CN109985573A - A kind of hydrogenator improving even in liquid phase degree - Google Patents
A kind of hydrogenator improving even in liquid phase degree Download PDFInfo
- Publication number
- CN109985573A CN109985573A CN201711468770.9A CN201711468770A CN109985573A CN 109985573 A CN109985573 A CN 109985573A CN 201711468770 A CN201711468770 A CN 201711468770A CN 109985573 A CN109985573 A CN 109985573A
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- Prior art keywords
- hydrogenator
- downspout
- wing plate
- reactor
- tray
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- 239000007791 liquid phase Substances 0.000 title claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 61
- 239000000463 material Substances 0.000 claims abstract description 55
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 51
- 238000005507 spraying Methods 0.000 claims description 51
- 238000009826 distribution Methods 0.000 claims description 47
- 239000001257 hydrogen Substances 0.000 claims description 36
- 229910052739 hydrogen Inorganic materials 0.000 claims description 36
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 21
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 150000002431 hydrogen Chemical class 0.000 claims description 15
- 229910000831 Steel Inorganic materials 0.000 claims description 12
- 239000010959 steel Substances 0.000 claims description 12
- 229910003460 diamond Inorganic materials 0.000 claims description 6
- 239000010432 diamond Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 5
- 238000003466 welding Methods 0.000 claims description 5
- 238000005520 cutting process Methods 0.000 claims description 4
- 230000010354 integration Effects 0.000 claims description 4
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 18
- 238000000034 method Methods 0.000 abstract description 8
- 230000008569 process Effects 0.000 abstract description 4
- 238000004517 catalytic hydrocracking Methods 0.000 abstract description 2
- 239000010410 layer Substances 0.000 description 23
- 230000000694 effects Effects 0.000 description 17
- 239000012530 fluid Substances 0.000 description 14
- 239000011148 porous material Substances 0.000 description 9
- 238000010586 diagram Methods 0.000 description 8
- 239000007921 spray Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 239000007769 metal material Substances 0.000 description 3
- 238000005381 potential energy Methods 0.000 description 3
- 238000004080 punching Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000011229 interlayer Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000005315 distribution function Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000002271 resection Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- B01J8/0492—Feeding reactive fluids
-
- 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
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
-
- 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
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of hydrogenators for improving even in liquid phase degree.Hydrogenator of the invention includes that material inlet pipe, inlet diffuser, reactor upper cover, fold type subtract and rush equal flow table, catalyst bed, catalyst support grid, reactor shell, reactor lower head, exit collector, material outlet pipe and unload agent pipe.The fold type, which subtracts, rushes several funnel-shaped distributors that equal flow table includes tower tray He is vertically arranged on tower tray；The funnel-shaped distributor includes downspout and and the wing plate that is set at the top of downspout.Hydrogenator of the invention is suitable for the larger hydrofinishing or hydrocracking process of all hydrogenation processes, especially reactor.
Description
Technical field
The present invention relates to a kind of hydrogenators, belong to field of chemical equipment.Hydrogenator of the invention is suitable for institute
The hydrofinishing for having hydrogenation process, especially reactor larger or hydrocracking process.
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, hydrogen addition technology plays more and more important in petroleum refining industry
Effect.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, the feedstock oil after mixing hydrogen by a certain percentage completes the reaction such as purification and cracking by the effect of hydrogenation catalyst.Add hydrogen
Hydrogenation reaction in reactor can stable operation, can hydrogenation catalyst its function can be fully exerted, and whether product quality can
Enough reach high-quality, is heavily dependent on the uniformity that gas-liquid is distributed in catalyst bed.And gas-liquid is in catalyst bed
In distribution it is whether uniform, the design with hydrogenator inner member has close relationship.In other words, inner member performance is good
It is the bad operation cycle for directly influencing catalyst life, product quality and device, i.e., excellent using a set of performance in hydrogenation process
The good obtained effect of inner member technology is never second to use a kind of higher catalyst of activity instead.Therefore anti-to hydrogen is added both at home and abroad
The research and engineering development for answering device and its inner member are paid much attention to always, its reactor component is constantly updated, in the hope of obtaining more
Good 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.
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.
Spraying disc is arranged between cold hydrogen disk and reallocation disk (gas-liquid partition tray).Quenching hydrogen is squeezed into cold hydrogen box, is
Neutralize the reaction heat that hydrogenation reaction is released, control temperature of charge is no more than specified value, the hydrogen stream that cold hydrogen tube sprays with it is upper
The reactant that bed comes enters cold hydrogen box after tentatively mixing, and is uniformly mixed herein.Mixed uniformly fluid is after spraying disc
It is reinjected on the reallocation disk (gas-liquid partition tray) of lower layer, reallocation disk plays as top distribution dish structure to lower bed layer
The effect of sectional uniform distribution.
And since position height limits, in level of approximation streamline flow when the fluid through supercooling hydrogen disk mixing is flowed out from cold hydrogen disk
State, cause liquid phase occur it is serious push away unrestrained phenomenon, i.e. reactor radial direction liquid distribution is uneven, and center is even on distribution plate
There is no liquid phase.And spraying disc generally uses the i.e. flat tower sieve pore dish structure of the hydrojet tower tray of uniform pore openings, the cold mixed stream of hydrogen disk
When body passes through sieve pore, only it is able to achieve from horizontal fluidised form and is converted into vertical fluidised form, cannot achieve and flow, i.e., can not change on tower tray
Unrestrained phenomenon is pushed away, i.e., provides uniform entry condition when can not give to reallocation disk, is brought to the distributor for relying on tray level degree
Unfavorable entry condition, even if the distributor that performance is best also cannot achieve and evenly distribute under the conditions of the liquid layer of different depth
Material, seriously affects the effect of redistributor, and radial temperature difference expands inevitable.
Traditional spraying disc, that is, flat tower sieve pore dish structure there are aiming at the problem that, it is necessary to developing can mention for reallocation disk
For the injection dish structure of uniform liquid phase entry condition, the first distribution of material is realized, for eliminating the cold inclined fluidised form of hydrogen disk
Fluid pushes away unrestrained phenomenon to liquid layer on reallocation disk, realizes evenly distributing for fluid.
