WO2021097794A1 - Aerobic fermentation system and process - Google Patents

Abstract

An aerobic fermentation system and process. The system comprises a fermentation tank used for using a specified strain to ferment a material; a separation tank; at least two micro-interface generators; and a return conduit. Compared with a traditional method, by breaking air to form micrometer-sized micro bubbles, and mixing the micro bubbles with a raw material to form a gas-liquid emulsion, a gas-liquid phase boundary area is increased, and the effect of enhancing mass transfer is achieved within a low preset operation condition range; moreover, the micro bubbles can be fully mixed with the raw material to form the gas-liquid emulsion, and by means of full gas-liquid phase mixing, it can be ensured that bacteria in the system can fully absorb oxygen in the raw material, thereby preventing the generation of a byproduct, and further improving the fermentation efficiency of the system.

Description

An aerobic fermentation system and process Technical field

The invention relates to the technical field of microbial aerobic fermentation, in particular to an aerobic fermentation system and process.

Background technique

Fermentation refers to the process in which people prepare the microbial cells themselves, or direct or secondary metabolites through the life activities of microorganisms under aerobic or anaerobic conditions. Fermentation is sometimes also written as fermented yeast, and its definition varies depending on the use situation. Generally speaking, fermentation refers to a certain decomposition process of organic matter by organisms. Fermentation is a kind of biochemical reaction that human beings came into contact with earlier, and it is now widely used in the food industry, biology and chemical industry.

Traditionally, people use solid-state fermentation to produce bread, malt, koji, alcoholic beverages, soy sauce, tempeh, mushrooms and other foods or intermediate raw materials. Recent studies have found that some foods produced by solid-state fermentation contain physiologically active substances, indicating that solid-state fermentation has advantages in the production of these foods and food additives. With the increasingly serious energy crisis and environmental problems, solid-state fermentation technology has attracted great interest due to its unique advantages. People have made great progress in the field of solid-state fermentation and its application in resource environment and protein feed, which are mainly manifested in the successful development and application of biological feed, biofuel, biological pesticide, biological transformation, biological detoxification and biological remediation. It provides strong support for the continuous development of solid-state fermentation and broad application prospects for the development of traditional technology.

Chinese Patent Publication Number: CN207632812U discloses a pullulan Bacillus acidophilus fermentation system. The fermentation system includes a culture bottle, a first-level seed tank, a second-level seed tank, a mixing tank, a buffer tank, a fermentation tank, and a storage tank. And a disc centrifuge; the culture bottle is connected to the top of the mixing tank; the first-level seed tank is connected to the second-level seed tank; the second-level seed tank is connected to the fermentation tank; the mixing tank is connected to the A buffer tank, the mixing tank is provided with a first stirring blade, the upper end of the first stirring blade is connected with a first stirring motor; the buffer tank is connected between the mixing tank and the fermentation tank; the fermentation tank is provided with a second stirring blade , The second stirring blade is connected with a second stirring motor; the upper part of the storage tank is connected with the lower part of the fermentation tank; the lower part of the storage tank is connected with the disc centrifuge. It can be seen that the system has the following problems:

First, in the system, only the stirring blades are used to break the air. The air forms large bubbles after being broken. However, the volume of the bubbles is too large to be fully mixed with the mixed materials, and the bacteria absorb oxygen unevenly, which reduces the The fermentation efficiency of the system.

Second, the system is prone to produce by-products when the bacteria and oxygen are not uniformly contacted, which causes the materials in the system to be unusable and increases the energy consumption of the system.

Third, the system uses a stirring blade to stir bacteria and materials. During the stirring process, the stirring blade will damage the bacteria, resulting in a reduction in the number of bacteria in the raw material and reducing the fermentation efficiency.

Summary of the invention

To this end, the present invention provides an aerobic fermentation system and process to overcome the problem of low fermentation efficiency caused by the inability of sterile air to be fully mixed with materials in the prior art to produce by-products.

In one aspect, the present invention provides an aerobic fermentation system, including:

The fermentation tank is used for fermenting materials with designated bacteria, and the fermentation tank includes: a full mixed flow biochemical reaction zone arranged below, used for loading fermentation raw materials and fermentation bacteria, and providing a reaction space for the fermentation of the two, and a set Above, the plug flow biochemical reaction zone for conveying the fermented materials and separating gas and liquid;

A separation tank, which is connected to the fermentation tank, and is used to separate the materials output from the fermentation tank to generate gaseous bacteria and fermentation broth;

The micro-interface generator, which is set at a designated position in the full-mixed flow biochemical reaction zone, converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the sterile air, so that the sterile air is broken to form a diameter Micron bubbles of ≥1μm and <1mm to increase the mass transfer area between the fermentation raw materials and sterile air, reduce the thickness of the liquid film, reduce the mass transfer resistance, and mix the fermentation raw materials with micron bubbles to form a gas-liquid emulsification after crushing To enhance the efficiency of the reaction between the oxidizing raw materials and the air within the preset operating conditions;

The return pipe is respectively connected with the fermentation tank and the separation tank, and is used to preheat the materials output from the fermentation tank and return the materials to the fermentation tank or output to the separation tank after preheating.

Further, the micro-interface generator includes:

The first micro-interface generator is a pneumatic micro-interface generator, the first micro-interface generator is arranged in the fully mixed flow biochemical reaction zone and located at the bottom of the reaction zone, and is used to break the sterile air into micron scale After the crushing is completed, the microbubbles are output to the fermentation tank and mixed with the materials in the fermentation tank to form a gas-liquid emulsion;

The second micro-interface generator is a hydraulic or gas-liquid linkage micro-interface generator. The second micro-interface generator is arranged in the fully mixed flow biochemical reaction zone and at the top of the reaction zone to receive the The material output from the reflux tube uses the material to entrain the under-used sterile air in the plug flow biochemical reaction zone and break the sterile air to form micro-sized micro-bubbles, and mix the micro-bubbles with the material to form a gas-liquid emulsion It is output to the fully mixed flow biochemical reaction zone to counteract the gas-liquid emulsion output from the first micro-interface generator, thereby prolonging the residence time of the microbubbles in the fully mixed flow biochemical reaction zone.

