CN108114670A - A kind of telescopic subtract rushes equal flow table - Google Patents
A kind of telescopic subtract rushes equal flow table Download PDFInfo
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- CN108114670A CN108114670A CN201611084901.9A CN201611084901A CN108114670A CN 108114670 A CN108114670 A CN 108114670A CN 201611084901 A CN201611084901 A CN 201611084901A CN 108114670 A CN108114670 A CN 108114670A
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- subtract
- flow table
- telescopic
- equal flow
- rushes
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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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
-
- 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
-
- 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
-
- 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
- B01J2208/0092—Perforated plates
Abstract
The invention discloses telescopic subtract of one kind to rush equal flow table.Telescopic subtract rushes several funnel-shaped distributors that equal flow table includes tower tray and is arranged on tower tray；Funnel-shaped distributor includes downspout and be arranged on downspout upper end subtract punching cylinder；It is described subtract rush cylinder and downspout be both ends open tubular structure, subtract and rush cylinder and downspout in arrangement up and down, subtract and rush the diameter of cylinder and be more than the diameter of downspout.The subtracting of the present invention rushes equal flow table and newly establishes inner member for reactor, is arranged in hydrogenation reactor upper cover idle space or hydrogenation reactor cylinder upper end.The subtracting of the present invention, which rushes equal flow table, can cut down the strong impact power that remnants kinetic energy when fluid enters reactor is formed, and eliminate central point into the inclined streamline of fashionable formation to " pushing away wave " phenomenon of distribution plate liquid layer.Telescopic subtract of the present invention 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
The present invention relates to telescopic subtract of one kind to rush equal flow table, belongs to field of chemical equipment.The telescopic of the present invention subtracts punching
Flow table increases inner member newly for reactor.Telescopic subtract of the present invention rushes equal flow table suitable for various hydrogenation reactors, especially suitable
In 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, the present invention provides telescopic subtract of one kind to rush equal flow table.Institute's sheath cartridge type subtracts punching
Equal flow table is arranged in idle reactor upper cover or is arranged on reactor shell upper end, top distribution plate the upper surface of.This hair
It is bright it is telescopic subtract that rush equal flow table be the reactor component newly established, remnants kinetic energy when entering reactor available for abatement fluid
The strong impact power of formation；The inclined streamline that central point into fashionable formation can be eliminated is existing to " the pushing away wave " of distribution plate liquid layer
As, eliminate fluid autoreactor entrance fall to top distribution plate potential energy and come impact force；Realize that fluid flow state is fine
Change the first distribution function of adjusting and material or substitute the distribution function of top distribution plate；It can be provided for top distribution plate good
Entry condition.Compared with prior art, of the invention telescopic subtract rushes that equal flow table distributed effect is good, takes full advantage of reactor envelope
Head idle space, has the characteristics that small, simple in structure, easy for installation and operating flexibility is big.
Technical scheme is as follows：
A kind of telescopic subtract rushes equal flow table, including tower tray and several funnel-shaped distributors being arranged on tower tray；The cigarette
Chimney formula distributor includes downspout and be arranged on downspout upper end subtract punching cylinder；It is described to subtract that rush cylinder and downspout be that both ends are opened
The tubular structure of mouth subtracts and rushes cylinder with downspout in arrangement up and down, and described subtract rushes diameter of the diameter of cylinder more than downspout.
Further, described subtract rushes cylinder and covers arrangement in upper and lower, coaxial, annulus with downspout.
Further, subtract and rush cylinder sectional area and chimney distributor sectional area and have correspondence.Subtract and rush cylinder bottom edge and downspout
Upper edge, which is overlapped or is not overlapped, to be fixedly connected, also can be with downspout top arranged superposed.When arranged superposed, stack height is descending liquid
The ratio of pipe height is 5%~30%, is preferably 10%~25%.
