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US20030194360A1 - Multifunctional entry method and device for downward flow tube reactor - Google Patents

Multifunctional entry method and device for downward flow tube reactor Download PDF

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Publication number
US20030194360A1
US20030194360A1 US10/119,037 US11903702A US2003194360A1 US 20030194360 A1 US20030194360 A1 US 20030194360A1 US 11903702 A US11903702 A US 11903702A US 2003194360 A1 US2003194360 A1 US 2003194360A1
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US
United States
Prior art keywords
catalyst
entry
multifunctional
collector
distributor vessel
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US10/119,037
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English (en)
Inventor
Wilson Huziwara
Waldir Martignoni
Mauro Silva
Jose Geraldo Ramos
Aurelio Dubois
Paulo Freire
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Petroleo Brasileiro SA Petrobras
Original Assignee
Petroleo Brasileiro SA Petrobras
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
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Assigned to PETROLEO BRASILEIRO S.A.-PETROBRAS reassignment PETROLEO BRASILEIRO S.A.-PETROBRAS ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MARTIGNONI, WALDIR PEDRO, DUBOIS, AURELIO MEDINO, FREIRE, PAULO SERGIO, HUZIWARA, WILSON KENZO, RAMOS, JOSE GERALDO FURTADO, SILVA, MAURO
Publication of US20030194360A1 publication Critical patent/US20030194360A1/en
Priority to US11/512,216 priority Critical patent/US7531142B2/en
Abandoned legal-status Critical Current

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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
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/70—Spray-mixers, e.g. for mixing intersecting sheets of material
    • B01F25/72—Spray-mixers, e.g. for mixing intersecting sheets of material with nozzles
    • B01F25/721—Spray-mixers, e.g. for mixing intersecting sheets of material with nozzles for spraying a fluid on falling particles or on a liquid curtain
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/065—Feeding reactive fluids
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872—Details of the fluidised bed reactor
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1881—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving downwards while fluidised
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00769—Details of feeding or discharging
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/0084—Stationary elements inside the bed, e.g. baffles

Definitions

  • the present invention relates to the area of petroleum refining.
  • the field of application of the invention is reactors used in fluid catalytic cracking (FCC) processes or other processes which make use of solid particulate catalyst.
  • FCC fluid catalytic cracking
  • the invention relates to a device and to a method for supplying and homogeneously distributing solid particulate catalyst and for intimately mixing it with a reagent fluid, for application in a tube reactor with downward flow (downer).
  • a fluid catalytic cracking (FCC) process aims to convert hydrocarbons with a high boiling point into lighter hydrocarbon fractions, such as gasoline and liquefied petroleum gas (LPG), inter alia.
  • FCC fluid catalytic cracking
  • the reactor used in a FCC process is of the tube type, with upward vertical flow, known in the technical literature as a riser type reactor.
  • a riser type reactor uses a solid catalyst consisting basically of a powder of fine particle size which, normally preheated, is introduced into the reactor.
  • the catalyst Upon entry into the reactor, in its lower portion, the catalyst is preaccelerated with vapour and intimately mixed with a preheated, sprayed hydrocarbon charge. After the so-called mixing region, the resulting mixture of vaporised hydrocarbon and catalyst continues to react, converting, during the upward vertical flow through the tube reactor, heavy hydrocarbon fractions with high boiling points into light hydrocarbon fractions with low boiling points.
  • a downer reactor offers certain technical and financial advantages when compared with the riser reactor, such as:
  • This invention relates to an entry device for downer-type reactors which is designed to allow the occurrence of an intimate and homogeneous mixing of the catalyst, in the form of heated solid particles, with the sprayed hydrocarbon charge, giving rise to rapid vaporisation of the charge.
  • the device enhances maintenance of the homogeneity of the mixture, minimising segregation between the charge and catalyst after the stream of fluid has left the mixing region and during its flow through a downward tube reactor.
  • Means or devices are known for supplying catalysts in fluid catalytic cracking tube reactors.
  • U.S. Pat. No. 4,338,187 discloses a device and a process for intimately mixing a hydrocarbon charge, in vapour or liquid phase, with solid particles of heated catalyst, which occurs in the final portion of one or more entry conduits of one or more mixing chambers.
