JPS61141923A - Method and device for charging fine particle material into vessel - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION Field of the Invention The present invention relates to a method and apparatus for uniformly charging particulate material into a cylindrical bed or vessel. In particular, the present invention uniformly deposits catalyst particles or the like onto a large diameter cylindrical vessel by simultaneously flowing the catalyst into multiple concentric rings of catalyst particles over an entire circular area of the catalyst bed. catalyst-oriented packing (COP) of the catalytic reaction bed by distributing the
) related to charging. The present invention is primarily directed to ensuring that a catalyst, such as a cylindrical extruded catalyst having a high angle of repose, is uniformly contained within the bed at a high catalyst-to-volume ratio. ).

A particular object of the invention is to increase the packing density of particles with a high angle of repose, including spheroidal particles, such that a bed is formed simultaneously by a large number of concentric rings across the entire diameter of the container. It is. A single rotating disk or rotor in which multiple rings of catalyst-like particles divide the flow of catalyst from an overhead flow tube into a number of radial sectors with different radii. Due to the uniform rotation of
It is formed. As a result, the rate of exit of catalyst particles from each fan of the distribution surface of the disk produces a number of different radial throw distances within the bed or vessel. All sectors of the disk rotate at the same speed so that concentric rings of catalyst are thrown into the vessel and deposited simultaneously in adjacent annular rings. Such annular rings preferably have a relatively narrow radial width but vary progressively in radial distance from the axis of the vessel to form a number of concentric rings uniformly covering the bed of catalyst. .

BACKGROUND OF THE INVENTION Catalytic reactor vessels having one or more fixed catalyst beds are commonly packed using catalyst distributors.

Such techniques are catalytically oriented (often CO
It is particularly useful for producing uniformity in permeability and total density of the catalyst bed. In modern catalytic processing, particles of catalyst are typically formed by extrusion into cylindrical rods with diameters of 1.59 mm to 6.35 mm. It is built A. The rod is then broken into lengths from 6.35 mm to 12.7 mm. Such extrudates are typically formed from alumina, silica-alumina or synthetic or natural zeolite materials and are considerably less expensive to produce than single spheroidal catalysts. However, the particles of this type of extrudate have a high angle of repose, the angle at which the free resting stack of the 11 is stable. As a result, it is difficult to distribute these particles evenly throughout a large diameter cylindrical container. Furthermore, due to differences in the size of these particles, as well as the depping and breaking that occur during both production and charging into the processing reactor,
These particles can be ``classified'' or ``minute!'' if the bed is packed by gravity alone from a central point within the container.
11."

The first purpose of the COP charge is to minimize as much as possible the space and therefore the local "holes" that can occur during the exothermic reaction of the hydrocarbons on the catalyst particles. Additionally, the increased packing density of the solid particulate material improves reactant flow distribution within the vessel. Furthermore, the increased density of the bed limits bed deposition when the reactor is put into production and fluid forces are applied to the fluid flow through the reactor. Generally, the catalyst capacity can be increased by several percentage points in existing vessels. On the contrary, a few percent smaller reactor volume is required for the same m of catalyst in a new vessel.

Generally, known catalyst-oriented charging devices have included a distributor disk having a uniform diameter and a number of radial blades or fin members on the top of the rotating disk. Generally, this distributor is a conical member or a flat circular plate. However, in order to distribute the catalyst over the entire cross-sectional area of the bed, the speed of the distributor must be varied since the distance over which the catalyst is thrown is proportional to the speed of the disk. If this disk is a flat plate with wings formed on its surface,
Several holes are provided in the plate to allow some of the catalyst particles to fall directly downward through the rotating member towards the center of the reactor vessel.

U.S. Pat. No. 3,804,273 Uhl's specification states:
An apparatus for charging a bed of catalyst with a radial distributor having a single circular 31E-shaped surface is disclosed. The only way to distribute the catalyst over the entire diameter of the bed is to increase or decrease the speed of the rotating disk.

Johnson et al., U.S. Pat. No. 3,972,686, describes a flat disk having vanes and a number of slots or holes through which a portion of the catalyst falls near the center of the bed. Disclosed: The remainder of the catalyst is thrown out towards the side of the container. This system also requires varying the speed of the rotating disk to load the catalyst so that it covers the entire plane of the catalytic reactor bed.

