CA1172832A - Reactor having dual upflow catalyst beds - Google Patents
Reactor having dual upflow catalyst bedsInfo
- Publication number
- CA1172832A CA1172832A CA000353100A CA353100A CA1172832A CA 1172832 A CA1172832 A CA 1172832A CA 000353100 A CA000353100 A CA 000353100A CA 353100 A CA353100 A CA 353100A CA 1172832 A CA1172832 A CA 1172832A
- Authority
- CA
- Canada
- Prior art keywords
- bed
- reactor
- catalyst bed
- grid plate
- effluent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- 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
- B01J8/0005—Catalytic processes under superatmospheric pressure
-
- 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
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
- B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
This invention provides a vertical catalytic reactor containing two catalyst beds located one above the other and connected in parallel flow arrangement. The effluent from the lower catalyst bed bypasses the adjacent upper bed, and the effluents from both beds are combined and pass out of the reactor at its upper end. A conical grid plate directing uni-form fluid flow to the lower catalyst bed is supported prin-cipally on rigid thermal insulation in the lower head, and is restrained from upward movement by tension members. The lower grid assembly also supports the upper catalyst bed and its grid plate.
This invention provides a vertical catalytic reactor containing two catalyst beds located one above the other and connected in parallel flow arrangement. The effluent from the lower catalyst bed bypasses the adjacent upper bed, and the effluents from both beds are combined and pass out of the reactor at its upper end. A conical grid plate directing uni-form fluid flow to the lower catalyst bed is supported prin-cipally on rigid thermal insulation in the lower head, and is restrained from upward movement by tension members. The lower grid assembly also supports the upper catalyst bed and its grid plate.
Description
7~ 7~3~
-- REACTOR HAVI~1G DUAL UPFL_~ CATALYST BEDS
~AcKGRourlD OF ~HE INVENTION
This invention ~ertains to pressurized reactors con-tainin~ upflow catalytic beds, and particularly to such a reactor having dual ebullated catalyst beds arranged for parallel upflow ~f the feedstream inside a single pressurizable shell, and a process for using same.
As design flow rates for high pressure catalytic reac~ion processes, such as petroleum residuum conversion, - 1 hydrocarbon ~pgrading and coal liquefaction and hydrogenation, increase to the point of requiring multiple reactors, such as 4 to 10 units connected in parallel or parallel/series arrangements, the investment costs for such multiple reactors increase substantially. Such cost increases are due in large ' part to the increased number of high pressure vessel heads required for the construction of the reactors.
In order to minimize the number of individual ; pressurized reactor vessels needed ~or large flow capacities, it has been proposed to provide two parallel Elow reaction zones or catalyst beds within a single elongated pressurized vessel. Although this arrangement increases the length of each reactor substantially, it halves the number of expensi-~e dished heads required, and results in significant vverall savings in cost and space needed for the reactor vessels for a particular total feed rate requirement.
Multiple reaction zones in catalytic reactors ha~e been used previously. For example, U.S. Patent No. 2e987,4~B
to Chervenak and U.S. Patent No. 3,183,178 to Wolk show use of ebullated catalyst bed reaction zones connected in series within a single pressure shell ~or petroleum processing.
However, reactors having ebullated catalytic beds connected in parallel within a common pressure shell have apparently no~
~ t 3~
~een ~reviously used. Accordingly, the present inventiorl pro~
vides a reactor having d~al ebullated catalyst beds in parallel flow arrangement, and also in which both reaction zones are preferably supported fro~ a special grid plate assembly ~ocated in the bottom portion of the reactor. The lower grid is supported principally by thermal insulation in the lower head and provides for uniform stress distribution within the grid and lower head during pressure and temperature cycling during process operations.
SUM~ARY OF INVENTION
This invention provides a vertical catalytic reactor having dual catalyst beds located one above the other within a single pressurizable vessel, and a process for its use. The reactor beds are operated in parallel flow arrangement of the feedstream for reaction processes using catalytic upflow fluidized or ebullated catalyst beds. The liquid and gaseous effluent from the lower bed flows around the upper bed and/or through one or more vertical conduits within the upper hed to the reactor outlet opening.
The lower catalyst reaction bed and its grid plate providing for uniform flow distribution in the bed can be sup-ported in any convenient manner, such as by ring support from the reactor shell; however the lower grid plate is preferably supported principally on cast refractory thermal insulation located in the bottom head of the reactor vessel. The upper catalyst reaction bed is supported by its inlet vertical con-duit, which is in turn attached to and supported from the lower grid plate.
