An improved gas-liquid reactor

Abstract

This utility model relates to an improved gas-liquid reactor, comprising a first feed section, a second feed section, a reaction section, and a discharge section arranged sequentially from top to bottom. An upper tube sheet isolates the first and second feed sections, a middle tube sheet isolates the second feed section and the reaction section, and a lower tube sheet isolates the reaction section and the discharge section. The reaction section contains several reaction tubes, each with its top end passing through the middle tube sheet and its bottom end penetrating the lower tube sheet. A limiting unit is provided at the bottom end of each reaction tube. The second feed section contains several distribution tubes, each with its top end passing through the upper tube sheet and its lower section extending into the reaction tubes to form an insertion section. Through holes are distributed on the wall of the insertion section. Compared with the prior art, this utility model has advantages such as improved gas-liquid mixing uniformity, full-process heat exchange control during gas-liquid mixing, and improved reaction safety and product selectivity.

Description

Technical Field

[0001] This utility model relates to the field of chemical reaction equipment technology, and in particular to an improved gas-liquid reactor. Background Technology

[0002] In many fields such as chemical engineering, pharmaceuticals, and energy, chemical reactions often involve two-phase or three-phase reactions, including gas-liquid reactions, and are strongly exothermic, such as ozonation, hydrogenation, and chlorination. These reactions not only require strict temperature control but are also highly sensitive to the composition ratio of the gas and liquid phases. For example, a slight excess of chlorine solution in a chlorination reaction can produce dichloro impurities, while substances such as ozone and diazomethane decompose significantly faster under high pressure.

[0003] Traditional methods for handling highly exothermic multiphase reactions primarily employ batch reactors, which suffer from numerous technical limitations. Inhomogeneous gas-liquid mixing leads to significant localized concentration variations in reactants, resulting in inconsistent reaction progress and a substantial reduction in conversion and yield. Furthermore, traditional gas-liquid mixing reactors have limited heat exchange coverage, making precise temperature control difficult for vigorous and highly exothermic gas-liquid reactions. Failure to promptly remove reaction heat can cause excessively high localized temperatures, increasing side reactions, affecting reaction rates and product selectivity, and posing serious safety hazards.

[0004] Microreactor technology, due to its excellent mixing and heat exchange capabilities, has been considered for application in strongly exothermic heterogeneous reactions. However, its small channel size and limited equipment volume result in low equipment capacity and large system pressure drop, making commercial production difficult. For example, prior art CN116037006 discloses a tubular gas-liquid homogeneous reactor for gas-liquid or gas-liquid-solid reactions such as hydrogenation and oxidation. The designed gas and liquid distributors ensure uniform distribution of the gas and liquid phases in each tube, and the reaction section includes heat removal technology. This equipment can react at low or atmospheric pressure, facilitating commercial mass production. However, this design lacks a heat removal feature in the gas-liquid mixing section. For many fast gas-liquid reactions, the initial mixing stage is the fastest, releasing a large amount of heat. If this heat is not removed in time, it may cause a rapid temperature rise, leading to material decomposition or reduced product selectivity. Utility Model Content

[0005] The purpose of this invention is to overcome the defects of the prior art by providing an improved gas-liquid reactor, which improves the uniformity of gas-liquid mixing, controls the heat exchange throughout the gas-liquid mixing process, and enhances reaction safety and product selectivity.

[0006] The objective of this utility model can be achieved through the following technical solutions:

[0007] An improved gas-liquid reactor includes a first feed section, a second feed section, a reaction section, and a discharge section arranged sequentially from top to bottom. An upper tube sheet is provided between the first feed section and the second feed section for isolation, a middle tube sheet is provided between the second feed section and the reaction section for isolation, and a lower tube sheet is provided between the reaction section and the discharge section for isolation.

[0008] The reaction section is provided with several reaction tubes. The top end of each reaction tube passes through the middle tube plate, and the bottom end of the reaction tube passes through the lower tube plate. The bottom end of the reaction tube is provided with a limiting unit.