A particular drawback of this type of prior art arrangement is that, at one velocity, particles of catalyst falling onto the surface tend to be thrown into a circular or annular mound. Larger particles fall to the bottom and out of the mound, and smaller particles settle on the mound itself.

These difficulties can be alleviated to some extent by changing the speed of the rotating disk, but since the charging rate is proportional to the speed, reducing the disk speed will reduce the charging time for the reactor. increases significantly. On the other hand, if the disk velocity becomes excessive, the result is that the catalyst is thrown out of the disk without sufficient residence time to control the radial throw distance. Moreover, the interior of the bed is usually so full of dust that the operator cannot actually see the bed of catalyst from the charger, making it difficult to achieve the desired radial throw distance. It is difficult to control the disc speed. It is therefore necessary to determine the expected distribution level by the number of drums of catalyst charged at a given bed level. Such methods are time consuming and are not always accurate enough to allow bed level charging. In practice, the bed above the reactor may be moved higher than necessary, e.g. from 152.4 am to 304 am.
Fill the bed at the outer edge 8 mm higher and then a similar amount (increase the height of the center level above that at the outer edge and the depth of the bed or beds from the corner of this reactor). It is common practice to repeat this alternately as the corners are increased.
This problem is further exacerbated when the lower bed has to be packed through a centrally located passageway in the overlying bed support. This makes visual inspection even more difficult.

U.S. Pat. No. 4,306,829 to Lauchtay et al. discloses a distributor for integrated storage of catalyst particles in a reactor or grain storage in a reactor. The distributor includes a flexible shaft lug pivotally supported by a hook along the length of the drive shaft. These laps may be made of reinforced rubber and either be of the same shape or be progressively lengthened as they move away from the outlet of the feed hopper.

These examples have shown that this system is suitable for packing into models of reactor vessels with a diameter of 60 cm. The effective length of the rotating slap appears to vary in diameter in proportion to the speed of the drive shaft [α and the interaction with the falling catalyst particles. Effective loading of vessels using the combination of the above arrangements is limited to relatively small diameter reactors for the reasons discussed below.

Farnum's No. 11 U.S. Patent No. 4, assigned to the assignee of the present invention.
．． , 433,707 describes the method of distributing catalyst particles uniformly from the center of a container to its outer wall using a number of discs of different diameters rotated at the same speed by a single drive shaft. A method and arrangement W7 for uniformly packing reactor vessels at each level a'3 with distribution is disclosed. Preferably, three conical discs are used, with the largest diameter located closest to the feed hopper feed tube. The upper disc has a central opening that allows delivery of catalyst to each of the lower discs. Because the discs have different diameters, each disc does not spread the catalyst to different areas around the vessel as long as the drive shaft rotates at a constant speed. Such equipment may be used for discharging catalyst into vessels of relatively small diameter and deep beds, where a suitable head chamber is available at the exchange section of the vessel or above each of several beds. However, this method is also limited to varying the speed of the rotor and to transversely only a small number of annular rings at the same time.

German Patent No. 2,703.329 (March 1978) discloses another particle charging system using multiple axially spaced discs rotated by a common drive shaft. has been done. This mode of operation is similar to that of the Fanham patent.

SUMMARY OF THE INVENTION In carrying out the process of the present invention, a single catalyst distributor is positioned at a suitable level above the bed to be packed. Catalyst is then fed to the distributor from a hopper having a feed tube positioned such that a substantially cylindrical column of catalyst falls onto a single rotor or disk member.

The particles of catalyst are thus distributed by a single disk in a substantially uniform high density across the entire diameter of the bed by forming multiple annular rings of catalyst concentric with the center of this vessel or bed. be done. Such action is accomplished by deflecting a cylinder of catalyst into a number of arcuate sectors or sections of varying radial length on a single rotating disk, without changing the disk velocity. achieved. Preferably, each arcuate section has a volume proportional to one of the annular areas of the floor within the cross-sectional area of the container. This desired volume is formed by both the radial length of the arcuate sector and the included angle on the disc. disk 1
In one preferred form, each adjacent arcuate sector or section has a width substantially equal to each other and has a mutually responsible volume so as to form such an annular ring of catalyst within said bed. It is desirable to have

Depending on the total cross-sectional area of the vessel, the cylindrical volume of catalyst flowing from the feed tube can be divided into an outer annular column and an inner cylindrical column. In a preferred embodiment, this can be accomplished by a frusto-conical member extending upwardly and inwardly from the main distribution surface of the disk into the feed tip. The large base of the circular if-shaped member and the main disk direct the catalyst into a number of other discrete arcuate channels of different radial lengths substantially perpendicular to the column. It serves as an auxiliary hopper or storage volume. Each of the other multiple channels described above is also rotated by a single rotor or disk. Preferably, each of these channels is shorter than the radius of any arcuate portion formed by the disc.

