WO1994009889A1 - Appareil pour traitment d'un liquide - Google Patents

Appareil pour traitment d'un liquide Download PDF

Info

Publication number
WO1994009889A1
WO1994009889A1 PCT/GB1993/002146 GB9302146W WO9409889A1 WO 1994009889 A1 WO1994009889 A1 WO 1994009889A1 GB 9302146 W GB9302146 W GB 9302146W WO 9409889 A1 WO9409889 A1 WO 9409889A1
Authority
WO
WIPO (PCT)
Prior art keywords
filtrate
bed
liquid
membrane
filtration
Prior art date
Application number
PCT/GB1993/002146
Other languages
English (en)
Inventor
Simon Dennis Roe
Anthony Henry Reading
Original Assignee
United Kingdom Atomic Energy Authority
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 United Kingdom Atomic Energy Authority filed Critical United Kingdom Atomic Energy Authority
Priority to AU52845/93A priority Critical patent/AU5284593A/en
Priority to GB9508171A priority patent/GB2286344B/en
Publication of WO1994009889A1 publication Critical patent/WO1994009889A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/18—Apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • 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
    • B01D63/02—Hollow fibre 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
    • B01D63/02—Hollow fibre modules
    • B01D63/024—Hollow fibre modules with a single potted end
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/40—Adsorbents within the flow path

