A gas distributor coupled to a kettle bottom bearing

Abstract

The utility model discloses a gas distributor coupled with kettle bottom bearing belongs to process engineering equipment technical field. The distributor includes cylindrical cavity, air inlet pipe, dispersion tooth, liquid inlet and gas liquid export, and the gas liquid export sets up at the top of cylindrical cavity, and the dispersion tooth sets up on the upper edge of cylindrical cavity, and the air inlet pipe is connected with the side of cylindrical cavity, and the joint of air inlet pipe and cylindrical cavity is the spiral pipe shape structure, and the liquid inlet is located at the bottom and the lower part of cylindrical cavity, and the bottom of cylindrical cavity extends locally and has fixed tongue plate, and the fixed tongue plate is fixedly connected with the bottom bearing, and the bottom bearing is installed with the stirring shaft in, and the stirring shaft is arranged in cylindrical cavity, and the stirring shaft is connected with radial flow agitator, and the bottom bearing, gas distributor, radial flow agitator are arranged in the reaction kettle from below to above in proper order. The distributor can improve the space utilization of kettle bottom, realize the zero liquid residual of shutdown, complete the efficient mixing of gas liquid with low energy consumption, and is suitable for large vertical stirring reaction kettle in the field such as biological fermentation, chemical synthesis.

Description

Technical Field

[0001] This utility model relates to a gas distributor coupled to a bottom bearing of a reactor, belonging to the field of process engineering equipment technology. Background Technology

[0002] The gas distributor is a crucial functional component of gas-liquid two-phase reaction equipment. Its core function is to work in conjunction with the radial flow agitator to uniformly disperse the gas into tiny bubbles and thoroughly mix it with the liquid. This increases the gas-liquid contact area, improves mass transfer efficiency, and ensures uniform mixing and gas-liquid dispersion within the reaction system. It is a key component determining the reaction rate, product yield, and equipment operational stability. This component is widely used in fields such as bio-fermentation (e.g., fermenters for antibiotic, enzyme, and amino acid production), chemical synthesis (e.g., emulsion polymerization, oxidation reactors, hydrogenation reactors), and environmental protection (e.g., biofilm wastewater treatment reactors). Especially in large-scale vertical stirred reactors, the performance of the gas distributor directly impacts overall production efficiency and product quality.

[0003] Currently, commonly used gas distributors in the industrial field mainly fall into three categories: First, perforated plate distributors, which achieve gas dispersion by opening dense small holes in a flat or curved plate. However, they are prone to clogging of the channels due to material agglomeration or crystallization, and the uniformity of bubble dispersion is poor in high-viscosity liquid systems. Second, bubble ring distributors, which consist of annular pipes and openings in the pipe walls. Gas is ejected from the annular pipes to the openings in the pipe walls. However, this structure suffers from problems such as clogging of the channels and uneven bubble distribution, resulting in significant differences in local mass transfer efficiency within the reaction system. Third, nozzle distributors, which rely on high-pressure gas to be ejected at high speed from the nozzles to drive liquid mixing. Although this can improve the bubble breaking effect, it requires additional high-pressure gas power, resulting in high energy consumption.

[0004] Furthermore, existing gas distributors are generally designed independently and are not integrated with the bottom bearing. In vertical stirred reactors, the bottom bearing supports the stirring shaft, while traditional gas distributors require a separate fixed structure. This not only occupies a large amount of installation space at the bottom of the reactor, resulting in low utilization of the bottom space, but also requires separate positioning and assembly, increasing the complexity of equipment installation and maintenance costs. Additionally, due to structural design flaws, some distributors are prone to leaving liquid residue after shutdown. Especially in bio-fermentation scenarios, this residual liquid can easily breed contaminants, increasing the risk of contamination in subsequent production. Moreover, existing structures struggle to balance the negative pressure liquid absorption effect under high gas flow rates with uniform bubble dispersion, making it difficult to meet actual production needs in scenarios requiring efficient gas-liquid mixing with low energy consumption. Utility Model Content

[0005] This invention aims to solve the technical problems of low space utilization, high installation and maintenance costs, easy contamination risk caused by liquid residue, and difficulty in achieving both low-energy negative pressure liquid absorption and uniform gas-liquid dispersion in existing gas distributors and bottom bearings. It provides a gas distributor coupled with a bottom bearing, which achieves efficient space utilization and low-energy efficient gas-liquid dispersion through structural integration and functional synergy, while avoiding liquid residue after shutdown. It is suitable for the production needs of large vertical stirred reactors in fields such as bio-fermentation and chemical synthesis.

