Premixing type inlet diffuser and fixed bed hydrogenation reactor

Abstract

The invention relates to a premixing type inlet diffuser and a fixed bed hydrogenation reactor. The premixing type inlet diffuser comprises a diffuser barrel, a diffusion assembly and a distribution assembly. The diffuser barrel comprises a mixing cavity, a feeding port and a discharging port, the feeding port and the discharging port are communicated with the mixing cavity, gas-liquid two-phase materials are fed into the mixing cavity through the feeding port to be mixed, and a distribution assembly is arranged in the mixing cavity. When the premixing type inlet diffuser is arranged at the inlet of the fixed bed hydrogenation reactor, the premixing type inlet diffuser is arranged in the mixing cavity so as to distribute materials in the mixing cavity to the first diffusion part corresponding to the central position of the mixing cavity and the second diffusion part surrounding the first diffusion part, so that the materials are dispersed more uniformly; the gas-liquid two-phase material can be uniformly dispersed after being mixed when passing through the premixing diffuser arranged in the fixed bed hydrogenation reactor, so that the mixed material can enter a bed layer more uniformly, and the reaction efficiency of the fixed bed hydrogenation reactor is further improved.

Description

Technical Field

[0001] The present invention relates to the field of chemical industry, and in particular to a premixing inlet diffuser and a fixed bed hydrogenation reactor. Background Art

[0002] Fixed bed hydrogenation is the mainstream oil hydrogenation technology at present. Fixed bed hydrogenation reactor involves a gas-liquid-solid three-phase system. A common operating state is that the gas and liquid phases flow downward into the catalyst bed in parallel to undergo a hydrogenation chemical reaction, in which the gas phase is a continuous phase and the liquid phase spreads on the catalyst surface in the form of a liquid film. The uneven distribution of gas and liquid phase fluids in the bed will reduce the utilization rate of the catalyst and even lead to the formation of local hot spots, affecting the normal operation of the reactor and reducing the reaction efficiency of the fixed bed. Therefore, in order to improve the utilization rate of the catalyst and improve the reaction efficiency of the fixed bed hydrogenation reactor, it is necessary to improve the uniformity of the distribution of the gas and liquid phases in the reactor. Summary of the invention

[0003] The purpose of the present disclosure is to provide a premixed inlet diffuser and a fixed bed hydrogenation reactor. The diffuser can make the diffused gas-liquid materials more evenly distributed. It is arranged at the inlet of the fixed bed hydrogenation reactor, which can improve the initial uniformity of the gas-liquid phase in the reactor, make the gas-liquid phase fluid entering the bed more uniform, improve the utilization rate of the catalyst, and then improve the reaction efficiency of the fixed bed hydrogenation reactor, so as to at least partially solve the above-mentioned technical problems.

[0004] In order to achieve the above-mentioned object, the present disclosure discloses a premixing inlet diffuser in a first aspect, comprising:

[0005] A diffuser cylinder, comprising a mixing chamber and a feed inlet and a discharge outlet communicated with the mixing chamber;

[0006] a diffusion component, disposed at the discharge port, comprising a first diffusion portion corresponding to the center of the mixing chamber and a second diffusion portion surrounding the first diffusion portion; and

[0007] The distribution component is disposed in the mixing chamber and is configured to distribute the material in the mixing chamber to the first diffusion part and the second diffusion part.

[0008] Optionally, the distribution assembly includes a fixed shaft extending from the feed port toward the discharge port and a swirl blade wound around the fixed shaft, and the swirl blade is used to guide the material in the mixing chamber to the first diffuser and the second diffuser;

[0009] The distribution assembly also includes a plurality of guide plates arranged at the bottom of the mixing chamber and extending from the center of the mixing chamber toward the inner wall of the diffuser cylinder, and is used to guide and disperse the material along the radial direction of the diffuser cylinder.

[0010] Optionally, the premixing inlet diffuser further comprises a flow breakers, which are located at the bottom of the mixing chamber and are arranged corresponding to the swirl blades, and a plurality of guide plates are arranged at intervals along the circumference of the flow breakers.

[0011] Optionally, the premixing inlet diffuser also includes a guide cylinder disposed in the diffuser cylinder, the guide cylinder being connected between the mixing chamber and the feed port, the guide cylinder including a guide chamber whose cross-sectional area gradually decreases from the feed port to the mixing chamber, and is used to guide the material entering from the feed port to gather in the mixing chamber.

