JPH0472571B2 - - Google Patents

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 container. 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. Concerning the charging of catalyst-oriented packing (COP) of the catalytic reaction bed by distribution. 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. ing.

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. The uniformity of a single rotating disk or rotor in which multiple rings of particles, such as catalyst, divide the flow of catalyst from an overhead flow tube into a number of radial sectors with different radii from each other. Due to rotation,
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 are preferably relatively narrow in radial width but have progressively different radial distances from the axis of the vessel to form a number of concentric rings uniformly covering the bed of catalyst.

B. Background of the Invention Catalytic reactor vessels having one or more fixed catalyst beds are commonly packed using catalyst distributors. Such a technique is known as catalyst-oriented packing (often referred to as COP charging) and is sometimes particularly useful in producing uniformity in permeability and overall density of the catalyst bed. In modern catalytic processing, catalyst particles generally have a diameter of
Manufactured by extrusion into cylindrical rod shapes ranging from 1.59 mm to 6.35 mm. Then the rod above is
It is broken from 6.35mm to 12.7mm in length. Such extrudates are typically made of alumina or silica.
They are formed from alumina or synthetic or natural zeolite materials and are significantly cheaper to produce than spheroidal catalysts. However, the particles of this type of extrudate have a high angle of repose, ie, the angle at which a freely stationary stack of materials is stable. As a result, these particles are difficult to distribute evenly throughout a large diameter cylindrical container. Moreover, due to differences in the size of such particles, as well as chipping and breaking during both production and charging into the processing reactor, these particles If they are packed together by gravity alone from a central point within, they tend to "classify" or "separate."

The primary purpose of COP charging is space, therefore
The aim is to minimize local "hot spots" that can occur during the exothermic reaction of the hydrocarbons on the catalyst particles. Moreover, the increased packing density of the solid particulate material improves the flow distribution of the reactants within the vessel. Furthermore, the increased density of the bed limits bed deposition when the reactor is put into production and subjected to fluid forces by fluid flow through the reactor. Generally, the amount of catalyst can be increased by several percent in existing vessels. On the contrary, a few percent smaller reactor volume is required for the same amount of catalyst in a new vessel.

Generally, known catalyst-oriented charging devices 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 vanes formed on its surface, several holes are provided in said plate so that some of the catalyst particles can be directed directly downward through the rotating member towards the center of the reactor vessel. Being allowed to fall.

U.S. Pat. No. 3,804,273 to Uhl discloses an apparatus for charging a bed of catalyst with a radial distributor having a single conical surface. 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, discloses a flat disc having vanes and a number of slots or holes through which a portion of the catalyst falls near the center of the bed. ; the remainder of the catalyst is thrown out towards the side of the vessel. 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 the particles of catalyst falling onto the surface are thrown into a circular or annular mound which tends to sort them. Larger particles fall to the bottom and out of the mound, and smaller particles stop 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 very 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, fill the bed above the reactor with the outer edge higher than necessary, e.g. 152.4 mm to 304.8 mm higher, and then raise the center level height above the outer edge by a similar amount. It is common practice to alternate and repeat this as the depth of the bed or beds increases throughout the reactor. This is the case when the container contains several separate beds supported by each separate support "screen" and the lower bed must be packed through a passage provided in the center of the transverse bed support above. The problem gets worse. Visual inspection is thus made increasingly difficult.

U.S. Pat. No. 4,306,829 to Rautatei et al. discloses a distributor for storage of catalyst particles in a reactor or grain in a silo. The distributor includes a flexible strap pivotally supported by a hook along the length of the drive shaft. These straps may be formed from unreinforced rubber and are of equal length or progressively longer as they move away from the feed hopper outlet. These examples show that this method is suitable for packing into models of reactor vessels with a diameter of 60 cm. The effective length of the rotating strap appears to vary in diameter in proportion to the speed of the drive shaft and its interaction with falling catalyst particles. Effective loading of vessels using each of the above arrangements is limited to relatively small diameter reactors for the reasons discussed above.

Huanum, U.S. Pat. No. 4,433,707, assigned to the assignee of the present invention, discloses the use of multiple discs of different diameters rotated at the same speed by a single drive shaft. A method and apparatus are disclosed for uniformly packing a reactor vessel at each level with an even distribution of particles of catalyst from the center to its outer wall. Preferably, three conical disks are used, with the largest diameter 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 spreads the catalyst to a different area around the vessel as the drive shaft rotates at a constant speed. Such a device may be equipped with a suitable "head" at the top of the container or above each of the several beds.
It is quite suitable for discharging the catalyst into a vessel with a relatively small diameter and deep bed where the chamber is available. However, this method is also limited to horizontally positioning only a small number of annular rings at the same time without changing the speed of the rotor.

