US2898292A

US2898292A - Method for distributing a vapor-liquid feed and apparatus therefor

Info

Publication number: US2898292A
Application number: US694621A
Authority: US
Inventors: Raymond R Halik; Donald F Hill
Original assignee: Socony Mobil Oil Co Inc
Current assignee: ExxonMobil Oil Corp
Priority date: 1957-11-05
Filing date: 1957-11-05
Publication date: 1959-08-04
Anticipated expiration: 1976-08-04

Description

Aug. 4, 1959 R. R. HALIK ET AL METHOD FOR DISTRIBUTING A VAPOR-LIQUID FEED AND APPARATUS THEREFOR 3 Sheets-Sheet 1 Filed NOV. 5, 1957 4, 1959 R. R. HALIK ETAL 2,898,292

METHOD FOR DISTRIBUTING A VAPOR-LIQUID FEED AND APPARATUS THEREFOR Filed Nov. 5, 1957 I5 Sheets-Sheet 2 I 2 n n i E 1 5 v INVENT R5 BY DwlM-"j fii ATTORNEY R. R. HALIK ETAL METHOD FOR DISTRIBUTING A VAPOR-LIQUID- Aug. 4, 1959 FEED AND APPARATUS THEREFOR 3 Sheets-Sheet 3 Filed Novv 5. 1957 I'I'I'I'I'IIA Fig.1).

ATTORNEY United States P tent 2,898,292 METHOD FOR A VAPOR-LIQUID FEED AND APPARATUS THEREFOR Raymond R. Hal ik, Pitman, and Donald F. Hill, West Dptford Township, Gloucester County, N ..l., assignors toSocony Mobil Oil Company, Inc., a corporation of New York Application November 1957, Serial No. 694,621

12 Claims. (Cl. 208-450 The present invent-ion'relates re means for distributing ateed to a reactor which feed comprises a liquid portion and a vaporous and/or gaseous portion. Thus, for ex ample, when hydrodesulfurizingpet'roleumfractions boiling above the gasoline boiling range, i.e., having an initial b'oiling'point of about 400 to "about 450 F at temperatures of about 600 to about 800 F. and 'at pressures of 1-00 to about 500 ip.s;i.g., a portion of the normally liquid hydrocarbon fraction is in the vapor state. Consequently, the introduction of a feed which is mixed phase, i.e., partly in the vapor phase and partly in the liquid phase, presents a problem. Furthermore, since it is generally'accepted by thoseskilled in the art that the hydro- .geri for the de'sulfurization reaction should be intimately mixed with the feed, a further problem is encountered.

A distributor meeting the requirements for distributing a mixed phase feed uniformly over the cross-section of a bed of catalyst must deliver the mixed phase feed in a manner to minimize hydraulic gradient effects. The distributor must also be capable of operating in a satisfactory manner although the volume of the petroleum fraction introduced per unit of time is subject to wide fluctuations.

It has been found that the use of inert pellets, preferably spheres, to supplement the distribution of the feed by the distributing means of the present invention improves the distribution pattern through the bed of catalyst. The layer of inert, i.e., chemically inert, spheres or like particles, provides additional intimate mixing of the hydrogen with the liquid prior to reaction. Furthermore, a layer of inert spheres prevents boiling or disturbance of the catalyst bed. It is particularly desirable to prevent dishing or hollowing-out of the center of thecatalyst bed. Dishing or hollowing-out of the center of the catalyst bed causes the flow of liquid to the center of the bed which results in a poor liquid distribution pattern within the bed.

The problems attendant upon the feeding of a mixed phase material (a material partially in the liquid phase and partially in the vapor phase at the temperature and pressure existing in the reaction zone) have been solved in the manner illustrated in the drawings. In general, the present invention includes a primary distributor constructed and arranged to provide for disengaging the vapor portion of the feed from the liquid portion of the feed while also providing a quiet non-turbulent flow of "the liquid portion of the mixed phase feed from the inlet pipe or pipes" to the outlet nipples of the primar distributor. A secondary distributor constructed and arranged to distribute the mixed phase fe'ed uniformly over the cross-section of the catalyst bed is also provided in several embodiments of the present invention. In con junction with the primary andsecondary distributor a layer of chemically inert spherical pellets or the like is interposed between the distributor and the upper surface of thejcatalystbeda Those skilled in' the art will have a better understanding of the present invention from the following descrip- 2,898,292 Patented Aug; 4, 1959 2 tion taken in conjunction with the drawings in which the same numbers refer to similar parts and in 'Which Figure 1 is a vertical section of'a reactor;

