CN85108813A - Uniformly loading particulate material is become the method and apparatus of cylindrical layer - Google Patents
Uniformly loading particulate material is become the method and apparatus of cylindrical layer Download PDFInfo
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- CN85108813A CN85108813A CN85108813.9A CN85108813A CN85108813A CN 85108813 A CN85108813 A CN 85108813A CN 85108813 A CN85108813 A CN 85108813A CN 85108813 A CN85108813 A CN 85108813A
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- 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
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- 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
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- 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
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
This specification sheets discloses with distribute simultaneously on whole catalytic bed a kind of method of catalyst granules of single rotor.Make catalytic bed have even high density by forming a plurality of catalyst concentric rings.This effect is not leaned on by changing rotating speed catalyst is obtained from a plurality of sectors that hopper imports on the disk.Each sector preferably has a volume that is proportional to an annulus area in the catalytic bed.This volume is formed by the radical length and the angle of sector.Be divided into outer annulated column and interior cylinder according to the long-pending cylindrical flow of container section with catalyst.This relies on, inwardly the frustum of a cone is stretched into the material pipe from the cloth charge level finishes.Be provided with the different runner by the disk rotation of a plurality of radical lengths, each flow channel length is all short than the radius of sector.
Description
The present invention relates to particulate material evenly pack into a cylindrical shape bed or container method and implement the equipment of filling.Refer more particularly to following method; by catalyst granules or similar material being evenly distributed to " catalyst directional loading " (cop) method of loading catalytic bed in the large diameter cylinder shape container; promptly on the whole area of a circle of catalytic bed simultaneously with under the catalyst stream, and become a plurality of concentric rings that catalyst granules forms.Main purpose of the present invention is to guarantee: the catalyst with column extrusion material form and so on of high loll can be with very high catalyst/container volume than loading into catalytic bed equably.
Specific purpose of the present invention is to improve the loading density of the particle (comprising round particle) with high loll, so that this catalytic bed can form simultaneously by a collection of concentric ring that is distributed on the whole bottom surface of container.Many the rings of catalyst granules and so on are to form by single rotating disk of even rotation or rotor, and this kind disk will be split into the different radially sector of many radiuses from the catalyst that last surface current material pipe gets off.The outgoing speed that the catalyst granules of each sector on the disk distribution surface is synthetic has formed a plurality of different radially casts in catalytic bed or container.Because all parts on the disk rotate with same speed, the concentric ring of catalyst promptly is thrown into container, makes it to settle into simultaneously adjacent a collection of annulus.These annulus have the satisfactory radial width that is rather narrow, but outside from the axis of container, radial distance but increases gradually, have so just formed a plurality of concentric rings that cover whole catalytic bed equably.
Catalytic reaction cell with one or more stationary catalyst bed generally uses the catalyst distributing device to load at present.This technology is referred to as " catalyst directional loading " (often being referred to as the cop filling), is specially adapted to make the penetrablility and the global density uniformization thereof of catalyst bed.In current catalytic treatment technology, catalyst granules is generally by extrusion process production, and the round bar shape that particle cut-off footpath is 1/16 inch to 1/4 inch then, is cut into rod 1/4 inch to 1/2 inch long section.This extrusion generally is to be made of aluminium oxide, siallite, synthetic or natural zeolite material, and it is cheap more than the production spheric catalyst to produce such extrusion.But this class extrusion has very high loll, and promptly free static bing is in the angle of stable state under this angle.Therefore, it is evenly distributed in a large diameter cylinder and describes that in the device be very difficult.Also since such particle at different size, and make and the reactor of packing in can not ftracture again and broken, if only depend on the center-point filling catalytic bed of gravity in the container, " layering " or separating phenomenon will appear.
Adopt the main purpose of cop filling method to be to reduce void space as far as possible, thereby, part " overheated " phenomenon that produces in hydro-carbon and the catalyst exothermal reaction can be reduced by this.In addition, owing to increased the loading density of particulate matter material and catalyst granules, also just improved the distribution of reactant streams in container.And, when having liquid stream to be subjected to fluid power from wherein flowing through aborning, reactor does the time spent, and will improve the density of catalytic bed and limited this layer sinking.In general, in existing container, the quantity of catalyst can increase per centum by this.Otherwise in new container, the container volume required to the catalyst of same quantity then can reduce per centum.