[0012] Optionally, the premixing inlet diffuser further comprises a fluid diffusion plate with diffusion holes, and the fluid diffusion plate is located on the opposite side of the feed port corresponding to the discharge port, and is used for diffusion of materials.

[0013] Optionally, the ratio of the inner diameter of the mixing chamber to the inner diameter of the diffuser cylinder is in the range of 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 distribution assembly includes a fixed shaft extending from the feed port toward the discharge port and a baffle disposed on the fixed shaft; or

[0016] The distribution assembly includes a guide grid disposed in 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 flat-conical combined plate.

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

[0019] A second aspect of the present disclosure discloses a fixed bed hydrogenation reactor, comprising a reactor barrel and a premixing inlet diffuser disposed at the inlet of the reactor barrel.

[0020] Optionally, the fixed bed hydrogenation reactor also includes an anti-bias flow assembly disposed in the reactor cylinder, the anti-bias flow assembly including an anti-bias flow cylinder disposed in the reactor cylinder and a plurality of first partitions circumferentially spaced around the anti-bias flow cylinder, each of the first partitions extending radially along the reactor cylinder to the inner wall of the reactor cylinder to form a plurality of first compartments, the anti-bias flow cylinder having an inner cavity open at both ends to form a second compartment, the first compartment and the second compartment being used for filling catalyst.

[0021] Optionally, the fixed bed hydrogenation reactor also includes a fluid distribution plate arranged in the reactor cylinder, the fluid distribution plate is located upstream of the anti-flow deviation component in the material flow direction, a plurality of fluid pipelines are arranged on the distribution plate, and the second compartment and each of the first compartments are correspondingly arranged upstream of the material flow direction with one or more of the fluid pipelines.

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

[0023] Optionally, the fixed bed hydrogenation reactor also includes a filter plate and an outlet filter arranged in the reactor cylinder, the filter plate is located between the diffuser and the fluid distribution plate to filter fixed impurities in the gas and liquid materials, and the outlet filter is arranged at the reactor outlet to filter out solid impurities in the reaction products.

[0024] Optionally, the fixed bed hydrogenation reactor further comprises a heat extraction component disposed in the reactor cylinder, the heat extraction component comprising a plurality of heat extraction pipes, and at least one heat extraction pipe is disposed in the second compartment and each of the first compartments to replace the heat generated by the reaction in the compartment.

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

[0026] Optionally, there are multiple anti-flow deviation components, and the multiple anti-flow deviation components are arranged in the reactor cylinder at intervals.

[0027] Through the above technical scheme, the diffuser barrel includes a mixing chamber and a feed port and a discharge port connected to the mixing chamber. The gas-liquid two-phase materials are introduced into the mixing chamber from the feed port for mixing. A distribution component is provided in the mixing chamber to distribute the materials in the mixing chamber to a first diffusion portion corresponding to the center position of the mixing chamber and a second diffusion portion surrounding the first diffusion portion, so that the materials are dispersed more evenly. When the premixing inlet diffuser is provided at the inlet of the fixed bed hydrogenation reactor, the gas-liquid two-phase materials can be evenly dispersed after mixing when passing through the premixing diffuser provided in the fixed bed hydrogenation reactor, so that the mixed materials can enter the bed layer more evenly, thereby improving the reaction efficiency of the fixed bed hydrogenation reactor.

[0028] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] The accompanying drawings are used to provide a further understanding of the present disclosure and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present disclosure but do not constitute a limitation of the present disclosure. In the accompanying drawings:

[0030] Figure 1 is a schematic structural diagram of a premixing inlet diffuser provided in an exemplary embodiment of the present disclosure;

[0031] Figure 2 This disclosure provides Figure 1 AA section view;

[0032] Figure 3 This disclosure provides Figure 1 BB section view in;

[0033] Figure 4 is a schematic structural diagram of another premixing inlet diffuser provided in an exemplary embodiment of the present disclosure;

[0034] Figure 5 is a schematic structural diagram of another premixing inlet diffuser provided in an exemplary embodiment of the present disclosure;

[0035] Figure 6 is a schematic structural diagram of a fixed bed hydrogenation reactor provided in an exemplary embodiment of the present disclosure;

[0036] Figure 7 This disclosure provides Figure 6 CC section view in;

[0037] Figure 8 This disclosure provides Figure 6 DD section view in;

[0038] Fig. 9 This disclosure provides Figure 6 EE cross-sectional view in;

[0039] Fig.10 This disclosure provides Figure 6 FF cross-sectional view in.

