EP0461004A1 - Gleichstrom zyklonische Abtrennvorrichtung und ihre Anwendungen - Google Patents

Gleichstrom zyklonische Abtrennvorrichtung und ihre Anwendungen Download PDF

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Publication number
EP0461004A1
EP0461004A1 EP91401389A EP91401389A EP0461004A1 EP 0461004 A1 EP0461004 A1 EP 0461004A1 EP 91401389 A EP91401389 A EP 91401389A EP 91401389 A EP91401389 A EP 91401389A EP 0461004 A1 EP0461004 A1 EP 0461004A1
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EP
European Patent Office
Prior art keywords
phase
mixture
enclosure
mixer
separator
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Granted
Application number
EP91401389A
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English (en)
French (fr)
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EP0461004B1 (de
Inventor
Thierry Gauthier
Maurice Bergougnou
Cédric Briens
Pierre Galtier
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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    • 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
    • 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
    • B04C3/02—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 with heating or cooling, e.g. quenching, means
    • 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
    • B04C7/00—Apparatus not provided for in group B04C1/00, B04C3/00, or B04C5/00; Multiple arrangements not provided for in one of the groups B04C1/00, B04C3/00, or B04C5/00; Combinations of apparatus covered by two or more of the groups B04C1/00, B04C3/00, or B04C5/00
    • 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
    • B04C2003/003—Shapes or dimensions of vortex chambers

