CN108114671A - A kind of fold type, which subtracts, rushes equal flow table - Google Patents
A kind of fold type, which subtracts, rushes equal flow table Download PDFInfo
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- CN108114671A CN108114671A CN201611084902.3A CN201611084902A CN108114671A CN 108114671 A CN108114671 A CN 108114671A CN 201611084902 A CN201611084902 A CN 201611084902A CN 108114671 A CN108114671 A CN 108114671A
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- Prior art keywords
- flow table
- downspout
- equal flow
- fold type
- wing plate
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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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
Abstract
Subtract the invention discloses a kind of fold type and rush equal flow table.The fold type, which subtracts, to be rushed equal flow table and includes tower tray and several funnel-shaped distributors for being vertically arranged on tower tray；The funnel-shaped distributor includes downspout and and the wing plate that is arranged at the top of downspout；The downspout is open at both ends structure, and the wing plate has certain angle, the length of side and height, and the wing plate is parallel with the axis of downspout or forms an angle.The fold type of the present invention, which subtracts, to be rushed equal flow table and is arranged in reactor upper cover idle space, or reactor shell upper end, the strong impact power that remnants kinetic energy when fluid enters reactor is formed can be cut down, eliminate central point into the inclined streamline of fashionable formation to " pushing away wave " phenomenon of distribution plate liquid layer.The fold type of the present invention, which subtracts, rushes equal flow table suitable for all hydrogenation reactors, is particularly suitable for the hydrogenation reactor that liquid-gas ratio is larger, larger.
Description
Technical field
Subtract the present invention relates to a kind of fold type and rush equal flow table, belong to field of chemical equipment.It is equal that the fold type of the present invention subtracts punching
Flow table increases inner member newly for reactor.A kind of fold type of the present invention, which subtracts, rushes equal flow table suitable for various hydrogenation reactors, especially
Suitable for the hydrogenation reactor that liquid-gas ratio is larger, larger.
Background technology
In recent years, with the fast development of Chinese national economy and the enhancing of environmental consciousness, to the quality of petroleum chemicals and
Environmental requirement is higher and higher.In order to adapt to the needs of Sulfur-Containing Crude, meet the needs of ever-increasing industrial chemicals, improve
The quality of product, importance and role of the hydrogen addition technology in petroleum refining industry are increasing.In hydrogenation plant, set as key
Standby hydrogenation reactor mixes effect of the feedstock oil after hydrogen by hydrogenation catalyst, completes refined and cracking by a certain percentage
Deng reaction.Hydrogenation reaction in hydrogenation reactor can stable operation, can hydrogenation catalyst fully play its effect, product
Whether quality can reach high-quality, be heavily dependent on the uniformity that gas-liquid is distributed in catalyst bed.And gas-liquid exists
Whether the distribution in catalyst bed is uniform, and the design with hydrogenation reactor inner member has close relationship.In other words, interior structure
The quality of part performance directly influences the service cycle of catalyst life, product quality and device, i.e., is used in hydrogenation process
The obtained effect of inner member technology of a set of function admirable is never second to use a kind of higher catalyst of activity instead.Therefore it is domestic
The research to hydrogenation reactor inner member and engineering development are paid much attention to always outside, constantly update its reactor component, in the hope of
Obtain better effect.
Hydrogenation reactor inner member has inlet diffuser, gas-liquid partition tray, sediment incrustation basket, catalyst bed supporting member, cold hydrogen
Case, exit collector and inert ceramic balls etc., wherein being also that most important inner member is gas directly concerning catalyst service efficiency
Liquid distribution plate and cold hydrogen box.
It is hydrocracked, during hydrodesulfurization reaction in airwater mist cooling, widely uses fixed bed hydrogenation reactor, and
Gas-liquid allotter is one of inner member of fixed bed hydrogenation reactor most critical.The function of gas-liquid allotter is that gas-liquid two-phase is former
Material is allocated, mixes and is equably sprayed onto catalyst bed layer surface, improves flow regime of the liquid phase in catalyst bed.
Gas-liquid allotter is assigned macro-uniformity and microscopic uniformity to reaction mass.Multiple gas-liquid allotters are with one
Fixed arrangement mode is mounted on tower tray and forms distribution tray.The amount of liquid phase flowed through from each distributor is identical with gas volume,
Ensure " uniform " covering of the material to catalyst bed, be defined as the macro-uniformity of gas-liquid allotter.Reach liquid distribution
Higher macro-uniformity is relatively difficult, the reason is that hydrogenation reactor diameter is increasing at present, distribution tray is by piecemeal group
Installation is closed, can not precisely ensure to distribute plate face level.Being commonly installed error can make distribution plate face have 1/8 °~1/ in the horizontal direction
2 ° of inclination, maximum inclination is up to 3/2 °.Even if distribution tray its levelness at the beginning of installation is higher, in operation,
Because under thermal expansion and material impact load collective effect distribution plate plate face can be made to lose levelness.Therefore, it is necessary to lean on distributor
Self structure realizes the uniformity of liquid phase macro-allocation.