It is an advantage of this dual catalyst bed reactor con~iguration that the to~al number of reac~or vessels needed for a particular total eed requirement is reduced in half, as the reactor dual catalyst beds are proYided in tandem within a ,, , common pressure shell. Thus, although each reactor shell is extended in length, fewer dished heads and less external piping are required, thereby resulting in significant overall cost savings. The catalyst beds operate in all-liquid phase, and the effluent from both beds is withdrawn from the top of the comrnon pressure ~essel and passes to a further processing such as external phase separation.
In an alternative design dual ebullated bed reac-or, a plurality of tubular riser conduits are provided which pass through the upper catalyst bed for handling the effluent from the lower catalyst bed, instead of having all the effluent pass around the upper reaction bed. Also, the lower catalyst bed is preferably supported principally on the cast refractory thermal insulation in the bottom head of the reac-tor, and is restrained from appreciable upward movement by a pluralit~ oE tension members extending between the grid assembly and the lower head of the reactor. The upper cata~
lyst bed and iks grid plate assembly are supported from the grid plate assembly for t.he lower catalyst bed.
Suitable operating pressure for this dual catalyst bed reackor can range from at least about 200 psig to as high as 10,000 psig, and reactor temperatures usually range between about 300~F to 1500F. For reactors operating at temperatures above about 400F, the reactor is usually lined internally with solid thermal insulation which is abrasion resistant~
This reactor configuration is particularly useful for the catalytic hydro-processing of hydrocarbon feedstreams, such as for petroleurn conversion and coal hydrogenation, in which the particulate catalyst material is introduced along with the feedstream. The particle size of catalys~s useful for this invention is usually within the range of 20-~00 mesh (U~S.
Sieve Series~ and the catalyst can be any shape such as spherical or extrudates. Used catalyst is withdrawn separa-~7~8~
ately from each bed as required ~o maintain the desirea levelof catalvtic activity. While this invention can be used or reactors having any upflow type particulate catalys~ beds, lt is most advantageously and preferably used for ebullated type catalyst beds as described in U.S. Patent No. Re, 25,770 to Johanson.
.
DESCRIPTIOM OF DRA~}INGS
Figure 1 shows a reactor vessel contain;ng dual catalyst beds connected in parallel flow arrangement.
Figure 2 shows an alternative reactor confiyuration having dual catalyst beds in parallel flow arrangement, with the grid assembly for the lower bed principally supported on the refractory insulation.
Figure 3 shows an enlarged view of the lower grid assembly having tension members between the grid and the lower head.
DESCRIPT N OF THE PR ERRED E _ODIrOENTS
As illustra-ted by Flgure 1, a reactor vessel generally shown at 10 contalns lower catalyst bed 12 and upper catalyst bed 20. The feed liquid for lower bed 12 is provided through annular conduit or passage 14 and then through lower grid plate assembly 16 containing multiple openings or nozzles 16a. The catalyst bed is expanded by the upflowing feed stream, which is usually a mixture of liquid and gas, to upper level 12a.
The grid plate assembly 16 is supported principally by refractory insulation 17 situated within lower head 18 of the vessel, so as to provide for uniform differen-tial thermal expansion of the grid plate 16 relative to the vessel wall and - head 18. Grid plate assembly 16 is also res-~rained rom .: .
: ~ 4 -
-- REACTOR HAVI~1G DUAL UPFL_~ CATALYST BEDS
~AcKGRourlD OF ~HE INVENTION
This invention ~ertains to pressurized reactors con-tainin~ upflow catalytic beds, and particularly to such a reactor having dual ebullated catalyst beds arranged for parallel upflow ~f the feedstream inside a single pressurizable shell, and a process for using same.
As design flow rates for high pressure catalytic reac~ion processes, such as petroleum residuum conversion, - 1 hydrocarbon ~pgrading and coal liquefaction and hydrogenation, increase to the point of requiring multiple reactors, such as 4 to 10 units connected in parallel or parallel/series arrangements, the investment costs for such multiple reactors increase substantially. Such cost increases are due in large ' part to the increased number of high pressure vessel heads required for the construction of the reactors.
