US20130299411A1 - Methods and apparatus for removing solids from a membrane module - Google Patents
Methods and apparatus for removing solids from a membrane module Download PDFInfo
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- US20130299411A1 US20130299411A1 US13/943,411 US201313943411A US2013299411A1 US 20130299411 A1 US20130299411 A1 US 20130299411A1 US 201313943411 A US201313943411 A US 201313943411A US 2013299411 A1 US2013299411 A1 US 2013299411A1
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- 239000012528 membrane Substances 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title abstract description 20
- 239000007787 solid Substances 0.000 title description 17
- 238000005374 membrane filtration Methods 0.000 claims abstract description 38
- 238000001914 filtration Methods 0.000 claims abstract description 37
- 239000000356 contaminant Substances 0.000 claims abstract description 5
- 239000012530 fluid Substances 0.000 claims description 14
- 239000012466 permeate Substances 0.000 claims description 13
- 238000004891 communication Methods 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 7
- 239000000706 filtrate Substances 0.000 abstract description 4
- 239000000835 fiber Substances 0.000 description 11
- 238000004140 cleaning Methods 0.000 description 4
- 239000012510 hollow fiber Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 238000012856 packing Methods 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000010408 sweeping Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
Images
Classifications
-
- 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
- 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
-
- 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
- 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
- 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
- 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
- B01D63/043—Hollow fibre modules comprising multiple hollow fibre assemblies with separate tube sheets
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/10—Specific supply elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/12—Specific discharge elements
-
- 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
- B01D2321/02—Forward flushing
-
- 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
Definitions
- the present disclosure relates to membrane filtration systems and, more particularly, to a method and apparatus for improving the filtration efficiency of such systems by providing an improved cleaning system for the membranes.
- a commonly used method to physically clean membranes is a backwash (also called “backflush” or “backpulse”) with the permeate/filtrate or a gas.
- the backwash method is typically used to eject solids blocking the membrane pores and partly dislodge the cake that may have formed on the membrane surface.
- the fouling occurs more quickly and more severely, in particular, where membranes are densely packed in a module.
- Backwash with pressurized gas has proved a very efficient cleaning method and is now widely used in the field of microfiltration processes.
- the limitation to this method is the membrane pore size.
- Backwash of membranes with permeate has no limitations to the pore size, but the backwash efficiency is generally lower than gas backwash and the transmembrane pressure (TMP) recovery is not enough to offset the fouling rate.
- TMP transmembrane pressure
- Further means are employed to enhance the backwash efficiency, such as dosing chemicals to the backwash permeate, or in combination with gas scrubbing.
- Maruyama et al. in Japanese Patent No. JP2031200 discloses a hollow fiber membrane backwashing method. The method involves the following sequence: stop filtration, air-scour membrane, fill the membrane vessel, backwash with permeate under pressurized air, and drain the waste. This procedure is repeated to achieve a higher efficiency.
- Sunaoka et al. in U.S. Pat. No. 5,209,852 describes a process for scrubbing hollow fiber membranes in modules. This process is composed of a two-stage air scrubbing and draining to clean the membranes.
- membrane modules are typically manufactured with a high packing density of membranes, usually in the form of fibers. This increases the amount of membrane area for filtration within a module.
- the higher the packing density the more difficult it is to effectively flush solids captured during the filtration process from the membrane bundle. Therefore, improvement in the efficiency of solids removal during backwash allows either higher solids levels to be processed or higher membrane packing densities to be used, reducing the cost of treatment.
- a membrane filtration module comprising one or more filtration membranes located in a vessel and extending longitudinally between vertically spaced upper headers and lower headers into which the ends of the one or more filtration membranes are potted, at least one of the upper and the lower headers having one or more openings defined therein, and an open-ended plenum chamber positioned at a base of the membrane filtration module below the lower header and having an open lower end spaced from a port in the base of the vessel without any intervening structures therebetween, wherein the one or more openings of the at least one of the upper and the lower headers, the open lower end of the open-ended plenum chamber, and the port in the base of the vessel are vertically aligned to the one or more longitudinally extending filtration membranes.
- the one or more openings are provided in the lower header and the membrane filtration module further comprises a permeate chamber in fluid communication with the upper header.
- the one or more openings in the lower header, the open lower end of the open-ended plenum chamber, and the port in the base of the vessel are configured to define an uninterrupted flow path for dislodged contaminant matter to exit the membrane filtration module in a direction substantially parallel to the one or more filtration membranes.
- the membrane filtration module further comprises a source of pressure configured to apply pressure to a feed liquid within the module.
