Hydroprocessing reactor and pre-distribution tray therefor

Abstract

The application discloses a pre-distribution tray, which comprises a plurality of trays, a circular tray and a plurality of annular trays, the inner and outer diameters of the plurality of trays are matched in sequence and are distributed in a multi-layer step form with the circular tray as the center, the circular tray is the lowest layer, the annular tray with the largest outer diameter is the highest layer, and the plurality of trays are each provided with a plurality of sieve holes; and a connecting piece which connects two adjacent layers of the trays and seals the interlayer gap of the two adjacent layers of the trays. The application further discloses a hydrogenation reactor. The pre-distribution tray of the application is formed in a multi-layer step form through the circular tray and the plurality of annular trays, the arrangement mode of the traditional pre-distribution tray is changed, the fault formed between the adjacent trays avoids the accumulation of liquid phase around the reactor, the phenomenon of the increasing distribution of the liquid layer from the center to the edge is eliminated, and the overall levelness of the pre-distribution tray does not need to be accurately ensured, so that the installation difficulty is reduced.

Description

TECHNICAL FIELD

[0001] The present application relates to the hydrogenation reaction equipment technical field, especially the hydrogenation reaction equipment of the reactor scale is larger, and particularly relates to a hydrogenation reactor and a pre-distribution plate thereof. BACKGROUND

[0002] In recent years, with the rapid development of economy and the enhancement of environmental protection consciousness, the quality and environmental protection requirements of petrochemical products are higher and higher. As one of the technical means for producing clean fuel, the importance and role of hydrogenation technology in the oil refining industry are becoming more and more important. In the hydrogenation device, like the hydrogenation catalyst technology and the hydrogenation process technology, the hydrogenation reactor internal component technology is also an important part of the reaction system, and the three constitute the three factors of the reactor performance.

[0003] In the hydrogenation device, as the key equipment of the hydrogenation reactor, the raw oil mixed with hydrogen in a certain proportion completes the refining and cracking reactions with the help of the hydrogenation catalyst. Whether the hydrogenation reaction in the hydrogenation reactor can be operated stably, whether the hydrogenation catalyst can fully play its role, and whether the product quality can reach high quality, to a large extent, depend on the uniformity of the distribution of gas-liquid phase in the catalyst bed. Whether the distribution of gas-liquid phase in the catalyst bed is uniform is closely related to the design of the hydrogenation reactor internals. It can be said that the performance of the internals directly affects the catalyst life, product quality and operation cycle of the device, and the use of a set of hydrogenation reactor internals with excellent performance is not inferior to the replacement of a hydrogenation catalyst with higher activity. Therefore, the research and engineering development of hydrogenation reactor and its internals have been paid great attention at home and abroad, and the reactor internals are constantly updated to achieve better results.

[0004] The hydrogenation reactor is usually fed from the center of the reactor top, and when the material is distributed through the inlet diffuser, the flow line of the liquid phase in the head space is inclined, and the residual kinetic energy will generate a strong inertial force, which will cause the material to accumulate along the four walls of the reactor after falling on the top distribution plate. Although the liquid layer of the top distribution plate tends to be horizontal under the action of gravity, as the processing scale of the hydrogenation device becomes larger and larger, the diameter of the hydrogenation reactor also gradually increases. From the engineering implementation, it can be observed that the liquid layer on the top distribution plate of the reactor presents an increasing distribution from the center position to the edge position, that is, the liquid layer height of the material in the center position area is relatively small, and the liquid layer height of the material at the edge wall is relatively large. The gas phase is affected by the partial pressure in the reactor head space, and after passing through the inlet diffuser, it will gather to the center area of the reactor, which will produce a completely opposite distribution rule to the liquid phase, resulting in that the larger the scale of the hydrogenation reactor, the more serious the distribution deviation of the gas-liquid phase material.

