CN113070001B

CN113070001B - Gas-liquid distribution device

Info

Publication number: CN113070001B
Application number: CN202110233901.5A
Authority: CN
Inventors: 邓矛; 晁君瑞
Original assignee: China Petroleum and Chemical Corp; Sinopec Engineering Group Co Ltd; Sinopec Guangzhou Engineering Co Ltd
Current assignee: China Petroleum and Chemical Corp; Sinopec Engineering Group Co Ltd; Sinopec Guangzhou Engineering Co Ltd
Priority date: 2021-03-03
Filing date: 2021-03-03
Publication date: 2022-10-14
Anticipated expiration: 2041-03-03
Also published as: CN113070001A

Abstract

The invention discloses a gas-liquid distribution device, which comprises a reactor wall, and a distribution plate, an overflow pipe and a distribution disc which are arranged along the reactor wall from top to bottom; the distribution plate is a flat plate, the shape of the distribution plate is consistent with the shape of the cross section of the reactor, the distribution plate is supported on the wall of the reactor, and the plate is provided with a flow guide hole; the overflow pipe is a circular pipe with two open ends, the lower end of the overflow pipe is fixed on the mounting hole of the distribution plate, and overflow holes are uniformly arranged on the pipe wall of the overflow pipe along the circumferential direction to serve as liquid phase channels; the upper end of the overflow pipe is a free end, is positioned below the distribution plate, faces the center of an area without holes between the diversion holes on the distribution plate and is completely shielded by the area without holes. Compared with the scheme of plugging the overflow pipe one by one, the distribution plate has the advantages that the processing amount is small, the manufacturing period is short, and the cost is low when the distribution plate can also achieve the purpose of preventing the upper liquid phase from directly entering the overflow pipe. The invention also prolongs the contact time of gas phase and liquid phase, promotes the dissolution of the gas phase in the liquid phase, and effectively avoids the wall flow phenomenon in the overflow pipe.

Description

Gas-liquid distribution device

Technical Field

The invention belongs to the field of petroleum refining and chemical equipment, relates to a reactor internal member, and particularly relates to a gas-liquid distribution device.

Background

In recent years, with the gradual upgrade of quality standards of petrochemical products and the stricter of environmental regulations, the hydrogenation technology plays an increasingly important role in the oil refining industry, and in addition, the requirement of 'eating, drying and squeezing out' of raw oil, and oil refining enterprises at home and abroad rapidly expand the hydrotreating capability of various oil products in order to improve the economic benefit and meet the requirement of environmental protection.

The key core equipment of hydrotreating is a hydrogenation reactor, and inside the hydrogenation reactor, a mixture of hydrogen (gas phase) and raw oil (liquid phase) in a certain proportion is subjected to various hydrogenation reactions under the action of a catalyst at a certain temperature and pressure. A fixed bed hydrogenation reactor is an important type of hydrogenation reactor, and a gas-liquid mixture flows downwards in parallel through a catalyst bed layer to perform reaction. Because the hydrogenation reaction is a strong exothermic reaction existing in three phases of gas, liquid and solid, if the material flow distribution at the inlet of the catalyst bed layer is not uniform, the material flow of the catalyst bed layer can form local bias flow or local axial channeling, the reaction speed of each point on the section of the bed layer is inconsistent, the bed layer is locally overheated, the quality of a product is influenced, and the catalyst can be inactivated, even coked and hardened when the temperature is too high. In addition, the hydrogen solubility in the liquid phase flow is low or the liquid phase flow can not contact hydrogen and other 'hydrogen deficiency' conditions, so that 'harmful reactions' such as polycondensation, condensation and the like can occur in the reactor, the catalyst loses activity, and the stable operation of the device is hindered. Therefore, in order to stabilize the performance of the catalyst and to ensure the stable operation of the device, a distribution disc is required to be arranged above the catalyst bed layer, and a plurality of groups of gas-liquid distributors are arranged on the distribution disc, so that the solubility of the hydrogen in the liquid phase flow is improved on one hand, and the gas-liquid two phases above the catalyst are uniformly and quickly distributed on the cross section of the whole reactor on the other hand. In addition, the reactor is developing towards the large-scale direction at present, which brings more challenges to the uniform distribution of gas and liquid in the section of the whole reactor, and the requirement for uniform distribution of gas and liquid is more urgent.