Definitions

  • This invention relates to an apparatus for treating a liquid, particularly but not exclusively a liquid which contains particulate material, and for separating a material dissolved in the liquid from the liquid.
  • a precipitate may be removed from a liquid stream by cross-flow membrane filtration; optionally the filtrate may subsequently be passed through an ion exchange column if removal of for example caesium ions is required.
  • ion exchange column if removal of for example caesium ions is required.
  • Combining different processes into a single treatment unit has also been suggested; for example Grinstead et al. (US 4 976 866) describe a unit which combines through-flow filtration through two tubular membranes, with ion exchange, the ion exchanger occupying the annular space between the membranes. In such an arrangement any non-uniformity of flow through the membranes leads to channelling through the ion exchanger, and so to premature breakthrough.
  • an apparatus for treating a liquid comprising means, including a filtrate-collecting chamber, and at least one filtration membrane, to subject the liquid undergoing treatment to cross-flow filtration, so that a filtrate liquid passes through the membrane into the filtrate collecting chamber, a filtrate treatment chamber containing a bed of particulate adsorbent material, means to distribute the filtrate liquid from the filtrate collecting chamber to the filtrate treatment chamber, and an outlet for treated filtrate which has passed through the bed of adsorbent material, the cross-flow filtration means being integral with the filtrate treatment chamber.
  • the apparatus is cylindrical, and the filtrate collecting chamber and the filtrate treatment chamber are concentric.
  • the filtrate treatment chamber may be of annular form, surrounding the filtrate collecting chamber.
  • the distribution means and the outlet are arranged so the filtrate flows through the bed in a direction parallel to the longitudinal axis of the apparatus; alternatively the filtrate may be arranged to flow radially.
  • the cross-filtration stage minimizes problems of membrane fouling, which can be particularly severe with dead-end filtration if the liquid contains particulate materials; and also minimizes fouling of the adsorbent material.
  • the filtrate collecting chamber and the distribution means minimize the problems of channelling of liquid through the adsorbent bed, which can lead to premature breakthrough of the material being adsorbed; the invention thus improves the efficiency of use of the adsorbent material.
  • the concentric annular arrangement enables a large volume of adsorbent material to be used, so large quantities of solute can be adsorbed before the adsorptive capacity of the bed is reached.
  • the provision of filtration and adsorption within a single, integral apparatus leads to a compact design, so saving on space.
  • the liquids undergoing treatment are more securely contained, and the apparatus can operate effectively under aseptic conditions, as the reduction in surface area and in liquid-tight joints reduces the risk of invasion of the apparatus by micro-organisms.
  • the adsorbent bed is in close proximity to the filter the time for which a solute is in free solution is minimised; this is particularly advantageous in recovering labile products.
  • the apparatus can reduce processing time, and can improve product yields.
  • filtration membranes there are a plurality of filtration membranes, each of tubular form, through which the liquid flows are in parallel, which extend through a common filtrate collecting chamber.
  • the filtration membranes are microfiltration membranes with pore sizes in the range 0.02 to 10 microns, particularly those with pore sizes in the range 0.05 to 0.5 microns, for example 0.1 microns or 0.45 microns. For dealing with liquids containing even smaller particles it may be desirable to use ultrafiltration membranes .
  • the tubular membranes may comprise hollow fibres of membrane material, typically of diameter less than 2mm, or may comprise a porous tubular support' (of porous ceramic or porous carbon, for example) with membrane material coating the inner surface, which may be of inner diameter between 1mm and 20mm.
  • the former are inexpensive and can provide a compact apparatus, while the latter are robust, and can be used to treat viscous liquids or liquids with a high solids content.
  • the pressure drop across the membrane clearly depends on the nature of the liquid, on the pore size, and on the rate at which filtrate passes through the membrane. Desirably these parameters are such that the pressure drop is no more than 5 atmospheres, more preferably about 1 atmosphere (100 kPa) .
  • the particulate adsorbent material may comprise particles of size in the range 1 micron to 5mm.
  • smaller particles also provide a larger pressure drop across the bed (for the same flow rate and bed thickness) , and the pressure drop across the bed is desirably no more than 5 atmospheres, as higher pressures make pumping the liquid more difficult, and require stronger construction materials for the apparatus.
  • the particles are of a size in the range 10 microns to 1mm, more preferably between 50 microns and 300 microns, for example about 100 microns.
  • the time taken for a portion of the filtrate to flow through the bed should be significantly more than the time taken for a solute molecule to diffuse into contact with an adsorbent particle, so as to ensure adsorption occurs.
  • D is the diffusion coefficient for that solute.
  • D the diffusion coefficient for alpha amylase (a protein of molecular weight 55000) in water is 6.5 x 10 -11 m 2 /s.
  • t 19.2 seconds
  • the bed is sufficiently thick that the filtrate flow time through it is at least five times, more preferably at least ten times, greater than the diffusion time, so as to ensure adsorption and minimize breakthrough.
