CA1237874A - Staged flow distribution grid assembly and method for ebullated bed reactor - Google Patents
Staged flow distribution grid assembly and method for ebullated bed reactorInfo
- Publication number
- CA1237874A CA1237874A CA000464399A CA464399A CA1237874A CA 1237874 A CA1237874 A CA 1237874A CA 000464399 A CA000464399 A CA 000464399A CA 464399 A CA464399 A CA 464399A CA 1237874 A CA1237874 A CA 1237874A
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- Prior art keywords
- grid plate
- flow
- primary
- grid
- tubes
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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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
Abstract
ABSTRACT OF DISCLOSURE
A staged distribution grid assembly and method for uniform fluid flow distribution upwardly into an ebullated catalyst bed of a reactor. In the staged grid assembly, the gas and liquid mixture flows first through a lower secondary flow distribution grid plate into an interim zone, and then flows upwardly through an upper primary flow distribution grid plate into the reactor ebullated bed. The staged grid assembly contains an upper primary grid plate containing multiple flow tubes covered by bubble caps, and a lower secondary grid plate containing multiple flow tubes. The staged flow distribution grid assembly enables the primary grid to provide a more uniform distribution of gas and liquid flow upwardly into the ebullated bed across the entire cross-sectional area of the reactor, and thereby provides improved operation of the ebullated catalyst bed reactor.
A staged distribution grid assembly and method for uniform fluid flow distribution upwardly into an ebullated catalyst bed of a reactor. In the staged grid assembly, the gas and liquid mixture flows first through a lower secondary flow distribution grid plate into an interim zone, and then flows upwardly through an upper primary flow distribution grid plate into the reactor ebullated bed. The staged grid assembly contains an upper primary grid plate containing multiple flow tubes covered by bubble caps, and a lower secondary grid plate containing multiple flow tubes. The staged flow distribution grid assembly enables the primary grid to provide a more uniform distribution of gas and liquid flow upwardly into the ebullated bed across the entire cross-sectional area of the reactor, and thereby provides improved operation of the ebullated catalyst bed reactor.
Description
1~3~ 74 D 1333 STAGED FLOW DISTRI~UTION GRID ASSEMBLY AND METHOD
FOR EBULLATED BED REACTOR
.
BACKGROUND OF INYENTION
This invention pertains to an improved flow distribution grid plate assembly and method used for providing uniform upward fluid flow distribution in ebullated bed catalytic reactors. It pertains particularly to a staged flow distri-bution method and grid plate assembly having an upper primary grid plate and a lower secondary grid plate located below the primary grid plate, each plate ~ontaining multiple vertical flow tubes.
In ebullated catalyst bed reactors operated at elevated temperature and pressure conditions, flow maldistribution problems sometimes exist below the distribution grid plate and in the catalyst bed. Such flow maldistribution is usually due to abnormal operating conditions such as plugging of openings in the grid plate by coke, or to excessive coke deposits on the catalyst particles in the bed. If such plugging of openings in the grid plate occurs, non-uniform flow distribution and bed ebullation results, which is very undesirable. The riser flow tubes and slotted tail pipes as now used in reactor grid plates usually perform adequately in distributing the recycle and feed liquid streams and hydrogen gas into the ebullated catalyst bed. However, the presently used grid plate arrangement has been found to be inadequate for handling severe flow maldistribution in the plenum of the reactor, for it can only moderately improve the flow distribution existing below the plate, but cannot alleviate "spouts" and major operational upset conditions which lead to .
~3~
an uneven depth of hydrogen in the plenum chamber, which can cause a greater length of the tail pipe slot to be exposed with a corresponding increase in hydrogen flow to those particular riser tubes. Such maldistribution flow conditions in a reactor plenum can be more or less constant depending on the manner in which the feed streams and recycle streams are introduced into the plenum Also, flow maldistribution could possibly occur as a sloshing effect where the liquid level in the plenum below the distribution grid is constantly tilting from one direction to another~
The use in such ebullated bed catalytic reactors of con-ventional cylindrical riser flow tubes covered by cylindrical-shaped bubble caps is disclosed by U. S. Patent No. 3,1979286 to Farkas et al; U. ~. 3,197,288 to Johanson, and U. S. 3,475,134 to Weber et al. However, it has been found that inadequate distribution if the gas and liquid flows are usually provided by these reactor designs.
Accordingly, improvements in flow distribution in ebullated bed catalytic reactors have been sought. An improved staged grid plate configuration has now been deve-loped which more effectively redistributes the gas and liquid flows below the primary grid plate whenever flow maldistribution problems exist below the grid, so as to pro-vide more uniform ebullation of the catalyst bed in the reactor. To aid in maintaining a "smooth" liquid level in the plenum and consequently a reasonably equal length of slot exposure on each riser tube for gas flow into each tube, a secondary grid plate is provided below the primary grid.
This secondary grid is similar to the single flow distribution grid presently used in ebullated bed reactors, however, the secondary grid does not have caps over the riser ~ 3'~8~
tubes on the upper side of the plate, but uses only slotted tubes attached to a plate which extends to near the inner walls of the reactor.
SUMMARY O~ INYEN~ION
This inven~ion proYides a staged distribution grid plate assembly and method used ~or improved flow distribution upwardly into an ebullated catalyst bed of a reactor vessel, in which a lower secondary flow distribution grid feeds gas and liquid flow upwardly to a upper primary flow distribution grid, and thence into the ebullated bed of the reactor. The flow tubes provided in the lower secondary grid plate are uniformly spaced and are relatively larger in diameter and have greater total cross-sectional area than flow tubes in the upper primary distribution grid, so that the grea~er and controlling pressure differential ocours across the upper primary grid plate to provide a more uni~orm flow distribution upwardly into the ebullated bed. This staged grid plate arrangement or assembly enables the upper primary grid to operate more effectively, so that the ebullated catalyst bed above the prinary grid plate will have a more uniform distribution of gas and liquid flowing upwardly therethrough across the entire cross-sectional area of the reactor.
In the staged grid plate assembly of the present invention, the upper primary grid plate can be supported from either the react~r lower head or ~rom th~ reactor L~ wall, and the lower secondar~ grid plate is usually supported from the upper primary grid, such as by multiple spacer rods extending ~9..;~3'7~4 between the two grids. Alternatively, the secondary gri d plate can be separately supported from the reactor lower head or wall, or it can be structurally integrated with the primary upper grid plate so as to help withstand the total differential pressure across the grid assembly caused by-the ~d fluid flow through the grids. Also, the lower secondary grid plate can be attached integrally to the primary upper plate by an extension of the primary flow tubes below the upper plate and rlgidly attached to the lower secondary plate, so that the ca ~ yst bed weight and total pressure diEferential across koth plates in the grid plate assembly is carried by the assembly.
