trickle bed reactor

Abstract

The embodiment of the application provides a kind of trickle bed reactor, it is related to chemical technology field.The trickle bed reactor includes: reactor shell and be arranged in the gas-liquid distributor of reaction cavity, interstage heat exchange structure and multiple layer catalyst bed;Gas-liquid each distributor, interstage heat exchange structure and catalyst bed are sequentially arranged from top to bottom along the height direction of reactor shell, interstage heat exchange structure is arranged between two layers of catalyst bed;Gas-liquid distributor includes cylinder, distribution plate and connecting pipe, distribution plate is fixed to the inner wall of reactor shell, cylinder is arranged on distribution plate, cylinder is provided with multiple communication ports, connecting pipe is inserted on distribution plate and part of connecting pipe is located in cylinder, the outlet of connecting pipe is in the shape of flared mouth, effectively expand the gas-liquid injection diffusion range, so that gas-liquid mixture is evenly sprayed in the shape of umbrella, further refine liquid drop, disperse airflow, improve the problem of uneven radial gas-liquid distribution of catalyst bed.

Description

Technical Field

[0001] This application relates to the field of chemical technology, and in particular to a trickle bed reactor. Background Technology

[0002] In the hydrogenation reaction of dimethyl terephthalate, a dimethyl terephthalate solution and hydrogen are introduced into a trickle bed reactor, where they react with a catalyst to produce high-value-added chemicals (such as dimethyl cyclohexanedicarboxylate).

[0003] In related technologies, a trickle bed reactor includes a reactor shell, from top to bottom, a gas-liquid distributor and a catalyst bed. The gas-liquid distributor is equipped with a sieve plate. After the liquid and gaseous materials enter the gas-liquid distributor, they are radially distributed through the sieve plate and then drip onto the catalyst bed for reaction.

[0004] However, traditional gas-liquid distributors are prone to liquid aggregation, resulting in uneven radial gas-liquid distribution in the catalyst bed and causing local overheating of the reaction. Summary of the Invention

[0005] This application provides a trickle bed reactor to overcome the problem in the prior art where the gas-liquid distributor is prone to liquid aggregation, resulting in uneven gas-liquid distribution, uneven radial temperature distribution, and local overheating in the catalyst bed, thereby reducing the service life of the catalyst.

[0006] This application provides a trickle bed reactor, including: a reactor shell, a gas-liquid distributor, an inter-stage heat exchange structure, and a multi-layer catalyst bed.

[0007] The reactor shell has a reaction chamber and a feed inlet communicating with the reaction chamber. The gas-liquid distributor, the catalyst bed and the inter-stage heat exchange structure are all disposed in the reaction chamber and arranged sequentially from top to bottom along the height direction of the reactor shell. The inter-stage heat exchange structure is disposed between the two catalyst bed layers and is used to receive the material output from the upper catalyst bed for heat exchange.

[0008] The gas-liquid distributor includes a cylinder, a distribution plate, and a connecting pipe. The edge of the distribution plate is attached to the inner wall of the reactor shell. The cylinder is disposed on the distribution plate and has multiple connecting ports. The connecting pipe is inserted into the distribution plate and part of the connecting pipe is located inside the cylinder. The connecting ports are used to connect the feed inlet and the connecting pipe. The outlet of the connecting pipe is funnel-shaped.

[0009] In one possible implementation, the connecting pipe is tapered, with its small-diameter end located inside the cylinder, forming an annular channel with the interior of the cylinder, the connecting port communicating with the annular channel, and its large-diameter end located outside the cylinder.

[0010] In one possible implementation, the connecting pipe and the cylinder form a communication group, and multiple communication groups are provided, with the multiple communication groups evenly distributed on the distribution plate.

[0011] The inclination angle of the connecting pipe is greater than or equal to 20° and less than or equal to 60°.

[0012] Multiple connecting ports are spaced apart along the circumference of the cylinder, and the connecting ports are slits.

[0013] In one possible implementation, a gas distributor and a liquid distributor are further included. The feed inlet includes a gas inlet and a liquid inlet. The gas distributor and the liquid distributor are arranged sequentially from top to bottom in the reaction chamber along the height direction of the reactor shell and are located above the gas-liquid distributor. The gas distributor is connected to the gas inlet, and the liquid distributor is connected to the liquid inlet. The liquid distributor is also connected to the connecting pipe through the connecting port.

[0014] In one possible implementation, the gas distributor includes a plurality of conical tubes arranged sequentially from the inside to the outside along the radial direction of the reactor shell, forming a gas delivery channel between adjacent conical tubes, and the diameter of each conical tube gradually increases from top to bottom along the height direction of the reactor shell.

[0015] Along the height direction of the reactor shell, the upper port positions of each layer of cone tubes are arranged in a stepped manner from top to bottom, and decrease layer by layer from the outside to the inside. The upper port of the outermost cone tube is connected to the gas inlet.

[0016] In one possible implementation, at least three conical tubes are provided, the included angle between adjacent conical tubes is greater than or equal to 6° and less than or equal to 14°, and the ratio of the diameter of the reactor shell to the diameter of the conical tube is greater than or equal to 1.5 and less than or equal to 4.

[0017] In one possible implementation, the liquid distributor includes a feed element and a plurality of distributing elements. The feed element is connected to the liquid inlet, and the distributing elements are connected to the feed element and located below the feed element. The plurality of distributing elements are spaced apart along the extension direction of the feed element, and the outlet of the distributing element is connected to the connecting port. The distributing elements are used to uniformly disperse the material.

[0018] In one possible implementation, the feeding component includes a feeding body and a sieve plate. The sieve plate is disposed in the feeding body and is divided within the feeding body to form an overflow trough. The sieve plate is connected to the liquid inlet. An opening is provided on the side wall of the feeding body for connecting the overflow trough and the distributing component.

[0019] In one possible implementation, a plurality of the material distribution components are connected to the feeding body and spaced apart along the extending direction of the feeding body. Each material distribution component has a flow-diverting groove, and the flow-diverting groove on each material distribution component is positioned corresponding to the position of each of the openings. Each material distribution component has a flow-diverting hole, which is used to connect the flow-diverting groove and the connecting port.

[0020] In one possible implementation, the opening is located above the sieve plate.

[0021] The diversion holes are spaced apart along the extension direction of the material distribution component, and the diversion holes are located near the top of the material distribution component.

[0022] In one possible implementation, the inter-segment heat exchange structure includes a gas-liquid pre-distributor and a heat exchanger arranged sequentially from top to bottom along the height direction of the reactor shell. The heat exchanger is in communication with the gas-liquid pre-distributor. The gas-liquid pre-distributor is disposed between two catalyst bed layers. The gas-liquid pre-distributor is used to receive the gas-liquid mixture after reaction in the upper catalyst bed layer. The heat exchanger is used to receive the gas-liquid mixture flowing out of the gas-liquid pre-distributor and perform heat exchange.

[0023] In one possible implementation, the gas-liquid pre-distribution component includes a connecting plate and a plurality of conduits, the outer periphery of the connecting plate being fitted to the inner wall of the reactor shell, and the conduits being inserted into the connecting plate and extending toward the heat exchanger.

[0024] The heat exchanger includes a receiving plate and multiple tubes. The outer periphery of the receiving plate is attached to the inner wall of the reactor shell. The receiving plate has a receiving cavity. The tubes are inserted into the receiving plate and partially located in the receiving cavity. The ports of the tubes located in the receiving cavity are V-shaped. The receiving plate is used to receive the gas-liquid mixture flowing out through the conduit.

[0025] In one possible implementation, the conduit is disposed within the receiving cavity, the conduit is arranged alternately with the tubes, and a portion of the conduit is inserted into the gap between two adjacent tubes.