Definitions

  • the present invention relates to a co-current cyclonic mixer-separator.
  • This chemical engineering equipment is an apparatus allowing the separation of a dense phase D1 contained in a first mixture M1 containing said dense phase D1 and a light phase L1, and the mixing of said light phase L1 with a dense phase D2 or with a second mixture M2 containing a dense phase D2 and a light phase L2.
  • the present invention also relates to the use of this mixer-separator (hereinafter referred to as the apparatus) for the rapid exchange of heat between a light phase L1 and a dense phase D2 or a mixture M2 containing at least one dense phase D2 and at least one light phase L2 (for example the ultra-rapid quenching of a gas by injection of a cold solid). It also relates to the use of this device for the rapid exchange or replacement of a dense phase D1 by another dense phase D2 different from D1 (for example from one solid to another) in a mixture containing a dense phase and a light phase (for example a reaction phase comprising a catalyst which is replaced very quickly by another catalyst or by the same less used catalyst).
  • this mixer-separator hereinafter referred to as the apparatus for the rapid exchange of heat between a light phase L1 and a dense phase D2 or a mixture M2 containing at least one dense phase D2 and at least one light phase L2 (for example the ultra-rapid quenching of
  • the apparatus of the present invention can thus be used in the process, called ultra-pyrolysis, described for example by Graham et al, World Fluidization Conference, May 1986, Elsinore Denmark, which is a high temperature cracking process, at l fluidized state and with residence times of the gas in the reactor of less than one second.
  • the heat of reaction is usually supplied by a solid coolant mixed with the charge at the inlet of the reactor, which causes a thermomechanical shock thereon.
  • separation and quenching should be as close together as possible.
  • the apparatus of the present invention allows an improvement in the efficiency of quenching and a simplification of the apparatus by grouping together in the same device the two functions of separation of gaseous products and hot solids and of ultra-rapid quenching of gaseous products by cold solids.
  • the apparatus makes it possible to separate the gaseous products of the reaction from the hot solids, and to inject very efficiently cold solids into the gaseous products of the reaction, using a modified cyclone.
  • the vortex induced to separate the hot solids from the gaseous products thanks to the centrifugal force and the differences in density of the two phases, is also used to efficiently mix the cold solids injected above the gas outlet and obtain very good heat transfer.
  • the separation of the hot gas-solid mixture and the cold gas-solid mixture thus take place in the same equipment and practically simultaneously.
  • the quenching of the gaseous products is therefore practically instantaneous, which allows the reaction to be stopped at the separator without significantly affecting the thermal efficiency of the hot part of the process, the hot solids not undergoing quenching.
  • FIGS. 1A, 1B, 2 and 3 in which the members similar are designated by the same reference numbers and letters.
  • Figure 1A is a perspective view of an apparatus according to the invention.
  • FIG. 1B is a perspective view of an apparatus according to the invention which differs from that shown in FIG. 1A only by the means of outlet (7) of the dense phase D1 introduced by the conduit (1), said means (7 ) allowing in the embodiment shown diagrammatically in FIG. 1A a lateral outlet (10) from the dense phase D1 and in that shown schematically in FIG. 1B an axial outlet (10) from this phase.
  • FIG. 2 is a sectional view of an apparatus according to the invention practically identical to that shown in FIG. 1A but comprising means (6) whose dimension in the direction perpendicular to the axis of the apparatus is less than the dimension of the external output (5).
  • the devices according to the invention shown diagrammatically in FIGS. 1A and 2, of elongated shapes, substantially regular, along an axis (AA ′) which is an axis of symmetry, comprise an outer enclosure, of diameter (Dc) and of length (L) having a tangential inlet (1) called external inlet, into which is introduced, in a direction substantially perpendicular to the axis of the apparatus, the mixture M1 containing at least one dense phase D1 and at least one phase slight L1.
  • This tangential entry preferably has a rectangular or square section whose side parallel to the axis of the device has a dimension (Lk) usually from about 0.25 to about 1 times the diameter (Dc), and the perpendicular side the axis of the device has a dimension (hk) usually from about 0.05 to about 0.5 times the diameter (Dc).
  • the mixture M1 thus introduced is wound around a first internal enclosure, arranged coaxially with respect to the external enclosure, having an axial inlet (3), called the first internal inlet, allowing the introduction of at least one dense phase D2 or preferably at least one mixture M2 containing a dense phase D2 and a light phase L2.
  • This dense phase D2 or this mixture M2 circulates parallel to the axis (AA ′) of the device to the first internal outlet (3 ′) of diameter (Di) less than the diameter (Dc) of the outer enclosure of the apparatus and usually from about 0.05 to about 0.9 times this diameter (Dc) and preferably from about 0.4 to about 0.8 times this diameter (Dc).
  • the length (Li), between the extreme level of the tangential inlet (1) and the first internal outlet, is less than (L) and is usually about 0.2 to about 9.5 times the diameter (Dc) and preferably from about 1 to about 3 times this diameter (Dc).
  • the dense phase D2 or the mixture M2 then penetrates at least partially into the second interior enclosure, arranged coaxially with respect to the first interior enclosure, by the second internal inlet (4) located at a distance (Le) from the first internal outlet. (3 ′), this distance preferably being approximately 0.2 to approximately 2 times the diameter (Dc).
  • This second enclosure also penetrates at least part of the light phase L1.
