Device for fermenting gas-feeding microorganisms and absorbing and utilizing carbon dioxide

Abstract

The utility model relates to a device for fermenting by utilizing gas-feeding microorganisms and absorbing and utilizing carbon dioxide, which is characterized in that a stirring shaft with a gas passage is arranged in each fermentation tank, an aeration stirring paddle is arranged on a first stirring shaft, a gas storage tank pipeline is communicated with the upper end of the first gas passage, and the first gas passage is communicated with an inner cavity of the aeration stirring paddle; the first fermentation tank is communicated with the upper end of a second air channel through a pipeline, the lower end of the second air channel is communicated with an inner cavity of the air spraying pipe A. The lower end of a third stirring shaft is provided with an air spraying pipe B. The second fermentation tank is communicated with the upper end of a third air channel through a pipeline, and the lower end of the third air channel is communicated with an inner cavity of the air spraying pipe B. The third fermentation tank is communicated with the upper end of a fourth air channel through a pipeline, the lower end of the fourth air channel is communicated with an inner cavity of the aeration pipe, all the fermentation tanks are sequentially connected through fermentation liquid pipelines, and the volumes of the fermentation tanks are sequentially halved. According to the utility model, the absorption and utilization rate of CO2 can be improved to more than 90% at one time.

Description

Technical Field

[0001] This utility model relates to the field of microbial fermentation technology, specifically a device that utilizes aerobic microorganisms for fermentation and absorption and utilization of carbon dioxide. Background Technology

[0002] In existing technologies, chemical catalysis methods (such as Fischer-Tropsch synthesis) can be used to convert gases containing carbon dioxide, carbon monoxide, and / or hydrogen, such as industrial waste gas or syngas, into various fuels and chemicals. With the development of technology, microbial gaseous fermentation, which can biologically fix the above gases, has also been gradually promoted and applied. Compared with chemical catalysis, microbial gaseous fermentation has milder process conditions, lower energy consumption, higher product specificity, higher yield, and stronger resistance to toxicity, thus showing good development prospects.

[0003] In the field of biotechnology, aerobic microbial fermentation is considered a promising method for CO2 absorption and utilization. Aerobic microorganisms are a major type of chemocarbon-fixing bacteria, belonging to the Gram-positive anaerobic clostridium species. Currently known aerobic microorganisms include *Clostridium yangdellense* (also known as *Clostridium yangdellense*). Clostridium ljungdahlii ), self-producing alcohol-producing Clostridium ( Clostridium autoethanogenum ), Clostridium carbonmonoxide( Clostridium carboxidivorans ) and Acetobacter wrasse ( Acetobacterium woodii In addition to fixing Cl gases such as CO / CO2, gas-eating microorganisms can also convert them into important metabolic intermediates—acetyl-CoA—through a series of catalytic reactions. These intermediates are then used to synthesize various products, such as acetic acid, ethanol, butanol, hexanol, and other chemicals and fuels, through various metabolic pathways. Therefore, they have great potential for industrial applications.

[0004] However, most of the tanks used for microbial fermentation in the current technology are single-tank fermentation systems, and their CO2 absorption and utilization rate is only 50-60%. This means that a large amount of CO2 is not effectively absorbed, which not only wastes the raw material gas, but also increases the cost and complexity of exhaust gas treatment.

[0005] Patent CN112300971B discloses a method for improving the carbon monoxide utilization rate of Clostridium aeruginosa using high-throughput gene synthesis, but the carbon monoxide utilization rate of the engineered Clostridium aeruginosa in this method is ≥30.0%, preferably ≥37.5%, and more preferably ≥40.0%.

[0006] Patent CN105039416B discloses a method for improving the fermentation efficiency of anaerobic aerobic microorganisms. The fermentation system is still a single-tank system, but the method filters and retains the bacterial liquid of anaerobic aerobic microorganisms with a hollow cellulose membrane, then backwashes it with culture medium and ferments the retained bacteria again, thereby achieving multiple continuous fermentation effects. However, as can be seen from the embodiments of this patent, the yield of alcohols such as ethanol still needs to be further improved. Utility Model Content

[0007] The purpose of this invention is to provide a device that utilizes aerobic microorganisms for fermentation and carbon dioxide absorption and utilization. It employs multiple fermentation tanks with successively halved volumes connected in series to achieve multi-stage CO2 utilization. At the same time, different types of stirring shaft structures are designed for tanks of different volumes, which can increase the CO2 absorption and utilization rate to over 90% in one go, while also significantly increasing the yield of alcohol products.

[0008] The objective of this utility model is achieved through the following technical solution:

[0009] An apparatus for utilizing aerobic microorganisms for fermentation and carbon dioxide absorption includes a first fermenter, a second fermenter, a third fermenter, a fourth fermenter, and a gas storage tank. The first fermenter contains a first stirring shaft with an aeration impeller equipped with aeration holes. The first stirring shaft has a first air passage, and the gas storage tank is connected to the upper end of the first air passage via an air inlet pipe. The shaft wall of the first stirring shaft has a connecting channel connecting the first air passage and the inner cavity of the aeration impeller. The second fermenter contains a second stirring shaft with a jet pipe A equipped with multiple gas nozzles at its lower end. The second stirring shaft has a second air passage, and the upper end of the first fermenter is connected to the upper end of the second air passage via a first air outlet pipe. The lower end of the second air passage is connected to the inner cavity of the jet pipe A. The third fermenter contains a third stirring shaft. The third fermentation tank has a third stirring shaft, and the lower end of the third stirring shaft is equipped with a jet pipe B with multiple jet nozzles. The third stirring shaft has a third air channel inside, and the upper end of the second fermentation tank is connected to the upper end of the third air channel through a second air outlet pipe. The lower end of the third air channel is connected to the inner cavity of the jet pipe B. The third stirring shaft is equipped with a honeycomb-shaped guide tube. The fourth fermentation tank has a fourth stirring shaft inside, and the lower end of the fourth stirring shaft is equipped with an aeration pipe with aeration holes. The fourth stirring shaft has a fourth air channel inside, and the upper end of the third fermentation tank is connected to the upper end of the fourth air channel through a third air outlet pipe. The lower end of the fourth air channel is connected to the inner cavity of the aeration pipe. The first fermentation tank, the second fermentation tank, the third fermentation tank, and the fourth fermentation tank are connected in sequence through corresponding fermentation liquid pipelines, and their volumes are halved in sequence. The upper ends of the first fermentation tank, the second fermentation tank, the third fermentation tank, and the fourth fermentation tank are all equipped with fermentation liquid feeding pipes.