[0006] The purpose of this utility model is to provide a gas distributor coupled with a bottom bearing of a reactor, comprising a cylindrical cavity, an inlet pipe, dispersion teeth, a liquid inlet, and a gas-liquid outlet. The cylindrical cavity, dispersion teeth, gas-liquid outlet, and liquid inlet are integrally formed. The gas-liquid outlet is located at the top of the cylindrical cavity, the dispersion teeth are located at the upper edge of the cylindrical cavity, the inlet pipe is connected to the side of the cylindrical cavity, and the connection between the inlet pipe and the cylindrical cavity is a spiral tubular structure, through which gas enters tangentially into the side of the cylindrical cavity. The liquid inlet is located at the bottom and lower side of the cylindrical cavity, allowing liquid to be drawn in from the bottom. A fixed tongue plate extends partially from the bottom of the cylindrical cavity, and a bottom bearing is fixedly connected to the fixed tongue plate. A stirring shaft is installed inside the bottom bearing and passes through the cylindrical cavity. The stirring shaft is connected to a radial flow stirrer. The bottom bearing, gas distributor, and radial flow stirrer are arranged sequentially from bottom to top inside the reactor.

[0007] In one embodiment of this utility model, the end of the air inlet pipe near the cylindrical cavity is a spiral tube structure, and the other end is a circular tube extending to the outside of the container wall of the reactor. Gas enters the cylindrical cavity spirally and tangentially from the side of the cylindrical cavity through the air inlet pipe. The large volume flow rate of gas rotates at high speed in the cylindrical cavity and forms a negative pressure state at the axis, attracting a small volume flow rate of liquid to enter the cylindrical cavity from the bottom liquid inlet. The gas and liquid two-phase fluid undergoes tangential mixing and dispersion in the cylindrical cavity, guiding the gas and liquid two-phase fluid to be sprayed upward from the gas and liquid outlet. The dispersion teeth perform secondary shearing on the gas and liquid flow, breaking the bubbles into smaller particles. Subsequently, the gas and liquid flow enters directly below the radial flow agitator, and completes the three-stage dispersion through the radial shearing force of the radial flow agitator.

[0008] In one embodiment of this utility model, the bottom bearing includes a protective sleeve, a bearing bush sleeved on the outside of the protective sleeve, and a base sleeved on the outside of the bearing bush. The stirring shaft is installed inside the protective sleeve. A pressure plate is fixedly connected above the bearing bush and the protective sleeve. A support flange is provided on the outside of the base. One side of the base is connected to the support flange and the fixing tongue plate by bolts and nuts.

[0009] In one embodiment of this utility model, the dispersing teeth are arranged circumferentially along the upper edge of the cylindrical cavity, the dispersing teeth are inclined towards the stirring shaft, the inclination angle is 30º~60º, the length of the dispersing teeth is 0.05~0.3 times the diameter of the cylindrical cavity, and the ratio of the width of the dispersing teeth to the tooth spacing is 0.25~0.8.

[0010] In one embodiment of this utility model, the air intake direction of the air intake pipe is the same as the rotation direction of the radial flow agitator, the ratio of the cross-sectional area of ​​the air inlet of the air intake pipe to the cross-sectional area of ​​the gas-liquid outlet is 0.3 to 2.0; the ratio of the cross-sectional area of ​​the liquid inlet to the air inlet of the air intake pipe is 0.05 to 0.3; and the height-to-diameter ratio of the cylindrical cavity is 1.0 to 4.0.

[0011] In one embodiment of this utility model, the ratio of the distance between the axis of the air intake pipe and the lower end face of the cylindrical cavity to the height of the cylindrical cavity is 0.1 to 0.5.

[0012] In one embodiment of this utility model, the fixed tongue plate and the cylindrical cavity are an integral structure or welded together, and the ratio of the area of ​​the fixed tongue plate to the bottom area of ​​the cylindrical cavity is 0.1 to 0.3.

[0013] In one embodiment of this utility model, the air inlet pipe is connected to the inner bottom wall of the reactor by at least one fixed bracket; a support foot is installed below the support flange, and the lower edge of the liquid inlet is flush with the upper end face of the support flange.

[0014] In one embodiment of this utility model, the cylindrical cavity adopts an integral structure; or adopts a split structure, wherein one side adopts a fixed structure and the other side adopts a detachable structure.

[0015] In one embodiment of this utility model, the liquid inlet is arch-shaped or square-shaped, and the number is 2 to 8.

[0016] Beneficial effects This invention, through structural integration and functional synergy, has the following advantages over existing technologies: 1. Space and cost optimization: Through the coupled design of "bottom bearing - gas distributor - radial flow agitator", the independent fixed structure is eliminated, the utilization rate of bottom space is increased by more than 10%, the installation steps are reduced by about 20%, and the maintenance cost is reduced by 15%~25%; 2. Prevention of residue and contamination: The design of the arch-shaped or square-shaped liquid inlet flush with the support flange ensures zero liquid residue after shutdown, significantly reducing the risk of contamination in bio-fermentation scenarios. 3. Low energy consumption and high efficiency mixing: The negative pressure liquid absorption formed by the spiral tangential air intake does not require additional power. After three-stage treatment of "cavity mixing - dispersion tooth shearing - stirring paddle three-stage dispersion", the gas-liquid contact area is increased by 5%~10% and the mass transfer efficiency is improved by 10%~15%. 4. High adaptability: The cylinder can be adapted to different volumes (10~500 m³) by adjusting the height-to-diameter ratio, dispersion tooth parameters, and the cross-sectional area ratio of the liquid inlet to the air inlet. 3 It can be used to develop reaction systems with different viscosity (1~10000 mPa∙s), and its application scope covers mainstream fields such as bio-fermentation and chemical synthesis. Attached Figure Description

[0017] Figure 1 A schematic diagram of a gas distributor for coupling a bottom bearing of a reactor provided by this utility model; Figure 2 for Figure 1 Sectional view along line AA in the middle; Figure 3 A front view of the gas distributor section structure of a coupled bottom bearing provided by this utility model; Figure 4 This is a top view of the gas distributor section of a coupled bottom bearing provided by this utility model.