General and opinion, known catalyst directional loading equipment comprise that one has the cloth disk of same diameter and at a plurality of radial vanes or the fin spare at rotating disk top.Usually, distributing device or be conical part or for the plane plectane.But, because the cast and the disk speed of catalyst are directly proportional, for the catalyst that distributes on the whole cross section of Catalytic Layer, the speed of distributing device must be different.When disk is got blade-carrying plane circular plate type, be provided with some holes onboard, make a part of catalyst granules directly drop to the reaction vessel middle part by tumbler.
No. 3804273 patents of the U.S. of You Er (Uhl) are the equipment at the radially distributing device filling catalytic body that has single conical surface.Here be by increasing and decreasing the speed of rotating disk with catalyst distribution to the unique method in the whole bed.
No. 3972686 patents of the U.S. of Johnson people such as (johnson) disclose a kind of plane disc that has blade and a plurality of groove or hole, and a part of catalyst can drop to the middle part of bed by the hole, and remaining catalyst is thrown to container edge.This device also needs to come loading catalyst by the speed that changes rotating disk, makes it can cover the whole surface of catalytic bed.
The peculiar defective of above-mentioned both cryopreservation devices, so at the heap that speed is circular or annular with the catalyst impelling with, so just often might make bigger particle be rolled into the heap end and outside the catalyst granules stratification that drops on the heap, smaller particles then stops on the heap.By changing the rotating speed of disk, can partly overcome above-mentioned difficulties to a certain extent, but because the filling rate is directly proportional with this speed, the speed of the disk that slows down can increase the loading lag of reaction bed again greatly.On the other hand, the speed of disk is too high can cause catalyst on the disk to fly out rapidly again and not have enough residence times to control the distance of radially dishing out.And, because dust abrim all usually in the catalytic bed, make the operator in fact the impassabitity rammer see catalytic bed clearly, be very difficult so obtain required radially cast by control rate.For this reason, must determine a level that may distribute by the number that is loaded into cylindricality catalyst on certain bed surface.Such process is very time taking, and does not have the catalytic bed of making and can evenly fill necessary precision.
In fact, common way is to be loaded at the outer rim place of catalytic bed to surpass required height, for example above 6 to 12 inches, the height of bed surface in the middle of increasing intermittently then, make it surpass a times of peripheral edge portion height, filling makes progress along reaction vessel so repeatedly, spreads all over the entire reaction container along with the degree of depth increase of one or more catalytic bed.Be provided with several discrete reaction beds in container, and each must be loaded by separately supporting " dividing plate " supporting and following bed all by the path that the center is supported on the upper strata, under these circumstances, problem is just even more serious.With the naked eye check difficulty more this moment.
Lu Tedi people's such as (Lontaty) No. 4306829 US Patent disclose and a kind ofly are used for the catalyst reactor particle or are used for the distributing device that silo has grain in reserve.Distributing device comprises by clamp some flexible bands along axle drive shaft length direction rotating support.These belts can be made of Reinforced Rubber, their length or equate, perhaps deviate from the feed hopper exit after length increase gradually.Relevant embodiment shows that this system can satisfy the reaction vessel of a kind of diameter of filling 60 centimetres (about 2 feet).It seems that the effective length of the belt during these rotate is to change with the effect between the catalyst granules of drive shaft speed and they and whereabouts on the diametric(al).Be limited to the quite little reactor of those diameters when for above-mentioned reasons, adopting above-mentioned this class device to come container effectively loaded.
