CN115301160A - Suction type rotational flow mixing distributor and gas-liquid mixing distribution equipment - Google Patents
Suction type rotational flow mixing distributor and gas-liquid mixing distribution equipment Download PDFInfo
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- CN115301160A CN115301160A CN202210883575.7A CN202210883575A CN115301160A CN 115301160 A CN115301160 A CN 115301160A CN 202210883575 A CN202210883575 A CN 202210883575A CN 115301160 A CN115301160 A CN 115301160A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00327—Controlling the temperature by direct heat exchange
- B01J2208/00336—Controlling the temperature by direct heat exchange adding a temperature modifying medium to the reactants
- B01J2208/00353—Non-cryogenic fluids
- B01J2208/00371—Non-cryogenic fluids gaseous
Abstract
The invention discloses a suction type rotational flow mixing distributor, which mainly comprises a rotational flow mixing cavity, a down pipe and a rotational flow distribution cavity, and is integrally in a vertical dumbbell shape, wherein the rotational flow mixing cavity at the upper part is communicated with the rotational flow distribution cavity at the lower part through the down pipe at the middle part, a spiral mixing channel is arranged in the rotational flow mixing cavity, and a radial distribution channel is arranged in the rotational flow distribution cavity; the descending pipe is internally provided with a bubble cap, a conical cylinder or a spiral blade and other reinforced mixing elements; the suction type rotational flow mixing distributor can strengthen the mass transfer process and improve the heat transfer efficiency, and is suitable for being used among catalyst bed layers of a large-diameter down-flow reactor. Meanwhile, the invention also discloses gas-liquid mixing and distributing equipment.
Description
Technical Field
The invention belongs to the field of petroleum processing, and particularly relates to a suction type rotational flow mixing distributor and gas-liquid mixing distribution equipment.
Background
In the hydrogenation process, because of the exothermic reaction of gas phase, liquid phase and solid phase, in order to make the reaction feed (gas phase and liquid phase) and the catalyst (solid phase) fully, uniformly and effectively contact, a hydrogenation reactor is generally designed with a plurality of catalyst bed layers, a distribution disc is arranged at the top of each bed layer, and a temperature control structure (cold hydrogen box) is arranged between the two bed layers, so as to ensure the safe and stable production of a hydrogenation device and prolong the service life of the catalyst.
The hydrogenation reaction of hydrocarbons belongs to exothermic reaction, for the hydrogenation reactor with multiple beds, the temperature of oil gas and hydrogen will rise after the reaction in the previous bed, and cold hydrogen must be introduced between the two beds to control the temperature for the next bed to continue effective reaction. The tubes that introduce and distribute the cold hydrogen gas inside the reactor are called cold hydrogen tubes. The role and requirements of the cold hydrogen addition system are: uniformly and stably supplying enough cold hydrogen; the cold hydrogen must be thoroughly mixed with the hot reactants and have a uniform temperature and material distribution on entering the next bed. The cold hydrogen pipe is divided into a direct-insert type, a tree-like type and an annular structure according to forms.
The cold hydrogen tank is a combination of a mixing tank and a pre-distribution plate. It is the place where the hot reactant and cold hydrogen in the hydrogenation reactor are mixed and heat exchanged. The reaction product flowing down from the upper layer and the cold hydrogen injected from the cold hydrogen pipe are fully mixed in the box to absorb the reaction heat, reduce the temperature of the reactant, meet the reaction requirement of the next catalyst bed layer and avoid the over-temperature of the reactor.
The first layer of the cold hydrogen box is a baffle plate disc, and the baffle plate is provided with a throttling hole. The cold hydrogen from the cold hydrogen pipe and the oil gas after the reaction of the previous bed layer are premixed on the baffle disc and then enter the cold hydrogen box through the throttling hole. Cold hydrogen entering the cold hydrogen box and hot oil gas from the upper layer are repeatedly baffled and mixed, then flow to a second layer of sieve plate disc of the cold hydrogen box, are baffled again on the sieve plate disc to strengthen the mixing effect, and then are distributed. And a layer of redistributing tray is arranged below the sieve tray to redistribute the oil gas after the predistribution.