[0040] Description of Reference Numerals

[0041] 10-premix inlet diffuser; 11-diffuser cylinder; 111-feed port; 112-mixing chamber; 113-discharge port; 12-diffuser assembly; 121-first diffuser; 122-second diffuser; 13-distribution assembly; 131-fixed shaft; 132-swirl blade; 133-guide plate; 134-circular baffle; 135-annular baffle; 14-fluid diffuser; 141-first diffuser; 1411-first diffuser hole; 142-second diffuser; 1421-second diffuser hole; 15-guide cylinder; 151-guide chamber; 16-broken flow plate; 161- Broken flow hole; 17-flow guide channel; 20-reactor cylinder; 21-reactor inlet; 22-reactor outlet; 30-filter plate; 40-fluid distribution plate; 41-fluid pipeline; 50-anti-bias flow assembly; 51-first partition; 52-anti-bias flow cylinder; 60-heat extraction assembly; 61-heat extraction pipe; 62-cooling water distribution plate; 63-diverter pipe; 64-water inlet pipe; 65-water outlet pipe; 70-catalyst unloading 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 DESCRIPTION

[0042] The specific implementation of the present disclosure is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described herein is only used to illustrate and explain the present disclosure, and is not used to limit the present disclosure.

[0043] In the present disclosure, the material flow direction in a premixed diffuser refers to the direction from the feed inlet of the diffuser barrel toward the discharge port of the diffuser barrel, and the material flow direction in a fixed bed hydrogenation reactor refers to the direction from the inlet of the reactor barrel toward the outlet of the reactor barrel. Unless otherwise specified, the directional words used, such as "inside and outside", refer to the inside and outside of the outline of the component or structure itself. "First, second" and the like are used to distinguish one element from another and do not have order or importance. In addition, in the description of the reference figures, the same mark in different figures represents the same element.

[0044] Fixed bed hydrogenation reactor is the mainstream oil hydrogenation technology at present. Fixed bed hydrogenation reactor involves a gas-liquid-solid three-phase system. A common operation is that the gas-liquid two-phase flows into the catalyst bed in parallel to undergo a hydrogenation reaction, in which the gas phase is a continuous phase and the liquid phase spreads on the catalyst surface in the form of a liquid film. The uneven distribution of the liquid phase in the bed will reduce the utilization rate of the catalyst and even lead to the formation of local hot spots, affecting the normal operation of the reactor, reducing the utilization rate of the catalyst, and thus reducing the reaction efficiency of the fixed bed hydrogenation reactor.

[0045] In order to improve the reaction efficiency of the fixed bed hydrogenation reactor, on the one hand, it is necessary to make the initial distribution of the gas and liquid phase materials entering the catalyst bed of the fixed bed hydrogenation reactor uniform. Figures 1 to 3 As shown, in a first aspect of the present disclosure, a premixing inlet diffuser 10 is provided, comprising a diffuser barrel 11, a diffuser assembly 12, and a distribution assembly 13. The diffuser barrel 11 comprises a mixing chamber 112, and a feed port 111 and a discharge port 113 connected to the mixing chamber 112. The diffuser assembly is disposed at the discharge port 113, and comprises a first diffuser portion 121 corresponding to the center position of the mixing chamber 112, and a second diffuser portion 122 surrounding the first diffuser portion 121. The distribution component 13 is arranged in the mixing chamber 112, and the gas-liquid two-phase material enters the mixing chamber 112 from the feed port 111 for mixing. The mixed gas-liquid two-phase material can be distributed by the distribution component 13 to the first diffusion part 121 corresponding to the center position of the mixing chamber 112 and the second diffusion part 122 surrounding the first diffusion part 121, so as to disperse the material evenly. When the premixing diffuser is arranged at the inlet of the fixed bed hydrogenation reactor, the gas-liquid two-phase material passes through the premixing diffuser arranged in the fixed bed hydrogenation reactor, and the gas-liquid two-phase material can be premixed and then evenly dispersed. The evenly dispersed material enters the catalyst bed, which can improve the utilization rate of the catalyst bed, thereby improving the reaction efficiency of the fixed bed hydrogenation reactor.

[0046] In the above-mentioned embodiment, the first diffusion portion 121 is a space at the bottom of the mixing chamber 112 corresponding to the center of the mixing chamber 112 , and the second diffusion portion 122 is a space surrounded by the first diffusion portion 121 at the discharge port 113 .