By uniformly rotating the disc, each of the multiple arcuate channels transverses concentric annular rings of different diameters. These rings substantially coat the surface area of the catalyst bed support within the vessel with catalyst. Since each ring is formed simultaneously at all levels, the catalyst depth is uniform across the entire vessel or bed diameter and the resulting bed of catalyst is relatively small compared to the same vessel or bed volume. The average density is large.

Still other objects and advantages of the present invention arise from the following detailed description of the preferred embodiments of the invention, which is made with reference to the accompanying drawings, which form an integral part of this specification.
It will be clear to those skilled in the art in light of Equation 1.

22 DESCRIPTION OF THE PREFERRED EMBODIMENTS OF THE INVENTION FIG. 1 shows a large diameter catalytic reactor vessel 10 using a preferred type of catalyst loading device 12 for transversely placing concentric rings of catalyst particles. The application of the method of the present invention to the loading of oriented catalyst to As shown in FIG. 2, a number of such concentric rings 14 with similar annular widths or average radial lengths deposit catalyst in bed 16 to the same depth and density across the entire diameter. The entire diameter of the container 10 is coated with the same diameter so that it is packed tightly.

Such methods aim at loading catalyst with a large angle of repose, such as cylindrical extrudate particles of catalyst that are relatively immobile after deposition.

As particularly illustrated in FIG. 1, vessel 10 may include multiple beds 16, each formed on a catalyst support structure or screen 18. As shown, multiple support structures 18 may be provided such that each of several serially interconnected flowbeds 16 is positioned one above the other. . floor 16
il! of this catalyst distributor to ensure that each of the il!s is packed with uniform density throughout its height or depth. The length in the II direction is made relatively short so that the top of the floor below the upper support structure 18 or the container 10
It is important that the top of the catalytic converter, constructed in accordance with the present invention, be packed so that there is little or no headroom. The rotor member 20 includes a first distribution surface formed by a plate 22 which is divided into a number of arcuate sectors 24 having a common apex at their axis of rotation 30. .But as shown,
For dynamic stability of the rotor, each sector has a different radius than any of its neighboring sectors. As previously mentioned, two sectors of equal area are positioned diametrically opposite each other to dynamically balance the rotor.

In the particular embodiment illustrated in FIGS. 3 and 4, the radial rib members 26 form the sector 24 and have widely varying radial lengths as shown. are doing. Rib members 26 are generally perpendicular to and extend axially from the dispensing surface of plate 22. The individual sectors 24 have different included angles, which together with the depth of the ribs 26 determine the total amount of catalyst that can be dumped into each ring on the surface of the bed 16. Particular attention should be paid to determining the volume. It will be appreciated that the total volume of each individual sector is proportional to the area of the corresponding catalyst ring 14 to be dumped onto the top of the bed 16. Generally, the sector 24
The said volume of will be proportional to the circumferential area of said ring and the width of each ring with respect to adjacent rings formed by other sectors 24.

As particularly shown in FIG. 4, the distributor plate 22 is attached to the distribution surface formed by the plates 22 and the individual sectors 24, for example, on a drive shaft attached by a hub 34 and a key or drive pin 36. Axis 3 substantially coaxial with 32
0 by the feed tube 28.

As illustrated in FIG. 1, the dispensing device of the present invention can be used with conventional catalyst orientation backing devices. As shown, hopper 38 is loaded with catalyst and gravity feeds the catalyst through feed tube 40 to feed hopper 42 below. The hopper 42 carries a head of catalyst above the distribution disk 20, preferably over a channel 44 provided in the upper grid 18 or on the upper flange 46 of the vessel 10! Preferably, the blade is supported by an arm 49 which is pivotally mounted. Next, the lower hopper 4 is moved so as to drive the rotating disk 20, the shaft 32, and the rotor 20 at a desired speed.
It can be driven by a local air motor mounted on 2 or an electric motor 48. The motor 48 is driven by an air hose or electrical cable 50.
: To be done.

Alternatively, it may be rotated by a drive 8@32 extending above the flange 46J to an external motor (not shown).