The existing gas-liquid distributor can be divided into three types according to the mode that liquid phase enters the gas-liquid distributor: overflow, suction, and a combination thereof. The overflow gas-liquid distributor has the main characteristics of small pressure drop, small size, more equivalent distributors in unit area, basically vertical flow direction of gas phase and liquid phase, simple structure, low manufacturing difficulty, suitability for high-viscosity media and severe requirement on the installation levelness of a distribution plate. The suction type distributor is mainly a bubble cap type distributor, liquid is broken into liquid drops by means of the suction effect of gas at a bubble cap strip seam, the liquid drops are carried by the gas to enter a central pipe, and gas-liquid mixing and distribution are achieved. The mixed gas-liquid distributor is provided with overflow holes below the middle lower part of a central pipe, and the pressure drop performance and the operation elasticity of the mixed gas-liquid distributor are improved compared with the overflow type gas-liquid distributor and the suction type gas-liquid distributor which are simple, but the distribution performance is reduced.

The united states patent US3524731 discloses an overflow type long and short pipe gas-liquid distributor, which is not uniform in gas-liquid distribution when viewed from a local part, but basically realizes uniform distribution of gas-liquid two phases through combination of a plurality of pairs of long and short pipes on the whole gas-liquid distribution disc. Chinese patent CN200520032630.3 discloses an overflow type distributor, which is a V-shaped opening gas-liquid separator and is more suitable for a large hydrogenation reactor; chinese patent CN205216800U discloses an overflow type distributor, which enlarges the gas-liquid phase spraying range by a throat-shaped structure; chinese patent CN201220737754.1 discloses an overflow-ejector tube type distributor which promotes the mixing of gas and liquid phases, but the height of the distributor is relatively high. Chinese patent CN202010857570.8 discloses a gas-liquid distributor, which adopts an umbrella cap to prevent the upper liquid phase from directly entering the overflow pipe, so as to ensure that all the liquid phases enter the overflow pipe through the liquid phase channel on the overflow pipe, and eliminate the uneven distribution of the lower liquid phase caused by the uneven distribution of the upper liquid phase.

The gas-liquid distributors have respective advantages and application ranges, but generally have the problems of poor gas-phase atomization liquid-phase capacity, short gas-phase and liquid-phase contact time, low solubility of gas in liquid phase, small gas-liquid two-phase spraying area, serious wall flow in the gas-liquid distributor pipe, large manufacturing workload and the like, and further improvement is needed.

Disclosure of Invention

The invention provides a gas-liquid distribution device, which can more conveniently realize uniform distribution of gas-liquid two phases, increase the contact of the gas-liquid two phases, promote the atomization effect of the gas-liquid two phases and reduce the wall flow phenomenon in a gas-liquid distributor pipe, and aims to solve the technical problems of poor gas-liquid atomization liquid phase capacity, short contact time of the gas phase and the liquid phase, low solubility of the gas in the liquid phase, small spraying area of the gas-liquid two phases, serious wall flow in the gas-liquid distributor pipe, large manufacturing workload and the like in the prior art.

The gas-liquid distribution device provided by the invention comprises a reactor wall, and a distribution plate, an overflow pipe and a distribution disc which are arranged from top to bottom along the reactor wall; the distribution plate is a flat plate, the shape of the distribution plate is consistent with the shape of the cross section of the reactor, the distribution plate is supported on the wall of the reactor, and the plate is provided with a diversion hole; the overflow pipe is a circular pipe with two open ends, the lower end of the overflow pipe is fixed on the mounting hole of the distribution plate, and one layer or two layers or multiple layers of overflow holes are uniformly arranged on the pipe wall of the overflow pipe along the circumferential direction to be used as liquid phase channels; the upper end of the overflow pipe is a free end, is positioned below the distribution plate, faces the center of an area without holes between the diversion holes on the distribution plate and is completely shielded by the area without holes.

