CA2683000C - Method of reducing volume of feed liquid required in a porous hollow fibre membrane filtration system - Google Patents
Method of reducing volume of feed liquid required in a porous hollow fibre membrane filtration system Download PDFInfo
- Publication number
- CA2683000C CA2683000C CA2683000A CA2683000A CA2683000C CA 2683000 C CA2683000 C CA 2683000C CA 2683000 A CA2683000 A CA 2683000A CA 2683000 A CA2683000 A CA 2683000A CA 2683000 C CA2683000 C CA 2683000C
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- Canada
- Prior art keywords
- feed liquid
- volume
- filler
- filler members
- filtration system
- 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 - Fee Related
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000005374 membrane filtration Methods 0.000 title claims abstract description 10
- 239000000835 fiber Substances 0.000 title claims description 12
- 239000000945 filler Substances 0.000 claims abstract description 45
- 239000012528 membrane Substances 0.000 claims abstract description 27
- 239000012530 fluid Substances 0.000 claims description 3
- 230000007935 neutral effect Effects 0.000 claims description 3
- 238000001914 filtration Methods 0.000 description 13
- 239000007789 gas Substances 0.000 description 6
- 239000012535 impurity Substances 0.000 description 4
- 238000009991 scouring Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000011148 porous material Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 238000011001 backwashing Methods 0.000 description 2
- 230000000295 complement effect Effects 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000004698 Polyethylene Substances 0.000 description 1
- 238000003491 array Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002991 molded plastic Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- -1 polyethylene Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- B01D63/08—Flat membrane modules
- B01D63/082—Flat membrane modules comprising a stack of flat membranes
- B01D63/0821—Membrane plate arrangements for submerged operation
-
- 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
- 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
- B01D61/20—Accessories; Auxiliary operations
-
- 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
- B01D63/04—Hollow fibre modules comprising multiple hollow fibre assemblies
- B01D63/046—Hollow fibre modules comprising multiple hollow fibre assemblies in separate housings
-
- 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
- B01D63/069—Tubular membrane modules comprising a bundle of tubular membranes
-
- 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
-
- 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
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
-
- 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
- B01D2321/04—Backflushing
-
- 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
- B01D2321/18—Use of gases
- B01D2321/185—Aeration
Abstract
A method for reducing volume of feed liquid required in a porous membrane filtration system having a number of porous membranes submersed in a volume of feed liquid to be filtered is provided. The method comprises the step of providing filler elements within said volume of feed liquid to be filtered.
The filler members substantially fills voids between porous membranes and occupy a space that would otherwise be occupied by the volume of feed liquid to be filtered.
The filler members can be provided in the form of a number of elements which fit together to form an integral unit.
The filler members substantially fills voids between porous membranes and occupy a space that would otherwise be occupied by the volume of feed liquid to be filtered.
The filler members can be provided in the form of a number of elements which fit together to form an integral unit.
Description
METHOD OF REDUCING VOLUME OF FEED LIQUID REQUIRED IN A POROUS
HOLLOW FIBRE MEMBRANE FILTRATION SYSTEM
FIELD OF THE INVENTION
The present invention relates to membrane filtration systems, and more particularly to those systems employing porous or permeable membranes located in a tank or cell open to atmosphere.
BACKGROUND ART
Any discussion of the prior art throughout the specification should in no way be considered as an admission that such prior art is widely known or forms part of common general knowledge in the field.
Porous membrane filtration systems require regular backwashing of the membranes to maintain filtration efficiency and flux while reducing transmernbrane pressure (TMP) which rises as the membrane pores become clogged with impurities. Typically, during the backwash cycle the impurities are forced out of the membrane pores by pressurised gas, liquid or both into the feed tank or cell. The liquid containing impurities and deposits from the membranes is then drained or flushed from the tank.
The waste liquid displaced from the tank needs to be disposed of or reprocessed, usually in an environmentally safe manner, so any reduction in the volume of such waste liquid is seen as advantageous in terms of environmental impact and cost.
The draining or flushing of the tank, particularly when large arrays of membranes are used also requires time which results in down time of the filtration cycle. In order to reduce this down time large pumping systems are required to quickly drain and refill the tank. Where tanks or cells are arranged in banks and feed is used to refill the tank, a lowering in levels in other cells may be produced during the refill process. This again impinges on operating efficiency of the filtration system.
Further, in filtration systems employing gas bubble scouring of the membranes it has been found advantageous to confine the bubbles as much as possible in the region of the membranes to assist with the scouring process.
