CA2019928A1 - Two direction inlet fluid distributor for downflow vessel containing bed of solid particles - Google Patents
Two direction inlet fluid distributor for downflow vessel containing bed of solid particlesInfo
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- CA2019928A1 CA2019928A1 CA 2019928 CA2019928A CA2019928A1 CA 2019928 A1 CA2019928 A1 CA 2019928A1 CA 2019928 CA2019928 CA 2019928 CA 2019928 A CA2019928 A CA 2019928A CA 2019928 A1 CA2019928 A1 CA 2019928A1
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- fluid
- inlet
- distributor
- bed
- outlet
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Abstract
"TWO DIRECTION INLET FLUID DISTRIBUTOR FOR
DOWNFLOW VESSEL CONTAINING BED OF SOLID PARTICLES
ABSTRACT
An inlet distributor for a fluid-solid contacting vessel uses a two direction distributor to prevent bed surface disturbances at high inlet velocities and high particle loadings. The distributor uses a series of partitions to peel off portions of the downward fluid flow and redirect them radially outward. Each outwardly directed fluid flow component passes through a series of perforations to effect any necessary circumferential redistribution before entering the space above the particle bed. By subdividing the fluid flow into a number of radially directed flow portions and circumferentially redistributing these flow portions, cross-currents and eddy currents on the particle bed surface are minimized or avoided so that disturbances at the bed surface are eliminated. This low pressure drop distributor is particularly effective in vessels having particles loaded to within a short distance of bed inlets and where elbows or other upstream flow devices introduce nonuniformities into the fluid flow to a particle bed.
DOWNFLOW VESSEL CONTAINING BED OF SOLID PARTICLES
ABSTRACT
An inlet distributor for a fluid-solid contacting vessel uses a two direction distributor to prevent bed surface disturbances at high inlet velocities and high particle loadings. The distributor uses a series of partitions to peel off portions of the downward fluid flow and redirect them radially outward. Each outwardly directed fluid flow component passes through a series of perforations to effect any necessary circumferential redistribution before entering the space above the particle bed. By subdividing the fluid flow into a number of radially directed flow portions and circumferentially redistributing these flow portions, cross-currents and eddy currents on the particle bed surface are minimized or avoided so that disturbances at the bed surface are eliminated. This low pressure drop distributor is particularly effective in vessels having particles loaded to within a short distance of bed inlets and where elbows or other upstream flow devices introduce nonuniformities into the fluid flow to a particle bed.
Description
2~199~8 "TWO DIRECTION INL~T FLUID DISTRIBUTOR FOR
DOWNFLOW VESSEL CONTAINING_BED OF SOLID PARTICLES' BACKGROUND OF THE INVENTTQN
This invention relates generally to the field of fluid-solid contacting. More specifically, this invention deals with the delivery of fluids to beds of particulate material.
Fluid-solid contacting deYices have a wide variety of application~. Such devices find common application in processes for hydrocarbon conversion and adsorption columns for separation of fluid components. When the fluid-solid contacting device is an adsorption column, the particulate material will comprise an adsorbent through which the fluid passes. In the case of hydrocarbon conversion, the fluid-solid contacting apparatus is typically a reactor containing c~talyst. Typical hydrocarbon conversion reactions that may be carried out are hydrogenation, hydrotreating, hydrocracking, and hydrodealkylation.
Fluid-solid contacting devices to which this invention apply are arranged as an elongated cylinder or vessel usually having a vertical orientation through which an essentially vertical flow of fluid is maintained.
Particulate material contained in this vessel is arranged in one or more beds. Fluid enters the vessel through an inlet located at an ups~ream end o~ the vessel. It is also commonly known to add or withdraw fluid from between the particulate beds. This is commonly done in adsorption schemes where the composition of the fluid passing between particle beds i5 changing or in hydrocarbon conversion processes where a ~uench system is used to cool fluid as it passes between beds.
Changes in the composition or properties of the fluid passing through the particular zone present little problem provided these changes occur uniformly. In 2 2~19~28 adsorpkion systems these changes are ~he resul~ of retention or displacement o~ fluids within the adsorbent.
For reaction systems changes in temperature as well as composition of the fluid are caused by the parkiculate catalyst material contained in the beds.
Nonuniform flow of fluid through these beds can be caused by poor initial mixing o~ the fluid entering the bed and/or variations in flow resistance across the particulate bed. Variations in the flow resistance across the bed can vary contact time of the fluid within the particles thereby resulting in uneven rsactions or adsorption of the fluid stream passing through the bed.
In extreme instances, this is referred to as channeling wherein fluid over a limited portion of the bed is allowed to move in a narrow open area with virtually no resistance to flow. When channeling occurs, a portion of the fluid passing through the bed will have minimal contact with the particulate matter of the bed. If the process is one of adsorption, the fluid passing through the channel area will not be absorbed, thereby altering the c~mposition of this fluid with respect to fluid passing through other portions of the bbsorbent bed. For a catalytic reaction, the reduction in catalyst contact time will also ~lter the - ~ product composition of fluid as it leaves different portions of the catalyst bed.
In addition to problems of fluid composition, irregularities in the particulate bed can al50 affect the density and temperature of the ~luid passiny through the bed. For many separation processes retained and displaced components of the fluid have different densities which tend to disrupt the flow profile through the bed.
Nonuniform contacting with the adsorbent p~rticles will exacerbate the problem by introducing more variation in the density of the fluid acro~s the bed thereby further disrupting the flow profile of the ~luid as it passes through the particle bed.
DOWNFLOW VESSEL CONTAINING_BED OF SOLID PARTICLES' BACKGROUND OF THE INVENTTQN
This invention relates generally to the field of fluid-solid contacting. More specifically, this invention deals with the delivery of fluids to beds of particulate material.
Fluid-solid contacting deYices have a wide variety of application~. Such devices find common application in processes for hydrocarbon conversion and adsorption columns for separation of fluid components. When the fluid-solid contacting device is an adsorption column, the particulate material will comprise an adsorbent through which the fluid passes. In the case of hydrocarbon conversion, the fluid-solid contacting apparatus is typically a reactor containing c~talyst. Typical hydrocarbon conversion reactions that may be carried out are hydrogenation, hydrotreating, hydrocracking, and hydrodealkylation.
Fluid-solid contacting devices to which this invention apply are arranged as an elongated cylinder or vessel usually having a vertical orientation through which an essentially vertical flow of fluid is maintained.
Particulate material contained in this vessel is arranged in one or more beds. Fluid enters the vessel through an inlet located at an ups~ream end o~ the vessel. It is also commonly known to add or withdraw fluid from between the particulate beds. This is commonly done in adsorption schemes where the composition of the fluid passing between particle beds i5 changing or in hydrocarbon conversion processes where a ~uench system is used to cool fluid as it passes between beds.
