CN108114668A - A kind of baffle plate type, which subtracts, rushes equal flow table - Google Patents
A kind of baffle plate type, which subtracts, rushes equal flow table Download PDFInfo
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- CN108114668A CN108114668A CN201611083262.4A CN201611083262A CN108114668A CN 108114668 A CN108114668 A CN 108114668A CN 201611083262 A CN201611083262 A CN 201611083262A CN 108114668 A CN108114668 A CN 108114668A
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- subtracts
- flow table
- baffle plate
- equal flow
- plate type
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- 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
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Subtract the invention discloses a kind of baffle plate type and rush equal flow table.The baffle plate type, which subtracts, to be rushed equal flow table and includes tower tray and several funnel-shaped distributors for being arranged on tower tray；The funnel-shaped distributor includes a downspout and subtracts punching with what downspout upper end was fixedly connected, and it is arrangement up and down to subtract punching with downspout, and it is parallel with the axis of reactor or at grade to subtract punching.The present invention's subtracts that rush equal flow table be the hydrogenation reactor inner member newly established, it 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.Subtracting for 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, can realize that fluid flow state becomes more meticulous adjusting and the first distribution of material.
Description
Technical field
Subtract the present invention relates to a kind of baffle plate type and rush equal flow table, belong to field of chemical equipment.The baffle plate type of the present invention subtracts
It is the reactor component newly established to rush equal flow table.The baffle plate type of the present invention, which subtracts, rushes equal flow table suitable for various hydrogenation reactions
Device is particularly 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.It next herein will be to comparing in these gas-liquid distributors
More representational structure and its operation principle are introduced.
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 baffle plate type and rush equal flow table.The present invention's subtracts punching
Equal flow table is arranged in the upper cover that reactor leaves unused or is arranged on reactor shell upper end, top distribution plate the upper surface of.
The baffle plate type of the present invention subtracts and rushes equal flow table, for the hydrogenation reactor inner member newly established, available for cutting down fluid
The strong impact power formed into remnants kinetic energy during reactor；Central point is eliminated into the inclined streamline of fashionable formation to distribution plate
" pushing away wave " phenomenon of liquid layer, eliminate fluid autoreactor entrance fall to top distribution plate potential energy and come impact force；It is real
Existing fluid flow state becomes more meticulous adjustings, realize the first distribution function of material or substitute at the top of distribution plate distribution function；It can be top
Distribution plate provides good entry condition.The baffle plate type of the present invention, which subtracts, rushes equal flow table, and distributed effect is good, takes full advantage of reaction
Device end socket 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 baffle plate type, which subtracts, rushes equal flow table, including tower tray and（Vertically）Several funnel-shaped distributors being arranged on tower tray；Often
A funnel-shaped distributor includes a downspout and subtracts punching with what downspout upper end was fixedly connected, subtracts punching and downspout
To arrange up and down, and the punching that subtracts is parallel with the axis of reactor or at grade or with reactor axis into one
Clamp angle.
Further, it is described to subtract punching（Place plane）It is tilted to nearest wall of reactor direction, and subtracts punching institute
Angle between plane and the axis of reactor is 15 °~80 °.
Further, several horizontal spout holes of different shapes are provided on the tube wall of the downspout, in order to liquid
Through the spout hole and along downspout flow down.Certain distance should be maintained between overflow centerline hole and tray deck surface.
The setting quantity of spout hole is generally 1~6, preferably 1~2.The total sectional area of spout hole is chimney distributor tube sectional area
10%~100%, be preferably 30%~50%.When only setting 1 spout hole, it is to subtract pair of punching tie point to set orientation
Face；When setting 2 spout holes, orientation is set on the vertical cross-section parallel with subtracting punching, to be arranged symmetrically.The overflow
The shape in hole can be circle, strip, triangle and polygon, it is preferably circular.