Reduction in backwash volume also reduces the volume of chemical io cleaning agents required in some systems. This has the two-fold advantage of reducing cost in terms of chemical requirements while also reducing waste disposal problems.
It has been found advantageous to reduce the volume of feed liquid in the filtration cell to ameliorate the above problems and provide at least some of the advantages outlined above.
SUMMARY
Some embodiments of the present invention seek to overcome one or more of the abovementioned problems of the prior art, provide one or more of the advantages outlined above or at least provide a useful alternative by reducing the feed volume presented to the porous membranes in a simple, cost effective manner.
HOLLOW FIBRE MEMBRANE FILTRATION SYSTEM
FIELD OF THE INVENTION
The present invention relates to membrane filtration systems, and more particularly to those systems employing porous or permeable membranes located in a tank or cell open to atmosphere.
BACKGROUND ART
Any discussion of the prior art throughout the specification should in no way be considered as an admission that such prior art is widely known or forms part of common general knowledge in the field.
Porous membrane filtration systems require regular backwashing of the membranes to maintain filtration efficiency and flux while reducing transmernbrane pressure (TMP) which rises as the membrane pores become clogged with impurities. Typically, during the backwash cycle the impurities are forced out of the membrane pores by pressurised gas, liquid or both into the feed tank or cell. The liquid containing impurities and deposits from the membranes is then drained or flushed from the tank.
The waste liquid displaced from the tank needs to be disposed of or reprocessed, usually in an environmentally safe manner, so any reduction in the volume of such waste liquid is seen as advantageous in terms of environmental impact and cost.
The draining or flushing of the tank, particularly when large arrays of membranes are used also requires time which results in down time of the filtration cycle. In order to reduce this down time large pumping systems are required to quickly drain and refill the tank. Where tanks or cells are arranged in banks and feed is used to refill the tank, a lowering in levels in other cells may be produced during the refill process. This again impinges on operating efficiency of the filtration system.
Further, in filtration systems employing gas bubble scouring of the membranes it has been found advantageous to confine the bubbles as much as possible in the region of the membranes to assist with the scouring process.
Reduction in backwash volume also reduces the volume of chemical io cleaning agents required in some systems. This has the two-fold advantage of reducing cost in terms of chemical requirements while also reducing waste disposal problems.
It has been found advantageous to reduce the volume of feed liquid in the filtration cell to ameliorate the above problems and provide at least some of the advantages outlined above.
SUMMARY
Some embodiments of the present invention seek to overcome one or more of the abovementioned problems of the prior art, provide one or more of the advantages outlined above or at least provide a useful alternative by reducing the feed volume presented to the porous membranes in a simple, cost effective manner.
According to one aspect, the present invention provides a method of reducing volume of feed liquid required In a membrane filtration system having a number of porous membranes submersed in a volume of feed liquid to be filtered, the method comprising the step of providing filler elements within said volume of feed liquid to be filtered.
Preferably, the filler elements substantially fill voids between the porous membranes while still permitting liquid flow communication with the membranes.
According to another aspect, the present invention provides a membrane filtration system having a number of porous membranes submersed in a volume of feed liquid to be filtered, wherein one or more filler members are provided in voids between said membranes to reduce said volume.
In one preferred form the membranes are porous hollow fibre membranes arranged in bundles to form membrane modules. The modules are submersed in a liquid volume provided in a tank or cell open to atmospheric pressure. In this form of the invention, the voids between the modules are at least partially filled by a filler member or members.
Preferably, the filler members are each formed of a number of elements which fit together to form an integral unit. This enables the filler members to be assembled around the membranes modules without the need for removal of the modules. This assists in initial set-up as well as with replacement and maintenance regimes.
The filler elements may comprise spheres, preferably hollow, which can be packed around the membranes to fill the voids. The spheres are preferably . .
Preferably, the filler elements substantially fill voids between the porous membranes while still permitting liquid flow communication with the membranes.
According to another aspect, the present invention provides a membrane filtration system having a number of porous membranes submersed in a volume of feed liquid to be filtered, wherein one or more filler members are provided in voids between said membranes to reduce said volume.
In one preferred form the membranes are porous hollow fibre membranes arranged in bundles to form membrane modules. The modules are submersed in a liquid volume provided in a tank or cell open to atmospheric pressure. In this form of the invention, the voids between the modules are at least partially filled by a filler member or members.
