Upflow reactor and gas-liquid distribution device therefor

Abstract

The utility model relates to the field of reactor discloses an upflow reactor and gas -liquid distribution device thereof. The gas -liquid distribution device includes base plate and a plurality of distribution pipes, and the base plate is equipped with through -hole, and the outer periphery of the one end of distribution pipe away from base plate is equipped with liquid phase import, and the lateral wall of distribution pipe is equipped with gas phase import, and the inside of distribution pipe is equipped with at least one bubble breaker, and bubble breaker is located in the side of gas phase import close to base plate, and bubble breaker is evenly distributed with a plurality of bubble breaking holes. The upflow reactor includes reactor shell, catalyst bed and above-mentioned gas -liquid distribution device. Based on the gas -liquid distribution device provided by the utility model, the big bubble into the distribution pipe is driven under the buoyancy and upflow liquid phase, passes at least one bubble breaker, makes the bubble be broken into smaller bubble, increases the breaking effect of bubble, and, the gas -liquid distribution device of this kind of design mode simple structure avoids the redundant structure, reduces the manufacturing and maintenance cost.

Description

Technical Field

[0001] This utility model relates to the field of reactors, specifically to an upflow reactor and its gas-liquid distribution device. Background Technology

[0002] Upflow reactors are widely used in the petrochemical industry, commonly in processes such as liquid-phase hydrogenation of distillate oils, hydrogenation of residue oils, desulfurization and denitrification, and liquid-phase isomerization of aromatics. In these processes, the uniform distribution of the gas and liquid phases is crucial to reactor performance. However, typically, the liquid phase is continuous and the gas phase is dispersed. Due to the significant differences in their physical properties, the upward flow of the gas stream causes disturbances, leading to the escape of some dissolved gas phase. This can result in uneven flow, localized bubble accumulation, and reduced mass transfer efficiency, leading to unsatisfactory reaction outcomes. Therefore, a gas-liquid distribution plate is needed before the catalyst bed to remix and distribute the gas and liquid streams. The mixing performance of the gas-liquid distribution plate directly affects the melting rate of the gas phase in the liquid phase.

[0003] In response, Chinese invention patent CN115672198A discloses a gas-liquid distributor. The distributor's riser pipe consists of a gas-liquid inlet section, a float dispersion section, and a gas-liquid outlet section from bottom to top. The gas-liquid inlet section has an open bottom, and the float dispersion section contains a float and upper and lower baffles to restrict the float's position. This gas-liquid distributor uses a combination of the gas-liquid inlet section, float dispersion section, and gas-liquid outlet section, and achieves uniform bubble dispersion through the design of the float and upper and lower baffles. However, the structure of this gas-liquid distributor is relatively complex, and the bubble breaking effect is poor. Utility Model Content

[0004] In order to solve the above-mentioned technical problems, or at least partially solve the above-mentioned technical problems, the present invention provides an upflow reactor and its gas-liquid distribution device.

[0005] This utility model provides a gas-liquid distribution device, including a substrate and a plurality of distribution tubes evenly distributed on one side of the substrate. The substrate is provided with through holes at positions corresponding to the distribution tubes. A liquid phase inlet is provided on the outer periphery of the end of the distribution tube away from the substrate. A gas phase inlet is provided on the side wall of the distribution tube. At least one bubble breaking plate is provided inside the distribution tube near the substrate. The bubble breaking plate is located on the side of the gas phase inlet near the substrate. A plurality of bubble breaking holes are evenly distributed on the bubble breaking plate.

[0006] Optionally, a buffer baffle is provided on the side of the substrate where the distribution tube is located. The buffer baffle coincides with the central axis of the substrate and is located on the side of the distribution tube away from the substrate.

[0007] Optionally, the diameter of the buffer baffle is 0.5-2m and the thickness is 20-80mm;

[0008] And / or, the distance between the buffer baffle and the end of the distribution pipe is 0.2-1.2m.

[0009] Optionally, the shape of the buffer baffle is a circular flat plate, a conical plate, an arc plate, a stepped plate, or a perforated plate.

[0010] Optionally, the number of bubble-breaking plates is one or more, and the equivalent diameter of the openings in the multiple bubble-breaking plates decreases from bottom to top.

[0011] Optionally, there are two bubble-breaking plates, the distance between the two bubble-breaking plates is 10-30mm, and the distance between the bubble-breaking plate disposed near the substrate and the substrate is 0-30mm.