Changes in the composition or properties of the fluid passing through the particular zone present little problem provided these changes occur uniformly. In 2 2~19~28 adsorpkion systems these changes are ~he resul~ of retention or displacement o~ fluids within the adsorbent.
For reaction systems changes in temperature as well as composition of the fluid are caused by the parkiculate catalyst material contained in the beds.
Nonuniform flow of fluid through these beds can be caused by poor initial mixing o~ the fluid entering the bed and/or variations in flow resistance across the particulate bed. Variations in the flow resistance across the bed can vary contact time of the fluid within the particles thereby resulting in uneven rsactions or adsorption of the fluid stream passing through the bed.
In extreme instances, this is referred to as channeling wherein fluid over a limited portion of the bed is allowed to move in a narrow open area with virtually no resistance to flow. When channeling occurs, a portion of the fluid passing through the bed will have minimal contact with the particulate matter of the bed. If the process is one of adsorption, the fluid passing through the channel area will not be absorbed, thereby altering the c~mposition of this fluid with respect to fluid passing through other portions of the bbsorbent bed. For a catalytic reaction, the reduction in catalyst contact time will also ~lter the - ~ product composition of fluid as it leaves different portions of the catalyst bed.
In addition to problems of fluid composition, irregularities in the particulate bed can al50 affect the density and temperature of the ~luid passiny through the bed. For many separation processes retained and displaced components of the fluid have different densities which tend to disrupt the flow profile through the bed.
Nonuniform contacting with the adsorbent p~rticles will exacerbate the problem by introducing more variation in the density of the fluid acro~s the bed thereby further disrupting the flow profile of the ~luid as it passes through the particle bed.
3 2~19~28 In r~action zones, temperature variations are most often associated with nonuniform catalyst ~ontact due to the endothermic or exothermic nature of such sys~ems.
Nonuniform contact with the catalyst will adversely affect the reaction taking place by overheating or overcooling the reactants. This probl~m is most severe in exothermic reactions where the hiyher temperature ~an cause ~urther reaction of feedstock or other fluid component~ into undesirable products or can introduce local hot spots that will cause damage to the catalyst and/or mechanical components.
Non-uniform fluid flow into the vessel can disrupt the top surface of the bed. The disruption results from transverse fluid flow across the surface of the bed at velocities sufficient to move the individual bed particles. For a confined bed, this disruption or movement of the particles will cause the particles to abrade against each other generating smaller particles which are referred to as fines. These fines may increase pressure drop within the bed or escape from the bed thereby reducing the overall quantity of particles in the bed and possibly interfering with downstream operations.
~n unconfined beds, transverse fluid flow may also shi~t large quantities of particles so that the bed surface is highly irregular.
These transverse currents are the result o~
charging fluid into a relativsly large diameter vessel khrough a relatively small diameter nozzle. Charging fluid into the vessel through a small diameter nozzle produces a high velocity jet that extends from the nozzle into the vessel. Impact of this iet on or adjacent to the surface of a relatively closed catalyst bed flares the fluid outward thereby producing eddy currents and fluid velocities transverse to the bed surface~ The inlet effects associated with the r~latively small diameter nozzle are compounded by the usual presence of an elbow just upstream of the nozzle which introduces another 4 20~28 transvers~ velocity component into the flUid flow entering the vessel. The overall result of these inle~ eff~cts is often the piling up of particles around the periphery of the particle bed or the shifting of particles from one side of the bed to the other.
These detrimental inlet effects are a~oided by uniformly dispersing the fluid as it enters the vessel.
Uniform dispersal can be obtained by providing a sufficient length between the nozzle and the catalyst bed lo surface ~uch that ~he fluid jet and any transverse velocitie~ are substantially dissipated upstream of the particle bedO However, in most cases, it is impractical to provide the length necessary for dissipation of the inlet effects due to the excessive vessel tangent length that would be required. In fact, the trend in many industries is to decrease the length b~tween the inlet nozzle and the particle bed surface in order to increase the total volume of particles in the vessel and thereby obtain greater fluid throughput or gr~ater particle bed service life.
For these reasons, inlet distributors are commonly used to break up the fluid jet and redistribute fluid flow over the top surface of a particle bed. One such device ~ ~ is shown in U.S. Patent 2,925,331 issued to Kazmierczak et al. where a fluid stream is downwardly directed onto the upper surface of ~he catalyst bed and passes first through a distributor consisting of a series o~ annular plates having inner diameters that progressively decrease in the direction of fluid flow so that portions of the Xluid stream are in e~fect peeled off and redirected radially outward over the surfac~ of the particle bed. It is also known in the hydrocarbon processing industry to attach cylindrical rings extending in the direction of fluid ~low to the inner edge of the annular plates. Another type of distributor used to redirect and remix fluid flow upstream o a particle bed is shown in U.S. Patent 3,598,541 issued to Hennemuth et al. and U.S. Patent 3,598,542 issu~d to 2 ~ 2 8 Carson et al. ~he Hennemuth distributor uses a series of circumferentially spaced holes ~o redistribute ~luid within a fluid mixing device that communicates with the upper surface of a particle bed. The distributor disclosed in Carson uses a series of circumferentially spaced holes to radially discharge fluid across the upper surface of a particle bed. Thus, the prior art is well acquainted with a number of distribution devices for use in ~luid solid contacting vessels.
Despite the use o~ different inlet distributors, bed disruption remains a problem. Distri~utors that use the annular plates or baffles of the Kazmierczak device reduce the severity of bed disturbances but have not eliminated it. Therefore, large scale shifting of particle bed surfaces, especially where fluid inlet velocities are high, still occurs. Such disruption i5 still known to occur even in cases where straightening vanes and other flow distribution devices are added to the upstream elbow as a means of eliminating a resulting ~ransverse flow component. It has now been discover~d that despite the presence of the baffles and additional redistribution devices, such as straightening vanes, fluid flow entering the vessel still remembers the change of - ~ direction that took place upstream o~ the inlet nozzle and a distribution device that disperses ~he fluid in two directions is needed to overcome these problems.
SUMMARY OF THE INVENTION
Therefore, it is an object of this invention to improve fluid dispersal over the surface of a particulate bed.
It is a further object of this invention to prevent disruption of the top surface of the bed.
It is a yet further ~bjective of this invention to dissipate inl~t effects such as jets and transverse currents associated with fluid flow into a vessel while 6 2~1~928 minimizing the distance betw~en the inlet nozzle and the particle bed sur~ace.
Another object of this invention is to provide a fluid distributor that eliminates transverse velocity components that enter the vessel through a relatively small nozzle.
These and other objects are satisfied by ~he device of this invention which is the first inlet distributor to radially and circumferentially redirect a majorit.y of an axial fluid flow over the surface o~ a par~icle bed. This two direc~ion redistribution dissipates~nQnuniform transverse velocity components and eddy currents that were not eliminated by cther inlet distributors. More specifically, this invention is a fluid distributor that divides a principally axial flow of fluid into a series of flow passages. These flow passages end in cylindrical outlet bands having uniformly spaced apertures about their circumference that provide a small pressure drop for circumferentially redistributing the fluid leaving each passage. The cylindrical bands of apertures are progressively spaced at increasing distanres from the inlet nozzle to increase the dispersal of ~luid flow over the entire particle bed surface.
- t Accordingly, in one embodiment, this invention is a fluid distributor comprising a conduit, a plurality of partitions, and a series of perforations. The ~onduit has an inlet for receiving a fluid stream. The plurality of partitions subdivide most of the cross-sectional area o~
the conduit into at least two annular collection zones.
The partitions also define, at least in part, a series of outlet bands that are centered about the longitudina7 axis of the conduit. Each outlet band is located at the end ~f one collection zone and the outl~t bands have an arrangement wherein the outermost collection zone ends with the outlet band located nearest the inlet and each successive inwardly spaced collection zone ends with an outlet band having an increased ~pacing from the inlet, 7 2~19928 The series of per~orations are spaced at regular intervals about the circumference o~ each b~nd to circumferentially redistribute ~luid flow out of ea~h outlet band.
In a second embodiment, this invention is a fluid 5 distributor that compris~s a cylindrical cont~iner, a plurality of partitions, an~ aperatures spac~d uniformly about the circumference of the container. The cylindrical csntainer has a primary inlet at one end and a closure plate at the opposite end. The plurality of partitions lo are located in the container and define a series of annular inlets inside the container and a sQries o~
cylindrical outlet bands along the wall of thP container.
The partitions communicate each inlet with one outlet and change the direction of fluid flow between the annular inlets and the outlets. A portion of the apertures lie within each cylindrical outlet band. The apertures are uniformly spaced circumferentially about each outlet band and provide a small pressure drop for circumferentially redistributing fluid flow out of each band.
Yet another embodiment involves a method of distributing a fluid straam across a bed of solid particles located in a downflow vessel having a fluid inlet and outlet comprising providing the flow distribution apparatus of the first or second embodiment in the fluid inlet to the vessel and charging the ~luid stream to said inlet at conditions s~lected to achieve two direction flow distribution prior to contact with said bed.
Additional objects, embodi~ents, aspects, and details of this invention are set forth in the following detailed description.
BRIEF DESCRIPTION OF TRE DRAWINGS
Figure 1 shows an arrangement of a downflow reactor having an inlet distributor and a particle bed.
8 2 ~ 2 ~
Figure 2 is one form of the inlet distributor of this invention.
Fi~ure 3 is an ~lternate form of the inlet distributor of this invention.
Figure 4 is a bottom view of the inlet distributor of Figure 3.
DETAILED DESCRIPTTON OF 'rHE INVENTION
The distributor of this invention can b~ u~ed in conjunction with any particle bed. Typically, the particle bed and inlet distributor will be located inside a vessel for a catalytic reaction or an adsorption process. This inVentiQn finds greatest advantage when us~d with a vessel having a downward flow of fluid ~rom an inlet nozzle through an unconfined bed of particles. The invention can also be used with confined particle beds.
In confined particle beds, large scale shifting of the upstream bed surface is not a concern due to restraint by a screen or other confining device but disturbance of the bed surface can still cause attrition and wear of the particles. Thus, while best suited for downflow type vessel, this invention can also be used in vessels where fluid flow i~ primarily horizontal or even up~low.
Most arrangements for piping fluid to the particle ~eds will dictate the use o~ pipe bend or ~lbow ju~t upstream of the inlet supplying fluid above a particle bed surface. Passage through the bend concentrates ~luid flow in the outer radius of the bend. The distributor of this invention is ~specially effective in preventing the bend affect from contributing to bed disturbances~ Bend effects are corrected by circumferentially redistributing the annularly segreyated portions of the fluid flow to the particle bed.
Fluid entering the distributor of this invention may be gaseous phase, liquid phase, or a combination of the two. Greatest advantage is obtained when the fluid 9 2~1 9~28 stream entering through the inl~t distributors is in gas phase.
This invention is more fully explained in the context of a typical downflow vessel arrangement as shown in Figure 1. The remainder of this description refers to the fluid as a gas~ ~his reference is not meant to limit the invention to gas phase flow. Referring again to Figure 1, an upper pipe 10 delivers a gas phas2 fluid to a ve~s 1 12 through an inlet nogzle 14 which is connected to pipe 10 through a pipe swedge 16 and an elbow 18. If unrestricted, discharge of the fluid from elbow 18 would produce a gas jet and also introduce a transverse velocity component into the gas stream that enters vessel 12.
However, all of the gas flow that enters vessel 12 is intercepted first by distributor 20. Distributor 20 has an inlet plate 22 sandwiched between the bottom of pipe swedge 16 and the top of inlet nozzle 14.
Sandwiching plate 22 between pipe swedge 16 and inlet 14 secures distributor 20 to vessel 12 and provides a seal between pipe swedge 16 and inlet plate ~2 that prevents fluid from entering vessel 12 without first passing through distributor 20. Other well-known means of attaching distributor 20 to vessel 12 or pipe swedge 16 - ~ can be used. Nevertheless, whatever method of attachment is used, it is important that the method prevent bypassing of fluid around distributor 20 and into the vessel 12.
This bypassing can produce concentrated jets of fluid ~low that will diminish or defeat the effect of distributor 20.
In a manner hereina~ter described, distri~utor 20 disperses the gas over the cross-section of vessel 12.
The dispersed gas enters a particle bed 24 having an upper sur~ace 25. Bed 24 is composed of solid particles which can be in the form of pills, spheres, cylinders, or any other desired shape. The actual properties of the particles will depend upon the process which is carried out in the containment vessel. Generally, the particles will either function as an adsorbent or as a catalyst. As lo 2~9928 a further m~ans of preventing bed disturbances, a laysr of support material, usually comprising ceramic balls, may be added and comprise the upper ~urface of the particle bed.
In the case of a downflow reactor, bed surface 25 will simply consis~ of particles that have been leveled at the time of loading. In the case of a confined catalyst bed, a screen or other layer of laminar ma~erial will be at the level of surface 25. As gas passes across upper surface 25, it proceeds down through the remainder of bed 24.
