EP0287462A2 - Verfahren und Vorrichtung zur Zentrifugaltrennung einer Mischung von mehreren Phasen - Google Patents

Verfahren und Vorrichtung zur Zentrifugaltrennung einer Mischung von mehreren Phasen Download PDF

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Publication number
EP0287462A2
EP0287462A2 EP88400890A EP88400890A EP0287462A2 EP 0287462 A2 EP0287462 A2 EP 0287462A2 EP 88400890 A EP88400890 A EP 88400890A EP 88400890 A EP88400890 A EP 88400890A EP 0287462 A2 EP0287462 A2 EP 0287462A2
Authority
EP
European Patent Office
Prior art keywords
rotor
mixture
disc
upstream
downstream
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.)
Ceased
Application number
EP88400890A
Other languages
English (en)
French (fr)
Other versions
EP0287462A3 (de
Inventor
Pierre Saget
Guy Ranger
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.)
Commissariat a lEnergie Atomique et aux Energies Alternatives CEA
Original Assignee
Commissariat a lEnergie Atomique CEA
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 Commissariat a lEnergie Atomique CEA filed Critical Commissariat a lEnergie Atomique CEA
Publication of EP0287462A2 publication Critical patent/EP0287462A2/de
Publication of EP0287462A3 publication Critical patent/EP0287462A3/de
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B5/00—Other centrifuges
    • B04B5/12—Centrifuges in which rotors other than bowls generate centrifugal effects in stationary containers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B5/00—Other centrifuges
    • B04B5/12—Centrifuges in which rotors other than bowls generate centrifugal effects in stationary containers
    • B04B2005/125—Centrifuges in which rotors other than bowls generate centrifugal effects in stationary containers the rotors comprising separating walls

