Distributor for improving gas-liquid distribution, distribution plate and reactor

Abstract

A distributor for improving gas-liquid distribution, a distribution plate and a reactor relate to the field of hydrogenation reaction, the distributor comprises a distributor pipe body, a gas inlet and a spray outlet are respectively formed at the top end and the bottom end of the distributor pipe body, a liquid-phase overflow hole is arranged on the distributor pipe body, a turbulent flow medium is arranged in the distributor pipe body close to the spray outlet, and the liquid-phase overflow hole is communicated with the liquid-phase overflow hole. The gas-liquid equilibrium state in the distributor pipe body is broken, and liquid phase gasification is promoted. The inner wall of the distributor pipe body is changed from the conventional smooth inner wall to the arrangement of the turbulent flow medium at the position, close to the ejection opening, of the inner wall, due to the existence of the turbulent flow medium, in the process that a gas phase and a liquid phase pass through the distributor, the gas-liquid balance state is broken, gasification of the liquid phase is enhanced, part of the liquid phase is converted into the gas phase, and the gas phase is separated from the liquid phase. The gas-liquid ratio of the distributor is increased, and the liquid phase distribution is improved.

Description

Technical Field

[0001] The present invention relates to the field of hydrogenation reactions, and more specifically, to a distributor, a distribution plate, and a reactor for improving gas-liquid distribution. Background Art

[0002] Under the background of increasingly strict environmental protection regulations, the standards for impurity content in various petroleum products are also increasing day by day. As an essential technology in the production process of clean fuels, hydrogenation technology plays a significant role in refinery production. Hydrogenation technology includes hydrocracking, hydrofining, etc. Hydrogenation reactions are exothermic reactions, and currently, the vast majority of domestic reactors adopt a downflow fixed-bed reactor structure. The reaction materials flow through the catalyst bed from top to bottom and undergo hydrogenation reactions under its action. During the reaction process, the uneven distribution of gas and liquid in the bed layer will cause hazards such as hot spots, catalyst coking, and runaway temperature in the reactor, which affect product quality and safety in production. Therefore, stable gas-liquid distribution is crucial for improving the flow characteristics and catalyst utilization rate in the reactor, and the gas-liquid distribution device is an internal component that has an important impact on the initial gas-liquid distribution in the reactor.

[0003] Existing gas-liquid distributors are basically straight pipes with smooth inner walls. The gas phase is inhaled from the top side, and the liquid phase is inhaled from the side wall, simply dispersing the gas-liquid two-phase from above the distribution plate to the catalyst bed layer below to participate in the reaction.

[0004] However, for some liquid phases, especially heavy oil with a relatively high viscosity, existing distributors can only ensure approximately uniform distribution on the surface of the entire catalyst bed layer (mainly relying on the uniformly distributed distributors on the distribution plate). However, when the gas-liquid two-phase passing through each distributor contacts the catalyst bed layer, in the injection area of the distributor, a good dispersion and uniform distribution effect cannot be achieved.

[0005] As is well known to those skilled in the art, compared with the liquid phase, the gas phase is more easily evenly distributed. Under the high-temperature and high-pressure conditions in the reactor, the gas-liquid two-phase is always in an equilibrium state in the reactor. Without external force intervention, it is very difficult to break the equilibrium of the gas-liquid two-phase and then convert part of the liquid phase into the gas phase. Summary of the Invention

[0006] The purpose of the present invention is to provide a distributor, a distribution plate, and a reactor for improving gas-liquid distribution. During the process of the gas-liquid two-phase passing through the distributor, the gas-liquid equilibrium state is broken, the gasification of the liquid phase is strengthened, part of the liquid phase is converted into the gas phase, the gas-liquid ratio passing through the distributor is increased, and the distribution of the liquid phase is improved.

[0007] The technical solution adopted by the present invention to achieve the above technical purpose is as follows: A distributor for improving gas-liquid distribution includes a distributor tube body with a gas inlet and a spray outlet formed at the top and bottom respectively, and a liquid-phase overflow hole is provided on the distributor tube body. A turbulence medium is provided near the spray outlet inside the distributor tube body to break the gas-liquid equilibrium state inside the distributor tube body and promote the gasification of the liquid phase.