[0026] In one possible implementation, the distance between the port of the conduit facing the receiving plate and the port of the tube facing the connecting plate is greater than or equal to 5 mm and less than or equal to 50 mm.

[0027] This application provides a trickle bed reactor. By sequentially arranging a gas-liquid distributor, a catalyst bed, and an inter-stage heat exchange structure along the height direction within the reactor shell, and utilizing the cooperation of the cylinder, distribution plate, and funnel-shaped connecting pipe at the outlet, the gas-liquid material entering through the feed inlet is first uniformly distributed through multiple sets of connecting ports on the side wall of the cylinder before entering the catalyst bed, suppressing flow deviation. Furthermore, the funnel-shaped outlet of the connecting pipe expands the gas-liquid spray diffusion range, spraying downwards in an umbrella-like uniform manner, further refining the droplets and dispersing the airflow, thus improving the problems of uneven radial gas-liquid distribution and local overheating in the lower catalyst bed. Attached Figure Description

[0028] The accompanying drawings, which are incorporated in and form part of this specification, illustrate embodiments consistent with this application and, together with the description, serve to explain the principles of this application.

[0029] Figure 1 This is a schematic diagram of the structure of the trickle bed reactor provided in this application;

[0030] Figure 2 for Figure 1 The front view of the gas-liquid distributor in the trickle bed reactor provided in the image;

[0031] Figure 3 for Figure 1 A top view of the gas-liquid distributor in the trickle bed reactor provided in the image;

[0032] Figure 4 for Figure 1 The schematic diagram of the gas distributor in the trickle bed reactor provided in the image;

[0033] Figure 5 for Figure 1 The schematic diagram of the liquid distributor in the trickle bed reactor provided in the image;

[0034] Figure 6 for Figure 1 A schematic diagram of the gas-liquid pre-distribution component in the trickle bed reactor provided in the diagram;

[0035] Figure 7 for Figure 1 The diagram shows the structure of the heat exchanger in the trickle bed reactor provided in the image.

[0036] Explanation of reference numerals in the attached figures:

[0037] 100 - Reactor shell; 110 - Reaction chamber; 120 - Feed inlet; 121 - Gas inlet; 122 - Liquid inlet; 130 - Discharge outlet;

[0038] 200 - Gas-liquid distributor; 210 - Cylinder; 211 - Connecting port; 220 - Distribution plate; 230 - Connecting pipe; 240 - Annular channel;

[0039] 300-catalyst bed;

[0040] 400 - Gas distributor; 410 - Cone tube; 420 - Gas delivery channel;

[0041] 500-Liquid distributor; 510-Feeding component; 511-Feeding body; 5111-Opening; 512-Sieve plate; 520-Distribution component; 521-Distribution channel; 5211-Distribution hole; 530-Overflow channel; 540-Reinforcing rod;

[0042] 600 - Inter-section heat exchange structure; 610 - Gas-liquid pre-distribution component; 611 - Connecting plate; 612 - Conduit; 620 - Heat exchange component; 621 - Receiving plate; 6211 - Receiving cavity; 622 - Tube set.

[0043] The accompanying drawings illustrate specific embodiments of this application, which will be described in more detail below. These drawings and descriptions are not intended to limit the scope of the concept in any way, but rather to illustrate the concept of this application to those skilled in the art through reference to particular embodiments. Detailed Implementation

[0044] Exemplary embodiments will now be described in detail, examples of which are illustrated in the accompanying drawings. When the following description relates to the drawings, unless otherwise indicated, the same numbers in different drawings denote the same or similar elements. The embodiments described in the following exemplary embodiments do not represent all embodiments consistent with this application. Rather, they are merely examples of apparatuses and methods consistent with some aspects of this application.

[0045] The terms "first," "second," "third," etc. (if present) in the specification, claims, and accompanying drawings of this application are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence. It should be understood that such data can be interchanged where appropriate so that the embodiments of this application described herein can be implemented in orders other than those illustrated or described herein.

[0046] Secondly, it should be noted that in the description of this application, the terms "inner", "outer", "first direction", "second direction", etc., indicating the direction or positional relationship are based on the direction or positional relationship shown in the drawings. This is only for the convenience of description and does not indicate or imply that the device or component must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, it should not be construed as a limitation of this application.

[0047] Furthermore, it should be noted that, in the description of this application, unless otherwise expressly specified and limited, the terms "connected" and "linked" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection between two components. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances.

[0048] The trickle bed reactor belongs to the technical field of gas-liquid-solid three-phase reaction equipment. It is often used in strongly exothermic hydrogenation processes such as the hydrogenation of dimethyl terephthalate to achieve continuous contact reaction of hydrogen, dimethyl terephthalate solution and catalyst.

[0049] In related technologies, trickle bed reactors are typically equipped with a feed inlet, a gas-liquid distribution component, and a catalyst bed. The material is dispersed from top to bottom through the gas-liquid distribution component and enters the trickle bed reactor, where mass transfer, heat transfer, and hydrogenation conversion are completed within the catalyst bed.

[0050] Among them, the trickle bed reactor is the main equipment. The gas phase and liquid phase usually enter from the top of the trickle bed reactor. After being initially dispersed by distribution components such as sieve plates and bubble caps, they flow into the catalyst bed and undergo an exothermic reaction in the catalyst bed. In order to suppress the temperature rise, the system is also often equipped with external heat exchange equipment and connecting pipelines between sections to cool the material before guiding it back to the subsequent reaction zone.

[0051] However, in sieve-type gas-liquid distribution components, the liquid phase is sprayed through the sieve holes only. Under the action of liquid surface tension, it is easy for the liquid to converge into large droplets and liquid streams on the plate surface and at the outlet of the channel. In bubble cap structures, the gas-liquid contact space is narrow, and the liquid phase is easy to flow in sheets along the outer wall of the bubble cap, unable to be broken into small and uniform droplets, resulting in local liquid enrichment. This causes local liquid overload in the bed, resulting in uneven gas-liquid distribution in the catalyst bed. Consequently, it causes radial mass transfer differences and temperature field imbalance in the bed, making it easier for local areas to overheat, affecting reaction stability and product selectivity.

[0052] In addition, inter-stage heat exchange relies on external equipment and long pipelines, resulting in a large number of devices, complex pipelines, poor structural compactness, and problems such as increased pressure drop, increased heat loss, and lag in temperature response, which are not conducive to axial temperature control and efficient operation of the trickle bed reactor.

[0053] To address the aforementioned issues, this application provides a trickle bed reactor, comprising: a reactor shell, a gas-liquid distributor, an inter-stage heat exchange structure, and a multi-layer catalyst bed.

[0054] The reactor shell has a reaction chamber and a feed inlet connected to the reaction chamber. The gas-liquid distributor, catalyst bed and inter-stage heat exchange structure are all located in the reaction chamber and are arranged sequentially from top to bottom along the height of the reactor shell. The inter-stage heat exchange structure is located between two catalyst bed layers and is used to receive the material output from the upper catalyst bed for heat exchange.

[0055] The gas-liquid distributor includes a cylinder, a distribution plate, and a connecting pipe. The edge of the distribution plate is attached to the inner wall of the reactor shell. The cylinder is set on the distribution plate and has multiple connecting ports. The connecting pipe is inserted into the distribution plate and part of the connecting pipe is located inside the cylinder. The connecting ports are used to connect the feed inlet and the connecting pipe. The outlet of the connecting pipe is funnel-shaped.

[0056] By sequentially arranging a gas-liquid distributor, a catalyst bed, and an inter-stage heat exchange structure along the height direction within the reactor shell, and utilizing the cooperation of the cylinder, distribution plate, and funnel-shaped connecting pipe at the outlet, the gas-liquid material entering through the feed inlet is first evenly distributed through multiple sets of connecting ports on the side wall of the cylinder before entering the catalyst bed, suppressing flow deviation. Furthermore, the funnel-shaped outlet of the connecting pipe expands the gas-liquid spray diffusion range, spraying downwards in an umbrella-like uniform manner, further refining droplets and dispersing the airflow, thus improving the problem of uneven radial gas-liquid distribution and localized overheating in the lower catalyst bed.