More specifically, the present invention comprises a staged grid plate assembly for providing uniform flow distribution of a gas/liquid mixture upwardly into an ebullated bed of a ~reactor, said grid plate assembly comprising an upper primary gr~d plate supported w~thin the reactor near the lower end of the reactor, said primary grid plate containing multiple flow pr~y distribution tubes exte~ng substantially vertically through said plate, said primary tubes being uniformly sized and spaced in the plate, a cap covering the upper end of each tube in said primary grid, said cap being rigidly attached to and spaced outwardly from the tube upper end above the grid plate, so as to permit flow of fluid upwardly through the tubes and then outwardly from under the lower edges of the cap into the ebullated bed; and a lower secondary grid plate located below and spaced from said primary grid plate, said secondary grid plate containing multiple flow secon~ distribution tubes passing subs~ntially Yertically through the secondary plate, said secondary tubes having uniform diameter and spacing, whereby fluid passes upwardly through the flow tubes in the secondary grid, and .
3~7~
then upwardly through the flow tubes in the primary grid and outwardly from under the lower edges of the caps to provide uniform fluid flow in the reactor ebullated bed.
In another aspect of the invention, it comprises a method for uniformly distributing gas and liquid flow upwardly into an ebullated bed reactor, wherein the method comprises introducing gas and liquid flow streams into a plenum located at the lower end of a reactor below a flow distribution grid;
passing said gas and liquid flow upwardly from said plenum through multiple tubular flow passages located in a secondary grid plate into an interim zone located above the secondary grid plate and below a primary grid plate; remixing and redistributing the gas and liquid flow in said interim zone above said lower grid plate; and passing the remixed gas and liquid upwardly through multiple tubular flow passages located in said upper primary grid plate, then under bubble caps each located over said multiple upper flow passages and uniformly into an ebullated catalyst bed of the reactor.
~RIEF DESCRIPTION OF DRAWINGS
FIG. 1 shows a partial vertical sectional view through the lower portion of a reactor vessel containing a staged grid plate assembly havintl multiple riser tubes therein in accordance with the invention.
FIG. 2 shows a portion of the primary upper grid plate containing multiple riser flow tubes each covered by a single bubble cap and containing a ball check.
FIG. 3 shows a partial vertical sectional view of an alternative staged grid plate assembly in which both grid plates are supported from the reactor lower head.
3'~74 FIG. 4 shows a partial sectional view of an alternative grid plate assembly in which the staged grid plates~ are structurally integrated into a single unit supported from the reactor wall.
DESCRIPTION OF INVENTION
In liquid phase catalytic reactors for contacting liquids, gases and par iculate solids, ~t is very important for achieving comple~e and effective catalytic reactions that the upflowing liquid and gas mixture be uniformly distributed across the entire horizontal cross-section of the reactor vessel~ so as to maintain the bed of partioulate solids or catalyst in a uniformly expanded condition with random motion of the catalys~. For certain reactions, such as the catalytic hydrogenation oF heavy oils or coal-oil slurries or the hydrocracking o~ heavy hydrocarbon feedstreams at elevated temperature and pressure conditions, such as at 500-1000F
temperature and 500-5000 psig pressure, to produce lower-boiling liquid fractions, flow maldistribution through the reactor flow distributor or grid plate assembly can cause relatively inactive zones in the bed where the catalyst is not in uniform random motion. This condition leads to the undesired formation of agglomerates of catalyst particles by coking of the hot oil or slurry. The desired uniform flow distribution upwardly through the grid plate into the ebullated catalyst bed can be impaired either by restrictions occurring in the riser tubes due to coking, or by catalyst particles in the tubes. The pr2sent invention provides an effective solution to these flow maldistribution problems in the ebullated catalyst bed.
~3'7~7~
The flow distributor or grid plate assembly must also function to prevent catalyst particles from draining down-wardly back through the distributor whenever the reactor is shutdown, while most of the liquid contained within the catalyst bed is drained down to below the bed. If catalyst is allowed to drain bark through the grid plate flow distri-butor, it can plug the flow passages therein and interfere with operations so that re-ebullating the catalyst bed be-comes very difficult because the flow passages are at least partly restricted. Furthermore, such restrictions can pro-duce undesired flow maldistribution in the catalyst bed. To prevent such backflow of catalyst, a ball check valve is usually pr~vided in each riser tube.
In the present invention, two grid plates are provided supported in a reactor vessel in ~eries flow relationship so that a relatively more unifonm flow distribution upwardly into the ebullated catalyst bed above the upper primary gr~d plate ~s thereby ~ch~eved. It is thus a basic feature of the present invention that both grid plates contain multiple flow tubes having uniform size and spacing, with only the tubes in the upper grid plate having caps covering the upper ends of the tubes. The flow tubes used in the secondary grid plate should be uniformly spaced and have relatively larger diameter and total cross-sectional area than the flow tubes in the upper primary grid plate. The secondary flow tubes do not necessarily need to be cylindrical in shape but can be square, rectangular) or triangular in cross-seotional shape or practically any configuration can be employe~. However, the combination of tube effective diameter and number of tubes should provide the desired uniform flow and differential pressure across the secondary grid, which should be between about 0.10 and 0.90 ~ 3'~7~
times the different7al pressure across the upper primary grid. Also, the length/diameter ratio for the secondary tubes should be at least about 1.0, and usually need not exceed aboùt 5Ø
In operation, the gas liquid mixture which passes through the multiple flow tubes ~in the lower secondary grid is redis~ributed in the horizontal space between the two grid plates. Thus, the flow of gas/liquid mixture flowing through the multiple flow tubes in the upper primary grid into the ebullated bed will be more uniform than when only a single grid plate is used.
As generally shcwn Ln FI~. 1, reactor vessel 10 contaLns primary upper grid plate 12 which is rigidly supported therein usually at its outer edges by a cylindrical shaped support skirt 13 connected to the reaotQr lower head 14, and is sealed to the s1de wall ~n the lower portion of the reactor, so as to provlde a plenum space 15 be1~ a lower secondary grid plate 30. The feedstream to the reactor enters through conduit ll and the flow is deflected radially outwardly by stationary baffle lla. The upper primary grid plate 12 serves to support catalyst bed 25 and contains multiple riser flow tubes 16. As shown in greater detail in Fl~. 2, each prima ~ riser tube 16 has at least one opening or slot 17 at its upper end and is covered by a cap 18, which is rigi~ly attached to the upper end of tube 16 by suitable fastening means 19~ such as a threaded bolt an~ nut.
