US2967618A - Vortical separator - Google Patents

Vortical separator Download PDF

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US2967618A
US2967618A US1809860A US2967618A US 2967618 A US2967618 A US 2967618A US 1809860 A US1809860 A US 1809860A US 2967618 A US2967618 A US 2967618A
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chamber
carrier
tubes
vortex
density
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Vane Zdenek
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Vane Zdenek
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B04CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04CAPPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00Apparatus in which the axial direction of the vortex (flow following a screw-thread type line) remains unchanged Also 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
    • B04C3/04Multiple arrangement thereof
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D21/00Separation of suspended solid particles from liquids by sedimentation
    • B01D21/26Separation of sediment aided by centrifugal force or centripetal force
    • B01D21/267Separation of sediment aided by centrifugal force or centripetal force by using a cyclone
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D21/00Separation of suspended solid particles from liquids by sedimentation
    • B01D21/30Control equipment
    • B01D21/34Controlling the feed distribution; Controlling the liquid level ; Control of process parameters
    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21DTREATMENT OF THE MATERIALS BEFORE PASSING TO THE PAPER-MAKING MACHINE
    • D21D5/00Purification of the pulp suspension by mechanical means; Apparatus therefor
    • D21D5/18Purification of the pulp suspension by mechanical means; Apparatus therefor with the aid of centrifugal force
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B04CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04CAPPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00Apparatus in which the axial direction of the vortex is reversed
    • B04C5/12Construction of the overflow ducting, e.g. diffusing or spiral exits
    • B04C5/13Construction of the overflow ducting, e.g. diffusing or spiral exits formed as a vortex finder and extending into the vortex chamber; Discharge from vortex finder otherwise than at the top of the cyclone; Devices for controlling the overflow
    • B04C2005/133Adjustable vortex finder

Description

1951 2. VANE 2,967,618

VORTICAL SEPARATOR Filed March 28, 1960 m if? 5 lA/Vt/V 7' 0E zazwex mu:

United States Patent VORTICAL SEPARATOR Zdenek Vane, Box 225, P Station, D, Ottawa, Ontario, Canada Filed Mar. 28, 1960, Ser. No. 18,098

'3 Claims. (Cl. 209-211) This invention relates to a method of multiple density separation by centrifugal force. This application is a continuation-in-part of my co-pending application, Serial No. 628,171, filed December 13, 1956, now abandoned.

In density separations carried out from a spinning column of carrier liquid containing suspended particles, methods of this character show that the cost of a process increases when the spread between the density of the carrier liquid and the separable particles is increasing. In order to decrease the cost, sink-and-float methods have been successfully combined with the centrifugal force for separating components whose respective densities differ only slightly. Thus, the carrier used in such combinations has a density which lies between the densities of the two components to be separated. The carrier alters the lighter one of the two sink components to a float component while the other remains a sink component. As a result, the selected lighter component is located far from the outer periphery of the vortex and close to the center thereof so that the lighter component is intercepted at a sufficient radial distance from the heavier one. This solution requires a special carrier whose density must be maintained at a constant value to preserve its separating capacity and can hardly yield more than two fractions in one separation. character and affords a limited choice only because few true liquids with densities over 2 are available. The suspension-type separatory media consist of finely comminuted solids in a liquid, such as water. To be produced and maintained, these media require an auxiliary equipment, and the cost thereby involved is increased by the necessity to separate the compound carrier from the fractions after the main separation. Many separable materials are excluded from this method since no suitable carrier can be found for them.

In the US. Patent No. 2,843,265, a method is employed for altering the apparent density of a suspensiontype carrying medium during the separation process by a dynamic action, the so-called angular deflection, that consists in increasing the angular velocity of the column, whereby the layer of the selected component is shifted from the outer periphery of the vortex towards its center. The process is based on the assumption that the suspension will behave as a slightly elastic matter which, under the influence of an increased centrifugal tension, will produce a column of carrier whose density is graduated along the radius of the vortex so that the carrier density on the outer periphery of the column is higher than in the central layers thereof.

