CA1254720A - Method and apparatus for uniformly loading particulate material into cylindrical beds - Google Patents
Method and apparatus for uniformly loading particulate material into cylindrical bedsInfo
- Publication number
- CA1254720A CA1254720A CA000496502A CA496502A CA1254720A CA 1254720 A CA1254720 A CA 1254720A CA 000496502 A CA000496502 A CA 000496502A CA 496502 A CA496502 A CA 496502A CA 1254720 A CA1254720 A CA 1254720A
- Authority
- CA
- Canada
- Prior art keywords
- catalyst
- disc
- bed
- vessel
- arcuate
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
- B65G69/00—Auxiliary measures taken, or devices used, in connection with loading or unloading
- B65G69/04—Spreading out the materials conveyed over the whole surface to be loaded; Trimming heaps of loose materials
- B65G69/0458—Spreading out the materials conveyed over the whole surface to be loaded; Trimming heaps of loose materials with rotating means, e.g. tables, arms
-
- 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
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/002—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor with a moving instrument
Abstract
METHOD AND APPARATUS FOR UNIFORMLY LOADING
PARTICULATE MATERIAL INTO CYLINDRICAL BEDS
Abstract A method for simultaneously distributing catalyst particles across the full diameter of catalyst bed with a single rotor is disclosed. The bed has substantially uniform high density by forming a multiplicity of annular rings of catalyst concentric with the vessel or bed center. Such action is achieved without varying rotor speed by deflecting catalyst from a feed hopper into a plurality of arcuate sectors or portions of different radial lengths on a rotating disc.
Preferably, each arcuate portion has a volume proportional to one of the annular areas of the bed within the cross-sectional area of the vessel. The desired volume is formed by both the radial length of the arcuate sector and its included angle on the disc.
Depending upon the overall cross-sectional area of the vessel, the cylindrical volume of catalyst flowing from the feed tube may be divided into an outer annular column and an inner cylindrical column. In a preferred embodiment this may be done by a frusto-conical member extending upwardly and inwardly into the feed tube from the main distribution surface of the disc. Another plurality of separate arcuate flow paths of different radial lengths are rotated by the single rotor or disc.
Desirably, each other path is shorter than the radius of any of the arcuate portions formed by the disc.
PARTICULATE MATERIAL INTO CYLINDRICAL BEDS
Abstract A method for simultaneously distributing catalyst particles across the full diameter of catalyst bed with a single rotor is disclosed. The bed has substantially uniform high density by forming a multiplicity of annular rings of catalyst concentric with the vessel or bed center. Such action is achieved without varying rotor speed by deflecting catalyst from a feed hopper into a plurality of arcuate sectors or portions of different radial lengths on a rotating disc.
Preferably, each arcuate portion has a volume proportional to one of the annular areas of the bed within the cross-sectional area of the vessel. The desired volume is formed by both the radial length of the arcuate sector and its included angle on the disc.
Depending upon the overall cross-sectional area of the vessel, the cylindrical volume of catalyst flowing from the feed tube may be divided into an outer annular column and an inner cylindrical column. In a preferred embodiment this may be done by a frusto-conical member extending upwardly and inwardly into the feed tube from the main distribution surface of the disc. Another plurality of separate arcuate flow paths of different radial lengths are rotated by the single rotor or disc.
Desirably, each other path is shorter than the radius of any of the arcuate portions formed by the disc.
Description
~ Z54~720 61936-1686 MET~IOD AND APPARATUS FOR
UNIFORMLY LOADING
PARTICULATE MATERIAL INTO
CYLINDRICAL BEDS
Fièld of the Invention . .
The present invention relates to a method of, and appara-tus for, uniformly loading particulate material into a cylindrical bed or vessel. More particulary, it relates to Catalyst Oriented Packing (COP) loading of catalytic reaction beds by uniformly distributing catalyst particles, or the like, over a large diameter cylindrical vessel by simultaneously flowing catalysts into multiple concentric rings of catalyst particles over the full circular area of the catalyst bed.
The invention is primarily directed to assuring that catalyst such as cylindrical extrudate catalyst having a high angle of repose, will pack uniformy in a bed with a high ratio of catalyst to volume.
It is the particular object of the present invention to increase the packed density of particles having a high angle of repose, including spheroidal particles, so that the bed is simultaneously formed by a plurality of concentric rings across the ful] diameter of the vessel. Multiple rings of particles, such as catalyst, are formed by uniform rotation of a single rotary disc or rotor which divides the catalyst flow from an overhead flow pipe into a multiplicity of radial segments, such segment having different radii. The resulting exit velocity of ~S'~ 72~ 61936-1686 catalyst particles from each segment or sector of the disc dis-tri-bution surface createsa plurality of different radial throw distances within the bed or vessel. Sin~e all segments of the disc turn at the same speed, concentric rings of catalyst are cast into the vessel so that they simultaneously settle into adjacent annular rings. Such annular rings are desirably relatively narrow in radial width, but of progressively different radial distances from the axis of the vessel to form a multiplicity of concentric rings to cover the catalyst bed uniformly.
BACKGROUND OF THE INVENTION
Catalytic reactor vessels having one or more fixed catalyst beds are now commonly filled by using a catalyst distributor. Su~h a technique is known as Catalyst Oriented Packing (frequently referred to as COP loading) and is particularly useful to produce uniformity in the permeability and overall density of the catalyst bed. In current catalytic processing, catalyst particles are generally manufactured by extrusion in the form of cylindrical rods of 1/16" to 1/4"
diameter. The rods are then broken into 1~4" to 1/2" lengths.
Such extrudates are typically formed of alumina, silica-alumina or synthetic or natural zeolitic materials and are substantially less expensive to produce than spherical catalyst. However, such extrudate particles have a high angle of repose; the angle at which a free standing pile of material is stable. Consequently, they are difficult to distribute evenly over a large diameter cylindrical vessel. Further, due to differences in size of such \
~5~7~0 particles, as well as chipping and breaking during both manufacture and loading into a process reactor, they tend to "classify" or separate if the bed is filled by gravity alone from a central point in the vessel.
The primary purpose of COP loading is to minimize void spaces and consequently local "hot spots" which can occur during exothermic reactions of hydrocarbons with the catalyst particles.
Additionally, increased packed density of the solid particulate material, catalyst particles, improves the flow distribution of reactants wIthin the vessel. Further, increased bed density limits settling of the bed when the reactor is brought on stream and subjected to hydraulic forces by fluid flow through the reactor. In general, the amount of catalyst can be increased several percent in an existing vessel. Conversely, several percent less reactor volume is required for the same amount of catalyst in a new vessel.
In general, previously known catalyst oriented loading apparatus included a distributor disc having a uniform diameter ~nd a plurality of radial blades or fin members on top of the rotating disc. In general the distributor is either a cone shaped member or a flat circular plate. However, the speed of the distributor must be varied in order to distribute catalyst across the entire cross-sectional area of the bed, since the distance the catalyst is thrown is proportional to the disc speed. Where the disc is a flat plate having vanes formed thereon, a few holes are formed in the plate so that some of the catalyst particles fall z~
directly downwardly through the rotating member toward the center of the reactor vessel.
