US20060163139A1 - Immersed membrane filtration system and overflow process - Google Patents
Immersed membrane filtration system and overflow process Download PDFInfo
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- US20060163139A1 US20060163139A1 US11/387,807 US38780706A US2006163139A1 US 20060163139 A1 US20060163139 A1 US 20060163139A1 US 38780706 A US38780706 A US 38780706A US 2006163139 A1 US2006163139 A1 US 2006163139A1
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- membranes
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- 238000000034 method Methods 0.000 title description 5
- 238000005374 membrane filtration Methods 0.000 title 1
- 239000012528 membrane Substances 0.000 claims abstract description 65
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 58
- 239000012465 retentate Substances 0.000 claims abstract description 19
- 238000001914 filtration Methods 0.000 claims abstract description 16
- 239000012466 permeate Substances 0.000 claims description 22
- 239000007787 solid Substances 0.000 claims description 15
- 230000000717 retained effect Effects 0.000 claims 1
- 238000005273 aeration Methods 0.000 abstract description 19
- 238000011001 backwashing Methods 0.000 abstract description 18
- 238000011010 flushing procedure Methods 0.000 abstract description 12
- 238000009991 scouring Methods 0.000 abstract description 4
- 238000001471 micro-filtration Methods 0.000 abstract description 2
- 238000000108 ultra-filtration Methods 0.000 abstract description 2
- 230000004907 flux Effects 0.000 description 8
- 238000005276 aerator Methods 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 239000000835 fiber Substances 0.000 description 4
- 239000003643 water by type Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 235000012206 bottled water Nutrition 0.000 description 2
- 239000003651 drinking water Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000002352 surface water Substances 0.000 description 2
- 101000916532 Rattus norvegicus Zinc finger and BTB domain-containing protein 38 Proteins 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000005465 channeling Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000004382 potting Methods 0.000 description 1
- 238000009420 retrofitting Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
Images
Classifications
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- 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
- 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
- B01D61/145—Ultrafiltration
-
- 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
- B01D61/147—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
-
- 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
- B01D63/026—Wafer type modules or flat-surface type 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
- B01D63/031—Two or more types of hollow fibres within one bundle or within one potting or tube-sheet
-
- 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
-
- 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
-
- 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
- B01D63/16—Rotary, reciprocated or vibrated modules
-
- 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
- B01D65/10—Testing of membranes or membrane apparatus; Detecting or repairing leaks
-
- 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
- B01D65/10—Testing of membranes or membrane apparatus; Detecting or repairing leaks
- B01D65/104—Detection of leaks in membrane apparatus or modules
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/06—External membrane module supporting or fixing means
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/54—Modularity of membrane module 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
- B01D2313/56—Specific mechanisms for loading the membrane in a module
-
- 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
- B01D2321/18—Use of gases
- B01D2321/185—Aeration
Definitions
- This invention relates to a filtration system using immersed suction driven filtering membranes to filter water, for example, to filter surface water to produce potable water, and to a method of operating such a system.
- FIG. 1 A prior art immersed membrane water filtration system is shown in FIG. 1 .
- An open tank (a) holds a membrane module (b) immersed in tank water (c). Feed water to be filtered flows into the tank, typically continuously. Suction on an inner surface of the membranes in the membrane module (b) draws filtered permeate through the membrane wall. Solids are rejected by the membranes and accumulate in the tank water (c). Solids rich retentate is continuously or periodically drained from the tank.
- the membrane module (b) is cleaned in part by backwashing and aeration.
- a backwashing liquid typically permeate or permeate with a chemical additive
- aeration air bubbles are created at an aerator (d) mounted below the membrane module (c).
- the air bubbles agitate and scour the membranes and create an air lift effect.
- the air lift effect moves tank water (c) in a recirculation pattern (e) upwards through the membrane module (b) and in a downcomer (f) through spaces between the perimeter of the module (b) and the sides of the tank (a).
- the tank water (c) flowing in the recirculation pattern (e) further physically cleans the membranes and disperses solids rich water from near the membrane module (b).
