CN111558339B - Gas-liquid mixing distribution system - Google Patents
Gas-liquid mixing distribution system Download PDFInfo
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- CN111558339B CN111558339B CN202010448040.8A CN202010448040A CN111558339B CN 111558339 B CN111558339 B CN 111558339B CN 202010448040 A CN202010448040 A CN 202010448040A CN 111558339 B CN111558339 B CN 111558339B
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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
- B01J8/04—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 the fluid passing successively through two or more beds
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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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- 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
- B01J8/0285—Heating or cooling the reactor
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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
- B01J8/0292—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 with stationary packing material in the bed, e.g. bricks, wire rings, baffles
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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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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a gas-liquid mixing distribution system, which comprises a shell, and a catalyst grid, a cold hydrogen distributor, a collecting disc, a gas-liquid distributor and a distribution disc which are arranged in the shell from top to bottom; the collecting tray is uniformly provided with mixing chambers; the distribution plate is fixedly connected with the distribution plate supporting beam and the inner wall of the shell respectively, the gas-liquid distributor is vertically fixed on the distribution plate, gas-liquid spray heads are arranged on the distribution plate on two sides of the distribution plate supporting beam and on the position of the inner wall of the shell, the gas-liquid spray heads on the two sides of the distribution plate supporting beam are arranged in opposite directions in a staggered mode or in a pairwise oblique mode, and the gas-liquid spray heads on the inner wall of the shell are arranged right opposite to the inner wall of the shell or obliquely opposite to the inner wall of the shell. The invention can ensure that the cold hydrogen is more uniformly distributed on the whole cross section of the reactor, reduces the dead zones at the inner wall of the shell and the support beam of the distribution plate, and fully ensures the uniform distribution of gas and liquid on the whole cross section of the reactor.
Description
Technical Field
The invention belongs to the field of petroleum processing, and particularly relates to a gas-liquid mixing distribution system.
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 through which the cold hydrogen is introduced into the interior of the reactor and distributed 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 as it enters the next bed. The cold hydrogen pipe is divided into a direct insertion type, a dendritic type and a ring structure according to the form.
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 disk, 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 the second layer of the cold hydrogen box, namely the sieve plate disc, and are baffled again on the sieve plate disc to strengthen the mixing effect, and then are distributed. A layer of redistributing tray is arranged below the sieve plate tray for redistributing 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.
CN201610010133.6 provides a cyclone cold hydrogen pipe for a hydrogenation reactor, which comprises a feeding pipe connected with an outlet of a cold hydrogen storage tank, a distribution loop pipe connected to the feeding pipe, and a plurality of nozzles disposed on the distribution loop pipe, wherein the nozzles are uniformly arranged around the outer wall of the distribution loop 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 outlet holes, 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 enlarged, the advanced applicability of the inner member becomes more important, and how to realize the uniform distribution of the 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 1 ℃, 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 gas-liquid mixing distribution system, 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 is not uniform enough and the heat transfer efficiency is low in the prior art.
The gas-liquid mixing distribution system provided by the invention comprises a shell, and a catalyst grid, a cold hydrogen distributor, a collecting disc, a gas-liquid distributor and a distribution disc which are arranged in the shell from top to bottom; the collecting tray is uniformly provided with mixing chambers; the distribution plate is fixedly connected with the distribution plate supporting beam and the inner wall of the shell respectively, the gas-liquid distributor is vertically fixed on the distribution plate, gas-liquid spray heads located below the distribution plate are arranged on the distribution plate and located on two sides of the distribution plate supporting beam and on the inner wall of the shell, the gas-liquid spray heads are 90-degree bent spray heads with horizontal outlets, the gas-liquid spray heads on two sides of the distribution plate supporting beam are arranged in a staggered mode or in a pairwise oblique mode, and the gas-liquid spray heads on the inner wall of the shell are arranged right opposite to the inner wall of the shell or obliquely opposite to the inner wall of the shell.
The whole heliciform that is of mixing chamber encloses by vertical spiral plate, apron on locating the catch tray and the catch tray as the bottom plate, forms the heliciform passageway in the mixing chamber, and the mixing chamber entry is for following the tangential rectangle mouth of mixing chamber, and the mixing chamber export communicates with the trompil of mixing chamber central point department on the catch tray.
