EP1115474A1 - Apparatus and method for cleaning membrane filtration modules - Google Patents

Abstract

A method and apparatus for cleaning a membrane module (5), the membrane module comprising a plurality of porous membranes (6), said membranes being arranged in close proximity to one another and mounted to prevent excessive movement therebetween, and means (10, 12) for providing, from within the module (5), by means other than gas passing through the pores of said membranes, gas bubbles entrained in a liquid flow such that, in use, said liquid and bubbles (18) entrained therein move past the surfaces of said membranes to dislodge fouling materials therefrom, said gas bubbles being entrained in said liquid by flowing said liquid past a source of gas to draw the gas into said liquid flow. The gas bubbles are entrained into the liquid using a venturi type device (12). The membranes (20) are preferably partitioned into discrete groups (23) to assist cleaning while maintaining high packing density.

Description

TITLE: APPARATUS AND METHOD FOR CLEANING MEMBRANE FILTRATION

MODULES

TECHNICAL FIELD

The present invention relates to an apparatus and the related method to effectively

clean membrane modules by means of a mixture of gas and liquid formed by a venturi, jet

or the like. For membrane modules to be applied to an environment of high concentration

of suspended solids, for example, in bioreactors, several improved module configurations

are described to reduce solid accumulation within a module.

BACKGROUND OF THE INVENTION

The importance of membrane for treatment of waste water is growing rapidly. It is

now well known that membrane processes can be used as an effective tertiary treatment of

sewage and provide quality effluent. However, the capital and operating cost can be

prohibitive. With the arrival of submerged membrane processes where the membrane

modules are immersed in a large feed tank and filtrate is collected through suction applied

to the filtrate side of the membrane, membrane bioreactors combining biological and

physical processes in one stage promise to be more compact, efficient and economic. Due

to their versatility, the size of membrane bioreactors can range from household (such as

septic tank systems) to the community and large-scale sewage treatment.

The success of a membrane filtration process largely depends on employing an

effective and efficient membrane cleaning method. Commonly used physical cleaning

methods include backwash (backpulse, backflush) using a liquid permeate or a gas, membrane surface scrubbing or scouring using a gas in the form of bubbles in a liquid.

Examples of the second type of method is illustrated in United States Patent no 5,192,456

to Ishida et al, United States Patent No. 5,248,424 to Cote et al, United States Patent No.

5,639,373 to Henshaw et al, United States Patent No. 5,783,083 to Henshaw et al and our

PCT Application No. WO98/28066.

In the examples referred to above, a gas is injected, usually by means of a pressurised

blower, into a liquid system where a membrane module is submerged to form gas bubbles.

The bubbles so formed then travel upwards to scrub the membrane surface to remove the

fouling substances formed on the membrane surface. The shear force produced largely

relies on the initial gas bubble velocity, bubble size and the resultant of forces applied to

the bubbles. The fluid transfer in this approach is limited to the effectiveness of the gas

lifting mechanism. To enhance the scrubbing effect, more gas has to be supplied.

However, this method has several disadvantages: it consumes large amounts of energy,

possibly forms mist or froth flow reducing effective membrane filtration area, and may be

destructive to membranes. Moreover, in an environment of high concentration of solids,

the gas distribution system may gradually become blocked by dehydrated solids or simply

be blocked when the gas flow accidentally ceases.

For most tubular membrane modules, the membranes are flexible in the middle

(longitudinal direction) of the modules but tend to be tighter and less flexible towards to

both potted heads. When such modules are used in an environment containing high

concentrations of suspended solids, solids are easily trapped within the membrane bundle,

especially in the proximity of two potted heads. The methods to reduce the accumulation

of solids include the improvement of module configurations and flow distribution when

gas scrubbing is used to clean the membranes. In the design of a membrane module, the packing density of the tubular membranes

in a module is an important factor. The packing density of the fibre membranes in a

membrane module as used herein is defined as the cross-sectional potted area taken up by

the fibre membranes divided by the total potted area and is normally expressed as a

percentage. From the economical viewpoint it is desirable that the packing density be as

high as possible to reduce the cost of making membrane modules. In practice solid

packing is reduced in a less densely packed membrane module. However, if the packing

density is too low, the rubbing effect between membranes could also be lessened, resulting

in less efficient scrubbing/scouring of the membrane surfaces. It is thus desirable to

provide a membrane configuration which assists removal of accumulated solids while

maximising packing density of the membranes.