Preferably, the filler members are each formed of a number of elements which fit together to form an integral unit. This enables the filler members to be assembled around the membranes modules without the need for removal of the modules. This assists in initial set-up as well as with replacement and maintenance regimes.
The filler elements may comprise spheres, preferably hollow, which can be packed around the membranes to fill the voids. The spheres are preferably . .
sized to avoid blocking or passing through any of the inlet/outlet ports or valves associated with the filtration system.
According to another aspect of the invention, there is provided a method of reducing a volume of feed liquid required in a porous membrane filtration system having a number of porous hollow fibre membranes arranged in bundles to form membrane submodules submersible in a volume of feed liquid to be filtered, the method comprising the step of providing filler members in voids between the submodules to reduce the volume and the filler members are each formed of a number of elements which fit together to form an integral unit wherein the filler members are neutrally buoyant with respect to said feed liquid.
BRIEF DESCRIPTION OF THE DRAWINGS
Preferred embodiments of the invention will now be described, by way of example only, with reference to the accompanying drawings, in which:
Figure 1 shows a perspective view of a bank of filtration modules having filler members according to one embodiment of the invention;
Figure 2 shows an enlarged perspective view of the upper portion of the bank of filtration modules of Figure 1;
Figure 3 shows an exploded view of the filler members of Figure 1 as they would be assembled around a filtration module;
Figure 4 shows an end elevation view of a central filler member of Figure 3;
Figure 5 shows a side elevation view of the filler member of Figure 4;
Figure 6 shows a perspective view of the filler member of Figure 4;
Figure 7 shows a plan view of the filler member of Figure 4;
- 4a -Figure 8 shows an end elevation view of side filler member of Figure 3;
Figure 9 shows a side elevation view of the filler member of Figure 8;
Figure 10 shows a perspective view of the filler member of Figure 8;
Figure 11 shows a plan view of the filler member of Figure 8; and Figure 12 shows a graph of transmembrane pressure over a period of time for two types of filtration system with a filler system being employed on one system part way through the test period.
DESCRIPTION OF PREFERRED EMBODIMENTS
. - 5 -Referring to Figures 1 to 11 of the drawings, the embodiments will be described in relation to a manifold and filtration system disclosed in our co-pending PCT Application No. WO 00/62908, however, it will be appreciated that the invention is equally applicable to other forms of filtration system requiring similar advantages.
The system includes a bank 5 of filter submodules 6 each attached in groups to a membrane filtration manifold 7. In this embodiment, the submodules 6 comprise elongate bundles of porous hollow fibre membranes (not shown) typically enclosed by a supporting cage (not shown). The submodules 6 are positioned within a feed tank or cell (not shown) and when the tank is filled the sub-modules are immersed in feed liquid. Each manifold 7 is connected to a filtrate conduit 8 for removal of filtrate.
During the backwash process, the fibre bundles of submodules 6 are cleaned externally by air bubbles or a mixture of air/liquid injected into each submodule to is scrub the outer surfaces of the fibre membranes. The submodules 6 may also be further cleaned by backwashing liquid and/or gas through the fibre pores.
In accordance with this embodiment, in order to reduce backwash volume, each submodule 6 is encased partially by a number of filler members 9 which are segmented to allow each to fit closely around the elongate fibre bundles. In this embodiment, the filler members 9 are spaced from the upper and lower manifolds to allow for flow of liquid and/or impurities in and out of the submodules 6.
It will be appreciated that other arrangements to allow liquid flow can also be employed, for example, the filler members 9 could be spaced radially from the outer periphery of each fibre bundle submodule 6 or various shapes of filler member 9 could be used which allowed for liquid flow to and from the submodule 6 while still substantially filling the voids between each submodule 6.
In this system, which employs a gas bubble scouring method, the use of the filler members 9 provides an additional advantage of confining the gas bubbles within the submodules 6 and thus improving scouring efficiency.
As best shown in Figures 3 to 11, the filler members 9 are formed from complementary segments comprising a central or core element 10 having two sets of parallel opposed semi-circular, in cross-section, channels 11 extending longitudinally along the length of the central element 10. The channels 11 have a diameter sized to accommodate and fit closely around the submodule 6. The sides 12 and inner edge 13 of the element 10 are provided with outwardly extending tabs or bosses 14 which mate with complementary slots 15 on other filler segments 16 to provide, in use, an integral filler member 9.
The side filler segments 16 are generally T-shaped in cross-section with half-semi circular sides 17 of the same diameter as the central element 10.