- a filtration system having immersed suction driven filtering membranes is used to filter water containing low concentrations of suspended solids, for example, to filter surface water to produce potable water.
- a process is provided for operating such a system.
- Membrane modules are arranged in a tank open to the atmosphere and fill most of its horizontal cross sectional area.
- An upper portion of the tank encloses a volume directly above the modules. This upper portion of the tank is provided with a retentate outlet from the tank. Tank water that is not withdrawn as permeate flows out of the tank through the retentate outlet.
- Permeate is withdrawn by suction on an inner surface of the membranes, preferably at a flux between 10 and 60 L/m 2 /h, more preferably between 20 and 40 L/m 2 /h. Feed water is added to the tank at a rate that substantially equals the rate at which permeate is withdrawn. Thus during permeation little if any tank water flows out of the outlet and the level of the tank water remains above the membranes.
- Permeation is stopped periodically for a deconcentration step.
- the membranes are backwashed, feed flow is provided from below the modules or both.
- Tank water rises through the modules, the water level in the tank rises and tank water containing solids (then called retentate) flows out of the retentate outlet to deconcentrate the tank water.
- Aeration with scouring bubbles is provided during the deconcentration step.
- FIG. 1 is a schematic representation of a prior art filtration system.
- FIG. 2 is a schematic representation of a filtering reactor made in accordance with a preferred embodiment of the present invention.
- FIG. 3 is a plan view of a filtering reactor made in accordance with a preferred embodiment of the present invention.
- FIG. 4 shows a plan view of a module of FIG. 1 .
- the membrane modules 10 are stacked on top of each other in a tank 12 .
- the tank 12 is open to the atmosphere although it may be covered with a vented lid 13 .
- the membrane modules 10 may contain flat sheet or hollow fibre membranes with pore sizes in the microfiltration or ultrafiltration range, preferably between 0.003 and 10 microns and more preferably between 0.01 and 1.0 microns.
- An inner surface of the membranes is connected to one or more headers.
- An aerator 14 is mounted below the membrane modules 10 .
- the aerator 14 is connected to an air supply pipe 14 in turn connected to a supply of air, nitrogen or other suitable gas.
- the membrane modules 10 contain hollow fibre membranes oriented horizontally and mounted in a slightly slackened state between pairs of horizontally spaced, vertically extending headers.
- U.S. patent application Ser. No. 09/505,718 filed Feb. 17, 2000, now U.S. Pat. No. 6,325,928, and assigned to ZENON Environmental Inc. describes an example of a suitable membrane module and aerator and is incoporated herein by this reference.
- Such modules can provide 500 to 1500 m 2 of membrane surface area for each m2 of horizontal cross sectional area of a large municipal or commercial tank and there is minimal channeling or dead zones when tank water flows through the modules.
- the module 10 has a plurality of elements 110 placed side by side in a row.
- Each element 110 has a vertically extending closed header 112 and a vertically extending open header 114 held in an opposed horizontally spaced relationship by one or more side plates 116 or struts 118 extending between the closed header 112 and open header 114 .
- the last element 110 in the row has two side plates 116 .
- a single side plate 116 between two elements 110 serves both such elements 110 .
- Side plates 116 , open headers 112 and closed headers 114 define vertical flow channels 172 through elements 110 .
- a plurality of hollow fibre membranes 126 are attached to and suspended between the closed header 112 and the open header 114 .
- the membranes 126 have at least one open end 132 each.
- the open ends 132 of the membranes 126 are held in a closely spaced apart relationship in a plug of potting resin 130 which encloses one or more permeate channels 128 of the open header 114 .
- the resin 130 surrounds each open end 132 of the membrane 126 so that water cannot enter the permeate channel 128 other than by passing through the walls of the membranes 126 .
- the interior of the membranes 126 are in fluid communication with the one or more permeate channels 128 so that permeate withdrawn through the membranes 126 can be collected in the one or more permeate channels 128 .