Definitions

  • Centrifugal separation methods and devices are known at the present time in which the mixture to be treated is rotated through a rotor in order to create an intense centrifugal field inside the mixture.
  • This, bearing the general reference 10 first comprises a substantially cylindrical enclosure 12 and arranged vertically, the mixture to be treated arriving at the lower part of this enclosure via a pipe 14.
  • the centrifuge device proper, bearing the reference 16 is located above the enclosure 12. It is rotated by a motor assembly 18 connected to the device 16 by a bearing system 20.
  • a pipe 22 makes it possible to create a pressure drop through the device 16 thanks to a fan (not shown) and to extract the mixture which has passed through the centrifuge device 16.
  • part of the mixture extracted by the pipe 22 can be recycled by means of a pipe 24 opening into the pipe 14.
  • the heavy dust or phases which have been separated by the device 16 fall into a space 26 at least partially surrounding the enclosure 12 and, from there, fall into a cyclone or other equivalent device 26 by the i ntermediate of a pipe 28.
  • a pipe 30 to the part bottom of cyclone 26 allows dust or heavy phases to be removed, while part of the gas passing through cyclone 26 can be returned to line 14 (in the example illustrated here, the latter is arranged so as to connect the upper part of cyclone 26 to the lower part of enclosure 12). It can also be seen in FIG.
  • a filter 34 can be provided immediately below the device 16, that is to say upstream thereof if we consider the direction of flow of the mixture at through this device.
  • This may include, as described for example in document FR-A-2 468 410, a stack of discs 17 arranged so that a pressure drop between the upstream and downstream of the stack causes the passage of the mixture through this stack following helical veins.
  • a rotary inlet distributor 19 can be provided upstream of the stack of discs 17 and a rectifier 21 immediately downstream of this stack.
  • Figure 2 is a developed section of the stack of discs and Figure 3 a section along line III-III of Figure 2.
  • the stack consists of a series of discs 36 each consisting of a thin plate located a certain distance from the adjacent upstream and downstream discs.
  • Each disc 36 has a number of openings 38 angularly offset from each other and arranged in staggered rows from one disc to the next.
  • a solid part 40a of the disc 36a ( Figure 2) is located immediately below an opening 38b of the disc 36b.
  • the slope of the veins relative to the discs is equal to 1/3.
  • the mixture is divided into a number of live veins 42 passing through the openings 38 of the discs 36. Between the live veins 42 are dead veins 44 in which the gas does not flow continuously, but where the presence of vortices 46 is noted.
  • the orientation of the veins is disturbed and they mix.
  • the heavy phases present in the vortex veins are ejected more efficiently than in the case of Figure 3 and quickly meet a solid surface on which they agglomerate and are guided gradually to the periphery.
  • the present invention aims to further improve the separation by providing a method and a device for centrifugal separation of a mixture of several phases leading to a more efficient and more selective separation.
  • Another object of the invention is to improve the efficiency of separation of phases having very similar specific masses, as well as the evacuation of the separated product out of the treatment zone without risk of remixing.
  • the subject of the invention is a process for centrifugal separation of a mixture of several phases comprising at least one heavy phase in which the mixture is passed through a rotor rotating at a given speed, the mixture being divided into a plurality of parallel veins flowing through the rotor along helical paths and being driven to an angular speed higher than that of the rotor.
  • This has the effect of creating a centrifugal field inside the veins, which allows the ejection of the heavy phase.
  • the veins are limited by solid walls linked to the rotor, a centrifugal field being thus created on the surface of these solid walls, and the heavy phase ejected under the action of the centrifugal field prevailing in the veins is collected on trap elements associated with the solid walls; in addition, it is guided towards the periphery of the rotor by guiding devices associated with these walls, the heavy phase moving towards the periphery of the rotor under the effect of the centrifugal field created on the surface of these walls.
  • the helical flow of the mixture is transformed into axial flow downstream of the rotor.
  • the kinetic energy of rotation of the mixture is recovered at the outlet of the rotor to drive the latter in rotation.
  • the invention also relates to a device for implementing this method.
  • This device comprises, in a known manner: - a rotor through which the mixture to be treated can pass, means for creating a pressure drop through this rotor, the latter being arranged so that the mixture passes through it by following helical veins under the effect of this pressure drop, and means for driving the rotor in rotation about an axis.
  • the rotor comprises: - solid walls limiting said helical veins, - trap elements, associated with these walls, for collecting said heavy phase, and - guide elements associated with these walls, to guide said heavy phase towards the periphery of the rotor.
  • the rotor comprises a set of contiguous discs whose axis coincides with the axis of rotation of the rotor, each disc having an upstream face and a downstream face and comprising at least one channel for circulation of the mixture. disposed along a portion of a propeller and limited by solid walls, this channel opening onto the upstream face by an inlet openwork and on the downstream face by an outlet openwork.
  • the outlet opening of a channel formed in a given disc is immediately opposite the entry opening of a channel formed in the next disc, said openings having the same shape.
  • the expression “contiguous disks” it means that two consecutive disks of the stack are in contact with one another on at least part of their surface.
