CN109985575A - With subtracting the hydrogenator for rushing component - Google Patents
With subtracting the hydrogenator for rushing component Download PDFInfo
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- CN109985575A CN109985575A CN201811291429.5A CN201811291429A CN109985575A CN 109985575 A CN109985575 A CN 109985575A CN 201811291429 A CN201811291429 A CN 201811291429A CN 109985575 A CN109985575 A CN 109985575A
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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
- B01J8/0446—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 the flow within the beds being predominantly vertical
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- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of with subtracting the hydrogenator for rushing component.Hydrogenator of the invention includes material inlet pipe, inlet diffuser, reactor upper cover, subtracts and rush equal flow table, catalyst bed, catalyst support grid, reactor shell, reactor lower head, exit collector, material outlet pipe and unload agent pipe.Described subtract rushes equal flow table and is arranged in the idle space of reactor upper cover or reactor shell upper end；Described to subtract that rush equal flow table include subtracting to rush tower tray and be set to several distributors for subtracting and rushing on tower tray, distributor includes grid, drop expects pipe and connecting rod, and grid is set to above drop expects pipe, grid with drop expects pipe and connect by connecting rod.Hydrogenator of the invention is suitable for hydrogenation process, especially reactor larger hydrofinishing or hydrocracking process.
Description
Technical field
The present invention relates to a kind of with the hydrogenator for rushing component is subtracted, and belongs to field of chemical equipment.Of the invention plus hydrogen
Reactor is suitable for the larger hydrofinishing or hydrocracking process of hydrogenation process, especially reactor.
Background technique
In recent years, with the enhancing of economic fast development and environmental consciousness, to the quality and environmental requirement of petroleum chemicals
It is higher and higher.As a kind of technological means of production clean fuel, importance and role of the hydrogen addition technology in petroleum refining industry is got over
Come bigger.In hydrogenation plant, with hydrogenation catalyst technology as hydrogenation technique technology, hydrogenator technology is reactor
The important component of system, three constitute three factor of reactor performance.In hydrogenation plant, add hydrogen anti-as key equipment
Device is answered, it is anti-to complete purification and cracking etc. by the effect of hydrogenation catalyst wherein for the feedstock oil after mixing hydrogen by a certain percentage
It answers.Hydrogenation reaction in hydrogenator can stable operation, can hydrogenation catalyst its function can be fully exerted, product quality
Whether can reach high-quality, be heavily dependent on the uniformity that gas-liquid is distributed in catalyst bed.And gas-liquid is being catalyzed
Whether the distribution in agent bed is uniform, and the design with hydrogenator inner member has close relationship.In other words, inner member
The quality of energy directly influences the operation cycle of catalyst life, product quality and device, i.e., using a set of in hydrogenation process
The obtained effect of inner member technology of function admirable is never second to use a kind of higher catalyst of activity instead.Therefore right both at home and abroad
The research of hydrogenator and its inner member and engineering development are paid much attention to always, its reactor component is constantly updated, in the hope of
Obtain better effect.
Commercial plant production practices show restrict the even running of hydrogenation technique device factor it is main there are two, one is
The reactor radial temperature difference caused by material is unevenly distributed is larger, and one is that reactor catalyst pressure drop of column increased
Fastly, lead to improper shut-down.
Hydrogenator is with the charging of reactor head center, and inlet diffuser, material convey residual despite the provision of
Remaining kinetic energy can generate powerful impact force；Another fluidised form feature of center charging is that material is in reactor end socket space
The streamline of formation be parallax, the fluidised form of the kinetic energy of material and inclined line, by the liquid layer on top dispenser tower tray to anti-
It answers the punching of device surrounding to send, forms " pushing away wave " phenomenon on the distribution plate of top of material, that is, reactor distribution plate is from center to side
The height of liquid layer of edge position is in being incrementally distributed: centre bit region material liquid layer is smaller, even without liquid layer, and reactor side wall
Locate material height of liquid layer maximum, unfavorable entry condition is brought to the distributor for relying on tray level degree, even if performance is best
Distributor also cannot achieve under the conditions of the liquid layer of different height and evenly distribute material.Increasingly with work hydrogenator scale
Greatly, material, which enters, " pushes away wave " caused by the impact force that remaining kinetic energy and potential energy are formed after reactor phenomenon is more and more tighter
Weight, leading to material distribution, there are serious deviations.