- the membrane modules 10 are sized and positioned to fill most of the horizontal cross-sectional area of the tank 12 leaving room only for necessary fittings and other apparatus and maintenance or set-up procedures. Space is not provided for downcomers outside the perimeter of the modules 10 and baffles are provided if necessary to block flow through any space left for fittings etc. or otherwise outside the perimeter of the membrane modules 10 . Preferably more than 90%, more preferably substantially all, of the horizontal cross-sectional area of the tank 12 is filled with modules 56 .
- a permeate pipe 18 connects the headers of the membrane modules 10 to means for permeating by suction on the inner surfaces of the membranes and backwashing means. Such means are known in the art and allow the permeate pipe 18 to be used to either withdraw permeate from the tank 12 or to flow a backwashing liquid (typically permeate or permeate mixed with a chemical) in a reverse direction through the membranes and into the tank 12 in which the backwashing liquid becomes part of tank water 36 .
- a backwashing liquid typically permeate or permeate mixed with a chemical
- An upper portion 20 of the tank 12 is provided with a retentate outlet 22 having an overflow area 24 connected to a drain pipe 26 to remove retentate from the tank 12 .
- Retentate outlet 22 preferably incorporates an overflow or weir 28 which helps foam produced by aeration (otherwise a cleanliness, safety or volatile chemical release problem) to flow into the overflow area 24 .
- the retentate outlet 22 preferably also has sufficient capacity to release expected flows of retentate quickly to reduce the required free board of the tank 12 .
- a filtration cycle has a permeation step followed by a deconcentration step and is repeated many times between more intensive maintenance or recovery cleaning procedures.
- the permeation step typically lasts for about 15 to 60 minutes, preferably 20 to 40 minutes and is carried out in the absence of aeration.
- Permeate flux is preferably between 10 and 60 L/m 2 /h, more preferably between 20 and 40 L/m 2 /h, wherein the surface area of hollow fibre membranes is based on the outside diameter of the membranes.
- feed water is added to the tank 12 from one of the inlets 30 , 32 at substantially the rate at which permeate is withdrawn.
- Tank water 36 flows through the membrane modules 10 to generally replace permeate as it is withdrawn from the tank 12 .
- the membrane module 10 acts to some extent like a media filter (such as the modules in U.S. patent application Ser. No. 09/505,718 referred to above)
- feed preferably enters the tank 12 through the second inlet 32 .
- the deconcentration step commences when permeation stops and lasts for about 20 to 90 seconds, preferably 30 to 60 seconds. During the deconcentration step, scouring bubbles are produced at the aerator 14 and rise through the membrane modules 10 . In addition one or both of the steps of backwashing and feed flushing are performed. To flush with feed water, feed enters the tank 12 through the first inlet 30 creating an excess of tank water 36 which rises upwards through the membrane modules 10 .
- the rate of flow of feed water during feed flushing is typically between 0.5 and 2, preferably between 0.7 and 1.5, times the rate of flow of feed water during permeation.
- tank water 36 With either backwashing or feed flushing, the level of the tank water 36 rises, tank water 36 flows upwards through the membrane modules 10 and tank water 36 containing solids (then called retentate) flows out of the retentate outlet 22 to deconcentrate the tank water 36 .
- retentate solids
- the upwards velocity of the tank water 36 may create forces on the membranes that exceed their strength, particularly if strong feed flushing and back washing are performed simultaneously. In these cases, the rate of flow of feed water or backwash liquid or both can be reduced to reduce the upward velocity of the tank water 36 .
- the flow of feed water can be turned off during backwashing and any feed flushing done while there is no backwashing and vice versa.
- a deconcentration step may involve backwashing preferably with aeration but without feed flushing for a first part of the deconcentration step and feed flushing preferably with aeration but without backwashing for a second part of the deconcentration step.
- deconcentration steps involving backwashing preferably with aeration but without feed flushing can be performed in some cycles and deconcentration steps involving feed flushing preferably with aeration but without backwashing can be used in other cycles.
- deconcentration steps involving feed flushing preferably with aeration but without backwashing can be used in other cycles.
- Other combinations of the above procedures might also be used.
