CA2535360A1 - Backwash - Google Patents
Backwash Download PDFInfo
- Publication number
- CA2535360A1 CA2535360A1 CA002535360A CA2535360A CA2535360A1 CA 2535360 A1 CA2535360 A1 CA 2535360A1 CA 002535360 A CA002535360 A CA 002535360A CA 2535360 A CA2535360 A CA 2535360A CA 2535360 A1 CA2535360 A1 CA 2535360A1
- Authority
- CA
- Canada
- Prior art keywords
- liquid
- feed
- level
- membranes
- containing vessel
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000007788 liquid Substances 0.000 claims abstract description 64
- 239000012528 membrane Substances 0.000 claims abstract description 58
- 238000001914 filtration Methods 0.000 claims abstract description 30
- 238000000034 method Methods 0.000 claims abstract description 27
- 239000000706 filtrate Substances 0.000 claims abstract description 12
- 238000011001 backwashing Methods 0.000 claims abstract description 7
- 239000000356 contaminant Substances 0.000 claims abstract description 6
- 238000005374 membrane filtration Methods 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims abstract description 3
- 238000005273 aeration Methods 0.000 claims description 13
- 238000005086 pumping Methods 0.000 claims description 2
- 238000012544 monitoring process Methods 0.000 claims 2
- 239000012535 impurity Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- 239000000835 fiber Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 238000003491 array Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
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
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- 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
- 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
- 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 of backwashing a membrane filtration module (4), said module (4) including one or more membranes (5) located in a feed-containing vessel (3), the membranes (5) having a permeable wall which is subjected to a filtration operation wherein feed containing contaminant matter is applied to one side of the membrane wall and filtrate is withdrawn from the other side of the membrane wall, the method including: removing liquid from the feed-containing vessel (3) until the level of liquid in the feed-containing vessel (3) falls to a first level (L2) below an upper level of the membranes; suspending the filtration operation; performing a liquid backwash of the membrane wall until liquid level within the feed-containing vessel (3) rises to a second predetermined level (L1) above said first level; aerating the membrane surface with gas bubbles to dislodge fouling materials therefrom; performing a sweep or drain down of the feed-containing vessel (3) to remove the liquid containing the dislodged contaminant matter; and recommencing the filtration operation.
Description
TITLE: BACKWASH
TECHNICAL FIELD
The present invention relates to membrane filtration systems and more s particularly, the backwashing of such systems.
BACKGROUND OF THE INVENTION
Porous membrane filtration systems require regular backwashing of the membranes to maintain filtration efficiency and flux while reducing transmembrane pressure (TMP) which rises as the membrane pores become to clogged with impurities. Such systems usually have a number of membranes in the form of bundles or arrays of membranes located in a feed tank. Feed is thus applied to the surfaces of the membranes and filtrate withdrawn from the membrane lumens. Typically, during the backwash cycle the impurities are forced out of the membrane pores by pressurised gas, liquid or both into the is 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 2o 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 2s 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.
Reduction in backwash volume also reduces the volume of chemical cleaning agents required in some systems. This has the two-fold advantage of s reducing cost in terms of chemical requirements while also reducing waste disposal problems.
Many filtration systems also employ a gas bubble aeration method to assist in scouring unwanted deposits from the surfaces of the porous membranes during the cleaning stage. In order for such aeration to be effective the io membranes must be fully immersed in liquid.
Typically the cleaning process in such systems includes ceasing flow of feed liquid to the vessel in which the membranes are located, continuing the filtration process until the level of liquid in the tank reaches the top of the membranes, aerating the membranes with gas bubbles to scour impurities from is the outer membrane surfaces for a period of time, then liquid backwashing the membrane pores. The tank is then drained or flushed to remove the waste liquid containing the impurities dislodged during the aeration and backwashing processes.
It will be appreciated that it is necessary to keep the membranes 2o submerged so as to make the aeration step effective. Adding the liquid backwash at the end of the aeration step results in the liquid level in the tank rising above the membranes. This is "wasted volume" in terms of the requirement of keeping the membranes submerged.
SUMMARY OF THE INVENTION
The present invention seeks to overcome or at least ameliorate this and other disadvantages of the prior art.