It will be in liquid distribution to bed catalyst by distributor.It is not present what is be not covered with the liquid on catalyst bed
White space ensures " complete " covering of the material to catalyst bed, and here it is the microscopic uniformities of gas-liquid allotter.It is body
Liquid distribution effect for existing reactor bed regional area.
Fixed bed hydrogenation reactor is a kind of trickle bed reactor.Reactant in the form of gas-liquid two-phase is flowed downward and worn parallel
Cross fixed catalyst bed.Liquid phase is flowed downward in the form of streams, is dispersed phase, and gas phase is continuous phase, with liquid phase
Cocurrent flows downward.Liquid phase soaks catalyst granules when flowing through the surface of catalyst granules, and reacts and be just happened at
On the catalyst granules of wetting, therefore the effective wetting rate of catalyst has overall reaction rate very important influence.And liquid phase
Material into catalyst bed when distribute it is uneven will form channel or bias current in catalyst bed, partial catalyst is caused to obtain
It is very poor less than wetting or wetting effect, make the performance of this partial catalyst cannot play, influence product quality.
Hydrogenation process is exothermic reaction, and material is unevenly distributed the position extent of reaction that catalyst irrigation effect can be caused good
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, and the superposition of the two effect can form heat spot, make this partial catalyst performance premature inactivation, damage catalyst
Performance results even in the coking, hardened of catalysing area subregion, and material can not normally flow through, since fixed bed hydrogenation reacts
Device is trickle bed fluidised form, causes the catalyst below hardened region that cannot play a role, so as to substantially reduce the use of catalyst
Service life and the on-stream time of device.The local hardened rise for also resulting in catalyst bed pressure drop, has to continue to run with
The operating pressure of reactor is improved, causes the rise of energy consumption；When the too fast rise of pressure drop reaches reactor design load, it has to
Improper shut-down carries out skimming processing, extraneous expense checking maintenance expense, while the screening of catalyst will also result in the stream of catalyst
It loses and wastes.Therefore, in fixed bed hydrogenation reactor, liquid phase material distributing uniformity is particularly significant.
Hydrogenation reactor is fed with reactor head center, despite the provision of inlet diffuser, and material conveys residual
Remaining kinetic energy can generate powerful impact force；Another fluidised form feature of center charging is that material is in reactor end socket space
Formation streamline for parallax, the liquid phase with kinetic energy generates " pushing away wave " phenomenon to the liquid layer on top dispenser tower tray, gives
The distributor for relying on tray level degree brings unfavorable entry condition, even if the distributor that performance is best, in the liquid of different depth
Under the conditions of layer, it can not also realize and evenly distribute material, radial temperature difference expands inevitable.
Gas-liquid partition tray is made of the gas-liquid distributor being mounted on distribution grid, and major function is that liquid phase reactor object is equal
Even is distributed on catalyst bed, to ensure that catalyst all in reactor can obtain homogeneous wetness degree so that
All catalyst possess similar catalytic efficiency, so as to effectively improve the whole production efficiency of reactor.In addition, liquid phase reactor object
Being uniformly distributed on entire catalyst bed layer cross section, additionally it is possible to reduce in catalyst bed the generation of " hot spot ", that is, avoid anti-
Device inner radial excessive temperature differentials is answered, so as to effectively inhibit coking and the inactivation of catalyst, extends the service life of catalyst and anti-
Answer the service cycle of device.And the widely applied gas-liquid distributor of current domestic field of hydrogenation, however it remains anti-column plate tilt capability
The defects of not strong and liquid dispersion performance is bad.
To liquid, the research of distributing homogeneity has the history of more than 50 years, Hen Duoyan in fixed bed reactors both at home and abroad
The person of studying carefully has found, liquid is the initial distribution on catalyst bed is to influence its overall distribution uniformity an important factor for, because single
The distance that stock liquid generally requires 4-5 times of reactor diameter could realize being uniformly distributed on entire bed.
Gas-liquid distributor is the important inner member in fixed bed Oxygenation device, and major function is for gas-liquid two-phase fluid
The place of mixing and interaction is provided, makes liquid crushing into droplet distribution into air-flow, and is fallen on air-flow on filler,
Form initial distribution of the liquid on filling batch.The uniformity of liquid initial distribution directly affects the wetting journey of downstream catalyst
Degree and service efficiency, if gas-liquid distributor design is unreasonable, reaction raw materials distribution effects is poor, and hydrogenation reaction can be caused to be catalyzed
Inhomogeneities in agent bed causes radial temperature difference excessive, so as to reduce the utilization rate of catalyst and service life or even cause product
Can't meet the quality requirement.
It is more and more urgent to the demand of clean fuel in world wide recently as the raising of people's environmental consciousness, it is right
The product quality of hydrogenation reactor proposes new higher requirement.And due to reaction raw materials be distributed on catalyst bed it is equal
Can even property has been largely fixed hydrogenation reactor realize that can the quality of stable operation and product reach high-quality, because
This requirement to gas-liquid distributor performance is also higher and higher.
