US3695509A - Centrifugal separator for separating emulsions - Google Patents

Centrifugal separator for separating emulsions Download PDF

Info

Publication number
US3695509A
US3695509A US57718A US3695509DA US3695509A US 3695509 A US3695509 A US 3695509A US 57718 A US57718 A US 57718A US 3695509D A US3695509D A US 3695509DA US 3695509 A US3695509 A US 3695509A
Authority
US
United States
Prior art keywords
chamber
hub
outlet
separator
emulsion
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
US57718A
Other languages
English (en)
Inventor
Alain Ferdinand Javet
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.)
TERMOMECCANICA ITALIANA SpA
Original Assignee
TERMOMECCANICA ITALIANA SpA
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 TERMOMECCANICA ITALIANA SpA filed Critical TERMOMECCANICA ITALIANA SpA
Application granted granted Critical
Publication of US3695509A publication Critical patent/US3695509A/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
    • B04B11/00—Feeding, charging, or discharging bowls
    • B04B11/02—Continuous feeding or discharging; Control arrangements therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0217—Separation of non-miscible liquids by centrifugal force
    • 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

Definitions

  • a centrifugal separator for emulsions comprises a rotating drum with an admission chamber at one end thereof, connected to atmosphere via an axial supply inlet, and a multitude of separating tubes arranged around an axial hub to extend longitudinally from the common admission chamber to a common outlet chamber at the other end of the drum.
  • One or more outlets connected to atmosphere are arranged to discharge the lighter constituent of the emulsion from the discharge chamber at a radial distance lying between the radius of the supply inlet and that of the hub.
  • An outlet duct connected to atmosphere extends from the periphery of the outlet chamber towards the drum axis so as to discharge the heavier constituent at a radial distance slightly greater than that of the discharge outlet for the lighter constituent of the emulsion. Liquid movement through the separator is provided through centrifugal force only. Emulsion supplied to the admission chamber is driven radially outward and forms therein a coaxial liquid level at atmospheric pressure. The lighter constituent forms in the outlet chamber a coaxial overflow level at atmospheric pressure at the discharge outlet. The heavier constituent forms a further coaxial overflow level at atmosphere pressure, at the discharge end of the outlet duct.
  • This invention relates generally to the separation of liquid mixtures and particularly to the separation of the two constituents or fractions of different density of an emulsion.
  • the separating means now existing require, for each application contemplated, that a compromise be made between the quality of the separation and the flow rate of the treated liquid mixture.
  • a compromise be made between the quality of the separation and the flow rate of the treated liquid mixture.
  • equipment e.g., supercentrifuges
  • it is desired to treat liquids of low value which are easy to separate one has a choice of relatively inexpensive equipment which is, however, cumbersome and much less effective.
  • a centrifugal separator for separating emulsions into two liquid constituents of different density comprises a rotating drum forming an admission chamber for the emulsion to be separated, arranged at one end of the drum, an outlet chamber for the separated constituents, arranged at the other end thereof, and an intermediate portion including a separating zone consisting of a multitude of longitudinally extending separating passages arranged around an axial hub and interconnecting these chambers.
  • the admission chamber has an axial inlet communicating with the ambient atmosphere, the outlet chamber being equipped with at least one outlet for the constituent of lower density; this outlet communicates with the ambient atmosphere and serves to discharge the lowerdensity constituent at a distance from the drum axis greater than the radius of the inlet and smaller than the radius of the hub, the outlet chamber being further equipped with at least one outlet duct for the constituent of higher density, which extends from a peripheral zone of the outlet chamber toward the axis of rotation, up to a radial distance equal to or slighter greater than that of the outlet for the constituent of lower density, and communicates with the ambient atmosphere.
  • FIG. 1 is a diagrammatic sectional view showing a first embodiment of the separator
  • FIG. 2 shows a second embodiment of the separator, in axial section
  • FIG. 3 is a cross-sectional view taken on line III-Ill of FIG. 2:
  • the separator shown in FIG. 1 includes a plurality of separating tubes 2 mounted parallel to its axis of rotation 5, along two circular rows, around a hub consisting of a hollow cylinder 3 closed at both ends.
  • This cylinder 3, the tubes 2 and a cylindrical casing 4 of the drum 1 are solidly connected with one another so that the tubes rotate around the horizontal axis 5 of the drum 1, the latter being driven by a driving device (not shown) at a given rotational speed.