[0018] In the diagram: 1. Support foot; 2. Support flange; 3. Liquid inlet; 4. Base; 5. Bearing bush; 6. Sheath; 7. Pressure plate; 8. Stirring shaft; 9. Dispersion teeth; 10. Cylindrical cavity; 11. Air inlet pipe; 12. Fixing tongue plate; 13. Bolt; 14. Nut; 15. Gas-liquid outlet. Detailed Implementation

[0019] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of the present utility model.

[0020] In this utility model, unless otherwise explicitly specified and limited, the terms "connected," "linked," and "fixed" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0021] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0022] Example 1 This embodiment provides a gas distributor coupled to a bottom bearing, including a cylindrical cavity 10, an inlet pipe 11, dispersion teeth 9, a liquid inlet 3, and a gas-liquid outlet 15. The cylindrical cavity 10, dispersion teeth 9, gas-liquid outlet 15, and liquid inlet 3 are integrally formed. The gas-liquid outlet 15 is located at the top of the cylindrical cavity 10, the dispersion teeth 9 are located at the upper edge of the cylindrical cavity 10, and the inlet pipe 11 is connected to the side of the cylindrical cavity 10. The connection between the inlet pipe 11 and the cylindrical cavity 10 is a spiral tubular structure, through which gas flows tangentially. The liquid inlet 3 is located at the bottom and lower side of the cylindrical cavity 10, allowing liquid to be drawn in from the bottom. A fixed tongue plate 12 extends partially from the bottom of the cylindrical cavity 10. A bottom bearing is fixedly connected to the fixed tongue plate 12. A stirring shaft 8 is installed inside the bottom bearing and passes through the cylindrical cavity 10. A radial flow stirrer is connected to the stirring shaft 8. A gas distributor is located directly below the radial flow stirrer. The bottom bearing, gas distributor, and radial flow stirrer are arranged sequentially from bottom to top inside the reactor.

[0023] Gas enters the cylindrical cavity 10 spirally and tangentially from the side of the cylinder 10 through the inlet pipe 11. The large volume flow of gas rotates at high speed in the cylindrical cavity 10 and forms a negative pressure state at the axis, attracting a small volume flow of liquid to enter the cylindrical cavity 10 from the bottom liquid inlet 3. The gas and liquid two-phase fluids undergo tangential mixing and dispersion in the cylindrical cavity 10, and are guided to be sprayed upward from the gas-liquid outlet 15. The dispersion teeth 9 perform secondary shearing on the gas-liquid flow, breaking the bubbles into smaller particles. Subsequently, the gas-liquid flow enters directly below the radial flow agitator, and completes a third dispersion through the radial shearing force of the radial flow agitator, further improving the uniformity of gas-liquid mixing.

[0024] Optionally, the bottom bearing includes a sleeve 6, a bearing shell 5 sleeved on the outside of the sleeve 6, and a base 4 sleeved on the outside of the bearing shell 5. The stirring shaft 8 is installed inside the sleeve 6. A pressure plate 7 is fixedly connected above the bearing shell 5 and the sleeve 6. A support flange 2 is provided on the outside of the base 4. One side of the base 4 is connected to the support flange 2 and the fixing tongue plate 12 by bolts 13 and nuts 14.

[0025] Optionally, the dispersing teeth 9 are arranged circumferentially along the upper edge of the cylindrical cavity 10, the dispersing teeth 9 are inclined towards the stirring shaft 8, the inclination angle is 30º~60º, the length of the dispersing teeth 9 is 0.05~0.3 times the diameter of the cylindrical cavity 10, and the ratio of the width of the dispersing teeth 9 to the tooth spacing is 0.25~0.8.

[0026] Optionally, one end of the air inlet pipe 11 near the cylindrical cavity 10 is a spiral tube structure, and the other end is a round tube that extends to the outside of the container wall of the reactor. The air inlet pipe 11 is connected to the inner bottom wall of the reactor by at least one fixed bracket to ensure a stable air intake process.

[0027] Optionally, the air intake direction of the air intake pipe 11 is the same as the rotation direction of the radial flow agitator, and the ratio of the cross-sectional area of ​​the air inlet of the air intake pipe 11 to the cross-sectional area of ​​the gas-liquid outlet 15 (excluding the cross-sectional area of ​​the agitator shaft 8) is 0.3 to 2.0.

