A large-flux gas-liquid heterogeneous reaction mixing heat exchange stirring device

Abstract

The application provides a large-flux gas-liquid heterogeneous reaction mixing heat exchange stirring equipment, and relates to the technical field of stirring equipment, which comprises a kettle body and a stirring shaft, the inner wall of the middle part of the kettle body is provided with a vertical upper baffle, a flow guide cylinder, a dispersion disc and a gas distributor are coaxially arranged from top to bottom below the vertical upper baffle, the flow guide cylinder is arranged at the axial position of the kettle body, a group of down-pressure stirrers are arranged above and below the flow guide cylinder respectively, a heat exchange assembly is arranged on the outer periphery of the flow guide cylinder, the inner side of the heat exchange assembly is connected with the outer wall of the flow guide cylinder, the outer side of the heat exchange assembly is connected with the inner wall of the kettle body, a vertical lower baffle connected with the inner wall of the kettle body is arranged below the heat exchange assembly, and the inner wall of the kettle body below the heat exchange assembly is further provided with an annular baffle. The application provides forced flow in the axial direction downward through the down-pressure stirrers, forms shear flow through the dispersion disc, forms vertical upward flow under the action of the lower head, the annular baffle and the vertical lower baffle, and reduces flow loss in front of the pipe.

Description

Technical Field

[0001] This application relates to the field of stirring equipment technology, and more specifically, to a high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring equipment. Background Technology

[0002] Chemical reactions often involve exothermic processes, especially in reaction systems requiring high conversion rates. These systems release significant amounts of heat during the reaction; if heat is not removed promptly, it can lead to heat concentration, triggering side reactions or even explosions. Furthermore, in heterogeneous gas-liquid reactions, the mixing effect between the gas and liquid phases directly impacts the final reaction outcome. Sufficient contact between the gas and liquid phases is crucial, and the gas bubbles must be sufficiently small to maximize the total contact area, thereby increasing the reaction rate and achieving complete reaction, ensuring optimal results. To address the heat exchange problem in stirred reaction equipment, the following technical solutions exist: Chinese utility model patent with publication number CN222369055U discloses a high-efficiency heat exchange polymerization reactor, which is equipped with a propulsion blade at the bottom to realize the flow of materials, thereby increasing the material flow rate in the heat exchange tube.

[0003] However, this technical solution has the following problems: First, only a small portion of the total displacement of the propeller blades is used to transport materials upward from the material processing chamber, and the propeller blades, positioned at the head, cannot fully utilize their axial flow capability. Second, the flow velocity of the material inside the heat exchange tubes is low and uneven. This is because the rotation of the propeller blades causes the fluid to rotate as well, forming a significant vortex at the head and preventing it from rising, resulting in a low fluid velocity entering the heat exchange tubes and severely weakening the axial flow capability of the propeller blades. Third, the heat exchange tubes are too long, resulting in high flow resistance and extremely low flow velocities or even flow "dead zones" in some tubes, reducing the actual utilization rate of the heat exchange tubes. Fourth, the number of heat exchange tubes is too small, and the presence of only one propeller blade leads to insufficient stirring intensity, failing to effectively increase the flow velocity inside the heat exchange tubes and failing to meet the requirements for high-throughput heat removal. Fifth, this reactor is not suitable for situations involving gas and liquid phase reactions. The gas phase, introduced from the bottom, will escape rapidly upward from the material processing chamber, which is not conducive to thorough gas-liquid mixing.

[0004] Chinese invention patent CN116272686B discloses a mixed flow tubular fixed bed reactor, which increases the heat transfer coefficient outside the tubes through the shell-side structure, thereby removing the reaction heat inside the tubes. It is suitable for relatively slow and mild reaction modes.

[0005] However, this equipment cannot achieve rapid heat removal for high-throughput reaction heats, especially due to the low flow velocity within the tubes, which relies solely on inlet pump pressure. The overall heat transfer coefficient is limited by the convective heat transfer coefficient inside the tubes. More critically, the flow velocity within the heat exchange tubes is uneven, with some tubes exhibiting high velocities while others have excessively low velocities, even creating velocity "dead zones," thus failing to fully utilize the heat exchange capacity of these low-velocity tubes. Furthermore, the reactor design is unsuitable for heterogeneous gas-liquid reaction processes, limiting its application and hindering its widespread adoption.