Further, described subtract rushes between cylinder and downspout horizontal direction that there are the gaps of certain distance.It is described to subtract punching cylinder
Sectional area be 1.1~3 times of downspout sectional area, be preferably 1.5~2.5 times.Subtract and rush between cylinder and downspout and can pass through
Pull rod（Or lacing wire）It is fixed and connects.
In the present invention, the tower tray also typically includes supporting beam and the tower tray connector for fixing tower tray.
Further, it is described subtract rush cylinder on along opening, several tooth sockets are set.
In the present invention, described telescopic subtract rushes that the reactor that equal flow table is applicable in is upper feeding and gas-liquid is cocurrent form
Fixed bed reactors are particularly suitable for fixed bed trickle bed reactor form.More preferably applicable reactor is containing not in raw material
Saturated hydrocarbons or dirty object are more and larger（Such as 4 meters of reactor diameter or more）Hydrogenation reactor.Telescopic subtract rushes equal flow table
Suitable for being arranged in idle reactor upper cover or being arranged on reactor shell upper end, top distribution plate the upper surface of.
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 funnel-shaped distributor may be employed any suitable material and be made, such as ceramics, metal material
Deng present invention preferably employs steel materials.It is described subtract rush cylinder and the downspout being integrated be made；Alternatively,
The upper edge of downspout, which is fixedly connected with a tubular and subtracts, rushes cylinder.Described being fixedly connected may be employed welding, be bolted, spiral shell
The various suitable modes such as silk connection.
Telescopic subtract of the invention is rushed in equal flow table, and cylinder is rushed in described subtracting and downspout is typically each made of metal tube.Descending liquid
Horizontally arranged 1~6 spout hole on the tube wall of pipe is preferably 1~2.Spout hole is total in each funnel-shaped distributor
Sectional area is the 10%~100% of downspout sectional area, is preferably 30%~50%.The shape of spout hole can be circle, strip,
Triangle and polygon, it is preferably circular.The overflow centerline hole set on downspout is preferably away from 5~100mm of tray surface
30~50mm；The height of downspout is 20~300mm, is preferably 50~120mm.
Of the invention telescopic subtract is rushed in equal flow table, and one layer telescopic to subtract and rush equal flow table a number of having can be set to subtract
Rush the funnel-shaped distributor of flow equalizing function.Several have the function of to subtract that the funnel-shaped distributor rushed is triangular in shape on tower tray, four sides
Shape, diamond shape arrangement.
Telescopic subtract of the invention is rushed in equal flow table, and tower tray is conventionally divided into several pieces, and sliceable is circular slab.The tower
The most outer edge of disk sets flanging folded over upwards；Tower tray flanging height is generally 5~80mm, is preferably 30~50mm.
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.
Compared with prior art, of the invention telescopic subtract rushes equal flow table and has the following advantages that：
1st, the telescopic equal flow table 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, the telescopic equal flow table of the present invention, setting have the function of to subtract the distributor rushed, and the subtracting of its upper part rushes cylinder and stop to be in incline
The injection fluid of oblique flow state, its impact force is cut down；Lose kinetic energy fluid be blocked after under the effect of gravity, inclined by original
Oblique line fluidised form is converted for vertical current state, and realizes that nature falls, and the consistent liquid layer of depth is formed on tower tray, eliminates inclination
" pushing away wave " phenomenon that line impact force is formed to liquid layer on tower tray, and uniform entry condition is created to funnel-shaped distributor, lead to
It crosses funnel-shaped distributor material is distributed on the distribution plate of top, realizes just distribution function, friendly, steady liquid is provided to distributor
Layer, uniform entry condition, of the invention subtracting rush equal flow table, realize that material is evenly distributed to the water of reactor together with distribution plate
On plane section.Setting quantity is suitable, has the chimney distributor for subtracting and rushing flow equalizing function, may replace existing top distribution plate, real
Existing material evenly distributes.Telescopic subtract i.e. of the invention rushes equal flow table and improves the entrance condition of the first bed distribution plate, improves
The distributed effect of distribution plate, the material distribution of optimization top bed improve the utilization rate of first bed catalyst.
