WO1990004451A1 - Filtration systems - Google Patents

Filtration systems Download PDF

Info

Publication number
WO1990004451A1
WO1990004451A1 PCT/GB1989/001222 GB8901222W WO9004451A1 WO 1990004451 A1 WO1990004451 A1 WO 1990004451A1 GB 8901222 W GB8901222 W GB 8901222W WO 9004451 A1 WO9004451 A1 WO 9004451A1
Authority
WO
WIPO (PCT)
Prior art keywords
stellated
membrane
filter tube
tubes
filter
Prior art date
Application number
PCT/GB1989/001222
Other languages
French (fr)
Inventor
Roger Stanley White
Original Assignee
White, Tessa, Jane
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 White, Tessa, Jane filed Critical White, Tessa, Jane
Publication of WO1990004451A1 publication Critical patent/WO1990004451A1/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/10—Supported membranes; Membrane supports
    • B01D69/107—Organic support material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/06—Tubular membrane modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/06—Tubular membrane modules
    • B01D63/062—Tubular membrane modules with membranes on a surface of a support tube
    • B01D63/063—Tubular membrane modules with membranes on a surface of a support tube on the inner surface thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/04—Tubular membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/10—Supported membranes; Membrane supports
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/20—By influencing the flow
    • B01D2321/2008—By influencing the flow statically
    • B01D2321/2016—Static mixers; Turbulence generators

Definitions

  • This invention relates to filtration systems and particularly to methods of improving the retentate, permeate flow rates and surface area of tubular crossflow filtration systems.
  • Tubular crossflow filtration systems are known in which a fluid containing dissolved and suspended solids, called the retentate, is made to flow across the suface of a membrane or layer of porous media whose pore size is insufficient to permit passage of the particles but which will allow the fluid to flow outwards and be collected, called the permeate.
  • the fluid is generally caused to flow at a high rate to create surface turbulence mini ⁇ mising clogging (blinding) of the membrane by deposited particles.
  • the membranes used in such tubular crossflow filtration systems have a pore size in the nanometre range up to 100 micrometres (microns). These membranes are currently manufactured from porous metal, particulate stone, ceramic or synthetic polymer compositions. The ceramic composit ⁇ ions are frequently based on aluminium and/or zirconium oxides.
  • the polymer compositions may be polya ides, such as nylons, cellulosic, such as cellulose esters, poly- sulphones, polyethylenes and polytetrafluroethylene (PTFE) .
  • the membranes may comprise a single layer or two or more superposed layers. Particularly useful membranes of this type are manufactured in tubular form either as single tubes or banks of tubes.
  • a filter tube comprising at least one layer of a porous membrane and a stellated inner surface.
  • the tube comprises an outer layer of a porous material with an inner coating of a second porous material being the active membrane surface.
  • the inner coating is may be a porous ceramic or a synthetic polymer in a porous form such as a layer of PTFE.
  • the outer and inner porous tube may be covered or have attached a coating, such as a silicone or a synthetic polymer, to minimise adsorption of the permeate to the membrane and the membrane supporting material.
  • the stellated inner surface is fabricated in the form of a spiral having up to 500 turns per metre.
  • the tubes may be prepared by extruding the coarse porosity ceramic outer membrane in paste form and thereafter drying and sintering the extruded tube.
  • the tubes may be slip cast in a porous mould from a slurry. The cast tube is then dried and fired to sinter the casting.
  • a fine porosity ceramic inner membrane may be prepared by slip casting on the inside surface of the coarse membrane.
  • a fine porosity polymer membrane it can be solvent cast on the inner surface of the ceramic membrane by known means.