[0057] In addition, by placing the inter-stage heat exchange mechanism between the two catalyst bed layers, heat exchange is carried out using the inter-stage heat exchange mechanism, which shortens the inter-stage process and reduces the equipment volume and floor space.

[0058] The technical solution of this application and how the technical solution of this application solves the above-mentioned technical problems are described in detail below with specific embodiments. These specific embodiments can be combined with each other, and the same or similar concepts or processes may not be described again in some embodiments. The embodiments of this application will now be described with reference to the accompanying drawings.

[0059] This application provides a trickle bed reactor, combined with... Figure 1 , Figure 2 and Figure 3 As shown, it includes: reactor shell 100, gas-liquid distributor 200, inter-stage heat exchange structure 600 and catalyst bed 300.

[0060] The reactor shell 100 has a reaction chamber 110 and a feed inlet 120 communicating with the reaction chamber 110. The gas-liquid distributor 200, the catalyst bed 300 and the inter-stage heat exchange structure 600 are all disposed in the reaction chamber 110 and arranged sequentially from top to bottom along the height direction of the reactor shell 100. The inter-stage heat exchange structure 600 is disposed between the two catalyst bed layers 300 and is used to receive the material output from the upper catalyst bed 300 for heat exchange.

[0061] The gas-liquid distributor 200 includes a cylinder 210, a distribution plate 220, and a connecting pipe 230. The edge of the distribution plate 220 is attached to the inner wall of the reactor shell 100. The cylinder 210 is disposed on the distribution plate 220 and has multiple connecting ports 211. The connecting pipe 230 is inserted into the distribution plate 220 and part of the connecting pipe 230 is located inside the cylinder 210. The connecting ports 211 are used to connect the feed inlet 120 and the connecting pipe 230. The outlet of the connecting pipe 230 is funnel-shaped.

[0062] The reactor shell 100 has a reaction chamber 110 inside for introducing, distributing and reacting gaseous and liquid materials. An inlet 120 and an outlet 130 communicating with the reaction chamber 110 are provided on the shell so that external gaseous raw materials, liquid raw materials or gas-liquid mixtures can enter the reaction system.

[0063] The gas-liquid distributor 200 is a fluid distribution component installed on the upper part of the reaction chamber 110 for guiding, dispersing, and uniformly distributing gaseous and liquid materials entering the reactor shell 100. The gas-liquid distributor 200 works in conjunction with the catalyst bed 300 to ensure that the material forms a relatively uniform circumferential and radial distribution before entering the catalyst bed 300.

[0064] Reference Figure 1 As shown, the gas-liquid distributor 200 is located downstream of the feed inlet 120 and above the catalyst bed 300. The cylinder 210 is fixed on the distribution plate 220. The edge of the distribution plate 220 is attached to the inner wall of the reactor shell 100 to define the distribution area. The connecting pipe 230 passes through the distribution plate 220 and partially extends into the cylinder 210 to form a guide channel from the feed inlet 120 to the downstream area.

[0065] Specifically, refer to Figure 2 As shown, the cylinder 210 refers to the cylindrical component set above or on the upper part of the distribution plate 220. The cylinder 210 is used to temporarily confine the gas-liquid material from the feed inlet 120 within a certain flow area, and guide the material to the connecting pipe 230 through multiple connecting ports 211 to achieve multi-point diversion and preliminary pressure equalization.

[0066] The distribution plate 220 refers to a plate-shaped component that is set at the lower part of the cylinder 210 and is used to support the cylinder 210, fix the connecting pipe 230, and define the gas-liquid distribution position. The edge of the distribution plate 220 is attached to the inner wall of the reactor shell 100, thereby forming a relatively stable installation reference and fluid distribution boundary within the reactor shell 100.

[0067] The connecting pipe 230 is a tubular flow guiding component inserted into the distribution plate 220. The connecting pipe 230 is partially located inside the cylinder 210 and guides the material inside the cylinder 210 to the catalyst bed 300. The outlet of the connecting pipe 230 is funnel-shaped, so that the fluid forms a diffused flow stream when leaving the connecting pipe 230 and reduces the high-speed jet phenomenon.

[0068] The catalyst bed 300 refers to a fixed-bed reaction zone located below the gas-liquid distributor 200, used to support the catalyst and facilitate contact and reaction between the gas and liquid phases. The catalyst bed 300 receives gas-liquid materials uniformly introduced from the gas-liquid distributor 200 in a drip-flow state, and mass transfer, heat transfer, and reaction are achieved within the bed pores.

[0069] Specifically, refer to Figure 2 As shown, the cylinder 210 is fixedly connected to the distribution plate 220. The distribution plate 220 separates the upper cylinder 210 from the lower catalyst bed 300. The cylinder 210 has multiple connecting ports 211 that are connected to the feed port 120 and the connecting pipe 230. One end of the connecting pipe 230 is connected to the distribution plate 220 and extends into the cylinder 210, while the other end is set towards the catalyst bed 300. The connecting pipe 230 forms a flow path from the connecting port 211 to the space above the catalyst bed 300. Multiple connecting pipes 230 can be distributed to correspond to different areas of the catalyst bed 300.

[0070] Understandably, after the external gaseous and liquid materials enter the reaction chamber 110 through the feed inlet 120, they first fall onto the distribution plate 220. The gaseous materials can enter the corresponding cylinder 210 through the connecting port 211 and undergo a certain degree of buffering and diffusion within the local space defined by the cylinder 210. Subsequently, under the action of pressure difference, the liquid materials on the distribution plate 220 are drawn in, enter the corresponding connecting pipe 230 through the connecting port 211, and then diffuse out through the funnel-shaped outlet of the connecting pipe 230, so that the originally possible concentrated jet is dispersed into multiple relatively uniform streams, thereby enabling the gaseous and liquid materials to obtain a more balanced circumferential distribution and radial spread before entering the catalyst bed 300.

[0071] In addition, the local velocity gradient of the material flowing in the connecting pipe 230 can be smoothly transitioned, and it is not easy to form strong scouring and local deviation after flowing out. When it enters the catalyst bed 300, it can contact the upper surface of the catalyst bed 300 more evenly, avoiding local overheating.

[0072] It should be understood that the above examples are for demonstration purposes only and are not limiting. The specific structural forms, connection methods and material selections of the cylinder 210, distribution plate 220 and connecting pipe 230 can be appropriately changed without departing from the spirit of this application.

[0073] In one possible implementation, such as Figure 2and Figure 3 As shown, the connecting pipe 230 is tapered, with its small-diameter end located inside the cylinder 210. The small-diameter end of the connecting pipe 230 forms an annular channel 240 with the inside of the cylinder 210, and the connecting port 211 communicates with the annular channel 240. The large-diameter end of the connecting pipe 230 is located outside the cylinder 210.

[0074] Among them, the connecting pipe 230 is a fluid introduction component with a gradually expanding structure along the axial cross section.

[0075] Understandably, in combination Figure 2 and Figure 3 As shown, an annular channel 240 is formed between the connecting pipe 230 and the cylinder 210. The material enters the annular channel 240 from the connecting port 211 on the side wall of the cylinder 210. The tapered connecting pipe 230 is narrow at the top and wide at the bottom. As the fluid flows from the small diameter end to the large diameter end, the flow cross-section continuously expands. The fluid velocity in the connecting pipe 230 decreases along the path, while the static pressure increases. The annular channel 240 is a narrow annular slit with a small flow cross-sectional area. The gas and liquid have a higher flow velocity and a lower static pressure in the annular channel 240. As a result, a stable pressure difference is formed between the annular channel 240 and the inner cavity of the tapered connecting pipe 230.