According to one aspect, the present invention provides a method of s backwashing a membrane filtration module, said module including one or more membranes located in a feed-containing vessel, the membranes having a permeable wall which is subjected to a filtration operation wherein feed containing contaminant matter is applied to one side of the membrane wall and filtrate is withdrawn from the other side of the membrane wall, the method io including:
a) removing liquid from the feed-containing vessel until the level of liquid in the feed-containing vessel falls to a first level below an upper level of the membranes;
b) suspending the filtration operation;
is c) performing a liquid backwash of the membrane wall until liquid level within the feed-containing vessel rises to a second predetermined level above said first level;
d) aerating the membrane surface with gas bubbles to dislodge fouling materials therefrom;
2o e) performing a sweep or drain down of the feed-containing vessel to remove the liquid containing the dislodged contaminant matter;
and f) recommencing the filtration operation.
Preferably, the second predetermined level is selected such that the liquid 2s level rises at least to the upper level of the membranes during the aeration step.
Preferably, the flow of feed into the feed-containing vessel is suspended prior to removal step a). For preference, the removal of liquid is achieved fully or partially by the filtration process. Preferably, in a pressurized filtration system, a pressurized gas is employed during the filtration process to push the liquid from s the feed side through the permeable membrane wall during the removal step a).
The aeration step may commence prior to removal of liquid step and continue until the sweep or drain down step e).
This process has the advantage of reducing the backwash volume. Also, rather than filtering down to the required liquid level, it is possible to drain or to pump away liquid in the feed-containing tank to achieve the same result.
This has the advantage of not increasing the flux of the membrane during the filter down step, and can be done quickly to reduce filtration down time. The drained feed may be returned to the inlet of the filtration plant so as not to be wasted, or transferred to other tanks operating in parallel.
is In an alternate method, the filtration step may be done at varying filtrate flows; the flow being adjusted to maintain a constant transmembrane pressure (TMP) as the liquid level drops down the membranes.
The TMP may be monitored during the removal of liquid step and used to determine when the liquid level has dropped below the top of the membranes, or 2o how far below the upper level of the membranes the liquid level has dropped.
This is possible because as more of the membrane is exposed the filtration area is less and the TMP will increase. TMP will also increase due to the fact that more of the filtrate flow travels further along the lumen so increasing the lumen pressure drop (assuming the flow is kept constant and filtrate is being withdrawn 2s from the upper end of the membrane lumen). Accordingly, the change in TMP
-s-may be used to monitor the liquid level in the feed tank before commencing the liquid backwash step. This may also be used to adjust the filtrate flow and maintain a constant TMP so avoiding significant changes in the flux on the remaining filtrate area. Alternatively, such a method can be used to control to s the TMP to any desired predetermined level, for example, it may desirable to lower the liquid level in the feed-containing tank, keeping the TMP at the maximum allowable TMP, say 35 kPa.
BRIEF DESCRIPTION OF THE DRAWINGS
A preferred embodiment of the invention will now be described, by way of io example only, with reference to the accompanying drawings in which:
Figures 1 a to 1 a show schematic views of the membrane module at various stages of the backwash process according to an embodiment of the invention.
DESCRIPTION OF THE PREFERRED EMBODIMENT
is Referring to the Figures 1 a to 1 e, an illustrative embodiment of the invention is described. The filtration module 4 is mounted within a housing vessel 3 which contains the feed to be filtered. The filtration module 8 contains a bundle or bundles of hollow fibre membranes 5 extending between upper and 20 lower headers 6 and 7, respectively. The lower header 7 is provided with a number of openings 9 communicating with the interior of the fibre bundle and an inlet port 10. Feed is supplied through port 11 under the control of valve AV1.
Permeate/filtrate is withdrawn through chamber 12 and line 13. A liquid backwash may also be applied through line 13.