[0006] In summary, existing stirred reaction equipment still suffers from several problems: some heat exchange tubes have low flow velocities, which prevent them from performing their heat exchange functions properly; the overall flow velocity inside the heat exchange tubes is low; flow "dead zones" and laminar flow phenomena are prone to occur; it is not suitable for heterogeneous gas-liquid mixing reactions; and it cannot achieve effective control of the flow field. Summary of the Invention

[0007] To address the aforementioned issues, this application employs a high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device, comprising a vessel body and a stirring shaft. A vertical upper baffle is installed on the inner wall of the middle part of the vessel body. Below the vertical upper baffle, a guide tube, a dispersion disk, and a gas distributor are coaxially arranged from top to bottom. The guide tube is located at the center of the vessel body. A set of downward-pressurized stirrers are installed above and below the guide tube. A heat exchange component is arranged around the outer periphery of the guide tube. The inner side of the heat exchange component is connected to the outer wall of the guide tube, and the outer side of the heat exchange component is connected to the inner wall of the vessel body. A vertical lower baffle connected to the inner wall of the vessel body is installed below the heat exchange component. An annular baffle is also installed on the inner wall of the vessel body below the heat exchange component.

[0008] Optionally, the stirring shaft is located at the axial center of the vessel body. The stirring shaft includes an upper stirring shaft and a lower stirring shaft. The upper stirring shaft is connected to a stirring shaft drive device, and the lower stirring shaft is connected to a bottom bearing. The bottom bearing is connected to the bottom of the vessel body. The upper stirring shaft and the lower stirring shaft are fixedly connected to each other by a rigid coupling. The stirring shaft drive device can adjust the speed of the stirring shaft.

[0009] Optionally, the pressure-type agitator is fixed to the outer wall of the agitator shaft, and a spiral guide plate is provided on the inner wall of the guide cylinder. There are 4 spiral guide plates, which are evenly distributed in a circumferential direction.

[0010] Optionally, a baffle plate is provided at the bottom of the guide tube, tilted outwards. The baffle plate is arranged around the guide tube, and the tilt direction of the baffle plate is 45° with the horizontal plane.

[0011] Optionally, the heat exchange assembly includes an annular fixed tube sheet, tie rods, heat exchange tubes, and an annular baffle plate. The fixed tube sheet is arranged around the guide tube, with its outer circumference fixed to the inner wall of the vessel and its inner circumference fixed to the outer wall of the guide tube. Both the upper and lower ends of the heat exchange tubes are fixedly connected to the fixed tube sheet. Multiple baffle plates are provided in the heat exchange assembly, with baffle plates on the outer wall of the guide tube and baffle plates on the inner wall of the vessel alternating, and the baffle plates are fixed together by tie rods.

[0012] Optionally, the axial direction of the heat exchange tubes is perpendicular to the horizontal plane, and the arrangement of the heat exchange tubes is such that the axes of three adjacent heat exchange tubes can be connected to form an equilateral triangle, with a total number of heat exchange tubes of 4500-6500.

[0013] Optionally, the diameter of the guide tube is larger than the diameter of the dispersion disk, and the diameter of the dispersion disk is larger than the diameter of the gas distributor.

[0014] Optionally, the pressure mixer is configured as a wide-blade mixer, with the ratio of blade width to blade length being 6:5, and each set of pressure mixers is provided with 4 blades evenly distributed circumferentially on the outer wall of the lower mixing shaft.

[0015] Optionally, the heat exchange assembly includes a shell-side inlet and a shell-side outlet. An upper baffle plate and a lower baffle plate, which are fixedly connected to the inner wall of the vessel, are respectively provided below the shell-side inlet and above the shell-side outlet. A middle baffle plate, which is fixedly connected to the outer wall of the guide tube, is provided between the upper baffle plate and the lower baffle plate. The circumferential width of the baffle plate is 0.85 times the circumferential width of the fixed tube plate.

[0016] Optionally, the annular baffle is positioned at the same height as the dispersion disk.

[0017] The beneficial effects of the high-throughput gas-liquid heterogeneous reaction mixing heat exchange stirring device provided in this application are as follows: (1) This application provides axial downward forced flow in the guide tube by a downward pressure agitator in the guide tube, and forms shear flow by a dispersion disk coaxially arranged with the guide tube to disperse the axial flow medium provided by the guide tube, which can avoid the strong axial flow medium directly impacting the bottom of the vessel and affecting the stability of the equipment. (2) The medium dispersed by the dispersion plate changes from axial flow to flow with both axial and radial properties. Under the action of the lower head, annular baffle and vertical lower baffle, it forms a vertical upward flow, which allows the stirred material to enter the heat exchange tube smoothly and reduces the flow loss in front of the heat exchange tube. (3) The vertical upper baffle prevents the fluid above the heat exchange tube from forming a large central vortex, thus preventing the solvent medium from becoming less effective. (4) After the gaseous medium enters the vessel through the gas distributor, it is sheared and dispersed into fine bubbles by the dispersion plate. It then encounters the liquid medium with strong axial flow above, increasing the residence time of the gas in the liquid phase. The mixture reacts fully here, releasing a large amount of heat of reaction. The reacted medium enters the heat exchange tube and exchanges heat with the heat exchange medium in the shell side through the tube wall. It is particularly suitable for heterogeneous gas-liquid high-efficiency mixing reactions, especially in applications where the reaction rate is fast and the amount of heat of reaction released is large. (5) The high-throughput gas-liquid heterogeneous reaction mixing heat exchange stirring equipment provided in this application increases the flow velocity in the heat exchange tube under the premise of meeting the power requirements. The average flow velocity in the heat exchange tube can reach 1.8 m / s, ensuring that the fluid flow in the heat exchange tube is in a turbulent state, thereby achieving the purpose of enhancing heat exchange. Attached Figure Description

