Premixing inlet diffuser and fixed bed hydrogenation reactor

Abstract

The present disclosure relates to a premixing inlet diffuser and a fixed bed hydrogenation reactor, comprising a diffuser cylinder, a diffusion assembly and a distribution assembly. The diffuser cylinder comprises a mixing chamber, and a feed inlet and a discharge outlet in communication with the mixing chamber. The gas-liquid two-phase material is introduced into the mixing chamber through the feed inlet for mixing. The distribution assembly is arranged in the mixing chamber to distribute the material in the mixing chamber to a first diffusion part corresponding to the central position of the mixing chamber and a second diffusion part surrounding the first diffusion part, so that the material is more uniformly dispersed. When the premixing inlet diffuser is arranged at the inlet of the fixed bed hydrogenation reactor, the gas-liquid two-phase material can be uniformly dispersed after mixing when passing through the premixing diffuser arranged in the fixed bed hydrogenation reactor, so that the mixed material can enter the bed layer more uniformly, thereby improving the reaction efficiency of the fixed bed hydrogenation reactor.

Description

Technical Field

[0001] This disclosure relates to the chemical industry, specifically to a premixed inlet diffuser and a fixed-bed hydrogenation reactor. Background Technology

[0002] Fixed-bed hydrotreating is currently the mainstream technology for oil product hydrotreating. Fixed-bed hydrotreating reactors involve a three-phase system of gas, liquid, and solid. A common operating state involves two phases, gas and liquid, flowing co-currently into the catalyst bed to undergo the hydrotreating reaction. The gas phase is continuous, while the liquid phase spreads as a liquid film on the catalyst surface. Non-uniform distribution of the gas and liquid phases within the bed reduces catalyst utilization and can even lead to the formation of localized hot spots, affecting the normal operation of the reactor and reducing the reaction efficiency of the fixed bed. Therefore, to improve catalyst utilization and the reaction efficiency of fixed-bed hydrotreating reactors, it is necessary to improve the uniformity of the gas-liquid phase distribution within the reactor. Summary of the Invention

[0003] The purpose of this disclosure is to provide a premixed inlet diffuser and a fixed-bed hydrogenation reactor. The diffuser enables a more uniform distribution of diffused gas and liquid materials. When located at the inlet of the fixed-bed hydrogenation reactor, it can improve the initial uniformity of the gas and liquid phases in the reactor, making the gas and liquid phase fluids entering the bed more uniform, improving the utilization rate of the catalyst, and thus improving the reaction efficiency of the fixed-bed hydrogenation reactor, thereby at least partially solving the above-mentioned technical problems.

[0004] To achieve the above objectives, a first aspect of this disclosure discloses a premixed inlet diffuser, comprising:

[0005] The diffuser cylinder includes a mixing chamber and an inlet and an outlet communicating with the mixing chamber;

[0006] A diffusion assembly, disposed at the discharge port, includes a first diffusion section corresponding to the center of the mixing chamber and a second diffusion section surrounding the first diffusion section; and

[0007] A dispensing component, disposed in the mixing chamber, is configured to dispense material from the mixing chamber to the first diffusion section and the second diffusion section.

[0008] Optionally, the dispensing assembly includes a fixed shaft extending along the feed inlet toward the discharge outlet and swirl blades surrounding the fixed shaft, the swirl blades being used to guide the material in the mixing chamber to the first diffusion section and the second diffusion section;

[0009] The dispensing assembly also includes a plurality of guide plates located at the bottom of the mixing chamber and extending from the center of the mixing chamber toward the inner wall of the diffuser cylinder, for guiding and dispersing the material radially along the diffuser cylinder.

[0010] Optionally, the premixed inlet diffuser further includes a flow breaker plate located at the bottom of the mixing chamber and corresponding to the swirl vanes, with multiple flow guide plates arranged at circumferential intervals along the flow breaker plate.

[0011] Optionally, the premixed inlet diffuser further includes a guide cylinder disposed within the diffuser cylinder, the guide cylinder being connected between the mixing chamber and the feed inlet, the guide cylinder including a guide cavity with a cross-sectional area that gradually decreases from the feed inlet to the mixing chamber, for guiding the material entering from the feed inlet to collect in the mixing chamber.

[0012] Optionally, the premixed inlet diffuser further includes a fluid diffusion plate with diffusion holes, the fluid diffusion plate being located on the opposite side of the inlet corresponding to the outlet, for material diffusion.

[0013] Optionally, the ratio of the inner diameter of the mixing chamber to the inner diameter of the diffuser cylinder ranges from 0.2 to 0.6:1; and / or

[0014] The ratio of the diameter of the swirl blade to the diameter of the mixing chamber ranges from 0.6 to 1:1.

[0015] Optionally, the dispensing assembly includes a fixed shaft extending along the feed inlet toward the discharge outlet and a baffle plate disposed on the fixed shaft; or

[0016] The dispensing assembly includes a flow guide grille disposed within the mixing chamber.

[0017] Optionally, the fluid diffusion plate is constructed as any one of a single-layer flat plate, a double-layer flat plate, a double-layer conical plate, and a combination of flat and conical plates.

