US2557629A - Method and apparatus for continuous centrifugal separation - Google Patents

Method and apparatus for continuous centrifugal separation Download PDF

Info

Publication number
US2557629A
US2557629A US663576A US66357646A US2557629A US 2557629 A US2557629 A US 2557629A US 663576 A US663576 A US 663576A US 66357646 A US66357646 A US 66357646A US 2557629 A US2557629 A US 2557629A
Authority
US
United States
Prior art keywords
liquid
suspension
centrifugal
solid particles
conduit
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.)
Expired - Lifetime
Application number
US663576A
Other languages
English (en)
Inventor
Boivinet Jean Henri
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.)
Compagnie de Produits Chimiques et Electrometallurgiques Alais Froges et Camargue
Original Assignee
Individual
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 Individual filed Critical Individual
Application granted granted Critical
Publication of US2557629A publication Critical patent/US2557629A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • B04B1/10—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with discharging outlets in the plane of the maximum diameter of the bowl
    • B04B1/12—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with discharging outlets in the plane of the maximum diameter of the bowl with continuous discharge
    • 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
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/04—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with inserted separating walls
    • B04B1/08—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with inserted separating walls of conical shape

Definitions

  • centrifugal separation of solid particles from a liquid in which they are in suspension could not .be obtained in continuous operation.
  • the suspension to be treated is subjected to centrifugal action and the clarified liquid is removed until the solid deposit reaches a given thickness on the peripheral wall of the centrifugal apparatus.
  • Apparatus of the type used for separating cream from milk in which the separation and extraction take place in a continuous manner, are perfectly well adapted to the separation of emulsions of two liquids. But they cannot be used for the separation of solid particles in suspension, where the densities of the suspensions are liable to vary during the separation operation, because in this case, the equilibriums that are obtained 'are unstable and simultaneous evacuation of the liquid and the mud formed by the solid particles is no longer possible.
  • the object of the present invention is to provide a method and apparatus for obviating these difiiculties and ensuring, with a continuous operation, the separation of solid particles from a liquidin which they are in suspension.
  • the suspension of solid particles in a liquid is treated in a centrifugal apparatus and the mud that collects at the periphery of this apparatus is driven in a centripetal direction by a stream of water or any other liquid the pressure of which is automatically regulated in accordance with the very op- I eration of the apparatus.
  • this regulation of the pressure of the water or other liquid that drives the mud in the centripetal direction is as- .sured in a very simple manner by feeding said liquid from the center towardthe periphery through a suitable supply conduit, while the mud carried along by said liquid is evacuated from the periphery toward the center through a suitable evacuation conduit.
  • the level of said liquid in the feed conduit establishes itself automatically at a distance from the axis of rotation such that there is always suflicient pressure for driving along the heavy elements, whatever .be its variations resulting from variations of the percentage of heavy elements, of densities,'viscosities, and so on.
  • the rate of flow of the liquid stream maintains itself always at the selected value and the flow of the heavy elements is thus ensured, because unstability of the equilibrium is automatically corrected.
  • the discharge orifices which may be either calibrated orifices or ordinary orifices, are located far enough from the periphery so that they can have a relatively large cross-section and, hence, not be liable to p ng.
  • the relative rate of flow of the auxiliary liquid that is to say of the liquid for carrying oil the heavy particles, may be made such that a portionof this liquid flows (ascends) outside the evacuation conduit into the centrifugal bowl, and in countercurrent fashion with respect to the movement of the heavy elements which flow toward the periphery.
  • the deposit is thus washed in the best possible conditions, if a certain dilution of the evacuated clarified liquid is not objectionable.
  • the method according to the present invention further permits of replacing, in a suspension, the dispersing liquid by another one.
  • the method and apparatus for the continuous centrifugal separation of solid particles from the liquid in which they are dispersed, as aboveset forth, is applied to the separation of red mu in suspension in solutions of sodium aluminate, obtained in the alkaline treatment of bauxite in autoclaves, which separation is to be carried out during the manufacture'of alumina according to the Bayer process.