[0018] To more clearly illustrate the technical solutions in the embodiments of this application, the accompanying drawings used in the description of the embodiments or the prior art will be briefly introduced below.

[0019] Figure 1 This is a schematic diagram of the structure of the high-throughput heat exchange stirring device provided in the embodiments of this application; Figure 2 This is a half-section axial side view of the high-throughput heat exchange stirring device provided in the embodiments of this application; Figure 3 This is a velocity distribution cloud map of the heat exchanger tube cross-section with a 1.5 m / s scale provided in the embodiments of this application; Figure 4 This is a velocity distribution cloud map of the heat exchanger tube cross-section with a scale of 2.0 m / s provided in the embodiments of this application; Figure 5 This is a velocity contour plot of the longitudinal section of the heat exchange tube provided in the embodiments of this application; Figure 6 This is a flow field trace diagram of the longitudinal section of the heat exchange tube provided in the embodiments of this application; Figure 7 This is a calculation diagram of the cross-sectional resultant velocity standard deviation and the y-direction velocity standard deviation provided in the embodiments of this application; Figure 8 This is the flow calculation page for the guide tube provided in the embodiments of this application; Figure 9 This is a schematic diagram of the heat exchanger tube layout structure provided in the embodiments of this application.

[0020] Explanation of reference numerals in the attached drawings: 1-Flanged connection flange; 2-Lower stirring shaft; 3-Bug body; 4-Rigid coupling; 5-Down-pressure agitator; 6-Vertical upper baffle; 7-Guide tube; 8-Guide tube baffle; 9-Helical guide plate; 10-Annular baffle; 11-Vertical lower baffle; 12-Dispersion disc; 13-Gas distributor; 14-Bottom bearing; 15-Upper stirring shaft; 16-Liquid level; 100-Heat exchange assembly; 101-Fixed tube sheet; 102-Tie rod; 103-Heat exchange tube; 104-Baffle tube sheet; A-Gas phase inlet; B1-Continuous liquid phase inlet; B2-Spray liquid phase inlet; C-Outlet; D1-Shell side inlet; D2-Shell side outlet; E-Drain port. Detailed Implementation

[0021] To make the technical problems, technical solutions, and beneficial effects to be solved by this application clearer, the following detailed description is provided in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative and are not intended to limit the scope of this application.

[0022] like Figures 1-2 As shown, this application provides a high-throughput gas-liquid heterogeneous reaction mixing heat exchange stirring device, including a vessel body 3 and a stirring shaft. A vertical upper baffle 6 is provided on the inner wall of the middle part of the vessel body 3. A guide tube 7, a dispersion disk 12 and a gas distributor 13 are arranged coaxially from top to bottom below the vertical upper baffle 6. The guide tube 7 is located at the center of the vessel body 3. A set of downward pressure stirrers 5 are respectively arranged above and below the guide tube 7. A heat exchange component 100 is arranged around the outer periphery of the guide tube 7. The inner side of the heat exchange component 100 is connected to the outer wall of the guide tube 7, and the outer side of the heat exchange component 100 is connected to the inner wall of the vessel body 3. A vertical lower baffle 11 connected to the inner wall of the vessel body 3 is provided below the heat exchange component 100. An annular baffle 10 is also provided on the inner wall of the vessel body 3 below the heat exchange component 100. The annular baffle 10 is disposed on the inner wall of the lower head of the vessel body 3, protruding into the interior of the vessel body 3. The upper and lower surfaces of the annular baffle 10 are respectively inclined to the inner wall of the lower head connected to the annular baffle 10.

[0023] The stirring shaft passes through the top of the vessel body 3 and enters the vessel body. From top to bottom, it is fixedly connected to the pressure-type stirrer 5 installed at the top of the guide tube 7, the pressure-type stirrer 5 installed at the bottom of the guide tube 7, and the dispersion plate 12.