The distribution plate mainly plays a role in collecting upper gas-liquid phases, and the distribution plate is provided with flow guide holes for the gas-liquid phases collected on the distribution plate to pass through. The diversion holes can be in any shape such as round, square and the like, and are preferably round holes with the diameter of 15-300 mm from the aspect of convenient processing; from the angle of being favorable to liquid phase evenly distributed, the water conservancy diversion hole should arrange according to square, regular triangle or rhombus etc. mode. From the perspective of convenient processing, more evenly distributed, the water conservancy diversion hole is preferably arranged according to square mode.

The diameter of the overflow pipe is generally 20-200 mm, the overflow holes on the wall of the overflow pipe can be round holes or can be strip seams or any other shapes, and the overflow holes are preferably round holes from the angle of convenient processing. The overflow holes are arranged at equal intervals, each layer is provided with 2-10 openings, the diameter of each opening is 2-30 mm, and the overflow holes of the two adjacent layers are arranged in a staggered manner. If two or more layers of overflow holes are arranged, the size of the holes formed along the wall of the overflow pipe from top to bottom is preferably reduced layer by layer, so that the liquid phase flow speed in the liquid phase channel at the lowest layer (the most common) is high, the wall flow in the overflow pipe is reduced, and the liquid phase is sprayed to the center of the overflow pipe as far as possible. The upper layer is provided with large holes, so that liquid phase distribution can be completed as soon as possible through the large holes on the upper layer under the condition that the liquid phase is increased, and the liquid phase can enter the overflow pipe through the gas phase channel and complete distribution under the extreme condition that the liquid phase is too high.

As an improved scheme, a flow guide pipe can be arranged in a flow guide hole on a distribution plate, the shape of the flow guide pipe is consistent with that of the flow guide hole, the upper end and the lower end of the flow guide pipe protrude out of the upper surface and the lower surface of the distribution plate, the upper end of the flow guide pipe extends out of the distribution plate by 10-200 mm, and the lower end of the flow guide pipe extends out of the distribution plate by 20-200 mm. The honeycomb duct is mainly used for guiding and enabling gas and liquid to pass through, so that the liquid phase is prevented from irregularly flowing along the lower side of the distribution plate, such as wall flow, drip flow and the like, and possibly directly entering the overflow pipe, and the collected gas and liquid are ensured to be completely collected on the distribution plate.

Under the condition of arranging the flow guide pipe, as an improvement, an overflow hole on the overflow pipe is over against the axial position of the flow guide pipe. If the diversion holes are arranged in a square mode, the overflow holes on the same layer on the overflow pipe are the same in size, because the distances from the overflow pipe to any adjacent diversion pipe are the same, the on-way flow resistance of the liquid is the same, and the liquid entering the overflow pipe is more uniform; if the flow guide holes are arranged in a regular triangle or rhombus mode, the overflow holes on the same layer on the overflow pipe are different in size suggestion, the overflow hole close to the flow guide pipe is small in size, the overflow hole far away from the flow guide pipe is large in size and is in an inverse relation with the distance from the flow guide pipe, and the on-way flowing resistance difference of liquid on the distribution disc is balanced by a method for controlling the size of the overflow holes, so that the liquid entering the overflow pipe is more uniform.

As a further improvement, a liquid collecting disc is arranged below each layer of overflow holes in the overflow pipe, the liquid collecting disc is a concave flat-bottom disc, the protruding concave edge is fixedly connected with the pipe wall of the overflow pipe, distribution holes are uniformly distributed in the bottom of the liquid collecting disc, and gas and liquid can pass through the distribution holes.

The liquid collecting disc is high in periphery, low in middle and concave, so that the liquid phase entering from the overflow holes is completely drained to enter the liquid collecting disc, the liquid phase is prevented from flowing downwards along the inner wall of the overflow pipe, and the wall flow phenomenon in the overflow pipe is fundamentally avoided. The liquid collecting disc is uniformly distributed with a plurality of distribution holes according to a square shape, a regular triangle shape or an annular shape, and the gas phase and the liquid phase pass through. The distribution hole can be a round hole or a strip seam or any other shape, and is preferably a round hole from the angle of convenient processing. When the circular hole is opened, the diameter of the opening is generally 2-20 mm. In order to increase the stroke of gas-liquid two phases in the overflow pipe, the distribution holes of the upper and lower adjacent layers of liquid collecting discs are staggered, namely the distribution holes of the lower layer of liquid collecting disc correspond to the central area of the part, which is not provided with the hole, of the upper layer of liquid collecting disc. Through one layer or two layers or multiple layers of liquid collecting discs, the contact time of gas and liquid phases is long, the dissolution of hydrogen in the liquid phase is promoted, and the wall flow phenomenon in the overflow pipe is avoided.