[0012] Optionally, the thickness of the bubble-breaking plate disposed near the substrate is 6-10 mm, and the thickness of the bubble-breaking plate disposed away from the substrate is 2-6 mm;

[0013] And / or, the opening ratio of the bubble-breaking plate disposed near the substrate is 10-40%, and the opening ratio of the bubble-breaking plate disposed away from the substrate is 20-50%;

[0014] And / or, the equivalent diameter of the bubble-breaking hole on the bubble-breaking plate disposed near the substrate is 1-3 mm, and the equivalent diameter of the bubble-breaking hole on the bubble-breaking plate disposed away from the substrate is 3-6 mm.

[0015] Optionally, the bubble-breaking plate may be one or more of the following shapes: a circular flat plate, a conical plate, an arc-shaped plate, and a corrugated plate.

[0016] And / or, the shape of the bubble breaking hole is one or more of the following: circular, elliptical, triangular, rectangular, polygonal, elongated, fan-shaped, or irregular.

[0017] Optionally, a guide plate is provided at one end of the distribution pipe away from the substrate, the diameter of the guide plate being greater than or equal to the diameter of the distribution pipe, and the liquid phase inlet is formed between the guide plate and the end of the distribution pipe.

[0018] This utility model also provides an upflow reactor, including a reactor shell, a catalyst bed disposed inside the reactor shell, and the aforementioned gas-liquid distribution device. The catalyst bed is located above the substrate of the gas-liquid distribution device, and a plurality of the distribution pipes are disposed at the bottom of the substrate.

[0019] The technical solution provided by this utility model has the following advantages compared with the prior art:

[0020] Based on the gas-liquid distribution device provided by this utility model, after the gas and liquid phases arrive at the gas-liquid distribution device, due to the closed end of the distribution pipe, the liquid phase will bypass the end of the distribution pipe and enter the interior of the distribution pipe from the liquid phase inlet on the outer periphery of the end of the distribution pipe. The gas phase will move upward due to buoyancy and accumulate below the substrate to form a gas cavity. Then, it will enter the distribution pipe through the air inlet hole on the side wall of the distribution pipe and form large bubbles under the action of surface tension. Driven by buoyancy and the upward liquid phase, these large bubbles pass through at least one bubble breaking plate, which breaks the bubbles into smaller bubbles, increasing the bubble breaking effect. These smaller bubbles have a higher specific surface area, and at the same time, it ensures that after the gas and liquid phases enter the catalyst bed above the gas-liquid distribution device, the liquid phase is the continuous phase and the gas phase is the dispersed phase, thereby significantly improving the mass transfer efficiency. Furthermore, the gas-liquid distribution device with this design has a simple structure, avoids redundant structures, and reduces manufacturing and maintenance costs. Attached Figure Description

[0021] The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present invention and, together with the description, serve to explain the principles of the present invention.

[0022] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, for those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0023] Figure 1 This is a schematic diagram of the gas-liquid distribution device according to an embodiment of the present invention;

[0024] Figure 2 This is a top view of the gas-liquid distribution device according to an embodiment of the present invention;

[0025] Figure 3 This is a schematic diagram of the internal structure of the distribution pipe according to an embodiment of the present invention;

[0026] Figure 4 This is a schematic diagram of the structure of the primary crushing plate described in an embodiment of the present invention;

[0027] Figure 5 This is a schematic diagram of the structure of the secondary crushing plate according to an embodiment of the present invention;

[0028] Figure 6 This is a schematic diagram of the internal structure of the upflow reactor described in this embodiment of the invention;

[0029] Figure 7 for Figure 6 A magnified view of a section at point A in the middle;

[0030] Figure 8 This is a front view of the interior of the upflow reactor described in this embodiment of the invention;

[0031] Figure 9 for Figure 8 A magnified view of a section at point B in the middle.

[0032] Explanation of reference numerals in the attached figures

[0033] 1. Substrate; 11. Through hole; 2. Distribution pipe; 21. Liquid phase inlet; 22. Gas phase inlet; 23. Bubble breaking plate; 231. Bubble breaking hole; 232. Primary breaking plate; 233. Secondary breaking plate; 24. Guide plate; 25. Connecting rod; 3. Buffer baffle; 31. Support; 4. Reactor shell; 41. Catalyst bed; 42. Reactor inlet; 43. Reactor outlet. Detailed Implementation

[0034] To better understand the above-mentioned objectives, features, and advantages of this utility model, the solution of this utility model will be further described below. It should be noted that, unless otherwise specified, the embodiments and features of this utility model can be combined with each other.