Unlike the above combinations in the prior art, the present invention works with dynamic means only, using a plain carrier liquid as pure water, both for spinning the suspended separable materials and for effecting the movement of the suspended particles from the outer periphery of the vortex towards its center in the radial direction. This deflection of particles is operated directly by the added carrier, a true liquid, without increasing the angular velocity. The friction of the spinning column on the The expedient has a static.

walls is limited on the carrier only so that the friction of the handled materials on said walls is avoided at least in the separation area. The radius of the column can be large enough thus permitting any desired number of central intercepting members to be placed in position to split, substantially in one point of the flow, the spinning carrier with the stratified material suspended therein into a number of fractions. The trajectory of the spinning material through the separator is very short whereby the wear by abrasion is reduced and the use of an inexpensive medium as water obviates the above inconveniences of the suspension media. The precision of this separation process is further increased by giving the central intercepting members a sliding movement in the axial direction of the vortex chamber so that the influence of any incidental fluctuations in the quality of the feed on the expected result of the process can be prevented, and the wear on the edges of said members can be compensated for. In this method, even materials with very high densities can be successfully handled with clean water as carrier because the lateral pressure on the spinning column can be increased to anydesired degree. It can be variedv also during the process. Finally, this method can be performed with gaseous carriers as well.

It is an object of this invention to provide a method of multiple centrifugal separation from a column of. fine solids suspended in a carrier spinning in free vortex wherein the sink particles, stratified in density layers substantially along the outer periphery of the column, are deflected or shifted in a radially inward direction bythe action of an additional carrier flow coming from outside in the direction of the radius of the vortex.

It is another object of the invention to provide a method of separation wherein the contact of the spinning suspension on the outer wall of the vortex chamber is avoided.

Other advantages of the invention-will be apparent from the following description and accompanying drawing in which the sectional elevation of an apparatus according to the invention is shown.

A vortex chamber 1 is bounded by a shell having a,

circular cross-section and consisting of two portions 2 and 3 which are flanged to form an outer, auxiliary vortex,

chamber 4. The shell portion 3 is provided with a'c'ircular vessel 5, the portion 2 with a cover 6 closing said ber 1 having an uninterrupted circumferential gap 9 whereby the two vortical chambers 1 and 4communicate.

. central intercepting members are-insertedkf These are co-axially-arranged tubes 15 to 18 of different diametersj The upper end of the main chamber 1 is closed by a tight; cover 10 and provided with a horizontal feed conduit '11};

which ends in the chamber 1 by a tangential inlet 12. A variable valve 11' is set inthe conduit 11 to control the rate of the feed. The auxiliary vortex chamber 4is provided with one or more feed pipes 13 supplying an additional fluid flow, volume controlled by a valve 13.

The vortex chamber 1 is closed at its lower end by a bottom 14 in the form of an annular space inwhich a set of and graduated from small to large, each of them being closed at its lower end by a similar bottom in form of an annular space in which the next smaller tube can slide in the axial direction. The length of each of the tubes 15 to 18 depends on its distance from thevortex axis as it can be seen in the drawing, and on its axial slidingmove Each of these spaces has to collect one separated fraction and is drained by an outlet having a flow rate control therein. The outlets are shown by numerals 16", 17", 18'-' and 19" respectively. The correct concentric position and a tight sliding connection is secured for each sliding tube by suitable guides 20 provided with stufiing boxes, not shown in the drawing, or with an equivalent thereof. The tubes are further retained in their co-axial position by sets of radial vanes 21 inserted between the tubes in sets of three or more vanes equally spaced along the circumference of each annular space. These vanes are fastened preferably to the smaller one of each tube couple and at such a distance from their intercepting edges that in no position of the tubes said vanes can proiect out of their respective annular spaces. Suitable spacing between the parting edges of the tubes and the vanes is required, since the latter serve also as spin straightening means in the spaces and must not disturb by their presence the spin in the separation area. The parting edges of tubes are beveled to reduce their resistance to the spinning flow. Suitable devices for moving the tubes 15 to 18 in the axial direction are shown schematically at 22 and an adequate supporting structure 23 completes the equipment of the apparatus. All the flow rate control means mentioned in this description are variable valves of any suitable well known type and are shown in the drawing by symbols only.