DISCLOSURE OF THE INVENTION

The present invention, at least in its embodiments, seeks to overcome or least

ameliorate some of the disadvantages of the prior art or at least provide the public with a

useful alternative.

According to one aspect, the present invention provides a method of scrubbing a

membrane surface using a liquid medium with gas bubbles entrained therein, including the

steps of entraining said gas bubbles into said liquid medium by flow of said liquid medium

past a source of said gas, and flowing said gas bubbles and liquid medium along said

membrane surface to dislodge fouling materials therefrom.

Preferably, the gas bubbles are entrained into said liquid stream by means of a

venturi device. For further preference, the gas bubbles are entrained or injected into said

liquid stream by means of devices which forcibly mix gas into a liquid flow to produce a

mixture of liquid and bubbles, such devices including a jet, nozzle, ejector, eductor, injector or the like. Optionally, an additional source of bubbles may be provided in said

liquid medium by means of a blower or like device. The gas used may include air, oxygen,

gaseous chlorine or ozone. Air is the most economical for the purposes of scrubbing

and/or aeration. Gaseous chlorine may be used for scrubbing, disinfection and enhancing

the cleaning efficiency by chemical reaction at the membrane surface. The use of ozone,

besides the similar effects mentioned for gaseous chlorine, has additional features, such as

oxidising DBP precursors and converting non-biodegradable NOM's to biodegradable

dissolved organic carbon.

According to a second aspect, the present invention provides a membrane module

comprising a plurality of porous membranes, said membranes being arranged in close

proximity to one another and mounted to prevent excessive movement therebetween, and

means for providing, from within the module, by means other than gas passing through the

pores of said membranes, gas bubbles entrained in a liquid flow such that, in use, said

liquid and bubbles entrained therein move past the surfaces of said membranes to dislodge

fouling materials therefrom, said gas bubbles being entrained in said liquid by flowing said

liquid past a source of gas to draw the gas into said liquid flow.

Preferably, said liquid and bubbles are mixed and then flowed past membranes to

dislodge the fouling materials.

According to one preferred form, the present invention provides a method of

removing fouling materials from the surface of a plurality of porous hollow fibre

membranes mounted and extending longitudinally in an array to form a membrane module,

said membranes being arranged in close proximity to one another and mounted to prevent

excessive movement therebetween, the method comprising the steps of providing, from

within said array, by means other than gas passing through the pores of said membranes, uniformly distributed gas bubbles entrained in a liquid flow, said gas bubbles being

entrained in said liquid flow by flowing said liquid past a source of gas so as to cause said

gas to be drawn and/or mixed into said liquid, said distribution being such that said bubbles

pass substantially uniformly between each membrane in said array to, in combination with

said liquid flow, scour the surface of said membranes and remove accumulated solids from

within the membrane module. Preferably, said bubbles are injected and mixed into said

liquid flow.

For preference, the membranes comprise porous hollow fibres, the fibres being fixed

at each end in a header, the lower header having one or more holes formed therein through

which gas/liquid flow is introduced. The holes can be circular, elliptical or in the form of a

slot. The fibres are normally sealed at the lower end and open at their upper end to allow

removal of filtrate, however, in some arrangements, the fibres may be open at both ends to

allow removal of filtrate from one or both ends. The fibres are preferably arranged in

cylindrical arrays or bundles. It will be appreciated that the cleaning process described is

equally applicable to other forms of membrane such flat or plate membranes.

According to a further aspect the present invention provides a membrane module

comprising a plurality of porous hollow fibre membranes, said fibre membranes being

arranged in close proximity to one another and mounted to prevent excessive movement

therebetween, the fibre membranes being fixed at each end in a header, one header having

one or more of holes formed therein through which gas/liquid flow is introduced, and

partition means extending at least part way between said headers to partition said

membrane fibres into groups. Preferably, the partition means are formed by a spacing

between respective fibre groups. The partitions may be parallel to each other or, in the

case of cylindrical arrays of fibre membranes, the partitions may extend radially from the centre of the array or be positioned concentrically within the cylindrical array. In an

alternative form, the fibre bundle may be provided with a central longitudinal passage

extending the length of the bundle between the headers.