The cold hydrogen distributor mainly comprises an air inlet pipe, an inner ring pipe, an outer ring pipe and branch pipes which are located in the same plane, wherein the outer ring pipe is an annular pipe with two closed ends and is not completely closed, the air inlet pipe penetrates through an unclosed area of the outer ring pipe to be communicated with the inner ring pipe, the inner ring pipe is communicated with the outer ring pipe through the branch pipes, oblique upward spray holes which are arranged in pairs are arranged on the inner ring pipe, the outer ring pipe and the branch pipes at intervals along the axis, and each spray hole is a cold hydrogen outlet.
The two spray holes which are arranged in pairs are arranged in an axial symmetry mode, and each spray hole forms an angle of 30-60 degrees with the horizontal plane.
The spray holes can be provided with straight nozzles, the end part of each straight nozzle is provided with a contraction hole, the spray holes are uniformly arranged near the end part of the straight nozzle along the circumferential direction, and the number of the spray holes is 2-8 so as to ensure the uniform distribution of the cold hydrogen.
As an improved scheme, a coarse distribution disc is arranged in the space inside the shell below the collection disc and above the gas-liquid distributor, and liquid distribution holes are uniformly distributed in the coarse distribution disc.
The working principle of the gas-liquid mixing distribution system provided by the invention is as follows:
the reaction oil gas of the upper catalyst bed layer flows downwards through the catalyst grating, and cold hydrogen is introduced between the two bed layers to control the temperature for the next bed layer to continue effective reaction. Cold hydrogen is introduced into the bed layer through the cold hydrogen distributor, reaction oil gas from the upper layer is uniformly mixed with cold hydrogen sprayed obliquely upwards, the mixture enters the bed layer space, the mixture is uniformly distributed in the radial direction and the circumferential direction of the whole cross section of the reactor, the mixture continues downwards, the mixture further enters the coarse distribution plate below the collection plate after being further mixed by the mixing chamber on the collection plate, the oil gas after being mixed and distributed by the coarse distribution plate enters the distribution plate below the collection plate, the gas-liquid distributor and the gas-liquid spray head for secondary distribution, particularly, the dead zones at the inner wall of the shell and the support beam of the distribution plate are reduced through the distribution of the gas-liquid spray head, so that the oil gas is more uniformly distributed on the whole cross section of the reactor, and the reaction of the next bed layer is more effective.
The invention has the following beneficial effects:
1) The unique structure of the cold hydrogen distributor ensures that the cold hydrogen is more uniformly distributed on the whole cross section of the reactor and can be fully mixed with reaction oil gas, thereby ensuring the uniform proceeding of mass transfer and heat transfer and improving the heat transfer efficiency of the medium in the reactor;
2) The cold hydrogen distributor consists of an air inlet pipe, an inner ring pipe, an outer ring pipe, a branch pipe and spray holes, has simple and compact structure, can greatly save the investment of the reactor, is more convenient to install and disassemble, and is suitable for being used between catalyst beds of a large-diameter downflow reactor.
3) The arrangement of the gas-liquid spray head reduces dead zones at the inner wall of the shell and a support beam of the distribution plate, so that the oil gas is distributed more uniformly on the whole cross section of the reactor.
4) The setting of rough distribution dish makes the reaction oil gas intensive mixing distribute in advance before the mixing distribution through gas-liquid distributor, makes that subsequent mixing distribution goes on more thoroughly, more even, and the reaction is more stable, changes in the operation of control reactor.