As a further improvement, a disperser coaxially arranged with the overflow pipe is fixed below the distribution plate, and the disperser can adopt different structures:

one of the structures is as follows: the disperser comprises a conical dispersing plate, the large end of the dispersing plate is upwards fixed below the distributing plate, and the small end of the dispersing plate is open. The diameter of the large end of the dispersion plate is preferably 1.3 to 3 times of the diameter of the overflow pipe, the cone angle is 70 to 160 degrees, and the diameter of the small end is preferably 0.4 to 1.2 times of the diameter of the overflow pipe.

As a further scheme, in order to solve the problems that the liquid phase is concentrated at the outer edge in an overflow pipe and the dispersion effect is poor when the flow rate of the liquid phase is small and the viscosity of the liquid phase is high, a secondary dispersion plate is arranged on the dispersion plate at a position which is 30-75% of the position of the dispersion plate from a distribution plate; the secondary dispersion plate extends into the dispersion plate, and the extending position is located in the diameter range of 55-90% of the projection of the overflow pipe. The secondary dispersion plate is also conical, with its small end facing upwards and its large end facing downwards. For make the gas-liquid double-phase of outflow in the overflow pipe pass through smoothly from the secondary dispersion board, be provided with the round reposition of redundant personnel hole on the dispersion board of secondary dispersion board and dispersion board cross department top for guide gas-liquid is double-phase further to be dispersed along the secondary dispersion board, the reposition of redundant personnel hole can be the round hole, also can be for the seam is bored. The area of the secondary dispersion plate extending out of the dispersion plate can be provided with one layer or two layers or more layers of dispersion holes, from the angle of convenient manufacture, the dispersion holes are preferably round holes, the diameter of the dispersion holes is 3-30 mm, and the dispersion holes can also be slots and other shapes. Under the combined action of dispersion board and secondary dispersion board, can collect, water conservancy diversion, dispersion to the liquid level of inclined to one side outer fringe in the overflow pipe, increase the double-phase diffusion area of gas-liquid, solve the poor liquid phase that causes of overflow effect and concentrate, distribute inhomogeneous scheduling problem for the double-phase distribution of gas-liquid is more even, and the catalyst bed layer of distributor below can evenly receive gas-liquid double-phase, has that the pressure drop is little, spray the area big, spray even advantage.

The second structure: the disperser is in a screen shape and is an integral body formed by fixedly connecting a connecting strip, a flow guide strip and a coaming, and the flow guide strip and the coaming are fixed below the connecting strip; the coaming and the overflow pipe are coaxial, and the edge of the diversion edge is fixed to form a closed ring body. Generally, the disperser is square or round on the whole, is fixed below the distribution disc through the support rib, and plays a role in uniformly and accurately distributing a liquid phase flowing down the overflow pipe to a catalyst bed layer below the overflow pipe.

The connecting strips can be cylinders, cuboids or any other shapes, and the number of the connecting strips is preferably 3-15.

The cross section of the flow guide strips can be rectangular, circular or triangular, and the distance between the flow guide strips is preferably 5-40 mm. In view of the scheme convenient for flow guiding, the cross section of the flow guiding strip is preferably a triangular cross section. The dispersion structure fully utilizes the wall flow characteristic of liquid and the wall flow characteristic of the liquid in the connecting strips and the flow guide strips to carry out secondary distribution on the liquid phase flowing down from the overflow pipe; horizontal water conservancy diversion is realized through the water conservancy diversion effect of connecting strip on the one hand, and on the other hand realizes fore-and-aft water conservancy diversion through the water conservancy diversion effect of water conservancy diversion strip to, liquid can directly get into the catalyst bed layer of below through the clearance between water conservancy diversion strip and the connecting strip, has realized atomizing and the breakage of liquid phase.