The redistributing tray consists of a tray plate and distributors uniformly distributed on the tray plate. The redistribution plate is arranged on the catalyst bed layer, and aims to uniformly distribute the reaction medium, improve the flow condition of the reaction medium, realize good contact with the catalyst and further achieve uniform distribution in the radial direction and the axial direction. The types of distributors are more, and the hydrogenation reactors designed and manufactured by China mostly adopt bubble cap type distributors.
Patent CN201610010133.6 provides a rotational flow cold hydrogen pipe of a hydrogenation reactor, which comprises a feeding pipe connected with an outlet of a cold hydrogen storage tank, a distribution ring pipe connected to the feeding pipe, and a plurality of nozzles mounted on the distribution ring pipe, wherein the plurality of nozzles are uniformly arranged around the outer wall of the ring of the distribution ring pipe; the nozzle is of a cylinder shape, a notch is formed at the tail end of the side wall of the nozzle, an end cover is arranged at the tail end of the nozzle, and the notches of the plurality of nozzles are in the same or opposite directions.
Patent CN201620014039.3 discloses a mixing system comprising: the catalyst comprises a shell, an upper catalyst layer, a lower catalyst layer and a hydrogenation pipe; the upper catalyst layer and the lower catalyst layer are arranged in the shell at intervals from top to bottom, and a mixing cavity is formed between the upper catalyst layer and the lower catalyst layer; one end of the hydrogenation pipe is arranged in the mixing cavity; the side wall of the hydrogenation pipe is provided with a plurality of air outlets. Cold hydrogen flows into the mixing cavity from the plurality of air outlets, the reaction fluid can be fully mixed with the cold hydrogen when flowing into the mixing cavity, and the reaction fluid and the cold hydrogen can be fully mixed when the hydrogenation pipe is introduced with the cold hydrogen, so that the space of the mixing cavity is reduced, but the heat transfer and mass transfer are not uniform enough, and the reaction is not stable enough.
At present, with the upsizing of a hydrogenation device and the development of a new hydrogenation technology, the diameter of a hydrogenation reactor is larger and larger, and the catalyst bed layer of a single hydrogenation reactor is increased. After the hydrogenation reactor is large-sized, the advanced applicability of the inner member becomes more important, and how to realize the uniform distribution of gas-liquid two-phase fluid in the bed layer, ensure the uniform proceeding of mass transfer and heat transfer and improve the heat transfer efficiency of the medium in the reactor becomes more difficult and more important. For example, the foreign advanced gas-liquid distributor is combined with the advanced catalyst filling technology to ensure that the temperature on the inner section of the reactor is very uniform, and the temperature difference reaches the level of less than or equal to 3 ℃, thereby being beneficial to the operation control of the reactor and greatly prolonging the service life of the catalyst.
Disclosure of Invention
The invention provides a suction type rotational flow mixing distributor and gas-liquid mixing distribution equipment, aiming at solving the technical problems that gas-liquid two-phase fluid is difficult to be uniformly distributed in a catalyst bed layer, the mass and heat transfer are not uniform enough and the heat transfer efficiency is low in the prior art.
The invention provides a suction type rotational flow mixing distributor which mainly comprises a rotational flow mixing cavity, a downcomer and a rotational flow distribution cavity, wherein the whole body is in a vertical dumbbell shape; the spiral mixing cavity is composed of a bottom plate, a top plate and a spiral partition plate, the spiral partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the spiral partition plate jointly enclose a spiral mixing channel, an inlet of the spiral mixing channel is positioned on the side surface of the cylinder and forms an inlet of the spiral mixing cavity, an outlet of the spiral mixing channel is positioned in the center of the cylinder and is communicated with a center hole of the bottom plate, the center hole of the bottom plate forms an outlet of the spiral mixing cavity, and the spiral mixing channel gradually reduces in width from outside to inside or keeps the same width; the cyclone distribution cavity consists of a bottom plate, a top plate and a partition plate, the partition plate is in a spiral shape or a straight plate shape, the cyclone distribution cavity is integrally cylindrical, the partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the partition plate jointly enclose a radial distribution channel which is diverged from the center to the periphery, the inlet of the radial distribution channel is positioned at the center of the cylinder and is communicated with the central hole of the top plate, the central hole of the top plate forms the inlet of the cyclone distribution cavity, and the outlet of the radial distribution channel is positioned on the side surface of the cylinder and forms the outlet of the cyclone distribution cavity; the upper end of the downcomer is communicated with a central hole of a bottom plate of the rotational flow mixing chamber, and the lower end of the downcomer is communicated with a central hole of a top plate of the rotational flow distribution chamber; the interior of the downcomer is provided with an intensified mixing element.