  • This second internal inlet (4) has an internal diameter (De) greater than or equal to (Di) and less than (Dc) and usually about 0.2 to about 0.9 times the diameter (Dc).
  • This diameter (Di) is preferably about 0.4 to about 0.8 times the diameter (Dc).
  • a mixture comprising at least part of the light phase L1 and at least part of the dense phase D2 or of the mixture M2 comprising a dense phase D2 and a light phase is recovered by the second internal outlet (4 ′) of the apparatus. L2.
  • the device comprises, downstream, in the direction of flow of the various phases, from the second internal input, means (6) limiting the progression of the light phase L1 in the space located between the internal wall of the external enclosure and the external wall of the second internal enclosure or external outlet (5).
  • These means (6) are preferably substantially planar blades whose plane includes the axis of the device.
  • These means (6) are usually fixed on at least one wall of one of the interior or exterior enclosures.
  • These means (6) are preferably fixed to the external wall of the second internal enclosure so that the distance (Lp) between the second internal inlet and the point of said blades closest to this second internal inlet is approximately 0 to about 5 times the diameter (Dc) and preferably about 0.1 to about 1 time this diameter (Dc).
  • the number of blades is variable according to the distribution of the residence time which is accepted for phase L1 and also according to the diameter (Dc) of the external enclosure. If the residence time of phase L1 can have a wide distribution then it will not be essential to have blades.
  • the number of blades is usually between 0 and about 50, most often, when blades are present, at least 2 and for example from 2 to about 50 and preferably from 3 to about 50.
  • the blades will allow, by limiting the continuation of the vortex over the entire section of the cyclone, around the internal outlet (4) of the light phase, a reduction and a control of the distribution of the residence times and consequently the degradation of the products contained in the light phase circulating around the internal outlet will be limited.
  • Each of these blades usually has a dimension or width (ep) measured in the direction perpendicular to the axis of the device and defined with respect to the inner diameter (Dc) of the outer enclosure and the outer diameter (D'e) of the second interior enclosure, approximately 0.01 to 1 times the value [((Dc) - (D'e)) / 2] of the half difference of these diameters (Dc) and (D'e), of preferably about 0.5 to 1 time this value and most often about 0.9 to 1 time this value.
  • These blades each have on their edge, the closest to the axis of the interior enclosures, in the direction parallel to this axis, an internal dimension or height (hpi) and an external dimension or height (hpe) measured in the direction of l 'axis of the device on the edge of said blade closest to the inner wall of the outer enclosure.
  • These dimensions (hpi) and (hpe) are usually greater than 0.1 times the diameter (Dc) and for example approximately 0.1 times to approximately 10 times the diameter (Dc) and most often approximately 1 to about 4 times this diameter (Dc).
  • these blades each have a dimension (hpi) greater than or equal to their dimension (hpe).
  • the device comprises, downstream, in the direction of flow of the various phases, from the second internal inlet, means (8) allowing the possible introduction of a light phase L3 at at least one point located between the second internal input (4) of the second internal enclosure and the external output (10) of the dense phase D1; this or these points are preferably at a distance (Lz) from the inlet (4) of the second interior enclosure.
  • Said distance (Lz) preferably has a value at least equal to the sum of the values of (Lp) and (hpi) and at most equal to the distance between the input (4) of the second interior enclosure and the output means (7) of the dense phase D1.
  • This phase light L3 can be introduced for example in the case where it is desirable to carry out a stripping of the dense phase D1.
  • the light phase L3 is preferably introduced at several points which are usually distributed symmetrically, in a plane at the level of which the introduction is carried out, around the external enclosure.
  • the point or points of introduction of this light phase L3 are usually located at a distance at least equal to 0.1 times the diameter (Dc) of the inlet (4) of the second interior enclosure when the device does not have means (6) or the point of said means (6) closest to the means (7) for outputting the dense phase D1 when the apparatus includes means (6).
  • the point or points of introduction of this light phase L3 are preferably located near the external outlet (10) and most often near the outlet means (7) of the dense phase D1.
  • the dimension (p ′) between the level of the second internal input (4) and the means (7) for outputting the dense phase D1 is determined from the other dimensions of the various means forming the device and the length (L ) of the outer enclosure measured between the extreme level of the tangential input (1) and the means (7) for outputting the dense phase D1.
  • This dimension (L) is usually about 1 to about 35 times the diameter (Dc) of the outer enclosure and most often about 1 to 25 times this diameter (Dc).
  • the means (6) limit the progression of the vortex of the light phase L1 in the external output (5).
  • the position of these means (6) and their number therefore influence the performance of the separation of phases D1 and L1 contained in the mixture M1 (pressure drop and efficiency of collection of the dense phase D1) and also on the penetration of the vortex of the light phase L1 in the outlet (5).
  • These parameters will therefore be carefully chosen by those skilled in the art, in particular as a function of the desired results and of the tolerated pressure drop.
  • D1 is a solid
  • the number of blades, their shape and their position will be chosen with care taking into account their influence on the flow of the solid in connection with the desired limitation of the progression of the vortex in the external output ( 5).