- the membrane filtration module further comprises a source of backwash fluid in fluid communication with the permeate chamber.
- the membrane filtration module further comprises a gas supply manifold configured to supply a gas to the one or more openings in the lower header.
- the gas supply manifold is positioned adjacent the one or more filtration membranes and is further configured to direct gas downward into the open-ended plenum chamber.
- the gas supply manifold includes a port vertically aligned to the open lower end of the open-ended plenum chamber and the port in the base of the vessel.
- the port is positioned below the one or more openings in the lower header.
- the vessel is open to atmosphere.
- a membrane filtration system comprising a plurality of filtration modules located in a vessel, each of the plurality of filtration modules including one or more membranes having permeable walls and extending longitudinally between vertically spaced upper headers and lower headers into which the ends of the one or more membranes are potted, the lower headers having one or more openings defined therein, a single open-ended plenum chamber in fluid communication with the one or more openings in the lower headers and having an open lower end spaced from a port in the base of the vessel without any intervening structures therebetween, and a gas supply manifold disposed between the plurality of filtration modules and configured to direct gas downward into the single open-ended plenum chamber between the plurality of filtration modules.
- the one or more openings in the lower headers, the open lower end of the single open-ended plenum chamber, and the port in the base of the vessel are vertically aligned to the one or more longitudinally extending filtration membranes.
- the one or more openings in the lower headers, the open lower end of the single open-ended plenum chamber, and the port in the base of the vessel are configured to define an uninterrupted flow path for dislodged contaminant matter to exit the membrane filtration system in a direction substantially parallel to the one or more membranes.
- the membrane filtration system further comprises a source of pressure configured to apply pressure to a feed liquid in the plurality of filtration modules.
- the membrane filtration system further comprises at least one permeate chamber in fluid communication with the upper headers. In some embodiments, the membrane filtration system further comprises a source of backwash fluid in fluid communication with the at least one permeate chamber.
- the gas supply manifold includes a port vertically aligned to the open lower end of the single open-ended plenum chamber and the port in the base of the vessel. In some aspects, the port is positioned below the one or more openings in the lower headers.
- FIG. 1 shows a schematic sectional view of a membrane module according to one embodiment
- FIG. 2 shows a schematic sectional view of a membrane module according to further embodiment
- FIGS. 3 a and 3 b show an enlarged schematic sectional view of the lower header of a non-pressurized filtration system during the aeration and drain-down phases, respectively.
- the filtration module 5 is mounted within a housing vessel 6 which contains the feed to be filtered.
- the filtration module 5 contains a bundle or bundles of hollow fiber membranes 7 extending between upper and lower headers 8 and 9 , respectively.
- the lower header 9 is provided with a number of openings 10 communicating with the interior of the fiber bundle and an open-ended plenum chamber 11 having an opening 11 ′.
- An inlet/outlet port 12 is provided at the base of the module 5 . Feed is supplied through ports 12 , 13 and 14 under the control of valves AV 5 , AV 1 and AV 2 .
- Permeate/filtrate is withdrawn through chamber 15 and port 16 under control of valve AV 3 .
- a backwash may also be applied through port 16 under the control of valve AV 4 .
- FIG. 2 shows a similar arrangement to FIG. 1 ; however, in this embodiment the hollow fiber membranes 7 are suspended vertically from the upper header 8 and are not potted at their lower distal ends 19 . The distal ends 19 of each fiber membrane 7 are closed and filtrate withdrawn through the upper header 8 .
- FIGS. 3 a and 3 b show an enlarged view of the lower headers 9 of a pair of modules 5 connected to a single plenum chamber 11 in a non-pressurized filtration system.
- the modules 5 in this embodiment are mounted in an open vessel (not shown) and the waste liquid containing solids accumulated within the modules 5 following filtration and backwash is drained through the openings 10 under force of gravity, as shown in FIG. 3 b.
- port 17 connected to a gas supply manifold 18 may also be used to supply gas to openings 10 to provide scouring bubbles within the module 5 to assist cleaning of the fiber membrane surfaces.
- Systems embodying the disclosure may provide a number of benefits including:
- feed liquid can be drawn into the centre of the bundle through the same holes during filtration). This also induces a form of crossflow during filtration.
- Rack inserts containing sets of membrane modules can be lowered down closer to the bottom of the module as an open area is no longer required beneath the modules to accommodate manifolds and piping used for solids removal and feed inlet, this now takes place through the openings in the pot. The result is better void space reduction efficiency as well as less space for drainage.