The reinforced mixing element can be a bubble cap, the bubble cap comprises an outer barrel with an opening end, an inner barrel with two open ends and a circular bottom plate, the lower end of the inner barrel is fixedly connected with a center hole of the circular bottom plate, the outer barrel is reversely buckled at the upper end of the inner barrel, the outer barrel and the inner barrel are fixedly connected through a supporting rib, the outer edge of the circular bottom plate is fixedly connected with the inner wall of a descending pipe, and an annular channel which is communicated from outside to inside is formed among the inner wall of the descending pipe, the outer barrel and the outer wall of the inner barrel.
The reinforced mixing element can also be a conical cylinder, two ends of the conical cylinder are open, the large end of the conical cylinder faces upwards, the small end of the conical cylinder faces downwards, the conical surface is provided with openings, the openings can be round holes, strip-shaped holes or square holes, the large end of the conical cylinder is fixedly connected with the inner wall of the downcomer, and the conical cylinder can be arranged at intervals of 2-4 along the axial direction of the downcomer.
The reinforced mixing element can also be a helical blade, the outer edge of the helical blade is fixedly connected with the inner wall of the downcomer and forms a helical descending channel together with the inner wall of the downcomer.
The arrangement of the reinforced mixing element can prolong the mixing path and time of the cold hydrogen and the reaction oil gas, enhance the collision mixing of the cold hydrogen and the reaction oil gas, and more effectively control the temperature of the reaction oil gas. In addition to the three configurations of the reinforced hybrid component described above, other suitable configurations may be used.
As an improvement, in order to make the gas-liquid distribution more uniform, the bottom plate of the radial distribution channel is provided with distribution holes.
The invention also provides gas-liquid mixing distribution equipment, which comprises a reactor shell, and a catalyst grid, a cold hydrogen distribution pipe, a suction type rotational flow mixing distributor, a liquid receiving disc, a gas-liquid distribution pipe and a distribution disc which are arranged in the reactor shell from top to bottom; the cold hydrogen distribution pipe is positioned below the catalyst grid, the liquid receiving disc is fixedly connected with the inner wall of the reactor shell, and the suction type rotational flow mixing distributor is fixed on the liquid receiving disc; the gas-liquid distribution pipe and the distribution plate are positioned below the liquid receiving plate, the distribution plate is fixedly connected with the inner wall of the reactor shell, and the gas-liquid distribution pipe is vertically fixed on the distribution plate.
The gas-liquid distribution pipe adopts short pipes, the outlets at the lower parts of the gas-liquid distribution pipe are in a throat shape with a thin middle part and two large ends, and the aperture ratio (the aperture ratio is defined by the ratio of the total area of the throat section to the radial sectional area of the reactor) of the throat part (the narrowest part of the outlets at the lower parts) is 2-6%; the ratio of the inner diameter of the gas-liquid distribution pipe to the diameter of the throat part is 1.5-3; the aperture ratio of the throat part and the ratio of the inner diameter of the distribution pipe to the diameter of the throat part jointly determine the proper spray angle of the gas-liquid distribution pipe.
As an improvement, a pre-distribution plate is arranged between the liquid receiving plate and the distribution plate, and the pre-distribution plate can make the gas and the liquid distributed more uniformly in the circumferential direction of the reactor shell.
The suction type rotational flow mixing distributor is fixed on the liquid receiving disc through a descending pipe of the suction type rotational flow mixing distributor, the rotational flow mixing cavity is located above the liquid receiving disc, and the rotational flow distribution cavity is located below the liquid receiving disc. The suction type rotational flow mixing distributor is uniformly distributed in a concentric circle shape by taking the center of the reactor shell as the circle center, and the number of the suction type rotational flow mixing distributor can be determined according to the actual working condition and is generally 2-10.