Further, the full mixed flow biochemical reaction zone in the fermentor includes:

A grille, which is arranged inside the fermentor to filter insoluble particles in the material;

The pH adjusting liquid inlet, which is arranged on the side wall of the fermentation tank and above the grid, is used to transport the pH adjusting liquid to adjust the pH value of the material;

Fermentation raw material feed inlet, which is arranged on the side wall of the fermentor and located below the grill, for conveying the fermentation raw material;

Fermentation strain feed inlet, which is arranged on the side wall of the fermentor and located below the fermented raw material feed inlet, and is used to transport designated strains into the fermentor and ferment the fermented raw materials;

The first gas-phase feed pipe is arranged on the side wall of the fermentor and connected to the micro-interface generator, and is used to transport sterile air from the side to the micro-interface generator in the fermentor;

A residue outlet, which is set at the bottom of the fermentor to discharge the residue after fermentation out of the system;

The partition is arranged on the inner wall of the fermentation tank and located below the grill, and is used to block the fluctuation of the fermentation raw material output from the fermentation raw material inlet and the bacteria output from the fermentation strain feed inlet.

Further, the plug flow reaction zone includes:

An exhaust pipe, which is arranged at the top of the fermentation tank, and is used to discharge the tail gas out of the system after the fermentation of the material in the fermentation tank is completed;

A second gas-phase feed pipe is arranged in the fermentor, and the bottom end of the second feed pipe is connected with the second micro-interface generator, and the top of the second feed pipe is located above the liquid level in the fermentor , To entrain the unused sterile air on the top of the fermentor into the micro-interface generator in the fermentor so that the micro-interface generator can break the sterile air;

A discharging port, which is arranged on the side wall of the fermentation tank, and is used to output the fermented material out of the fermentation tank;

The reflux feed pipe is arranged on the side wall of the fermentor, and is used to output part of the material output from the reflux pipe to the micro-interface generator in the fermentor.

Further, the return pipe includes:

A circulating pump, which is connected to the fermentation tank, and is used to output the fermented materials in the fermentation tank;

The heat exchanger is connected with the circulating pump and is used to exchange heat for the material output by the circulating pump so that the material reaches a specified temperature.

Further, the output end of the heat exchanger is provided with a shunt pipe, and the shunt pipe is respectively connected with the fermentation tank and the separation tank for refluxing and outputting materials to the separation tank.

Further, the separation tank is a sealed tank, including:

A feed port, which is arranged at the top of the separation tank, and is used to transport the material output from the return pipe to the inside of the separation tank;

An exhaust port, which is arranged at the top of the separation tank for outputting gaseous bacterial species;

The discharging port is arranged at the bottom end of the separation tank, and is used to output the separated fermentation broth and transport the fermentation broth to the next section.

In another aspect, the present invention provides an aerobic fermentation process, including:

Step 1: Transport the specified type of fermentation raw material to the full mixed-flow biochemical reaction zone in the fermentor through the fermentation raw material inlet, and transport the specified type of bacteria to the fermentor through the fermentation bacteria inlet Inside the fermentation tank;

Step 2: The sterile air is delivered to the first micro-interface generator through the first gas-phase feed pipe, and the first micro-interface generator breaks the sterile air into micro-sized micro-bubbles and outputs the micro-bubbles to the Among the fermentation raw materials in the fermenter, microbubbles are fully mixed with the fermentation raw materials to provide an aerobic environment for bacteria;

Step 3: The bacteria react with the fermentation raw materials in an aerobic environment. After the fermentation is completed, the fermentor will transport the fermented materials to the horizontal plug flow biochemical reaction zone, and the materials will flow through the grid, and the grid will transfer the materials into the biochemical reaction zone. The residue is filtered out, and after the filtration, the residue will settle to the bottom of the fermentor and be discharged out of the fermentor through the residue outlet;

Step 4: After filtering, the material will flow in the designated direction in the plug flow biochemical reaction zone. When the material flows to the top of the fermentation tank, the gas in the material will be output to the fermentation tank through the exhaust pipe, and the material will pass through the first outlet. The material port is output to the return pipe;

Step 5: The reflux pipe draws out the material in the fermentor, and divides the flow after preheating, and returns a part of the preheated material to the second micro-interface generator to adjust the full mixed flow biochemical reaction zone And output the other part to the separation tank for separation;

Step 6: After the preheated material is refluxed, it enters the second micro-interface generator through the reflux feed pipe, and the second micro-interface generator removes the unused materials on the top of the fermentor through the second gas-phase feed pipe. Bacterial air is entrained to the second interface generator, and the material is used to break the sterile air to form micro-sized micro-bubbles and mix the micro-bubbles with the material to form a gas-liquid emulsion. After the gas-liquid emulsion is formed, the second micro-interface occurs The device outputs the gas-liquid emulsion to the full-mixed flow biochemical reaction zone to adjust the temperature in the full-mixed flow biochemical reaction zone while reusing materials;

Step 7: After the preheated materials are output to the separation tank, the separation tank separates the materials from gas and liquid to form gaseous bacteria and fermentation broth. After separation, the gaseous bacteria are discharged from the separation tank through the exhaust port, and the fermentation The liquid is discharged from the separation tank through the second discharge port and transported to the next section.

Further, when the system is running, the pH adjusting liquid inlet will deliver the pH adjusting liquid to adjust the pH value of the materials in the fermenter.

Compared with the prior art, the beneficial effect of the present invention is that compared with the traditional method, the present invention breaks the air to form micro-sized micro-bubbles and mixes the micro-bubbles with the raw materials to form a gas-liquid emulsion to increase the gas-liquid emulsion. The phase boundary area of the two phases can achieve the effect of enhancing mass transfer within the lower preset operating conditions; at the same time, the microbubbles can be fully mixed with the raw materials to form a gas-liquid emulsion. By fully mixing the gas-liquid two phases, it can be guaranteed The bacteria in the system can fully absorb the oxygen in the material, thereby preventing the generation of by-products, and further improving the fermentation efficiency of the system.

In addition, the range of preset operating conditions can be flexibly adjusted according to different raw material compositions or different product requirements, which further ensures the full and effective progress of the reaction, thereby ensuring the reaction rate, and achieving the purpose of strengthening the reaction.

In particular, in the present invention, a full-mixed flow biochemical reaction zone is set in the fermentor. By arranging the micro-interface generator in the full-mixed flow biochemical reaction zone, the inside of the full-mixed flow biochemical reaction zone is closer to the full-mixed flow model, which ensures the temperature of the materials in the reaction zone. And the concentration is uniform, and when the materials enter the reaction zone, they can be quickly mixed uniformly, so as to prevent some bacteria in the reaction zone from not absorbing enough oxygen to generate by-products, and further improving the fermentation efficiency of the system.

In particular, the present invention also sets a horizontal plug flow biochemical reaction zone in the fermentation tank. By setting the horizontal plug flow biochemical reaction zone, the material can move at a uniform speed in the specified direction, effectively preventing the material from producing backflow during the conveying process, and the horizontal plug flow The biochemical reaction zone can further promote the reaction rate of the materials in the full mixed flow biochemical reaction zone, thereby further improving the fermentation efficiency of the system.