[0009] The second feed section is provided with several distribution pipes. The top end of the distribution pipe passes through the upper tube sheet, and the lower section of the distribution pipe extends into the reaction tube to form an extension section. The extension section has through holes distributed on its pipe wall.

[0010] The reaction section is provided with a heat exchange medium inlet and a heat exchange medium outlet, and the heat exchange medium fills the entire reaction section and surrounds the reaction tubes.

[0011] Furthermore, the gap between the outer diameter of the distribution tube and the inner diameter of the extended reaction tube is 1 to 10 mm.

[0012] Furthermore, when the distribution pipe is a circular pipe, the outer diameter of the circular pipe is 8-30 mm and the wall thickness is 1-5 mm. The outer diameter of the single pipe in the reaction section of the corresponding reactor can be selected as 10-50 mm and the wall thickness as 1-5 mm.

[0013] Furthermore, when the distribution tube is a rectangular tube, the outer dimensions of the rectangular tube are 5-100 mm wide, 3-20 mm high, and 1-5 mm thick. More preferably, the outer dimensions are 10-50 mm wide, 3-10 mm high, and 1-5 mm thick. The corresponding reaction tubes are also rectangular tubes, with inner dimensions of 8-120 mm wide, 5-25 mm high, and 1-5 mm thick. More preferably, the inner dimensions are 14-60 mm wide, 5-15 mm high, and 1-5 mm thick.

[0014] Furthermore, the bottom end of the distribution tube is flush with the bottom end of the reaction tube.

[0015] Furthermore, the reaction tubes are filled with a catalyst or packing material. Even further, the packing material is made of metal.

[0016] Furthermore, a heat exchange medium is provided outside the reaction section tube to exchange heat with the reactants; at the same time, fins are provided on the outer wall of the reaction tubes inside the reaction section to increase the turbulence on the medium side and improve the heat transfer coefficient on the medium side.

[0017] Furthermore, the distribution pipe includes a first branch pipe and a second branch pipe that are interconnected or integrally formed. The second branch pipe may be a silicon carbide pipe, graphite pipe, cast iron pipe, stainless steel pipe, Hastelloy pipe, titanium pipe, titanium alloy, nickel alloy pipe, tantalum pipe or zirconium pipe. The second branch pipe is an extension section and has through holes distributed thereon.

[0018] Furthermore, the diameter of the through hole is 500um to 2mm.

[0019] Furthermore, the limiting unit is a supporting sieve plate, which is disposed within the discharge section to support the reaction tubes.

[0020] Furthermore, it is preferable that the first feeding section is a gas feeding section and the second feeding section is a liquid feeding section.

[0021] Furthermore, the top of the reaction tube is provided with a V-shaped notch, wherein the bottom end of the V-shaped notch is flush with the middle tube plate.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] (1) This utility model features a specially designed distribution pipe inserted into the reaction tube to achieve gas-liquid mixing, increasing the gas-liquid contact area. Through holes distributed on the wall of the extension section of the distribution pipe allow gas to flow out and fully mix with the liquid phase between the inner and outer tubes. The corresponding arrangement of the distribution pipe and the reaction tube ensures that the gas-liquid mixing process in each reaction tube has the same material ratio and reaction time. The gas-liquid mixing area of ​​the distribution pipe and the tube reactor is simply designed, easy to process, and easy to install. Simultaneously, through this design, the gas-liquid exchange point, i.e., the extension section of the distribution pipe, is entirely within the reaction section, allowing heat exchange through the heat exchange medium in the reaction section. During the strongly exothermic phase, heat is rapidly removed, effectively controlling the temperature and improving the reaction effect and safety.

[0024] (2) The outer diameter of the distribution tube and the inner diameter of the extended reaction tube maintain a reasonable gap to ensure sufficient gas-liquid mixing.