The working principle of the gas-liquid mixing and distributing equipment provided by the invention is as follows:
the oil gas reacted by the upper catalyst bed layer flows downwards through the catalyst grating; in order to meet the requirement of the next bed for continuous effective reaction, cold hydrogen is introduced between two beds to control the temperature, the cold hydrogen is uniformly injected above the liquid receiving disc through spray holes (or nozzles) of a cold hydrogen distribution pipe, then enters a rotational flow mixing cavity together with reaction oil gas through an inlet of the rotational flow mixing cavity and enters a descending pipe through an outlet of the rotational flow mixing cavity, the mixture in the descending pipe after being mixed by a reinforced mixing element enters the rotational flow distribution cavity through an inlet of the rotational flow distribution cavity, is finally sprayed to the periphery through an outlet of the rotational flow distribution cavity, and then is distributed again through a gas-liquid distribution pipe and a distribution disc, so that the oil gas is distributed more uniformly on the whole section of the reactor, and the reaction of the next bed is more stably and effectively carried out.
The invention has the following beneficial effects:
1) The suction type rotational flow mixing distributor can strengthen the mass transfer process, improve the heat transfer efficiency and realize the rapid cooling of high-temperature oil gas;
2) The suction type rotational flow mixing distributor mainly comprises a rotational flow mixing cavity, a downcomer and a rotational flow distribution cavity, has simple and compact structure, saves space, can greatly save the investment of the reactor, is more convenient to install and disassemble, and is suitable for being used between catalyst bed layers of a large-diameter down-flow reactor;
3) The reinforced mixing element can prolong the mixing path and time of cold hydrogen and reaction oil gas, enhance the collision mixing of the cold hydrogen and the reaction oil gas, and more effectively control the temperature of the reaction oil gas. (ii) a
4) The gas-liquid mixing and distributing device adopting the suction type rotational flow mixing distributor can be used for large-scale hydrogenation reactors, and the temperature on the inner section of the reactor can be very uniform by combining with the advanced catalyst filling technology, so that the operation control of the reactor is facilitated, and the service life of the catalyst can be greatly prolonged;
5) The pre-distribution disc is arranged, so that reaction oil gas is pre-mixed and distributed before being mixed and distributed through the gas-liquid distribution pipe, subsequent mixing distribution is more thorough and uniform, the reaction is more stable, and the operation of the reactor is easier to control;
6) The specific gas-liquid distribution pipe and the distribution plate are arranged, so that the materials are mixed more uniformly, the operation elasticity is high, and the reaction is more stable.
Drawings
FIG. 1 is a schematic diagram of one configuration of the suction swirl mixing distributor of the present invention;
FIG. 2 is another schematic construction of the suction swirl mixing distributor of the present invention;
FIG. 3 is a schematic view of yet another configuration of the suction swirl mixing distributor of the present invention;
FIG. 4 is a schematic diagram of a spiral mixing channel in a swirl mixing chamber;
FIG. 5 is a schematic view of a radial distribution passage in the swirl distribution chamber;
FIG. 6 is a schematic view of another configuration of radially distributed passages in a swirl distribution chamber;
FIG. 7 is a schematic structural view of the gas-liquid mixture distribution apparatus of the present invention;
fig. 8 is a schematic view showing the structure of the gas-liquid distribution pipe of fig. 7.
In the figure: 1-cyclone mixing chamber top plate, 2-cyclone mixing chamber, 3-cyclone mixing chamber spiral clapboard, 4-cyclone mixing chamber bottom plate, 5-cyclone mixing chamber bottom plate center hole, 6-downcomer, 7-cyclone distribution chamber top plate, 8-cyclone distribution chamber clapboard, 9-cyclone distribution chamber bottom plate, 10-cyclone distribution chamber top plate center hole, 11-cyclone distribution chamber, 12-cyclone mixing chamber spiral mixing channel, 13-cyclone distribution chamber radial distribution channel, 14-distribution hole, 15-reactor shell, 16-catalyst grid, 17-catalyst grid support beam, 18-cold hydrogen distribution pipe, 19-pipe clamp, 20-suction type cyclone mixing distributor, 21-liquid receiving plate, 22-liquid receiving plate support beam, 23-liquid distribution plate, 24-gas-liquid distribution pipe, 25-plate support beam, 26-outer cylinder, 27-support rib, 28-inner cylinder, 29-circular ring bottom plate, 30-cone, 31-spiral blade, 32-predistribution plate, 33-lower outlet.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