[0008] As an optimized scheme of the above distributor for improving gas-liquid distribution, the height of the turbulence medium is not less than 2 times the inner diameter of the distributor tube body.

[0009] As another optimized scheme of the above distributor for improving gas-liquid distribution, the turbulence medium is a rough surface distributed on the inner wall of the distributor tube body. The rough surface is distributed with several protruding spikes, and the area between the spikes is a plane or a concave surface.

[0010] As another optimized scheme of the above distributor for improving gas-liquid distribution, the turbulence medium is a wire mesh sleeve arranged around the inner wall of the distributor tube body. The thickness of the wire mesh sleeve is 10-30% of the radius of the distributor tube body, and the porosity of the wire mesh sleeve is 40-80%.

[0011] As another optimized scheme of the above distributor for improving gas-liquid distribution, a filter area is filled inside the wire mesh sleeve, and both ends of the filter area do not extend beyond the wire mesh sleeve. The porosity of the filter area is 60-95%, and is greater than the porosity of the wire mesh sleeve.

[0012] As another optimized scheme of the above distributor for improving gas-liquid distribution, the turbulence medium is a mesh structure formed by stacking multiple layers of metal wire meshes. The bottom layer of the metal wire mesh is fixedly connected to the inner wall of the distributor tube body, and the remaining metal wire meshes can slide up and down along the inner wall of the distributor tube body. Adjacent two layers of metal wire meshes are connected by elastic members to form a buffer cavity; each layer of metal wire mesh is composed of a central area and an edge area surrounding the central area, and the diameter of the central area is 40-80% of the diameter of the metal wire mesh. The porosity of the edge area is less than the porosity of the central area.

[0013] As another optimized scheme of the above distributor for improving gas-liquid distribution, the porosity of the edge area is 40-80%, and the porosity of the central area is 60-95%.

[0014] As another optimized scheme of the above distributor for improving gas-liquid distribution, the top end of the distributor tube body has an extension part inclined to one side, and the included angle formed by the extension part and the distributor tube body is 130-160°. The top end of the extension part forms a gas inlet in a horizontal state.

[0015] As another optimized solution of the distributor for improving gas-liquid distribution, the projected length of the extension part on the horizontal plane is not less than 2 times and not more than 3 times the inner diameter of the distributor tube body.

[0016] As another optimized solution of the distributor for improving gas-liquid distribution, the distance from the top end of the distributor tube body to the liquid-phase overflow hole is not less than 6 times the inner diameter of the distributor tube body.

[0017] As another optimized solution of the distributor for improving gas-liquid distribution, the spray outlet is a flared outward expansion structure, and the smaller-diameter end is connected to the distributor tube body, and a flow-breaking plate is arranged below the spray outlet.

[0018] A distribution plate for improving gas-liquid distribution includes a plate body and distributors distributed on the plate body, and the distributors are the above-mentioned distributors.

[0019] A reactor has the above-mentioned distribution plate inside the reactor.

[0020] In the present invention, the mechanism by which the turbulent flow medium breaks the gas-liquid equilibrium state in the distributor tube body and promotes the gasification of the liquid phase is as follows:

[0021] During the gasification process, the superheat of the liquid is one of the necessary conditions for phase change. The superheat required for liquid evaporation is proportional to 2σ / R (σ is the surface tension of the liquid, and R is the curvature radius of the evaporation bubble). The larger R is, the smaller the wall superheat required is. Currently, the inside of the existing tubular gas-liquid distributors is basically a smooth tube. The surface roughness of the smooth tube is small, and the curvature radius of the vapor bubble is also very small. Vapor bubbles can only be generated at a relatively high superheat.

[0022] However, the present invention uses a turbulent flow medium. Whether it is the protruding spikes or the wire mesh structure (wire mesh sleeve, metal wire mesh), its essence is to change the roughness when the liquid passes through and the curvature radius of the formed bubbles. Especially for the wire mesh structure, the micropores on the porous surface and the interconnected tunnels provide a large number of vaporization nuclei. The vapor bubbles generated in one micropore can stimulate the adjacent micropores, and the small vapor bubbles are interconnected and easy to grow. Therefore, the superheat required for vaporization is greatly reduced, so as to achieve stable vaporization at a low temperature difference, increase the volume ratio of the gas phase, and can greatly improve the material flow distribution.