[0035] The following description sets forth many specific details to provide a full understanding of the present invention, but the present invention may also be implemented in other ways different from those described herein; obviously, the embodiments described in the specification are only some embodiments of the present invention, and not all embodiments.

[0036] Combination Figures 1 to 3As shown, the gas-liquid distribution device provided in this embodiment of the present invention includes a substrate 1 and a plurality of distribution tubes 2 evenly distributed on one side of the substrate 1. Specifically, the plurality of distribution tubes 2 are evenly arranged on the side of the substrate 1 away from the catalyst bed 41, and the number and density of the distribution tubes 2 can be designed according to actual needs. A through hole 11 is provided at the position corresponding to the distribution tube 2 on the substrate 1. The through hole 11 is connected to the cavity of the corresponding distribution tube 2, allowing the liquid phase and gas phase to flow upward through the through hole 11. A liquid phase inlet 21 is provided on the outer periphery of the end of the distribution tube 2 away from the substrate 1. That is, the end of the distribution tube 2 away from the substrate 1 is closed, and a liquid phase inlet 21 is opened on the outer periphery of the end of the distribution tube 2 away from the substrate 1. The liquid phase inlet 21 is connected to the cavity of the distribution tube 2. The method of opening the liquid phase inlet 21 is not limited and can be designed according to actual needs. A gas phase inlet 22 is provided on the side wall of the distribution tube 2. The gas phase inlet 22 penetrates the tube wall of the distribution tube 2, allowing the gas phase to enter the cavity of the distribution tube 2 through the gas phase inlet 22. At least one bubble-breaking plate 23 is provided inside the distribution pipe 2 near the substrate 1. The bubble-breaking plate 23 matches the cross-sectional shape of the cavity of the distribution pipe 2, so that the bubble-breaking plate 23 can be transversely cut inside the cavity of the distribution pipe 2. The bubble-breaking plate 23 is located on the side of the gas phase inlet 22 near the substrate 1. A number of bubble-breaking holes 231 are evenly distributed on the bubble-breaking plate 23, so that large bubbles can be broken into smaller bubbles by the bubble-breaking holes 231 after passing through the bubble-breaking plate 23. The extending direction of the bubble-breaking holes 231 is perpendicular to the plane of the bubble-breaking plate 23. It can be understood that the extending direction of the bubble-breaking holes 231 can be inclined relative to the plane of the bubble-breaking plate 23, and can be designed according to actual needs.

[0037] Based on the gas-liquid distribution device provided by this utility model, after the gas and liquid phases arrive at the gas-liquid distribution device, due to the closed end of the distribution pipe 2, the liquid phase will bypass the end of the distribution pipe 2 and enter the interior of the distribution pipe 2 from the liquid phase inlet 21 on the outer periphery of the end of the distribution pipe 2. The gas phase will move upward due to buoyancy and accumulate below the substrate 1 to form a gas cavity. Then, it will enter the distribution pipe 2 through the air inlet hole on the side wall of the distribution pipe 2 and form large bubbles under the action of surface tension. Driven by buoyancy and the upward liquid phase, these large bubbles pass through at least one bubble breaking plate 23, which breaks the bubbles into smaller bubbles, increasing the bubble breaking effect. These smaller bubbles have a higher specific surface area, and at the same time, it ensures that after the gas and liquid phases enter the catalyst bed 41 above the gas-liquid distribution device, the liquid phase is the continuous phase and the gas phase is the dispersed phase, thereby significantly improving the mass transfer efficiency. In addition, the gas-liquid distribution device with this design has a simple structure, avoids redundant structures, and reduces manufacturing and maintenance costs.

[0038] In some implementations, combined Figure 1 , Figure 6 and Figure 8 As shown, a buffer baffle 3 is provided on the side of the substrate 1 where the distribution pipe 2 is located. The buffer baffle 3 coincides with the central axis of the substrate 1 and is located on the side of the distribution pipe 2 away from the substrate 1. Specifically, the buffer baffle 3 is installed on the bottom of the substrate 1 by a bracket 31, so that the buffer baffle 3 is located below the distribution pipe 2 at the center of the substrate 1. With this design, the buffer baffle 3 can maintain the horizontal state of the liquid level in the gas chamber of the gas-liquid distribution device.