The lcwer end of cap 18 is spaced outwardly from tube 16 to provide for uniform flow of fluid upwardly through the tubes 16 and slot 17 of the grid plate 12 and into the bed 25 of catalyst particles.
As shown in FIG. 2, the lo~er edge of ~he cap 18 is pre-ferably provi~bd with numer~us notches 18a to provide for the loca-~ 3'~
lized exit flow Df gas and promote the formation of small ga;
bubbles in bed 25. The notches are intended to let the gas emerge from under the caps 18 ~ ~11 discrete bubbles instead of larye globs of gas, and the notch widths should usually be 5-10 times the catalyst effective particle diameter. The notches located around the bottom of the caps can be used with indiYidual caps of any shape, such ~ a cylindrical or tapered shape. Also to prevent backflow of catalyst from the bed 25 to plenum 15 below the grid plate following reactor shutdown or loss of recycle liquid flow, a ball check 20 is usually provided and is prefera~ly located in the upper end of each riser tube 16, as shown in FI&. 2. The ball check 20 mates with seat 22 provided within the upper end of the riser tube 16 to prevent any backf!ow of catalyst from the bed 25 ~o the plenum 15 below the distributor plate 12. To facilitate the entry of gas suoh as hydrogen into the lower end of the riser tube 16, openings such as holes 23 or vertical slots 24 are provided in the tube below the grid plate 12.
Located below the primary grid plate 12 is a secondary grid plate 30, containing multiple parallel secc~ndary flc~w tu~es 32 each having ope ~ gs such as holes 33 or vertical slot 34 in the lower end thereof. The secondary grid plate 30 is spaced below and usually supported from the upper grid plate 12, such as by multiple rods 36 ~ith each rod having a spacer tube 37 located around the rod for maintaining the desired space 35 between the upper and lower grid plates, as shown in FIG. 1. The secondary grid 30 can be extended to contact support skirt 13, or pre~era~ly can have a small annular spa~e 38 therebetween and be provided with a circumferential skirt 40 extending downwardly from plate 30. The lower end of , . . . .
~.~ 3'~8~ ~
skirt 40 should extend to substantially the same level as the lower ends of secondary flow tubes 32. Also, the skirt 40 is provided with openings such as holes 39 or slots 41, which are similar to holes 33 or slots 34 in the secondary flow tubes 32. Furthermore, the flow area of the annular space 38 should not exceed about lO percent of the total flow area for the openings in the secondary grid plate, i.e. that provided both by multiple flow tubes 3Z and annular flow space 38.
In operation of the dual grid plate assembly, the gas/liq3id mixture fed into pl~n 15 forms a gas space 15a bel~ lower sec~ndary grid plate 30 and abave liqu~d level 15b. me gas an~ liquid mixture in plenum 15 passes upwardly ~hrough multiple flow tubes 32 and annular space 38 into space 35 between the upper and lower grid plates. In space 35, the gas/liquid mixture is redistr~buted generatly horizontally and the gas portion rises to form gas space 35a above the liquid level 35b. The liquid level 35b is controlled by the vertical location of slots 24 in the lower ends of riser tubes 16 and by the flow rate ~hrough the grid plate.
It is thus an advantage of the present invention that the lower secondary grid plate prov1des for the lateral redistribution of fluid flow below the upper primary grid plate and thereby tends to correct any flow maldistribution .below the primary grid plate, which may be caused by flow maldistribution problems on the underside of the grid.
Reactor bed ebullation wfll be generally uniform unless some riser tubes become plugged by coke formation, etc.
In an alternative embodiment of the present invention, as shown in FIG. 3~ ~oth the upper primary grid plate 12 and the lower secondary grid plate 30 can be separately supported ~3'7~
from the reactor lower head 14 by means of an outer cylindrical support skirt 13 for upper grid 12 and an inner cylindrical skirt 45 for supporting the lower grid plate 30.
For this grid plate configuration, the support rods 36 and spacer tubes 3~ used for the FIG. 1 embodiment are not needed. Also, the multiple flow tubes 32 m grid plate 30 are provided with multiple openings 33 or slots 34 to faci-litate the entry of gas such as hydrogen into the flow tubes, similarly as for the flow tubes 16 in the upper grid plate 12. If desired9 dual nozzles 11 for the rea~r f~stream ~ be provided into plenum 15.
It is another important feature of the present invention that the two grid plates can be structurally integrated, ~o that the total pressure differential across the grid plate assembly due to upward fluid flow therethrough and the cata-lyst bed weight is carried by the assembly of bothgridplates.
As shown in FIG. 49 the riser tubes 42 for the primary upper grid plate 12 are ex~ended downwardly and rigidly attached such as by welding to the lower secondary grid plate 30.
Openings such as holes 43 or slots 44 are provided in the lower end of each tube 42 as before, to provide for entry of gas such as hydrogen into the flow tube. Also, the upper primary grid plate 12 can be suitably supported from the reactcr inner wall by a continuous ring 26 welded to the wall. The upper grid plate 12 is attached to ring 26 by multiple fastener bolts 28 and nuts 29. In this grid plate assembly, the periphery of lower grid plate 30 can be extended to near the inner wall of reactor 10 so as to pro-vide a small annular space 46 therebetween, and be provided with a peripheral depending skirt 48 and holes 49 similarly as previously described for the FIG. 1 embodiment.
3~
The utility and effectiveness of the staged flow distri-bution grid assembly is illustrated by the ~ollowing specific example, which should not be construed as l~miting the scope of the invention.
EXAMPLE
In an ebullated bed catalytic hydrogenation reactor for petrole~n feedstoc3c material, a du~l grid assembly provided near the reac~r er end has the foll~wing characteristics and diIrensior~
Reactor Temperature, F 750-850 Reactor Pressure, psig 1000-3009 Reactor Ins~de Diameter9 ft 12 Vertical Spacing Between Primary and Secondary Grid Plates, in. 16 Primary Grid Flow Tube Diameter, in. 1.30 Bubble Cap Diameter, in. 3 Primary Flow Tube Extension Below Primary Grid Plate, in. 9 Flow Area of Primary Grid Tubes, in. Z.16 Secondary Grid Flow Tube Diameter, in. 4 Secondary Flow Tube Extension Below Grid Plate, in. 5 Fl ow Area of Secondary Grid Tubes, in. 12.7 Pressure Differential Across Upper Primary Grid, ~si 5-8 Pressure Differential Across Lower Secondary Grid, psi 1-3 The catalyst ebullation pattern in the reactor is uniform o~er a wide range of liquid and gas flow rates from the plenum upwardly into the reactor bed.