  • adsorbent particles depends upon what solute is to be adsorbed. They may for example comprise ion exchange materials such as resins, or a derivatised material such as QA-cellulose, or a mixed- functionality adsorbent such as QMA spherosil (a wide pore (0.1 micron) silica-based material), or a hydrophobic adsorbent such as Amberlite XAD resin. They may be of spherical shape or of fibrous shape, or indeed of any shape.
  • adsorbents which combine ion exchange with hydrophobic characteristics, or hydrophobic adsorbents, are preferred if the filtrate has a conductivity above about 1 S m _1 (corresponding to a salt concentration of about 0.1 M) . At lower conductivities ion exchangers can be used.
  • adsorbed material is subsequently eluted depends on the type of adsorber; if the adsorber is an ion exchange material the solute may be eluted with 0.5 M to 1.0 M salt, with a mixed functionality adsorbent the solute may be eluted with 0.5 M salt and a water-miscible solvent such as acetone, ethanol or methanol, typically at between 5 and 20% by volume, and with a non-ionic adsorbent the solute may be eluted with water and 10% acetone or another solvent, or by reducing the conductivity of the solution.
  • a water-miscible solvent such as acetone, ethanol or methanol
  • Figure 1 shows a longitudinal sectional view through a liquid treatment apparatus
  • Figure 2 shows a longitudinal sectional view through an alternative liquid treatment apparatus
  • FIG. 3 shows diagrammatically the flow system in the valve block of the apparatus of Figure 2;
  • Figure 4 shows a longitudinal sectional view through another liquid treatment apparatus.
  • a liquid treatment apparatus 10 includes an outer tube 12 of polymethylmethacrylate whose ends are closed by end blocks 14 and 16 held axially by annular end plates 18 clamped together by four rods 20 (only two are shown) with threaded ends and nuts.
  • Associated with each end block 14 and 16 is a respective flanged sleeve 22 and 23, an O-ring 24 being located between the end of the sleeve 22 or 23 and a step on the outer surface of the end block 14 or 16, and nuts engaging bolts 26 embedded in the end block 14 or 16 enable the O-ring 24 to be compressed so as to ensure a good seal between the end block 14 or 16 and the outer tube 12 .
  • the lower surface of the upper end block 14 defines a central cylindrical recess 30, from which a duct extends axially to a stub outlet pipe 32- projecting from the upper surface of the end block 14.
  • the lower end block 16 defines a large cup-shaped recess 34 in its upper surface, and a duct extends axially from the recess 34 to a stub pipe 36 projecting from the lower surface.
  • An inner block 40 locates in the recess 34, and a tube 42 integral with the block 40 extends coaxially within the pipe 36, defining an annular channel 43 between them, and having a threaded end portion projecting beyond the end of the pipe 36.
  • the block 40 is supported by studs 38 clear of the bottom of the recess 34 so the channel 43 communicates with the upper surface of the lower end block 16.
  • a cap 44 seals the lower end of the annular channel 43, and an outlet fitting 45 is provided near the end of the pipe 36 communicating with the channel 43.
  • a central cylindrical recess 46 (with which the bore of the tube 42 communicates) , which is stepped so as to define a shallow annular recess 47 around its mouth.
  • the module 50 includes a polymethylmethacrylate tube 52 of uniform bore, but with end portions of reduced external diameter which locate in the recesses 30 and 46, sealed to the upper end block 14 by an O-ring in the recess 30, and sealed to the inner block 40 by O-rings in the recess 46 and in the annular recess 47.
  • Four equally spaced apertures 54 are defined through the wall of the tube 52 near the upper end, but outside the recess 30.
  • the tube 52 encloses about fifty polyethersulphone hollow fibres
  • each of interna.1 diameter 1mm and whose walls define pores of diameter 0.1 microns.
  • the end portions of the fibres 56 are embedded in resin, but their ends are open.
  • the annular chamber defined between the outer tube 12 and the module 50 is almost filled with particles of ion exchange resin 58, but leaving a void between the top of the bed of resin 58 and the lower surface of the end block 14 with which the apertures 54 communicate.
  • Above and below the bed of resin 58 are annular stainless steel wire meshes 60.
  • a liquid to be treated is supplied under pressure to the bottom of the tube 42, and so flows along the hollow fibres 56 of the module 50 to emerge from the stub outlet pipe 32.
  • the pressure drop across the walls of the hollow fibres 56 is desirably no greater than 1.5 atmospheres to avoid damaging the fibres 56. Filtrate which passes through the pores in the walls of the fibres 56 then flows upwardly in the tube 52 to emerge through the apertures
  • FIG. 2 there is shown an alternative liquid treatment apparatus 70, with several similarities to that of Figure 1.
  • the module 50 extends coaxially within an outer tube 72 so as to define an annular space 73, the tube 72 having flanges and end portions of wider bore.
  • Annular end blocks 74 and 75 are attached by bolts 76 to the flanges at the ends of the outer tube 72, and are sealed to the wider bore portions of the tube 72 and to the steps in the external diameter of the tube 52 (of the module 50) by gaskets 77 with holes which communicate with the annular space 73.
  • Stoppers 78 with an axial bore and a threaded external surface engage a threaded portion of the bore of each end block 74 and 75 and are sealed by gaskets 79 to the ends of the module 50.
  • the annular space 73 is filled with a particulate affinity adsorbent material 80 such as protein A on agarose beads (which is highly selective for antibodies) , with glass wool plugs 82 at each end.
  • the lower end block 74 defines four equally spaced ducts 84 which communicate between the holes in the gasket 77 and an annular duct 85 from which an outlet duct 86 emerges radially.