Due to gas-liquid distributor for fixed bed Oxygenation device stable operation or hydrogenated products quality all
It plays the important and pivotal role, therefore the interest of numerous experts and scholars is caused to the research of its structure and performance, while
Receive the attention of main oil refining company and scientific research institution both at home and abroad.Domestic such as Sinopec Engineering Construction Company is comforted
Along the units such as Petroleum Chemical Engineering Institute and Luoyang petroleum chemical engineering company;External such as British Petroleum Company (BP), joint oil
Company (Union Oil), Texaco Inc. (TEXACO), Praxair Technology, Inc (UOP), Xue Folong companies (CHEVRON) and
International Shell Co. Ltd (SHELL) etc., great effort has all been entered in the development and application of gas-liquid distributor, has also all been had developed
The gas-liquid distributor of a variety of each tool styles.Different gas-liquid allotters realizes macro-allocation uniformity and Micro-distribute uniformity
Method is different.Three classes are broadly divided into according to its mechanism of action：The mixed type of overflow type, suction type and the two.Their structure,
Working mechanism is different, and also difference is very big for Micro-distribute uniformity.
Generally speaking, according to the dispersion mechanism of liquid, above-mentioned overflow type, suction type and the mixed of overflow and swabbing action is had both
In mould assembly three classes gas-liquid partition tray, suction type gas-liquid distributor, can be by liquid point due to having preferable liquid crushing performance
It dissipates for the smaller drop of grain size, distributing homogeneity of the liquid on catalyst bed will compared with other two types under its effect
Good, such as domestic oxygenation field is widely applied at present combines oil type gas-liquid distributor.But since joint oil type gas-liquid distributor is adopted
With identical gas-liquid entrance, gas access area will be with the fluctuation of liquid level and change, so as to cause gas velocity and liquid
The variation of body suction capactity, when gas-liquid partition tray is there are during certain gradient, the gas-liquid distributor in differentiated levels
By with different gas access area and liquid suction capactity, the liquid distribution for causing gas-liquid partition tray is not uniform enough, also
It is to say that the anti-column plate tilt capability of joint oil type gas-liquid distributor is not strong.In addition, some nearest research reports show joint oil
For type gas-liquid distributor there are more serious central bus phenomenon, the distributing homogeneity of liquid is also not ideal enough.
In recent years, as domestic market is continuously increased the demand of high-quality distillate, environmental regulation in world wide in addition
Increasingly strict, clean fuel the whole world popularization and application, it is desirable that the technology that traditional oil Refining Technologies must upgrade
It improves.The height of hydrogenation technique technical merit, depends primarily upon the advance of catalyst performance, and the performance of catalyst performance,
Then depend greatly on inside reactor advanced structure and reasonability.Wherein one of key technology is exactly that reactor must
Must have and the peak use rate for realizing catalyst is redistributed between good liquid, gas initial distribution and bed, it is otherwise impossible
Produce ultra-low-sulphur diesel.And in order to realize economic scale, the raising of hydrogenation plant manufacturing capacity, hydrogenation reactor is
Develop towards enlargement, the continuous increase of reactor diameter, it is also more next to the reaction stream distribution effects requirement of reactor component
It is higher.
At present, there are situations unevenly distributed, such as state in various degree for hydrogenation reactor gas-liquid distributor at present both at home and abroad
It is interior widely used for bubble cap type distributor or modified bubble cap distributor, the apparent uneven feelings of gas-liquid distribution performance presence
Condition, the distributor are based on suction principle：Liquid phase is formed during gas phase baffling and is carried secretly, realizes liquid phase distribution.
Bubble cap type distributor mainly overcomes distribution plate installation to incline the swabbing action of liquid phase on distribution plate by gas phase
Uniformity that is oblique and keeping liquid macro-allocation.But the overflow port category vertical masonry joint notch of bubble cap type distributor, macro-uniformity
Not as good as overflow type distributor.And bubble cap dispenser size is larger, and it is more to occupy space reactor away from larger for clipping room.Moreover,
Since the central area flow of bubble cap distributor is big, the Micro-distribute of liquid phase is uneven；And due to the fluidised form of bubble cap distributor
For plug flow, impact force is larger.For these reasons, bubble cap distributor must not be not filled with the inertia of adequate thickness when in use
Porcelain layers of balls for slowing down impact force, and aids in homodisperse liquid phase, and after need to flowing through certain section producing depth, could realize
Even in liquid phase is disperseed, and wastes valuable space reactor.
Broad fraction scope all can be divided into full gas as the raw material of hydrogenation plant, fluidised form operating mode from raw gasoline to residual oil
Phase and biphase gas and liquid flow, even gas-liquid two-phase operating mode, there is very big difference in hydrogen-oil ratio, density of liquid phase, viscosity differences are larger,
Therefore, the bubble cap distributor based on suction principle, it is impossible to suitable for above-mentioned all operating modes.
In addition, with feedstock oil in poor quality is on the rise, processing process is increasingly longer, serialization degree increasingly
Height, in feedstock oil containing acid cause equipment and process pipelines corrode caused by rust deposite, the entrainment of process upstream unstability auxiliary agent,
Dissolved oxygen in storage and transport process etc., into hydrogenation reactor after can generate dirty object, covering top distribution plate.Based on suction principle
Bubble cap distributor is easy to capped or part and covers, and material is caused to be unevenly distributed, and when Inlet fluid is unevenly distributed, meeting
Seriously affect hydrogenation reactor top dispenser effect.