  • the temperature of a decantation apparatus hardly exceeds 95 C. and the molecular ratio of caustic NazO to A110: of the aluminate liquors that leave the autoclave is generally close to 1.8. It is therefore obvious that the solutions that are treated are metastable and that a more or less advanced decomposition is always to be feared. This fact is well known to the experts on alumina, who are aware that a slowing down of the decantation process is almost sure to cause a drop in the yield of the plant.
  • the invention can be carried out with centrifugal' apparatus of all kinds.
  • the annexed drawings show, by way of example, the application of the invention to the case of centrifugal apparatu comprising a container fitted with a plurality of superposed discs or conical elements, and to that of a centrifugal apparatus provided with a plurality of peripheral cones, but these examples should not be considered as having any limitative character.
  • Fig. 1 is a vertical sectional view of an apparatus made accordingto a first t of the invention
  • Fig. 2 isaviempdrtlyinelevatidnandparfly in vertical section, of a second embodiment;
  • Fig.2a isaview,partlyinelevationandpartiy in vertical section, of a slight modification of the embodiment shown in Fig. 2;
  • Fig. 4 is a sectional view of a modification of the apparatus of Fig. 1;
  • Fig.7 isanaiualsectionalviewofacenirifugation cone
  • Fig. 8a is a perspective view of the same arrangement as Fig. 8;
  • Fig. 9 is a view partially in elevation and partially in axial section on the line IXIX of Fig. 8;
  • Fig. 10 is a sectional view of the end of a cone of a centrifugal machine, made according to still another modification.
  • the apparatus includes a main body I and a cover 2 fixed to said main body by means of a nut ring I 3. A plurality of conical plates it are superposed in body I.
  • the mixture to be decanted or separated is introduced through tube I into the space between partition 9 and the bottom of body i anditisledtothebaseoftheplleof plates is on the outer side thereof.
  • the heavy elements or particles collect at the periphery of body i, where they meet with liquid streams of centripetal direction. These heavy elements are driven into and through pipes I and evacuated through calibrated orifices I.
  • the mud that accumulates at the periphery of the container formed by .body I and cover 2 forms funnel-shaped deposits around pipes l, the spaces limited by these funnel-shaped mud deposits serving in the separation operation.
  • the liquid for driving out these heavy elements is introduced through conduit II into distributing means where it is divided into as many equal portions as there are devices for the evacuation of the heavy elements.
  • Each of these portions is led, through pipes i5, disposed between partition 1 and the bottom of body I. to the points of the periphery where the heavy elements collect together.
  • the liquid in course of clarification ascends 60 between discs II and flows out in the clarified ,stafe through calibrated orifice II.
  • the apparatus includes a central body i on which are fixed a plurality of cones 2' located either all in the same plane or in different parallel planes.
  • These cones include a partition I, also of conical shape, and an axial pipe 4' leading to calibratedoriiices 5'.
  • the mixture to be separated or decanted is introduced through conduit 0' into distributing device I where, by means of a set of radial partitions, it is divided into as many equal portions as there are cones I in the apparatus.
  • the clarified liquid flows inwardly between distributor 9' and partition 3', enters space II and escapes through calibrated orifices l2.
  • the heavy elements collect at the apex of the cone, where they meet with a stream of liquid of centripetal direction. These elements are driven into pipe 4' and evacuated through calibrated orifice 5'.
  • the driving liquid is fed through conduit I3 into passage l5 between cones 2' and 3', after passing through distributing device H where, owing to the action of a plurality of radial partitions, it has been divided into as many equal portions as there are cones.
  • I may cause a portion of the liquid of the initial suspension to flow out through conduits 4 or 4'.
  • I may also cause a portion of the auxiliary liquid to mix with the liquid of said suspension. For this purpose, it suffices, for' instance, either to reduce or to increase the volume' of liquid introduced into distributing device I or H.
  • the distance between the various parts of centrifugal apparatus is suitably determined in such manner that the liquid level in conduit I5 is normally located in the middle part of this conduit.
  • this level very quickly comes to such a distance from the axis of revolution that the variation of pressure that results from this variation of position of the liquid level keeps the fiow of liquid at the chosen rate.
  • Figs. 1, 2 and 3 are given merely by way of example, and many modifications can be made therein without, departing from the principle of the invention.