According to yet a further aspect, the present invention provides a membrane module

for use in a membrane bioreactor including a plurality of porous hollow membrane fibres

extending longitudinally between and mounted at each end to a respective potting head,

said membrane fibres being arranged in close proximity to one another and mounted to

prevent excessive movement therebetween, said fibres being partitioned into a number of

bundles at least at or adjacent to their respective potting head so as to form a space

therebetween, one of said potting heads having an array of aeration openings formed

therein for providing gas bubbles within said module such that, in use, said bubbles move

past the surfaces of said membrane fibres to dislodge fouling materials therefrom.

The fibre bundle is protected and fibre movement is limited by a module support

screen which has both vertical and horizontal elements appropriately spaced to provide

unrestricted fluid and gas flow through the fibres and to restrict the amplitude of fibre

motion reducing energy concentration at the potted ends of the fibres.

Preferably, said aeration openings are positioned to coincide with the spaces formed

between said partitioned bundles. For preference, said openings comprise a slot, slots or a

row of holes. Preferably, the fibre bundles are located in the potting head between the slots

or rows of holes.

For further preference, the gas bubbles are entrained or mixed with a liquid flow

before being fed through said holes or slots, though it will be appreciated that gas only may

be used in some configurations. The liquid used may be the feed to the membrane module.

The fibres and/or fibre bundles may cross over one another between the potting heads though it is desirable that they do not.

Preferably, the fibres within the module have a packing density (as defined above) of

between about 5 to about 70% and, more preferably, between about 8 to about 55%.

For preference, said holes have a diameter in the range of about 1 to 40 mm and more

preferably in the range of about 1.5 to about 25 mm. In the case of a slot or row of holes,

the open area is chosen to be equivalent to that of the above holes.

Typically, the fibre inner diameter ranges from about 0.1 mm to about 5 mm and is

preferably in the range of about 0.25 mm to about 2 mm. The fibres wall thickness is

dependent on materials used and strength required versus filtration efficiency. Typically

wall thickness is between 0.05 to 2 mm and more often between 0.1 mm to 1 mm.

According to another aspect, the present invention provides a membrane bioreactor

including a tank having means for the introduction of feed thereto, means for forming

activated sludge within said tank, a membrane module according to the first aspect

positioned within said tank so as to be immersed in said sludge and said membrane module

provided with means for withdrawing filtrate from at least one end of said fibre

membranes.

According to yet another aspect, the present invention provides a method of

operating a membrane bioreactor of the type described in the second aspect comprising

introducing feed to said tank, applying a vacuum to said fibres to withdraw filtrate

therefrom while periodically or continuously supplying gas bubbles through said aeration

openings to within said module such that, in use, said bubbles move past the surfaces of

said membrane fibres to dislodge fouling materials therefrom. Preferably, the gas bubbles

are entrained or mixed with a liquid flow when fed through said holes or slots.

If required, a further source of aeration may be provided within the tank to assist microorganism activity. For preference, the membrane module is suspended vertically

within the tank and said further source of aeration may be provided beneath the suspended

module. Preferably, the further source of aeration comprises a group of air permeable

tubes. The membrane module may be operated with or without backwash depending on

the flux. A high mixed liquor of suspended solids (5,000 to 20,000 ppm) in the bioreactor

has been shown to significantly reduce residence time and improve filtrate quality. The

combined use of aeration for both degradation of organic substances and membrane

cleaning has been shown to enable constant filtrate flow without significant increases in

transmembrane pressure while establishing high concentration of MLS S. The use of

partitioned fibre bundles enables higher packing densities to be achieved without

significantly compromising the gas scouring process. This provides for higher filtration

efficiencies to be gained.