As shown in fig. 1, the suction type cyclone mixing distributor provided by the invention mainly comprises a cyclone mixing chamber 2, a downcomer 6 and a cyclone distribution chamber 11, and is integrally in a vertical dumbbell shape, wherein the cyclone mixing chamber 2 at the upper part is communicated with the cyclone distribution chamber 11 at the lower part through the downcomer 6 in the middle; the cyclone mixing cavity 2 is composed of a cyclone mixing cavity bottom plate 4, a cyclone mixing cavity top plate 1 and a cyclone mixing cavity spiral partition plate 3, the whole cyclone mixing cavity 2 is cylindrical, the cyclone mixing cavity spiral partition plate 3 is vertically arranged between the cyclone mixing cavity bottom plate 4 and the cyclone mixing cavity top plate 1, the cyclone mixing cavity bottom plate 4, the cyclone mixing cavity top plate 1 and the cyclone mixing cavity spiral partition plate 3 jointly enclose a cyclone mixing cavity spiral mixing channel 12 (shown in figure 4), the inlet of the cyclone mixing cavity spiral mixing channel 12 is positioned on the side surface of the cylinder, the outlet of the cyclone mixing cavity spiral mixing channel 12 is positioned in the center of the cylinder and is communicated with a cyclone mixing cavity bottom plate center hole 5 (shown in figure 4), and the width of the cyclone mixing cavity spiral mixing channel 12 is gradually reduced from the outside to the inside or keeps the same width; the cyclone distribution cavity 11 is composed of a cyclone distribution cavity bottom plate 9, a cyclone distribution cavity top plate 7 and a cyclone distribution cavity partition plate 8, the cyclone distribution cavity partition plate 8 is in a spiral shape (see fig. 5) or a straight plate shape (see fig. 6), the cyclone distribution cavity 11 is integrally cylindrical, the cyclone distribution cavity partition plate 8 is vertically arranged between the cyclone distribution cavity bottom plate 9 and the cyclone distribution cavity top plate 7, the cyclone distribution cavity bottom plate 9, the cyclone distribution cavity top plate 7 and the cyclone distribution cavity partition plate 8 jointly enclose a cyclone distribution cavity radial distribution channel 13 (see fig. 5 and 6) which is diverged from the center to the periphery, the inlet of the cyclone distribution cavity radial distribution channel 13 is positioned at the center of the cylinder and is communicated with a cyclone distribution cavity top plate center hole 10 (see fig. 5 and 6), and the outlet of the cyclone distribution cavity radial distribution channel 13 is positioned on the side surface of the cylinder; the upper end of the down pipe 6 is communicated with a central hole 5 of a bottom plate of the rotational flow mixing cavity, and the lower end of the down pipe 6 is communicated with a central hole 10 of a top plate of the rotational flow distribution cavity; a reinforced mixing element bubble cap is arranged in the downcomer 6, the bubble cap comprises an outer cylinder 26 with one open end, an inner cylinder 28 with two open ends and a circular bottom plate 29, the lower end of the inner cylinder 28 is fixedly connected with a central hole of the circular bottom plate 29, the outer cylinder 26 is inversely buckled at the upper end of the inner cylinder 28, the outer cylinder 26 and the inner cylinder 28 are fixedly connected through a support rib 27, the outer edge of the circular bottom plate 29 is fixedly connected with the inner wall of the downcomer 6, and an annular channel communicated from outside to inside is formed among the inner wall of the downcomer 6, the outer cylinder 26 and the outer wall of the inner cylinder 28; the bottom plate of the radial distribution channel 13 of the cyclone distribution cavity is provided with distribution holes 14.
The inlet of the spiral mixing channel 12 of the swirl mixing cavity forms the inlet of the swirl mixing cavity 2, and the central hole 5 of the bottom plate of the swirl mixing cavity forms the inlet of the swirl mixing cavity 2; the central hole 10 of the top plate of the cyclone distribution cavity forms the inlet of the cyclone distribution cavity 11, and the outlet of the radial distribution channel 13 of the cyclone distribution cavity forms the outlet of the cyclone distribution cavity 11.
Wherein, the number of the spiral baffle plates 3 of the rotational flow mixing cavity can be set to be 2-4; the number of the cyclone distribution chamber partition plates 8 can be set to be 4-12.