- Aeration is typically performed at the same time as the other steps to reduce the total time of the deconcentration step. Aeration may, however, begin several seconds (approximately the time required for a bubble to rise from the aerator 14 to the surface of the tank water 36 ) before backwashing or feed flushing. Such aeration in the absence of tank water 36 flow (because no space was left for downcomers) causes turbulence which help loosen some foulants and float some solids to near the top of the tank 12 before retentate starts flowing out the retentate outlet 20 .
- Aeration during the deconcentration step does not need to overcome suction to dislodge solids from the membranes and is provided at a superficial velocity (m 3 /h of air at standard conditions per m 2 of module cross-sectional area) between 25 m/h and 75 m/h.
- a superficial velocity m 3 /h of air at standard conditions per m 2 of module cross-sectional area
- additional aeration is not required.
- a smaller amount of aeration may be provided with difficult feed water during permeation to disperse solids from dead zones in a membrane module 10 and homogenize the tank water 36 .
- aeration is provided at a superficial velocity less than 25 m/h or intermittently at the higher rates described above.
- the feed water or backwashing liquid introduced into the tank 12 creates a flow of tank water 36 upwards through the modules 10 .
- the tank water 36 flowing through the membrane modules 10 helps remove solids loosened by the scouring bubbles from the membrane modules 10 and also directly acts on the surface of the membranes.
- the tank water 36 flows most rapidly near the top of the tank 12 which helps reduce preferential fouling of upper membranes when membrane modules 10 are stacked, for example to depths of 2 m or more.
- Some solids in the tank water 36 may have a settling velocity greater than the velocity of the upflow velocity and will settle. The volume of these solids is small and they may be removed from time to time by partially draining the tank 12 through a supplemental drain 38 .
- the required flow of feed water during permeation can be calculated and delivered, typically by adjusting a feed pump or feed valve.
- the frequency and intensity of deconcentration events is then selected to achieve a desired loss in membrane permeability over time. If flux during permeation is kept below about 60 L/m 2 /h, preferably less than 40 L/m 2 /h, the inventors have found that surprising little fouling occurs and the periodic deconcentration events are usually sufficient. More surprisingly, the energy cost savings produced by operating at low flux and low aeration more than offsets the cost of filling the tank 12 with membrane modules 10 .
- FIG. 3 shows a plan view of a larger filtering reactor.
- a tank 200 encloses several cassettes 220 each of which may contain a plurality of membrane modules. Open channels 202 are provided between adjacent cassettes 220 to receive tank water overflowing the cassettes 210 as described above.
- the channels 202 are sloped to drain towards a larger trough 204 , which is in turn sloped to drain towards a second outlet 206 .
- the second outlet 206 has an outlet box 208 to temporarily hold the discharged tank water before it flows into a drain pipe_ 210 .
- feed water enters the tank 200 at a point below the cassettes 220 , but several second inlets 212 are attached to an inlet header 214 to provide a distributed supply of feed.
Abstract
Modules of ultrafiltration or microfiltration membranes are arranged in a tank open to the atmosphere to substantially cover the cross sectional area of the tank. A filtration cycle has permeation steps and deconcentration steps. During permeation, supply of feed substantially equals feed removed and little if any aeration is used. During deconcentration, aeration with scouring bubbles is provided with one or both of backwashing and feed flushing. In feed flushing, feed water is supplied to the tank from below the modules. Excess tank water created during deconcentration flows generally upwards through the modules and out through a retentate outlet or overflow at the top of the tank.
Description
- This is a continuation of U.S. application Ser. No. 11/038,278, filed Jan. 21, 2005, which is a continuation of U.S. application Ser. No. 09/565,032 filed May 5, 2000. U.S. application Ser. Nos. 11/038,278 and 09/565,032 are incorporated herein, in their entirety, by this reference to them.
- This invention relates to a filtration system using immersed suction driven filtering membranes to filter water, for example, to filter surface water to produce potable water, and to a method of operating such a system.