  • the upper end block 75 defines a circumferential groove on the portion of its bore adjacent to the apertures 54, and four equally spaced ducts 87 (only one is shown) , between the groove and the upper surface of the block 75.
  • the block 75 also defines four equally spaced ducts 89 (only one is shown) between the holes in the upper gasket 77 and the upper surface of the block 75. (The ducts 87 and 89, although shown in the same plane in Figure 2, are actually in different planes) .
  • valve block 90 Above the upper end block is an annular valve block 90, attached to it by the bolts 76, and sealed by a gasket 91 which defines holes where the ducts 87 and 89 emerge.
  • gasket 91 In the lower surface of the valve block 90 are two concentric annular grooves 92 and 93 which act as manifolds for the ducts 87 and the ducts 89 respectively.
  • the valve block 90 also includes three adjustable needle valves 94, 95 and 96, and ducts described in relation to Figure 3.
  • valve block 90 the ducts in the valve block 90 and the valves 94, 95 and 96 are shown diagrammatically.
  • the manifold grooves 92 and 93 are connected by a duct 97 in which is the valve 94.
  • a duct in which is a valve At either side of the valve 94 is a T-junction with a duct in which is a valve: the inlet duct 98 with the valve 95 and the inlet duct 99 with the valve 96.
  • the liquid to be treated is supplied under pressure to the bore of the lower stopper 78, and so flows through the hollow fibres 56 of the module 50 to emerge from the bore of the upper stopper 78.
  • a filtrate liquid passes through the pores of the fibres 56 into the tube 52 of the module 50, and flows out of the apertures 54 into the circumferential groove and so via the ducts 87 to the manifold groove 92 in the valve block 90.
  • the valves 95 and 96 are closed, and the valve 94 is open and adjusted to provide a desired pressure drop across the walls of the hollow fibres 56.
  • the filtrate hence flows via the duct 97 to the manifold groove 93 and so via the ducts 89 to the annular space 73.
  • the filtrate emerges, via the ducts 84 and the annular duct 85, from the outlet duct 86.
  • the depth of the bed of adsorbent material 80 in the apparatus 70 is the same as that of the bed of material 58 in the apparatus 10 (as both are equal to the length of the wider diameter part of the module 50, which is about 125 mm) , but the annular space 73 is narrower so less adsorbent material is required (the radial widths are about 3mm and 16mm respectively) .
  • This may be preferable where the adsorbent material 80 is expensive, although the adsorptive capacity is correspondingly reduced, and so elution and regeneration will be necessary after a shorter period of operation.
  • regeneration can readily be performed in situ, as described above, whereas in the apparatus 10 the ion exchange material 58 would have to be removed from the apparatus 10 to be regenerated.
  • a liquid treatment apparatus may differ in many ways from those described above.
  • a different filtration module might be used, for example one incorporating porous carbon tubes of internal diameter 10mm with a coating of zirconia to provide a desired pore size.
  • Such tubes can withstand much higher pressure differences than can the hollow fibres 56 of the module 50, and because of their larger bore are suitable for use with more viscous liquids or those with more particulates.
  • the apparatuses 10 and 70 have been described in the orientation as shown in the drawings, using terms such as upper and lower, nevertheless the apparatuses can be operated in any desired orientation.
  • the apparatus 10 or 70 is typically entirely filled with a liquid such as water, prior to operation as described.
  • the apparatus 10 or 70 can be of a desired size and throughput, and can be scaled up, without changing the depth of the adsorbent bed, by increasing the diameter of the adsorbent-filled chamber.
  • the filtrate flows radially through an adsorbent bed; in this case the apparatus can be scaled up by merely changing its length, without thereby changing the pressure drop.
  • Such an apparatus 100 is shown in Figure 4, to which reference is now made.
  • the liquid treatment apparatus 100 includes an upper circular end plate 102 and a lower circular end plate 104 held together by bolts (not shown) . Between the end plates 102 and 104 extends an outer polymethyl- methacrylate tube 106, a pleated tubular filter membrane 108, and two stainless steel mesh tubes 110 and 112 all of which are concentric and spaced apart from each other, and which are sealed to the end plates 102, 104 by gaskets 113, 114, 115. The annular chamber between the mesh tubes 110 and 112 is filled with particulate ion exchange medium 118.
  • An inlet tube 120 for a liquid to be treated communicates via several radial ducts 122 in the upper end plate 102 with the annular channel 124 outside the filter membrane 108; several similar ducts 125 in the lower end plate 104 provide communication between the channel 124 and an outlet pipe 126.
  • a permeate outlet pipe 128 communicates with the bore of the inner mesh tube 112.
  • the apparatus 100 operates in a similar manner to that described earlier.
  • the liquid to be treated is supplied via the inlet tube 120, undergoes cross-flow filtration as it flows through the channel 124, and emerges from the outlet pipe 126 (which incorporates a valve to control the operating pressure) .
  • the liquid may be treated once, or be recirculated.
  • the filtrate flows through the bed of adsorbent medium 118 radially, to emerge from the pipe 128.
  • the end plates 102, 104 may define ducts (not shown) with valves, communicating with the chamber between the mesh tubes 110, 112, so the adsorbent can be regenerated without dismantling the apparatus 100.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Analytical Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)