3rd, the telescopic equal flow table of the present invention is rushed on cylinder by subtracting for setting along opening up tooth socket, inclined line injection
Liquid phase is impinged upon on tooth socket, forms larger splash area, forms dispersed phase, is conducive to cut down impact force, is formed simultaneously larger
Region of being scattered in area, beneficial to forming uniform liquid layer on tower tray.
4th, the telescopic equal flow table of the present invention rushes cylinder and the realization liquid phase distribution of funnel-shaped distributor by subtracting for setting, compares
The bubble cap distributor of more general suction principle, the disperse power of liquid phase distribution are changed to, using potential energy, form spray by gas phase suction
It splashes, so as to reduce pressure drop.
5th, the telescopic equal flow table of the present invention sets chimney distributor tube wall overflow hole site and shape, is formed rational
Tower tray liquid storage depth, reduction tray level degree deviation and the macro-allocation that level fluctuation is brought are uneven.
6th, the telescopic equal flow table of the present invention using unique design principle and hydrodynamics feature, realizes the uniform of material
Distribution makes the reduction of catalyst bed radial temperature difference, catalyst bed radial temperature difference≤3 DEG C, since radial temperature difference reflects fluid
Distributed effect, this absolutely proved the equal flow table of grating type of the present invention to the distribution of reaction feed logistics and gas-liquid mixed effect compared with
It is good, there is certain booster action to hydrogenation catalyst reaction process and catalyst coking control.
7th, telescopic subtract of the invention rushes equal flow table compared with prior art, and simple in structure, easy for installation, operating flexibility is big,
Hydrogenation reactor space availability ratio can be improved, improvement reactor top divides material inlet condition, the radial direction for improving reactor feed
Distributed effect effectively eliminates reactor radial temperature difference, eliminates catalyst bed heat spot caused by material is unevenly distributed, is
Catalyst is effective using excellent entry condition is provided in hydrogenation reactor, reduces catalyst skimming or changes agent number, extends
The on-stream time of device improves hydrogenation technique effect, with good economic efficiency.
Description of the drawings
Fig. 1 is that telescopic subtract of the invention rushes equal flow table structure diagram.
Wherein, 1 is funnel-shaped distributor, and 2 be tower tray, and 3 be tower tray connector, and 4 be tray brace summer, and 5 be spout hole.
Fig. 2 is the structure diagram of funnel-shaped distributor.Wherein, 1-1 is subtracts punching cylinder, and 1-2 is downspout, and 1-3 is pull rod.
Fig. 3 is the structure top view of funnel-shaped distributor.
Fig. 4, which is that the present invention is telescopic, subtracts the fluid flow pattern schematic diagram for rushing equal flow table.
Fig. 5 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, if telescopic subtract of the invention rushes equal flow table including tower tray 2 and be vertically arranged on tower tray
Do funnel-shaped distributor 1.Funnel-shaped distributor includes downspout 1-2 and is arranged on subtracting for downspout upper end and rushes cylinder 1-1, the two it
Between be fixedly connected by pull rod 1-3.Subtract rush cylinder and downspout be both ends open tubular structure, subtract and rush cylinder and presented with downspout
Lower arrangement, and subtract and rush diameter of the diameter of cylinder more than downspout.
Wherein, subtract and rush cylinder with certain specification.Subtract and rush cylinder height and be generally 30~400mm, be preferably 100~300mm；Subtract
The diameter for rushing cylinder is generally 30~260mm, is preferably 80~150mm.Subtract rush cylinder on along opening preferably also set up tooth socket, tooth socket
Shape is triangle, rectangle or arc-shaped, is preferably triangle.The height of tooth socket is to subtract rush cylinder height 1%~20%, is preferably
2%~10%.