Further, several funnel-shaped distributors should be vertically arranged on tower tray.Funnel-shaped distributor middle pipe
The lower ending opening of shape structure 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, it is preferred to use steel material.It is described to subtract punching and the downspout and be integrated chemical conversion type and be made, it can will such as drop
Liquid pipe and subtract punching（It is flat）Plate integration is processed into；Alternatively, it is done at the top certain position with certain altitude downspout vertical
Straight and horizontal resection, retains the incomplete cutting of wall thickness, then spreads out to be made and subtracts punching；Or along solid on downspout
Surely connect a strip and subtract punching.It is described be fixedly connected welding may be employed, be bolted, snap connection etc. it is various suitable
Suitable mode.
Further, the punching that subtracts preferably is arranged on downspout upper end close to or away from tower tray center（Or the center of circle）One
Side is preferably arranged adjacent to tower tray center（Or the center of circle）One side.It is described subtract punching be arranged at it is nearest with tower tray center or the center of circle
At distance, and the normal for subtracting punching intersects perpendicular to reactor center axis and the two.
Further, the tower tray further includes the supporting beam being used to support below and tower tray connector.
Further, the flanging that setting flips up at the edge of the tower tray most outer.The height of the flanging is general
It should be above the height of set spout hole on tubular structure.
The baffle plate type of the present invention, which subtracts, to be rushed in equal flow table, and described is several（Band subtracts punching）Funnel-shaped distributor is in tower tray
Upper general triangular in shape, quadrangle, diamond shape arrangement.
Further, the tower tray is conventionally divided into several pieces, and can be spliced into circular slab.
In the present invention, the downspout is both fluid passage, while is also the passage of gas circulation.
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 preferably applied to fixed bed trickle bed reactor form, it is larger to be more preferably applied to liquid-gas ratio（Hydrogen to oil volume ratio
It is smaller）, it is larger（If reactor diameter is 4 meters or more）Hydrogenation reactor.
Compared with prior art, baffle plate type of the present invention, which subtracts, rushes equal flow table and has the following advantages that：
1st, baffle plate type of the present invention, which subtracts, rushes equal flow table, the inner member newly established for hydrogenation reactor, by special structure design,
Reduce distributor installation dimension, be easily installed at idle reactor upper cover or be arranged on reactor shell upper end, top
Distribution plate the upper surface of achievees the purpose that save space reactor, improves the space availability ratio of hydrogenation reactor, convenient for loading more
More catalyst or reduction reactor scale.
2nd, baffle plate type of the present invention, which subtracts, rushes in equal flow table, sets a number of funnel-shaped distributor, its upper part cutting, folding
The metallic plate of the elongated metal plate formed or fixed strip is made, for stopping because central feeding causes inclined fluidised form
Fluid is sprayed, its impact force is cut down；Lose kinetic energy fluid be blocked after terrestrial gravitation effect under, by original parallax
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 parallax punching
" pushing away wave " phenomenon that power is formed to liquid layer on tower tray is hit, and uniform entry condition is created to funnel-shaped distributor, passes through cigarette
Material is distributed on the distribution plate of top by chimney formula distributor, is realized just distribution function, and is provided friendly, steady liquid to distributor
Layer, uniform entry condition.The baffle plate type of the present invention, which subtracts, rushes equal flow table, realizes that material is evenly distributed to instead together with distribution plate
It answers on the horizontal cross-section of device.Setting quantity is suitable, has the funnel-shaped distributor for subtracting and rushing flow equalizing function, may replace existing top
Distribution plate realizes evenly distributing for material.
3rd, baffle plate type of the present invention, which subtracts, rushes in equal flow table, by a number of funnel-shaped distributor of setting, compares
The bubble cap distributor of general suction principle, the disperse power of liquid phase distribution are changed to, using potential energy, form splash by gas phase suction,
So as to reduce pressure drop.
4th, baffle plate type of the present invention, which subtracts, rushes in equal flow table, by setting position and the shape in descending liquid tube wall overflow hole,
Rational tower tray liquid storage depth is formed, it is uneven with macro-allocation that level fluctuation is brought to reduce tray level degree deviation.
