EP1262225A2 - Dispositif et procédé de préparation d'emulsions - Google Patents

Dispositif et procédé de préparation d'emulsions Download PDF

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Publication number
EP1262225A2
EP1262225A2 EP02011487A EP02011487A EP1262225A2 EP 1262225 A2 EP1262225 A2 EP 1262225A2 EP 02011487 A EP02011487 A EP 02011487A EP 02011487 A EP02011487 A EP 02011487A EP 1262225 A2 EP1262225 A2 EP 1262225A2
Authority
EP
European Patent Office
Prior art keywords
membrane
shaft
housing
emulsion
continuous phase
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.)
Granted
Application number
EP02011487A
Other languages
German (de)
English (en)
Other versions
EP1262225B1 (fr
EP1262225A3 (fr
Inventor
Ursula Dipl.-Ing. Schliessmann
Norbert Dipl.-Ing. Stroh
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.)
Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
Original Assignee
Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
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 Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV filed Critical Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
Publication of EP1262225A2 publication Critical patent/EP1262225A2/fr
Publication of EP1262225A3 publication Critical patent/EP1262225A3/fr
Application granted granted Critical
Publication of EP1262225B1 publication Critical patent/EP1262225B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/43—Mixing liquids with liquids; Emulsifying using driven stirrers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/41—Emulsifying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3131—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit with additional mixing means other than injector mixers, e.g. screens, baffles or rotating elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3133—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit characterised by the specific design of the injector
    • B01F25/31331—Perforated, multi-opening, with a plurality of holes
    • B01F25/313311—Porous injectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3133—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit characterised by the specific design of the injector
    • B01F25/31333—Rotatable injectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/27—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices
    • B01F27/271—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed radially between the surfaces of the rotor and the stator
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/051—Stirrers characterised by their elements, materials or mechanical properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/115—Stirrers characterised by the configuration of the stirrers comprising discs or disc-like elements essentially perpendicular to the stirrer shaft axis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/19—Stirrers with two or more mixing elements mounted in sequence on the same axis
    • B01F27/191—Stirrers with two or more mixing elements mounted in sequence on the same axis with similar elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/21—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by their rotating shafts
    • B01F27/2122—Hollow shafts