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 hydrogenators for improving even in liquid phase degree.
A kind of hydrogenator of raising even in liquid phase degree of the invention, including material inlet pipe, inlet diffuser, reaction
Device upper cover, fold type subtract rush equal flow table, catalyst bed, catalyst support grid, reactor shell, reactor lower head,
Exit collector, material outlet pipe and unload agent pipe composition；Wherein the fold type, which subtracts, rushes equal flow table setting and seals on reactor
In the idle space of the head or upper end of reactor shell；The fold type subtracts that rush equal flow table include tower tray and being vertically arranged at tower
Funnel-shaped distributor on disk, the funnel-shaped distributor include downspout and the wing plate for being set to downspout top.
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 and bed.Hydrogenator i.e. of the invention includes more than two hydrogenation catalyst beds.
In further preferred embodiment, hydrogenator of the invention further includes top distribution plate, the top
Distribution plate is located at fold type and subtracts the lower section for rushing equal flow table, and is located at the top of topmost catalyst bed.
In hydrogenator of the invention, fold type subtracts that rush equal flow table be the reactor septal fossula part newly established.Wherein, described
Downspout be both ends open (tubular) structure, the wing plate have certain angle, side length and height.The wing plate and drop
The axis of liquid pipe is parallel or the center line of the wing plate forms an angle with reactor axis.
Further, fold type subtracts the angle for rushing wing plate in equal flow table far from the center of tower tray or the center of circle or wing plate angle
The cylinder wall nearest in face of reactor.Further, the center line of the wing plate angle is overlapped with reactor shell ray.
Further, the wing plate is tilted towards apart from nearest wall of reactor, and the center line of the angle of wing plate with
Angle between reactor axis is 15 °~80.
Further, the wing plate has certain angle, side length and height.The quantity phase of the wing plate and downspout
Together, and wing plate and downspout are in arrangement up and down.The bottom of the wing plate is Chong Die with upper edge (top) of downspout or not along (lower part)
Overlapping connection；When overlapping connection, lap height is that the ratio of downspout height is 5%~30%, preferably 10%~25%.
Further, several funnel-shaped distributors should be vertically arranged on tower tray.It is dropped in funnel-shaped distributor
The lower ending opening of liquid pipe is directly opened on tower tray or through tray perforation.
Further, the tower tray further includes the supporting beam being used to support below and tower tray connector.
Further, several overflow holes are provided on the tube wall of the downspout, in order to which liquid enters across overflow hole
Downspout and along downspout flow down.Certain distance should be maintained between the center line and tray deck surface of the overflow hole.It overflows
The setting quantity of discharge orifice is generally 1~6, preferably 1~2.The total sectional area of overflow hole is downspout (level) sectional area
10%~100%, preferably 30%~50%.When the overflow hole opened up on downspout is only arranged 1, orientation is arranged in downspout
With the opposite of wing plate tie point；When the quantity that overflow hole is arranged is 2, downspout and wing plate tie point is arranged in orientation
Two sides.The shape of set overflow hole can be circle, strip, triangle and polygon, it is preferably circular.
The funnel-shaped distributor can be made of any suitable material, such as ceramics, metal material, preferably be adopted
Use steel material.The wing plate and downspout can be made for integration, can such as be added by downspout and wing plate integration
Work is made；Alternatively, doing vertical (vertical) and horizontal resection at the top certain altitude of the downspout with certain altitude, retain
Then the incomplete cutting of wall thickness spreads out certain angle and wing plate is made, or is fixedly connected with one on the upper edge of downspout
Wing plate with certain angle.It is described be fixedly connected can using weld, be bolted, screw connection, buckle link
Etc. various suitable modes.
In the present invention, the fold type, which subtracts, to be rushed the tower tray of equal flow table and is conventionally divided into several pieces, and sliceable is circular slab.
Flanging is set at the edge of tower tray most outer, flanging flips up.It should be above descending liquid tube wall along general on the flanging
The lower edge of set overflow hole.The flanging set up can maintain certain liquid level on tower tray, so as to one
The horizontal Shortcomings for determining to eliminate tower tray in the prior art in degree are influenced to liquid phase distribution bring.
In the present invention, fold type subtracts several funnel-shaped distributors rushed on equal flow table usually according to certain regular arrangement, such as
It can triangular in shape on tower tray, quadrangle, diamond shape arrangement.
In the present invention, the downspout in addition to for liquid by outer, while being also that the circulation of gas feed in charging is led to
Road.
Further, hydrogenator of the invention includes more than two catalyst beds, therefore the reactor is also
Distribution plate between agent pipe, cold hydrogen tube, cold hydrogen disk, spraying disc and bed is unloaded including bed.The spraying disc preferably uses fold type
Spraying disc, the structure of fold type spraying disc subtracts with mentioned-above fold type rushes equal flow table.The fold type spraying disc setting exists
Between the cold hydrogen disk and bed of hydrogenator between distribution plate.The fold type spraying disc, including jet tray and set vertically
The funnel-shaped distributor being placed on jet tray；The funnel-shaped distributor includes downspout and is set to downspout top
Wing plate.
Further, the downspout of fold type spraying disc is the tubular structure of open at both ends.Upper edge and the drop of the wing plate
Along edge on downspout is flushed with or slightly higher than in liquid pipe, the wing plate has certain angle, side length and height, and the lower edge of wing plate is pasted
It is attached to tray deck upper surface, or there are the gaps of certain altitude with tray deck upper surface.
Further, the wing plate angle of the fold type spraying disc is far from the center of tower tray or the center of circle.Further, institute
The center line for stating wing plate angle is overlapped with reactor shell ray, the wing plate angle cylinder wall nearest in face of reactor.This hair
In bright, the wing plate is parallel with the axis of downspout.The wing plate is to have certain angle, the flanging of side length and height
Plate.Wing plate is identical with the quantity of downspout, and is one-to-one relationship.The middle and lower part of the wing plate and the middle and upper part of downspout can
With the setting that partly overlaps；When overlapping, the ratio that lap height accounts for downspout total height is 50%~90%, preferably
60%~80%.