Figure 2 is a plan view of a secondary distributor at line 22 of Figure 1;

Figure 3 is a side elevation ofa feed box of the'primary distributor shown in Figures 1 and 2;

Figure 3a is an end elevation of the feed box shown in Figure 3; I I Figure 4 is a vertical section of a downcornei' shown in Figures 1 and 2; p t

Figure 5 is a vertical section of a reactorshowing 'a primary distributor and secondary'distributor of the present invention and omitting the catalyst bed and the superposed layer of inert pellets for simplicity;

Figure 6 is a plan view of the reactor shown iii sectidh in Figure 5;

Figure 7 is a vertical section of a reactor showiiig primary and secondary distributor of'the present invention and omitting the catalyst bed and the superposed layer of inert pellets for simplicity; v

Figure 8 is a plan view of the primary distributor of Figure 7; V

Figure 9 is a vertical section of a reactor omitting the catalyst bed and superposed layer of inert pellets and showing primary and secondary distributors of the present invention; V

4 Figure 10 is a plan View of the primary distributor of Figure i Figure 11 is a plan view of a secondary distributor showing the distributor nipples in only onequadrant of the plate for simplicity; and

Figure 12 is a vertical section or anenlarged secondary distributor nipple. t a v I Referring to Figure 1; a cylindrical r'eactor shell suitably insulated for the temperatures employed and preferably resistant to co'r'r'osio'ri is provided with a tap 2 and a bottom 3. Bottom 3 is provided with an dutlet conduit 4. Concentric with the vertical axis efeuflet' 4 reactor 1 is provided with a foraminoussolids-fiuids' sa ara'tor 5. The catalyst particles are withheld from en'- tering chamber 5 by any suitable means. This caricomprise a perforated plate 6 supported by channels 7. Piererably, this plate 6 can be omitted and the lower chamber of the reactor 8 can be filled with inert materials such as- Mull ite or Alundum pellets or sph res; A distributor plate 9 is rigidly mounted in any suitable rii'arni'er in reactor 1 vertically spaced from perforated plate 6 a distance to provide for a bed of particle-form solid goat alyst of required depth and a superposed la er of inert pellets, such as"Mull'ite or Alundun'izl Distributor plate 9 is rigidly'moun'ted in reactor 1 and supportedin any suitable manner as by angles 10 and channels not shown. Distributor plate'9 must be mounted substantially horizontally, i.e. the variation from the true horizontal must not be more than about /i-' inch'for'a reactor 6 feet in diameter. 7

In the embodiment of the present invention illustrated in Figure 1 the secondary distributor consists of a fplu ra-lity of distributor channels or boxes 11 suppo ed by secondary distributor plate 9. Each of'thedistributor channels or boxes isprovided with" at least one inlet 12. The construction of distributor channels l'l 'is readily understood by reference to Figures 3 and 3a. Inspection of Figure 3 makes it" manifest that box or channel 1 1 has longitudinal sides which are cut away to leave a central portion 13 flanking the inlet 12 so that the in; coming mixed phase or liquid phase feed cannot now laterally of the inlet but must flow longitudinally a distance sufiicient to permit the flow to become non-turbiF lent. Preferably, central portion or baffle 13 rests upon secondary distributor plate 9 or at least is in close proxirnity thereof, say about 0.25 inch maximum. End 14 of channel or box 11 is provided with a skirt covering approximately the upper one-half area and leaving an opening 15 under the liquid surface as illustrated in Figure 3a. The distance from the plate 9 to the top of channel 11 is preferably equal to or slightly greater than the depth of liquid during operation.