[0047] In some embodiments, the distribution assembly 13 includes a fixed shaft 131 extending from the feed port 111 toward the discharge port 113 and a swirl blade 132 disposed around the fixed shaft 131, and the swirl blade 132 is used to guide the material in the mixing chamber 112 to the first diffuser 121 and the second diffuser 122. Specifically, the gas-liquid two-phase material entering the mixing chamber 112 from the feed port 111 of the diffuser collides with the swirl blade 132 disposed in the mixing chamber 112 in the mixing chamber 112 to form a swirl flow, thereby promoting the mixing of the gas-liquid two-phase material. In addition, the swirl blade 132 can extend in a circumferential spiral along the fixed shaft 131, and is used to guide the material in the mixing chamber 112 to the first dispersion section and the second dispersion section.

[0048] In the above-mentioned embodiment, the distribution assembly 13 also includes a plurality of guide plates 133 arranged at the bottom of the mixing chamber 112 and extending from the center of the mixing chamber 112 toward the inner wall of the diffuser barrel 11, which are used to guide and disperse the material along the radial direction of the diffuser barrel 11 so that the mixed material can be more evenly dispersed from the center of the diffuser barrel 11 toward the inner wall of the diffuser barrel 11.

[0049] In other embodiments, Figure 5 As shown, a baffle can be used to replace the swirl blade 132, so the distribution assembly 13 may include a fixed shaft 131 extending from the feed port 111 toward the discharge port 113 and a baffle disposed on the fixed shaft 131 to promote the mixing of gas-liquid two-phase materials. The baffle can be configured as a circular baffle 134, and an annular baffle 135 can be disposed at intervals on the inner wall of the mixing chamber 112. When the gas-liquid two-phase materials pass through the mixing chamber 112, the gas-liquid materials collide to promote the fusion of the gas-liquid materials.

[0050] In addition, the distribution assembly 13 may include a guide grid disposed in the mixing chamber 112 to promote the fusion of materials in the mixing chamber 112. It should be understood that any appropriate structure can be disposed in the mixing chamber 112 to promote the mixing of gas and liquid materials in the mixing chamber 112, which will not be described in detail here.

[0051] like Figure 1 and Figure 2 As shown, in some embodiments, the premixing inlet diffuser 10 further includes a breakers 16 , which is located at the bottom of the mixing chamber 112 . The breakers 16 are arranged corresponding to the mixing chamber 112 , and a plurality of guide plates 133 are arranged at intervals along the circumference of the breakers 16 .

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

[0053] In some embodiments, Figure 1As shown, an upper cover plate is provided in the mixing chamber 112 in the diffuser cylinder 11, and a guide plate 133 extends radially along the mixing chamber 112. The top edge of the guide plate 133 is fixedly connected to the upper 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 cylinder 11 to fix the flow-breaking plate 16. At the same time, the upper cover plate can prevent the gas-liquid material in the guide channel 17 from backflowing. Figure 2 The arrow direction is the direction in which the fluid diffuses in the flow guide channel 17. In order 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 transported into the mixing chamber 112 through the feed port 111 of the diffuser through a pipeline, the liquid phase material may be biased. Therefore, a guide cylinder 15 body can be set in the diffuser cylinder 11. The guide cylinder 15 body is connected between the mixing chamber 112 and the feed port 111. The guide cylinder 15 body includes a guide chamber 151 whose cross-sectional area gradually decreases from the feed port 111 to the mixing chamber 112, and is used to guide the material entering from the feed port 111 to gather in the mixing chamber 112, so as to prevent the gas-liquid two-phase material from being biased, so that the gas-liquid two-phase material can be better mixed.

[0055] In some embodiments, Figure 1 and Figure 3 As shown, the premixing inlet diffuser 10 further includes a fluid diffusion plate 14 with diffusion holes. The fluid diffusion plate 14 is located on the opposite side of the feed port 111 corresponding to the discharge port 113 and is used for diffusion of materials.

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

[0057] In addition, the material dispersed into each guide channel 17 in the second diffusion portion 122 can directly flow out from the discharge port 113 and directly flow to the first diffusion plate 141 , and diffused 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 cone plate, and a flat-cone combination plate. Figure 4 As shown, the fluid diffuser plate 14 is constructed in the form of a double-layer cone plate. In addition, the flat cone combined plate includes a flat plate and a cone plate, and the flat plate and the cone plate are spaced apart along the material flow direction in the diffuser.