U.S. Patent 3,804,273 Uhl is directed to apparatus for loading a catalyst bed with a radial distributor having a single conical surface. The only method of distributing catalyst across the full bed diameter is to increase and decrease the speed of the rotating disc.
U.S. Patent 3,972,686 Johnson et al, discloses a flat disc having vanes and a plurality of slots or holes through which some of the catalyst may fall near the center of the bed;
the remainder of the catalyst is thrown toward the vessel side.
This system also requires variation in the speed of the rotating disc to load catalyst so that it covers the entire level of a catalyst reactor bed.
A particular disadvantage of such prior arrangements lies in the fact that at one speed the catalyst is thrown into a circular or annular mound which tends to classify catalyst particles falling on it. The larger particles roll to the botton and outside of the mound while the smaller particles stop on the mound itself. While to a certain extent, these difficulties are alleviated by varying the speed of the rotating disc, slo~/ing disc speed significantly increases the loading time for the reactor bed, because loading rate is proportional to such speed. On the other hand, excessive speed of the disc results in catalyst flying of the disc without sufficient residence time thereon to control the radial throw distance. Further, it is difficult to control disc speed to achieve a desired radial throw distance because 1~5~2V 61936-1686 the interior of such a bed is usually too full of dust to permit the operator to actually see the catalyst bed from the loader. Accord-ingly, lt is necessary to determine the probable level of distri-bution by the number of drums of catalyst that have been loaded at a given bed level. Such a procedure is time consuming and not necessarily accurate enough to permit level filling of the bed. In fact, it is general practice to fill the bed at the outer edge higher than necessary say 6 to 12 inches and then alternately increase the height of the center level above that at the outer edge by a similar amount, and 50 forth, up the reactor as the depth of the bed or beds is increased throughout the reactor. The problem is further aggravated where the vessel contains several separate beds, each supported by a separate support "screen" and the lower beds must be filled through accessways in the center of the overlying bed support. Visual inspection is thus made more difficult.
U.S. Patent ~,306,829 Loutaty et al disclose a distribu-tor for catalyst particles in a reactor or grain storage in a silo.
The distributor includes flexible straps pivotally supported by hooks along the length of a drive shaft. The straps may be formed of reinforced rubber and are either of equal length or progressively longer away from the feed hopper discharge. The examples indicate t.he system to be satisfactory for filling a model of reactor vessel 60 cm (about 2 feet) in diameter. It appears that the active lengths of the rotating straps vary in diameter with the speed of the drive shaft and their interaction with falling catalyst particles. Efficient loading of vessels with each of ~S~720 the above noted arragements has been limited to relatively small diameter xeactors, for reasons noted above.
U.S. Patent ~1433~707 - Farnham, assigned to the assignee of the present invention, discloses a method and apparatus for uniformly filling a reactor vessel at each level with an even distribution of catalyst particles from the center of the vessel to its outex wall by using a plurality of discs of differing diameters rotated at the same speed by a single drive shaft. Desirably, three conical discs are used with the largest diameter nearest the supply hopper feed tube. The upper discs include a central openings to permit catalyst to be fed to each of the lower discs. Because the discs are of different ~iameters each spreads catalyst to a different area around the vessel with the drive shaft rotating at constant speed. Such a system is quite satisfactory for delivery of catalyst to vessels Of smaller diameter and deep beds,where adequate "head" room is available at the top of the vessel or above each of several beds.
However, the method is also limited to laying down only a few annular rings simultaneoulsy, without changing rotor speed.
Federal Republic of Germany patent 2,703,329 issued March 1978 discloses another particle loading system using a~ially spaced multiple discs rotated by a common drive shaft. The mode of operation is similar to the above-noted Farnham pa-tent.
SU~ARY OF THE INVENTION
In carrying out the method of the present invention, a single catalyst distributor is positioned at a suitable level above a bed to be filled. Catalyst is then supplied to the l~S~
- 7 - 61936-16g6 distributor from a hopper having a feed tube positioned so that a substantially cylindrical column of catalyst falls on the sinyle rotor or disc member.
Catalyst particles are then distributed by the single disc across the full diameter of the bed with substantially uniformly high density by forming a multiplicity of annular rings of catalyst concentric with the center of the vessel or bed.
Such action is achieved without varying the disc speed by deflecting the cylindrical column of catalyst into a plurality of arcuate sectors or portions of different radial lengths on the single rotating disc. Preferablyr each arcuate portion has a volume proportional to one of the annular areas of the bed within the cross~sectional area of the vessel. The desired volume is formed by both the radial length of the arcuate sector and its included angle on the disc. In a preferred form of the disc, each adjacent arcuate sector or portion desirably has a different volume to form such annular rings of catalyst in the bed with substantially equal widths.
Dependin-g upon the overall cross-sectional area of the vessel, the cylindrical volume of catalyst flowing from the feed tube may be divided into an outer annular column and an inner cylindrical column. In a preferred embodiment this may be done by a frusto-conical member extending upwardly and inwardly into the feed tube from the r.lain di~tribution surface of the disc. The major base of the conical member and the main disc form an auxiliary hopper or storage volume which supplies catalyst to ~s~z~
another plurality of separate arcuate flow paths of different radial lengths at substantially right angles to -the column.
Each of such other plurality of flow paths is also rotated by the single rotor or disc. Desirably, each of these flow paths is shorter than the radius of any of the arcuate portions formed by the disc above.
By uniformly rotating the disc each of the plurality of arcuate flow paths lays down a concentric annular ring of different diameter. These rings substantially cover the surface area of the catalyst bed support in the vessel with catalyst. Because each ring is formed simultaneously, at all levels, the depth of catalyst is uniform across the full vessel or bed diameter and the resulting catalyst bed has a higher average density for the same vessel or bed volume.
Furhter objects and advantages of the present invention will become apparent to those skilled in the art in light of the following detailed description of the preferred embodiments of the invention taken in conjunction with the drawings which form an integral part of this specification.
BRIEF DESCRIPTION OF THE DRAWINGS
-In the drawings:
Fig. 1 is an elevation view partially in cross-section through a large diameter hydrocarbon reactor and illustrates the method of the present invention using a single rotor distributor to lay down a plurality of concentric rings of catalyst to form one l~S4~;20 of several beds within the vessel;
Fig. 2 is a cr`oss-seetional plan view, taken in the direction of arrows 2-2 in Fig. 1, illustrating the concentric rings of catalyst particles being east by the single rotor distributor of the present invention;
Fig. 3 is a p]an view of the primary eatalyst distributor rotor shown in Fig. 1, partieularly illustrating a preferred arrangement of radial lengths and areuate spans required for laying down a plurality of eoneentrie circles of catalyst particles of similar depth, as shown in Fig. 2;
Fig. 4. is an elecation cross-sectional view through the rotor of Fig. 3 taken in the direction of arrows 4-4 and also illustrates the eooperation of the conical portion of the rotor to divide flow from the hopper feed tube to the upper distributor plate and the lower distributing ehannels earried by the rotor;
Fig. 5 is a plan view taken in the direction of arrows 5-5 in Fig. 4, partially in eross-section, through the lowe portion of the rotor assembly whieh illustrates the distribution of eatalyst to the multiple tubes and distribution holes, partieularly useful in filling the inner annular rings of a large diameter vessel;
iZ$4'~20 - 9a - 61936-1686 Fig~ 6 is a plan view, taken in the direction of arrows 6-6 in Fig. ~ of the lower distribution assembly and particularly illustrates further distribution by the lower plate for simultaneously filling the innermost portions of a catalyst bed; and Fig. 7 is an exploded view of the rotor assembly.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
OF T~IE INVENTION
Fig. 1 illustratesapplication of the method of the present invention to oriented catalyst loading in a large diameter catalytic reactor vessel 10 using a preferred form of catalyst loading apparatus 12 to lay down concentric rings of catalyst particles. As indicated in Fig. 2, such a plurality of concentric rings 14 or similar annular width, or average radial length, simultaneously cover the full diameter or vessel 10 to fill bed 16 with catalyst to equal depths and density across the full diameter. Such method is particularly directed to loading catalyst having a high angle of repose, such ascylindrical extrudate particles of catalyst which are relatively immobile after deposition.