Hydrogenation process is exothermic reaction, and material, which is unevenly distributed, will lead to the good position extent of reaction of catalyst irrigation effect
Acutely, it is more to generate heat；Influence the radial temperature difference of reactor.When radial temperature difference is larger, catalyst local temperature is higher,
Reaction rate is faster, forms heat spot, makes this partial catalyst performance premature inactivation, damage the performance of catalyst, or even can lead
The coking, hardened of catalysing area subregion is caused, material can not normally flow through, since fixed bed hydrogenation reactor is trickle bed stream
State causes the catalyst below hardened region that cannot play a role, to substantially reduce the service life and device of catalyst
On-stream time.The hardened raising for also resulting in catalyst bed pressure drop in part, has to improve reactor to continue to run
Operating pressure causes the raising of energy consumption.
With being growing for hydrogenator scale, Product Precision requires increasingly to improve, and material is on catalyst bed
Evenly distribute it is particularly significant.Since hydrogenation process is exothermic reaction, feedstock oil is distributed not on catalyst bed radial section
Uniformly, it will lead to extent of reaction difference and generate radial temperature difference, or even will appear hot-spot, damage the performance of catalyst, from
And substantially reduce the service life of catalyst.Therefore select the hydrogenator rationally designed very necessary.
Summary of the invention
Aiming at the shortcomings in the prior art, the present invention provides a kind of with subtracting the hydrogenator for rushing component.
It is of the invention have subtract the hydrogenator for rushing component and include material inlet pipe, inlet diffuser, seal on reactor
Head subtracts and rushes equal flow table, catalyst bed, catalyst support grid, reactor shell, reactor lower head, exit collector, object
Expect outlet and unloads agent pipe；Described subtract rushes equal flow table and is arranged in the idle space of reactor upper cover or reactor shell
Upper end；Described to subtract that rush equal flow table include subtracting several distributors for rushing tower tray and being arranged on tower tray, the distributor includes lattice
Grid, drop expects pipe and connecting rod, grid are set to above drop expects pipe, and grid is connect with drop expects pipe by connecting rod.Described subtract rushes equal flow table
Have the characteristics that have subtract rush flow equalizing function, distributed effect be good, small in size and installation accuracy require it is low.
In some embodiments, hydrogenator of the invention further includes that bed unloads agent pipe, cold hydrogen tube, cold hydrogen disk, spray
Penetrate distribution plate between disk, bed.I.e. hydrogenator includes more than two hydrogenation catalyst beds.
In further preferred embodiment, hydrogenator of the invention further includes top distribution plate, the top
Distribution plate, which is located to subtract, to be rushed below equal flow table.
Of the present invention subtract rushes in equal flow table, and there are space, institutes between the lower surface of grid and the most upper edge for dropping expects pipe
State the flow channel that space constitutes gaseous phase materials.
Further, the flanging that the ragged edge of the tower tray has direction upward along setting, flanging have certain altitude.Tower
Disk can be divided into several pieces of small tower trays, and several pieces of small tower trays can be assembled into a whole tower tray.
Further, the grid includes several pieces of flase floors and flase floor connecting rod, and several pieces of flase floors pass through grid
Plate connecting rod links together.Several pieces of flase floors parallel arrangement in the horizontal direction, and be obliquely installed.Flase floor inclines
Tilted direction is reactor outer direction, and flase floor inclination angle is 10 °~90 °, preferably 20 °~45 °.The width of flase floor be 10~
200mm, preferably 50~120mm；(level) spacing between adjacent grid plate is 10~300mm, preferably 50~150mm.
Several pieces of flase floors grille-like that parallel arrangement is formed in the horizontal direction is rectangle, or is cut into circle.