Furthermore, the fermentation tank of the present invention is provided with a pneumatic micro-interface generator and a gas-liquid linkage micro-interface generator. By using different types of micro-interface generators, the mixing of microbubbles and materials is more uniform, thereby improving the inside of the fermentation tank. The mixing efficiency of materials and sterile air can further improve the fermentation efficiency of the system.

Furthermore, the fermentation tank is also provided with a grid, through which the residue in the material can be effectively filtered out and discharged through the residue outlet at the bottom of the fermentation tank, thereby improving the purity of the fermentation broth.

In particular, the side wall of the fermenter is also provided with a pH adjustment liquid inlet. When the system is running, the pH adjustment liquid inlet can control the pH of the material in the fermentor by sending the pH adjustment liquid into the fermentor. Adjusting the value can effectively adjust the pH value of the material without destroying the bacteria, thereby improving the reaction efficiency of the bacteria.

In particular, the inner wall of the fermentation tank is also provided with a partition plate, which is located at the outlet of the fermentation raw material feed inlet and the fermentation strain feed inlet, and by shielding the two feed inlet outlets, This is to prevent the fluctuation of each feed port when outputting materials and bacteria from affecting the second micro-interface generator and reducing the mixing efficiency of the second micro-interface generator.

Further, the system is also provided with a reflux pipe, which can re-use the materials by refluxing the materials after fermentation, thereby improving the utilization rate of the materials, thereby further improving the fermentation efficiency of the system.

In particular, a heat exchanger is provided in the reflux pipe. When the fermented material is refluxed and output, the heat exchange can be performed on the material through the heat exchanger so that the material reaches a specified temperature, so as to improve the material in the fermentation tank. The temperature is adjusted to provide a suitable fermentation environment for the bacteria in the fermentor to further improve the fermentation efficiency of the system.

Description of the drawings

Figure 1 is a schematic diagram of the structure of the aerobic fermentation system of the present invention.

Detailed ways

The preferred embodiments of the present invention will be described below with reference to the drawings. Those skilled in the art should understand that these embodiments are only used to explain the technical principles of the present invention, and are not intended to limit the protection scope of the present invention.

It should be noted that in the description of the present invention, the terms "upper", "lower", "left", "right", "inner", "outer" and other terms indicating directions or positional relationships are based on the attached drawings. The direction or position relationship shown is only for ease of description, and does not indicate or imply that the device or element must have a specific orientation, be configured and operated in a specific orientation, and therefore cannot be understood as a limitation of the present invention.

In addition, it should be noted that, in the description of the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense. For example, they can be fixed or fixed. It is a detachable connection or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication between two components. For those skilled in the art, the specific meaning of the above-mentioned terms in the present invention can be understood according to specific circumstances.

Please refer to FIG. 1, which is a schematic structural diagram of the aerobic fermentation system of the present invention, which includes a fermentation tank 1, a micro-interface generator 2 (not shown in the figure), a return pipe 3, and a separation tank 4. Wherein, the micro-interface generator 2 is arranged inside the fermenter to break the sterile air to form micro-sized micro-bubbles and mix the micro-bubbles with the materials in the fermentor to form a gas-liquid emulsion to form a gas-liquid emulsion Bacteria provide an aerobic environment. The return pipe 3 is connected to the fermentation tank 1 to output the fermented materials in the fermentation tank 1 and return part of the output materials to the fermentation tank 1. The separation tank 4 is connected with the output branch in the return pipe 3 to separate and concentrate the material output from the fermentation tank 1 and output the processed fermentation liquid to the next section.

When the system is running, the fermentation raw materials and the fermentation bacteria of the designated strain are first delivered into the fermentor 1, and at the same time sterile air is delivered into the fermentor 1, and the sterile air will enter the micro-interface generator 2, and the micro-interface The generator 2 breaks the sterile air to form micro-sized micro-bubbles and mixes the micro-bubbles with the fermentation raw materials to form a gas-liquid emulsion to provide a uniform aerobic environment for the bacteria. After the fermentation is completed, the fermentation tank 1 will The gas and residue are discharged out of the system separately, and the fermented materials are output to the return pipe 3. The return pipe 3 preheats the materials and divides the materials. After the split, a part of the materials are returned to the fermentation tank 1, and the fermentation is adjusted while being reused. The temperature of the material in the tank, another part of the material will be output to the separation tank 4, the separation tank will separate the material from gas and liquid, discharge the residual gaseous bacteria in the material and output the separated and concentrated fermentation broth to the next section. Those skilled in the art can understand that the fermentation strains that can be used in the system are not specifically limited in this embodiment, as long as the strains are capable of aerobic fermentation.

Please continue to refer to FIG. 1, the fermentation tank 1 of the present invention includes a fully mixed flow biochemical reaction zone 11 and a plug flow biochemical reaction zone 12. The full mixed flow biochemical reaction zone 11 is located at the lower part of the fermentor 1 and is used to fully mix the bacteria and microbubbles with the fermentation raw materials. The horizontal plug flow biochemical reaction zone 12 is located at the upper part of the fermentor 1, and is used to transport the fermented material in a designated direction while promoting the reaction speed in the fermentor 1. When the fermentation tank 1 starts to ferment, the fully mixed-flow biochemical reaction zone 11 will receive fermentation bacteria, fermentation raw materials, and microbubbles respectively, and fully mix the three to make the bacteria ferment in an aerobic environment. After the fermentation is completed, the whole The mixed flow biochemical reaction zone 11 transports the fermented materials to the horizontal plug flow biochemical reaction zone 12, and the horizontal plug flow biochemical reaction zone 12 transports the materials in a designated direction. It is understandable that the length-to-diameter ratio of the plug flow biochemical reaction zone 12 is not specifically limited in this embodiment, as long as the length of the plug flow biochemical reaction zone 12 is satisfied to keep the material flowing continuously and stably.

Please continue to refer to FIG. 1, the fully mixed flow biochemical reaction zone 11 of the present invention includes a grid 111, a pH adjusting liquid inlet 112, a fermentation raw material inlet 113, a fermentation strain inlet 114, and a first gas phase inlet The material pipe 115, the residue outlet 116 and the partition 117. Wherein, the grill 111 is arranged inside the fermentor 1 to filter out residues generated in the fermentor 1 during the fermentation process. The pH adjusting liquid inlet is arranged on the inner wall of the fermentor 1 and above the grid 111 to deliver the pH adjusting liquid to the fermentor 1. The fermentation raw material inlet 113 is arranged on the side wall of the fermentation tank 1 and is located below the grill 111 for conveying fermentation raw materials to the fermentation tank 1. The fermentation bacteria feed inlet 114 is arranged on the side wall of the fermentor 1 and is located below the fermentation raw material feed inlet 113, and is used to convey a specified type of bacteria to the fermentor 1. The first gas-phase feed pipe 115 is arranged on the side wall of the fermentor 1 and connected to the micro-interface generator 2 for conveying sterile air. The residue outlet 116 is arranged at the bottom of the fermentation tank 1 to discharge residues produced after fermentation out of the fermentation tank 1. The partition plate 117 is arranged on the inner wall of the fermentor 1 and is located on the same side as the fermentation raw material inlet 113 to block the fermentation raw material inlet 113 from outputting the fermentation raw material and the fermentation strain inlet 114 Fluctuations when exporting bacteria.