As particularly shown in Fig 1, vessel 10 may include a plurality of beds 16, each formed on a catalyst support structure or screen 18. As indicated, a plurality of support structures 18 may be provided so that each of the several serially interconnected flow beds 16 is located one above the other. To assure that each of beds 16 is filled with uniform i;~S~7Z~
density throughout its height or depth it is also important that the axial length of the catalyst distribution apparatus be rela~iuely short so th~t the top of the bed, beneath upper support structure 18, or the top of vessel 10, may be ~illed as full as possible, with little or no headroom above catalyst bed 16. For this reason, the catalyst distribution rotor member 20, constructed in accordance with the present invention, includes a primary distribution surface formed by plate 22 that is divided into a plurality of arcuate sectors or segments 24 having a common vertex at the rotational axis 30 of disc member 22.
~ut as shown, for dynamic rotor stability each segment or sector has a different radius than either of its adjacent sectors. As indicated desirably two equal area segments are located diametric-ally opposite to each other to balance the rotor dynamically.
In the particular embodiment shown in Figs. ~ and 4, radial rib members 26 form sectors 24 and have different radial lengths as indicated. Rib members 26 extend axially away from and generally perpendicular to the distributing surface of plate 22. It is also to be particularly noted that individual sectors or segments 24 have different included angles and that such angles together with the depth of ribs 26 determine the total volume of catalyst that may be thrown to each ring on the surface of bed 16.
It will, of course, be understood that the total volume of each individual sector or segment is proportional to the area of the corresponding catalyst ring 14 to be cast on top o~ bed 16~ In general such volumes of the sectors 24 will be proportional to the :~2~4'72V
~l - 61936-1686 circumferential areas of the rings and the width of each ring relative to adjacent rings formed by other sectors or segments 24.
As particularly shown in Fig. 4, catalyst is supplied to the distribution surface formed by plate 22 and individual segments 24 by a feed tube 28 having an axis 30 which is substantially coaxial with the drive shaft 32 to which the distributor plate 22 is attached as by hub 34 and key or drive pin 36.
As illustrated in Fig. 1, the distribution system of the present invention may be used with conventional catalyst oriented packing apparatus. As there seen, hopper 38 is loaded with catalyst and by gravity feeds catalyst through supply tube 40 to lower feed hopper 42. Hopper 42 maintains a constant head cf catalyst above distribution disc 20 and preferably is supported~ as by pivoted arms 49, over manway 44 formed in upper grid 18, or on upper flange 46 of vessel lO. Rotary disc 20 may then be driven by a local air, or electric, motor 48 mounted on lower hopper 42 to drive shaft 32 and rotor 20 at the desired speed. Drive motor 48 may be through an air hose, or electric cable, 50. Alternatively, shaft 32 may be rotated by extending drive shaft 32 above flange 46 to an external motor (not shown).
A particular problem in the distribution of catalyst in large diameter vessels is to get even catalyst distribution near the center of the vessel. To lay catalyst evenly across the full diameter of a vessel of, say of 8-15 feet, including the center portion, is quite critical. Merely dumping catalyst - 12 - 1 ~ S 47 2 0 61936-1686 through the center of the distributor plate and allowing it to spill outwardlv from a center heap is quite unsatisfactory.
In accordance with the preferred embodiment of the present invention this problem is solved by -the use of a plurality of rectangular tubes or channels 52, 54, 56 and 58, each of different radial lengths. As best seen in Fig. 5, these channels, together with plate 60 supported on lower collar 62, provide additional annular catalyst distribution rings. Plate 60 is supported below collar 62 by a plurality of threaded studs 64 and nuts 66 which permits plate 60 to be properly spaced relative to ~lange 68 of collar 62. Plate 60 itself serves as a further distributor of catalyst through the action of radial bar 70 carried on its top surface. A suitable port 72 radially spaced from the axis of rotation of plate 60 controls the amount of catalyst permitted to flow to the innermost ring.
While not shown in detail, it will be understood that feed tube 40 is adjustably positioned relative to the conical surface of frus-to-conical disc 86 so as to proportion the amount of catalyst that flows annularly to multiple sectors 24, as compared to the amount of catalyst that flows cylindrically over the upper and inner edge 87 of disc 86. Chamber 88 formed by frusto-conical section 86 and plate 22 then serves to distribute catalyst to tubes 52, 54, 56 and 58 and plate 60. Similarly, the opening between 60 ard collar 68, as noted above, controls the total catalyst flow fromthe edge of plate 60, with the aid of bar 70, and through orifice 76.
il~S~72~
As best seen in ~i~g. 5, the supply of catalyst :Elowing in the internal cylindrical portion from feed tube 40 flows to the four rectangular tubes 52, 54, and 58 through square openings 84 in plate 22 while catalyst passing to distributor plate 60 passes through four circular openings 90 also formed in plate 22.
By forming tubes 52, 54, and 56, and 58 with different radial lengths, each shorter than any of the radial paths of the sectors 24, the inner diameter rings or annular portions of the catalyst bed are filled simultaneously as catalyst is being thrown by sectors 24 to the outer portions of the bed or vessel.
Also, at the same time catalyst passing through openings 90 is selectively laid down at the innermost part of the bed by control of the spacing oE plate 60 from collar 68 and the radial placement of bar 70 and the~ size of orifice 76. In the present embodiment it will accordingly be seen that a single rotor makes possible distribution of catalyst to a multiplicity of bands which in the present embodiment form sixteen separate rings comprising then laid down by arcuate segments 24, four laid down by tubes 52, 54, 56 and 58 and two by plate 60.
In the present arrangement collar 62 and plate 60 are disconnectably connected to distribution plate 22 by screws 80.
Tubes 52, 54, 56, and 58 are formed as a permanent part of plate 22. Alternatively, the entire rotor assembly may be made as one piece, or other portions permanently connected or disconnectably connected to distributor plate 22. It will also ~zs~zv be apparent to those skilled in the art that plate 22 may be conical rather than flat, if desired.
Because the single catalyst distribution disc or rotor includes a multiplicity of flow paths, each arranged to lay down concentric annular rings of limited, but approximately e~ual radial width, across the entire circumferential area, of vessel 10, the rotor is preferably turned at a constant speed.