As Figure 2-3, telescopic subtract of the invention is rushed in equal flow table, subtracts and exists between rushing cylinder and downspout in the horizontal direction
Gap is preferably 10~50mm to as gas phase channel, gap width is generally 5~200mm.Subtract and rush cylinder and downspout
It is preferred that above and below, coaxial, annulus set arrangement.Subtract rush cylinder sectional area as downspout sectional area 1~8 times, preferably 2~6 times.Subtract punching
Cylinder bottom is connected along with edge on downspout, also can be with downspout arranged superposed.When subtract punching bottom along it is Chong Die with downcomer sections when, weigh
Folded height is generally the 5%~30% of downspout height, is preferably 10%~25%.
Of the invention telescopic subtract is rushed in equal flow table, is subtracted and is rushed cylinder and downspout is generally made of metal tube.The height of downspout
Generally 20~300mm is preferably 50~120mm.On the tube wall of downspout, 1~6 overflow is usually set in horizontal direction
Hole is preferably 1~2.The total sectional area of spout hole is generally the 10%~100% of the sectional area of downspout, preferably 30%~
50%.The shape of spout hole can be circle, strip, triangle and polygon, it is preferably circular.It is set on downspout to overflow
The center line of discharge orifice is preferably 30~50mm away from 5~100mm of tower tray upper surface.
Of the invention telescopic subtract is rushed in equal flow table, and one layer telescopic to subtract and rush equal flow table a number of having can be set to subtract punching
The funnel-shaped distributor of flow equalizing function.It is several have the function of to subtract the funnel-shaped distributor rushed triangular in shape on tower tray, quadrangle,
Diamond shape is arranged.Funnel-shaped distributor is usually plugged on tower tray by downspout lower end（Plate）On, and can be connected by welding, screw thread
It the modes such as connects, snap connection to be fixedly connected.
Telescopic subtract of the invention is rushed in equal flow table, and tower tray is conventionally divided into several pieces, and sliceable is circular slab.Tower tray is most
The edge of outer sets flanging folded over upwards, and flanging height is generally 5~80mm, is preferably 30~50mm.
With reference to Fig. 1-4, the present invention is telescopic to subtract that rush equal flow table method of work process as follows：
During work, there is the fluid that greater impact power, autoreactor center enter, inclined line sprays around, fluid impact
Rushed to subtracting on cylinder, can effectively stop in oblique line fluidised form spray fluid, by its impact force cut down tune, and fluid be blocked,
It falls naturally under gravity after losing kinetic energy, forms vertical downward flow state, liquid phase potential energy is the dynamic of freely falling body
Can, and fall to subtracting and rush on the tray deck of equal flow table.The telescopic equal flow table of the present invention is rushed on cylinder by subtracting for setting along opening up tooth
Slot, the liquid phase of inclined line injection impinge upon on tooth socket, form larger splash area, form dispersed phase, be conducive to disappear
Impact-reducing power, the region of being scattered being formed simultaneously in larger area, beneficial to forming uniform liquid layer on tower tray.Due to distributor material
Passage is in horizontally disposed and poor with certain altitude apart from tray deck, thus material can be formed on the tray deck for rushing equal flow table is subtracted
Liquid layer, thus material can subtract the liquid layer for the tray deck upper surface formation certain depth for rushing equal flow table in grating type, even if tower tray water
Pingdu still can ensure that each distributor with the presence of liquid phase there are deviation.Since distributor quantity is more, catalyst bed layer surface is appointed
One point of meaning has a certain number of distributors to work so that the distributor uniformity is protected.Material is from funnel-shaped distributor
The overflow hole path opened up on tube wall is flowed into distribution pipe, realizes the first distribution of liquid.Due to the object after over-subtraction rushes equal flow table
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 tray deck
Liquid layer on surface eliminates " pushing away wave " phenomenon of material to liquid layer on distribution plate, is provided to top dispenser there is no thrust
Friendly, steady liquid layer, uniform entry condition, it is uniform on catalyst bed to realize material together with the distribution plate of top
Distribution.