  • Such methods for preparing polymeric membranes are described in 'Synthetic Membranes : Science, Engineering and Applications' : P M Bungay et al, Reidel Publishing Company 1986.
  • Figure 1 is a perspective view of a filter tube of known type
  • Figure 2 is a perspective view of a multi-channel filter tube of known type
  • Figure 3 is a cross-sectional view of a single filter tube of known type and filter tubes according to the invention.
  • a filter tube of known type see Figure 1, consists of a single tubular membrane 1 having an inner membrane layer 2. Fluid travels along the tube in the direction shown by the arrows 3 and the permeate, free from solids, passes out of the side of the membrane 1 as shown by the arrows 4. It is most important that the flow shown by the arrows 3 is turbulent or the fine membrane layer 2 will become clogged (surface blinded) with deposited solids and become totally or partially impermeable.
  • a multi-channel filter of known type consists of a tubular membrane block 11 pierced by a number of cylindrical channels 12. Each channel 12 has an inner membrane layer 13. Fluid travels along the channels in the direction shown by the arrows 14 and the permeate, filtered material, passes through the block of membrane 11 as shown by the arrows 15. As with the filter tubes it is most important that the flow shown by the arrows 14 is turbulent or the fine membrane layers 13 will become clogged with deposited solids.
  • a cross section of a filter tube of known type, see Figure 3a, is shown on an enlarged scale.
  • the tube has an outer membrane 21 having a coarse porosity and an inner channel 22 having a circular cross section.
  • the inner surface of the membrane 21 carries a second membrane layer 23 having a finer pore size. Turbulence in the fluid passing down the axis of the tube is ensured by pumping the fluid at a high rate of flow.
  • the inner channel 22 of the coarse membrane has a stellated cross section, see Figures 3b and 3c.
  • the stellated cross section increases the effective surface area of the inner flow channel and decreases the cross section of the flow channel thus reducing the mass retentate flow whilst maintaining the velocity of the retentate at the membrane surface 23. Furthermore the stellated contour increases the tendency for turbulent flow to take place so that lower flow rates can be used than with the known filters without clogging.
  • a surface velocity at the membrane should be between 4 to 6 metres per second.
  • the stellated surface provides an increase in surface area of about 25 percent over cylindrical tubes having the same diameter. This will allow a reduction in flow rate of about 50 percent.
  • the induced turbulence caused by the stellations further reduces the necessary flow rate.
  • a membrane surface velocity as high as 6 meters per second is not required when the turbulence is high.
  • the stellated inner surface is fabricated in the form of a spiral.
  • the spiral may have up to 500 turns per metre.
  • the spiral shape together with the stellated cross section makes the filter tube most efficient and provides a high rate of permeate flow in conjunction with a lower rate of retentate flow than that required by known filters to reduce clogging.
  • the single filter tubes according to the invention may be up to 2 metres in length, or even longer, and 3 to 10 mm in average diameter.
  • the peripheral area provided by the stellated inner surface of the tubes is greater than the area available with a conventional tube having a circular inner surface.
  • a filtration system may be formed by arranging one or more filter tubes., according to the invention, to be supplied continuously with a flow of retentate and arranging collecting means to receive the permeate. The permeate is directed to an appropriate collecting vessel.
  • the invention also provides a method of removing fluid from a liquid containing suspended solids and comprising the fluid wherein the liquid is caused to flow through such a filtration system so that the fluid is separated as the permeate.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

