EP1472004A1 - Separation de fines matieres particulaires solides d'un flux de gaz - Google Patents

Separation de fines matieres particulaires solides d'un flux de gaz

Info

Publication number
EP1472004A1
EP1472004A1 EP02736482A EP02736482A EP1472004A1 EP 1472004 A1 EP1472004 A1 EP 1472004A1 EP 02736482 A EP02736482 A EP 02736482A EP 02736482 A EP02736482 A EP 02736482A EP 1472004 A1 EP1472004 A1 EP 1472004A1
Authority
EP
European Patent Office
Prior art keywords
cyclone
gas
cyclone body
gas stream
tube sheet
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.)
Withdrawn
Application number
EP02736482A
Other languages
German (de)
English (en)
Inventor
Paul A. c/o UOP LLC SECHRIST
Brian W. c/o UOP LLC HEDRICK
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.)
Honeywell UOP LLC
Original Assignee
UOP LLC
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
Publication date
Application filed by UOP LLC filed Critical UOP LLC
Publication of EP1472004A1 publication Critical patent/EP1472004A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/14—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by rotating vanes, discs, drums or brushes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/04—Multiple arrangement thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/06—Construction of inlets or outlets to the vortex chamber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C2003/006—Construction of elements by which the vortex flow is generated or degenerated