In operation, a plain carrier fluid as water or air, with the separable fine material suspended therein, is fed into the chamber 1 through the tangential inlet 12 under pressure and rotated. The sink particles, subject to centrifugal tension, are flung towards the outer periphery of the vortex chamber and take their place in a density spectrum which is quickly formed close to the periphery, according to the density of each of the components. An additional fluid is supplied into the outer vortex chamber 4 by the pipe 13 having a tangential inlet so that the added fluid is rotated in the vortex chamber 4 and introduced into the chamber 1 as a spinning flow having substantially the same angular velocity as the spinning flow in chamber 1. The volume of the added fluid will depend on the spread between densities of the carrier fluid and the lightest sink component. It will normally be twice as much as that entered by inlet 12 in most cases, and considerably more if very heavy components are to be separated. The gap 9 has a uniform width along the whole circumference and said width can be varied by varying the thickness of the packing 7. The added spinning fluid exerts an equal pressure in each point of the gap 9. By a simultaneous operation of the controls 11 and 13, and all the valves in the outlets 15 to 19", the spinning flow is directed in the form of a whirlpool towards the inlets of the central tube 15 and 16. It is achieved when the drain capacity of the outlet 15 is approximately equal to the volume of the added fluid, while the other outlets drain smaller volumes of carrier fluid, totalling that infed at the inlet 12. Due to the pressure maintained within the chamber 1, a relatively small partial vacuum develops in the central part of the shell portion 2. The general direction of the whirlpool is shown in the drawing by dotted lines connecting the gap 9 to the inlet of tube 15. The apex angle of the whirlpool cone is variable to a certain extent by position of the edge of tube 15, and must be maintained so as to suit the pitch of the spin of the mixture fed by inlet 12 to avoid unnecessary turbulence in the separating area. For the same reason, the slope of the bottom of vessel 5, and the bevel of edges defining the gap 9 must suit said apex angle. The density layers of the spinning mixture travel along the wall 2, very close to each other and sometimes intermixed. When they approach the gap 9, they are deflected away from the wall and follow the pull of the whirlpool in the direction of the inlets of tubes 15 and 16. The tube 15 drains the volume of fluid equal to that entering by the gap 9. The spaces 16, 17, 18' and 19 drain together a quantity approximately equal to that supplied by the inlet 12, in fractions decreasing progressively from space 16' to 19 so that the free vortex in the whirlpool is undisturbed. The carrier supplied by inlet 12 is collected by tube 15, while that intercepted by the other spaces is rather a part of that entered by gap 9. The cross-section area of each collecting space is made proportional to the volume to be collected. For a moment, the solids shifted from the wall 2-3 are spinning in the fluid carrier directed radially inwardly. They are thus subject to centrifugal tension which is opposed to the centripetal pull of the whirlpool. In this interaction of the two forces, the density of each particle determines the radial distance which it is deflected from the wall 23. An extended density spectrum is formed and the particles which were originally gathered on the wall 2, are spread in density layers along the major part of the vortex radius when they come out of the whirlpool zone to continue their spin in the axial direction. When the particles are out of said zone, they would tend to return to the wall 3. They can be fractioned in several different manners. If a set of intercepting tubes is arranged to have their parting edges in a straight line parallel with and near to the whirlpool outline shown in the drawing, they will divide the spinning body so that most of the clean carrier fluid with some incidental float particles is intercepted by tube 15, the lightest sink particles entering the space 16', and the heaviest components being deflected only slightly in the radially inward direction, returning to the wall 3 to enter the space 19. The particles with intermediate densities are intercepted by tubes 17 and 18.