2s Figure 1 a shows the module in normal filtration operation with the liquid level in the vessel 3 at L1 covering the upper header 6. When the backwash stage is to be commenced, in this embodiment, the flow of feed is stopped by shutting valve AV1. Filtrate continues to be withdrawn through the fibre lumens and chamber 12 and line 13. The level of liquid in the vessel 3 falls, as shown in Figure 1 b, to level L2.
s Once level L2 is reached, a liquid backwash is commenced by flowing liquid back through the fibre lumens and walls via line 13. This results in the liquid level again rising in the vessel to L1 as shown in Figure 1 c. An aeration step is then commenced by feeding gas through port 10 and openings 9 as shown in Figure 1d. In another embodiment, the liquid level resulting from the to liquid backwash may be just below level L1 such that level L1 is reached during the aeration step with the liquid level rising further as a result of bubbles present in the liquid. A similar result may be achieved by commencing the aeration step during the liquid backwash.
Once the aeration step is completed the vessel is swept or drained as is shown in Figure 1 a to remove dislodged waste materials accumulated in the vessel liquid. Following this step feed is reintroduced to the vessel by opening valve AV1 and filtration recommenced.
Although the embodiment relates to vertically orientated membranes, it will be appreciated that the invention is not limited to such an orientation and the 2o membranes may be orientated in any desired position or configuration.
It will be appreciated that the invention may be applied to both pressurized and non-pressurized systems where the feed-containing vessel is open to atmosphere.
_7_ It will be appreciated that further embodiments and exemplifications of the invention are possible with departing from the spirit or scope of the invention described.
TECHNICAL FIELD
The present invention relates to membrane filtration systems and more s particularly, the backwashing of such systems.
BACKGROUND OF THE INVENTION
Porous membrane filtration systems require regular backwashing of the membranes to maintain filtration efficiency and flux while reducing transmembrane pressure (TMP) which rises as the membrane pores become to clogged with impurities. Such systems usually have a number of membranes in the form of bundles or arrays of membranes located in a feed tank. Feed is thus applied to the surfaces of the membranes and filtrate withdrawn from the membrane lumens. Typically, during the backwash cycle the impurities are forced out of the membrane pores by pressurised gas, liquid or both into the is 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 2o 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 2s 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.
Reduction in backwash volume also reduces the volume of chemical cleaning agents required in some systems. This has the two-fold advantage of s reducing cost in terms of chemical requirements while also reducing waste disposal problems.
Many filtration systems also employ a gas bubble aeration method to assist in scouring unwanted deposits from the surfaces of the porous membranes during the cleaning stage. In order for such aeration to be effective the io membranes must be fully immersed in liquid.
Typically the cleaning process in such systems includes ceasing flow of feed liquid to the vessel in which the membranes are located, continuing the filtration process until the level of liquid in the tank reaches the top of the membranes, aerating the membranes with gas bubbles to scour impurities from is the outer membrane surfaces for a period of time, then liquid backwashing the membrane pores. The tank is then drained or flushed to remove the waste liquid containing the impurities dislodged during the aeration and backwashing processes.
It will be appreciated that it is necessary to keep the membranes 2o submerged so as to make the aeration step effective. Adding the liquid backwash at the end of the aeration step results in the liquid level in the tank rising above the membranes. This is "wasted volume" in terms of the requirement of keeping the membranes submerged.
SUMMARY OF THE INVENTION
The present invention seeks to overcome or at least ameliorate this and other disadvantages of the prior art.
According to one aspect, the present invention provides a method of s backwashing a membrane filtration module, said module including one or more membranes located in a feed-containing vessel, the membranes having a permeable wall which is subjected to a filtration operation wherein feed containing contaminant matter is applied to one side of the membrane wall and filtrate is withdrawn from the other side of the membrane wall, the method io including:
a) removing liquid from the feed-containing vessel until the level of liquid in the feed-containing vessel falls to a first level below an upper level of the membranes;
b) suspending the filtration operation;
is c) performing a liquid backwash of the membrane wall until liquid level within the feed-containing vessel rises to a second predetermined level above said first level;
d) aerating the membrane surface with gas bubbles to dislodge fouling materials therefrom;
2o e) performing a sweep or drain down of the feed-containing vessel to remove the liquid containing the dislodged contaminant matter;
and f) recommencing the filtration operation.
Preferably, the second predetermined level is selected such that the liquid 2s level rises at least to the upper level of the membranes during the aeration step.
Preferably, the flow of feed into the feed-containing vessel is suspended prior to removal step a). For preference, the removal of liquid is achieved fully or partially by the filtration process. Preferably, in a pressurized filtration system, a pressurized gas is employed during the filtration process to push the liquid from s the feed side through the permeable membrane wall during the removal step a).