123~7~'74 Although this invention has been described broadly and in terms of certain preferred embodiments thereof, it will be understood that modifications and variations to the apparatus can be made and that some elements can be used without others all within the spirit and ~cope of the invention, which is defined by the following claims.
FOR EBULLATED BED REACTOR
.
BACKGROUND OF INYENTION
This invention pertains to an improved flow distribution grid plate assembly and method used for providing uniform upward fluid flow distribution in ebullated bed catalytic reactors. It pertains particularly to a staged flow distri-bution method and grid plate assembly having an upper primary grid plate and a lower secondary grid plate located below the primary grid plate, each plate ~ontaining multiple vertical flow tubes.
In ebullated catalyst bed reactors operated at elevated temperature and pressure conditions, flow maldistribution problems sometimes exist below the distribution grid plate and in the catalyst bed. Such flow maldistribution is usually due to abnormal operating conditions such as plugging of openings in the grid plate by coke, or to excessive coke deposits on the catalyst particles in the bed. If such plugging of openings in the grid plate occurs, non-uniform flow distribution and bed ebullation results, which is very undesirable. The riser flow tubes and slotted tail pipes as now used in reactor grid plates usually perform adequately in distributing the recycle and feed liquid streams and hydrogen gas into the ebullated catalyst bed. However, the presently used grid plate arrangement has been found to be inadequate for handling severe flow maldistribution in the plenum of the reactor, for it can only moderately improve the flow distribution existing below the plate, but cannot alleviate "spouts" and major operational upset conditions which lead to .
~3~
an uneven depth of hydrogen in the plenum chamber, which can cause a greater length of the tail pipe slot to be exposed with a corresponding increase in hydrogen flow to those particular riser tubes. Such maldistribution flow conditions in a reactor plenum can be more or less constant depending on the manner in which the feed streams and recycle streams are introduced into the plenum Also, flow maldistribution could possibly occur as a sloshing effect where the liquid level in the plenum below the distribution grid is constantly tilting from one direction to another~
The use in such ebullated bed catalytic reactors of con-ventional cylindrical riser flow tubes covered by cylindrical-shaped bubble caps is disclosed by U. S. Patent No. 3,1979286 to Farkas et al; U. ~. 3,197,288 to Johanson, and U. S. 3,475,134 to Weber et al. However, it has been found that inadequate distribution if the gas and liquid flows are usually provided by these reactor designs.
Accordingly, improvements in flow distribution in ebullated bed catalytic reactors have been sought. An improved staged grid plate configuration has now been deve-loped which more effectively redistributes the gas and liquid flows below the primary grid plate whenever flow maldistribution problems exist below the grid, so as to pro-vide more uniform ebullation of the catalyst bed in the reactor. To aid in maintaining a "smooth" liquid level in the plenum and consequently a reasonably equal length of slot exposure on each riser tube for gas flow into each tube, a secondary grid plate is provided below the primary grid.
This secondary grid is similar to the single flow distribution grid presently used in ebullated bed reactors, however, the secondary grid does not have caps over the riser ~ 3'~8~
tubes on the upper side of the plate, but uses only slotted tubes attached to a plate which extends to near the inner walls of the reactor.
SUMMARY O~ INYEN~ION
This inven~ion proYides a staged distribution grid plate assembly and method used ~or improved flow distribution upwardly into an ebullated catalyst bed of a reactor vessel, in which a lower secondary flow distribution grid feeds gas and liquid flow upwardly to a upper primary flow distribution grid, and thence into the ebullated bed of the reactor. The flow tubes provided in the lower secondary grid plate are uniformly spaced and are relatively larger in diameter and have greater total cross-sectional area than flow tubes in the upper primary distribution grid, so that the grea~er and controlling pressure differential ocours across the upper primary grid plate to provide a more uni~orm flow distribution upwardly into the ebullated bed. This staged grid plate arrangement or assembly enables the upper primary grid to operate more effectively, so that the ebullated catalyst bed above the prinary grid plate will have a more uniform distribution of gas and liquid flowing upwardly therethrough across the entire cross-sectional area of the reactor.
In the staged grid plate assembly of the present invention, the upper primary grid plate can be supported from either the react~r lower head or ~rom th~ reactor L~ wall, and the lower secondar~ grid plate is usually supported from the upper primary grid, such as by multiple spacer rods extending ~9..;~3'7~4 between the two grids. Alternatively, the secondary gri d plate can be separately supported from the reactor lower head or wall, or it can be structurally integrated with the primary upper grid plate so as to help withstand the total differential pressure across the grid assembly caused by-the ~d fluid flow through the grids. Also, the lower secondary grid plate can be attached integrally to the primary upper plate by an extension of the primary flow tubes below the upper plate and rlgidly attached to the lower secondary plate, so that the ca ~ yst bed weight and total pressure diEferential across koth plates in the grid plate assembly is carried by the assembly.
More specifically, the present invention comprises a staged grid plate assembly for providing uniform flow distribution of a gas/liquid mixture upwardly into an ebullated bed of a ~reactor, said grid plate assembly comprising an upper primary gr~d plate supported w~thin the reactor near the lower end of the reactor, said primary grid plate containing multiple flow pr~y distribution tubes exte~ng substantially vertically through said plate, said primary tubes being uniformly sized and spaced in the plate, a cap covering the upper end of each tube in said primary grid, said cap being rigidly attached to and spaced outwardly from the tube upper end above the grid plate, so as to permit flow of fluid upwardly through the tubes and then outwardly from under the lower edges of the cap into the ebullated bed; and a lower secondary grid plate located below and spaced from said primary grid plate, said secondary grid plate containing multiple flow secon~ distribution tubes passing subs~ntially Yertically through the secondary plate, said secondary tubes having uniform diameter and spacing, whereby fluid passes upwardly through the flow tubes in the secondary grid, and .
3~7~
then upwardly through the flow tubes in the primary grid and outwardly from under the lower edges of the caps to provide uniform fluid flow in the reactor ebullated bed.
In another aspect of the invention, it comprises a method for uniformly distributing gas and liquid flow upwardly into an ebullated bed reactor, wherein the method comprises introducing gas and liquid flow streams into a plenum located at the lower end of a reactor below a flow distribution grid;
passing said gas and liquid flow upwardly from said plenum through multiple tubular flow passages located in a secondary grid plate into an interim zone located above the secondary grid plate and below a primary grid plate; remixing and redistributing the gas and liquid flow in said interim zone above said lower grid plate; and passing the remixed gas and liquid upwardly through multiple tubular flow passages located in said upper primary grid plate, then under bubble caps each located over said multiple upper flow passages and uniformly into an ebullated catalyst bed of the reactor.