- the plenum chambers can be connected to a pipe or manifold and the backwash waste pumped out of the module rather than gravity flowed, and/or the feedwater pumped in during filtration.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
- This application claims priority under 35 U.S.C. §120 as a division of U.S. application Ser. No. 11/575,234 filed on Mar. 14, 2007, titled METHODS AND APPARATUS FOR REMOVING SOLIDS FROM A MEMBRANE MODULE, which is a U.S. national stage application that claims priority under 35 U.S.C. §371 to International Application No. PCT/AU05/01396 filed on Sep. 13, 2005, titled METHODS AND APPARATUS FOR REMOVING SOLIDS FROM A MEMBRANE MODULE, that claims priority to Australian Provisional Application Ser. No. 2004905292, titled METHODS AND APPARATUS FOR REMOVING SOLIDS FROM A MEMBRANE MODULE, filed Sep. 14, 2004, each of which is herein incorporated by reference in their entirety for all purposes.
- The present disclosure relates to membrane filtration systems and, more particularly, to a method and apparatus for improving the filtration efficiency of such systems by providing an improved cleaning system for the membranes.
- In a membrane filtration process, the method used to physically clean membranes is of vital importance. An efficient membrane cleaning strategy can maintain a stable permeability of the membrane and reduce the frequency of chemical cleans. A commonly used method to physically clean membranes is a backwash (also called “backflush” or “backpulse”) with the permeate/filtrate or a gas. The backwash method is typically used to eject solids blocking the membrane pores and partly dislodge the cake that may have formed on the membrane surface. In a system exposed to a feed containing a high concentration of solids, the fouling occurs more quickly and more severely, in particular, where membranes are densely packed in a module.
- Backwash with pressurized gas has proved a very efficient cleaning method and is now widely used in the field of microfiltration processes. The limitation to this method is the membrane pore size. Backwash of membranes with permeate has no limitations to the pore size, but the backwash efficiency is generally lower than gas backwash and the transmembrane pressure (TMP) recovery is not enough to offset the fouling rate. Further means are employed to enhance the backwash efficiency, such as dosing chemicals to the backwash permeate, or in combination with gas scrubbing.
- Maruyama et al. in Japanese Patent No. JP2031200 discloses a hollow fiber membrane backwashing method. The method involves the following sequence: stop filtration, air-scour membrane, fill the membrane vessel, backwash with permeate under pressurized air, and drain the waste. This procedure is repeated to achieve a higher efficiency. Sunaoka et al. in U.S. Pat. No. 5,209,852 describes a process for scrubbing hollow fiber membranes in modules. This process is composed of a two-stage air scrubbing and draining to clean the membranes.
- In order to minimize footprint and cost, membrane modules are typically manufactured with a high packing density of membranes, usually in the form of fibers. This increases the amount of membrane area for filtration within a module. However, the higher the packing density, the more difficult it is to effectively flush solids captured during the filtration process from the membrane bundle. Therefore, improvement in the efficiency of solids removal during backwash allows either higher solids levels to be processed or higher membrane packing densities to be used, reducing the cost of treatment.
- In prior art fiber membrane systems, removal of solids is usually effected by sweeping with feedwater from one end of the module to the other and then out of the module through a side exit port. In this case, solids are first swept along the fibers to the exit end of the module, but must then cross the fiber bundle to exit the module. In many applications this requirement for the flow to change direction and pass perpendicular to the fiber bundle to exit the module can lead to accumulation of solids near the exit due to the tendency for the fibers to act like a string filter and capture or hinder the exit of solids from the module at this point.
- In accordance with one or more embodiments, a membrane filtration module is provided, comprising one or more filtration membranes located in a vessel and extending longitudinally between vertically spaced upper headers and lower headers into which the ends of the one or more filtration membranes are potted, at least one of the upper and the lower headers having one or more openings defined therein, and an open-ended plenum chamber positioned at a base of the membrane filtration module below the lower header and having an open lower end spaced from a port in the base of the vessel without any intervening structures therebetween, wherein the one or more openings of the at least one of the upper and the lower headers, the open lower end of the open-ended plenum chamber, and the port in the base of the vessel are vertically aligned to the one or more longitudinally extending filtration membranes.