  • the calibrated orifices 5' and I2 of Fig. 2 can be replaced.
  • the rate of fiow is'determined by giving suitable lengths to tubes l6 and II, the latter opposing to the circulation of the elements a counter-pressure which is the higher the nearer their orifices are from the axis of rotation a-b.
  • the sections of these tubes should be chosen relatively large so that only their length need be taken into account, whatever be the rate of flow and the viscosity of the elements conveyed therethrough.
  • the driving liquid may itself be constituted of a suspension instead of being constituted of a clear liquid.
  • This auxiliary liquid or suspension may, if advantageous, be introduced under pressure, by replacing, for instance, tube I3 of Fig. 2 by an axial tube l3 as in Fig. 1, but provided with a stufiing box.
  • the auxiliary liquid or suspension for carrying along the heavy elements may be introduced by means of a piston pump the discharge pressure of which will add its action to the automatic action of the centrifugal apparatus, so as to overcome the resistances that are opposed to the evacuation of the heavy elements.
  • I may also introduce into the tube 4 or 4', in addition to the auxiliary liquid, a gas or vapor intended to reduce the weight of the column of suspension to be evacuated.
  • I may also replace the auxiliary liquid or suspension that is fed through conduit l3 or l3 by an emulsion of a gas or vapor.
  • pipes 4 and I5 may be replaced by annular channels of small width, which makes it possible todispense with the formation of funnel-shaped stable mud deposits as above set forth, the whole of the bowl being then utilized for decantation cf the mixture.
  • the amount of dispersive phase that is evacuated with the dry matters also varies, which may involve certain drawbacks, in particular that of collectin a smaller amount of the dispersive phase that is employed.
  • Fig. 4 which is of a type analogous to that of Fig. 1, makes it possible to vary during the course of the operation the volume of clarified liquid and, therefore, to collect the desired quantity of this liquid.
  • the orifices l2 for the discharge of the clarified liquid open into a circular channel 20 which rotates together with the body I of the apparatus.
  • ] may be varied either manually or automatically as a function of the flow rates.
  • I may also arrange the heavy elements outlet orifices 5 sothat they open into a circular channel 22, and remove solid particles mixed with the driving liquid by means of a pipe 23 the position of which is adjustable so as to vary'the fiow rate.
  • Channels 20 and 22 may be used either simultaneously or separately, orifices l2 and 5 being both either calibrated orifices or uncalibrated.
  • the centrifuging apparatus shown by Figs. 5 and 6 is of a type analogous to that of Figs. 2 and 3.
  • This apparatus includes a system of discharge pipes 2 I and 23 analogous to those above referred to, projecting more or less into channels 20 and 22'' respectively, and designed to receive the outflowing clarified liquid and the mixture of solid particles and of driving liquid.
  • the apparatus may be arranged in such manner that a portion of the driving liquid is mixed with the liquid of the suspension and performs a relative washing of the mud.
  • Fig. 8 is an axial cross-sectional view of the apparatus across the cones which it comprises.
  • Fig. 9 is a view partially in elevation and partially in axial section of the same arrangement but through a plane perpendicular to that of Fig. 8
  • the conical inner partition 8 is provided, at the apex thereof with a block 24 provided with a e 11 for the evacuation of the decanted solid particles.
  • FIG. 8a is a perspective view of the same 81'! rangement in partial cross-section through two axial planes perpendicular to one another, one being that of Fig. 8 and the other that of Fig. 9.
  • I provide at the interior of the apexes of the cone 1 of the centrifuging apparatus a removable block 28 upon which concentric tubes 4 and 28 are fitted.
  • the driving liquid is fed into the annular space between'these two tubes and enters conduit" provided in block 28.
  • the decanted solid particles, accumulated at the apex of cone 2 pass through aperture 3
  • conduit 88 One of the ends of the conduit 88 is screwed into the wall of the cone 2.and the end of this screw forms a tight joint with the block 18. 'nie other end of the conduit 38 is connected to a circular partition, not shown, analogous to the partitions designed for the introduction of the mixture to be decanted and for the driving liquid. In the case of a centrifugation with washing there.
  • a conical piece 33 made in the shape of the plug of a cock, is fitted in a fluid-tight manner in a corresponding housing formed in block 28.
  • conduit 84 which is connected tooutlet tube 4.
  • conduit 84 which is connected tooutlet tube 4.
  • a small plate Ila which can be made of any desired length and thickness to obtain a given rate of flow. It is pomble, by modi- Conical piece It fying the length and thickness of this plate 88a,
  • cones l and 8 entersblock It in the centripetal direction in the form of an annular sheet given thereto by a piece 26, of predetermined length and diameter. presenting a double portion substantially conical fixed to the summit of the centrifugal cone.