[0028] Optionally, the ratio of the cross-sectional area of ​​the liquid inlet 3 to the cross-sectional area of ​​the air inlet of the air inlet pipe 11 is 0.05 to 0.3.

[0029] Optionally, the height-to-diameter ratio of the cylindrical cavity 10 is 1.0 to 4.0.

[0030] Optionally, the ratio of the distance between the axis of the intake pipe 11 and the lower end face of the cylindrical cavity 10 to the height of the cylindrical cavity 10 is 0.1 to 0.5.

[0031] Optionally, the fixed tongue plate 12 and the cylindrical cavity 10 are integral structures or welded together, and the ratio of the area of ​​the fixed tongue plate 12 to the bottom area of ​​the cylindrical cavity 10 is 0.1 to 0.3.

[0032] Optionally, a support foot 1 is installed below the support flange 2, and the lower edge of the liquid inlet 3 is flush with the upper end face of the support flange 2. After the operation stops, the liquid will be discharged under the action of gravity and will not remain in the gas distributor.

[0033] Optionally, the cylindrical cavity 10 adopts an integral structure to suit small reactors; or it adopts a split structure, wherein one side is fixed and the other side is detachable, to suit large reactors or scenarios requiring regular maintenance, thereby improving equipment adaptability.

[0034] Optionally, the radial flow agitator includes an agitator blade, which is fixedly connected to the outer periphery of the agitator shaft 8.

[0035] Optionally, the liquid inlet 3 is arch-shaped or square-shaped, and the number is 2 to 8.

[0036] In summary, the gas distributor of the coupled bottom bearing provided by this utility model uses a cylindrical cavity 10 as the core load-bearing component. The cylindrical cavity 10, dispersing teeth 9, gas-liquid outlet 15, liquid inlet 3, and fixing tongue plate 12 are manufactured using an integrated molding process, avoiding sealing hazards and space waste caused by separate connections. The height-to-diameter ratio of the cylindrical cavity 10 is set to 1.0~4.0, ensuring sufficient mixing time for gas and liquid within the cylindrical cavity 10 while avoiding excessive occupation of bottom space. The cylindrical cavity 10 is located directly below the bottom radial flow agitator and directly above the bottom bearing in the reactor, forming a coaxial coupling layout of "bottom bearing - gas distributor - radial flow agitator" from bottom to top. This eliminates the need for a separate fixing bracket for the gas distributor, significantly improving the utilization rate of bottom space.

[0037] The air inlet pipe 11 is connected to the side of the cylindrical cavity 10. It adopts a spiral tubular structure to allow the gas to enter the cavity tangentially, and the air inlet direction is consistent with the rotation direction of the radial flow agitator. The ratio of the cross-sectional area of ​​the air inlet to the cross-sectional area of ​​the gas-liquid outlet 15 (excluding the cross-sectional area of ​​the agitator shaft) is 0.30~2.0. When a large volume of gas enters the cylindrical cavity 10 tangentially along the spiral trajectory, a high-speed rotating flow field will be formed in the cylindrical cavity 10. A stable negative pressure is generated at the axis of the cylindrical cavity 10 due to centrifugal force. This negative pressure can actively attract liquid from the liquid inlet 3 into the cylindrical cavity 10.

[0038] The liquid inlet 3 is located at the bottom and lower side of the cylindrical cavity 10, and is in the shape of an arch or a square hole. Its lower edge is flush with the upper end face of the support flange 2. The ratio of the cross-sectional area of ​​the liquid inlet 3 to that of the air inlet is 0.05~0.3, which ensures stable liquid intake under negative pressure and allows the liquid in the cylindrical cavity 10 to be completely discharged along the liquid inlet 3 after shutdown, avoiding residue. At the same time, the small volume flow rate of liquid and the high-speed rotating gas undergo tangential impact and shearing in the cylindrical cavity 10, and the gas-liquid mixing is initially completed.

[0039] The fixed tongue plate 12 is a structure formed by a partial extension of the bottom of the cylindrical cavity 10 (or welded to the cylindrical cavity 10). Its area is 0.1~0.3 times the bottom area of ​​the cylindrical cavity 10. Fixing holes are provided on the fixed tongue plate 12, and it is directly connected and fixed to the support flange 2 using bolts 13 and nuts 14, achieving rigid fixation between the gas distributor and the bottom support structure without the need for additional fixing components, simplifying the installation process. The dispersing teeth 9 are arranged along the upper edge of the cylindrical cavity 10, inclined towards the stirring shaft 8 at an angle of 30º~60º, and their length is 0.05~0.3 times the diameter of the cylindrical cavity 10. The width of the dispersing teeth 9 is 0.25 to 0.8 times the spacing between the teeth. When the initially mixed gas and liquid in the cylindrical cavity 10 is sprayed upward from the gas-liquid outlet 15, the dispersing teeth 9 can perform secondary shearing on the gas-liquid flow, breaking the bubbles into smaller particles. Subsequently, the gas-liquid flow directly flows to the bottom radial flow stirring paddle, where it completes a third dispersion with the help of the radial shearing force of the stirring paddle, further improving the uniformity of gas-liquid mixing. Thus, this gas distributor coupled with the bottom bearing achieves coupling with the bottom bearing and efficient gas-liquid dispersion through the structural design and functional synergy of its components.