- According to another embodiment, the one or more openings are provided in the lower header and the membrane filtration module further comprises a permeate chamber in fluid communication with the upper header. In various embodiments, the one or more openings in the lower header, the open lower end of the open-ended plenum chamber, and the port in the base of the vessel are configured to define an uninterrupted flow path for dislodged contaminant matter to exit the membrane filtration module in a direction substantially parallel to the one or more filtration membranes. In certain embodiments, the membrane filtration module further comprises a source of pressure configured to apply pressure to a feed liquid within the module. In some embodiments, the membrane filtration module further comprises a source of backwash fluid in fluid communication with the permeate chamber. In various embodiments, the membrane filtration module further comprises a gas supply manifold configured to supply a gas to the one or more openings in the lower header. In at least one aspect, the gas supply manifold is positioned adjacent the one or more filtration membranes and is further configured to direct gas downward into the open-ended plenum chamber. In one or more aspects, the gas supply manifold includes a port vertically aligned to the open lower end of the open-ended plenum chamber and the port in the base of the vessel. In certain embodiments, the port is positioned below the one or more openings in the lower header. According to some embodiments, the vessel is open to atmosphere.
- According to one or more embodiments, a membrane filtration system is provided, comprising a plurality of filtration modules located in a vessel, each of the plurality of filtration modules including one or more membranes having permeable walls and extending longitudinally between vertically spaced upper headers and lower headers into which the ends of the one or more membranes are potted, the lower headers having one or more openings defined therein, a single open-ended plenum chamber in fluid communication with the one or more openings in the lower headers and having an open lower end spaced from a port in the base of the vessel without any intervening structures therebetween, and a gas supply manifold disposed between the plurality of filtration modules and configured to direct gas downward into the single open-ended plenum chamber between the plurality of filtration modules.
- In various embodiments, the one or more openings in the lower headers, the open lower end of the single open-ended plenum chamber, and the port in the base of the vessel are vertically aligned to the one or more longitudinally extending filtration membranes. In another aspect, the one or more openings in the lower headers, the open lower end of the single open-ended plenum chamber, and the port in the base of the vessel are configured to define an uninterrupted flow path for dislodged contaminant matter to exit the membrane filtration system in a direction substantially parallel to the one or more membranes. In at least one embodiment, the membrane filtration system further comprises a source of pressure configured to apply pressure to a feed liquid in the plurality of filtration modules. In certain embodiments, the membrane filtration system further comprises at least one permeate chamber in fluid communication with the upper headers. In some embodiments, the membrane filtration system further comprises a source of backwash fluid in fluid communication with the at least one permeate chamber. In various aspects, the gas supply manifold includes a port vertically aligned to the open lower end of the single open-ended plenum chamber and the port in the base of the vessel. In some aspects, the port is positioned below the one or more openings in the lower headers.
- Embodiments of the disclosure will now be described, by way of example only, with reference to the accompanying drawings in which:
-
FIG. 1 shows a schematic sectional view of a membrane module according to one embodiment; -
FIG. 2 shows a schematic sectional view of a membrane module according to further embodiment; and -
FIGS. 3 a and 3 b show an enlarged schematic sectional view of the lower header of a non-pressurized filtration system during the aeration and drain-down phases, respectively. - Referring to the
FIG. 1 , thefiltration module 5 is mounted within ahousing vessel 6 which contains the feed to be filtered. Thefiltration module 5 contains a bundle or bundles ofhollow fiber membranes 7 extending between upper andlower headers lower header 9 is provided with a number ofopenings 10 communicating with the interior of the fiber bundle and an open-ended plenum chamber 11 having an opening 11′. An inlet/outlet port 12 is provided at the base of themodule 5. Feed is supplied throughports - Permeate/filtrate is withdrawn through
chamber 15 andport 16 under control of valve AV3. A backwash may also be applied throughport 16 under the control of valve AV4. -
FIG. 2 shows a similar arrangement toFIG. 1 ; however, in this embodiment thehollow fiber membranes 7 are suspended vertically from theupper header 8 and are not potted at their lowerdistal ends 19. Thedistal ends 19 of eachfiber membrane 7 are closed and filtrate withdrawn through theupper header 8. - In use, solids accumulated within the
modules 5 following filtration and backwash are flushed or swept from themodules 5 through theopenings 10 by opening port 12 and applying a suitable pressure to the feed within themodule 5. The waste is flushed through theopening 11′ in theplenum chamber 11 and removed through open port 12. -
FIGS. 3 a and 3 b show an enlarged view of thelower headers 9 of a pair ofmodules 5 connected to asingle plenum chamber 11 in a non-pressurized filtration system. Themodules 5 in this embodiment are mounted in an open vessel (not shown) and the waste liquid containing solids accumulated within themodules 5 following filtration and backwash is drained through theopenings 10 under force of gravity, as shown inFIG. 3 b. - As best shown in
FIG. 3 a,port 17 connected to agas supply manifold 18 may also be used to supply gas toopenings 10 to provide scouring bubbles within themodule 5 to assist cleaning of the fiber membrane surfaces. - Systems embodying the disclosure may provide a number of benefits including:
- 1. Enhanced solids removal during backwash due to sweeping action along the fiber surface rather than across multiple fibers.