Drawings
FIG. 1 is a schematic structural view of a gas-liquid mixing distribution system according to the present invention;
FIG. 2 is a schematic diagram of the configuration of a cold hydrogen distributor;
FIG. 3 isbase:Sub>A schematic view of the structure of FIG. 2 taken along line A-A;
FIG. 4 is a schematic structural view of a straight nozzle;
FIG. 5 is a schematic structural view of a mixing chamber;
FIG. 6 is a schematic top view of the structure of FIG. 5 (without the cover plate);
FIG. 7 is a schematic view showing an assembly structure of the gas-liquid shower head and the gas-liquid distributor;
FIG. 8 is a schematic view of a structure in which gas-liquid nozzles at two sides of a support beam of a distribution plate on the distribution plate are obliquely arranged two by two and gas-liquid nozzles at the inner wall of a shell are obliquely arranged;
FIG. 9 is a schematic view of the structure of the distribution plate with gas-liquid nozzles on the two sides of the support beam of the distribution plate arranged in opposite directions and the gas-liquid nozzles on the inner wall of the casing arranged obliquely.
In the figure: 1-shell, 2-catalyst grid, 3-catalyst grid supporting beam, 4-cold hydrogen distributor supporting beam, 5-collecting tray, 6-rough distribution tray, 7-distribution tray supporting beam, 8-distribution tray, 9-gas-liquid spray head, 10-gas-liquid distributor, 11-mixing chamber, 12-cold hydrogen distributor, 13-gas inlet pipe, 14-inner ring pipe, 15-outer ring pipe, 16-straight pipe, 17-straight spray nozzle, 18-contraction hole, 19-spray hole, 20-collecting tray hole, 21-spiral plate, 22-spiral channel, 23-cover plate.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
As shown in fig. 1, the gas-liquid mixing distribution system of the present invention comprises a housing 1, a catalyst grid 2 fixed on the inner wall of the housing 1 and a catalyst grid support beam 3, a cold hydrogen distributor 12 fixed on a cold hydrogen distributor support beam 4 under the catalyst grid 2, a mixing chamber 11 fixed on a collection tray 5 under the cold hydrogen distributor 12, a rough distribution tray 6 under the collection tray 5, and a gas-liquid distributor 10 fixed on a distribution tray 8 under the rough distribution tray 6; the distribution plate 8 is fixedly connected with the distribution plate support beam 7 and the inner wall of the shell 1 respectively, gas-liquid spray heads 9 located below the distribution plate 8 are arranged on the distribution plate 8 and located on the two sides 7 of the distribution plate support beam and on the inner wall of the shell 1, the gas-liquid spray heads 9 are 90-degree bent spray heads with horizontal outlets, and liquid distribution holes are uniformly distributed in the rough distribution plate 6.
Fig. 7 is a schematic view of an assembly structure of the gas-liquid shower head 9 and the distribution plate 8.
Fig. 8 shows a schematic structural diagram of the distribution plate in which two gas-liquid nozzles 9 on two sides of the distribution plate support beam 7 are obliquely arranged in pairs and the gas-liquid nozzles 9 on the inner wall of the casing 1 are obliquely arranged on the inner wall of the casing, and arrows in the diagram indicate the orientations of the gas-liquid nozzles 9, that is, the gas-liquid nozzles 9 on two sides of the distribution plate support beam 7 are pairwise arranged and the orientations are obliquely arranged with a certain inclination angle.
Fig. 9 shows a schematic structural diagram of the distribution plate with the gas-liquid nozzles 9 on the two sides of the distribution plate support beam 7 arranged in opposite directions in a staggered manner and the gas-liquid nozzles 9 on the inner wall of the casing 1 arranged in an oblique manner to the inner wall of the casing 1, wherein arrows in the diagram indicate the orientations of the gas-liquid nozzles 9, that is, the gas-liquid nozzles 9 on the two sides of the distribution plate support beam 7 are arranged in a staggered manner at intervals and face the distribution plate support beam.
Of course, the gas-liquid nozzle 9 at the inner wall of the casing 1 may be arranged to face the inner wall of the casing.
As shown in figure 2, the cold hydrogen distributor mainly comprises an air inlet pipe 13, an inner ring pipe 14, an outer ring pipe 15 and branch pipes 16 which are positioned in the same plane, wherein the outer ring pipe 15 is an annular pipe with two closed ends, the two closed ends are not completely closed, the air inlet pipe 13 penetrates through the unclosed area of the outer ring pipe 15 and is communicated with the inner ring pipe 14, the inner ring pipe 14 is communicated with the outer ring pipe 15 through the branch pipes 16, oblique and upward spray holes which are arranged in pairs are arranged on the inner ring pipe 14, the outer ring pipe 15 and the branch pipes 16 at intervals along the axis, each spray hole is a cold hydrogen outlet, the two spray holes which are arranged in pairs are arranged in an axial symmetry mode, and each spray hole forms an angle of 30-60 degrees with the horizontal plane.