[0010] The gas nozzle assembly includes a reduced-diameter nozzle, a connecting frame, and a spray bar, wherein one end of the spray bar is provided with an intake nozzle and the other end is provided with an output nozzle, the reduced-diameter nozzle is mounted on the jet pipe A, and the reduced-diameter nozzle and the intake nozzle are respectively located on both sides of the connecting frame.

[0011] The first fermenter has a first air outlet at its upper end, and the first air outlet is connected to the upper end of the second air passage through a first air outlet pipe. The second fermenter has a second air outlet at its upper end, and the second air outlet is connected to the upper end of the third air passage through a second air outlet pipe. The third fermenter has a third air outlet at its upper end, and the third air outlet is connected to the upper end of the fourth air passage through a third air outlet pipe. The fourth fermenter has a fourth air outlet at its upper end, and the fourth air outlet is connected to a gas output pipe.

[0012] An intake flow meter is installed on the intake pipe, a gas output flow meter is installed on the gas output pipe, and an outlet flow control valve is installed on the first outlet pipe, the second outlet pipe, and the third outlet pipe.

[0013] The first fermenter has a feeding port at its upper end and a first liquid inlet on one side. The second fermenter has a second liquid outlet on one side and a second liquid inlet on the other side. The third fermenter has a third liquid outlet on one side and a third liquid inlet on the other side. The fourth fermenter has a fourth liquid outlet on one side. The first liquid inlet is connected to the second liquid outlet through a first fermentation liquid pipeline. The second liquid inlet is connected to the third liquid outlet through a second fermentation liquid pipeline. The third liquid inlet is connected to the fourth liquid outlet through a third fermentation liquid pipeline. In addition, the lower ends of the first, second, third, and fourth fermenters are all provided with discharge ports.

[0014] Fermentation broth flow meters and fermentation broth control valves are installed on the first, second, and third fermentation broth pipelines.

[0015] The first fermenter is provided with a first feeding port at its upper end, the second fermenter is provided with a second feeding port at its upper end, the third fermenter is provided with a third feeding port at its upper end, and the fourth fermenter is provided with a fourth feeding port at its upper end. The first feeding port, the second feeding port, the third feeding port and the fourth feeding port are respectively connected to a feeding main pipe through corresponding fermentation liquid feeding pipes. The feeding main pipe is connected to a feeding tank. The fermentation liquid feeding pipe is provided with a feeding flow control valve.

[0016] The first fermenter is provided with a first drive assembly for driving the first stirring shaft to rotate at its upper end; the second fermenter is provided with a second drive assembly for driving the second stirring shaft to rotate at its upper end; the third fermenter is provided with a third drive assembly for driving the third stirring shaft to rotate at its upper end; and the fourth fermenter is provided with a fourth drive assembly for driving the fourth stirring shaft to rotate at its upper end.

[0017] The first drive assembly, the second drive assembly, the third drive assembly, and the fourth drive assembly have the same structure, each including a stirring reduction motor, a transmission belt, and a stirring shaft adapter. The stirring shaft adapter has a rotating shaft sleeve inside that is fitted onto a corresponding pipeline. A driven pulley is fitted on the outside of the stirring shaft adapter. A driving pulley is provided on the output shaft of the stirring reduction motor, and the driving pulley is connected to the driven pulley via a transmission belt.

[0018] The first, second, third, and fourth fermenters are all equipped with sensor mounting ports and sampling ports; the first stirring shaft is also equipped with a first defoaming paddle, the second stirring shaft is also equipped with a second defoaming paddle and stirring blade A, the third stirring shaft is also equipped with a third defoaming paddle, and the third defoaming paddle is located on the upper side of the honeycomb guide tube; the fourth stirring shaft is also equipped with a fourth defoaming paddle and stirring blade B.

[0019] The advantages and positive effects of this utility model are as follows:

[0020] This invention uses multiple fermenters with successively halved volumes connected in series to achieve multi-stage CO2 utilization. At the same time, different types of stirring shaft structures are designed for different tank volumes, which can increase the CO2 absorption and utilization rate to over 90% in one go, while also significantly increasing the yield of alcohol products.

[0021] In this invention, the aeration impeller on the first stirring shaft of the first fermentation tank, which has the largest volume, aerates the gas through the aeration holes on the impeller blades. The bubbles can be dispersed by the impeller blades, thus achieving a more dispersed gas distribution.

[0022] In this invention, the gas nozzle assembly on the jet pipe A of the second fermenter includes a reduced-diameter nozzle, a connecting frame, and a spray bar. The gas is first ejected from the reduced-diameter nozzle into the hollow part of the connecting frame. At this time, its static pressure energy is converted into velocity energy, and the pressure of the suction nozzle is also reduced. Under the action of the gas jet, the fermentation liquid and the gas enter the spray bar together and are ejected through the output nozzle. In this way, the gas and liquid phases in the spray bar develop from initial mixing to intense mixing and oscillation, and generate gas dynamic atomization and pressure atomization, which pulverizes the fermentation liquid and air into a large number of tiny particles, creating a highly turbulent, expanded, and constantly renewed emulsion interface between the gas and liquid. At the same time, it can improve the degree of gas solubility and significantly reduce the stirring power required by the agitator, and reduce the shear force damage of the agitator to the fermentation liquid. This can meet the gas distribution needs of the second fermenter with a volume reduced by half.

[0023] In this invention, considering the counter-current flow characteristics of the fermentation liquid and gas in the third fermenter, a honeycomb-shaped guide tube is set on the third stirring shaft. This increases the solid-liquid contact area while also guiding the flow, and is beneficial to the mass transfer of the fermentation medium and the gas distribution. Attached Figure Description

[0024] Figure 1 This is a schematic diagram of the structure of this utility model.

[0025] Figure 2 for Figure 1 A schematic diagram of the structure of the first fermentation tank.

[0026] Figure 3 for Figure 1 Enlarged view of point A in the image.