~RIEF DESCRIPTION OF DRAWINGS
FIG. 1 shows a partial vertical sectional view through the lower portion of a reactor vessel containing a staged grid plate assembly havintl multiple riser tubes therein in accordance with the invention.
FIG. 2 shows a portion of the primary upper grid plate containing multiple riser flow tubes each covered by a single bubble cap and containing a ball check.
FIG. 3 shows a partial vertical sectional view of an alternative staged grid plate assembly in which both grid plates are supported from the reactor lower head.
3'~74 FIG. 4 shows a partial sectional view of an alternative grid plate assembly in which the staged grid plates~ are structurally integrated into a single unit supported from the reactor wall.
DESCRIPTION OF INVENTION
In liquid phase catalytic reactors for contacting liquids, gases and par iculate solids, ~t is very important for achieving comple~e and effective catalytic reactions that the upflowing liquid and gas mixture be uniformly distributed across the entire horizontal cross-section of the reactor vessel~ so as to maintain the bed of partioulate solids or catalyst in a uniformly expanded condition with random motion of the catalys~. For certain reactions, such as the catalytic hydrogenation oF heavy oils or coal-oil slurries or the hydrocracking o~ heavy hydrocarbon feedstreams at elevated temperature and pressure conditions, such as at 500-1000F
temperature and 500-5000 psig pressure, to produce lower-boiling liquid fractions, flow maldistribution through the reactor flow distributor or grid plate assembly can cause relatively inactive zones in the bed where the catalyst is not in uniform random motion. This condition leads to the undesired formation of agglomerates of catalyst particles by coking of the hot oil or slurry. The desired uniform flow distribution upwardly through the grid plate into the ebullated catalyst bed can be impaired either by restrictions occurring in the riser tubes due to coking, or by catalyst particles in the tubes. The pr2sent invention provides an effective solution to these flow maldistribution problems in the ebullated catalyst bed.
~3'7~7~
The flow distributor or grid plate assembly must also function to prevent catalyst particles from draining down-wardly back through the distributor whenever the reactor is shutdown, while most of the liquid contained within the catalyst bed is drained down to below the bed. If catalyst is allowed to drain bark through the grid plate flow distri-butor, it can plug the flow passages therein and interfere with operations so that re-ebullating the catalyst bed be-comes very difficult because the flow passages are at least partly restricted. Furthermore, such restrictions can pro-duce undesired flow maldistribution in the catalyst bed. To prevent such backflow of catalyst, a ball check valve is usually pr~vided in each riser tube.
In the present invention, two grid plates are provided supported in a reactor vessel in ~eries flow relationship so that a relatively more unifonm flow distribution upwardly into the ebullated catalyst bed above the upper primary gr~d plate ~s thereby ~ch~eved. It is thus a basic feature of the present invention that both grid plates contain multiple flow tubes having uniform size and spacing, with only the tubes in the upper grid plate having caps covering the upper ends of the tubes. The flow tubes used in the secondary grid plate should be uniformly spaced and have relatively larger diameter and total cross-sectional area than the flow tubes in the upper primary grid plate. The secondary flow tubes do not necessarily need to be cylindrical in shape but can be square, rectangular) or triangular in cross-seotional shape or practically any configuration can be employe~. However, the combination of tube effective diameter and number of tubes should provide the desired uniform flow and differential pressure across the secondary grid, which should be between about 0.10 and 0.90 ~ 3'~7~
times the different7al pressure across the upper primary grid. Also, the length/diameter ratio for the secondary tubes should be at least about 1.0, and usually need not exceed aboùt 5Ø
In operation, the gas liquid mixture which passes through the multiple flow tubes ~in the lower secondary grid is redis~ributed in the horizontal space between the two grid plates. Thus, the flow of gas/liquid mixture flowing through the multiple flow tubes in the upper primary grid into the ebullated bed will be more uniform than when only a single grid plate is used.
As generally shcwn Ln FI~. 1, reactor vessel 10 contaLns primary upper grid plate 12 which is rigidly supported therein usually at its outer edges by a cylindrical shaped support skirt 13 connected to the reaotQr lower head 14, and is sealed to the s1de wall ~n the lower portion of the reactor, so as to provlde a plenum space 15 be1~ a lower secondary grid plate 30. The feedstream to the reactor enters through conduit ll and the flow is deflected radially outwardly by stationary baffle lla. The upper primary grid plate 12 serves to support catalyst bed 25 and contains multiple riser flow tubes 16. As shown in greater detail in Fl~. 2, each prima ~ riser tube 16 has at least one opening or slot 17 at its upper end and is covered by a cap 18, which is rigi~ly attached to the upper end of tube 16 by suitable fastening means 19~ such as a threaded bolt an~ nut.
The lcwer end of cap 18 is spaced outwardly from tube 16 to provide for uniform flow of fluid upwardly through the tubes 16 and slot 17 of the grid plate 12 and into the bed 25 of catalyst particles.
As shown in FIG. 2, the lo~er edge of ~he cap 18 is pre-ferably provi~bd with numer~us notches 18a to provide for the loca-~ 3'~
lized exit flow Df gas and promote the formation of small ga;
bubbles in bed 25. The notches are intended to let the gas emerge from under the caps 18 ~ ~11 discrete bubbles instead of larye globs of gas, and the notch widths should usually be 5-10 times the catalyst effective particle diameter. The notches located around the bottom of the caps can be used with indiYidual caps of any shape, such ~ a cylindrical or tapered shape. Also to prevent backflow of catalyst from the bed 25 to plenum 15 below the grid plate following reactor shutdown or loss of recycle liquid flow, a ball check 20 is usually provided and is prefera~ly located in the upper end of each riser tube 16, as shown in FI&. 2. The ball check 20 mates with seat 22 provided within the upper end of the riser tube 16 to prevent any backf!ow of catalyst from the bed 25 ~o the plenum 15 below the distributor plate 12. To facilitate the entry of gas suoh as hydrogen into the lower end of the riser tube 16, openings such as holes 23 or vertical slots 24 are provided in the tube below the grid plate 12.