[0024] The working principle of this embodiment is as follows: A stirring shaft drives three stirrers (two downward-pressure stirrers 5 and one dispersion disc 12) to rotate synchronously. The downward-pressure stirrers 5 create a downward forced circulation flow within the guide tube 7. The main function of the dispersion disc 12 is to create a strong shear flow, dispersing the strong axial flow medium provided by the guide tube 7, thus preventing the strong axial flow medium from directly impacting the bottom of the vessel and affecting equipment stability. The medium dispersed by the dispersion disc 12 changes from axial flow to a flow combining axial and radial directions, and then, under the combined action of the lower end cap, annular baffle 10, and vertical lower baffle 11, forms a vertically upward flow, allowing the stirred medium to smoothly enter the heat exchange assembly 100, effectively reducing flow losses of the stirred medium before entering the heat exchange assembly 100. Figure 1 As shown, the lower head of the vessel body 3 refers to the bottom of the vessel body below the cylindrical side wall of the vessel body 3, and the lower head of the vessel body 3 is semi-ellipsoidal.

[0025] The vertical upper baffle 6 can prevent the fluid above the heat exchange tube 103 from forming a large central vortex, thus preventing the mixing effect of the solvent medium introduced from above from deteriorating. Figure 1 The discontinuity line in the middle of the vessel body indicates the position of liquid level 16, and the curve with arrows indicates the general flow direction of the medium in the shell side within the heat exchange assembly 100.

[0026] The gas outlet of the gas distributor 13 faces downwards, providing an initial buffer for the gaseous medium entering the vessel 3. After entering through the gas inlet A, the gaseous medium first enters the vessel 3 through the gas outlet of the gas distributor 13, and is then sheared and dispersed into fine bubbles by the high-speed rotating dispersion disk 12. These bubbles encounter the strongly axially flowing solvent above, where they undergo a thorough mixing reaction, releasing a large amount of heat. The reacted medium then enters the heat exchange tube 103 and exchanges heat with the shell-side medium through the tube wall. The shell-side medium enters through the shell-side inlet D1 and exits through the shell-side outlet D2, carrying away the heat. The medium leaving the heat exchange tube 103 is re-entrained into the guide tube 7 by the downward-pressure agitator 5, forming a strongly axial flow. This process is repeated to complete a high-cycle heat exchange process. The solvent enters through the continuous liquid inlet B1 for continuous replenishment, and the upper spray liquid inlet B2 is also used to introduce solvent, allowing it to enter the vessel 3 in a spray state. The final product floats to the surface due to its density and is discharged through the outlet C. Drain port E is used to completely drain the medium inside the vessel.

[0027] "Fluidity" refers to the amount of matter that a device or process can process, transmit, pass through, or generate per unit time. In this application, "flux" refers to the liquid and gaseous mixed medium passing through the heat exchange tube per unit time. "High flux" means that the gas-liquid heterogeneous reaction mixing heat exchange stirring equipment provided in this application is applicable to 25-60m. 3 Reactor, and suitable for 25m 3When in a reaction vessel, the reaction medium is circulated more than 15 times per minute.

[0028] like Figure 2 As shown, the annular baffle 10, the vertical lower baffle 11, and the guide tube baffle 8 are used to reduce stirring power consumption, increase the flow velocity within the heat exchange tube 103 to meet turbulence requirements, and ensure that the flow velocity in all heat exchange tubes 103 is relatively uniform, preventing large velocity gradients. When large velocity gradients occur, such as higher flow velocities in the heat exchange tubes 103 at the center and lower flow velocities in the heat exchange tubes 103 at the edges, or even the appearance of velocity "dead zones," the heat exchange effect will be affected, reducing the effective utilization rate of the heat exchange tubes 103.

[0029] In this embodiment, the number of heat exchange tubes is 5500, and Figures 3-7 All simulation results are based on this condition.

[0030] like Figures 3-6 As shown, the medium flows at high speed inside the heat exchange tube 103, with an overall average flow velocity of The Reynolds number is calculated under the conditions of flow velocity, pipe diameter, and physical properties, which is approximately 1.77 m / s or higher. In this embodiment, the hydrodynamic viscosity of the liquid fluid medium inside the vessel 3 is... It is 0.4 cp, density It is 1124 kg / m 3 Single-channel inner diameter The value is 34 mm. Substitute the above physical quantities into the Reynolds number calculation formula. The calculated Reynolds number Re = 169105, which is far above the definition benchmark for turbulence (Reynolds number 4000) and falls within the standard turbulence range. In the field of heat transfer, turbulence can effectively enhance the ability of convective heat transfer.

[0031] like Figures 3-4 As shown, the high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring equipment provided in this application can increase the proportion of heat exchange tubes 103 with flow velocities higher than 1 m / s to 98% of the total number of heat exchange tubes 103, and the proportion of heat exchange tubes 103 with flow velocities higher than 1.5 m / s to over 85% of the total number of heat exchange tubes 103. This fully utilizes the heat exchange capacity of each heat exchange tube 103, greatly improves the effective utilization rate of the heat exchange tubes 103, and effectively saves equipment costs. Figure 3 and Figure 4 The cross-section is the cross-section taken at the midpoint along the length of the heat exchange tube.