[0027] Figure 4 for Figure 1 Enlarged view of point B in the image.

[0028] Figure 5 for Figure 1 Schematic diagram of the structure of the second fermentation tank.

[0029] Figure 6 for Figure 5 A schematic diagram of the structure of the gas nozzle assembly.

[0030] Figure 7 for Figure 1 Schematic diagram of the structure of the third fermentation tank in the middle.

[0031] Figure 8 for Figure 1 Schematic diagram of the structure of the fourth fermentation tank in the middle.

[0032] Figure 9 This is a schematic diagram illustrating the effect of one application example of this utility model.

[0033] Figure 10 This is a schematic diagram illustrating the theoretical utilization efficiency of each fermenter after its volume is successively halved.

[0034] Wherein, 1 is the first fermentation tank, 101 is the stirring reduction motor, 102 is the transmission belt, 103 is the first stirring shaft, 1031 is the first defoaming impeller, 1032 is the aeration stirring impeller, 10321 is the impeller aeration hole, 10322 is the connecting channel, 1033 is the stirring shaft adapter, 10331 is the rotating bushing, 10332 is the driven pulley, 1034 is the first air passage, 104 is the first air outlet, 105 is the first feeding port, 106 is the first liquid inlet, 107 is the sensor mounting port, and 108 is the sampling port. Sample port, 109 is the discharge port, 110 is the feeding port, 2 is the second fermentation tank, 201 is the second liquid outlet, 202 is the second liquid inlet, 203 is the second stirring shaft, 2031 is the second defoaming impeller, 2032 is the stirring impeller blade A, 2033 is the second air passage, 204 is the second air outlet, 205 is the second feeding port, 206 is the second drive assembly, 207 is the jet pipe A, 208 is the gas nozzle assembly, 2081 is the diameter reduction nozzle, 2082 is the suction nozzle, 2083 is the spray bar, 2084 is the output spray bar. 2085 is the connecting frame, 3 is the third fermentation tank, 301 is the third liquid outlet, 302 is the second liquid inlet, 303 is the third stirring shaft, 304 is the third air outlet, 305 is the third feed inlet, 306 is the third drive assembly, 307 is the jet pipe B, 308 is the jet nozzle, 309 is the honeycomb guide tube, 4 is the fourth fermentation tank, 401 is the fourth liquid outlet, 402 is the gas output flow meter, 403 is the fourth stirring shaft, 4031 is the fourth defoaming impeller, 4032 is the stirring blade B, and 4033 is the aeration... The components are as follows: 404 is the fourth air outlet, 405 is the fourth feed inlet, 406 is the fourth drive assembly, 5 is the air storage tank, 6 is the feed tank, 7 is the feed main pipe, 701 is the fermentation broth feed pipe, 8 is the air inlet pipe, 801 is the air inlet flow meter, 9 is the first air outlet pipe, 10 is the second air outlet pipe, 11 is the third air outlet pipe, 12 is the air outlet flow control valve, 13 is the first fermentation broth pipe, 14 is the second fermentation broth pipe, 15 is the third fermentation broth pipe, 16 is the fermentation broth flow meter, and 17 is the fermentation broth pipe control valve. Detailed Implementation

[0035] The present invention will now be described in further detail with reference to the accompanying drawings.

[0036] like Figures 1-9 As shown, this utility model includes a first fermentation tank 1, a second fermentation tank 2, a third fermentation tank 3, a fourth fermentation tank 4, and a gas storage tank 5, wherein... Figures 1-3As shown, the first fermenter 1 is equipped with a first stirring shaft 103, and the first stirring shaft 103 is equipped with an aeration stirring paddle 1032 with aeration holes 10321. The first stirring shaft 103 is equipped with a first air passage 1034, and the air storage tank 5 is connected to the upper end of the first air passage 1034 through an air inlet pipe 8. The shaft wall of the first stirring shaft 103 is equipped with a connecting channel 10322 connecting the first air passage 1034 and the inner cavity of the aeration stirring paddle 1032. Figure 5 As shown, the second fermenter 2 is equipped with a second stirring shaft 203 inside, and the lower end of the second stirring shaft 203 is equipped with a jet pipe A207 with multiple gas nozzle assemblies 208. The second stirring shaft 203 is equipped with a second air passage 2033 inside, and the upper end of the first fermenter 1 is connected to the upper end of the second air passage 2033 through a first air outlet pipe 9. The lower end of the second air passage 2033 is connected to the inner cavity of the jet pipe A207. Figure 7 As shown, the third fermenter 3 is equipped with a third stirring shaft 303 inside, and the lower end of the third stirring shaft 303 is equipped with a jet pipe B307 with multiple jet nozzles 308. The third stirring shaft 303 is equipped with a third air passage inside, and the upper end of the second fermenter 2 is connected to the upper end of the third air passage through a second air outlet pipe 10. The lower end of the third air passage is connected to the inner cavity of the jet pipe B307. In addition, the third stirring shaft 303 is equipped with a honeycomb-shaped guide tube 309, such as... Figure 8 As shown, the fourth fermenter 4 is equipped with a fourth stirring shaft 403 inside, and the lower end of the fourth stirring shaft 403 is equipped with an aeration pipe 4033 with aeration holes. The fourth stirring shaft 403 is equipped with a fourth air passage inside, and the upper end of the third fermenter 3 is connected to the upper end of the fourth air passage through a third air outlet pipe 11. The lower end of the fourth air passage is connected to the inner cavity of the aeration pipe 4033. Additionally, as shown... Figure 1 As shown, the first fermenter 1, the second fermenter 2, the third fermenter 3 and the fourth fermenter 4 are connected in sequence through corresponding fermentation liquid pipelines and their volumes are halved in sequence. The upper ends of the first fermenter 1, the second fermenter 2, the third fermenter 3 and the fourth fermenter 4 are all provided with fermentation liquid feeding pipes 701.