[0018] Optionally, the aperture ratio of the diffusion holes on the diffusion plate ranges from 5% to 20%.

[0019] A second aspect of this disclosure discloses a fixed-bed hydrogenation reactor, including a reactor shell and a premixed inlet diffuser disposed at the inlet of the reactor shell.

[0020] Optionally, the fixed-bed hydrogenation reactor further includes an anti-deviation assembly disposed within the reactor cylinder. The anti-deviation assembly includes an anti-deviation cylinder disposed within the reactor cylinder and a plurality of first baffles spaced circumferentially around the anti-deviation cylinder. Each first baffle extends radially along the reactor cylinder to the inner wall of the reactor cylinder to form a plurality of first compartments. The anti-deviation cylinder has an inner cavity open at both ends to form a second compartment. The first compartments and the second compartments are used to fill catalyst.

[0021] Optionally, the fixed-bed hydrogenation reactor further includes a fluid distribution plate disposed within the reactor cylinder. The fluid distribution plate is located upstream of the anti-deviation component in the material flow direction. The distribution plate is provided with multiple fluid pipes, and one or more of the fluid pipes are correspondingly arranged upstream of the second compartment and each of the first compartments in the material flow direction.

[0022] Optionally, when a fluid pipe is arranged upstream of the second compartment in the material flow direction, the fluid pipe corresponding to the second compartment is located on the geometric center line of the second compartment. When a fluid pipe is arranged upstream of each first compartment in the material flow direction, the fluid pipe arranged upstream of each first compartment is located on the geometric center line of the first compartment.

[0023] Optionally, the fixed-bed hydrogenation reactor further includes a filter disc and an outlet filter disposed within the reactor body. The filter disc is located between the diffuser and the fluid distribution disc to filter fixed impurities in the gas-liquid materials, and the outlet filter is disposed at the reactor outlet to filter out solid impurities in the reaction products.

[0024] Optionally, the fixed-bed hydrogenation reactor further includes a heat exchange component disposed within the reactor cylinder. The heat exchange component includes multiple heat exchange tubes, and at least one heat exchange tube is disposed in the second compartment and each of the first compartments to displace the heat generated by the reaction within the compartment.

[0025] Optionally, the inner diameter of the reactor cylinder ranges from 100mm to 800mm.

[0026] Optionally, there may be multiple anti-deviation components, which are spaced apart within the reactor cylinder.

[0027] Through the above technical solution, the diffuser cylinder includes a mixing chamber and an inlet and an outlet communicating with the mixing chamber. The gas-liquid two-phase material is introduced into the mixing chamber through the inlet for mixing. A distribution component is provided in the mixing chamber to distribute the material in the mixing chamber to a first diffusion section corresponding to the center position of the mixing chamber and a second diffusion section surrounding the first diffusion section, so as to make the material more uniformly dispersed. When the premixed inlet diffuser is installed at the inlet of the fixed bed hydrogenation reactor, the gas-liquid two-phase material can be uniformly dispersed after mixing when passing through the premixed diffuser installed in the fixed bed hydrogenation reactor, so that the mixed material can enter the bed more uniformly, thereby improving the reaction efficiency of the fixed bed hydrogenation reactor.

[0028] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Attached Figure Description

[0029] The accompanying drawings are provided to further illustrate the present disclosure and form part of the specification. They are used together with the following detailed description to explain the present disclosure, but do not constitute a limitation thereof. In the drawings:

[0030] Figure 1 This is a schematic diagram of the structure of a premixed inlet diffuser provided in an exemplary embodiment of this disclosure;

[0031] Figure 2 This is publicly available Figure 1 AA section view;

[0032] Figure 3 This is publicly available Figure 1 BB section view in the middle;

[0033] Figure 4 This is a schematic diagram of the structure of another premixed inlet diffuser provided in an exemplary embodiment of this disclosure;

[0034] Figure 5 This is a schematic diagram of the structure of another premixed inlet diffuser provided in an exemplary embodiment of this disclosure;

[0035] Figure 6 This is a schematic diagram of the structure of a fixed-bed hydrogenation reactor provided in an exemplary embodiment of this disclosure;

[0036] Figure 7 This is publicly available Figure 6 CC section view in the middle;

[0037] Figure 8 This is publicly available Figure 6 DD section view in the middle;

[0038] Figure 9 This is publicly available Figure 6 EE section view;

[0039] Figure 10 This is publicly available Figure 6 FF section view in the image.