5th, baffle plate type of the present invention, which subtracts, rushes in equal flow table, using unique design principle and hydrodynamics feature, realizes object
Material evenly distributes, and makes the reduction of catalyst bed radial temperature difference, catalyst bed radial temperature difference≤3 DEG C, since radial temperature difference is anti-
Reflected the distributed effect of fluid, this absolutely proved baffle plate type of the present invention subtract rush equal flow table to the distribution of reaction feed logistics and
Gas-liquid mixed effect is preferable, has certain booster action to hydrogenation catalyst reaction process and catalyst coking control.
6th, baffle plate type of the present invention subtracts the inner member for rushing equal flow table to newly establish in hydrogenation reactor, have it is simple in structure,
Easy for installation, operating flexibility is big, can greatly improve hydrogenation reactor space availability ratio, improvement reactor top divides material inlet item
Part, the radial distribution effect for improving reactor feed effectively eliminate reactor radial temperature difference, eliminate catalyst bed because of material point
Heat spot caused by cloth is uneven, effective use for catalyst in hydrogenation reactor provide excellent entry condition, and reduction is urged
Agent skimming 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 baffle plate type of the present invention subtracts and rushes equal flow table schematic diagram.Wherein 1 is chimney distributor, and 2 be tower tray, and 3 be tower tray
Supporting beam, 4 be tower tray connector, and 5 be spout hole.
Fig. 2 is the structure diagram of chimney distributor of the present invention.For wherein 1-1 to subtract punching, 1-2 is downspout.
Fig. 3 is the structure top view of chimney distributor of the present invention.
Fig. 4 is that baffle plate type of the present invention subtracts and rushes the liquid of equal flow table and flow to schematic diagram.
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, equal flow table is rushed including tower tray 2 and is vertically arranged on tower tray if baffle plate type of the invention subtracts
Do funnel-shaped distributor 1.The funnel-shaped distributor 1 includes a downspout 1-2 and is fixedly connected with downspout 1-2 upper ends
Subtract punching 1-1, the downspout 1-2 is upper and lower ends hatch frame, it is described subtract punching 1-1 it is parallel with the axis of reactor,
Or it forms an angle at grade or with reactor axis.The axis for subtracting punching 1-1 and reactor in Fig. 1 is mutually flat
Row.Subtract center or the center of circle of the punching towards tower tray.The punching that subtracts is arranged at at tower tray center or center of circle minimum distance, and subtracting
The normal of punching intersects perpendicular to reactor center axis and the two.Wherein, it is described to subtract punching 1-1 and downspout 1-2 is usual
It is made of metal.
It is described subtract punching and the downspout being integrated be made, can such as be put down by downspout and strip
Plate integration machine-shaping is made；Alternatively, it is done vertically and horizontally at the top certain altitude of the downspout with certain altitude
Cutting, retains the incomplete cutting of wall thickness, then spreads out to be made and subtracts punching or the edge on downspout（Portion）It is fixed to connect
It connects a strip and subtracts punching structure.Described being fixedly connected may be employed welding, be bolted, snap connection connection etc. respectively
The suitable mode of kind.
In one embodiment of the invention, the funnel-shaped distributor is that vertical and water is done to the upper end of downspout
Truncation is cut, and is retained the incomplete cutting of wall thickness, is then made into tablet.In this embodiment, its upper part cut-point distance
The distance on edge is generally the 10%~60% of funnel-shaped distributor total height on funnel-shaped distributor, is preferably 20%~50%.
In another embodiment of the invention, edge is fixedly connected with an elongated plates structure on downspout, described
The width of elongated plates is 20~300mm, preferably 80~200mm；The length of elongated plates be 50~300mm, preferably 80~
220mm。
Wherein, horizontally arranged several spout holes 5 on the tube wall of downspout middle and lower part.The center line of spout hole is away from tower tray
The distance of upper surface is generally 5~100mm, is preferably 30~50mm.The height of downspout is generally 20~300mm, is preferably
50~120mm.
The baffle plate type of the present invention subtracts and rushes in equal flow table, several funnel-shaped distributors on tower tray can it is triangular in shape, four
Side shape, diamond shape arrangement.Funnel-shaped distributor is usually plugged on by downspout lower end on tower tray, and can pass through welding, screw thread
It the modes such as connects, snap connection to be fixedly connected.