When the full mixed-flow biochemical reaction zone is operating, the fermentation raw material feed port 113 will transport the fermentation raw material into the fermentor 1, and the fermentation strain feed port 114 will transport the fermenting bacteria into the fermentor 1. The partition 117 will block the fluctuation generated when the fermentation raw material feed port 113 and the fermentation strain feed port 114 output materials, and the first gas-phase feed pipe 115 will transport sterile air to the micro-interface generator 2. The micro-interface generator 2 crushes the sterile air to form micro-sized micro-bubbles, and mixes the micro-bubbles with the fermentation raw materials to form a gas-liquid emulsion. After the gas-liquid emulsion is mixed with bacteria, fermentation begins. During the fermentation process, the pH The adjusting liquid inlet 113 will deliver the pH adjusting liquid into the fermentor 1 to adjust the pH value of the mixed material in the fermentor 1. After the fermentation is completed, the fully mixed flow biochemical reaction zone 11 will transport the fermented material to the flat In the push-flow biochemical reaction zone 12, during the transportation process, the grid 111 will filter out the residue in the material, and the residue will begin to settle after the filtration and will be discharged out of the fermentation tank 1 through the residue outlet 116.

Specifically, the grill 111 is a sieve plate, which is arranged inside the fermentor 1 to filter the fermented materials. After the fermentation in the full mixed-flow biochemical reaction zone 11 is completed, the fermented material will flow through the grid 111, and the grid 111 will filter out the residue in the material. It is understandable that the type and the size of the through holes of the grid 111 are not specifically limited in this embodiment, as long as the grid 111 can filter the solid residues in the material.

Specifically, the first gas-phase feed pipe 115 is arranged on the side wall of the fermenter, and the outlet of the first gas-phase feed pipe 115 is connected to the micro-interface generator 2 to deliver sterile air to the micro-interface generator. Interface generator 2. When the fully mixed-flow biochemical reaction zone 11 is running, the first gas-phase feed pipe 115 will transport sterile air to the micro-interface generator 2, and the micro-interface generator 2 will break the sterile air into micro-bubbles, and the micro-bubbles It is output to the inside of the fermentor 1 and mixed with the fermentation raw materials. It is understandable that the material and size of the first gas-phase feed pipe 115 are not specifically limited in this embodiment, as long as the first gas-phase feed pipe 115 can transport a specified volume of sterile air within a specified time That's it.

Specifically, the partition 117 is a baffle, which is fixedly connected to the inner wall of the fermentation tank 1 to block the fluctuations generated when the fermentation tank receives materials. When the fully mixed flow biochemical reaction zone 11 is operating, the fermentation raw material feed port 113 will transport the fermentation raw material into the fermentor 1, the fermentation strain feed port 114 will transport bacteria into the fermentor 1, and the partition 117 will block The discharging position prevents the fluctuation of the two materials during the conveying process, so as to prevent the fluctuation from affecting the micro-interface generator. It can be understood that the connection manner between the partition 117 and the fermentor 1 may be welding, integral connection or other types of connection, as long as the partition 117 can reach its designated working state.

Please continue to refer to FIG. 1, the plug flow biochemical reaction zone 12 of the present invention is located on the upper part of the fermentor 1 for conveying the fermented material in a specified direction, including an exhaust pipe 121 and a second gas phase feed The pipe 122, the first discharge port 123, and the return feed pipe 124. Wherein, the exhaust pipe 121 is arranged on the top of the fermentation tank 1 to discharge the gas generated during the fermentation process. The second gas-phase feed pipe 122 is arranged on the top of the fermentor 1 and is connected to the micro-interface generator 2 for conveying tail gas from the top of the fermentor. The first discharging port 123 is arranged on the side wall of the fermentation tank 1 for outputting fermented materials. The reflux feed pipe 124 is arranged on the side wall of the fermentor 1 and located below the discharge port 123 to convey the refluxed material to the fermentor 1. When the plug flow reaction zone 12 is running, the materials will be transported upwards at a constant speed in the reaction zone. When the materials reach the top of the fermenter 1, the gas in the materials is output to the fermenter 1 through the exhaust pipe 121, and the liquid phase materials It is output to the reflux pipe 3 through the first discharge port 123, and part of the material is refluxed through the reflux pipe 3 and then returned to the fermentor 1 through the reflux feed pipe 124. After reflux, the second gas phase feed pipe 122 transports tail gas to the micro-interface generator 2, the tail gas is mixed with the refluxed material after being crushed and is transported to the fully mixed flow biochemical reaction zone 11 for repeated use.

Specifically, the second gas-phase feed pipe 122 is arranged on the top of the fermentor, and the outlet of the second gas-phase feed pipe 122 is connected to the micro-interface generator 2 for conveying the tail gas from the top of the fermentor to the micro-interface. Interface generator 2. When the horizontal plug flow biochemical reaction zone 12 is operating, the second gas-phase feed pipe 122 will transport the tail gas to the micro-interface generator 2, and the micro-interface generator 2 will break the tail gas into micro-bubbles, and output the micro-bubbles to the fermentation Inside the tank 1 and mixed with the materials. It is understandable that the material and size of the second gas-phase feed pipe 122 are not specifically limited in this embodiment, as long as the second gas-phase feed pipe 122 can transport a specified volume of tail gas within a specified time. .

Specifically, the reflux feed pipe 124 is arranged on the side wall of the fermentor 1 and the outlet of the reflux feed pipe 124 is connected to the micro-interface generator 2 for conveying the refluxed material to the micro-interface generator 2. When the horizontal plug flow biochemical reaction zone is operating, the reflux pipe 3 will transport the refluxed material to the reflux feed pipe 124, and the reflux feed pipe 124 will transport the material to the micro-interface generator 2 to make The material is mixed with microbubbles. It can be understood that the material and size of the reflux feed pipe 124 are not specifically limited in this embodiment, as long as it is satisfied that the reflux feed pipe 124 can transport a specified flow of material within a specified time.