[0040] Explanation of reference numerals in the attached figures

[0041] 10-Premixed inlet diffuser; 11-Diffuser cylinder; 111-Inlet; 112-Mixing chamber; 113-Outlet; 12-Diffusor assembly; 121-First diffuser section; 122-Second diffuser section; 13-Distribution assembly; 131-Fixed shaft; 132-Swirl vane; 133-Guide plate; 134-Circular baffle; 135-Annular baffle; 14-Fluid diffuser plate; 141-First diffuser plate; 1411-First diffuser hole; 142-Second diffuser plate; 1421-Second diffuser hole; 15-Guide cylinder; 151-Guide cavity; 16-Breaker plate; 161- 17-Flow guide channel; 20-Reactor body; 21-Reactor inlet; 22-Reactor outlet; 30-Filter plate; 40-Fluid distribution plate; 41-Fluid pipe; 50-Anti-flow deviation component; 51-First baffle; 52-Anti-flow deviation cylinder; 60-Heat extraction component; 61-Heat extraction pipe; 62-Cooling water distribution plate; 63-Diverter pipe; 64-Inlet pipe; 65-Outlet pipe; 70-Catalyst discharge port; 80-Catalyst bed support plate; 90-Outlet filter; 100-Hydrogen replenishment distributor; 101-Hydrogen replenishment inlet pipe; 200-First compartment; 300-Second compartment. Detailed Implementation

[0042] The specific embodiments of this disclosure will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit this disclosure.

[0043] In this disclosure, the material flow direction in a premixed diffuser refers to the direction of flow from the feed inlet of the diffuser cylinder towards the discharge outlet of the diffuser cylinder, and the material flow direction in a fixed-bed hydrogenation reactor refers to the direction of flow from the inlet of the reactor cylinder towards the outlet of the reactor cylinder. Unless otherwise stated, directional terms such as "inner" and "outer" refer to the inner and outer contours of a component or structure itself. Terms such as "first" and "second" are used to distinguish one element from another and do not indicate sequence or importance. Furthermore, in the description with reference to the accompanying drawings, the same reference numerals in different drawings denote the same element.

[0044] Fixed-bed hydrotreating reactors are currently the mainstream technology for oil hydrotreating. A fixed-bed hydrotreating reactor involves a gas-liquid-solid three-phase system. A common operation involves two phases, gas and liquid, flowing concurrently into the catalyst bed for the hydrotreating reaction. The gas phase is continuous, while the liquid phase spreads as a liquid film on the catalyst surface. Uneven distribution of the liquid phase within the bed reduces catalyst utilization and can even lead to the formation of localized hot spots, affecting the normal operation of the reactor and consequently reducing the reaction efficiency of the fixed-bed hydrotreating reactor.

[0045] To improve the reaction efficiency of a fixed-bed hydrogenation reactor, it is necessary to ensure a uniform initial distribution of the gas-liquid phase materials entering the catalyst bed. Therefore, as... Figures 1 to 3 As shown, a first aspect of this disclosure provides a premixed inlet diffuser 10, including a diffuser body 11, a diffusion assembly 12, and a distribution assembly 13. The diffuser body 11 includes a mixing chamber 112 and an inlet 111 and an outlet 113 communicating with the mixing chamber 112. The diffuser assembly is disposed at the outlet 113 and includes a first diffusion section 121 corresponding to the center position of the mixing chamber 112 and a second diffusion section 122 surrounding the first diffusion section 121. The distribution component 13 is located in the mixing chamber 112. The gas-liquid two-phase material enters the mixing chamber 112 through the feed inlet 111 for mixing. The mixed gas-liquid two-phase material can be distributed by the distribution component 13 to the first diffusion section 121 corresponding to the center position of the mixing chamber 112 and the second diffusion section 122 surrounding the first diffusion section 121, so as to disperse the material evenly. When the premixed diffuser is installed at the inlet of the fixed bed hydrogenation reactor, the gas-liquid two-phase material can be premixed and evenly dispersed after passing through the premixed diffuser installed in the fixed bed hydrogenation reactor. The evenly dispersed material enters the catalyst bed, which can improve the utilization rate of the catalyst bed and thus improve the reaction efficiency of the fixed bed hydrogenation reactor.

[0046] In the above embodiment, the first diffusion section 121 is the space at the bottom of the mixing chamber 112 corresponding to the center position of the mixing chamber 112, and the second diffusion section 122 is the space surrounding the first diffusion section 121 at the discharge port 113.

[0047] In some embodiments, the dispensing assembly 13 includes a fixed shaft 131 extending from the inlet 111 toward the outlet 113 and swirling blades 132 surrounding the fixed shaft 131. The swirling blades 132 are used to guide the material in the mixing chamber 112 to the first diffusion section 121 and the second diffusion section 122. Specifically, the gas-liquid two-phase material entering the mixing chamber 112 from the inlet 111 of the diffuser collides with the swirling blades 132 disposed in the mixing chamber 112 to form a swirling flow, promoting the mixing of the gas-liquid two-phase material. In addition, the swirling blades 132 can extend circumferentially spirally along the fixed shaft 131 to guide the material in the mixing chamber 112 to the first dispersion section and the second dispersion section.

[0048] In the above embodiments, the dispensing assembly 13 further includes a plurality of guide plates 133 disposed at the bottom of the mixing chamber 112, which extend from the center of the mixing chamber 112 toward the inner wall of the diffuser cylinder 11, for guiding and dispersing the material radially along the diffuser cylinder 11, so that the mixture can be more uniformly dispersed from the center of the diffuser cylinder 11 toward the inner wall of the diffuser cylinder 11.