In the fold type spraying disc, several funnel-shaped distributors are vertically arranged on jet tray.Funnel-shaped distribution
Device usually passes through downspout lower end and is plugged on jet tray, and can by welding, the modes such as be threadedly coupled, snap connection and carry out
It is fixedly connected.The lower ending opening of downspout is directly opened on jet tray or is open through jet tray.The spray tower
Disk further includes the supporting beam being used to support below and tower tray connector.
Further, several overflow holes are provided on the tube wall of downspout described in fold type spraying disc, in order to liquid
Enter downspout across overflow hole and along downspout flow down.It should be maintained between the center line and tray deck surface of overflow hole
Certain distance.The quantity of overflow hole is generally 1~6, preferably 1~2.The total sectional area of overflow hole cuts for downspout (level)
The 10%~100% of area, preferably 30%~50%.When the overflow hole opened up on downspout is only arranged 1, orientation setting exists
The opposite of downspout and wing plate tie point；When the quantity that overflow hole is arranged is 2, the wing plate axis of symmetry is arranged in orientation
Two sides.The shape of set overflow hole can be circle, strip, triangle and polygon, it is preferably circular.
In the fold type spraying disc, funnel-shaped distributor can be used any suitable material and be made, such as ceramics, metal
Material etc., it is preferred to use steel material.The wing plate and downspout can be integrated chemical conversion type and be made；Alternatively, wing plate and
Downspout is assembled to be formed, and such as can be fixedly connected with a wing plate with certain angle in downspout middle and upper part.Described consolidates
Fixed connection can using weld, be bolted, screw connection, snap connection etc. it is various it is suitable by the way of.It is described when concrete application
Downspout can be made of steel pipe, the wing plate preferably uses steel plate to fold.
In the present invention, the jet tray is conventionally divided into several pieces, and sliceable is circular slab.Jet tray most
The flanging flipped up is arranged in the edge of outer.The upper edge of the flanging should be above set overflow hole on descending liquid tube wall
Upper edge.The setting of flanging can maintain certain liquid level on jet tray, existing so as to eliminate to a certain extent
There are the horizontal Shortcomings of jet tray in technology to influence to liquid phase distribution bring.
In the fold type spraying disc, several funnel-shaped distributors can such as spray usually according to certain regular arrangement
Penetrate triangular in shape, quadrangle on tower tray, diamond shape arrangement.
Compared with prior art, hydrogenator of the present invention has the advantages that
1, the equal flow table of fold type described in hydrogenator of the present invention is designed by special structure, is reduced distributor and is installed ruler
It is very little, it is easily installed at idle reactor upper cover, or be arranged in the upper surface of reactor shell upper end, top distribution plate, reaches
To the purpose for saving space reactor, the space utilization rate of hydrogenator is improved, convenient for loading more catalyst, or is subtracted
Small reactor scale.
2, hydrogenator of the invention, the fold type, which subtracts, rushes equal flow table and fold type spraying disc is provided with the wing
Plate can stop to cause to cut down its impact force in the fluid of oblique line fluidised form injection because center enters；Lose the stream of kinetic energy
Body be blocked after under the effect of gravity, converted by original parallax fluidised form for vertical current state, and realize that nature falls, in tower
The consistent liquid layer of depth is formed on disk, eliminates " pushing away wave " phenomenon that parallax impact force is formed to liquid layer on tower tray, and give cigarette
Chimney formula distributor creates uniform entry condition, and material is distributed to catalyst bed or top part by funnel-shaped distributor
With just distribution function on disk, is realized, friendly, steady liquid layer, uniform entry condition are provided to catalyst bed or distributor.I.e.
Fold type of the present invention, which subtracts, to be rushed equal flow table and improves the entrance condition of the first bed distribution plate, and the distribution effect of top distribution plate is improved
Fruit, the material distribution of optimization top bed, improves the utilization rate of the first bed catalyst.Fold type spraying disc of the present invention improves
Material distribution situation among bed, improves the distributed effect of distribution plate between bed.
3, hydrogenator of the invention, the fold type, which subtracts, rushes equal flow table and fold type spraying disc, passes through setting
Wing plate and funnel-shaped distributor realize liquid phase distribution, compared to the bubble cap distributor of more general suction principle, point of liquid phase distribution
Power is dissipated to be changed to splash be formed, to reduce pressure drop using potential energy by gas phase suction.
4, hydrogenator of the invention, the fold type, which subtracts, rushes equal flow table and fold type spraying disc, setting chimney point
Orchestration tube wall overflow hole site and shape form reasonable tower tray liquid storage depth, reduce tray level degree deviation and liquid level wave
Dynamic bring macro-allocation is uneven.
5, hydrogenator of the invention, the fold type, which subtracts, rushes equal flow table and fold type spraying disc, and use is unique
Design principle and hydrodynamics feature, realize evenly distributing for material, make the reduction of catalyst bed radial temperature difference, catalyst bed
Radial temperature difference≤3 DEG C, since radial temperature difference reflects the distributed effect of fluid, it is equal that this has absolutely proved that fold type of the present invention subtracts punching
Flow table is preferable to the distribution of reaction feed logistics and gas-liquid mixed effect, controls hydrogenation catalyst reaction process and catalyst coking
With certain booster action.
6, compared with prior art, hydrogenator of the invention, the equal flow table of fold type and fold type spraying disc are new
The hydrogenator inner member added has structure simple, and easy for installation, operating flexibility is big, and hydrogenator sky can be improved
Between utilization rate, improve material distribution situation in reactor, effectively eliminate reactor radial temperature difference, eliminate catalyst bed because of material
It is unevenly distributed caused heat spot, effective use for catalyst in hydrogenator provides excellent entry condition, reduces
Catalyst skimming changes agent number, extends the on-stream time of device, improves hydrogenation technique effect, with good economic efficiency.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram for the hydrogenator for improving even in liquid phase degree of the present invention.