  • the drum 1 comprises, in addition, two transverse end walls or headers 6, 7 in the shape of a truncated cone which are solidly connected with the casing 4 and respectively prolonged by an inlet tube 8 and a discharge tube 9 attached thereto at their small base.
  • the inlet tube 8 arranged axially at the inlet end of the drum 1 has a smaller diameter than the discharge tube 9 situated at the outlet end, these tubes 8 and 9 being mounted in bearings 10, 1 1, respectively.
  • the tube 8 is closed at its free end with the exception of an axial opening through which passes, with clearance,
  • a fixed pipe 12 for feeding the separator with emulsion coming from a suitable source (not shown).
  • the emulsion introduced into the tube 8 spreads over the wall thereof owing to centrifugal force, advances along this tube and reaches an inlet chamber 13 where it meets a baffle 14 in the shape of a truncated cone arranged in the vicinity of the end wall 6 to form an annular passage 15 emerging into the inlet chamber 13.
  • the latter is further provided with a transverse baffle 16 solidly connected to the casing 4 and provided with an axial circular opening 17 having a diameter larger than that of the tube 8.
  • This baffle 16 is arranged upstream of the cylinder 3 and of the tubes 2 so as to form an annular passage 18 for bringing forward the emulsion to the entry end of these tubes.
  • These baffles 14 and 16 are adapted to deviate the liquid mixture so as to separate therefrom any solid impurity, under the effect of centrifugal force, before entry into the tubes.
  • the tubes 2 emerge into an outlet chamber 19 bounded by another frustoconical baffle 20 mounted opposite the end wall 7 and solidly connected thereto, by means not shown in the drawing, so as to form an annular outlet duct 27 extending from the periphery of chamber 19 toward the rotational axis 5.
  • a tube 21 fixed to this baffle 20 at the end of duct 27 extends coaxially within the tube 9 to provide an annular discharge channel 22 between these two tubes.
  • the free ends of the tubes 21 and 9 bear outer flanges 23 and 24 for directing the separated fractions towards annular collectors 25 and 26, respectively, constituted by a pair of coaxial channels.
  • the described separator operates in the following manner:
  • the inlet chamber 13 and the outlet chamber 19 of the drum communicate with the atmosphere through the tubes 8 and 9, 21, respectively.
  • the liquid mixture arriving through the pipe 12 spreads on the inner surface of the rotating inlet tube 8 and advances along the latter towards the entry chamber 13 where it is driven radially outward through the passage 15, then returns towards the axis 5, between the baffles 14 and 16, to the opening 17 from which it overflows and is then driven through the annular passage 18.
  • the liquid thus reaches inlet end of the tubes 2 wherein it flows towards the exit chamber 19.
  • the centrifugal separation takes place in the tubes 2 in the manner described below.
  • the emulsion consists of two constituents, of which a constituent A of lower density is dispersed in the form of globules in the other constituent B of higher density.
  • These two constituents will hereinafter be referred to by the name of light fraction and heavy fraction, respectively Owing to the rotation of the tubes 2 around the axis 5, the liquid mixture circulating in these tubes is subjected to the action of centrifugal force. Because of the difference in density between the two fractions, the globules of the light fraction are subjected to a thrust directed towards the axis of rotation 5, thereby providing a progressive separation of the two fractions along the tubes 2.
  • the heavy fraction is thus gradually brought to the far side of each tube 2, that is the side remote from the axis of rotation 5, while the globules of the light fraction accumulate, by coalescence on the inner surface of the tubes 2, on the side which is nearer to the axis 5.
  • the heavy fraction B On arrival of the two fractions in the chamber 19, the heavy fraction B is first driven outwardly to the periphery of this chamber, then passes between the baffle 20 and the end wall 7 and thereupon flows into the discharge channel 22 at the outlet of which this heavy fraction passes over the flange 24 and is drained off by the collector 26.
  • the enlarged globules of the light fraction A which are subjected to a thrust towards the axis 5, accumulate before the inner end of the tube 21. The light fraction thus separated then flows into the tube 21 and proceeds toward the flange 23 which deviates it towards the collector 25.
  • the separation through centrifugal force will be obtained in the same manner in the tubes 2 except that the globules will then be separated on the side remote from the axis 5.
  • the inner end of tube 21 constitutes an outlet orifice through which the light fraction A can flow over while forming, in the outlet chamber 19, the level shown in FIG. 1.
  • the annular duct 27 extending radially inward up to the vicinity of the inner tube 21 allows this level to be established while at the same time ensuring discharge of the heavy fraction from the periphery of the outlet chamber 19.
