CN116020395A - Hydrogenation reactor and pre-distribution plate thereof - Google Patents

Abstract

The invention discloses a pre-distribution plate, which comprises: the plurality of trays comprise a circular tray and a plurality of annular trays, the inner diameter and the outer diameter of the plurality of trays are sequentially matched and are distributed in a multi-layer stepped mode by taking the circular tray as a 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 all provided with a plurality of sieve holes; and a connecting member connecting the adjacent two trays and sealing the inter-layer gap of the adjacent two trays. The invention also discloses a hydrogenation reactor. The pre-distribution plate disclosed by the invention is formed into multi-layer stepped distribution through the circular tray and the plurality of annular trays, the arrangement mode of the traditional pre-distribution plate is changed, and the liquid phase is prevented from accumulating around the reactor through faults manufactured between the adjacent trays; the incremental distribution phenomenon of the liquid layer from the central position to the edge position is eliminated; the integral levelness of the pre-distribution plate is not required to be ensured accurately, so that the installation difficulty is reduced.

Description

Hydrogenation reactor and pre-distribution plate thereof

Technical Field

The invention relates to the technical field of hydrogenation reaction equipment, in particular to hydrogenation reaction equipment with larger reactor scale, and particularly relates to a hydrogenation reactor and a pre-distribution disc thereof.

Background

In recent years, with the rapid development of economy and the enhancement of environmental awareness, the requirements on quality and environmental protection of petrochemical products are higher and higher. As one of the technical means for producing clean fuels, the importance and the roles of hydrogenation technology in the oil refining industry are increasing. In a hydrogenation device, the hydrogenation catalyst technology and the hydrogenation process technology are the same, the internal component technology of the hydrogenation reactor is also an important component part of a reaction system, and the three components form three factors of the performance of the reactor.

In a hydrogenation device, a hydrogenation reactor serving as key equipment is used for refining, cracking and other reactions of raw oil mixed with hydrogen according to a certain proportion under the action of a hydrogenation catalyst. Whether the hydrogenation reaction in the hydrogenation reactor can be stably operated, whether the hydrogenation catalyst can fully play the role of the hydrogenation reaction, whether the product quality can reach high quality or not depends on the uniformity of the distribution of the gas phase and the liquid phase in the catalyst bed layer to a great extent. Whether the distribution of the gas phase and the liquid phase in the catalyst bed is uniform or not has close relation with the design of the internal components of the hydrogenation reactor. It can be said that the performance of the inner member directly affects the service life of the catalyst, the quality of the product and the running period of the device, and the inner member of the hydrogenation reactor with excellent performance is not inferior to the replacement of a hydrogenation catalyst with higher activity. Therefore, research and engineering development of the hydrogenation reactor and the internal components thereof are always very important at home and abroad, and the internal components of the reactor are continuously updated to obtain better effects.

The hydrogenation reactor is usually fed from the center position of the top of the reactor, when materials are distributed through an inlet diffuser, a streamline of a liquid phase in a head space is an inclined line, and residual kinetic energy of the liquid phase can generate strong inertia force, so that the residual kinetic energy falls on a top distribution plate and is accumulated along the periphery of the reactor. Although the liquid layer of the top distribution plate tends to be horizontal under the action of gravity, as the treatment scale of the hydrogenation device is larger and larger, the diameter of the hydrogenation reactor is gradually increased, and the liquid layer on the top distribution plate of the reactor is gradually distributed from the central position to the edge position, namely the height of the liquid layer in the central position area is relatively smaller, and the height of the liquid layer at the side wall is relatively larger, which can be obviously observed from engineering implementation. The gas phase is affected by partial pressure in the space of the reactor head, and gathers towards the central area of the reactor after passing through the inlet diffuser, so that a distribution rule which is completely opposite to the liquid phase is generated, and the larger the scale of the hydrogenation reactor is, the more serious the distribution deviation of gas-liquid phase materials is.