Fig. 2 is that fold type subtracts the schematic diagram for rushing equal flow table in the present invention.
Fig. 3 is that fold type of the present invention subtracts the structural schematic diagram for rushing funnel-shaped distributor 4-1 in equal flow table.
Fig. 4 is that fold type of the present invention subtracts the structure top view for rushing funnel-shaped distributor 4-1 in equal flow table.
Fig. 5 is that the liquid that fold type of the present invention subtracts when rushing the work of equal flow table flows to schematic diagram.
Fig. 6 is the distributor schematic diagram of fold type spraying disc of the present invention.
Fig. 7 is the distributor schematic diagram of funnel-shaped distributor 10-1 in fold type spraying disc of the present invention.
Fig. 8 is the dispensing arrangement top view of funnel-shaped distributor 10-1 in fold type spraying disc of the present invention.
Liquid flows to schematic diagram when Fig. 9 is fold type spraying disc of the present invention work.
Figure 10 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, the invention discloses a kind of hydrogenators, including material inlet pipe 1, inlet diffuser
2, reactor upper cover 3, fold type, which subtract, rushes equal flow table 4, catalyst bed 5,6 reactor shell 12 of catalyst support grid, anti-
It answers device lower head 13, exit collector 14, material outlet pipe 15 and unloads agent pipe 16.In some embodiments, hydrogenator
It further include that bed unloads distribution plate 11 between agent pipe 7, cold hydrogen tube 8, cold hydrogen disk 9, fold type spraying disc 10, bed.Further preferred
Embodiment in, hydrogenator further includes top distribution plate 17, and top distribution plate 17, which is located at fold type and subtracts, to be rushed under equal flow table 4
Side, the top of top layer's catalyst bed.
The fold type, which subtracts, rushes several funnel-shaped distributor 4- that equal flow table includes tower tray 4-2 He is vertically arranged on tower tray
1.Funnel-shaped distributor 4-1 includes downspout 4-1-2 and and the wing plate 4-1-1 that is set at the top of downspout 4-1-2.Downspout 4-
1-2 is both ends open structure.Wing plate 4-1-1 and downspout 4-1-2 is in arrangement up and down.Wing plate 4-1-1 has certain angle, side length
And height, generally folded by steel plate.Wing plate 4-1-1 is parallel with the axis of downspout 4-1-2.
Wherein, wing plate 4-1-1 is identical as downspout 4-1-2 quantity and corresponds.The angle of wing plate 4-1-1 is generally
15 °~180 °, preferably 90 °~120 °；The side length of wing plate 4-1-1 is generally 20mm~200mm, preferably 60mm~120mm；
The height of wing plate 4-1-1 is generally 30mm~200mm, preferably 60mm~120mm.Bottom edge and the downspout 4- of wing plate 4-1-1
1-2 is upper along connection, and can also partly overlap arrangement with downspout 4-1-2.When the bottom wing plate 4-1-1 along with downspout 4-1-2 on along weigh
When laying up is set, lap height can be the 10%~100% of downspout 4-1-2 height, preferably 5%~20%.Wing plate 4-1-1 folder
Angle center line is overlapped with 12 ray of reactor shell, the angle cylinder wall nearest in face of reactor.
In hydrogenator of the present invention, downspout 4-1-2 is generally made of metal tube.The height of downspout 4-1-2 is general
20~300mm, preferably 50~120mm.1~6 overflow hole 4-1-3 is set in the horizontal direction on downspout 4-1-2, preferably 1
~2；The total sectional area of its overflow hole is the 10%~100% of downspout sectional area, preferably 30%~50%.When being opened on downspout
If overflow hole be arranged 1 when, the opposite of downspout 4-1-2 Yu wing plate 4-1-1 tie point is arranged in orientation；When setting overflow
When the quantity of hole 4-1-3 is 2, the two sides of downspout 4-1-2 Yu wing plate 4-1-1 tie point are arranged in orientation.Overflow hole
Shape can be circle, strip, triangle and polygon, it is preferably circular.Overflow centerline hole away from tower tray upper surface 5~
100mm, preferably 30~50mm.
In hydrogenator of the present invention, one layer of fold type subtracts that rush equal flow table include a number of funnel-shaped distributor 4-1.
Several funnel-shaped distributor 4-1 are triangular in shape on tower tray, quadrangle, diamond shape arrangement.Funnel-shaped distributor 4-1 usually passes through drop
The lower end liquid pipe 4-1-2 is plugged on tower tray, and can by welding, the modes such as be threadedly coupled, snap connection and be fixedly connected.
In hydrogenator of the present invention, tower tray 4-2 is conventionally divided into several pieces, and sliceable is circular slab.Tower tray 4-2 is most
The flanging flipped up is arranged in the edge of outer, and flanging height is generally 5~80mm, preferably 30~50mm.
As shown in Fig. 1, Fig. 6, Fig. 7 and Fig. 8, a kind of hydrogenator of the invention, including material inlet pipe 1, entrance expand
Scattered device 2, reactor upper cover 3, fold type, which subtract, rushes equal flow table 4, top distribution plate 17, catalyst bed 5, catalyst support grid
6, bed unloads distribution plate 11 between agent pipe 7, cold hydrogen tube 8, cold hydrogen disk 9, fold type spraying disc 10, bed, reactor shell 12, reaction
Device lower head 13, exit collector 14, material outlet pipe 15 and unload agent pipe 16.Wherein, the setting of fold type spraying disc 10 is adding hydrogen
Between the cold hydrogen disk 9 of reactor and bed between distribution plate 11.Fold type spraying disc 10 includes tray deck 10-2 and is vertically arranged at tower
Funnel-shaped distributor 10-1 in plate；The funnel-shaped distributor 10-1 includes downspout 10-1-2 and is set to downspout
The wing plate 10-1-1 on top.