[0023] Due to the evaporation of the liquid film around the vaporization layer, the vapor bubbles gradually grow and quickly detach. After the vapor bubbles detach, the pressure in the void or channel drops, the volume shrinks, and the external liquid is sucked into the void or channel under the action of the pressure difference and capillary force for re-vaporization. The vapor bubbles grow and detach again, so that the rapid cycle of the liquid being sucked into the void and channel for re-evaporation keeps going, maintaining a high re-circulation rate in the structure, thereby strengthening the vaporization process.

[0024] Compared with the prior art, the present invention has the following beneficial effects:

[0025] 1) In the present invention, the inner wall of the dispenser tube is changed from the conventional smooth inner wall to a position near the spray outlet on the inner wall where a flow disturbing medium is provided. Due to the presence of the flow disturbing medium, the gas-liquid equilibrium state is broken during the process of the gas-liquid two-phase passing through the dispenser, the gasification of the liquid phase is strengthened, part of the liquid phase is converted into the gas phase, the gas-liquid ratio passing through the dispenser is increased, and the distribution of the liquid phase is improved.

[0026] 2) The flow disturbing medium of the present invention, whether it is a protruding spike or a wire mesh structure, essentially changes the roughness when the liquid passes through and the radius of curvature of the formed bubbles, so that the liquid phase is easily gasified during the process of passing through the flow disturbing medium. The wire mesh structure of the present invention can have various forms, such as a sleeve formed by the wire mesh, or a filter area formed by arranging a wire mesh in the wire mesh sleeve, but it is required that the porosity of the filter area is greater than that of the wire mesh sleeve to form the main flow channel for the liquid phase to pass through, or it is formed by stacking multiple layers of wire meshes, and the adjacent wire meshes can slide. Each layer of wire mesh is divided into a central area and an edge area, and the porosity of the central area is greater than that of the edge area. This elastic wire mesh structure can also effectively balance the average amount of the liquid phase passing through per unit time (when the liquid phase is too much in a short time, it will press the upper layer of wire mesh to move downward, so that the whole becomes "dense" and reduces the passing of the liquid phase; while when the liquid phase is less in a certain period of time, the wire mesh will rebound upward, so that the whole becomes "loose" and increases the passing amount of the liquid phase).

[0027] 3) In the present invention, an extension part inclined to one side is provided at the top end of the dispenser tube, and a gas inlet is formed at the end of the extension part. Compared with the structure of the existing dispenser that sucks air from the side, it can not only prevent the liquid from directly entering the tube body and causing blockage, but more importantly, it can reduce the gas resistance entering the dispenser tube body. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 is a schematic structural diagram of the present invention;

[0029] Figure 2 is Figure 1 an enlarged schematic structural diagram of part A in

[0030] Figure 3 is Figure 1 another enlarged schematic structural diagram of part A in

[0031] Figure 4 is another schematic structural diagram of the present invention;

[0032] Figure 5 is still another schematic structural diagram of the present invention;

[0033] Figure 6 is Figure 5Enlarged schematic diagram of the middle turbulence medium;

[0034] Figure 7 Another structural schematic diagram of the present invention;

[0035] Figure 8 is Figure 7 Schematic diagram of a state when the multi-layer metal wire mesh in the middle is compressed by the liquid phase;

[0036] Figure 9 Planar schematic diagram of a single-layer metal wire mesh;

[0037] Reference numerals: 1, distributor tube body; 2, spray outlet; 3, fragmentation plate; 4, extension part; 5, liquid phase overflow hole; 6, turbulence medium; 601, spike; 602, concave surface; 603, wire mesh sleeve; 604, filter area; 605, metal wire mesh; 6051, central area; 6052, edge area; 606, buffer cavity; 7, disk body. Detailed implementation manners

[0038] The technical solutions of the present invention will be further elaborated in detail below in conjunction with specific embodiments. For parts not clarified in the following embodiments of the present invention, such as the installation position and installation method of the distributor on the distribution disk, the overall dimensions of the distributor, etc., shall all be regarded as the prior art known or should be known to those skilled in the art.