The top and bottom surface 18 of the central element 10 are provided with a spacer peg 19 which positions the filler element 9 in a spatial relationship from the manifold 7 to allow fluid flow to and from the top and bottom of the fibre bundles.
The filler members 9 are desirably formed from material which is resistant to any destructive substances present in the feed stream as well as chemicals, gases, etc. which may be used in the backwash or other cleaning processes.
The filler members 9 are also desirably of neutral buoyancy so they will remain in position during submersion of the submodules in the feed tank. They can be formed from foamed plastics material such as polyethylene foam or blow or rotor moulded plastic. When blow-moulded, the filler elements may be hollow to allow for filling with a fluid (usually water) to produce the required neutral buoyancy.
Figure 12 shows the effect on the transmembrane pressure characteristics of two filtration machines. The upper graph shows a machine without the filler members whereas the lower graph shows a machine with filler members employed part way through the test cycle. This graph demonstrates the improved effectiveness of the backwash when filler members are employed.
It will be appreciated that further embodiments and exemplifications of the invention are possible without departing from the spirit or scope of the invention described.
According to another aspect of the invention, there is provided a method of reducing a volume of feed liquid required in a porous membrane filtration system having a number of porous hollow fibre membranes arranged in bundles to form membrane submodules submersible in a volume of feed liquid to be filtered, the method comprising the step of providing filler members in voids between the submodules to reduce the volume and the filler members are each formed of a number of elements which fit together to form an integral unit wherein the filler members are neutrally buoyant with respect to said feed liquid.
BRIEF DESCRIPTION OF THE DRAWINGS
Preferred embodiments of the invention will now be described, by way of example only, with reference to the accompanying drawings, in which:
Figure 1 shows a perspective view of a bank of filtration modules having filler members according to one embodiment of the invention;
Figure 2 shows an enlarged perspective view of the upper portion of the bank of filtration modules of Figure 1;
Figure 3 shows an exploded view of the filler members of Figure 1 as they would be assembled around a filtration module;
Figure 4 shows an end elevation view of a central filler member of Figure 3;
Figure 5 shows a side elevation view of the filler member of Figure 4;
Figure 6 shows a perspective view of the filler member of Figure 4;
Figure 7 shows a plan view of the filler member of Figure 4;
- 4a -Figure 8 shows an end elevation view of side filler member of Figure 3;
Figure 9 shows a side elevation view of the filler member of Figure 8;
Figure 10 shows a perspective view of the filler member of Figure 8;
Figure 11 shows a plan view of the filler member of Figure 8; and Figure 12 shows a graph of transmembrane pressure over a period of time for two types of filtration system with a filler system being employed on one system part way through the test period.
DESCRIPTION OF PREFERRED EMBODIMENTS
. - 5 -Referring to Figures 1 to 11 of the drawings, the embodiments will be described in relation to a manifold and filtration system disclosed in our co-pending PCT Application No. WO 00/62908, however, it will be appreciated that the invention is equally applicable to other forms of filtration system requiring similar advantages.
The system includes a bank 5 of filter submodules 6 each attached in groups to a membrane filtration manifold 7. In this embodiment, the submodules 6 comprise elongate bundles of porous hollow fibre membranes (not shown) typically enclosed by a supporting cage (not shown). The submodules 6 are positioned within a feed tank or cell (not shown) and when the tank is filled the sub-modules are immersed in feed liquid. Each manifold 7 is connected to a filtrate conduit 8 for removal of filtrate.
During the backwash process, the fibre bundles of submodules 6 are cleaned externally by air bubbles or a mixture of air/liquid injected into each submodule to is scrub the outer surfaces of the fibre membranes. The submodules 6 may also be further cleaned by backwashing liquid and/or gas through the fibre pores.
In accordance with this embodiment, in order to reduce backwash volume, each submodule 6 is encased partially by a number of filler members 9 which are segmented to allow each to fit closely around the elongate fibre bundles. In this embodiment, the filler members 9 are spaced from the upper and lower manifolds to allow for flow of liquid and/or impurities in and out of the submodules 6.
It will be appreciated that other arrangements to allow liquid flow can also be employed, for example, the filler members 9 could be spaced radially from the outer periphery of each fibre bundle submodule 6 or various shapes of filler member 9 could be used which allowed for liquid flow to and from the submodule 6 while still substantially filling the voids between each submodule 6.
In this system, which employs a gas bubble scouring method, the use of the filler members 9 provides an additional advantage of confining the gas bubbles within the submodules 6 and thus improving scouring efficiency.