[0032] To evaluate the degree of fluctuation in the velocity distribution among the heat exchange tubes 103, the standard deviation of the velocity in each heat exchange tube 103 is calculated. A smaller standard deviation indicates a higher uniformity of velocity within the heat exchange tube 103. In this embodiment, the standard deviation values ​​of the three cross-sections of the heat exchange tube 103 are directly derived using CFD. The software data export method is described in [link to software documentation]. Figure 7 .exist Figure 7 Below are the standard deviation values. Each set of data, from top to bottom, represents data at three locations: 0.1m, 0.7m, and 1.7m above the lower inlet of heat exchanger tube 103. The top set of data represents the standard deviation of the resultant velocity, and the bottom set represents the standard deviation of the velocity component in the y-direction. It can be seen that the standard deviations of the resultant velocity at the three locations above the lower inlet of heat exchanger tube 103 are 0.6791, 0.4659, and 0.4670, respectively; and the standard deviations of the y-direction velocity at the same locations are 0.6803, 0.4659, and 0.4670, respectively. The standard deviations are all within the range of 0.45 to 0.7, which meets the requirements for reaction uniformity. The positive y-direction refers to the direction vertically upward from the horizontal plane.

[0033] To evaluate the mixing efficiency of the high-throughput gas-liquid heterogeneous reaction mixing heat exchanger provided in the embodiments of this application, the fluid flow rate through the heat exchanger tubes is calculated.

[0034] like Figure 8 As shown, the flow rate is calculated based on guide tube 7. Figure 8 The medium gray section represents half of the cross-section of guide tube 7. The average flow velocity inside guide tube 7 is 2.867 m / s, and half of the cross-sectional area of ​​guide tube 7 is 1.5517 m². 2 According to the formula: mass flow rate = average flow velocity × total area × density, 2.867 × (1.5517 × 2) × 1124 = 10000.73 kg / s. With a total material volume of 25 cubic meters, it can circulate 21.35 times per minute.

[0035] The flow rate was calculated using the heat exchanger tubes. The inlet velocity was 1.93722 m / s, the total number of tubes was 5500, and the total area was 4.99 m². 2 Therefore, the calculated total volumetric flow rate is: 9.74 m³ / s. 3 / s, converted to mass flow rate (density 1124kg / m³) 3 With a total material volume of 25 cubic meters, the flow rate is 10865 kg / s, and the cycle time is 23.20 times per minute.

[0036] Under turbulent conditions, the flow of the circulating medium inside the actual vessel 3 is extremely complex. In the simulation, there is a deviation between the flow velocity inside the heat exchange tube 103 and the flow velocity at the inlet of the heat exchange tube 103. In addition, there are backflow situations in the guide tube 7 and the heat exchange tube 103. Therefore, it is normal for the flow rate calculated based on the guide tube 7 to deviate from the flow rate calculated through the heat exchange tube 103. The above calculation is only an example to demonstrate the circulation capacity of the high-throughput gas-liquid heterogeneous reaction mixing heat exchange stirring equipment provided in this application.

[0037] Since the density difference between gaseous and liquid media is 2-3 orders of magnitude, the above calculations and simulations are based on the liquid phase, but they can still provide a reference for the case of gas-liquid mixing.

[0038] In another embodiment of this application, the stirring shaft is located at the axial center of the vessel body 3. The stirring shaft includes an upper stirring shaft 15 and a lower stirring shaft 2. The upper stirring shaft 15 is connected to a stirring shaft transmission device, and the lower stirring shaft 2 is connected to a bottom bearing 14. The bottom bearing 14 is connected to the bottom of the vessel body 3. The upper stirring shaft 15 and the lower stirring shaft 2 are fixedly connected to each other by a rigid coupling 4. The stirring shaft transmission device can adjust the rotational speed of the stirring shaft.

[0039] As a feasible implementation method, the actual adjustment of the rotational speed is based on the following flow field control method: The total heat exchange capacity Q can be determined from the temperature and flow rate parameters of the shell-side inlet D1 and shell-side outlet D2. To adjust the Q value and control the temperature inside the vessel 3, the stirring speed can be adjusted. Specifically, CFD simulation calculations determine that the average flow velocity of the total heat exchange tubes is higher than 1.5 m / s, at which point the stirring speed is N1 rpm. Similarly, CFD simulation calculations determine that the average flow velocity of the total heat exchange tubes is higher than 1.8 m / s, at which point the stirring speed is N2 rpm. The calculated stirring power is within a reasonable range. The average flow velocity and stirring power of the heat exchange tube 103 are calculated every 5 rpm for N1 and N2, forming a relationship table between stirring speed, stirring power, and average flow velocity of the heat exchange tubes. By adjusting the stirring speed, the average flow velocity inside the heat exchange tube 103 is changed, thus changing the total heat exchange capacity. If the heat exchange capacity is too large and the water temperature at the shell-side outlet D2 is too low, the stirring speed can be reduced to decrease the average flow velocity of the heat exchange tube 103 and reduce the heat exchange capacity, and vice versa.