Located below the primary grid plate 12 is a secondary grid plate 30, containing multiple parallel secc~ndary flc~w tu~es 32 each having ope ~ gs such as holes 33 or vertical slot 34 in the lower end thereof. The secondary grid plate 30 is spaced below and usually supported from the upper grid plate 12, such as by multiple rods 36 ~ith each rod having a spacer tube 37 located around the rod for maintaining the desired space 35 between the upper and lower grid plates, as shown in FIG. 1. The secondary grid 30 can be extended to contact support skirt 13, or pre~era~ly can have a small annular spa~e 38 therebetween and be provided with a circumferential skirt 40 extending downwardly from plate 30. The lower end of , . . . .
~.~ 3'~8~ ~
skirt 40 should extend to substantially the same level as the lower ends of secondary flow tubes 32. Also, the skirt 40 is provided with openings such as holes 39 or slots 41, which are similar to holes 33 or slots 34 in the secondary flow tubes 32. Furthermore, the flow area of the annular space 38 should not exceed about lO percent of the total flow area for the openings in the secondary grid plate, i.e. that provided both by multiple flow tubes 3Z and annular flow space 38.
In operation of the dual grid plate assembly, the gas/liq3id mixture fed into pl~n 15 forms a gas space 15a bel~ lower sec~ndary grid plate 30 and abave liqu~d level 15b. me gas an~ liquid mixture in plenum 15 passes upwardly ~hrough multiple flow tubes 32 and annular space 38 into space 35 between the upper and lower grid plates. In space 35, the gas/liquid mixture is redistr~buted generatly horizontally and the gas portion rises to form gas space 35a above the liquid level 35b. The liquid level 35b is controlled by the vertical location of slots 24 in the lower ends of riser tubes 16 and by the flow rate ~hrough the grid plate.
It is thus an advantage of the present invention that the lower secondary grid plate prov1des for the lateral redistribution of fluid flow below the upper primary grid plate and thereby tends to correct any flow maldistribution .below the primary grid plate, which may be caused by flow maldistribution problems on the underside of the grid.
Reactor bed ebullation wfll be generally uniform unless some riser tubes become plugged by coke formation, etc.
In an alternative embodiment of the present invention, as shown in FIG. 3~ ~oth the upper primary grid plate 12 and the lower secondary grid plate 30 can be separately supported ~3'7~
from the reactor lower head 14 by means of an outer cylindrical support skirt 13 for upper grid 12 and an inner cylindrical skirt 45 for supporting the lower grid plate 30.
For this grid plate configuration, the support rods 36 and spacer tubes 3~ used for the FIG. 1 embodiment are not needed. Also, the multiple flow tubes 32 m grid plate 30 are provided with multiple openings 33 or slots 34 to faci-litate the entry of gas such as hydrogen into the flow tubes, similarly as for the flow tubes 16 in the upper grid plate 12. If desired9 dual nozzles 11 for the rea~r f~stream ~ be provided into plenum 15.
It is another important feature of the present invention that the two grid plates can be structurally integrated, ~o that the total pressure differential across the grid plate assembly due to upward fluid flow therethrough and the cata-lyst bed weight is carried by the assembly of bothgridplates.
As shown in FIG. 49 the riser tubes 42 for the primary upper grid plate 12 are ex~ended downwardly and rigidly attached such as by welding to the lower secondary grid plate 30.
Openings such as holes 43 or slots 44 are provided in the lower end of each tube 42 as before, to provide for entry of gas such as hydrogen into the flow tube. Also, the upper primary grid plate 12 can be suitably supported from the reactcr inner wall by a continuous ring 26 welded to the wall. The upper grid plate 12 is attached to ring 26 by multiple fastener bolts 28 and nuts 29. In this grid plate assembly, the periphery of lower grid plate 30 can be extended to near the inner wall of reactor 10 so as to pro-vide a small annular space 46 therebetween, and be provided with a peripheral depending skirt 48 and holes 49 similarly as previously described for the FIG. 1 embodiment.
3~
The utility and effectiveness of the staged flow distri-bution grid assembly is illustrated by the ~ollowing specific example, which should not be construed as l~miting the scope of the invention.
EXAMPLE
In an ebullated bed catalytic hydrogenation reactor for petrole~n feedstoc3c material, a du~l grid assembly provided near the reac~r er end has the foll~wing characteristics and diIrensior~
Reactor Temperature, F 750-850 Reactor Pressure, psig 1000-3009 Reactor Ins~de Diameter9 ft 12 Vertical Spacing Between Primary and Secondary Grid Plates, in. 16 Primary Grid Flow Tube Diameter, in. 1.30 Bubble Cap Diameter, in. 3 Primary Flow Tube Extension Below Primary Grid Plate, in. 9 Flow Area of Primary Grid Tubes, in. Z.16 Secondary Grid Flow Tube Diameter, in. 4 Secondary Flow Tube Extension Below Grid Plate, in. 5 Fl ow Area of Secondary Grid Tubes, in. 12.7 Pressure Differential Across Upper Primary Grid, ~si 5-8 Pressure Differential Across Lower Secondary Grid, psi 1-3 The catalyst ebullation pattern in the reactor is uniform o~er a wide range of liquid and gas flow rates from the plenum upwardly into the reactor bed.
123~7~'74 Although this invention has been described broadly and in terms of certain preferred embodiments thereof, it will be understood that modifications and variations to the apparatus can be made and that some elements can be used without others all within the spirit and ~cope of the invention, which is defined by the following claims.
Claims (17)
1. A staged grid plate assembly for providing uniform flow distribution of a gas/liquid mixture upwardly into an ebullated bed of a reactor vessel, said grid plate assembly comprising:
(a) an upper primary grid plate supported within the reactor vessel near the lower end of said reactor vessel, said primary grid plate containing multiple flow distri-bution tubes extending substantially vertically through said plate, said primary tubes being uni-formly sized and spaced in the plate;
(b) a cap covering the upper end of each tube in said primary grid, said cap being rigidly attached to and spaced outwardly from the tube upper end above the grid plate, so as to permit flow of fluid upwardly through the tubes and then outwardly from under the lower edges of the cap into the ebullated bed; and (c) a lower secondary grid plate located below and spaced from said primary grid plate, said secondary grid containing multiple flow distribution tubes passing substantially vertically through the secon-dary plate, said secondary tubes having uniform diameter and spacing, whereby fluid passes upwardly through the flow tubes in the secondary grid, and then upwardly through the flow tubes in the primary grid and outwardly from under the lower edges of the caps to provide uniform fluid flow in the reactor vessel ebullated bed.