[0076] The low-pressure annular channel 240 will continuously draw liquid material adhering to the wall of the cylinder 210 and the distribution plate 220, and promptly draw the accumulated liquid into the annular channel 240 and then into the connecting pipe 230, thus preventing the liquid from stagnating on the inner wall of the cylinder 210 and the surface of the distribution plate 220, and from accumulating into a large liquid film or liquid column.

[0077] Specifically, the small-diameter end of the connecting pipe 230 can be placed inside the cylinder 210 and enclosed to form an annular channel 240 that communicates with the connecting port 211. When the fluid flows through the conical connecting pipe 230, the flow cross-section gradually expands and the static pressure increases. The fluid velocity in the annular slit channel is fast and the static pressure is lower. The two form a stable pressure difference, which can continuously suction the liquid phase retained on the inner wall of the cylinder 210 and the distribution plate 220, avoiding liquid phase adhesion and aggregation, and large-area agglomeration. At the same time, the annular channel 240 realizes the circumferential pre-uniform distribution of materials, eliminates airflow vortices and gas deviation, and, together with the conical gradually expanding pipe, shears and breaks up the gas and liquid phases and diffuses them radially. Compared with the traditional sieve plate and bubble cap distribution structure, it effectively improves the problem of uneven radial gas and liquid distribution in the catalyst bed 300, eliminates defects such as local overheating, improves catalyst utilization and reaction conversion efficiency, and extends the continuous operation cycle of the reactor.

[0078] Furthermore, refer to Figure 3 As shown, the connecting pipe 230 and the cylinder 210 form a connecting group, and multiple connecting groups are provided, which are evenly distributed on the distribution plate 220.

[0079] It is understandable that multiple sets of connecting groups consisting of cylinder 210 and connecting pipe 230 can be arranged on the same distribution plate 220, and all connecting groups are evenly arrayed along the circumference and radial direction of the distribution plate 220, dividing the entire cross-section of the reactor shell 100 into multiple independent and equal gas-liquid distribution units. The gas and liquid feed is evenly distributed to each group for independent distribution, avoiding radial deviation caused by single-point concentration of material.

[0080] Each set of interconnected annular channels 240 can simultaneously form a differential pressure suction distribution plate 220 to retain liquid phase material, thereby achieving full-area suppression of liquid aggregation; and after diversion, the fluid load of each connecting pipe 230 is reduced, the gas-liquid shearing and crushing effect is better, and the gas-liquid ratio of the entire cross section of the catalyst bed 300 is more uniform.

[0081] In one possible implementation, the inclination angle of the connecting pipe 230 is greater than or equal to 20° and less than or equal to 60°. This setting ensures sufficient flow guidance and diffusion within this angle range, while avoiding situations where the inclination angle is too small, resulting in insignificant flow guidance, or too large, leading to increased local resistance and poor fluid return.

[0082] In one possible implementation, a plurality of connecting ports 211 are arranged at intervals along the circumference of the cylinder 210, and the connecting ports 211 are slits.

[0083] The slots can be any one of straight slots, arc slots, or staggered slots, or a combination thereof, and the slots are arranged at intervals along the circumference of the cylinder 210 to form multiple discrete liquid inlet channels.

[0084] Understandably, the gas-liquid mixture from the feed inlet 120 first enters the cylinder 210 region located above the distribution plate 220, and then enters the corresponding connecting group through multiple slotted connecting ports 211 spaced apart along the circumference of the cylinder 210. Since the multiple connecting groups are evenly distributed on the distribution plate 220, the material is dispersed and introduced into connecting pipes 230 at different locations on the distribution plate 220. Each connecting pipe 230, under the action of its inclined angle, forms a directional flow and secondary diffusion for the material, so that when the material enters the downstream space, it is no longer concentrated and sprayed in a single direction, but rather dispersed and spread along multiple oblique pathways. This effectively suppresses flow deviation, local jetting, and liquid coalescence, improves the uniformity of gas-liquid distribution at the catalyst bed 300 inlet, thereby reducing radial mass transfer differences and local temperature fluctuations in the catalyst bed 300. This allows the trickle bed reactor to maintain a more stable reaction state under strongly exothermic hydrogenation conditions, and is beneficial for improving product selectivity and the reliability of continuous operation.

[0085] It should be understood that the above examples are for demonstration purposes only and are not limiting. Specific parameters and structural forms can be adjusted according to actual process conditions.

[0086] In one possible implementation, combining Figure 1 and Figure 4 As shown, it also includes a gas distributor 400 and a liquid distributor 500. The feed inlet 120 includes a gas feed inlet 121 and a liquid feed inlet 122. The gas distributor 400 and the liquid distributor 500 are arranged sequentially from top to bottom in the reaction chamber 110 along the height direction of the reactor shell 100 and are located above the gas-liquid distributor 200. The gas distributor 400 is connected to the gas feed inlet 121, and the liquid distributor 500 is connected to the liquid feed inlet 122. The liquid distributor 500 is also connected to the connecting pipe 230 through the connecting port 211.

[0087] Gas distributor 400 is a component used to distribute gaseous materials entering reaction chamber 110, and liquid distributor 500 is a component used to pre-disperse and uniformly distribute liquid materials entering reaction chamber 110.

[0088] It is understandable that the gas distributor 400 and the liquid distributor 500 can be used to pre-rectify and homogenize the gaseous and liquid materials before they enter the gas-liquid distributor 200, thereby reducing the flow deviation, agglomeration and local accumulation caused by the direct impact of the two phases, and making the distribution of materials entering the catalyst bed 300 through the gas-liquid distributor 200 more stable.

[0089] Specifically, refer to Figure 1 As shown, gaseous materials can first enter the gas distributor 400 through the gas inlet 121, and after diffusion, deceleration and uniform distribution inside the gas distributor 400, they enter the gas-liquid distributor 200 in a relatively uniform state; liquid materials enter the liquid distributor 500 through the liquid inlet 122, and after further distribution and rectification inside the liquid distributor 500, they enter the gas-liquid distributor 200.

[0090] This configuration allows the gas and liquid phases to undergo upstream pre-distribution, rectification, and secondary uniform distribution processes, which can effectively reduce local impacts and flow concentration, improve the gas-liquid contact state before entering the catalyst bed 300, thereby reducing radial distribution differences and local temperature rise fluctuations within the catalyst bed 300, and improving reaction stability and operational continuity under strongly exothermic hydrogenation conditions.

[0091] It should be understood that the above examples are for illustrative purposes only and are not intended to be limiting.

[0092] In one possible implementation, such as Figure 4 As shown, the gas distributor 400 includes multiple cone tubes 410. Along the radial direction of the reactor shell 100, the multiple cone tubes 410 are sequentially arranged from the inside to the outside, and a gas delivery channel 420 is formed between adjacent cone tubes 410. Along the height direction of the reactor shell 100, the diameter of each cone tube 410 gradually increases from top to bottom.

[0093] Reference Figure 4 As shown, the multi-layer cone tubes 410 are arranged concentrically from the inside to the outside, and the sandwich between two adjacent layers of cone tubes 410 forms an annular gas transmission channel 420; all cone tubes 410 are gradually expanding cones that are narrow at the top and wide at the bottom, and the diameter of the tubes gradually increases from top to bottom. The multi-layer annular gas transmission channel 420 synchronously transports the gas phase in layers.

[0094] This configuration distributes the gas from the gas inlet 121 into the reactor cross section layer by layer along radial and axial paths, allowing the gas to undergo velocity attenuation, pressure homogenization, and flow reforming before entering the catalyst bed 300. The gently decelerating airflow prevents high-speed airflow from directly impacting the catalyst bed 300, thus avoiding splashing and local gas-liquid imbalance caused by impacting the liquid phase.