  • the discs are in peripheral contact thanks to studs formed on the upstream face of one and which rest on the downstream face of the other, these studs being separated by slots allowing the extraction of certain particles.
  • each disc can be flat and perpendicular to the axis of the rotor.
  • the upstream and downstream faces of each disc can be designed so as to present a part in the form of a truncated cone of the same angle at the top and diverging upstream relative to the direction of flow of the mixture. through the rotor.
  • each disc has the form of a hollow circular case comprising: - an entry openwork on its upstream face, - an outlet opening on its downstream face, guiding means forcing the mixture to perform at least one complete revolution inside the disc between these two openings, - a set of elements in the form of truncated cones, located inside the housing and diverging upstream, and - a peripheral slot for the ejection of the heavy phase.
  • This device can also comprise, upstream of the rotor, a rotary distributor comprising a set of blades oriented from the center towards the periphery and whose concavity opens downstream, each blade having a trailing edge whose inclination corresponds to the slope of said helical veins relative to the rotor.
  • the trailing edges of the blades are integral with the first upstream disc of the rotor and coincide with the rear edges of the openings provided on the upstream face of this disc.
  • the rotor is placed inside an enclosure having an internal surface which diverges upstream.
  • the internal surface of the enclosure is smooth and of generally conical shape diverging upstream.
  • the internal surface of the enclosure has a set of circular parts, each of which faces the lateral edge of a disc of the rotor, the diameter said circular parts increasing from downstream to upstream.
  • the distance between the edge of a disc and the internal face of the enclosure can be constant or increase regularly from downstream to upstream.
  • the enclosure 12 inside which circulates the mixture to be treated before arriving at the rotor; the space 26 between the enclosure 12 and the enclosure 50 is used for the evacuation of the heavy phases ejected under the effect of the centrifugal fields created inside the mixture and falling by gravity.
  • this trailing edge coincides with the front edge of an inlet opening of the first upstream disc at the lower part of the stack 17: thus, the space between two successive vanes of the distributor 19 constitutes a continuous path with the helical channel, the inlet opening of which is located at this point on the disc.
  • the distributor 19 transforms the axial speed of the mixing upstream of the rotor at helical speed through the rotor, reducing turbulence and corresponding energy losses.
  • the distributor 19 also has a primary heavy phase separation function which it channels towards the periphery. The curvature of the concavity of the vanes 23 and the conformation of their leading edge are established as a function of the aero or hydrodynamic characteristics of the mixture and of the operating regime.
  • a rectifier 21 constituted by a turbine with a given action or degree of reaction can be provided.
  • This rectifier consists of a set of blades 27 whose concavity is turned upstream, if one considers the direction of flow of the mixture through the rotor.
  • Each blade 27 has a leading edge which coincides with the front edge of an outlet perforation on the downstream face of the last disc of the stack 17 and the inclination of this leading edge is equal to the slope of the veins helical following which the mixture circulates inside the rotor. Since the mixture circulates along a helical trajectory, its speed has a tangential component and an axial component.
  • the design of the concavity of the blades 27 is designed so as to cancel the tangential component. There therefore remains only the axial component and the mixture leaves the rectifier 21 in a direction parallel to the axis 52.
  • the enclosure 50 has an internal surface 51 which diverges downwards, that is to say upstream by considering the direction of flow of the mixture through the rotor.
  • the surface 51 has a number of circular parts 53 whose height is equal to the thickness of each disc. There is thus a surface 53 facing the lateral edge of each disc.
  • the diameter of the discs is constant and that of the parts 53 increases from downstream to upstream, which means that the thickness of the space 26 also increases from downstream to upstream by considering the direction of flow of the mixture through the rotor.
  • discs of variable diameter so that the distance between the lateral edge of a disc and the parts 53 of the surface 51 is constant.
  • the openings 65 are distributed equianglely on a given disc and extend from the center to the periphery. They are separated by solid parts 67. If we consider the direction of rotation T of the discs, the outlet opening of a given channel is located downstream of the entry opening. In FIG. 6, the openings 65 are limited by radii of the disc 36 and therefore have a substantially trapezoidal shape, as do the parts 67.
  • Each channel 62 is thus limited by a lower wall 64, an upper wall 66 and two walls lateral 68 and 70.
  • the lower 64 and upper 66 faces are generally helical in shape with the same slope as that of the channels.
  • the first lateral face 68 limiting a channel 62 that is to say that which is closest to the axis of the rotor, is cylindrical and of axis coincident with that of the rotor.
  • the other lateral face 70 is located in the vicinity of the periphery of the disc and it is inclined relative to the axis of the rotor. In other words, it is in the form of a portion of truncated cone diverging upstream if we consider the direction of flow of the mixture through the rotor.
  • the mixture is thus separated into a plurality of helical veins. Since the mixture is subjected on the one hand to the pressure drop through the rotor and, on the other hand, to the effect of driving the latter in rotation, it flows at through the discs with a tangential speed greater than that of the rotor.