(a) an upper primary grid plate supported within the reactor vessel near the lower end of said reactor vessel, said primary grid plate containing multiple flow distri-bution tubes extending substantially vertically through said plate, said primary tubes being uni-formly sized and spaced in the plate;
(b) a cap covering the upper end of each tube in said primary grid, said cap being rigidly attached to and spaced outwardly from the tube upper end above the grid plate, so as to permit flow of fluid upwardly through the tubes and then outwardly from under the lower edges of the cap into the ebullated bed; and (c) a lower secondary grid plate located below and spaced from said primary grid plate, said secondary grid containing multiple flow distribution tubes passing substantially vertically through the secon-dary plate, said secondary tubes having uniform diameter and spacing, whereby fluid passes upwardly through the flow tubes in the secondary grid, and then upwardly through the flow tubes in the primary grid and outwardly from under the lower edges of the caps to provide uniform fluid flow in the reactor vessel ebullated bed.
2. A grid plate assembly according to claim 1, wherein the total cross-sectional area of secondary flow tubes in the secondary grid plate exceeds that of the primary flow tubes in the primary grid plate.
3. A grid plate assembly according to claim 1, wherein each flow tube in said secondary grid plate has a larger cross-sectional area than each tube in the primary grid plate.
4. A grid plate assembly according to claim 1, wherein said tubes in said lower secondary grid plate have a length/diameter ratio from about 1.0 to about 5Ø
5. A grid plate assembly according to claim 1, wherein said secondary grid plate is supported from said primary grid plate by multiple support rods.
6. A grid plate assembly according to claim 5, wherein said secondary grid plate is spaced below said primary grid plate by a spacer means provided on said support rods.
7. A grid plate assembly according to claim 1, wherein said primary grid plate is attached to the reactor head by a skirt means extending below said primary grid plate to an attachment point below said secondary grid plate.
8. A grid plate assembly according to claim 1, wherein both primary and secondary grid plates are structurally integrated so as to withstand the catalyst bed weight and the total differential pressure across the grid plate assembly.
9. A grid plate assembly according to claim 1, wherein the primary tubes contain check valves to prevent backflow of catalyst from above the grid plate to below the grid.
10. A grid plate assembly according to claim 9, wherein said check valve is a ball and a mating seat located in the upper portion of the riser tube.
11. A staged grid plate assembly for providing uniform flow distribution of a gas/liquid mixture upwardly into an ebullated bed of a reactor vessel, said grid plate assembly comprising:
(a) an upper primary grid plate supported within the reactor vessel near the lower end of said reactor vessel, said primary grid plate containing multiple uniformly spaced flow distribution tubes extending substan-tially vertically through said plate, said primary tubes being uniformly sized and spaced in the plate;
(b) a cap covering the upper end of each tube in said primary grid, said cap being rigidly attached to and spaced outwardly from the tube upper end above the grid plate, so as to permit flow of fluid upwardly through the tubes and then outwardly from under the lower edges of the cap into the ebullated bed; and (c) a lower secondary grid plate located below and spaced from said primary grid plate, said secondary grid containing multiple flow distribution tubes having uniform size and spacing and passing substantially vertically through the secondary plate, said tubes in the secondary plate having uniform diameter and spacing and greater cross-sectional area than tubes in the primary grid plate, whereby fluid passes first upwardly through the flow tubes in the secondary grid, and then upwardly through the flow tubes in the primary grid and outwardly from the lower edges of the caps to provide uniform fluid flow in the reactor ebullated bed.
(a) an upper primary grid plate supported within the reactor vessel near the lower end of said reactor vessel, said primary grid plate containing multiple uniformly spaced flow distribution tubes extending substan-tially vertically through said plate, said primary tubes being uniformly sized and spaced in the plate;
(b) a cap covering the upper end of each tube in said primary grid, said cap being rigidly attached to and spaced outwardly from the tube upper end above the grid plate, so as to permit flow of fluid upwardly through the tubes and then outwardly from under the lower edges of the cap into the ebullated bed; and (c) a lower secondary grid plate located below and spaced from said primary grid plate, said secondary grid containing multiple flow distribution tubes having uniform size and spacing and passing substantially vertically through the secondary plate, said tubes in the secondary plate having uniform diameter and spacing and greater cross-sectional area than tubes in the primary grid plate, whereby fluid passes first upwardly through the flow tubes in the secondary grid, and then upwardly through the flow tubes in the primary grid and outwardly from the lower edges of the caps to provide uniform fluid flow in the reactor ebullated bed.
12. A method for uniformly distributing gas and liquid flow upwardly into an ebullated bed reactor vessel, said method comprising:
(a) introducing gas and liquid flow streams into a plenum located at the lower end of a reactor vessel below a flow distribution grid;
(b) passing said gas and liquid flow upwardly from said plenum through multiple parallel tubular flow passages located in a lower secondary grid plate into an interim zone located above the secondary grid plate and below a primary grid plate;
(c) mixing and redistributing the gas and liquid flow in said interim zone above said lower grid plate; and (d) passing the mixed gas and liquid upwardly through multiple tubular flow passages located in an upper primary grid plate, then under bubble caps each located over said multiple upper flow passages and uniformly into an ebullated catalyst bed of the reactor vessel.
(a) introducing gas and liquid flow streams into a plenum located at the lower end of a reactor vessel below a flow distribution grid;
(b) passing said gas and liquid flow upwardly from said plenum through multiple parallel tubular flow passages located in a lower secondary grid plate into an interim zone located above the secondary grid plate and below a primary grid plate;
(c) mixing and redistributing the gas and liquid flow in said interim zone above said lower grid plate; and (d) passing the mixed gas and liquid upwardly through multiple tubular flow passages located in an upper primary grid plate, then under bubble caps each located over said multiple upper flow passages and uniformly into an ebullated catalyst bed of the reactor vessel.
13. A uniform flow distribution method according to claim 12, wherein the fluid differential pressure across said upper primary grid plate exceeds that which occurs across the lower secondary grid plate.
14. A flow distribution method according to claim 12, wherein the inlet gas and liquid flow streams are each introduced through separate conduits into said plenum, and are each passed around a flow distributor baffle associated with each conduit within said plenum.
15. A flow distribution method according to claim 12, wherein the liquid is a hydrocarbon liquid and the gas is hydrogen.
16. A flow distribution method according to claim 12, wherein the liquid temperature is 500-900°F and the liquid pressure is 500-5000 psig.