  • the solid particles that are driven along pass between block N and wall 8 and are conveyed to outlet tube 4 through conduit 21.
  • any of the above described devices can be used.
  • I may, for instance, employ a centrifuging apparatus of the kind illustrated by Fig. 20 including means for annular distribution or the driivng liq id such as shown by Fig. 10.
  • This centrifuging apparatus may, for instance, have the following characteristics:
  • Width 0 of the annular slot provided for the passage of the driving liquid-0.6 mms.
  • Example 2 I introduce into the centrifugal apparatus:
  • the suspension, on leaving the autoclave may be introduced into the centrifuging machine either as it is or after suitable dilution.
  • the clear liquid that is utilized for the extraction of red mud may be replaced by water, or a suspension of red mud or of any other suitable powdery product.
  • the driving liquid or suspension may also be emulsified inside the apparatus by means of a gas or vapor introduced in any suitable manner.
  • the suspension of red mud that leaves the centrifuging apparatus may be introduced into a second centrifuging apparatus where separation and washing of the mud' will take place. These operations may be pursued in a third centrifugin apparatus and so on.
  • the suspension resulting from the attack of bauxite in the autoclave may,
  • a classifying and selecting apparatus of any suitable type with a view to separating the mud grains of a diameter higher than a given limit (for instance 50 microns). These grains may be treated separately, only the fine portion being introduced into the centrifuging apparatus.
  • the mud driving liquid may be constituted of the liquor serving to attack the bauxite, in a more or less concentrated state, thus forming a suspension with the mud.
  • This suspension heated for a further attack, dissolved a further portion of alumina, which had remained in the bauxite after the first attack.
  • This method of operation permits of methodically exhausting bauxite in several operations.
  • a continuous method for the centrifugal separation of solid particles suspended in a liquid comprising the steps of, introducing a suspension of solid particles in a liquid into a centrifuge, rotating the centrifuge and effecting the separation of the solid particles from the liquid in the suspension by centrifugal force,
  • a method according to claim 1 characterized in that the suspension comprises ,red mud ll in a solution of sodium aluminate as formed in the autoclave in the treatment of bauxite by the Bayer process.
  • a method according to claim 4 characterised in that the original suspension as obtained in the autoclave is diluted and the. auxiliary fluid is constituted of a weak solution of sodium aluminate.
  • auxiliary fluid is constituted of a liquor capable of attacking bauxite and further, in that the mixture of such liquor and entrained solid particles discharged from the centrifuge is recycled thereto to efl'ect treatment of further quantities of bauxite.
  • a plurality of radiallyaxised particle collecting cones each cone in- .cluding.
  • means for introducing the solid particle containing liquid means for introducing in a centrifugal direction an auxiliary fluid, inlet delivery tubes for said auxiliary fluid terminating at a point adjacent the apex and peripheral walls of the cones.
  • discharge tubes extending from a ,point adjacent the apex of said cone in a radial ,centripetal direction along the axis and through ethe entirety of said cone for said solid particle (containing auxiliary fluid, a removable block fltted in fluid-tight relationship in the apex of ,said cones, three parallel ducts located within .the block in planes parallel to the axis of said .cone, means including a groove interconnecting the ends of the three ducts within the block at a point remote from the other ends of said ducts, the flrst of the three ducts connected to the inlet delivery tube for the auxiliary fluid, the second of the three ducts openly connected to the interior of the cone at a point adjacent the apex of the cone, and the third of the three ducts connected to the discharge tube for the solid particle containing auxiliary fluid.
  • a discharge tube for said particle containing auxiliary fluid extending from a point adjacent said outlet in a radial centripetal direction and through the collecting means, said discharge being connected to an outlet on the exterior of the rotating body member, and independent means for removing the liquid separated from the suspension.
  • the particle collecting means comprise a plurality of radially-axised cones, and each cone is provided adjacent its apex with an inlet for the auxiliary fluid and with a discharge tube for the solid particles containing auxiliary fluid, said tube extending along the axis of the cone.
  • An apparatus according to claim 10 provided with deflector means adjacent the outlet for the auxiliary fluid in the collecting means, whereby the auxiliary fluid is injected in an annular sheet into the collected mass of separated solid particles.