[0040] Example 2 This embodiment is adapted for 320m³ penicillin production on a large scale in the field of bio-fermentation. 3 The fermenter is equipped with a 1700mm diameter radial flow agitator (120 r / min) at the bottom. The bottom bearing uses a high-strength graphite-metal composite bearing (220mm diameter). The equipment is required to be suitable for high-flow-rate gas-liquid processing (compressed air flow rate 200 Nm³). 3 It features high oxygen mass transfer efficiency ( / min) and no liquid residue to control the risk of contamination, while also meeting the requirements for penicillin synthesis.

[0041] The cylindrical cavity of the gas distributor is a one-piece molded structure with an inner diameter of Φ600mm and a height of 1200mm, with a height-to-diameter ratio of 2.0 (balancing mixing time and space utilization). It is made of 304 stainless steel. The gas distributor's inlet pipe is a DN450mm round pipe, tangentially connected to the side of the cavity via a 180° spiral tubular structure (the centerline of the round pipe is 400mm from the lower end face, and the distance between the axis and the lower end face / cavity height = 0.36). The inlet direction is consistent with the agitator's rotation direction (clockwise); the inlet cross-sectional area is 0.159m². 2 The cross-sectional area of ​​the gas-liquid outlet (after deducting the cross-sectional area of ​​the stirring shaft, the cross-sectional area of ​​the gas-liquid outlet is set to 0.245m) is also considered. 2 The ratio is 0.65; Liquid inlet: 6 arched holes, each with an area of ​​0.006 m² 2 Total cross-sectional area: 0.036 m² 2The ratio of its cross-sectional area to that of the air inlet is 0.22, and its lower edge is flush with the upper surface of the support flange. Dispersed teeth: 24 rectangular teeth (25mm wide, 75mm long), arranged circumferentially along the upper edge of the cavity, with an inward inclination angle of 45° and a tooth spacing of 78.5mm (width to tooth spacing ratio 0.32). Fixed tongue plate: integrally connected to the cylindrical cavity, the tongue plate extends inward, with an area of ​​0.0707m². 2 (The bottom area of ​​the cylindrical cavity is 0.283m²) 2 (0.25 times the original size), six Φ25mm fixing holes are opened, and the flange is rigidly fixed with M25 bolts.

[0042] Installation: The coaxial assembly is located directly above the bottom bearing and directly below the radial flow agitator (350mm spacing). After the air inlet pipe passes through the vessel wall, it is connected to the bottom wall of the vessel through two fixed brackets. Operation: 200 Nm 3 / min compressed air creates a stable negative pressure along the axis of the chamber. The fermentation broth is drawn in from the inlet and dispersed three times by tangential mixing, dispersion tooth shearing, and agitator. The dissolved oxygen level is maintained above 20% throughout the fermentation process. There is no liquid residue in the distributor after shutdown. The contamination rate is 0 after 300 days of continuous operation. The number of maintenance times is reduced by 50% compared to the traditional structure (loop distributor).

[0043] Example 3 This embodiment is adapted for high-density fermentation of Pichia pastoris in the field of bio-fermentation using a 103 m³ mol / L solution. 3 Fermentation tank (liquid volume 75m³) 3 The fermenter has an inner diameter of Φ3600mm and a straight section height of 9000mm. It is equipped with a Φ1250mm BT-6 bottom radial flow agitator (170 r / min), and the bottom bearing uses a graphite-PTFE composite bearing (Φ180 mm diameter). High-density fermentation of Pichia pastoris requires high dissolved oxygen, no liquid residue to prevent contamination, and a ventilation intensity of 1.2 vvm (corresponding to a ventilation volume of 90 Nm³). 3 ( / min), the split structure makes it easy to disassemble, wash, disinfect and maintain after fermentation, and is suitable for long-term continuous production needs.

[0044] (1) Cylindrical cavity Structure: Split-type (fixed on the left, detachable on the right), assembled by flange bolts, with fluororubber gaskets at the joints to ensure gas-liquid sealing performance; Material: 304 stainless steel (resistant to acid and alkali corrosion of fermentation liquid, meeting the requirements of food-grade biological fermentation); Dimensions: Inner diameter Φ400mm, height 500mm, height-to-diameter ratio 1.25; Gas-liquid outlet cross-sectional area: π×(0.2) 2 -0.09 2 )≈0.1002m 2 .

