes penetrating the horizontal distribution plate, and the upper end of each overflow pipe is provided with a plurality of fixing columns, and the upper end of each hole cover is provided with a plurality of fixing holes, and the inner part is provided with a groove, and the fixing holes on the hole cover can be sleeved on the upper end of the fixing column at the upper end of the overflow pipe, so that the overflow pipe is accommodated in the groove of the hole cover to form a plurality of overflow ports and an opening.

In one embodiment of the present invention, the anaerobic reaction chamber is provided with a feed pipe and a magnetic agitator, wherein the feed pipe is used to provide an input organic material source into the anaerobic reaction chamber, and the magnetic agitator is used to provide stirring of the organic material source.

In one embodiment of the present invention, the aeration reaction chamber is provided with an acid-base detector, an alkaline liquid feed pipe, an air inlet pipe, an agitator, and a discharge pipe, wherein the acid-base detector is used to detect the acidity and alkalinity of the liquid in the aeration reaction chamber, the alkaline liquid feed is used to transport the alkaline liquid into the aeration reaction chamber, the air inlet pipe is used to provide oxygen to enter the aeration reaction chamber, the agitator is used to stir the liquid in the aeration reaction chamber, and the discharge pipe is used to provide output hydrogen ( _H2 ) and polyhydroxy fatty acid ester (PHA).

In one embodiment of the present invention, the circulating heat preservation tank is provided with a reflux pipe and a warm water delivery pipe, which are used to provide circulating constant temperature water into the circulating heat preservation tank, so that the liquid in the anaerobic reaction chamber and the aeration reaction chamber is maintained at a constant temperature.

In one embodiment of the present invention, an annular fixed plate is provided inside the inner tank, and the liquid horizontal distributor is assembled above the annular fixed plate.

Common symbols:

10, 30: Aeration reactor

11, 21: Trough

12, 31: Alkaline liquid tank

20: Anaerobic reactor

Symbol of this invention:

40: Continuous airlift double chamber bioreactor

401: Trough

402: Alkaline liquid tank

403: Constant temperature heating tank

404: Gas-liquid separator

405: Gas flow meter

406: Collection tank

41: Inner groove

42: Upper cover

43: External groove

44: Liquid horizontal distributor

45: Incubator

451: Reflux pipe

452:Transmission pipe

46: Anaerobic reaction chamber

461: Feed pipe

462:Magnetic stirrer

47: Aeration reaction chamber

471: Acid and Alkali Detector

472: Intake pipe

473: Mixer

474: Feed pipe

475: Discharge pipe

48: Fixed disk

49: Horizontal distribution plate

50: Hole cover

51: Overflow pipe

52:Fixed column

53:Fixing hole

54: Groove

55: Overflow port

56: Open mouth

Figure 1 is a schematic diagram of the production of polyhydroxyalkanoate (PHA) in an aerated reactor.

Figure 2 is a schematic diagram of the production of polyhydroxyalkanoate (PHA) using double tanks.

FIG3 is a schematic diagram of a system for producing hydrogen (H ₂ ) and polyhydroxyalkanoate (PHA) using a continuous gas-lift dual-chamber bioreactor according to a preferred embodiment of the present invention.

Figure 4 is a schematic cross-sectional view of a continuous airlift double-chamber bioreactor according to a preferred embodiment of the present invention.

Figure 5 is an enlarged schematic diagram of detail A in Figure 4.

Figure 6 is a three-dimensional exploded schematic diagram of a preferred liquid horizontal distributor in a continuous gas-lift double-chamber bioreactor of a preferred embodiment of the present invention.

Figure 7 is an enlarged schematic diagram of detail B in Figure 6.

Figure 8 is a three-dimensional cross-sectional schematic diagram of a preferred liquid horizontal distributor in a continuous gas-lift double-chamber bioreactor of a preferred embodiment of the present invention.

Figure 9 is a schematic cross-sectional view of a preferred liquid horizontal distributor in a continuous gas-lift double-chamber bioreactor of a preferred embodiment of the present invention.