As an improved scheme, the diversion strip can be grooved in the length direction, the grooves can be V-shaped grooves or rectangular grooves, and the liquid phase can accurately drip by utilizing the dripping principle of the liquid phase at the discontinuous part of the structure. As another alternative to this solution, a flow guiding column may be welded on the flow guiding strip, and the liquid phase may be distributed in a trickle manner through the flow guiding column. The diversion column can be in the shape of cuboid, cylinder, tetrahedron or cone.

As a further scheme, in order to solve the problems that the liquid phase in the overflow pipe has poor jet effect and gradually reduces to the inner liquid phase along the radial direction of the overflow pipe, the cross section of the disperser can be made into a V shape, and the V-shaped included angle is preferably 140-175 degrees. The liquid realizes the drip distribution through the dispersion effect of dispersion structure on the one hand, utilizes the gravity of liquid phase in addition, realizes the secondary distribution with the ascending liquid phase of overflow pipe diameter direction, promotes the liquid phase below the overflow pipe to the central point put the distribution. In order to facilitate the distribution of the liquid phase to the center of the overflow pipe, the distance between the diversion strips is preferably gradually increased from the outer edge of the disperser to the center.

As a further proposal, in order to increase the distribution area of the disperser, the cross section of the disperser can be made into a double-ripple shape, and the V-shaped included angle between two wave crests is preferably 150-170 degrees. The wave crests are located in the range of 50-90% of the diameter of the projection of the overflow pipe, and the arrangement of the two wave crests can disperse the liquid phase to two sides and the middle, so that the dispersion area is increased while the liquid phase is uniformly dispersed. During this kind of dispersed structure, the interval of water conservancy diversion strip should be for being close to that the crest department interval is little, the scheme that the trough department interval is big.

The area of the enclosing plate is not more than 4 times of the area of the overflow pipe.

The working process of the invention is as follows:

the gas phase and the liquid phase flowing down from the upper part are collected on the distribution plate, and the gas phase and the liquid phase are completely collected on the distribution plate and outside the overflow pipe under the guide effect of the guide pipe through the guide holes on the distribution plate. Due to the difference of gravity, the gas phase is accumulated above and enters the overflow pipe from the upper end of the overflow pipe; the liquid phase is deposited on the distribution disc, and after the liquid phase is accumulated to a certain liquid level, the liquid phase enters the overflow pipe through the overflow hole under the action of pressure difference. When the liquid phase passes through the overflow holes, the flow velocity is increased due to the small flow area of the overflow holes, and a jet flow is formed and is jetted onto the liquid collecting disc under the action of inertia. Of course, part of the liquid phase can flow along the inner wall of the overflow pipe after entering the overflow pipe, and the liquid phase is completely collected on the liquid collecting tray under the collecting action of the liquid collecting trays with high peripheries and low middle. After the gas phase and the liquid phase leave the overflow pipe through the distribution holes on the liquid collecting disc, the gas phase and the liquid phase are further dispersed by the disperser, so that the gas phase and the liquid phase are fully contacted and uniformly distributed.

The invention has the following beneficial effects:

1) Through the relative position relation of distributing plate and overflow pipe, the distributing plate can play the effect that prevents upper portion liquid phase and directly get into the overflow pipe, simultaneously under the water conservancy diversion effect of honeycomb duct on the distributing plate, can ensure that upper portion liquid phase is whole to be collected on the plate of distributor, and whole liquid phase must get into the overflow pipe through the liquid phase passageway on the overflow pipe, eliminates the inhomogeneous phenomenon of lower part liquid phase distribution that brings of upper portion liquid phase. Compared with the scheme of plugging the overflow pipe one by one, the distribution plate has the advantages that the processing amount is small, the manufacturing period is short, and the cost is low when the distribution plate can also achieve the purpose of preventing the upper liquid phase from directly entering the overflow pipe.

2) All liquid-phase materials are collected on the distribution plate and then distributed, so that uneven distribution caused by uneven feeding is avoided;

3) The gas-liquid two-phase contact time is long, so that the dissolution of a gas phase in a liquid phase is promoted, and the wall flow phenomenon in an overflow pipe is effectively avoided;

4) The gas phase atomization liquid phase capacity is good, the gas-liquid two-phase dispersion area is large, the dispersion liquid drop is small, the dispersion is uniform, and the stable operation of the hydrogenation reaction is facilitated.