A particular problem with the distribution of catalyst in large diameter vessels is to even out the distribution of catalyst near the center of the vessel. For example, from 2.44m including the center part/
Evenly distributing the catalyst across the entire diameter of the vessel, which is 1.57 m, is extremely difficult. Merely throwing the catalyst down through the center of the distribution plate and not letting it roll outwards from the center pile will not give satisfactory results.

In this preferred embodiment of the invention, this problem is solved by a number of rectangular tubes or channels 52.5=1.5, each having a different radial length from each other. .

This problem is solved by using 56 and 58.

As can be clearly seen in FIG. 5, these channels, together with the plate 60 supported on the lower collar 62, provide an annular catalyst distribution ring.

The plate 60 is supported below the collar 62 by a number of threaded rods 64 and a collar 66 so that the plate 60 can be properly spaced with respect to the flange 68 of the collar 62. The plate 60 itself serves as a further distributor of catalyst by the action of the radial rods 7o carried on the top surface. 111 in the radial direction from the axis of rotation of the plate 60
A suitable directing lower 2 spaced apart controls the flow of catalyst 61 to the innermost force ring.

Although not shown in detail, the feed tube 40 is annularly shaped into a number of sectors 24 relative to the amount of catalyst flowing in a cylindrical manner over the upper and inner edge 87 of the disk 86. The truncated circle ε11 is proportional to the side of the catalyst flowing as follows.
It will be appreciated that the shaped disc 86 is adjustably positioned relative to the conical surface of the disc 86. The chamber 88 formed by the frustoconical section 86 and the plate 22 thus serves to distribute the catalyst between the tubes 52, 54, 56 and 58 and the plate 60. Similarly, as previously discussed, the opening between 60 and collar 68 controls the overall flow of catalyst from the edge of plate 60 and through orifice 76 with the aid of rod 70.

As most clearly illustrated in FIG. 5, the supply of catalyst flowing within the internal cylindrical portion from the feed tube 40 passes through rectangular openings 84 in the plate 22 into four rectangular shapes. The catalyst flowing to the tubes 52, 54, 56 and 58 and to the distributor 4k 60 similarly passes through four circular openings 90 provided in the plate 22.

Each radial passage J of sector 24 is shorter;
R-b 52 having different lengths in the radial direction,
54. , 56 and 58, the inner diameter ring or annular portion of this catalyst is
Stuffed at the same time as it is being thrown onto the floor or into the outer part of the container. At the same time, catalyst passing through opening 90 selectively crosses the innermost valve of this bed due to constraints 611 on the spacing of plate 6o from collar 68, the radial placement of rod 7o, and the size of orifice 76. be placed. Therefore, in this embodiment, the arcuate sector 24 has 10 transversely placed tubes and 52, 54, 56 and 5 tubes.
It can be seen that a single rotor enables the distribution of catalyst into a number of zones, 4 transversely by plates 8 and 2 transversely by plates 60, forming a total of 16 separate rings. Probably.

In this arrangement, collar 62 and plate 60 are attached to screws 80
It is separably connected to the distribution plate 22 by. Tubes 52, 54, 56 and 58 are formed as permanent parts of plate 22. Instead, the entire rotor body may be made in one piece, or other portions may be permanently or reliably connected to the distribution plate 22. It will be apparent to those skilled in the art that plate 22 may be circular rather than flat, if desired.

A single catalyst distribution disk or rotor contains a number of channels, each of which traverses concentric annular rings of slightly but approximately equal width across the entire circumference of the vessel 10. Preferably, the rotor is rotated at a constant speed. The speed is adjusted to a constant value determined by the bed diameter so that the rotor throws the catalyst over the entire lateral area of the vessel. Once adjusted, the speed remains substantially constant during the complete packing of each bed from support 18 to the top of bed 16. As a result of this uniform transverse h'' of the bed over the entire depth, the density of the total catalyst volume that can be charged into the individual beds or over the entire vessel is increased. In practice, compared to prior art COP charging methods using varying speed melons of rotatable disks, J: is determined by the total weight of catalyst that can be charged into a known volume of the vessel. Approximately 10
% increase in density has been found. Since the conversion rate of the hydrocarbon feed through the vessel depends on such total volume of catalyst, the present invention provides a high feed rate of hydrocarbons through the reactor or the same for the same product output. Both of these conditions allow for either increased hydrocarbon conversion at a constant feed rate to the volume of the vessel. is highly desirable and represents a considerable saving of money in such processing.