The speed is re~ulated to such a constant value, determined by the bed diameter, so that the rotor will cast catalyst over the entire cross-sectional area of the vessel. Once adjusted, that speed is maintained substantially constant for complete filling of each bed from support 18 to the top of the bed 16. Such uniform laying of the bed throughout its dep-th results in increased density of the total catalyst volume that can be loaded into an individual bed or throughout the vessel. In actual practice, an increase in density of about 106 has been found, as determined by the total weight of catalyst that can be loaded into a known volume of the vessel, as compared to prior methods of COP loading, using varying speeds of a rotatable disc. Since the conversio.n rate of hydrocarbon feed passing through the vessel is dependent upon such total volume of catalyst, the present invention makes possible either a higher rate of hydrocarbon feed through the reactor for yield of the same products or an increased hydrocarbon conversion at a constant feed rate in the same volume of vessel. Both of these conditions are greatly - 15 - ~ ~ ~ 4 ~ ~70 61936-1686 desirable in processing hydrocarbon feeds for catalytic conversion and represent significant cost savings in such processing.
The above described embodiments of the inventi.on are particularly directed to loading extrudate catalyst particles across the full cross-sectional area of a large diameter reactor vessel. However, the method and apparatus are also applicable to load other particulate material, such as spherical or pellet catalyst or grain, as in a silo. Other contacting materials in particle form, such as sulfur sorbers, and ion exchange materials are also frequently loaded in large diameter vessels. The present invention is particularly useful for such service to insure high density throughout a bed of solid particles in a large diameter vessel.
From the foregoing description, various modifications and changes in the apparatus and in the method of operating such apparatus will occur to those skilled in the art, all such modifications or changes coming within the scope of the appended claims are intended to be included therein.
` ~'J
UNIFORMLY LOADING
PARTICULATE MATERIAL INTO
CYLINDRICAL BEDS
Fièld of the Invention . .
The present invention relates to a method of, and appara-tus for, uniformly loading particulate material into a cylindrical bed or vessel. More particulary, it relates to Catalyst Oriented Packing (COP) loading of catalytic reaction beds by uniformly distributing catalyst particles, or the like, over a large diameter cylindrical vessel by simultaneously flowing catalysts into multiple concentric rings of catalyst particles over the full circular area of the catalyst bed.
The invention is primarily directed to assuring that catalyst such as cylindrical extrudate catalyst having a high angle of repose, will pack uniformy in a bed with a high ratio of catalyst to volume.
It is the particular object of the present invention to increase the packed density of particles having a high angle of repose, including spheroidal particles, so that the bed is simultaneously formed by a plurality of concentric rings across the ful] diameter of the vessel. Multiple rings of particles, such as catalyst, are formed by uniform rotation of a single rotary disc or rotor which divides the catalyst flow from an overhead flow pipe into a multiplicity of radial segments, such segment having different radii. The resulting exit velocity of ~S'~ 72~ 61936-1686 catalyst particles from each segment or sector of the disc dis-tri-bution surface createsa plurality of different radial throw distances within the bed or vessel. Sin~e all segments of the disc turn at the same speed, concentric rings of catalyst are cast into the vessel so that they simultaneously settle into adjacent annular rings. Such annular rings are desirably relatively narrow in radial width, but of progressively different radial distances from the axis of the vessel to form a multiplicity of concentric rings to cover the catalyst bed uniformly.
BACKGROUND OF THE INVENTION
Catalytic reactor vessels having one or more fixed catalyst beds are now commonly filled by using a catalyst distributor. Su~h a technique is known as Catalyst Oriented Packing (frequently referred to as COP loading) and is particularly useful to produce uniformity in the permeability and overall density of the catalyst bed. In current catalytic processing, catalyst particles are generally manufactured by extrusion in the form of cylindrical rods of 1/16" to 1/4"
diameter. The rods are then broken into 1~4" to 1/2" lengths.
Such extrudates are typically formed of alumina, silica-alumina or synthetic or natural zeolitic materials and are substantially less expensive to produce than spherical catalyst. However, such extrudate particles have a high angle of repose; the angle at which a free standing pile of material is stable. Consequently, they are difficult to distribute evenly over a large diameter cylindrical vessel. Further, due to differences in size of such \
~5~7~0 particles, as well as chipping and breaking during both manufacture and loading into a process reactor, they tend to "classify" or separate if the bed is filled by gravity alone from a central point in the vessel.
The primary purpose of COP loading is to minimize void spaces and consequently local "hot spots" which can occur during exothermic reactions of hydrocarbons with the catalyst particles.
Additionally, increased packed density of the solid particulate material, catalyst particles, improves the flow distribution of reactants wIthin the vessel. Further, increased bed density limits settling of the bed when the reactor is brought on stream and subjected to hydraulic forces by fluid flow through the reactor. In general, the amount of catalyst can be increased several percent in an existing vessel. Conversely, several percent less reactor volume is required for the same amount of catalyst in a new vessel.
In general, previously known catalyst oriented loading apparatus included a distributor disc having a uniform diameter ~nd a plurality of radial blades or fin members on top of the rotating disc. In general the distributor is either a cone shaped member or a flat circular plate. However, the speed of the distributor must be varied in order to distribute catalyst across the entire cross-sectional area of the bed, since the distance the catalyst is thrown is proportional to the disc speed. Where the disc is a flat plate having vanes formed thereon, a few holes are formed in the plate so that some of the catalyst particles fall z~
directly downwardly through the rotating member toward the center of the reactor vessel.
U.S. Patent 3,804,273 Uhl is directed to apparatus for loading a catalyst bed with a radial distributor having a single conical surface. The only method of distributing catalyst across the full bed diameter is to increase and decrease the speed of the rotating disc.
U.S. Patent 3,972,686 Johnson et al, discloses a flat disc having vanes and a plurality of slots or holes through which some of the catalyst may fall near the center of the bed;
the remainder of the catalyst is thrown toward the vessel side.
This system also requires variation in the speed of the rotating disc to load catalyst so that it covers the entire level of a catalyst reactor bed.
A particular disadvantage of such prior arrangements lies in the fact that at one speed the catalyst is thrown into a circular or annular mound which tends to classify catalyst particles falling on it. The larger particles roll to the botton and outside of the mound while the smaller particles stop on the mound itself. While to a certain extent, these difficulties are alleviated by varying the speed of the rotating disc, slo~/ing disc speed significantly increases the loading time for the reactor bed, because loading rate is proportional to such speed. On the other hand, excessive speed of the disc results in catalyst flying of the disc without sufficient residence time thereon to control the radial throw distance. Further, it is difficult to control disc speed to achieve a desired radial throw distance because 1~5~2V 61936-1686 the interior of such a bed is usually too full of dust to permit the operator to actually see the catalyst bed from the loader. Accord-ingly, lt is necessary to determine the probable level of distri-bution by the number of drums of catalyst that have been loaded at a given bed level. Such a procedure is time consuming and not necessarily accurate enough to permit level filling of the bed. In fact, it is general practice to fill the bed at the outer edge higher than necessary say 6 to 12 inches and then alternately increase the height of the center level above that at the outer edge by a similar amount, and 50 forth, up the reactor as the depth of the bed or beds is increased throughout the reactor. The problem is further aggravated where the vessel contains several separate beds, each supported by a separate support "screen" and the lower beds must be filled through accessways in the center of the overlying bed support. Visual inspection is thus made more difficult.