- A prior art immersed membrane water filtration system is shown in
FIG. 1 . An open tank (a) holds a membrane module (b) immersed in tank water (c). Feed water to be filtered flows into the tank, typically continuously. Suction on an inner surface of the membranes in the membrane module (b) draws filtered permeate through the membrane wall. Solids are rejected by the membranes and accumulate in the tank water (c). Solids rich retentate is continuously or periodically drained from the tank. - The membrane module (b) is cleaned in part by backwashing and aeration. In backwashing, a backwashing liquid (typically permeate or permeate with a chemical additive) is pumped into the inner spaces of the membranes and flows into the tank water (c). In aeration, air bubbles are created at an aerator (d) mounted below the membrane module (c). The air bubbles agitate and scour the membranes and create an air lift effect. The air lift effect moves tank water (c) in a recirculation pattern (e) upwards through the membrane module (b) and in a downcomer (f) through spaces between the perimeter of the module (b) and the sides of the tank (a). The tank water (c) flowing in the recirculation pattern (e) further physically cleans the membranes and disperses solids rich water from near the membrane module (b).
- It is an object of the present invention to improve on the prior art. This object is met by the combination of features, steps or both found in the independent claims, the dependent claims disclosing further advantageous embodiments of the invention. The following summary may not describe all necessary features of the invention which may reside in a sub-combination of the following features or in a combination with features described in other parts of this document.
- In various aspects of the invention, a filtration system having immersed suction driven filtering membranes is used to filter water containing low concentrations of suspended solids, for example, to filter surface water to produce potable water. A process is provided for operating such a system.
- Membrane modules are arranged in a tank open to the atmosphere and fill most of its horizontal cross sectional area. An upper portion of the tank encloses a volume directly above the modules. This upper portion of the tank is provided with a retentate outlet from the tank. Tank water that is not withdrawn as permeate flows out of the tank through the retentate outlet.
- Permeate is withdrawn by suction on an inner surface of the membranes, preferably at a flux between 10 and 60 L/m2/h, more preferably between 20 and 40 L/m2/h. Feed water is added to the tank at a rate that substantially equals the rate at which permeate is withdrawn. Thus during permeation little if any tank water flows out of the outlet and the level of the tank water remains above the membranes.
- Permeation is stopped periodically for a deconcentration step. During the deconcentration step the membranes are backwashed, feed flow is provided from below the modules or both. Tank water rises through the modules, the water level in the tank rises and tank water containing solids (then called retentate) flows out of the retentate outlet to deconcentrate the tank water. Aeration with scouring bubbles is provided during the deconcentration step.
-
FIG. 1 is a schematic representation of a prior art filtration system. -
FIG. 2 is a schematic representation of a filtering reactor made in accordance with a preferred embodiment of the present invention. -
FIG. 3 is a plan view of a filtering reactor made in accordance with a preferred embodiment of the present invention. -
FIG. 4 shows a plan view of a module ofFIG. 1 . - Referring to
FIG. 2 , threemembrane modules 10 are stacked on top of each other in atank 12. Thetank 12 is open to the atmosphere although it may be covered with a ventedlid 13. Themembrane modules 10 may contain flat sheet or hollow fibre membranes with pore sizes in the microfiltration or ultrafiltration range, preferably between 0.003 and 10 microns and more preferably between 0.01 and 1.0 microns. An inner surface of the membranes is connected to one or more headers. Anaerator 14 is mounted below themembrane modules 10. Theaerator 14 is connected to anair supply pipe 14 in turn connected to a supply of air, nitrogen or other suitable gas. - Preferably, the