[0045] (2) Intake pipe Specifications: DN200mm seamless round tube (material: 304 stainless steel); Connection method: It is tangentially connected to the fixed side of the cylindrical cavity through a 180° spiral tubular structure to ensure that the gas enters in a spiral tangential direction; Axis spacing: The distance between the intake pipe axis and the lower end face of the cylindrical cavity is 200mm, and the ratio to the cavity height is 0.4; Inlet direction: Consistent with the rotation direction of the radial flow agitator (counterclockwise) to avoid flow field interference; Cross-sectional area ratio: Inlet cross-sectional area π × (0.1m) 2 ≈0.0314 m 2 The gas-liquid outlet is the annular area at the upper edge of the cavity. After deducting the stirring shaft (Φ180mm), the ratio of the actual air inlet to the gas-liquid outlet cross-sectional area is 0.313.

[0046] (3) Liquid inlet Structural features: 6 rectangular holes (symmetrically distributed at the bottom and lower sides of the cavity), each hole measuring 40mm × 30mm; Total cross-sectional area: 6 × (0.04 × 0.03) = 0.0072 m² 2 ; Cross-sectional area ratio: 0.229 compared to the cross-sectional area of ​​the air intake; Installation height: The lower edge of the liquid inlet is flush with the upper end face of the bottom support flange of the reactor. After the machine is stopped, the fermentation liquid in the cavity can be completely discharged without any residual liquid.

[0047] (4) Dispersion teeth Structural parameters: 24 rectangular dispersion teeth (material 304 stainless steel), each tooth is 20mm wide and 100mm long; Arrangement: The arrangement is uniformly distributed along the upper edge of the cylindrical cavity, with the tilt direction facing the stirring shaft at an angle of 45°. Tooth pitch ratio: The distance between adjacent dispersed teeth is 52mm, and the ratio of tooth width to tooth pitch is 0.385.

[0048] (5) Fix the tongue plate Connection method: The fixed side tongue plate is integrally formed with the cylindrical cavity, and the detachable side tongue plate is integrally formed with the cavity. The total number of tongue plates is 6, with 3 tongue plates on each side, all extending inward. Area ratio: Single tongue plate area 0.004m² 2 The total area of ​​the tongue plate is 0.024m².2 ; Fixed structure: Each tongue plate has a Φ20mm fixing hole, which is rigidly connected to the bottom support flange of the vessel by M20 high-strength bolts. The detachable side is equipped with a quick-release pin to simplify the disassembly and cleaning process.

[0049] (6) Installation process Coaxial positioning: First, align the fixed side of the gas distributor with the bottom bearing (Φ180mm bearing shell) and assemble it directly below the bottom radial flow agitator. Set the distance between the upper edge of the distributor and the lower edge of the agitator blades to 300mm to ensure that the gas and liquid flow directly enters the stirring and shearing zone. Splicing and fixing: The detachable side and the fixed side are spliced ​​together by flange bolts, and the sealing gasket is tightened to ensure no leakage; Air inlet pipe fixing: The end of the air inlet pipe away from the cavity extends through the side wall of the fermenter and is connected to the bottom wall of the vessel through two pairs of fixed brackets. The brackets are welded to the bottom wall to prevent the pipe from vibrating during ventilation.

[0050] (7) Operational effect Gas-liquid mixing and dissolved oxygen: 90 Nm 3 After sterile air is introduced at a constant rate, the fermentation broth is drawn in from the inlet and dispersed three times by "tangential mixing, dispersion tooth shearing, and radial flow stirring paddle". The dissolved oxygen is maintained at 20%~30% throughout the fermentation process, which meets the high oxygen requirements of Pichia pastoris high-density fermentation. Prevention of residue and prevention of contamination: After shutdown, the fermentation liquid in the chamber is completely discharged through the inlet. There are no dead corners with residue when cleaning the detachable side. The contamination rate is 0 after 180 days of continuous operation. Convenience of maintenance: The split structure reduces the time for disassembly and washing after fermentation by 40% and the frequency of maintenance by 30% compared to the one-piece structure, making it suitable for the continuous production rhythm of high-density fermentation.

[0051] Example 4 This embodiment is adapted for the 30m³ process of hydrogenating butyrynethiol to prepare 1,4-butanediol in the field of chemical synthesis. 3 The hydrogenation reactor operates at a pressure of 2.0 MPa. The reactor body has an inner diameter of 2800 mm and a straight section height of 5000 mm. It is equipped with a BT-6 type bottom radial flow agitator (1000 mm diameter, 150 rpm). The reactor bottom bearing uses a silicon carbide-metal composite bearing (Φ100 mm diameter). The reaction system is hydrogen gas (inlet flow rate 12 Nm³). 3 The process involves a hydrogen dispersion of 1,4-butanediol solution and Raney nickel catalyst (35 μm particle size), requiring high uniformity of hydrogen dispersion and no liquid residue to avoid catalyst deposition, while also meeting the production requirements for high conversion of 1,4-butanediol.

[0052] (1) Cylindrical cavity Structural form: Integrated structure; Material: 316L stainless steel (resistant to corrosion from hydrogen, butynediol and its products); Dimensions: Inner diameter Φ120mm, height 180mm, height-to-diameter ratio 1.5 (suitable for small-capacity vessel space); Base area: π × (0.06 m) 2 ≈0.0113m 2 .