[0037] like Figures 1-9As shown, in this embodiment, the first fermenter 1 is provided with a first air outlet 104 at its upper end, and the first air outlet 104 is connected to the upper end of the second air passage 2033 through the first air outlet pipe 9. The second fermenter 2 is provided with a second air outlet 204 at its upper end, and the second air outlet 204 is connected to the upper end of the third air passage through the second air outlet pipe 10. The third fermenter 3 is provided with a third air outlet 304 at its upper end, and the third air outlet 304 is connected to the upper end of the fourth air passage through the third air outlet pipe 11. The fourth fermenter 4 is provided with a fourth air outlet 404 at its upper end, and the fourth air outlet 404 is connected to a gas output pipe. In operation, CO2 from the gas storage tank 5 is input into the first air passage 1034 within the first stirring shaft 103 of the first fermentation tank 1 via the air inlet pipe 8. During the rotation of the first stirring shaft 103, CO2 is output into the tank body of the first fermentation tank 1 through the slurry aeration holes 10321 on each aeration stirring paddle 1032. Then, the fermentation gas in the first fermentation tank 1 is output from the first air outlet 104 and enters the second air passage 203 within the second stirring shaft 203 via the first air outlet pipe 9. During the rotation of the second stirring shaft 203, CO2 is ejected into the tank body of the second fermentation tank 2 through the jet pipe A207 at its lower end. Then, the second fermentation... Fermentation gas in fermenter 2 is output from the second outlet 204 and enters the third air passage in the third stirring shaft 303 through the second outlet pipe 10. Then, it is ejected into the tank body of the third fermenter 3 through the jet pipe B307 at the lower end of the third stirring shaft 303. Fermentation gas in the third fermenter 3 is then output from the third outlet 304 and enters the fourth air passage in the fourth stirring shaft 403 through the third outlet pipe 11. Finally, it is output into the tank body of the fourth fermenter 4 through the aeration pipe 4033 at the lower end of the fourth stirring shaft 403. Excess gas in the fourth fermenter 4 can be discharged through the gas output pipe through the fourth outlet 404.

[0038] One of the primary objectives of this invention is to address the problem of low CO2 absorption and utilization rate in existing single-fermentation tank systems (60% in this embodiment), assuming a CO2 intake of 1m³. 3 If so, then the discharged gas will still have 0.4m³. 3 This invention achieves multi-stage CO2 utilization by using multiple fermenters connected in series, with the volume of each fermenter decreasing by half in successive stages. Thus, its theoretical utilization efficiency is as follows: Figure 10 As shown.

[0039] Secondly, this invention designs different types of stirring shaft structures for tanks of different volumes. During the gas flow process, in the largest fermentation tank 1, the aeration stirring paddle 1032 on the first stirring shaft 103 aerates gas through the aeration holes 10321. The bubbles are dispersed by the paddle, resulting in a more dispersed gas distribution. In the second fermentation tank 2, the gas nozzle assembly 208 on the jet pipe A207... Figure 6 As shown, it includes a converging nozzle 2081, a connecting frame 2085, and a spray bar 2083. One end of the spray bar 2083 has an intake nozzle 2082, and the other end has an output nozzle 2084. The converging nozzle 2081 is mounted on the jet pipe A207, and the converging nozzle 2081 and the intake nozzle 2082 are respectively located on both sides of the connecting frame 2085. Gas is first ejected from the converging nozzle 2081 into the hollow part of the connecting frame 2085. At this time, its static pressure energy is converted into velocity energy, and the pressure of the intake nozzle 2082 is also reduced. Under the action of this gas injection, the fermentation broth, along with the gas, enters the spray bar 2083 and is ejected through the output nozzle 2084. In this way, the gas and liquid phases develop from initial mixing within the spray bar 2083. The intense mixing and oscillation generate gas dynamic atomization and pressure atomization, breaking the fermentation broth and air into numerous tiny particle groups. This creates a highly turbulent, expanded, and continuously renewing emulsified interface between the gas and liquid, simultaneously improving gas solubility and significantly reducing the stirring power required by the agitator, thus minimizing shear force damage to the fermentation broth. In the third fermenter 3, since the flow direction of the fermentation broth is opposite to that of the gas, the honeycomb-shaped guide tube 309 on the third stirring shaft 303 increases the solid-liquid contact area while also guiding the flow, which is beneficial for mass transfer and gas distribution in the fermentation medium. Finally, in the fourth fermenter 4, the aeration pipe 4033 at the lower end of the fourth stirring shaft 403 can fully utilize the residual fermentation gas, further improving gas utilization. This invention, through the above structural combination design, can ensure the CO2 absorption and utilization rate of the actual equipment system, such as... Figure 9 As shown, in one application example of this utility model, the absorption and utilization rate of CO2 can be increased to over 90% in one go, while the production of acetic acid is also greatly increased.

[0040] like Figure 1 and Figure 8 As shown, in this embodiment, an intake flow meter 801 is provided on the intake pipe 8, and a gas output flow meter 402 is provided on the gas output pipe for real-time monitoring of the intake and output air volume of this utility model. Additionally, as shown... Figure 1 As shown, in this embodiment, the first gas outlet pipe 9, the second gas outlet pipe 10, and the third gas outlet pipe 11 are all equipped with gas outlet flow control valves 12 to control the gas outlet flow of each fermenter.

[0041] like Figures 1-9 As shown in this embodiment, the first fermenter 1 has a feeding port 110 at its upper end, a first liquid inlet 106 on one side, a second liquid outlet 201 on one side and a second liquid inlet 202 on the other side, a third liquid outlet 301 on one side and a third liquid inlet 302 on the other side, and a fourth liquid outlet 401 on one side. The first liquid inlet 106 is connected to the second liquid outlet 201 through a first fermentation liquid pipeline 13, the second liquid inlet 202 is connected to the third liquid outlet 301 through a second fermentation liquid pipeline 14, and the third liquid inlet 302 is connected to the fourth liquid outlet 401 through a third fermentation liquid pipeline 15. In addition, the lower ends of the first fermenter 1, the second fermenter 2, the third fermenter 3, and the fourth fermenter 4 are all provided with discharge ports 109. In operation, the feeding port 110 is used to feed a fixed amount of fermentation liquid into the first fermentation tank 1. Simultaneously, the flow direction of the fermentation liquid in each tank is opposite to that of the gas, that is, the fermentation liquid flows along the direction of the fourth fermentation tank 4, the third fermentation tank 3, and the second fermentation tank 2, ultimately accumulating in the first fermentation tank 1. Figures 1-9 As shown, the first fermenter 1 is provided with a first feeding port 105 at its upper end, the second fermenter 2 is provided with a second feeding port 205 at its upper end, the third fermenter 3 is provided with a third feeding port 305 at its upper end, and the fourth fermenter 4 is provided with a fourth feeding port 405 at its upper end. The first feeding port 105, the second feeding port 205, the third feeding port 305, and the fourth feeding port 405 are respectively connected to a feeding main pipe 7 through corresponding fermentation liquid feeding pipes 701. The feeding main pipe 7 is connected to a feeding tank 6. The above structure is used to replenish fresh culture medium into each tank. The fermentation liquid feeding pipe 701 is provided with a feeding flow control valve to control the feeding amount.