It is affected for traditional anti-column plate tilt capability of gas-liquid allotter is weaker, distribution plate upper liquid layer depth is uneven
The technical issues of, it is necessary to exploitation, which has to subtract, rushes flow equalizing function, the new interior structure small, distributed effect is good, installation accuracy is low
Part technology, the strong impact power that the fluid remnants kinetic energy for cutting down into reactor is formed, for eliminating inclined fluidised form
Fluid realizes evenly distributing for fluid to " pushing away wave " phenomenon of liquid layer on distribution plate.
The content of the invention
For deficiency of the prior art, subtract the present invention provides a kind of fold type and rush equal flow table.The fold type of the present invention
Subtract that rush equal flow table be the reactor component newly established, be arranged in idle reactor upper cover or be arranged on reactor
Cylinder upper end, top distribution plate the upper surface of；The strong impact power that remnants kinetic energy is formed when entering reactor available for abatement fluid；
Central point is eliminated into the inclined streamline of fashionable formation to " pushing away wave " phenomenon of distribution plate liquid layer, eliminates fluid autoreactor entrance
Fall to top distribution plate potential energy and come impact force；Realize that fluid flow state becomes more meticulous the first distribution work(of adjusting and material
It can or substitute the distribution function of top distribution plate；Good entry condition can be provided for top distribution plate.The fold type of the present invention
Subtract and rush that equal flow table distributed effect is good, takes full advantage of reactor end socket idle space, there is small, simple in structure, installation side
Just the features such as and operating flexibility is big.
Technical scheme is as follows：
A kind of fold type, which subtracts, rushes equal flow table, including tower tray and the funnel-shaped distributor being vertically arranged on tower tray；The chimney
Formula distributor includes downspout and and the wing plate that is arranged at the top of downspout；The downspout is both ends open structure, described
Wing plate has certain angle, the length of side and height；The wing plate is parallel with the axis of downspout or the center line of the wing plate with
Reactor axis forms an angle.
Subtracting for the present invention is rushed in equal flow table, center or the center of circle of the angle away from tower tray of the wing plate.Further, it is described
The center line of wing plate angle is overlapped with reactor shell ray, and wing plate angle is in face of the nearest cylinder wall of reactor.
Further, the wing plate has certain angle, the length of side and height.The wing plate and the quantity phase of downspout
Together, and wing plate goes to upper and lower arrangement with downspout.The bottom edge of the wing plate is Chong Die with the upper edge of downspout or is not overlapped connection；Weight
During folded connection, stack height is that the ratio of downspout height is 5%~30%, is preferably 10%~25%.
Further, the wing plate is tilted towards closest wall of reactor, and the center line of the angle of wing plate with
Angle between reactor axis is 15 °~80 °.
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 spout holes are provided on the tube wall of the downspout, in order to which liquid enters through spout hole
Downspout and along downspout flow down.Certain distance should be maintained between the center line and tray deck surface of the spout hole.It overflows
The setting quantity of discharge orifice is generally 1~6, preferably 1~2.The total sectional area of spout hole is downspout（It is horizontal）Sectional area
10%~100%, it is preferably 30%~50%.When the spout hole opened up on downspout only sets 1, orientation is arranged on downspout
With the opposite of wing plate tie point；When the quantity of spout hole is set to be 2, orientation is arranged in downspout and wing plate tie point
Both sides.The shape of set spout hole can be circle, strip, triangle and polygon, it is preferably circular.
Further, the funnel-shaped distributor may be employed any suitable material and be made, such as ceramics, metal material
Deng, it is preferred to use steel material.The wing plate and the downspout being integrated be made, such as can by downspout and
Wing plate integration is processed into；Alternatively, it is done at the top certain altitude of the downspout with certain altitude vertical（Vertically）With
Horizontal resection retains the incomplete cutting of wall thickness, then spreads out certain angle and wing plate is made or in the upper of downspout
There is the wing plate of certain angle along being fixedly connected with one.Described being fixedly connected may be employed welding, be bolted, screw company
It connects, be buckled the various suitable modes such as link.
The present invention, which subtracts, to be rushed in equal flow table, and the tower tray is conventionally divided into several pieces, and sliceable is circular slab.In tower tray
The edge of most outer sets flanging, and flanging flips up.On the flanging set on downspout overflow is should be above along general
The lower edge of discharge orifice.The setting of flanging can maintain certain liquid level on tower tray, so as to eliminate to a certain extent
The influence that the horizontal Shortcomings of tower tray are brought to liquid phase distribution in the prior art.
The baffle plate type of the present invention subtracts and rushes in equal flow table, and several funnel-shaped distributors are 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 is also that the circulation of gas feed in charging is led to except for liquid in addition to
Road.
In the present invention, the deflector type, which subtracts, rushes that the reactor that equal flow table is applicable in is upper feeding and gas-liquid is consolidating for cocurrent form
Fixed bed reactor is particularly suitable for fixed bed trickle bed reactor form；More preferably various fixed bed hydrogenation reactors, especially
It is the hydrogenation reactor that liquid-gas ratio is larger, larger.