German Patent No. 2703329 (March 1978) discloses another particle charging system using multiple axially spaced discs rotated by a common drive shaft. This mode of operation is similar to that of the Fanham patent.

SUMMARY OF THE INVENTION In carrying out the method 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 in a single disc across the entire diameter of the bed in a substantially uniformly high density, forming multiple annular rings of catalyst not concentric with the center of the vessel or bed. distributed. 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. if you can,
Preferably, each arcuate portion 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 defined both by the radial length of the arcuate sector and by the included angle formed by adjacent sides of the sector on the disc. In one preferred form of disk, each adjacent arcuate sector or section has a width substantially equal to each other, so as to form such an annular ring of catalyst within the bed. It is desirable to have different volumes.

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 may be accomplished by a frusto-conical member extending upwardly and inwardly into the feed tube from the main distribution surface of the disk. The large base of the conical member and the main disc supply catalyst to 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 disc. 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. Because 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 will become apparent to those skilled in the art in light of the following detailed description of preferred embodiments of the invention, taken in conjunction with the accompanying drawings, which form an integral part of this specification. It will be obvious.

D. DESCRIPTION OF THE PREFERRED EMBODIMENTS OF THE INVENTION FIG. 1 shows a preferred type of catalyst loading device 12 for transversely placing concentric rings of catalyst particles.
The application of the method of the invention to the loading of oriented catalyst into a large diameter catalytic reactor vessel 10 using a catalytic reactor vessel 10 is illustrated. As shown in Figure 2,
The entire diameter of the vessel 10 is such that a large number of such concentric rings 14 of similar annular width or average radial length pack the catalyst in the bed 16 to the same depth and density across the entire diameter. are coated at the same time.
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.

Specifically, as shown in FIG. 1, vessel 10 can 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. . To ensure that each bed 16 is packed with uniform density throughout its height or depth, the axial length of the catalyst distribution device is kept relatively short so that the upper support structure It is important that the top of the floor below the body 18, or the top of the container 10, is made to be packed as tightly as possible so that there is little or no head space. For this reason, the catalyst distribution roller member 20 constructed in accordance with the present invention includes a first distribution surface formed by a plate 22, which plate 22 has a common apex at its axis of rotation 30. A bow fan-shaped body with many shapes 2
It is divided into 4 parts. However, as shown, each sector has a different radius than any of its adjacent sectors for dynamic stability of the rotor. 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 different radial lengths as shown. There is. Rib member 2
6 is generally perpendicular to the dispensing surface of plate 22 and extends axially therefrom. individual sectors 24
The ribs 26 have mutually different groove angles formed with the adjacent sides, and the above groove angle is
It should be noted that the depth of the catalytic converters 16 as well as the depth determine the total volume of catalyst that can be dumped into each ring on the surface of the bed 16. 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 volume of the sector 24 will be proportional to the circumferential area of the 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 plate 22 and the individual sectors 24, such as a drive shaft attached by a hub 34 and a key or drive pin 36. 3
2 and a feed tube 28 having an axis 30 substantially coaxial with the feed tube 28.

As illustrated in FIG. 1, the distribution apparatus of the present invention can be used with conventional catalyst orientation and packing apparatus. As shown,
The hopper 38 is loaded with catalyst and gravity feeds the catalyst through the feed tube 40 to the lower feed hopper 4.
2. The hopper 42 maintains a constant head of catalyst above the distribution disk 20 and is preferably mounted over a passageway 44 in the upper grid 18 or on an upper flange 46 of the vessel 10, for example by an arm pivotally mounted. 49 is preferred. The rotating disk 20 is then connected to the shaft 32
and rotor 20 at the desired speed, it can be driven by a local air motor mounted on the lower hopper 42, or by an electric motor 48. Motor 48 is driven by an air hose or electrical cable 50.
Otherwise, the drive shaft 3 extends above the flange 46 to an external mater (not shown).
It may be rotated by 2.