Reactor 1 is provided with an inlet 16 having closure flange l7 and matching closure plate 18. Closure plate 18 preferably is provided with one or more gas inlets 19 constructed and arranged to deliver the gas in a direction parallel or perpendicular to the plane of distributor plate 9. Closure plate 18 is also provided with a liquid phase or mixed phase feed inlet 20 connecting with vapor-liquid tight inlet box 21. Inlet box or primary distributor 21 is provided with a plurality of outlets 22. These outlets are so sized or provided with inlet orifices to provide substantially uniform flow to each pipe 24. Inlet box outlets 22 and distributor channel inlets 12 are connected in a vaporand fluid-tight manner as by pipes 24 so that the feed introduced into inlet box 21 flows to channels 11. To support distributor plate 9 and increase the rigidity thereof distributor plate 9 is provided with ribs 23. Ribs 23 also act to make the flow of liquid across distributor plate less turbulent. Distributor plate 9 is provided with a plurality of outlet nipples 25 having a plurality of serrations or notches 26 equally spaced on the circumference of the outlet nipple. (See Fig. 4.)

Mixed phase feed flows to the reactor inlet 20, thence to primary distributor 21. From inlet box 21 the mixed phase feed flows through primary distributor outlets 22, conduits or pipes 24 and channel inlets 12 to distributor channels or boxes 11. From distributor channels or boxes 11 the mixed phase feed flows over distributor plate 9 until the depth of the liquid on plate 9 is somewhat greater than the height of the bottoms'of the notches 26 in distributor plate outlets 25. The actual liquid level will increase or decrease as the flow rate to the reactor--and thus to each downcomer-is increased or decreased. The distributor plate outlet nipples 25 are distributed substantially as shown in Figure 2. The liquid and vapor flow downwardly through distributor plate nipples 25. The contact of vapors with liquid in the concurrent flow through the nipples 25 and especially through the inert layer 27 intimately mixes the vapors and liquid prior to their entry into the catalyst bed.

The liquid feed, vaporous feed and hydrogen gas flow downwardly through the layer of inert pellets 27. While the primary and secondary distributors are of primary importance in establishing uniform distribution of feed over the cross-section of the catalyst bed 28, the layer of inert pellets contributes to further equalize any nonuniformity which may exist. The mixed phase hydrocarbon feed and hydrogen flows downwardly through the layer of inert pellets, and the bed of particle-form solid catalyst to fiow from the reactor through liquid-vaporsolids separator and thence to 'reactor outlet 4 to fractionating and other finishing processes. can be spaced a negligible distance from solids-liquidvapor separator 5, it is preferred to omit space plate 6 and support the bed of catalyst on a bed of inert pellets filling the lower section of the reactor. When plenum 8 is filled with inerts, plate 6 may be omitted with no ill effect on the operation.

Referring now to Figures 5 and 6; reactor 31 suitably lined to resist corrosion and preferably insulated is proyided with secondary distributor plate 9 similar in construction and arrangement to distributor plate 9 (Figure l) and having distributor plate nipples constructed and arranged as distributor plate nipples 25 (Figure l). Distributor plate 9 is supported and strengthened by angles and ribs as more fully discussed in the de scription of Figures 1 and 2. Reactor 31 is provided with a flange 17 and closure plate 18 similar to those While plate 6 t described in conjunction with Figure 1. Reactor 31 is also provided with a vapor-solids separator similar to that (5) described in the discussion of Figures 1 and 2 and with a liquid products outlet similar to that (4) described in the discussion of Figures 1 and 2.

Primary distributor 21 is a box-like structure open at the top to the reactor and provided with a plurality of outlets 22 in the bottom thereof. The secondary distributor comprises plate 9 and nipples or downcomers 25 similar in size and distribution to plate 9 and nipples 25 in Figures 1 and 2 or distributed as are downcomers 25 in Figure 12. The boxes 11 are similar in construction and purpose to boxes 11 in Figures 1, 2 and 3. Boxes 11 and outlets 22 are connected in any suitable manner bymeans of conduits 12.