  • the absolute tangential speed of a particle located at a radial distance R is: - ⁇ * R if this particle is in a sequestration zone of the mixture, - ⁇ * R + V t if this particle is in the circulating part of the vein, at the tangential speed V t .
  • the choice of these parameters allows, in relation to the regime of the apparatus and the composition of the mixture, to define the preferred helical path of the mixing veins through the openings of a disc.
  • the mixture can continue its journey by crossing the homologous perforation of the next disc, that is to say the one which is offset downstream of the angle of offset of the discs. This offset angle is such that the outlet opening of the first disc is opposite the inlet opening of the second disc.
  • the latter may include curved generators and, if they are straight or curved, concurrent with or left with respect to the axis of rotation with any angle of index.
  • the discs can be delimited by regulated surfaces, such as conics or any balanced surfaces of revolution, which does not can constitute a major difficulty of execution since the discs can be, because of the reduced stresses which they undergo, manufactured by molding and even out of plastic.
  • FIG. 8 shows how steps, projections or other prominent elements can be provided on the lower and / or upper faces of the channels 62.
  • steps 72 on the lower face of the channels 62, but there are identical steps on the upper face, the latter being invisible in FIG. 8.
  • FIGS. 9a to 9d show other possible shapes for these prominent elements.
  • the upper and lower surfaces of the channel 62 have steps whose edges constitute radial edges, that is to say that these edges are perpendicular to the axis of rotation of the rotor.
  • the steps 72 appear as the steps of a spiral staircase whose axis would be that of the rotor. The internal angles of the steps are therefore right angles.
  • steps 72a and 72b on the upper wall of the channel 62
  • the radial vertical surfaces of the bleachers create low-pressure areas which tend to trap impurities in the attached vortex they create.
  • steps 72b on the bottom wall of the channel 62
  • the radial vertical surfaces function as multiple impact separators. They temporarily stop heavy particles or droplets. The agglomeration effect which they bring accelerates the routing towards the periphery of the heavy phases and correlatively improves the overall efficiency of the device.
  • steps 72b of the lower wall are identical to those of FIG. 9a.
  • steps of the upper wall of the channel 62 they have inclined parts 74 whose slope is slightly greater than the slope chosen for the helical veins of the mixture, the parts 74 being connected by parts 76 whose height is less than the width of the parts 74.
  • a chamfer 75 is provided at the lower part of the lower face 64, but this is not compulsory. This arrangement causes alternating diverging and converging oblique zones, which creates a more pronounced undulation of the mixing vein and a higher probability of lateral exit of the heavy fractions which are then collected in the steps.
  • the steps 72 are replaced by grooves 78 of semi-circular section and arranged radially, that is to say that their axis is perpendicular to the axis of rotation of the rotor.
  • the semi-circular radial channels thus created are at the origin of vortex zones which slow down and collect the heavy phases.
  • FIGS 11 and 12 illustrate another embodiment in which each disc 36 is in the form of a hollow circular housing.
  • the disc 36 consists of a lower wall 82 having the shape of a flat disc, connected to an upper wall 84 by a ferrule 86.
  • the upper wall 84 has a central part 87 having the shape of a flat disc of the same axis than the wall 82, but of smaller diameter.
  • the part 87 is connected to a peripheral edge 88 by a part in the form of a truncated cone 90.
  • the edge 88 is circular and of the same diameter as the bottom wall 82. It is separated from the latter by a peripheral slot 92, the width is less than the distance between the lower wall 82 and the central part 87 of the upper wall.
  • a set of elements in the form of a frustoconical cone or frustoconical ferrules 94 is provided inside the housing thus defined.
  • the frustoconical ferrules 94 have an upper edge which is welded to the central part 87 of the upper wall 84 while their lower edge is located at a certain distance from the lower wall 82.
  • FIGS. 11 and 12 also show an inlet opening 63 formed in the bottom wall 82 and an outlet opening 65 formed in the central part 87 of the upper part 84.
  • the angular position of the openings 63 and 65 relative to the disc 36 is exactly the same.
  • a deflector 96 has a lower edge welded to the lower wall 82 behind the perforation 63 and an upper edge welded to the upper wall 84 in front of the perforation 65. Thanks to this arrangement, the mixture which enters the disc by the openwork 63 is forced to do one complete turn, walking in the spaces between the frustoconical ferrules 94 before exiting through the outlet perforation 65.
  • the deflector 96 must ensure a good seal to prevent direct leakage of the mixture from the inlet perforation to the perforation Release. Thanks to this arrangement, the radial displacement of the heavy phases under the action of the centrifugal field brings them into contact with the surface of these ferrules. This contact creates a gathering effect of the heavy phases, which then slide on the surface and are resuspended, but after having been more or less strongly agglomerated. The consequent increase in their particle size accelerates their radial movement towards the periphery of the rotor and correlatively increases the separation efficiency of the device.
  • the frustoconical ferrules 94 also play a role of guiding surface and limiting turbulence, their surface being parallel to the direction of flow of the mixture inside the disc.
  • the average slope per disc is then equal to: at radius R, p being the thickness of the disc.
  • the centrifugal field is also maximum for this configuration, since it is proportional to the square of the sum of the tangential drive speed and the tangential speed of the mixture relative to the rotor.
  • the method and apparatus which are the subject of the invention are usable for separation in a mixture of any state phases.