Definitions

  • the present invention relates to a Device and a method for producing Emulsions using one or more membranes, through the one disperse phase of a liquid medium into a continuous phase of another liquid Medium is introduced finely divided. At a Emulsion is the disperse phase in the form of fine Drops distributed in the continuous phase.
  • emulsions are often produced in rotor-stator systems.
  • rotor-stator systems are simple agitators, gear rim dispersing machines and colloid mills.
  • the continuous and the disperse phase are brought together in a container and mixed with one another by the operation of the rotor to form an emulsion.
  • High-pressure homogenizers or the application of ultrasound to a system composed of a disperse and continuous phase are known as further systems for producing emulsions.
  • the energy required to operate these devices is very high.
  • there is also a lot of heat which can heat the emulsion to undesirably high temperatures.
  • the diameter of the emulsion droplets is between 0.1 and 100 ⁇ m, with a generally very wide droplet size distribution.
  • Another method for the production of emulsions uses a membrane technology to produce finely divided droplets of the disperse phase in the continuous phase.
  • the disperse phase is pressed through the pores of a membrane, so that drops form on the surface of the membrane, which tear off after reaching a critical drop diameter and are carried away by the continuous phase flowing over the surface.
  • a tubular membrane is used, through which a continuous phase flows.
  • the disperse phase is pressed from the outside through the porous system of the tubular membrane into the continuous phase flowing inside.
  • the flow of the disperse phase comes about due to an applied transmembrane pressure difference.
  • the actual process of emulsification, ie the formation of drops, takes place on the inner surface of the tubular membrane.
  • the droplets continue to grow on this surface until the droplet-removing forces become greater than the forces that hold the droplet to the respective pore.
  • the drop with the diameter reached is then detached from the continuous phase that flows over the membrane surface and carried away by the flow. This enables very homogeneous emulsions with a relatively narrow droplet size distribution to be produced.
  • a strong pump In order to achieve a sufficiently large overflow of the membrane surface through the continuous phase, a strong pump must also be used in these systems, which leads to high energy consumption and undesirable heating of the emulsion produced.
  • the object of the present invention is therein an apparatus and method for Preparation of emulsions to indicate a homogeneous Droplet size distribution with low energy consumption allows.
  • the device has a housing with one and Outlet opening for a continuous phase of a first liquid medium, one rotating in the housing Drivable shaft, on or in the one Feed channel for a disperse phase of a second liquid medium is formed, and one or several hollow membrane bodies on the Shaft are attached.
  • the feed channel is at the present device on the shaft with the hollow trained membrane bodies connected to the Feed of the disperse phase via the feed channel in to enable the membrane body.
  • the shaft is driven by a motor that is separate from the Device may be present, driven in rotation, so that the attached membrane body in the continuous phase around the longitudinal axis of the shaft rotate.
  • the disperse phase is through the pores the membrane body into the continuous phase pressed, whereby the droplet detachment as in the Membrane technology described above takes place.
  • the present device and the associated method have particular advantages due to their structure and the associated mode of operation. Due to the rotation of the hollow membrane bodies in the continuous phase, it is not necessary to additionally pump this phase around in the housing. The required overflow speed of the continuous phase over the membrane surface is already achieved by rotating the membrane body. A sufficiently large pump with a correspondingly high energy consumption can therefore be dispensed with in the present device and the present method. Even if the continuous phase is additionally pumped around in the housing, a much smaller pump is sufficient for this, since it does not have to be designed to generate the required overflow speeds. Due to the rotation of the membrane body in the continuous phase, centrifugal forces occur which act on the disperse phase in the membrane bodies in addition to the pressure present.
  • the hollow membrane bodies attached to the shaft can take advantage of the above effect different have geometric shapes. You can For example, as a tubular boom around the Shaft axis can be arranged around. A preferred one However, embodiment sets disc-shaped A membrane hollow body, through the center of symmetry Wave runs. The individual discs show preferably the same disc diameter on and are approximately constant distance and parallel arranged to each other on the shaft. This makes one approximately cylindrical rotation space, defined by a cylindrical housing are enclosed can.
  • the Feed channel not as a separate channel on the shaft attached.
  • the shaft is rather a hollow shaft trained so that it forms the supply channel itself.
  • the connection between the supply channel and the interior the hollow membrane body is opened using suitable openings the hollow shaft or the feed channel and the membrane body at the corresponding attachment points of the Membrane body reached on the shaft.
  • the housing preferably has an inner contour based on the outer shape of the membrane body and the Shaft is adjusted without impeding its rotation. Between the inner contour and the surface of the Membrane body and the shaft remain Gap from the continuous phase is filled out. With such a configuration it is ensured that a large proportion of the volume continuous phase present in the housing the surface of the membrane body is in contact.