Transfer the assignee of the present invention's, No. 4433707 US Patent of Fa Enhamu (Fannham), disclose a kind of by adopting a plurality of disks that on an axle, rotate different-diameter with same speed, and from the center of container to outer wall on each level the rectangular distribution catalyst granules with the method and apparatus of even filling reaction vessel.Here desiredly be, three such conical disks should be arranged, their maximum gauge part is the delivery pipe of close feed hopper.The top disk has a centre hole so that catalyst transport arrives each lower disk.Because the diameter difference of these disks, each disk are all removed catalyst when axle drive shaft rotates with constant speed on the circles different in container.Above container top or several layers of catalytic bed, be provided with under the situation of suitable head room clearance, a kind ofly like this install complete energy and satisfy catalyst packed into and have container than minor diameter and dark catalytic bed.But when not changing rotating speed, this method only limits to the several annulus of spreading simultaneously.
In No. 2703329 Germany patents that announce in March, 1978, a plurality of axially spaced disks are rotated in another kind of employing on an axle drive shaft granule materials filling device is disclosed.Identical in its mode of operation and the above-mentioned Fa Enhamu patent.
In implementing method of the present invention, be that a catalyst distributing device is arranged at a suitable At The Height in bed top to be loaded. Then, catalyst is fed distributing device from the hopper of being furnished with feed pipe, the residing position of feed pipe makes roughly that cylindrical catalyst falls into single rotor or disc.
Then, catalyst granules is distributed in the gamut of catalytic bed by single disk, realizes roughly uniform densification by forming the concentric annulus of a plurality of and container or catalytic bed.This operation can use a plurality of fan-shaped parts with different radical lengths that cylinder shape catalyst is imported on the single rotary disk to realize under the condition that does not change disk speed.Best, the volume of each sector all therewith in the container cross section annulus area of catalytic bed be directly proportional.This required volume is to be formed by the angle that the radical length of this sector and it are occupied on disk.In a kind of preferred form of this kind disk, each adjacent sector all has different volumes to form the catalyst annulus that roughly waits width on catalytic bed.
Among the whole embodiment according to container, this can realize by a frustum cone piece that inwardly stretches into feed pipe from disk master cloth surface.The maximum sole of cone piece and disk have formed an auxiliaring bucket or reservoir volume, and it has different radical lengths and roughly provide catalyst with the rectangular a plurality of arc runners that separate of stock column to another group.Desired is that each this runner is all short than the radius that is made of any sector above-mentioned disk.
By rotary disk equably, each in these many arc runners is all spread down the donut with different-diameter.These rings have covered the surface of Catalytic Layer supporting member in the container basically with catalyst.Because each ring all forms simultaneously, on each horizontal surface, for the cross section of entire container or catalytic bed, the degree of depth of catalyst all is consistent, and the catalyst bed that makes formation has higher average density under the condition of same containers or identical catalytic bed volume.
Other purposes of the present invention and preceence by the preferred embodiment of the invention and with reference to the accompanying drawing that constitutes a specification sheets part, for being familiar with the technical personnel of this technology, will be conspicuous.
In the accompanying drawings:
Fig. 1 is the front elevation by major diameter hydrocarbon reaction container part bench section, shows that bright the present invention adopts a rotation distributing device to spread following a plurality of catalyst concentric rings to form the method for one of several catalytic beds therein in container;
Fig. 2 is the cross sectional drawing along arrow 2-2 direction intercepting among Fig. 1, shows the concentric ring of the catalyst granules that is become by a rotation distributing device impelling of the present invention;
Fig. 3 is the planar view of catalyst master distributing device rotor shown in Figure 1, has shown to have to shed the required radical length of the identical catalyst granules concentric ring of a plurality of degree of depth and the arc preferred structure to width;
The cross sectional drawing that Fig. 4 intercepts along arrow 4-4 direction for the rotor by Fig. 3, and represented to be assigned to the rotor tapering part of top drapery panel and the conspiracy relation between the below distributing trough on the rotor from the materials flow of hopper conveying pipeline;
The planar view of Fig. 5 for being looked along arrow 5-5 direction among Fig. 4 analysed and observe the situation that catalyst is assigned to a plurality of pipes and dispensing orifice that shows by part is made in rotor structure bottom, and this structure is specially adapted to load the interior annulus of major diameter container;
Fig. 6 be among Fig. 4 along the planar view of the lower part distribution structure of arrow 6-6 direction intercepting, shown the further cloth that loads catalytic bed penetrale by lower plate simultaneously especially;
Fig. 7 is the exploded perspective view of Fig. 1 to whole wheel word shown in Figure 6.