Once the gas has moved a short distance past the bed surface, provided the surface remains level, a complete redist~ibution of the gas is ef~ected such that it will pass uniformly through the remainder of the bed.
Therefore, it is not essential that distributor 20 provide a completely uniform distribution of gas across the bed sur~ace 2S. The purpose of distributor 20 is to provide a fluid, or in this case gas, dispersion that has enough uniformity to eliminate any eddy or cross-currents having sufficient velocity to disrupt surface 25. After a predetermined contact time, gas leaves the catalyst bed 24 by passing through a porou~ support member 26~ Member 26 can be screen or any other rigid layer of porous material having sufficient strength to support the weight and ~ ~ pressure loading of catalyst bed 24. Exiting gases pass through an outlet screen 28 that collects any ~ine particles that have passed out of a catalyst bed and through support member 26. From screen 28, exiting gases leave the veesel 12 through an outlet nozzle 30 which is connected to a lower pipe 32.
The ~unctlon of distributor 20 in dlspersing fluid can be more fully appreciated by a consideration of the device shown in Figure 2 which is one form of a two direction distributor designed in accordance with this invention. Figure 2 shows inlet plate 22 having a series of perforations 34 which collectively provide an inlet for gas flow into the distributor. Although pre*erred, it is not necessary that perforations 34 be used across the 11 2~19928 inlet of plate 22. Inlet plate 22 may be provided with a few large openings or a sinyle opening. The use of perforations increases the uniformity of the gas flow int~
the distributor the advantage of which must be balanced against an increased pressure drop across the inlet.
Therefore, pressure drop considerations will control the number and size of openings in inlet plate 22. In normal practice, the holes in the inlet plate will be sized to provide a pressure drop at least equal to twice the velocity head of the incoming gas stream. The opening or openings may extend as far as the wall of a conduit 36 that receives the gas flow passing throuqh inlet plate 22.
A series of partitions 42, 44, 46, 48, 50, and 52 divide the projection of the cross-sectional area of conduit 36 into a series of annular collection zones. A series of outlet bands 54, 56, 58, 60, 62, and 64 are associated respectively with one of the partitions to define the collection zones as that volume lying in both the space above a given partition and the cylindrical space confined by each outlet band. The collection zone associated with partition 42 and outlet band 54 takes the outermost annular layer of gas flow passing through conduit 36 and redirects it in a radial direction out o~ series of ~ ~ apertures 66 located in outlet band 54. Apertures 66, in this case, are simply a series o~ holes spaced circumferentially about outlet 54 at a uni~orm spacing.
The pressure drop across opening 66 is kept low so that the horizontal velocity component created by the impact of gas flou against partition 42 will be preserved and contribute to the radial momentum of the gas as it leaves the distributor~ Holes 66 serve the important function of circumferentially redistributing the gas flow at each partition. Thereforel a completely open outlet band, as practiced in the prior art, does not provide the necessary pressure drop for circumferential redistribution. A
minimum pressure drop in excess of the radial velocity head and preferably several times greater than the radial 12 2 ~ 2 8 velocity head across the opening 66 will provide the necessary circumferential redistribution. The collection zones associated with the downstream par~itions 44, ~6, 48, 50, and 52 take the remaining gas flow ~rom annular layers of progressively decreasing diameter and redirects it radially outward. The gas flow de~lected by each partition passe~ through apertures 66 of its respective outlet band whi~h circumferential}y redistribute the flow in the manner described.
Fluid that passes below partition 52 enters a final outlet arrangement which, in this case, consists o,f an outlet band 68 and a bottom plate 70. End plate 70 is usually imperforate. When end plate 70 has a large diameter relative to the bed, small perforations may be provided to direct a small portion of the gas downwardly onto the center of the particle bed to avoid the foxmation of a dead space below the distributor which could again introduce eddy currents above the bed. However, the majority of the gas flow passing below parti~ion 52 is radially redirected through outlet band 68. Any gas flow permitted through an opening in plate 70 should not exceed the volum~tric gas addition that satisfies the average gas flow requirements through the central por~ion of the bed ~ ~ that is not in the immediate flow path of the radially discharged gas. Gas flow through plate 70 can produce a jet which can impact and distuxb the downstream bed sur~ace. Therefore, jet length con~iderations may limit the siæe of any opening in plate 7Q.
The configuration of distributor 20 will vary depending primarily on the geometry of the vessel in which it is inserted and the number and type of collection zones. The length of conduit 36 between inlet plate 22 and the ~irst outlet band is sized to get the apertures 66 below the inlet nozzle 14 ~o that the radially directed fluid passing therethrough does not impinge on the nozzle wall. The number of collection zones us~d in a particular distributor will vary with the velocity of gas flow, the 13 2~928 relative size of the inlet nozzle and vessel, and the susceptibility of the particl~ bed to ~low-induced disturbance. Two or more collection zones may be used.
Generally, the more collection zones used, the better the distribution across the catalyst beds. In the specific configuration of the Figure 1 distributor increasing the width of the partitions will increase the radial gas ~low at each outlet band. Adjusting the size and number o~
apertures in each outlet band will also vary the radial gas velocity or through aperatures in dif~erent outlet bands. By appropriate sizing of the collection zones and aperatures, this distributor can provide good gas dispersion over a particle bed of almost any shape or size.
An alternate and often preferred arrangement for the distributor of this invention is shown in Figure 3.
In this case, the diskributor consists of an inlet plate 22', a cylindrical container 72, an upper partition 74, intermediate partitions 76, a lower partition 78, and an end plate 80. The upper end of container 72 referred to as the inlet or primary inlet is attached to inlet plate 22'. Inlet plate 22' is perforated with a series of equally spaced holes to provide a pressure drop ~or the t gas passing across the inlet plate. Partition 74 consists of an annular plate ~2 which is attached along its ou~er perimeter to the interior of container 72 and a ring 84 which is attached to the inner perimeter of plate 82 and extends upward towards the primary inlet. Ring ~4 together with the wall of cylinder 72 defines an annular inlet extending between the top of ring 84 and the cylinder wall which collects gas ~low traveling in a principally downward direction along the wall o~ cylinder 72. The gas ~low is r~directed radially outward by partition 74 and passes through a series of hol~s 88 in an outlet band 90. Outlet band 90 is de~ined as that section of container 72 lying in khe radial projection of ring 84.
14 2~19928 Holes 88 are again sized to provide only a mall amoun~ of pressure drop across the outlet band.
Intermediate partitions 76 consist~ of annular plates 92 having their outer perimeter attached to the inside of container 72 and an inner perimeter to which a ring 94 is attached. The number and size of holes 88 in any outlet band may be adjusted to provide khe desired flow rate and to some degree the desired pressure drop at any band level. The velocity head produc~d a~ each annular inlet provides additional pressure drop that may be used to adjust and vary the pressure drop at any ~iven band level without upsetting, to any great degree, the overall pressure balance across all the annular inlets.