U.S. Patent ~,306,829 Loutaty et al disclose a distribu-tor for catalyst particles in a reactor or grain storage in a silo.
The distributor includes flexible straps pivotally supported by hooks along the length of a drive shaft. The straps may be formed of reinforced rubber and are either of equal length or progressively longer away from the feed hopper discharge. The examples indicate t.he system to be satisfactory for filling a model of reactor vessel 60 cm (about 2 feet) in diameter. It appears that the active lengths of the rotating straps vary in diameter with the speed of the drive shaft and their interaction with falling catalyst particles. Efficient loading of vessels with each of ~S~720 the above noted arragements has been limited to relatively small diameter xeactors, for reasons noted above.
U.S. Patent ~1433~707 - Farnham, assigned to the assignee of the present invention, discloses a method and apparatus for uniformly filling a reactor vessel at each level with an even distribution of catalyst particles from the center of the vessel to its outex wall by using a plurality of discs of differing diameters rotated at the same speed by a single drive shaft. Desirably, three conical discs are used with the largest diameter nearest the supply hopper feed tube. The upper discs include a central openings to permit catalyst to be fed to each of the lower discs. Because the discs are of different ~iameters each spreads catalyst to a different area around the vessel with the drive shaft rotating at constant speed. Such a system is quite satisfactory for delivery of catalyst to vessels Of smaller diameter and deep beds,where adequate "head" room is available at the top of the vessel or above each of several beds.
However, the method is also limited to laying down only a few annular rings simultaneoulsy, without changing rotor speed.
Federal Republic of Germany patent 2,703,329 issued March 1978 discloses another particle loading system using a~ially spaced multiple discs rotated by a common drive shaft. The mode of operation is similar to the above-noted Farnham pa-tent.
SU~ARY OF THE INVENTION
In carrying out the method of the present invention, a single catalyst distributor is positioned at a suitable level above a bed to be filled. Catalyst is then supplied to the l~S~
- 7 - 61936-16g6 distributor from a hopper having a feed tube positioned so that a substantially cylindrical column of catalyst falls on the sinyle rotor or disc member.
Catalyst particles are then distributed by the single disc across the full diameter of the bed with substantially uniformly high density by forming a multiplicity of annular rings of catalyst concentric with the center of the vessel or bed.
Such action is achieved without varying the disc speed by deflecting the cylindrical column of catalyst into a plurality of arcuate sectors or portions of different radial lengths on the single rotating disc. Preferablyr each arcuate portion has a volume proportional to one of the annular areas of the bed within the cross~sectional area of the vessel. The desired volume is formed by both the radial length of the arcuate sector and its included angle on the disc. In a preferred form of the disc, each adjacent arcuate sector or portion desirably has a different volume to form such annular rings of catalyst in the bed with substantially equal widths.
Dependin-g upon the overall cross-sectional area of the vessel, the cylindrical volume of catalyst flowing from the feed tube may be divided into an outer annular column and an inner cylindrical column. In a preferred embodiment this may be done by a frusto-conical member extending upwardly and inwardly into the feed tube from the r.lain di~tribution surface of the disc. The major base of the conical member and the main disc form an auxiliary hopper or storage volume which supplies catalyst to ~s~z~
another plurality of separate arcuate flow paths of different radial lengths at substantially right angles to -the column.
Each of such other plurality of flow paths is also rotated by the single rotor or disc. Desirably, each of these flow paths is shorter than the radius of any of the arcuate portions formed by the disc above.
By uniformly rotating the disc each of the plurality of arcuate flow paths lays down a concentric annular ring of different diameter. These rings substantially cover the surface area of the catalyst bed support in the vessel with catalyst. Because each ring is formed simultaneously, at all levels, the depth of catalyst is uniform across the full vessel or bed diameter and the resulting catalyst bed has a higher average density for the same vessel or bed volume.
Furhter objects and advantages of the present invention will become apparent to those skilled in the art in light of the following detailed description of the preferred embodiments of the invention taken in conjunction with the drawings which form an integral part of this specification.
BRIEF DESCRIPTION OF THE DRAWINGS
-In the drawings:
Fig. 1 is an elevation view partially in cross-section through a large diameter hydrocarbon reactor and illustrates the method of the present invention using a single rotor distributor to lay down a plurality of concentric rings of catalyst to form one l~S4~;20 of several beds within the vessel;
Fig. 2 is a cr`oss-seetional plan view, taken in the direction of arrows 2-2 in Fig. 1, illustrating the concentric rings of catalyst particles being east by the single rotor distributor of the present invention;
Fig. 3 is a p]an view of the primary eatalyst distributor rotor shown in Fig. 1, partieularly illustrating a preferred arrangement of radial lengths and areuate spans required for laying down a plurality of eoneentrie circles of catalyst particles of similar depth, as shown in Fig. 2;
Fig. 4. is an elecation cross-sectional view through the rotor of Fig. 3 taken in the direction of arrows 4-4 and also illustrates the eooperation of the conical portion of the rotor to divide flow from the hopper feed tube to the upper distributor plate and the lower distributing ehannels earried by the rotor;
Fig. 5 is a plan view taken in the direction of arrows 5-5 in Fig. 4, partially in eross-section, through the lowe portion of the rotor assembly whieh illustrates the distribution of eatalyst to the multiple tubes and distribution holes, partieularly useful in filling the inner annular rings of a large diameter vessel;
iZ$4'~20 - 9a - 61936-1686 Fig~ 6 is a plan view, taken in the direction of arrows 6-6 in Fig. ~ of the lower distribution assembly and particularly illustrates further distribution by the lower plate for simultaneously filling the innermost portions of a catalyst bed; and Fig. 7 is an exploded view of the rotor assembly.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
OF T~IE INVENTION
Fig. 1 illustratesapplication of the method of the present invention to oriented catalyst loading in a large diameter catalytic reactor vessel 10 using a preferred form of catalyst loading apparatus 12 to lay down concentric rings of catalyst particles. As indicated in Fig. 2, such a plurality of concentric rings 14 or similar annular width, or average radial length, simultaneously cover the full diameter or vessel 10 to fill bed 16 with catalyst to equal depths and density across the full diameter. Such method is particularly directed to loading catalyst having a high angle of repose, such ascylindrical extrudate particles of catalyst which are relatively immobile after deposition.
As particularly shown in Fig 1, vessel 10 may include a plurality of beds 16, each formed on a catalyst support structure or screen 18. As indicated, a plurality of support structures 18 may be provided so that each of the several serially interconnected flow beds 16 is located one above the other. To assure that each of beds 16 is filled with uniform i;~S~7Z~
density throughout its height or depth it is also important that the axial length of the catalyst distribution apparatus be rela~iuely short so th~t the top of the bed, beneath upper support structure 18, or the top of vessel 10, may be ~illed as full as possible, with little or no headroom above catalyst bed 16. For this reason, the catalyst distribution rotor member 20, constructed in accordance with the present invention, includes a primary distribution surface formed by plate 22 that is divided into a plurality of arcuate sectors or segments 24 having a common vertex at the rotational axis 30 of disc member 22.