  • the separating tubes could also be inclined in relation to the axis of rotation so that their distance to the latter increases from their inlet toward their outlet, to enhance circulation in the tubes through an increased centrifugal pumping effect.
  • the cross-section of the tubes may, if desired, be noncircular and in particular asymmetrical so as to promote coalescence of the globules separated therein.
  • each tube may have an inner surface which is more concave in the zone where the globules are accumulated.
  • the separating tubes need not necessarily be rectilinear as described above.
  • One may contemplate using, for example, helicoidal tubes having a large pitch in relation to the winding diameter, to render the separator more compact in length.
  • the device may be arranged with its axis in any desired position other than the horizontal.
  • the centrifugal separator according to the second embodiment shown in FIGS. 2 and 3 comprises a rotatable drum 1 with a vertical axis 5, forming at its upper end an admission chamber 13 provided with a circular axial inlet 8 communicating with the ambient atmosphere and at its lower end an outlet chamber 19 likewise communicating with atmosphere.
  • the intermediate part of the drum comprises a multitude of vertical separating tubes 2 distributed equidistantly around the axially positioned cylindrical hub 3 and extending, parallel to the rotational axis 5, between the admission chamber 13 and the outlet chamber 19.
  • the drum 1 is mounted on the hollow cylindrical hub 3 which is driven by an electric motor 28 mounted on a vertical base 29.
  • the separating tubes 2 are arranged side by side so as to form a nest of tubes filling the annular space between the hub 3 and the cylindrical casing 4 of the drum 1. Assembly of the tubes 2 may be effected by using a suitable mass, of adhesive material for example, allowing them to be solidly connected together.
  • the admission chamber 13 is not equipped with deflecting means such as the deflectors 14, 16 shown in FIG. 1, as such means are not required in numerous applications of the separator where the emulsion to be separated does not contain solid impurities.
  • the feed pipe 12 for introducing the emulsion into the admission chamber 13 is equipped with a valve 30 for adapting the emulsion feed rate to the constituents to be separated in each case.
  • the emulsion entering the admission chamber 13 is driven radially by the centrifugal force due to rotation of the drum 1 and forms, between header- 6 and hub 3, an annular body of liquid centered on the axis of rotation 5, as indicated by dash-dotted lines in FIG. 2, with an inner cylindrical boundary of radius R1 which is slightly greater than the radius ofinlet opening8 but less than that of hub 3.
  • the lighter constituent A is discharged by means of a group of discharge tubes 31 each mounted at an orifice in'the partition 20 so as to communicate with chamber 19.
  • These tubes 31 are evenly distributed on a circle with radius R2 (see FIG. 3), this radius being larger than that of the axial inlet 8 but smaller than the radius of the hub 3.
  • the tubes 31 and 32 each comprise a first longitudinal portion followed by a second outwardly turned radial portion emerging in a fixed annular collector and 26, respectively, which communicates with the ambient atmosphere.
  • the radially extending legs of the generally L-shaped tubes 31 and 32 open with clearance into the nested channels 25 and 26, respectively.
  • the lighter constituent A arriving at the inlet of the tubes 31 communicating with the atmosphere, flows into these tubes while forming around the axis 5 a liquid-overflow level situated at an equal distance R2 therefrom.
  • This liquid level formed in the outlet chamber 19 and in the longitudinal entrance portion of tubes 31 is indicated by dash-dotted lines in FIG. 2.
  • the heavier constituent B arriving at the inlet of the discharge tubes 32 after passing through the annular duct 27 flows into these tubes while likewise forming a liquid-overflow level in the annular duct 27 and in the longitudinal entrance portion of the tubes 32.
  • This overflow level formed by the heavier constituent B also indicated by dash-dotted lines in FIG.
  • separators described above are of simple and compact design. They nevertheless permit emulsions to be separated into their constituents very efiectively at a high rate. These substantial advantages are obtained through the particular arrangement of the separating passages and of the common admission and outlet chambers in the rotating drum.
  • the use of separating passages surrounding a hub and extending longitudinally in the rotating drum between common admission and outlet chambers provided with the described inlet and outlet means allows very effective use of a multitude of separating tubes and, consequently enables very high flow rates to be achieved without, however, necessitating the use of complicated feed and discharge means as was hitherto the case.
  • a closely spaced arrangement of the tubes allows the annular space between the hub 3 and the casing 4 of the drum to be subdivided into a maximum number of separating passages 2 and hence afiords very high flow rates in the separator with minimum space requirements.