Baffle plate type of the present invention, which subtracts, to be rushed in equal flow table, and the tower tray 2 can be divided into several pieces, and sliceable for circle
Plate.The edge of tower tray most outer sets flanging, and the height of flanging is generally 5~80mm, is preferably 30~50mm.
With reference to Fig. 1-4, the present invention subtracts 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
To subtracting on punching for funnel-shaped distributor top, it can effectively stop the fluid sprayed in oblique line fluidised form, its impact force is cut
Subtract tune, and fluid falls naturally under gravity after being blocked, losing kinetic energy, forms vertical fluidised form, and fall to subtracting punching
On the tray deck of equal flow table.Since downspout overflow discharge orifice, that is, material channel is in horizontally disposed and apart from tray deck with certain high
Degree is poor, thus liquid phase material can form the liquid layer with certain altitude on the tray deck for rushing equal flow table is subtracted, even if tray level
Degree still can ensure that each distributor with the presence of liquid phase there are deviation.Due to large number of, the catalyst bed layer surface of distributor
Any one point has a certain number of distributors working so that the distributor uniformity is protected.Liquid phase material is from chimney
The overflow hole path opened up on formula distributor descending liquid tube wall flows into distribution pipe（Downspout）It is interior, realize the first distribution of liquid.
Since the liquid phase material after over-subtraction rushes equal flow table has been converted into vertical fluidised form, and kinetic energy when being assigned on the distribution plate of top
It disappears, therefore to the liquid layer on the distribution plate tray deck surface of top there is no thrust, so as to eliminate material on distribution plate
" pushing away wave " phenomenon of liquid layer provides friendly, steady liquid layer, uniform entry condition, with top distribution plate to top dispenser
Material being uniformly distributed on catalyst bed is realized together.
When liquid phase material amount is less in the operating mode of reactor application or catalyst bed top filling tooth spherical shape shape protection
When agent or hollow ball-type protective agent, baffle plate type of the invention, which subtracts, rushes equal flow table, can substitute top distribution plate, realization subtract punching,
It flows and distributes integration.Inside reactor structure can thus be greatly simplified, reduce investment.
Illustrate the reaction effect of the present invention, but the protection model being not intended to limit the present invention with reference to specific embodiment
It encloses.
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
Maximum temperature difference is shown in Table 1.
Embodiment 1
After transformation, the baffle plate type that the present invention is added in upper cover subtracts and rushes equal flow table, using baffle plate type as shown in Figure 1
Subtract and rush equal flow table and be applied in combination with common ERI type bubble cap formula gas-liquid allotters.Subtract the major parameter for rushing equal flow table：Band subtracts punching
Chimney distributor do and vertically and horizontally cut for the top of chimney distributor, retain the incomplete cutting of wall thickness, then by it
Tablet is made.Its upper part cut-point is on funnel-shaped distributor along the 40% of preferably funnel-shaped distributor total height；Downspout
Horizontally arranged circle spout hole, sets quantity 2 on the tube wall of middle and lower part；It sets orientation to be parallel with subtracting punching vertical
On section, it is arranged symmetrically.The total sectional area of spout hole is the 30% of downspout sectional area.Overflow centerline hole is away from tower tray upper table
Face is preferably 40mm.Highly preferred downspout is 50mm.The baffle plate type of the present invention, which subtracts, to be 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 catalyst bed entrance radial temperature and most
The big temperature difference is shown in Table 1.