In order to minimize the number of individual ; pressurized reactor vessels needed ~or large flow capacities, it has been proposed to provide two parallel Elow reaction zones or catalyst beds within a single elongated pressurized vessel. Although this arrangement increases the length of each reactor substantially, it halves the number of expensi-~e dished heads required, and results in significant vverall savings in cost and space needed for the reactor vessels for a particular total feed rate requirement.
Multiple reaction zones in catalytic reactors ha~e been used previously. For example, U.S. Patent No. 2e987,4~B
to Chervenak and U.S. Patent No. 3,183,178 to Wolk show use of ebullated catalyst bed reaction zones connected in series within a single pressure shell ~or petroleum processing.
However, reactors having ebullated catalytic beds connected in parallel within a common pressure shell have apparently no~
~ t 3~
~een ~reviously used. Accordingly, the present inventiorl pro~
vides a reactor having d~al ebullated catalyst beds in parallel flow arrangement, and also in which both reaction zones are preferably supported fro~ a special grid plate assembly ~ocated in the bottom portion of the reactor. The lower grid is supported principally by thermal insulation in the lower head and provides for uniform stress distribution within the grid and lower head during pressure and temperature cycling during process operations.
SUM~ARY OF INVENTION
This invention provides a vertical catalytic reactor having dual catalyst beds located one above the other within a single pressurizable vessel, and a process for its use. The reactor beds are operated in parallel flow arrangement of the feedstream for reaction processes using catalytic upflow fluidized or ebullated catalyst beds. The liquid and gaseous effluent from the lower bed flows around the upper bed and/or through one or more vertical conduits within the upper hed to the reactor outlet opening.
The lower catalyst reaction bed and its grid plate providing for uniform flow distribution in the bed can be sup-ported in any convenient manner, such as by ring support from the reactor shell; however the lower grid plate is preferably supported principally on cast refractory thermal insulation located in the bottom head of the reactor vessel. The upper catalyst reaction bed is supported by its inlet vertical con-duit, which is in turn attached to and supported from the lower grid plate.
It is an advantage of this dual catalyst bed reactor con~iguration that the to~al number of reac~or vessels needed for a particular total eed requirement is reduced in half, as the reactor dual catalyst beds are proYided in tandem within a ,, , common pressure shell. Thus, although each reactor shell is extended in length, fewer dished heads and less external piping are required, thereby resulting in significant overall cost savings. The catalyst beds operate in all-liquid phase, and the effluent from both beds is withdrawn from the top of the comrnon pressure ~essel and passes to a further processing such as external phase separation.
In an alternative design dual ebullated bed reac-or, a plurality of tubular riser conduits are provided which pass through the upper catalyst bed for handling the effluent from the lower catalyst bed, instead of having all the effluent pass around the upper reaction bed. Also, the lower catalyst bed is preferably supported principally on the cast refractory thermal insulation in the bottom head of the reac-tor, and is restrained from appreciable upward movement by a pluralit~ oE tension members extending between the grid assembly and the lower head of the reactor. The upper cata~
lyst bed and iks grid plate assembly are supported from the grid plate assembly for t.he lower catalyst bed.
Suitable operating pressure for this dual catalyst bed reackor can range from at least about 200 psig to as high as 10,000 psig, and reactor temperatures usually range between about 300~F to 1500F. For reactors operating at temperatures above about 400F, the reactor is usually lined internally with solid thermal insulation which is abrasion resistant~
This reactor configuration is particularly useful for the catalytic hydro-processing of hydrocarbon feedstreams, such as for petroleurn conversion and coal hydrogenation, in which the particulate catalyst material is introduced along with the feedstream. The particle size of catalys~s useful for this invention is usually within the range of 20-~00 mesh (U~S.
Sieve Series~ and the catalyst can be any shape such as spherical or extrudates. Used catalyst is withdrawn separa-~7~8~
ately from each bed as required ~o maintain the desirea levelof catalvtic activity. While this invention can be used or reactors having any upflow type particulate catalys~ beds, lt is most advantageously and preferably used for ebullated type catalyst beds as described in U.S. Patent No. Re, 25,770 to Johanson.
.
DESCRIPTIOM OF DRA~}INGS
Figure 1 shows a reactor vessel contain;ng dual catalyst beds connected in parallel flow arrangement.
Figure 2 shows an alternative reactor confiyuration having dual catalyst beds in parallel flow arrangement, with the grid assembly for the lower bed principally supported on the refractory insulation.