As shown in fig. 3 and 4, straight nozzles 17 may be disposed on the obliquely upward nozzles, a contraction hole 18 is disposed at an end of each straight nozzle, injection holes 19 are uniformly disposed near the end of the straight nozzle along the circumferential direction, and the number of the injection holes 19 is 2 to 8, so as to ensure uniform distribution of cold hydrogen.
As shown in fig. 5 and fig. 6, the collecting tray 5 is uniformly provided with a mixing chamber, the mixing chamber is wholly spiral, and is defined by a spiral plate 21 vertically arranged on the collecting tray 5, a cover plate 23 and the collecting tray 5 as a bottom plate, a spiral channel 22 is formed in the mixing chamber, the inlet of the mixing chamber is a rectangular port tangential to the mixing chamber, the outlet of the mixing chamber is communicated with the opening at the center of the mixing chamber on the collecting tray 5, and the opening is the collecting tray opening 20.
The working principle of the invention is explained below with reference to the drawings:
the reaction oil gas of the upper catalyst bed layer flows downwards through the catalyst grid 2, and cold hydrogen is introduced between the two bed layers to control the temperature for the requirement of the next bed layer on continuous effective reaction. Cold hydrogen is introduced into the bed layer through a cold hydrogen distributor 12, reaction oil gas from the upper layer is uniformly mixed with cold hydrogen sprayed obliquely upwards, the mixture enters the space of the bed layer, the mixture is uniformly distributed in the radial direction and the circumferential direction of the whole cross section of the reactor, the mixture continues downwards, the mixture further enters a coarse distribution plate 6 below after being further mixed by a spiral channel 22 of a mixing chamber 11 on a collecting plate 5, the mixture is further distributed by the coarse distribution plate 6, the oil gas after being mixed and distributed by the coarse distribution plate 6 enters a distribution plate 8, a gas-liquid distributor 10 and a gas-liquid sprayer 9 below for further distribution, particularly, the distribution by the gas-liquid sprayer 9 reduces dead zones at the inner wall of a shell 1 and the support beam 7 of the distribution plate, so that the oil gas is distributed more uniformly on the whole cross section of the reactor, and the reaction of the next bed layer is more effective.
Claims (5)
1. A gas-liquid mixture distribution system which characterized in that: comprises a shell, and a catalyst grid, a cold hydrogen distributor, a collecting disc, a gas-liquid distributor and a distributing disc which are arranged in the shell from top to bottom; the collecting tray is uniformly provided with mixing chambers; the distribution plate is fixedly connected with the distribution plate support beam and the inner wall of the shell respectively, the gas-liquid distributor is vertically fixed on the distribution plate, gas-liquid spray heads positioned below the distribution plate are arranged on the distribution plate at the two sides of the distribution plate support beam and at the position of the inner wall of the shell, the gas-liquid spray heads are 90-degree bent spray heads with horizontal outlets, the gas-liquid spray heads at the two sides of the distribution plate support beam are arranged in opposite directions in a staggered mode or obliquely arranged in pairs, and the gas-liquid spray heads at the inner wall of the shell are arranged in a manner of facing the inner wall of the shell or obliquely facing the inner wall of the shell; and a coarse distribution disc is arranged in the space in the shell below the collection disc and above the gas-liquid distributor, and liquid distribution holes are uniformly distributed in the coarse distribution disc.
2. The system of claim 1, wherein: the whole heliciform that is of mixing chamber encloses by vertical spiral plate, apron on locating the catch tray and the catch tray as the bottom plate, forms the heliciform passageway in the mixing chamber, and the mixing chamber entry is for following the tangential rectangle mouth of mixing chamber, and the mixing chamber export communicates with the trompil of mixing chamber central point department on the catch tray.