Please continue to refer to FIG. 1, the micro-interface generator 2 of the present invention includes a first micro-interface generator 21 and a second micro-interface generator 22. The first micro-interface generator 21 is arranged at the bottom of the full-mixed flow biochemical reaction zone 11 for breaking sterile air to form micro-bubbles. The second micro-interface generator 22 is arranged on the top of the full-mixed flow biochemical reaction zone 11 and connected to the grid 111 for breaking the sterile air to form microbubbles and mixing the microbubbles with the reflux material. When the fermentation tank 1 is running, the first micro-interface generator 21 will break the sterile air to form micro-bubbles, and mix the micro-bubbles with the fermentation raw materials to form a gas-liquid emulsion, and the second micro-interface generator 22. Receiving the reflux material and sterile air respectively, breaking the sterile air into microbubbles and mixing with the materials to form a gas-liquid emulsion. It is understandable that the micro-interface generator 2 of the present invention can also be used in other multi-phase reactions, such as through micro-interface, micro-nano interface, ultra-micro interface, micro-bubble biochemical fermentation tank or micro-bubble biological fermentation tank, etc. Use micro-mixing, micro-fluidization, ultra-micro-fluidization, micro-bubble fermentation, micro-bubble bubbling, micro-bubble mass transfer, micro-bubble transfer, micro-bubble reaction, micro-bubble absorption, micro-bubble oxygenation, micro-bubble contact and other processes or Method to make the material form multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsified flow, multi-phase micro-structured flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsified flow, gas-liquid-solid flow Microstructured flow, microbubbles, microbubble flow, microbubbles, microbubble flow, micro gas liquid flow, gas-liquid micro-nano emulsified flow, ultra-micro flow, micro-dispersion flow, two micro-mixed flow, micro-turbulent flow, micro-bubble flow, Micro-bubble, micro-bubble flow, micro-nano bubble, micro-nano bubble flow and other multiphase fluids formed by micro-scale particles, or multi-phase fluids formed by micro-nano-scale particles (referred to as micro-interface fluid), thus effective The ground increases the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction.

Specifically, the first micro-interface generator 21 of the present invention is a pneumatic micro-interface generator, which is connected to the first gas-phase feed pipe 115 and is used to crush the air transported by the first gas-phase feed pipe 115 And the formation of micro-scale micro-bubbles. When the fermentation tank 1 is in operation, the first gas-phase feed pipe 115 will transport sterile air to the first micro-interface generator 21, and the first micro-interface generator 21 will break the sterile air and Micro-scale micro-bubbles are formed. After the crushing is completed, the first micro-interface generator 21 will output the micro-bubbles into the fermentor 1 and mix them with the fermentation raw materials to provide an aerobic environment for bacteria.

Specifically, the second micro-interface generator 22 of the present invention is a gas-liquid linkage type micro-interface generator, which is connected to the second gas-phase feed pipe 122 and the return feed pipe 124, respectively, for receiving tail gas and Reflux materials, and through the pressure of the reflux materials, the tail gas can be broken to form micro-sized micro-bubbles. When the second micro-interface generator 22 is running, it will receive the tail gas and the reflux material respectively, use the pressure of the reflux material to break the tail gas to form microbubbles, and form a gas-liquid emulsion by mixing the microbubbles with the reflux material. Output to the full mixed flow biochemical reaction zone 11 for repeated fermentation.

Please continue to refer to FIG. 1, the return pipe 3 of the present invention includes a circulating pump 31 and a heat exchanger 32. The circulating pump 31 is connected to the first discharge port 123 for pumping out the fermented materials in the fermentor 1. The heat exchanger 32 is connected to the circulating pump 31 to preheat the material output by the circulating pump 31. After the fermentation of the material in the fermentation tank 1 is completed, the circulating pump 31 starts to operate and draws the material out through the first discharge port 123, and transports the material to the heat exchanger 32, which will The materials are heat exchanged and divided after the heat exchange, a part of the materials are returned to the return feed pipe 124, and another part of the materials is output to the separation tank 4. It is understandable that the model and power of the circulating pump 31 are not specifically limited in this embodiment, as long as the circulating pump 31 can reach its designated working state.

Specifically, the outlet of the heat exchanger 32 is provided with a shunt pipe. One end of the shunt pipe is connected with the return feed pipe 124 to return a part of the material output by the heat exchanger 32. The other end of the shunt pipe is connected to the return feed pipe 124. The separation tank 4 is connected to output another part of the material output from the heat exchanger 32 to the separation tank 4 for separation.

Please continue to refer to FIG. 1, the separation tank 4 of the present invention is a sealed tank with a feed port at its top, and the feed port is connected to the heat exchanger 32 to receive the waste heat completed material The top end of the separation tank 4 is also provided with an exhaust port to discharge gaseous bacteria during separation; the bottom end of the separation tank 4 is provided with a second discharge port to output the separated fermentation broth to the next Construction section. When the heat exchanger 32 outputs the preheated material, the material will enter the separation tank 4 through the feed port and undergo gas-liquid separation. After the separation, the bacteria remaining in the material will pass through the exhaust gas together with the gas. The outlet is discharged from the separation tank 4, and the material is separated to form a fermentation liquid, and is output to the next section through the second outlet. It is understandable that the material and size of the separation tank 4 are not specifically limited in this embodiment, as long as the separation tank 4 can reach its designated working state.

In order to make the purpose and advantages of the present invention clearer, the following further describes the present invention in conjunction with the embodiments; it should be understood that the specific embodiments described here are only used to explain the present invention, not to limit the present invention.

An aerobic fermentation process includes the following steps:

Step 1: Transport the specified type of fermentation raw material to the full mixed-flow biochemical reaction zone in the fermentor through the fermentation raw material inlet, and transport the specified type of bacteria to the fermentor through the fermentation bacteria inlet Inside the fermentation tank;

Step 2: The sterile air is delivered to the first micro-interface generator through the first gas-phase feed pipe, and the first micro-interface generator breaks the sterile air into micro-sized micro-bubbles and outputs the micro-bubbles to the Among the fermentation raw materials in the fermenter, microbubbles are fully mixed with the fermentation raw materials to provide an aerobic environment for bacteria;

Step 3: The bacteria react with the fermentation raw materials in an aerobic environment. After the fermentation is completed, the fermentor will transport the fermented materials to the horizontal plug flow biochemical reaction zone, and the materials will flow through the grid, and the grid will transfer the materials into the biochemical reaction zone. The residue is filtered out, and after the filtration, the residue will settle to the bottom of the fermentor and be discharged out of the fermentor through the residue outlet;