As shown in fig. 2, another suction type swirl mixing distributor provided by the present invention is different from fig. 1 in that: the intensive mixing element that sets up in downcomer 6 is a conical drum 30, and conical drum 30 both ends are uncovered, and its main aspects is up, and the tip is down, is equipped with the trompil on the conical surface, and the trompil can be round hole, bar hole or square hole, and conical drum 30 has set up 2 along 6 axial intervals of downcomer with its main aspects and 6 inner walls fixed connection of downcomer, conical drum 30.
As shown in fig. 3, the present invention provides a further suction swirl mixing distributor which is different from that of fig. 1 in that: the intensive mixing element arranged in the downcomer 6 is a helical blade 31, the outer edge of the helical blade 31 is fixedly connected with the inner wall of the downcomer 6, and a helical descending channel is formed together with the inner wall of the downcomer 6.
As shown in fig. 7, the gas-liquid mixing distribution apparatus of the present invention comprises a reactor shell 15, and a catalyst grid 16, a cold hydrogen distribution pipe 18, a suction type cyclone mixing distributor 20, a liquid receiving tray 21, a gas-liquid distribution pipe 24 and a distribution tray 23, which are arranged in the reactor shell from top to bottom; the cold hydrogen distribution pipe 18 is positioned under the catalyst grid 16 and fixed on the catalyst grid support beam 17 by the pipe clamp 19, the catalyst grid 16 is fixed on the catalyst grid support beam 17, the liquid receiving disc 21 is fixed on the distribution disc support beam 25 and is fixedly connected with the inner wall of the reactor shell 15, and the suction type rotational flow mixing distributor 20 is fixed on the liquid receiving disc 21; the gas-liquid distribution pipe 24 and the distribution plate 23 are positioned below the liquid receiving plate 21, the distribution plate 23 is fixed on the distribution plate support beam 25 and is fixedly connected with the inner wall of the reactor shell 15, and the gas-liquid distribution pipe 24 is vertically fixed on the distribution plate 23. A pre-distribution tray 32 is also arranged between the liquid receiving tray 21 and the distribution tray 23.
The suction type cyclone mixing distributor 20 is fixed on a liquid receiving disc 21 through a downcomer 6, a cyclone mixing cavity 2 is positioned above the liquid receiving disc 21, a cyclone distribution cavity 11 is positioned below the liquid receiving disc 21 (see figure 1), and a conical cylinder (not marked with a serial number in figure 7) of an intensified mixing element is arranged in the downcomer 6.
As shown in fig. 8, the lower outlet 33 of the gas-liquid distribution pipe 24 is in the shape of a narrow-middle narrow-end large-throat pipe, the aperture ratio (aperture ratio defined by the ratio of the total area of the throat section to the radial cross-sectional area of the reactor) of the throat (the narrowest part of the lower outlet 33) is 2 to 6%, and the ratio of the inner diameter of the gas-liquid distribution pipe to the diameter of the throat is 1.5 to 3.
The working principle of the invention is explained below with reference to the accompanying drawings 1 to 8:
the oil gas reacted by the upper catalyst bed layer flows downwards through the catalyst grating 16; in order to meet the requirement of the next bed for continuous effective reaction, cold hydrogen is introduced between the two beds to reduce the temperature of reaction oil gas, and the cold hydrogen is injected into the bed space through a cold hydrogen distribution pipe 18, is uniformly distributed in the radial and circumferential directions of the whole section of the reactor and is primarily mixed with the reaction oil gas; the preliminarily mixed reaction oil gas and cold hydrogen are accumulated on a liquid receiving disc 21, then enter a rotational flow mixing cavity 2 through a rotational flow mixing cavity spiral mixing channel 12 of a suction type rotational flow mixing distributor 20, enter a descending pipe 6 through a rotational flow mixing cavity bottom plate central hole 5, are mixed in the descending pipe 6 through a reinforced mixing element (a bubble cap, a conical barrel 30 or a spiral blade 31 and the like), then flow through a rotational flow distribution cavity top plate central hole 10, enter a rotational flow distribution cavity 11 and flow through a rotational flow distribution cavity radial distribution channel 13, and finally flow out through a rotational flow distribution cavity radial distribution channel outlet and a distribution hole 14. The oil gas mixed and distributed by the suction type cyclone mixing distributor 20 is continuously distributed again downwards through the pre-distribution disc 32, the distribution disc 23 and the gas-liquid distribution pipe 24 below, so that the oil gas is distributed more uniformly on the whole cross section of the reactor, and the reaction of the next catalyst bed layer is more effective.