BRIEF DESCRIPTION OF THE DRAWINGS

Preferred embodiments of the invention will now be described, by way of example

only, with reference to the accompanying drawings in which:-

Figure 1 shows a schematic side elevation of one embodiment of a membrane

module and illustrates the method of cleaning according to the invention;

Figure 2 shows an enlarged schematic side elevation of one form of the jet type

arrangement used to form entrained gas bubbles;

Figure 3a shows a schematic side elevation of a partitioned membrane module

according to one embodiment of the present invention;

Figure 3b shows a section through the membrane bundle of Figure 3a;

Figure 4a shows a schematic side elevation of a partitioned membrane module according to a further embodiment of the present invention;

Figure 4b shows a section through the membrane bundle of Figure 4a;

Figure 5a shows a schematic side elevation of a partitioned membrane module

according to another embodiment of the present invention;

Figure 5b shows a section through the membrane bundle of Figure 5a;

Figure 6a shows a schematic side elevation of a partitioned membrane module

according to another embodiment of the present invention;

Figure 6b shows a section through the membrane bundle of Figure 6a;

Figure 7 shows a similar view to Figure 2 of a further embodiment of the invention;

Figure 8 shows a similar view to Figure 2 of yet a further embodiment of the

invention;

Figure 9 shows a sectioned perspective pictorial view of the lower end of another

preferred embodiment of the membrane module according to the invention; and

Figure 10 shows a sectioned perspective pictorial view of the upper end of the

membrane module o f Figure 9.

PREFERRED EMBODIMENTS OF THE INVENTION

Referring to the drawings, the embodiments of the invention will be described in

relation to a membrane module of the type disclosed in our earlier PCT application No.

WO98/28066 which is incorporated herein by cross-reference, however, it will be

appreciated that the invention is equally applicable to other forms of membrane module.

The membrane module 5 typically comprises fibre, tubular or flat sheet form membranes 6

potted at two ends 7 and 8 and encased in a support structure, in this case a screen 9.

Either one or both ends of the membranes may be used for the permeate collection. The bottom of the membrane module has a number of through apertures 10 in the pot 11 to

distribute a mixture of gas and liquid feed past the membrane surfaces.

Referring to the embodiment shown in Figure 1, a venturi device 12 or the like is

connected to the base of the module. The venturi device 12 intakes gas through inlet 13,

mixes or entrains the gas with liquid flowing through feed inlet 14, forms gas bubbles and

diffuses the liquid/gas mix into the module apertures 10. After passing through the

distribution apertures 10, the entrained gas bubbles scrub membrane surfaces while

travelling upwards along with the liquid flow. Either the liquid feed or the gas can be a

continuous or intermittent injection depending on the system requirements. With a venturi

device it is possible to create gas bubbles and aerate the system without a blower. The

venturi device 12 can be a venturi tube, jet, nozzle, ejector, eductor, injector or the like.

Referring to Figure 2, an enlarged view of jet or nozzle type device 15 is shown. In

this embodiment, liquid is forced through a jet 16 having a surrounding air passage 17 to

produce a gas entrained liquid flow 18. Such a device allows the independent control of

gas and liquid medium by adjusting respective supply valves.

The liquid commonly used to entrain the gas is the feed water, wastewater or mixed

liquor to be filtered. Pumping such an operating liquid through a venturi or the like creates

a vacuum to suck the gas into the liquid, or reduces the gas discharge pressure when a

blower is used. By providing the gas in a flow of the liquid, the possibility of blockage of

the distribution apertures 10 is substantially reduced.

The present invention at least in its preferred embodiments may provide a number of

advantages which may be summarised as follows:

1. By using a venturi device or the like it is possible to generate gas bubbles to scrub

membrane surfaces without the need for a pressurised gas supply such as a blower. When a motive fluid passes through a venturi it generates a vacuum to draw the gas into the

liquid flow and generate gas bubbles therein. Even if a blower is still required, the use of

the above process reduces the discharge pressure of the blower and therefore lowers the

cost of operation.

2. The liquid and gas phases are well mixed in the venturi and then diffuse into the

membrane module to scrub the membranes. Where a jet type device is used to forcibly

mix the gas into the liquid medium, an additional advantage is provided in that a higher

velocity of bubble stream is produced. In treatment of wastewater, such thorough mixing

provides excellent oxygen transfer when the gas used is air or oxygen. If the gas is directly

injected into a pipe filled with a liquid, it is possible that the gas will form a stagnant gas

layer on the pipe wall and therefore gas and liquid will bypass into different parts of a

module, resulting in poor cleaning efficiency.

3. The flow of gas bubbles is enhanced by the liquid flow along the membrane resulting

in a large scrubbing shear force being generated. This method of delivery of gas/liquid

provides a positive fluid transfer and aeration with the ability to independently adjust flow

rates of gas and liquid.