The mixed phase feed flows into primary distributor box 21 through inlet 20 which is a conduit of suitable size to permit free flow of the volume of feed charged. The outlet of conduit 20 is in the vicinity of the bottom of box 21. The mixed phase feed enters box 21, the vapors are disengaged in box 21, the liquid portion of the feed flows from box 21 through outlets 22 and conduits 12 to discharge boxes 11. From discharge channels 11 the liquid flows non-turbulently to the downcomers 25 in secondary distributor 9. The liquid portion of the feed flows downwardly through downcomers 25 together with the vaporous portion of the feed and any additional gaseous reactant which can be introduced into the reactor through separate inlets 19. Secondary distributor 9 spreads the feed over the cross-section of the layer of chemically inert pellets (preferably spheres) which improves the substantially uniform distribution of the feed produced by the primary and secondary distributors. Those skilled in the 'art will understand that there is a negligible pressure differential between the space above plate 9 and the space below plate 9.

Referring now to Figures 7 and 8; the mixed phase feed is introduced into the primary distributor 21 through conduit 20. The gaseous reactant, when introduced separately, enters the reactor through one or more pipes 19. The secondary distributor is similar in construction and arrangement of downcomers 25 and ribs 23 to the secondary distributors of Figures 1, 2, 5, 11, and 12. However, in the embodiment of the present invention illustrated in Figures 7 and 8 the primary distributor, while serving the same purpose of disengaging the vaporous portion of the mixed phase feed and delivering the liquid portion of the mixed phase feed to the secondary distributor is of somewhat different construction.

Primary distributor 21 comprises a box, preferably circular, preferably concentric with conduit 20, which rests upon and is supported by secondary distributor plate 9. Primary distributor 21 preferably is constructed as a large conduit having plate 30 mounted in a substantially liquid-tight manner a short distance upwardly from the bottom 0f the conduit. The upper edge of this box 21 may be smooth as shown or provided with a multiplicity of notches. A second conduit 31 is mounted in a substantially liquid-tight manner concentric with conduit 20 on plate 30. Below the plane of plate 30 the periphery of conduit or box 21 is provided with a plurality of notches 32 of suflicient size and number to provide non-turbulent flow of liquid to the downcomers 25 within the periphery of conduit or box 21. The tops of the notches 32 are somewhat above the liquid phase at the tops of downcomers 25.

The flow of feed is as follows: The mixed-phase feed flows through conduit 20 into internal conduit or weir 31. At least a portion of the vapors of the mixed phase feed is disengaged within conduit or weir 31. The liquid portion of the feed and entrained vapors flow over the top of primary weir 31 into the annulus or weir 21. In annulus 21 the disengagement of the vaporous portion of the feed is substantially completed and the liquid portion of ,the feed flowsin a non-turbulent manner over the top ofweir 21 on to secondary distributor plate 9.

Secondary distributor plate 9 is similar in' construction and arrangement of downcomers to plates 9 in Fig .ures 2 and 11. The liquid, disengaged vapors and gaseous reactant, if any, flow in non-turbulent manner through downcomers 25 in distributor plate 9 including those within the area immediately beneath primary distributor 21. The liquid feed, the vapor feed and the gaseous reactant, if any, flow downwardly through downcomers. 25 onto the surface of a layer of chemically inert pellets which further improve the distribution of the mixed ,phase feed and gaseous reactant, if any, over the cross- :section of the catalyst bed beneath the layer of inert ,pellets.

In'Figures 9 and I is-illustrated another embodiment of the present invention. ,-A primary distributor box 21 having a circular, hexagonal, or other suitable shape 'is provided with a plurality of downcomers 32 near the periphery of .the box distributed in 'apattern similar to that shown in Figure 10. Downcomers 32 :arenipples provided with :slots either V-shaped or rectangularshaped with the bottom of the notch appreciably above the outlet edge of conduit 20 to provide non-turbulent flow without hydraulic gradient from'conduit 20 over the surface of box 21. The 'outlet ends of downcomers 32 are slotted similarlyv to provide non-turbulent flow of liquid from downcomers 32 to downcomers 25 in secondary distribution plate -9. Those skilled in the art will understand that at least a portion of the vaporous component of the mixed phase feed is disengaged as the mixed phase feed flows-fromconduit 20 to downcomers 32 "and that the balance of the vaporous portion of the mixed phase feed is disengaged when the feed flows from downcomers 32 to downcomers 25 in non-turbulent-manner. As in the other embodiments of the present invention the liquid component flows from secondary distribution plate 9 downwardly through downcomers 25 onto-a layer of inert pellets resting on thetop of the bed of particle-form catalyst. 'Due to the negligible pressure differential between the space under plate 9 and above plate 9 the vaporous component of the mixed phase feed and the gaseous reactant, if any, flow concurrently with the liquid component of the mixed phase feed downwardly through-downcomers 25 onto and throughthe layer of inert pellets and the bed of particle-form catalyst.