Further, the distributor is arranged according to certain rules on tower tray, triangular in shape, quadrangle, diamond shape
Or circular arrangement.
Further, the distributor and tower tray can using welding, be bolted, screw connection or snap connection,
Preferably it is bolted.
Further, the quantity of the grid and drop expects pipe is identical or different, preferably identical.
Further, a certain number of overflow holes, the center line and tower tray of the overflow hole are opened up in the drop expects pipe
There is certain altitude between upper surface.
Further, it when grating type subtracts and rushes equal flow table and be set to reactor shell upper end, is preferably disposed in reactor
The top of top distribution plate.
Compared with prior art, it is of the invention have subtract the hydrogenator for rushing component and have the advantages that
1, present invention firstly provides grating type is arranged in reactor subtracts to rush the structure of this novel reactor inner member of equal flow table
Think, the grating type subtracts that rush equal flow table be the reactor component newly established, and can cut down when material enters reactor because of remnants
The strong impact power that kinetic energy is formed；It eliminates because the material using inclined fluidised form caused by existing central feeding mode is to reaction
" pushing away wave " effect of liquid layer on device inner top distribution plate；Eliminate liquid material autoreactor entrance fall on the distribution plate of top by
Potential energy and come impact force；Realize that the fining of liquid material fluid flow state is adjusted；Realize the first distribution of material.The grid
Formula subtract rush equal flow table can also substitute top distribution plate distribution function, can be provided for top catalyst bed it is good enter pig's tongue
Part.The grating type that the present invention increases newly subtract rush equal flow table have subtract rush flow equalizing function and also distributed effect it is good, it is small in size, installation essence
Degree requires the features such as low.
2, equal flow table is rushed in hydrogenator of the invention, described subtracting, and setting, which has, subtracts the distributor for rushing function, and described point
The grid on orchestration top can stop the injection fluid of the inclined fluidised form because being formed using central feeding mode, eliminate fluid certainly
The impact force that reactor inlet falls to top distribution plate from potential energy, lose kinetic energy fluid be blocked after in gravity
Under effect, vertical fluidised form is converted by original inclination fluidised form, and realize that nature falls, eliminates material to liquid layer on distribution plate
" pushing away wave " phenomenon.Fluid falls can form the consistent liquid layer of depth on tower tray, give catalyst bed or top dispenser
The entry condition of friendly even is provided, realizes fluid flow state fining adjusting and the first distribution of material.Be arranged quantity be suitable for,
Equal flow table is rushed with subtracting the grating type for rushing function and subtracting, alternative existing top distribution plate, that realizes material evenly distributes function.
3, it in hydrogenator of the invention, rushes equal flow table by subtracting for setting and realizes even in liquid phase distribution, and it is traditional
The bubble cap distributor of suction principle is compared, and the disperse power of liquid phase distribution is changed to form splash using potential energy by gas phase suction, from
And reduce pressure drop.
4, hydrogenator of the invention, by the way that the overflow hole of suitable shape is arranged in the suitable position of drop expects pipe tube wall,
Guarantee to be formed on tower tray and there are the liquid layers of certain reasonable depth, reduces macro by tray level degree deviation and level fluctuation bring
It is uneven to see distribution.
5, hydrogenator of the invention realizes the uniform of material using unique design principle and hydrodynamics feature
Distribution can make the reduction of catalyst bed radial temperature difference, urge especially when being applied to the reactor catalysis reaction equipped with catalyst
Agent bed radial temperature difference is not more than 3 DEG C, and since radial temperature difference reflects the distributed effect of fluid, this has absolutely proved the present invention
Formula equal flow table in tooth weir is preferable to the distribution of reaction feed logistics and gas-liquid mixed effect, to catalytic reaction process and catalyst coking
Control has certain booster action.