[0042] Other examples Figure 1 As shown in this embodiment, the first fermentation broth pipeline 13, the second fermentation broth pipeline 14, and the third fermentation broth pipeline 15 are all equipped with a fermentation broth flow meter 16 and a fermentation broth pipeline control valve 17 to control the fermentation broth flow and pipeline opening and closing.

[0043] like Figures 1-9As shown, the first fermenter 1 has a first driving assembly at its upper end for driving the first stirring shaft 103 to rotate; the second fermenter 2 has a second driving assembly 206 at its upper end for driving the second stirring shaft 203 to rotate; the third fermenter 3 has a third driving assembly 306 at its upper end for driving the third stirring shaft 303 to rotate; and the fourth fermenter 4 has a fourth driving assembly 406 at its upper end for driving the fourth stirring shaft 403 to rotate. In this embodiment, the first driving assembly, the second driving assembly 206, the third driving assembly 306, and the fourth driving assembly 406 have the same structure, each including a stirring reduction motor 101, a transmission belt 102, and a stirring shaft adapter 1033, wherein, as shown in the figure... Figure 3 Taking the first drive assembly shown as an example, the stirring shaft adapter 1033 is located at the upper end of the first stirring shaft 103, and a rotating bushing 10331 is provided inside the stirring shaft adapter 1033 and fitted onto the output end of the air intake pipe 8. This achieves a rotatable connection between the stirring shaft adapter 1033 and the air intake pipe 8. Simultaneously, the air intake pipe 8 is connected to the first air passage 1034 inside the first stirring shaft 103. A driven pulley 10332 is fitted onto the outer side of the stirring shaft adapter 1033. A driving pulley is provided on the output shaft of the stirring reduction motor 101, and the driving pulley is connected to the driven pulley 10332 via a transmission belt 102. The stirring shaft adapters of other drive assemblies are replaced with those rotatably connected to the corresponding air outlet pipe output ends. Additionally, as shown... Figure 2 As shown, each fermenter body is also equipped with bearings at the position where the stirring shaft passes through to support its rotation.

[0044] like Figure 2 As shown, the first fermenter 1, the second fermenter 2, the third fermenter 3, and the fourth fermenter 4 are all equipped with sensor mounting ports 107 and sampling ports 108. The sensor mounting ports 107 can be equipped with appropriate sensors, such as temperature sensors, pressure sensors, etc., according to actual needs. The sampling ports 108 are used for sampling and analysis.

[0045] like Figure 2 As shown, in this embodiment, the first stirring shaft 103 is also provided with a first defoaming paddle 1031, such as... Figure 5 As shown, in this embodiment, the second stirring shaft 203 is also provided with a second defoaming impeller 2031 and a stirring blade A2032, as follows: Figure 7 As shown, in this embodiment, the third stirring shaft 303 is further provided with a third defoaming impeller, and the third defoaming impeller is located on the upper side of the honeycomb-shaped guide tube 309, as shown. Figure 8 As shown in this embodiment, the fourth stirring shaft 403 is also provided with a fourth defoaming paddle 4031 and a stirring blade B4032.

[0046] The working principle of this utility model is as follows:

[0047] In operation, CO2 from the gas storage tank 5 is input into the first air passage 1034 within the first stirring shaft 103 via the air inlet pipe 8. During the rotation of the first stirring shaft 103, CO2 is output through the aeration holes 10321 on each aeration stirring paddle 1032 into the tank body of the first fermentation tank 1. Then, the fermentation gas in the first fermentation tank 1 is output from the first air outlet 104 and enters the second air passage 203 within the second stirring shaft 203 via the first air outlet pipe 9. During the rotation of the second stirring shaft 203, CO2 is ejected from its lower end through the jet pipe A207 into the tank body of the second fermentation tank 2. Then, the second fermentation tank 2... The fermentation gas inside the fermentation tank is output from the second outlet 204 and enters the third air passage within the third stirring shaft 303 via the second outlet pipe 10. The gas is then ejected from the jet pipe B307 at the lower end of the third stirring shaft 303 into the tank body of the third fermenter 3. The fermentation gas in the third fermenter 3 is then output from the third outlet 304 and enters the fourth air passage within the fourth stirring shaft 403 via the third outlet pipe 11. Finally, the gas is output from the aeration pipe 4033 at the lower end of the fourth stirring shaft 403 into the tank body of the fourth fermenter 4. Excess gas in the fourth fermenter 4 can be discharged through the gas outlet pipe via the fourth outlet 404. The fermentation liquid flows in the opposite direction to the gas, i.e., it flows along the direction of the fourth fermenter 4, the third fermenter 3, and the second fermenter 2, eventually accumulating in the first fermenter 1. Simultaneously, the feeding tank 6 replenishes fresh culture medium to each tank.

[0048] The fermentation strains used in this invention are aerobic microbial strains, including Clostridium yunnanense (Clostridium yunnanense). Clostridium ljungdahlii ), self-producing alcohol-producing Clostridium ( Clostridium autoethanogenum ), Clostridium carbonmonoxide( Clostridium carboxidivorans ) and Acetobacter wrasse ( Acetobacterium woodii ).

[0049] This invention achieves multi-stage CO2 utilization by using multiple fermenters connected in series, with the volume of each fermenter being halved in turn. This increases the CO2 utilization efficiency to over 90% and significantly increases the yield of acetic acid / alcohol products. In addition, this invention designs different types of stirring shaft structures for different tank volumes to ensure improved CO2 absorption and utilization.

[0050] The following test examples further illustrate the working principle of this utility model.