  • this subdivision into a multitude of separating passages allows a very small hydraulic diameter to be obtained in each passage whereby the centrifugal separation is promoted to a great extent for reasons explained below.
  • the Reynolds number (Re) which corresponds to the product of the flow speed w in a passage times the hydraulic diameter d divided by the viscosity (v) of the fluid considered, is generally used for defining the flow conditions of a fluid.
  • an effective centrifugal separation becomes difficult or even impossible to achieve when the mixture tobe separated passes through the separating passage under turbulent flow conditions. It is thus generally necessary to ensure laminar flow conditions, i.e., a flow corresponding to Reynolds numbers (Re wd/v) of lessthan about 2,000, in a centrifugal separating passage.
  • each separating passage allows laminar flow to be achieved at a higher flow velocity.
  • the separator according to this invention allows efficient use of any desired number of separating passages. This is due, in particular, to the fact that all the passages are fed with emulsion from a common admission chamber or entrance manifold and emerge in a single outlet chamber forming part of an exit manifold.
  • the entrance and exit manifolds 13 (or 13, 18) and 19, 27 formed between the generally 'frustoconical headers 6, 7 and the closed hub 3 converge radially outwardly toward the zones of the tubular passages 2.
  • the increased radial pressure differential due to this outward convergence promotes the gravitation of the light fraction toward the central axis, thereby enhancing the separation of the constituents.
  • the progressive narrowing of the chamber 13 increases the axial pressure differential driving the liquid through the conduits 2 clustered about hub 3.
  • the maximum flow rate at which laminar flow and hence complete separation may be achieved will depend from case to case on the size of the liquid globules to be separated from the emulsion.
  • the drum having the above dimensions and rotating at 2,000 r.p.m. enables complete separation with flow rates as high as 47 m /h when the size of the globules to be separated is 0.03 mm.
  • the maximum flow rate for ensuring complete separation of an emulsion comprising globules of 0.01 mm would be about 4 m /h.
  • centrifugal separator avoids the cited disadvantages of known separators in a most simple manner.
  • this is a direct consequence of the provision in a rotating drum, of a multiplicity of separating passages with relatively small cross-section, extending longitudinally in the drum, around a hub of much larger diameter than that of the passages, between common admission and outlet manifolds each communicating with the atmosphere. Thanks to this particular arrangement, it thus becomes possible to achieve, in a most economical manner, not only optimum separating conditions but also a very high separating capacity with a rotating drum of very simple and compact design.
  • the described separator may be readily applied in a widely varying range of technical fields. Indeed, it no longer is necessary to comprise, for each application, between the degree of separation desired and the flow rate of the treated liquid mixture.
  • my improved system may be used with advantage for treating waste waters such as the water used for washing the tanks of oil tankers or the effluents of steel-mills.
  • the separator may be used in various industrial fields, for example in industrial mineral chemistry and extraction.
  • this separator is the food processing industry. Thus, for example, it is most suitable for the treatment of milk and vegetable oils or fish oils.
  • a centrifugal separator for dividing an emulsion into a light and a heavy fraction comprising:
  • a drum rotatable about a central axis said drum having a cylindrical casing with a pair of end walls and a closed hub within said casing axially spaced from said end walls, one of said end walls forming a first header defining an entrance manifold with said hub, the other of said end walls forming a second header defining an exit manifold with said hub, said first header being provided with a central opening of a radius smaller than the hub radius connecting said entrance manifold with the atmosphere;
  • conduits clustered about said hub, said conduits forming passages between said manifolds of a diameter substantially smaller than their distances from said axis;
  • feed means for introducing an emulsion into said entrance manifold, said feed means passing with clearance through said opening;
  • baffle means in said exit manifold dividing same into an annular duct for the heavy fraction and an outlet chamber for the light fraction, said duct being open toward said passages near the periphery of said casing and extending inwardly along said second header in spaced relationship therewith;
  • first collector means communicating with said duct for extracting said heavy fraction therefrom while venting said duct to the atmosphere;
  • both said first and second collector means communicating with said exit manifold at locations spaced from said axis by distances larger than the radius of said opening but smaller than the radius of said hub.
  • said first and second collector means further comprises two sets of tubes opening with clearance into said channels.