The actual arrangement of the parting edges of tubes 15 and 18 shown in the drawing, in combination with the sliding movement of the tubes in axial direction provides a means for an improved density control of the separated fractions, when a heavy particle is shifted by the whirlpool into an intermediate position between the layer traveling in the direction of the space 19 and the space 18'. The particle shows to have an intermediate density between the two fractions. When it is desired to keep the fraction in 19 as clean as possible with exclusion of any middling, said intermediate particles can be attracted by an increased drain in outlet 18" towards the space 18, during the travel of those particles from the whirlpool zone towards the collecting spaces. When, on the contrary, it is desired to keep the fraction in space 18 as clean as possible, an increased drain in outlet 19" will pull the middling towards the space 19. When at the same time the tube 18 is put into advanced position shown by dotted lines in the drawing, only a minimum of particles traveling on the inner periphery of the outer layer will be pulled into the space 18'. In order to protect the layer traveling towards the space 17' against the increased draft in outlet 18", the tube 17 can be risen more or less as the one at 18. When a larger number of intercepting tubes is used than that shown, any one of the tubes pushed into an advanced position divides the separation area under the whirlpool into two parts so that in one part changes of density as that described above can be achieved without disturbing the separation in the other part, even when larger variations in draining capacity of the spaces takes place. Obviously, the sliding movement of the tubes in the axial direction allows for compensation for any wear by abrasion on the tube parting edges. A uniform grain size of the fed fine solids and an undisturbed spin of the carrier in the separation area are prerequisite for a sharp density separation. Therefore, said spin should continue for a small distance within spaces 15 to 19; for that reason the spacing vanes 21 are placed at a sufficient distance from the tube inlets, and the edges are beveled.

The inlet 12 should be as close as possible to the gap 9 so that the infed mixture tends less to cut short its spiralling way towards the inlet of tube 15. The outer vortex chamber 4 can be built separately as a gasket of smaller vertical height and inserted between the shell portions 2 and 3. The space for rotating the added fluid is developed in a radial direction, and has several channels curved as involute discharging from outside circumferentially equally spaced flows to obtain a well equalized spinning flow in the gap 9, directed substantially in right angle towards the axis of the vortex chamber 1.

In a variation of the apparatus shown in the drawing, the fine solids to be separated are fed by a separate feed conduit 24 drawn in dotted lines. The conduit 11 is of smaller size to supply the clean carrier only. The pressure maintained within the chamber 1 is increased to reduce to a minimum any vacuum around said feed conduit 24. A provision must be made that the solids discharged through said conduit cannot fall directly into the inlet of tube 15. A suitable feed conduit meeting this requirement is the object of my co-pending application for patent, Serial No. 712,000, filed January 29, 1958. The fine solids discharged centrally into the spinning clean carrier are rotated by the carrier and, being sink" particles, spread in the radially outward direction within the spinning carrier. The conditions of spin are controlled in such a manner that the particles must reach the whirl pool before they would come in contact with the shell portion 2. Thus, before they reach said wall 2 they are shifted centerwards and the process proceeds as described above. The heaviest fraction after separation can be intercepted by the space 18' instead of space 19; this depends only on flow rate controls by variable valves and on the position of the parting edge of the tube 18.

For very short movements of tubes in the axial direction, the packing in bottoms 14 can be made inexpensive when said bottoms are made of some flexible material such as rubber and fixed to ecah of the adjacent tubes so that the bottom forms a tight fit without any stufling box.

I claim:

1. An apparatus for multiple separation of suspended articles from a fluid carrier by density difference comprising in combination: a closed main vortex chamber having a substantially horizontal top portion, a circular wall section and a bottom portion, tangential feeding.

means in said circular wall section enabling said fluid carrier to spin in said vortex chamber, a continuous circumferential gap in said chamber wall section for discharging an additional fluid carrier into said main chamber, an outer vortex chamber enclosing said gap from outside, feeding means connected to said outer vortex chamber and adapted to supply said additional fluid carrier and to impart it a spin, a series of intercepting tubes in said bottom portion of said main chamber and concentric with each other and with said chamber, said tubes being of difierent lengths and diameters and graduated from small to large having lower ends slidingly connected with each other to form a bottom of said chamber, said tubes thus having a sliding movement along said chamber in an axial direction thereof enabling each of them to be adjusted individually and to control a distance of the upper edge of each of said tubes from said circumferential gap, means to drain products of separation from annular spaces defined by said tubes and by said circular wall of said main chamber, and means to control said sliding movement of said tubes.