[0051] In this test case, the aerobic microbial strain used was *Clostridium yunnanense* (Clostridium yunnanense). Clostridium ljungdahlii The specific process is as follows:

[0052] 1. Inoculate Clostridium yongdarii into an anaerobic bottle containing PETC medium at an inoculation rate of 5-10% v / v. Fill the bottle with a CO2:H2 mixture of 6:4, maintain a pressure of 0.12 MPa and a temperature of 37℃, and incubate for 48-72 hours.

[0053] The PETC culture medium formula is as follows:

[0054] Component A: NH4Cl 1 g / L, KCl 0.1 g / L, MgSO4·7H2O 0.2 g / L, NaCl 0.8 g / L, KH2PO4 0.1 g / L;

[0055] Component B: MnSO4·H2O 0.011 g / L, MnCl2·4H2O 0.013 g / L, CoCl·2H2O 0.002 g / L, ZnSO4·7H2O 0.002 g / L, NiCl·6H2O 0.0002 g / L, Na2WO4·2H2O 0.25 mg / L, Na2SeO3 0.2mg / L, NaMoO4·2H2O 2 mg / L;

[0056] Component C: CaCl2·7H2O 0.023 g / L;

[0057] Component D: Aminotriacetic acid 0.02 g / L;

[0058] Component E: Yeast extract 0.5 g / L, cysteine ​​0.1 g / L, cysteine ​​hydrochloride 1.5-3.0 g / L, NaHCO3 0.99 g / L;

[0059] Component F: Vitamins (1000x): Biotin 10 mg / L, Folic Acid 20 mg / L, Vitamin B6 100 mg / L, Thiamine 250 mg / L, Riboflavin 50 mg / L, Niacin 50 mg / L, Calcium Pantothenate 40 mg / L, Cyanocobalamin 50 mg / L, Para-aminobenzoic Acid 50 mg / L, Alpha-lipoic Acid 50 mg / L;

[0060] Prepare a stock solution by adding 1 mL per liter of culture medium.

[0061] Component G: FeSO4·7H2O 4 mg / L;

[0062] Adjust the pH to 5.6-5.8.

[0063] II. Single-tank test.

[0064] Clostridium yongdarii cultured to OD 600When the concentration reaches approximately 0.5, the inoculum is transferred to a 20 L seed tank for expansion culture. The culture conditions are PETC medium, 37°C, H2:CO2 gas ratio of 6:4, and pressure of 0.12 MPa, and cultured until OD... 600 After approximately 3 hours, the culture medium is inoculated into the first fermenter 1 via inlet 110. The fermenter pressure is 1.8 MPa, the inoculation ratio is 10%–20%, and the culture conditions are the same as the 20 L seed tank. The initial stirring rate is 200 rpm, and the initial aeration rate is maintained at 0.6 L / min. When the bacteria begin to consume gas, the aeration rate and stirring rate are gradually increased to 2 L / min and 400 rpm, respectively. Fresh culture medium is continuously added from the feed tank 6 via the first feed inlet 105. At the same time, excess fermentation broth is discharged to the microfiltration device through outlet 109 to separate the fermentation cells from the fermentation products, controlling the overall dilution rate at 1.0 / day. During fermentation, the fermentation status is monitored using temperature sensors, pH sensors, and OPR sensors. After fermentation, the fermentation broth is passed through outlet 109 into the filtration and collection system to collect the fermentation products.

[0065] Samples were taken from the sampling port every 6 hours during the fermentation culture.

[0066] Bacterial biomass was determined by measuring absorbance at 600 nm using a spectrophotometer for all samples, and product levels were determined by high-performance liquid chromatography (HPLC). Detection conditions were as follows: HPLC (Agilent 1260B, Agilent Technologies, USA), equipped with a UV detector and an Aminex HPX-87H column (Bio-Rad, USA), column temperature 50°C, mobile phase 5 mM sulfuric acid aqueous solution, flow rate 0.6 mL / min.

[0067] Tail gas analysis: The components of the fermentation tail gas were detected using a gas chromatograph connected to the headspace of the fermenter. The detection conditions were as follows: Huifen gas chromatograph (HF 601), injection volume of 1 mL, injection port temperature of 250℃, chromatographic column of TDX-01 (30m × 0.32mm × 0.5 μm), TCD detector temperature of 300℃, and carrier gas (argon) flow rate of 30 mL / min. The column oven temperature program was as follows: initial temperature of 60℃, then increased to 80℃ (10 min) at a rate of 5℃ / min, then increased to 170℃ (6 min) at a rate of 10℃ / min, and held for 1 min.

[0068] Sampling interval 15 min.

[0069] Experimental results:

[0070] After 7 days of fermentation, the CO2 utilization rate was 56.9%, and the average daily yield of acetic acid was 36.4 g / L. Figure 9 (As shown).

[0071] Dual-tank test.

[0072] The fermentation method, strain cultivation, sampling, and analysis methods are the same as those for single-tank testing. The volume of each fermenter decreases progressively. With the diameter-to-height ratio (D / H) remaining constant, the volume of the second fermenter (2) is half that of the first fermenter (1). The tank pressure decreases sequentially: the pressure of the first fermenter (1) is 1.8 MPa, and the pressure of the second fermenter (2) is 1.5 MPa. The gas flow rate entering the first fermenter (1) is 2 L / min, and the aeration flow rate from the first fermenter (1) to the second fermenter (2) is set to 0.8 L / min. The raw material gas is first introduced into the first fermenter (1), and the fermentation tail gas from the first fermenter (1) is then introduced into the second fermenter (2), finally exiting from the outlet of the second fermenter (2). A portion of the exhaust gas is sampled and detected by gas chromatography. In addition, the fermentation broth in the second fermenter 2 is fed into the first fermenter 1, and fresh culture medium is added from the feed tank 6 to the second fermenter 2 and the first fermenter 1 to maintain the overall dilution rate at 1.0 / day. Excess fermentation broth is discharged to the filtration and collection system through the discharge port 109. The fermentation products are enriched in the first fermenter 1 and finally separated from the fermentation cells and fermentation products through a microfiltration device.

[0073] After 7 days of fermentation, the CO2 utilization rate of the dual-tank series fermentation reached 80.2%. Figure 9 As shown in the figure, the average daily yield of acetic acid is 44.2 g / L.

[0074] Three-can test.