Filtration systems which improve the retentate, permeate flow rates and surface area of tubular crossflow filtration systems use filter tubes comprising at least one layer of a porous membrane and a stellated inner surface. The filter tubes may have a membrane comprising two layers, the inner one (23) having finer pores than the outer one (21). In a preferred form the stellated inner surface has a spiral configuration which may have up to 500 turns per metre. The stellated surface provides an increase in surface area of about 25 percent over cylindrical tubes having the same diameter allowing a reduction in flow rate of about 50 percent over prior cylindrical filter tubes. The induced turbulence caused by the spirals further reduces the necessary flow rate.

Description

FIL RATION SYSTEMS
This invention relates to filtration systems and particularly to methods of improving the retentate, permeate flow rates and surface area of tubular crossflow filtration systems.
Tubular crossflow filtration systems are known in which a fluid containing dissolved and suspended solids, called the retentate, is made to flow across the suface of a membrane or layer of porous media whose pore size is insufficient to permit passage of the particles but which will allow the fluid to flow outwards and be collected, called the permeate. In such systems the fluid is generally caused to flow at a high rate to create surface turbulence mini¬ mising clogging (blinding) of the membrane by deposited particles.
The membranes used in such tubular crossflow filtration systems have a pore size in the nanometre range up to 100 micrometres (microns). These membranes are currently manufactured from porous metal, particulate stone, ceramic or synthetic polymer compositions. The ceramic composit¬ ions are frequently based on aluminium and/or zirconium oxides. The polymer compositions may be polya ides, such as nylons, cellulosic, such as cellulose esters, poly- sulphones, polyethylenes and polytetrafluroethylene (PTFE) .
The membranes may comprise a single layer or two or more superposed layers. Particularly useful membranes of this type are manufactured in tubular form either as single tubes or banks of tubes.
According to the present invention there is provided a filter tube comprising at least one layer of a porous membrane and a stellated inner surface.
Preferably the tube comprises an outer layer of a porous material with an inner coating of a second porous material being the active membrane surface. The inner coating is may be a porous ceramic or a synthetic polymer in a porous form such as a layer of PTFE. Additionally or alternat¬ ively the outer and inner porous tube may be covered or have attached a coating, such as a silicone or a synthetic polymer, to minimise adsorption of the permeate to the membrane and the membrane supporting material.
In a most preferred form of the invention the stellated inner surface is fabricated in the form of a spiral having up to 500 turns per metre.
The tubes may be prepared by extruding the coarse porosity ceramic outer membrane in paste form and thereafter drying and sintering the extruded tube. Alternatively the tubes may be slip cast in a porous mould from a slurry. The cast tube is then dried and fired to sinter the casting. A fine porosity ceramic inner membrane may be prepared by slip casting on the inside surface of the coarse membrane. In the case of a fine porosity polymer membrane it can be solvent cast on the inner surface of the ceramic membrane by known means. Such methods for preparing polymeric membranes are described in 'Synthetic Membranes : Science, Engineering and Applications' : P M Bungay et al, Reidel Publishing Company 1986.
In order that the invention may be clearly understood it will now be described with reference to the accompanying drawings in which: Figure 1 is a perspective view of a filter tube of known type, Figure 2 is a perspective view of a multi-channel filter tube of known type, and
Figure 3 is a cross-sectional view of a single filter tube of known type and filter tubes according to the invention.
A filter tube of known type, see Figure 1, consists of a single tubular membrane 1 having an inner membrane layer 2. Fluid travels along the tube in the direction shown by the arrows 3 and the permeate, free from solids, passes out of the side of the membrane 1 as shown by the arrows 4. It is most important that the flow shown by the arrows 3 is turbulent or the fine membrane layer 2 will become clogged (surface blinded) with deposited solids and become totally or partially impermeable.
A multi-channel filter of known type, see Figure 2, consists of a tubular membrane block 11 pierced by a number of cylindrical channels 12. Each channel 12 has an inner membrane layer 13. Fluid travels along the channels in the direction shown by the arrows 14 and the permeate, filtered material, passes through the block of membrane 11 as shown by the arrows 15. As with the filter tubes it is most important that the flow shown by the arrows 14 is turbulent or the fine membrane layers 13 will become clogged with deposited solids.
A cross section of a filter tube of known type, see Figure 3a, is shown on an enlarged scale. The tube has an outer membrane 21 having a coarse porosity and an inner channel 22 having a circular cross section. The inner surface of the membrane 21 carries a second membrane layer 23 having a finer pore size. Turbulence in the fluid passing down the axis of the tube is ensured by pumping the fluid at a high rate of flow. In a filter tube according to the invention the inner channel 22 of the coarse membrane has a stellated cross section, see Figures 3b and 3c. The stellated cross section increases the effective surface area of the inner flow channel and decreases the cross section of the flow channel thus reducing the mass retentate flow whilst maintaining the velocity of the retentate at the membrane surface 23. Furthermore the stellated contour increases the tendency for turbulent flow to take place so that lower flow rates can be used than with the known filters without clogging.
In known filter tubes it is generally recommended that a surface velocity at the membrane should be between 4 to 6 metres per second. For a filter tube having 4 mm internal diameter this represents a flow rate of 0.27 cubic meters per hour; such a tube has a surface area of about 0.012 square metres per metre length. In the case of filter tubes according to the invention, such as those described with reference to figures 3b and 3c, the stellated surface provides an increase in surface area of about 25 percent over cylindrical tubes having the same diameter. This will allow a reduction in flow rate of about 50 percent. The induced turbulence caused by the stellations further reduces the necessary flow rate. A membrane surface velocity as high as 6 meters per second is not required when the turbulence is high.
In a preferred embodiment the stellated inner surface is fabricated in the form of a spiral. The spiral may have up to 500 turns per metre. The spiral shape together with the stellated cross section makes the filter tube most efficient and provides a high rate of permeate flow in conjunction with a lower rate of retentate flow than that required by known filters to reduce clogging. The single filter tubes according to the invention may be up to 2 metres in length, or even longer, and 3 to 10 mm in average diameter. The peripheral area provided by the stellated inner surface of the tubes is greater than the area available with a conventional tube having a circular inner surface.
A filtration system may be formed by arranging one or more filter tubes., according to the invention, to be supplied continuously with a flow of retentate and arranging collecting means to receive the permeate. The permeate is directed to an appropriate collecting vessel. The invention also provides a method of removing fluid from a liquid containing suspended solids and comprising the fluid wherein the liquid is caused to flow through such a filtration system so that the fluid is separated as the permeate.
The invention has been described in detail with particular reference to preferred embodiments thereof, but it will be understood that variations and modifications can be effected within the spirit and scope of the invention.