Landscapes

  • Centrifugal Separators (AREA)
US663576A 1946-02-21 1946-04-19 Method and apparatus for continuous centrifugal separation Expired - Lifetime US2557629A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR210246X 1946-02-21
FR996069T 1946-02-27
FR270246X 1946-02-27

Publications (1)

Publication Number Publication Date
US2557629A true US2557629A (en) 1951-06-19

Family

ID=27248966

Family Applications (1)

Application Number Title Priority Date Filing Date
US663576A Expired - Lifetime US2557629A (en) 1946-02-21 1946-04-19 Method and apparatus for continuous centrifugal separation

Country Status (7)

Country Link
US (1) US2557629A (el)
BE (1) BE464440A (el)
CH (1) CH256911A (el)
DE (1) DE925400C (el)
FR (1) FR996069A (el)
GB (1) GB610995A (el)
NL (1) NL68133C (el)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2755293A (en) * 1951-12-04 1956-07-17 Barber Greene Co Method of treating materials
US2806766A (en) * 1952-11-28 1957-09-17 Kaiser Aluminium Chem Corp Process of purifying caustic aluminate liquors
US2889982A (en) * 1952-11-25 1959-06-09 Kaiser Aluminium Chem Corp Process of purifying caustic aluminate liquors
US2981600A (en) * 1952-12-01 1961-04-25 Kaiser Aluminium Chem Corp Process of purifying caustic aluminate liquors
EP1487585A1 (en) * 2002-01-25 2004-12-22 Econova Inc. Methods for centrifugally separating mixed components of a fluid stream
US20060217255A1 (en) * 1999-08-06 2006-09-28 Econova, Inc. Method for separating particulate matter from a fluid stream
US20130023397A1 (en) * 2010-03-29 2013-01-24 Newcastle Innovation Limited Enhanced gravity separation device using closely spaced channels
US20150024922A1 (en) * 2012-02-02 2015-01-22 Pall Technology Uk Limited Centrifugation system and related method
US20150306606A1 (en) * 2012-12-05 2015-10-29 Gea Mechanical Equipment Gmbh Outlet nozzle for a centrifuge drum
JP2020058986A (ja) * 2018-10-11 2020-04-16 三菱化工機株式会社 遠心分離装置
JP2020058987A (ja) * 2018-10-11 2020-04-16 三菱化工機株式会社 遠心分離装置

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH07114982B2 (ja) * 1988-06-07 1995-12-13 ヴェストファリア ゼパラトール アクチエンゲゼルシャフト 遠心分離機

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US304607A (en) * 1884-09-02 Meistek
US671573A (en) * 1899-08-25 1901-04-09 Frans Henrik Aubert Wielgolaski Ore-separator.
US1429320A (en) * 1922-02-21 1922-09-19 Bouillon Charles Apparatus for separating solids from liquids
US2280998A (en) * 1940-04-13 1942-04-28 Aluminum Co Of America Alumina recovery process
US2291849A (en) * 1934-04-18 1942-08-04 Arthur M Hood Counterflow centrifuge and method of treating one liquid with another liquid of different specific gravity
US2313541A (en) * 1941-05-26 1943-03-09 Laval Separator Co De Machine for purifying liquids

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US304607A (en) * 1884-09-02 Meistek
US671573A (en) * 1899-08-25 1901-04-09 Frans Henrik Aubert Wielgolaski Ore-separator.
US1429320A (en) * 1922-02-21 1922-09-19 Bouillon Charles Apparatus for separating solids from liquids
US2291849A (en) * 1934-04-18 1942-08-04 Arthur M Hood Counterflow centrifuge and method of treating one liquid with another liquid of different specific gravity
US2280998A (en) * 1940-04-13 1942-04-28 Aluminum Co Of America Alumina recovery process
US2313541A (en) * 1941-05-26 1943-03-09 Laval Separator Co De Machine for purifying liquids