  • the hydrocarbon charge is injected, forming a certain angle with respect to the direction of flow of the catalyst.
  • the performance of the device depends on the number of mixing chambers, which has to be high so that a good distribution of catalyst and hydrocarbon is obtained throughout the transverse section of a tube reactor. If the number is insufficient, segregation will occur between the streams of hydrocarbon and of catalyst.
  • Another problem with the disclosure of this patent is the need for control of the catalyst volume, which is based on the pressure differential between the catalyst reservoir and the mixing chamber.
  • U.S. Pat. No. 4,919,898 relates to a device for catalytic cracking with heated solid particles, in which a curtain of particles is introduced into a reactor via peripheral apertures and a hydrocarbon charge is introduced into the reactor at an angle through the curtain of solid particles.
  • a curtain of particles is introduced into a reactor via peripheral apertures and a hydrocarbon charge is introduced into the reactor at an angle through the curtain of solid particles.
  • use is made of a single mixing chamber. Vapour or gas is injected, at an angle of 45° below the horizontal, in order to preaccelerate the catalyst.
  • Use is made of a stationary plug, with a spherical format, in order to give a shape to the catalyst curtain, which is supplied via the periphery of the plug.
  • U.S. Pat. No. 5,296,131 discloses a cracking process which is characterised in that it is based on a short contact time.
  • a downward annular curtain of regenerated catalyst, or of heated inert solids is formed over a valve of plug type, in the form of a cone, for controlling the catalyst.
  • the hydrocarbon charge is injected via inlets installed in the conical plug of the control valve and inlets installed in the conical seat of said valve, against the solids curtain.
  • the performance of the device is affected by the geometrical interference of the shaft and of the plug of the valve installed inside the tube reactor, which will lead to segregation of the mixture of the stream of catalyst from the stream of hydrocarbon.
  • U.S. Pat. No. 5,344,554 makes use of a vapour- or gas-injection ring installed below the catalyst-supply point, with the aim of distributing and adjusting the density and velocity of the stream of catalyst within acceptable values prior to the injection of the hydrocarbon charge. Injection takes place through radial inlets forming an angle with the horizontal, which provides the stream with a velocity component in the direction of the flow.
  • the redistribution ring in the form proposed by this patent, does not guarantee satisfactory distribution of catalyst over the entire transverse section of the tube reactor; the use of charge-injection inlets forming an angle with the horizontal and with a component in the direction of the flow, i.e. in the downward vertical direction, does not permit the maintenance of a satisfactory distribution of the catalyst since the greater force component, owing to the inherent weight and to the velocity of the catalyst, is also in this direction.
  • U.S. Pat. No. 5,468,369 makes use of the conditions favourable to mixing of the stream of catalyst with the stream of hydrocarbon, which is characteristic of vertical tube reactors with upward flow (risers) and takes advantage of the characteristic of maintenance, with less segregation, of the satisfactory conditions of mixing of catalyst and hydrocarbon which is offered by vertical reactors with downward flow (downers).
  • U.S. Pat. No. 6,099,720 has a region for mixing of the catalyst with the hydrocarbon charge which is similar to that advocated by Patent U.S. Pat. No. 5,296,131, except that in U.S. Pat. No. 6,099,720, there is no valve shaft installed inside the tube reactor. Therefore, this is not an annular tube reactor, and there are likewise no comments as to the way in which such a valve shaft would be installed.
  • the present invention relates to a device and to the respective method of use, for application in the entry region of a vertical tube reactor with downward flow (downer), the aim being the homogeneous distribution of solid particulate catalyst inside a mixing chamber with a view to its intimate mixing with a reagent fluid in liquid or gaseous phase.
  • a further object of the invention is to maintain the homogeneity of the mixture during its downward travel to the reaction region of a downward vertical tube reactor.
  • a yet further object of the invention is to offer a method for supplying, homogeneously distributing and intimately mixing the catalyst with a sprayed hydrocarbon charge and for maintaining adequate mixing conditions during the flow of the mixture towards the reaction zones of a downer reactor.