Figure 3 shows an enlarged view of the lower grid assembly having tension members between the grid and the lower head.
DESCRIPT N OF THE PR ERRED E _ODIrOENTS
As illustra-ted by Flgure 1, a reactor vessel generally shown at 10 contalns lower catalyst bed 12 and upper catalyst bed 20. The feed liquid for lower bed 12 is provided through annular conduit or passage 14 and then through lower grid plate assembly 16 containing multiple openings or nozzles 16a. The catalyst bed is expanded by the upflowing feed stream, which is usually a mixture of liquid and gas, to upper level 12a.
The grid plate assembly 16 is supported principally by refractory insulation 17 situated within lower head 18 of the vessel, so as to provide for uniform differen-tial thermal expansion of the grid plate 16 relative to the vessel wall and - head 18. Grid plate assembly 16 is also res-~rained rom .: .
: ~ 4 -
2~3~
substantial upward rnovement due to differential pressure across the nozzles by inlet conduit 15. Fresh catalyst is provided mixed with th~ feed as needed, and used catalyst is withdrawn through con~uit 13 as needed to maintain the desired catalytic activity within the bed.
Upper catalyst bed 20 is arranged in parallel fluid flow arrangement with the lower bed 12, with the feed liquid being provided flowing upwardly through central inlet conduit 21. Catalyst bed 20 is similarly expanded by the upflowing fluid to level 20a. The central conduit 21 also provides ~he support for upper catalyst bed 20 and grid plate assembly 22 from lower grid assembly 16. The effluent flow from lower bed 12 passes around upper bed 20 through annular passageway 24l and is combined with the effluent from upper bed 20 beLor4 it leaves the reactor vessel at outlet opening 26. Fresh cata-lyst is provided mixed with the feedstream as needed, and used catalyst is withdrawn through conduit 23 similarly as for the lower bed, with conduit 23 being preferably located within inlet flow conduit 21. The length/diameter ratio for each catalyst bed in its settled condition should be between about 1 and 10, with lower ratios usually being used for larger dîameter beds, and ~he percent bed expansion during operations should be between about 30 and 150% of its settled height. For reactors having normal operating tempera~ures above about 400F, an internal thermal insulation lining 19 is usually pro-vided of erosion-resistant solid refractory type insulation, such as '~ractocrete"~o. 3400 available from Combustion Engineering Company. ( Fractocrete" is a trademark) Figure 2 shows an alternative flow configuration ~or the upper catalyst bed 20 in reactor 10. In addition to pro-viding annular passageway 24 around the bed for Elow of the effluent from the lower ~atalyst bed 1~, a plurality of generally vertical conduits 28 are also provided through the bed~ Conduits ~8 pass through upper grid 22 and extend to a , '' level above the expanded catalyst ~ed level 20a. Thus, if for : any reason the annular flo,7 passagewa~ 24 becomes obstructed : ~5_ . , ~ ~7~32 during operations, the additional ~low passayeways 28 are a~ailable to convey -the effluent from lower bed 12 to outlet 26. A7so, the upper bed 20 and grid pla~e 22 are supported by flow conduit 21, which is in turn supported by lower grid 16 principally by the refractory insulation 17 situated wi-thin lower head 18. This grid support arrangement provides for uniform differential thermal expansion of the grid plate 16 relative to reactor wall 19. A layer 17a of refractory fibers, such as "Kaowool" , provided by Babcock.~Jilcox Co., is prefer-ably placed between the lower plate of grid 16 and the refrac-tory insulation 17 to provide for more uni~orm contact between these elements. Also as mentioned, lower grid plate assembly 16 is restrained ~rom upward movement due to differential pressure across the grid nozzles 22a by a plurality of tension members 30 extending :Erom the grid assembly 16 through refrac-tory insulation 17 to reactor lower head 1~. Compression spring means 32, pre~erably a Belleville type spring, is pro-vided at the upper end oE memher 30 to accommodate thermal expansion of ~tructural parts and pro~ide a net downward ~orce on the grid against insulation 17v ~s shown by Figure 3, a pressure-tight cap 34 is provided to retain reactor pres~$ure within the grid assembly 16. Spring 32 also restrains upward movement of the grid.