Landscapes

  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Centrifugal Separators (AREA)
US57718A 1969-08-08 1970-07-23 Centrifugal separator for separating emulsions Expired - Lifetime US3695509A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CH1207169A CH514358A (fr) 1969-08-08 1969-08-08 Dispositif de séparation centrifuge des deux constituants à densité différente d'une émulsion

Publications (1)

Publication Number Publication Date
US3695509A true US3695509A (en) 1972-10-03

Family

ID=4379568

Family Applications (1)

Application Number Title Priority Date Filing Date
US57718A Expired - Lifetime US3695509A (en) 1969-08-08 1970-07-23 Centrifugal separator for separating emulsions

Country Status (6)

Country Link
US (1) US3695509A (ja)
JP (1) JPS5231588B1 (ja)
CH (1) CH514358A (ja)
DE (1) DE2037366A1 (ja)
FR (1) FR2057066B1 (ja)
GB (1) GB1251167A (ja)

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3814307A (en) * 1973-01-12 1974-06-04 Standard Oil Co Centrifugal clarifier
US3876135A (en) * 1973-03-12 1975-04-08 Foster Miller Ass Centrifuge for separation of oil from water
US4994097A (en) * 1987-03-25 1991-02-19 B. B. Romico B.V. I.O. Rotational particle separator
WO1995026223A1 (en) * 1994-03-29 1995-10-05 United Technologies Corporation Fluid/liquid separator
WO1997004874A1 (en) * 1995-07-25 1997-02-13 Centritec Hb Apparatus and method for discontinuous separation of solid particles from a liquid
WO2006107192A2 (en) * 2005-04-04 2006-10-12 Rowe Parsons International B.V. Device and method for separation of a fluid and more in particular an emulsion
US20080005478A1 (en) * 2006-06-30 2008-01-03 Seagate Technology Llc Dynamic adaptive flushing of cached data
US20110097249A1 (en) * 2005-11-18 2011-04-28 Ferrum Ag Centrifuge cartridge
NL2004559C2 (en) * 2010-04-15 2011-10-18 Coalessense B V Device and method for coalescing droplets dispersed in a flowing mixture.
US20110263405A1 (en) * 2010-04-22 2011-10-27 Specialist Process Technologies Limited Separator
US20110303621A1 (en) * 2007-01-24 2011-12-15 Patel Vipul P Oil centrifuge for extracting particulates from a continuous flow of fluid
US20120010064A1 (en) * 2007-11-26 2012-01-12 Patel Vipul P Oil centrifuge
CN102413896A (zh) * 2009-04-29 2012-04-11 国际壳牌研究有限公司 用于从包含气体和液体的混合物中移除液体的分离装置
US20130164789A1 (en) * 2011-04-07 2013-06-27 Life Technologies Corporation System and Methods for Making and Processing Emulsions
US20130327726A1 (en) * 2006-02-25 2013-12-12 Cameron International Corporation Method and Apparatus for Fluid Separation
US20140296052A1 (en) * 2011-06-29 2014-10-02 The University Of British Columbia Method and apparatus for continuously fractionating particles contained within a viscoplastic fluid
US9017993B2 (en) 2011-04-07 2015-04-28 Life Technologies Corporation System and methods for making and processing emulsions
US10300410B2 (en) * 2014-03-03 2019-05-28 The Trustees Of Princeton University Advanced liquid centrifuge using differentially rotating cylinders and optimized boundary conditions, and methods for the separation of fluids
CN110935198A (zh) * 2019-12-20 2020-03-31 四川大学 一种旋转式微通道破乳方法
CN115041308A (zh) * 2017-06-15 2022-09-13 阿法拉伐股份有限公司 离心分离器和操作离心分离器的方法