membrane modules 10 contain hollow fibre membranes oriented horizontally and mounted in a slightly slackened state between pairs of horizontally spaced, vertically extending headers. U.S. patent application Ser. No. 09/505,718 filed Feb. 17, 2000, now U.S. Pat. No. 6,325,928, and assigned to ZENON Environmental Inc. describes an example of a suitable membrane module and aerator and is incoporated herein by this reference. Such modules can provide 500 to 1500 m2 of membrane surface area for each m2 of horizontal cross sectional area of a large municipal or commercial tank and there is minimal channeling or dead zones when tank water flows through the modules. - Referring now to
FIG. 4 , a plan view of amodule 10 is shown. Themodule 10 has a plurality ofelements 110 placed side by side in a row. Eachelement 110 has a vertically extendingclosed header 112 and a vertically extendingopen header 114 held in an opposed horizontally spaced relationship by one ormore side plates 116 orstruts 118 extending between the closedheader 112 andopen header 114. Thelast element 110 in the row has twoside plates 116. For other elements, asingle side plate 116 between twoelements 110 serves bothsuch elements 110.Side plates 116,open headers 112 and closedheaders 114 definevertical flow channels 172 throughelements 110. - A plurality of
hollow fibre membranes 126 are attached to and suspended between the closedheader 112 and theopen header 114. Themembranes 126 have at least oneopen end 132 each. Theopen ends 132 of themembranes 126 are held in a closely spaced apart relationship in a plug ofpotting resin 130 which encloses one ormore permeate channels 128 of theopen header 114. Theresin 130 surrounds eachopen end 132 of themembrane 126 so that water cannot enter thepermeate channel 128 other than by passing through the walls of themembranes 126. The interior of themembranes 126 are in fluid communication with the one or morepermeate channels 128 so that permeate withdrawn through themembranes 126 can be collected in the one or morepermeate channels 128. - The
membrane modules 10 are sized and positioned to fill most of the horizontal cross-sectional area of thetank 12 leaving room only for necessary fittings and other apparatus and maintenance or set-up procedures. Space is not provided for downcomers outside the perimeter of themodules 10 and baffles are provided if necessary to block flow through any space left for fittings etc. or otherwise outside the perimeter of themembrane modules 10. Preferably more than 90%, more preferably substantially all, of the horizontal cross-sectional area of thetank 12 is filled with modules 56. - A
permeate pipe 18 connects the headers of themembrane modules 10 to means for permeating by suction on the inner surfaces of the membranes and backwashing means. Such means are known in the art and allow thepermeate pipe 18 to be used to either withdraw permeate from thetank 12 or to flow a backwashing liquid (typically permeate or permeate mixed with a chemical) in a reverse direction through the membranes and into thetank 12 in which the backwashing liquid becomes part oftank water 36. - An
upper portion 20 of thetank 12 is provided with aretentate outlet 22 having anoverflow area 24 connected to adrain pipe 26 to remove retentate from thetank 12.Retentate outlet 22 preferably incorporates an overflow orweir 28 which helps foam produced by aeration (otherwise a cleanliness, safety or volatile chemical release problem) to flow into theoverflow area 24. Theretentate outlet 22 preferably also has sufficient capacity to release expected flows of retentate quickly to reduce the required free board of thetank 12. - Feed water enters the
tank 12 through afirst inlet 30 or asecond inlet 32 as determined byfeed valves 34. Once in thetank 12, feed water may be calledtank water 36 which flows generally upwards or downwards through themembrane modules 10. - A filtration cycle has a permeation step followed by a deconcentration step and is repeated many times between more intensive maintenance or recovery cleaning procedures. The permeation step typically lasts for about 15 to 60 minutes, preferably 20 to 40 minutes and is carried out in the absence of aeration. Permeate flux is preferably between 10 and 60 L/m2/h, more preferably between 20 and 40 L/m2/h, wherein the surface area of hollow fibre membranes is based on the outside diameter of the membranes.