[0039] Embodiment 1

[0040] A distributor for improving gas-liquid distribution, as Figure 1 shown, includes a distributor tube body 1 with a gas inlet and a spray outlet 2 formed at the top and bottom respectively. The distributor tube body 1 is generally made of high-quality stainless steel, and its overall dimensions need to be processed according to design requirements. A liquid phase overflow hole 5 is provided on the distributor tube body 1, and the liquid phase overflow hole 5 is located on the upper surface of the distribution disk, so that the liquid phase accumulated on the distribution disk can enter the distributor tube body 1 through the liquid phase overflow hole 5. The number of the liquid phase overflow holes 5 is generally two symmetrically arranged, and its size is also designed according to the working conditions. A turbulence medium 6 is provided near the spray outlet 2 inside the distributor tube body 1. The function of the turbulence medium 6 is that when the gas-liquid two-phase passes through, it changes the bubble curvature when the liquid phase evaporates into the gas phase, so as to break the gas-liquid equilibrium state inside the distributor tube body 1 and promote more liquid phase to be converted into the gas phase. Any structure that can achieve the function of the present invention is within the protection scope of the present invention.

[0041] In this embodiment, the height of the turbulence medium 6 is generally not less than 2 times the inner diameter of the distributor tube body 1, the distance between the bottom of the turbulence medium 6 and the spray outlet 2 does not exceed 10% of the inner diameter of the distributor tube body 1, and the distance between the top of the turbulence medium 6 and the disk body 7 of the distribution disk is generally 20 - 50% of the inner diameter of the distributor tube body 1.

[0042] The above is the basic implementation mode of the present invention. Further improvements, optimizations and limitations can be made on this basis to obtain the following embodiments:

[0043] Embodiment 2

[0044] This embodiment is an example of the structure of the spoiler medium 6 based on Embodiment 1. Its main structure is the same as that of Embodiment 1. The structure of the spoiler medium 6 is as follows: As Figure 1 shown, the spoiler medium 6 is a rough surface distributed on the inner wall of the distributor tube body 1. As Figure 2 and 3 shown, several raised spikes 601 are randomly and disorderly distributed on the rough surface. The so-called spike 601 refers to a strip structure whose height-to-diameter ratio is greater than 5:1. The lengths of the spikes 601 are inconsistent, some are long and some are short. However, the height of the longest spike 601 is generally 10-30% of the radius of the distributor tube body 1. The shape of the spike 601 can be cylindrical or conical. However, when it is conical, the height-to-maximum diameter ratio is greater than 5:1. In addition to these two shapes, it can also be other regular shapes, such as triangular pyramids, triangular prisms, etc., or other irregular shapes. The area between the spikes 601 is a plane or a concave surface 602. As Figure 2 and 3 shown.

[0045] Embodiment 3

[0046] This embodiment is another example of the structure of the spoiler medium 6 based on Embodiment 1. Its main structure is the same as that of Embodiment 1. The structure of the spoiler medium 6 is as follows: As Figure 4 shown, the spoiler medium 6 is a wire mesh sleeve 603 arranged around the inner wall of the distributor tube body 1. The wire mesh sleeve 603 is a sleeve shape with a certain thickness formed by weaving metal wire mesh. Its outer wall is fixedly connected to the inner wall of the distributor tube body 1 by bonding or other means. And the thickness of the wire mesh sleeve 603 is 10-30% of the radius of the distributor tube body 1, and the porosity of the wire mesh sleeve 603 is 40-80%.

[0047] In this embodiment, most of the gas phase and liquid phase move downward through the channel in the middle of the wire mesh sleeve 603. Due to the existence of pores in the wire mesh sleeve 603, part of the gas phase and liquid phase will also pass through it. The micropores and interconnected tunnels on the surface provide a large number of vaporization nuclei. The bubbles generated in one micropore can stimulate adjacent micropores, and the small bubbles are interconnected and easy to grow. Therefore, the superheat required for vaporization is greatly reduced, so as to achieve stable vaporization at a low temperature difference and increase the volume ratio of the gas phase.