  • FIG 3 is a perspective view of an apparatus according to the invention comprising an outer enclosure, of diameter (Dc) having an inlet (1) called axial external inlet, into which is introduced in a direction substantially parallel to the axis (AA ′) of the apparatus, the mixture M1 containing a dense phase D1 and a light phase L1.
  • This device also comprises means (2) placed inside the entrance (1) in the space located between the internal wall of the external enclosure and the external wall of the first internal enclosure making it possible to confer downstream , in the direction of circulation of said mixture M1, a helical or swirling movement at least in phase L1 of said mixture M1.
  • These means are usually inclined blades.
  • the length L of the device is counted between these means making it possible to create a vortex, at least on the phase L1, and the means (7) for outputting the dense phase D1.
  • This device does not include means (6) for limiting the penetration of the vortex into the external outlet (5). All the other characteristics are identical to those described in connection with the devices shown in FIGS. 1A and 2, in particular the various dimensions are those mentioned in the description of these devices.
  • the variants described in connection with the devices shown in FIGS. 1A and 2 are also possible in the case of the device according to the present invention shown diagrammatically in FIG. 3.
  • the output means (7) of the dense phase D1 usually make it possible to collect and channel this dense phase D1 to the external output (10). These means are most often an inclined bottom or a cone focused or not on the internal outlet (4 ′).
  • the devices according to the present invention thus allow the transfer of heat and / or material between the various phases present.
  • These phases are, for the light phases L1, L2 and L3 of the liquid, gaseous phases or phases containing both liquid and gas, and for the dense phases D1 and D2 of the solid phases (under particle form), liquids or phases containing both solid and liquid.
  • Two cases are frequently encountered: the first in which the dense phases are solids and the light phases of gases and the second in which there is a liquid phase which can be the dense phase or the light phase.
  • the apparatuses of the present invention shown diagrammatically in the appended figures have a single axis (AA ′) but it would not go beyond the scope of the present invention in the case where an apparatus comprising several axes, for example making an angle between them, is produced.
  • the axis (AA ′) mentioned above would be the axis of the part of the device located between the first internal inlet (3) and the first internal outlet (3 ′) and the diameter value (Dc ) would be that measured at this internal output (3 ′), this axis (AA ′) also remaining in this case the axis of the second interior enclosure, the two interior enclosures remaining arranged coaxially (such a case is for example that of a device comprising an angled external enclosure).
  • the diameter (Dc) of the device measured at the first internal outlet (3 ′) is usually about 0.01 to about 10 m (meters) and most often about 0.05 to about 2 m . It is usually preferable to keep a constant diameter over the entire length (L) of the apparatus or even from the level of injection of the mixture M1 to the level of the means (7) for outputting the dense phase D1; however, it would not be departing from the scope of the invention in the case of an apparatus comprising enlargements or narrowing of sections between said levels.
  • phase L1 contained in a mixture M1 also comprising at least one phase D1 and an effective mixture of this phase L1 with at least one phase D2 it is preferable to have a surface velocity of entry of this phase L1 high and for example from approximately 5 to approximately 150 mxs ⁇ 1 (meter per second) and preferably from approximately 10 to approximately 75 mxs -1.
  • the weight ratio of the flow from phase D1 to the flow from phase L1 is usually from about 0.0001: 1 to about 50: 1 and most often from about 0.1: 1 to about 15: 1.
  • flow rate of phase D2 usually represents by weight of approximately 0.1 to approximately 1000% of the flow rate of phase D1 and most often approximately 10 to approximately 300% of the flow from phase D1.
  • the surface speed V2 will preferably be from about 5 to about 150% of the speed V1.
  • phase L1 withdrawn with phase D1 The pressure variations allowing to play on the quantity of phase L1 withdrawn with phase D1 are ensured by means well known to those skilled in the art and for example by varying the quenching temperature by modifying the flow rates of phases L2 and / or D2, or by modifying the flow rate of phase L3, or by modifying the operating conditions downstream of the output (10).
  • the apparatus will comprise at least one means allowing the withdrawal, by the external output, of at least part of the light phase L1 in admixture with the dense phase D1.
  • the choice between a device comprising a tangential inlet, for the mixture M1, and a device comprising an axial inlet, for this mixture M1, is usually guided by the weight ratio of the flow rates of the phases L1 and D1. If this ratio is less than 2: 1, it may be advantageous to choose a device with axial input.
  • FIGS. 1A and 2 Two apparatuses are produced, with vertical axes, in accordance with those shown diagrammatically in FIGS. 1A and 2 comprising a tangential entry with a roof descending on 3/4 of a turn regularly over a height equal to the value of Lk. These devices have the geometrical characteristics mentioned in Table I below.
  • inlet temperature T heat capacity: Cp thermal conductivity: k mass flow: F volume flow: Q density: R surface speed: V diameter of jumping particles: ds
  • ED1 separation efficiency of D1 in the device (ratio of the mass flow of D1 measured in the external output (10) to the mass flow of D1 introduced into l 'tangential input (1)) with a withdrawal of phase L1 in the external output (10) of 2% by weight relative to the weight of L1 introduced into the tangential input (1).
  • Pvortex distance between the end of the vortex of L1 in the external output (5) and the top of the second internal input (4).
  • Tempering temperature of the gas mixture formed by L1 and L2 measured at a distance of 1 m from the top of the second internal inlet (4).