When the less operating mode of liquid phase material amount in hydrogenation reactor or the filling tooth spherical shape shape protection of catalyst bed top
When agent or hollow ball-type protective agent, telescopic subtract of the invention rushes equal flow table, it might even be possible to which substitution top distribution plate, realization subtract
Punching flows and distributes integration, so as to greatly 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
A hydrofining reactor in certain refinery gasoline hydro-refining unit, the reactor diameter be 3.0m, upper envelope
It leaves unused in head, top layer's catalyst bed inlet is provided with top distribution plate, and the ERI types of this field routine are used in the distribution plate of top
Bubble cap formula gas-liquid allotter, hydrogenating materials are gasoline fraction, and catalyst is the FGH-21 types of Fushun Petrochemical Research Institute's production
Hydrobon catalyst, the process conditions of the reactor are：Operating pressure 1.85MPa, volume space velocity 2.5h-1, hydrogen oil volume
Than for 355:1,285 DEG C of reactor inlet temperature, catalyst bed radial temperature and the temperature difference are shown in Table 1.
Embodiment 1
After transformation, telescopic subtract that the present invention is added in upper cover rushes equal flow table, telescopic subtracts punching using as shown in Figure 1
Equal flow table is applied in combination with common ERI type bubble cap formula gas-liquid allotters.The major parameter of telescopic equal flow table：Subtract and rush cylinder height
Preferably 300mm；Subtract that rush cylinder diameter be preferably 150mm；Subtract and rush the upper along triangle tooth socket is set of cylinder, the height of tooth socket is to subtract punching
The 10% of cylinder height.Subtract that rush gap between cylinder and chimney distributor horizontal direction be preferably 30mm；Subtract and rush cylinder sectional area as chimney point
5 times of orchestration sectional area；Subtract and rush cylinder bottom edge and chimney distributor arranged superposed；Lap position is the 20% of chimney distributor height；
Chimney distributor height is 120mm；On chimney distributor tube wall, 2 overflow ports are set in horizontal direction.The total of spout hole cuts
Area is the 30% of chimney distributor tube sectional area；The spout hole opened up on chimney distributor tube wall, shape are circle；Chimney
The overflow centerline hole set on distributor tube wall is away from tower tray upper surface 50mm.Telescopic subtract of the present invention is rushed in equal flow table, cigarette
Chimney formula distributor is triangularly arranged on tower tray.The tower tray can be divided into 9 pieces, and sliceable for circular slab, every piece
3 funnel-shaped distributors are set on cutting plate, and the edge of tower tray most outer sets flanging, and the height of flanging is generally 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 and maximum temperature difference are shown in Table 1.
Embodiment 2
After transformation, telescopic subtract that the present invention is added in upper cover rushes equal flow table, eliminates this field in former reactor
Conventional ERI type gas-liquid allotters, wherein, it is telescopic to subtract the major parameter for rushing equal flow table：Subtract that rush cylinder highly preferred for 300mm；
Subtract that rush cylinder diameter be preferably 150mm；Subtract and rush the upper along triangle tooth socket is set of cylinder, the height of tooth socket is to subtract rush cylinder height 10%.
Subtract that rush gap between cylinder and chimney distributor horizontal direction be preferably 30mm；Subtract and rush cylinder sectional area as chimney distributor sectional area
5 times；Subtract and rush cylinder bottom edge and chimney distributor arranged superposed；Lap position is the 20% of chimney distributor height；Chimney distributor is high
It spends for 120mm；On chimney distributor tube wall, 2 overflow ports are set in horizontal direction.The total sectional area of spout hole is chimney point
The 30% of orchestration tube section product；The spout hole opened up on chimney distributor tube wall, shape are circle；On chimney distributor tube wall
The overflow centerline hole of setting is away from tower tray upper surface 50mm.Telescopic subtract of the present invention is rushed in equal flow table, and funnel-shaped distributor exists
It is triangularly arranged on tower tray.The tower tray can be divided into 9 pieces, and sliceable is circular slab, and 3 are set on every piece of cutting plate
A funnel-shaped distributor, the edge of tower tray most outer set flanging, and the height of flanging is generally 50mm.