[0049] In other implementations, such as Figure 5 As shown, baffles can be used to replace the swirl vanes 132. Therefore, the distribution assembly 13 may include a fixed shaft 131 extending along the feed inlet 111 toward the discharge outlet 113 and baffles disposed on the fixed shaft 131 to promote the mixing of gas and liquid two-phase materials. The baffles may be constructed as circular baffles 134, or annular baffles 135 may be spaced on the inner wall of the mixing chamber 112. When the gas and liquid two-phase materials pass through the mixing chamber 112, the gas and liquid materials collide to promote the fusion of the gas and liquid materials.

[0050] Furthermore, the dispensing assembly 13 may include a flow guide grid disposed within the mixing chamber 112 to promote the mixing of materials in the mixing chamber 112. It should be understood that any suitable structure may be disposed in the mixing chamber 112 to promote the mixing of gas-liquid materials in the mixing chamber 112, which will not be elaborated here.

[0051] like Figure 1 and Figure 2 As shown, in some embodiments, the premixed inlet diffuser 10 further includes a flow breaker 16, which is located at the bottom of the mixing chamber 112. The flow breaker 16 is disposed corresponding to the mixing chamber 112, and a plurality of flow guides 133 are arranged at circumferential intervals along the flow breaker 16.

[0052] In the above embodiment, the fixed shaft 131 is located at the center of the mixing chamber 112, and one end is connected to the flow-breaking plate 16. The flow-breaking plate 16 is correspondingly arranged with the swirling blades 132 arranged on the fixed shaft 131, that is, in the material flow direction, the swirling blades 132 are projected onto the flow-breaking plate 16 located in the mixing chamber 112. The flow-breaking plate 16 has a plurality of flow-breaking holes 161. Along the material flow direction, the area of ​​the mixing chamber 112 projected onto the flow-breaking plate 16 is smaller than the area of ​​the flow-breaking plate 16. The flow-breaking plate 16 is located at the bottom of the first diffuser section 121. The fluid distributed to the first diffuser section 121 by the distribution component 13 flows out of the outlet 113 through the flow-breaking holes 161 on the flow-breaking plate 16, and is dispersed radially along the diffuser cylinder 11 to the second diffuser section 122. A plurality of guide plates 133 are arranged at intervals along the circumference of the flow-breaking plate 16. In this design, one end of each guide plate 133 is fixedly connected to the edge of the flow breaker 16, and the other end of the guide plate 133 is fixedly connected to the inner wall of the diffuser cylinder 11. A flow channel 17 is formed between two adjacent guide plates 133. The multiple guide plates 133 divide the second diffuser section 122 located at the discharge port 113 into multiple flow channels 17 to guide the mixed gas-liquid two-phase material to be more evenly dispersed into the diffuser section.

[0053] In some implementations, such as Figure 1As shown, a top cover plate is provided in the mixing chamber 112 inside the diffuser body 11. A guide plate 133 extends radially along the mixing chamber 112, and the top edge of the guide plate 133 is fixedly connected to the top cover plate. One end of the guide plate 133 in the radial direction of the mixing chamber 112 is connected to the flow-breaking plate 16, and the other end is connected to the inner wall of the diffuser body 11 to fix the flow-breaking plate 16. Simultaneously, the top cover plate prevents backflow of gas-liquid materials in the guide channel 17. Figure 2 The arrows shown indicate the direction of fluid diffusion in the flow channel 17. To better guide the flow, the flow guide plate 133 can be constructed as an arc-shaped plate.

[0054] When the gas-liquid two-phase material is conveyed into the mixing chamber 112 through the diffuser inlet 111 via a pipeline, the liquid phase material may deviate. Therefore, a guide cylinder 15 can be installed inside the diffuser cylinder 11. The guide cylinder 15 is connected between the mixing chamber 112 and the inlet 111. The guide cylinder 15 includes a guide cavity 151 with a cross-sectional area that gradually decreases from the inlet 111 to the mixing chamber 112. It is used to guide the material entering from the inlet 111 to gather in the mixing chamber 112 to prevent the gas-liquid two-phase material from deviating and to enable the gas-liquid two-phase material to be mixed better.

[0055] In some implementations, such as Figure 1 and Figure 3 As shown, the premixed inlet diffuser 10 also includes a fluid diffuser plate 14 with diffusion holes. The fluid diffuser plate 14 is located on the opposite side of the inlet 111 to the outlet 113 and is used for material diffusion.

[0056] In the above embodiment, the fluid diffuser plate 14 may include a first diffuser plate 141 and a second diffuser plate 142. The first diffuser plate 141 is connected to the flow breaker plate 16 by support bolts, and the second diffuser plate 142 is connected to the first diffuser plate 141 by support bolts. The diffusion holes include a first diffusion hole 1411 and a second diffusion hole 1421. The first diffuser plate 141 is provided with a first diffusion hole 1411 for material passage, and the second diffuser plate 142 is provided with a second diffusion hole 1421 for material passage. The second diffuser plate 142 is located downstream of the material flow direction of the first diffuser plate 141. The first diffuser plate 141 is constructed as an annular structure so that material passing through the flow breaker plate 16 through the flow breaker hole 161 of the flow breaker plate 16 can directly pass through the inner ring of the first diffuser plate 141 and reach the second diffuser plate 142.