[0059] In some embodiments, the porosity of the fluid diffuser plate 14 with diffuser holes may be in the range of 5% to 20%, so that the material flowing to the fluid diffuser plate 14 can be discharged from the diffuser plate in time without clogging. When the fluid diffuser plate 14 is a single plate, the porosity is the porosity of the fluid diffuser plate 14 with a single plate structure. When the fluid diffuser plate 14 is a double plate structure, the porosity of the fluid diffuser plate 14 is the porosity 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 barrel 11 is in the range of 0.2 to 0.6:1; and / or the ratio of the diameter of the swirl blade 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 material can better pass through the mixing chamber 112 and achieve a better mixing effect.

[0061] The present disclosure exemplarily describes the use process of the premixing diffuser. The gas-liquid two-phase material enters the premixing inlet diffuser 10 from the feed pipeline, and first enters the mixing chamber 112 under the guidance of the guide cylinder 15. The setting of the guide cylinder 15 avoids the impact of excessive local flow caused by the liquid phase deviation in the pipeline on the inlet premixing inlet diffuser 10. Then the gas-liquid two-phase material contacts the swirl blade 132 and flows downward along the flow channel formed by the swirl blade 132. In this process, the gas-liquid two-phase material fully contacts and promotes the mixing of the gas and liquid phases. The gas-liquid materials are mixed in the mixing chamber 112 and then distributed to the first diffuser 121 and the second diffuser 122. Part of the gas-liquid materials entering the first diffuser 121 are directly transported to the diffuser plate through the flow breaking plate 16, and part of the gas-liquid materials entering the second diffuser 122 are guided by the guide plate 133 provided in the second diffuser 122, so that the gas-liquid materials are evenly distributed in the radial direction of the diffuser cylinder 11, and then the evenly distributed gas-liquid materials collide with the fluid diffuser plate 14 through the discharge port 113 and diffuse. After passing through the premixed inlet diffuser 10, the gas-liquid materials transported out are more uniform and have a larger diffusion angle.

[0062] In order to further improve the reaction efficiency of the fixed bed hydrogenation reactor, it is necessary to improve the uniformity of the fluid distribution in the catalyst bed. Figures 6 to 10In a second aspect of the present disclosure, a fixed bed hydrogenation reactor is provided. The fixed bed hydrogenation reactor includes a reactor barrel 20 and a premixing inlet diffuser 10 disposed at the inlet of the reactor barrel 20 .

[0063] In some embodiments, Figure 6 , Figure 7 as well as Fig. 9 As shown, the fixed bed hydrogenation reactor also includes an anti-bias flow assembly 50 disposed in the reactor barrel 20, the anti-bias flow assembly 50 includes an anti-bias flow cylinder 52 disposed in the reactor barrel 20 and a plurality of first partitions 51 circumferentially spaced around the anti-bias flow cylinder 52, each first partition 51 extends along the radial direction of the reactor barrel 20 to the inner wall of the reactor barrel 20 to form a plurality of first compartments 200, the anti-bias flow cylinder 52 has an inner cavity with both ends open to form a second compartment 300, and the first compartment 200 and the second compartment 300 are used for filling catalyst.

[0064] In the above embodiment, 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 gas-liquid material enters each catalyst layer, it will not flow between different catalyst layers, thereby preventing the gas-liquid material from flowing sideways, so that the gas-liquid material is more evenly distributed in the catalyst layer.

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

[0066] In some embodiments, for ease of understanding, the anti-bias flow assembly 50 and its setting can also be described from another perspective. In the related art, a catalyst bed is provided in the reactor cylinder 20, and an anti-bias flow assembly 50 is provided in the catalyst bed. The anti-bias flow cylinder 52 in the anti-bias flow assembly 50 and a plurality of first partitions 51 arranged around the outer periphery of the anti-bias flow cylinder 52 separate the catalyst bed into independent partitions, and the materials in each partition flow in their respective partitions without interflow, so that the materials in the catalyst bed are more evenly distributed.