17. A method for uniformly distributing gas and liquid flowing upwardly into an ebulaated bed reactor vessel, said method comprising:
(a) introducing a hydrocarbon liquid and hydrogen gas flow streams into a plenum located at the lower end of a reactor vessel below a flow distribution grid;
(b) passing said gas and liquid flow upwardly from said plenum through multiple parallel tubular flow passages located in a lower secondary grid plate into an interim zone located above the secondary grid plate and below a primary grid plate;
(c) mixing and redistributing the gas and liquid flow in said interim zone above said lower grid plate; and (d) passing the mixed gas and liquid upwardly through multiple tubular flow passages located in an upper primary grid plate, then under bubble caps each located over said multiple upper flow passages and uniformly into an ebullated catalyst bed of the reactor vessel, wherein the differential pressure across tubular passages in the primary grid exceeds that across tubular passages in the lower secondary grid plate.
(a) introducing a hydrocarbon liquid and hydrogen gas flow streams into a plenum located at the lower end of a reactor vessel below a flow distribution grid;
(b) passing said gas and liquid flow upwardly from said plenum through multiple parallel tubular flow passages located in a lower secondary grid plate into an interim zone located above the secondary grid plate and below a primary grid plate;
(c) mixing and redistributing the gas and liquid flow in said interim zone above said lower grid plate; and (d) passing the mixed gas and liquid upwardly through multiple tubular flow passages located in an upper primary grid plate, then under bubble caps each located over said multiple upper flow passages and uniformly into an ebullated catalyst bed of the reactor vessel, wherein the differential pressure across tubular passages in the primary grid exceeds that across tubular passages in the lower secondary grid plate.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US54195083A | 1983-10-14 | 1983-10-14 | |
| US541,950 | 1983-10-14 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1237874A true CA1237874A (en) | 1988-06-14 |
Family
ID=24161744
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000464399A Expired CA1237874A (en) | 1983-10-14 | 1984-10-01 | Staged flow distribution grid assembly and method for ebullated bed reactor |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JPS6097041A (en) |
| CA (1) | CA1237874A (en) |
| DE (1) | DE3434336C2 (en) |
| FR (1) | FR2553300B1 (en) |
| GB (1) | GB2148141B (en) |
| ZA (1) | ZA847002B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4715996A (en) * | 1986-10-31 | 1987-12-29 | Amoco Corporation | Bubble cap assembly |
| US5101576A (en) * | 1990-10-22 | 1992-04-07 | Foster Wheeler Energy Corporation | Uni-directional fluidization nozzle and a fluidized bed system utilizing same |
| EP0824961A1 (en) * | 1996-08-23 | 1998-02-25 | Shell Internationale Researchmaatschappij B.V. | Gas sparger for a suspension reactor and use thereof |
| NL1004621C2 (en) * | 1996-11-27 | 1998-05-28 | Ind Tech Res Inst | Distribution of fluids into industrial reaction vessel |
| DE102005050283A1 (en) | 2005-10-20 | 2007-04-26 | Basf Ag | Distributor device for a gas-liquid phase mixture for apparatus |
| DE102005050284A1 (en) * | 2005-10-20 | 2007-05-10 | Basf Ag | Distributor device for a gas-liquid phase mixture for apparatus |
| FR2917306B1 (en) * | 2007-06-12 | 2011-04-15 | Inst Francais Du Petrole | ENCLOSURE CONTAINING A GRANULAR BED AND A DISTRIBUTION OF A GAS PHASE AND A LIQUID PHASE CIRCULATING INTO AN ASCENDING FLOW IN THIS ENCLOSURE |
| FR2933877B1 (en) * | 2008-07-15 | 2011-04-15 | Inst Francais Du Petrole | REACTOR FOR TREATMENT OR HYDROTREATMENT WITH A GRANULAR BED AND AN ESSENTIALLY LIQUID PHASE AND AN ESSENTIALLY GAS PHASE THROUGH THE BED |
| US20120315202A1 (en) * | 2011-06-07 | 2012-12-13 | c/o Chevron Corporation | Apparatus and method for hydroconversion |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE376874A (en) * | ||||
| US3124518A (en) * | 1964-03-10 | Product | ||
| US1743131A (en) * | 1927-10-03 | 1930-01-14 | Victor F Grace | Bubble-tower baffle plate |
| US2876079A (en) * | 1956-03-07 | 1959-03-03 | Exxon Research Engineering Co | Gas distributing arrangement for fluidized solids vessels |
| US3197288A (en) * | 1961-05-29 | 1965-07-27 | Hydrocarbon Research Inc | Catalytic reactor |
| US3197286A (en) * | 1963-02-18 | 1965-07-27 | Hydrocarbon Research Inc | Liquid phase reactor |
| US3367638A (en) * | 1963-10-25 | 1968-02-06 | Leva Max | Gas-liquid contact apparatus |
| US3475134A (en) * | 1965-05-05 | 1969-10-28 | Hydrocarbon Research Inc | Liquid phase reactor |
| GB1191220A (en) * | 1968-07-05 | 1970-05-13 | Shell Int Research | Process and apparatus for carrying out chemical reactions |
| DE2262359A1 (en) * | 1972-12-20 | 1974-06-27 | Bayer Ag | DISTRIBUTION FLOOR |
| FR2529905B1 (en) * | 1982-07-09 | 1988-04-08 | Inst Francais Du Petrole | PROCESS AND DEVICE FOR HYDROPROCESSING HYDROCARBONS IN LIQUID PHASE, IN THE PRESENCE OF A CATALYST IN EXPANDED OR BOILING BED |
| ZA835908B (en) * | 1982-09-09 | 1984-05-30 | Hri Inc | Fluid flow distribution system for ebullated bed reactor |
| US4764347A (en) * | 1983-04-05 | 1988-08-16 | Milligan John D | Grid plate assembly for ebullated bed reactor |
-
1984
- 1984-09-06 ZA ZA847002A patent/ZA847002B/en unknown
- 1984-09-19 DE DE3434336A patent/DE3434336C2/en not_active Expired - Lifetime
- 1984-10-01 CA CA000464399A patent/CA1237874A/en not_active Expired
- 1984-10-09 JP JP59210604A patent/JPS6097041A/en active Granted
- 1984-10-11 FR FR848415613A patent/FR2553300B1/en not_active Expired - Lifetime
- 1984-10-12 GB GB08425858A patent/GB2148141B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| FR2553300B1 (en) | 1992-08-14 |
| JPH0432695B2 (en) | 1992-06-01 |
| DE3434336A1 (en) | 1985-05-02 |
| FR2553300A1 (en) | 1985-04-19 |
| DE3434336C2 (en) | 1995-04-27 |
| GB8425858D0 (en) | 1984-11-21 |
| ZA847002B (en) | 1985-05-29 |
| JPS6097041A (en) | 1985-05-30 |
| GB2148141A (en) | 1985-05-30 |
| GB2148141B (en) | 1987-05-28 |
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