[0057] Furthermore, the material dispersed into each of the guide channels 17 in the second diffusion section 122 can flow directly out of the discharge port 113 and flow directly to the first diffusion plate 141, and diffuse through the first diffusion plate 141.

[0058] It should be understood that the fluid diffuser plate 14 can be constructed as any one of a single-layer flat plate, a double-layer flat plate, a double-layer conical plate, or a combination of flat and conical plates. For example... Figure 4 As shown, the fluid diffuser plate 14 is constructed in the form of a double-layered conical plate. Furthermore, the flat-conical composite plate includes a flat plate and a conical plate, which are spaced apart along the material flow direction within the diffuser.

[0059] In some embodiments, the opening ratio of the diffusion holes in the fluid diffuser plate 14 can range from 5% to 20%, so that the material flowing to the fluid diffuser plate 14 can be discharged from the diffuser plate in a timely manner without clogging. Specifically, when the fluid diffuser plate 14 is a single plate, the opening ratio is the opening ratio relative to the opening ratio of a single-plate fluid diffuser plate 14. When the fluid diffuser plate 14 is constructed as a double plate, the opening ratio is the opening ratio of each plate.

[0060] In some embodiments, the ratio of the inner diameter of the mixing chamber 112 to the inner diameter of the diffuser cylinder 11 is in the range of 0.2 to 0.6:1; and / or the ratio of the diameter of the swirl vane 132 to the diameter of the mixing chamber 112 is in the range of 0.6 to 1:1, so that the gas-liquid two-phase materials can pass through the mixing chamber 112 better and achieve a better mixing effect.

[0061] This disclosure exemplarily describes the use of a premixed diffuser. A gas-liquid two-phase material enters the premixed inlet diffuser 10 from the feed line. First, guided by the guide tube 15, it enters the mixing chamber 112. The guide tube 15 prevents excessive local flow caused by liquid phase deviation in the pipeline from impacting the inlet premixed inlet diffuser 10. Subsequently, the gas-liquid two-phase material contacts the swirl vanes 132 and flows downward along the flow channel formed by the swirl vanes 132. During this process, the gas-liquid two-phase material is fully contacted, promoting gas-liquid mixing. After being mixed in the mixing chamber 112, the gas-liquid phase materials are distributed to the first diffusion section 121 and the second diffusion section 122. Part of the gas-liquid material entering the first diffusion section 121 is directly conveyed to the diffusion plate through the flow breaker 16, and part of the gas-liquid material entering the second diffusion section 122 is guided by the guide plate 133 provided in the second diffusion section 122 so that the gas-liquid material is evenly distributed radially in the diffuser cylinder 11. Then, the evenly distributed gas-liquid material is diffused after colliding with the fluid diffusion plate 14 through the outlet 113. After passing through the premixed inlet diffuser 10, the gas-liquid material delivered is more uniform and the diffusion angle is larger.

[0062] To further improve the reaction efficiency of a fixed-bed hydrogenation reactor, it is also necessary to improve the uniformity of fluid distribution within the catalyst bed. Therefore, such as Figures 6 to 10In a second aspect of this disclosure, a fixed-bed hydrogenation reactor is provided, the fixed-bed hydrogenation reactor comprising a reactor body 20 and a premixed inlet diffuser 10 disposed at the inlet of the reactor body 20.

[0063] In some implementations, such as Figure 6 , Figure 7 as well as Figure 9 As shown, the fixed-bed hydrogenation reactor also includes an anti-deviation assembly 50 disposed within the reactor body 20. The anti-deviation assembly 50 includes an anti-deviation cylinder 52 disposed within the reactor body 20 and a plurality of first baffles 51 circumferentially spaced around the anti-deviation cylinder 52. Each first baffle 51 extends radially along the reactor body 20 to the inner wall of the reactor body 20 to form a plurality of first compartments 200. The anti-deviation cylinder 52 has an inner cavity with open ends to form a second compartment 300. The first compartments 200 and the second compartments 300 are used to fill catalyst.

[0064] In the above embodiments, the first compartment 200 and the second compartment 300 are used to fill the catalyst to form a catalyst layer. Multiple catalyst layers constitute a catalyst bed. Each catalyst layer is separated from each other so that after the gaseous and liquid materials enter each catalyst layer, they will not flow between different catalyst layers, thus preventing the deviation of the gaseous and liquid materials and making the gaseous and liquid materials more evenly distributed in the catalyst layer.

[0065] In the above embodiment, one end of each first partition 51 is fixedly connected to the outer peripheral wall of the anti-deflection cylinder 52, and the other end of each first partition 51 is fixedly connected to the inner wall of the anti-deflection cylinder 52. The first compartment 200 and the second compartment 300 are filled with catalyst to form multiple independent catalyst layers. The distance between the bottom of the first partition 51 and the bottom of the catalyst layer is not less than 100 mm, and the distance between the bottom of the anti-deflection cylinder 52 and the bottom of the catalyst layer is not less than 100 mm. A catalyst bed support plate 80 is provided inside the reactor cylinder 20 to support the catalyst layer. Furthermore, each first compartment 200 has an equal area.