[0039] The stability of the gas-liquid surface is related to the differences in the air and liquid inflow rates of each distribution pipe 2, thus determining the uniformity of the gas-liquid distribution device. Since the gas and liquid phases enter from the reactor inlet 42 at the center of the bottom of the upflow reactor, the velocity at the center of the reactor is relatively high, which disturbs the gas-liquid surface. To avoid this, this invention adds a buffer baffle 3 below the distribution pipe 2 at the center of the upflow reactor, and fixes it to the lower surface of the base plate 1 via a bracket 31. The position and size of the buffer baffle 3 must be reasonably set. If the position of the buffer baffle 3 is too low, the gas and liquid will bypass the buffer baffle 3 and re-converge to form a high-speed central flow, disturbing the gas-liquid surface; if the position of the buffer baffle 3 is too high, its distance from the gas-liquid surface is too close, and the upward flow formed at its edge will also disturb the gas-liquid surface. If the diameter of the buffer baffle 3 is too small, its suppression of the high-speed central flow of the upflow reactor is too weak; if the diameter of the buffer baffle 3 is too large, it will reduce the axial flow area of ​​the upflow reactor, resulting in a larger upward flow velocity at its edge.

[0040] In response, the buffer baffle 3 of this application adopts the following design:

[0041] In some embodiments, the buffer baffle 3 is a circular flat plate with a diameter of 0.5-2m and a thickness of 20-80mm. It is worth noting that the shape of the buffer baffle 3 is schematic; in other specific embodiments, it can be a circular flat plate, a conical plate, an arc plate, a stepped plate, or a perforated plate.

[0042] In some embodiments, the distance between the buffer baffle 3 and the end of the distribution pipe 2 is 0.2-1.2m, that is, the distance between the buffer baffle 3 and the end of the distribution pipe 2 away from the substrate 1 is 0.2-1.2m, in order to meet the above requirements.

[0043] In some implementations, the shape of the buffer baffle 3 is a circular flat plate, a conical plate, an arc plate, a stepped plate, or a perforated plate, which can be designed according to actual needs. Figure 1 The diagram illustrates the case where the shape of the buffer baffle 3 is a circular flat plate. It is understood that in other embodiments, the shape of the buffer baffle 3 may also be a conical plate, an arc plate, a stepped plate, or a perforated plate.

[0044] In some implementations, such as Figure 3As shown, the number of bubble-breaking plates 23 can be one or more. When there are multiple bubble-breaking plates 23, the equivalent diameter of the openings in the multiple bubble-breaking plates 23 decreases from bottom to top. Specifically, when there are multiple bubble-breaking plates 23, the number of bubble-breaking plates 23 can be 2-4, preferably 2. This number of bubble-breaking plates 23 can ensure the bubble-breaking effect and reduce the overall cost of the device. In addition, the distribution pipe 2 includes a pipe body and a top mounting plate. The mounting plate has a certain thickness. When one bubble-breaking plate 23 is provided, the bottom of the mounting plate is provided with a stepped hole. The top end of the pipe body is inserted into the stepped hole, and the bubble-breaking plate 23 is installed at the end of the pipe body and is inserted into the stepped hole along with the pipe body. The stepped surface of the stepped hole limits the connection between the pipe body and the end of the pipe body, increasing the convenience and firmness of the installation.

[0045] When the gas phase enters the distribution pipe 2 through the gas phase inlet 22 on the side wall of the distribution pipe 2, it forms bubbles with a large diameter and a low specific surface area. Driven by buoyancy and the rising liquid phase, these large bubbles enter the catalyst bed 41, causing a portion of the gas phase in the catalyst bed 41 to become a continuous phase, affecting mass transfer efficiency. While reducing the diameter of the gas phase inlet 22 on the side wall of the distribution pipe 2 can create smaller bubbles, this method increases the resistance of the gas phase through-hole and requires higher gas chamber pressure. If the gas phase inlet 22 on the side wall of the distribution pipe 2 is close to the bottom of the distribution pipe 2, the gas chamber will be too high, and the gas phase may enter the distribution pipe 2 through the gap between the distribution pipe 2 and the guide plate 24, resulting in poor distribution uniformity. This invention preferably uses a multi-layer bubble-breaking plate 23 inside the distribution pipe 2 to break up the bubbles and form smaller bubbles.

[0046] In some implementations, reference continues. Figure 3 There are two bubble-breaking plates 23, with a spacing of 10-30 mm between them. The bubble-breaking plate 23 positioned closer to the substrate 1 is 0-30 mm away from the substrate 1. For ease of description, the bubble-breaking plate 23 positioned further away from the substrate 1 is referred to as the primary breaking plate 232, and the bubble-breaking plate 23 positioned closer to the substrate 1 is referred to as the secondary breaking plate 233. The distance between the primary breaking plate 232 and the secondary breaking plate 233 is 10-30 mm, and the distance between the secondary breaking plate 233 and the substrate 1 is 0-30 mm.