[0025] (3) After mixing, the packing in the tube can ensure the continuous mixing of the gas and liquid phases, and greatly improve the heat transfer coefficient and heat transfer efficiency of the equipment.

[0026] (4) Metal packing is installed in the reaction section to further improve the heat transfer efficiency and control the temperature of the reaction section in all aspects, thereby reducing the hot spot temperature. The packing in the reaction tube can also quickly transfer the material temperature from the inside to the tube wall, reduce the temperature difference between the center of the reaction tube and the tube wall, and maintain the uniformity of temperature.

[0027] (5) A support sieve plate is installed at the bottom of the reaction tube to support the packing material in the reaction tube. Attached Figure Description

[0028] Figure 1 This is a structural schematic diagram of an embodiment of the present utility model.

[0029] Figure 2 This is a structural schematic diagram of an embodiment of the present invention with a supporting sieve plate.

[0030] Figure 3 This is a schematic diagram of the structure of the supporting sieve plate of this utility model.

[0031] Figure 4 This is a schematic diagram of an embodiment of the present invention where the bottoms of the distribution tube and the reaction tube are flush.

[0032] Figure 5 This is a schematic diagram of a square tube-shaped distribution pipe structure.

[0033] Figure 6 This is a schematic diagram of the structure of the first and second branch pipes.

[0034] Figure 7 This is a schematic diagram of a pipe structure with non-uniformly distributed through holes.

[0035] Figure 8 This is a schematic diagram of a reaction tube with a V-shaped notch.

[0036] Figure label:

[0037] 1. First feeding section; 101. First feed inlet;

[0038] 2. Second feeding section; 201. Second feeding inlet;

[0039] 3. Reaction section; 301. Heat exchange medium inlet; 302. Heat exchange medium outlet;

[0040] 4. Discharge section; 401; Discharge port;

[0041] 5. Upper tube sheet;

[0042] 6. Tube sheet;

[0043] 7. Lower tube sheet;

[0044] 8. Distribution pipe; 801. First branch pipe; 802. Second branch pipe; 803. Through hole;

[0045] 9. Reaction tubes;

[0046] 10. Packing material;

[0047] 11. Restriction unit; 1101. Sieve hole. Detailed Implementation

[0048] The present invention will now be described in detail with reference to the accompanying drawings and specific embodiments. This embodiment is based on the technical solution of the present invention and provides detailed implementation methods and specific operating procedures; however, the scope of protection of the present invention is not limited to the following embodiments.

[0049] This embodiment provides an improved gas-liquid reactor to ensure continuous and uniform mixing and heat exchange in the gas-liquid reaction under strong exothermic conditions, improve the reaction conversion rate and reduce the reaction risk. Furthermore, the equipment can be operated at atmospheric pressure or relatively low pressure for commercial-scale production.