~ut as shown, for dynamic rotor stability each segment or sector has a different radius than either of its adjacent sectors. As indicated desirably two equal area segments are located diametric-ally opposite to each other to balance the rotor dynamically.
In the particular embodiment shown in Figs. ~ and 4, radial rib members 26 form sectors 24 and have different radial lengths as indicated. Rib members 26 extend axially away from and generally perpendicular to the distributing surface of plate 22. It is also to be particularly noted that individual sectors or segments 24 have different included angles and that such angles together with the depth of ribs 26 determine the total volume of catalyst that may be thrown to each ring on the surface of bed 16.
It will, of course, be understood that the total volume of each individual sector or segment is proportional to the area of the corresponding catalyst ring 14 to be cast on top o~ bed 16~ In general such volumes of the sectors 24 will be proportional to the :~2~4'72V
~l - 61936-1686 circumferential areas of the rings and the width of each ring relative to adjacent rings formed by other sectors or segments 24.
As particularly shown in Fig. 4, catalyst is supplied to the distribution surface formed by plate 22 and individual segments 24 by a feed tube 28 having an axis 30 which is substantially coaxial with the drive shaft 32 to which the distributor plate 22 is attached as by hub 34 and key or drive pin 36.
As illustrated in Fig. 1, the distribution system of the present invention may be used with conventional catalyst oriented packing apparatus. As there seen, hopper 38 is loaded with catalyst and by gravity feeds catalyst through supply tube 40 to lower feed hopper 42. Hopper 42 maintains a constant head cf catalyst above distribution disc 20 and preferably is supported~ as by pivoted arms 49, over manway 44 formed in upper grid 18, or on upper flange 46 of vessel lO. Rotary disc 20 may then be driven by a local air, or electric, motor 48 mounted on lower hopper 42 to drive shaft 32 and rotor 20 at the desired speed. Drive motor 48 may be through an air hose, or electric cable, 50. Alternatively, shaft 32 may be rotated by extending drive shaft 32 above flange 46 to an external motor (not shown).
A particular problem in the distribution of catalyst in large diameter vessels is to get even catalyst distribution near the center of the vessel. To lay catalyst evenly across the full diameter of a vessel of, say of 8-15 feet, including the center portion, is quite critical. Merely dumping catalyst - 12 - 1 ~ S 47 2 0 61936-1686 through the center of the distributor plate and allowing it to spill outwardlv from a center heap is quite unsatisfactory.
In accordance with the preferred embodiment of the present invention this problem is solved by -the use of a plurality of rectangular tubes or channels 52, 54, 56 and 58, each of different radial lengths. As best seen in Fig. 5, these channels, together with plate 60 supported on lower collar 62, provide additional annular catalyst distribution rings. Plate 60 is supported below collar 62 by a plurality of threaded studs 64 and nuts 66 which permits plate 60 to be properly spaced relative to ~lange 68 of collar 62. Plate 60 itself serves as a further distributor of catalyst through the action of radial bar 70 carried on its top surface. A suitable port 72 radially spaced from the axis of rotation of plate 60 controls the amount of catalyst permitted to flow to the innermost ring.
While not shown in detail, it will be understood that feed tube 40 is adjustably positioned relative to the conical surface of frus-to-conical disc 86 so as to proportion the amount of catalyst that flows annularly to multiple sectors 24, as compared to the amount of catalyst that flows cylindrically over the upper and inner edge 87 of disc 86. Chamber 88 formed by frusto-conical section 86 and plate 22 then serves to distribute catalyst to tubes 52, 54, 56 and 58 and plate 60. Similarly, the opening between 60 ard collar 68, as noted above, controls the total catalyst flow fromthe edge of plate 60, with the aid of bar 70, and through orifice 76.
il~S~72~
As best seen in ~i~g. 5, the supply of catalyst :Elowing in the internal cylindrical portion from feed tube 40 flows to the four rectangular tubes 52, 54, and 58 through square openings 84 in plate 22 while catalyst passing to distributor plate 60 passes through four circular openings 90 also formed in plate 22.
By forming tubes 52, 54, and 56, and 58 with different radial lengths, each shorter than any of the radial paths of the sectors 24, the inner diameter rings or annular portions of the catalyst bed are filled simultaneously as catalyst is being thrown by sectors 24 to the outer portions of the bed or vessel.
Also, at the same time catalyst passing through openings 90 is selectively laid down at the innermost part of the bed by control of the spacing oE plate 60 from collar 68 and the radial placement of bar 70 and the~ size of orifice 76. In the present embodiment it will accordingly be seen that a single rotor makes possible distribution of catalyst to a multiplicity of bands which in the present embodiment form sixteen separate rings comprising then laid down by arcuate segments 24, four laid down by tubes 52, 54, 56 and 58 and two by plate 60.
In the present arrangement collar 62 and plate 60 are disconnectably connected to distribution plate 22 by screws 80.
Tubes 52, 54, 56, and 58 are formed as a permanent part of plate 22. Alternatively, the entire rotor assembly may be made as one piece, or other portions permanently connected or disconnectably connected to distributor plate 22. It will also ~zs~zv be apparent to those skilled in the art that plate 22 may be conical rather than flat, if desired.
Because the single catalyst distribution disc or rotor includes a multiplicity of flow paths, each arranged to lay down concentric annular rings of limited, but approximately e~ual radial width, across the entire circumferential area, of vessel 10, the rotor is preferably turned at a constant speed.
The speed is re~ulated to such a constant value, determined by the bed diameter, so that the rotor will cast catalyst over the entire cross-sectional area of the vessel. Once adjusted, that speed is maintained substantially constant for complete filling of each bed from support 18 to the top of the bed 16. Such uniform laying of the bed throughout its dep-th results in increased density of the total catalyst volume that can be loaded into an individual bed or throughout the vessel. In actual practice, an increase in density of about 106 has been found, as determined by the total weight of catalyst that can be loaded into a known volume of the vessel, as compared to prior methods of COP loading, using varying speeds of a rotatable disc. Since the conversio.n rate of hydrocarbon feed passing through the vessel is dependent upon such total volume of catalyst, the present invention makes possible either a higher rate of hydrocarbon feed through the reactor for yield of the same products or an increased hydrocarbon conversion at a constant feed rate in the same volume of vessel. Both of these conditions are greatly - 15 - ~ ~ ~ 4 ~ ~70 61936-1686 desirable in processing hydrocarbon feeds for catalytic conversion and represent significant cost savings in such processing.
The above described embodiments of the inventi.on are particularly directed to loading extrudate catalyst particles across the full cross-sectional area of a large diameter reactor vessel. However, the method and apparatus are also applicable to load other particulate material, such as spherical or pellet catalyst or grain, as in a silo. Other contacting materials in particle form, such as sulfur sorbers, and ion exchange materials are also frequently loaded in large diameter vessels. The present invention is particularly useful for such service to insure high density throughout a bed of solid particles in a large diameter vessel.
From the foregoing description, various modifications and changes in the apparatus and in the method of operating such apparatus will occur to those skilled in the art, all such modifications or changes coming within the scope of the appended claims are intended to be included therein.