"Thesize and distribution of downcomers'in' secondary distribution plate 9 is important. Each downcomer pipe in-the secondary distributor should feed a catalyst bed area of not less than about 0.1 square foot (roughly -4 inch diameter) and not more than about 1.0 square foot (14 inch diameter). Coverage ofan area smaller than 0.1 square foot is not practical since tray area is almost completely filled at this spacing and there would be only slight gain in distribution. An area-coverage greater than 1.0 square foot would result in a large loss 'of catalyst volume. This is due to the fact that liquid issuing from a downcomer pipe must spread out as the flow moves downward through the bed. Therefore, increasing the area of each downcomer also increases the bed depth required before the liquid fans out to cover the entire cross-section of the bed. In general, the preferred coverage, withinthe above-mentioned range, would be downcomers spaced every 8 to 10 inches apart.

The preferred design features for each downcomer discharging liquid and gas to .the catalyst bed are:

(l) The downcomer-pipe diameter should preferably be at least percent and not more than about 50 percent of the diameter for thearea each downcomer-feeds. (In our commercial and laboratory designs, 2'' diameter downcomers were spaced 8 to 9 inches apart, or a downcomer diameter equal to 22 percent to 25 percent of the diameter for the bed area covered by each downcomer.)

(2) At the same time, the downcomer diameter where V =total volume of liquid per second at operating conditions, ftfi/sec.

"V,=total volume of vapor per second at operating conditions, .ft. sec. A=cross sectional area of each downcomer, ft.

N=total number of downcomers Superficial velocities of less than about 30 feet per secondprovide satisfactory results.

.It may be desirable to provide two or more sizes of downcomer pipes on the primary distributor tray. For example, in a cylindrical vessel as shown in Figure l, a standard pattern or arrangement of downcomers will leave unwetted areas in the catalyst bed near the periphery. Consequently, somewhat smaller downcomers, than used on the rest of the tray, may be used to fill in these spaces to completely wet the bed.

If the liquid phase is introducedon to the secondary distributor tray in such a'manner that a hydraulic gradient exists across the secondary tray, 'maldistribution will :occur. To minimize the hydraulic gradient, devices previously described for distributing the liquid to the secondary downcomertray are recommended. Preferably, these devices would limit the hydraulic gradient between any two points on the secondary distributor tray toless than about M".

We claim:

.1. A method of distributing a mixed phase-feed uniformly over the cross-section of a bed of particle-form material confined in a reactor which comprises introducing a mixed phase feed comprising a vaporous component and a liquid component into a reactor at a point spaced vertically from the top of a bed of particle-form material, disengaging at least aportion of said vaporous component whilst subjecting said liquid component to non-turbulent flow through a distributing zone spaced above, concentric with, and having substantially thesame cross-sectional area as said bed of particle-form material, flowing said liquid component from said distributing zone as a plurality of streams downwardly onto the upper surface of said bed of particle-form material, each of said plurality of streams having a superficial velocity notexceeding 30 feet per second and flowing said disengaged vaporous component through the aforesaid bed of particle-form material in intimate association with said liquid component.

2. The method of distributing a mixed phase feed uniformly over the cross-section of a bed'of particle-form material comprising a catalyst as set forth and described in claim 1 wherein the plurality of streams each having a'superficial velocity not exceeding 30 feet per second flow onto and through a layer of inert pellets, and the multiplicity of streams of liquid component produced inssaid2layer of inert pellets'flow onto andthrough'said bed .ofparticle-form catalyst.

.3. The method of distributing a mixed phase feed uniformly over thecross-section of a bed of particle- 'form material comprising a catalyst as set forth anddescribed in claim 1 wherein the plurality of streams each having a superficial velocity not exceeding 30 feet per second flow onto and through a layer of inert substantially spherical pellets, and the multiplicity of streams of liquid component produced in said layer of inert sub- 7 stantially spherical pellets flow onto and through said bed of particle-form catalyst.