Compared with prior art, fold type of the present invention, which subtracts, rushes equal flow table and has the following advantages that：
1st, the equal flow table of fold type of the present invention by special structure design, reduces distributor installation dimension, is easily installed in idle
Reactor upper cover at or be arranged on reactor shell upper end, top distribution plate the upper surface of, reach and save space reactor
Purpose improves the space availability ratio of hydrogenation reactor, convenient for loading more catalyst or reducing reactor scale.
2nd, fold type of the present invention, which subtracts, rushes equal flow table, sets wing plate, stops because center is into when causing in the injection of oblique line fluidised form
Come fluid, its impact force is cut down, lose kinetic energy fluid be blocked after under the effect of gravity, by original parallax fluidised form
Conversion realizes that nature falls for vertical current state, and the consistent liquid layer of depth is formed on tower tray, eliminates parallax impact force
To " pushing away wave " phenomenon that liquid layer on tower tray is formed, and uniform entry condition is created to funnel-shaped distributor, by funnel-shaped
Material is distributed on the distribution plate of top by distributor, realizes just distribution function, to friendly, the steady liquid layer of distributor offer, uniformly
Entry condition, of the invention subtracting rush equal flow table, realize that material is evenly distributed to the horizontal cross-section of reactor together with distribution plate
On.Setting quantity is suitable, has the funnel-shaped distributor for subtracting and rushing flow equalizing function, it might even be possible to substitute existing top distribution plate,
Realize evenly distributing for material.Fold type i.e. of the present invention, which subtracts, to be rushed equal flow table and improves the entrance condition of the first bed distribution plate, is carried
The high distributed effect of distribution plate, the material distribution of optimization top bed improve the utilization rate of the first bed catalyst.
3rd, fold type of the present invention, which subtracts, rushes equal flow table, realizes that liquid phase is distributed by the wing plate of setting and funnel-shaped distributor, phase
The bubble cap distributor of more common suction principle, the disperse power of liquid phase distribution are changed to, using potential energy, be formed by gas phase suction
Splash, so as to reduce pressure drop.
4th, fold type of the present invention, which subtracts, rushes equal flow table, sets chimney distributor tube wall overflow hole site and shape, is formed and closed
The tower tray liquid storage depth of reason, reduction tray level degree deviation and the macro-allocation that level fluctuation is brought are uneven.
5th, fold type of the present invention, which subtracts, rushes equal flow table, using unique design principle and hydrodynamics feature, realizes material
It evenly distributes, makes 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, this has absolutely proved that fold type of the present invention subtracts and has rushed equal flow table the distribution of reaction feed logistics and gas-liquid are mixed
It is preferable to close effect, there is certain booster action to hydrogenation catalyst reaction process and catalyst coking control.
6th, the equal flow table of fold type of the present invention is the hydrogenation reactor inner member newly established, have it is simple in structure, it is easy for installation,
Operating flexibility is big, can improve hydrogenation reactor space availability ratio, improvement reactor top divides material inlet condition, improves reactor
The radial distribution effect of charging effectively eliminates reactor radial temperature difference, eliminates catalyst bed and causes because material is unevenly distributed
Heat spot, in hydrogenation reactor catalyst it is effective using excellent entry condition is provided, reduce catalyst skimming or change
Agent number extends the on-stream time of device, improves hydrogenation technique effect, with good economic efficiency.
Description of the drawings
A kind of fold type that Fig. 1 is the present invention subtracts and rushes equal flow table structure diagram.
Wherein, 1 is chimney distributor, and 2 be tower tray, and 3 be tower tray connector, and 4 be tray brace summer, 5- spout holes.
Fig. 2 is the funnel-shaped dispensing arrangement schematic diagram that band of the present invention subtracts punching.Wherein, 11 be wing plate, and 12 be downspout.
Fig. 3 is funnel-shaped dispensing arrangement top view in the present invention.
Fig. 4 is the fluid flow pattern schematic diagram of funnel-shaped distributor in the present invention.
Fig. 5 is the fluid flow pattern top view of funnel-shaped distributor in the present invention.
Fig. 6 is the orientation schematic diagram of different temperature measuring points on same bed section in the embodiment of the present invention.
Specific embodiment
As shown in Figs. 1-3, fold type of the invention, which subtracts, rushes equal flow table, if including tower tray 2 and being vertically arranged on tower tray
Do funnel-shaped distributor 1.Funnel-shaped distributor 1 includes downspout 1-2 and and the wing plate 11 that is arranged at the top of downspout 1-2.Drop
Liquid pipe 12 is both ends open structure.Wing plate 11 is with downspout 12 in arrangement up and down.Wing plate 11 has certain angle, the length of side and height
Degree, is generally folded by steel plate.Wing plate 11 is parallel with the axis of downspout 12.