` ~'J
Claims (11)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A method of loading catalyst particles in a large diameter vessel with substantially uniform density across the full cross-sectional area of a bed within said vessel which comprises flowing a cylindrical column of catalyst onto a single disc rotating about an axis substantially concentric with said cylindrical column, radially dividing particles from said column into a plurality of arcuate sectors having a common vertex at the rotational axis of said single rotating disc, each of said arcuate sectors having an included angle and a radial length proportional to the annular area of one of a plurality of concentric rings covering the cross sectional area of said bed, the arcuate sectors on said disc having different radii, and uniformly rotating said disc so that each of said plurality of radial and arcuate flow paths lays down said plurality of concentric annular rings to cover the surface cross-sectional area of said bed with a uniformity of depth of said catalyst particles.
2. A method in accordance with claim 1 wherein a central portion of said column of flowing catalyst is simultaneously directed to a plurality of flow channels carried by said rotating disc, each of said channels having a radial length shorter than said arcuate sectors.
3. In catalyst loading apparatus for uniformly distributing catalyst particles radially over a large diameter reactor bed from a supply hopper, said apparatus including hopper means supportable by a reactor vessel for supplying catalyst particles to said distribution surface including feed tube means positioned directly over and substantially coaxial with a catalyst distributor disc, said disc being rotatable within said reactor vessel and adapted to be supported above a reactor bed, drive means extending substantially coaxially with the axis of a hopper feed tube for discharging catalyst to said disc and means for rotatably supporting said disc perpendicular to said drive shaft means, the improvement comprising means for dividing the distribution surface of said disc into a plurality of arcuate sectors, each sector having a common vertex at the center of said disc member, and each sector having a different radius than an adjacent sector, each of said dividing means including a radial rib member between each of said sectors extending axially from said distributing surface, and each sector having an included angle proportional to the area of an annular ring on the surface of said bed of catalyst.
4. Catalyst loading apparatus in accordance with Claim 3 wherein each of said sectors includes a diametrically opposed sector having substantially the same radius and included angle.
5. In catalyst loading apparatus in accordance with Claim 3 wherein said distribution surface of said disc additionally includes a frusto-conical surface extending upwardly and inwardly - 17a -from said disc, said conical surface having a major base whose radius is less than the radius of any of said sectors and whose minor base radius is less than the radius of said feed tube means, and means for adjusting the axial distance between said discharge opening from said feed tube means and said frusto-conical surface to control the rate of flow of catalyst to said catalyst distribution surface of said disc.
6. In catalyst loading apparatus in accordance with Claim 5 wherein said minor base radius of said frusto-conical surface and the enclosed volume of said disc forms a compartment for distribution of catalyst and said disc includes a plurality of channel members, each having a radius different than said sectors, formed below said distribution surface and rotatable therewith and having feed means formed from said enclosed volume to said plurality of channel members to supply catalyst to said bed over another plurality of annular rings forming said bed.
7. A method of loading catalyst particles in a large diameter vessel with substantially uniformly high density across a bed within said vessel which comprises first dividing catalyst particles falling by gravity in a substantially cylindrical column into an annular column formed by the outer portion of said cylindrical column and a smaller diameter inner cylindrical column deflecting said annular column onto a single disc rotating about an axis substantially concentric with said cylindrical column, radially dividing particles from said annular column into a plurality of arcuate sectors on said single rotating disc, each of said arcuate sectors having a volume proportional to an annular area within the cross-sectional area of the vessel, said volume being formed by the radial length of said arcuate sector and the angular width of said sector on said disc, each adjacent arcuate sector having a different radius, dividing said inner cylindrical column into a plurality of arcuately separate flow paths substantially perpendicular to said column, said plurality of flow paths having different radial lengths and rotatable with said single disc, and each flow path being shorter than the radius of any of said arcuate sectors formed by said disc and uniformly rotating said disc so that each of said plurality of radial and arcuate flow paths lays down a plurality of concentric annular rings of differing diameters to cover substantially the surface cross-sectional area of said vessel simultaneously with a catalyst bed having uniformity of depth and substantially the same average density across the full diameter of said vessel.
8. Catalyst loading apparatus for uniformly distributing catalyst particles radially over a large diameter reactor bed from a supply hopper comprising a disc member rotatable within a reactor vessel above said reactor bed and adapted to be supported therein, said disc member having a distribution surface including a plurality of arcuate sectors, each sector having a common vertex at the center of said disc member and a different radius from at least one of the adjacent sectors, radial rib members between each of said sectors extending axially from said distributing surface, hopper means supportable by a reactor vessel for supplying catalyst particles to said distribution surface including feed tube means positioned directly over and substantially coaxial with said disc, drive shaft means extending substantially coaxially with the axis of said hopper tube discharge opening, and means for rotatably supporting said distribution surface of said disc member perpendicular to said drive shaft means.
9. Catalyst loading apparatus in accordance with claim 8 wherein each of said arcuate sectors includes a diametrically opposed sector having the same radius.
10. Catalyst loading apparatus in accordance with claim 8 wherein said distribution surface of said disc includes a frusto-conical surface extending upwardly and inwardly from said disc, said conicial surface having a major base with a radius less than the radius of any of said sectors and with the radius of the minor base less than that of said feed tube means, and means for adjusting the axial distance between said discharge opening from said feed tube means and said frusto-conical surface to control the rate of flow of catalyst therebetween to said distribution surface.