[0005] The hydrogenation process is an exothermic reaction, and uneven distribution of materials can cause the reaction to be more intense in areas where the catalyst is wet, the reaction rate is faster, and more heat is generated, which in turn affects the radial temperature difference of the reactor. When the radial temperature difference is large, the local temperature of the catalyst rises to form a superheating point, causing the performance of this part of the catalyst to be deactivated prematurely, damaging the performance of the catalyst, and even causing coking and hardening in some areas of the catalyst, preventing the material from flowing normally. Since the fixed-bed hydrogenation reactor is a trickle bed flow state, the catalyst below the hardened area cannot continue to function, which greatly reduces the service life of the catalyst and the operating cycle of the device, and the occurrence of local hardening also causes the pressure drop of the catalyst bed to rise, passively increasing the operating pressure of the reactor, which on the one hand increases energy consumption and on the other hand poses a hidden danger to the stable operation of the device. When the pressure drop rises too quickly to reach the design value of the reactor, it must be shut down abnormally for head removal, incurring additional inspection and repair costs, and the screening of the catalyst also causes the loss and waste of the catalyst.

[0006] Traditional hydrogenation reactors have a layer of gas-liquid pre-distribution tray placed above the top distribution tray to improve the inlet conditions of the top distributor. Chinese patent CN109985573A discloses a hydrogenation reactor that improves the uniformity of the liquid phase, and a folded-edge shock-reducing and flow-distributing tray is arranged in the headspace of the reactor or on the upper end of the reactor cylinder. The material is distributed to the top distribution tray by a chimney-type distributor arranged vertically on the tray, providing a smooth and uniform inlet condition for the top distribution tray, optimizing the material distribution of the top bed, and achieving the function of preliminary distribution. Chinese patent CN204058374U discloses a fluid pre-distributor and a fluid pre-distribution tray, which pre-distribute the hydrogenation feedstock by installing a fluid pre-distribution tray above the gas-liquid distribution tray in the fixed-bed hydrogenation reactor, reducing the impact of the gas-liquid two-phase on the lower gas-liquid distribution tray, and maintaining a stable liquid level to form a more uniform and better distribution effect.

[0007] The existing technology does not fundamentally solve the problem of incremental distribution of the liquid phase from the center to the edge of the tray. First, the reason for the accumulation of the liquid phase comes from the change of the material flow line by the inlet diffuser. Although the addition of the gas-liquid pre-distribution tray avoids direct impact on the top distribution tray, it still forms an incremental distribution on the pre-distribution tray. The distributors on the pre-distribution tray usually need to reach a certain liquid level height before they enter the working state, which leads to the formation of a liquid phase blank area in the center of the top distribution tray when the distributors at the edge of the reactor start to work due to insufficient liquid level height in the center of the pre-distribution tray. This still forms an incremental distribution from the center to the edge. Even the best distributor cannot achieve uniform distribution of materials under different liquid level conditions, which severely affects the working effect of the top distributor and inevitably widens the radial temperature difference.

[0008] Secondly, the gas phase is affected by the pressure distribution in the reactor head space, and after passing through the inlet diffuser, the gas phase will gather to the center area of the reactor, forming a distribution rule completely opposite to the liquid phase. When the distributor at the center position of the pre-distribution plate cannot be normally started, the gas phase can directly pass through the pre-distribution plate without mixing with the liquid phase, and in severe cases, it can directly pass through the top distribution plate into the catalyst bed, and as the diameter of the hydrogenation reactor becomes larger and larger, it causes a great deviation of the gas-liquid phase material distribution.

[0009] Thirdly, in order to ensure that the amount of liquid phase flowing through each distributor is the same, and to achieve uniform coverage of the material to the catalyst bed, the pre-distribution plate has a very high requirement for the levelness, but as the diameter of the current hydrogenation reactor becomes larger and larger, the tray is usually installed in a block combination manner, and the overall levelness of the distribution plate cannot be accurately guaranteed. The installation error will cause the distribution plate to have a tilt of 1 / 8° to 1 / 2° along the horizontal direction, and the maximum tilt can reach 3 / 2°. Even if the levelness is high at the beginning of installation, it will also lose the levelness during operation due to the combined action of thermal expansion and material impact load, thereby affecting the use effect of the distributor.

[0010] The information disclosed in this BACKGROUND section is only for the purpose of increasing the understanding of the overall background of the present application and should not be taken as an acknowledgment or any form of suggestion that it forms the prior art that is already known to those of ordinary skill in the art. SUMMARY

[0011] One of the purposes of the present application is to provide a hydrogenation reactor and a pre-distribution plate thereof, so as to improve the problem of uneven gas-liquid phase material distribution caused by the inlet diffuser in the existing hydrogenation reactor.