Fig. 1 has shown and has used the inventive method is carried out the catalyst directional loading in a major diameter catalytic reaction cell 10 process that this method taked the preferred form of catalyst loading equipment 12 to shed the concentric ring of catalyst granules.As shown in Figure 2, above-mentioned have same widths or etc. a plurality of concentric rings whole bottom surface of covering containers 10 simultaneously of length radially, be able in gamut with catalyst even depth, equidensity ground filling catalytic bed.This method be have a high loll at filling catalyst as columniform catalyst extruding grain, this particle is falling behind quite stable down.Especially as shown in Figure 1, container 103 comprises a plurality of catalytic beds 16, and each bed all is formed on catalyst support or the plate 18.As shown in the figure, these many supporting structures be arranged so that mutually continuous each catalytic bed 16 of bonded assembly all one be positioned on another and place.In order to guarantee that each catalytic bed 16 all has uniform density in its whole height or depth range, the axis of catalyst distribution device should be shorter, so that be lower than the catalytic bed top of upper support structure 18 or the top of container 10 is filled in catalytic bed 16 tops as far as possible, and only stay very little space or do not stay head room, this point also is very important.For this reason, the catalyst cloth tumbler 20 that the present invention constitutes comprises a main cloth surface, and this surface is made of the plate 22 that is divided into a plurality of sectors 24, and these sectors 24 have common summit in the rotating shaft 30 of disc 22.But as shown in the figure, the dynamic stability of rotating for obtaining, it is all different that each sector is adjacent the two radius of part.As we can see from the figure, need establish the dynamical equilibrium of parts to keep rotating of two homalographics on the radially relative direction.
In Fig. 3 and specific embodiments shown in Figure 4, radial fins 26 has constituted parts 24 and has had different radical lengths.Fin 26 axially stretches the cloth surface of leaving plate 22 and is approximately perpendicular to this surface.Will should be mentioned that especially that also each sector 24 all has different angles, the degree of depth of this angle and fin 26 has determined to be thrown into the catalyst cumulative volume of each ring on catalytic bed 16 surfaces jointly.Certainly, should be understood that the cumulative volume of each sector is directly proportional with the area of the corresponding catalyst rings 14 of throwing catalytic bed 16 tops.In general, the volume of sector 24 should be proportional to the area of annulus and each ring width with respect to the adjacent ring that is formed by other fan-shaped parts 24.
As showing especially among Fig. 4, catalyst is transported on the cloth surface and each sector 24 that is made of plate 22 by feed pipe 28, and the axle 30 of pipe 28 is roughly coaxial with transmission shaft 32, and drapery panel 22 is contained on the axle 32 by sleeve 34 and key or trundle 36 and so on.
As shown in Figure 1, cloth system of the present invention can adopt existing catalyst directional loading equipment.By 3 seeing that catalyst loaded onto by hopper 38 and by gravity drops to down in the feed hopper 42 by delivery pipe 40 among the figure.Hopper 42 is kept the catalyst drop of constant above cloth disk 20, and preferably by for example supporting at the pivoted arm on the passage 44 that forms on the top grid 18 or on the upper flange 46 of container 10 49.Then, can come rotary disk 20 by local air pushing mechanism or electrical motor 48, this motor mounting is on hopper 42, with required speed drive axle 32 and disk 20.Can come energy supply with driving motor or air push mechanism by air duct or cable 50.On the other hand, axle 32 can be connected the flange 46 on the external motor (not shown) via himself upwards stretching and rotate.In the major diameter container during distribution catalyst, near this container center, obtain uniform catalyst distribution and be difficulty especially.The even spreading to 8 of catalyst is comprised on the whole bottom surface of core be considerable to the container of 15 ft diams.Only stack catalyst and it can not be met the demands to outflow fully from center stack by the drapery panel center.According to the preferred embodiment of the invention, this problem is by adopting a plurality of rectangular tube or grooves 52,54,56 and 58 with different radical lengths to solve.Can be clear that by the utmost point that in Fig. 5 the plate 60 of these grooves on being bearing in case in 62 provides other ring-type catalyst cloth ring.Plate 60 is bearing in sleeve pipe 62 belows by a plurality of bolts 64 and nut 66, and screw bolt and nut guarantees that plate 60 has suitable gap with respect to the flange 68 of sleeve pipe 62.Plate 60 self has also played the effect of catalyst distributing device by the effect that is installed in the radial bars 70 on its face.The suitable mouth 76 radially spaced apart with the rotating shaft of plate 60 controlled the catalyst amounts that allows to flow to down innermost ring.