The aeration step may commence prior to removal of liquid step and continue until the sweep or drain down step e).
This process has the advantage of reducing the backwash volume. Also, rather than filtering down to the required liquid level, it is possible to drain or to pump away liquid in the feed-containing tank to achieve the same result.
This has the advantage of not increasing the flux of the membrane during the filter down step, and can be done quickly to reduce filtration down time. The drained feed may be returned to the inlet of the filtration plant so as not to be wasted, or transferred to other tanks operating in parallel.
is In an alternate method, the filtration step may be done at varying filtrate flows; the flow being adjusted to maintain a constant transmembrane pressure (TMP) as the liquid level drops down the membranes.
The TMP may be monitored during the removal of liquid step and used to determine when the liquid level has dropped below the top of the membranes, or 2o how far below the upper level of the membranes the liquid level has dropped.
This is possible because as more of the membrane is exposed the filtration area is less and the TMP will increase. TMP will also increase due to the fact that more of the filtrate flow travels further along the lumen so increasing the lumen pressure drop (assuming the flow is kept constant and filtrate is being withdrawn 2s from the upper end of the membrane lumen). Accordingly, the change in TMP
-s-may be used to monitor the liquid level in the feed tank before commencing the liquid backwash step. This may also be used to adjust the filtrate flow and maintain a constant TMP so avoiding significant changes in the flux on the remaining filtrate area. Alternatively, such a method can be used to control to s the TMP to any desired predetermined level, for example, it may desirable to lower the liquid level in the feed-containing tank, keeping the TMP at the maximum allowable TMP, say 35 kPa.
BRIEF DESCRIPTION OF THE DRAWINGS
A preferred embodiment of the invention will now be described, by way of io example only, with reference to the accompanying drawings in which:
Figures 1 a to 1 a show schematic views of the membrane module at various stages of the backwash process according to an embodiment of the invention.
DESCRIPTION OF THE PREFERRED EMBODIMENT
is Referring to the Figures 1 a to 1 e, an illustrative embodiment of the invention is described. The filtration module 4 is mounted within a housing vessel 3 which contains the feed to be filtered. The filtration module 8 contains a bundle or bundles of hollow fibre membranes 5 extending between upper and 20 lower headers 6 and 7, respectively. The lower header 7 is provided with a number of openings 9 communicating with the interior of the fibre bundle and an inlet port 10. Feed is supplied through port 11 under the control of valve AV1.
Permeate/filtrate is withdrawn through chamber 12 and line 13. A liquid backwash may also be applied through line 13.
2s Figure 1 a shows the module in normal filtration operation with the liquid level in the vessel 3 at L1 covering the upper header 6. When the backwash stage is to be commenced, in this embodiment, the flow of feed is stopped by shutting valve AV1. Filtrate continues to be withdrawn through the fibre lumens and chamber 12 and line 13. The level of liquid in the vessel 3 falls, as shown in Figure 1 b, to level L2.
s Once level L2 is reached, a liquid backwash is commenced by flowing liquid back through the fibre lumens and walls via line 13. This results in the liquid level again rising in the vessel to L1 as shown in Figure 1 c. An aeration step is then commenced by feeding gas through port 10 and openings 9 as shown in Figure 1d. In another embodiment, the liquid level resulting from the to liquid backwash may be just below level L1 such that level L1 is reached during the aeration step with the liquid level rising further as a result of bubbles present in the liquid. A similar result may be achieved by commencing the aeration step during the liquid backwash.
Once the aeration step is completed the vessel is swept or drained as is shown in Figure 1 a to remove dislodged waste materials accumulated in the vessel liquid. Following this step feed is reintroduced to the vessel by opening valve AV1 and filtration recommenced.
Although the embodiment relates to vertically orientated membranes, it will be appreciated that the invention is not limited to such an orientation and the 2o membranes may be orientated in any desired position or configuration.
It will be appreciated that the invention may be applied to both pressurized and non-pressurized systems where the feed-containing vessel is open to atmosphere.
_7_ It will be appreciated that further embodiments and exemplifications of the invention are possible with departing from the spirit or scope of the invention described.