- During permeation, feed water is added to the
tank 12 from one of theinlets Tank water 36 flows through themembrane modules 10 to generally replace permeate as it is withdrawn from thetank 12. Thus during permeation little if anytank water 36 flows out of theretentate outlet 22 and the level of thetank water 36 remains above the membranes. If themembrane module 10 acts to some extent like a media filter (such as the modules in U.S. patent application Ser. No. 09/505,718 referred to above), feed preferably enters thetank 12 through thesecond inlet 32. In this way, solids in some feed waters are preferentially deposited in theupper membrane module 10, closer to theretentate outlet 22 and where the upward velocity of thetank water 36 during a deconcentration step will be the greatest, as will be explained below. This set up is also useful in retrofitting sand filters which are typically set up to receive feed from the top and to backwash from below. Forother membrane modules 10, installations or feed waters, thefirst inlet 30 may be used during permeation. - The deconcentration step commences when permeation stops and lasts for about 20 to 90 seconds, preferably 30 to 60 seconds. During the deconcentration step, scouring bubbles are produced at the
aerator 14 and rise through themembrane modules 10. In addition one or both of the steps of backwashing and feed flushing are performed. To flush with feed water, feed enters thetank 12 through thefirst inlet 30 creating an excess oftank water 36 which rises upwards through themembrane modules 10. The rate of flow of feed water during feed flushing is typically between 0.5 and 2, preferably between 0.7 and 1.5, times the rate of flow of feed water during permeation. With either backwashing or feed flushing, the level of thetank water 36 rises,tank water 36 flows upwards through themembrane modules 10 andtank water 36 containing solids (then called retentate) flows out of theretentate outlet 22 to deconcentrate thetank water 36. - In some cases, the upwards velocity of the
tank water 36 may create forces on the membranes that exceed their strength, particularly if strong feed flushing and back washing are performed simultaneously. In these cases, the rate of flow of feed water or backwash liquid or both can be reduced to reduce the upward velocity of thetank water 36. Alternatively, the flow of feed water can be turned off during backwashing and any feed flushing done while there is no backwashing and vice versa. For example, a deconcentration step may involve backwashing preferably with aeration but without feed flushing for a first part of the deconcentration step and feed flushing preferably with aeration but without backwashing for a second part of the deconcentration step. Further alternatively, deconcentration steps involving backwashing preferably with aeration but without feed flushing can be performed in some cycles and deconcentration steps involving feed flushing preferably with aeration but without backwashing can be used in other cycles. Other combinations of the above procedures might also be used. - Aeration is typically performed at the same time as the other steps to reduce the total time of the deconcentration step. Aeration may, however, begin several seconds (approximately the time required for a bubble to rise from the
aerator 14 to the surface of the tank water 36) before backwashing or feed flushing. Such aeration in the absence oftank water 36 flow (because no space was left for downcomers) causes turbulence which help loosen some foulants and float some solids to near the top of thetank 12 before retentate starts flowing out theretentate outlet 20. - Aeration during the deconcentration step does not need to overcome suction to dislodge solids from the membranes and is provided at a superficial velocity (m3/h of air at standard conditions per m2 of module cross-sectional area) between 25 m/h and 75 m/h. For many if not most feed waters, particularly those feed waters having low turbidity and solids concentrations less than about 500 mg/L, additional aeration is not required. Nevertheless, a smaller amount of aeration may be provided with difficult feed water during permeation to disperse solids from dead zones in a
membrane module 10 and homogenize thetank water 36. For this purpose, aeration is provided at a superficial velocity less than 25 m/h or intermittently at the higher rates described above. - During the deconcentration step, the feed water or backwashing liquid introduced into the
tank 12 creates a flow oftank water 36 upwards through themodules 10. Thetank water 36 flowing through themembrane modules 10 helps remove solids loosened by the scouring bubbles from themembrane modules 10 and also directly acts on the surface of the membranes. Thetank water 36 flows most rapidly near the top of thetank 12 which helps reduce preferential fouling of upper membranes whenmembrane modules 10 are stacked, for example to depths of 2 m or more. Some solids in thetank water 36 may have a settling velocity greater than the velocity of the upflow velocity and will settle. The volume of these solids is small and they may be removed from time to time by partially draining thetank 12 through asupplemental drain 38. - Based on a design permeate flux, the required flow of feed water during permeation can be calculated and delivered, typically by adjusting a feed pump or feed valve. The frequency and intensity of deconcentration events is then selected to achieve a desired loss in membrane permeability over time. If flux during permeation is kept below about 60 L/m2/h, preferably less than 40 L/m2/h, the inventors have found that surprising little fouling occurs and the periodic deconcentration events are usually sufficient. More surprisingly, the energy cost savings produced by operating at low flux and low aeration more than offsets the cost of filling the
tank 12 withmembrane modules 10. Despite the low flux (compared to a more typical flux of 50 to 100 L/m2/h), high tank velocities (flux of permeate in m3/h divided by tank horizontal cross sectional area in m2) are achieved which compare favourably with sand filtration. Further, resulting recovery rates are generally adequate for single stage filtration and are typically adequate for the first stage of two stage filtration (wherein the retentate is refiltered) even with aggressive deconcentration. -
FIG. 3 shows a plan view of a larger filtering reactor. Atank 200 enclosesseveral cassettes 220 each of which may contain a plurality of membrane modules.Open channels 202 are provided betweenadjacent cassettes 220 to receive tank water overflowing thecassettes 210 as described above. Thechannels 202 are sloped to drain towards alarger trough 204, which is in turn sloped to drain towards asecond outlet 206. Thesecond outlet 206 has anoutlet box 208 to temporarily hold the discharged tank water before it flows into a drain pipe_210. As in the embodiment ofFIG. 2 , feed water enters thetank 200 at a point below thecassettes 220, but severalsecond inlets 212 are attached to aninlet header 214 to provide a distributed supply of feed. - It is to be understood that what has been described are preferred embodiments of the invention for example and without limitation to the combination of features necessary for carrying the invention into effect. The invention may be susceptible to certain changes and alternative embodiments without departing from the subject invention, the scope of which is defined in the following claims.