Definitions

  • the present invention relates to a novel cyclone separator for removing fine solid particulates from a gas stream.
  • the cyclone is especially applicable in a third stage separator apparatus, often used to purify the catalyst fines-laden flue gas stream exiting a
  • FCC refinery fluid catalytic cracking
  • the FCC process comprises a reactor that is closely coupled with a catalyst regenerator, followed by downstream hydrocarbon product separation.
  • a major distinguishing feature of the process is the continuous fluidization and circulation of large amounts of catalyst having an average particle diameter of 50- 100 microns, equivalent in size and appearance to very fine sand. For every ton of cracked product made, approximately 5 tons of catalyst are needed, hence the
  • regenerator has provided over 99% separation efficiency of solid catalyst.
  • regenerator includes first and second (or primary and secondary) stage separators for the purpose of preventing catalyst contamination of the regenerator flue gas, which is essentially the resulting combustion product of catalyst coke in air. While normal-sized catalyst particles are effectively removed in the internal regenerator cyclones, fines material (generally catalyst fragments smaller than 50 microns resulting from attrition
  • the FCC flue gas will usually contain a particulate
  • the solids content in the FCC flue gas may be sufficient to damage turbine blades of an air blower to the regenerator if such a power recovery scheme is indeed selected.
  • Electrostatic precipitators are known to be effective for this gas/solid
  • a cyclone separator for an FCC flue gas effluent will normally contain many, perhaps 100, small individual cylindrical cyclone bodies installed within a single vessel acting as a manifold. Tube sheets affixing the
  • upper and lower ends of the cyclones act to distribute contaminated gas to the cyclone inlets and also to divide the region within the vessel into sections for collecting the separated gas and solid phases.
  • the gas outlet is a tube normally concentric with
  • the open bottom design provides a relatively large surface area for exiting "dirty" gas to enter the bodies
  • the present invention is an improved cyclone for the separation of solid
  • cyclones can be combined in a vessel for use as a third stage separator in the treatment of solid-contaminated gas streams, and in particular flue gas from a refinery fluid catalytic cracking unit or other solid- contaminated gas streams.
  • the cyclone provides a high separation efficiency because a
  • particulate-laden gas vortex is established and travels through the device with minimal flow pattern disturbances.
  • the feed gas and exiting clean gas move in the same direction throughout the separation, and the clean gas, representing the bulk of the feed gas on a volume basis, is removed from the central portion of the vortex using a gas outlet tube extending with the cyclone body. Furthermore, solid particles are forced through
  • openings in the sidewall of the cyclone body to prevent backflow and gas communication among adjacent cyclones, rather than discharged axially.
  • exits act as a "check valve" to prevent backflow and particle re-entrainment into the
  • the cyclone of the present invention is effective for separating even fine dust particles as small as 4-5 microns in diameter from the feed gas stream.
  • FIG. 1 is a simplified schematic view of an FCC unit of the prior art.
  • FIG. 2 is a simplified schematic view of a third stage separator of the prior
  • FIG. 3 is a cross sectional view of the cyclone of the present invention.
  • FIG. 4 is a sectional view of FIG. 3 taken along line AA.
  • FIG. 5 shows the improved separation performance efficiency of the cyclone
  • FIG. 6 shows the improvement associated with the present invention in terms of its d50 value, or measure of the particle diameter for which 50% removal would be
  • the present invention applies to the purification of a broad range of solid- contaminated gas streams, and especially those containing dust particles in the 1-10 » m range.
  • a number of commercial gas purification operations meet this description,
  • fluid catalytic cracking is a well-known oil refinery
  • FIG. 1 represents a typical FCC process unit of the prior art, where a heavy hydrocarbon feed or raw oil in line 12 is contacted with a newly regenerated catalyst entering from a regenerated catalyst standpipe 14. This contacting occurs along a narrow section extending from the bottom of the reactor 10, known as the reactor riser 16. Heat from the catalyst vaporizes the oil, and the oil is thereafter cracked
  • the catalyst is therefore referred to as being spent (or at least partially spent) and requires regeneration for further use. Spent catalyst, after separation from the
  • hydrocarbon product falls into a stripping section 24 where steam is injected in line 26 to purge any residual hydrocarbon vapor.
  • a stream of air from line 34 is introduced through an air distributor 28 to contact the spent catalyst, burn coke deposited thereon, and provide regenerated catalyst.
  • the catalyst regeneration process adds a substantial
  • regenerator 30 located within the regenerator 30 and, after regeneration (i.e. coke burn), are initially separated by discharge through a "T" disengager 40, also within the regenerator 30. Finer separation of the regenerated catalyst and flue gas exiting the disengager 40 is
  • first stage 44 and second stage 46 regenerator cyclone separators can remove the vast majority of the regenerated catalyst from the flue gas in line 42, fine catalyst particles, resulting mostly from attrition,
  • TSS third stage separator
  • the TSS vessel 50 is normally lined with refractory material 52 to reduce erosion of the metal surfaces by the entrained catalyst particles.
  • contaminated flue gas from the FCC regenerator enters the top of the TSS at its inlet 54 above an upper tube sheet 56 that retains the top ends 58 of each cylindrical cyclone body 62.