In order to help the examiner understand the features, contents and advantages of the invention and the effects that can be achieved, the invention is described in detail as follows with accompanying drawings and in the form of an embodiment. The drawings used are only for illustration and auxiliary purposes of the manual. In addition, the same symbols in the illustrations of this description represent the same components.

First, please refer to FIG. 3 , which is a schematic diagram of a preferred embodiment of a system for producing hydrogen (H ₂ ) and polyhydroxyalkanoate (PHA) using a continuous gas-lift double-chamber bioreactor 40. The system mainly includes a continuous gas-lift double-chamber bioreactor 40, a feed tank 401, an alkaline liquid tank 402, a constant temperature heating tank 403, a gas-liquid separator 404, a gas flow meter 405, and a collection tank 406.

Referring to FIG. 3 and FIG. 4 , the aforementioned continuous airlift double chamber bioreactor 40 includes an inner tank 41, an upper cover 42, an outer tank 43 and a liquid horizontal distributor 44; wherein an insulation chamber 45 is formed between the inner tank 41 and the outer tank 43, and the liquid horizontal distributor 44 is disposed inside the inner tank 41, so that the inner tank 41 is divided into two different reaction spaces, the lower reaction space being an anaerobic reaction chamber 46, and the upper reaction space being an aerated reaction chamber 47.

The aforementioned anaerobic reaction chamber 46 is provided with a feed pipe 461 and a magnetic agitator 462. The feed pipe 461 is connected to the material tank 401 and is mainly used to deliver the organic material source in the material tank 401 into the anaerobic reaction chamber 46. The magnetic agitator 462 is arranged at the bottom of the anaerobic reaction chamber 46 and is mainly used to stir the organic material source.

The aeration reaction chamber 47 is provided with an acid-base detector 471, an air inlet pipe 472, a stirrer 473, an alkaline solution feeding pipe 474 and an outlet pipe 475; wherein the alkaline solution feeding pipe 474 is connected to the alkaline solution tank 402, and the alkaline solution tank 402 detects the acid-base level of the aeration reaction chamber 47 through the acid-base detector 471 and provides alkaline solution to the aeration reaction chamber 47 in a timely manner; The gas pipe 472 is used to transport oxygen into the bottom of the aeration reaction chamber 47 (near the top of the liquid horizontal distributor 44) through a pump to provide the aeration reaction chamber 47 with oxygen consumption reaction; the agitator 473 is used to stir the liquid in the aeration reaction chamber 47; the discharge pipe 475 is connected to the gas-liquid separator 404 to provide hydrogen (H ₂ ) and polyhydroxy fatty acid ester (PHA) are output to the gas-liquid separator 404. The hydrogen (H ₂ ) separated after the gas-liquid separation process can be measured by the gas flow meter 405 to obtain the content of hydrogen (H ₂ ). The polyhydroxy fatty acid ester (PHA) flows from the bottom of the gas-liquid separator 404 to the collection tank 406.

The aforementioned heat preservation chamber 45 is provided with a reflux pipe 451 and a delivery pipe 452 connected to the constant temperature heating tank 403. The constant temperature heating tank 403 can circulate and deliver warm water into the heat preservation chamber 45, so that the anaerobic reaction chamber 46 and the aeration reaction chamber 47 maintain a constant temperature state, providing better reaction conditions.

Please refer to Figures 3 and 4. In order to ensure that the upper and lower reaction spaces do not exchange liquid (to prevent the upper layer from flowing back to the lower layer), the continuous gas lift double chamber bioreactor 40 of the preferred embodiment of the present invention can simultaneously achieve the conditions of anaerobic in the lower layer and aerobic in the upper layer. Therefore, a disk-shaped liquid horizontal distributor 44 is provided inside the continuous gas lift double chamber bioreactor 40 to raise the volatile fatty acid (VFA) liquid and hydrogen ( _H2 ) produced in the lower anaerobic reaction chamber 46 to the upper aeration reaction chamber 47 for oxygen consumption reaction, thereby obtaining hydrogen ( _H2 ) and polyhydroxy fatty acid ester (PHA). A ring-shaped fixed plate 48 is provided on the inner wall of the inner tank 41, and the liquid horizontal distributor 44 is fixed on the fixed plate 48. In this embodiment, the liquid horizontal distributor 44 and the fixed plate 48 are fixed by plugging as shown in FIG5 .