2. Apparatus of claim 1 further comprising separate feed means for a mixture of particles treated arranged in said chamber top portion concentrically with said chamber so as to discharge said mixture axially.

3. Apparatus of claim 1 further comprising flexible connectors between said tubes to form a bottom for the main vortex chamber and for each of said annular spaces.

2,843,265 Rakowsky July 15, 1958 Fontein Nov. 6, 1956,

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Cited By (42)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3211535A (en) * 1962-06-18 1965-10-12 Fmc Corp Liquid separation apparatus
US3215272A (en) * 1961-05-16 1965-11-02 Phillips Petroleum Co Process of separation of suspended foreign materials from an aqueous medium
US3438890A (en) * 1965-09-10 1969-04-15 Fmc Corp Method and apparatus for separating solids-liquids mixtures
US3743102A (en) * 1971-03-17 1973-07-03 United Aircraft Corp Vortex separator using core plates
US3784009A (en) * 1971-12-13 1974-01-08 Univ Oklahoma State Hydroclone for separating an immiscible heavy phase from a light phase liquid
US3901799A (en) * 1973-10-29 1975-08-26 Maxie C Adkison Cyclone separator
US3929639A (en) * 1973-07-23 1975-12-30 Gaston County Dyeing Mach Filtering apparatus and process
USB330719I5 (en) * 1971-12-06 1976-03-16
US3990976A (en) * 1974-03-20 1976-11-09 Yasuhito Nishioka Cyclone with plural peripheral discharge tubes
US4087261A (en) * 1976-08-30 1978-05-02 Biphase Engines, Inc. Multi-phase separator
US4120795A (en) * 1977-12-05 1978-10-17 Laval Claude C Device for separating a plural phase fluid system into its constituent phases
DE2900931A1 (en) * 1978-08-24 1980-03-13 Geosource Inc A method and apparatus for mixing materials with solid fliessfaehigen
US4212653A (en) * 1978-06-27 1980-07-15 General Electric Company Process and apparatus for separating particulate matter from gaseous media
US4219340A (en) * 1978-12-14 1980-08-26 Clark & Vicario Corporation Method and apparatus for outflowing liquids from chamber maintained under vacuum
US4317716A (en) * 1979-01-11 1982-03-02 Liller Delbert I Vortex finder and sleeve kit
US4333499A (en) * 1980-04-15 1982-06-08 Conoco Inc. Pressure dissipation apparatus
US4341352A (en) * 1979-08-06 1982-07-27 Liller Delbert I Method of coal washing at low speed pumping
US4378289A (en) * 1981-01-07 1983-03-29 Hunter A Bruce Method and apparatus for centrifugal separation
US4443331A (en) * 1980-03-21 1984-04-17 Centre Technique De L'industries Des Papiers Carton Et Celluloses Process and device for separating particles in a fluid especially for the cleaning of the suspensions handled in the paper industry