4. The injection of a mixture of two-phase fluid (gas/liquid) into the holes of the air

distribution device can eliminate the formation of dehydrated solids and therefore prevent

the gradual blockage of the holes by such dehydrated solids.

5. The injection arrangement further provides an efficient cleaning mechanism for

introducing cleaning chemicals effectively into the depths of the module while providing

scouring energy to enhance chemical cleaning. This arrangement, in combination with the

high packing density obtainable with the module configuration described, enables the

fibres to be effectively cleaned with a minimal amount of chemicals. 6. The module configuration described allows a higher fibre packing density in a

module without significantly increasing solid packing. This adds an additional flexibility

that the membrane modules can be either integrated into the aerobic basin or arranged in a

separate tank. In the latter arrangement, the advantage is a significant saving on chemical

usage due to the small chemical holding in the tank and in labor costs because the chemical

cleaning process can be automated. The reduction in chemicals used is also important

because the chemicals, which may be fed back to the bio process, are still aggressive

oxidisers and therefore can have a deleterious effect on bio process. Accordingly, any

reduction in the chemical load present in the bio-process provides significant advantages.

7. The positive injection of a mixture of gas and liquid feed to each membrane module

provides a uniform distribution of process fluid around membranes and therefore

minimises the feed concentration polarisation during filtration. The concentration

polarisation is greater in a large-scale system and for the process feed containing large

amounts of suspended solids. The prior art systems have poor uniformity because the

process fluid often enters one end of the tank and concentrates as it moves across the

modules. The result is that some modules deal with much higher concentrations than

others resulting in inefficient operation.

8. The filtration efficiency is enhanced due to a reduced filtration resistance. The feed

side resistance is decreased due to a reduced transverse flow passage to the membrane

surfaces and the turbulence generated by the gas bubbles and the two-phase flow.

9. Such a cleaning method can be used to the treatment of drinking water, wastewater

and the related processes by membranes. The filtration process can be driven by suction or

pressurisation.

Referring to Figures 3 to 5, embodiments of various partitioning arrangements are shown. Again these embodiments are illustrated with respect to cylindrical tubular or fibre

membrane bundles 20, however, it will be appreciated that the invention is not limited to

such applications.

Figure 3 shows a bundle of tubular membranes 20 partitioned vertically into several

thin slices 21 by a number of parallel partition spaces 22. This partitioning of the bundle

enables accumulated solids to be removed more easily without significant loss of packing

density. Such partitioning can be achieved during the potting process to form complete

partitions or partial partitions. Another method of forming a partitioned module is to pot

several small tubular membrane bundles 23 into each module as shown in Figure 4.

Another improved configuration of membrane module is illustrated in Figure 5. The

central membrane-free zone forms a passage 24 to allow for more air and liquid injection.

The gas bubbles and liquid then travel along the tubular membranes 20 and pass out

through arrays of fibres at the top potted head 8, scouring and removing solids from

membrane walls. A single gas or a mixture of gas/liquid can be injected into the module.

Figure 6 illustrates yet a further embodiment similar to Figure 5 but with single

central hole 30 in the lower pot 7 for admission of the cleaning liquid/gas mixture to the

fibre membranes 20. In this embodiment, the fibres are spread adjacent the hole 30 and

converge in discrete bundles 23 toward the top pot 8. The large central hole 30 has been

found to provide greater liquid flow around the fibres and thus improved cleaning

efficiency.

Figures 7 and 8 show further embodiments of the invention having a similar

membrane configuration to that of Figure 6 and jet mixing system similar to that of the

embodiment of Figure 2. The use of a single central hole 30 allows filtrate to drawn off

from the fibres 20 at both ends as shown in Figure 8. Referring to Figures 9 and 10 of the drawings, the module 45 comprises a plurality of

hollow fibre membrane bundles 46 mounted in and extending between an upper 47 and

lower potting head 8. The potting heads 47 and 48 are mounted in respective potting

sleeves 49 and 50 for attachment to appropriate manifolding (not shown). The fibre

bundles 46 are surrounded by a screen 51 to prevent excessive movement between the

fibres.