Claims (14)
1. A suction swirl mixing distributor characterized in that: the cyclone mixing chamber at the upper part is communicated with the cyclone distribution chamber at the lower part through the down pipe in the middle; the spiral mixing cavity is composed of a bottom plate, a top plate and a spiral partition plate, the spiral partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the spiral partition plate jointly enclose a spiral mixing channel, an inlet of the spiral mixing channel is positioned on the side surface of the cylinder and forms an inlet of the spiral mixing cavity, an outlet of the spiral mixing channel is positioned in the center of the cylinder and is communicated with a center hole of the bottom plate, the center hole of the bottom plate forms an outlet of the spiral mixing cavity, and the spiral mixing channel gradually reduces in width from outside to inside or keeps the same width; the cyclone distribution cavity consists of a bottom plate, a top plate and a partition plate, the partition plate is in a spiral shape or a straight plate shape, the cyclone distribution cavity is integrally cylindrical, the partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the partition plate jointly enclose a radial distribution channel which is diverged from the center to the periphery, the inlet of the radial distribution channel is positioned at the center of the cylinder and is communicated with the central hole of the top plate, the central hole of the top plate forms the inlet of the cyclone distribution cavity, and the outlet of the radial distribution channel is positioned on the side surface of the cylinder and forms the outlet of the cyclone distribution cavity; the upper end of the downcomer is communicated with a central hole of a bottom plate of the rotational flow mixing chamber, and the lower end of the downcomer is communicated with a central hole of a top plate of the rotational flow distribution chamber; the interior of the downcomer is provided with an intensified mixing element.
2. The aspirating cyclonic mixing distributor of claim 1, wherein: the reinforced mixing element is a bubble cap which comprises an outer barrel with an opening end, an inner barrel with two openings and a circular bottom plate, the lower end of the inner barrel is fixedly connected with a center hole of the circular bottom plate, the outer barrel is reversely buckled at the upper end of the inner barrel, the outer barrel and the inner barrel are fixedly connected through a supporting rib, the outer edge of the circular bottom plate is fixedly connected with the inner wall of a descending pipe, and an annular channel which is communicated from outside to inside is formed among the inner wall of the descending pipe, the outer barrel and the outer wall of the inner barrel.
3. The aspirating cyclonic mixing distributor of claim 1, wherein: the reinforced mixing element is a conical cylinder, two ends of the conical cylinder are open, the large end of the conical cylinder faces upwards, the small end of the conical cylinder faces downwards, an opening is formed in the conical surface, and the large end of the conical cylinder is fixedly connected with the inner wall of the descending pipe.
4. The aspirating cyclonic mixing distributor of claim 1, wherein: the reinforced mixing element is a helical blade, the outer edge of the helical blade is fixedly connected with the inner wall of the downcomer, and a helical descending channel is formed together with the inner wall of the downcomer.
5. The aspirating cyclonic mixing distributor of claim 1, wherein: distribution holes are arranged on the bottom plate of the radial distribution channel.
6. A gas-liquid mixing distribution apparatus using the suction swirl mixing distributor of claim 1, characterized in that: comprises a reactor shell, and a catalyst grid, a cold hydrogen distribution pipe, a suction type rotational flow mixing distributor, a liquid receiving disc, a gas-liquid distribution pipe and a distribution disc which are arranged in the reactor shell from top to bottom; the cold hydrogen distribution pipe is positioned below the catalyst grid, the liquid receiving disc is fixedly connected with the inner wall of the reactor shell, and the suction type rotational flow mixing distributor is fixed on the liquid receiving disc; the gas-liquid distribution pipe and the distribution plate are located below the liquid receiving plate, the distribution plate is fixedly connected with the inner wall of the reactor shell, and the gas-liquid distribution pipe is vertically fixed on the distribution plate.
7. The gas-liquid mixture distribution apparatus according to claim 6, wherein: the reinforced mixing element is a bubble cap, the bubble cap comprises an outer cylinder with an open end, an inner cylinder with two open ends and a circular ring-shaped bottom plate, the lower end of the inner cylinder is fixedly connected with a central hole of the circular ring-shaped bottom plate, the outer cylinder is reversely buckled at the upper end of the inner cylinder, the outer cylinder and the inner cylinder are fixedly connected through a supporting rib, the outer edge of the circular ring-shaped bottom plate is fixedly connected with the inner wall of a descending pipe, and an annular channel which is communicated from outside to inside is formed among the inner wall of the descending pipe, the outer cylinder and the outer wall of the inner cylinder.