[0053] (2) Intake pipe Specifications: DN40mm seamless round tube (material: 316L stainless steel); Connection method: It is tangentially connected to the side of the cylindrical cavity through a 180° spiral tubular structure to ensure smooth tangential gas entry; Axis spacing: The distance between the intake pipe axis and the lower end face of the cylindrical cavity is 50mm, and its ratio to the cavity height is 50 / 180=0.278; Air intake direction: Same as the rotation direction of the BT-6 agitator (counterclockwise) to avoid mutual interference between airflow and agitation flow field; Cross-sectional area ratio: The cross-sectional area of ​​the air inlet is π × (0.02m). 2 ≈0.00126m 2 The gas-liquid outlet is the annular area at the upper edge of the cylindrical cavity, excluding the stirring shaft (diameter Φ100mm, cross-sectional area π×(0.05m). 2 ≈0.00785m 2 After that, the actual gas-liquid outlet cross-sectional area is π×[(0.06m)]. 2 -(0.05m) 2 ]≈0.00346m 2 The ratio of their cross-sectional areas is 0.00126 / 0.00346≈0.364. Combined with the low flow rate of hydrogen, the flow area of ​​the gas-liquid outlet is adjusted to ensure a stable negative pressure is formed in the cavity.

[0054] (3) Liquid inlet Structural form: 2 square holes (symmetrically distributed on both sides of the cylindrical cavity), each hole is 30mm×30mm in size; Total cross-sectional area: 2 × (0.03m × 0.03m) = 0.0018m² 2 ; Cross-sectional area ratio: The ratio of the cross-sectional area of ​​the liquid inlet to the air inlet is 0.0018 / 0.00126≈0.143; Installation height: The lower edge of the liquid inlet is flush with the upper end face of the bottom support flange of the vessel. After the machine is stopped, the liquid in the cavity can be completely discharged through the square hole, avoiding the deposition of Raney nickel catalyst in the cavity.

[0055] (4) Dispersion teeth Structural parameters: 8 rectangular dispersion teeth (material 316L stainless steel), each tooth is 15mm wide and 10mm long; Arrangement: The arrangement is uniformly distributed along the upper edge of the cylindrical cavity, with the tilt direction facing the stirring shaft at an angle of 30°; Tooth pitch ratio: The distance between adjacent dispersed teeth is 47mm, and the ratio of tooth width to tooth pitch is 15 / 47=0.319, which can efficiently shear the rising gas-liquid flow.

[0056] (5) Fix the tongue plate Connection method: The connection with the cylindrical cavity is made by welding to ensure pressure resistance stability; Area ratio: Due to the small difference between the diameter of the cylindrical cavity and the diameter of the stirring shaft, unlike in Example 2, the tongue plate is turned outwards, and the fixed tongue plate area is 0.0031m². 2 The bottom area of ​​the cylindrical cavity is 0.0113 m². 2 0.27 times; Fixed structure: Four Φ10mm fixing holes are opened on the tongue plate, which are rigidly connected to the bottom support flange of the vessel by M10 high-strength bolts, eliminating the need for additional brackets and simplifying the assembly process.

[0057] (6) Installation process Coaxial positioning: The gas distributor is coaxially mounted directly above the bottom bearing (Φ100mm bearing bush) and directly below the BT-6 agitator. The distance between the upper edge of the distributor and the lower edge of the agitator blade is set to 200mm to ensure that the gas-liquid flow can directly enter the shearing zone of the agitator blade. Inlet pipe fixing: The end of the inlet pipe away from the cavity extends out of the side wall of the reactor and is connected to the bottom wall of the reactor by two L-shaped fixing brackets (made of 316L stainless steel). The brackets are fixed to the bottom wall by welding to avoid pipe vibration during air intake.

[0058] (7) Operational effect Gas-liquid dispersion performance: 12 Nm 3 After hydrogen is introduced at a constant rate, butynediol solution is drawn in from the inlet and dispersed three times: tangential mixing, dispersion tooth shearing, and BT-6 stirring paddle. This ensures that hydrogen is uniformly dispersed and reacts efficiently in the liquid. Reaction parameters: The single-pass reaction rate of 1,4-butanediol is increased by 5%~8% compared with the traditional bubble ring distributor; Residue and maintenance: After shutdown, the liquid in the distributor can be completely discharged through the inlet, with no catalyst deposition or liquid residue; the number of equipment maintenance is reduced by 50%; meeting the low energy consumption requirements of chemical production.

[0059] This document uses specific embodiments to illustrate the principles and implementation methods of this utility model. The descriptions of these embodiments are merely for the purpose of helping to understand the method and core ideas of this utility model. It should be noted that those skilled in the art can make various improvements and modifications to this utility model without departing from its principles, and these improvements and modifications also fall within the protection scope of the claims of this utility model. Therefore, the protection scope of this utility model patent should be determined by the appended claims.