The hydrogenation process is exothermic reaction, uneven material distribution can lead to severe reaction degree at the position with good catalyst wetting effect, and the faster the reaction rate, the more heat generated, thereby affecting the radial temperature difference of the reactor. When the radial temperature difference is large, the local temperature of the catalyst rises to form hot spots, so that the performance of the catalyst is deactivated prematurely, the performance of the catalyst is damaged, even coking and hardening of the catalyst in a partial area can be caused, and materials can not normally flow. Because the fixed bed hydrogenation reactor is in a trickle bed state, the catalyst below the hardening area cannot continue to play a role, the service life of the catalyst and the operating period of the device can be greatly reduced, the local hardening phenomenon can also cause the pressure drop of the catalyst bed to be increased, the operating pressure of the reactor is passively increased, on one hand, the energy consumption is increased, and on the other hand, hidden danger is brought to the stable operation of the device. When the pressure drop is excessively fast increased to reach the design value of the reactor, abnormal shutdown is required, skimming treatment is carried out, inspection and maintenance cost is additionally paid, and meanwhile, catalyst loss and waste are caused by screening of the catalyst.

A layer of gas-liquid pre-distribution plate is added above the top distribution plate of the traditional hydrogenation reactor to improve the inlet condition of the work of the top distribution plate. Chinese patent CN109985573a discloses a hydrogenation reactor for improving uniformity of liquid phase, in the idle space of the upper end enclosure of the reactor or at the upper end of the reactor cylinder, a hemming type flow reducing and equalizing disc is arranged, materials are distributed to a top distribution disc through a chimney type distributor vertically arranged on the tray, a stable and uniform inlet working condition is provided for the top distribution disc, material distribution of a top bed layer is optimized, and a primary distribution function is realized. Chinese patent CN204058374U discloses a fluid pre-distributor and a fluid pre-distributor tray, which pre-distributes hydrogenation raw materials by means of the fluid pre-distributor tray installed above the gas-liquid distributor tray in the fixed bed hydrogenation reactor, reduces the impact of the gas-liquid two-phase lower gas-liquid distributor tray, and keeps the liquid level stable to form a more uniform and good distribution effect.

The prior art does not fundamentally solve the problem of incremental distribution of liquid phase from a central position to an edge position on a tray, firstly, the reason for liquid phase aggregation is from the change of material streamline by an inlet diffuser, and the incremental distribution is still formed on a pre-distribution plate although the top distribution plate is prevented from being directly influenced after the gas-liquid pre-distribution plate is additionally arranged. The distributor with the distribution function on the pre-distribution plate usually needs to reach a certain liquid layer height to enter a working state, so that when the distributor at the side wall of the reactor is started, the distributor in the central position area of the pre-distribution plate still forms an incremental distribution phenomenon from the central position to the edge position due to the fact that the liquid layer height is insufficient and a liquid phase blank area appears in the center of the top distribution plate. Even the best performance distributor can not realize even distribution of materials under the condition of liquid layers with different heights, the working effect of the top distributor is seriously affected, and the expansion of radial temperature difference is unavoidable.

Secondly, the gas phase is influenced by the pressure distribution in the space of the reactor head, and the gas phase can be gathered to the central area of the reactor after passing through the inlet diffuser, so that a distribution rule which is completely opposite to the liquid phase is formed. When the distributor in the central position area of the pre-distributing disc can not be normally started, the gas phase can directly pass through the pre-distributing disc without being mixed with the liquid phase, and seriously and even directly pass through the top distributing disc to enter the catalyst bed layer, so that the gas-liquid phase material distribution generates great deviation along with the increasing diameter of the hydrogenation reactor.

Thirdly, in order to ensure that the liquid phase amount flowing through each distributor is the same, the uniform coverage of materials to the catalyst bed layer is realized, the requirement of a pre-distribution plate on levelness is extremely high, but as the diameter of the current hydrogenation reactor is larger and larger, the tray is installed in a block combination mode, and the integral levelness of a distribution plate surface cannot be accurately ensured. The distribution plate surface is inclined by 1/8-1/2 degrees along the horizontal direction due to common installation errors, and the maximum inclination can reach 3/2 degrees, so that even if the levelness at the beginning of installation is higher, the levelness can be lost due to the combined action of thermal expansion and material impact load in the operation process, and the using effect of the distributor is further affected.