[0066] In some embodiments, for ease of understanding, the anti-deflection assembly 50 and its arrangement can also be described from another perspective. In related technologies, the reactor shell 20 has a catalyst bed, and the anti-deflection assembly 50 is arranged in the catalyst bed. The anti-deflection shell 52 in the anti-deflection assembly 50 and a plurality of first baffles 51 surrounding the anti-deflection shell 52 divide the catalyst bed into mutually independent partitions. The material in each partition flows in its own partition and will not cross-flow, so that the material in the catalyst bed is more evenly distributed.

[0067] In some implementations, such as Figures 6 to 9As shown, the fixed-bed hydrogenation reactor also includes a fluid distribution plate 40 disposed within the reactor shell 20. The fluid distribution plate 40 is located upstream of the anti-deviation component 50 in the material flow direction. Multiple fluid pipes 41 are disposed on the fluid distribution plate 40. One or more of the fluid pipes 41 are correspondingly arranged in the second compartment 300 and each of the first compartments 200 in the material flow direction. The inner diameter of the fluid pipes 41 can range from 10 mm to 50 mm, and more specifically, from 12 mm to 25 mm.

[0068] In the above embodiment, the fluid distribution disk 40 is a conventional disc-type fluid distribution disk. When the gaseous and liquid materials flow through the fluid distribution disk 40, the gaseous and liquid materials are distributed to the second compartment 300 and each first compartment 200 through the fluid pipes 41 on the fluid distribution disk 40, so that the gaseous and liquid materials are evenly distributed in the catalyst layer.

[0069] In some implementations, such as Figures 6 to 9 As shown, when a fluid pipe 41 is arranged upstream of the second compartment 300 in the material flow direction, the fluid pipe 41 corresponding to the second compartment 300 is located on the geometric center line of the second compartment 300, so that the gaseous and liquid materials entering the catalyst layer of the second compartment 300 can be more evenly distributed in the catalyst layer of the second compartment 300. When a fluid pipe 41 is arranged upstream of each first compartment 200 in the material flow direction, the fluid pipe 41 arranged upstream of each first compartment 200 is located on the geometric center line of the first compartment 200, so that the gaseous and liquid materials entering the catalyst layer of the first compartment 200 can be more evenly distributed in the catalyst layer of the first compartment 200.

[0070] In some implementations, such as Figure 6 and Figure 7 As shown, the fixed-bed hydrogenation reactor also includes a filter disc 30 and an outlet filter 90 disposed inside the reactor body 20. The filter disc 30 is located between the premixed inlet diffuser 10 and the fluid distribution disc 40 to filter solid impurities in the gas-liquid materials. The outlet filter 90 is disposed at the reactor outlet 22 to filter out solid impurities in the reaction products.

[0071] In the above embodiments, both the filter disc 30 and the outlet filter 90 are filters and outlet filter discs 30 in the related art.

[0072] In some embodiments, the fixed-bed hydrogenation reactor further includes a heat exchange component 60 disposed within the reactor body 20. The heat exchange component 60 includes a plurality of heat exchange tubes 61. At least one heat exchange tube 61 is disposed in each of the second compartment 300 and each of the first compartments 200 to displace the heat generated by the material reaction in the first compartments 200 and the second compartments 300, thereby improving the reaction efficiency of the material.

[0073] The ratio of the inner diameter of the heat-extracting pipe 61 located in the second compartment 300 to the inner diameter of the reactor shell 20 of the hydrogenation reactor ranges from 1 / 25 to 1 / 6. Further, the range can be selected as 1 / 12 to 1 / 8. The ratio of the inner diameter of the heat-extracting pipe 61 located in the first compartment 200 to the inner diameter of the hydrogenation reactor ranges from 1 / 25 to 1 / 6.

[0074] In addition, the ratio of the total flow cross-sectional area of ​​the heat exchange pipe 61 located in the second compartment 300 to the flow cross-sectional area of ​​the main pipe is 0.8 to 1.2:1.

[0075] In other embodiments, the inner diameter of the fixed-bed hydrogenation reactor can be in the range of 100mm to 800mm, and can be further set to 200mm to 600mm.

[0076] In the above embodiment, cooling water is filled into the heat pipe 61, and the cooling water carries away the heat generated by the material reaction to improve the reaction efficiency of the material.

[0077] In some specific implementation methods, such as Figures 6 to 9 As shown, the heat exchange component 60 also includes an inlet pipe 64 and an outlet pipe 65. The inlet pipe 64 is connected to the heat exchange tubes located in the second compartment 300. The other end of the heat exchange tubes 61 located in the second compartment 300 is connected to the cooling water distribution plate 62. The cooling water distribution plate 62 is also connected to the heat exchange tubes 61 located in each first compartment 200 via a branch pipe 63. The other end of each heat exchange tube 61 in the first compartment 200 is connected to the outlet pipe 65. Cooling water enters the heat exchange tubes 61 located in the second compartment 300 through the inlet pipe 64, then flows into the cooling water distribution plate 62. The cooling water flowing into the cooling water distribution plate 62 flows into the heat exchange tubes 61 located in each first compartment 200 through the branch pipe 63, and then the cooling water collects in the outlet pipe 65 and flows out of the reactor shell 20. During the flow of cooling water, the heat generated by the reaction of materials in the second compartment 300 and multiple first compartments 200 can be carried away, thereby improving the reaction efficiency of the materials.