Lower partition 78 consists of an annular plate 96 having its outer perimeter attached to the inside of container 72 and an inner perimeter to which a ring 98 is attached and extends upward towards the primary inlet. Annular plates 82, 92, and 96 divide the portion of container wall 72 located therebetween into a number of vertically spaced outlet bands 100. Annular inlets, defined as the horizontal area between the top o~ ~ne ring and a superadjacent ring, collect annular sections of axially flowing gas from the region immediately above the annular inlets. The gas collected by th~ annular inlets is redirected and discharged in a radial direction through a series of holes 88 located in annular bands 100. Holes 88 are uniformly spaced about the circumference of each outlet band. By providing a small pressure drop, holes 88 ensurP that radial gas flow from the outlet bands is uniform across the entire circumference. Again, only a small pressure drop through holes 88 is required to provide any needed circumferential redistribution. Rings 94 and 98 extend upward towards the primary inlet and preferably extends above the next adjacent annular plate.
Extending the ring above the next adjacsnt annular plate defines at least a small vertical flow passage between adjacent rings that aids in trapping an annular section of 2 ~ 2 8 ~5 gas ~low by preventing inward deflection o~ the gas as it contacts the partition and undergoe~ a change in direction. Preferably, the extension of the ring above the next ~djacent annular plate equ~ls at l~ast a ~uarter of the horizontal distance between the adjacent rings.
Gas flow traveling down the very center o~
cylindrical container 72 passes inside ring 98 and into a chamber bordered by annular plate 96, plate 80, and container 72. A portion of the gas entering this chamber is directed radially outward through holes 102. The remainder of ~he entering gas passes downwardly through perforations in end plate 80. The arrangement of perforations in end plate 80 is more clearly shown in Figure 4. End plate 80 is imperforate about a central diameter equal to the inner diameter of ring 98. The remaining area of end plate 80 is perforated by smaller holes 106 that are equally spaced about the plate. The total open area pxovided by holes 102 and 106 will provide a very small pressure drop through these openings. Small holes 10~ are located under annular plate 96 to prevent any direct axial gas f]ow out of the distributor and preferably sized to provide a gas flow to that portion of the particle bed surface underlying horizontal projection distributor that is at least equal to the average gas ~low across the entire particle bed surface. As previously mentioned, providing downward or axial gas flow across the top surface of the bed prevents horizontal or transverse gas flow that could disturb the bed.
Nonuniform contact with the catalyst will adversely affect the reaction taking place by overheating or overcooling the reactants. This probl~m is most severe in exothermic reactions where the hiyher temperature ~an cause ~urther reaction of feedstock or other fluid component~ into undesirable products or can introduce local hot spots that will cause damage to the catalyst and/or mechanical components.
Non-uniform fluid flow into the vessel can disrupt the top surface of the bed. The disruption results from transverse fluid flow across the surface of the bed at velocities sufficient to move the individual bed particles. For a confined bed, this disruption or movement of the particles will cause the particles to abrade against each other generating smaller particles which are referred to as fines. These fines may increase pressure drop within the bed or escape from the bed thereby reducing the overall quantity of particles in the bed and possibly interfering with downstream operations.
~n unconfined beds, transverse fluid flow may also shi~t large quantities of particles so that the bed surface is highly irregular.
These transverse currents are the result o~
charging fluid into a relativsly large diameter vessel khrough a relatively small diameter nozzle. Charging fluid into the vessel through a small diameter nozzle produces a high velocity jet that extends from the nozzle into the vessel. Impact of this iet on or adjacent to the surface of a relatively closed catalyst bed flares the fluid outward thereby producing eddy currents and fluid velocities transverse to the bed surface~ The inlet effects associated with the r~latively small diameter nozzle are compounded by the usual presence of an elbow just upstream of the nozzle which introduces another 4 20~28 transvers~ velocity component into the flUid flow entering the vessel. The overall result of these inle~ eff~cts is often the piling up of particles around the periphery of the particle bed or the shifting of particles from one side of the bed to the other.
These detrimental inlet effects are a~oided by uniformly dispersing the fluid as it enters the vessel.
Uniform dispersal can be obtained by providing a sufficient length between the nozzle and the catalyst bed lo surface ~uch that ~he fluid jet and any transverse velocitie~ are substantially dissipated upstream of the particle bedO However, in most cases, it is impractical to provide the length necessary for dissipation of the inlet effects due to the excessive vessel tangent length that would be required. In fact, the trend in many industries is to decrease the length b~tween the inlet nozzle and the particle bed surface in order to increase the total volume of particles in the vessel and thereby obtain greater fluid throughput or gr~ater particle bed service life.
For these reasons, inlet distributors are commonly used to break up the fluid jet and redistribute fluid flow over the top surface of a particle bed. One such device ~ ~ is shown in U.S. Patent 2,925,331 issued to Kazmierczak et al. where a fluid stream is downwardly directed onto the upper surface of ~he catalyst bed and passes first through a distributor consisting of a series o~ annular plates having inner diameters that progressively decrease in the direction of fluid flow so that portions of the Xluid stream are in e~fect peeled off and redirected radially outward over the surfac~ of the particle bed. It is also known in the hydrocarbon processing industry to attach cylindrical rings extending in the direction of fluid ~low to the inner edge of the annular plates. Another type of distributor used to redirect and remix fluid flow upstream o a particle bed is shown in U.S. Patent 3,598,541 issued to Hennemuth et al. and U.S. Patent 3,598,542 issu~d to 2 ~ 2 8 Carson et al. ~he Hennemuth distributor uses a series of circumferentially spaced holes ~o redistribute ~luid within a fluid mixing device that communicates with the upper surface of a particle bed. The distributor disclosed in Carson uses a series of circumferentially spaced holes to radially discharge fluid across the upper surface of a particle bed. Thus, the prior art is well acquainted with a number of distribution devices for use in ~luid solid contacting vessels.
Despite the use o~ different inlet distributors, bed disruption remains a problem. Distri~utors that use the annular plates or baffles of the Kazmierczak device reduce the severity of bed disturbances but have not eliminated it. Therefore, large scale shifting of particle bed surfaces, especially where fluid inlet velocities are high, still occurs. Such disruption i5 still known to occur even in cases where straightening vanes and other flow distribution devices are added to the upstream elbow as a means of eliminating a resulting ~ransverse flow component. It has now been discover~d that despite the presence of the baffles and additional redistribution devices, such as straightening vanes, fluid flow entering the vessel still remembers the change of - ~ direction that took place upstream o~ the inlet nozzle and a distribution device that disperses ~he fluid in two directions is needed to overcome these problems.