5) Simple structure and convenient processing.

Drawings

FIG. 1 is a schematic view of a gas-liquid distribution device according to the present invention;

FIG. 2 is a schematic view of the structure of the distribution plate of FIG. 1;

FIG. 3 is a schematic structural view of the secondary dispersion plate of FIG. 1;

FIG. 4 is a schematic view of a screen-like disperser according to the present invention;

FIG. 5 is a schematic top view of the disperser of FIG. 4;

FIG. 6 is a schematic view of another structure of the disperser of the present invention in the form of a mesh;

FIG. 7 is a schematic view showing still another structure of the disperser of the present invention in the form of a mesh;

FIG. 8 is a structural schematic view of the slitting of the guide strips of the present invention;

fig. 9 is a schematic structural view of a guide column arranged below the guide strip of the present invention.

In the figure: 1-reactor wall, 2-distribution plate, 3-draft tube, 4-distribution plate, 5-overflow tube, 6-overflow hole, 7-liquid collecting plate, 8-distribution hole, 9-dispersion plate, 10-secondary dispersion plate, 11-dispersion hole, 12-diversion hole, 13-diversion hole, 14-connecting strip, 15-diversion strip, 16-coaming plate, 17-support rib and 18-diversion column.

Detailed Description

As shown in fig. 1 to 3, the gas-liquid distribution device provided by the present invention comprises a reactor wall 1, a distribution plate 2, a draft tube 3, an overflow tube 5, a distribution plate 4, and a disperser fixed below the distribution plate 4 and coaxial with the overflow tube 5, wherein the distribution plate 2, the draft tube 3, the overflow tube 5, the distribution plate 4 and the disperser are arranged from top to bottom along the reactor wall; the distribution plate 2 is a flat plate, the shape of the distribution plate is consistent with the shape of the cross section of the reactor, the distribution plate is supported on the wall 1 of the reactor, circular diversion holes 13 are formed in the plate, and the diversion holes 13 are arranged in a square mode; a flow guide pipe 3 is arranged in the flow guide hole 13, the shape of the flow guide pipe is consistent with that of the flow guide hole, and the upper end and the lower end of the flow guide pipe are protruded out of the upper surface and the lower surface of the distribution plate 1; the overflow pipe 5 is a circular pipe with two open ends, the lower end of the overflow pipe is fixed on the mounting hole of the distribution plate 4, and one layer or two layers or multiple layers of circular overflow holes 6 are uniformly arranged on the pipe wall of the overflow pipe along the circumferential direction to be used as a liquid phase channel; the upper end of the overflow pipe 5 is a free end, is positioned below the distribution plate 1, is directly opposite to the center of the non-perforated area between the diversion holes on the distribution plate and is completely shielded by the non-perforated area.

And an overflow hole 6 on the overflow pipe 5 is over against the axis position of the draft tube 3. The overflow holes 6 on the same layer on the overflow pipe 6 have the same size. And a liquid collecting disc 7 is arranged below each layer of overflow holes 6 in the overflow pipe 5, and the liquid collecting disc 7 is a concave flat-bottom disc and is fixedly connected with the pipe wall of the overflow pipe 5 by a protruding concave edge. The liquid collecting disc 7 is uniformly distributed with a plurality of distribution holes 8 according to a square shape, a regular triangle shape or a ring shape, and the gas phase and the liquid phase pass through. The distribution holes 8 of the drip trays 7 of two adjacent layers are staggered, namely the distribution holes 8 of the drip trays 7 of the lower layer correspond to the central area of the part, which is not provided with the holes, of the drip trays 7 of the upper layer.