[0050] like Figure 1 As shown, this embodiment includes a first feeding section 1, a second feeding section 2, a reaction section 3, and a discharge section 4, distributed sequentially from top to bottom. An upper tube sheet 5 is provided between the first feeding section 1 and the second feeding section 2 for isolation; a middle tube sheet 6 is provided between the second feeding section 2 and the reaction section 3 for isolation; and a lower tube sheet 7 is provided between the reaction section 3 and the discharge section 4 for isolation. The upper end of the first feeding section 1 has a first inlet 101, the side wall of the second feeding section 2 has a second inlet 201, and the lower end of the discharge section 4 has an outlet 401. The reaction section 3 contains several reaction tubes 9. The top end of each reaction tube 9 passes through the middle tube sheet 6, and the bottom end of each reaction tube 9 passes through the lower tube sheet 7. The reaction tubes 9 either directly pass through or just pass through the lower tube sheet 7. A limiting unit 11 is provided at the bottom end of each reaction tube 9. The second feed section 2 is equipped with several distribution pipes 8, which are the same number as and correspond one-to-one with the reaction tubes 9. The outer diameter of the distribution pipes 8 is smaller than the inner diameter of the reaction tubes 9. Thus, the top end of the distribution pipe 8 passes through the upper tube sheet 5, and the lower section of the distribution pipe 8 extends into the reaction tubes 9 to form an extension section, with through holes 803 distributed on the wall of the extension section. The reaction section 3 is equipped with a heat exchange medium inlet 301 and a heat exchange medium outlet 302, and the heat exchange medium fills the entire reaction section 3, surrounding the reaction tubes 9. The first reactant enters the first feed section 1 through the first inlet 101, and then enters the multiple distribution pipes 8 for redistribution. The second reactant enters the second feed section 2 through the second inlet 201 on the side wall of the second feed section 2, and is distributed into the reaction tubes 9 within the second feed section 2. The positional relationship between the heat exchange medium inlet 301 and the heat exchange medium outlet 302 is not limited. For example, in the figure, the heat exchange medium inlet 301 is located on the upper right, and the heat exchange medium outlet 302 is located on the lower left. The first reactant and the second reactant are a gas and a liquid, respectively, which can be interchanged and mixed in the reaction tube 9.

[0051] In this embodiment, the extension section of the distribution pipe 8 can be a circular or rectangular pipe, mainly consistent with the shape of the reaction tube 9 into which it is inserted. The through hole 803 can be designed as a circular, rectangular, elliptical, or polygonal hole, with a preferred aperture range of 500 μm to 2 mm. The confinement unit 11 can be a metal screen, a porous ceramic plate, or a sintered metal filter element, with its pore size matched according to the particle size of the packing 10 or catalyst to prevent leakage of the packing 10 or catalyst. The heat exchange medium can be water, thermal oil, or molten salt, specifically selected according to the reaction temperature range.

[0052] This embodiment first proposes a tubular reactor with a top-in, bottom-out feeding method. This reduces the pressure drop in the reactor, enabling commercial production at atmospheric or low pressure and avoiding the rapid decomposition of flammable and explosive substances under high pressure. It also avoids flooding problems that might occur with bottom-feeding. Secondly, this embodiment achieves orderly material flow and isolation through a layered structural design, with each functional section strictly separated by a tube sheet. The nested structure of the distribution pipe 8 and the reaction tube 9 allows direct mixing of the gas and liquid phases at the gaps within the tubes, significantly increasing the gas-liquid contact area. Simultaneously, this structure ensures that the area where the gas and liquid phases first begin to mix is ​​completely surrounded by the heat exchange medium, forming a highly efficient heat exchange system that can promptly remove the initial rapidly released heat of reaction. In summary, this scheme solves the problem of uneven gas-liquid mixing through structural optimization. Furthermore, the design of the distribution pipe 8 extending into the reaction tube 9 ensures that the mixing process occurs inside the reaction section 3, allowing for direct temperature regulation via an external heat exchange medium.

[0053] In this embodiment, the gap between the outer diameter of the single tube of the distribution pipe 8 and the inner diameter of the single tube of the extended reaction tube 9 is 1–10 mm, preferably 2–5 mm. For example, the gap size can be set to typical values ​​such as 2 mm, 3 mm, 4 mm, or 5 mm. This gap setting can improve the mixing adequacy by precisely controlling the interaction distance of the gas-liquid two-phase flow boundary layers. When the gap is less than 1 mm, the boundary layer of the gas phase flow and the boundary layer of the liquid phase interfere excessively, resulting in a sharp increase in pressure drop; when the gap is greater than 10 mm, the gas phase jet velocity decays too quickly, reducing the shearing effect on the liquid phase. The gap range of 1–10 mm allows the gas phase to form a stable annular flow, generating sufficient turbulent kinetic energy at the through-hole 803 while maintaining a reasonable pressure drop level.