Abstract

L'invention concerne un appareil (70) avec lequel un liquide tel qu'un effluent ou le liquide de sortie d'un réacteur biologique, peut être traité pour, par exemple, enlever et concentrer les métaux lourds ou pour séparer une enzyme. L'appareil comporte un module de filtration (50) et un lit de matériau absorbant (80), dans une unité complète, le liquide étant soumis à une filtration par flux transversal et le filtrat étant collecté dans une chambre (52) avant d'être distribué dans le lit absorbant. L'encrassement de la membrane filtrante (56) et du matériau absorbant (80) est supprimé et l'écoulement à travers le lit absorbant est empêché.
PCT/GB1993/002146 1992-10-23 1993-10-18 Appareil pour traitment d'un liquide WO1994009889A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU52845/93A AU5284593A (en) 1992-10-23 1993-10-18 Liquid treatment apparatus
GB9508171A GB2286344B (en) 1992-10-23 1993-10-18 Liquid treatment apparatus and method

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB929222248A GB9222248D0 (en) 1992-10-23 1992-10-23 Liquid treatment apparatus
GB9222248.8 1992-10-23

Publications (1)

Publication Number Publication Date
WO1994009889A1 true WO1994009889A1 (fr) 1994-05-11

Family

ID=10723908

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB1993/002146 WO1994009889A1 (fr) 1992-10-23 1993-10-18 Appareil pour traitment d'un liquide

Country Status (3)

Country Link
AU (1) AU5284593A (fr)
GB (2) GB9222248D0 (fr)
WO (1) WO1994009889A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999022850A1 (fr) * 1997-11-04 1999-05-14 Millipore Corporation Dispositif de purification a membrane
WO1999025726A1 (fr) * 1997-11-14 1999-05-27 New Jersey Institute Of Technology Procede et appareil d'isolation et de purification de biomolecules
US6986847B2 (en) 2002-05-10 2006-01-17 New Jersey Institute Of Technology Method and apparatus for isolation and purification of biomolecules
GB2436076A (en) * 2006-03-17 2007-09-19 Fairey Ceramics A fluid treatment assembly

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2040724A (en) * 1979-01-29 1980-09-03 Baxter Travenol Lab Plasma treatment apparatus
FR2510412A1 (fr) * 1981-07-29 1983-02-04 Layme Investment Bv Appareil de filtration du sang et d'epuration simultanee de l'hemofiltrat
US4711723A (en) * 1986-05-27 1987-12-08 Nimbus Water Systems, Inc. Water purification system
WO1988009693A1 (fr) * 1987-06-03 1988-12-15 Eastman Kodak Company Appareil d'osmose inverse
JPH0356126A (ja) * 1989-07-26 1991-03-11 Hitachi Ltd 脱塩機能を有する中空糸膜フィルタ
EP0434219A1 (fr) * 1989-11-22 1991-06-26 Alberta Research Council Elément formé d'un faisceau de fibres creuses
JPH04145932A (ja) * 1990-10-04 1992-05-19 Toshiba Corp 中空糸膜濾過装置
JPH04180887A (ja) * 1990-11-16 1992-06-29 Mitsubishi Rayon Co Ltd 浄水器

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5032268A (en) * 1989-08-17 1991-07-16 Wallace von Medlin Self-contained canister unit for filtering tap water

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2040724A (en) * 1979-01-29 1980-09-03 Baxter Travenol Lab Plasma treatment apparatus
FR2510412A1 (fr) * 1981-07-29 1983-02-04 Layme Investment Bv Appareil de filtration du sang et d'epuration simultanee de l'hemofiltrat
US4711723A (en) * 1986-05-27 1987-12-08 Nimbus Water Systems, Inc. Water purification system
WO1988009693A1 (fr) * 1987-06-03 1988-12-15 Eastman Kodak Company Appareil d'osmose inverse
JPH0356126A (ja) * 1989-07-26 1991-03-11 Hitachi Ltd 脱塩機能を有する中空糸膜フィルタ
EP0434219A1 (fr) * 1989-11-22 1991-06-26 Alberta Research Council Elément formé d'un faisceau de fibres creuses
JPH04145932A (ja) * 1990-10-04 1992-05-19 Toshiba Corp 中空糸膜濾過装置
JPH04180887A (ja) * 1990-11-16 1992-06-29 Mitsubishi Rayon Co Ltd 浄水器

Non-Patent Citations (6)