The disperser that is fixed in distribution plate 4 below and coaxial setting with overflow pipe 5 includes a conical dispersion board 9 and secondary dispersion board 10, and 9 main aspects of dispersion board are fixed in distribution plate 4 below up, and the tip is uncovered. The diameter of the large end of the dispersion plate 9 is preferably 1.3 to 3 times of the diameter of the overflow pipe 5, the cone angle is 70 to 160 degrees, and the diameter of the small end is preferably 0.4 to 1.2 times of the diameter of the overflow pipe 5. The secondary dispersion plate 10 is arranged on the dispersion plate 9 at a position which is 30 to 75 percent downward from the distribution plate 4; the secondary dispersion plate 10 extends into the dispersion plate 9, and the extending position is positioned in the diameter range of 55-90% of the projection of the overflow pipe 5. The secondary dispersion plate 10 is also conical with its small end facing upwards and its large end facing downwards. A circulation of shunt holes 12 are arranged on the dispersion plate 9 above the intersection of the secondary dispersion plate 10 and the dispersion plate 9 and used for guiding the gas-liquid two-phase to be further dispersed along the secondary dispersion plate 10. The area of the secondary dispersion plate 10 extending out of the dispersion plate 9 is provided with dispersion holes 11, and the dispersion holes 11 are round holes with the diameter of 3-30 mm.

As shown in fig. 4 and 5, the disperser fixed below the distribution tray 4 and coaxial with the overflow pipe 5 is a mesh-shaped disperser formed by fixedly connecting a connecting bar 14, a flow guide bar 15 and a surrounding plate 16, and the flow guide bar 15 and the surrounding plate 16 are fixed below the connecting bar 14; the enclosing plate 16 is coaxial with the overflow pipe 5, fixes the edge of the diversion strip 15 and forms a closed ring body. The disperser is round on the whole and is fixed below the distribution disc 4 through the support ribs 17, the section of the flow guide strips 15 is a rectangular section, and the distance between the flow guide strips 15 is preferably 5-40 mm.

As shown in fig. 6, the difference from fig. 4 is that: the cross section of the disperser is V-shaped, the cross section of the flow guide strip 15 is a triangular cross section, and the included angle of the V shape is 140-175 degrees. The distance between the flow guide strips 15 is preferably gradually increased from the outer edge of the disperser to the center.

As shown in fig. 7, the difference from fig. 4 is that: the cross section of the disperser is double-corrugated, and the cross section of the flow guide strip 15 is a triangular cross section. The V-shaped included angle between the two wave crests is 150-170 degrees. The wave crest is positioned in the range of 50-90% of the diameter of the projection of the overflow pipe 5. The distance between the diversion strips 15 is preferably small near the wave crest and large near the wave trough.

As shown in fig. 8, the diversion strips 15 may be grooved in the length direction, the grooves may be V-shaped grooves or rectangular grooves, and the liquid phase may drip precisely by using the principle that the liquid phase drips at the discontinuous part of the structure. As an alternative to this, as shown in fig. 9, a flow guide column 18 may be welded to the flow guide strip 15, and the liquid phase may be distributed in a trickle manner through the flow guide column 18.

The working process of the invention is as follows: as shown in FIG. 1, two phases of gas and liquid flowing down from above are collected on a distribution plate 1, and are collected in the space in the reactor above a distribution plate 4 and outside an overflow pipe 5 by the flow guide of a flow guide pipe 3. Due to the difference in gravity, the gas phase accumulates above and enters the overflow pipe 5 from the upper end of the overflow pipe 5; the liquid phase is deposited on the distribution disc 4, and after the liquid phase is accumulated to a certain liquid level, the liquid phase enters the overflow pipe 5 through the overflow hole 6 under the action of pressure difference. When the liquid phase passes through the overflow holes 6, the flow velocity is increased due to the small flow area of the overflow holes 6, and a jet flow is formed and is jetted onto the liquid collecting tray 7 under the action of inertia. Of course, part of the liquid phase can flow along the inner wall of the overflow pipe 5 after entering the overflow pipe 5, and the liquid phase is completely collected on the liquid collecting tray 7 under the collecting action of the liquid collecting tray 7 with high periphery and low middle. After the gas phase and the liquid phase leave the overflow pipe through the distribution holes 8 on the liquid collection disc, the gas phase and the liquid phase are further dispersed by a disperser which is fixed below the distribution disc 4 and is coaxially arranged with the overflow pipe 5, so that the gas phase and the liquid phase are fully contacted and uniformly distributed.