The above-described embodiments of the invention are specifically directed to the loading of extruded catalyst particles across the entire cross-sectional area of a large diameter reactor vessel. However, the method and the device are also applicable to charging spherical or helet-shaped catalysts or other granular materials such as grains in silos. Other catalytic phases in the form of particulates, such as sulfur absorbers and ion exchange materials, are also often placed in large diameter vessels. The present invention is particularly useful in such installations to ensure high density throughout the bed of solid micromolecules within large diameter vessels.

From the above description, various modifications and variations in the apparatus and methods of operating the apparatus will be apparent to those skilled in the art. It is further intended that all such modifications or variations be included within the scope of the appended claims.

[Brief explanation of the drawing]

FIG. 1 is an elevational view, partially in section, of a large diameter hydrocarbon reactor in which a number of concentric catalyst rings are placed transversely to form one of several beds within the vessel. Figure 2 is a diagram illustrating the method of the present invention using a single-port distributor.
A plan view of a cross section taken in the direction of arrow 2-2 in the figure.
A diagram illustrating the manner in which concentric rings of catalyst micromolecules are cast into the single-port distributor of the present invention; FIG. 3 shows the first catalyst distributor rotor illustrated in FIG. 1; The preferred arrangement of radial lengths and arc spans required to transverse a number of concentric circles of catalyst particles having similar depths is shown in FIG. Figure 4 specifically shows the rotor in Figure 3.
Elevation in section along the line and looking in the direction of the arrow, showing the cone of the rotor for dividing the flow from the popper feed tube into an upper distributor root and a lower distribution channel carried by the rotor. A diagram illustrating the cooperation of shape parts;
Figure M5 passes through the lower part of the rotor structure and is 5-5 in Figure 4.
Plan view, partially in section, along the line and looking in the direction of the arrows, illustrating the distribution of catalyst into multiple tubes and distribution holes, which is particularly useful for filling the inner annular ring of large diameter vessels. FIG. 6 is a plan view of the lower distribution structure taken along line 6-1m1 of FIG. Figure 7 shows the entire day shown in Figures 1 to 6.
FIG. 2 is a structural perspective view showing each part of the tar structure arranged in sequence. 10- Large diameter catalytic reactor? ! A: 12-catalyst loading fffi: 14-concentric ring; 16-
floor; 18-support structure or screen; 20-distribution [J
-Tap part; 22-Root; 24-Sector body; 26-Rib: 2
8-feeding tube; 30-axis: 32-axis; 34-hub: 36-driving pin: 38-hopper: 40--feeding scoop: 42-feeding hopper: 44-manway: 46-upper flange :48-motor;50
- Electrical cable: 52.54.56 J: and 58 - Channel: 60 - Plate: 62 - Lower collar: 64 - Threaded stud: 6 Row nuts 1 -; 6
8-flangenia 0-radial rod; 72-inlet; 7-low orifice: 84-unilateral opening: 86--truncated 311-shaped disc: 87-inner edge: 88-chamber: 90-opening :

Claims (11)