Claims (3)
1. A filtering reactor comprising,
a) a tank open to the atmosphere;
b) one or more modules of suction driven filtering membranes in the tank for withdrawing a filtered permeate;
c) an inlet to add feed water to the tank from below the one or more modules;
d) one or more open channels spanning a portion of the tank above the one or more modules; and,
e) a retentate outlet connected to the one or more open channels to discharge water containing retained solids from the tank from above the one or more modules.
2. The reactor of claim 1 wherein the modules cover most of the horizontal cross sectional area of the tank.
3. The reactor of claim 1 wherein the filtering membranes are hollow fibres oriented horizontally.
Priority Applications (1)
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US11/387,807 US20060163139A1 (en) | 1999-11-18 | 2006-03-24 | Immersed membrane filtration system and overflow process |
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CA002290053A CA2290053C (en) | 1999-11-18 | 1999-11-18 | Immersed membrane module and process |
CA2,290,053 | 1999-11-18 | ||
US09/565,032 US6893568B1 (en) | 1999-11-18 | 2000-05-05 | Immersed membrane filtration system and overflow process |
US11/038,278 US7052610B2 (en) | 1999-11-18 | 2005-01-21 | Immersed membrane filtration system and overflow process |
US11/387,807 US20060163139A1 (en) | 1999-11-18 | 2006-03-24 | Immersed membrane filtration system and overflow process |
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US11/038,278 Continuation US7052610B2 (en) | 1999-11-18 | 2005-01-21 | Immersed membrane filtration system and overflow process |
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US20060163139A1 true US20060163139A1 (en) | 2006-07-27 |
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US09/565,032 Expired - Fee Related US6893568B1 (en) | 1998-11-23 | 2000-05-05 | Immersed membrane filtration system and overflow process |
US11/038,278 Expired - Lifetime US7052610B2 (en) | 1999-11-18 | 2005-01-21 | Immersed membrane filtration system and overflow process |
US11/387,807 Abandoned US20060163139A1 (en) | 1999-11-18 | 2006-03-24 | Immersed membrane filtration system and overflow process |
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US09/505,718 Expired - Lifetime US6325928B1 (en) | 1998-11-23 | 2000-02-17 | Immersed membrane element and module |
US09/565,032 Expired - Fee Related US6893568B1 (en) | 1998-11-23 | 2000-05-05 | Immersed membrane filtration system and overflow process |
US11/038,278 Expired - Lifetime US7052610B2 (en) | 1999-11-18 | 2005-01-21 | Immersed membrane filtration system and overflow process |
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Also Published As
Publication number | Publication date |
---|---|
CA2290053A1 (en) | 2001-05-18 |
US6893568B1 (en) | 2005-05-17 |
CA2290053C (en) | 2009-10-20 |
US6325928B1 (en) | 2001-12-04 |
US7052610B2 (en) | 2006-05-30 |
US20050121389A1 (en) | 2005-06-09 |
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