  • the present device can be used for both batch and continuous production of emulsions.
  • the continuous phase is first introduced into the housing.
  • the membrane bodies are then set in motion via the shaft and the disperse phase is introduced into the membrane bodies under pressure. After a predeterminable time interval, which is sufficient for the production of the desired emulsion, this is drawn off via the outlet opening and the entire process starts again.
  • the continuous phase is continuously supplied via the inlet opening and the emulsion is continuously drawn off via the outlet opening.
  • the pump required for this only has to ensure the transport of the liquid medium from the inlet to the outlet opening.
  • the required overflow speeds over the surface of the membrane body are achieved by the rotation of the membrane body.
  • the number of membrane bodies as well as the dimensions of the membrane body and the Housing as well as the pressure of the disperse phase in the Membrane bodies and the dwell time of the continuous Phase chosen in the housing by a specialist to suit the desired result depending on the used to reach liquid media.
  • the same goes for for the choice of materials of the membrane body as well their separation limits.
  • ceramic materials for the membrane body also polymer materials or other inorganic materials, such as metals, Carbon, glasses, are used.
  • the bringing in the disperse in the continuous phase can by the choice of membrane materials with defined Surface properties can be improved. It can it may be advantageous to make the membrane surface hydrophilic, to be hydrophobic to oleophobic.
  • membrane material This can through the choice of membrane material or through additional coatings also for inorganic Materials can be achieved.
  • the membranes themselves can be used as nanofiltration membranes, ultrafiltration membranes or microfiltration membranes his.
  • a suitable material is used for the housing chosen that with the liquid media used is tolerated.
  • FIG. 1 shows schematically the mode of operation of membrane technology for the production of emulsions, as is known from the prior art.
  • a tubular membrane 12 is used, through which a continuous phase 9 flows.
  • the disperse phase 8 is pressed through the pores 13 of the tubular membrane 12, so that droplets 15 form on the inner membrane surface, which are entrained by the continuous phase 9 after reaching a certain droplet size, so that they emerge at the outlet the tube membrane 12 is an emulsion 10.
  • a sufficiently high overflow speed of the continuous phase 9 must be achieved over the membrane surface 14, which requires a pump with high energy consumption.
  • FIG. 2 shows an embodiment of a Device according to the present invention, the no such high energy consumption to generate the Has emulsion.
  • the device consists of a Housing 1 with an inlet opening 2 for the continuous phase 9 and an outlet 3 for the finished emulsion. On the 2 and the Outlet opening 3 are each provided to 16 the inflow or outflow of the continuous phase 9 or to be able to interrupt the emulsion 10.
  • the housing is a shaft 4 that can be driven in rotation trained on the four in the present example disk-shaped membrane body 6 are attached.
  • the Wave 4 is a hollow shaft, which simultaneously the Feed channel 5 for the disperse phase 8 forms.
  • the Feed channel 5 is attached to the membrane discs 6 with the hollow shaft 4 with the hollow Interiors of the trained as filter elements Membrane discs 6 connected.
  • the hollow shaft 4 runs here by the symmetry center of the individual Membrane disks 6 so that they are about their axis of symmetry are driven in rotation by the hollow shaft 4.
  • the Housing 1 has an inner contour 7, which is based on the Contour of the membrane discs 6 and the hollow shaft 4th adjusts so that only small gaps between the inner contour 7 and the membrane bodies 6 or the hollow shaft 4, as shown in the figure can be seen. These gaps 11 form the Feed or emulsion space through which the continuous Phase 9 on the surfaces of the membrane body 6 is led past.
  • the hollow shaft 4 is over a corresponding bearing 17 within the housing 1 stored.
  • the membrane discs 6 have a diameter of approximately 150 mm, the housing has a diameter and a height of the order of 20 cm.
  • the Membrane disks themselves are made of a ceramic material educated.
  • the disperse phase 8 is introduced under pressure, which is applied, for example, by a pump or a gas cushion generated by compressed air, through the feed channel 5 of the hollow shaft 4 into the membrane disks 6.
  • the continuous phase 9 is conducted via the valve 16 and the inlet opening 2 into the emulsion space 11 of the housing 1.
  • the membrane disks are rotated in the continuous phase 9 by rotary drive of the shaft 4. This rotation causes an overflow of the membrane surfaces with the continuous phase 9, which is necessary for the detachment of the droplets of the disperse phase 8 from the surface of the membrane body 6.
  • the detachment mechanism is carried out in the same way as in the conventional membrane technology of FIG. 1.
  • the present device and the associated processes are both oil / water as well Water / oil emulsions and liposomes can be produced.
  • the Device leads to a slight heating of the Emulsion during the manufacturing process, which is precisely what Use of heat sensitive substances of great Advantage is.
  • the technology can be achieved with the present device also a sterile way of driving without intermediate sterilization to the end product.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Colloid Chemistry (AREA)
  • Medicinal Preparation (AREA)
  • Polymerisation Methods In General (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)
EP02011487A 2001-06-02 2002-05-24 Dispositif et procédé de préparation d'emulsions Expired - Lifetime EP1262225B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10127075A DE10127075C2 (de) 2001-06-02 2001-06-02 Vorrichtung und Verfahren zur Herstellung von Emulsionen mittels Membrankörpern
DE10127075 2001-06-02