The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information forms the prior art already known to a person of ordinary skill in the art.

Disclosure of Invention

The invention aims to provide a hydrogenation reactor and a pre-distribution plate thereof, so as to solve the problem of uneven distribution of gas-liquid phase materials caused by an inlet diffuser in the existing hydrogenation reactor.

Another object of the present invention is to provide a hydrogenation reactor and a pre-distribution plate thereof, so as to solve the problems of high installation accuracy requirement of the pre-distribution plate in the existing hydrogenation reactor, easy deformation in the operation process, etc.

To achieve the above object, according to a first aspect of the present invention, there is provided a pre-distribution plate comprising: the plurality of trays comprise a circular tray and a plurality of annular trays, the inner diameter and the outer diameter of the plurality of trays are sequentially matched and are distributed in a multi-layer stepped mode by taking the circular tray as a 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 all provided with a plurality of sieve holes; and a connecting member connecting the adjacent two trays and sealing the inter-layer gap of the adjacent two trays.

Furthermore, in the technical scheme, each annular tray is formed by splicing a plurality of tray plates.

Further, in the above-mentioned technical scheme, the connecting piece includes vertical portion and horizontal portion, in two-layer adjacent tower trays, the inner edge of upper tray is connected with vertical portion, and the outer edge of lower floor's tower tray is connected with horizontal portion, and vertical portion is sealed the interlaminar clearance of two-layer adjacent tower trays.

Further, in the above technical scheme, one or more of welding, threaded connection and snap connection are adopted between the connecting piece and the two adjacent layers of trays.

Further, in the above technical solution, the connecting member is a flange extending downward from an inner edge of the annular tray.

Further, in the above technical scheme, the connecting piece is angle steel, and the angle steel is welded on the inner edge of each annular tray.

Further, in the technical scheme, the connecting piece is an I-shaped beam, the inner edge of the upper tray is lapped on the upper surface of the upper wing plate of the I-shaped beam, and the outer edge of the lower tray is lapped on the upper surface of the lower wing plate of the I-shaped beam in two adjacent trays.

Furthermore, in the above technical solution, the i-beam is a ring beam.

Further, in the above technical solution, the pre-allocation disk further includes: the support beams are arranged along the radial direction and are respectively connected with two adjacent layers of ring beams.

Further, in the technical scheme, the height difference of two adjacent trays is 70-400 mm.

According to a second aspect of the present invention there is provided a hydrogenation reactor comprising: the body is of a cylindrical structure, and a feed inlet is arranged in the center of the upper end of the body; an inlet diffuser disposed at the feed inlet; the pre-distribution plate according to any one of the above technical solutions, coaxially arranged under the inlet diffuser; and a top distribution tray disposed below the pre-distribution tray.

Further, in the above technical scheme, a circle of boss is arranged on the inner wall of the body, and the periphery of the pre-distribution plate is arranged in the body through the boss.

Further, in the above technical scheme, the boss is welded in the upper seal head of the body.

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

Compared with the prior art, the invention has one or more of the following beneficial effects:

1. the pre-distribution plate disclosed by the invention is formed into multi-layer stepped distribution through the circular tray and the plurality of annular trays, so that the arrangement mode of the traditional pre-distribution plate is changed, and the liquid layers on all trays are not in the same horizontal plane through faults manufactured between the adjacent trays, so that the blocking effect of the same-direction liquid in the flowing process is reduced, and the liquid phase is prevented from accumulating around the reactor; the liquid layers on the adjacent trays are not in direct contact, and single continuous liquid level which is distributed over the section of the whole reactor is not present, so that the bridge approach effect generated by mutual support between liquid phases is fundamentally broken, and the incremental distribution phenomenon of the liquid layers from the central position to the edge position is eliminated.

2. The pre-distribution plate is not provided with a conventional gas-liquid distributor, liquid phase flows down through the sieve holes on each layer of tray, the liquid phase quantity passing through each sieve hole is basically the same, the gas partial pressure of each part of the cross section of the whole reactor is ensured to be approximately the same, the uniform distribution of gas phase is realized, the generation of great deviation of gas-liquid phase materials is avoided, and good preconditions are provided for the stable operation of a hydrogenation device.