Although there is not detailed expression, but should understand to such an extent that delivery pipe 40 is adjustable with respect to the position of the conical surface of frustum circular cone dish 86, make and suitably to divide to be equipped with the quantity that annular flow is gone into the catalyst of a plurality of parts 24 with respect to dropping to the going up of disk 86, interior along the catalyst amounts on 87 with cylindrical.The chamber 88 that forms by frustum cone piece 86 and plate 22 with catalyst be assigned to pipe 52,54,56 and 58 and plate 60 in.Equally, the hole between plate 60 and the sleeve pipe 68 control slave plate 60 edges cooperate through bar 70 and flow down and by the dirty catalyst total amount in hole 76.From Fig. 5, can know and see, flow in four rectangular tubes 52,54,56 and 58 by the square hole on the plate 22 84 from delivery pipe 40 and at the mobile catalyst of interior column part, the catalyst that flows on the plate 60 then flows through four circular ports 90 that are formed on equally on the plate 22.
Has all short pipe 52,54,56 and 58 of different radical lengths and each by formation than the radial flow path of arbitrary sector 24, when catalyst was thrown outer part in catalytic bed or the container by sector 24, the annulus part by the lining in the catalytic bed was filled simultaneously.Simultaneously, by gap and the radial position of bar 70 and the size in hole 76 of control desk 60, can make the catalyst that flows through hole 90 drop to the innermost part of catalytic bed selectively to sleeve pipe 68.Can see that in the present embodiment single disk just may become catalyst distribution a plurality of endless belt, has formed 16 rings that separate in the present embodiment, wherein spreads into 10 by sector 24, spread into 4 by pipe 52,54,56 and 58, and spread into 2 by plate 60.
In this structure, sleeve pipe 62 and plate 60 are detachably connected on the drapery panel 22 by screw 80.Manage 52,54,56 and 58 permanent components that constitute on the plate 22.
On the other hand, whole wheel word can be made one, or makes miscellaneous part permanently or be detachably connected on the drapery panel 22 and form.In case of necessity, plate 22 can be got conical rather than flat, and this is conspicuous for the technical personnel of knowing this technology.
Because single catalyst cloth disk or rotor comprise a plurality of runners, each runner be designed to spread down limit but concentric ring with equal approximately radial width, and the whole round bottom face of covering container 10, like this, the speed of rotor is preferably constant.Speed is adjusted to the such steady state value that is determined by the Catalytic Layer diameter, and the entire cross section that makes the rotation physical efficiency that catalyst is thrown container is amassed.In case speed setting just remains on this speed roughly unmodified state, finish each the filling process at 16 tops from support plate 18 to catalytic bed.This in the dark scope of whole bed the method for rectangular distribution catalyst, improved the density of the catalyst cumulative volume that can put into a catalytic bed or entire container.In real work, have found that the existing COP filling method variable with adopting rotary speed compares, and increased about 10% by the determined density of the total catalyst weight of the container that can put into known volume.Because the hydro-carbon by container infeeds the cumulative volume that the number turnover of material depends on catalyst, like this, the present invention is under the identical situation of vessel volume, and it is higher to make hydro-carbon by reactor infeed rate when producing product of the same race; Or under constant feed rate, can improve the number turnover of hydro-carbon.More than two kinds of situations in hydro-carbon being carried out the processing that catalysis changes, be in demand and can reduce disposal cost greatly.