  • the present invention provides a device and a method for supplying a downer reactor with catalyst, flowing out from a control valve, which is directed to a collector/distributor vessel whose bottom has uniformly distributed through-holes.
  • Said holes normally allow the passage of a portion of the stream.
  • the portion of the stream of catalyst which does not pass through the holes which depends on the amount of catalyst released by the valve, uniformly overflows via the upper edges of the collector/distributor vessel in the form of an annular curtain which, after passing beyond the lower edge of the collector/distributor vessel, enters the so-called mixing region with an angular component towards the longitudinal axis of the device.
  • Suitable conditions for distribution of catalyst are obtained through combined effects of flow through the perforated plate, of flow in the form of an annular curtain formed by overflowing from the perforated plate, and through the use of a surrounding tube with a diameter which is smaller than that of the associated downer reactor.
  • vapour may be injected by means of injector nozzles or by means of a ring.
  • a further option, for improving the distribution of catalyst is the use of a fluidisation ring, inside the collector/distributor vessel, via which vapour is injected. Both options mentioned above may be used simultaneously.
  • the hydrocarbon charge is injected via a set of inlets.
  • These injection inlets are distributed, preferably uniformly, over the periphery of the mixing region It is possible to use one or more levels of inlets whose angle with respect to the horizontal may vary between ⁇ 30° and +30° in the direction of, or against, the direction of the downward flow of catalyst.
  • the diameter of the device expands slightly up to the diameter of the upper part of the associated tube reactor, with a taper half angle of 0° to 4°, preferably from 2° to 4°, with respect to the vertical so that there is no segregation of the stream of catalyst from the reagent hydrocarbon stream.
  • FIG. 1 shows a diagrammatic longitudinal section through a preferred embodiment of the invention.
  • FIG. 2 shows a diagrammatic longitudinal section through a further preferred embodiment of the invention, in which it is possible to see a fluidisation ring inside the distributor vessel.
  • FIG. 3 shows a diagrammatic longitudinal section through an embodiment of the invention, as constructed for preliminary tests.
  • FIG. 4 shows a diagrammatic transverse section on the line “A-A” shown in FIG. 3, at the level of the cylindrical vessel;
  • FIG. 5 shows a diagrammatic transverse section on the line “B-B” shown in FIG. 3, in the region of the charge-injection inlets.
  • the invention presents an entry device for use in downer-type vertical reactors for catalyst/hydrocarbon-charge ratios preferably in the range from 6 to 8, but the ratio may be below or above this range.
  • a typical application would be, for example, in a unit processing from 5000 to 10000 m 3 /day of gas oil or atmospheric residue (bottom product of the petroleum or crude-oil atmospheric distillation tower).
  • FIGS. 1 to 5 Two preferred embodiments of the invention and the design of one prototype are shown in FIGS. 1 to 5 .
  • FIG. 1 shows a diagrammatic longitudinal section, where the principal internal components can be seen, taken through a preferred embodiment of the invention.
  • This embodiment of the invention consists basically of a predominantly cylindrical surrounding tube 1 , preferably having a small diameter in comparison with the nominal diameter of the reactor to which it will be coupled. Downstream of the coupling, the diameter of the lower portion 10 of the surrounding tube 1 expands slightly up to the diameter of the corresponding section of the reactor. Said surrounding tube 1 , being connected axially and longitudinally to a downward flow tube reactor (downer), together with its internal components, will constitute the upper portion of this reactor.
  • a downward flow tube reactor downer
  • the invention is equipped with means for:
  • the device of the invention has a valve 4 for controlling the supply of catalyst 15 .
  • This valve 4 may be any of the types normally used in riser-type reactors. It may also, for example, be (i) of the plug type or (ii) of the simple displacement slide type, associated with a mechanism for redirecting the catalyst to the centre of the downer-type reactor. Preferably, it may be of the dual displacement slide type, which makes it unnecessary to use the mechanism for redirecting the catalyst to the centre of the downer.
  • a predominantly cylindrical catalyst collector/distributor vessel 2 mounted axially and longitudinally below the control valve 4 , has in its bottom wall 3 preferably circular perforations which are homogeneously distributed with the aim of receiving and distributing the catalyst 15 homogeneously throughout the transverse section of the surrounding tube 1 , in the portion thereof below the collector/distributor vessel 2 .