As shown in Figure 9, the lower potting head 48 is provided with a number of

parallel arranged slot type aeration holes 52. The fibre membranes 53 are potted in bundles

46 to form a partitioned arrangement having spaces 54 extending transverse of the fibre

bundles. The aeration holes 52 are positioned to generally coincide with the partition

spaces, though there is generally a number of aeration holes associated with each space.

The lower potting sleeve 50 forms a cavity 55 below the lower pot 48. A gas or a

mixture of liquid and gas is injected into this cavity 55 by a jet assembly 57 (described

earlier) before passing through the holes 52 into the membrane array.

In use, the use of partitioning enables a high energy flow of scouring gas and liquid

mixture, particularly near the pot ends of the fibre bundles, which assist with removal of

buildup of accumulated solids around the membrane fibres.

Air is preferably introduced into the module continuously to provide oxygen for

microorganism activities and to continuously scour the membranes. Alternatively, in some

applications, pure oxygen or other gas mixtures may be used instead of air. The clean

filtrate is drawn out of the membranes by a suction pump attached to the membrane lumens

which pass through the upper pot as described in our earlier aforementioned application.

Preferably, the membrane module is operated under low transmembrane pressure

(TMP) conditions because of the high concentration of suspended solids (MLSS) present in the reactor.

The membrane bioreactor is preferably combined with an anaerobic process which

assists with further removal of nutrients from the feed sewage.

It has been found that the module system employed is more tolerant of high MLSS

than many present systems and the efficient air scrub and back wash (when used) assists

efficient operation and performance of the bioreactor module.

It will be appreciated that, although the invention and embodiments have been

described in relation to an application to bioreactors and like systems, the invention may be

equally applicable to other types of application.

It will be appreciated that the invention is not limited to the specific embodiments

described and other embodiments and exemplifications of the invention are possible

without departing from the sprit or scope of the invention.

Claims

CLAIMS:

1. A method of scrubbing a membrane surface using a liquid medium with gas bubbles

entrained therein, including the steps of entraining said gas bubbles into said liquid

medium by flow of said liquid medium past a source of gas, and flowing said gas bubbles

and liquid medium along said membrane surface to dislodge fouling materials therefrom.

2. A method according to claim 1 wherein the gas bubbles are entrained into said liquid

flow by means of a venturi device.

3. A method according to claim 1 wherein the gas bubbles are entrained or injected into

said liquid flow by means of devices which forcibly mix gas into a liquid flow to produce a

mixture of liquid and bubbles.

4. A method according to claim 1, 2 or 3 wherein the gas includes air, oxygen, gaseous

chlorine, ozone or any combination thereof.

5. A membrane module comprising a plurality of porous membranes, said membranes

being arranged in close proximity to one another and mounted to prevent excessive

movement therebetween, and means for providing, from within the module, by means

other than gas passing through the pores of said membranes, gas bubbles entrained in a

liquid flow such that, in use, said liquid and bubbles entrained therein move past the

surfaces of said membranes to dislodge fouling materials therefrom, said gas bubbles being

entrained in said liquid by flowing said liquid past a source of gas to draw the gas into said

liquid flow.

6. A membrane module according to claim 5 wherein said liquid and bubbles are mixed

and then flowed past membranes to dislodge the fouling materials.

7. A method of removing fouling materials from the surface of a plurality of porous

hollow fibre membranes mounted and extending longitudinally in an array to form a membrane module, said membranes being arranged in close proximity to one another and

mounted to prevent excessive movement therebetween, the method comprising the steps of

providing, from within said array, by means other than gas passing through the pores of

said membranes, uniformly distributed gas bubbles entrained in a liquid flow, said gas

bubbles being entrained in said liquid flow by flowing said liquid past a source of gas so as

to cause said gas to be drawn and/or mixed into said liquid, said distribution being such

that said bubbles pass substantially uniformly between each membrane in said array to, in

combination with said liquid flow, scour the surface of said membranes and remove

accumulated solids from within the membrane module.

8. A method according to claim 7 wherein said bubbles are injected and mixed into said

liquid flow.

9. A method according to claim 7 or claim 8 wherein the membranes comprise porous

hollow fibres, the fibres being fixed at each end in a header, at least one header having one

or more holes formed therein through which gas/liquid flow is introduced.