[0040] The upper stirring shaft 15 and the lower stirring shaft 2 are connected by a rigid coupling 4, which avoids excessive stirring shaft deflection caused by an excessively long single stirring shaft and improves the stability of the transmission. The bottom bearing 14 is set at the bottom of the lower stirring shaft 2 to further enhance the stability of the stirring shaft transmission. The power of the upper stirring shaft 15 comes from the transmission device, and the outer shell of the transmission device is fixed to the flange connecting flange 1.

[0041] In another embodiment of this application, such as Figure 1 As shown, the pressure mixer 5 is fixed to the outer wall of the lower mixing shaft 2, and the inner wall of the guide tube 7 is provided with a spiral guide plate 9. There are 4 spiral guide plates 9, which are evenly distributed in the circumference.

[0042] The guide tube 7 and the downward-pressure agitator 5 work together to form a strong forced flow inside the guide tube 7. The inner wall of the guide tube 7 is provided with four spiral guide plates 9, which guide the fluid to flow downward axially and reduce the upward backflow phenomenon inside the guide tube 7.

[0043] In another embodiment of this application, such as Figures 1-2 As shown, a baffle plate 8 is inclined outward from the bottom of the guide tube 7. The baffle plate 8 is arranged around the guide tube 7, and the inclination direction of the baffle plate 8 is 45° with the horizontal plane.

[0044] like Figure 2 As shown, the flow guide tube 7 is connected to the flow guide tube baffle 8. The flow guide tube baffle 8 is arranged in a ring at a 45° angle to the horizontal direction. This structure is used to solve the problem of uneven flow velocity in each heat exchange tube 103. The structure of the flow guide tube baffle 8 can effectively guide the fluid to flow in the set direction.

[0045] In another embodiment of this application, such as Figure 1 As shown, the heat exchange assembly 100 includes an annular fixed tube sheet 101, a tie rod 102, a heat exchange tube 103, and an annular baffle plate 104. The fixed tube sheet 101 is arranged around the guide tube 7. The outer circumference of the fixed tube sheet 101 is fixed to the inner wall of the vessel body 3, and the inner circumference of the fixed tube sheet 101 is fixed to the outer wall of the guide tube 7. The fixed tube sheet 101 is provided with a circular hole that matches the inner diameter of the heat exchange tube 103. Both the upper and lower ends of the heat exchange tube 103 are fixedly connected to the fixed tube sheet 101. The internal space of the heat exchange tube 103 is aligned with the circular hole on the fixed tube sheet 101, so that the heat exchange tube 103 is open from top to bottom after being fixed, allowing the fluid below the heat exchange tube bundle to pass through the heat exchange tube 103 and reach the top of the heat exchange tube bundle. The heat exchange assembly 100 is provided with multiple baffle plates 104. The baffle plates 104 on the outer wall of the guide tube 7 and the baffle plates 104 on the inner wall of the vessel body 3 are alternately distributed, and the baffle plates 104 are fixed together by tie rods 102.

[0046] The heat exchange assembly 100 includes a fixed tube sheet 101, a tie rod 102, heat exchange tubes 103, and a baffle tube sheet 104. The fixed tube sheet 101 is used to fix the heat exchange tubes. Since there are a large number of heat exchange tubes 103, up to 5,500, the use of two fixed tube sheets 101 can effectively fix a large number of heat exchange tubes 103 and prevent the heat exchange tubes 103 from moving axially.

[0047] The baffle plate 104 serves to both fix the heat exchange tube 103 and deflect the flow. Since the heat exchange tube 103 is relatively long, when the shell-side medium enters the heat exchange tube 103, it impacts the heat exchange tube 103 and causes radial vibration. Using the baffle plate 104 can reduce the radial vibration of the heat exchange tube 103.

[0048] The main function of the tie rod 102 is to effectively fix the baffle plate 104. Since the baffle plate 104 is subject to the impact of the shell-side fluid, the tie rod 102 can effectively enhance the stability of the baffle plate 104.

[0049] In another embodiment of this application, such as Figure 1 , Figure 2 and Figure 9 As shown, the axial direction of the heat exchange tube 103 is perpendicular to the horizontal plane. The arrangement of the heat exchange tubes 103 is such that the axes of three adjacent heat exchange tubes 103 can be connected to form an equilateral triangle. The total number of heat exchange tubes is 4500-6500.