[0054] In this embodiment, the extension section of the distribution tube 8 is 1 / 10 to 1 / 2 of the length of the reaction tube 9, as shown in the figure as 1 / 10. The area below the extension section of the reaction tube 9 is filled with packing material 10 or a catalyst. If packing material 10 is used, it can be glass, metal, ceramic, or plastic. The packing material can increase the gas-liquid contact area, enhance mass transfer, and improve reaction efficiency. Simultaneously, the packing material can also improve the heat transfer coefficient of the reaction system. If a catalyst is used, it depends on the actual product and can be a noble metal catalyst, transition metal oxide catalyst, such as platinum / alumina catalyst, copper-zinc-aluminum catalyst, platinum / carbon catalyst, Raney nickel, etc. Filling the reaction tube 9 with packing material 10 is particularly suitable for strongly exothermic gas-liquid reaction processes.

[0055] In another preferred embodiment, fins (not shown in the figure) are provided on the outer wall of the reaction tubes 9 within the reaction section 3. This fin structure can be used to increase the degree of turbulence on the heat transfer medium side and improve the heat transfer coefficient of the heat transfer medium.

[0056] A specific example of this embodiment is as follows:

[0057] The reactor is used for ozonation reactions. For example... Figure 1 As shown, the reactor comprises, from top to bottom, a first feed section 1, a second feed section 2, a reaction section 3, and a discharge section 4. The first feed section 1 is a gas feed section, and the second feed section 2 is a liquid feed section. The first feed section 1 has a first inlet 101 at its upper end, the second feed section 2 has a second inlet 201 on its side wall, the reaction section 3 has a heat exchange medium inlet 301 and a heat exchange medium outlet 302 on its side wall, and the discharge section 4 has a discharge outlet 401 at its lower end. An upper tube sheet 5 is fixed to the lower end of the first feed section 1, a middle tube sheet 6 is fixed to the lower end of the second feed section 2, and a lower tube sheet 7 is fixed to the lower section of the reaction section 3. Multiple distribution pipes 8 are installed and fixed inside the upper tube sheet 5, and multiple reaction tubes 9 are installed and fixed between the middle tube sheet 6 and the lower tube sheet 7. The number and position of the reaction tubes 9 correspond one-to-one with the distribution pipes 8. The lower ends of the reaction tubes 9 are connected to the discharge section 4, and the product is discharged from the discharge outlet 401 at the lower end of the discharge section 4. The distribution tube 8 has an outer diameter of 10mm, an inner diameter of 14mm, a wall thickness of 2mm, a length of 300mm, and a quantity of 40 tubes. There are 48 holes around the tube, each with a diameter of 1mm. The reaction tube 9 has an inner diameter of 14mm, a wall thickness of 2mm, a length of 1000mm, and a quantity of 40 tubes. The distribution tube 8 extends 200mm into the reaction tube 9, forming the 200mm extension section. The reaction tube 9 is circular in shape. The space between the lower end of the distribution tube 8 and the lower tube sheet 7 is filled with 2mm stainless steel bead packing material 10. The heat exchange medium inlet and outlet are located on the side wall of the reaction section 3, at the upper and lower ends respectively. The heat exchange medium is either bottom-inlet / top-outlet or top-inlet / bottom-outlet.

[0058] The working process of this embodiment is as follows: ozone enters the reaction device from the first inlet 101 and liquid raw material enters from the second inlet 201; the liquid raw material is distributed into the reaction tube 9; after the liquid raw material and ozone react in the gap area between the reaction tube 9 and the distribution tube 8, the resulting mixed liquid is discharged from the outlet 401 after passing through the limiting unit 11.