Wherein, the downspout 10-1-2 is open at both ends (tubular) structure, upper edge and the downspout 10- of wing plate 10-1-1
The upper edge 1-2 flushes with or slightly higher than edge on downspout 10-1-2.The wing plate 10-1-1 has certain angle, side length and height,
The lower edge of wing plate 10-1-1 is attached to the upper surface tray deck 10-2, or there are the seams of certain altitude with the upper surface tray deck 10-2
Gap.Center or the center of circle of the angle of wing plate 10-1-1 far from tower tray 10-2.Further, in the wing plate 10-1-1 angle
Heart line is overlapped with 12 ray of reactor shell, the wing plate 10-1-1 angle cylinder wall nearest in face of reactor.The wing plate
10-1-1 is parallel with the axis of downspout 10-1-2.The wing plate 10-1-1 has certain angle, side length and height.Wing plate
10-1-1 has certain angle, the flanged plate of side length and height.The quantity of the wing plate 10-1-1 and downspout 10-1-2
It is identical, and be one-to-one relationship.The middle and lower part of the wing plate 10-1-1 and the middle and upper part of downspout 10-1-2 can partially weigh
Folded connection；Overlapping connection when, stack height account for downspout 10-1-2 total height ratio be 50%~90%, preferably 60%~
80%。
Several funnel-shaped distributor 10-1 should be vertically arranged on tray deck 10-2.Funnel-shaped distributor 10-1
Usually be plugged on tray deck 10-2 by the lower end downspout 10-1-2, and can by welding, be threadedly coupled, snap connection
Mode is fixedly connected.The lower ending opening of the downspout 10-1-2 is directly opened on tray deck 10-2 or through tray deck
10-2 opening.The tower tray further includes the supporting beam 10-4 being used to support below and tower tray connector 10-3.
Several overflow hole 10-1-3 are provided on the tube wall of the downspout, in order to liquid pass through overflow hole 10-1-3 into
Enter downspout 10-1-2 and along downspout 10-1-2 flow down.The center line of overflow hole 10-1-3 and the surface tray deck 10-2
Between should maintain certain distance.The setting quantity of overflow hole 10-1-3 is generally 1~6, preferably 1~2.Overflow hole 10-
The total sectional area of 1-3 is that downspout 10-1-2(is horizontal) sectional area 10%~100%, preferably 30%~50%.As downspout 10-
When the overflow hole 10-1-3 opened up on 1-2 is only arranged 1, orientation is arranged in downspout 10-1-2 and wing plate 10-1-1 tie point
Opposite；When the quantity that overflow hole 10-1-3 is arranged is 2, the two sides of the wing plate 10-1-1 axis of symmetry are arranged in orientation.
The shape of set overflow hole 10-1-3 can be circle, strip, triangle and polygon, it is preferably circular.
The funnel-shaped distributor 10-1 can be made of any suitable material, such as ceramics, metal material, excellent
Choosing uses steel material.The wing plate 10-1-1 and downspout 10-1-2 can be integrated chemical conversion type and be made；Alternatively, wing plate
10-1-1 and downspout 10-1-2 is assembled forms, such as can be fixedly connected with one in the middle and upper part downspout 10-1-2 has certain angle
Wing plate 10-1-1.It is described be fixedly connected can using weld, be bolted, screw connection, snap connection etc. it is various
Suitable mode.When concrete application, the downspout 10-1-2 can be made of steel pipe, and the wing plate 10-1-1 is preferably adopted
It is folded with steel plate.
The tower tray 10-2 of the fold type spraying disc is conventionally divided into several pieces, and sliceable is circular slab.In tower tray
Flanging 10-5 is arranged in the edge of the most outer 10-2, and flanging 10-5 is flipped up.It should be above descending liquid along general on flanging 10-5
The upper edge of set overflow hole 10-1-3 on pipe 10-1-2.The setting of flanging 10-5 can maintain certain liquid on tower tray 10-2
Face height distributes bring shadow to liquid phase so as to eliminate the horizontal Shortcomings of tower tray in the prior art to a certain extent
It rings.
In the fold type spraying disc, several funnel-shaped distributor 10-1, such as can be with usually according to certain regular arrangement
Triangular in shape, quadrangle, diamond shape arrangement on tray deck 10-2.
In conjunction with Fig. 5, further illustrate that fold type subtracts the course of work for rushing equal flow table in hydrogenator of the present invention: the folding
Side formula subtracts when rushing the work of equal flow table, and material is entered in reactor by the inlet diffuser of reactor, and because pump conveys, fluid has
Remaining kinetic energy, thus material has powerful impact force.Since material autoreactor center is fed, although existing reaction
Device is respectively provided with inlet diffuser, but material is still in that oblique line fluidised form is sprayed around.It is provided when the present invention is arranged in reactor
Fold type subtract and rush equal flow table after, fluid strikes the wing plate 4-1-1 of funnel-shaped distributor 4-1 first, and wing plate 4-1-1 can be effective
Stop to cut out its impact force in the fluid mechanics of oblique line fluidised form injection, by the way that wing plate 4-1-1 is arranged by the stream of material
State is changed, fluid is blocked, lose kinetic energy after under gravity, from oblique line fluidised form become vertical fluidised form fall to
On tower tray 4-2.Since downspout 4-1-2 is provided with overflow hole 4-1-3, i.e., material channel is in horizontally disposed, and overflow hole 4-1-3
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 funnel-shaped distributor 4-1 with the presence of liquid phase.Due to funnel-shaped distributor
4-1 quantity is more, it is ensured that any one point of catalyst in reactor bed face has a certain number of funnel-shaped distributors
4-1 work, so that the funnel-shaped distributor 4-1 uniformity is protected.The overflow hole that fluid is opened up from downspout 4-1-2 tube wall
In 4-1-3 inflow reactor on top distribution plate, the preliminary distribution of material is realized.Due to after fold type subtracts swash of wave disk
Material has been converted into vertical fluidised form when being assigned on the distribution plate of top, and kinetic energy disappears, therefore to top distribution plate tower tray
There is no thrusts for liquid layer on surface, eliminate material and act on " the pushing away wave " of liquid layer on distribution plate, provide to top distribution plate
Friendly, steady, uniform entry condition, realized together with the distribution plate of top material on catalyst bed uniformly point
Cloth.