4. An apparatus for distributing a mixed phase feed comprising a vaporous component and a liquid component uniformly over a bed of particle-form solid ma- ,terial which comprises a closed container, a mixed feed inlet, an outlet, a bed of particle-form solid material in the lower region of said container, a secondary distributor vertically spaced upwardly from said bed of particle-form material constructed and arranged to provide a plurality of downwardly extending conduits in the ratio of one conduit for each 0.1 to not more than about ,1.0 square foot of horizontal cross-sectional area of said bed of particle-form solid material, a primary distributor constructed and arranged to deliver in substantially nonturbulent flow to said secondary distributor said liquid component whilst disengaging at least a portion of said vaporous component of said mixed phase feed, and means for introducing said mixed phase feed to said primary distributor. i

5. In the apparatus described and set forth in claim '4 a mass of substantially inert material interposed between said catalyst bed and said secondary distributor, said mass of substantially inert material being provided with a multiplicity of interconnected fissures providing 'a multiplicity of tortuous paths from the side of said mass facing said secondary distributor through said mass of substantially inert material to the side of said mass facing said catalyst bed. 6. An apparatus for distributing a mixed phase feed comprising a vaporous component and a liquid component uniformly over the cross-section of a bed of particle-form solid material which comprises in a closed container having a mixed phase feed inlet located in the region of the top thereof, a products outlet in the region of the bottom of said container, and a bed of particle-form solid material therein interposed between said mixed feed inlet and said products-outlet, said bed of particle-form solid material having the bottom thereof contiguous'to said products outlet and having the top thereof spaced downwardly from said mixed phase feed inlet, said bed of particle-form solid material having a cross-section substantially that of said container, a sec- .ondary distributor comprising a plate mounted horizontally in a liquidand gas-tight manner to provide substantially no hydraulic gradient horizontally to said plate and provided with a plurality of conduits in the ratio of one conduit per 0.1 to about 1.0 square foot of horizontal cross-sectional area of said bed of particle-form solid material, a primary distributor mounted horizontally in spaced relation above said secondary distributor comprising a tray and a plurality of conduits mounted in said tray, the lower portions of said conduits being notched and contiguous to said horizontal plate of said secondary distributor to provide substantially nonr turbulent flow of liquid component of said mixed phase feed over said horizontal plate of said secondary distributor whilst disengaging the vaporous component of said mixed phase feed, the upper portions of said conduits being notched, the sides of said tray extending j mass of substantially inert material being provided with a multiplicity of interconnected channels providinga multiplicity of tortuous paths from the side of said mass of substantially inert material facing said secondary distributor through said mass of substantially inert material to the side of said mass of substantially inert material facing said bed of particle-form material.

8. In the apparatus for distributing a mixed phase feed over a bed of particle-form solid material as'set forth and described in claim 4 wherein the primary dis- .tributor comprises a first conduit interposed between the horizontal plate of thesecondary distributor aud'the :means for delivering mixed phase feed to said primary distributor, the lower end of said conduit being notched and contiguous to'said horizontal plate, a horizontal plate mounted in a liquidand gas-tight manner in s'aid conduit above theupper edges of saidnotches, and a second conduit mounted vertically in a liquid and "gastight manner within said first conduit on said horizon.- tal plate, the upper edge of said second conduit being in .a plane above the plane of said first conduit, said second conduit being concentric with said means for delivering mixed phase feed to said primary distributor. 1

9. In the apparatus for distributing a mixed phase feed over a bed of particle-form solid material as set forth and described in claim 4 wherein the primary distributor comprises a tray concentric with the means for delivering mixed phase feed to said primary distributor and interposed between said mixed phase delivery means and said secondary distributing means, a plurality of partially closed end channels having the open side contiguous to said secondary distributor constructed and arranged to provide non-turbulent flow of liquid component -whilst disengaging vaporous componentof said mixed phase feed, and means connecting said tray and said channels. 10. In the apparatus for distributing a mixed pha feed over a bed of particle-form solid material asset forth and described in claim 4 wherein the-primary distributor comprises a plurality of partially closed end channels having the open side contiguous 'to said secondary distributor constructed and arranged to provide non-turbulent flow of liquid component whilst disengaging vaporous component of said mixed phase feed, and a plurality of conduits connecting said mixed phase feed inlet with said plurality of closed end channels.