[0059] In this specific embodiment, the second feed section 2 is set as a liquid feed section. At this time, the upper end of the reaction tube 9 is higher than the middle tube plate 6, forming an overflow structure. The liquid entering the second feed section 2 needs to reach a certain height before entering the reaction tube 9 and mixing with the gas in the distribution pipe 8. This forms a delayed buffer structure, preventing the liquid from immediately mixing with the gas after entering the second feed section 2, thus improving safety. Simultaneously, the flow rate of the liquid entering the reaction tube 9 after overflowing is more uniform, effectively improving the mixing quality. Figure 8 As shown, in another embodiment, to balance the overflow effect during the reaction with the cleaning and sanitation after the reaction, a V-shaped notch is provided at the top of the reaction tube 9. The bottom of the V-shaped notch is flush with the middle tube plate 6, and the angle of the V-shaped notch is 0 to 80 degrees. The angle can be adjusted according to the required fluid flow rate. If the flow rate is high, the angle of the V-shaped notch is designed to be larger; if the flow rate is low, the angle is reduced. This structure and angle setting can both create an overflow during the liquid feeding in the second feed section 2 to evenly distribute the liquid into each tube, and allow residual waste liquid to flow out from the V-shaped notch during the post-reaction cleaning of the equipment, thus thoroughly cleaning the equipment.

[0060] like Figure 2 and Figure 3 As shown, in another embodiment, the limiting unit 11 is a supporting sieve plate, which is fixed inside the discharge section 4, allowing the bottom of the reaction tube 9 to be placed on and supported on the supporting sieve plate. Simultaneously, the supporting sieve plate is provided with sieve holes 1101, which can both allow the reaction products to flow through and support components such as the packing 10 in the reaction tube 9. The supporting sieve plate can be made of porous metal plate, sintered metal mesh, or composite ceramic material; for example, the sieve holes 1101 range from 0.5 to 3 mm, and the porosity is controlled between 30% and 60%. In specific implementation, the supporting sieve plate can be fixed inside the discharge section 4 by flange connection or welding, with its mounting plane perpendicular to the axis of the reaction tube 9. In another embodiment, the supporting sieve plate can be designed as a detachable structure, allowing for quick assembly and disassembly via clips or bolts. The sieve plate thickness can be 2-20 mm, and the material selection must consider corrosion resistance and mechanical strength, such as stainless steel or Hastelloy. By integrating the support sieve plate inside the discharge section 4, a dual function is achieved: on the one hand, it provides stable bottom support for the reaction tube 9, ensuring the reliability of the overall reactor structure; on the other hand, it effectively fixes the catalyst or packing 10 inside the reaction tube 9, preventing the packing 10 from being lost or blocking the downstream pipeline with the flow of materials.

[0061] like Figure 4 As shown, in another embodiment, its basic structure is the same as the embodiment where the limiting unit 11 is a supporting sieve plate, the difference being that the bottom end of the distribution pipe 8 is flush with the bottom end of the reaction tube 9. That is, no packing or catalyst is placed inside the reaction tube 9, and the extension section of the distribution pipe 8 extends downwards to be flush with the reaction tube 9. In this structure, because the packing is omitted, installation is more convenient, and the entire reaction tube 9 becomes a mixing zone. While ensuring sufficient mixing, it can avoid some problems that may be caused by traditional packing, such as uneven filling leading to poor mixing, and increased maintenance frequency due to packing blockage.

[0062] A specific example of this embodiment is as follows:

[0063] The reactor is used for chlorination reactions. For example... Figure 4 and Figure 5 As shown, the distribution tube 8 has a rectangular structure, with an outer dimension of 15mm width, 5mm height, 2mm wall thickness, and 1300mm length. There are 30 of these tubes. The reaction tubes 9 have an inner diameter of 20mm, a wall thickness of 2mm, a length of 1000mm, and are also 30 in number. The insertion depth of the distribution tube 8 into the reaction tube 9 is 1000mm. Small holes are evenly distributed on the wall of the distribution tube 8 below the middle tube plate 6, with 10 through holes 803 evenly distributed radially on each of its four sides (width, height, and center), totaling 40 holes with a diameter of 0.5mm. The supporting sieve plate is fixed to the bottom of the lower tube plate 7. The heat exchange medium inlet and outlet are located on the side wall of the reaction section 3, at the upper and lower ends respectively, allowing the heat exchange medium to enter from the bottom and exit from the top or vice versa. The advantage of having multiple holes along the pipeline is that chlorine gas is added in batches along the direction of material flow, avoiding excessively high chlorine concentration at the material inlet, which could lead to violent exothermic reactions and difficulty in temperature control, and also preventing excessive chlorine flow in the later stages from causing side reactions. The rectangular tube design is to increase the heat exchange area and improve temperature control.