Although the lower grid plate assembly 16 is sup-ported principally by rigid insulation 17 shown being used with dua:L catalyst beds, this grid assembly can also be used advantageously in a reactor having a single ca-talyst bed.
Although I have disclosed certain preferred embodi~..
ments of my invention, it is recognized tha-t modifications can be made thereto and -that some :Eeatures can be empl.oyed without others all within -the spirit and s.cope of ~.he invention~ which is defined solely by the following claims.
*Trade mark ~ 6
substantial upward rnovement due to differential pressure across the nozzles by inlet conduit 15. Fresh catalyst is provided mixed with th~ feed as needed, and used catalyst is withdrawn through con~uit 13 as needed to maintain the desired catalytic activity within the bed.
Upper catalyst bed 20 is arranged in parallel fluid flow arrangement with the lower bed 12, with the feed liquid being provided flowing upwardly through central inlet conduit 21. Catalyst bed 20 is similarly expanded by the upflowing fluid to level 20a. The central conduit 21 also provides ~he support for upper catalyst bed 20 and grid plate assembly 22 from lower grid assembly 16. The effluent flow from lower bed 12 passes around upper bed 20 through annular passageway 24l and is combined with the effluent from upper bed 20 beLor4 it leaves the reactor vessel at outlet opening 26. Fresh cata-lyst is provided mixed with the feedstream as needed, and used catalyst is withdrawn through conduit 23 similarly as for the lower bed, with conduit 23 being preferably located within inlet flow conduit 21. The length/diameter ratio for each catalyst bed in its settled condition should be between about 1 and 10, with lower ratios usually being used for larger dîameter beds, and ~he percent bed expansion during operations should be between about 30 and 150% of its settled height. For reactors having normal operating tempera~ures above about 400F, an internal thermal insulation lining 19 is usually pro-vided of erosion-resistant solid refractory type insulation, such as '~ractocrete"~o. 3400 available from Combustion Engineering Company. ( Fractocrete" is a trademark) Figure 2 shows an alternative flow configuration ~or the upper catalyst bed 20 in reactor 10. In addition to pro-viding annular passageway 24 around the bed for Elow of the effluent from the lower ~atalyst bed 1~, a plurality of generally vertical conduits 28 are also provided through the bed~ Conduits ~8 pass through upper grid 22 and extend to a , '' level above the expanded catalyst ~ed level 20a. Thus, if for : any reason the annular flo,7 passagewa~ 24 becomes obstructed : ~5_ . , ~ ~7~32 during operations, the additional ~low passayeways 28 are a~ailable to convey -the effluent from lower bed 12 to outlet 26. A7so, the upper bed 20 and grid pla~e 22 are supported by flow conduit 21, which is in turn supported by lower grid 16 principally by the refractory insulation 17 situated wi-thin lower head 18. This grid support arrangement provides for uniform differential thermal expansion of the grid plate 16 relative to reactor wall 19. A layer 17a of refractory fibers, such as "Kaowool" , provided by Babcock.~Jilcox Co., is prefer-ably placed between the lower plate of grid 16 and the refrac-tory insulation 17 to provide for more uni~orm contact between these elements. Also as mentioned, lower grid plate assembly 16 is restrained ~rom upward movement due to differential pressure across the grid nozzles 22a by a plurality of tension members 30 extending :Erom the grid assembly 16 through refrac-tory insulation 17 to reactor lower head 1~. Compression spring means 32, pre~erably a Belleville type spring, is pro-vided at the upper end oE memher 30 to accommodate thermal expansion of ~tructural parts and pro~ide a net downward ~orce on the grid against insulation 17v ~s shown by Figure 3, a pressure-tight cap 34 is provided to retain reactor pres~$ure within the grid assembly 16. Spring 32 also restrains upward movement of the grid.
Although the lower grid plate assembly 16 is sup-ported principally by rigid insulation 17 shown being used with dua:L catalyst beds, this grid assembly can also be used advantageously in a reactor having a single ca-talyst bed.
Although I have disclosed certain preferred embodi~..
ments of my invention, it is recognized tha-t modifications can be made thereto and -that some :Eeatures can be empl.oyed without others all within -the spirit and s.cope of ~.he invention~ which is defined solely by the following claims.
*Trade mark ~ 6
Claims (17)
1. A process for catalytically reacting a feedstock, comprising the steps of:
(a) introducing a portion of the feedstock into a catalyst bed located in the lower portion of a vertically oriented reactor vessel;
(b) introducing the remaining portion of the feedstock into a catalyst bed located in the upper portion of the reactor vessel;
said catalyst beds operating in all-liquid phase;
(c) passing the effluent from the lower catalyst bed upwardly to bypass the upper catalyst bed;
and (d) combining the effluent from both catalyst beds and withdrawing it from the reactor vessel at its upper end as a common effluent stream.
(a) introducing a portion of the feedstock into a catalyst bed located in the lower portion of a vertically oriented reactor vessel;
(b) introducing the remaining portion of the feedstock into a catalyst bed located in the upper portion of the reactor vessel;
said catalyst beds operating in all-liquid phase;
(c) passing the effluent from the lower catalyst bed upwardly to bypass the upper catalyst bed;
and (d) combining the effluent from both catalyst beds and withdrawing it from the reactor vessel at its upper end as a common effluent stream.
2. The process of claim 1 wherein all the effluent from the lower catalyst bed flows upwardly around the periphery of the upper catalyst bed.
3. The process of claim 1 wherein effluent from the lower catalyst bed bypasses the upper catalyst bed by passing upwardly through a plurality of conduits extending through the upper catalyst bed.
4. The process of claim 1 wherein the feedstock is a heavy hydrocarbon liquid to produce lower boiling gas and liquid effluent products by catalytic reaction within the pressure range of 200 to 10,000 psig and temperature of 300 to 1500°F.
5. A vertically oriented catalytic reactor assembly comprising:
(a) a pressurizable vessel having upper and lower heads;
(b) a catalyst bed located in the lower portion of the vessel and above a grid plate;
(c) a catalyst bed located in the upper portion of the vessel and supported from the lower bed ?-grid plate by an elongated inlet pipe, said upper bed being adapted so that effluent from the lower bed can bypass the upper bed;
(d) conduit means for introducing a feedstream into said lower catalyst bed;
(e) conduit means for separately introducing a feedstream into said upper catalyst bed; and (f) outlet means for withdrawing the combined effluent stream from both catalyst beds of the reactor at the upper end of said reactor.
(a) a pressurizable vessel having upper and lower heads;
(b) a catalyst bed located in the lower portion of the vessel and above a grid plate;
(c) a catalyst bed located in the upper portion of the vessel and supported from the lower bed ?-grid plate by an elongated inlet pipe, said upper bed being adapted so that effluent from the lower bed can bypass the upper bed;
(d) conduit means for introducing a feedstream into said lower catalyst bed;
(e) conduit means for separately introducing a feedstream into said upper catalyst bed; and (f) outlet means for withdrawing the combined effluent stream from both catalyst beds of the reactor at the upper end of said reactor.
6. The reactor assembly of claim 5 wherein the upper catalyst bed has an outside diameter smaller than the vessel inner wall, said bed being centrally located to provide an annular space between the catalyst bed and inner wall sur-face of the reactor for passage of effluent from the lower bed.
7. The reactor of claim 5 wherein the upper cata-lyst bed contains a plurality of conduits extending vertically therethrough for passing effluent from the lower bed to the reactor outlet means.
8. The reactor of claim 5 wherein the upper cata-lyst bed is supported from the flow distributor grid of the lower bed.
9. The reactor of claim 5, wherein the lower grid plate is supported principally by solid thermal insulation in the lower head and is restrained from substantial upward move-ment by a plurality of tension members extending between the grid and the lower head of the reactor.
10. The reactor of claim 5 wherein the reactor is internally lined with solid thermal insulation.
11. A vertically oriented catalytic bed type reactor assembly, comprising:
(a) a pressurizable vessel having upper and lower heads and containing internal solid type ther-mal insulation adjacent to its inner wall;
(b) a lower catalyst bed located in the lower por-tion of the vessel and above a flow distribu-tion grid plate, said grid plate being supported principally by solid thermal insulation located in the lower head;
(c) an upper catalyst bed located in the upper por-tion of the vessel and supported from the lower flow distribution grid plate by an elongated inlet pipe, said upper bed being adapted so that effluent from the lower bed bypasses the upper bed;
(d) conduit means for introducing a pressurized feed stream upwardly through said lower grid plate;
(e) conduit means for separately introducing a feedstream into the upper catalyst bed;
(f) structural means for restraining upward move-ment of the lower grid plate due to pressure differential existing therein; and (g) outlet means for withdrawing the combined effluent stream from both catalyst beds of the reactor at the upper end of said reactor.