Referring to FIGS. 4 to 8 , the aforementioned liquid horizontal distributor 44 includes a horizontal distribution plate 49 and a plurality of hole covers 50; wherein the horizontal distribution plate 49 is provided with a plurality of overflow pipes 51 penetrating the horizontal distribution plate 49, and each overflow pipe 51 is provided with a plurality of fixing posts 52 at the upper end thereof, and each hole cover 50 is provided with a plurality of fixing holes 53 corresponding to the number of the plurality of fixing posts 52. In the present embodiment, four fixing posts 52 and four fixing holes 53 are provided, and each hole cover 50 is provided with a plurality of fixing posts 52 and a plurality of fixing holes 53 corresponding to the number of the plurality of fixing posts 52. As shown in FIG7 and FIG8, the fixing hole 53 can be sleeved on the upper end of the fixing column 52 of the overflow pipe 51, so that the overflow pipe 51 is accommodated in the groove 54 of the hole cover 50 to form a plurality of overflow ports 55 and an annular opening 56. Through the design of the horizontal distribution plate 49 of the liquid horizontal distributor 44 and the plurality of hole covers 50, the volatile fatty acids (VFA) that rise to the upper aeration reaction chamber 47 can be prevented from flowing back to the lower anaerobic reaction chamber 46.

When in use, as shown in FIG. 3 and FIG. 9 , first, the inner tank 41 of the continuous gas lift double chamber bioreactor 40 of the present invention uses a constant temperature heating tank 403 to circulate 37°C constant temperature water into the insulation chamber 45 between the inner tank 41 and the outer tank 43, so that the anaerobic reaction chamber 46 and the aeration reaction chamber 47 are kept at a constant temperature. The organic material source in the substrate tank 401 is pumped into the lower anaerobic reaction chamber 46 to react with the anaerobic hydrogen-producing immobilized microorganisms therein, and after being uniformly stirred by the magnetic stirrer 462, hydrogen (H ₂ ) and volatile fatty acids (VFA) are produced through anaerobic fermentation. The hydrogen (H ₂ ) and volatile fatty acids (VFA) produced by the anaerobic reaction chamber 46 pass through the overflow ports 55 in the liquid horizontal distributors 44 and enter the upper aeration reaction chamber 47 through the annular opening 56 (as shown in FIG. 9 ). When the lower anaerobic reaction chamber 46 is continuously fed, only a single-direction overflow will enter the upper aeration reaction chamber 47. At the same time, air is pumped into the aeration reaction chamber 47 to allow the volatile fatty acids (VFA) in the upper aeration reaction chamber 47 to undergo an oxygen-consuming reaction with aerobic and immobilized microorganisms. The upper aeration reaction chamber 47 uses a motor agitator 473 to mix the liquid phase evenly. The upper aeration chamber 47 is connected to a peristaltic pump via an acid-base detector 471 for pH control. If the pH of the aeration chamber 47 is detected to be lower than a set range due to an acidification reaction, the peristaltic pump is driven to introduce alkaline solution (NaOH) to control the pH of the aeration chamber 47. An air inlet pipe 472 is placed above the liquid horizontal distributor 44 in the upper aeration reaction chamber 47 for producing polyhydroxy fatty acid ester (PHA), and air is pumped into the upper aeration reaction chamber 47 by a peristaltic pump to make it an aerobic environment. The hydrogen ( _H2 ) and polyhydroxy fatty acid ester (PHA) produced in the upper aeration reaction chamber 47 enter the gas-liquid separator 404 through the discharge pipe 475. The hydrogen ( _H2 ) part enters the gas flow meter 405 from the upper part of the gas-liquid separator 404 through the water seal to calculate the hydrogen ( _H2 ) production. The polyhydroxy fatty acid ester (PHA) is collected by the collecting tank 406 and then separated into polyhydroxy fatty acid ester (PHA).