[0012] Another purpose of the present application is to provide a hydrogenation reactor and a pre-distribution plate thereof, so as to improve the problems of high installation precision requirement of the pre-distribution plate and easy deformation during operation in the existing hydrogenation reactor.

[0013] In order to achieve the above-mentioned purposes, according to a first aspect of the present application, the present application provides a pre-distribution plate, comprising: a plurality of trays including a circular tray and a plurality of annular trays, the inner and outer diameters of the plurality of trays are matched in sequence and are distributed in a multi-layered stepped manner with the circular tray as the center, the circular tray is the lowest layer, and the annular tray with the largest outer diameter is the highest layer, and each of the plurality of trays is provided with a plurality of sieve holes; and a connecting piece connecting two adjacent layers of trays and sealing the interlayer gap of the two adjacent layers of trays.

[0014] Further, in the above technical solution, each annular tray is spliced by a plurality of tray plates.

[0015] Further, in the technical solution, the connecting piece comprises a vertical part and a horizontal part, the inner edge of the upper tray is connected with the vertical part, and the outer edge of the lower tray is connected with the horizontal part.

[0016] Further, in the technical solution, the connecting piece and the adjacent two trays are connected by one or more of welding, threaded connection and buckle connection.

[0017] Further, in the technical solution, the connecting piece is a folded edge extending downward from the inner edge of the ring tray.

[0018] Further, in the technical solution, the connecting piece is an angle steel, and the angle steel is welded on the inner edge of each ring tray.

[0019] Further, in the technical solution, the connecting piece is an I-beam, and the inner edge of the upper tray is overlapped on the upper surface of the upper flange of the I-beam, and the outer edge of the lower tray is overlapped on the upper surface of the lower flange of the I-beam.

[0020] Further, in the technical solution, the I-beam is a ring beam.

[0021] Further, in the technical solution, the pre-distribution tray further comprises a plurality of support beams arranged in the radial direction, and the plurality of support beams are connected with the adjacent two ring beams, respectively.

[0022] Further, in the technical solution, the height difference between the adjacent two trays is 70-400 mm.

[0023] According to the second aspect of the present application, the present application provides a hydrogenation reactor, comprising: a body in a cylindrical structure, a feed inlet is arranged at the center of the upper end of the body; an inlet diffuser is arranged at the feed inlet; a pre-distribution tray according to any one of the above technical solutions is coaxially arranged below the inlet diffuser; and a top distribution tray is arranged below the pre-distribution tray.

[0024] Further, in the technical solution, a protrusion is arranged on the inner wall of the body, and the outer periphery of the pre-distribution tray is mounted in the body through the protrusion.

[0025] Further, in the technical solution, the protrusion is welded in the upper head of the body.

[0026] Further, in the technical solution, the diameter of the body is greater than or equal to 3.5 m.

[0027] Compared with the prior art, the present application has one or more of the following beneficial effects:

[0028] 1. The pre-distribution plate of the present application forms a multi-layer stepped distribution through a circular tray and a plurality of annular trays, changes the arrangement of the conventional pre-distribution plate, ensures that the liquid layers on each tray are not at the same level through the fault made between adjacent trays, reduces the hindering effect of the same direction liquid in the flow process, avoids the accumulation of liquid phase around the reactor; the liquid layers on adjacent trays do not directly contact, there is no single continuous liquid surface covering the entire reactor cross section, which fundamentally breaks the "bridge" effect generated by the mutual support between liquid phases, and eliminates the incremental distribution phenomenon of liquid layers from the center position to the edge position.

[0029] 2. The pre-distribution plate of the present application does not set a conventional gas-liquid distributor, the liquid phase flows down through the screen holes on each layer of the tray, and the amount of liquid phase passing through each screen hole is basically the same, which ensures that the gas partial pressure at each part of the reactor cross section is approximately the same, realizes the uniform distribution of the gas phase, avoids the great deviation of the gas-liquid phase materials, and provides a good prerequisite for the stable operation of the hydrogenation device.

[0030] 3. The trays in the pre-distribution plate of the present application are at different horizontal positions, which effectively reduces the cumulative error in the radial direction, and only needs to ensure the levelness of the trays in the same layer during installation, without the need to accurately ensure the overall levelness of the pre-distribution plate, thereby reducing the installation difficulty of the pre-distribution plate.