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3795361A (en) * 1972-09-06 1974-03-05 Pennwalt Corp Centrifuge apparatus
US3858793A (en) * 1973-02-28 1975-01-07 Donaldson Co Inc Cartridge centrifuge
USRE32381E (en) * 1973-02-28 1987-03-24 Donaldson Company, Inc. Cartridge centrifuge
JPS53147988U (ja) * 1977-04-27 1978-11-21
DE4437340C2 (de) * 1993-11-04 1999-01-28 Peter Weinmann Zentrifuge zur Trennung eines Flüssigkeitsgemisches mit mehr als zwei Bestandteilen von unterschiedlicher Dichte in die Komponenten
CN112452555A (zh) * 2020-11-09 2021-03-09 衡阳市凯信化工试剂股份有限公司 一种化学试剂生产的离心装置

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US507442A (en) * 1893-10-24 Atto lentsch
US1113005A (en) * 1914-01-22 1914-10-06 John M Freisinger Cream-separator.
US1712184A (en) * 1926-10-07 1929-05-07 Reinhold M Wendel Centrifugal concentrator
US2519971A (en) * 1944-12-22 1950-08-22 Tecalemit Ltd Centrifuging apparatus

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US507442A (en) * 1893-10-24 Atto lentsch
US1113005A (en) * 1914-01-22 1914-10-06 John M Freisinger Cream-separator.
US1712184A (en) * 1926-10-07 1929-05-07 Reinhold M Wendel Centrifugal concentrator
US2519971A (en) * 1944-12-22 1950-08-22 Tecalemit Ltd Centrifuging apparatus

Cited By (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3814307A (en) * 1973-01-12 1974-06-04 Standard Oil Co Centrifugal clarifier
US3876135A (en) * 1973-03-12 1975-04-08 Foster Miller Ass Centrifuge for separation of oil from water
US4994097A (en) * 1987-03-25 1991-02-19 B. B. Romico B.V. I.O. Rotational particle separator
US5073177A (en) * 1987-03-25 1991-12-17 B.B. Romico B.V. I.O. Rotational particle separator
WO1995026223A1 (en) * 1994-03-29 1995-10-05 United Technologies Corporation Fluid/liquid separator
CN1090062C (zh) * 1995-07-25 2002-09-04 森特拉泰克公司 固体颗粒与液体间断分离方法与装置
US6083147A (en) * 1995-07-25 2000-07-04 Centritech Hb Apparatus and method for discontinuous separation of solid particles from a liquid
US6248053B1 (en) 1995-07-25 2001-06-19 Ehnstroem Lars Centrifugal separator comprising tubular elements
WO1997004874A1 (en) * 1995-07-25 1997-02-13 Centritec Hb Apparatus and method for discontinuous separation of solid particles from a liquid
WO2006107192A2 (en) * 2005-04-04 2006-10-12 Rowe Parsons International B.V. Device and method for separation of a fluid and more in particular an emulsion
WO2006107192A3 (en) * 2005-04-04 2006-11-23 Rowe Parsons Internat B V Device and method for separation of a fluid and more in particular an emulsion
US20110097249A1 (en) * 2005-11-18 2011-04-28 Ferrum Ag Centrifuge cartridge
US9636605B2 (en) * 2006-02-25 2017-05-02 Onesubsea Ip Uk Limited Method and apparatus for fluid separation
US20130327726A1 (en) * 2006-02-25 2013-12-12 Cameron International Corporation Method and Apparatus for Fluid Separation
US20080005478A1 (en) * 2006-06-30 2008-01-03 Seagate Technology Llc Dynamic adaptive flushing of cached data
US20110303621A1 (en) * 2007-01-24 2011-12-15 Patel Vipul P Oil centrifuge for extracting particulates from a continuous flow of fluid
US8574144B2 (en) * 2007-01-24 2013-11-05 Fram Group Ip Llc Method for extracting particulates from a continuous flow of fluid
US8956271B2 (en) * 2007-11-26 2015-02-17 Fram Group Ip Llc Method for removing particulates from a fluid
US20120010064A1 (en) * 2007-11-26 2012-01-12 Patel Vipul P Oil centrifuge
CN102413896A (zh) * 2009-04-29 2012-04-11 国际壳牌研究有限公司 用于从包含气体和液体的混合物中移除液体的分离装置
CN102413896B (zh) * 2009-04-29 2014-06-04 国际壳牌研究有限公司 用于从包含气体和液体的混合物中移除液体的分离装置
WO2011129697A1 (en) * 2010-04-15 2011-10-20 Coalessense B.V. Device and method for coalescing droplets dispersed in a flowing mixture
NL2004559C2 (en) * 2010-04-15 2011-10-18 Coalessense B V Device and method for coalescing droplets dispersed in a flowing mixture.
US20110263405A1 (en) * 2010-04-22 2011-10-27 Specialist Process Technologies Limited Separator
US9458485B2 (en) * 2011-04-07 2016-10-04 Life Technologies Corporation System and methods for making and processing emulsions
US9017993B2 (en) 2011-04-07 2015-04-28 Life Technologies Corporation System and methods for making and processing emulsions
US9121047B2 (en) * 2011-04-07 2015-09-01 Life Technologies Corporation System and methods for making and processing emulsions
US20150314294A1 (en) * 2011-04-07 2015-11-05 Life Technologies Corporation System and methods for making and processing emulsions
US20130164789A1 (en) * 2011-04-07 2013-06-27 Life Technologies Corporation System and Methods for Making and Processing Emulsions
US9776146B2 (en) 2011-04-07 2017-10-03 Life Technologies Corporation System and methods for making and processing emulsions
US9901887B2 (en) 2011-04-07 2018-02-27 Life Technologies Corporation Systems and methods for making and processing emulsions
US20140296052A1 (en) * 2011-06-29 2014-10-02 The University Of British Columbia Method and apparatus for continuously fractionating particles contained within a viscoplastic fluid
US9849466B2 (en) * 2011-06-29 2017-12-26 The University Of British Columbia Method and apparatus for continuously fractionating particles contained within a viscoplastic fluid
US10300410B2 (en) * 2014-03-03 2019-05-28 The Trustees Of Princeton University Advanced liquid centrifuge using differentially rotating cylinders and optimized boundary conditions, and methods for the separation of fluids
CN115041308A (zh) * 2017-06-15 2022-09-13 阿法拉伐股份有限公司 离心分离器和操作离心分离器的方法
US11998931B2 (en) * 2017-06-15 2024-06-04 Alfa Laval Corporate Ab Centrifugal separator having a generator for generating an electric current
CN110935198A (zh) * 2019-12-20 2020-03-31 四川大学 一种旋转式微通道破乳方法