Referring to FIG. 9 , in this embodiment, a liquid horizontal distributor 44 is provided in the inner tank 41 to divide the inner tank 41 into two different reaction spaces (the lower anaerobic reaction chamber 46 and the upper aeration reaction chamber 47), which can ensure that the upper and lower reaction spaces do not exchange liquids (to prevent the upper layer from flowing back to the lower layer). The continuous airlift double-chamber bioreactor 40 can simultaneously achieve the conditions of anaerobic in the lower layer and aerobic in the upper layer, so that the volatile fatty acids (VFA) and hydrogen (H ₂ ) produced in the lower anaerobic reaction chamber 46 rise to the upper aeration reaction chamber 47 for oxygen consumption reaction, thereby obtaining hydrogen (H ₂ ) and polyhydroxy fatty acid esters (PHA), which can reduce the production cost and operating expenses of polyhydroxy fatty acid esters (PHA), and can realize industrial production and have environmental protection effects.

The above-mentioned embodiments are descriptions of the preferred implementation methods of the present invention and do not limit the scope of the present invention. Under the premise of not departing from the design spirit of the present invention, various modifications and improvements made by ordinary technicians in this field to the technical solution of the present invention should fall within the scope of protection determined by the claims of the present invention.

40: Continuous airlift double chamber bioreactor

41: Inner groove

42: Upper cover

43: External groove

44: Liquid horizontal distributor

45: Incubator

451: Reflux pipe

452:Transmission pipe

46: Anaerobic reaction chamber

461: Feed pipe

462:Magnetic stirrer

47: Aeration reaction chamber

471: Acid and Alkali Detector

472: Intake pipe

473: Mixer

474: Alkaline liquid feed pipe

475: Discharge pipe

Claims (7)

A continuous airlift double chamber bioreactor includes at least an inner tank, an upper cover is provided on the upper part of the inner tank, an outer tank is provided on the outside, and an insulation chamber is formed between the inner tank and the outer tank; its characteristic is that a liquid horizontal distributor is provided inside the inner tank, so that the inner tank is divided into two different reaction spaces, the lower reaction space is an anaerobic reaction chamber, and the upper reaction space is an aerated reaction chamber. As described in claim 1, the continuous gas-lift double-chamber bioreactor, wherein the liquid horizontal distributor includes a horizontal distribution plate and a plurality of hole covers, wherein the horizontal distribution plate is provided with a plurality of overflow pipes penetrating the horizontal distribution plate, and the upper end of each overflow pipe is provided with a plurality of fixing columns, and the upper end of each hole cover is provided with a plurality of fixing holes, and the inner part is provided with a groove, and the fixing holes on the hole cover can be sleeved on the upper end of the fixing column at the upper end of the overflow pipe, so that the overflow pipe is accommodated in the groove of the hole cover to form a plurality of overflow ports and an opening. The continuous airlift double-chamber bioreactor as described in claim 1, wherein the anaerobic reaction chamber is provided with a feed pipe and a magnetic agitator, the feed pipe is used to provide an input organic material source into the anaerobic reaction chamber, and the magnetic agitator is used to provide stirring of the organic material source. A continuous gas-lift double-chamber bioreactor as described in claim 1, wherein the aeration chamber is provided with an acid-base detector, an alkaline liquid feed pipe, an air inlet pipe, an agitator, and a discharge pipe, wherein the acid-base detector is used to detect the acidity and alkalinity of the liquid in the aeration chamber, the alkaline liquid feed is used to transport the alkaline liquid into the aeration chamber, the air inlet pipe is used to provide oxygen to enter the aeration chamber, the agitator is used to stir the liquid in the aeration chamber, and the discharge pipe is used to output hydrogen ( _H2 ) and polyhydroxy fatty acid ester (PHA). The continuous airlift double-chamber bioreactor as described in claim 1, wherein the insulation chamber is provided with a reflux pipe and a delivery pipe for delivering warm water into the insulation chamber so as to maintain a constant temperature of the liquid in the anaerobic reaction chamber and the aeration reaction chamber. The continuous airlift double-chamber bioreactor as described in claim 1, wherein an annular fixed plate is provided inside the inner tank, and the liquid horizontal distributor is assembled above the annular fixed plate. A continuous airlift double-chamber bioreactor as described in claim 1, wherein the liquid level distributor is in the shape of a disk.

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