Publications (3)

Publication Number Publication Date
EP1262225A2 true EP1262225A2 (fr) 2002-12-04
EP1262225A3 EP1262225A3 (fr) 2003-05-02
EP1262225B1 EP1262225B1 (fr) 2006-10-18

Family

ID=7687130

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02011487A Expired - Lifetime EP1262225B1 (fr) 2001-06-02 2002-05-24 Dispositif et procédé de préparation d'emulsions

Country Status (6)

Country Link
EP (1) EP1262225B1 (fr)
AT (1) ATE342765T1 (fr)
DE (2) DE10127075C2 (fr)
DK (1) DK1262225T3 (fr)
ES (1) ES2273944T3 (fr)
PT (1) PT1262225E (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006021375A1 (fr) * 2004-08-23 2006-03-02 Eth-Zürich, Institut Für Lebensmittelwissenschaft, Laboratorium Für Lebensmittelverfahren- Stechnik Procede pour produire par une action mecanique douce des micro et nanoemulsions finement dispersees a distribution dimensionnelle etroite des gouttes et dispositif pour la mise en oeuvre dudit procede
WO2006089939A1 (fr) * 2005-02-24 2006-08-31 Basf Aktiengesellschaft Procede de production d'une dispersion polymere
WO2010072237A1 (fr) * 2008-12-23 2010-07-01 Kmpt Ag Procédé et dispositif pour traiter des fluides
WO2010072230A1 (fr) * 2008-12-22 2010-07-01 Kmpt Ag Procédé et dispositif destiné à produire des émulsions et/ou suspensions
WO2010136602A1 (fr) * 2009-05-29 2010-12-02 Novoflow Gmbh Système de manipulation de fluide et ses utilisations
GB2505160A (en) * 2012-07-06 2014-02-26 Micropore Technologies Ltd Dispersion apparatus with membrane
WO2014133701A1 (fr) 2013-02-27 2014-09-04 Rohm And Haas Company Émulsification par balayage de membrane
WO2019219890A1 (fr) 2018-05-17 2019-11-21 Csl Behring Ag Procédé et système d'extraction de protéine

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10306259A1 (de) * 2003-02-14 2004-09-02 Ferrero Ohg Mbh Auf Milchbestandteilen basierende Süßware mit definierten Speisefettagglomeraten, sowie Verfahren und Vorrichtung zu ihrer Herstellung
MY149295A (en) 2006-07-17 2013-08-30 Nestec Sa Cylindrical membrane apparatus for forming foam
US8771778B2 (en) 2010-09-09 2014-07-08 Frito-Lay Trading Company, Gmbh Stabilized foam

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2146867A1 (de) * 1971-09-20 1973-04-05 Kalle Ag Rotierende filtereinrichtung
DE4329077C1 (de) * 1993-08-30 1994-07-14 Chmiel Horst Konzentrisch angeordnete mikroporöse Zylinder zum Stoffaustausch in feinkörnigen Schüttungen, konzentrierten Suspensionen oder Emulsionen
DE19823839A1 (de) * 1998-05-29 1999-12-09 Franz Durst Verfahren und Vorrichtung zum Mischen und Dispergieren mindestens zweier Phasen
WO2001045830A1 (fr) * 1999-12-22 2001-06-28 University Of Leeds Membrane de rotation
US6386751B1 (en) * 1997-10-24 2002-05-14 Diffusion Dynamics, Inc. Diffuser/emulsifier