US4594149A (en) * 1982-05-21 1986-06-10 Mag-Sep Corp. Apparatus and method employing magnetic fluids for separating particles
DE3623892A1 (en) * 1985-07-16 1987-02-19 Koezponti Banyaszati Fejleszte A method and apparatus for separating the individual phases of multi-phase flowing media
US4789476A (en) * 1985-03-19 1988-12-06 Siegbert Schulz Cyclone separator with two separating zones and static guide mechanisms
US4819808A (en) * 1982-05-21 1989-04-11 Mag-Sep Corp. Apparatus and method employing magnetic fluids for separating particles
US4842738A (en) * 1988-04-29 1989-06-27 Greenspan Harvey P Centrifuge device
US4960525A (en) * 1988-09-26 1990-10-02 The United States Of America, As Represented By The Secretary Of Agriculture Hydrocyclone for washing particles in liquid suspension
US4961841A (en) * 1982-05-21 1990-10-09 Mag-Sep Corporation Apparatus and method employing magnetic fluids for separating particles
US5112498A (en) * 1989-11-28 1992-05-12 Orkney Water Test Centre Limited Method of coalescing a disperse phase within a continous phrase of a fluid mixture
US5224604A (en) * 1990-04-11 1993-07-06 Hydro Processing & Mining Ltd. Apparatus and method for separation of wet and dry particles
US5300222A (en) * 1990-09-28 1994-04-05 Broussard Paul C Sr Water clarification method and apparatus
US5498329A (en) * 1994-09-12 1996-03-12 Interclean Equipment, Inc. Vehicle wash apparatus using reclaimed water
WO1998042424A1 (en) * 1997-03-24 1998-10-01 Rochat Jean Denis Device and method for separating particules contained in a fluid
DE19811090A1 (en) * 1998-03-13 1999-09-16 Georg Klas Cyclone separator for effluent household gray water
EP1180400A1 (en) * 2000-08-02 2002-02-20 Newcastle University Ventures Limited Cyclone separation apparatus
US6365047B1 (en) * 1997-06-05 2002-04-02 Applikations-und Technikzentrum für Energieverfahrens-Umwelt-, und Strömungstechnik (ATZ-EVUS) Method and device for treating biogenic residues
US6645382B1 (en) 2000-11-13 2003-11-11 George E. Wilson Energy-efficient head cell entry duct
US20060065609A1 (en) * 2004-09-30 2006-03-30 Arthur David J Fluid control device
US20070138085A1 (en) * 2004-03-09 2007-06-21 Cameron International Corporation Separation device
WO2008072087A2 (en) * 2006-12-14 2008-06-19 Aker Process Systems As Fluid treatment
WO2014058382A1 (en) * 2012-10-09 2014-04-17 Nano Control Ab Device for separation of particles from a gas flow
US8882873B2 (en) 2011-02-14 2014-11-11 David Brownlee Vortex finder for cyclone separator
WO2015168567A1 (en) * 2014-05-02 2015-11-05 Eaton Corporation Multistage separator assembly
EP2830752A4 (en) * 2012-03-29 2015-12-23 Exxonmobil Upstream Res Co System and method to treat a multiphase stream