As shown in Fig. 2, in funnel-shaped distributor, wing plate is identical with funnel-shaped distributor quantity and corresponds.Wing plate
Angle is generally 15 °~180 °, is preferably 90 °~120 °；The length of side of wing plate is generally 20mm~200mm, and preferably 60mm~
120mm；The height of wing plate is generally 30mm~200mm, is preferably 60mm~120mm.The bottom of wing plate connects along with edge on downspout
It connects, it also can be with downcomer sections arranged superposed.When wing plate bottom along on downspout along overlaps when, can be downspout height 10%
~100%, it is preferably 5%~20%.When its wing plate angle center line is overlapped with reactor shell ray, angle faces reactor
Nearest cylinder wall.
Fold type of the present invention, which subtracts, to be rushed in equal flow table, and downspout is generally made of metal tube.The height general 20 of downspout~
300mm is preferably 50~120mm.Horizontally arranged 1~6 spout hole on downspout, preferably 1~2；Its spout hole is total
Sectional area is the 10%~100% of downspout sectional area, is preferably 30%~50%.When the spout hole opened up on downspout sets 1
When, orientation is arranged on downspout and subtracts the opposite of punching tie point；When the quantity of spout hole is set to be 2, orientation is set
It puts in downspout and the both sides for subtracting punching tie point.The shape of spout hole can be circle, strip, triangle and polygon,
It is preferably circular.Overflow centerline hole is preferably 30~50mm away from 5~100mm of tray surface.
Fold type of the present invention, which subtracts, to be rushed in equal flow table, and one layer of fold type, which subtracts, rushes a number of funnel-shaped distribution of equal flow table setting
Device.Several funnel-shaped distributors are triangular in shape on tower tray, quadrangle, diamond shape arrangement.Funnel-shaped distributor usually passes through descending liquid
Pipe lower end is plugged on tower tray, and can be by welding, being threadedly coupled, the modes such as snapping connection and be fixedly connected.
The present invention, which subtracts, to be rushed in equal flow table, and tower tray is conventionally divided into several pieces, and sliceable is circular slab.Tower tray most outer
The flanging that edge setting flips up.Flanging height is generally 5~80mm, is preferably 30~50mm.
With reference to Fig. 1-5, fold type of the present invention subtracts that rush equal flow table method of work process as follows：
During work, the fluid spraying around, in oblique line fluidised form, that there is greater impact power of autoreactor center entrance,
It strikes on wing plate, because wing plate is with certain angle arrangement, can effectively stop the fluid sprayed in oblique line fluidised form, Jiang Qichong
It hits power to cut down, using wing plate barrier effect, Vapor Entrainment drop is forced to disperse around, realize the larger angle of flare of material, stream
Body drips naturally under the effect of gravity after kinetic energy exhausts, and forms vertical downward flow state, and liquid phase potential energy is freely falling body
Kinetic energy, and fall to subtracting and rush on the tray deck of equal flow table, since distributor material channel is in horizontally disposed and have apart from tray deck
Have that certain altitude is poor, thus material can subtract in fold type and rush the tray deck upper surface of equal flow table and form the liquid layer of certain depth, i.e.,
Tray level degree is made still to can ensure that each distributor with the presence of liquid phase there are deviation.Since distributor quantity is more, catalyst bed
Any one point of layer surface has a certain number of distributors to work so that the distributor uniformity is protected.Material is from chimney
The overflow hole path opened up on formula distributor tube wall is flowed into distribution pipe, realizes the first distribution of liquid.Due to subtracting by fold type
The material rushed after equal flow table has been converted into vertical fluidised form when being assigned on the distribution plate of top, and kinetic energy disappears, therefore to top
Liquid layer on distribution plate tray deck surface eliminates " pushing away wave " phenomenon of material to liquid layer on distribution plate, to top there is no thrust
Part orchestration provides friendly, steady liquid layer, uniform entry condition, and material is realized together with the distribution plate of top in catalyst
Being uniformly distributed on bed.
During the less operating mode of liquid phase material amount or catalyst bed top filling tooth spherical shape shape protective agent or hollow ball-type are protected
When protecting agent, fold type of the invention, which subtracts, rushes equal flow table, may replace top distribution plate, and realization subtracts punching, flows and distributes integration.Greatly
It is big to simplify inside reactor structure, reduce investment.
Illustrate the reaction effect of the present invention, but the protection domain being not intended to limit the present invention with reference to embodiment.
Comparative example 1
Certain hydrogenation reactor, diameter 4.6m leave unused before transformation in upper cover, and top distribution plate, top are included at only the first bed inlet
Using the ERI type bubble cap formula gas-liquid allotters of this field routine in distribution plate, hydrogenating materials are diesel oil, diesel oil density 860kg/
m3, sulfur content 1.7%, the catalyst trade mark is RS-2000 type Hydrobon catalysts, and process conditions are：Hydrogen partial pressure 6.8MPa
（G）, volume space velocity 1.9h-1, hydrogen to oil volume ratio 400:1,365 DEG C of reactor inlet temperature.Before transformation, bed radial temperature and
The temperature difference is shown in Table 1.