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2755293A (en) * 1951-12-04 1956-07-17 Barber Greene Co Method of treating materials
US2889982A (en) * 1952-11-25 1959-06-09 Kaiser Aluminium Chem Corp Process of purifying caustic aluminate liquors
US2806766A (en) * 1952-11-28 1957-09-17 Kaiser Aluminium Chem Corp Process of purifying caustic aluminate liquors
US2981600A (en) * 1952-12-01 1961-04-25 Kaiser Aluminium Chem Corp Process of purifying caustic aluminate liquors
US20060217255A1 (en) * 1999-08-06 2006-09-28 Econova, Inc. Method for separating particulate matter from a fluid stream
US7314441B2 (en) 1999-08-06 2008-01-01 Econova, Inc. Method for separating particulate matter from a fluid stream
AU2003209319B2 (en) * 2002-01-25 2008-09-04 Econova Inc. Methods for centrifugally separating mixed components of a fluid stream
EP1487585A4 (en) * 2002-01-25 2006-09-20 Econova Inc METHOD FOR THE CENTRIFUGAL SEPARATION OF MIXED COMPONENTS OF A FLUID CURRENT
EP1487585A1 (en) * 2002-01-25 2004-12-22 Econova Inc. Methods for centrifugally separating mixed components of a fluid stream
US20130023397A1 (en) * 2010-03-29 2013-01-24 Newcastle Innovation Limited Enhanced gravity separation device using closely spaced channels
EP2552593A4 (en) * 2010-03-29 2016-02-24 Newcastle Innovation Ltd SEPARATING DEVICE WITH INCREASED HEAVY DUTY AND CHANNELS WITH CLOSE DISTANCE
US9789490B2 (en) * 2010-03-29 2017-10-17 Newcastle Innovation Limited Enhanced gravity separation device using closely spaced channels
US20150024922A1 (en) * 2012-02-02 2015-01-22 Pall Technology Uk Limited Centrifugation system and related method
US20150306606A1 (en) * 2012-12-05 2015-10-29 Gea Mechanical Equipment Gmbh Outlet nozzle for a centrifuge drum
US10315203B2 (en) * 2012-12-05 2019-06-11 Gea Mechanical Equipment Gmbh Outlet nozzle for a centrifuge drum
JP2020058986A (ja) * 2018-10-11 2020-04-16 三菱化工機株式会社 遠心分離装置
JP2020058987A (ja) * 2018-10-11 2020-04-16 三菱化工機株式会社 遠心分離装置

Also Published As

Publication number Publication date
CH256911A (fr) 1948-09-15
FR996069A (fr) 1951-12-12
DE925400C (de) 1955-03-21
BE464440A (el)
NL68133C (el)
GB610995A (en) 1948-10-22

Similar Documents

Publication Publication Date Title
US2831754A (en) Solvent extraction process
US2312706A (en) Method and apparatus for separating heavy particles from paper pulp suspensions
US2557629A (en) Method and apparatus for continuous centrifugal separation
US3027390A (en) Apparatus and method for centrifugal purification of fatty oils
US3018091A (en) Precipitation apparatus
US9023216B2 (en) Device for turbulence reduction
US2599619A (en) Method and apparatus for centrifugal separation
US4009823A (en) Bowl of solids-concentration centrifuge
US2193871A (en) Process for separating solids from animal raw material
US2230386A (en) Separation of solids from liquids
JPS6045921B2 (ja) 連続的に作業する全壁型向流式遠心抽出器
GB1582599A (en) Method and installation for the treatment of crystal suspensions
US4505697A (en) Underflow concentration control for nozzle centrifuges
US1429320A (en) Apparatus for separating solids from liquids
SU513598A3 (ru) Устройство дл разделени водных суспензий
US2819014A (en) Centrifugal phase contactor
US2700468A (en) Centrifugal method and apparatus for separating solids
US2779536A (en) Anti-foaming centrifugal methods and apparatus
US2645346A (en) Paper machinery
US1718871A (en) Method of and means for separating comminuted matter from the liquid in which it is immersed
US3365066A (en) Centrifuge
US2375826A (en) Vortex separator apparatus for treating paper pulp
US1923455A (en) Mill-starch treatment and method
US2310649A (en) Evaporating apparatus
US2731147A (en) Hydraulic classifier