In conjunction with Fig. 9, the course of work of fold type spraying disc in hydrogenator of the present invention is further illustrated: when work, warp
The fluid of mixed, in level of approximation streamline the inclination fluidised form of hydrogen disk 9 is subcooled, strikes on wing plate 10-1-1, because of wing plate 10-
1-1 is arranged with certain angle, can effectively stop the fluid in the injection of oblique line fluidised form, its impact force is cut down；It utilizes
Wing plate 10-1-1 barrier effect, forces Vapor Entrainment drop to disperse around, realizes that the larger angle of flare of material, fluid wait for that kinetic energy consumes
It is dripped naturally under the effect of gravity after to the greatest extent, forms vertical downward flow state, liquid phase potential energy is the kinetic energy of freely falling body, and falls
Onto the tray deck 10-2 of spraying disc, since the material channel of downspout 10-1-2 setting is in horizontally disposed and apart from tray deck
10-2 has certain altitude poor, thus material can form the liquid layer of certain depth on the tray deck 10-2 of spraying disc, even if tower
There are deviations for disk 10-2 levelness, still can ensure that each downspout 10-1-2 with the presence of liquid phase.Due to being sprayed by fold type
Material after disk has been converted into vertical fluidised form when being assigned on spraying disc 10-2, and kinetic energy disappears, therefore to spraying disc tower tray
There is no thrusts for liquid layer on the surface plate 10-2, eliminate material to " pushing away wave " phenomenon of liquid layer on distribution plate, give redistributor
Friendly, steady liquid layer, uniform entry condition are provided, it is equal on catalyst bed that material is realized together with reallocation disk
Even distribution.
Fold type spraying disc of the invention may replace reallocation disk, and realization subtracts punching, flows and distribute integration, significantly simple
Change inside reactor structure, reduce investment.
Fold type of the present invention is subtracted below by way of specific embodiment and rushes the effect of equal flow table and fold type spraying disc and retouches
It states.
Comparative example 1
Certain hydrogenator, diameter 4.6m leave unused in upper cover, and top layer's catalyst bed inlet is provided with top distribution plate,
Push up the ERI type bubble cap formula gas-liquid allotter in distribution plate using this field routine, the process conditions of the reactor are as follows: hydrogen partial pressure
2.0MPa, volume space velocity 2.0h-1, hydrogen to oil volume ratio 300:1,280 DEG C of reactor inlet temperature, the reactor include three urge
Agent bed.Its first, second catalyst bed interlayer uses the spray of existing uniform pore openings between cold hydrogen box and reallocation disk
Liquid tower tray, i.e., flat tower sieve pore dish structure；Equally also adopted between cold hydrogen box and reallocation disk in second, third catalyst bed interlayer
With flat tower sieve pore dish structure, tower tray opens up the uniform circular hole that diameter is 3mm, and tower tray percent opening is 8%.Hydrogenating materials are wax oil (sulphur
Content 2.0wt%), catalyst be 3936 hydrotreating catalysts, process conditions are as follows: hydrogen partial pressure 9.0MPa(G), volume space velocity be
1.5h-1, hydrogen to oil volume ratio 700:1,260 DEG C of reactor inlet temperature.Before transformation, the second bed, third bed inlet are radial
Temperature and the temperature difference are shown in Table 1.
Embodiment 1
Compared with embodiment 1, is subtracted in the upper cover of hydrogenator with fold type of the invention and rush equal flow table instead of bubble cap
Formula gas-liquid allotter, with fold type spraying disc of the invention instead of flat tower screen tray pore structure.Fold type subtracts the master for rushing equal flow table
Want parameter are as follows: wing plate angle is 120 °；Wing plate side length is 120mm；Wing plate height is 60mm.Its wing plate and chimney distributor axis
In parallel.Its wing plate bottom is overlapped along with edge on chimney distributor, and coincidence point is distributor height 20%.Chimney distributor height is
120mm；On chimney distributor tube wall, 2 overflow ports are set in horizontal direction.The total sectional area of overflow hole is chimney distributor
The 30% of tube section product；The overflow hole opened up on chimney distributor tube wall, shape are circle；It is arranged on chimney distributor tube wall
Overflow centerline hole away from tower tray upper surface 50mm；Fold type of the invention, which subtracts, to be rushed in equal flow table, and funnel-shaped distributor is in tower tray
On be triangularly arranged.The tower tray is divided into 9 pieces, and sliceable is circular slab, and setting 3 is funnel-shaped on every piece of cutting plate
Flanging is arranged in distributor, the edge of tower tray most outer, and the height of flanging is 50mm.
The major parameter of fold type spraying disc: wing plate is identical with the quantity of downspout, and wing plate is folded by steel plate, wing plate
Angle is 90 °, and wing plate side length is 60mm.Wing plate height is equal to downspout height, the angle center line and reactor cylinder of wing plate 1-1
Body ray is overlapped, and angle is in face of wall of reactor apart from nearest cylinder wall.The height of downspout is 60mm.Downspout pipe
2 round overflow holes are set on wall, and are arranged in horizontal direction.The overflow hole being arranged on descending liquid tube wall, total sectional area
It is the 30% of downspout sectional area.The center line of set overflow hole is 20mm away from tray surface on downspout.Flanging of the invention
In formula spraying disc, tower tray is divided into 9 pieces of small tower trays, and sliceable is circular slab, and funnel-shaped distributor is in fold type spray tower
It is triangularly arranged on disk, 3 funnel-shaped distributors is set on every piece small tower tray.The tower tray edge setting of most outer flips up
Flanging, the height of flanging is 50mm.
After transformation, the first catalyst bed entrance, the second catalyst bed, third catalyst bed entrance radial temperature point
Cloth and the temperature difference are shown in Table 1.