[0050] like Figure 1 , Figure 2 and Figure 9 As shown, the heat exchange tubes 103 are arranged vertically, connected to the fixed tube sheet 101 at both ends. The total number of heat exchange tubes is 4500-6500, and the spacing between adjacent heat exchange tubes is equal. Any three adjacent heat exchange tubes 103 form a standard equilateral triangle structure. This structure allows the heat exchange tubes 103 to better receive the incoming fluid, thereby enhancing the heat exchange effect. The large number of heat exchange tubes 103 increases the contact area between the fluid and the heat exchange tubes 103, achieving high-throughput heat exchange and increasing the upper limit of the equipment's heat exchange capacity.

[0051] Table 1 shows the performance differences between high-throughput gas-liquid heterogeneous reaction mixing heat exchange and stirring equipment with different numbers of heat exchange tubes: Table 1 Performance of mixing and stirring equipment with different numbers of heat exchange tubes

[0052] The simulation calculations in Table 1 are based on the following conditions: the vessel body 3 has a diameter of 25m. 3 The reaction vessel (referring to the vessel body 3 with a mixing medium volume of 25m³) 3 The heat exchange tubes 103 of each group of equipment have the same diameter and the same arrangement. The spacing between adjacent heat exchange tubes 103 is equal. The change in the number of heat exchange tubes 103 only causes a change in the inner diameter of the guide tube 7, without changing the structure or size of the pressure stirrer 5, the lower stirring shaft 2, the vessel body 3, etc. Since the inner diameter of the guide tube 7 changes, but the size and structure of the pressure stirrer 5 do not change, the spacing between the blades of the pressure stirrer 5 and the inner wall of the guide tube 7 changes accordingly.

[0053] The average velocity in Table 1 is the average velocity inside the heat exchange tubes. As can be seen from Table 1, as the number of heat exchange tubes 103 decreases, the fluid flowing through the heat exchange tubes 103 decreases, and the backflow in the guide tube 7 increases. Although the flow velocity increases slightly, the overall circulation capacity weakens. If the number of heat exchange tubes 103 is too large, the intermediate guide tube becomes smaller, the fluid flowing through decreases, and the number of circulations also decreases.

[0054] In another embodiment of this application, such as Figure 1 and Figure 2 As shown, the diameter of the guide tube 7 is larger than the diameter of the dispersion disk 12, and the diameter of the dispersion disk 12 is larger than the diameter of the gas distributor 13.

[0055] The gaseous medium introduced into the vessel by the gas distributor 13 naturally moves upward under the action of density difference. The diameter of the dispersion disk 12 is larger than the diameter of the gas distributor 13, so that the gaseous medium can be fully affected by the dispersion of the dispersion disk 12. The liquid medium conveyed downward by the guide tube 7 can be directly or indirectly affected by the dispersion of the dispersion disk 12. The diameter of the guide tube 7 is larger than the diameter of the dispersion disk 12, so that the dispersion disk mainly acts on the liquid medium at the axis of the guide tube. The flow velocity distribution in the guide tube 7 is that the flow velocity is higher at the axis and the flow velocity of the liquid phase at the edge is lower. After the liquid phase at the edge is dispersed, it is easy to form local stagnation, which reduces the overall flow efficiency. Therefore, the diameter of the guide tube 7 is larger than the diameter of the dispersion disk 12 to prevent the liquid phase at the edge from being excessively dispersed.

[0056] In another embodiment of this application, such as Figure 1 As shown, the down-pressure agitator 5 is configured as a wide-blade agitator, with a blade width to blade length ratio of 6:5. Each set of down-pressure agitators 5 has four blades evenly distributed circumferentially on the outer wall of the down-pressure agitator 2. The down-pressure wide-blade agitator has strong axial flow capability and a large axial displacement, enabling it to form a strong axial flow and create high-speed forced circulation within the guide tube 7.

[0057] In another embodiment of this application, such as Figure 1 As shown, the heat exchange assembly 100 includes a shell-side inlet D1 and a shell-side outlet D2. An upper baffle plate and a lower baffle plate, which are fixedly connected to the inner wall of the vessel body 3, are respectively provided below the shell-side inlet D1 and above the shell-side outlet D2. A middle baffle plate, which is fixedly connected to the outer wall of the guide tube 7, is provided between the upper baffle plate and the lower baffle plate. The circumferential width of the baffle plate 104 is 0.85 times the circumferential width of the fixed tube plate 101.

[0058] like Figure 1 As shown, the baffle plate 104 can guide the shell-side fluid to form a longer flow channel. Using a three-baffle plate can create… Figure 1The indicated fluid flow pattern enhances heat exchange capacity. The width of the baffle plate is 0.85 times the width of the fixed tube sheet. If the width is too small, the flow path will be too short, resulting in poor heat exchange. If the width is too large, the flow resistance will be too large, forming obvious flow "dead zones" at the corners of the baffle plate.