[0031] 4. The pre-distribution plate of the present application can not use a conventional support, but is self-supported through the rigidity of the tray, and the entire pre-distribution plate is tilted towards the center direction by using the weight of the tray, so that the levelness of the trays in the same layer during installation does not need to be ensured, and the overall levelness of the pre-distribution plate does not need to be accurately ensured, thereby reducing the installation difficulty of the tray.

[0032] 5. Each tray can be divided into a plurality of tray plates according to the size of the manhole, and the number of tray plates and the number of tray layers increase accordingly as the diameter of the hydrogenation reactor increases, thereby improving the resistance to thermal expansion and material impact load during device operation.

[0033] The above description is only a summary of the technical solutions of the present application, in order to more clearly understand the technical means of the present application and can be implemented according to the content of the specification, at the same time, in order to make the above and other purposes, technical features and advantages of the present application more easily understood, one or more preferred embodiments are listed as follows, and are described in detail as follows with reference to the drawings. BRIEF DESCRIPTION OF DRAWINGS

[0034] Figure 1 is a partial structure schematic diagram of a hydrogenation reactor according to an embodiment of the present application.

[0035] Figure 2 is a top view structure schematic diagram of a pre-distribution plate according to an embodiment of the present application.

[0036] Figure 3 is a partial structural schematic diagram of a hydrogenation reactor according to another embodiment of the present application.

[0037] Figure 4 is a bottom structural schematic diagram of a pre-distribution tray according to another embodiment of the present application.

[0038] Explanation of Reference Numerals:

[0039] 100 - hydrogenation reactor, 110 - body, 111 - feed inlet, 112 - boss, 120 - inlet diffuser, 130 - pre-distribution tray, 131 - circular tray, 132 - ring tray, 1320 - tray plate, 133 - connecting piece, 1331 - vertical portion, 1332 - horizontal portion, 140 - top distribution tray, 150 - catalyst bed.

[0040] 200 - hydrogenation reactor, 210 - body, 211 - feed inlet, 212 - boss, 220 - inlet diffuser, 230 - pre-distribution tray, 231 - circular tray, 232 - ring tray, 233 - I-beam, 234 - support beam, 240 - top distribution tray, 250 - catalyst bed. DETAILED DESCRIPTION

[0041] The specific embodiments of the present application will be described in detail below with reference to the attached drawings, but the scope of protection of the present application is not limited by the specific embodiments.

[0042] Unless otherwise clearly indicated, throughout the description and the claims, the term "comprise" or variations such as "comprises" or "comprising" will be understood to imply the inclusion of a stated element or group of elements but not the exclusion of any other element or group of elements.

[0043] In this document, spatially relative terms, such as "beneath", "below", "lower", "above", "upper", and the like, can be used to describe one element's or feature's relationship to another element or feature as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientations depicted in the figures. For example, if the device in the figures is turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the other elements or features. Thus, the exemplary term "below" can encompass both an orientation of above and below. The device can be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative terms used herein interpreted accordingly.

[0044] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0045] like Figure 1 As shown, the hydrogenation reactor according to a specific embodiment of the present invention has a cylindrical body 110, and a feed inlet 111 is provided at the center of the upper end of the body 110. An inlet diffuser 120 is provided at the feed inlet 111, and a pre-distribution disk 130, a top distribution disk 140, and a catalyst bed 150 are arranged sequentially from top to bottom below the inlet diffuser 120.

[0046] Furthermore, in one or more exemplary embodiments of the present invention, a ring of bosses 112 is provided on the inner wall of the body 110, and the outer periphery of the pre-dispensing disc 130 is mounted inside the body 110 via the bosses 112. Furthermore, in one or more exemplary embodiments of the present invention, the bosses 112 are welded to the upper end cap of the body 110. It should be understood that the bosses 112 may also not be provided inside the upper end cap.

[0047] Combination Figure 1 and Figure 2 As shown, the pre-dispensing tray 130 according to a specific embodiment of the present invention includes multiple trays, one of which is a circular tray 131, and the others are annular trays 132. The inner and outer diameters of the multiple trays are matched sequentially, and they are distributed in multiple stepped layers with the circular tray 131 as the center, wherein the circular tray 131 is the lowest layer, and the annular tray 132 with the largest outer diameter is the highest layer. Both the circular tray 131 and the multiple annular trays 132 are provided with multiple sieve holes (not shown in the figure). Adjacent trays are connected by connectors 133, and the connectors 133 seal the interlayer gap between adjacent trays.