[0048] Embodiment 4

[0049] This embodiment is an improved solution based on Embodiment 3. Its main structure is the same as that of Embodiment 3. The improvement lies in that, as Figure 5 and Figure 6 shown, a filter screen area 604 is filled inside the wire mesh sleeve 603. The filter screen area 604 is actually a columnar structure formed by weaving metal wire meshes, and is fixed to the wire mesh sleeve 603 to form an integral whole. Moreover, both ends of the filter screen area 604 do not extend beyond the wire mesh sleeve 603. Preferably, the upper and lower ends of the wire mesh sleeve 603 are flush with those of the filter screen area 604. The porosity of the filter screen area 604 is generally 60-95%, and is greater than the porosity of the wire mesh sleeve 603, so that the liquid phase is more likely to pass through relative to the wire mesh sleeve 603, and a porosity stratification is formed with the edge of the wire mesh sleeve 603.

[0050] Embodiment 5

[0051] This embodiment is another example of the structure of the flow disturbing medium 6 based on Embodiment 1. Its main structure is the same as that of Embodiment 1. The structure of the flow disturbing medium 6 is as follows: as Figure 7 and Figure 8 shown, the flow disturbing medium 6 is a mesh structure formed by stacking multiple layers of metal wire meshes 605. Each layer of metal wire mesh 605 is a planar mesh structure formed by weaving metal wires, and its shape and size match the inner wall of the distributor pipe body 1. The thickness of each layer of metal wire mesh 605 is generally 5-10 mm. The lowermost layer of metal wire mesh 605 is fixedly connected to the inner wall of the distributor pipe body 1, and its position is fixed. The remaining metal wire meshes 605 can slide up and down along the inner wall of the distributor pipe body 1. In practice, it is squeezed by the amount of the liquid phase entering, so that it slides up and down. Adjacent layers of metal wire meshes 605 are connected by elastic members. The elastic members are generally springs, and a buffer cavity 606 is formed. When there is no liquid phase, the height of the buffer cavity 606 is generally 0.5-2 times the thickness of the metal wire mesh 605; each layer of metal wire mesh 605 is composed of a central area 6051 and an edge area 6052 surrounding the central area 6051. The edge area 6052 is annular, and its outer edge contacts the inner wall of the distributor pipe body 1. The diameter of the central area 6051 is 40-80% of the diameter of the metal wire mesh 605. The porosity of the central area 6051 is 60-95%; the porosity of the edge area 6052 is 40-80%, and the porosity of the edge area 6052 is less than that of the central area 6051.

[0052] Embodiment 6

[0053] This embodiment is an improvement on the structure of the dispenser body 1 based on Embodiment 1. Its main structure is the same as that of Embodiment 1, and the improved parts are as follows: The top end of the dispenser body 1 has an extension part 4 that slopes upward to one side. The extension part 4 is also a stainless steel pipe body, and its inner diameter and outer diameter are both equal to those of the dispenser body 1, and the two form an integral structure. The included angle formed by the extension part 4 and the dispenser body 1 is 130 - 160°. The top end of the extension part 4 forms a gas inlet in a horizontal state, that is to say, the plane formed at the top end of the extension part 4 is in a vertical state. Compared with the existing structure of side suction of the dispenser, by setting the extension part 4, not only can it prevent liquid from directly entering the pipe body and causing blockage, but more importantly, it can reduce the gas resistance entering the dispenser pipe 1;

[0054] In this embodiment, the projection length of the extension part 4 on the horizontal plane is not less than 2 times the inner diameter of the dispenser body 1 and not greater than 3 times the inner diameter of the dispenser body 1; At this time, the distance from the top end of the dispenser body 1 (that is, the position where it is joined to the extension part 4) to the liquid phase overflow hole 5 is not less than 6 times the inner diameter of the dispenser body 1.