Claims (14)
1. A method of backwashing a membrane filtration module, said module including one or more membranes located in a feed-containing vessel, the membranes having a permeable wall which is subjected to a filtration operation wherein feed containing contaminant matter is applied to one side of the membrane wall and filtrate is withdrawn from the other side of the membrane wall, the method including:
a) removing liquid from the feed-containing vessel until the level of liquid in the feed-containing vessel falls to a first level below an upper level of the membranes;
b) suspending the filtration operation;
c) performing a liquid backwash of the membrane wall until liquid level within the feed-containing vessel rises to a second predetermined level above said first level;
d) aerating the membrane surface with gas bubbles to dislodge fouling materials therefrom;
e) performing a sweep or drain down of the feed-containing vessel to remove the liquid containing the dislodged contaminant matter;
and f) recommencing the filtration operation.
a) removing liquid from the feed-containing vessel until the level of liquid in the feed-containing vessel falls to a first level below an upper level of the membranes;
b) suspending the filtration operation;
c) performing a liquid backwash of the membrane wall until liquid level within the feed-containing vessel rises to a second predetermined level above said first level;
d) aerating the membrane surface with gas bubbles to dislodge fouling materials therefrom;
e) performing a sweep or drain down of the feed-containing vessel to remove the liquid containing the dislodged contaminant matter;
and f) recommencing the filtration operation.
2. A method according to claim 1 including selecting the second predetermined level such that the liquid level rises at least to the upper level of the membranes during the aeration step.
3. A method according to claim 1 or 2, wherein the flow of feed into the feed-containing vessel is suspended prior to removal step a).
4. A method according to any one of the preceding claims wherein the aeration step is commenced prior to removal of liquid step and continues until the sweep or drain down step e).
5. A method according to any one of the preceding claims wherein the removal of liquid is achieved fully or partially by the filtration process.
6. A method according to claim 5 including applying a pressurized gas to the liquid on the said one side of the membrane wall to push the liquid through the membrane wall during the filtration process.
7. A method according to any one of claims 1 to 4 wherein the removal of liquid is achieved by drain down of liquid in the feed-containing tank.
8. A method according to any one of claims 1 to 4 wherein the removal of liquid is achieved by pumping liquid from the feed-containing tank.
9. A method according to any one of the preceding claims including the step of returning the removed liquid to the feed-containing vessel when filtration is recommenced.
10. A method according to any one of the preceding claims including the step of returning the removed liquid to the feed-containing vessel of a further filtration system.
11. A method according to anyone of the preceding claims including the step of varying filtrate flow from membranes to maintain a substantially constant transmembrane pressure (TMP) across said membranes as the liquid level is reduced within the feed-containing vessel.
12. A method according to claim 11 wherein the transmembrane pressure is maintained at or below a predetermined value.
13. A method according to any one of the preceding claims including the step of monitoring the transmembrane pressure across said membranes to determine the level of liquid in said feed-containing vessel.