Embodiment 2
Compared with embodiment 1, folding of the invention is arranged in the top of bubble cap formula gas-liquid allotter in the upper cover of hydrogenator
Side formula, which subtracts, rushes equal flow table, with fold type spraying disc of the invention instead of flat tower screen tray pore structure.Fold type, which subtracts, rushes equal flow table
Major parameter are as follows: wing plate angle is 120 °；Wing plate side length is 120mm；Wing plate height is 60mm.Its wing plate and chimney distributor axis
Line is parallel.Its wing plate bottom is overlapped along with edge on chimney distributor, and coincidence point is distributor height 20%.Chimney distributor height is
120mm；On chimney distributor tube wall, 2 overflow ports are set in horizontal direction.The total sectional area of overflow hole is chimney distributor
The 30% of tube section product；The overflow hole opened up on chimney distributor tube wall, shape are circle；It is arranged on chimney distributor tube wall
Overflow centerline hole away from tower tray upper surface 50mm；Fold type of the invention, which subtracts, to be rushed in equal flow table, and funnel-shaped distributor is in tower tray
On be triangularly arranged.The tower tray is divided into 9 pieces, and sliceable is circular slab, and setting 3 is funnel-shaped on every piece of cutting plate
Flanging is arranged in distributor, the edge of tower tray most outer, and the height of flanging is 50mm.
The major parameter of fold type spraying disc: wing plate is identical with the quantity of downspout, and wing plate is folded by steel plate, wing plate
Angle is 90 °, and wing plate side length is 60mm.Wing plate height is equal to downspout height, the angle center line and reactor cylinder of wing plate 1-1
Body ray is overlapped, and angle is in face of wall of reactor apart from nearest cylinder wall.The height of downspout is 60mm.Downspout pipe
2 round overflow holes are set on wall, and are arranged in horizontal direction.The overflow hole being arranged on descending liquid tube wall, total sectional area
It is the 30% of downspout sectional area.The center line of set overflow hole is 20mm away from tray surface on downspout.Flanging of the invention
In formula spraying disc, tower tray is divided into 9 pieces of small tower trays, and sliceable is circular slab, and funnel-shaped distributor is in fold type spray tower
It is triangularly arranged on disk, 3 funnel-shaped distributors is set on every piece small tower tray.The tower tray edge setting of most outer flips up
Flanging, the height of flanging is 50mm.
After transformation, the first catalyst bed entrance, the second catalyst bed, third catalyst bed entrance radial temperature point
Cloth and the temperature difference are shown in Table 1.
Table 1 applies result
| Comparative example 1 | Embodiment 1 | Embodiment 2 | |
| First catalyst bed entrance | |||
| Radial temperature a | 266.6 | 265.2 | 265.1 |
| Radial temperature difference b | 265.5 | 264.5 | 265.5 |
| Radial temperature c | 270.3 | 264.9 | 265.9 |
| Radial temperature d | 276.0 | 265.0 | 265.0 |
| Radial temperature difference e | 278.4 | 265.8 | 265.8 |
| Maximum bed radial temperature difference | 12.9 | 1.3 | 0.9 |
| Second catalyst bed entrance | |||
| Radial temperature a | 276.6 | 275.2 | 275.1 |
| Radial temperature difference b | 279.5 | 274.5 | 274.5 |
| Radial temperature c | 280.3 | 274.9 | 274.8 |
| Radial temperature d | 286.0 | 275.0 | 275.2 |
| Radial temperature difference e | 288.4 | 275.8 | 275.6 |
| Maximum bed radial temperature difference, DEG C | 11.8 | 1.3 | 1.1 |
| Third catalyst bed entrance | |||
| Radial temperature a | 281.3 | 282.9 | 282.9 |
| Radial temperature difference b | 283.6 | 283.5 | 283.4 |
| Radial temperature c | 292.5 | 284.5 | 284.3 |
| Radial temperature d | 286.7 | 284.3 | 284.5 |
| Radial temperature difference e | 289.6 | 283.7 | 283.9 |
| Maximum bed radial temperature difference, DEG C | 11.2 | 1.6 | 1.4 |
Claims (44)
1. it is a kind of improve even in liquid phase degree hydrogenator, including material inlet pipe, inlet diffuser, reactor upper cover,
Fold type, which subtracts, rushes equal flow table, catalyst bed, catalyst support grid, reactor shell, reactor lower head, outlet collection
Device, material outlet pipe and unload agent pipe；It is characterized in that, the fold type subtracts, to rush the setting of equal flow table idle in reactor upper cover
Space in or reactor shell top；The fold type subtracts that rush equal flow table include tower tray and being vertically arranged on tower tray
Funnel-shaped distributor, the funnel-shaped distributor includes downspout and the wing plate for being set to downspout top, the wing plate
With downspout in arrangement up and down.
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, the top distribution plate are located at fold type and subtract the lower section for rushing equal flow table.
4. according to any hydrogenator of claim 1-3, which is characterized in that the downspout is both ends open cylinder
Shape structure, the wing plate have certain angle, side length and height.
5. according to any hydrogenator of claim 4, which is characterized in that the axis of the wing plate and downspout is flat
The center line of the capable or described wing plate forms an angle with reactor axis.
6. hydrogenator according to claim 5, which is characterized in that fold type subtract rush wing plate in equal flow table angle it is remote
Center or the center of circle from tower tray.
7. hydrogenator according to claim 6, which is characterized in that the center line and reactor cylinder of the wing plate angle
Body ray is overlapped, and the cylinder wall that wing plate angle is nearest in face of reactor.
8. hydrogenator according to claim 4, which is characterized in that the wing plate is identical with the quantity of downspout, and
It corresponds.
9. according to any hydrogenator of claim 1-3, which is characterized in that bottom edge and the downspout of the wing plate
Upper edge overlapping or not connection.
10. hydrogenator according to claim 9, which is characterized in that the bottom of the wing plate is along the upper edge with downspout
When overlapping connection, lap height is that the ratio of downspout height is 5%~30%.
11. hydrogenator according to claim 6, which is characterized in that the wing plate is towards apart from nearest reactor
Wall inclination, and the angle between the center line and reactor axis of wing plate angle is 15 °~80 °.
12. hydrogenator according to claim 4, which is characterized in that the lower ending opening of the downspout directly open in
On tower tray or through tray perforation.