8. The gas-liquid mixture distribution apparatus according to claim 6, wherein: the reinforced mixing element is a conical cylinder, two ends of the conical cylinder are open, the large end of the conical cylinder faces upwards, the small end of the conical cylinder faces downwards, an opening is formed in the conical surface, and the large end of the conical cylinder is fixedly connected with the inner wall of the descending pipe.
9. The gas-liquid mixture distribution apparatus according to claim 6, wherein: the reinforced mixing element is a helical blade, the outer edge of the helical blade is fixedly connected with the inner wall of the downcomer and forms a helical descending channel together with the inner wall of the downcomer.
10. The gas-liquid mixture distribution apparatus according to claim 6, wherein: distribution holes are arranged on the bottom plate of the radial distribution channel.
11. The gas-liquid mixture distribution apparatus according to claim 6, wherein: the lower outlet of the gas-liquid distribution pipe is in a throat shape with a thin middle part and two large ends, and the aperture ratio of the throat part is 2-6%; the ratio of the inner diameter of the gas-liquid distribution pipe to the diameter of the throat part is 1.5-3.
12. The gas-liquid mixture distribution apparatus according to claim 6, wherein: a pre-distribution disc is arranged between the liquid receiving disc and the distribution disc.
13. The gas-liquid mixture distribution apparatus according to claim 6, characterized in that: the suction type rotational flow mixing distributor is fixed on the liquid receiving disc through a descending pipe of the suction type rotational flow mixing distributor, the rotational flow mixing cavity is located above the liquid receiving disc, and the rotational flow distribution cavity is located below the liquid receiving disc.
14. The gas-liquid mixture distribution apparatus according to claim 13, wherein: the suction type rotational flow mixing distributors are uniformly distributed in a concentric circle shape by taking the center of the reactor shell as a circle center.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210883575.7A CN115301160A (en) | 2022-07-26 | 2022-07-26 | Suction type rotational flow mixing distributor and gas-liquid mixing distribution equipment |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210883575.7A CN115301160A (en) | 2022-07-26 | 2022-07-26 | Suction type rotational flow mixing distributor and gas-liquid mixing distribution equipment |
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| CN115301160A true CN115301160A (en) | 2022-11-08 |
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| CN202210883575.7A Pending CN115301160A (en) | 2022-07-26 | 2022-07-26 | Suction type rotational flow mixing distributor and gas-liquid mixing distribution equipment |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101766978A (en) * | 2008-12-31 | 2010-07-07 | 中国石油化工股份有限公司 | Material-flow mixing and dispersing device |
| CN102421510A (en) * | 2009-05-29 | 2012-04-18 | 雪佛龙美国公司 | Mixing device for a down-flow reactor |
| CN111558343A (en) * | 2020-05-25 | 2020-08-21 | 中国石油化工股份有限公司 | Gas-liquid mixing distribution system |
| CN111992143A (en) * | 2020-08-24 | 2020-11-27 | 中国石油化工股份有限公司 | Gas-liquid distribution equipment |
| EP3933013A2 (en) * | 2020-07-04 | 2022-01-05 | Indian Oil Corporation Limited | Quench-box assembly for hydroprocessing reactors |
-
2022
- 2022-07-26 CN CN202210883575.7A patent/CN115301160A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101766978A (en) * | 2008-12-31 | 2010-07-07 | 中国石油化工股份有限公司 | Material-flow mixing and dispersing device |
| CN102421510A (en) * | 2009-05-29 | 2012-04-18 | 雪佛龙美国公司 | Mixing device for a down-flow reactor |
| CN111558343A (en) * | 2020-05-25 | 2020-08-21 | 中国石油化工股份有限公司 | Gas-liquid mixing distribution system |
| EP3933013A2 (en) * | 2020-07-04 | 2022-01-05 | Indian Oil Corporation Limited | Quench-box assembly for hydroprocessing reactors |
| CN111992143A (en) * | 2020-08-24 | 2020-11-27 | 中国石油化工股份有限公司 | Gas-liquid distribution equipment |
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