[0075] The fermentation method, strain cultivation, sampling, and analysis methods are the same. The volume of each fermenter decreases progressively, with the diameter-to-height ratio (D / H) remaining constant, each volume being half that of the previous fermenter. The tank pressure decreases sequentially: fermenter 1 has a pressure of 1.8 MPa, fermenter 2 has a pressure of 1.5 MPa, and fermenter 3 has a pressure of 1.2 MPa. The gas flow rate entering fermenter 1 is 3 L / min, the aeration flow rate from fermenter 1 to fermenter 2 is 1.2 L / min, and the gas flow rate from fermenter 2 to fermenter 3 is 0.5 L / min. The raw material gas is sequentially introduced into fermenter 1, fermenter 2, and finally discharged from the outlet of fermenter 3. The fermentation products are enriched in the first fermenter 1 from the third fermenter 3. The feeding tank 6 replenishes fresh culture medium to the third fermenter 3, the second fermenter 2 and the first fermenter 1 respectively, keeping the overall dilution rate at 1.0 / day. Excess fermentation liquid is discharged to the filtration and collection system through the discharge port 109, and finally the fermentation cells and fermentation products are separated by the microfiltration device.

[0076] After 7 days of fermentation, the gas utilization rate of the three tanks in series reached 89.6%. Figure 9 As shown in the figure, the average daily yield of acetic acid is 48.6 g / L.

[0077] Four-can test.

[0078] The fermentation method, strain cultivation, sampling, and analysis methods are the same. The volume of each fermenter decreases progressively, with the diameter-to-height ratio (D / H) remaining constant, each volume being half the size of the previous fermenter. The tank pressure decreases progressively: fermenter 1 has a pressure of 1.8 MPa, fermenter 2 has a pressure of 1.5 MPa, fermenter 3 has a pressure of 1.2 MPa, and fermenter 4 has a pressure of 0.9 MPa. The gas flow rate entering fermenter 1 is 4 L / min. The aeration flow rate from fermenter 1 to fermenter 2 is set to 1.6 L / min, from fermenter 2 to fermenter 3 is 0.6 L / min, and from fermenter 3 to fermenter 4 is 0.3 L / min. The raw material gas passes sequentially through fermenter 1, fermenter 2, fermenter 3, and fermenter 4, and finally exits from the outlet of fermenter 4. The fermentation products are enriched in the first fermenter 1 from the fourth fermenter 4. The feeding tank 6 replenishes fresh culture medium to the fourth fermenter 4, the third fermenter 3, the second fermenter 2 and the first fermenter 1 respectively, maintaining the overall dilution rate at 1.0 / day. Excess fermentation liquid is discharged to the filtration and collection system through the discharge port 109, and finally the fermentation cells and fermentation products are separated by the microfiltration device.

[0079] The gas utilization rate of the four-tank series fermentation reached 94.3%. Figure 9 As shown in the figure, the average daily yield of acetic acid is 54.2 g / L.

[0080] VI. Four tanks connected in series for continuous fermentation using industrial simulated gas as raw material.

[0081] In addition to CO2 and H2, the exhaust gas emitted by coal chemical enterprises also contains a certain proportion of CO, CH4, N2 and other components. In this embodiment, a mixed gas of N2:H2:CO:CO2:CH4=25:35:10:20:10 is used to simulate the exhaust gas of coal chemical enterprises. Continuous aeration and feeding are used during the fermentation process. The fermentation method, activation culture of the strain, fermentation control parameters, sampling and analysis methods are the same as those of the four-tank series fermentation.

[0082] Fermentation lasted 15 days, with a CO2 utilization rate of 95.5%, an average daily yield of acetic acid of 50.36 g / L, and an average daily yield of ethanol of 8.35 g / L.

[0083] Furthermore, as can be seen from the above test examples, this invention can flexibly start the number of fermentation tanks as needed, and can produce one or more fermentation products depending on the composition and proportion of the gaseous raw materials, which can improve the flexibility and applicability of this invention.

Claims

1. A device for utilizing aerobic microorganisms for fermentation and carbon dioxide absorption and utilization, characterized in that: The application relates to a fermentation device, which comprises a first fermentation tank (1), a second fermentation tank (2), a third fermentation tank (3), a fourth fermentation tank (4) and a gas storage tank (5), wherein the first fermentation tank (1) is internally provided with a first stirring shaft (103), the first stirring shaft (103) is provided with an aeration stirring paddle (1032) with a paddle aeration hole (10321), the first stirring shaft (103) is internally provided with a first gas channel (1034), the gas storage tank (5) is communicated with the upper end of the first gas channel (1034) through a gas inlet pipeline (8), the shaft wall of the first stirring shaft (103) is provided with a connecting hole (10322) which is communicated with the first gas channel (1034) and the inner cavity of the aeration stirring paddle (1032), the second fermentation tank (2) is internally provided with a second stirring shaft (203), the lower end of the second stirring shaft (203) is provided with a gas injection pipe A (207) with a plurality of gas nozzle assemblies (208), the second stirring shaft (203) is internally provided with a second gas channel (2033), the upper end of the first fermentation tank (1) is communicated with the upper end of the second gas channel (2033) through a first gas outlet pipeline (9), the lower end of the second gas channel (2033) is communicated with the inner cavity of the gas injection pipe A (207), the third fermentation tank (3) is internally provided with a third stirring shaft (303), the lower end of the third stirring shaft (303) is provided with a gas injection pipe B (307) with a plurality of gas injection nozzles (308), the third stirring shaft (303) is internally provided with a third gas channel, the upper end of the second fermentation tank (2) is communicated with the upper end of the third gas channel through a second gas outlet pipeline (10), the lower end of the third gas channel is communicated with the inner cavity of the gas injection pipe B (307), the third stirring shaft (303) is provided with a honeycomb-shaped flow guide cylinder (309), the fourth fermentation tank (4) is internally provided with a fourth stirring shaft (403), the lower end of the fourth stirring shaft (403) is provided with an aeration pipe (4033) with an aeration hole, the fourth stirring shaft (403) is internally provided with a fourth gas channel, the upper end of the third fermentation tank (3) is communicated with the upper end of the fourth gas channel through a third gas outlet pipeline (11), the lower end of the fourth gas channel is communicated with the inner cavity of the aeration pipe (4033), the first fermentation tank (1), the second fermentation tank (2), the third fermentation tank (3) and the fourth fermentation tank (4) are sequentially connected through corresponding fermentation liquid pipelines and the volumes are sequentially halved, the upper end of the first fermentation tank (1), the upper end of the second fermentation tank (2), the upper end of the third fermentation tank (3) and the upper end of the fourth fermentation tank (4) are all provided with fermentation liquid feeding pipes (701).