13. hydrogenator according to claim 4, which is characterized in that the tower tray further includes below for branch
The supporting beam and tower tray connector of support.
14. hydrogenator according to claim 4, which is characterized in that be provided on the tube wall of the downspout several
Overflow hole keeps certain distance between the center line and tray deck surface of overflow hole.
15. hydrogenator according to claim 14, which is characterized in that the total sectional area of the overflow hole is downspout
The 10%~100% of sectional area.
16. hydrogenator according to claim 13, which is characterized in that the setting quantity of the overflow hole is 1~6
It is a.
17. hydrogenator according to claim 16, which is characterized in that when the overflow hole is only arranged 1, set
It sets on the opposite of downspout and wing plate tie point.
18. hydrogenator according to claim 16, which is characterized in that when the quantity of the discharge orifice is 2, orientation
It is arranged in the two sides of downspout and wing plate tie point.
19. hydrogenator according to claim 16, which is characterized in that the shape of the overflow hole is round, strip
Shape, triangle or polygon.
20. hydrogenator according to claim 4, which is characterized in that the wing plate and downspout is integration system
It forms；It is vertically and horizontally cut alternatively, being done on the top of the downspout with certain altitude, retains not exclusively cutting for wall thickness
It cuts, then spreads out certain angle and wing plate is made；Or one is fixedly connected with certain angle on the upper edge of downspout
Wing plate.
21. hydrogenator according to claim 20, which is characterized in that described is fixedly connected using welding, bolt
Connection, screw connection at least one of snap connection mode.
22. hydrogenator according to claim 16, which is characterized in that the edge setting of the tower tray most outer is upward
The flanging of fold, the upper edge of the flanging is when the lower edge for being higher than overflow hole set by descending liquid tube wall.
23. according to any hydrogenator of claim 1-3, which is characterized in that several funnel-shaped distributors are in tower tray
Upper triangular in shape, quadrangle or diamond shape arrangement.
24. according to hydrogenator described in claim 2 or 3, which is characterized in that the spraying disc is sprayed using fold type
Disk, the fold type spraying disc are arranged between the cold hydrogen disk of hydrogenator and bed between distribution plate；Fold type spraying disc packet
The funnel-shaped distributor for including jet tray and being vertically arranged on jet tray；The funnel-shaped distributor include downspout and
It is set to the wing plate on downspout top.
25. according to the hydrogenator described in claim 24, which is characterized in that the downspout is open at both ends tubular knot
Structure, the upper edge of the wing plate flush with or slightly higher than edge on downspout with edge on downspout.
26. according to the hydrogenator described in claim 25, which is characterized in that the axis of the wing plate and downspout is flat
Row.
27. according to the fold type spraying disc described in claim 25, which is characterized in that the angle of the wing plate is far from tower tray
The heart or the center of circle.
28. according to the hydrogenator described in claim 26, which is characterized in that the center line of the angle of the wing plate with react
Device cylinder ray is overlapped, the wing plate angle cylinder wall nearest in face of reactor.
29. according to the hydrogenator described in claim 25, which is characterized in that the middle and lower part of the wing plate and downspout it is upper
It is fixedly connected along overlapping, when overlapping connects, the ratio that lap height accounts for downspout total height is 50%~90%.
30. according to the hydrogenator described in claim 24, which is characterized in that the lower ending opening of the downspout is directly open
In on jet tray or through tray perforation.
31. according to the hydrogenator described in claim 25, which is characterized in that several overflow is arranged on the tube wall of the downspout
Discharge orifice keeps certain distance between the center line and tray deck surface of overflow hole.
32. according to the hydrogenator described in claim 31, which is characterized in that the total sectional area of the overflow hole is downspout
The 10%~100% of sectional area.
33. according to the hydrogenator described in claim 31, which is characterized in that the setting quantity of the overflow hole is 1~6
It is a.
34. according to the hydrogenator described in claim 33, which is characterized in that the overflow hole is only arranged 1, orientation
The opposite of downspout Yu wing plate tie point is set.
35. according to the hydrogenator described in claim 33, which is characterized in that the quantity of the overflow hole is 2, orientation
The two sides of the wing plate axis of symmetry are set.
36. according to the hydrogenator described in claim 31, which is characterized in that the shape of the overflow hole is round, strip
Shape, triangle or polygon.
37. according to the hydrogenator described in claim 24, which is characterized in that the wing plate and downspout is integrated chemical conversion
Type is made.
38. according to the hydrogenator described in claim 24, which is characterized in that the funnel-shaped distributor is by wing plate and drop
Liquid pipe assembles, i.e., is fixedly connected with a wing plate with certain angle in downspout middle and upper part.
39. according to the hydrogenator described in claim 38, which is characterized in that described is fixedly connected using welding, bolt
Connection, screw connection snap connection mode.
40. according to the hydrogenator described in claim 38, which is characterized in that the downspout is made of steel pipe, institute
Wing plate is stated to fold using steel plate.
41. according to the hydrogenator described in claim 24, which is characterized in that the jet tray is several pieces, and can
It is spliced into circular slab.
42. according to the hydrogenator described in claim 31, which is characterized in that the edge of the jet tray most outer is arranged
The flanging flipped up, the upper edge of flanging are higher than the lower edge of set overflow hole on downspout.
43. according to the hydrogenator described in claim 31, which is characterized in that several funnel-shaped distributors are spraying
Triangular in shape on tower tray, quadrangle, diamond shape arrangement.
44. according to the hydrogenator described in claim 24, which is characterized in that the height of the wing plate is equal to or more than descending liquid
Pipe height.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711468770.9A CN109985573B (en) | 2017-12-29 | 2017-12-29 | Hydrogenation reactor for improving liquid phase uniformity |
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|---|---|---|---|
| CN201711468770.9A CN109985573B (en) | 2017-12-29 | 2017-12-29 | Hydrogenation reactor for improving liquid phase uniformity |
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| Publication Number | Publication Date |
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| CN109985573B CN109985573B (en) | 2021-08-31 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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Effective date of registration: 20231008 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. |