Claims

1. A filter tube comprising at least one layer of a porous membrane and a stellated inner surface.
2. A filter tube according to claim 1 in which the stellated inner surface has a spiral configuration.
3. A filter tube according to claim 2 in which the stellated inner surface is fabricated in the form of a spiral having up to 500 turns per metre.
4. A filter tube according to any of the preceding claims in which the membrane comprises two layers, the inner one having finer pores than the outer one.
5. A filter tube according to claim 4 in which the membrane comprises an outer layer of a porous ceramic material with an inner coating of a second porous material.
6. A filter tube according to claim 5 in which the inner coating is formed from a synthetic polymer in a porous form such as a layer of PTFE.
7. A filter tube according to any of the preceding claims in which the membrane comprises sintered alumina and/or zirconia or other porous material.
8. Filter tubes as claimed in claim 1 and as herein described with reference to the accompanying drawings.
9. A filtration system comprising one or more filter tubes, as claimed in any of the claims 1 to 8 , adapted to be supplied continuously with a flow of retentate and having collecting means to receive and provide a flow of permeate.
10. A method of removing fluid from a liquid containing suspended solids and comprising the fluid wherein the liquid is caused to flow through a filtration system as claimed in claim 9 so that the fluid is separated as the permeate.
11. Methods of removing fluid from a liquid containing suspended solids, using filter tubes according to any of the 1 to 8 , as herein described.
PCT/GB1989/001222 1988-10-17 1989-10-16 Filtration systems WO1990004451A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8824273.0 1988-10-17
GB8824273A GB2223690B (en) 1988-10-17 1988-10-17 Filtration systems

Publications (1)

Publication Number Publication Date
WO1990004451A1 true WO1990004451A1 (en) 1990-05-03

Family

ID=10645309

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB1989/001222 WO1990004451A1 (en) 1988-10-17 1989-10-16 Filtration systems

Country Status (3)

Country Link
AU (1) AU4415289A (en)
GB (1) GB2223690B (en)
WO (1) WO1990004451A1 (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005079962A1 (en) * 2004-01-21 2005-09-01 Valerio Vernocchi Module with non-deformable support for filter septa and membrane type filter elements

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5112760A (en) * 1990-06-05 1992-05-12 Centocor, Incorporated Mass transfer membrane for oxygenation of animal cell reactors
FR2686269A1 (en) * 1992-01-21 1993-07-23 Millipore Sa FILTERING TUBULAR CARTRIDGE AND ITS APPLICATION TO THE MANUFACTURE OF SPARKLING WINE IN BOTTLE.
GB9504908D0 (en) * 1995-03-10 1995-04-26 Bellhouse Brian John Filter
NL1002397C2 (en) * 1996-02-20 1997-08-25 Stork Friesland Bv Membrane filtration element.
GB0906751D0 (en) * 2009-04-18 2009-06-03 Fairey Filtration Systems Ltd Filter
FR3024663B1 (en) * 2014-08-11 2020-05-08 Technologies Avancees Et Membranes Industrielles NOVEL GEOMETRIES OF TANGULAR FLOW SEPARATION SINGLE-CHANNEL TUBULAR ELEMENTS INCLUDING TURBULENCE PROMOTERS AND MANUFACTURING METHOD
FR3024664B1 (en) * 2014-08-11 2020-05-08 Technologies Avancees Et Membranes Industrielles NOVEL GEOMETRIES OF TANGENTIAL FLOW SEPARATION MULTI-CHANNEL TUBULAR ELEMENTS INCLUDING TURBULENCE PROMOTERS AND MANUFACTURING METHOD
FR3024665B1 (en) * 2014-08-11 2020-05-08 Technologies Avancees Et Membranes Industrielles TANGENTIAL FLOW SEPARATION ELEMENT INCLUDING TRAFFIC OBSTACLES AND MANUFACTURING METHOD
FR3036626B1 (en) 2015-05-29 2019-12-20 Technologies Avancees Et Membranes Industrielles SEPARATION ELEMENT WITH A THREE-DIMENSIONAL CIRCULATION NETWORK FOR THE FLUID MEDIUM TO BE TREATED
FR3060410B1 (en) 2016-12-21 2019-05-24 Technologies Avancees Et Membranes Industrielles TANGENTIAL FLOW SEPARATION ELEMENT INTEGRATING FLEXIBLE CHANNELS
CN108715801B (en) * 2018-06-01 2021-12-03 苏州凯虹高分子科技有限公司 Cell separation filter element and manufacturing method thereof