Family Cites Families (3)

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Publication number Priority date Publication date Assignee Title
US4201691A (en) * 1978-01-16 1980-05-06 Exxon Research & Engineering Co. Liquid membrane generator
JPS58216726A (ja) * 1982-06-10 1983-12-16 Toshio Araki エマルジヨン流体の製造装置
JPH082416B2 (ja) * 1988-09-29 1996-01-17 宮崎県 エマルションの製造方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2146867A1 (de) * 1971-09-20 1973-04-05 Kalle Ag Rotierende filtereinrichtung
DE4329077C1 (de) * 1993-08-30 1994-07-14 Chmiel Horst Konzentrisch angeordnete mikroporöse Zylinder zum Stoffaustausch in feinkörnigen Schüttungen, konzentrierten Suspensionen oder Emulsionen
US6386751B1 (en) * 1997-10-24 2002-05-14 Diffusion Dynamics, Inc. Diffuser/emulsifier
DE19823839A1 (de) * 1998-05-29 1999-12-09 Franz Durst Verfahren und Vorrichtung zum Mischen und Dispergieren mindestens zweier Phasen
WO2001045830A1 (fr) * 1999-12-22 2001-06-28 University Of Leeds Membrane de rotation

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
DATABASE WPI Week 199020 Derwent Publications Ltd., London, GB; AN 1990-151461 XP002233393 & JP 02 095433 A ((MIYA-N)MIYAZAKI KEN), 6. April 1990 (1990-04-06) *

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006021375A1 (fr) * 2004-08-23 2006-03-02 Eth-Zürich, Institut Für Lebensmittelwissenschaft, Laboratorium Für Lebensmittelverfahren- Stechnik Procede pour produire par une action mecanique douce des micro et nanoemulsions finement dispersees a distribution dimensionnelle etroite des gouttes et dispositif pour la mise en oeuvre dudit procede
US8267572B2 (en) 2004-08-23 2012-09-18 ETH-Zurich Institut fur Lebensmittelwissenschaft, Laboratorium fur Lebensmittelverfahren-Stechnik ETH-Zentrum/LFO Method for gentle mechanical generation of finely dispersed micro-/nano-emulsions with narrow particle size distribution and device for carrying out said method
WO2006089939A1 (fr) * 2005-02-24 2006-08-31 Basf Aktiengesellschaft Procede de production d'une dispersion polymere
WO2010072230A1 (fr) * 2008-12-22 2010-07-01 Kmpt Ag Procédé et dispositif destiné à produire des émulsions et/ou suspensions
WO2010072237A1 (fr) * 2008-12-23 2010-07-01 Kmpt Ag Procédé et dispositif pour traiter des fluides
WO2010136602A1 (fr) * 2009-05-29 2010-12-02 Novoflow Gmbh Système de manipulation de fluide et ses utilisations
GB2505160A (en) * 2012-07-06 2014-02-26 Micropore Technologies Ltd Dispersion apparatus with membrane
WO2014133701A1 (fr) 2013-02-27 2014-09-04 Rohm And Haas Company Émulsification par balayage de membrane
US9393532B2 (en) 2013-02-27 2016-07-19 Dow Global Technologies Llc Swept membrane emulsification
WO2019219890A1 (fr) 2018-05-17 2019-11-21 Csl Behring Ag Procédé et système d'extraction de protéine

Also Published As

Publication number Publication date
EP1262225B1 (fr) 2006-10-18
DK1262225T3 (da) 2007-02-19
ES2273944T3 (es) 2007-05-16
EP1262225A3 (fr) 2003-05-02
DE10127075C2 (de) 2003-04-10
DE10127075A1 (de) 2002-12-12
DE50208468D1 (de) 2006-11-30
ATE342765T1 (de) 2006-11-15
PT1262225E (pt) 2007-02-28

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