[0047] In this design, large bubbles are broken once by the first-stage breaking plate 232, and the broken bubbles are then broken a second time by the second-stage breaking plate 233 to ensure the breaking effect of the bubbles. The distance between the second-stage breaking plate 233 and the substrate 1 is small, specifically the distance between the second-stage breaking plate 233 and the through hole 11 of the substrate 1 is small, to prevent the broken bubbles from re-aggregating.

[0048] In some embodiments, the thickness of the bubble-breaking plate 23 (secondary breaking plate 233) disposed near the substrate 1 is 6-10 mm, and the thickness of the bubble-breaking plate 23 (primary breaking plate 232) disposed away from the substrate 1 is 2-6 mm.

[0049] In some implementations, such as Figure 5 As shown, the bubble-breaking plate 23 (secondary breaking plate 233) disposed near the substrate 1 has an opening ratio of 10-40%, such as... Figure 4 As shown, the opening ratio of the bubble breaking plate 23 (first-stage breaking plate 232) located away from the substrate 1 is 20-50%.

[0050] In some embodiments, the equivalent diameter of the bubble-breaking holes 231 on the bubble-breaking plate 23 (secondary breaking plate 233) disposed near the substrate 1 is 1-3 mm, and the equivalent diameter of the bubble-breaking holes 231 on the bubble-breaking plate 23 (primary breaking plate 232) disposed away from the substrate 1 is 3-6 mm. Preferably, the bubble-breaking holes 231 on the bubble-breaking plate 23 (secondary breaking plate 233) disposed near the substrate 1 are circular with a diameter of 1-3 mm, and the bubble-breaking holes 231 on the bubble-breaking plate 23 (primary breaking plate 232) disposed away from the substrate 1 are circular with a diameter of 3-6 mm.

[0051] In this design, the bubble breaking plate 23 (secondary breaking plate 233) located near the substrate 1 is thicker, has a lower porosity, and a smaller opening diameter than the bubble breaking plate 23 (primary breaking plate 232) located away from the substrate 1. It is used to finally break up the bubbles and form bubbles with smaller diameters.

[0052] In some embodiments, the bubble-breaking plate 23 is shaped as one or more of a circular flat plate, a conical plate, an arc-shaped plate, and a corrugated plate, and can be designed according to actual needs. Preferably, it is combined with... Figure 4 and Figure 5 As shown, both the bubble-breaking plate 23 located near the substrate 1 and the bubble-breaking plate 23 located away from the substrate 1 are preferably circular flat plates.

[0053] In some implementations, reference continues. Figure 4 and Figure 5 The shape of the bubble breaking hole 231 can be one or more of the following: circular, elliptical, triangular, rectangular, polygonal, elongated, or irregular.

[0054] Understandable, Figure 4 and Figure 5In this illustration, the shape of the bubble-breaking plate 23 and the shape of the openings are schematic. In other specific embodiments, the shape of the bubble-breaking plate 23 can be one or more of a circular plate, a conical plate, an arc-shaped plate, and a corrugated plate, and the shape of the openings can be one or more of a circle, an ellipse, a triangle, a rectangle, a polygon, a strip, a fan, or an irregular shape. The irregular shape here refers to an irregular shape. Specifically, the number and size of the bubble-breaking holes 231 are not limited. For example, when the bubble-breaking holes 231 are circular, elliptical, triangular, rectangular, polygonal, strip, or irregular shapes, there can be multiple bubble-breaking holes 231 evenly distributed on the bubble-breaking plate 23; or, for example, when the bubble-breaking holes 231 are fan-shaped, the middle part of the bubble-breaking plate 23 is a circular plate, and the outer periphery is provided with a circular ring. The circular plate and the circular ring are connected by multiple evenly arranged ribs to form a fan-shaped bubble-breaking hole 231 between two adjacent ribs. These are not limiting factors.

[0055] Based on the arrangement of multiple bubble-breaking plates 23, after the gas phase enters the distribution pipe 2 through the gas phase inlet 22 on the side wall of the distribution pipe 2, it will form large bubbles under the action of surface tension. Driven by buoyancy and the upward liquid phase, these large bubbles pass through multiple layers of bubble-breaking plates 23 in sequence. The thickness of the bubble-breaking plates 23 increases layer by layer, and the opening diameter decreases layer by layer, so that the bubbles are broken into smaller bubbles. These smaller bubbles have a higher specific surface area, while ensuring that after the gas and liquid phases enter the catalyst bed 41 above the gas-liquid distribution device, the liquid phase is the continuous phase and the gas phase is the dispersed phase, thereby significantly improving the mass transfer efficiency.

[0056] In some implementations, combined Figure 3 , Figure 7 and Figure 9 As shown, a guide plate 24 is provided at the end of the distribution pipe 2 facing away from the substrate 1. The guide plate 24 is installed at the end of the distribution pipe 2 facing away from the substrate 1 via a connecting rod 25. The diameter of the guide plate 24 is greater than or equal to the diameter of the distribution pipe 2. A liquid inlet 21 is formed between the guide plate 24 and the end of the distribution pipe 2. The gas and liquid phases enter from the reactor inlet 42 and flow upward to the gas-liquid distribution device. The liquid phase enters each distribution pipe 2 through the liquid inlet 21 between the distribution pipe 2 and the guide plate 24. The gas phase continues to move upward due to buoyancy and accumulates below the substrate 1 to form a gas cavity. When the liquid level in the gas cavity is lower than the gas inlet 22 on the side wall of the distribution pipe 2, the gas phase enters the distribution pipe 2 through the gas inlet 22 and then converges with the upward-flowing liquid phase in the distribution pipe 2, and together enters the catalyst bed 41.

[0057] Based on the arrangement of the guide plate 24 and the buffer baffle 3, during operation, the gas and liquid phases enter from the reactor inlet 42 at the bottom of the reactor. After reaching the gas-liquid distribution device, due to the guide plate 24 located below each distribution pipe 2, the liquid phase enters the distribution pipe 2 from the liquid phase inlet 21 between the guide plate 24 and the distribution pipe 2, while the gas phase moves upward due to buoyancy and accumulates below the substrate 1, forming a gas cavity. Subsequently, it enters the distribution pipe 2 through the air inlet hole on the side wall of the distribution pipe 2. Because the center velocity of the upflow reactor is relatively high, this will disturb the liquid surface of the gas cavity formed by the gas-liquid distribution device, resulting in differences in the gas intake of different distribution pipes 2. Based on this, the present invention sets a buffer baffle 3 below the distribution pipe 2 at the center of the upflow reactor to avoid this phenomenon. The position and size of the buffer baffle 3 are reasonably designed to maintain the horizontal state of the liquid surface in the gas cavity under different operating conditions, so that the amount of gas entering each distribution pipe 2 through the gas phase inlet 22 is basically the same. Meanwhile, the cooperation between the buffer baffle 3 and the guide plate 24 ensures that the liquid inlet flow rate of each distribution pipe 2 is basically the same, thereby achieving uniform gas-liquid distribution. In addition, the reasonable configuration of the buffer baffle 3, the guide plate 24, and the bubble breaking plate 23 not only achieves uniform gas-liquid two-phase distribution, but also ensures the stable operation of the gas-liquid distribution device under different operating conditions. This design is suitable for a variety of processes and has broad application prospects.

[0058] This invention also provides an upflow reactor, comprising a reactor shell 4, a catalyst bed 41 disposed inside the reactor shell 4, and the aforementioned gas-liquid distribution device. The catalyst bed 41 is located above the substrate 1 of the gas-liquid distribution device, so that the substrate 1 supports the catalyst bed 41 above it. A plurality of distribution pipes 2 are disposed at the bottom of the substrate 1. The bottom of the reactor shell 4 is provided with a reactor inlet 42, and the top of the reactor shell 4 is provided with a reactor outlet 43.

[0059] Combination Figure 6 and Figure 8 As shown, the upflow reactor provided by this utility model has the advantages of simple structure, low cost, easy manufacturing and installation, uniform gas-liquid distribution, and stable operation for a long time. It can improve the uniform distribution of gas and liquid phases in the upflow reactor, and improve reaction efficiency and product quality.

[0060] The following description uses specific embodiments and comparative examples:

[0061] Example 1:

[0062] The parameters of the upflow reactor and its gas-liquid distribution device in this embodiment are as follows: the reactor shell 4 has a diameter of 4m and a tangential height of 15.6m. A base plate 1 is installed 2.2m above the tangent of the lower end cap of the reactor shell 4. The catalyst bed 41 above the base plate 1 has a height of 11.2m. The distribution pipe 2 has an inner diameter of 40mm, a wall thickness of 3mm, a length of 500mm, and a quantity of 780 pipes. The gas phase inlet 22 on the side wall of the distribution pipe 2 has a diameter of 6mm and is located 150mm from the top of the distribution pipe 2. A guide plate 24 with a diameter of 65mm and a thickness of 3mm is fixed 15mm below the distribution pipe 2 via a connecting rod 25. At the center of the reactor shell 4, 0.422m below the guide plate 24, a buffer baffle 3 with a diameter of 1.02m and a thickness of 60mm is fixed via a bracket 31. The gas and liquid phases enter the reactor shell 4 from the reactor inlet 42 at the bottom of the reactor shell 4, with a gas phase volumetric flow rate of 238m³. 3 / h, liquid phase volumetric flow rate is 609m³ 3 / h.

[0063] This embodiment uses the Eulerian model of Ansys Fluent (fluid simulation) for numerical simulation. The uniformity of gas-liquid distribution is characterized by the distribution non-uniformity calculated by the following formula:

[0064]

[0065] Where N is the number of units driven by distribution pipe 2. Q i It refers to the gas or liquid phase flow rate that enters the catalyst bed 41 through a single distribution pipe 2. Q mean It is the average value of the gas or liquid phase flow rate entering the catalyst bed 41 through a single distribution pipe 2. The value is between 0 and 1. Indicates an ideal uniform distribution. This indicates that all fluids enter the catalyst bed 41 through a single distribution pipe 2. A cross-section is set at the top of each distribution pipe 2, and data extraction and statistics are performed. The results show that the gas phase distribution non-uniformity is 0.1177 and the liquid phase distribution non-uniformity is 0.0740 in this embodiment.

[0066] Comparative Example 1:

[0067] The upflow reactor and its gas-liquid distribution device used in this comparative example are the same as those in Example 1. The difference is that the buffer baffle 3 is not installed below the guide plate 24 at the center of the reactor shell 4. Using the same simulation conditions and data processing method as in Example 1, the gas phase distribution non-uniformity of this comparative example is 0.2111, and the liquid phase distribution non-uniformity is 0.0724.

[0068] Example 2:

[0069] The parameters of the gas-liquid distribution device used in this embodiment are as follows: the inner diameter of the distribution pipe 2 is 40mm, the wall thickness is 3mm, the length is 500mm, the diameter of the air inlet hole on the side wall of the distribution pipe 2 is 4mm, and the distance from the top of the distribution pipe 2 is 150mm. Two layers of bubble breaking plates 23 (divided into a primary breaking plate 232 and a secondary breaking plate 233 from bottom to top) are provided above the gas phase inlet 22 on the inner wall of the distribution pipe 2. The primary breaking plate 232 is 4mm thick, the secondary breaking plate 233 is 8mm thick, the distance between the secondary breaking plate 233 and the substrate 1 is 10mm, the spacing between the primary breaking plate 232 and the secondary breaking plate 233 is 15mm, and the opening shape of all openings is circular. Figure 4 As shown, the primary crushing plate 232 has 37 holes with a diameter of 4mm, resulting in a hole rate of 37%. Figure 5 As shown, the secondary crushing plate 233 has an opening diameter of 2mm, 55 openings, and an opening rate of 13.75%. Gas enters distribution pipe 2 through gas inlet 22 on the side wall of distribution pipe 2 at a flow rate of 0.068m³. 3 The liquid phase enters the distribution pipe 2 from the liquid phase inlet 21 at the bottom of the distribution pipe 2 at a flow rate of 0.181 m³ / h. 3 / h. In this embodiment, the VOF model of Ansys Fluent was used for numerical simulation, and the average diameter of the bubble after passing through two layers of bubble breaking plates 23 was found to be 4.52 mm.

[0070] Comparative Example 2:

[0071] In this comparative example, the gas-liquid distribution device used is the same as that in Example 2, except that two layers of bubble-breaking plates 23 are not installed above the gas phase inlet 22 on the side wall of the distribution pipe 2. Under the same conditions as in Example 2, the average diameter of the bubbles in the distribution pipe 2 in this comparative example is 12.61 mm.

[0072] In summary, the upflow reactor and its gas-liquid distribution device proposed in this utility model can achieve uniform distribution of the gas and liquid phases by setting buffer baffles 3 of appropriate size and position, and can achieve effective bubble breaking by setting multiple layers of bubble breaking plates 23 above the gas phase inlet 22 on the side wall of the distribution pipe 2. Its design is reasonable, avoids redundant structure, and reduces manufacturing and maintenance costs.

[0073] It should be noted that the above embodiments are only a part of this utility model and are used to describe the technical solution of this utility model in detail. They should not be construed as limiting the scope of protection of this utility model.

[0074] The data for the examples and comparative examples are from the Electronic Experiment Recording System (ELN) of Sinopec Research Institute of Petroleum Processing.

[0075]

[0076] It should be noted that, in this document, relational terms such as "first" and "second" are used merely to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or apparatus. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or apparatus that includes said element.

[0077] The above description is merely a specific embodiment of this utility model, enabling those skilled in the art to understand or implement it. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of this utility model. Therefore, this utility model is not to be limited to the embodiments described herein, but is to be accorded the widest scope consistent with the principles and novel features of the utility model described herein.

Claims

1. A gas-liquid distribution device, characterized by, The device includes a substrate (1) and a plurality of distribution tubes (2) evenly distributed on one side of the substrate (1). The substrate (1) is provided with through holes (11) at positions corresponding to the distribution tubes (2). The outer periphery of the distribution tube (2) away from the substrate (1) is provided with a liquid phase inlet (21). The sidewall of the distribution tube (2) is provided with a gas phase inlet (22). The interior of the distribution tube (2) near the substrate (1) is provided with at least one bubble breaking plate (23). The bubble breaking plate (23) is located on the side of the gas phase inlet (22) near the substrate (1). The bubble breaking plate (23) is evenly distributed with a plurality of bubble breaking holes (231).

2. The gas-liquid distribution device of claim 1, wherein, A buffer baffle (3) is provided on the side of the substrate (1) where the distribution tube (2) is located. The buffer baffle (3) coincides with the central axis of the substrate (1) and is located on the side of the distribution tube (2) away from the substrate (1).

3. The gas-liquid distribution device of claim 2, wherein, The diameter of the buffer baffle (3) is 0.5-2m and the thickness is 20-80mm; And / or, the distance between the buffer baffle (3) and the end of the distribution pipe (2) is 0.2-1.2m.

4. The gas-liquid distribution device of claim 2, wherein, The shape of the buffer baffle (3) is a circular flat plate, a conical plate, an arc plate, a stepped plate, or a perforated plate.

5. The gas-liquid distribution device of claim 1, wherein, The number of the bubble breaking plates (23) is one or more, and the equivalent diameter of the openings in the multiple bubble breaking plates (23) decreases from bottom to top.

6. The gas-liquid distribution device of claim 1, wherein, There are two bubble-breaking plates (23), the distance between the two bubble-breaking plates (23) is 10-30mm, and the distance between the bubble-breaking plate (23) located close to the substrate (1) and the substrate (1) is 0-30mm.

7. The gas-liquid distribution device of claim 6, wherein, The thickness of the bubble-breaking plate (23) disposed near the substrate (1) is 6-10 mm, and the thickness of the bubble-breaking plate (23) disposed away from the substrate (1) is 2-6 mm. And / or, the opening ratio of the bubble breaking plate (23) disposed near the substrate (1) is 10-40%, and the opening ratio of the bubble breaking plate (23) disposed away from the substrate (1) is 20-50%; And / or, the equivalent diameter of the bubble breaking hole (231) on the bubble breaking plate (23) disposed near the substrate (1) is 1-3 mm, and the equivalent diameter of the bubble breaking hole (231) on the bubble breaking plate (23) disposed away from the substrate (1) is 3-6 mm.

8. The gas-liquid distribution device of claim 1, wherein, The bubble-breaking plate (23) is shaped as one or more of the following: a circular flat plate, a conical plate, an arc plate, and a corrugated plate. And / or, the shape of the bubble breaking hole (231) is one or more of the following: circular, elliptical, triangular, rectangular, polygonal, elongated, fan-shaped, or irregular.

9. The gas-liquid distribution device of claim 1, wherein, A guide plate (24) is provided at one end of the distribution pipe (2) away from the substrate (1). The diameter of the guide plate (24) is greater than or equal to the diameter of the distribution pipe (2). The liquid phase inlet (21) is formed between the guide plate (24) and the end of the distribution pipe (2).

10. An upflow reactor characterized by, The reactor comprises a reactor shell (4), a catalyst bed (41) arranged inside the reactor shell (4), and a gas-liquid distribution device as claimed in any one of claims 1 to 9, the catalyst bed (41) being arranged above the base plate (1) of the gas-liquid distribution device, and a plurality of distribution tubes (2) being arranged at the bottom of the base plate (1).

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