The above embodiment of the present invention is at the catalyst granules that is squeezed into of filling on the entire cross section of a major diameter reaction vessel.But this method and apparatus also is applicable to other particulate materials of filling, as spheric catalyst or in silo loading food.Other are got granular contact material such as sulfur absorbing agent and ion exchange material and also often are seated in the major diameter container.The present invention is specially adapted to and need guarantees highdensity situation on the whole granular bed in the major diameter container.
From the above description as can be known, equipment and this apparatus operation method various change shape and variation, all can carry out knowing the person skilled in art, all are at the various remodeling of claim scope of the present invention and change and all be included within this claim.
Claims (11)
1, in a major diameter container with the uniform method of loading catalyst particle on the entire cross section of density catalytic bed in container roughly, it is characterized in that: the cylindrical flow of a catalyst is flow to around roughly flowing on the single disk of coaxial axle rotation with this cylinder, enter the sector that a plurality of rotating shafts at above-mentioned single rotary disk have common vertex from the radially divided particle of this cylindricality grain stream, each sector has an angle and a radical length that is directly proportional with the annulus area of one of a plurality of concentric rings that cover the whole sectional area of catalytic bed, the fan-shaped part of disk has different radiuses, the uniform rotation disk makes each radially spread next donut with the arc runner, gets so that the surface of inhomogeneity catalyst pellets subcovering catalytic bed entire cross section is all arranged on each layer depth.
2, according to the process of claim 1 wherein, the core that the catalyst cylinder flows is aimed at a plurality of chute mouths on the rotary disk simultaneously, and each chute all has the radical length that is shorter than sector.
3, radially in the catalyst loading equipment of rectangular distribution catalyst granules, comprising to a major diameter reactor from a feed hopper:
By reactor supporting, provide the magazine attachment of catalyst granules to catalyst cloth surface, it is positioned at directly over the catalyst cloth disk and is roughly coaxial with it;
Above-mentioned disk rotates in reaction vessel and is suitable for being bearing in above the responding layer, and actuating device is stretched with the roughly coaxial edge of feeder sleeve axis of adorning catalyst to disk, and the device of rotating support disk is then vertical with drive shaft device.
Said apparatus is characterised in that: the cloth surface of device for disc is divided into a plurality of sectors, each sector has common summit at the disc center, the two radius of each sector and adjacent sector is all different, each discrete distribution device comprises that one is in from cloth surface axially along the radial fins between per two sectors of stretching, and each sector has an angle that is proportional to catalytic bed surface one annulus area.
4, according to the catalyst loading equipment of claim 3, wherein, it is basic identical with angle and at radially relative with it parts that each sector all has a radius.
5, according to the catalyst loading equipment of claim 3, wherein, annulus cloth surface also comprise one from disk upwards and inwardly along the frustum conical surface of stretching, the big end radius of this circular conical surface is less than the radius of arbitrary sector, its small end radius is then less than the radius of conveying pipeline device;
Adjust the device of the axial distance between the discharge gate peace frusto-conical surface of conveying pipeline device, be used for controling flow to the catalyst flow on the catalyst cloth surface of disk.
6, according to the catalyst loading equipment of claim 5, wherein, the small end scope of frustum conical surface and the volume that disk surrounds have constituted the chamber of a distribution catalyst, this disk is furnished with a plurality of channels, each channel all has the radius different with sector, channel forms and therewith rotates in the cloth lower face, also have the feeding device that is formed at from the above-mentioned volume that surrounds to a plurality of channels with catalyst transport to the bed that forms at more than one annulus bed.
7, in a major diameter container, with the uniform method of high density loading catalyst on the whole Catalytic Layer in container basically, it is characterized in that: will lean on earlier action of gravity with roughly cylindrical flow down the catalyst granules that falls be divided into annulated column stream and one that the outer ring by cylinder stream forms the interior cylinder of minor diameter flow, then this annulated column conductance is guided to around roughly flowing on the single rotary disk of coaxial axle rotation with cylinder, radially the particle of annulated column stream is assigned on a plurality of quadrntnts on the single rotary disk again, each sector has one to be proportional to the volume that container cross section is amassed an interior annulus area, this volume is formed by the angular breadth of this arcuate member on the radical length of sector and the disk, and adjacent sector all has different radiuses.