Embodiment 1
After transformation, the fold type that the present invention is added in upper cover subtracts and rushes equal flow table, subtracts punching using fold type as shown in Figure 1
Equal flow table is applied in combination with common ERI type bubble cap formula gas-liquid allotters.Fold type subtracts the major parameter for rushing equal flow table：Wing plate presss from both sides
Angle is 120 °；The wing plate length of side is 120mm；Wing plate height is 60mm.Its wing plate is parallel with chimney distributor axis.Its wing plate bottom edge
It is overlapped with edge on chimney distributor, coincidence point is distributor height 20%.Chimney distributor height is 120mm；In chimney distributor
On tube wall, 2 overflow ports are set in horizontal direction.The total sectional area of spout hole is the 30% of chimney distributor tube sectional area；Chimney
The spout hole opened up on distributor tube wall, shape are circle；The overflow centerline hole set on chimney distributor tube wall is away from tower
Disk upper surface 50mm；The fold type of the present invention, which subtracts, to be rushed in equal flow table, and funnel-shaped distributor is triangularly arranged on tower tray.It is described
Tower tray can be divided into 9 pieces, it is and sliceable for circular slab, 3 funnel-shaped distributors are set on every piece of cutting plate, tower tray is outermost
The edge on edge sets flanging, and the height of flanging is 50mm.
Hydrogenating materials and process conditions are the same as comparative example 1.
Again after going into operation, bed radial temperature difference is shown in Table 1.
Embodiment 2
After transformation, board-like subtract of flanging that the present invention is added in upper cover rushes equal flow table, eliminates the ability in former reactor
The ERI type gas-liquid allotters of domain routine, wherein, fold type subtracts the major parameter for rushing equal flow table：Wing plate angle is 120 °；Wing plate side
A length of 120mm；Wing plate height is 60mm.Its wing plate is parallel with chimney distributor axis.Its wing plate bottom along on chimney distributor
Along overlapping, coincidence point is distributor height 20%.Chimney distributor height is 120mm；On chimney distributor tube wall, in level
Direction sets 2 overflow ports.The total sectional area of spout hole is the 30% of chimney distributor tube sectional area；On chimney distributor tube wall
The spout hole opened up, shape are circle；The overflow centerline hole set on chimney distributor tube wall is away from tower tray upper surface 50mm；
The fold type of the present invention, which subtracts, to be rushed in equal flow table, and funnel-shaped distributor is triangularly arranged on tower tray.The tower tray can divide
9 pieces are segmented into, and sliceable is circular slab, and 3 funnel-shaped distributors are set on every piece of cutting plate, the edge of tower tray most outer is set
Flanging, the height of flanging is 50mm.
Hydrogenating materials and process conditions are the same as comparative example 1.Again after going into operation, the first catalyst bed entrance radial temperature profile
And the temperature difference is shown in Table 1.
Table 1 applies result
Claims (25)
1. a kind of fold type, which subtracts, rushes equal flow table, including tower tray and several funnel-shaped distributors being vertically arranged on tower tray；It is described
Funnel-shaped distributor include downspout and and the wing plate that is arranged at the top of downspout；The downspout is open at both ends structure,
The wing plate has certain angle, the length of side and height；The wing plate is parallel with the axis of downspout or the wing plate with it is anti-
Device axis is answered to form an angle.
2. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the angle of the wing plate is away from tower tray
Center or the center of circle.
3. subtract according to the fold type described in claim 1 or 2 and rush equal flow table, which is characterized in that the center of the angle of the wing plate
Line is overlapped with reactor shell ray, and wing plate angle is in face of the nearest cylinder wall of reactor.
4. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the quantity phase of the wing plate and downspout
Together, and wing plate is arranged with downspout in upper and lower.
5. subtract according to the fold type described in claim 4 and rush equal flow table, which is characterized in that bottom edge and the downspout of the wing plate
Upper edge overlapping or not connection.
6. subtract according to the fold type described in claim 5 and rush equal flow table, which is characterized in that bottom edge and the downspout of the wing plate
Upper edge partly overlaps connection, and stack height is that the ratio of downspout height is 5%~30%, is preferably 10%~25%.
7. subtract according to the fold type described in claim 4 and rush equal flow table, which is characterized in that the deflector type, which subtracts, to be rushed equal flow table and be applicable in
Reactor be upper feeding and fixed bed reactors that gas-liquid is cocurrent form, be particularly suitable for fixed bed trickle bed reactor shape
Formula.
8. subtract according to the fold type described in claim 7 and rush equal flow table, which is characterized in that the fold type, which subtracts, to be rushed equal flow table and set
Put in idle reactor upper cover or be arranged on reactor shell upper end, top distribution plate the upper surface of.
9. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the lower ending opening of the downspout is direct
It is opened on tower tray or through tray perforation.
10. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the tower tray further includes below
The supporting beam and tower tray connector being used to support.
11. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that is set on the tube wall of the downspout
There are several spout holes, the total sectional area of spout hole is the 10%~100% of downspout sectional area, is preferably 30%~50%.
12. subtract according to the fold type described in claim 11 and rush equal flow table, which is characterized in that the center line and tower of the spout hole
Plate maintains certain distance between surface.
13. subtract according to the fold type described in claim 11 and rush equal flow table, which is characterized in that the setting quantity of the spout hole is
1~6, preferably 1~2.
14. subtract according to the fold type described in claim 13 and rush equal flow table, which is characterized in that the spout hole opened up on downspout is only
1 is set, orientation is arranged on the opposite of downspout and wing plate tie point.