Hydrogenating materials and process conditions are the same as comparative example 1.
Again after going into operation, the first bed inlet radial temperature profile and maximum temperature difference are shown in Table 1.
Table 1 applies result
| Comparative example 1 | Embodiment 1 | Embodiment 2 | |
| Temperature a, DEG C | 285.3 | 285.8 | 286.0 |
| Temperature b, DEG C | 289.6 | 286.3 | 286.2 |
| Temperature c, DEG C | 278.6 | 286.7 | 286.1 |
| Temperature d, DEG C | 278.3 | 285.5 | 284.6 |
| Temperature e, DEG C | 284.3 | 285.4 | 285.6 |
| Maximum bed radial temperature difference, DEG C | 11.3 | 1.3 | 1.6 |
Claims (26)
1. a kind of telescopic subtract rushes equal flow table, including tower tray and several funnel-shaped distributors being arranged on tower tray；The cigarette
Chimney formula distributor includes downspout and be arranged on downspout upper end subtract punching cylinder；It is described to subtract that rush cylinder and downspout be that both ends are opened
The tubular structure of mouth subtracts and rushes cylinder with downspout in arrangement up and down, and described subtract rushes diameter of the diameter of cylinder more than downspout.
2. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that described subtracting rushes cylinder with downspout in same
Axis, annulus set arrangement.
3. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that described to subtract the bottom edge for rushing cylinder and downspout
Upper edge, which is overlapped or is not overlapped, to be fixedly connected.
4. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that described subtract rushes cylinder and downspout level side
There are the gaps of certain distance between.
5. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that described subtracting is rushed between cylinder and downspout
It is fixed and connects by pull rod or lacing wire.
6. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that the tower tray further include supporting beam and
For fixing the tower tray connector of tower tray.
7. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that it is described subtract rush cylinder on set along opening
Several tooth sockets.
8. rush equal flow table according to telescopic subtract described in claim 7, which is characterized in that the shape of the tooth socket for triangle,
Rectangle is arc-shaped.
9. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that described telescopic subtract rushes equal flow table and fit
The fixed bed reactors that reactor is upper feeding and gas-liquid is cocurrent form, are particularly suitable for fixed bed trickle bed reactor
Form.
10. rush equal flow table according to telescopic subtract described in claim 1 or 9, which is characterized in that telescopic subtract rushes equal flow table
Suitable for being arranged in idle reactor upper cover or being arranged on reactor shell upper end, top distribution plate the upper surface of.
11. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that the lower ending opening of the downspout is straight
It connects and is opened on tower tray or through tray perforation.
12. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that cylinder and the descending liquid are rushed in described subtracting
Being integrated of pipe is made；Cylinder is rushed alternatively, being fixedly connected with a tubular on the upper edge of downspout and subtracting.
13. rush equal flow table according to telescopic subtract described in claim 12, which is characterized in that described is fixedly connected using weldering
It connects, be bolted or screw connection.
14. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that horizontal on the tube wall of the downspout
Direction sets 1~6 spout hole, and the total sectional area of spout hole is the 10%~100% of downspout sectional area.
15. telescopic subtract according to claim 14 rushes equal flow table, which is characterized in that the number of the spout hole is 1~2
A, the total sectional area of spout hole is that the ratio of downspout sectional area is 30%~50%.
16. telescopic subtract according to claim 14 rushes equal flow table, which is characterized in that the shape of the spout hole is circle
Shape, strip, triangle and polygon.
17. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that several funnel-shaped distributors
Triangular in shape on tower tray, quadrangle, diamond shape arrangement.
18. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that the tower tray is divided into several pieces,
And sliceable is circular slab.
19. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that the most outer edge of the tower tray is set
Put flanging folded over upwards.
20. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that the center line of the spout hole is away from tower
5~100mm of panel surface is preferably 30~50mm.
21. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that the height of the downspout for 20~
300mm is preferably 50~120mm；Described subtract rushes the height of cylinder as 30~400mm, is preferably 100~300mm；Subtract and rush the straight of cylinder
Footpath is 30~260mm, is preferably 80~150mm.
22. rush equal flow table according to telescopic subtract described in claim 19, which is characterized in that the height of the flanging for 5~
80mm is preferably 30~50mm.
23. rush equal flow table according to telescopic subtract described in claim 7 or 8, which is characterized in that the height of the tooth socket is to subtract punching
The 1%~20% of cylinder height is preferably 2%~10%.
24. rush equal flow table according to telescopic subtract described in claim 4, which is characterized in that the width in the gap for 5~
200mm is preferably 10~50mm.
25. telescopic subtract described in accordance with the claim 1 rushes equal flow table, which is characterized in that described subtract rushes the sectional area of cylinder as drop
1~8 times of liquid pipe sectional area, preferably 2~6 times.
26. telescopic subtract described in accordance with the claim 3 rushes equal flow table, which is characterized in that described to subtract punching bottom edge and downspout
When partly overlapping, stack height is the 5%~30% of downspout height, is preferably 10%~25%.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611084901.9A CN108114670B (en) | 2016-11-30 | 2016-11-30 | Sleeve type impact reducing and flow equalizing disc |
| RU2017140962A RU2672742C1 (en) | 2016-11-25 | 2017-11-24 | Disc having impact absorbing action and creating uniform flow and reactor |
| TW106140943A TWI664021B (en) | 2016-11-25 | 2017-11-24 | Underflow equalizing plate and reactor |
| SG10201709746QA SG10201709746QA (en) | 2016-11-25 | 2017-11-24 | Impact-Reducing Uniform-Flowing Disc and Reactor |
| GB1719542.1A GB2560066B (en) | 2016-11-25 | 2017-11-24 | Impact-reducing uniform-flowing disc and reactor |
| KR1020170158615A KR101989328B1 (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 |
|---|---|---|---|
| CN201611084901.9A CN108114670B (en) | 2016-11-30 | 2016-11-30 | Sleeve type impact reducing and flow equalizing disc |
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| Publication Number | Publication Date |
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| CN108114670A true CN108114670A (en) | 2018-06-05 |
| CN108114670B CN108114670B (en) | 2021-12-07 |
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| CN201611084901.9A Active CN108114670B (en) | 2016-11-25 | 2016-11-30 | Sleeve type impact reducing and flow equalizing disc |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111617704A (en) * | 2020-05-12 | 2020-09-04 | 中国石油化工股份有限公司 | Hydrogenation reactor inlet diffuser |
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| US20070145610A1 (en) * | 2004-01-15 | 2007-06-28 | Rasmus Breivik | Vapour-liquid distribution tray |
| CN101391197A (en) * | 2007-09-20 | 2009-03-25 | 中国石油化工股份有限公司 | Logistics mixing distribution system |
| US20110011769A1 (en) * | 2009-07-14 | 2011-01-20 | Sutton Clay R | Feed Delivery System For A Solid-Liquid Separation Vessel |
| CN103906563A (en) * | 2011-11-03 | 2014-07-02 | Ifp新能源公司 | Distributor plate for gas/liquid mixture equipped with distributor elements largely insensitive to the lack of horizontality |
| CN103100354A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Gas-liquid distributor capable of reducing catalyst skimming and hydrogenation process |
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| CN111617704A (en) * | 2020-05-12 | 2020-09-04 | 中国石油化工股份有限公司 | Hydrogenation reactor inlet diffuser |
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| CN108114670B (en) | 2021-12-07 |
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