[0059] In another embodiment of this application, the annular baffle 10 is at the same height as the dispersion disk 12. For example... Figure 1 , Figure 5 and Figure 6 As shown in the figure, the effect of this position and structure can be seen in CFD simulation. The annular baffle 10 can guide the flow direction of the fluid, so that the fluid flows in a vertically upward direction. The fluid can directly enter the heat exchange tube 103. After passing through the heat exchange tube 103, it is drawn into the guide tube 7 by the first layer of downward pressure agitator 5 above, completing the circulation flow. The arc-shaped structure adopted by the annular baffle 10 can effectively reduce the flow loss and achieve the purpose of guiding the fluid flow.

[0060] The above embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of this application, and should all be included within the protection scope of this application.

Claims

1. A high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device, comprising a vessel and a stirring shaft, characterized in that: A vertical upper baffle is provided on the inner wall of the middle part of the vessel body. Below the vertical upper baffle, a guide tube, a dispersion plate, and a gas distributor are arranged coaxially from top to bottom. The guide tube is located at the center of the vessel body. A set of downward pressure agitators are respectively arranged above and below the guide tube. A heat exchange assembly is arranged around the outer periphery of the guide tube. The inner side of the heat exchange assembly is connected to the outer wall of the guide tube, and the outer side of the heat exchange assembly is connected to the inner wall of the vessel body. A vertical lower baffle connected to the inner wall of the vessel body is provided below the heat exchange assembly. An annular baffle is also provided on the inner wall of the vessel body below the heat exchange assembly.

2. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 1, characterized in that: The stirring shaft is located at the axial center of the vessel body. The stirring shaft includes an upper stirring shaft and a lower stirring shaft. The upper stirring shaft is connected to a stirring shaft drive device, and the lower stirring shaft is connected to a bottom bearing. The bottom bearing is connected to the bottom of the vessel body. The upper stirring shaft and the lower stirring shaft are fixedly connected to each other by a rigid coupling. The stirring shaft drive device can adjust the rotational speed of the stirring shaft.

3. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 1, characterized in that: The downward-pressurized agitator is fixed to the outer wall of the agitator shaft, and the inner wall of the guide tube is provided with a spiral guide plate. There are 4 spiral guide plates, which are evenly distributed in a circumferential direction.

4. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 1, characterized in that: The bottom of the guide tube is inclined outwards and a guide tube baffle is provided. The guide tube baffle is arranged around the guide tube and the inclination direction of the guide tube baffle is 45° with the horizontal plane.

5. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 3, characterized in that: The heat exchange assembly includes an annular fixed tube sheet, a tie rod, heat exchange tubes, and an annular baffle plate. The fixed tube sheet is arranged around the flow guide tube, with its outer circumference fixed to the inner wall of the vessel body and its inner circumference fixed to the outer wall of the flow guide tube. Both the upper and lower ends of the heat exchange tubes are fixedly connected to the fixed tube sheet. The heat exchange assembly contains multiple baffle plates, with baffle plates on the outer wall of the flow guide tube and baffle plates on the inner wall of the vessel body alternating in distribution, and the baffle plates are fixed together by the tie rod.

6. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 5, characterized in that: The axial direction of the heat exchange tubes is perpendicular to the horizontal plane. The arrangement of the heat exchange tubes is such that the axes of three adjacent heat exchange tubes can be connected to form an equilateral triangle. The total number of heat exchange tubes is 4500-6500.

7. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 2, characterized in that: The diameter of the guide tube is larger than the diameter of the dispersion disk, and the diameter of the dispersion disk is larger than the diameter of the gas distributor.

8. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 1, characterized in that: The pressure mixer is configured as a wide-blade mixer, and the ratio of the blade width to the blade length of the pressure mixer is 6:

5. Each set of pressure mixers is provided with 4 blades evenly distributed circumferentially on the outer wall of the lower mixing shaft.

9. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 5, characterized in that: The heat exchange assembly includes a shell-side inlet and a shell-side outlet. An upper baffle plate and a lower baffle plate, which are fixedly connected to the inner wall of the vessel, are respectively provided below the shell-side inlet and above the shell-side outlet. A middle baffle plate, which is fixedly connected to the outer wall of the guide tube, is provided between the upper baffle plate and the lower baffle plate. The circumferential width of the baffle plate is 0.85 times the circumferential width of the fixed tube plate.

10. The high-throughput gas-liquid heterogeneous reaction mixing and heat exchange stirring device according to claim 1, characterized in that: The annular baffle plate is at the same height as the dispersion disk.

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