As best shown in Figures 3 to 11, the filler members 9 are formed from complementary segments comprising a central or core element 10 having two sets of parallel opposed semi-circular, in cross-section, channels 11 extending longitudinally along the length of the central element 10. The channels 11 have a diameter sized to accommodate and fit closely around the submodule 6. The sides 12 and inner edge 13 of the element 10 are provided with outwardly extending tabs or bosses 14 which mate with complementary slots 15 on other filler segments 16 to provide, in use, an integral filler member 9.
The side filler segments 16 are generally T-shaped in cross-section with half-semi circular sides 17 of the same diameter as the central element 10.
The top and bottom surface 18 of the central element 10 are provided with a spacer peg 19 which positions the filler element 9 in a spatial relationship from the manifold 7 to allow fluid flow to and from the top and bottom of the fibre bundles.
The filler members 9 are desirably formed from material which is resistant to any destructive substances present in the feed stream as well as chemicals, gases, etc. which may be used in the backwash or other cleaning processes.
The filler members 9 are also desirably of neutral buoyancy so they will remain in position during submersion of the submodules in the feed tank. They can be formed from foamed plastics material such as polyethylene foam or blow or rotor moulded plastic. When blow-moulded, the filler elements may be hollow to allow for filling with a fluid (usually water) to produce the required neutral buoyancy.
Figure 12 shows the effect on the transmembrane pressure characteristics of two filtration machines. The upper graph shows a machine without the filler members whereas the lower graph shows a machine with filler members employed part way through the test cycle. This graph demonstrates the improved effectiveness of the backwash when filler members are employed.
It will be appreciated that further embodiments and exemplifications of the invention are possible without departing from the spirit or scope of the invention described.
Claims (4)
1. A method of reducing a volume of feed liquid required in a porous membrane filtration system having a number of porous hollow fibre membranes arranged in bundles to form membrane submodules submersible in a volume of feed liquid to be filtered, the method comprising the step of providing filler members in voids between the submodules to reduce the volume and the filler members are each formed of a number of elements which fit together to form an integral unit wherein the filler members are neutrally buoyant with respect to said feed liquid.
2. A method according to claim 1 wherein the volume of feed liquid to be filtered is provided in a tank or cell open to atmospheric pressure.
3. A method according to any one of claims 1 to 2 wherein said filler members are provided in the form of members which are spherical in shape.
4. A method according to claim 1 wherein said filler members are hollow and adapted to be filled with a fluid to provide said neutral buoyancy.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AUPR0648 | 2000-10-09 | ||
| AUPR0648A AUPR064800A0 (en) | 2000-10-09 | 2000-10-09 | Improved membrane filtration system |
| CA002424590A CA2424590C (en) | 2000-10-09 | 2001-10-03 | Improved membrane filtration system |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002424590A Division CA2424590C (en) | 2000-10-09 | 2001-10-03 | Improved membrane filtration system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2683000A1 CA2683000A1 (en) | 2002-04-18 |
| CA2683000C true CA2683000C (en) | 2013-11-26 |
Family
ID=3824706
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2683000A Expired - Fee Related CA2683000C (en) | 2000-10-09 | 2001-10-03 | Method of reducing volume of feed liquid required in a porous hollow fibre membrane filtration system |
| CA002424590A Expired - Fee Related CA2424590C (en) | 2000-10-09 | 2001-10-03 | Improved membrane filtration system |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002424590A Expired - Fee Related CA2424590C (en) | 2000-10-09 | 2001-10-03 | Improved membrane filtration system |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US6872305B2 (en) |
| EP (2) | EP1328335B1 (en) |
| JP (2) | JP3917937B2 (en) |
| CN (1) | CN1224450C (en) |
| AT (2) | ATE489159T1 (en) |
| AU (3) | AUPR064800A0 (en) |
| CA (2) | CA2683000C (en) |
| DE (2) | DE60143550D1 (en) |
| MY (1) | MY129690A (en) |
| NZ (1) | NZ525149A (en) |
| WO (1) | WO2002030550A1 (en) |
Families Citing this family (59)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2551202C (en) | 1996-12-20 | 2010-10-26 | Usf Filtration And Separations Group, Inc. | Scouring method |
| AUPQ680100A0 (en) * | 2000-04-10 | 2000-05-11 | Usf Filtration And Separations Group Inc. | Hollow fibre restraining system |
| AUPR421501A0 (en) | 2001-04-04 | 2001-05-03 | U.S. Filter Wastewater Group, Inc. | Potting method |
| AUPR692401A0 (en) | 2001-08-09 | 2001-08-30 | U.S. Filter Wastewater Group, Inc. | Method of cleaning membrane modules |
| AUPS300602A0 (en) | 2002-06-18 | 2002-07-11 | U.S. Filter Wastewater Group, Inc. | Methods of minimising the effect of integrity loss in hollow fibre membrane modules |
| EP1551535B1 (en) | 2002-10-10 | 2012-01-25 | Siemens Industry, Inc. | Membrane filter and backwash method for it |
| AU2002953111A0 (en) | 2002-12-05 | 2002-12-19 | U. S. Filter Wastewater Group, Inc. | Mixing chamber |
| AU2003903507A0 (en) | 2003-07-08 | 2003-07-24 | U. S. Filter Wastewater Group, Inc. | Membrane post-treatment |
| US8268176B2 (en) | 2003-08-29 | 2012-09-18 | Siemens Industry, Inc. | Backwash |
| CN100421772C (en) | 2003-11-14 | 2008-10-01 | 西门子水技术公司 | Improved module cleaning method |
| WO2005092799A1 (en) | 2004-03-26 | 2005-10-06 | U.S. Filter Wastewater Group, Inc. | Process and apparatus for purifying impure water using microfiltration or ultrafiltration in combination with reverse osmosis |
| KR100534526B1 (en) * | 2004-04-07 | 2005-12-07 | 주식회사 코오롱 | Submerged hollow fiber membrane module |
| EP2380854A3 (en) | 2004-04-22 | 2012-07-04 | Siemens Industry, Inc. | Filtration apparatus comprising a membrane bioreactor and a treatment vessel for digesting organic materials |
| WO2006002469A1 (en) * | 2004-07-02 | 2006-01-12 | U.S. Filter Wastewater Group, Inc | Gas transfer membrane |
| US8524794B2 (en) | 2004-07-05 | 2013-09-03 | Siemens Industry, Inc. | Hydrophilic membranes |
| CA2577137C (en) * | 2004-08-20 | 2014-04-22 | Siemens Water Technologies Corp. | Membrane modules with gas and filtrate conduits and racks formed therefrom |
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- 2001-10-03 NZ NZ525149A patent/NZ525149A/en not_active IP Right Cessation
- 2001-10-03 AU AU9151401A patent/AU9151401A/en active Pending
- 2001-10-03 JP JP2002533986A patent/JP3917937B2/en not_active Expired - Fee Related
- 2001-10-03 AT AT01971515T patent/ATE314134T1/en not_active IP Right Cessation
- 2001-10-03 EP EP05021957A patent/EP1618946B1/en not_active Expired - Lifetime
- 2001-10-09 MY MYPI20014696A patent/MY129690A/en unknown
-
2003
- 2003-04-02 US US10/406,807 patent/US6872305B2/en not_active Expired - Lifetime
-
2006
- 2006-10-17 JP JP2006282736A patent/JP4617285B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| US20030234221A1 (en) | 2003-12-25 |
| AU2001291514B2 (en) | 2006-11-09 |
| JP4617285B2 (en) | 2011-01-19 |
| DE60116356T2 (en) | 2006-08-17 |
| EP1618946A1 (en) | 2006-01-25 |
| CN1468140A (en) | 2004-01-14 |
| DE60116356D1 (en) | 2006-02-02 |
| CA2424590A1 (en) | 2002-04-18 |
| JP2007021498A (en) | 2007-02-01 |
| CA2683000A1 (en) | 2002-04-18 |
| EP1328335A4 (en) | 2004-08-25 |
| AUPR064800A0 (en) | 2000-11-02 |
| MY129690A (en) | 2007-04-30 |
| EP1328335A1 (en) | 2003-07-23 |
| WO2002030550A1 (en) | 2002-04-18 |
| JP2004509760A (en) | 2004-04-02 |
| NZ525149A (en) | 2004-09-24 |
| ATE314134T1 (en) | 2006-01-15 |
| US6872305B2 (en) | 2005-03-29 |
| JP3917937B2 (en) | 2007-05-23 |
| CN1224450C (en) | 2005-10-26 |
| EP1618946B1 (en) | 2010-11-24 |
| ATE489159T1 (en) | 2010-12-15 |
| AU9151401A (en) | 2002-04-22 |
| CA2424590C (en) | 2010-01-19 |
| DE60143550D1 (en) | 2011-01-05 |
| EP1328335B1 (en) | 2005-12-28 |
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| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20161003 |