Also Published As

Publication number Publication date
FR2057066A1 (ja) 1971-05-07
FR2057066B1 (ja) 1973-01-12
GB1251167A (ja) 1971-10-27
DE2037366A1 (de) 1971-02-18
JPS5231588B1 (ja) 1977-08-16
CH514358A (fr) 1971-10-31

Similar Documents

Publication Publication Date Title
US3695509A (en) Centrifugal separator for separating emulsions
US3006474A (en) Method and means for converting the kinetic energy of a fluid stream into random turbulence
US3092678A (en) Apparatus for gasifying liquids
US5387342A (en) Centrifugal separator and method
US4235602A (en) Installation for mixing and separating two non-miscible liquids, inter alia for liquid-liquid extraction
EP0068792A2 (en) Arrangement of multiple fluid cyclones
US2793186A (en) Apparatus for classifying or settling fluid suspensions
KR950702858A (ko) 현탁물질의 분리
US3794171A (en) Apparatus for purifying waste liquids
US3027390A (en) Apparatus and method for centrifugal purification of fatty oils
US2619280A (en) Centrifugal contactor and method of contacting
US20120074046A1 (en) froth flotation method and an apparatus for extracting a valuable substance from a slurry
US2266521A (en) Countercurrent contact apparatus
EP0574364B1 (en) Centrifuge for oil extraction from oily slurries working without addition of drinkable water
US3282497A (en) Processes and apparatus for the separation of solids from a suspension
US1589097A (en) Apparatus for continuously separating liquids from solids
US5965021A (en) Hydrocyclone
US2638409A (en) Countercurrent extraction apparatus and process
US3107218A (en) Rotating column contact device
US2120786A (en) Treatment of sewage
US4338195A (en) Liquid treatment apparatus
US1682256A (en) Clabifieb and thickener
US3708067A (en) Separating apparatus
US2612356A (en) Homogenizing device
US2641363A (en) Apparatus for clarifying liquids