A particular problem in distributing catalyst in large diameter vessels is equalizing the distribution of catalyst near the center of the vessel. It is extremely difficult to lay the catalyst evenly over the entire diameter of the vessel, for example from 2.44 m to 4.57 m, including the central part.
Simply dumping the catalyst through the center of the distribution plate and rolling the catalyst outward from the center pile does not give satisfactory results. According to this preferred embodiment of the invention, this problem is solved by using a number of rectangular tubes or channels 52, 54, 56 and 58, each having a different radial length from each other. As can be clearly seen in FIG.
0 to provide an additional annular catalyst distribution ring. The plate 60 has a large number of threaded rods 64 and nuts 66.
The plate 6 is supported below the collar 62 by
0 can be appropriately spaced with respect to the flange 68 of the collar 62. board 60
radial rod 70 itself carried on the top surface
The catalyst acts as a further distributor. A suitable inlet 72 spaced radially from the axis of rotation of plate 60 controls the amount of catalyst flowing to the innermost ring.

Although not shown in detail, the feed tube 4
0 is proportional to the amount of catalyst flowing in an annular manner into the plurality of sectors 24 as compared to the amount of catalyst flowing in a cylindrical manner over the upper and inner edge 87 of the disk 86. It will be appreciated that the frusto-conical disc 86 is adjustably positioned relative to the conical surface. Therefore, the truncated conical part 8
A chamber 88 formed by 6 and plate 22 serves to distribute the catalyst between tubes 52, 54, 56 and 58 and plate 60. Similarly, as mentioned above, 6
0 and the collar 68 with the help of a rod 70;
The overall flow of catalyst from the edge of plate 60 and through inlet 72 is controlled.

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. tube 52,
Flow or distributor plate 60 to 54, 56 and 58
The catalyst flowing to the 4
It passes through two circular openings 90.

By forming tubes 52, 54, 56 and 58 of differing radial lengths, each shorter than any radial passage in the sector 24, the inner diameter ring or annular portion of the catalyst is shaped like a sector. It is simultaneously jammed while being thrown by the body 24 onto the floor or into the outer part of the container. At the same time, the catalyst passing through the openings 90 is selectively transversely disposed in the innermost portion of this bed by controlling the spacing of the plates 60 from the collar 68, the radial positioning of the rods 70, and the size of the inlets 72. be done. Therefore, in this embodiment, 10 tubes 52, 54, 56 and 58 are placed horizontally by the arcuate fan-shaped body 24, 4 tubes are horizontally placed by the plate 60, and 2 tubes are horizontally placed by the plate 60. It will be appreciated that a single rotor allows distribution of catalyst into multiple zones forming a total of 16 separate rings.

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

A single catalyst distribution disk or rotor contains a number of flow passages, each passage forming a concentric annular ring of small but approximately equal width across the entire circumferential area of the vessel 10. Since it is arranged horizontally, the rotor is preferably 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 transposition of the floor throughout its depth,
The density of the total catalyst volume that can be charged into individual beds or over the entire vessel will be increased. In practice, compared to prior art COP charging methods using varying speeds of a rotatable disk, the total weight of catalyst that can be charged into a known volume of the vessel Na, approx.
A 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. Allows either increased hydrocarbon conversion at a constant feed rate in a volumetric vessel. Both of these conditions are highly desirable for processing hydrocarbon feeds for catalytic conversion and represent significant savings in 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 apparatus are also applicable to charging spherical or heret-shaped catalysts or other particulate materials, such as grains in silos. Other contact materials in the form of particulates, such as sulfur absorbers and ion exchange materials, are also often loaded into large diameter vessels. The present invention is particularly useful in such installations to ensure high density throughout the bed of solid particulates within large diameter vessels.

From the above description, various modifications and changes 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 horizontally to form one of several beds within the vessel. A diagram illustrating the method of the invention using a single rotor distributor; FIG. 2 is a plan view taken in the direction of arrow 2-2 of FIG. FIG. 3 is a plan view of the first catalyst distributor rotor shown in FIG. FIG.
The figure is a cross-sectional elevational view of the rotor of Figure 3 taken along line 4--4 and viewed in the direction of the arrow, directing the flow from the hopper feed tube to the upper distributor plate and the lower distribution carried by the rotor. Figure 5 is a diagram illustrating the cooperation of the conical portion of the rotor to divide it into channels; A plan view in partial section illustrating the distribution of catalyst into multiple tubes and distribution holes that are particularly useful for filling the inner annular ring of large diameter vessels; FIG. 7 is a plan view of the lower distribution structure taken along the line and in the direction of the arrow, particularly showing the distribution by the lower plate for simultaneous packing of the innermost part of the bed of catalyst; FIG. FIG. 6 is a structural perspective view showing each part of the entire rotor structure shown in the figures up to FIG. 6 arranged in sequence; 10... large diameter catalytic reactor vessel; 12... catalyst charging device; 14... concentric ring; 16... bed;
18... support structure or screen; 20... distribution rotor member; 22... plate; 24... sector;
26...Rib; 28...Feeding tube; 30...
Axis line; 32...axis; 34...hub; 36...drive pin; 38...hopper; 40...supply tube; 42...feeding hopper; 44...manway;
46... Upper flange; 48... Motor; 5
0...Electric cable; 52, 54, 56 and 5
8... Channel; 60... Plate; 62... Lower collar; 64... Threaded stud; 6
6... Nut; 68... Flange; 70... Radial rod; 72... Inlet; 76... Orifice;
84...square aperture; 86...truncated conical disc;
87...inner edge; 88...chamber; 90...opening.