SUMMARY OF THE INVENTION
Therefore, it is an object of this invention to improve fluid dispersal over the surface of a particulate bed.
It is a further object of this invention to prevent disruption of the top surface of the bed.
It is a yet further ~bjective of this invention to dissipate inl~t effects such as jets and transverse currents associated with fluid flow into a vessel while 6 2~1~928 minimizing the distance betw~en the inlet nozzle and the particle bed sur~ace.
Another object of this invention is to provide a fluid distributor that eliminates transverse velocity components that enter the vessel through a relatively small nozzle.
These and other objects are satisfied by ~he device of this invention which is the first inlet distributor to radially and circumferentially redirect a majorit.y of an axial fluid flow over the surface o~ a par~icle bed. This two direc~ion redistribution dissipates~nQnuniform transverse velocity components and eddy currents that were not eliminated by cther inlet distributors. More specifically, this invention is a fluid distributor that divides a principally axial flow of fluid into a series of flow passages. These flow passages end in cylindrical outlet bands having uniformly spaced apertures about their circumference that provide a small pressure drop for circumferentially redistributing the fluid leaving each passage. The cylindrical bands of apertures are progressively spaced at increasing distanres from the inlet nozzle to increase the dispersal of ~luid flow over the entire particle bed surface.
- t Accordingly, in one embodiment, this invention is a fluid distributor comprising a conduit, a plurality of partitions, and a series of perforations. The ~onduit has an inlet for receiving a fluid stream. The plurality of partitions subdivide most of the cross-sectional area o~
the conduit into at least two annular collection zones.
The partitions also define, at least in part, a series of outlet bands that are centered about the longitudina7 axis of the conduit. Each outlet band is located at the end ~f one collection zone and the outl~t bands have an arrangement wherein the outermost collection zone ends with the outlet band located nearest the inlet and each successive inwardly spaced collection zone ends with an outlet band having an increased ~pacing from the inlet, 7 2~19928 The series of per~orations are spaced at regular intervals about the circumference o~ each b~nd to circumferentially redistribute ~luid flow out of ea~h outlet band.
In a second embodiment, this invention is a fluid 5 distributor that compris~s a cylindrical cont~iner, a plurality of partitions, an~ aperatures spac~d uniformly about the circumference of the container. The cylindrical csntainer has a primary inlet at one end and a closure plate at the opposite end. The plurality of partitions lo are located in the container and define a series of annular inlets inside the container and a sQries o~
cylindrical outlet bands along the wall of thP container.
The partitions communicate each inlet with one outlet and change the direction of fluid flow between the annular inlets and the outlets. A portion of the apertures lie within each cylindrical outlet band. The apertures are uniformly spaced circumferentially about each outlet band and provide a small pressure drop for circumferentially redistributing fluid flow out of each band.
Yet another embodiment involves a method of distributing a fluid straam across a bed of solid particles located in a downflow vessel having a fluid inlet and outlet comprising providing the flow distribution apparatus of the first or second embodiment in the fluid inlet to the vessel and charging the ~luid stream to said inlet at conditions s~lected to achieve two direction flow distribution prior to contact with said bed.
Additional objects, embodi~ents, aspects, and details of this invention are set forth in the following detailed description.
BRIEF DESCRIPTION OF TRE DRAWINGS
Figure 1 shows an arrangement of a downflow reactor having an inlet distributor and a particle bed.
8 2 ~ 2 ~
Figure 2 is one form of the inlet distributor of this invention.
Fi~ure 3 is an ~lternate form of the inlet distributor of this invention.
Figure 4 is a bottom view of the inlet distributor of Figure 3.
DETAILED DESCRIPTTON OF 'rHE INVENTION
The distributor of this invention can b~ u~ed in conjunction with any particle bed. Typically, the particle bed and inlet distributor will be located inside a vessel for a catalytic reaction or an adsorption process. This inVentiQn finds greatest advantage when us~d with a vessel having a downward flow of fluid ~rom an inlet nozzle through an unconfined bed of particles. The invention can also be used with confined particle beds.
In confined particle beds, large scale shifting of the upstream bed surface is not a concern due to restraint by a screen or other confining device but disturbance of the bed surface can still cause attrition and wear of the particles. Thus, while best suited for downflow type vessel, this invention can also be used in vessels where fluid flow i~ primarily horizontal or even up~low.
Most arrangements for piping fluid to the particle ~eds will dictate the use o~ pipe bend or ~lbow ju~t upstream of the inlet supplying fluid above a particle bed surface. Passage through the bend concentrates ~luid flow in the outer radius of the bend. The distributor of this invention is ~specially effective in preventing the bend affect from contributing to bed disturbances~ Bend effects are corrected by circumferentially redistributing the annularly segreyated portions of the fluid flow to the particle bed.
Fluid entering the distributor of this invention may be gaseous phase, liquid phase, or a combination of the two. Greatest advantage is obtained when the fluid 9 2~1 9~28 stream entering through the inl~t distributors is in gas phase.
This invention is more fully explained in the context of a typical downflow vessel arrangement as shown in Figure 1. The remainder of this description refers to the fluid as a gas~ ~his reference is not meant to limit the invention to gas phase flow. Referring again to Figure 1, an upper pipe 10 delivers a gas phas2 fluid to a ve~s 1 12 through an inlet nogzle 14 which is connected to pipe 10 through a pipe swedge 16 and an elbow 18. If unrestricted, discharge of the fluid from elbow 18 would produce a gas jet and also introduce a transverse velocity component into the gas stream that enters vessel 12.
However, all of the gas flow that enters vessel 12 is intercepted first by distributor 20. Distributor 20 has an inlet plate 22 sandwiched between the bottom of pipe swedge 16 and the top of inlet nozzle 14.
Sandwiching plate 22 between pipe swedge 16 and inlet 14 secures distributor 20 to vessel 12 and provides a seal between pipe swedge 16 and inlet plate ~2 that prevents fluid from entering vessel 12 without first passing through distributor 20. Other well-known means of attaching distributor 20 to vessel 12 or pipe swedge 16 - ~ can be used. Nevertheless, whatever method of attachment is used, it is important that the method prevent bypassing of fluid around distributor 20 and into the vessel 12.
This bypassing can produce concentrated jets of fluid ~low that will diminish or defeat the effect of distributor 20.
In a manner hereina~ter described, distri~utor 20 disperses the gas over the cross-section of vessel 12.
The dispersed gas enters a particle bed 24 having an upper sur~ace 25. Bed 24 is composed of solid particles which can be in the form of pills, spheres, cylinders, or any other desired shape. The actual properties of the particles will depend upon the process which is carried out in the containment vessel. Generally, the particles will either function as an adsorbent or as a catalyst. As lo 2~9928 a further m~ans of preventing bed disturbances, a laysr of support material, usually comprising ceramic balls, may be added and comprise the upper ~urface of the particle bed.
In the case of a downflow reactor, bed surface 25 will simply consis~ of particles that have been leveled at the time of loading. In the case of a confined catalyst bed, a screen or other layer of laminar ma~erial will be at the level of surface 25. As gas passes across upper surface 25, it proceeds down through the remainder of bed 24.
Once the gas has moved a short distance past the bed surface, provided the surface remains level, a complete redist~ibution of the gas is ef~ected such that it will pass uniformly through the remainder of the bed.
Therefore, it is not essential that distributor 20 provide a completely uniform distribution of gas across the bed sur~ace 2S. The purpose of distributor 20 is to provide a fluid, or in this case gas, dispersion that has enough uniformity to eliminate any eddy or cross-currents having sufficient velocity to disrupt surface 25. After a predetermined contact time, gas leaves the catalyst bed 24 by passing through a porou~ support member 26~ Member 26 can be screen or any other rigid layer of porous material having sufficient strength to support the weight and ~ ~ pressure loading of catalyst bed 24. Exiting gases pass through an outlet screen 28 that collects any ~ine particles that have passed out of a catalyst bed and through support member 26. From screen 28, exiting gases leave the veesel 12 through an outlet nozzle 30 which is connected to a lower pipe 32.
The ~unctlon of distributor 20 in dlspersing fluid can be more fully appreciated by a consideration of the device shown in Figure 2 which is one form of a two direction distributor designed in accordance with this invention. Figure 2 shows inlet plate 22 having a series of perforations 34 which collectively provide an inlet for gas flow into the distributor. Although pre*erred, it is not necessary that perforations 34 be used across the 11 2~19928 inlet of plate 22. Inlet plate 22 may be provided with a few large openings or a sinyle opening. The use of perforations increases the uniformity of the gas flow int~
the distributor the advantage of which must be balanced against an increased pressure drop across the inlet.
Therefore, pressure drop considerations will control the number and size of openings in inlet plate 22. In normal practice, the holes in the inlet plate will be sized to provide a pressure drop at least equal to twice the velocity head of the incoming gas stream. The opening or openings may extend as far as the wall of a conduit 36 that receives the gas flow passing throuqh inlet plate 22.
A series of partitions 42, 44, 46, 48, 50, and 52 divide the projection of the cross-sectional area of conduit 36 into a series of annular collection zones. A series of outlet bands 54, 56, 58, 60, 62, and 64 are associated respectively with one of the partitions to define the collection zones as that volume lying in both the space above a given partition and the cylindrical space confined by each outlet band. The collection zone associated with partition 42 and outlet band 54 takes the outermost annular layer of gas flow passing through conduit 36 and redirects it in a radial direction out o~ series of ~ ~ apertures 66 located in outlet band 54. Apertures 66, in this case, are simply a series o~ holes spaced circumferentially about outlet 54 at a uni~orm spacing.
The pressure drop across opening 66 is kept low so that the horizontal velocity component created by the impact of gas flou against partition 42 will be preserved and contribute to the radial momentum of the gas as it leaves the distributor~ Holes 66 serve the important function of circumferentially redistributing the gas flow at each partition. Thereforel a completely open outlet band, as practiced in the prior art, does not provide the necessary pressure drop for circumferential redistribution. A
minimum pressure drop in excess of the radial velocity head and preferably several times greater than the radial 12 2 ~ 2 8 velocity head across the opening 66 will provide the necessary circumferential redistribution. The collection zones associated with the downstream par~itions 44, ~6, 48, 50, and 52 take the remaining gas flow ~rom annular layers of progressively decreasing diameter and redirects it radially outward. The gas flow de~lected by each partition passe~ through apertures 66 of its respective outlet band whi~h circumferential}y redistribute the flow in the manner described.
Fluid that passes below partition 52 enters a final outlet arrangement which, in this case, consists o,f an outlet band 68 and a bottom plate 70. End plate 70 is usually imperforate. When end plate 70 has a large diameter relative to the bed, small perforations may be provided to direct a small portion of the gas downwardly onto the center of the particle bed to avoid the foxmation of a dead space below the distributor which could again introduce eddy currents above the bed. However, the majority of the gas flow passing below parti~ion 52 is radially redirected through outlet band 68. Any gas flow permitted through an opening in plate 70 should not exceed the volum~tric gas addition that satisfies the average gas flow requirements through the central por~ion of the bed ~ ~ that is not in the immediate flow path of the radially discharged gas. Gas flow through plate 70 can produce a jet which can impact and distuxb the downstream bed sur~ace. Therefore, jet length con~iderations may limit the siæe of any opening in plate 7Q.
The configuration of distributor 20 will vary depending primarily on the geometry of the vessel in which it is inserted and the number and type of collection zones. The length of conduit 36 between inlet plate 22 and the ~irst outlet band is sized to get the apertures 66 below the inlet nozzle 14 ~o that the radially directed fluid passing therethrough does not impinge on the nozzle wall. The number of collection zones us~d in a particular distributor will vary with the velocity of gas flow, the 13 2~928 relative size of the inlet nozzle and vessel, and the susceptibility of the particl~ bed to ~low-induced disturbance. Two or more collection zones may be used.
Generally, the more collection zones used, the better the distribution across the catalyst beds. In the specific configuration of the Figure 1 distributor increasing the width of the partitions will increase the radial gas ~low at each outlet band. Adjusting the size and number o~
apertures in each outlet band will also vary the radial gas velocity or through aperatures in dif~erent outlet bands. By appropriate sizing of the collection zones and aperatures, this distributor can provide good gas dispersion over a particle bed of almost any shape or size.
An alternate and often preferred arrangement for the distributor of this invention is shown in Figure 3.
In this case, the diskributor consists of an inlet plate 22', a cylindrical container 72, an upper partition 74, intermediate partitions 76, a lower partition 78, and an end plate 80. The upper end of container 72 referred to as the inlet or primary inlet is attached to inlet plate 22'. Inlet plate 22' is perforated with a series of equally spaced holes to provide a pressure drop ~or the t gas passing across the inlet plate. Partition 74 consists of an annular plate ~2 which is attached along its ou~er perimeter to the interior of container 72 and a ring 84 which is attached to the inner perimeter of plate 82 and extends upward towards the primary inlet. Ring ~4 together with the wall of cylinder 72 defines an annular inlet extending between the top of ring 84 and the cylinder wall which collects gas ~low traveling in a principally downward direction along the wall o~ cylinder 72. The gas ~low is r~directed radially outward by partition 74 and passes through a series of hol~s 88 in an outlet band 90. Outlet band 90 is de~ined as that section of container 72 lying in khe radial projection of ring 84.