Embodiment 2
After transformation, the swash plate type that subtracts that the present invention is added in upper cover subtracts and rushes equal flow table, eliminates the ability in former reactor
The ERI type gas-liquid allotters of domain routine, wherein, subtract the major parameter for rushing equal flow table：The chimney distributor that band subtracts punching is chimney
The top of distributor, which is done, vertically and horizontally cuts, and retains the incomplete cutting of wall thickness, is then made into tablet.Its upper part is split
Point is on funnel-shaped distributor along the 40% of preferably funnel-shaped distributor total height；On chimney distributor upper, middle and lower portion tube wall
Horizontally arranged circle spout hole, sets quantity 2；It sets orientation as on the vertical cross-section parallel with subtracting punching, in pair
Claim arrangement.The total sectional area of spout hole is the 30% of downspout sectional area.Overflow centerline hole is preferably away from tower tray upper surface
40mm.Highly preferred downspout is 50mm.The baffle plate type of the present invention, which subtracts, to be rushed in equal flow table, and funnel-shaped distributor is on tower tray
Triangular arrangement.The tower tray can be divided into 9 pieces, and sliceable for circular slab, set on every piece of cutting plate 3 it is 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 catalyst bed entrance radial temperature profile
And the temperature difference is shown in Table 1.
Table 1 applies result
| Comparative example 1 | Embodiment 1 | Embodiment 2 | |
| Temperature a, DEG C | 370.5 | 365.5 | 364.4 |
| Temperature b, DEG C | 367.3 | 366.2 | 365.0 |
| Temperature c, DEG C | 363.6 | 365.8 | 365.3 |
| Temperature d, DEG C | 361.0 | 365.7 | 365.9 |
| Temperature e, DEG C | 369.8 | 366.9 | 364.8 |
| Maximum bed radial temperature difference, DEG C | 9.5 | 1.2 | 1.5 |
Claims (26)
1. a kind of baffle plate type, which subtracts, rushes equal flow table, including tower tray and several funnel-shaped distributors being arranged on tower tray；Each institute
The funnel-shaped distributor stated includes a downspout and subtracts punching with what downspout upper end was fixedly connected, and subtract punching is with downspout
Arrangement up and down, and the punching that subtracts is parallel with the axis of reactor or at grade or with reactor axis into certain
Angle.
2. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the most outer edge of the tower tray is set
Put the flanging flipped up.
3. subtract according to the baffle plate type described in claim 1 or 2 and rush equal flow table, which is characterized in that on the tube wall of the downspout
It is provided with spout hole.
4. baffle plate type described in accordance with the claim 3, which subtracts, rushes equal flow table, which is characterized in that the center line and tower of the spout hole
Certain distance should be kept between plate surface.
5. baffle plate type described in accordance with the claim 3, which subtracts, rushes equal flow table, which is characterized in that the total sectional area of the spout hole is
The 10%~100% of downspout sectional area is preferably 30%~50%.
6. baffle plate type described in accordance with the claim 3, which subtracts, rushes equal flow table, which is characterized in that the setting quantity of the spout hole
For 1~6.
7. subtract according to the baffle plate type described in claim 6 and rush equal flow table, which is characterized in that when only setting 1 spout hole,
It is to subtract the opposite of punching tie point to set orientation；When setting 2 spout holes, orientation is set to be parallel with subtracting punching vertical
On section, it is arranged symmetrically.
8. subtract according to any baffle plate types of claim 3-7 and rush equal flow table, which is characterized in that the shape of the spout hole
For circle, strip, triangle or polygon.
9. subtract according to any baffle plate types of claim 3-7 and rush equal flow table, which is characterized in that the height of the flanging is not
Less than the height of set spout hole on downspout.
10. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the deflector type, which subtracts, rushes equal flow table
The fixed bed reactors that applicable reactor is upper feeding and gas-liquid is cocurrent form.
11. baffle plate 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
Directly it is opened on tower tray or through tray perforation.
12. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the tower tray is further included under it
The supporting beam and tower tray connector being just used to support.
13. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the funnel-shaped distributor is adopted
It is made of steel material.
14. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that described subtracts punching and downspout
Being integrated is made；It vertically and horizontally cuts, retains alternatively, being done in the top certain position with certain altitude downspout
The incomplete cutting of wall thickness, then spreads out to be made and subtracts punching；Or subtract on downspout along being fixedly connected with a strip
Punching.
15. subtract according to the baffle plate type described in claim 12 and rush equal flow table, which is characterized in that described is fixedly connected using weldering
It connects, be bolted, be buckled connection.
16. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the punching that subtracts is arranged on drop
Liquid pipe upper end is close to or away from tower tray center or the one side in the center of circle.
17. baffle plate type according to claim 14, which subtracts, rushes equal flow table, which is characterized in that the punching that subtracts is arranged on drop
Liquid pipe upper end is close to tower tray center or the one side in the center of circle.
18. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that it is equal that the baffle plate type subtracts punching
Flow table is arranged in the upper cover that reactor leaves unused or is arranged on reactor shell upper end, top distribution plate the upper surface of.
19. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that several funnel-shaped distribution
Device is triangular in shape on tower tray, quadrangle or diamond shape are arranged.
20. baffle plate 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
Block, and sliceable is circular slab.
21. subtract according to the baffle plate type described in claim 4 and rush equal flow table, which is characterized in that the center line of the spout hole away from
The distance of tower tray upper surface is 5~100mm.
22. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that the height of the downspout is 20
~300mm.
23. baffle plate type described in accordance with the claim 2, which subtracts, rushes equal flow table, which is characterized in that the height of the flanging for 5~
80mm。
24. baffle plate type according to claim 14, which subtracts, rushes equal flow table, which is characterized in that the positional distance of the cut point
The distance on edge is the 10%~60% of funnel-shaped distributor total height on funnel-shaped distributor.
25. baffle plate type according to claim 14, which subtracts, rushes equal flow table, which is characterized in that the width for subtracting punching is 20
~300mm, the length for subtracting punching are 50~300mm.
26. baffle plate type described in accordance with the claim 1, which subtracts, rushes equal flow table, which is characterized in that subtracts the plane where punching to most
Near wall of reactor direction tilts, and the angle between the axis of reactor is 15 °~80 °.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611083262.4A CN108114668B (en) | 2016-11-25 | 2016-11-25 | Baffle type impact-reducing 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 |
|---|---|---|---|
| CN201611083262.4A CN108114668B (en) | 2016-11-25 | 2016-11-25 | Baffle type impact-reducing flow-equalizing disc |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108114668A true CN108114668A (en) | 2018-06-05 |
| CN108114668B CN108114668B (en) | 2020-06-05 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611083262.4A Active CN108114668B (en) | 2016-11-25 | 2016-11-25 | Baffle type impact-reducing flow-equalizing disc |
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| CN (1) | CN108114668B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52131973A (en) * | 1976-04-28 | 1977-11-05 | Mitsubishi Kakoki Kk | Continuous multiistage fluidized layer type soliddliquid contact apparatus |
| CN2325104Y (en) * | 1998-03-13 | 1999-06-23 | 王立英 | Collision type gas/liquid distributing equipment with layer tower structure |
| RU2259229C2 (en) * | 2003-10-29 | 2005-08-27 | ООО Инженерная фирма "ПНЭк" | Distributing apparatus |
| CA2538401C (en) * | 2003-09-10 | 2013-03-12 | Uhde Gmbh | Multi-phase liquid distributor for a tube-bundle reactor |
| CN205216809U (en) * | 2015-11-25 | 2016-05-11 | 中石化洛阳工程有限公司 | Gas -liquid distributor |
-
2016
- 2016-11-25 CN CN201611083262.4A patent/CN108114668B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52131973A (en) * | 1976-04-28 | 1977-11-05 | Mitsubishi Kakoki Kk | Continuous multiistage fluidized layer type soliddliquid contact apparatus |
| CN2325104Y (en) * | 1998-03-13 | 1999-06-23 | 王立英 | Collision type gas/liquid distributing equipment with layer tower structure |
| CA2538401C (en) * | 2003-09-10 | 2013-03-12 | Uhde Gmbh | Multi-phase liquid distributor for a tube-bundle reactor |
| RU2259229C2 (en) * | 2003-10-29 | 2005-08-27 | ООО Инженерная фирма "ПНЭк" | Distributing apparatus |
| 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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| Publication number | Publication date |
|---|---|
| CN108114668B (en) | 2020-06-05 |
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