Interior cylinder stream is divided into the runner that a plurality of roughly vertical with this post stream arcs separate, and these many runners have different radical lengths and rotate with single disk.Each runner is all short than the radius of the arbitrary sector that is formed by disk, the uniform rotation disk, make the different donut of a plurality of diameters radially and under a plurality of runner arc spreads, basically the areal cross-section that covers container is long-pending, makes catalytic bed degree of depth unanimity simultaneously and have uniform density on the whole sectional area of container.
8, from feed hopper, catalyst granules radially is evenly distributed on catalyst loading equipment on the major diameter responding layer, it is characterized in that, this equipment has the disc that rotates and be suitable for being bearing in this place above the responding layer in reaction vessel, this disc has a cloth surface that comprises a plurality of sectors, each sector has one in the common vertex at disc center and have the radius different with at least one sector, and have from the cloth surface axially along the radial fins part between the per two adjacent sectors of stretching.
Magazine attachment is by reaction vessel supporting and coaxial and be positioned on the cloth surface of the conveying pipeline device directly over the disk catalyst granules is provided with disk for being furnished with roughly;
Drive shaft device is roughly stretched with the coaxial edge of hopper pipe discharge gate axis, and the device on rotating support disk cloth surface is vertical with drive shaft device.
9, according to the catalyst loading equipment of claim 8, wherein, each sector all have a same radius with its radially relative sector.
10, according to the catalyst loading equipment of claim 8, wherein, the cloth surface of disk has from the frustum conical surface that disk makes progress, stretch on inside edge, this conical surface has one and holds greatly, its radius less than its small end radius of radius of arbitrary sector then less than the radius of conveying pipeline device, adjust the device of the axial distance between the conveying pipeline discharge gate peace frusto-conical surface in addition in addition, be used for controlling through flowing to the flow of the catalyst on cloth surface therebetween.
11, according to the catalyst loading equipment of claim 10, wherein, disc is furnished with a plurality of formation groove thereunder, and each groove all has different radical lengths, and the small end of frustum circular cone has a passage, supplies with catalyst for above-mentioned groove through this passage.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US67915484A | 1984-12-07 | 1984-12-07 | |
US679,154 | 1984-12-07 |
Publications (2)
Publication Number | Publication Date |
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CN85108813A true CN85108813A (en) | 1986-08-20 |
CN1011762B CN1011762B (en) | 1991-02-27 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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CN85108813A Expired CN1011762B (en) | 1984-12-07 | 1985-12-04 | Method and apparatus for uniformly loading particulate material into cylindrical beds |
Country Status (8)
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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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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 |
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- 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 CN CN85108813A patent/CN1011762B/en not_active Expired
- 1985-12-04 GB GB08529844A patent/GB2168330B/en not_active Expired
- 1985-12-05 EG EG775/85A patent/EG17295A/en active
- 1985-12-05 KR KR1019850009128A patent/KR930002241B1/en not_active IP Right Cessation
- 1985-12-06 JP JP60273607A patent/JPS61141923A/en active Granted
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Also Published As
Publication number | Publication date |
---|---|
KR930002241B1 (en) | 1993-03-27 |
GB8529844D0 (en) | 1986-01-15 |
CA1254720A (en) | 1989-05-30 |
KR860004646A (en) | 1986-07-11 |
CN1011762B (en) | 1991-02-27 |
EG17295A (en) | 1991-08-30 |
GB2168330B (en) | 1988-12-14 |
JPH0472571B2 (en) | 1992-11-18 |
IN166220B (en) | 1990-03-31 |
GB2168330A (en) | 1986-06-18 |
DE3542340A1 (en) | 1986-06-12 |
JPS61141923A (en) | 1986-06-28 |
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