[0067] In some embodiments, Figures 6 to 9As shown, the fixed bed hydrogenation reactor further includes a fluid distribution plate 40 disposed in the reactor barrel 20, the fluid distribution plate 40 is located upstream of the anti-bias flow assembly 50 in the material flow direction, a plurality of fluid pipelines 41 are disposed on the fluid distribution plate 40, and one or more fluid pipelines 41 are correspondingly arranged in the second compartment 300 and each first compartment 200 in the material flow direction. The inner diameter of the fluid pipeline 41 may range from 10 mm to 50 mm, and further, the inner diameter of the fluid pipeline 41 may range from 12 mm to 25 mm.

[0068] In the above embodiment, the fluid distribution plate 40 is an existing disc-type fluid distribution plate. When the gas-liquid material flows through the fluid distribution plate 40, the gas-liquid material is distributed to the second compartment 300 and each first compartment 200 through the fluid pipeline 41 on the fluid distribution plate 40, so that the gas-liquid material is evenly distributed in the catalyst layer.

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

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

[0071] In the above-mentioned embodiment, the filter disc 30 and the outlet filter 90 are both the filter and the outlet filter disc 30 in the related art.

[0072] In some embodiments, the fixed bed hydrogenation reactor also includes a heat extraction component 60 disposed in the reactor barrel 20, and the heat extraction component 60 includes a plurality of heat extraction pipes 61. At least one heat extraction pipe 61 is disposed in the second compartment 300 and each first compartment 200 to displace the heat generated by the material reaction in the first compartment 200 and the second compartment 300, thereby improving the reaction efficiency of the material.

[0073] The ratio of the inner diameter of the heat extraction pipe 61 disposed in the second compartment 300 to the inner diameter of the reactor barrel 20 of the hydrogenation reactor is in the range of 1 / 25 to 1 / 6. Further, the range of the ratio can be 1 / 12 to 1 / 8. The ratio of the inner diameter of the heat extraction pipe 61 disposed in the first compartment 200 to the inner diameter of the hydrogenation reactor is in the range of 1 / 25 to 1 / 6.

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

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

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

[0077] In some specific embodiments, Figures 6 to 9 As shown, the heat extraction assembly 60 further includes an inlet pipe 64 and an outlet pipe 65. The inlet pipe 64 is connected to the heat exchange pipe arranged in the second compartment 300. The other end of the heat extraction pipe 61 arranged 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 extraction pipe 61 arranged in each first compartment 200 through the shunt pipe 63. The other end of the heat extraction pipe 61 in each first compartment 200 is connected to the outlet pipe 65. The cooling water is passed into the heat extraction pipe 61 arranged in the second compartment 300 through the inlet pipe 64, and then flows into the cooling water distribution plate 62. The cooling water flowing into the cooling water distribution plate 62 flows into the heat extraction pipe 61 arranged in each first compartment 200 through the shunt pipe 63, and then the cooling water is collected in the outlet pipe 65 and flows out of the reactor barrel 20. In the process of cooling water flowing, the heat generated by the reaction of the materials in the second compartment 300 and the plurality of first compartments 200 can be taken away, thereby improving the reaction efficiency of the materials.

[0078] In some embodiments, there are multiple anti-deviation flow assemblies 50, and the multiple anti-deviation flow assemblies 50 are spaced apart in the reactor cylinder.

[0079] In the above-mentioned embodiment, the first compartment 200 and the plurality of second compartments 300 of each anti-bias flow assembly 50 are filled with catalyst to form mutually separated catalyst layers, and the plurality of catalyst layers are combined to form a catalyst bed. The plurality of anti-bias flow assemblies 50 are arranged at intervals in the reactor barrel, and each anti-bias flow assembly 50 corresponds to a catalyst bed. Therefore, when the plurality of anti-bias flow assemblies 50 are arranged at intervals in the reactor barrel 20, the reactor barrel 20 corresponds to a plurality of catalyst beds arranged at intervals.

[0080] In some embodiments, when multiple catalyst beds are arranged in the reactor cylinder 20, in addition to the fluid distribution plate 40 between the catalyst bed near the reactor inlet 21 and the filter plate 30, a fluid distribution plate 40 is also arranged between adjacent catalyst beds. Figure 6 to Figure 7 As shown, two catalyst beds are arranged in the reactor cylinder 20, and a fluid distribution plate 40 is arranged between the catalyst bed near the reactor inlet 21 and the filter plate 30, and a fluid distribution plate 40 is also arranged between adjacent catalyst beds. In addition, a hydrogen replenishment distributor 100 is arranged between two adjacent catalyst beds, and hydrogen 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 disposed at the bottom of each catalyst bed layer, and the inner diameter of the catalyst discharge port 70 ranges from 40 mm to 200 mm to facilitate the discharge of the catalyst.