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  • Centrifugal Separators (AREA)
EP88400890A 1987-04-17 1988-04-13 Verfahren und Vorrichtung zur Zentrifugaltrennung einer Mischung von mehreren Phasen Ceased EP0287462A3 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8705520A FR2613956B1 (fr) 1987-04-17 1987-04-17 Procede et dispositif de separation centrifuge d'un melange de plusieurs phases
FR8705520 1987-04-17

Publications (2)

Publication Number Publication Date
EP0287462A2 true EP0287462A2 (de) 1988-10-19
EP0287462A3 EP0287462A3 (de) 1989-10-25

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Application Number Title Priority Date Filing Date
EP88400890A Ceased EP0287462A3 (de) 1987-04-17 1988-04-13 Verfahren und Vorrichtung zur Zentrifugaltrennung einer Mischung von mehreren Phasen

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EP (1) EP0287462A3 (de)
JP (1) JPS63283771A (de)
KR (1) KR880012273A (de)
FR (1) FR2613956B1 (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2648361A1 (fr) * 1989-06-16 1990-12-21 Alsthom Gec Separateur de particules pour flux gazeux
WO2004063538A3 (de) * 2003-01-11 2004-09-10 Mann & Hummel Gmbh Zentrifugal-ölabscheider
DE102017108168A1 (de) * 2017-04-18 2018-10-18 Hengst Se Rotor eines Zentrifugalabscheiders zum Abscheiden von Flüssigkeits- und/oder Feststoffpartikeln aus einem Gasstrom

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE533471C2 (sv) * 2009-02-05 2010-10-05 Alfa Laval Corp Ab Anläggning för avskiljning av olja från en gasblandning samt förfarande för avskiljning av olja från en gasblandning
SE533562C2 (sv) * 2009-03-06 2010-10-26 Alfa Laval Corp Ab Centrifugalseparator
JP6009458B2 (ja) * 2010-12-30 2016-10-19 セ３テク、シェ、エ、アソシエ、コンスルタン、アン、テクノロジＣ３Ｔｅｃｈ Ｃｈａｉｘ ＆ Ａｓｓｏｃｉｅｓ，Ｃｏｎｓｕｌｔａｎｔｓ Ｅｎ Ｔｅｃｈｎｏｌｏｇｉｅｓ 熱エネルギーを機械的エネルギーに変換するための装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2305237A2 (fr) * 1975-03-28 1976-10-22 Saget Pierre Procede et appareil pour le traitement d'un melange de phases diverses en vue de les separer
FR2468410A1 (fr) * 1979-10-31 1981-05-08 Saget Pierre Procede de separation centrifuge et appareil pour sa mise en oeuvre applicables a un melange de phases d'etats quelconques
FR2575677A1 (fr) * 1985-01-08 1986-07-11 Saget Pierre Appareil separateur centrifuge pour le traitement d'un melange comprenant au moins une phase gazeuse, avec collecte forcee de la phase lourde

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2305237A2 (fr) * 1975-03-28 1976-10-22 Saget Pierre Procede et appareil pour le traitement d'un melange de phases diverses en vue de les separer
FR2468410A1 (fr) * 1979-10-31 1981-05-08 Saget Pierre Procede de separation centrifuge et appareil pour sa mise en oeuvre applicables a un melange de phases d'etats quelconques
FR2575677A1 (fr) * 1985-01-08 1986-07-11 Saget Pierre Appareil separateur centrifuge pour le traitement d'un melange comprenant au moins une phase gazeuse, avec collecte forcee de la phase lourde

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2648361A1 (fr) * 1989-06-16 1990-12-21 Alsthom Gec Separateur de particules pour flux gazeux
WO2004063538A3 (de) * 2003-01-11 2004-09-10 Mann & Hummel Gmbh Zentrifugal-ölabscheider
US7445653B2 (en) 2003-01-11 2008-11-04 Mann & Hummel Gmbh Centrifugal oil separator
DE102017108168A1 (de) * 2017-04-18 2018-10-18 Hengst Se Rotor eines Zentrifugalabscheiders zum Abscheiden von Flüssigkeits- und/oder Feststoffpartikeln aus einem Gasstrom

Also Published As

Publication number Publication date
FR2613956B1 (fr) 1991-05-17
JPS63283771A (ja) 1988-11-21
FR2613956A1 (fr) 1988-10-21
KR880012273A (ko) 1988-11-26
EP0287462A3 (de) 1989-10-25

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