6, compared with prior art, it is of the invention have subtract the hydrogenator for rushing component, subtract and rush equal flow table structure letter
Single, easy for installation, operating flexibility is big, can be installed in reactor upper cover or be arranged in reactor shell upper end, top
The space utilization rate of reactor can be improved, convenient for loading more catalyst in reactor and other set in the upper surface of distribution plate
Standby or diminution reactor scale.Improve reactor top to divide material inlet condition, the radial distribution effect for improving reactor feed, have
Elimination reaction device radial temperature difference is imitated, heat spot caused by catalyst bed is unevenly distributed because of material is eliminated, to be urged in reactor
Effective entry condition excellent using offer of agent, reduces catalyst skimming or changes agent number, extend the on-stream time of device,
Technological effect is improved, it is with good economic efficiency.
Detailed description of the invention
Fig. 1 is hydrogenator structural schematic diagram of the present invention.
Fig. 2 is that the present invention subtracts and rushes equal flow table schematic diagram.
Fig. 3 is that the present invention subtracts the distributor schematic diagram for rushing equal flow table.
Fig. 4 is that the present invention subtracts the equal flow table schematic diagram for rushing equal flow table.
Fig. 5 be the present invention subtract rush equal flow table work when liquid flow to schematic diagram.
Fig. 6 is the orientation schematic diagram of different temperature measuring points on same bed section in the embodiment of the present invention and comparative example.
Specific embodiment
Embodiments of the present invention are described in further detail with reference to the accompanying drawings and examples.Following embodiment is used for
Illustrate the present invention, but cannot be used to limit the scope of the invention.
In the description of the present invention, it should be noted that unless otherwise indicated, " several " are meant that one or one
More than, the meaning of " plurality " is two or more；The instruction such as term " on ", "lower", "inner", "outside", " top ", " bottom "
Orientation or positional relationship be based on the orientation or positional relationship shown in the drawings, be merely for convenience of description the present invention and simplification retouch
It states, rather than the device or element of indication or suggestion meaning must have a particular orientation, be constructed and operated in a specific orientation,
Therefore it is not considered as limiting the invention.
In the description of the present invention, it is also necessary to which explanation is unless specifically defined or limited otherwise, term " installation ",
" connected ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integrally connect
It connects；It can be directly connected, it can also be indirectly connected through an intermediary.For the ordinary skill in the art, may be used
The concrete meaning of above-mentioned term in the present invention is understood depending on concrete condition.
As shown in Figures 1 to 4, hydrogenator of the invention includes material inlet pipe 1, inlet diffuser 2, on reactor
End socket 3 subtracts and rushes equal flow table 4, catalyst bed 5, catalyst support grid 6, reactor shell 12, reactor lower head 13, goes out
Mouth collector 14, unloads agent pipe 16 and supporting element 18 at material outlet pipe 15.In some embodiments, the hydrogenator
It further include that bed unloads distribution plate 11 between agent pipe 7, cold hydrogen tube 8, cold hydrogen disk 9, spraying disc 10 and bed, i.e. hydrogenator includes two
A above catalyst bed.And in further preferred embodiment, the also included top of hydrogenator of the invention
Distribution plate 17, top distribution plate 17, which is located at, subtracts the lower section for rushing equal flow table.
It is described to subtract that rush equal flow table 4 include subtracting to rush tower tray 4-2, tower tray connector 4-3 and be set to point for subtracting and rushing on tower tray
Orchestration 4-1；The distributor 4-1 includes grid 4-1-1, drop expects pipe 4-1-4 and connecting rod 4-1-3, and grid 4-1-1, which is set to, drops material
Above pipe 4-1-4, grid 4-1-1 is connect with drop expects pipe 4-1-4 by connecting rod 4-1-3.The most lower edge and drop of the grid 4-1-1
There are space between the most upper edge of expects pipe 4-1-4, the space constitutes the flow channel of gaseous phase materials.The spatial altitude be 5 ~
200mm, preferably 10 ~ 50mm, the flanging 4-4 that the ragged edge of the tower tray 4-2 has direction upward along setting.The flanging is high
Degree is 5 ~ 80mm, preferably 30 ~ 50mm.The grid 4-1-1 includes flase floor 4-1-6 and flase floor connecting rod 4-1-2, and several pieces
Flase floor 4-1-6 is linked together by flase floor connecting rod 4-1-2, and several pieces of flase floor 4-1-6 are put down in the horizontal direction
Row arrangement, and flase floor 4-1-6 is obliquely installed, inclined direction is towards reactor outer direction.The inclination angle the flase floor 4-1-6
Generally 10 °~90 °, preferably 20 °~45 °.The flase floor 4-1-6 width is 10~200mm, preferably 50~120mm.