[0048] Furthermore, in one or more exemplary embodiments of the present invention, each annular tray 132 may be formed by splicing together multiple tray plates 1320, such as... Figure 2 As shown. The tray plate 1320 can be divided according to the size of the manhole.

[0049] Further, in one or more exemplary embodiments of the present application, the connecting piece 133 comprises a vertical portion 1331 and a horizontal portion 1332, the inner edge of the upper tray is connected with the vertical portion 1331, and the outer edge of the lower tray is connected with the horizontal portion 1332, and the vertical portion 1331 seals the gap between the adjacent two layers of trays. Exemplarily, the connecting piece 133 can be a folded edge extending downward from the inner edge of the annular tray 132, and the connecting piece 133 can also be an angle steel welded on the inner edge of the annular tray 132, and the present application is not limited thereto. Further, in one or more exemplary embodiments of the present application, the height difference between the adjacent two layers of trays is about 70-200 mm.

[0050] Further, in one or more exemplary embodiments of the present application, as shown in Figure 1 the horizontal portion 1332 of the connecting piece 133 is threadedly connected with the outer edge of the lower tray of the adjacent two layers of trays. It should be understood that the connecting piece 133 and the adjacent two layers of trays can be connected by one or more of welding, thread connection and buckle connection, and the present application is not limited thereto.

[0051] In combination Figure 1 , in one or more exemplary embodiments of the present application, the working process of the pre-distribution tray 130 is as follows: the material enters the body 110 of the hydrogenation reactor through the inlet diffuser 120 from the feed inlet 111, and is sprayed in a diagonal flow state under the strong impact of residual kinetic energy. The liquid phase first gathers along the inner wall of the body 110, and the liquid layer tends to flow to the center position under the action of gravity, and part of the liquid phase will fall into the top distribution tray 140 through the sieve hole of the annular tray 132, and the remaining liquid phase will flow through the annular tray 132. Since the adjacent trays are arranged in a stepped manner in the axial direction, the liquid phase on each layer of trays is not at the same horizontal plane, and there is no direct contact between the liquid layers, and the remaining liquid phase is hindered by the inner wall of the body 110 or the vertical portion of the connecting piece 133, and can only flow inward through the artificially created fault to flow to the lower tray.

[0052] As shown in Figure 3 , the hydrogenation reactor according to the specific embodiment of the present application has a cylindrical body 210, and the upper end of the body 210 is provided with a feed inlet 211. The inlet diffuser 220 is arranged at the feed inlet 211, and the pre-distribution tray 230, the top distribution tray 240 and the catalyst bed 250 are sequentially arranged from top to bottom below the inlet diffuser 220.

[0053] Further, in one or more exemplary embodiments of the present application, a ring of bosses 212 is arranged on the inner wall of the body 210, and the outer periphery of the pre-distribution tray 230 is mounted in the body 210 through the bosses 212. Further, in one or more exemplary embodiments of the present application, the bosses 212 are welded in the upper head of the body 210.

[0054] Combination Figure 3 and Figure 4 As shown, the pre-distribution tray 230 according to a specific embodiment of the present invention includes multiple trays, one of which is a circular tray 231, and the others are annular trays 232. The inner and outer diameters of the multiple trays are matched sequentially, and they are distributed in multiple stepped layers with the circular tray 231 as the center, where the circular tray 231 is the lowest layer and the annular tray 232 with the largest outer diameter is the highest layer. Both the circular tray 231 and the multiple annular trays 232 are provided with multiple sieve holes. Each annular tray 232 can be assembled from multiple tray plates divided according to the size of the manhole. Adjacent tray layers are connected by an I-beam 233. In two adjacent tray layers, the inner edge of the upper tray overlaps the upper surface of the upper flange of the I-beam 233, and the outer edge of the lower tray overlaps the upper surface of the lower flange of the I-beam 233. The web of the I-beam 233 seals the interlayer gap between adjacent tray layers. For example, the I-beam 233 is a ring beam, and adjacent layers of I-beams 233 (ring beams) are connected by multiple radially arranged support beams 234 to form an integral mounting frame. The distribution of the support beams 234 and the ring beams can be as follows: Figure 4 As shown, the present invention is not limited thereto. Furthermore, in one or more exemplary embodiments of the present invention, the height difference between two adjacent trays is approximately 200–400 mm, i.e., the height of the I-beam.