10. A membrane module comprising a plurality of porous hollow fibre membranes, said

fibre membranes being arranged in close proximity to one another and mounted to prevent

excessive movement therebetween, the fibre membranes being fixed at each end in a

header, one header having one or more of holes formed therein through which gas/liquid

flow is introduced, and partition means extending at least part way between said headers to

partition said membrane fibres into groups.

11. A module according to claim 10 wherein the partition means are formed by a spacing

between respective fibre groups.

12. A module according to claim 11 wherein the fibre membranes are arranged in

cylindrical arrays and the partitions extend radially from the centre of the array or are positioned concentrically within the cylindrical array.

13. A membrane module comprising a plurality of porous hollow fibre membranes, said

fibre membranes being arranged in close proximity to one another to form a bundle and

mounted to prevent excessive movement therebetween, the fibre membranes being fixed at

each end in a header, one header having one or more of holes formed therein through

which gas/liquid flow is introduced, and the fibre bundle having a central longitudinal

passage extending the length of the bundle between the headers.

14. A membrane module for use in a membrane bioreactor including a plurality of

porous hollow membrane fibres extending longitudinally between and mounted at each end

to a respective potting head, said membrane fibres being arranged in close proximity to one

another and mounted to prevent excessive movement therebetween, said fibres being

partitioned into a number of bundles at least at or adjacent to their respective potting head

so as to form a space therebetween, one of said potting heads having an array of aeration

openings formed therein for providing gas bubbles within said module such that, in use,

said bubbles move past the surfaces of said membrane fibres to dislodge fouling materials

therefrom.

15. A membrane module according to claim 14 wherein said aeration openings are

positioned to coincide with the spaces formed between said partitioned bundles.

16 A membrane module according to claim 15 wherein said openings comprise a slot,

slots or a row of holes and fibre bundles are located in the potting head between the slots or

rows of holes.

17. A membrane module according to claim 10, claim 13 or claim 14 wherein the fibres

within the module have a packing density of between about 5 to about 10%.

18. A membrane module according to claim 10, claim 13 or claim 14 wherein the fibres within the module have a packing density of between about 8 to about 55%.

19. A membrane module according to claim 16 wherein said holes have a diameter or an

equivalent diameter in the range of about 1 to 40 mm.

20. A membrane module according to claim 16 wherein said holes have a diameter or an

equivalent diameter in the range of about 1.5 to about 25 mm.

21. A membrane module according to claim 10, claim 13 or claim 14 wherein an inner

diameter of each said fibre is in the range from about 0.1 mm to about 5 mm.

22. A membrane module according to claim 10, claim 13 or claim 14 wherein an inner

diameter of each said fibre is in the range of about 0.25 mm to about 2 mm.

23. A membrane module according to claim 10, claim 13 or claim 14 wherein a wall

thickness of each said fibre is between about 0.05 to about 2 mm.

24. A membrane module according to claim 10, claim 13 or claim 14 wherein a wall

thickness of each said fibre is between about 0.1 mm to about 1 mm.

25. A membrane bioreactor including a tank having means for the introduction of feed

thereto, means for forming activated sludge within said tank, a membrane module

according to claim 10, claim 13 or claim 14 positioned within said tank so as to be

immersed in said sludge and said membrane module provided with means for withdrawing

filtrate from at least one end of said fibre membranes.

26. A method of operating a membrane bioreactor of the type according to claim 14

comprising introducing feed to said tank, applying a vacuum to said fibres to withdraw

filtrate therefrom while periodically or continuously supplying gas bubbles through said

aeration openings to within said module such that, in use, said bubbles move past the

surfaces of said membrane fibres to dislodge fouling materials therefrom.

27. A method according to claim 26 wherein the gas bubbles are entrained or mixed with a liquid flow when fed through said holes or slots.

28. A membrane module according to claim 25 wherein the membrane module is

suspended vertically within the tank and a further source of aeration is provided beneath

the suspended module.

29. A membrane module according to claim 28 wherein the further source of aeration

comprises a group of air permeable tubes or gas distributors.

30. A membrane module substantially as hereinbefore described with reference to any

one of the described embodiments and its associated drawings.

31. A method of scrubbing a membrane surface substantially as hereinbefore described

with reference to any one of the described embodiments and its associated drawings.