(a) a pressurizable vessel having upper and lower heads and containing internal solid type ther-mal insulation adjacent to its inner wall;
(b) a lower catalyst bed located in the lower por-tion of the vessel and above a flow distribu-tion grid plate, said grid plate being supported principally by solid thermal insulation located in the lower head;
(c) an upper catalyst bed located in the upper por-tion of the vessel and supported from the lower flow distribution grid plate by an elongated inlet pipe, said upper bed being adapted so that effluent from the lower bed bypasses the upper bed;
(d) conduit means for introducing a pressurized feed stream upwardly through said lower grid plate;
(e) conduit means for separately introducing a feedstream into the upper catalyst bed;
(f) structural means for restraining upward move-ment of the lower grid plate due to pressure differential existing therein; and (g) outlet means for withdrawing the combined effluent stream from both catalyst beds of the reactor at the upper end of said reactor.
12. The assembly of claim 11 wherein said flow distribution grid plate contains a plurality of nozzle openings in its upper surface, and the upward movement restraining means comprises multiple rods connecting the grid to to the lower head.
13. The assembly of claim 11 wherein said flow distribution grid plate is restrained from upward movement by a tubular connection between the inner diameter of the grid and the reactor inlet nozzle opening.
14. A vertically oriented catalytic bed type reactor assembly, comprising:
(a) a pressurizable vessel having upper and lower heads;
(b) a lower catalyst bed located in the lower portion of the vessel and above a flow distribution grid plate, said grid plate being supported principally by solid thermal insulation located in the lower head;
(c) an upper catalyst bed located in the upper portion of the vessel and supported from the lower flow distribution grid plate by a vertical inlet conduit, said upper bed being adapted so that effluent from the lower bed can bypass the upper bed;
(d) conduit means for introducing a pressurized feed stream upwardly through said grid plate;
(e) structural means for restraining upward movement of the grid plate due to pressure differential existing therein; and (f) outlet means for withdrawing the effluent stream from the catalyst bed.
(a) a pressurizable vessel having upper and lower heads;
(b) a lower catalyst bed located in the lower portion of the vessel and above a flow distribution grid plate, said grid plate being supported principally by solid thermal insulation located in the lower head;
(c) an upper catalyst bed located in the upper portion of the vessel and supported from the lower flow distribution grid plate by a vertical inlet conduit, said upper bed being adapted so that effluent from the lower bed can bypass the upper bed;
(d) conduit means for introducing a pressurized feed stream upwardly through said grid plate;
(e) structural means for restraining upward movement of the grid plate due to pressure differential existing therein; and (f) outlet means for withdrawing the effluent stream from the catalyst bed.
15. The assembly of claim 14 wherein said flow distribution grid plate contains a plurality of nozzle openings in its upper surface, and the upward movement restraining means comprises multiple rods connecting the grid to the lower head.
16. The assembly of claim 14 wherein said flow distribution grid plate is restrained from upward movement by a tubular connection between the inner diameter of the grid and the reactor inlet nozzle opening.