[0055] refer to Figure 3 In one or more exemplary embodiments of the present invention, the pre-distribution tray 230 operates as follows: Material enters the body 210 of the hydrogenation reactor through the inlet 211 and inlet diffuser 220. Under the powerful impact of residual kinetic energy, it is sprayed outwards in an oblique flow pattern. The liquid phase first accumulates along the inner wall of the body 210. Under gravity, the liquid layer tends to flow towards the center. Some of the liquid phase falls into the top distribution tray 240 through the sieve holes on the annular tray 232, while the remaining liquid phase flows through the annular tray 232. Because adjacent trays are arranged in a stepped manner along the axial direction, the liquid phases on each tray are not on the same horizontal plane, and there is no direct contact between the liquid layers. The remaining liquid phase is obstructed by the inner wall of the body 210 or the web of the I-beam 233, and can only flow inwards through the artificially created fault to reach the lower tray.

[0056] The present invention will now be described in more detail by way of specific embodiments. It should be understood that the present invention is not limited thereto.

[0057] Example 1

[0058] In this embodiment, reference Figure 1 and Figure 2As shown in the figure, the pre-distribution tray 130 of the present application is arranged between the inlet diffuser 120 and the top distribution tray 140 of the hydrogenation reactor 100. The diameter of the hydrogenation reactor 100 is 3.5 m, and the structure of the pre-distribution tray 130 is as described above, wherein the annular tray 132 is divided into a plurality of tray plates 1320 according to the size of the manhole, and the inner edge of each tray plate 1320 is welded with an angle steel 133 as a connecting piece. # The body 110 of the hydrogenation reactor 100 of the embodiment is provided with a ring-shaped boss 112.

[0059] During installation, the outer edges of the plurality of tray plates 1320 of the outermost annular tray 132 are bolted to the boss 112, the outer edges of the plurality of tray plates 1320 of the next annular tray 132 are bolted to the angle steel of the outermost annular tray 132, and finally the outer edges of the circular tray 131 are bolted to the angle steel of the middle annular tray 132. The height difference between the adjacent two layers of trays is about 75 mm. The pre-distribution tray 132 of the embodiment is not supported by the conventional support form, but is self-supported by the rigidity of the tray. During installation, the levelness of the trays in the same layer does not need to be ensured, and the overall levelness of the pre-distribution tray does not need to be accurately ensured, thereby reducing the installation difficulty of the trays.

[0060] The pre-distribution tray 130 is not provided with a traditional gas-liquid distributor, which avoids the deviation of the distribution of gas-liquid phase materials and provides a friendly, stable and uniform inlet condition for the top distribution tray 140. Together with the top distribution tray 140, the pre-distribution tray 130 realizes the uniform distribution of materials on the downstream catalyst bed 150. After the pre-distribution tray 130 of the embodiment is used, by comparing the five temperature measuring points arranged at the same height, it can be found that the maximum bed radial temperature difference of the catalyst bed 150 is reduced from 11.6℃ to 1.6℃.

[0061] Example 2

[0062] In the embodiment, reference is made to Figure 3 and Figure 4 As shown in the figure, the pre-distribution tray 230 of the present application is arranged between the inlet diffuser 220 and the top distribution tray 240 of the hydrogenation reactor 200. The diameter of the hydrogenation reactor 200 is 5.8 m, and the structure of the pre-distribution tray 230 is as described above, wherein the annular tray 232 is divided into a plurality of tray plates according to the size of the manhole. The connecting piece is an I-beam 233, and the I-beam 233 is a ring beam, and the adjacent two layers of ring beams are connected by a support beam 234. The body 210 of the hydrogenation reactor 200 of the embodiment is provided with a ring-shaped boss 212.

[0063] During installation, the mounting frame composed of the I-beam 233 (ring beam) and the support beam 234 is fixed in the body 210 of the hydrogenation reactor 200, and the multiple tray plates of each layer of the annular tray 232 and the circular tray 231 are respectively connected and installed with the ring beam. The height difference between the adjacent two layers of trays is about 260 mm.