[0082] The present disclosure describes the use process of the fixed bed hydrogenation reactor by way of example. The gas-liquid two-phase material enters the premixed inlet diffuser 10 from the feed pipeline, and first enters the mixing chamber 112 under the guidance of the guide cylinder 15. The setting of the guide cylinder 15 avoids the impact of excessive local flow caused by the liquid phase deviation in the pipeline on the inlet diffuser. Subsequently, the gas-liquid two-phase material contacts the swirl blade 132 and flows downward along the flow channel formed by the swirl blade 132. In this process, the gas-liquid two-phase material contacts fully and promotes the mixing of the gas-liquid phase. After the gas-liquid phase material is mixed in the mixing chamber 112, it is distributed to the first diffusion part 121 and the second diffusion part 122, so that the gas-liquid material is evenly distributed in the radial direction of the diffuser barrel 11, and then the evenly distributed gas-liquid material collides with the fluid diffusion plate 14 through the discharge port 113, so that the pre-dispersed gas-liquid material is sprayed on the filter disc 30, and the solid impurities in the raw material are filtered out, and then the gas-liquid material is evenly distributed in the catalyst layers of the catalyst bed that are independently partitioned through the fluid distribution disc 40. The gas-liquid material flows independently in its respective partitions and does not circulate with each other. The gas-liquid material undergoes a hydrogenation chemical reaction in the catalyst bed, and the final product flows out of the fixed bed hydrogenation reactor after the solid impurities are filtered out by the outlet filter 90. The reactor can be provided with multiple catalyst beds, and a hydrogen replenishment distributor 100 is provided between the two catalyst beds to replenish fresh hydrogen or circulating hydrogen, and at the same time, between the two catalyst beds and the fluid distribution disc 40, the fluid is evenly distributed. In addition, a heat extraction assembly 60 of the present invention is provided in each section of the catalyst bed. Cooling water enters the center of the catalyst bed from the heat extraction pipe 61 provided in the second compartment 300, and after reaching the bottom, it is dispersed to the heat extraction pipe 61 in the first compartment 200 on the periphery of the catalyst bed, and flows upward along the heat extraction pipe 61 provided in the first compartment 200, and finally converges to the water outlet pipe 65 at the upper part and then flows out of the fixed bed hydrogenation reactor.

[0083] It can be understood that after the gas-liquid materials enter the inlet of the fixed bed hydrogenation reactor, they are pre-distributed by the premixing diffuser, so that the gas-liquid materials entering the reactor barrel 20 are evenly distributed. Then, the evenly distributed gas-liquid materials flow evenly in the catalyst layer under the restriction of the anti-bias flow component 50, which can further improve the utilization rate of the catalyst and improve the reaction efficiency.

[0084] The preferred embodiments of the present disclosure are described in detail above in conjunction with the accompanying drawings; however, the present disclosure is not limited to the specific details in the above embodiments. Within the technical concept of the present disclosure, a variety of simple modifications can be made to the technical solution of the present disclosure, and these simple modifications all fall within the protection scope of the present 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, the present disclosure will not further describe various possible combinations.

[0086] In addition, various embodiments of the present disclosure may be arbitrarily combined, and as long as they do not violate the concept of the present disclosure, they should also be regarded as the contents disclosed by the present disclosure.

Claims

1. A premixed inlet diffuser, characterized in that: include: A diffuser cylinder, comprising a mixing chamber and a feed inlet and a discharge outlet communicated with the mixing chamber; A diffusion component, arranged at the discharge port, comprising a first diffusion part corresponding to the center of the mixing chamber and a second diffusion part surrounding the first diffusion part; as well as The distribution component is disposed in the mixing chamber and is configured to distribute the material in the mixing chamber to the first diffusion part and the second diffusion part.

2. The premixing inlet diffuser according to claim 1, characterized in that: The distribution assembly includes a fixed shaft extending from the feed port toward the discharge port and a swirl blade wound around the fixed shaft, the swirl blade is used to guide the material in the mixing chamber to the first diffuser and the second diffuser; The distribution assembly also includes a plurality of guide plates arranged at the bottom of the mixing chamber and extending from the center of the mixing chamber toward the inner wall of the diffuser cylinder, and is used to guide and disperse the material along the radial direction of the diffuser cylinder.