Spacing between the adjacent grid plate 4-1-6 is 10~300mm, preferably 50~150mm.The grid 4-1-1 and drop material
Pipe 4-1-4 quantity is identical or different, preferably identical.Overflow hole 4-1-5 is offered on the drop expects pipe 4-1-4.The overflow hole
4-1-5 is 1~6, preferably 1 ~ 2.The total sectional area of the overflow hole 4-1-5 be drop expects pipe 4-1-4 sectional area 10% ~
100%, preferably 30% ~ 50%.The shape of the overflow hole 4-1-5 is polygon, specifically triangle, quadrangle or circle,
It is preferably circular.The center line of the overflow hole 4-1-5 is away from 5 ~ 100mm of tower tray upper surface, preferably 30 ~ 50mm.The distribution
Device 4-1 and tower tray 4-2 is preferably bolted using welding, being bolted, screw connection or snapping connection.The distributor
4-1 arranges according to certain rules on tower tray 4-2, triangular in shape, quadrangle, diamond shape or circular arrangement.It is described subtract punching flow
Disk 4 is set in the upper cover of reactor, or is set to reactor shell upper end；When being set to reactor shell upper end,
It is preferably disposed on the top of top distribution plate in reactor.The lower end of drop expects pipe, which is plugged on to subtract, to be rushed on tower tray, and rushes tower with subtracting
Disk is fixedly connected, end with subtract rush tower tray it is concordant or stretch out tower tray.
As shown in figure 5, further illustrating in hydrogenator of the present invention in conjunction with Fig. 1-4 and subtracting the course of work for rushing equal flow table:
It is described subtract rush equal flow table work when, material is entered in reactor by the inlet diffuser of reactor, because pump conveying have remnants
Kinetic energy, thus material has powerful impact force.Since material autoreactor center is fed, although existing reactor is equal
Inlet porting diffuser, but material is still in that oblique line fluidised form is sprayed around.When tooth provided by the invention is arranged in reactor
Weir formula subtracts rush equal flow table after, fluid is struck first on the grid 4-1-1 of distributor 4-1, because of the oblique cloth of flase floor 4-1-6
It sets, can effectively stop the fluid in the injection of oblique line fluidised form, its impact force is cut down, stop to make using flase floor 4-1-6
With, force Vapor Entrainment drop to disperse around, realize the larger angle of flare of material, fluid after kinetic energy exhausts under the effect of gravity
Naturally it drips, forms vertical downward flow state, liquid phase potential energy is the kinetic energy of freely falling body, and falls to subtracting the tower for rushing equal flow table
On disk 4-2, due to being provided with overflow hole 4-1-5 on drop expects pipe 4-1-4, i.e., material channel is in horizontally disposed, and overflow hole 4-1-5
Have certain altitude poor apart from tower tray 4-2, thus material can form the liquid layer with certain depth on tower tray 4-2, even if tower
There are deviations for disk 4-2 levelness, still can ensure that each distributor 4-1 with the presence of liquid phase.It, can since distributor 4-1 quantity is more
To guarantee that any one point of catalyst in reactor bed face has a certain number of distributor 4-1 to work, so that distributor
The 4-1 uniformity is protected.The overflow hole 4-1-5 that fluid is opened up from drop expects pipe 4-1-3 tube wall flows into top in reactor
On distribution plate, the preliminary distribution of material is realized.Since the material after subtracting and rushing equal flow table is when being assigned on the distribution plate of top
Vertical fluidised form is had been converted into, and kinetic energy disappears, therefore there is no thrusts to the liquid layer on the distribution plate tray surface of top, eliminate
Material acts on " the pushing away wave " of liquid layer on distribution plate, to top distribution plate provides friendly, steady, uniform entry condition,
Material being uniformly distributed on catalyst bed is realized together with the distribution plate of top.