Step 4: After filtering, the material will flow in the designated direction in the plug flow biochemical reaction zone. When the material flows to the top of the fermentation tank, the gas in the material will be output to the fermentation tank through the exhaust pipe, and the material will pass through the first outlet. The material port is output to the return pipe;

Step 5: The reflux pipe draws out the material in the fermentor, and divides the flow after preheating, and returns a part of the preheated material to the second micro-interface generator to adjust the full mixed flow biochemical reaction zone And output the other part to the separation tank for separation;

Step 6: After the preheated material is refluxed, it enters the second micro-interface generator through the reflux feed pipe, and the second micro-interface generator removes the unused materials on the top of the fermentor through the second gas-phase feed pipe. Bacterial air is entrained to the second interface generator, and the material is used to break the sterile air to form micro-sized micro-bubbles and mix the micro-bubbles with the material to form a gas-liquid emulsion. After the gas-liquid emulsion is formed, the second micro-interface occurs The device outputs the gas-liquid emulsion to the full-mixed flow biochemical reaction zone to adjust the temperature in the full-mixed flow biochemical reaction zone while reusing materials;

Step 7: After the preheated materials are output to the separation tank, the separation tank separates the materials from gas and liquid to form gaseous bacteria and fermentation broth. After separation, the gaseous bacteria are discharged from the separation tank through the exhaust port, and the fermentation The liquid is discharged from the separation tank through the second discharge port and transported to the next section.

It is understandable that the range of preset operating conditions can be adjusted flexibly according to different raw material compositions or different product requirements to ensure the full and effective progress of the reaction, thereby ensuring the reaction rate, and achieving the purpose of strengthening the reaction.

Example one

Use the above system and process to carry out the biological fermentation of penicillin, among which:

When cultivating bacteria, use agar slant medium, and cultivate in the medium at 25°C for 7 days to generate slant spores. After the cultivation is completed, the slant spore suspension is inoculated on rice or millet substrate and cultured at 25°C for 6 days to generate rice spores. Inoculate with spore rice grains or spore suspension, aerate at 26°C, culture with stirring for 60h to produce bacteria for fermentation.

The temperature of the solution in the fermenter is 26°C, and the pH is 6.5. The pH adjustment solution uses _{one or more of sugar, natural oil, CaCO 3} and ammonia. When the pH is high, it can be controlled by adding sugar or natural oil; When the pH is low, CaCO ₃ or ammonia can be added for adjustment.

When using the micro-interface generator to deliver sterile air, it is ensured that the dissolved oxygen concentration of the material in the fermenter is greater than or equal to 30%.

After testing, the purity of penicillin prepared by using the system of the present invention is 99.53%.

Example two

Use the above system and process to carry out the biological fermentation of penicillin, among which:

When cultivating bacteria, use agar slant medium, and cultivate in the medium at 25°C for 9 days to generate slant spores. After the cultivation is completed, the slant spore suspension is inoculated on rice or millet substrate and cultured at 25°C for 7 days to generate rice spores. Inoculate with spore rice or spore suspension, aerate and stir culture at 26°C for 68 hours to generate bacteria for fermentation.

The temperature of the solution in the fermenter is 27°C, and the pH is 7.0. The pH adjustment solution uses _{one or more of sugar, natural oil, CaCO 3} and ammonia. When the pH is high, it can be controlled by adding sugar or natural oil; when When the pH is low, CaCO ₃ or ammonia can be added for adjustment.

When using the micro-interface generator to deliver sterile air, it is ensured that the dissolved oxygen concentration of the material in the fermenter is greater than or equal to 30%.

After testing, the purity of penicillin prepared by using the system of the present invention is 99.65%.

Comparative example one

The existing technology is used to carry out the biological fermentation of penicillin, wherein the process parameters in the fermentation process are the same as the process parameters in the second embodiment.

After testing, the purity of penicillin prepared by using the system of the present invention is 98.97%.

Example three

The above-mentioned system and process are used to carry out the biological fermentation of amino acids, wherein the biological fermentation of amino acids includes four stages: adaptation period, logarithmic growth period, growth stop period and late fermentation period:

During the adaptation period: control the amount of inoculation and fermentation conditions to shorten the period of the adaptation period. The adaptation period lasts for 2 hours.

In the logarithmic growth phase: maintain the temperature in the fermentor at 30°C, use urea as the pH adjustment solution, and adopt the method of adding urea to timely supply the necessary nitrogen source for bacterial growth, and maintain the pH in the fermentor at 7.5.

During the growth stop period: maintain the temperature in the fermentor at 34°C, use urea as the pH adjustment solution, and add urea in time to provide enough ammonia to maintain the pH in the fermentor at 7.2.

At the later stage of fermentation, the acid concentration in the fermenter is tested, and when the nutrients are exhausted, the acid concentration does not increase, put the tank in time. The fermentation cycle is generally 30h.

After testing, the purity of the amino acid prepared by using the system of the present invention is 99.49%.

Example four

The above-mentioned system and process are used to carry out the biological fermentation of amino acids, wherein the biological fermentation of amino acids includes four stages: adaptation period, logarithmic growth period, growth stop period and late fermentation period:

During the adaptation period: control the amount of inoculation and fermentation conditions to shorten the period of the adaptation period. The adaptation period lasts for 4 hours.

In the logarithmic growth phase: maintain the temperature in the fermentor at 32°C, use urea as the pH adjustment solution, and adopt the method of adding urea to timely supply the necessary nitrogen source for bacterial growth, and maintain the pH in the fermentor at 8.0.

During the growth stop period: maintain the temperature in the fermentor at 37°C, use urea as the pH adjustment solution, and add urea in time to provide enough ammonia to maintain the pH in the fermentor at 7.4.

At the later stage of fermentation, the acid concentration in the fermenter is tested, and when the nutrients are exhausted, the acid concentration does not increase, put the tank in time. The fermentation cycle is generally 30h.

After testing, the purity of the amino acid prepared by using the system of the present invention is 99.62%.

Comparative example two

The existing technology is used to carry out the biological fermentation of amino acids, wherein the process parameters in the fermentation process are the same as those in the fourth embodiment.

After testing, the purity of the amino acid prepared by using the system of the present invention is 99.10%.

Example five

Use the above system and process to carry out the biological fermentation of citric acid, among which:

When cultivating strains: add 25% agar to the wort of 4 Baume degrees, then insert Aspergillus niger strains (aseptic operation), and cultivate at 30°C for 4 days. Mix the bran and water in a ratio of 1:1, then add 10% calcium carbonate, 0.5% ammonium sulfate and stir evenly, and sterilize with 1.5 kg pressure for 60 minutes. Connect the strains cultivated by the inclined plane culture method, and wait for use after 96 hours of cultivation.