  • the contaminated gas stream is then distributed among cyclone feed gas inlets
  • the swirl vanes are structures within the cyclone body that have the characteristic of restricting the passageway through which incoming gas can flow, thereby accelerating the flowing gas stream.
  • vanes also change the direction of the contaminated gas stream to provide a helical or spiral formation of gas flow through the length of the cyclone body. This spinning motion imparted to the gas sends the higher-density solid phase toward the wall of the cyclone body 62.
  • the cyclone design shown in FIG. 2 represents the so-called "uniflow" apparatus where a bottom end 66 of the cyclone body 62 is open, allowing solid particles that have been thrown near the wall of this cylinder to fall into the space 68 between the
  • Clean gas flowing along the centerline of the cyclone body, passes through an inlet 70 of a gas outlet tube 72 before reaching the bottom end 66 of
  • the clean gas is then discharged via the gas outlet tube 72 below a lower tube sheet 74.
  • the combined clean gas stream representing the bulk of the fines-
  • contaminated flue gas then exits through a gas outlet 76 at the bottom of the TSS vessel 50.
  • the separated particles and a minor amount (typically less than 10% of the fines- contaminated flue gas) of underflow gas are removed through a separate particulate and underflow gas outlet 78 at the bottom of the TSS 50.
  • the cyclone 100 comprises an essentially vertical cyclone body 106 having a closed bottom
  • the closed bottom end 108 is preferably in the form of a horizontal plate.
  • the cyclone body defines a feed gas inlet 112 at its top end 110 for receiving a particle-contaminated gas
  • the cyclone body further defines a plurality of openings 114 for discharging gas. These openings 114 are between the upper, tube sheet 102 and the lower tube sheet 104, and are generally located in the lower portion of the cyclone body 106. Preferably, these openings 114 are proximate the bottom end 108 and extend upward from it.
  • openings allow for the discharge of particles along with a minor amount of an underflow
  • One or more swirl vanes 116 are located proximate the gas inlet at the top of
  • a gas outlet tube 118 is located centrally within the cyclone body 106, extends through the closed bottom end 108, and further extends upward through the lower tube sheet 104.
  • this gas outlet tube 118 defines, respectively, a clean gas inlet
  • the clean gas inlet 120 is generally located above the discharge openings 114.
  • the clean gas outlet 122 can be located anywhere below the bottom end
  • the cyclone body 106 is oriented generally vertically, so that separation of the solid phase is assisted by gravity.
  • the cyclone body is in the
  • the major advantage of this design is that it provides a very uniform vortex of swirling gas that is essentially undisturbed along its downward path through the cyclone body and gas outlet tube.
  • a further advantage is related to the increased pressure drop accompanying the ejection of particulate-rich gas through the cylinder wall openings. These openings provide a relatively small surface area for gas to exit, compared to the larger bottom ring-shaped surface between the cyclone body and the gas outlet tube, used in the aforementioned uniflow cyclone designs.
  • each opening provides a type of "check valve" through which backflow of discharged gas, a cause of reduced separation efficiency, is substantially eliminated.
  • the openings may be of virtually any shape and located anywhere on the cyclone cylinder body, although it is preferred that at least some of these openings are near the closed bottom end of the cyclone to prevent an accumulation of solid particles in this region.
  • the openings may also be of varying shapes, for example, slots and holes,
  • the openings are in the form of rectangular slots with their major dimension (length) substantially parallel to the axis of the cyclone body, as depicted in FIG. 3.
  • the vertical slot lengths usually range from 5% to 25% of the length of the cyclone body.
  • the lower ends of the rectangular slots are adjacent to the closed bottom of the cyclone body.
  • FIG. 4 An example of this desired configuration is illustrated in FIG. 4, where the slots 114 also have edges 200 that are beveled (i.e. not normal to the line tangent to the circular cross section of the cyclone body 106 where the slots 114 are located). This beveling with respect to the curvature of the cyclone body 106 has the desired effect of allowing gas to exit the cyclone body 106 with a significant tangential velocity component and minimal change from the direction of gas flow within the cyclone body. Also, the leading edge along the principal length of
  • each rectangular slot may be slightly raised from the general curvature of the cyclone body to divert the gas flow in the desired tangential direction.
  • the trailing edge of the slot may be sunk into the general curvature for a similar effect.
  • the total open area through which spinning gas may be discharged is preferably from 0.05% to 5% of the surface area of the cyclone body. This parameter, of course, depends on several factors including solid contaminant
  • the separator performance efficiency preferably includes a d50 particle size of below 5 microns.
  • the d50 value represents the diameter of a dust particle that is 50% removed in the underflow gas of the TSS.
  • the purified gas stream has a concentration of particles of 5 microns or greater that is less than 50% of the concentration of particles of
  • This gas contained 300-400 mg/Nm ⁇ of solids with a median particle diameter of 10-20 microns. After exiting the swirl vanes near the gas
  • the gas velocity gas was accelerated due to the flow restriction effected by these vanes.
  • the cyclone separator of the present invention is superior for removing particulates of 4-5 microns in diameter, which are relevant for the overall improvement of FCC third stage separator designs.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Cyclones (AREA)