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EP91401389A 1990-06-05 1991-05-29 Gleichstrom zyklonische Abtrennvorrichtung und ihre Anwendungen Expired - Lifetime EP0461004B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9006938A FR2662619B1 (fr) 1990-06-05 1990-06-05 Melangeur-separateur cyclonique a co-courant et ses applications.
FR9006938 1990-06-05

Publications (2)

Publication Number Publication Date
EP0461004A1 true EP0461004A1 (de) 1991-12-11
EP0461004B1 EP0461004B1 (de) 1995-08-30

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EP91401389A Expired - Lifetime EP0461004B1 (de) 1990-06-05 1991-05-29 Gleichstrom zyklonische Abtrennvorrichtung und ihre Anwendungen

Country Status (7)

Country Link
US (1) US5186836A (de)
EP (1) EP0461004B1 (de)
JP (1) JP3362259B2 (de)
CA (1) CA2043880C (de)
DE (1) DE69112498T2 (de)
ES (1) ES2079596T3 (de)
FR (1) FR2662619B1 (de)

Cited By (6)

* Cited by examiner, † Cited by third party
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FR2678280A1 (fr) * 1991-06-27 1992-12-31 Inst Francais Du Petrole Procede et dispositif pour le craquage catalytique d'une charge d'hydrocarbures utilisant un separateur cyclonique a co-courant.
WO1999022873A1 (en) * 1997-11-04 1999-05-14 B.H.R. Group Limited Cyclone separator
AU724082B3 (en) * 2000-01-18 2000-09-14 Westdeen Holdings Pty Ltd Soil sample collection device
US6531066B1 (en) 1997-11-04 2003-03-11 B.H.R. Group Limited Cyclone separator
CN101489645B (zh) * 2006-07-12 2011-04-27 财团法人国际石油交流中心 气固分离器
EP2342006A1 (de) * 2008-10-30 2011-07-13 Jean-Xavier Morin Wirbelschichtvorrichtung mit schneller verwirbelung und gesättigtem strom von zirkulierenden feststoffen

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FR2672590B1 (fr) * 1991-02-07 1993-04-23 Inst Francais Du Petrole Procede et dispositif de conversion catalytique en lit entraine d'une charge contenant un compose oxygene.
FR2684566B1 (fr) * 1991-12-05 1994-02-25 Institut Francais Petrole Separateur extracteur cyclonique a co-courant.
EP0887096A1 (de) * 1997-06-27 1998-12-30 Merpro Products Limited Vorrichtung und Verfahren zur Trennung einer Mischung einer weniger dichten Flüssigkeit und einer dichteren Flüssigkeit
US6238579B1 (en) * 1998-05-12 2001-05-29 Mba Polymers, Inc. Device for separating solid particles in a fluid stream
FR2798864B1 (fr) * 1999-09-24 2001-12-14 Inst Francais Du Petrole Systeme de separation gaz/liquide intervenant dans un procede de conversion d'hydrocarbures
US6331196B1 (en) * 2000-06-01 2001-12-18 Negev Tornado Ltd. Low turbulence co-current cyclone separator
US6379567B1 (en) * 2000-08-18 2002-04-30 Thomas Randall Crites Circular hydro-petroleum separation filter
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US7465391B2 (en) * 2005-09-09 2008-12-16 Cds Technologies, Inc. Apparatus for separating solids from flowing liquids
JP4854408B2 (ja) 2006-07-12 2012-01-18 財団法人 国際石油交流センター 気固分離器の設計方法
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EP2342006A1 (de) * 2008-10-30 2011-07-13 Jean-Xavier Morin Wirbelschichtvorrichtung mit schneller verwirbelung und gesättigtem strom von zirkulierenden feststoffen

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DE69112498D1 (de) 1995-10-05
EP0461004B1 (de) 1995-08-30
JPH04227868A (ja) 1992-08-17
DE69112498T2 (de) 1996-03-14
US5186836A (en) 1993-02-16
CA2043880A1 (fr) 1991-12-06
FR2662619A1 (fr) 1991-12-06
ES2079596T3 (es) 1996-01-16
JP3362259B2 (ja) 2003-01-07
FR2662619B1 (fr) 1993-02-05
CA2043880C (fr) 2001-07-24

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