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3400825A (en) * 1966-08-22 1968-09-10 Frank R. Shippey Desalination cell with osmotic membrane element
US3676193A (en) * 1970-05-08 1972-07-11 Abcor Inc Process for casting integrally supported tubular membranes
GB2011796A (en) * 1978-01-05 1979-07-18 Kuesters E Grooved Filter Elements
WO1986003423A1 (en) * 1984-12-11 1986-06-19 Pabst Richard E Flow through filter with backflush clearing capability
FR2575398A1 (en) * 1984-12-29 1986-07-04 Ngk Insulators Ltd FILTER CONSISTING OF A SUBSTRATE OF POROUS CERAMIC MATERIAL AND A MICROPOROUS MEMBRANE OF POLYMER RESINOUS MATERIAL AND PROCESS FOR PREPARING THE SAME
EP0217482A1 (en) * 1985-07-19 1987-04-08 Hr Textron Inc. Filter element

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE634211A (en) * 1962-07-10
NL179546C (en) * 1973-05-10 Union Carbide Corp MODULE FOR USE IN AN ULTRAFILTRATION DEVICE.
DE2536271C3 (en) * 1975-08-14 1984-08-23 Sintermetallwerk Krebsöge GmbH, 5608 Radevormwald Filter cartridge
JPS5348976A (en) * 1976-10-18 1978-05-02 Nippon Zeon Co Ltd Mass transfer apparatus of hollow fiber type
JPS62266109A (en) * 1986-05-12 1987-11-18 Japan Gore Tex Inc Filter mechanism

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3400825A (en) * 1966-08-22 1968-09-10 Frank R. Shippey Desalination cell with osmotic membrane element
US3676193A (en) * 1970-05-08 1972-07-11 Abcor Inc Process for casting integrally supported tubular membranes
GB2011796A (en) * 1978-01-05 1979-07-18 Kuesters E Grooved Filter Elements
WO1986003423A1 (en) * 1984-12-11 1986-06-19 Pabst Richard E Flow through filter with backflush clearing capability
FR2575398A1 (en) * 1984-12-29 1986-07-04 Ngk Insulators Ltd FILTER CONSISTING OF A SUBSTRATE OF POROUS CERAMIC MATERIAL AND A MICROPOROUS MEMBRANE OF POLYMER RESINOUS MATERIAL AND PROCESS FOR PREPARING THE SAME
EP0217482A1 (en) * 1985-07-19 1987-04-08 Hr Textron Inc. Filter element

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005079962A1 (en) * 2004-01-21 2005-09-01 Valerio Vernocchi Module with non-deformable support for filter septa and membrane type filter elements

Also Published As

Publication number Publication date
GB2223690A (en) 1990-04-18
GB2223690B (en) 1991-05-01
GB8824273D0 (en) 1988-11-23
AU4415289A (en) 1990-05-14

Similar Documents

Publication Publication Date Title
EP0570384B1 (en) Back flushable filtration device and method of forming and using same
US6499606B1 (en) Cross-flow filter membrane and method of manufacturing it
KR100232013B1 (en) Monoless type ceramic filter
EP0780148A1 (en) Filtration device or membrane device with increasing thickness walls
US4186100A (en) Inertial filter of the porous metal type
EP2274066B9 (en) A ceramic dead-end filter, a filter system and method of filtering
WO1990004451A1 (en) Filtration systems
GB1593127A (en) Filter of the porous metal type
JP2011519310A (en) Monolith diaphragm module for filtering liquids
JP4177813B2 (en) Tangential filtration membrane and method for producing the same
US5895572A (en) Porous monolithic support for filtration membranes
EP0310632B1 (en) Cross-flow filtration device and method of manufacturing said device
JP4358538B2 (en) Ceramic filter
EP1832327A2 (en) Filter and method for backwashing of the filter
JP2002143655A (en) Ceramic filter and producing method of ceramic filter
JP7191861B2 (en) Integral membrane filtration structure
SU1708491A1 (en) Filter for cleaning molten metal from non-metallic inclusions
AU2021383406A1 (en) Element for separating a liquid medium with high parietal shear stress
RU2036187C1 (en) Ceramic filtering member
JPH05293342A (en) Ceramic filter
JPH0640938B2 (en) Porous filter
JPS6261323B2 (en)
JPS62149309A (en) Production of ceramic porous thin membrane
JPH0583516B2 (en)

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AT AU BB BG BR CH DE DK FI GB HU JP KP KR LK LU MC MG MW NL NO RO SD SE SU US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE BF BJ CF CG CH CM DE FR GA GB IT LU ML MR NL SE SN TD TG

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642