14 2~19928 Holes 88 are again sized to provide only a mall amoun~ of pressure drop across the outlet band.
Intermediate partitions 76 consist~ of annular plates 92 having their outer perimeter attached to the inside of container 72 and an inner perimeter to which a ring 94 is attached. The number and size of holes 88 in any outlet band may be adjusted to provide khe desired flow rate and to some degree the desired pressure drop at any band level. The velocity head produc~d a~ each annular inlet provides additional pressure drop that may be used to adjust and vary the pressure drop at any ~iven band level without upsetting, to any great degree, the overall pressure balance across all the annular inlets.
Lower partition 78 consists of an annular plate 96 having its outer perimeter attached to the inside of container 72 and an inner perimeter to which a ring 98 is attached and extends upward towards the primary inlet. Annular plates 82, 92, and 96 divide the portion of container wall 72 located therebetween into a number of vertically spaced outlet bands 100. Annular inlets, defined as the horizontal area between the top o~ ~ne ring and a superadjacent ring, collect annular sections of axially flowing gas from the region immediately above the annular inlets. The gas collected by th~ annular inlets is redirected and discharged in a radial direction through a series of holes 88 located in annular bands 100. Holes 88 are uniformly spaced about the circumference of each outlet band. By providing a small pressure drop, holes 88 ensurP that radial gas flow from the outlet bands is uniform across the entire circumference. Again, only a small pressure drop through holes 88 is required to provide any needed circumferential redistribution. Rings 94 and 98 extend upward towards the primary inlet and preferably extends above the next adjacent annular plate.
Extending the ring above the next adjacsnt annular plate defines at least a small vertical flow passage between adjacent rings that aids in trapping an annular section of 2 ~ 2 8 ~5 gas ~low by preventing inward deflection o~ the gas as it contacts the partition and undergoe~ a change in direction. Preferably, the extension of the ring above the next ~djacent annular plate equ~ls at l~ast a ~uarter of the horizontal distance between the adjacent rings.
Gas flow traveling down the very center o~
cylindrical container 72 passes inside ring 98 and into a chamber bordered by annular plate 96, plate 80, and container 72. A portion of the gas entering this chamber is directed radially outward through holes 102. The remainder of ~he entering gas passes downwardly through perforations in end plate 80. The arrangement of perforations in end plate 80 is more clearly shown in Figure 4. End plate 80 is imperforate about a central diameter equal to the inner diameter of ring 98. The remaining area of end plate 80 is perforated by smaller holes 106 that are equally spaced about the plate. The total open area pxovided by holes 102 and 106 will provide a very small pressure drop through these openings. Small holes 10~ are located under annular plate 96 to prevent any direct axial gas f]ow out of the distributor and preferably sized to provide a gas flow to that portion of the particle bed surface underlying horizontal projection distributor that is at least equal to the average gas ~low across the entire particle bed surface. As previously mentioned, providing downward or axial gas flow across the top surface of the bed prevents horizontal or transverse gas flow that could disturb the bed.
Claims (7)
1. A fluid distributor [20] comprising:
a) a conduit [36] having an inlet [22] for receiving a fluid stream:
b) a plurality of partitions [42, 44, 46/ 48, 50 and 52] subdividing at least half of the cross-sectional area of said conduit into at least two annular collection zones;
c) a series of outlet bands [54, 56, 58, 60, 62 and 64] spaced along and centered about the longitudinal axis of said conduit, with each outlet band located along the outer boundary of a collection zone, said outlet bands having an arrangement wherein the outlet hand located nearest said inlet borders the outermost collection zone and succeeding outlet bands having an increased axial spacing from said inlet border collection zones have progressively increasing inward locations;
d) a series of perforations [66] spaced at regular intervals about the circumference of each outlet band to circumferentially redistribute any fluid flow out of each band.
a) a conduit [36] having an inlet [22] for receiving a fluid stream:
b) a plurality of partitions [42, 44, 46/ 48, 50 and 52] subdividing at least half of the cross-sectional area of said conduit into at least two annular collection zones;
c) a series of outlet bands [54, 56, 58, 60, 62 and 64] spaced along and centered about the longitudinal axis of said conduit, with each outlet band located along the outer boundary of a collection zone, said outlet bands having an arrangement wherein the outlet hand located nearest said inlet borders the outermost collection zone and succeeding outlet bands having an increased axial spacing from said inlet border collection zones have progressively increasing inward locations;
d) a series of perforations [66] spaced at regular intervals about the circumference of each outlet band to circumferentially redistribute any fluid flow out of each band.
2. The distributor of Claim 1 wherein said partitions [74, 76 and 78] define axially oriented flow passages for restricting any radial fluid flow away from said outlet bands.
3. The distributor of Claim 1 wherein said conduit [36] and said outlet bands have a uniform diameter and comprise a cylindrical vessel [72] having a closure plate [80] at an end opposite said inlet [22°].
4. The distributor of Claim 3 wherein said inlet [22'] communicates with said closure plate and said closure plate [80] is perforated.
5. The distributor of Claim 1 wherein said outlet bands have progressively decreasing diameters with the smallest diameter band located the greatest distance from said inlet.
6. The distributor of Claim 1 wherein said partitions comprise annular plates having inner diameters that progressively decrease in size as the distance of the annular plate from said inlet increases and a ring extending toward said inlet from the inner diameter of each annular plate past the preceding annular plate.
7. A method of distributing a fluid stream across a bed of solid particles located in a downflow vessel having a fluid inlet and outlet comprising providing the fluid distribution apparatus of any of Claims 1 to 6 in the fluid inlet to the vessel and charging the fluid stream to said inlet at conditions selected to achieve two direction fluid distribution prior to contact with said bed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA 2019928 CA2019928A1 (en) | 1990-06-27 | 1990-06-27 | Two direction inlet fluid distributor for downflow vessel containing bed of solid particles |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA 2019928 CA2019928A1 (en) | 1990-06-27 | 1990-06-27 | Two direction inlet fluid distributor for downflow vessel containing bed of solid particles |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2019928A1 true CA2019928A1 (en) | 1991-12-27 |
Family
ID=4145347
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2019928 Abandoned CA2019928A1 (en) | 1990-06-27 | 1990-06-27 | Two direction inlet fluid distributor for downflow vessel containing bed of solid particles |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA2019928A1 (en) |
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1990
- 1990-06-27 CA CA 2019928 patent/CA2019928A1/en not_active Abandoned
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