[Claims] (1) Particles of catalyst are charged into a vessel of large diameter at a substantially uniform density over the entire cross-sectional area of the bed within said vessel, with an axis substantially concentric with the cylinder of catalyst; flowing said cylinder of catalyst over a single rotating disk; a plurality of arcuate sectors each having a common apex at the axis of rotation of said single rotating disk; a sector having a radial length and an included angle proportional to the annular area of one of a number of concentric rings covering the cross-sectional area of the bed, and the arcuate sector on the disk; radially distributing particles from said column into a plurality of arcuate sectors having different radii; each of said plurality of radial and arcuate channels having said plurality of concentric placing an annular ring on its side and uniformly rotating the disk so as to cover a cross-sectional area of the surface of the bed with a uniform depth of particles of the catalyst. (2) The method of claim 1, wherein the central portions of the cylindrical bodies of the flowing catalyst each have a radial length shorter than the arcuate sectors; A method characterized in that it is simultaneously directed into a number of flow channels carried by a rotating disk. (3) a catalyst loading device positioned immediately above the catalyst distributor disk for uniformly distributing catalyst particles radially from the feed hopper to one side of the large diameter reactor; a hopper arrangement including a feed tube arrangement substantially coaxial with the reactor vessel and supportable by the reactor vessel for supplying particles of catalyst to the distribution surface; a disk adapted to be supported above the reactor floor; a drive extending substantially coaxially with the axis of the hopper feed tube for discharging catalyst into the disk; and a drive shaft device. a device for rotatably supporting said disk perpendicular to said disk; and a device for dividing said distribution surface of said disk into a number of arcuate sectors, each segment sectors have a common vertex at the center of the disk member, and each sector has a different radius than an adjacent sector, and each of the separation devices extends axially from the dispensing surface. a radial rib member between each of said elongated sectors, and each sector has an included angle proportional to the area of the annular ring on the surface of said catalyst bed. A catalyst charging device characterized by: (4) A catalyst charging device according to claim 3, which includes diametrically opposed sectors, each of which has substantially the same radius and included angle. input device. 5. The catalyst charging device of claim 3, wherein the distribution surface of the disk additionally includes a frusto-conical surface extending upwardly and inwardly from the disk; a conical surface has a large base having a radius smaller than the radius of any of the sectors, and the radius of the smaller base is smaller than the radius of the feed tube arrangement, and the catalyst distribution surface of the disc; a catalyst loading device, wherein a device is provided for adjusting the axial distance between the discharge opening from the feed tube device and the frustoconical surface so as to control the amount of catalyst discharged into the feed tube device; . (6) The catalyst charging device according to claim 5, wherein the radial range of the small base of the frustoconical surface and the enclosed volume of the disc form a partition for distributing the catalyst. and a number of other annular rings having different radii than said sector and said disk including a number of channel members, each of which is formed below said distribution surface and is rotatable therewith. Catalyst loading device having a feed system formed from said enclosed volume to said plurality of tube members for supplying catalyst to said bed covering said bed. (7) A method is adopted in which catalyst particles are charged in a large-diameter container at a substantially uniform high density across the bed in the container, so that the catalyst particles are actually dropped by gravity in a cylindrical shape. first dividing the particle into an annular column formed by an outer portion of the column and an inner column of small diameter, rotating about an axis substantially concentric with said column; deflecting the annular column onto a single disk; and radially dividing the particles from the annular column into volumes each proportional to the area of the annular within the cross-sectional area of the vessel. and the volume is formed by the radial length of the arcuate sectors and the angular width of the sectors on the disc. ,
each adjacent arcuate sector having a radius different from each other; and dividing the inner cylindrical body into a plurality of arcuate separation channels substantially perpendicular to the column; the radius of any one of said arcuate sectors in which the channels have different radial lengths and are rotatable with said single disc, and each channel is defined by said disc; the surface of the vessel with a bed of catalyst, each of the plurality of radial and arcuate channels having a uniform depth and substantially the same average density across the entire diameter of the vessel; A method comprising uniformly rotating said disk so as to transverse a number of concentric annular rings of different diameters to substantially cover the cross-sectional area. (8) a catalyst charging device for uniformly distributing particles of catalyst radially from a feed hopper over the bed of a large diameter reactor within the reactor vessel above the reactor bed; a disc member adapted to rotate and be supported therein, the disc member having a distributing surface including a plurality of arcuate sectors, each sector having a common center point of the disc member; radial rib members between each of said sectors extending axially from said distribution surface and having a radius different from at least one of the adjacent sectors; a hopper arrangement supportable by the reactor vessel for supplying catalyst particles to the distribution surface, the feed being positioned substantially coaxially with and immediately above the disc; a hopper arrangement including a tube arrangement; a drive shaft arrangement extending substantially coaxially with the axis of the hopper tube discharge opening; and a dispensing surface of the disk member perpendicular to the drive shaft arrangement. and a device for rotatably supporting the catalyst. (9) A catalyst charging device according to claim 8, comprising diametrically opposed sectors, each of the arcuate sectors having the same radius. 10. The catalyst charging device of claim 8, wherein the distribution surface of the disk includes a frusto-conical surface extending upwardly and inwardly from the disk, the surface has a large base portion having a radius smaller than the radius of any of the sectors, and a smaller base portion having a radius smaller than the radius of the feed tube arrangement; adjusting the axial distance between the aperture and the frustoconical surface;
A catalyst loading device including a device for controlling the flow of catalyst to and from the distribution surface. (11) The catalyst charging device according to claim 10, including a plurality of channels formed below the disk, each channel having a different length in the radial direction, and Catalyst loading device in which the small base of the conical surface includes a through passage for supplying catalyst to said channel.