[0064] The working process of this embodiment is as follows: chlorine gas enters the reactor from the first inlet 101 and liquid raw material enters from the second inlet 201; the liquid raw material enters the reaction tube 9 from the overflow structure; after the liquid raw material and chlorine gas react in the gap between the reaction tube 9 and the distribution tube 8, the resulting mixed liquid is discharged from the outlet 401 after passing through the support sieve plate.

[0065] like Figure 6As shown, in this embodiment, the distribution pipe 8 includes a first branch pipe 801 and a second branch pipe 802 connected to each other. The first branch pipe 801 and the second branch pipe 802 can be the upper and lower parts of a complete pipe, or they can be assembled from two pipes. The assembly method is not limited to welding, threaded connection, flange connection, snap-fit, or bonding. That is to say, the second branch pipe 802 is the extension section with through holes 803 distributed thereon. The second branch pipe 802 can be made of silicon carbide pipe, graphite pipe, cast iron pipe, stainless steel pipe, Hastelloy pipe, titanium pipe, titanium alloy, nickel alloy pipe, tantalum pipe, or zirconium pipe, etc. For example, the first branch pipe 801 can be made of ordinary carbon steel to reduce costs, and the second branch pipe 802 can be made of Hastelloy C-276 pipe. In this embodiment, a segmented structural design is adopted, using corrosion-resistant materials in key gas-liquid mixing areas. The second branch pipe 802, extending into the reaction tube 9, directly contacts the highly corrosive medium. Using highly corrosion-resistant materials such as stainless steel, Hastelloy, tantalum, or zirconium effectively resists corrosion from acidic, alkaline, or halogen-containing media. By confining the corrosion-resistant material to key areas, long-term stable operation of the equipment in corrosive environments is ensured, while avoiding excessive costs associated with using expensive materials throughout. The through-hole 803 on the corrosion-resistant pipe section ensures that the gas-liquid mixing effect is not affected by material replacement, while the mechanical properties of the corrosion-resistant material maintain the stability of the pore structure during long-term use.

[0066] like Figure 7As shown, in another embodiment, the diameter of the through-hole 803 increases radially from top to bottom along the extension section. Specifically, the diameter gradient can be achieved by using an arithmetic progression sequence, for example, an upper diameter of 500 μm, a middle diameter of 750 μm, and a lower diameter of 1 mm; or by using a geometric progression, such as an upper diameter of 500 μm, a middle diameter of 1 mm, and a lower diameter of 2 mm. As another embodiment, the diameter can also be designed with continuous variation, using CNC drilling to make the diameter increase linearly or non-linearly along the axial direction. Furthermore, the diameter gradient can be adjusted according to the physical properties of the gas / liquid, with a steeper gradient for gases / liquids with higher viscosity. This structure solves the problem of uneven gas-liquid reaction through fluid dynamics compensation. Because of the pressure drop along the pipe flow path, traditional constant diameter designs lead to a decrease in the outflow velocity of the lower gas / liquid. By gradually increasing the orifice diameter, the lower gas / liquid flow area can be increased, matching the reduction in flow resistance with the pressure drop loss, thereby maintaining the stability of the kinetic energy of the gas / liquid outflow at various axial positions. Experimental data show that when the orifice diameter gradient design controls the difference in outflow velocity at each cross-section within ±5%, the axial temperature distribution uniformity of the reaction tube 9 can be improved by more than 40%. This dynamic compensation mechanism effectively avoids the problem of decreased product selectivity caused by the weakening of the lower reaction intensity in traditional designs, and is particularly suitable for fast reaction processes such as chlorination and ozonation that are sensitive to the gas-liquid ratio. Furthermore, this through-hole 803 variation structure preferably incorporates liquid within the distribution tube, i.e., the first feed section is a liquid feed section, and the second feed section is a gas feed section.