* Cited by examiner, † Cited by third party
Title
DATABASE WPI Section Ch Week 9116, Derwent World Patents Index; Class D04, AN 91-114337 *
DATABASE WPI Section Ch Week 9226, Derwent World Patents Index; Class D04, AN 92-214444 *
DATABASE WPI Section Ch Week 9232, Derwent World Patents Index; Class D04, AN 92-264384 *
PATENT ABSTRACTS OF JAPAN vol. 15, no. 202 (C - 0834) 23 May 1991 (1991-05-23) *
PATENT ABSTRACTS OF JAPAN vol. 16, no. 425 (C - 0982) 7 September 1992 (1992-09-07) *
PATENT ABSTRACTS OF JAPAN vol. 16, no. 490 (C - 0994) 12 October 1992 (1992-10-12) *

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999022850A1 (fr) * 1997-11-04 1999-05-14 Millipore Corporation Dispositif de purification a membrane
WO1999022851A1 (fr) * 1997-11-04 1999-05-14 Millipore Corporation Dispositif de filtration a membrane
US6709598B1 (en) 1997-11-04 2004-03-23 Millipore Corporation Membrane filtration device
WO1999025726A1 (fr) * 1997-11-14 1999-05-27 New Jersey Institute Of Technology Procede et appareil d'isolation et de purification de biomolecules
US6022477A (en) * 1997-11-14 2000-02-08 New Jersey Institute Of Technology Method and apparatus for isolation purification of biomolecules
US6986847B2 (en) 2002-05-10 2006-01-17 New Jersey Institute Of Technology Method and apparatus for isolation and purification of biomolecules
GB2436076A (en) * 2006-03-17 2007-09-19 Fairey Ceramics A fluid treatment assembly
GB2436076B (en) * 2006-03-17 2011-07-13 Fairey Ceramics Fluid treatment assemblies

Also Published As

Publication number Publication date
AU5284593A (en) 1994-05-24
GB9222248D0 (en) 1992-12-09
GB2286344A (en) 1995-08-16
GB9508171D0 (en) 1995-06-07
GB2286344B (en) 1996-02-07

Similar Documents

Publication Publication Date Title
US6294090B1 (en) Adsorptive substance separation device
US9156001B2 (en) Method and apparatus for further purifying ultrapure water
JP4020917B2 (ja) 真空アシスト方式のアフィニティクロマトグラフィー装置及び方法
EP0815928B1 (fr) Module à membrane jetable ayant un faible volume mort
JP5133987B2 (ja) クロマトグラフィーカラム、システム及び方法
JP2008514424A5 (fr)
JP7458462B2 (ja) 濾過と吸着のステップを含む１つの膜積層体
JPH02150263A (ja) 液状媒質の濾過および安定化法、安定剤の使用、安定化―および濾過法を実施するための装置、ならびにその装置の操作法
JP2014066727A (ja) 膨張床カラムおよび使い捨て可能なクロマトグラフィー
US10935474B1 (en) Membrane filter device
KR20080049791A (ko) 액체 혼합물로부터 목표 분자를 분리하기 위한 단일 경로방법 및 장치
US6911148B1 (en) Adsorptive membrane device for treating particle-laden liquid feeds
WO1994009889A1 (fr) Appareil pour traitment d'un liquide
CN215403546U (zh) 一种新型的超滤水处理系统
JPS58163406A (ja) 液体の「ろ」過方法
CN215799067U (zh) 一种超滤预处理系统
Xu et al. A new integrated membrane filtration and chromatographic device
CN213652028U (zh) 一种新型多阀控制水处理系统
CN211770775U (zh) 一种高浓度污水浓缩处理系统
CN211946638U (zh) 一种制药用净水装置
JPS63126513A (ja) クロスフロ−型精密濾過における逆洗方法
JPH01245893A (ja) 超純水の製造方法
JPH04118032A (ja) ジェット流型濾過器
JP2023104650A (ja) 細胞外小胞の分離精製方法
JPH04190835A (ja) クロスフロー型濾過器

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AT AU BB BG BR BY CA CH CZ DE DK ES FI GB HU JP KP KR KZ LK LU LV MG MN MW NL NO NZ PL PT RO RU SD SE SK UA US UZ VN

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN ML MR NE SN TD TG

DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
121 Ep: the epo has been informed by wipo that ep was designated in this application
REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: CA