[0078] In some embodiments, there are multiple anti-deviation components 50, which are spaced apart inside the reactor cylinder.

[0079] In the above embodiment, each anti-flow-deflection component 50 has its first compartment 200 and multiple second compartments 300 filled with catalyst to form mutually spaced catalyst layers, and the multiple catalyst layers are combined to form a catalyst bed. Multiple anti-flow-deflection components 50 are spaced apart within the reactor body, and each anti-flow-deflection component 50 corresponds to one catalyst bed. Therefore, when multiple anti-flow-deflection components 50 are spaced apart within the reactor body 20, the reactor body 20 corresponds to multiple spaced-apart catalyst beds.

[0080] In some embodiments, when multiple catalyst beds are spaced apart inside the reactor shell 20, in addition to a fluid distribution plate 40 being provided between the catalyst bed near the reactor inlet 21 and the filter plate 30, a fluid distribution plate 40 is also provided between adjacent catalyst beds. For example... Figures 6 to 7 As shown, two catalyst beds are spaced apart inside the reactor shell 20. A fluid distribution plate 40 is installed between the catalyst bed near the reactor inlet 21 and the filter plate 30, and fluid distribution plates 40 are also installed between adjacent catalyst beds. In addition, a hydrogen replenishment distributor 100 is installed between two adjacent catalyst beds. Hydrogen gas is introduced into the hydrogen replenishment distributor 100 through a hydrogen replenishment inlet pipe 101 connected to the hydrogen replenishment distributor 100 to replenish hydrogen or circulate hydrogen.

[0081] In some embodiments, a catalyst discharge port 70 is provided at the bottom of each catalyst bed section, and the inner diameter of the catalyst discharge port 70 ranges from 40mm to 200mm to facilitate the discharge of the catalyst.

[0082] This disclosure exemplarily describes the use of a fixed-bed hydrogenation reactor. The gas-liquid two-phase material enters the premixed inlet diffuser 10 from the feed line. First, guided by the guide tube 15, it enters the mixing chamber 112. The guide tube 15 prevents excessive local flow caused by liquid phase deviation in the pipeline from impacting the inlet diffuser. Subsequently, the gas-liquid two-phase material comes into contact with the swirl vanes 132 and flows downward along the flow channel formed by the swirl vanes 132. During this process, the gas-liquid two-phase material is fully contacted, promoting gas-liquid mixing. After being mixed in the mixing chamber 112, the gaseous and liquid materials are distributed to the first diffusion section 121 and the second diffusion section 122 to ensure uniform radial distribution of the gaseous and liquid materials in the diffuser cylinder 11. The uniformly distributed gaseous and liquid materials then collide with the fluid diffusion plate 14 through the outlet 113, causing the pre-dispersed gaseous and liquid materials to be sprayed onto the filter plate 30, filtering out solid impurities in the raw material. Subsequently, they are evenly distributed in the catalyst bed within the independently partitioned catalyst layers via the fluid distribution plate 40. The gaseous and liquid materials flow independently within their respective partitions and do not flow between each other. The gaseous and liquid materials undergo a hydrogenation chemical reaction in the catalyst bed. Finally, the product flows out of the fixed-bed hydrogenation reactor after being filtered by the outlet filter 90 to remove solid impurities. The reactor can be equipped with multiple catalyst bed sections. A hydrogen replenishment distributor 100 is installed between two catalyst bed layers to replenish fresh or recycled hydrogen. Simultaneously, fluid is evenly distributed between the two catalyst bed layers and in the fluid distribution plate 40. In addition, the heat collection component 60 of the present invention is provided in each catalyst bed. Cooling water enters the center of the catalyst bed from the heat collection pipe 61 provided in the second compartment 300, and after reaching the bottom, it is dispersed to the heat collection pipe 61 in the first compartment 200 on the periphery of the catalyst bed. It then flows upward along the heat collection pipe 61 provided in the first compartment 200, and finally flows out of the fixed bed hydrogenation reactor after converging into the outlet pipe 65 at the top.

[0083] It is understandable that after the gaseous and liquid materials enter the inlet of the fixed-bed hydrogenation reactor, they are pre-distributed by the premixed diffuser, which makes the gaseous and liquid materials entering the reactor shell 20 uniformly distributed. Then, under the restriction of the anti-deviation component 50, the uniformly distributed gaseous and liquid materials are evenly distributed in the catalyst layer and flow, which can further improve the utilization rate of the catalyst and improve the reaction efficiency.