3. The system according to claim 1 or 2, characterized in that: the cold hydrogen distributor mainly comprises an air inlet pipe, an inner ring pipe, an outer ring pipe and branch pipes which are located in the same plane, wherein the outer ring pipe is an annular pipe with two closed ends and is not completely closed, the air inlet pipe penetrates through an unclosed area of the outer ring pipe to be communicated with the inner ring pipe, the inner ring pipe is communicated with the outer ring pipe through the branch pipes, oblique upward spray holes which are arranged in pairs are arranged on the inner ring pipe, the outer ring pipe and the branch pipes at intervals along the axis, and each spray hole is a cold hydrogen outlet.
4. The system of claim 3, wherein: the two spray holes which are arranged in pairs are arranged in an axial symmetry mode, and each spray hole forms an angle of 30-60 degrees with the horizontal plane.
5. The system of claim 3, wherein: the straight nozzles are arranged on the spray holes, the end part of each straight nozzle is provided with a contraction hole, and spray holes are uniformly arranged on the end part, close to the straight nozzles, of the straight nozzles along the circumferential direction.
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| CN202010448040.8A CN111558339B (en) | 2020-05-25 | 2020-05-25 | Gas-liquid mixing distribution system |
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| CN202010448040.8A CN111558339B (en) | 2020-05-25 | 2020-05-25 | Gas-liquid mixing distribution system |
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| CN111558339B true CN111558339B (en) | 2023-03-31 |
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| CN102943475A (en) * | 2012-11-23 | 2013-02-27 | 上海工程机械厂有限公司 | Cooling device of diesel hammer |
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| CN106040106A (en) * | 2015-04-01 | 2016-10-26 | Ifp 新能源公司 | Mixing and distribution device comprising a distribution plate with peripheral openings |
| CN205886828U (en) * | 2016-05-31 | 2017-01-18 | 兰州兰石集团有限公司 | Cold hydrogen case of spiral overhead paddle |
| CN106422542A (en) * | 2016-12-02 | 2017-02-22 | 郑州经度知识产权代理服务有限公司 | Pulp gas-water separation device for papermaking field on basis of centrifugal force principle |
| CN109200952A (en) * | 2018-11-15 | 2019-01-15 | 中石化炼化工程（集团）股份有限公司 | A kind of gas-liquid mixed component and the catalyst bed structure for reactor |
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2020
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0716881A1 (en) * | 1994-08-23 | 1996-06-19 | Shell Internationale Researchmaatschappij B.V. | Distributor device for multiple-bed downflow reactors |
| CN1891333A (en) * | 2005-05-13 | 2007-01-10 | 赫多特普索化工设备公司 | Improved distributor system for downflow reactors |
| CN102076873A (en) * | 2008-06-26 | 2011-05-25 | 环球油品公司 | Improved quench zone design using spray nozzles |
| CN101811930A (en) * | 2009-02-19 | 2010-08-25 | 中国石油化工股份有限公司 | Selective hydrogenation method for phenylacetylene in phenylacetylene-containing styrene material flow |
| CN102943475A (en) * | 2012-11-23 | 2013-02-27 | 上海工程机械厂有限公司 | Cooling device of diesel hammer |
| CN106040106A (en) * | 2015-04-01 | 2016-10-26 | Ifp 新能源公司 | Mixing and distribution device comprising a distribution plate with peripheral openings |
| CN105921078A (en) * | 2016-05-31 | 2016-09-07 | 兰州兰石集团有限公司 | Vortex broken flow type hydrogen cold box |
| CN205886828U (en) * | 2016-05-31 | 2017-01-18 | 兰州兰石集团有限公司 | Cold hydrogen case of spiral overhead paddle |
| CN106422542A (en) * | 2016-12-02 | 2017-02-22 | 郑州经度知识产权代理服务有限公司 | Pulp gas-water separation device for papermaking field on basis of centrifugal force principle |
| CN109200952A (en) * | 2018-11-15 | 2019-01-15 | 中石化炼化工程（集团）股份有限公司 | A kind of gas-liquid mixed component and the catalyst bed structure for reactor |
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