[0067] The preferred embodiments of this utility model have been described in detail above. It should be understood that those skilled in the art can make numerous modifications and variations based on the concept of this utility model without creative effort. Therefore, all technical solutions that can be obtained by those skilled in the art based on the concept of this utility model through logical analysis, reasoning, or limited experimentation on the basis of existing technology should be within the scope of protection defined by the claims.

Claims

1. An improved gas-liquid reactor characterized by, It includes a first feeding section (1), a second feeding section (2), a reaction section (3), and a discharge section (4) arranged sequentially from top to bottom. An upper tube sheet (5) is provided between the first feeding section (1) and the second feeding section (2) for isolation. A middle tube sheet (6) is provided between the second feeding section (2) and the reaction section (3) for isolation. A lower tube sheet (7) is provided between the reaction section (3) and the discharge section (4) for isolation. The reaction section (3) is provided with a number of reaction tubes (9), the top end of each reaction tube (9) passes through the middle tube plate (6), the bottom end of the reaction tube (9) passes through the lower tube plate (7), and the bottom end of the reaction tube (9) is provided with a limiting unit (11). The second feed section (2) is provided with a number of distribution pipes (8). The top end of the distribution pipe (8) passes through the upper tube sheet (5), and the lower section of the distribution pipe (8) extends into the reaction tube (9) to form an extension section. The extension section has through holes (803) distributed on its tube wall. The reaction section (3) is provided with a heat exchange medium inlet (301) and a heat exchange medium outlet (302), and the heat exchange medium fills the entire reaction section (3) and surrounds the reaction tube (9).

2. The improved gas-liquid reactor according to claim 1, wherein The gap between the outer diameter of the single tube of the distribution tube (8) and the inner diameter of the single tube of the extended reaction tube (9) is 1 to 10 mm.

3. The improved gas-liquid reactor according to claim 1, wherein The bottom end of the distribution tube (8) is flush with the bottom end of the reaction tube (9).

4. The improved gas-liquid reactor according to claim 1, wherein The reaction tube (9) is filled with a catalyst or filler (10).

5. The improved gas-liquid reactor according to claim 4, wherein The packing material (10) is a metal packing material.

6. An improved gas-liquid reactor according to claim 1, characterized in that, Within the reaction section (3), fins are provided on the outer wall of the reaction tube (9).

7. An improved gas-liquid reactor according to claim 1, characterized in that, The distribution pipe (8) includes a first branch pipe (801) and a second branch pipe (802) that are connected to each other or are integral. The second branch pipe (802) is a silicon carbide pipe, graphite pipe, cast iron pipe, stainless steel pipe, Hastelloy pipe, titanium pipe, titanium alloy, nickel alloy pipe, tantalum pipe or zirconium pipe. The second branch pipe (802) is an extension section with through holes (803) distributed thereon.

8. An improved gas-liquid reactor according to claim 1, characterized in that, The diameter of the through hole (803) is 500μm to 2mm.

9. The improved gas-liquid reactor as claimed in claim 1, wherein, The limiting unit (11) is a supporting sieve plate, which is set in the discharge section (4) to support the reaction tube (9).

10. The improved gas-liquid reactor as claimed in claim 1, wherein, The top of the reaction tube (9) is also provided with a V-shaped notch, wherein the bottom end of the V-shaped notch is flush with the middle tube plate (6).

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