When the less operating condition of liquid phase object doses or when the filling protective agent of catalyst bed top, hydrogenation reaction of the invention
Equal flow table is rushed in device, subtracting for setting, may replace the top distribution plate in reactor, and realization subtracts punching, flows and distribute integration.
The protection scope for illustrating reaction effect of the invention below with reference to embodiment, but being not intended to limit the present invention.
Comparative example 1
A hydrogenator in certain Refinery Coking Gasoline hydrofining unit, the reactor diameter are 3.2m, upper envelope
It leaves unused in head, top layer's catalyst bed inlet is provided with top distribution plate, and the ERI type of this field routine is used in the distribution plate of top
Bubble cap formula gas-liquid allotter, hydrogenating materials are coker naphtha, and catalyst is the FGH- of Fushun Petrochemical Research Institute's production
21 type Hydrobon catalysts, the process conditions of the reactor are as follows: hydrogen partial pressure 2.0MPa, volume space velocity 2.0h-1, hydrogen oil volume
Than for 300:1,280 DEG C of reactor inlet temperature, catalyst bed radial temperature and the temperature difference are shown in Table 1.
Embodiment 1
Compared with comparative example 1, the embodiment of the present invention 1 uses hydrogenator of the invention, in the upper cover of hydrogenator
It is interior to rush equal flow table provided with of the invention subtracting, equal flow table and common ERI type bubble cap formula gas-liquid point are rushed using as shown in Figure 2 subtracting
Orchestration is applied in combination.It is described to subtract the parameter for rushing equal flow table are as follows: the spacing between adjacent flase floor is 100mm；Flase floor inclination angle is
30°；Grid board width is 100mm；Drop expects pipe height is 120mm；2 circles are arranged in horizontal direction on drop expects pipe tube wall to overflow
Discharge orifice, the total sectional area of overflow hole are drop expects pipe sectional area 30%；Overflow centerline hole is away from tower tray upper surface 50mm；Grid
Spatial altitude between lower surface and the drop most upper edge of expects pipe is 50mm.The tower tray is assembled by 9 pieces of small tower trays, every piece of trourelle
It is provided with 2 tooth weir formulas on disk subtracts and rushes equal flow table.Distributor is triangularly arranged on tower tray.Catalyst bed radial temperature
And the temperature difference is shown in Table 1.
Embodiment 2
It is same as Example 1, the difference is that eliminating the ERI type gas-liquid distribution of this field routine in former hydrogenator
Device only remains subtracting of being arranged in the present invention and rushes equal flow table, and bed radial temperature and the temperature difference are shown in Table 1.
Table 1 applies result
The embodiment of the present invention is given for the purpose of illustration and description, and is not exhaustively or by the present invention to limit
In disclosed form.Many modifications and variations are obvious for the ordinary skill in the art.Selection and
Description embodiment is and to enable those skilled in the art to more preferably illustrate the principle of the present invention and practical application
Understand the present invention to design various embodiments suitable for specific applications with various modifications.
Claims (22)
1. a kind of with subtracting the hydrogenator for rushing component, including material inlet pipe, inlet diffuser, reactor upper cover, subtract
Equal flow table, catalyst bed, catalyst support grid, reactor shell, reactor lower head, exit collector, material is rushed to go out
Agent pipe is managed and unloaded to mouth；It is characterized in that, described in subtract and rush equal flow table and be arranged in the idle space of reactor upper cover, Huo Zheshe
It is placed in reactor shell upper end；It is described to subtract that rush equal flow table include subtracting to rush tower tray and being arranged in and subtract several distribution rushed on tower tray
Device, the distributor include grid, drop expects pipe and connecting rod, and grid is set to above drop expects pipe, and grid and drop expects pipe pass through connecting rod
Connection.