[0095] In one possible implementation, combining Figure 1 and Figure 4 As shown, along the height direction of the reactor shell 100, the upper port positions of each layer of cone tubes 410 are arranged in a stepped manner from top to bottom, and decrease layer by layer from the outside to the inside. The upper port of the outermost cone tube 410 is connected to the gas inlet 121.

[0096] Combination Figure 1 and Figure 4 As shown, the upper ports of the multi-layered cone tubes 410 are arranged in a staggered manner along the height of the shell. Among them, the upper port of the outermost ring of cone tubes 410 is closed and connected to the gas inlet 121. The gaseous material will first be completely introduced into the top chamber of the outermost cone tube 410. With the arrangement of the upper ports decreasing from the outside to the inside, the gaseous material will be diverted from the outside to the inside into the annular gas conveying channel 420 between the adjacent cone tubes 410.

[0097] Specifically, the gaseous material enters the outermost cone tube 410 through the gas inlet 121 and flows step by step in the gas delivery channel 420 formed between each cone tube 410. The velocity of the gaseous material is gradually reduced, the pressure distribution tends to be balanced, and the phenomena of flow deviation, local concentration and jetting are avoided. It also helps to improve the stability of gas-liquid contact in the bed and the uniformity of the reaction temperature field, thereby providing more stable operating conditions for the strongly exothermic hydrogenation process.

[0098] It should be understood that the above examples are for illustrative purposes only and are not intended to be limiting.

[0099] Furthermore, at least three cone tubes 410 are provided, the included angle between adjacent cone tubes 410 is greater than or equal to 6° and less than or equal to 14°, and the ratio of the diameter of the reactor shell 100 to the diameter of the cone tube 410 is greater than or equal to 1.5 and less than or equal to 4.

[0100] Understandably, by controlling the included angle between adjacent cone tubes 410 within this range, the expansion rate of the cone tubes 410 will neither be too slow to weaken the dispersion effect, nor too fast to cause obvious eddies, separation flow or additional pressure drop.

[0101] Furthermore, the ratio of the diameter of the reactor shell 100 to the diameter of the cone tube 410 is not less than 1.5, which allows for the reservation of an outer ring buffer gas supply area between the outermost cone tube 410 and the shell, eliminating the dry bed on the reactor wall; a ratio of not more than 4 ensures that the multiple cone tubes 410 occupy the main flow section of the reactor shell 100, avoiding insufficient central gas supply and disordered gas flow.

[0102] This configuration, combined with the external high-heat-reducing and internal low-heat-reducing stepped cone tube 410 upper port structure, enables fine and uniform stratification of the gas phase along the radial direction of the reactor shell 100, without gas deviation or vortex. This helps to reduce local load differences and temperature fluctuations in the catalyst bed 300, thereby improving the stable operation and process controllability of the trickle bed reactor under strong exothermic conditions.

[0103] In one possible implementation, combining Figure 1 and Figure 5 As shown, the liquid distributor 500 includes a feed element 510 and multiple distribution elements 520. The feed element 510 is connected to the liquid inlet 122, and the distribution elements 520 are connected to the feed element 510 and located below the feed element 510. The multiple distribution elements 520 are spaced apart along the extension direction of the feed element 510. The outlet of the distribution element 520 is connected to the connecting port 211. The distribution elements 520 are used to uniformly disperse the material.

[0104] Reference Figure 5 As shown, the feeder 510 can be understood as the liquid collection and primary distribution component in the liquid distributor 500, which is used to receive the liquid material entering through the liquid inlet 122 and guide it into multiple distribution components 520.

[0105] Multiple feeder units 520 are secondary distribution units that cooperate with feeder unit 510 to further divert, disperse and uniformly output the liquid from feeder unit 510.

[0106] In one possible implementation, the feeder 510 may be made into a tubular, trough-shaped, or box-shaped structure.

[0107] The distribution component 520 can adopt a branch pipe type, a flow channel type 521, or a distribution nozzle type structure to adapt to different liquid flow rates and distribution requirements. It should be understood that the above examples are for demonstration purposes only and are not limiting.

[0108] Specifically, multiple distribution components 520 are spaced apart along the extension direction of the feed component 510. When the liquid phase enters each distribution component 520, it can avoid concentrated falling, reduce local jetting and excessively thick liquid film, thereby making the liquid flow rate entering the connecting port 211 more balanced. With this configuration, the liquid distributor 500 can be converted from single-point or few-point input through the liquid inlet 122 to multi-point, staged, and dispersed output, so that the liquid is initially uniformly distributed before entering the gas-liquid distributor 200. This reduces the local overload problem at the inlet of the catalyst bed 300 and helps to suppress temperature fluctuations caused by uneven radial distribution, improving the operational stability and mass transfer uniformity of the trickle bed reactor under strongly exothermic hydrogenation conditions.

[0109] It should be noted that the above embodiments are only used to illustrate the technical concept of this application. It should be understood that the above examples are only demonstrations and not limitations.

[0110] Furthermore, refer to Figure 5 As shown, the feeding component 510 includes a feeding body 511 and a sieve plate 512. The sieve plate 512 is disposed in the feeding body 511 and forms an overflow trough 530 within the feeding body 511. The sieve plate 512 is connected to the liquid inlet 122. An opening 5111 is provided on the side wall of the feeding body 511. The opening 5111 is used to connect the overflow trough 530 and the distributing component 520.

[0111] The feeding body 511 is a shell-type container used to collect, buffer, and distribute the incoming liquid to the downstream distribution component 520, and its interior forms a space for temporary storage and transfer of the liquid.

[0112] The sieve plate 512 has through holes and is correspondingly set with the liquid inlet 122. After the liquid enters the feeding body 511 from the liquid inlet 122, a relatively stable liquid surface is first formed above the sieve plate 512 or in its defined area. The continuous replenishment of liquid and overflow regulation are achieved through the connecting effect of the sieve plate 512, thereby weakening the liquid pulsation and instantaneous impact, so that the liquid enters the distribution component 520 through the side wall opening 5111 in a more uniform state, which is conducive to the uniform distribution of materials by each distribution component 520.

[0113] Specifically, in combination Figure 5 As shown, the feeding body 511 is usually located in the upper or middle area of ​​the liquid distributor 500 and is in direct communication with the liquid inlet 122. After the screen plate 512 is installed inside the feeding body 511, it divides its space into at least one overflow trough 530. The side wall opening 5111 is located at the lateral position corresponding to the feeding body 511 and the distributing component 520, so that the liquid in the overflow trough 530 can be discharged from the opening 5111 and sent into the distributing component 520 under the action of gravity.

[0114] In one possible implementation, the feeding body 511 can be a cylinder 210, a trough, or a box; the screen plate 512 can be a flat screen, a mesh screen, or a perforated screen plate 512, or it can be a perforated plate, a grid plate, or an inclined guide plate, depending on the installation and flow requirements, and there are no specific limitations.

[0115] Specifically, by setting a sieve plate 512 inside the feed body 511, and the sieve plate 512 forming an overflow groove 530 inside the feed body 511, and using the side wall opening 5111 to connect the overflow groove 530 with the distribution component 520, the liquid enters the feed body 511 through the liquid inlet 122 and is first intercepted by the sieve plate 512, forming a stable liquid level under its action. Then, the liquid overflows into the overflow groove 530 defined by the sieve plate 512, and under the action of gravity, flows through the side wall opening 5111 of the feed body 511 to the distribution component 520 arranged downward or laterally. Multiple distribution components 520 then disperse the incoming liquid to the corresponding connecting port 211 area, thereby making the liquid distribution into the gas-liquid distributor 200 and the subsequent catalyst bed 300 more uniform, reducing the probability of local flow deviation and liquid aggregation, and thus helping to improve the mass transfer uniformity and temperature distribution stability in the bed.

[0116] It should be understood that the above examples are for illustrative purposes only and are not intended to be limiting.

[0117] And, as Figure 5 As shown, multiple material distribution components 520 are connected to the feeding body 511 and are spaced apart along the extension direction of the feeding body 511. Each material distribution component 520 has a flow distribution groove 521. The flow distribution groove 521 on each material distribution component 520 is positioned corresponding to each opening 5111. Each material distribution component 520 has a flow distribution hole 5211, which is used to connect the flow distribution groove 521 and the connecting port 211.

[0118] The distributor 520 is a flow guide component located below the feed body 511. Its function is to redistribute the liquid after it enters through the side wall opening 5111 of the feed body 511 and guide it to the communication port 211 of the downstream gas-liquid distributor 200, thereby forming a liquid supply path that first collects and then releases the liquid.

[0119] The material distribution component 520 and the feeding body 511 can be integrally formed and connected, or they can be detachably connected by welding, bolting, snap-fitting or inserting. They are arranged at intervals along the extension direction of the feeding body 511 so that the liquid enters each material distribution component 520 in segments along the axial direction.

[0120] In this configuration, the distribution groove 521 on each distribution component 520 is positioned corresponding to the opening 5111. Liquid entering through the opening 5111 can be directly introduced into the corresponding distribution groove 521, and then connected to the connecting port 211 through the distribution hole 5211 on the distribution component 520, thereby achieving multi-point liquid supply and gradual distribution.

[0121] Based on the above structure, the material distribution component 520 can weaken the local impact and concentrated flow generated after the liquid enters, so that the liquid can be dispersed twice before entering the connecting port 211, thereby improving the uniformity of the subsequent gas-liquid distribution area and reducing local deviation and liquid aggregation.

[0122] In addition, the liquid distributor 500 may also include a reinforcing rod 540, through which multiple distributors can be connected to enhance the connection strength of the distributors and prevent shaking.

[0123] In one possible implementation, such as Figure 5 As shown, the opening 5111 is located above the screen plate 512; the diversion holes 5211 are spaced apart along the extension direction of the material distribution component 520, and the diversion holes 5211 are located near the top of the material distribution component 520.

[0124] With this configuration, the overflow trough 530 can temporarily store and equalize the pressure of the liquid entering the feed body 511. Under the action of gravity, the liquid first passes over the screen plate 512 and then enters the distribution component 520 through the opening 5111 located above it. This allows the liquid to be stably collected before entering the distribution component 520, reducing the splashing phenomenon caused by the liquid flow directly impacting the bottom of the distribution trough 521.

[0125] Meanwhile, the diversion holes 5211 are spaced apart along the extension direction of the distribution component 520 and arranged close to the top of the distribution component 520, so that the liquid can be distributed from top to bottom and released preferentially near the top of the distribution component 520, forming a relatively stable gravity flow path, which helps to reduce the impact of local liquid level fluctuations on the uniformity of outflow.

[0126] In one possible implementation, the opening 5111 can be in the form of a slit, a round opening, or a fan-shaped opening, so as to be adapted according to the liquid flow rate and installation space; the material distribution component 520 can be arranged as a long strip structure along the extension direction of the feeding body 511, and a diversion groove 521 is formed inside it. The diversion holes 5211 are arranged at intervals near the top along the length direction of the material distribution component 520, and can be in the form of top holes, oblique holes, or side holes, so that the liquid is preferentially discharged from the upper area in stages after entering the diversion groove 521.

[0127] It should be understood that the above examples are for illustrative purposes only and are not intended to be limiting.

[0128] In one possible implementation, combining Figure 1 , Figure 6 and Figure 7 As shown, the inter-stage heat exchange structure 600 includes a gas-liquid pre-distribution component 610 and a heat exchange component 620 arranged sequentially from top to bottom along the height direction of the reactor shell 100. The heat exchange component 620 is connected to the gas-liquid pre-distribution component 610. The gas-liquid pre-distribution component 610 is disposed between two catalyst bed layers 300. The gas-liquid pre-distribution component 610 is used to receive the gas-liquid mixture after reaction in the upper catalyst bed layer 300. The heat exchange component 620 is used to receive the gas-liquid mixture flowing out of the gas-liquid pre-distribution component 610 and perform heat exchange.

[0129] The gas-liquid pre-distribution component 610 is a fluid pretreatment component used to redisperse, rectify, and guide the gas-liquid mixture after passing through the catalyst bed 300 located above into the heat exchanger 620. In this application, it serves to buffer the flow and homogenize the temperature field.

[0130] The heat exchanger 620 is a heat exchange unit used to remove heat from the gas-liquid mixture from the gas-liquid pre-distribution unit 610. The heat exchanger 620 is arranged in communication with the gas-liquid pre-distribution unit 610 to form a continuous inter-section flow path, thereby cooling the material before it enters the subsequent reaction section.

[0131] In addition, it should be noted that, in combination Figure 1 As shown, a liquid distributor 500 can be installed between the gas-liquid pre-distribution component 610 and the catalyst bed 300. The gas-liquid pre-distribution component 610 is connected to the liquid distributor 500 so that when the liquid phase material is insufficient to continue the reaction, liquid phase material can be added through the liquid distributor 500.

[0132] like Figure 1 As shown, a catalyst bed 300 is provided below the heat exchanger 620. The material that has undergone heat exchange and is uniformly distributed can be transported to the catalyst bed 300 below the heat exchanger 620 to continue the reaction.

[0133] It is understandable that the catalyst bed 300 located below the gas-liquid distributor 200 undergoes a hydrogenation reaction. Due to the exothermic reaction, the material temperature rises along the axial direction of the catalyst bed 300. After the gas-liquid mixture is discharged from the lower end of the catalyst bed 300, it can enter the gas-liquid pre-distribution component 610. After being dispersed, buffered and rectified in this component, the previously possible local jetting, entrainment unevenness or flow deviation phenomena are weakened, and the velocity distribution and phase distribution of the gas-liquid mixture tend to be uniform.

[0134] Furthermore, under the guidance of the gas-liquid pre-distribution component 610, the material can enter the heat exchange component 620, where it can indirectly exchange heat with the cooling medium, thereby removing the exothermic reaction in a timely manner and reducing the temperature of the material entering the subsequent catalyst bed 300 to the reaction range.

[0135] This setup not only reduces the additional pressure drop and heat loss caused by external pipelines, but also enables gas-liquid redistribution during inter-stage heat exchange, effectively shortening the inter-stage process.

[0136] It should be understood that the above examples are for illustrative purposes only and are not intended to be limiting.

[0137] In one possible implementation, reference is made to Figure 6 As shown, the gas-liquid pre-distribution component 610 includes a connecting plate 611 and a plurality of conduits 612. The outer periphery of the connecting plate 611 is attached to the inner wall of the reactor shell 100, and the conduits 612 are inserted into the connecting plate 611 and extend toward the heat exchanger 620.

[0138] Reference Figure 7 As shown, the heat exchanger 620 includes a receiving plate 621 and a plurality of tubes 622. The outer periphery of the receiving plate 621 is attached to the inner wall of the reactor shell 100. The receiving plate 621 has a receiving cavity 6211. The tubes 622 are inserted into the receiving plate 621 and partially located in the receiving cavity 6211. The ports of the tubes 622 located in the receiving cavity 6211 are V-shaped. The receiving plate 621 is used to receive the gas-liquid mixture flowing out through the conduit 612.

[0139] The connecting plate 611 serves as the receiving base for the gas-liquid pre-distribution component 610, and its edges are sealed and fitted against the inner wall of the reactor shell 100. The connecting plate 611 divides the reaction chamber 110 into an upper gas-liquid distribution zone and a lower heat exchange reaction zone, preventing gas and liquid from short-circuiting and flowing through the gap between the connecting plate 611 and the reactor shell 100.