11. Catalyst loading means in accordance with claim 10 wherein said disc member includes a plurality of channels formed below said disc, each channel having a different radial length and said minor base of said frusto-conical surface includes a passageway therethrough for supplying catalyst to said channels.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US67915484A | 1984-12-07 | 1984-12-07 | |
| US679,154 | 1984-12-07 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1254720A true CA1254720A (en) | 1989-05-30 |
Family
ID=24725783
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000496502A Expired CA1254720A (en) | 1984-12-07 | 1985-11-29 | Method and apparatus for uniformly loading particulate material into cylindrical beds |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JPS61141923A (en) |
| KR (1) | KR930002241B1 (en) |
| CN (1) | CN1011762B (en) |
| CA (1) | CA1254720A (en) |
| DE (1) | DE3542340A1 (en) |
| EG (1) | EG17295A (en) |
| GB (1) | GB2168330B (en) |
| IN (1) | IN166220B (en) |
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| US4972884A (en) * | 1984-12-07 | 1990-11-27 | Chevron Research & Technology Company | Method and apparatus for uniformly loading particulate material into cylindrical beds |
| US5296202A (en) * | 1984-12-07 | 1994-03-22 | Chevron Research And Technology Co. | Apparatus for uniformly loading particulate material into cylindrical beds |
| CH671753A5 (en) * | 1987-02-17 | 1989-09-29 | Johann Arnold | |
| JPH0644987B2 (en) * | 1988-07-01 | 1994-06-15 | 出光エンジニアリング株式会社 | Catalyst filling device |
| JPH0644988B2 (en) * | 1988-07-01 | 1994-06-15 | 出光エンジニアリング株式会社 | Catalyst filling method |
| FR2646399B1 (en) * | 1989-04-27 | 1991-08-30 | Inst Francais Du Petrole | APPARATUS FOR FILLING A CONTAINER WITH A DIVIDED SOLID PRODUCT |
| EP0470142B1 (en) * | 1989-04-27 | 1993-07-07 | Institut Francais Du Petrole | Equipment for filling a container with a divided solid product |
| FR2668131B1 (en) * | 1990-10-22 | 1993-01-29 | Inst Francais Du Petrole | APPARATUS FOR FILLING A CONTAINER WITH A DIVIDED SOLID PRODUCT. |
| US5324159A (en) * | 1992-10-02 | 1994-06-28 | Praxair Technology, Inc. | Particle loader |
| US5348434A (en) * | 1992-10-21 | 1994-09-20 | East Coast Terminal Assoc., Ltd. | Cargo loading system |
| DK171911B1 (en) * | 1993-12-02 | 1997-08-11 | Topsoe Haldor As | Method and device for uniform filling of catalyst tubes |
| FR2727875B1 (en) * | 1994-12-09 | 1997-03-21 | Air Liquide | INSTALLATION FOR TREATING AT LEAST ONE FLUID, APPLICATIONS FOR TREATING AN AIRFLOW AND METHOD FOR LOADING A MASS OF PARTICULATE MATERIAL OF SUCH AN INSTALLATION |
| US5837021A (en) | 1994-12-09 | 1998-11-17 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Installation for the treatment of at least one fluid, by passage through two adjacent masses of material |
| FR2862893B1 (en) * | 2003-11-28 | 2006-02-24 | Commissariat Energie Atomique | DEVICE FOR FILLING A MOLD WITH A POWDER OR A MIXTURE OF POWDERS |
| DE602007001938D1 (en) * | 2006-12-01 | 2009-09-24 | Haldor Topsoe As | Device for filling pipes with particulate catalytic material and filling method |
| CN101279672B (en) * | 2008-04-22 | 2010-06-02 | 苏州启成精密工业有限公司 | High speed rotating feeding device |
| CN101857147B (en) * | 2010-05-26 | 2012-07-18 | 三一重工股份有限公司 | Isolation-proof device and mixed material storing system with the same |
| CN102249098B (en) * | 2011-06-28 | 2012-11-07 | 周瑞 | Machine for filling catalyst in converter reaction tube |
| ES2465391B1 (en) * | 2012-12-04 | 2015-04-13 | Felix Martin Suñer, S.A.U. | Solid Materials Distribution Machine |
| CN103057869B (en) * | 2013-01-04 | 2015-07-08 | 浙江乐客来机械有限公司 | Leakage-proof hopper |
| DE102013101949A1 (en) | 2013-02-27 | 2014-08-28 | Thyssenkrupp Uhde Gmbh | Device for filling in particular radial reactors with catalyst material |
| CN104129659B (en) * | 2014-07-15 | 2017-02-08 | 国电科学技术研究院 | Passive even material distributing method and device |
| CN105750096B (en) * | 2014-12-17 | 2018-12-25 | 中国石油天然气股份有限公司 | Centrifuge dissipates mud device and centrifuge |
| JP6383679B2 (en) * | 2015-02-12 | 2018-08-29 | ソフタード工業株式会社 | Catalyst filling apparatus and catalyst filling method |
| CN105129448A (en) * | 2015-09-06 | 2015-12-09 | 吴刚 | Device capable of continuously supplying powder or granules in accurate flow mode without vibration |
| CN105383959A (en) * | 2015-12-16 | 2016-03-09 | 中储粮油脂有限公司 | Squat silo grain feeding distributor |
| CN105398705A (en) * | 2015-12-16 | 2016-03-16 | 中储粮油脂有限公司 | Pressure door for squat silo distributing device |
| CN105692240B (en) * | 2016-03-04 | 2017-11-17 | 曾周玉 | A kind of storage bin of logistics |
| CN105966932B (en) * | 2016-04-05 | 2018-11-23 | 烟台南山学院 | A kind of storage bin |
| CN106225484B (en) * | 2016-07-28 | 2018-08-03 | 台州宝诚科技服务有限公司 | A kind of environment-friendly type concrete pouring robot |
| DE102017118750B4 (en) * | 2017-08-17 | 2019-09-05 | Zeppelin Systems Gmbh | Distributor head of a gravimetric loading system for bulk materials |
| FR3083527B1 (en) * | 2018-07-04 | 2022-09-02 | Crealyst Group | COMPENSATED FLOW FILLING SYSTEM |
| CN111921460B (en) * | 2020-06-19 | 2021-03-16 | 宁波巨化化工科技有限公司 | Gas-phase aldehyde hydrogenation reactor |
| CN112642383A (en) * | 2020-12-22 | 2021-04-13 | 山东滨农科技有限公司 | Synthetic acyl chlorination device of mesotrione that protecting effect is good |
| CN113666478B (en) * | 2021-09-09 | 2022-12-02 | 宜兴市凯斯特环保机械有限公司 | Sewage treatment pipeline and sewage treatment system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3804273A (en) * | 1972-06-16 | 1974-04-16 | Atlantic Richfield Co | Catalyst distribution apparatus |
| US3972686A (en) * | 1974-01-31 | 1976-08-03 | Universal Oil Products Company | Device for loading catalyst particles into a reaction zone |
| DE2703329C3 (en) * | 1977-01-27 | 1981-04-16 | Gebrüder Weiss KG, 6340 Dillenburg | Arrangement for level filling of vertical containers |
| FR2431449A1 (en) * | 1978-07-20 | 1980-02-15 | Raffinage Cie Francaise | DEVICE FOR DISTRIBUTING A DIVIDED SOLID IN AN ENCLOSURE |
| US4433707A (en) * | 1981-09-25 | 1984-02-28 | Chevron Research Company | Method and apparatus for level loading of vessels using catalyst oriented packing |
-
1985
- 1985-11-15 IN IN912/MAS/85A patent/IN166220B/en unknown
- 1985-11-29 DE DE19853542340 patent/DE3542340A1/en not_active Withdrawn
- 1985-11-29 CA CA000496502A patent/CA1254720A/en not_active Expired
- 1985-12-04 GB GB08529844A patent/GB2168330B/en not_active Expired
- 1985-12-04 CN CN85108813A patent/CN1011762B/en not_active Expired
- 1985-12-05 KR KR1019850009128A patent/KR930002241B1/en not_active IP Right Cessation
- 1985-12-05 EG EG775/85A patent/EG17295A/en active
- 1985-12-06 JP JP60273607A patent/JPS61141923A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0472571B2 (en) | 1992-11-18 |
| KR930002241B1 (en) | 1993-03-27 |
| IN166220B (en) | 1990-03-31 |
| DE3542340A1 (en) | 1986-06-12 |
| JPS61141923A (en) | 1986-06-28 |
| CN85108813A (en) | 1986-08-20 |
| CN1011762B (en) | 1991-02-27 |
| KR860004646A (en) | 1986-07-11 |
| GB8529844D0 (en) | 1986-01-15 |
| GB2168330A (en) | 1986-06-18 |
| EG17295A (en) | 1991-08-30 |
| GB2168330B (en) | 1988-12-14 |
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