[0055] In this embodiment, the spray outlet 2 can be in the shape of an ordinary straight pipe, but the preferred structure is a flared outward expansion structure, and the smaller diameter end is connected to the dispenser body 1. A fragmentation plate 3 is provided below the spray outlet 2. The fragmentation plate 3 is a horizontal metal flat plate, perpendicular to the axis of the dispenser body 1, and small holes can be distributed on it or no small holes can be provided; The fragmentation plate 3 is fixed to the inner wall of the spray outlet 2 through a support rod, and the support rod can be rigid or elastic; A mixed phase channel is formed between the edge of the fragmentation plate 3 and the spray outlet 2, and the height of the fragmentation plate 3 can be inside the spray outlet 2 or below the spray outlet 2.

[0056] Embodiment 7

[0057] A distribution plate for improving gas-liquid distribution includes a plate body 7 and dispensers distributed on the plate body 7. Installation holes are arranged on the plate body 7 according to a pre-designed scheme, and one of the dispensers in the above Embodiments 1 - 6 is installed in each installation hole, and the liquid phase overflow hole 5 on the dispenser body 1 is above the plate body 7, and the turbulence medium 6 in the dispenser body 1 is below the plate body 7.

[0058] Embodiment 8

[0059] A reactor has the distribution plate of the above Embodiment 7, and the remaining components in the reactor are prior art.

[0060] In order to verify the promotion effect of the present invention on liquid phase gasification, the following comparative experiments are carried out:

[0061] Select heavy oil and hydrogen as reactants, and simulate the internal environment of the reactor under the conditions of a temperature of 400 °C and a pressure of 14 MPa; hydrogen is introduced into the reactor from the top of the reactor at a pressure of 14.1 MPa, and heavy oil, as a liquid phase, enters the distributor from the liquid-phase overflow port;

[0062] Comparative Example 1

[0063] Select a straight-tube distributor with a smooth inner wall. It has an extension part 4 that slopes upward to one side at the top, and the end of the extension part 4 serves as the air inlet. The tube body has two symmetric liquid-phase overflow holes 5 at a position above the disk body 7, and the bottom of the tube body extends below the disk body 7;

[0064] Comparative Example 2

[0065] The distributor in this comparative example is the same as that in Comparative Example 1, except that its inner wall is not smooth. A turbulator medium 6 in Example 2 is provided on the inner wall of the tube body below the disk body 7, that is, a rough surface is provided on the inner wall, and raised spikes are irregularly distributed on the rough surface;

[0066] Comparative Example 3

[0067] The distributor in this comparative example is the same as that in Comparative Example 1, except that its inner wall is not smooth. A turbulator medium 6 in Example 3 is provided on the inner wall of the tube body below the disk body 7, that is, a wire mesh sleeve 603 is provided on the inner wall;

[0068] Comparative Example 4

[0069] The distributor in this comparative example is an adjustment based on Comparative Example 3. The adjustment is that a filter mesh area 604 is filled inside the wire mesh sleeve 603, that is, the structure of Example 4;

[0070] Comparative Example 5

[0071] The distributor in this comparative example is the same as that in Comparative Example 1, except that its inner wall is not smooth. A turbulator medium 6 in Example 5 is provided on the inner wall of the tube body below the disk body 7, that is, the turbulator medium 6 is a mesh structure formed by stacking multiple layers of metal wire meshes 605;

[0072] Load the same mass of heavy oil into the distributors of Comparative Examples 1 - 5 respectively. Then, under the same reaction conditions, introduce hydrogen in the same state, and detect the total mass of the liquid phase ejected from the spray outlet of the distributor within a certain period of time, as well as the remaining liquid phase amount that has not been sucked into the distributor. The difference between the sum of the two and the total mass of the liquid phase before the reaction is the gasification amount of the liquid phase. After dividing the difference by the total mass of the liquid phase before the reaction and expressing it as a percentage, it is used as the gasification amount investigation index;

[0073] It was measured that the gasification amount index in Comparative Example 1 was 2.96%, the gasification amount index in Comparative Example 2 was 3.41%, the gasification amount index in Comparative Example 3 was 5.46%, the gasification amount index in Comparative Example 4 was 4.58%, and the gasification amount index in Comparative Example 5 was 4.73%.

[0074] It can be seen from the above comparative experiments that in the present invention, by arranging a flow disturbing medium on the smooth inner wall, the gasification amount can be increased (comparison between Comparative Example 1 and Comparative Examples 2-5), and for different structures of the flow disturbing medium 6, the gasification amounts are also different. The optimal way is the wire mesh sleeve (Comparative Example 3). When the filter screen area is filled inside the sleeve, it will cause a slight decrease in its gasification amount (comparison between Comparative Example 3 and Comparative Example 4); and when using a stacked multi-layer metal wire mesh structure, it will also cause a slight decrease in its gasification amount (comparison between Comparative Example 3 and Comparative Example 5).

Claims

1. A distributor for improving gas-liquid distribution, comprising a distributor tube body (1) with a gas inlet and a spray outlet (2) formed at the top end and the bottom end respectively, and a liquid-phase overflow hole (5) is provided on the distributor tube body (1), and it is characterized in that: A turbulence medium (6) is provided at a position close to the spray outlet (2) inside the dispenser body (1) to break the gas-liquid equilibrium state inside the dispenser body (1) and promote the gasification of the liquid phase.

2. The distributor for improving gas-liquid distribution according to claim 1, wherein: The height of the turbulence medium (6) is not less than 2 times the inner diameter of the dispenser body (1).

3. The distributor for improving gas-liquid distribution according to claim 1, characterized in that: The turbulence medium (6) is a rough surface distributed on the inner wall of the dispenser body (1), and a number of raised spikes (601) are distributed on the rough surface. The area between the spikes (601) is a plane or a concave surface (602).

4. The distributor for improving gas-liquid distribution according to claim 1, characterized in that: The turbulence medium (6) is a wire mesh sleeve (603) provided around the inner wall of the dispenser body (1), and the thickness of the wire mesh sleeve (603) is 10 - 30% of the radius of the dispenser body (1), and the porosity of the wire mesh sleeve (603) is 40 - 80%.

5. The distributor for improving gas-liquid distribution according to claim 4, characterized in that: A filter screen area (604) is filled inside the wire mesh sleeve (603), and both ends of the filter screen area (604) do not extend beyond the wire mesh sleeve (603). The porosity of the filter screen area (604) is 60 - 95%, and is greater than the porosity of the wire mesh sleeve (603).

6. The distributor for improving gas-liquid distribution according to claim 1, wherein: The turbulence medium (6) is a net structure stacked by multiple layers of wire meshes (605). The bottom layer of the wire mesh (605) is fixedly connected to the inner wall of the dispenser body (1), and the remaining wire meshes (605) can slide up and down along the inner wall of the dispenser body (1). Adjacent two layers of wire meshes (605) are connected by elastic members to form a buffer cavity (606); each layer of wire mesh (605) is composed of a central area (6051) and an edge area (6052) surrounding the central area (6051), and the diameter of the central area (6051) is 40 - 80% of the diameter of the wire mesh (605). The porosity of the edge area (6052) is less than the porosity of the central area (6051).

7. The distributor for improving gas-liquid distribution according to claim 1, wherein: The top end of the dispenser body (1) has an extension part (4) inclined to one side, and the included angle formed by the extension part (4) and the dispenser body (1) is 130 - 160°. The top end of the extension part (4) forms a gas inlet in a horizontal state.

8. The distributor for improving gas-liquid distribution according to claim 7, wherein: The projection length of the extension part (4) on the horizontal plane is not less than 2 times the inner diameter of the dispenser body (1) and not greater than 3 times the inner diameter of the dispenser body (1).

9. The distributor for improving gas-liquid distribution according to claim 7, characterized in that: The distance from the top end of the dispenser body (1) to the liquid phase overflow hole (5) is not less than 6 times the inner diameter of the dispenser body (1).

10. The distributor for improving gas-liquid distribution according to claim 1, wherein: The spray outlet (2) is a flared outward expansion structure, and the smaller diameter end is connected to the dispenser body (1). A fragmentation plate (3) is provided below the spray outlet (2).

11. A distribution tray for improving gas-liquid distribution, comprising a tray body (7) and distributors distributed on the tray body (7), characterized in that: The dispenser is the dispenser described in any one of claims 1 - 10.

12. A reactor, characterized in that: The reactor is provided with the distribution plate described in claim 12.

Images