[0140] Reference Figure 6 As shown, mounting holes are evenly opened on the surface of the connecting plate 611 along the circumferential and radial directions. Each conduit 612 is vertically inserted and fixed in the mounting hole, and the conduit 612 passes through the connecting plate 611 from top to bottom.

[0141] The lower end of the conduit 612 extends downwards and is directly opposite the receiving plate 621 of the heat exchanger 620 below.

[0142] Reference Figure 7 As shown, the receiving plate 621 is an integral plate with its outer edge attached to the inner wall of the reactor shell 100. The plate of the receiving plate 621 is recessed upward to form a receiving cavity 6211. The top surface of the receiving cavity 6211 is directly opposite the outlet of all the upper conduits 612. All the gas and liquid phases falling from the conduits 612 fall into the interior of the receiving cavity 6211 and will not flow sideways from the edge of the receiving plate 621.

[0143] Multiple heat exchange tubes 622 are densely inserted into the plate of the receiving plate 621, and the upper end of the tubes 622 extends into the receiving cavity 6211. The upper end of the tubes 622 extending into the receiving cavity 6211 is processed into a V-shaped cut (V-shaped bevel), with the tip of the V-shaped cut facing upward and the opening 5111 facing into the receiving cavity 6211.

[0144] The heat exchange medium can flow around the outer periphery of the tubes 622 outside the receiving cavity 6211, and the gas-liquid reaction materials flow and exchange heat inside the receiving cavity 6211 and the tubes 622 to reduce the temperature.

[0145] Understandably, the gas-liquid pre-distribution component 610 is equipped with a connecting plate 611 that fits against the inner wall of the shell and multiple downward-extending conduits 612. The connecting plate 611 can seal the edge gaps of the reactor shell 100 to prevent gas and liquid from short-circuiting and flowing across the wall. The multiple conduits 612 can perform secondary pre-distribution of the upper gas-liquid mixture and directionally guide the gas and liquid into the receiving cavity 6211 of the lower receiving plate 621.

[0146] The receiving plate 621 is integrally attached to the inner wall of the reactor shell 100. The gas-liquid mixture flowing out through the conduit 612 can be transported to the receiving cavity 6211. The gas and liquid are collected and mixed through the receiving cavity 6211 to offset the upstream distribution deviation, and at the same time, the gas and liquid are forced to fully contact and exchange heat with the heat exchange tube 622.

[0147] In addition, the tube 622 port extending into the receiving cavity 6211 is set in a V shape. The V-shaped bevel can shear and break the liquid flow and inhibit liquid phase aggregation. At the same time, it can significantly increase the contact area between the gas and liquid and the heat exchange tube wall, enhance the heat exchange and temperature control effect, and the V-shaped structure has no dead corners for slag accumulation, making it less likely to cause tube blockage.

[0148] This configuration achieves integrated multi-stage uniform gas-liquid distribution and efficient heat exchange, ensuring uniform gas-liquid ratio and temperature across the entire catalyst bed 300. It effectively eliminates defects such as local overheating in the catalyst bed 300 and improves the continuous operation of the trickle bed reactor under strong exothermic conditions.

[0149] Furthermore, such as Figure 7 As shown, the conduit 612 is disposed in the receiving cavity 6211. The conduit 612 and the tube 622 are arranged alternately, and the conduit 612 is partially inserted into the gap between two adjacent tubes 622.

[0150] Reference Figure 7 As shown, multiple conduits 612 can extend toward the receiving plate 621 and be inserted into the receiving cavity 6211. The conduits 612 and the multiple heat exchange tubes 622 in the receiving cavity 6211 are arranged in an alternating manner. The bottom end of each conduit 612 extends into the middle gap between two adjacent tubes 622, and the gas-liquid mixture is directly sprayed from the outlet of the conduit 612 into the gap area between the tubes 622.

[0151] This configuration allows the tube 622 to act as a guide and barrier for the gas-liquid material, breaking up large-scale vortices and causing the gas-liquid mixture to undergo lateral diversion and local backmixing within the receiving chamber 6211. This corrects for flow deviations caused by minor uneven distribution in the upper layer, preventing the fluid from concentrating along a single axis into any one tube 622, effectively breaking up concentrated liquid flows and inhibiting liquid phase aggregation. Combined with... Figure 7 As shown, when the material in the receiving cavity 6211 rises to the port of the tube 622, the V-shaped port can guide the material to flow into the tube 622 and perform heat exchange and cooling treatment.

[0152] In addition, it should be noted that, referring to Figure 1 As shown, a catalyst bed 300 is disposed below the heat exchanger 620, and the outlet of the tube 622 is connected to the catalyst bed 300. With this configuration, the material discharged through the tube 622 is not only cooled to allow it to enter the catalyst bed 300 for the next stage of reaction, but also achieves uniform material distribution, shortening the inter-stage process.

[0153] Specifically, in combination Figure 1 As shown, the mixture after reaction in the catalyst bed 300 in the previous stage first enters the receiving chamber 6211 through the gas-liquid pre-distribution device 610. The conduit 612 disperses the material and guides it to different areas inside the receiving chamber 6211. Since the conduit 612 and the tube array 622 are arranged in an alternating manner and the end of the conduit 612 is inserted into the gap between two adjacent tube arrays 622, the material will be blocked and diverted by the tube array 622 near the outlet of the conduit 612. As a result, it is redistributed between adjacent tube arrays 622 and enters the tube array 622 evenly. This can effectively avoid the problems of flow deviation, local high load and uneven heat exchange caused by the material rushing directly into a local tube array 622 along a single shortest path, making the flow distribution between tube arrays 622 more balanced.

[0154] Furthermore, the material undergoes secondary disturbance and redistribution in the intersecting space between the conduit 612 and the tube 622, enabling the heat exchanger 620 to receive and exchange heat more fully, thereby reducing local overheating, minimizing temperature fluctuations, and improving the overall heat exchange efficiency and operational stability of the inter-section heat exchange structure 600.

[0155] It should be understood that the above examples are merely illustrative and not limiting. Without departing from the concept of this application, staggered, quincunx, or other equivalent interlaced array methods can be used to achieve the same or similar flow guiding effect.

[0156] Furthermore, the distance between the port of the conduit 612 facing the receiving plate 621 and the port of the tube 622 facing the connecting plate 611 is greater than or equal to 5 mm and less than or equal to 50 mm.

[0157] Combination Figure 6 and Figure 7As shown, the liquid outlet end of the conduit 612 in the gas-liquid pre-distribution component 610 and the liquid inlet end of the tube 622 in the heat exchanger 620 are spaced apart in the axial direction to limit the buffer space when the gas-liquid mixture transitions from the conduit 612 to the tube 622.

[0158] It is understandable that the vertical distance between the port of the conduit 612 facing the receiving plate 621 and the port of the tube 622 facing the connecting plate 611 is limited to 5 mm to 50 mm; the spacing is not less than 5 mm, which can reserve diffusion buffer space for gas and liquid, so that the gas-liquid mixture output through the conduit 612 can be properly diffused and rectified in the receiving plate 621 before entering the tube 622, preventing the outlet of the conduit 612 from sticking to the port of the tube 622, causing liquid phase accumulation and blockage of the channel; the spacing is not more than 50 mm, which can constrain the gas-liquid diffusion range and avoid long-distance splashing and crossflow of materials, the formation of airflow vortices and gas deviation in the cavity.

[0159] Furthermore, this spacing range allows for appropriate dispersion of gas and liquid before secondary shearing and refinement through the V-shaped port of the tube 622, ensuring uniform gas and liquid load in each heat exchange tube 622, improving the heat exchange uniformity of the receiving chamber 6211, stabilizing the operating pressure drop of the reactor, and reducing the overall height of the receiving chamber 6211, thereby lowering the equipment manufacturing cost.