- 2. Easier contact of feed liquid with the inside of the membrane bundle during filtration (feed liquid can be drawn into the centre of the bundle through the same holes during filtration). This also induces a form of crossflow during filtration.
- 3. Rack inserts containing sets of membrane modules can be lowered down closer to the bottom of the module as an open area is no longer required beneath the modules to accommodate manifolds and piping used for solids removal and feed inlet, this now takes place through the openings in the pot. The result is better void space reduction efficiency as well as less space for drainage.
- 4. The plenum chambers can be connected to a pipe or manifold and the backwash waste pumped out of the module rather than gravity flowed, and/or the feedwater pumped in during filtration.
- It will be appreciated that further embodiments and exemplifications of the disclosure are possible with departing from the spirit or scope of the disclosure described.
Claims (19)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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US13/943,411 US20130299411A1 (en) | 2004-09-14 | 2013-07-16 | Methods and apparatus for removing solids from a membrane module |
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2004905292A AU2004905292A0 (en) | 2004-09-14 | Methods and apparatus for removing solids from a membrane module | |
AU2004905292 | 2004-09-14 | ||
PCT/AU2005/001396 WO2006029456A1 (en) | 2004-09-14 | 2005-09-13 | Methods and apparatus for removing solids from a membrane module |
US57523407A | 2007-03-14 | 2007-03-14 | |
US13/943,411 US20130299411A1 (en) | 2004-09-14 | 2013-07-16 | Methods and apparatus for removing solids from a membrane module |
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PCT/AU2005/001396 Division WO2006029456A1 (en) | 2004-09-14 | 2005-09-13 | Methods and apparatus for removing solids from a membrane module |
US57523407A Division | 2004-09-14 | 2007-03-14 |
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US20130299411A1 true US20130299411A1 (en) | 2013-11-14 |
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US13/943,411 Abandoned US20130299411A1 (en) | 2004-09-14 | 2013-07-16 | Methods and apparatus for removing solids from a membrane module |
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US (2) | US8506806B2 (en) |
EP (1) | EP1799334B1 (en) |
JP (1) | JP4896025B2 (en) |
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US20180221826A1 (en) * | 2014-10-22 | 2018-08-09 | Koch Membrane Systems, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
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KR20000069628A (en) | 1996-12-20 | 2000-11-25 | 브라이언 디어 | Scouring method |
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 |
KR101002466B1 (en) | 2002-10-10 | 2010-12-17 | 지멘스 워터 테크놀로지스 코포레이션 | Backwash method |
WO2005021140A1 (en) | 2003-08-29 | 2005-03-10 | U.S. Filter Wastewater Group, Inc. | Backwash |
WO2005046849A1 (en) | 2003-11-14 | 2005-05-26 | U.S. Filter Wastewater Group, Inc. | Improved module cleaning method |
US8758621B2 (en) | 2004-03-26 | 2014-06-24 | Evoqua Water Technologies Llc | Process and apparatus for purifying impure water using microfiltration or ultrafiltration in combination with reverse osmosis |
CA2579168C (en) | 2004-09-07 | 2015-06-23 | Siemens Water Technologies Corp. | Membrane filtration with reduced volume cleaning step |
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- 2005-09-13 CA CA002579857A patent/CA2579857A1/en not_active Abandoned
- 2005-09-13 CN CN200580034570.1A patent/CN101039739B/en active Active
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2013
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Also Published As
Publication number | Publication date |
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CN101039739B (en) | 2014-10-08 |
WO2006029456A1 (en) | 2006-03-23 |
CA2579857A1 (en) | 2006-03-23 |
JP4896025B2 (en) | 2012-03-14 |
EP1799334B1 (en) | 2013-12-11 |
JP2008513187A (en) | 2008-05-01 |
AU2005284677A1 (en) | 2006-03-23 |
EP1799334A4 (en) | 2009-05-06 |
CN101039739A (en) | 2007-09-19 |
US8506806B2 (en) | 2013-08-13 |
AU2005284677B2 (en) | 2010-12-23 |
US20080053923A1 (en) | 2008-03-06 |
EP1799334A1 (en) | 2007-06-27 |
NZ553742A (en) | 2010-09-30 |
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