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US2769546A (en) * 1951-10-17 1956-11-06 Stamicarbon Process and apparatus for causing a liquid to flow along different conduits depending on the viscosity of the liquid concerned
US2843265A (en) * 1956-07-17 1958-07-15 Rakowsky Victor Method of density separation

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2769546A (en) * 1951-10-17 1956-11-06 Stamicarbon Process and apparatus for causing a liquid to flow along different conduits depending on the viscosity of the liquid concerned
US2843265A (en) * 1956-07-17 1958-07-15 Rakowsky Victor Method of density separation

Cited By (51)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3215272A (en) * 1961-05-16 1965-11-02 Phillips Petroleum Co Process of separation of suspended foreign materials from an aqueous medium
US3211535A (en) * 1962-06-18 1965-10-12 Fmc Corp Liquid separation apparatus
US3438890A (en) * 1965-09-10 1969-04-15 Fmc Corp Method and apparatus for separating solids-liquids mixtures
US3743102A (en) * 1971-03-17 1973-07-03 United Aircraft Corp Vortex separator using core plates
USB330719I5 (en) * 1971-12-06 1976-03-16
US4001121A (en) * 1971-12-06 1977-01-04 Messerschmitt-Bolkow-Blohm Gmbh - Division Hamburger Flugzeugbau Centrifugal treatment of fluids
US3784009A (en) * 1971-12-13 1974-01-08 Univ Oklahoma State Hydroclone for separating an immiscible heavy phase from a light phase liquid
US3929639A (en) * 1973-07-23 1975-12-30 Gaston County Dyeing Mach Filtering apparatus and process
US3901799A (en) * 1973-10-29 1975-08-26 Maxie C Adkison Cyclone separator
US3990976A (en) * 1974-03-20 1976-11-09 Yasuhito Nishioka Cyclone with plural peripheral discharge tubes
US4087261A (en) * 1976-08-30 1978-05-02 Biphase Engines, Inc. Multi-phase separator
US4120795A (en) * 1977-12-05 1978-10-17 Laval Claude C Device for separating a plural phase fluid system into its constituent phases
US4212653A (en) * 1978-06-27 1980-07-15 General Electric Company Process and apparatus for separating particulate matter from gaseous media
DE2900931A1 (en) * 1978-08-24 1980-03-13 Geosource Inc A method and apparatus for mixing materials with solid fliessfaehigen
US4219340A (en) * 1978-12-14 1980-08-26 Clark & Vicario Corporation Method and apparatus for outflowing liquids from chamber maintained under vacuum
US4317716A (en) * 1979-01-11 1982-03-02 Liller Delbert I Vortex finder and sleeve kit
US4341352A (en) * 1979-08-06 1982-07-27 Liller Delbert I Method of coal washing at low speed pumping
US4443331A (en) * 1980-03-21 1984-04-17 Centre Technique De L'industries Des Papiers Carton Et Celluloses Process and device for separating particles in a fluid especially for the cleaning of the suspensions handled in the paper industry
US4333499A (en) * 1980-04-15 1982-06-08 Conoco Inc. Pressure dissipation apparatus
US4378289A (en) * 1981-01-07 1983-03-29 Hunter A Bruce Method and apparatus for centrifugal separation
US4594149A (en) * 1982-05-21 1986-06-10 Mag-Sep Corp. Apparatus and method employing magnetic fluids for separating particles
US4819808A (en) * 1982-05-21 1989-04-11 Mag-Sep Corp. Apparatus and method employing magnetic fluids for separating particles
US4961841A (en) * 1982-05-21 1990-10-09 Mag-Sep Corporation Apparatus and method employing magnetic fluids for separating particles
US4789476A (en) * 1985-03-19 1988-12-06 Siegbert Schulz Cyclone separator with two separating zones and static guide mechanisms
DE3623892A1 (en) * 1985-07-16 1987-02-19 Koezponti Banyaszati Fejleszte A method and apparatus for separating the individual phases of multi-phase flowing media
US4842738A (en) * 1988-04-29 1989-06-27 Greenspan Harvey P Centrifuge device
US4960525A (en) * 1988-09-26 1990-10-02 The United States Of America, As Represented By The Secretary Of Agriculture Hydrocyclone for washing particles in liquid suspension
US5112498A (en) * 1989-11-28 1992-05-12 Orkney Water Test Centre Limited Method of coalescing a disperse phase within a continous phrase of a fluid mixture
US5224604A (en) * 1990-04-11 1993-07-06 Hydro Processing & Mining Ltd. Apparatus and method for separation of wet and dry particles
US5300222A (en) * 1990-09-28 1994-04-05 Broussard Paul C Sr Water clarification method and apparatus
US5498329A (en) * 1994-09-12 1996-03-12 Interclean Equipment, Inc. Vehicle wash apparatus using reclaimed water
WO1998042424A1 (en) * 1997-03-24 1998-10-01 Rochat Jean Denis Device and method for separating particules contained in a fluid
US6273264B1 (en) 1997-03-24 2001-08-14 Jean Denis Rochat Device and method for separating particles contained in a fluid
US6365047B1 (en) * 1997-06-05 2002-04-02 Applikations-und Technikzentrum für Energieverfahrens-Umwelt-, und Strömungstechnik (ATZ-EVUS) Method and device for treating biogenic residues
DE19811090A1 (en) * 1998-03-13 1999-09-16 Georg Klas Cyclone separator for effluent household gray water
EP1180400A1 (en) * 2000-08-02 2002-02-20 Newcastle University Ventures Limited Cyclone separation apparatus
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