[0160] Finally, it should be noted that other embodiments of this application will readily conceive of by those skilled in the art upon consideration of the specification and practice of the application disclosed herein. This application is intended to cover any variations, uses, or adaptations of this application that follow the general principles of this application and include common knowledge or customary techniques in the art not disclosed herein, and is not limited to the precise structures described above and shown in the accompanying drawings, and various modifications and changes may be made without departing from its scope.

Claims

1. A trickle bed reactor, characterized in that, include: Reactor shell (100), gas-liquid distributor (200), inter-stage heat exchange structure (600) and multi-layer catalyst bed (300); The reactor shell (100) has a reaction chamber (110) and a feed inlet (120) communicating with the reaction chamber (110). The gas-liquid distributor (200), the catalyst bed (300) and the inter-stage heat exchange structure (600) are all disposed in the reaction chamber (110) and arranged sequentially from top to bottom along the height direction of the reactor shell (100). The inter-stage heat exchange structure (600) is disposed between two catalyst beds (300) and is used to receive the material output from the upper catalyst bed (300) for heat exchange. The gas-liquid distributor (200) includes a cylinder (210), a distribution plate (220), and a connecting pipe (230). The edge of the distribution plate (220) is attached to the inner wall of the reactor shell (100). The cylinder (210) is disposed on the distribution plate (220). The cylinder (210) has multiple connecting ports (211). The connecting pipe (230) is inserted into the distribution plate (220), and part of the connecting pipe (230) is located inside the cylinder (210). The connecting ports (211) are used to connect the feed inlet (120) and the connecting pipe (230). The outlet of the connecting pipe (230) is funnel-shaped.

2. The trickle bed reactor according to claim 1, characterized in that, The connecting pipe (230) is tapered, with its small-diameter end located inside the cylinder (210). The small-diameter end of the connecting pipe (230) forms an annular channel (240) with the interior of the cylinder (210). The connecting port (211) communicates with the annular channel (240), and the large-diameter end of the connecting pipe (230) is located outside the cylinder (210).

3. The trickle bed reactor according to claim 2, characterized in that, The connecting pipe (230) and the cylinder (210) form a communication group, and multiple communication groups are provided, which are evenly distributed on the distribution plate (220). The inclination angle of the connecting pipe (230) is greater than or equal to 20° and less than or equal to 60°; Multiple connecting ports (211) are arranged at intervals along the circumference of the cylinder (210), and the connecting ports (211) are slits.

4. The trickle bed reactor according to claim 1, characterized in that, It also includes a gas distributor (400) and a liquid distributor (500). The feed inlet (120) includes a gas feed inlet (121) and a liquid feed inlet (122). The gas distributor (400) and the liquid distributor (500) are arranged sequentially from top to bottom in the reaction chamber (110) along the height direction of the reactor shell (100) and are located above the gas-liquid distributor (200). The gas distributor (400) is connected to the gas feed inlet (121), and the liquid distributor (500) is connected to the liquid feed inlet (122). The liquid distributor (500) is connected to the connecting pipe (230) through the connecting port (211).

5. The trickle bed reactor according to claim 4, characterized in that, The gas distributor (400) includes a plurality of cone tubes (410). Along the radial direction of the reactor shell (100), the plurality of cone tubes (410) are sequentially arranged from the inside to the outside, and a gas delivery channel (420) is formed between adjacent cone tubes (410). Along the height direction of the reactor shell (100), the diameter of each cone tube (410) gradually increases from top to bottom. Along the height direction of the reactor shell (100), the upper port positions of each layer of the cone tube (410) are arranged in a stepped manner from top to bottom, and decrease layer by layer from the outside to the inside. The upper port of the outermost cone tube (410) is connected to the gas inlet (121).

6. The trickle bed reactor according to claim 5, characterized in that, At least three cone tubes (410) are provided, the included angle between adjacent cone tubes (410) is greater than or equal to 6° and less than or equal to 14°, and the ratio of the diameter of the reactor shell (100) to the diameter of the cone tube (410) is greater than or equal to 1.5 and less than or equal to 4.

7. The trickle bed reactor according to claim 4, characterized in that, The liquid distributor (500) includes a feed element (510) and a plurality of distribution elements (520). The feed element (510) is connected to the liquid inlet (122). The distribution elements (520) are connected to the feed element (510) and located below the feed element (510). The plurality of distribution elements (520) are spaced apart along the extension direction of the feed element (510). The outlet of the distribution element (520) is connected to the connecting port (211). The distribution elements (520) are used to uniformly disperse the material.

8. The trickle bed reactor according to claim 7, characterized in that, The feeding component (510) includes a feeding body (511) and a sieve plate (512). The sieve plate (512) is disposed in the feeding body (511) and the sieve plate (512) is divided in the feeding body (511) to form an overflow groove (530). The sieve plate (512) is connected to the liquid inlet (122). An opening (5111) is provided on the side wall of the feeding body (511) and the opening (5111) is used to connect the overflow groove (530) and the distributing component (520).

9. The trickle bed reactor according to claim 8, characterized in that, Multiple material distribution components (520) are connected to the feeding body (511) and spaced apart along the extending direction of the feeding body (511). Each material distribution component (520) has a flow distribution groove (521). The flow distribution groove (521) on each material distribution component (520) is positioned corresponding to each opening (5111). Each material distribution component (520) has a flow distribution hole (5211). The flow distribution hole (5211) is used to connect the flow distribution groove (521) and the connecting port (211).

10. The trickle bed reactor according to claim 9, characterized in that, The opening (5111) is located above the sieve plate (512); The diversion holes (5211) are spaced apart along the extending direction of the material distribution component (520), and the diversion holes (5211) are located near the top of the material distribution component (520).

11. The trickle bed reactor according to claim 1, characterized in that, The inter-segment heat exchange structure (600) includes a gas-liquid pre-distribution element (610) and a heat exchange element (620) arranged sequentially from top to bottom along the height direction of the reactor shell (100). The heat exchange element (620) is connected to the gas-liquid pre-distribution element (610). The gas-liquid pre-distribution element (610) is disposed between two catalyst bed layers (300). The gas-liquid pre-distribution element (610) is used to receive the gas-liquid mixture after reaction in the upper catalyst bed layer (300). The heat exchange element (620) is used to receive the gas-liquid mixture flowing out of the gas-liquid pre-distribution element (610) and perform heat exchange.

12. The trickle bed reactor according to claim 11, characterized in that, The gas-liquid pre-distribution component (610) includes a connecting plate (611) and a plurality of conduits (612). The outer periphery of the connecting plate (611) is attached to the inner wall of the reactor shell (100), and the conduits (612) are inserted into the connecting plate (611) and extend toward the heat exchange component (620). The heat exchanger (620) includes a receiving plate (621) and a plurality of tubes (622). The outer periphery of the receiving plate (621) is attached to the inner wall of the reactor shell (100). The receiving plate (621) has a receiving cavity (6211). The tubes (622) are inserted into the receiving plate (621) and partially located in the receiving cavity (6211). The ports of the tubes (622) located in the receiving cavity (6211) are V-shaped. The receiving plate (621) is used to receive the gas-liquid mixture flowing out through the conduit (612).

13. The trickle bed reactor according to claim 12, characterized in that, The conduit (612) is disposed in the receiving cavity (6211), the conduit (612) and the tubes (622) are arranged alternately, and the conduit (612) is partially inserted into the gap between two adjacent tubes (622).

14. The trickle bed reactor according to claim 13, characterized in that, The distance between the port of the conduit (612) facing the receiving plate (621) and the port of the tube (622) facing the connecting plate (611) is greater than or equal to 5 mm and less than or equal to 50 mm.

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