  • the size of the holes is defined as a function of the catalyst/charge ratio, or rather of the flow rate of catalyst.
  • the sum of the areas of the holes is a percentage of the area of the transverse section of the so-called mixing region 8 , of the device of the invention located below the collector/distributor vessel 2 . This percentage varies from 22% to 55%, preferably from 30% to 40%, of the area of the transverse section of the mixing region 8 .
  • Said holes normally allow the passage of a portion of the stream. That portion of the stream of catalyst 15 which does not pass through the holes, which depends on the amount of catalyst 15 released by the valve 4 per unit of time, uniformly flows over the upper edges of the collector/distributor vessel 2 which act as a weir. Therefore, depending on the supply rate, i.e.
  • the catalyst 15 will accumulate in the collector/distributor vessel 2 and will be able to pass over its upper edge.
  • the catalyst forms a small mound which is preferably symmetrical and, over and above a certain height, overflows and flows via the outer part of the collector/distributor vessel 2 along the annular space between said vessel 2 and the surrounding tube 1 , forming a type of curtain 16 .
  • vapour injectors for example inlets 5 .
  • a further option is the installation, in this region, of a vapour-injection ring having inlets or holes. The injection of vapour via said inlets, or ring, prevents the entry of the charge into the upper portion of the surrounding tube 1 where it would give rise to an undesirable coking of the control valve 4 and of the inner surface of the surrounding tube 1 . It also contributes to a better distribution of the catalyst 15 which accumulates over the collector/distributor vessel 2 .
  • FIG. 2 illustrates a further preferred embodiment, in which vapour is injected by means of a fluidisation ring 11 positioned inside the collector/distributor vessel 2 .
  • This ring 11 is preferably positioned horizontally and at a distance of 20 to 40 cm from the bottom 3 of the collector/distributor vessel 2 .
  • the positioning of the fluidisation ring 11 inside the collector/distributor vessel 2 prevents coke formation at the top of the vessel 2 and induces some degree of fluidisation of the catalyst so as to provide, as a priority, homogenization and a better distribution of the catalyst and also assist the introduction of vapour.
  • the ideal is the simultaneous injection of vapour, both via injection inlets 9 or an injection ring, at the top of the device, below the catalyst entry valve 4 , as shown in FIG. 1, and also by means of a fluidisation ring 11 , inside the collector/distributor vessel 2 , as shown in FIG. 2.
  • Said angle preferably within the range up to 30° with respect to the horizontal, and in the direction of the longitudinal axis of the mixing region 8 , is identical to the angle of repose of the catalyst retained on the horizontally arranged annular screen 7 , on the inner surface of the surrounding tube 1 of the device of the invention, below the collector/distributor vessel 2 .
  • Charge injectors for example inlets 9 , are installed on the walls of the surrounding tube 1 below the annular screen 7 .
  • twelve inlets 9 are distributed over the circumference of one or more cross sections of the surrounding tube 1 .
  • the inlets 9 are mounted in the form of two or more levels, i.e. in two or more cross sections of the surrounding tube 1 , there will preferably have to be an angular offset between corresponding inlets located at adjacent levels. In other words, the inlets would not be mounted vertically aligned with one another.
  • the number of charge-injection inlets 9 depends on the diameter of the downer and on the charge being processed, (e.g. the magnitude and nature of the charge).
  • the inlets 9 should preferably be mounted on two levels, with an angular offset defined between these two sets, in order to optimise the volume of the downer under the influence of the charge injectors.
  • these would be distributed on two levels, each with 6 inlets, spaced at 60° intervals in each level. Between one level and the next, the inlets would be offset by 30°.
  • the inlets 9 may be inclined with angles of between ⁇ 30° and +30° with respect to the horizontal.
  • the inlets 9 are mounted with an inclination of 0° to +30°, or with a slight negative angle, injecting sprayed charge with a movement component in the direction counter to the stream of catalyst. The injection of charge under such conditions contributes to the production of an adequate mixture.
  • the region in the vicinity of the charge-injection inlets 9 and between those inlets 9 and the annular screen 7 is the so-called mixing region 8 .
  • the catalyst is intimately mixed with the heavy hydrocarbon charge.
  • the diameter of the surrounding tube 1 expands slightly, at a taper of around 0° to 4° with respect to the vertical, preferably a taper of from 2° to 4°, until the diameter of the surrounding tube 1 reaches a value close to that of the diameter of the section of the reactor where it will be connected.
  • the selection of an angle of 0°, the range limit value means that, depending on circumstances, the invention may be embodied without the installation of this expansion.
  • the surrounding tube is constructed with a diameter which is smaller than that of the associated reactor in order to improve the conditions of homogeneous distribution of the catalyst in the cross section of said tube 1 and to facilitate the maintenance of an adequate distribution of catalyst and mixing of the catalyst with the charge during downward flow.
  • FIG. 3 shows a diagrammatic longitudinal section through a prototype embodiment of the invention manufactured for preliminary tests.
  • the prototype has vapour injection at 5 below the control valve 4 as in FIG. 1, and a fluidisation ring 11 may be seen positioned inside the collector/distributor vessel 2 , as in FIG. 2.
  • the principal internal components, described with reference to FIGS. 1 and 2, are retained, with the same numbering. However, the expanding lower portion is not shown.
  • FIG. 4 shows a transverse section (“A-A”) through the prototype, at the level of the collector/distributor vessel 2 . It is possible to see the orifices 12 in the bottom plate 3 and the supports 13 of the collector/distributor vessel 2 . In this preferred test-embodiment the supports 13 have the form of uniformly spaced radially extending shafts connected between the surrounding tube 1 and the collector/distributor vessel 2 .
  • FIG. 5 shows a further transverse section (“B-B”) through the prototype, at the level of the mixing region 8 , showing the injector inlets 9 .
  • B-B transverse section
  • the inlets 9 there are 12 inlets, on two levels. At each level, the inlets 9 are angularly spaced by 60°, and they are offset by 30° with respect to the inlets of the other level. The inlets 9 are mounted radially, sloping upwards, forming an angle of 30° with respect to the horizontal.
  • the entry flow of catalyst 15 is controlled, centralized and initially distributed as homogeneously as possible, by means of a control valve 4 .
  • the catalyst tends to accumulate on the perforated plate 3 which forms the floor of the collector/distributor vessel 2 mounted axially and concentrically in the upper inner portion of the multifunctional entry device of the invention.
  • vapour is injected above the collector/distributor vessel 2 by means of injector inlets 5 , or an injector ring.
  • FIG. 2 Another option for the injection of vapour is the use of a fluidization ring 11 having injection orifices, mounted inside the collector/distributor vessel 2 as shown in FIG. 2.
  • the fluidisation ring inside the collector/distributor vessel 2 allows better distribution of the catalyst and prevents the formation of coke in the top of the device.
  • the curtain 16 of catalyst After passing beyond the collector/distributor vessel 2 , the curtain 16 of catalyst, encounters the annular screen 7 and undergoes a change in direction towards the longitudinal axis of the surrounding tube 1 of the device, where it is mixed with the stream of catalyst originating from the orifices 12 in the bottom plate 3 of the collector/distributor vessel 2 .
  • the stream of catalyst enters the mixing region 8 , where a hydrocarbon charge is injected through injectors 9 , initiating the anticipated thermal and catalytic reactions. From the mixing region 8 , the stream continues to the lower parts of the reactor; the surrounding tube 1 of the device of the invention in this path expands slightly up to the diameter of the section of the reactor to which it will be connected.
  • the method of the invention for supplying, distributing and intimately mixing catalyst with a hydrocarbon charge comprises the following stages:
  • a device for controlling the entry volume of catalyst 15 in the form of a preferably automatic valve 4 based on selected process parameters and installed in the entry device.
  • the catalyst 15 may be supplied independently of the differential pressure between a mixing chamber and a reservoir of catalyst, as is customary in the state of the art. This is a desirable characteristic from the operational standpoint.
  • the stream of catalyst is distributed uniformly over the cross section of the reactor in the form of threads with a diameter equal to that (normally of the order of 50 mm) of the holes 12 in the plate 3 of the bottom of the collector/distributor vessel 2 .
  • the flow of catalyst 15 above this ratio overflows the sides of the collector/distributor vessel 2 .
  • the stream 16 of catalyst which overflows the upper edge of the collector/distributor vessel 2 encounters an annular screen 7 which produces in it an angular flow deflection of the order of 30° with respect to the horizontal, with a velocity component radially towards the centre of the flow section of the surrounding tube 1 , the velocity component being downward and vertical.
  • this angle is given by the profile of the column of catalyst at rest on the screen. (Known as its “angle of repose”).
  • This same angle of deflection of the stream 16 in the form of a curtain may also be obtained by giving the cross section of the screen 7 a suitable angular profile.
  • This effect of deflecting the stream 16 of catalyst in the form of a curtain is important in that it prevents the concentration of catalyst in the vicinity of the wall of a downer-type reactor, improving the catalyst-distribution profile, as catalyst would normally tend to concentrate in the region close to the wall. It also prevents the concentration of catalyst in the region where the injector inlets are installed, minimising erosion of the injectors.
  • the hydrocarbon charge is injected in sprayed form, preferably by two sets of multiple inlets 9 , at speeds above 50 m/s, preferably between 50 and 100 m/s.
  • the inlets 9 are mounted with a positive slope with respect to the horizontal, i.e. the jets are directed against the stream of catalyst. In this way, better back mixing is obtained, allowing the occurrence of at least two contacts between the catalyst and the charge, one during the rise and the other during the fall of the mixture.
  • Another option is the installation of the inlets with a slight negative slope (less back mixing effect).
  • the stream of the greater part of the catalyst through the perforated plate 3 allows a satisfactory radial distribution of the catalyst before it is bombarded by the charge.
  • the curtain 16 of catalyst which, from a certain height has attained a radial velocity component towards the centre of the cross section of the surrounding tube 1 , allows maximization of the energy present in the sprayed charge for the intimate mixing of the catalyst with the charge in the entire reaction region of the downer, causing a greater mixing-chamber effect to be obtained.
  • This characteristic favourably differentiates the invention from curtain devices with a radial velocity component towards the wall of the reactor and from those which make use solely of the curtain stream with a radial velocity component towards the centre.
  • the diameter of the device of the invention expands slightly, for example at an angle with respect to the vertical of 0° to 4°, up to the nominal diameter of the reactor, so as to reduce segregation of the catalyst from the reagent hydrocarbon current.
  • the selection of an angle of 0° with respect to the vertical, the limit situation avoids the use of said expansion portion.
  • vapour injection into the upper part of the device of the invention by means of the vapour inlets 5 , shown in FIG. 1, or by means of an injector ring 11 of FIG. 2 (not shown in FIG. 1), prevents the stream of hydrocarbon from reaching that region, thereby minimising the formation of coke and other undesirable products.
  • This form of vapour injection may be used simultaneously with the fluidisation ring 11 shown in FIG. 2.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US10/119,037 2001-04-10 2002-04-10 Multifunctional entry method and device for downward flow tube reactor Abandoned US20030194360A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US11/512,216 US7531142B2 (en) 2001-04-10 2006-08-30 Multifunctional entry device for a downward flow tube reactor

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
BRPI0101433-1A BR0101433B1 (pt) 2001-04-10 2001-04-10 método e dispositivo de entrada multi-funcional para reator tubular de fluxo descendente.
BR0101433-1 2002-04-10

Related Child Applications (1)

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WO2010049619A1 (fr) * 2008-10-30 2010-05-06 Jean-Xavier Morin Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants
WO2011149636A1 (en) * 2010-05-24 2011-12-01 Tubemaster, Inc Device for loading catalyst into a reactor vessel
KR20140131356A (ko) * 2012-04-27 2014-11-12 제이엑스 닛코닛세키 에네루기 가부시키가이샤 유동 접촉 분해 장치에서의 원료와 촉매를 혼합하는 혼합 장치
US9138709B2 (en) 2010-05-24 2015-09-22 Extundo Incorporated Device and method for dispensing pellets
US9149778B2 (en) 2010-05-24 2015-10-06 Extundo Incorporated Device and method for dispensing catalyst pellets
JP2017104789A (ja) * 2015-12-08 2017-06-15 Ｊｘｔｇエネルギー株式会社 触媒供給装置の触媒流量設定方法、及び混合装置
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US11492701B2 (en) 2019-03-19 2022-11-08 Asm Ip Holding B.V. Reactor manifolds
US11830731B2 (en) 2019-10-22 2023-11-28 Asm Ip Holding B.V. Semiconductor deposition reactor manifolds
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Cited By (22)

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WO2005080531A1 (en) * 2004-02-10 2005-09-01 Petroleo Brasileiro S.A. - Petrobras Apparatus and process for downflow fluid catalytic cracking
CN100564486C (zh) * 2004-02-10 2009-12-02 巴西石油公司 下流式流化催化裂化装置与方法
WO2010049619A1 (fr) * 2008-10-30 2010-05-06 Jean-Xavier Morin Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants
FR2937886A1 (fr) * 2008-10-30 2010-05-07 Jean Xavier Morin Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants
WO2011149636A1 (en) * 2010-05-24 2011-12-01 Tubemaster, Inc Device for loading catalyst into a reactor vessel
US8646492B2 (en) 2010-05-24 2014-02-11 Extundo Incorporated Device for loading catalyst into a reactor vessel
US9138709B2 (en) 2010-05-24 2015-09-22 Extundo Incorporated Device and method for dispensing pellets
US9149778B2 (en) 2010-05-24 2015-10-06 Extundo Incorporated Device and method for dispensing catalyst pellets
US10370761B2 (en) 2011-10-28 2019-08-06 Asm America, Inc. Pulsed valve manifold for atomic layer deposition
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EP2843028A4 (en) * 2012-04-27 2015-12-09 Jx Nippon Oil & Energy Corp MIXING DEVICE FOR MIXING A RAW MATERIAL AND CATALYST IN A CATALYTIC FLUID CRACKING DEVICE
KR101689765B1 (ko) 2012-04-27 2017-01-09 제이엑스 에네루기 가부시키가이샤 유동 접촉 분해 장치에서의 원료와 촉매를 혼합하는 혼합 장치
KR20140131356A (ko) * 2012-04-27 2014-11-12 제이엑스 닛코닛세키 에네루기 가부시키가이샤 유동 접촉 분해 장치에서의 원료와 촉매를 혼합하는 혼합 장치
JP2017104789A (ja) * 2015-12-08 2017-06-15 Ｊｘｔｇエネルギー株式会社 触媒供給装置の触媒流量設定方法、及び混合装置
US20170350011A1 (en) * 2016-06-01 2017-12-07 Asm Ip Holding B.V. Manifolds for uniform vapor deposition
US10662527B2 (en) * 2016-06-01 2020-05-26 Asm Ip Holding B.V. Manifolds for uniform vapor deposition
US11377737B2 (en) 2016-06-01 2022-07-05 Asm Ip Holding B.V. Manifolds for uniform vapor deposition
US12416081B2 (en) 2016-06-01 2025-09-16 Asm Ip Holding B.V. Manifolds for uniform vapor deposition
US11492701B2 (en) 2019-03-19 2022-11-08 Asm Ip Holding B.V. Reactor manifolds
US11830731B2 (en) 2019-10-22 2023-11-28 Asm Ip Holding B.V. Semiconductor deposition reactor manifolds
WO2024078904A1 (fr) * 2022-10-13 2024-04-18 IFP Energies Nouvelles Procédé de craquage catalytique en lit fluidisé à co-courant gaz-solide descendant avec injecteur de charge orienté
FR3140778A1 (fr) * 2022-10-13 2024-04-19 IFP Energies Nouvelles Réacteur à lit fluidisé à co-courant gaz-solide descendant à injecteur orienté.

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MXPA02003591A (es) 2004-11-12
US20060286009A1 (en) 2006-12-21
US7531142B2 (en) 2009-05-12
PE20030005A1 (es) 2003-01-13
BR0101433B1 (pt) 2011-02-22
BR0101433A (pt) 2003-02-04
AR033133A1 (es) 2003-12-03
UY27251A1 (es) 2002-07-31

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