[0064] The great deviation of gas-liquid phase materials is avoided by the pre-distribution tray 230, and the top distribution tray 240 is provided with friendly, stable and uniform inlet conditions, and the uniform distribution of materials on the downstream catalyst bed 250 is realized together with the top distribution tray 240. After the pre-distribution tray 230 of the embodiment is adopted, by comparing the five temperature measuring points arranged at the same height, it can be found that the maximum bed radial temperature difference of the catalyst bed 250 is reduced from the original 13.4°C to 1.8°C.

[0065] The foregoing description of specific exemplary embodiments of the application is presented for the purpose of illustration and description. It is not intended to be a limitation on the precise form disclosed, and clearly, many modifications and variations are possible in light of the above teachings. The exemplary embodiments were chosen and described in order to explain the principles of the application and its practical application, thereby enabling others skilled in the art to implement and utilize the application in various embodiments and with various modifications as are suited to the particular use contemplated. Any simple modification, equivalent replacement, and modification of the above-described exemplary embodiments should fall within the scope of the application.

Claims

1. A pre-dispensing tray, characterized in that, The application is applied in a hydrogenation reactor, comprising: a plurality of trays including a circular tray and a plurality of annular trays, the inner and outer diameters of the plurality of trays are matched in turn and are distributed in a plurality of layers of steps with the circular tray as the center, the circular tray is the lowest layer, and the annular tray with the largest outer diameter is the highest layer, the plurality of trays are each provided with a plurality of sieve holes; liquid phase flows down through the sieve holes on each layer of trays, the amount of liquid phase passing through each sieve hole is basically the same, which ensures that the gas partial pressure at each part of the entire reactor cross section is basically the same, and uniform distribution of the gas phase is realized; and a connecting piece connecting and sealing the interlayer gap of the adjacent two layers of trays; the connecting piece includes a vertical part and a horizontal part, the inner edge of the upper tray in the adjacent two layers of trays is connected with the vertical part, and the outer edge of the lower tray is connected with the horizontal part, and the vertical part seals the interlayer gap of the adjacent two layers of trays; the liquid phase first gathers along the inner wall of the reactor body, the liquid layer tends to flow to the center position under the action of gravity, part of the liquid phase falls into the top distribution plate through the sieve holes on the annular tray, and the remaining liquid phase flows through the annular tray; the remaining liquid phase is hindered by the inner wall of the reactor body or the vertical part of the connecting piece, can only flow inwards through the artificially created fault to flow to the lower tray.

2. The pre-portioned tray of claim 1, wherein, Each of the annular trays is spliced by a plurality of tray plates.

3. The pre-portioned tray of claim 1, wherein, The connecting piece and the adjacent two layers of trays are connected by one or more of welding, threaded connection and buckle connection.

4. The pre-portioned tray of claim 1, wherein, The connecting piece is a folded edge extending downward from the inner edge of the annular tray.

5. The pre-portioned tray of claim 1, wherein, The connecting piece is an angle steel welded on the inner edge of each annular tray.

6. The pre-portioned tray of claim 1, wherein, The connecting piece is an I-beam, the inner edge of the upper tray in the adjacent two layers of trays is lapped on the upper surface of the upper flange of the I-beam, and the outer edge of the lower tray is lapped on the upper surface of the lower flange of the I-beam.

7. The pre-portioned tray of claim 6, wherein, The I-beam is a ring beam.

8. The pre-portioned tray of claim 7, wherein, Further comprising: a plurality of support beams arranged in the radial direction, the plurality of support beams are respectively connected with the adjacent two layers of ring beams.

9. The pre-portioned tray of claim 1, wherein, The height difference between the adjacent two layers of trays is 70-400 mm.

10. A hydrogenation reactor characterized by, Comprising: a body in a cylindrical structure, a feed inlet is arranged at the center of the upper end of the body; an inlet diffuser arranged at the feed inlet; a pre-distribution plate coaxially arranged below the inlet diffuser according to any one of claims 1-9; and a top distribution plate arranged below the pre-distribution plate.

11. The hydrogenation reactor of claim 10, wherein, A protrusion is arranged on the inner wall of the body, and the outer periphery of the pre-distribution plate is mounted on the body through the protrusion.

12. The hydrogenation reactor of claim 11, wherein, The protrusion is welded in the upper head of the body.

13. The hydrogenation reactor of claim 10, wherein, The diameter of the body is greater than or equal to 3.5 m.

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