US3627129A - Process and apparatus for the separating out of coarse and/or heavy particles from a variable particle size and/or variable particle weight mixture of granular solids maintained in a fluidized state - Google Patents

Process and apparatus for the separating out of coarse and/or heavy particles from a variable particle size and/or variable particle weight mixture of granular solids maintained in a fluidized state Download PDF

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US3627129A
US3627129A US792682*A US3627129DA US3627129A US 3627129 A US3627129 A US 3627129A US 3627129D A US3627129D A US 3627129DA US 3627129 A US3627129 A US 3627129A
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zone
fluid
elutriant
reactor
cross
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US792682*A
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Rainer Hartmann
Oskar Dorschner
Hans-Werner Gross
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GEA Group AG
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Metallgesellschaft AG
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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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/44—Fluidisation grids
    • 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
    • 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
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • 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
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • 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
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours

Definitions

  • the upwardly flowing gas generating the fluidized condition in the mixture of solids is referred to hereinafter as carrier gas or elutrient.
  • mixture of solids of variable size or weight of the individual particles can be sorted out of the fluidized solids in that the finer particles are upwardly blown or flushed out of the fluidized solids by means of the carrier gas, with the coarser particles collecting for instance on the oncoming flow floor for the carrier gas, designed for instance as a grate, or where the coarser particles fall out of the spinning mixture, counter to the flow of the carrier gas, from a grateless, preferably conical zone.
  • Such a relatively dense bed can be compared with a boiling liquid since the carrier gas is apparently forming the dispersed phase -corresponding to steam bubbles in the liquid. Between the bubbles and tunnels, the mixture of solids forms coherent areas in which it is hardly possible for the individual particles to move with respect to one another.
  • the individual particles in this state, can be considered as the dispersed phase in view of the fact that they are distributed in the carrier gas in a comparatively low concentration and can, therefore, move practically independently of one another.
  • the granular mixture is held in the grateless chamber in a strongly agitated and brokenup (aerated) condition.
  • the amount of carrier gas to the amount of solids in the chamber it is possible to achieve an unstable state of the dispersed suspension in which solid particles fall out of the lower opening of the chamber.
  • the coarser particles whose speed of fall is greater than the velocity of the carrier gas are preferably discharged out of the chamber downwardly counter to the direction of flow of the gas.
  • the finer particles contained in the mixture and whose speed of fall is smaller than the velocity of the carrier gas are carried along by the carrier gas and discharged upwardly out of the dispersed suspension.
  • the carrier medium flow entering the chamber has been broken up by means of suitable installations into a plurality of currents of smaller cross section, with the individual flow paths being designed for instance as Venturi tubes.
  • the individual flow paths being designed for instance as Venturi tubes.
  • this design does not make it possible to achieve any substantially larger assemblies. Reactors exceeding a diameter of 50 cm. in the most narrow reactor cross sections are thus far unknown.
  • the object of the invention is a process and apparatus for the continuous separation of a coarse grain fraction, having a close grain size distribution, out of a mixture of solids having variable grain sizes, maintained in a fluidized state by means of a carrier gas, whose grain size distribution can be modified by agglomeration or polymerization.
  • This process is characterized in that the mixture of solids is maintained by the carrier gas in the upper area of the reactor at a greater reactor cross section in a state of a dense fluidized bed and, in the lower area of the reactor at a smaller reactor cross section in a state of a dispersed: suspension and that in the boundary cross section between these areas the velocity of flow of the carrier gas is increased, by means of a reduction in the cross section, to more than 1,2 times the velocity of flow in the area of the dispersed suspension.
  • the great advantage of the discovered process consists, furthermore, in that the required velocity of the carrier gas for any desired suspension state is independent of the diameter of the selected fluidized bed and that, as a result based on the instant invention, it is possible to operate reactors of any engineering dimensions.
  • a part of the carrier gas can be shunted ofl and discharged to the outside ahead of the reduced border area cross section.
  • This shunted off part of the carrier medium can be reintroduced in whole or in part above the narrowed boundary area cross section into the dense fluidized bed in the upper reactor area; however, it can be returned also beneath the oncoming flow floor thereby achieving a cycle of the carrier medium across the area of the dispersed suspension.
  • a further amount of carrier gas can be introduced above the reduced boundary area cross section.
  • the possibility for an individual change in the velocity of flow of the carrier gas in a single, in two or in all three zones of the reactor is advantageous if the grain size distribution of the mixed charge is being altered during its presence in the reactor, eg. as a result of agglomeration, deposition of solids e.g., coking) on the particles. or by means of polymerization.
  • This is applicable. for example, with regard to the polymerization in the gaseous phase of oleflns through contact with a catalystcontaining fine-grained polymer held in the fluidized state by means of an olefin-containing carrier gas (as set forth in one of the following examples).
  • a reactor for the execution of the process according to the invention comprises two superpositioned preferably substantially coaxial cylindrical jackets, the upper one of which has a wider cross section than the lower one.
  • the cross section ratio can be about 1:2 to 1:15, preferably I13 to 1:10, between the lower and the upper cross sections, respectively.
  • the two cylindrical jackets can be interconnected at their adjoining extremities by means of an ordinary, annular disk.
  • a conical spacer as a connecting element in order to avoid producing blind angles in which solids are likely to deposit.
  • the carrier gas is introduced at the lower end of the lower cylinder via a floor suitable to receive the oncoming flow, a grate, or the like, and discharged at the upper end of the cylinder, possibly via a cyclone.
  • the granular mixture of solids to be sorted is being introduced laterally into the upper or lower cylinder.
  • the coarse material accumulates on the oncoming flow floor or grate whence it is removed periodically or continuously in a per se known manner via a central peripheral or lateral removal means.
  • the fine grain material can, in a per se known manner, be discharged by the carrier gas current out of the upper cylinder and be separated out of the gas current in a cyclone, and/or be drawn off laterally from the level of the dense fluidized bed layer.
  • Such a reduction in cross section can be brought about for instance by means of a perforated plate, or by means of a concentrically inserted element, and should have an orifice total cross section not exceeding 0.85 times the cross section of the lower cylinder.
  • the aperture in the perforated plate are preferably dimensioned so that their individual diameters represent 5 to 20 times the size of the coarse grain particles to be separated out.
  • the annular clearance formed by it with respect to the reactor cross section should have a width of 2 to 10 times the particle size of the coarse grain to be separated out. These values are preferred and may be adjusted upwardly or downwardly in given cases.
  • the concentric insert element can be connected with the reactor by means of radial supports. Its shape may be conical or double truncated conical and it can be movably arranged on a vertical rod displaceable along the reactor axis.
  • openings can be arranged in the reactor jacket, which lead to annular ducts.
  • annular ducts By means of these annular ducts, partial amounts of the carrier medium can be drawn off from and/or introduced into the reactor.
  • a part of the carrier medium can be drawn off from the lower reactor zone through the lower annular duct ahead of the reduction in area and be reintroduced into the upper reactor zone above the reduction in area.
  • FIG. 1 schematically shows an axial cross section of a reactor
  • FIG. 2 is a cross section along line AA of FIG. 1 and through the intermediate perforated plate narrowing down the flow cross section;
  • FIG. 3 represents another embodiment of the reduction in cross section between the two reactor zones by means of a concentric insert element shown as an axial section;
  • FIG. 4 represents a horizontal section through FIG. 3 along line BB;
  • FIG. 5 illustrates a variant of the device according to FIG. 4, with adjustable intermediate area-reducing member
  • FIG. 6 illustrates a perforated plate according to FIGS. 1 and 2, with means for the additional introduction of carrier gas into the upper reactor zone;
  • FIG. 7 shows another device for the introduction of additional carrier gas into the upper reaction zone. in a vertical cross section
  • FIG. 8 represents a horizontal section through FIG. 7 along line CC;
  • FIG. 9 shows a mode of realization of the coarse grain discharge above the floor suitable to receive the oncoming flow, represented as a vertical section
  • F IO. 10 represents, as an axial cross section, a special design of the lower reactor zone
  • FIG. 11 is the flow diagram of a plant for the execution of the process according to the invention applied to the polymerization of gaseous monoolefins.
  • the reactor 1 schematically illustrated in FIG. 1 substantially comprises an upper chamber 2 having a larger cross section, a lower chamber 3 having a smaller cross section, a connecting intermediate zone 4 having a more narrow cross section, a floor 5 suitable to receive feed flow of a carrier gas via an air chamber 6, and is provided with supply lines 7 and 8 for solid material to be processed, as well as with a discharge line 9 for coarse grain product that has been separated out, and an outlet 10 for fine grain product.
  • the connecting zone 4 is designed as a truncated cone 11.
  • the reduction in area is by means of a perforated plate 12 illustrated enlarged as a horizontal cross section in FIG. 2.
  • the upper reactor zone 2 can be joined via a truncated cone 18 to a stabilizer chamber 19 from which the carrier gas is drawn off through a cyclone separator by means of a line (not shown).
  • the perforated plate 12 can be replaced by an insert 20, concentrically arranged in the area of the contact point of the jackets of the lower chamber 3 and the connecting zone 4, which is fixedly connected to the elutriation apparatus jacket.
  • the reduction in cross section area is in this case accomplished by an annular clearance 22.
  • the concentrically arranged insert element 23 may have the shape of a cone and be fastened to a rod 24 displaceable along the apparatus axis.
  • the cross section area reduction 25 can be altered during operation. This principle may be applied also with regard to each individual bore of a perforated plate.
  • the system for the introduction of additional carrier gas into the upper reactor zone consisting of an annular duct 15 with appropriate openings 13 and a pipe connection 16 (FIG. I), can be replaced for instance by a special design of perforated plate 12 illustrated in FIG. 6.
  • the perforated plate consists of a plurality of pipes 26 held at their extremities in support elements 27 and 28.
  • the support elements are connected with a cylindrical housing 29, which may also be the jacket of the lower chamber 3 (FIG. I), and which is provided with a pipe connection 30 for the supply of carrier gas.
  • a cylindrical housing 29 which may also be the jacket of the lower chamber 3 (FIG. I)
  • a pipe connection 30 for the supply of carrier gas.
  • bores 31 have been arranged between the end points of the pipes 26, which lead to the hollow space between the pipes in the housing, thereby permitting the carrier gas supplied through a pipe connection 30 to issue through said bores.
  • Pipes 32 provided with screen covers 33 are shown inserted in the bores 31.
  • FIGS. 7 and 8 illustrate another mode of realization for the supply of additional carrier gas to the upper reactor zone 2.
  • a pipe 34 leading, via a bend 35, to a pipe connection 36 in the jacket of the lower chamber.
  • the pipe 34 is provided at its upper end with a porous or perforated gas distribution plate 37.
  • perforated distributor pipes 38 emanate radially from the upper pipe end, which can in per se known manner be provided with screen covers (not shown).
  • Additional carrier gas is introduced via the pipe connection 36 and enters into the upper chamber through the openings in the gas distributor pipe 37 and in the distributor pipes 38.
  • FIG. 9 illustrates a variant of the coarse grain discharge means.
  • the jacket of the lower chamber can, as shown in FIG. 9, be expanded at its lower extremity to form a beadlike annular space 39 constituting a cover over the floor 5 and the air chamber 6 and can be provided with a delivery pipe 40 comprising a bucket-wheel valve 41 for the removal of the coarse grain product.
  • FIG. 10 illustrates a particular design of the lower reactor zone 3, by means of which the selectivity with regard to the grain size to be sorted can be improved if need be.
  • a conical insert element 42 Spaced a short distance above the floor 5 for the feed flow, which comprises a central aperture for the coarse grain particle outlet 9, there is arranged a conical insert element 42 attached to the floor for instance by means of supports 43.
  • the annular edge of this conical insert forms a narrowed passage 44 with the wall of the lower chamber.
  • the carrier medium coming in through the oncoming flow floor flows first under the floor of the cone horizontally with respect to passage 44 at a velocity of flow somewhat greater than that of the velocity of the gas in the reactor zone, and generates in this area a final crosscurrent classification.
  • the carrier medium comprises a reactant in view of the fact that it contains the monomer.
  • the monomer can react with the catalyst still active in the polymer particles in the area of the lower reaction zone and thus use up the residual activity thereof while standardizing the grain size.
  • FIG. 11 illustrates the application of the process to the gaseous phase polymerization of ethylene.
  • a reactor 50 designed according to the invention, there is a dense turbulent fluidized layer formed by polymer and catalyst particles.
  • a growth in the particles owing to the growth of polymer on the catalyst nuclei, which results in an increase in the volume of the fluidized bed.
  • the large polymer particles containing only small amounts of still partially active catalyst must be flushed out of the process and, to this end, one uses the process according to the invention.
  • the coarse particles that have been produced are flushed out of the process by means of the pipe portions associated with reduced area intermediate member designed according to FIG. 6 and a coarse grain particle discharge means 53 and enter a lower reactor part 52 where the state of an aerated dispersed suspension is formed and maintained.
  • the particles containing still partially active catalyst can permit full reaction before they enter the bin 56 by means of a discharge pipe 54 via a bucket-wheel valve 55.
  • a mixture comprising fine polymer and catalyst particles is continuously fed into the upper part of the apparatus (fluidized bed) via a dosing device 57 and input pipe 58 from a bin 60.
  • Fine particles can be drawn off at the surface of the dispersed turbulent layer via a discharge pipe 59 and a bucketwheel valve 61, as initial preparation of the polymer particle and catalyst mixture.
  • the carrier gas consisting, substantially, of the monomer to be polymerized enters a chamber 63 of the reactor via pipe connections 62 and flows sequentially via a gas distribution grid 64 through the lower part 52, the intermediate reduction in area member 53 and the fluidized bed 51 of the reactor.
  • the carrier gas emerges from the reactor at 66, via line 67, and enters a cyclone 68 where the dust portion taken up by the carrier gas is separated out and falls into a dust accumulator 69.
  • the dust-free carrier gas is subsequently fed into a circular gas compressor '70 where it is compressed to the required pressure.
  • the monomer consumed in the course of the reaction is replenished via a line 71 and a pressure-regulating valve 72.
  • Control of the amount of carrier gas supplied to the reactor is achieved by means of a bypass valve 77 of the compressor.
  • EXAMPLE 1 For polymerization of ethylene in the gaseous phase, the plant was operated as illustrated in FIG. 11 and described above.
  • the upper cylindrical reactor part for accommodating the fluidized bed had a diameter of 200 mm. and a height of L meter.
  • the lower reactor zone had a diameter of 90 mm. and a height of 15 cm.
  • the two zones were connected by means of a l cm. high conical junction element.
  • the height of the cylindrical part was 50 cm. while the overall height was 100 mm.
  • the cone had been displaceably arranged in a manner similar to that shown in FIG. 5 and, in order to close the 40 mm. diameter central discharge tube 9 (see FIG. 1), could be moved completely down. For the purpose of emptying the reactor completely, the cone could be slidably displaced up to a point in the upper reactor zone.
  • the height of the fluidized bed in the upper reactor part varied between 400 and 800 mm.
  • the grain size of the spinning material formed by catalyst and polymer particles was between 0.5 and 4.0 mm.
  • the polymerization reaction was carried out at a slight overpressure l.2 atm. absolute'pressure.
  • a suitable Ziegler catalyst which was applied onto fine-grain polyethylene particles having an average grain size of approximately 0.5 mm.
  • the catalyst represented 8 percent by weight of the catalystpolymer mixture.
  • 125 g./hour of catalystpolymer mixture were fed into the reactor.
  • 5 kg. of polyethylene particles of a'diameter between 2.0 and 3.5 mm. were discharged per hour from the central discharge tube 9 via the bucket-wheel valve.
  • the dust resulting from abrasion in the vortex bed was separated out in a cyclone; it amounted to approximately l0 g./hr.
  • the polymer particles discharged in the process exhibited the following grain spectrum:
  • Part hy Weight (1) up to 1.0 5.2 1.0-2.0 2L0 2.0-3.0 44.8 3.0-4.0 25.8
  • EXAMPLE 2 For the purpose of separating out a fraction of coarse grain from an aggregate of polypropylene particles and for treating the particles simultaneously with air to deactivate the catalyst contained in the particles. a device was operated in accordance with FIG. 1, in which the annular ducts 14 and 15, as well as the gasinlet and outlet openings 13 had been omitted.
  • the overall height of the reactor was 4.5 m., the height of the fluidized bed was varied between 1.0 and b 1.5 m.
  • Particle Size (mm.) Part by Weight ('1) up to L0 [0.0 l.0-2.0 29.0 2.0-3.0 34.] 3.0-4.0 [7.6 4.0-5.0 5.5
  • the enriched fine material was drawn off from the surface of the fluidized bed by means of an overflow discharge tube 10.
  • EXAMPLE 3 To improve the selectivity of the process described in example 2, a device according to FIG. 10 was mounted into the lower part of the reactor. The ratio of the diameter of the base of the cone to the diameter of the lower reactor part amounted to 0.69. The cone had an angle of 42 and was situated at a distance of 15 mm. from the oncoming flow floor. The supplying of the charge material and the discharging of the coarse and fine material was carried out as in example 2. The hourly yield was 13.5 kg. of coarse material having the following composition:
  • EXAMPLE 4 A grain fraction having a greater proportion of coarse material than that referred to in examples 2 and 3 was treated by performing the process. in the identical device used in such examples. There was used as a reduction in area member a perforated plate designed according to FIG. 6 and having gas outlet bores 31 of a diameter of 2 mm. each, without, how ever, tubes 32 and cover screens 33. In view of the fact that the velocity of the carrier gas required to maintain a moderately agitated fluidized state amounted to 0.3 msec. with regard to the granulation of the material in question, another volume of gas representing approximately 20 percent of that entering the reactor via the floor receiving the oncoming flow was introduced additionally into the upper part of the reactor via the pipe connection 30 and the bores 31.
  • the charge material supply and volume were the same as in example 1.
  • the discharging of the coarse and fine fractions was carried out as in example 1.
  • the charge product exhibited the following composition:
  • Elutriation apparatus comprising a lower chamber, an upper chamber having a larger cross section than said lower chamber, an intermediate chamber between said upper and said lower chambers having a smaller cross section than said upper and said lower chambers, means for feeding particulate material to said apparatus for elutriation.
  • Elutriation apparatus as claimed in claim 3 including elutriant supply means connected to the space between said perforated plates of said intermediate member and communicating with said upper chamber through bores provided in said upper plate.
  • insert element consists at least partially of a conical member having an axis substantially coincident with the axis of said upper and lower chambers and having a maximum diameter which is no greater than the inside diameter of said lower member. which conical member is axially displaceable.
  • Elutriation apparatus as claimed in claim 1 including elutriant fluid discharge means disposed below said intermediate member and elutriant fluid introduction means disposed above said intermediate member.
  • Process of continuously elutriating a particulate material of varying grain size which comprises feeding a fluid to and through a first zone; establishing and maintaining a dispersed suspension in said first zone; feeding said fluid from said first zone through an intermediate zone whose cross section is a smaller cross section with respect to said dispersed suspension zone up to about 0.85 thereof, increasing the velocity thereof to more than 1.2 times the velocity thereof in said first zone; feeding said fluid from said intermediate zone to a second zone having a crosssectional ratio of about 2:] to l5:l with respect to said first zone; establishing and maintaining a dense fluidized bed in said second zone; recovering coarser grain particles from the base of said dispersed suspension zone.
  • Process as claimed in claim 8 including providing said intermediate zone as an annulus between a jacket means and an insert element which annulus has a gap which is about 2 to 10 times the diameter of said coarser grain particles withdrawn from said lower zone.
  • Process as claimed in claim 8 including tapping a portion of said elutriant fluid upstream of said intermediate zone.
  • Process as claimed in claim 11 including reintroducing said tapped elutriant fluid to said process downstream of said intermediate zone.
  • Process as claimed in claim 12 including admixing said tapped elutriant fluid with fresh elutriant fluid and feeding said admixture to said process downstream of said intermediate zone.
  • Process as claimed in claim 8 with said elutriant fluid is gas.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Polymerisation Methods In General (AREA)
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  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
US792682*A 1968-01-24 1969-01-21 Process and apparatus for the separating out of coarse and/or heavy particles from a variable particle size and/or variable particle weight mixture of granular solids maintained in a fluidized state Expired - Lifetime US3627129A (en)

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DE19681607648 DE1607648B2 (de) 1968-01-24 1968-01-24 Verfahren und vorrichtung zum abtrennen grober und/oder schwerer partikel aus einem mittels eines traegergases im wirbelzustand gehaltenen feststoffgemisches

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AT (1) AT290118B (de)
BR (1) BR6905822D0 (de)
ES (2) ES362839A1 (de)
FR (1) FR2000682A1 (de)
GB (1) GB1246406A (de)
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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3931134A (en) * 1968-01-24 1976-01-06 Veba-Chemie Ag Process and apparatus for the separating out of coarse and/or heavy particles from a variable particle size and/or variable particle weight mixture of granular solids maintained in a vortex state
USRE29625E (en) * 1972-03-21 1978-05-09 Brown & Williamson Tobacco Corporation Process and apparatus for separating sand from botanical materials
US4116823A (en) * 1975-08-11 1978-09-26 Occidental Petroleum Corporation Vessel for stripping oil from fluidized ash and char particles
US4280903A (en) * 1980-08-06 1981-07-28 Brown & Williamson Tobacco Corporation Apparatus for separating sand from botanical fines
US4714553A (en) * 1986-01-20 1987-12-22 Bp Chemicals Limited Treatment of catalyst particles
US6391985B1 (en) 1999-10-21 2002-05-21 Union Carbide Chemicals & Plastics Technology Corporation High condensing mode polyolefin production under turbulent conditions in a fluidized bed
US6759489B1 (en) 2003-05-20 2004-07-06 Eastern Petrochemical Co. Fluidized bed methods for making polymers
US20080149541A1 (en) * 2006-12-05 2008-06-26 Bigney Nicholas D Apparatus, system, and method for detecting and removing flawed capsules
US20100078363A1 (en) * 2008-09-26 2010-04-01 Uchicago Argonne, Llc Process and apparatus for separating solid mixtures
CN102935428A (zh) * 2012-11-08 2013-02-20 品孚罗特过滤设备（北京）有限公司 一种分离固体颗粒的分离装置及其应用

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USRE29625E (en) * 1972-03-21 1978-05-09 Brown & Williamson Tobacco Corporation Process and apparatus for separating sand from botanical materials
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FR2000682A1 (de) 1969-09-12
IL31470A (en) 1971-08-25
GB1246406A (en) 1971-09-15
BR6905822D0 (pt) 1973-01-04
AT290118B (de) 1971-05-25
NL6901152A (de) 1969-07-28
IL31470A0 (en) 1969-03-27
ES362839A1 (es) 1970-09-01
ES362840A1 (es) 1970-09-01

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