15. subtract according to the fold type described in claim 13 and rush equal flow table, which is characterized in that the spout hole opened up on downspout is
At 2, orientation is arranged on the both sides in downspout and wing plate tie point.
16. subtract according to the fold type described in claim 11 and rush equal flow table, which is characterized in that the shape of the spout hole is circle
Shape, strip, triangle and polygon.
17. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the wing plate and the downspout
Being integrated is made, and is processed by downspout and wing plate integration.
18. subtract according to the fold type described in claim 17 and rush equal flow table, which is characterized in that the integration processing refers to have
The top for having the downspout of certain altitude, which is done, vertically and horizontally cuts, and retains the incomplete cutting of wall thickness, then spreads out one
Determine angle and wing plate is made.
19. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the wing plate and downspout are group
It fills, one is fixedly connected on the upper edge of downspout has the wing plate of certain angle.
20. subtract according to the fold type described in claim 19 and rush equal flow table, which is characterized in that described is fixedly connected using weldering
It connects, be bolted, screw connection or at least one of snapping connection connection mode.
21. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the tower tray is divided into several pieces,
And sliceable is circular slab.
22. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that is set at the edge of tower tray most outer
The flanging flipped up, the upper edge of the flanging are higher than the upper edge of set spout hole on downspout.
23. subtract according to the fold type described in claim 22 and rush equal flow table, which is characterized in that several funnel-shaped distributors
Triangular in shape on tower tray, quadrangle, diamond shape arrangement.
24. subtract according to the fold type described in claim 22 and rush equal flow table, which is characterized in that the height of the flanging for 5~
80mm is preferably 30~50mm.
25. fold type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the wing plate is towards closest
Wall of reactor direction tilt, and the angle between the center line of the angle of wing plate and reactor axis is 15 °~80 °.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611084902.3A CN108114671B (en) | 2016-11-25 | 2016-11-25 | Flanging type impact-reducing flow-equalizing disc |
| TW106140943A TWI664021B (en) | 2016-11-25 | 2017-11-24 | Underflow equalizing plate and reactor |
| GB1719542.1A GB2560066B (en) | 2016-11-25 | 2017-11-24 | Impact-reducing uniform-flowing disc and reactor |
| RU2017140962A RU2672742C1 (en) | 2016-11-25 | 2017-11-24 | Disc having impact absorbing action and creating uniform flow and reactor |
| KR1020170158615A KR101989328B1 (en) | 2016-11-25 | 2017-11-24 | Impact-Reducing Uniform-Flowing Disc and Reactor |
| SG10201709746QA SG10201709746QA (en) | 2016-11-25 | 2017-11-24 | Impact-Reducing Uniform-Flowing Disc and Reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611084902.3A CN108114671B (en) | 2016-11-25 | 2016-11-25 | Flanging type impact-reducing flow-equalizing disc |
Publications (2)
| Publication Number | Publication Date |
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| CN108114671A true CN108114671A (en) | 2018-06-05 |
| CN108114671B CN108114671B (en) | 2020-01-10 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611084902.3A Active CN108114671B (en) | 2016-11-25 | 2016-11-25 | Flanging type impact-reducing flow-equalizing disc |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111375219A (en) * | 2018-12-31 | 2020-07-07 | 中国石油化工股份有限公司 | Dividing wall tower and dividing wall rectification method |
| CN113117362A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Liquid phase distribution control device and partition plate rectifying tower comprising same |
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| CN2355786Y (en) * | 1998-12-20 | 1999-12-29 | 中国石油化工集团公司 | Gas-liquid distributor |
| WO2006061409A1 (en) * | 2004-12-10 | 2006-06-15 | Shell Internationale Research Maatschappij B.V. | Reactor tube apparatus |
| CN103785332A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | A two-phase hydrogenation reactor and applications thereof |
| CN205216809U (en) * | 2015-11-25 | 2016-05-11 | 中石化洛阳工程有限公司 | Gas -liquid distributor |
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2016
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2355786Y (en) * | 1998-12-20 | 1999-12-29 | 中国石油化工集团公司 | Gas-liquid distributor |
| WO2006061409A1 (en) * | 2004-12-10 | 2006-06-15 | Shell Internationale Research Maatschappij B.V. | Reactor tube apparatus |
| CN103785332A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | A two-phase hydrogenation reactor and applications thereof |
| CN205216809U (en) * | 2015-11-25 | 2016-05-11 | 中石化洛阳工程有限公司 | Gas -liquid distributor |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111375219A (en) * | 2018-12-31 | 2020-07-07 | 中国石油化工股份有限公司 | Dividing wall tower and dividing wall rectification method |
| CN111375219B (en) * | 2018-12-31 | 2022-02-08 | 中国石油化工股份有限公司 | Dividing wall tower and dividing wall rectification method |
| CN113117362A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Liquid phase distribution control device and partition plate rectifying tower comprising same |
| CN113117362B (en) * | 2019-12-31 | 2022-08-12 | 中国石油化工股份有限公司 | Liquid phase distribution control device and partition plate rectifying tower comprising same |
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| CN108114671B (en) | 2020-01-10 |
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