[0084] The preferred embodiments of this disclosure have been described in detail above with reference to the accompanying drawings. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0085] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0086] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A premixed inlet diffuser, characterized in that, include: The diffuser cylinder includes a mixing chamber and an inlet and an outlet communicating with the mixing chamber; A diffusion assembly is provided at the discharge port, including a first diffusion section corresponding to the center position of the mixing chamber and a second diffusion section surrounding the first diffusion section; as well as A distribution assembly is configured to distribute material from the mixing chamber to the first diffusion section and the second diffusion section. The distribution assembly includes a fixed shaft disposed in the mixing chamber and extending along the inlet toward the outlet, and swirling blades surrounding the fixed shaft. The swirling blades guide the material in the mixing chamber to the first diffusion section and the second diffusion section. The distribution assembly also includes multiple guide plates disposed at the bottom of the mixing chamber and extending from the center of the mixing chamber toward the inner wall of the diffuser cylinder, for guiding and dispersing the material radially along the diffuser cylinder. The premixed inlet diffuser also includes a flow-breaking plate, which is located at the bottom of the mixing chamber and is arranged corresponding to the swirl blades. Multiple flow-guiding plates are arranged at circumferential intervals along the flow-breaking plate, wherein one end of each flow-guiding plate is fixedly connected to the edge of the flow-breaking plate and the other end is fixedly connected to the inner wall of the diffuser cylinder. The premixed inlet diffuser also includes a fluid diffusion plate with diffusion holes, which is located on the opposite side of the inlet corresponding to the outlet, and is used to further diffuse the material flowing out after passing through the break-through plate or the second diffusion section.

2. The premixed inlet diffuser according to claim 1, characterized in that, The premixed inlet diffuser also includes a guide cylinder disposed within the diffuser cylinder. The guide cylinder is connected between the mixing chamber and the feed inlet. The guide cylinder includes a guide cavity with a cross-sectional area that gradually decreases from the feed inlet to the mixing chamber, used to guide the material entering from the feed inlet to collect in the mixing chamber.

3. The premixed inlet diffuser according to claim 1, characterized in that, The ratio of the inner diameter of the mixing chamber to the inner diameter of the diffuser cylinder ranges from (0.2~0.6):1; and / or The ratio of the diameter of the swirl blade to the diameter of the mixing chamber ranges from (0.6 to 1):

1.

4. The premixed inlet diffuser according to claim 1, characterized in that, Use baffles instead of swirl blades.

5. The premixed inlet diffuser according to claim 1, characterized in that, The dispensing assembly includes a flow guide grille disposed within the mixing chamber.

6. The premixed inlet diffuser according to claim 1, characterized in that, The fluid diffusion plate can be constructed as any one of a single-layer flat plate, a double-layer flat plate, a double-layer conical plate, or a combination of flat and conical plates.

7. The premixed inlet diffuser according to claim 1, characterized in that, The opening ratio of the diffusion holes in the fluid diffusion plate ranges from 5% to 20%.

8. A fixed-bed hydrogenation reactor, characterized in that, It includes a reactor shell and a premixed inlet diffuser as described in any one of claims 1-7, located at the inlet of the reactor shell.

9. The fixed-bed hydrogenation reactor according to claim 8, characterized in that, The fixed-bed hydrogenation reactor further includes an anti-deviation assembly disposed within the reactor cylinder. The anti-deviation assembly includes an anti-deviation cylinder disposed within the reactor cylinder and a plurality of first baffles spaced circumferentially around the anti-deviation cylinder. Each first baffle extends radially along the reactor cylinder to the inner wall of the reactor cylinder to form a plurality of first compartments. The anti-deviation cylinder has an inner cavity open at both ends to form a second compartment. The first compartments and the second compartments are used to fill catalyst.

10. The fixed-bed hydrogenation reactor according to claim 9, characterized in that, The fixed-bed hydrogenation reactor further includes a fluid distribution plate disposed within the reactor cylinder. The fluid distribution plate is located upstream of the anti-deviation component in the material flow direction. The distribution plate is provided with multiple fluid pipes. One or more of the fluid pipes are arranged upstream of the second compartment and each of the first compartments in the material flow direction.

11. The fixed-bed hydrogenation reactor according to claim 10, characterized in that, When a fluid pipe is arranged upstream of the second compartment in the material flow direction, the fluid pipe corresponding to the second compartment is located on the geometric center line of the second compartment. When a fluid pipe is arranged upstream of each first compartment in the material flow direction, the fluid pipe arranged upstream of each first compartment is located on the geometric center line of the first compartment.

12. The fixed-bed hydrogenation reactor according to claim 10, characterized in that, The fixed-bed hydrogenation reactor further includes a filter disc and an outlet filter disposed within the reactor body. The filter disc is located between the premixed inlet diffuser and the fluid distribution disc to filter solid impurities in the gas-liquid materials. The outlet filter is disposed at the reactor outlet to filter out solid impurities in the reaction products.

13. The fixed-bed hydrogenation reactor according to claim 9, characterized in that... The fixed-bed hydrogenation reactor further includes a heat exchange component disposed within the reactor cylinder. The heat exchange component includes multiple heat exchange tubes, and at least one heat exchange tube is disposed in the second compartment and each of the first compartments to displace the heat generated by the reaction of materials in the first compartment and the second compartment.

14. The fixed-bed hydrogenation reactor according to claim 8, characterized in that, The inner diameter of the reactor cylinder ranges from 100mm to 800mm.

15. The fixed-bed hydrogenation reactor according to any one of claims 9-14, characterized in that, The number of anti-deviation flow components is multiple, and the multiple anti-deviation flow components are spaced apart inside the reactor cylinder.

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