When the raw materials are pretreated: the wet powder slag is pressed and dewatered to make the water content 60%; the dry powder slag is supplemented with water at a ratio of 60%; the agglomerated powder slag needs to be crushed into 2mm particles. Then add 2% calcium carbonate, 10% rice bran, stir evenly, stack for 2 hours, and cook. The steaming can be done in two ways: pressurized steaming and atmospheric steaming. First use a bran raising machine to crush the cooked materials, and then add boiling water containing anti-pollution drugs.

When the bacteria are inoculated: when the water temperature of the above raw material is cooled to 37°C, it is connected to the bacterial suspension. After inoculation, it is sent to the koji room for fermentation (at this time, the material temperature is greater than or equal to 27°C). Among them, the production process is aseptic operation.

During fermentation: keep the fermenter ventilated and keep the relative humidity at 86%. The fermentation includes three stages: the first stage is the first 18 hours, the room temperature is between 27°C, and the material temperature is about 27°C; the second stage is 18 hours, the material temperature is 40°C, not exceeding 44°C, and the room temperature requires 33°C About; the third stage is 60h, the material temperature is about 35℃, and the room temperature is 30℃.

After testing, the purity of citric acid prepared by using the system of the present invention is 99.41%.

Example Six

Use the above system and process to carry out the biological fermentation of citric acid, among which:

When cultivating strains: add 30% agar to the wort of 6 Baume degrees, then insert Aspergillus niger strains (aseptic operation), and cultivate at 32°C for 4 days. Mix the bran and water in a ratio of 1:1, then add 10% calcium carbonate, 0.5% ammonium sulfate and stir evenly, and sterilize with 1.5 kg pressure for 60 minutes. Connect the strains cultivated by the inclined plane culture method and wait for use after 120 hours of cultivation.

When the raw material is pretreated: the wet powder slag is pressed and dehydrated to make the water content 60%; the dry powder slag is supplemented with water at a ratio of 60%; the agglomerated powder slag needs to be crushed into 4mm particles. Then add 2% calcium carbonate and 11% rice bran, stir evenly, stack for 2 hours, and cook. The steaming can be done in two ways: pressurized steaming and atmospheric steaming. First use a bran raising machine to crush the cooked materials, and then add boiling water containing anti-pollution drugs.

When the bacteria are inoculated: when the water temperature of the above raw material is cooled to 40°C, it is connected to the bacterial suspension. After inoculation, it is sent to the koji room for fermentation (at this time, the material temperature is greater than or equal to 27°C). Among them, the production process is aseptic operation.

During fermentation: keep the fermenter ventilated and keep the relative humidity at 90%. The fermentation includes three stages: the first stage is the first 18 hours, the room temperature is between 30°C, and the material temperature is around 35°C; the second stage is 60 hours, the material temperature is 43°C, not exceeding 44°C, and the room temperature requires 33°C About; the third stage is 60h, the material temperature is about 37℃, and the room temperature is 32℃.

After testing, the purity of citric acid prepared by using the system of the present invention is 99.57%.

Comparative example three

The existing technology is used to carry out the biological fermentation of citric acid, wherein the process parameters in the fermentation process are the same as those in the sixth embodiment.

After testing, the purity of citric acid prepared by using the system of the present invention is 99.01%.

Example Seven

Use the above system and process to carry out the biological fermentation of starch, among which:

Put the sterilized potato starch into the fermenter, fill the fermenter with 3L of fermentation raw materials, insert the seeds according to the 10% inoculum, control the rotation speed at 240±2r/min, the ventilation rate at 35L/h, and the temperature at 32℃. The fermentation time is 72h. Light calcium carbonate is selected as the pH adjusting solution and the pH of the solution in the fermenter is controlled to maintain at 5.1.

After testing, the starch produced by the system of the present invention has a purity of 99.69%.

Example eight

Use the above system and process to carry out the biological fermentation of starch, among which:

Put the sterilized potato starch into the fermenter, fill the fermenter with 3L of fermentation raw materials, insert the seeds according to the 10% inoculum, control the rotation speed at 240±2r/min, the ventilation rate at 35L/h, and the temperature at 32℃. The fermentation time is 72h. Light calcium carbonate is selected as the pH adjusting liquid and the pH of the solution in the fermenter is controlled to maintain at 5.2.

After testing, the starch produced by the system of the present invention has a purity of 99.74%.

Comparative example four

The existing technology is used to carry out the biological fermentation of starch, wherein the process parameters in the fermentation process are the same as the process parameters in the second embodiment.

After testing, the starch produced by the system of the present invention has a purity of 99.34%.

In summary, after using the fermentation system of the present invention, high purity can be achieved when the specified product is prepared, and the fermentation efficiency is high.

So far, the technical solutions of the present invention have been described in conjunction with the preferred embodiments shown in the drawings. However, it is easy for those skilled in the art to understand that the protection scope of the present invention is obviously not limited to these specific embodiments. Without departing from the principle of the present invention, those skilled in the art can make equivalent changes or substitutions to the relevant technical features, and the technical solutions after these changes or substitutions will fall within the protection scope of the present invention.

The above descriptions are only preferred embodiments of the present invention and are not used to limit the present invention; for those skilled in the art, the present invention can have various modifications and changes. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (9)

1. An aerobic fermentation system, characterized in that it comprises:

   The fermentation tank is used for fermenting materials with designated bacteria, and the fermentation tank includes: a full mixed flow biochemical reaction zone arranged below, used for loading fermentation raw materials and fermentation bacteria, and providing a reaction space for the fermentation of the two, and a set Above, the plug flow biochemical reaction zone for conveying the fermented materials and separating gas and liquid;

   A separation tank, which is connected to the fermentation tank, and is used to separate the materials output from the fermentation tank to generate gaseous bacteria and fermentation broth;

   The micro-interface generator, which is set at a designated position in the full-mixed flow biochemical reaction zone, converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the sterile air, so that the sterile air is broken to form a diameter Micron bubbles of ≥1μm and <1mm to increase the mass transfer area between the fermentation raw materials and sterile air, reduce the thickness of the liquid film, reduce the mass transfer resistance, and mix the fermentation raw materials with micron bubbles to form a gas-liquid emulsification after crushing To enhance the efficiency of the reaction between the oxidizing raw materials and the air within the preset operating conditions;

   The return pipe is respectively connected with the fermentation tank and the separation tank, and is used to preheat the materials output from the fermentation tank and return the materials to the fermentation tank or output to the separation tank after preheating.
2. The aerobic fermentation system according to claim 1, wherein the micro-interface generator comprises:

   The first micro-interface generator is a pneumatic micro-interface generator, the first micro-interface generator is arranged in the fully mixed flow biochemical reaction zone and located at the bottom of the reaction zone, and is used to break the sterile air into micron scale After the crushing is completed, the microbubbles are output to the fermentation tank and mixed with the materials in the fermentation tank to form a gas-liquid emulsion;

   The second micro-interface generator is a hydraulic or gas-liquid linkage micro-interface generator. The second micro-interface generator is arranged in the fully mixed flow biochemical reaction zone and at the top of the reaction zone to receive the The material output from the reflux tube uses the material to entrain the under-used sterile air in the plug flow biochemical reaction zone and break the sterile air to form micro-sized micro-bubbles, and mix the micro-bubbles with the material to form a gas-liquid emulsion It is output to the fully mixed flow biochemical reaction zone to counteract the gas-liquid emulsion output from the first micro-interface generator, thereby prolonging the residence time of the microbubbles in the fully mixed flow biochemical reaction zone.
3. The aerobic fermentation system according to claim 1, wherein the fully mixed flow biochemical reaction zone in the fermentor comprises:

   A grille, which is arranged inside the fermentor to filter insoluble particles in the material;

   The pH adjusting liquid inlet, which is arranged on the side wall of the fermentation tank and above the grid, is used to transport the pH adjusting liquid to adjust the pH value of the material;

   Fermentation raw material feed inlet, which is arranged on the side wall of the fermentor and located below the grill, for conveying the fermentation raw material;

   Fermentation strain feed inlet, which is arranged on the side wall of the fermentor and located below the fermented raw material feed inlet, and is used to transport designated strains into the fermentor and ferment the fermented raw materials;

   The first gas-phase feed pipe is arranged on the side wall of the fermentor and connected to the micro-interface generator, and is used to transport sterile air from the side to the micro-interface generator in the fermentor;

   A residue outlet, which is set at the bottom of the fermentor to discharge the residue after fermentation out of the system;

   The partition is arranged on the inner wall of the fermentation tank and located below the grill, and is used to block the fluctuation of the fermentation raw material output from the fermentation raw material inlet and the bacteria output from the fermentation strain feed inlet.
4. The aerobic fermentation system according to claim 1, wherein the plug flow reaction zone comprises:

   An exhaust pipe, which is arranged at the top of the fermentation tank, and is used to discharge the tail gas out of the system after the fermentation of the material in the fermentation tank is completed;

   A second gas-phase feed pipe is arranged in the fermentor, and the bottom end of the second feed pipe is connected with the second micro-interface generator, and the top of the second feed pipe is located above the liquid level in the fermentor , To entrain the unused sterile air on the top of the fermentor into the micro-interface generator in the fermentor so that the micro-interface generator can break the sterile air;

   A discharging port, which is arranged on the side wall of the fermentation tank, and is used to output the fermented material out of the fermentation tank;

   The reflux feed pipe is arranged on the side wall of the fermentor, and is used to output part of the material output from the reflux pipe to the micro-interface generator in the fermentor.
5. The aerobic fermentation system according to claim 1, wherein the return pipe comprises:

   A circulating pump, which is connected to the fermentation tank, and is used to output the fermented materials in the fermentation tank;

   The heat exchanger is connected with the circulating pump and is used to exchange heat for the material output by the circulating pump so that the material reaches a specified temperature.
6. The aerobic fermentation system according to claim 5, characterized in that the output end of the heat exchanger is provided with a shunt pipe, and the shunt pipe is connected to the fermentation tank and the separation tank, respectively The material is refluxed and output to the separation tank.
7. The aerobic fermentation system according to claim 1, wherein the separation tank is a sealed tank, comprising:

   A feed port, which is arranged at the top of the separation tank, and is used to transport the material output from the return pipe to the inside of the separation tank;

   An exhaust port, which is arranged at the top of the separation tank for outputting gaseous bacterial species;

   The discharging port is arranged at the bottom end of the separation tank, and is used to output the separated fermentation broth and transport the fermentation broth to the next section.
8. An aerobic fermentation process, which is characterized in that it comprises:

   Step 1: Transport the specified type of fermentation raw material to the full mixed-flow biochemical reaction zone in the fermentor through the fermentation raw material inlet, and transport the specified type of bacteria to the fermentor through the fermentation bacteria inlet Inside the fermentation tank;

   Step 2: The sterile air is delivered to the first micro-interface generator through the first gas-phase feed pipe, and the first micro-interface generator breaks the sterile air into micro-sized micro-bubbles and outputs the micro-bubbles to the Among the fermentation raw materials in the fermenter, microbubbles are fully mixed with the fermentation raw materials to provide an aerobic environment for bacteria;

   Step 3: The bacteria react with the fermentation raw materials in an aerobic environment. After the fermentation is completed, the fermentor will transport the fermented materials to the horizontal plug flow biochemical reaction zone, and the materials will flow through the grid, and the grid will transfer the materials into the biochemical reaction zone. The residue is filtered out, and after the filtration, the residue will settle to the bottom of the fermentor and be discharged out of the fermentor through the residue outlet;

   Step 4: After filtering, the material will flow in the designated direction in the plug flow biochemical reaction zone. When the material flows to the top of the fermentation tank, the gas in the material will be output to the fermentation tank through the exhaust pipe, and the material will pass through the first outlet. The material port is output to the return pipe;

   Step 5: The reflux pipe draws out the material in the fermentor, and divides the flow after preheating, and returns a part of the preheated material to the second micro-interface generator to adjust the full mixed flow biochemical reaction zone And output the other part to the separation tank for separation;

   Step 6: After the preheated material is refluxed, it enters the second micro-interface generator through the reflux feed pipe, and the second micro-interface generator removes the unused materials on the top of the fermentor Bacterial air is entrained to the second interface generator, and the material is used to break the sterile air to form micro-sized micro-bubbles and mix the micro-bubbles with the material to form a gas-liquid emulsion. After the gas-liquid emulsion is formed, the second micro-interface occurs The device outputs the gas-liquid emulsion to the full-mixed flow biochemical reaction zone to adjust the temperature in the full-mixed flow biochemical reaction zone while reusing materials;

   Step 7: After the preheated materials are output to the separation tank, the separation tank separates the materials from gas and liquid to form gaseous bacteria and fermentation broth. After separation, the gaseous bacteria are discharged from the separation tank through the exhaust port, and the fermentation The liquid is discharged from the separation tank through the second discharge port and transported to the next section.
9. The aerobic fermentation process according to claim 8, characterized in that, when the system is running, the pH adjusting liquid inlet will deliver the pH adjusting liquid to adjust the pH value of the materials in the fermentation tank.

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