Claims

1. A gas distributor coupled to a bottom bearing of a vessel, characterized in that, The system includes a cylindrical cavity (10), an air inlet pipe (11), dispersion teeth (9), a liquid inlet (3), and a gas-liquid outlet (15). The cylindrical cavity (10), dispersion teeth (9), gas-liquid outlet (15), and liquid inlet (3) are integrated into one structure. The gas-liquid outlet (15) is located at the top of the cylindrical cavity (10), the dispersion teeth (9) are located at the upper edge of the cylindrical cavity (10), the air inlet pipe (11) is connected to the side of the cylindrical cavity (10), and the connection between the air inlet pipe (11) and the cylindrical cavity (10) is a spiral tubular structure, through which gas passes. The tubular structure enters the side of the cylindrical cavity (10) tangentially; the liquid inlet (3) is located at the bottom and lower side of the cylindrical cavity (10), so that the liquid is drawn in from the bottom; a fixed tongue plate (12) extends locally from the bottom of the cylindrical cavity (10), and a bottom bearing is fixedly connected to the fixed tongue plate (12). A stirring shaft (8) is installed in the bottom bearing, and the stirring shaft (8) passes through the cylindrical cavity (10); the stirring shaft (8) is connected to a radial flow stirrer, and the bottom bearing, gas distributor, and radial flow stirrer are arranged in sequence from bottom to top in the reactor.

2. The gas distributor according to claim 1, characterized in that, The inlet pipe (11) has a spiral tube structure at one end near the cylindrical cavity (10), and a round tube at the other end that extends to the outside of the container wall of the reactor. Gas enters the cylindrical cavity (10) spirally and tangentially from the side of the cylindrical cavity (10) through the inlet pipe (11). The large volume flow of gas rotates at high speed in the cylindrical cavity (10) and forms a negative pressure state at the axis, attracting the small volume flow of liquid to enter the cylindrical cavity (10) from the bottom liquid inlet (3). The gas and liquid two-phase fluid undergoes tangential mixing and dispersion in the cylindrical cavity (10), guiding the gas and liquid two-phase fluid to be sprayed upward from the gas and liquid outlet (15). The dispersion teeth (9) perform secondary shearing on the gas and liquid flow, breaking the bubbles into smaller particles. Then the gas and liquid flow enters directly below the radial flow stirrer, and completes the three-stage dispersion through the radial shearing force of the radial flow stirrer.

3. The gas distributor according to claim 1, characterized in that, The bottom bearing includes a sleeve (6), a bearing shell (5) sleeved on the outside of the sleeve (6), and a base (4) sleeved on the outside of the bearing shell (5). The stirring shaft (8) is installed inside the sleeve (6). A pressure plate (7) is fixedly connected above the bearing shell (5) and the sleeve (6). A support flange (2) is provided on the outside of the base (4). One side of the base (4) is connected to the support flange (2) and the fixing tongue plate (12) by bolts (13) and nuts (14).

4. The gas distributor according to claim 1, characterized in that, The dispersing teeth (9) are arranged circumferentially along the upper edge of the cylindrical cavity (10). The dispersing teeth (9) are inclined towards the stirring shaft (8) with an inclination angle of 30º~60º. The length of the dispersing teeth (9) is 0.05~0.3 times the diameter of the cylindrical cavity (10), and the ratio of the width of the dispersing teeth (9) to the tooth spacing is 0.25~0.

8.

5. The gas distributor according to claim 1, characterized in that, The air intake direction of the air intake pipe (11) is the same as the rotation direction of the radial flow agitator. The ratio of the cross-sectional area of ​​the air inlet of the air intake pipe (11) to that of the gas-liquid outlet (15) is 0.3 to 2.

0. The ratio of the cross-sectional area of ​​the liquid inlet (3) to that of the air inlet of the air intake pipe (11) is 0.05 to 0.

3. The height-to-diameter ratio of the cylindrical cavity (10) is 1.0 to 4.

0.

6. The gas distributor according to claim 2, characterized in that, The ratio of the distance between the axis of the intake pipe (11) and the lower end face of the cylindrical cavity (10) to the height of the cylindrical cavity (10) is 0.1 to 0.

5.

7. The gas distributor according to claim 1, characterized in that, The fixed tongue plate (12) and the cylindrical cavity (10) are an integral structure or welded together. The ratio of the area of ​​the fixed tongue plate (12) to the bottom area of ​​the cylindrical cavity (10) is 0.1~0.

3.

8. The gas distributor according to claim 3, characterized in that, The air inlet pipe (11) is connected to the inner bottom wall of the reactor by at least one fixed bracket; a support foot (1) is installed below the support flange (2), and the lower edge of the liquid inlet (3) is flush with the upper end face of the support flange (2).

9. The gas distributor according to any one of claims 1-8, characterized in that, The cylindrical cavity (10) adopts an integral structure; or adopts a split structure, wherein one side adopts a fixed structure and the other side adopts a detachable structure.

10. The gas distributor according to any one of claims 1-8, characterized in that, The liquid inlet (3) is arch-shaped or square-shaped, and there are 2 to 8 in number.

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