11. Inthe apparatus for distributing a mixed phase feed as described and set forth in claim 4 means for introducing gaseous reactant separately into said container. I

12. In the apparatus for distributing a mixed phase feed over a bed of particle-form solid material as set forth and described in claim 4 wherein the primary distributor comprises a tray concentric with the means'for delivering mixed phase feed to said primary distributor and interposed between said mixed phase feed delivery means and said secondary distributing means, a plurality of partially closed end channels having the open sides contiguous to said secondary distributor, trapezoidal baffle mounted substantially in the plane of the open sides and opposite each mixed phase feed delivery means with the shorter of-the two parallel sides of said baffle substantially in the plane of the lower edge of said partially closed ends. I

References Cited in the file of this patent UNITED STATES PATENTS "at v

Claims

1. A METHOD OF DISTRIBUTING A MIXTURE PHASE FEED UNIFORMLY OVER THE CROSS-SECTION OF A BED PARTICLE-FORM MATERIAL CONFINED IN A REACTOR WHICH COMPRISES INTRODUCING A MIXED PHASE FEED COMPRISING A VAPOROUS COMPONENT AND A LIQUID COMPONENT INTO A REACTOR AT A POINT SPACED VERTICALLY FROM THE TOP OF A BED OF PARTICLE-FORM MATERIAL, DISENGAGING AT LEAST A PORTION OF SAID VAPOROUS COMPONENT WHILST SUBJECTING SAID LIQUID COMPONENT TO NON-TURBULENT FLOW THROUGH A DISTRIBUTING ZONE SPACED ABOVE, CONCENTRIC WITH, AND HAVING SUBSTANITALLY THE SAME CROSS-SECTIONAL AREA AS SAID BED OF PARTICLE-FORM MATERIAL FLOWING SAID LIQUID COMPONENT FROM SAID DISTRIBUTING ZONE AS A PLURALITY OF STREAMS DOWNWARDLY ONTO THE UPPER SURFACE OF SAID BED OF PARTICLE-FORM MATERIAL, EACH OF SAID PLURALITY OD STREAMS HAVING A SUPERFICIAL VELOCITY NOT EXCEEDING 30 FEET PER SECOND AND FLOWING SAID DISENGAGED VAPOROUS COMPONENT THROUGH THE AFORESAID BED OF PARTICLE-FORM MATERIAL IN INTIMATE ASSOCIATION WITH SAID LIQUID COMPONENT.

4. AN APPARATUS FOR DISTRIBUTING AMIXED PHASE FEED COMPRISING A VAPOROUS COMPONENT AND A LIQUID COMPONENET UNIFORMLY OVER A BED OF PARTICLE-FORM SOLID MATERIAL WHICH COMPRISES A CLOSED CONTAINER, A MIXED FEED INLET, AN OUTLET, A BED OF PARTICLE-FORM SOLID MATERIAL IN THE LOWER REGION OF SAID CONTAINER, A SECONDARY DISTRIBUTOR VERTICALLY SPACED UPWARDLY FROM SAID BED PARTICLE-FROM MATERIAL CONSTRUCTED AND ARRANGED TO PROVIDE A PLURALITY OF DOWNWARDLY EXTENDING CONDUITS IN THE RATIO OF ONE CONDUIT FOR EACH 0.1 TO NOT MORE THAN ABOUT 1.0 SQUARE FOOT OF HORIZONTAL CROSS-SECTIONAL AREA OF SAID BED OF PARTICLE-FORM SOLID MATERIAL, A PRIMARY DISTRIBUTOR CONSTRUCTED AND ARRANGED TO DELIVER IN SUBSTANTIALLY NONTURBULENT FLOW TO SAID SECONDARY DISTRIBUTOR SAID LIQUID COMPONENT WHILST DISENGAGING AT LEAST A PORTION OF SAID VAPOROUS COMPONENT OF SAID MIXED PHASE FEED, AND MEANS FOR INTRODUCING SAID MIXED PHASE FEED, AND PRIMARY DISTRIBUTOR.