Claims

1. A gas-liquid distribution device, characterized by: comprises a reactor wall, a distribution plate, an overflow pipe and a distribution plate which are arranged from top to bottom along the reactor wall; the distribution plate is a flat plate, the shape of the distribution plate is consistent with the shape of the cross section of the reactor, the distribution plate is supported on the wall of the reactor, and the plate is provided with a flow guide hole; the overflow pipe is a circular pipe with two open ends, the lower end of the overflow pipe is fixed on the mounting hole of the distribution plate, and one or more layers of overflow holes are uniformly arranged on the pipe wall of the overflow pipe along the circumferential direction to be used as liquid phase channels; the upper end of the overflow pipe is a free end, is positioned below the distribution plate, faces the center of an area without holes between the diversion holes on the distribution plate and is completely shielded by the area without holes; and the guide pipe is arranged in the guide hole on the distribution plate, the shape of the guide pipe is consistent with that of the guide hole, and the upper end and the lower end of the guide pipe are protruded out of the upper surface and the lower surface of the distribution plate.

2. The apparatus of claim 1, wherein: the overflow holes are arranged in multiple layers, and the two adjacent layers of overflow holes are arranged in a staggered mode.

3. The apparatus of claim 2, wherein: the overflow hole reduces from top to bottom along the overflow pipe wall trompil size successive layer.

4. The apparatus of claim 1, wherein: and a liquid collecting disc is arranged below each layer of overflow holes in the overflow pipe, is a concave flat-bottom disc and is fixedly connected with the wall of the overflow pipe through a protruding concave edge, and distribution holes are uniformly distributed in the bottom of the liquid collecting disc.

5. The apparatus of claim 2, wherein: and the liquid collecting discs are concave flat-bottomed discs and are fixedly connected with the pipe wall of the overflow pipe by protruding concave edges, distribution holes are uniformly distributed at the bottoms of the liquid collecting discs, the distribution holes of the upper layer and the lower layer of the liquid collecting discs are arranged in a staggered manner, namely the distribution holes of the lower layer of the liquid collecting discs correspond to the central area of the part, which is not provided with the hole, of the upper layer of the liquid collecting discs.

6. The apparatus according to any one of claims 1 to 5, wherein: a disperser which is coaxially arranged with the overflow pipe is fixed below the distribution disc.

7. The apparatus of claim 6, wherein: the disperser comprises a conical dispersing plate, the large end of the dispersing plate is upwards fixed below the distributing plate, and the small end of the dispersing plate is open.

8. The apparatus of claim 7, wherein: be equipped with the secondary dispersion board on the dispersion board, inside the secondary dispersion board stretched into the dispersion board, the secondary dispersion board was conical equally, and its tip is up, and the main aspects is provided with the round reposition of redundant personnel hole down on the dispersion board of secondary dispersion board and dispersion board cross section top, and the secondary dispersion board stretches out the regional one deck or multilayer dispersion hole of seting up of dispersion board.

9. The apparatus of claim 8, wherein: the secondary dispersion plate is arranged on the dispersion plate at a position which is 30-75% downward from the distribution plate.

10. The apparatus of claim 8, wherein: the extending position of the secondary dispersion plate extending into the dispersion plate is positioned in the diameter range of 55-90% of the projection of the overflow pipe.

11. The apparatus of claim 6, wherein: the disperser is in a screen mesh shape and is an integral body formed by fixedly connecting a connecting strip, a flow guide strip and a coaming, and the flow guide strip and the coaming are fixed below the connecting strip; the coaming and the overflow pipe are coaxial, and the edge of the diversion edge is fixed to form a closed ring body.

12. The apparatus of claim 11, wherein: the disperser is a square or round section on the whole and is fixed below the distribution plate through a support rib.

13. The apparatus of claim 11, wherein: the cross section of the flow guide strip is rectangular, circular or triangular.

14. The apparatus of claim 13, wherein: the water guide strips are provided with grooves in the length direction, and the grooves are V-shaped grooves or rectangular grooves.

15. The apparatus of claim 11, wherein: the guide strips are welded with guide columns.

16. The apparatus of claim 11, wherein: the cross-section of the disperser is V-shaped, and the distance between the flow guide strips is gradually increased from the outer edge of the disperser to the center.

17. The apparatus of claim 11, wherein: the cross section of the disperser is double-corrugated, the distance between the guide strips is small near the wave crest, and the distance between the guide strips is large near the wave trough.