Abstract

La présente invention concerne un séparateur à cyclone destiné à être utilisé entre une plaque tubulaire supérieure (102) et une plaque tubulaire inférieure (104), le cyclone (100) comprenant: un corps de cyclone sensiblement vertical (106) présentant une extrémité inférieure fermée (108) ainsi qu'une extrémité supérieure (110) fixée par rapport à la plaque tubulaire supérieure (102), le corps (106) du cyclone définissant une entrée (112) de gaz d'alimentation au niveau de son extrémité supérieure (110), l'entrée (112) de gaz d'alimentation s'étendant au-dessus de la plaque tubulaire supérieure (102) afin de recevoir de celle-ci un flux de gaz contaminé par des particules, le corps (106) du cyclone définissant également une paroi latérale du corps de cyclone, la paroi latérale définissant une pluralité d'orifices de décharge (114) situés entre la plaque tubulaire supérieure (102) et la plaque tubulaire inférieure (104) afin de décharger des particules ainsi qu'une quantité mineure d'un flux de gaz de fond; une ou plusieurs aubes de tourbillonnement (116) situées à proximité de l'entrée (112) de gaz destinées à induire une accélération centripète du flux de gaz contaminé par des particules; un tube de sortie (118) de gaz définissant une extrémité d'entrée (120) de gaz propre située centralement à l'intérieur du corps (106) du cyclone afin de recevoir un flux de gaz purifié et définissant également une sortie (122) de gaz propre située sous la plaque tubulaire inférieure (104) pour décharger le flux de gaz purifié, le tube de sortie (118) de gaz s'étendant à travers l'extrémité inférieure fermée (108) du corps (106) du cyclone et s'étendant également à travers la plaque tubulaire inférieure (108).
EP02736482A 2002-01-24 2002-01-24 Separation de fines matieres particulaires solides d'un flux de gaz Withdrawn EP1472004A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2002/002232 WO2003066225A1 (fr) 2002-01-24 2002-01-24 Separation de fines matieres particulaires solides d'un flux de gaz

Publications (1)

Publication Number Publication Date
EP1472004A1 true EP1472004A1 (fr) 2004-11-03

Family

ID=27732062

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02736482A Withdrawn EP1472004A1 (fr) 2002-01-24 2002-01-24 Separation de fines matieres particulaires solides d'un flux de gaz

Country Status (5)

Country Link
EP (1) EP1472004A1 (fr)
CN (1) CN1287902C (fr)
AU (1) AU2002309484A1 (fr)
CA (1) CA2477482A1 (fr)
WO (1) WO2003066225A1 (fr)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20090064082A (ko) * 2007-12-14 2009-06-18 현대자동차주식회사 엔진의 흡기 덕트 시스템
US8419835B2 (en) 2010-08-10 2013-04-16 Uop Llc Apparatuses and methods for gas-solid separations using cyclones
CN102343188A (zh) * 2011-10-27 2012-02-08 北京德天御投资管理有限责任公司 一种用于管道上的除尘装置
US8709115B2 (en) * 2011-12-16 2014-04-29 Uop Llc Cyclone separators and separator apparatuses including the cyclone separators
CN108499750B (zh) * 2017-02-27 2019-12-20 松下知识产权经营株式会社 分离装置
US10688504B2 (en) * 2017-09-30 2020-06-23 Uop Llc Apparatus and process for gas-solids separation
CN109174478A (zh) * 2018-08-28 2019-01-11 中石化（洛阳）科技有限公司 一种组合式直流分离单管及旋风分离器
CN113041759B (zh) * 2019-12-27 2024-05-28 中国石油大学(北京) 多管式旋风分离器底流气固分离方法及分离装置
CN111495040B (zh) * 2020-04-30 2021-03-16 西安交通大学 一种水平管道式气液分离装置和方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2632214B1 (fr) * 1988-06-02 1992-07-10 Cyclofil Pty Ltd Dispositif de separation a tube a tourbillon
US5514271A (en) * 1994-04-28 1996-05-07 Mobil Oil Corporation Underflow cyclone with perforated barrel
US5538696A (en) * 1994-05-02 1996-07-23 Mobil Oil Corporation FCC process and apparatus with contained vortex third stage separator
AUPN474095A0 (en) * 1995-08-09 1995-08-31 Barnes, Peter Haddon Improved dust separator for process flue gas

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO03066225A1 *

Also Published As

Publication number Publication date
CN1287902C (zh) 2006-12-06
WO2003066225A1 (fr) 2003-08-14
CN1622860A (zh) 2005-06-01
CA2477482A1 (fr) 2003-08-14
AU2002309484A1 (en) 2003-09-02

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