2. The apparatus for fermentation by using the gas-eating microorganism and absorption of carbon dioxide according to claim 1, wherein: The gas nozzle assembly (208) comprises a reduced-diameter nozzle (2081), a connecting frame (2085) and a spray rod (2083), wherein one end of the spray rod (2083) is provided with a suction nozzle (2082), the other end is provided with an output nozzle (2084), the reduced-diameter nozzle (2081) is installed on the gas injection pipe A (207), and the reduced-diameter nozzle (2081) and the suction nozzle (2082) are separately arranged on the two sides of the connecting frame (2085).

3. The apparatus for fermentation by aerophyllic microorganism and utilization of carbon dioxide absorption according to claim 1, wherein: The first fermentor (1) is provided with a first gas outlet (104) at the upper end, and the first gas outlet (104) is communicated with the upper end of the second gas channel (2033) through a first gas outlet pipeline (9); the second fermentor (2) is provided with a second gas outlet (204) at the upper end, and the second gas outlet (204) is communicated with the upper end of the third gas channel through a second gas outlet pipeline (10); the third fermentor (3) is provided with a third gas outlet (304) at the upper end, and the third gas outlet (304) is communicated with the upper end of the fourth gas channel through a third gas outlet pipeline (11); and the fourth fermentor (4) is provided with a fourth gas outlet (404) at the upper end, and the fourth gas outlet (404) is connected with a gas output pipeline.

4. The apparatus for fermentation by using the microorganism that eats gas and absorbing carbon dioxide according to claim 3, wherein: An air inlet flowmeter (801) is arranged on the air inlet pipeline (8), a gas output flowmeter (402) is arranged on the gas output pipeline, and air outlet flow control valves (12) are arranged on the first, second and third gas outlet pipelines (9, 10, 11).

5. The apparatus for fermentation by aerophyllic microorganism and utilization of carbon dioxide absorption according to claim 1, wherein: The first fermentor (1) is provided with a feeding port (110) at the upper end, a first liquid inlet (106) is arranged on one side of the first fermentor (1), a second liquid outlet (201) is arranged on one side of the second fermentor (2), and a second liquid inlet (202) is arranged on the other side of the second fermentor (2); a third liquid outlet (301) is arranged on one side of the third fermentor (3), and a third liquid inlet (302) is arranged on the other side of the third fermentor (3); a fourth liquid outlet (401) is arranged on one side of the fourth fermentor (4); the first liquid inlet (106) is connected with the second liquid outlet (201) through a first fermentation liquid pipeline (13), the second liquid inlet (202) is connected with the third liquid outlet (301) through a second fermentation liquid pipeline (14), and the third liquid inlet (302) is connected with the fourth liquid outlet (401) through a third fermentation liquid pipeline (15); in addition, the first, second, third and fourth fermentors (1, 2, 3, 4) are all provided with a discharging port (109) at the lower end.

6. The apparatus for fermentation by using the microorganism that eats gas and absorbing carbon dioxide according to claim 5, wherein: Fermentation liquid flowmeters (16) and fermentation liquid pipeline control valves (17) are arranged on the first, second and third fermentation liquid pipelines (13, 14, 15).

7. The apparatus for fermentation by aerophyllic microorganism and utilization of carbon dioxide absorption according to claim 1, wherein: The first fermentor (1) is provided with a first feeding port (105) at the upper end, the second fermentor (2) is provided with a second feeding port (205) at the upper end, the third fermentor (3) is provided with a third feeding port (305) at the upper end, and the fourth fermentor (4) is provided with a fourth feeding port (405) at the upper end; the first, second, third and fourth feeding ports (105, 205, 305, 405) are respectively connected with a feeding main pipeline (7) through corresponding fermentation liquid feeding pipelines (701), the feeding main pipeline (7) is connected with a feeding tank (6), and the fermentation liquid feeding pipelines (701) are provided with feeding flow control valves. 8.The device of Claim 1, wherein the device is characterized by: The first fermenter (1) is provided with a first driving assembly for driving the first stirring shaft (103) to rotate, the second fermenter (2) is provided with a second driving assembly (206) for driving the second stirring shaft (203) to rotate, the third fermenter (3) is provided with a third driving assembly (306) for driving the third stirring shaft (303) to rotate, and the fourth fermenter (4) is provided with a fourth driving assembly (406) for driving the fourth stirring shaft (403) to rotate.

9. The apparatus for fermentation by aerophyllic microorganism and utilization of carbon dioxide absorption according to claim 8, wherein: The first driving assembly, the second driving assembly (206), the third driving assembly (306) and the fourth driving assembly (406) are the same in structure, and each includes a stirring reduction motor (101), a transmission belt (102) and a stirring shaft adapter (1033), wherein the stirring shaft adapter (1033) is internally provided with a rotating shaft sleeve (10331) sleeved on a corresponding pipeline, the stirring shaft adapter (1033) is externally sleeved with a driven pulley (10332), the output shaft of the stirring reduction motor (101) is provided with a driving pulley, and the driving pulley is connected with the driven pulley (10332) through the transmission belt (102).

10. The apparatus for fermentation by aerophyllic microorganism and utilization of carbon dioxide absorption according to claim 1, wherein: The first fermenter (1), the second fermenter (2), the third fermenter (3) and the fourth fermenter (4) are each provided with a sensor mounting port (107) and a sampling port (108), the first stirring shaft (103) is further provided with a first defoaming paddle (1031), the second stirring shaft (203) is further provided with a second defoaming paddle (2031) and a stirring paddle A (2032), the third stirring shaft (303) is further provided with a third defoaming paddle, the third defoaming paddle is arranged on the upper side of the honeycomb flow guide cylinder (309), and the fourth stirring shaft (403) is further provided with a fourth defoaming paddle (4031) and a stirring paddle B (4032).

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