3. The trays in the pre-distribution tray are positioned at different horizontal positions, so that the accumulated error in the radial direction is effectively reduced, the levelness of the trays in the same layer is only required to be ensured in the installation process, and the integral levelness of the pre-distribution tray is not required to be accurately ensured, thereby reducing the installation difficulty of the pre-distribution tray.

4. The pre-distribution plate can be self-supported through the rigidity of the tray instead of the conventional support, the whole pre-distribution plate is inclined towards the center direction by utilizing the dead weight of the tray, the levelness of the tray in the same layer is not required to be ensured in the installation process, the integral levelness of the pre-distribution plate is not required to be accurately ensured, and therefore the installation difficulty of the tray is reduced.

5. Each tray can be divided into a plurality of tray plates according to the manhole size, the number of the tray plates and the number of the tray layers are correspondingly increased along with the increase of the diameter of the hydrogenation reactor, and the resistance to thermal expansion and material impact load in the running process of the device is improved.

The foregoing description is only an overview of the present invention, and it is to be understood that it is intended to provide a more clear understanding of the technical means of the present invention and to enable the technical means to be carried out in accordance with the contents of the specification, while at the same time providing a more complete understanding of the above and other objects, features and advantages of the present invention, and one or more preferred embodiments thereof are set forth below, together with the detailed description given below, along with the accompanying drawings.

Drawings

FIG. 1 is a schematic partial structure of a hydrogenation reactor according to an embodiment of the present invention.

Fig. 2 is a schematic top view of a pre-distribution tray according to an embodiment of the present invention.

Fig. 3 is a schematic partial structure of a hydrogenation reactor according to another embodiment of the present invention.

Fig. 4 is a schematic bottom view of a pre-distribution plate according to another embodiment of the present invention.

The main reference numerals illustrate:

100-hydrogenation reactor, 110-body, 111-feed inlet, 112-boss, 120-inlet diffuser, 130-pre-distribution tray, 131-circular tray, 132-annular tray, 1320-tray deck, 133-connector, 1331-vertical section, 1332-transverse section, 140-top distribution tray, 150-catalyst bed.

200-hydrogenation reactor, 210-body, 211-feed inlet, 212-boss, 220-inlet diffuser, 230-pre-distribution tray, 231-circular tray, 232-annular tray, 233-i-beam, 234-support beam, 240-top distribution tray, 250-catalyst bed.

Detailed Description

The following detailed description of embodiments of the invention is, therefore, to be taken in conjunction with the accompanying drawings, and it is to be understood that the scope of the invention is not limited to the specific embodiments.

Throughout the specification and claims, unless explicitly stated otherwise, the term "comprise" or variations thereof such as "comprises" or "comprising", etc. will be understood to include the stated element or component without excluding other elements or other components.

Spatially relative terms, such as "below," "beneath," "lower," "above," "upper," and the like, may be used herein for ease of description to describe one element's or feature's relationship to another element's or feature's in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the article in use or operation in addition to the orientation depicted in the figures. For example, if the article in the figures is turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the elements or features. Thus, the exemplary term "below" may encompass both a direction of below and a direction of above. The article may have other orientations (rotated 90 degrees or other orientations) and the spatially relative descriptors used herein interpreted accordingly.

The terms "first," "second," and the like herein are used for distinguishing between two different elements or regions and are not intended to limit a particular position or relative relationship. In other words, in some embodiments, the terms "first," "second," etc. may also be interchanged with one another.

As shown in fig. 1, the hydrogenation reactor according to the embodiment of the present invention has a cylindrical body 110, and a feed port 111 is provided at the center of the upper end of the body 110. An inlet diffuser 120 is arranged at the feed inlet 111, and a pre-distribution plate 130, a top distribution plate 140 and a catalyst bed 150 are arranged below the inlet diffuser 120 from top to bottom in sequence.

Further, in one or more exemplary embodiments of the present invention, a circle of bosses 112 are provided on an inner wall of the body 110, and an outer circumference of the pre-distribution plate 130 is installed in the body 110 through the bosses 112. Further, in one or more exemplary embodiments of the invention, the boss 112 is welded within the upper head of the body 110. It should be appreciated that boss 112 may not be disposed within the upper head.

As shown in connection with fig. 1 and 2, a pre-distribution tray 130 according to an embodiment of the present invention includes a plurality of trays, one of which is a circular tray 131 and the other is an annular tray 132. The inner diameters and the outer diameters of the trays are sequentially matched and are distributed in a multi-layer stepped mode by taking 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. The circular tray 131 and the plurality of annular trays 132 are each provided with a plurality of mesh openings (not shown). Adjacent trays are connected by a connector 133, and the connector 133 seals the inter-layer gap of the adjacent trays.

Further, in one or more exemplary embodiments of the invention, each annular tray 132 may be spliced from a plurality of tray panels 1320, as shown in FIG. 2. Tray deck 1320 may be divided according to the size of the manhole.

Further, in one or more exemplary embodiments of the present invention, the connection 133 includes a vertical portion 1331 and a lateral portion 1332, and an inner edge of an upper tray is connected to the vertical portion 1331 and an outer edge of a lower tray is connected to the lateral portion 1332, and the vertical portion 1331 seals an inter-layer gap of the adjacent two trays. Illustratively, the connecting member 133 may be a flange extending downward from the inner edge of the annular tray 132, or the connecting member 133 may be an angle steel welded to the inner edge of the annular tray 132, which is not limited to this. Further, in one or more exemplary embodiments of the present invention, the height difference between adjacent two layers of trays is about 70 to 200mm.

Further, in one or more exemplary embodiments of the present invention, the lateral portion 1332 of the connector 133 shown in fig. 1 is threaded with the outer edge of the lower tray of the adjacent two trays. It should be understood that one or more of welding, threading, and snap-fit connection may be used between the connector 133 and the adjacent two trays, and the invention is not limited thereto.

In one or more exemplary embodiments of the invention, and in conjunction with fig. 1, the pre-distribution tray 130 operates as follows, material enters the hydrogenation reactor body 110 from the feed inlet 111 via the inlet diffuser 120, and is ejected in a diagonal flow regime to the periphery 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 under gravity toward a central position, a portion of the liquid phase will fall through the mesh openings in the annular tray 132 into the top distribution tray 140, and the remaining liquid phase flows through the annular tray 132. Because the adjacent trays are arranged in a stepped manner along the axial direction, the liquid phases on each layer of trays are not in the same horizontal plane, the liquid phases are not in direct contact with each other, and the rest liquid phases are blocked by the inner wall of the body 110 or the vertical part of the connecting piece 133, and can only flow inwards through the artificially-made faults and then flow to the lower layer of trays.

As shown in fig. 3, the hydrogenation reactor according to the embodiment of the present invention has a cylindrical body 210, and a feed port 211 is provided at the center of the upper end of the body 210. An inlet diffuser 220 is arranged at the feed inlet 211, and a pre-distribution plate 230, a top distribution plate 240 and a catalyst bed 250 are arranged below the inlet diffuser 220 from top to bottom in sequence.

Further, in one or more exemplary embodiments of the present invention, a ring of bosses 212 are provided on the inner wall of the body 210, and the outer circumference of the pre-distribution plate 230 is mounted in the body 210 by the bosses 212. Further, in one or more exemplary embodiments of the invention, the boss 212 is welded within the upper head of the body 210.

As shown in connection with fig. 3 and 4, a pre-distribution tray 230 according to an embodiment of the present invention includes a plurality of trays, one of which is a circular tray 231 and the other is an annular tray 232. The inner diameters and the outer diameters of the trays are sequentially matched and are distributed in a multi-layer stepped mode by taking the circular tray 231 as the center, wherein the circular tray 231 is the lowest layer, and the annular tray 232 with the largest outer diameter is the highest layer. The circular tray 231 and the plurality of annular trays 232 are each provided with a plurality of mesh openings. Each of the ring-shaped trays 232 may be formed by splicing a plurality of tray decks divided according to the size of the manhole. The adjacent two layers of trays are connected through the I-beam 233, the inner edge of the upper layer of trays is lapped on the upper surface of the upper wing plate of the I-beam 233, the outer edge of the lower layer of trays is lapped on the upper surface of the lower wing plate of the I-beam 233, and the web plate of the I-beam 233 seals the interlayer gap of the adjacent two layers of trays. Illustratively, the i-beams 233 are ring beams, and two adjacent layers of i-beams 233 (ring beams) are connected by a plurality of radially disposed support beams 234 to form a unitary mounting bracket. The distribution of the support beams 234 and the ring beams can be shown in fig. 4, and the present invention is not limited thereto. Further, in one or more exemplary embodiments of the present invention, the height difference between adjacent two layers of trays is about 200 to 400mm, i.e., the height of an I-beam.

Referring to fig. 3, in one or more exemplary embodiments of the present invention, the pre-distribution tray 230 operates as follows, and material is introduced into the body 210 of the hydrogenation reactor from the feed inlet 211 through the inlet diffuser 220, and is sprayed in a diagonal flow pattern to the periphery under the strong impact of residual kinetic energy. The liquid phase first gathers along the inner wall of the body 210 and the liquid layer tends to flow under gravity toward a central location, a portion of the liquid phase will fall through the mesh openings in the annular tray 232 into the top distribution tray 240, and the remaining liquid phase flows through the annular tray 232. Because the adjacent trays are arranged in a stepped manner along the axial direction, the liquid phases on each layer of trays are not in the same horizontal plane, the liquid phases are not in direct contact with each other, and the rest liquid phases are blocked by the inner wall of the body 210 or the web of the I-beam 233, and can only flow inwards through the artificially-made faults and then flow to the lower layer of trays.

The present invention will be described in more detail by way of specific examples, and it should be understood that the present invention is not limited thereto.

Example 1

In this embodiment, and referring to FIGS. 1 and 2, a pre-distribution tray 130 of the present invention is disposed between the inlet diffuser 120 and the top distribution tray 140 of the hydrogenation reactor 100. The hydrogenation reactor 100 has a diameter of 3.5m and the pre-distribution tray 130 is constructed as described above, wherein the annular tray 132 is divided into a plurality of tray plates 1320 according to the manhole size, and the inner edge of each tray plate 1320 is welded 75 ^# The angle steel serves as a connecting piece 133. A circle of bosses 112 are provided in the body 110 of the hydrogenation reactor 100 of this embodiment.

During installation, the outer edges of a plurality of tray plates 1320 of the outermost annular tray 132 are connected to the boss 112 through bolts, the outer edges of a plurality of tray plates 1320 of the next annular tray 132 are connected to the angle steel of the outermost annular tray 132 through bolts, and finally the outer edges of the circular trays 131 are connected to the angle steel of the middle annular tray 132 through bolts. The height difference between two adjacent trays is about 75mm. The pre-distribution plate 132 of the embodiment does not adopt a conventional supporting form, but is self-supported through the rigidity of the tray, so that the levelness of the tray in the same layer is not required to be ensured in the installation process, the integral levelness of the pre-distribution plate is not required to be accurately ensured, and the installation difficulty of the tray is reduced.

The absence of a conventional gas-liquid distributor on the pre-distributor tray 130 avoids the deviation in the distribution of the gas-liquid phase material, provides friendly, smooth, uniform inlet conditions to the top distributor tray 140, and achieves uniform distribution of the material on the downstream catalyst bed 150 with the top distributor tray 140. After the pre-distribution plate 130 of this embodiment is adopted, by comparing 5 temperature measuring points set at the same height, it can be found that the maximum radial temperature difference of the catalyst bed 150 is reduced from 11.6 ℃ to 1.6 ℃.

Example 2

In this embodiment, referring to FIGS. 3 and 4, a pre-distribution tray 230 of the present invention is provided between the inlet diffuser 220 and the top distribution tray 240 of the hydrogenation reactor 200. The hydrogenation reactor 200 has a diameter of 5.8m and the pre-distribution tray 230 is constructed as described above, wherein the annular tray 232 is divided into a plurality of tray decks according to manhole dimensions. The connecting piece is an I-beam 233, the I-beam 233 is a ring beam, and two adjacent layers of ring beams are connected through a supporting beam 234. A ring of bosses 212 are provided in the body 210 of the hydrogenation reactor 200 of this embodiment.

When in installation, the installation 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 a plurality of tray plates of each layer of annular tray 232 and the circular tray 231 are respectively connected with the ring beam for installation. The height difference between two adjacent trays is about 260mm.

The gas-liquid phase material is prevented from being greatly deviated by the pre-distribution tray 230, a friendly, stable and uniform inlet condition is provided for the top distribution tray 240, and a uniform distribution of the material on the downstream catalyst bed 250 is achieved together with the top distribution tray 240. After the pre-distribution plate 230 of this embodiment is adopted, by comparing 5 temperature measuring points set at the same height, it can be found that the maximum radial temperature difference of the catalyst bed 250 is reduced from the original 13.4 ℃ to 1.8 ℃.

The foregoing descriptions of specific exemplary embodiments of the present invention are presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application to thereby enable one skilled in the art to make and utilize the invention in various exemplary embodiments and with various modifications as are suited to the particular use contemplated. Any simple modifications, equivalent variations and modifications of the above-described exemplary embodiments should fall within the scope of the present invention.

Claims (14)

1. A pre-distribution tray, comprising:

the plurality of trays comprise a circular tray and a plurality of annular trays, the inner diameter and the outer diameter of the trays are sequentially matched and are in multi-layer stepped distribution taking the circular tray as a center, the circular tray is the lowest layer, the annular tray with the largest outer diameter is the highest layer, and the trays are all provided with a plurality of sieve holes; and

and the connecting piece is used for connecting the adjacent two layers of trays and sealing the interlayer gaps of the adjacent two layers of trays.

2. The pre-distribution tray of claim 1, wherein each of said annular trays is formed from a plurality of tray decks that are spliced together.

3. The pre-distribution tray of claim 1, wherein the connector comprises a vertical portion and a lateral portion, wherein the inner edge of an upper tray is connected to the vertical portion, and the outer edge of a lower tray is connected to the lateral portion, and the vertical portion seals the inter-layer gap of the adjacent two trays.

4. A pre-distribution tray according to claim 3, wherein one or more of welding, screwing and snap-in connection is used between the connecting piece and the adjacent two trays.

5. A pre-distribution tray according to claim 3, wherein the connection is a downwardly extending flange at the inner edge of the annular tray.

6. A pre-distribution tray according to claim 3, wherein the connection is an angle welded to the inner edge of each annular tray.

7. A pre-distribution plate according to claim 3, wherein the connecting piece is an i-beam, the inner edge of the upper tray is lapped on the upper surface of the upper wing plate of the i-beam, and the outer edge of the lower tray is lapped on the upper surface of the lower wing plate of the i-beam in two adjacent trays.

8. The pre-distribution tray of claim 7, wherein the i-beam is a ring beam.

9. The pre-distribution plate of claim 8, further comprising:

and the support beams are arranged along the radial direction and are respectively connected with two adjacent layers of ring beams.

10. The pre-distribution tray according to claim 1, wherein the height difference between two adjacent trays is 70-400 mm.

11. A hydrogenation reactor, comprising:

the device comprises a body, a feeding hole and a sealing device, wherein the body is of a cylindrical structure, and the center of the upper end of the body is provided with the feeding hole;

an inlet diffuser disposed at the feed inlet;

the pre-distribution tray of any one of claims 1 to 10, coaxially disposed below said inlet diffuser; and

a top distribution tray disposed below the pre-distribution tray.

12. The hydrogenation reactor according to claim 11, wherein a ring of bosses are provided on an inner wall of said body, and wherein an outer periphery of said pre-distribution plate is mounted in said body by said bosses.

13. The hydrogenation reactor of claim 12, wherein the boss is welded within an upper head of the body.

14. The hydrogenation reactor of claim 11, wherein the body has a diameter of greater than or equal to 3.5m.

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