2. hydrogenator described in accordance with the claim 1, which is characterized in that the hydrogenator further includes that bed unloads agent
Distribution plate between pipe, cold hydrogen tube, cold hydrogen disk, spraying disc and bed.
3. hydrogenator according to claim 2, which is characterized in that the hydrogenator further includes that top part is matched
Disk.
4. according to any hydrogenator of claim 1-3, which is characterized in that the lower surface of the grid and drop expects pipe
Most upper edge between there are space, the space constitutes the flow channel of gaseous phase materials.
5. hydrogenator according to claim 4, which is characterized in that the ragged edge for rushing tower tray that subtracts has along setting
The upward flanging in direction.
6. according to any hydrogenator of claim 1-3, which is characterized in that described subtracting rush tower tray be divided into it is several
The small tower tray of block, several pieces of small tower trays are assembled into a whole tower tray.
7. hydrogenator according to claim 4, which is characterized in that the grid includes several pieces of flase floors and grid
Plate connecting rod, several pieces of flase floors are linked together by flase floor connecting rod.
8. hydrogenator according to claim 7, which is characterized in that several pieces of flase floors are in the horizontal direction
Parallel arrangement, and be obliquely installed.
9. hydrogenator according to claim 8, which is characterized in that the inclined direction of the flase floor is towards reaction
Device outer direction.
10. according to hydrogenator described in claim 8 or 9, which is characterized in that the inclination angle of the flase floor be 10 °~
90°。
11. hydrogenator according to claim 7, which is characterized in that the width of the flase floor is 10~200mm,
Horizontal space between adjacent grid plate is 10~300mm.
12. according to any hydrogenator of claim 1-3, which is characterized in that several pieces of flase floors are in the horizontal direction
The grille-like that upper parallel arrangement is formed is rectangle, or is cut into circle.
13. according to any hydrogenator of claim 1-3, which is characterized in that several distributors are subtracting punching
Triangular in shape on tower tray, quadrangle, diamond shape or circular arrangement.
14. according to any hydrogenator of claim 1-3, which is characterized in that the distributor and subtract and rush tower tray
Between using weld, be bolted, screw connection or snap connection is fixedly connected.
15. hydrogenator according to claim 4, which is characterized in that overflow hole is opened up in the drop expects pipe, it is described to overflow
There are gaps between the center line and tower tray upper surface of discharge orifice.
16. hydrogenator according to claim 4, which is characterized in that the height in the space is 5 ~ 200mm.
17. hydrogenator according to claim 5, which is characterized in that the height of the flanging is 5 ~ 80mm.
18. hydrogenator according to claim 15, which is characterized in that the quantity of the overflow hole is 1~6.
19. hydrogenator according to claim 15, which is characterized in that the total sectional area of the overflow hole is drop expects pipe
The 10% ~ 100% of sectional area.
20. hydrogenator according to claim 15, which is characterized in that the shape of the overflow hole is triangle, four
Side shape or circle.
21. hydrogenator according to claim 15, which is characterized in that the center line of the overflow hole is away from table on tower tray
5 ~ 100mm of face.
22. hydrogenator described in accordance with the claim 3, which is characterized in that the top distribution plate, which is located to subtract to rush, to flow
Below disk, the top of topmost catalyst bed.
Applications Claiming Priority (2)
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|---|---|---|---|
| CN2017114707327 | 2017-12-29 | ||
| CN201711470732 | 2017-12-29 |
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| CN109985575A true CN109985575A (en) | 2019-07-09 |
| CN109985575B CN109985575B (en) | 2021-08-31 |
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| CN201811291429.5A Active CN109985575B (en) | 2017-12-29 | 2018-10-31 | Hydrogenation reactor with impact reduction assembly |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112745892A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Residual oil hydrotreating method |
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| CN109985575B (en) | 2021-08-31 |
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Effective date of registration: 20230928 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |