WO2008063463A1 - Système destiné à fluidiser des particules solides comprenant une nouvelle sortie pour récipient - Google Patents

Système destiné à fluidiser des particules solides comprenant une nouvelle sortie pour récipient Download PDF

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Publication number
WO2008063463A1
WO2008063463A1 PCT/US2007/023750 US2007023750W WO2008063463A1 WO 2008063463 A1 WO2008063463 A1 WO 2008063463A1 US 2007023750 W US2007023750 W US 2007023750W WO 2008063463 A1 WO2008063463 A1 WO 2008063463A1
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WIPO (PCT)
Prior art keywords
fluidized bed
section
outlet
velocity
outlet end
Prior art date
Application number
PCT/US2007/023750
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English (en)
Inventor
Robert O. Hagerty
Mark B. Davis
Marc L. Dechellis
David F. Hussein
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Univation Technologies, Llc
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Publication date
Application filed by Univation Technologies, Llc filed Critical Univation Technologies, Llc
Priority to BRPI0719119-7A priority Critical patent/BRPI0719119A2/pt
Priority to CN2007800429316A priority patent/CN101535756B/zh
Priority to EP07840023A priority patent/EP2084478A1/fr
Publication of WO2008063463A1 publication Critical patent/WO2008063463A1/fr

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Classifications

    • 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
    • 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
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00061—Temperature measurement of the reactants
    • 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
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/00247—Fouling of the reactor or the process equipment

Definitions

  • This disclosure relates generally to fluidized bed systems, and particularly to gas phase fluidized bed systems with reduced solids entrainment in the recycle stream.
  • Fluidized bed vessels are utilized in a variety of processes, for example olefins cracking and polymerization processes.
  • One of the most economic and commonly used methods to manufacture polymers is gas phase polymerization using a fluidized bed reactor.
  • a gaseous stream containing one or more monomers is continuously passed through a fluidized bed under reactive conditions in the presence of a catalyst.
  • This gaseous stream is withdrawn from the fluidized bed and recycled back into the reactor.
  • polymer product is withdrawn from the reactor and new monomer is added to replace the polymerized monomer.
  • the recycle gas stream is heated in the reactor by the heat of polymerization. This heat is removed in another part of the cycle by a cooling system external to the reactor.
  • the amount of polymer produced in a fluidized bed polymerization process is directly related to the amount of heat that can be withdrawn from the fluidized bed reaction zone since the exothermic heat generated by the reaction is directly proportional to the rate of polymer production.
  • the rate of heat removal from the fluidized bed must equal the rate of rate of heat generation, such that the bed temperature remains constant.
  • heat has been removed from the fluidized bed by cooling the gas recycle stream in a heat exchanger external to the reactor.
  • a requirement of a fluidized bed process is that the velocity of the gaseous cycle stream be sufficient to maintain the reaction zone in a fluidized state.
  • the amount of fluid circulated to remove the heat of polymerization is greater than the amount of fluid required for support of the fluidized bed and for adequate mixing of the solids in the fluidized bed.
  • the excess velocity provides additional gas flow to (and through) the fluid bed for additional cooling capacity and more intensive mixing of the reactor bed.
  • the velocity of the gaseous stream must be regulated.
  • a conventional gas phase fluidized bed reactor used in polymerizing olefins and/or diolefins contains a fluidized dense-phase bed and a freeboard above the dense-phase surface (bed level).
  • the freeboard contains mainly gas and a small amount of particles, especially the fine particles (fines).
  • the dense-phase bed is usually but not always maintained in a cylindrical straight section of the reactor.
  • the freeboard section is above the dense-phase bed.
  • the freeboard section (or disengagement section) often has a larger diameter, the so called expanded section, to reduce the gas velocity for the purpose of reducing the amount of fines carried out of the reactor to other parts of the reaction system.
  • the expanded section typically consists of a tapered conical section and a hemispherical top head of the reactor.
  • a reactor outlet is located at the top of the hemispherical top head.
  • a gas mixture is removed out of the top of the fluidized bed vessel through an outlet located in the top head of the fluidized bed vessel.
  • the gas mixture is circulated back to the inlet of the fluidized bed vessel through a recycle loop or recycle line.
  • the recycle loop includes other equipment essential to the operation of the fluidized bed process, such as recycle compressors or pumps, and recycle coolers.
  • fines present in the disengagement section may be entrained with the gas mixture and circulated through the recycle loop with the recycle stream.
  • the recycle stream exits the reactor outlet, passes through any equipment in the recycle loop, and re-enters the reactor near the bottom of the fluidized bed vessel.
  • the recycle gas or gas/liquid stream typically passes through a gas distributor plate and back into the fluidized bed.
  • Entrained fines in the recycle loop can become lodged in the equipment in the recycle loop, such as the recycle compressor or recycle cooler, causing various quality and operating problems. Such fines promote undesirable polymer growth and fouling of surfaces in the cycle piping, cycle cooler, compressor, lower reactor head, and distributor plate resulting in undesirable reactor shutdowns for system cleaning.
  • Adhered particles in the recycle system may continue to polymerize over time under process conditions different from the fluidized bed, forming polymer of significantly different properties, such as molecular weight, density, and molecular weight distribution, from that of the fluidized bed. Some particles are eventually released from the recycle system surfaces and are conveyed by the recycle fluid (recycle flow) back into the fluidized bed.
  • 4,588,790 shows a process wherein an expanded section is the only device used to disengage fines from the gas mixture before the gas mixture reaches the outlet of the fluidized bed vessel.
  • Other methods of addressing the problems with fines in the recycle loop include formulating the catalyst as disclosed in U.S. Patent No. 4,383,095 to minimize fines produced in the process, and poisoning the catalyst fines in the recycle loop as disclosed in U.S. Patent No. 6,180,729.
  • Other background references include U.S. Patent No. 3,089,824, JP 59 052524, DE 197 44 710, and FR 2 764 207.
  • the invention provides a system for fluidizing solid particles with a reduced amount of solid particulates exiting the top of the fluidized bed vessel.
  • the fluidized bed system comprises: a fluidized bed vessel; a fluidized bed section in the fluidized bed vessel; a disengagement section above the fluidized bed section, wherein the disengagement section comprises a top head; a recycle line in fluid communication with the disengagement section; and a tapered outlet comprising a first outlet end connected to the top head and a second outlet end connected to the recycle line.
  • a first outlet cross section of the first outlet end is at least about 1.2 times a second outlet cross section of the second outlet end, while in another embodiment the first outlet cross section is at least about 2.0 times the second outlet cross section, and in yet another embodiment the first outlet cross section is at least about 3.0 times the second outlet cross section.
  • the first outlet cross section is at least about 0.15 times a disengagement section maximum cross section, while in another embodiment the first outlet cross section is at least about 0.25 times a disengagement section maximum cross section, and in yet another embodiment, the first outlet cross section is at least about 0.35 times a disengagement section maximum cross section.
  • a transition section of the tapered outlet is a conical frustum shape, while in another embodiment the tapered outlet is a parabolic cone shape.
  • the invention also provides a method of fluidizing solids comprising the steps of: providing a fluidized bed system, wherein the fluidized bed system comprises a fluidized bed vessel, a fluidized bed section in the fluidized bed vessel, a disengagement section above the fluidized bed section, wherein the disengagement section comprises a top head, a recycle line in fluid communication with the disengagement section, and a tapered outlet comprising a first outlet end connected to the top head and a second outlet end connected to the recycle line; fluidizing a bed comprising a plurality of solid particles in the fluidized bed section; and removing a recycle stream from the fluidized bed vessel through the tapered outlet.
  • a velocity of the recycle stream at the first outlet end is about 71% or less of the velocity of the recycle stream at the second outlet end.
  • the velocity of the recycle stream at the first outlet end is about 25% or less of the velocity of the recycle stream at the second outlet end. In yet another embodiment, the velocity of the recycle stream at the first outlet end is about 11 % or less of the velocity of the recycle stream at the second outlet end.
  • the plurality of solids comprises a polymer solid, for example, polyethylene or polypropylene polymers.
  • the polymer solid comprises polyethylene polymer
  • a pressure in the fluidized bed vessel is about 250 psig (1724 kPa) to about 350 psig (2414 kPa)
  • a velocity of the recycle stream at the first outlet end is about 2.4 to about 20 meters/sec.
  • the velocity of the recycle stream at the first outlet end is about 2.4 to about 15 meters/sec.
  • the recycle stream comprises about 2 wt% or less of the plurality of solid particles.
  • the cross section may be a diameter
  • Figure 1 is schematic drawing of a gas phase fluidized bed polymerization system including an outlet of the prior art.
  • Figure 2 is a schematic drawing of a portion of a gas phase fluidization system with a inventive, tapered outlet.
  • FIGs 3 and 4 show the results of the CFD simulations for two values of superficial gas velocity (SGV).
  • a system for fluidizing solid particles with a reduced amount of solid particulates exiting the top of the fluidized bed vessel is provided.
  • the system is useful in any gas phase fluidized bed system. It is particularly useful in a gas phase polymerization system wherein polymer and/or catalyst fines may be carried out (or entrained) with the recycle stream exiting the top of the gas phase fluidized bed reactor.
  • the system may reduce "popcorn" or sheet carryover.
  • the invention is described in reference to a gas phase fluidized bed polymerization system; however, this is only intended to provide an example and should not limit the invention as a skilled artisan will recognize other useful applications.
  • a typical gas phase fluidization system comprises a fluidized bed vessel 10 with a fluidized bed section 12, and a disengagement section 14 (also known as a freeboard section) comprising a top head 13.
  • the top head 13 is a hemispherical top head
  • the disengagement section 14 further comprises a conical section 1 1.
  • the fluidized bed section 12 contains a bed of solid particles, which in some embodiments may be growing in size during the polymerization process.
  • the solid particles are fluidized by the continuous flow of fluid components, referred to herein as a fluidizing fluid, flowing up through the fluidized bed section 12.
  • the fluidized bed has the general appearance of a bubbling bed of solid polymer particles, wherein the upward flow of gas bubbles provides significant mixing of the solid particles.
  • a flow of cycle fluid (also referred to herein as a fluidizing fluid), which may be a gas or a gas/liquid combination, enters the reactor at point below the fluidized bed section 12.
  • a gas distributor plate 18 to aid in the distribution of the cycle fluid evenly to the fluidized bed section 12.
  • the cycle fluid absorbs the heat of reaction generated by a polymerization or other reaction.
  • the portion of the cycle fluid that does not react in the bed exits the top of the fluidized bed section 12 and enters the disengagement section 14. As the cycle fluid passes through the disengagement section 14 above the fluidized bed section 12, most of the solid particles drop back into the bed.
  • the cycle fluid exits the top of the fluidized bed vessel 10 as a recycle stream via the recycle line 16, is compressed in a compressor 20, and passed through a heat exchanger 22 wherein the heat of reaction, if any, is removed before the recycle stream is returned to the fluidized bed vessel 10.
  • the temperature of the fluidized bed may be monitored by means of an internal temperature sensor 19.
  • the invention provides a fluidized bed system for fluidizing solid particles comprising a fluidized bed vessel 10; a fluidized bed section 12 in the fluidized bed vessel; a disengagement section 14 above the fluidized bed section 12 comprising a top head 13; a recycle line 16 in fluid communication with the disengagement section 14; and a tapered outlet 24 comprising a first outlet end 26 connected to the top head 13 and a second outlet end 28 connected to the recycle line 16.
  • the disengagement section 14 comprises a conical section 1 1 and a hemispherical top head 13.
  • tapeered outlet generally refers to any outlet having a first outlet in fluid communication with a second outlet, wherein the cross sections, such as, for example, diameters, of the first outlet and the second outlet are different.
  • the cross section of the first outlet is greater than the cross section of the second outlet, regardless of shape.
  • the shape may be conical, parabolic, etc.
  • the fluidized bed vessel 10 may be any design appropriate for the fiuidized bed system of interest.
  • the fluidized bed vessel 10 has a disengagement section 14 located above the fluidized bed section 12 to allow the solids that may escape with the gas exiting the top of the fluidized bed to fall back into the bed.
  • the disengagement section 14 of the fluidized bed vessel 10 may be an expanded section, a straight-sided section, or a combination thereof.
  • the disengagement section 14 may be the same or larger cross section, such as, for example, diameter than the fluidized bed section 12.
  • the tapered outlet 24 may be any shape and be constructed of any materials suitable for the fluidization process of interest.
  • the tapered outlet 24 further comprises a transition section 30 in the shape of a conical frustum.
  • the tapered outlet 24 further comprises a transition section 30 with a parabolic cone shape.
  • a first outlet cross section, such as, for example, diameter, of the first outlet end 26 is larger than a second outlet cross section, such as, for example, diameter, of the second end 28.
  • the second outlet cross section is substantially equal to the recycle line 16 cross section.
  • the first outlet cross section is at least about 1.2 times the second outlet cross section, preferably the first outlet cross section is at least about 2.0 times the second outlet cross section, and even more preferably the first outlet cross section is at least about 3.0 times the second outlet cross section.
  • the ratio of the first outlet cross section to a disengagement section maximum diameter 32 also influences the amount of solid particle carryover.
  • the disengagement section maximum diameter 32 is the largest inside cross section of the fluidized bed vessel 10 above the fluidized bed section 12.
  • the first outlet cross section is at least about 0.15 times a disengagement section maximum diameter 32, preferably at least about 0.25 times the disengagement section maximum cross section 32, and more preferably at least about 0.35 times the disengagement section maximum cross section 32.
  • the invention also provides for a method of fluidizing solids comprising the steps of: providing a fluidized bed system, wherein the fluidized bed system comprises a fluidized bed vessel 10, a fluidized bed section 12 in the fluidized bed vessel 10, a disengagement section 14 above the fluidized bed section 12, wherein the disengagement section 14 comprises a top head 13, a recycle line 16 in fluid communication with the disengagement section 14, and a tapered outlet 24 comprising a first outlet end 26 connected to the top head 13 and a second outlet end 28 connected to the recycle line 16; fluidizing a bed comprising a plurality of solid particles in the fluidized bed section 12; and removing a recycle stream from the fluidized bed vessel 10 through the tapered outlet 24.
  • a velocity of the recycle stream at the first outlet end 26 is about 71% or less of the velocity of the recycle stream at the second outlet end 28, preferably, about 25% or less of the velocity of the recycle stream at the second outlet end 28, and even more preferably, about 1 1% or less of the velocity of the recycle stream at the second outlet end 28.
  • a velocity of the recycle stream at the first outlet end 26 is about 20 times or less a superficial velocity in the fluidized bed section 12, preferably, about 8 times or less the superficial velocity of the fluidization stream in the fluidized bed section 12, and more preferably, about 3.5 or less times the superficial velocity of the fluidization stream in the fluidized bed section 12.
  • the superficial velocity as used herein is the volumetric flow of the fluidization stream divided by the cross sectional area of the fluid bed section 12. It is generally understood in the art that this calculation of velocity ignores the volume occupied by the fluidized solids.
  • the amount of solids carried out of the fluidized bed vessel 10 to the recycle line 16 also depends on the type of solid being fluidized, pressure or density of the fluidizing stream, and velocity at various points in the fluidized bed vessel 10. Solids carryover is of particular concern for polymerization system wherein catalyst fines or polymer fines containing active catalyst may circulate through the system and lodge in undesirable locations. Because, in some embodiments, the invention helps minimize the amount of fines carryover, it is particularly useful for the fluidized bed polymerization of alpha olefins.
  • the plurality of solids comprises a polymer solid.
  • the polymer solids may be polyethylene, polypropylene, or any other polymer produced in a fluidized bed system.
  • the invention is also particularly useful in various polymerization processes, such as polyethylene and polypropylene processes.
  • the polymer solid comprises polyethylene polymer
  • a pressure in the fluidized bed vessel 10 is about 250 psig (1724 kPa) to about 350 psig (2414 kPa)
  • a velocity of the recycle stream at the first outlet end 26 is preferably about 2.4 to about 20 meters/sec, and more preferably the velocity of the recycle stream at the first outlet end 26 is about 2.4 to about 15 meters/sec.
  • the recycle stream comprises about 2 wt% or less of the plurality of solid particles.
  • Embodiments of the invention described herein are suitable for use in any gas phase fluid bed process.
  • a gas phase polymerization process is preferred ⁇ see,or example, U.S. Pat. Nos. 4,543,399, 4,588,790, 5,028,670, 5,317,036, 5,352,749, 5,405,922, 5,436,304, 5,453,471, 5,462,999, 5,616,661 and 5,668,228).
  • the process of this invention is directed toward a gas phase polymerization process of one or more olefin monomers having from 2 to 30 carbon atoms, preferably 2 to 12 carbon atoms, and more preferably 2 to 8 carbon atoms.
  • the invention is particularly well suited to the polymerization of two or more olefin monomers of ethylene, propylene, butene-1, pentene-1, 4- methyl-pentene-1, hexene-1, octene-1, and decene-1.
  • monomers useful in the process of the invention include ethylenically unsaturated monomers, diolefins having 4 to 18 carbon atoms, conjugated or nonconjugated dienes, polyenes, vinyl monomers and cyclic olefins.
  • Useful monomers also include norbornene, norbornadiene, isobutylene, isoprene, vinylbenzocyclobutane, styrenes, alkyl substituted styrene, ethylidene norbornene, dicyclopentadiene and cyclopentene.
  • a copolymer of ethylene is produced, wherein ethylene and one or more alpha-olefin comonomers having from 3 to 15 carbon atoms, preferably from 4 to 12 carbon atoms, and most preferably, from 4 to 8 carbon atoms, are polymerized in a gas phase process.
  • the reactor pressure in a gas phase polymerization process may vary from about 100 psig (690 kPa) to about 600 psig (4138 kPa), preferably in the range of from about 200 psig (1379 kPa) to about 400 psig (2759 kPa), more preferably in the range of from about 250 psig (1724 kPa) to about 350 psig (2414 kPa).
  • the temperature of the fluidized bed in a gas phase polymerization process may vary from about 30 0 C to about 14O 0 C, preferably from about 60 0 C to about 115°C, more preferably in the range of from about 7O 0 C to 110 0 C, and most preferably in the range of from about 75°C to about 95°C.
  • the superficial velocity in one embodiment of the invention may vary from 0.4 to 1.5 meters/sec, preferably from 0.5 to 0.9 meters/sec.
  • gas phase processes contemplated by the process of the invention include series or multistage polymerization processes.
  • Other gas phase processes contemplated by the invention include those described in U.S. Patent Nos. 5,627,242, 5,665,818 and 5,677,375, and European publications EP-A- 0 794 200 EP-Bl-O 649 992, EP-A- 0 802 202 and EP-B- 634 421.
  • the invention is directed to a gas phase process for polymerizing ethylene or propylene alone or with one or more other monomers including olefins having from 2 to 12 carbon atoms.
  • Polymers may be produced using the metallocene catalysts as described in U.S. Patent Nos. 5,296,434 and 5,278,264.
  • the invention is not necessarily limited to the application of any one catalyst system type.
  • the invention has application with metallocene catalysts, constrained geometry catalysts, Ziegler-Natta catalysts, chrome based catalysts, iron based catalysts, nickel based catalysts, as well as dual catalysts systems, including the application of at least one metallocene with at least one Group 15 atom (such as N) metal compound.
  • Figures 3 and 4 are derived from Computational Fluid Dynamics (CFD) simulations. This is a well known method to solve equations (e.g., the Navier- Stokes equations) of fluid dynamics to produce calculations of gas flow fields. As used here, CFD is used to model the flow field in the top (expanded) section of a UNIPOLTM Reactor. The results show the advantages of embodiments of the invention employing a tapered outlet design.
  • CFD Computational Fluid Dynamics
  • Figures 3 & 4 show calculated centerline velocities as a function of height in the expanded section. Note that the position of 0.0 height corresponds to the top of the reactor cylindrical section. (This position, at the junction of the cylindrical and conical sections, is also referred to as the "neck" of the reactor. In the case of the standard design (without the tapered outlet) the top of the reactor is at an elevation of 37.1 feet above the neck. This marks a convenient point of reference to compare the velocity profiles of the different outlet designs.
  • SGV superficial gas velocity
  • the gas velocity in the expanded section is approximately constant over the range of elevations between zero and 30 feet. Above this height, the gas velocity is seen to increase rapidly as the flow field approaches the outlet.
  • Figures 3 & 4 show that the effect of the tapered outlet is to delay the increase in velocity, effectively moving the point of velocity increase (or point of transition) to higher elevations.
  • the effect of the 2:1 cone is to move the point of transition approximately 1.2 ft. higher.
  • the 3;1 and 4:1 tapered outlets move the point of transition approximately 2.5 feet higher.
  • the tapered reactor outlet is effective in altering the gas flow.
  • the tapered outlet produces a higher point of transition to high velocity, which is expected to produce a reduction in particle carryover, at a given value of SGV.
  • ranges from any lower limit may be combined with any upper limit to recite a range not explicitly recited, as well as, ranges from any lower limit may be combined with any other lower limit to recite a range not explicitly recited, in the same way, ranges from any upper limit may be combined with any other upper limit to recite a range not explicitly recited.
  • within a range includes every point or individual value between its end points even though not explicitly recited. Thus, every point or individual value may serve as its own lower or upper limit combined with any other point or individual value or any other lower or upper limit, to recite a range not explicitly recited.

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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)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Polymerisation Methods In General (AREA)

Abstract

L'invention concerne un système destiné à fluidiser des particules solides, dans lequel le système à lit fluidisé comprend un récipient à lit fluidisé, une section à lit fluidisé, une section de désengagement, une ligne de recyclage, et une sortie conique. L'invention concerne également un procédé consistant à fluidiser des solides grâce à l'agencement d'un système tel que décrit ci-dessus, à fluidiser un lit comprenant des particules solides, et à retirer un flux de recyclage à travers la sortie conique.
PCT/US2007/023750 2006-11-20 2007-11-13 Système destiné à fluidiser des particules solides comprenant une nouvelle sortie pour récipient WO2008063463A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
BRPI0719119-7A BRPI0719119A2 (pt) 2006-11-20 2007-11-13 Sistema para a fluidização de partículas sólids incluindo um orifício de descarga novo para recipiente
CN2007800429316A CN101535756B (zh) 2006-11-20 2007-11-13 包括新型容器出口的使固体颗粒流态化的系统
EP07840023A EP2084478A1 (fr) 2006-11-20 2007-11-13 Système destiné à fluidiser des particules solides comprenant une nouvelle sortie pour récipient

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US86016606P 2006-11-20 2006-11-20
US60/860,166 2006-11-20

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Cited By (1)

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