3. The premixing inlet diffuser according to claim 2, characterized in that: The premixing inlet diffuser further comprises a flow-breaking plate, which is located at the bottom of the mixing chamber and is arranged corresponding to the swirl blades. A plurality of guide plates are arranged at intervals along the circumference of the flow-breaking plate.

4. The premixing inlet diffuser according to claim 1, characterized in that: The premixing inlet diffuser also includes a guide cylinder disposed in the diffuser cylinder, the guide cylinder being connected between the mixing chamber and the feed port, the guide cylinder including a guide chamber whose cross-sectional area gradually decreases from the feed port to the mixing chamber, and is used to guide the material entering from the feed port to gather in the mixing chamber.

5. The premixing inlet diffuser according to claim 1, characterized in that: The premix inlet diffuser further comprises a fluid diffuser plate with diffusion holes, and the fluid diffuser plate is located on the opposite side of the feed port corresponding to the discharge port, and is used for diffusing the material.

6. The premixing inlet diffuser according to claim 2, characterized in that: The ratio of the inner diameter of the mixing chamber to the inner diameter of the diffuser cylinder is in the range of 0.2 to 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.

7. The premixing inlet diffuser according to claim 1, characterized in that: The distribution assembly includes a fixed shaft extending from the feed port toward the discharge port and a baffle disposed on the fixed shaft; or The distribution assembly includes a guide grid disposed in the mixing chamber.

8. The premixing inlet diffuser according to claim 5, characterized in that: 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 flat-conical combined plate.

9. The premixing inlet diffuser according to claim 5, characterized in that: The opening ratio of the diffusion holes in the fluid diffusion plate is in the range of 5% to 20%.

10. A fixed bed hydrogenation reactor, characterized in that: The invention comprises a reactor cylinder and a premixing inlet diffuser arranged at the inlet of the reactor cylinder.

11. The fixed bed hydrogenation reactor according to claim 10, characterized in that: The fixed bed hydrogenation reactor also includes an anti-bias flow assembly arranged in the reactor cylinder, the anti-bias flow assembly includes an anti-bias flow cylinder arranged in the reactor cylinder and a plurality of first partitions circumferentially spaced around the anti-bias flow cylinder, each of the first partitions extending along the radial direction of the reactor cylinder to the inner wall of the reactor cylinder to form a plurality of first compartments, the anti-bias flow cylinder has an inner cavity with both ends open to form a second compartment, and the first compartment and the second compartment are used for filling catalyst.

12. The fixed bed hydrogenation reactor according to claim 11, characterized in that: The fixed bed hydrogenation reactor also includes a fluid distribution plate arranged in the reactor cylinder, and the fluid distribution plate is located upstream of the anti-flow deviation component in the material flow direction. A plurality of fluid pipelines are arranged on the distribution plate, and one or more of the fluid pipelines are correspondingly arranged upstream of the second compartment and each of the first compartments in the material flow direction.

13. The fixed bed hydrogenation reactor according to claim 12, characterized in that: When a fluid pipeline is arranged upstream of the second compartment in the material flow direction, the fluid pipeline corresponding to the second compartment is located on the geometric center line of the second compartment; when a fluid pipeline is arranged upstream of each of the first compartments in the material flow direction, the fluid pipeline arranged upstream of each of the first compartments is located on the geometric center line of the first compartment.

14. The fixed bed hydrogenation reactor according to claim 12, characterized in that: The fixed bed hydrogenation reactor also includes a filter plate and an outlet filter arranged in the reactor cylinder. The filter plate is located between the premixed inlet diffuser and the fluid distribution plate to filter solid impurities in the gas and liquid materials. The outlet filter is arranged at the reactor outlet to filter out solid impurities in the reaction products.

15. The fixed bed hydrogenation reactor according to claim 11, characterized in that The fixed bed hydrogenation reactor also includes a heat extraction component arranged in the reactor cylinder, and the heat extraction component includes a plurality of heat extraction pipes. At least one heat extraction pipe is arranged in the second compartment and each of the first compartments to replace the heat generated by the reaction of the materials in the first compartment and the second compartment.

16. The fixed bed hydrogenation reactor according to claim 10, characterized in that: The inner diameter of the reactor cylinder ranges from 100 mm to 800 mm.

17. The fixed bed hydrogenation reactor according to any one of claims 11 to 16, characterized in that: There are multiple anti-deviation flow components, and the multiple anti-deviation flow components are arranged in the reactor cylinder at intervals.

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