14. A method according to claim 13 wherein said monitoring step is performed during the removal step a).
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2003904748 | 2003-08-29 | ||
| AU2003904748A AU2003904748A0 (en) | 2003-08-29 | Backwash | |
| AU2003905139 | 2003-09-19 | ||
| AU2003905139A AU2003905139A0 (en) | 2003-09-19 | Improved method of cleaning membrane modules | |
| PCT/AU2004/001157 WO2005021140A1 (en) | 2003-08-29 | 2004-08-27 | Backwash |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2535360A1 true CA2535360A1 (en) | 2005-03-10 |
| CA2535360C CA2535360C (en) | 2013-02-12 |
Family
ID=34275845
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2535360A Active CA2535360C (en) | 2003-08-29 | 2004-08-27 | Backwash |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US8268176B2 (en) |
| EP (1) | EP1677898B1 (en) |
| JP (1) | JP4611982B2 (en) |
| KR (1) | KR101115173B1 (en) |
| CN (1) | CN103285737B (en) |
| CA (1) | CA2535360C (en) |
| NZ (1) | NZ545206A (en) |
| WO (1) | WO2005021140A1 (en) |
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| CA2639642C (en) * | 1996-12-20 | 2013-01-15 | Siemens Water Technologies Corp. | Scouring method |
| US20040007527A1 (en) * | 1998-11-23 | 2004-01-15 | Zenon Environmental Inc. | Membrane filtration device and process |
| 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 |
| JP4282598B2 (en) | 2002-10-10 | 2009-06-24 | シーメンス・ウォーター・テクノロジーズ・コーポレーション | Filtration device and method for cleaning the filtration device |
| US20040262209A1 (en) * | 2003-04-25 | 2004-12-30 | Hiroyuki Umezawa | Filtration apparatus |
| JP4611982B2 (en) | 2003-08-29 | 2011-01-12 | シーメンス・ウォーター・テクノロジーズ・コーポレーション | Backwash method |
| KR20070003783A (en) | 2003-11-14 | 2007-01-05 | 유.에스. 필터 웨이스트워터 그룹, 인크. | Improved module cleaning method |
| WO2005082498A1 (en) * | 2004-02-27 | 2005-09-09 | Zenon Environmental Inc. | Water filtration using immersed membranes |
| US20050194315A1 (en) * | 2004-02-27 | 2005-09-08 | Adams Nicholas W.H. | Membrane batch filtration process |
| 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 |
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| CN101287538B (en) * | 2005-08-22 | 2013-03-06 | 西门子工业公司 | An assembly for water filtration using a tube manifold to minimise backwash |
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| DE102007041991A1 (en) | 2007-09-05 | 2009-03-12 | Fülling, Rainer, Dr. | Process for the purification of substrates by oxidants and reducing agents and the use of oxidizing agents for the oxidation of extracellular polymeric substances |
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| WO2010009518A1 (en) | 2008-07-24 | 2010-01-28 | Siemens Water Technologies Corp. | Frame system for membrane filtration modules |
| WO2010019751A1 (en) | 2008-08-14 | 2010-02-18 | Siemens Water Technologies Corp. | Block configuration for large scale membrane distillation |
| KR20110044312A (en) | 2008-08-20 | 2011-04-28 | 지멘스 워터 테크놀로지스 코포레이션 | Improved membrane system backwash energy efficiency |
| AU2010257526A1 (en) | 2009-06-11 | 2012-01-12 | Siemens Industry, Inc | Methods for cleaning a porous polymeric membrane and a kit for cleaning a porous polymeric membrane |
| US9358505B2 (en) | 2009-09-03 | 2016-06-07 | General Electric Company | Gas sparger for an immersed membrane |
| US9364805B2 (en) | 2010-10-15 | 2016-06-14 | General Electric Company | Integrated gas sparger for an immersed membrane |
-
2004
- 2004-08-27 JP JP2006524173A patent/JP4611982B2/en not_active Expired - Fee Related
- 2004-08-27 KR KR1020067003923A patent/KR101115173B1/en not_active IP Right Cessation
- 2004-08-27 CA CA2535360A patent/CA2535360C/en active Active
- 2004-08-27 EP EP04761194.2A patent/EP1677898B1/en active Active
- 2004-08-27 US US10/569,565 patent/US8268176B2/en active Active
- 2004-08-27 WO PCT/AU2004/001157 patent/WO2005021140A1/en active Search and Examination
- 2004-08-27 NZ NZ545206A patent/NZ545206A/en active IP Right Revival
- 2004-08-27 CN CN201310180783.1A patent/CN103285737B/en active Active
Also Published As
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|---|---|
| US20070007205A1 (en) | 2007-01-11 |
| CA2535360C (en) | 2013-02-12 |
| KR101115173B1 (en) | 2012-02-24 |
| WO2005021140A1 (en) | 2005-03-10 |
| US8268176B2 (en) | 2012-09-18 |
| EP1677898A1 (en) | 2006-07-12 |
| EP1677898A4 (en) | 2006-11-02 |
| EP1677898B1 (en) | 2016-03-09 |
| KR20060080584A (en) | 2006-07-10 |
| JP2007503972A (en) | 2007-03-01 |
| CN103285737B (en) | 2016-01-13 |
| JP4611982B2 (en) | 2011-01-12 |
| CN103285737A (en) | 2013-09-11 |
| NZ545206A (en) | 2009-03-31 |
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