Claims (1)

Claims: 1. A method of charging particles of catalyst into a vessel of large diameter at a substantially uniform density over the entire cross-sectional area of the bed within said vessel, comprising: delivering catalyst particles on a single disk rotating about a concentric axis; each sector is formed by adjacent sides of the sector and a radial length proportional to the area of the corresponding ring of a number of concentric rings of catalyst particles arranged on the bed; radially distributing the delivered catalyst particles into a plurality of arcuate sectors having a bevel angle of about 100 m, and wherein the arcuate sectors on the disk have mutually different radii; and each of the plurality of radial and arcuate channels transverses the plurality of concentric annular rings to cover a cross-sectional area of the surface of the bed with a uniform depth of particles of the catalyst. uniformly rotating said disc so that 2. In the method described in claim 1,
A method characterized in that the fed catalyst particles are simultaneously directed into a number of flow channels carried by the rotating disk, each having a radial length shorter than the arcuate sector. 3. a catalyst loading device for uniformly distributing particles of catalyst radially from a feed hopper over one side of a large diameter reactor, the device being positioned immediately above the catalyst distributor disk;
a hopper apparatus including a feed tube apparatus substantially coaxial therewith and supportable by the reactor vessel for supplying particles of catalyst to the distribution surface; a hopper apparatus rotatable within the reactor vessel; the disk adapted to be supported above the floor of the reactor; a drive extending substantially coaxially with the axis of the hopper feed tube for discharging catalyst to the disk; and a drive shaft. a device for rotatably supporting the disk perpendicular to the device; and a device for dividing the distribution surface of the disk into a number of arcuate sectors; Each sector has a common apex at the center of the disk member, and each sector has a different radius than adjacent sectors, and each sector has an axial distance from the dispensing surface. one radial rib member between each of said sectors extending in length, and each sector being proportional to the area of an annular ring formed by catalyst particles on the surface of the bed of said reactor vessel. A catalyst charging device characterized by having a included angle. 4. A catalyst charging device according to claim 3, comprising diametrically opposed sectors, each sector having substantially the same radius and included angle. . 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 surface having a large base portion having a radius smaller than the radius of any of the sectors, the radius of the small base portion being smaller than the radius of the feed tube device; A catalyst loading 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. 6. Catalyst charging device according to claim 5, wherein the radial extent of the minor base of the frustoconical surface and the enclosed volume of the disc form a compartment for the distribution of catalyst. and said disc includes a number of channel members, each of which has a different radius from said sector formed below said distribution surface and is rotatable therewith, and covers a number of other annular rings. A catalyst loading device having a feed device formed from the enclosed volume to the plurality of channel members for supplying catalyst to the bed containing the catalyst. 7. A method in which the catalyst particles are charged into a large diameter vessel at a substantially uniform high density across the bed in said vessel, so that the catalyst particles descend by gravity in a substantially cylindrical form. first dividing into an annular cylinder formed by an outer portion of the cylinder and an inner cylinder of small diameter; a single cylinder rotating about an axis substantially concentric with said cylinder; deflecting said annular column onto a disk of said annular column; and transferring particles from said annular column to a volume proportional to the area of an annular ring, each formed by catalyst particles disposed on the floor of said vessel. a plurality of arcuate sectors on the single rotating disc having a volume defined by the radial length of the arcuate sector and adjacent sides of the disc-shaped sector; radially dividing the inner cylindrical body into a plurality of arcuate sectors, each adjacent arcuate sector having a different radius; divided into a plurality of substantially vertical arcuate separation channels, said plurality of channels having mutually different radial lengths and rotatable with said single disk; is shorter than the radius of any one of the arcuate sectors formed by the disc; and each of the plurality of radial and arcuate channels crosses the entire diameter of the container. Said disk is aligned so as to transverse a number of concentric annular rings of different diameters to substantially cover the surface cross-sectional area of said vessel with a bed of catalyst having varying depths and substantially the same average density. A method consisting of rotating in a similar manner.