17. The assembly of claim 14 wherein the reactor is internally lined with solid thermal insulation.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US7296279A | 1979-09-06 | 1979-09-06 | |
| US072,962 | 1979-09-06 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1172832A true CA1172832A (en) | 1984-08-21 |
Family
ID=22110846
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000353100A Expired CA1172832A (en) | 1979-09-06 | 1980-05-30 | Reactor having dual upflow catalyst beds |
Country Status (6)
| Country | Link |
|---|---|
| AU (1) | AU6036780A (en) |
| CA (1) | CA1172832A (en) |
| DE (1) | DE3022815A1 (en) |
| GB (1) | GB2060426B (en) |
| NL (1) | NL8003503A (en) |
| ZA (1) | ZA803718B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016028698A1 (en) * | 2014-08-19 | 2016-02-25 | The Alloy Engineering Company | Dual grid catalyst basket and method of independently supporting primary and secondary catalysts |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0155341B1 (en) * | 1983-09-06 | 1988-03-09 | Man Gutehoffnungshütte Gmbh | Standing reactor for the production of methanol |
| CA1225818A (en) * | 1984-01-06 | 1987-08-25 | John D. Milligan | Reactor having dual upflow catalyst beds |
| US4743432A (en) * | 1984-11-16 | 1988-05-10 | M.A.N. Maschinenfabrik Augsburg-Nurnberg | Vertical reactor for the generation of methanol |
| US6102656A (en) * | 1995-09-26 | 2000-08-15 | United Technologies Corporation | Segmented abradable ceramic coating |
| US7179426B2 (en) * | 2002-09-12 | 2007-02-20 | Chevron Phillips Chemical Company, Lp | Large catalyst activator |
| CN101942325B (en) * | 2009-07-09 | 2013-08-28 | 中国石油化工股份有限公司 | Heavy oil hydroprocessing method and reactor |
| CN102453525B (en) * | 2010-10-15 | 2014-07-23 | 中国石油化工股份有限公司 | Multi-stage boiling bed hydrogenation process |
-
1980
- 1980-05-30 CA CA000353100A patent/CA1172832A/en not_active Expired
- 1980-06-12 GB GB8019309A patent/GB2060426B/en not_active Expired
- 1980-06-17 NL NL8003503A patent/NL8003503A/en not_active Application Discontinuation
- 1980-06-19 DE DE19803022815 patent/DE3022815A1/en not_active Withdrawn
- 1980-06-23 ZA ZA00803718A patent/ZA803718B/en unknown
- 1980-07-11 AU AU60367/80A patent/AU6036780A/en not_active Abandoned
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016028698A1 (en) * | 2014-08-19 | 2016-02-25 | The Alloy Engineering Company | Dual grid catalyst basket and method of independently supporting primary and secondary catalysts |
| US10744473B2 (en) | 2014-08-19 | 2020-08-18 | The Alloy Engineering Company | Dual grid catalyst basket and method of independently supporting primary and secondary catalysts |
Also Published As
| Publication number | Publication date |
|---|---|
| DE3022815A1 (en) | 1981-04-02 |
| NL8003503A (en) | 1981-03-10 |
| GB2060426B (en) | 1984-01-25 |
| AU6036780A (en) | 1981-03-12 |
| ZA803718B (en) | 1981-06-24 |
| GB2060426A (en) | 1981-05-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1929908B (en) | Gas distributor for a reactor | |
| AU664117B2 (en) | Bubble column, tube side slurry process and apparatus | |
| US4579647A (en) | Multiphase catalytic process with improved liquid distribution | |
| EP0154492B1 (en) | Multiple-stage reactor system for a moving catalyst bed | |
| CA2304955C (en) | Slurry hydrocarbon synthesis with reduced catalyst attrition and deactivation | |
| EP3259053B1 (en) | Reactor comprising a catalyst support grid | |
| CA1163781A (en) | Reactor for exothermic reactions and process for the preparation of hydrocarbons using this reactor | |
| US5120691A (en) | Process for regulating or checking the thermal level of a pulverulent solid incorporating a heat exchanger with fluidized bed compartments | |
| CA1172832A (en) | Reactor having dual upflow catalyst beds | |
| CA1302054C (en) | Fluidizing gas distribution device | |
| CA1156439A (en) | Moving catalyst bed reactor treating hydrocarbons | |
| US4743433A (en) | Catalytic reactor system | |
| EP1142631A1 (en) | Catalytic reactor for dehydrogenation of ethylbenzene to styrene | |
| US4568523A (en) | Moving catalyst bed reactor | |
| US3492221A (en) | Apparatus and method for conversion of hydrocarbons | |
| EP0905216B1 (en) | Countercurrent reactor with interstage stripping in gas/liquid contacting zones | |
| US2585274A (en) | Catalytic reactor | |
| EP0711331A1 (en) | Catalyst, method and apparatus for a particle replacement system for countercurrent feed-packed bed contact | |
| CA1225818A (en) | Reactor having dual upflow catalyst beds | |
| KR101348119B1 (en) | Reactor for solid/liquid/gas reactions | |
| AU721219B2 (en) | Gas sparger for a suspension reactor and use thereof | |
| JPH0263547A (en) | Entrainment fluidized bed reactor equipped with solid particle flow control means and use thereof | |
| CA1296023C (en) | Process for converting a gaseous feed into an at least partly liquidproduct | |
| EP0752402A1 (en) | Process for dehydrogenation of ethylbenzene to styrene | |
| GB868043A (en) | Distributing gas to fluidized beds |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |