WO1998009718A1 - Systeme de filtration modulaire - Google Patents

Systeme de filtration modulaire Download PDF

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Publication number
WO1998009718A1
WO1998009718A1 PCT/US1997/015181 US9715181W WO9809718A1 WO 1998009718 A1 WO1998009718 A1 WO 1998009718A1 US 9715181 W US9715181 W US 9715181W WO 9809718 A1 WO9809718 A1 WO 9809718A1
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WO
WIPO (PCT)
Prior art keywords
fluid
depth
permeate
filter
disposing
Prior art date
Application number
PCT/US1997/015181
Other languages
English (en)
Other versions
WO1998009718A9 (fr
Inventor
Dennis Chancellor
Mark Chancellor
Jacquetta Vogel
Original Assignee
Nate International
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Nate International filed Critical Nate International
Priority to AU42393/97A priority Critical patent/AU717474B2/en
Priority to IL12862197A priority patent/IL128621A/en
Priority to UA99031345A priority patent/UA61925C2/uk
Priority to EP97940671A priority patent/EP0930931A4/fr
Priority to JP51274998A priority patent/JP3522768B2/ja
Priority to CA002264853A priority patent/CA2264853C/fr
Priority to ZA981743A priority patent/ZA981743B/xx
Publication of WO1998009718A1 publication Critical patent/WO1998009718A1/fr
Publication of WO1998009718A9 publication Critical patent/WO1998009718A9/fr
Priority to NO19991014A priority patent/NO991014L/no

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D36/00—Filter circuits or combinations of filters with other separating devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F16—ENGINEERING ELEMENTS AND UNITS; GENERAL MEASURES FOR PRODUCING AND MAINTAINING EFFECTIVE FUNCTIONING OF MACHINES OR INSTALLATIONS; THERMAL INSULATION IN GENERAL
    • F16L—PIPES; JOINTS OR FITTINGS FOR PIPES; SUPPORTS FOR PIPES, CABLES OR PROTECTIVE TUBING; MEANS FOR THERMAL INSULATION IN GENERAL
    • F16L9/00—Rigid pipes
    • F16L9/006—Rigid pipes specially profiled
    • 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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/06—Energy recovery
    • 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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/08—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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/10—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
    • B01D63/10—Spiral-wound membrane modules
    • B01D63/12—Spiral-wound membrane modules comprising multiple spiral-wound 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
    • B01D63/14—Pleat-type membrane 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
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D13/00—Pumping installations or systems
    • F04D13/12—Combinations of two or more pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/02—Forward flushing
    • 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
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone

Definitions

  • the present invention relates generally to filtration of fluids, including especially filtration of water.
  • membrane refers to a functional filtering unit, and may include one or more semi-permeable layers and one or more support layers.
  • reverse osmosis can remove particles varying in size from the macro-molecular to the microscopic, and modern reverse osmosis units are capable of removing particles, bacteria, spores, viruses and even ions such as Cl' or Ca ++ .
  • RO reverse osmosis
  • the design is impractical.
  • the Chenoweth design teaches a central riser surrounded at many different depths by clusters of five satellite RO units.
  • Each of the satellite units has its own collector, and the various collectors of each cluster flow together at a manifold into the central riser.
  • Such a design is inherently inefficient.
  • Clustering of satellite RO units adds unnecessary complexity and expense, and the presence of multiple satellite casings on the same level wastes precious channel volume.
  • apparatus and methods are provided in which the head pressure developed by the weight of a fluid is used to drive a plurality of filters to produce a permeate, and in at least some level (i.e. at some depth) within the apparatus at least 30% of the permeate produced is collected within a single filter casing.
  • the inventive subject matter can thereby reduce or eliminate clustering in channel-based and other filtration systems, and thus provide for improved efficiency and cost effectiveness.
  • substantially all of the filter material at a given depth is wrapped about one or more permeate collectors within a single filter casing.
  • the filters and lengths of collector tube(s) form the inner cores of a series of production modules.
  • each of the production modules further includes a transport zone for transporting brine and a transport zone for transporting permeate.
  • the ends of adjacent production modules may be designed to mate with one another using a slip fit joint, and the production modules may be maintained in mating relationship through connections to supporting cables or rods.
  • a submerged pump may be used to raise permeate towards the surface.
  • the pump can operate at least using centrifugal and/or air lift principles, and where an air lift principle is used an energy recovery system can be employed to recover energy from the rising fluid and gas. It is also contemplated to employ a gas produced via electrolysis to assist in the pumping.
  • feed fluid can be provided from a salty or brackish water source such as an ocean or bay using pipes having removable inlet plugs which resist clogging. It is also contemplated that such pipes can be laid using an underwater sled which digs a trench while concurrently laying the pipe.
  • Figure 1 is a schematic of a reverse osmosis system.
  • Figure 2 is a schematic of a production module.
  • Figure 3 is a perspective schematic of a production module.
  • Figure 4 is a vertical cross-section of the production module of Figure 3 at 4-4.
  • Figure 5 is a vertical cross-section of the production module of Figure 3 at 5-5
  • Figure 6 is a perspective drawing of a transition assembly being installed or removed.
  • Figure 7 is a perspective drawing of a portable lifting tool.
  • Figure 8 A is a schematic of a wrapped filter subassembly.
  • Figure 8B is a schematic of an unwrapped filter subassembly.
  • Figure 8C is a more detailed schematic of a portion of the unwrapped filter subassembly of Figure 8B.
  • Figure 8D is a schematic of an alternative filter subassembly in which the filter material is depicted in a folded configuration.
  • Figure 8E is a schematic of another alternative filter subassembly.
  • a filtration system 10 generally comprises a headworks 1 1, a plurality of transition modules 60, a pump module 50, a plurality of production modules 40, and cables 23 which support the various modules.
  • the headworks 11 and various modules 60, 50, 0 all cooperate to provide a feed liquid flowpath 18, a permeate flowpath 18 A and a flushing liquid flowpath 19.
  • the various modules of system 10 may be contained in a well or other channel (not shown), or may be situated in an open ocean or other body of water (not shown).
  • one of the flowpaths 18, 18A or 19 can advantageously be formed as an annular space between the outer casings of the modules 60, 50, 40 and the lining 20 of the channel.
  • the feed liquid and flushing liquid flowpaths, 18 and 19, respectively can comprise the open body of liquid.
  • channel is used generically to mean a space having a relatively deep and relatively narrow portion which can contain a fluid.
  • a channel As used herein, the term "channel" is used generically to mean a space having a relatively deep and relatively narrow portion which can contain a fluid.
  • an ocean, bay, lake or other large body of water cannot be considered a channel as the term is used herein because such bodies are broad relative to their depth.
  • a water or oil well, or an underground chamber connected via a passageway would all be considered channels as the term is used herein.
  • the lining of the channel is not especially important, and suitable channels may have the conventional steel, cast iron, concrete or other casings, or they may have no casing at all.
  • a channel employed according to the present invention may be located near the ocean or other salty or brackish body of water to provide a convenient source of water. In such cases the channel can descend from a point in the body of water or from a point on the land. In other instances an appropriate channel may be utilized which is many kilometers from a source of water. Appropriate channels may even be inclined rather than vertically oriented. In short, apparatus and methods as described herein may be utilized in conjunction with many different types of channels, regardless of their original purpose, shape, orientation, and location.
  • feed liquid which may, for example, comprise salt water or brine
  • feed liquid supply 12 is fed into the system 10 via feed liquid supply 12, while waste liquid is expelled at flushing liquid discharge 14, and purified liquid (permeate) is expelled at permeate discharge 13.
  • Feed liquid supply 12, permeate discharge 13 and flushing liquid discharge 14 may be welded or otherwise secured to head works 11.
  • the system 10 can be pressurized to approximately 3 bars by feed liquid pump 56. This helps overcome friction losses in feed liquid flowpath 18, head losses through the production assemblies 40, and friction losses in flushing liquid flowpath 19.
  • a pre-filtration system 57 may optionally be employed as appropriate, depending on the paniculate concentration in the feed liquid.
  • a receiving tank 58 may also be utilized to receive permeate.
  • Transition modules 60 are primarily designed to provide conduits between the headworks 11 and the pump module 50. Transition modules 60 can therefore be quite simple in design, such as a pipe within a pipe (not shown), or one or more collector tubes disposed in a side-by-side configuration (not shown).
  • Pump module 50 generally comprises a centrifugal or other pump 53 which raises permeate from the production modules 40 the headworks 11. Pump 53 is most likely operated electrically, and electrical energy can be brought to the pump using a power cable
  • Pump 53 may comprise an air lift pump or some composite pump which utilizes an air lift principle. In such circumstances the gas employed could be compressed at the surface and transported to the pump using a high pressure gas line, or at least some of the gas could be produced at or near the pump through electrolysis.
  • the system 10 may include multiple pump modules (not shown), or a single pump module may contain more than one pump. It is advantageous to provide a means of raising and lowering pump 53 without dismantling the transition modules 60, and this may be accomplished using pump installation cables 51.
  • pump 53 may be employed to reduce net positive suction to about one bar, and to discharge permeate into permeate flowpath 18 A at between 60 and 70 bars.
  • the actual discharge pressure is at least partially a function of the depth below the surface at which pump 53 is mounted and the salinity of the feed liquid.
  • Production modules 40 generally comprise an intake subassembly 70 and a plurality of adjacent filtering subassemblies 30.
  • the intake subassembly 70 directs feed liquid from the feed liquid flowpath 18 into the uppermost or lowermost filtering subassembly 30, and directs flushing liquid away from the filters 35 contained within the filtering subassemblies 30.
  • the filtering subassembly 30 contains one or more filters 35 which separate feed liquid into permeate and flushing liquid.
  • production modules can be placed at depths of at least about 50 meters. Such a depth is sufficient to perform reverse osmosis on brackish water using currently available membranes, and it is expected that as membrane technology improves, production modules will perform well at depths of less than 50 meters.
  • systems will employ filters at a great range of depths, including depths of at least 100 meters, at least 250 meters, at least 350 meters, at least 500 meters, at least 750 meters, and at least 1000 meters.
  • Cables 23 are employed to hold the various modules 60, 50, 40 together, and to support their weight. As described below in greater detail with respect to Figure 5, cables 23 can be replaced with bars (not shown), rods (not shown), straps (not shown), or other supports, and alternatively can be eliminated altogether by employing other supporting and connecting means between adjacent modules.
  • Modules 60, 50 and 40 may be constructed in virtually any workable sizes and shapes, using virtually any suitable materials, and not all of the modules need have the same structural or compositional characteristics.
  • transition modules 60, permeate pump assembly 50, and production modules 40 will be substantially tubular, and will be constructed primarily of suitable materials.
  • construction materials such as PVC, epoxy fiberglass, stainless or other steels may be used. Still other construction materials may include new composites or materials not yet developed.
  • production modules 40 would generally be joined or otherwise juxtaposed end to end with other production modules 40 to form a chain.
  • One or more pump modules 50 would be placed on top of the uppermost production module, and transition modules 60 would be added above the pump module(s) to reach the headworks 11.
  • the assemblies would be lowered into an open area or channel to the required depth using an apparatus such as that depicted in Figures 6 or 7.
  • the various modules are preferably coupled using slip fit couplings.
  • two or more of the modules may be coupled by other means, including threaded connections, clamps, bolts, and glues.
  • systems according to the inventive subject matter may be associated with some sort of support facility, which may include one or more buildings, pump houses and so forth. While not explicitly shown, it is anticipated that the feed fluid may be pre-filtered, and such pre-filtering may occur at any point upstream of the feed liquid supply 12 passing into the production assemblies 40.
  • the ability to pre-filter salt water extracted from a body of water such as a bay or ocean may be relatively important in terms of long-term protection of the filter material, and may render apparatus and methods according to the present subject superior to that of merely placing the filters in the open ocean, and either relying upon the natural water currents or pumping water past the filters to achieve adequate flushing.
  • a production module 40 generally comprises one or more filter subassemblies 30 and a single transition subassembly 70.
  • Each filter subassembly 30 comprises an outer shell 31, an annular space 19A, and one or more filter subassemblies 44.
  • each filter subassembly 44 may advantageously comprise one or more filter casings 32, each of which may house a plurality of filter leaves 35 and spacers 41 coupled to a collector tube 33.
  • Figure 2 shows a plurality of intake holes ports 74 in intake subassembly 70 contains which communicate fluid from feed liquid flowpath 18 through spokes 77, and into filter feed area 78.
  • Figure 2 also details a possible coupling 22 between cable 23 and production module 40.
  • the coupling can take place at any point or points along the production modules 40, but it is preferred that such coupling will take place near the top and near the bottom of production assemblies 40.
  • production modules there are many alternative configurations of production modules, which, though not shown in the present drawings, are consistent with the inventive concepts herein.
  • the fluid transport annulus in the production modules 40 it is not necessary for the fluid transport annulus in the production modules 40 to be annular, and it is not even necessary for the production modules 40 to include a fluid transport zone.
  • the feed liquid can be transported in a space between the production modules and the channel lining, and it would also be possible to transport feed liquid or permeate in a separate pipe or compartment external to the production modules.
  • the filter leaves 35, spacers 41 and collector tube(s) may be disposed differently from that shown here.
  • a preferred arrangement includes three filter subassemblies 30 bracketed by single transition subassemblies 70. It should, however, be appreciated that a greater or lesser number of filter subassemblies 30 could be located between transition subassemblies
  • a filtering system utilized in desalinization of salt water would have five series mounted filter subassemblies 30 located between transition subassemblies 70, each filter subassembly 30 being approximately six meters long. The number five is contemplated to be particularly advantageous because it is thought to properly balance flux (flush) rate against pressure drop and recovery rate.
  • Figures 4 and 5 arrows are used to indicate possible flow directions of feed liquid. In the particular embodiment show, feed liquid flows downward along flowpath 18, through intake ports 74, along spokes 77, and into filter feed area 78. The feed liquid then flows downward through spacers 41 (see Figure 8C), where it is divided by the filter material 45 into separate streams of permeate and flushing liquids.
  • Permeate then passes through collector holes 34 and into collector tube 33, from which it flows upwards toward permeate pump 53.
  • the flushing liquid continues to flow downwards through the spacers 41 of one or more filter subassemblies 44, until it reaches collection space 79 located within the next lower transition subassembly 70.
  • the flushing liquid then leaves the transition subassembly 70 and passes upward through successive overhead production modules 40, pump module 50 (not shown), and transition modules 60 (not shown) into the headworks (not shown).
  • an upper transition module 60U is being coupled or decoupled from a lower transition module 60L.
  • each transition module 60U is being coupled or decoupled from a lower transition module 60L.
  • 60L has an outer pipe 61 and an inner pipe 62.
  • the outer pipes 61 are coupled through slip fit coupling 61 A
  • the inner pipes 62 are coupled through slip fit coupling 62 A.
  • ring seals 61 A and 62B are used to seal pipes 61 and 62 respectively.
  • optional guiding ribs or spokes may be advantageously deployed in the various annular spaces, such as between pipes 61 and 62, and between pipe 61 and channel lining 20.
  • the couplings depicted in Figure 6 are exemplary only, and other types of couplings and connecting strategies are contemplated as well.
  • cable 23 comprises upper cable terminal 27, lifting point 28, resting point 29 and lower cable terminal 26.
  • Connecting pins 27A are used to secure the coupling between adjacent cables 23, and cable clamps 25 are used to couple the cables 23 to the modules 60.
  • each cable is only as long as the module 60 in this particular embodiment, each cable can be longer or shorter than a corresponding module, and a single cable may run the entire length of the system 10.
  • the cable clamps 25 depicted are different in design from the cable clamps 22 of Figures 2 and 3, and that other types of cable clamping or arresting means are contemplated as well.
  • Lifting assembly 80 can be used to assemble or disassemble system 10. There are many possible configurations here, including the assembly 80 shown comprising telescoping support 82 and rams 81.
  • FIG. 7 depicts a portable mechanical lifting assembly 90 including a telescoping support 92 and rams 91. Also depicted is a lifting harness 95, which is employed to pin upper cable terminal 27 and raise or lower any of modules 60, 50 or 40. Lifting assembly 90 can be controlled by any convenient controller, including transportable control panel 94.
  • two or more discrete filters are folded and glued into filter leaves 35, and spirally wrapped about collector tube 33, along with interspacing spacers 41.
  • This design produces high pressure sides and low pressure sides of the filter leaves 35. It should be appreciated that it is not necessary to have more than one filter leave 35 disposed about collector tube 33, and it is not necessary for the disposition to comprise wrapping. In alternative embodiments, for example, it is contemplated that the filter leave(s) could be partially wrapped and/or partially folded about collector tube 33.
  • each of the filter leaves 35 comprises a layer of filter material 45 on each side of a permeate carrier material 42.
  • the permeate carrier material 42 is sealed at seal 43 and drains into collector holes 34 provided in the collector tubes 33.
  • a spacer 41 is disposed between overlapping filter leaves 35. Feed liquid not passing through the filter leaves 35 would continue to flush the high pressure side of the leaves 35, and would eventually be carried out of the system via flushing flowpath 19.
  • the filter material 45 contemplated herein includes, but is not limited to membranes used in reverse osmosis processes.
  • the inventive subject matter herein may employ materials designed to filter macro particles (100 to 1000 Micrometers), micro particles ( 1.0 to 100 Micrometers), macro molecular particles (0.1 to 1.0 Micrometers), molecular particles (0.001 to 0.1 Micrometers) or ionic particles (less than 0.001 to 0.001 micrometers).
  • Future filter developments may increase the range of filtration even further to include even smaller particles, and perhaps even molecular lysis, such as separating hydrogen from oxygen as in hydrolysis. In this manner the contemplated processes would cover the entire filtration spectrum for liquids.
  • the filtration spectrum identified above would include particle filtration, and continue through Microfiltration, Ultrafiltration, Nanofiltration and Hyperfiltration (Reverse Osmosis).
  • a single outer shell 31 could contain multiple filter casings 32.
  • multiple collectors 33 can be employed while still maintaining efficient use of the space inside filter casing 32, and such an embodiment satisfies the limitation that in at least some level within the apparatus at least 30% of the permeate produced is collected within single filter subassemblies 30 at any given level. In other preferred embodiments 40%, 60% and up to substantially all of the permeate produced is collected from within single filter subassemblies 30 suspended at any given depth.
  • 33 A could be positioned in other than a central position (as in Figures 8D and 8E) , or that the collector could be positioned completely outside the filter subassembly.
  • one or more collectors could be positioned inside the production assembly 40, and permeate could flow from the collector(s) into an external section comprising a new annulus (not shown).
  • the critical limitation is that in at least some level within the apparatus more than a 30% of the permeate produced at a given depth is collected within single filter subassembly 30.
  • the invention is not limited to the embodiments expressly shown and described. In alternative embodiments, for example, any of the liquid flows could operate in reverse to that described herein.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Nanotechnology (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Cyclones (AREA)
  • Filtration Of Liquid (AREA)

Abstract

On utilise le poids d'un fluide pour produire un perméat par l'intermédiaire d'une pluralité de membranes semi-perméables ou d'autres matériaux filtrants et, dans un étage au moins de l'appareil, on récupère plus de 30 % du perméat produit à l'intérieur d'un caisson (32). Dans une réalisation, le matériau filtrant est au moins partiellement contenu à l'intérieur de modules (40) de production en série qui peuvent comporter des zones de transport pour le transport de matière d'alimentation ou de fluide de rinçage. Dans une autre réalisation, les extrémités de modules de production adjacents peuvent être conçus pour s'accoupler l'un à l'autre par ajustement glissant, et les modules de production peuvent être maintenus en relation d'accouplement par l'intermédiaire de connexions avec les câbles ou tiges de support (23). Dans une autre réalisation, il est possible d'utiliser une pompe immergée (53) pour faire remonter le perméat à la surface, ladite pompe pouvant avantageusement mettre en oeuvre au moins partiellement une force centrifuge et/ou un principe de pompage par émulsion. Dans d'autres réalisations, le fluide d'alimentation peut provenir d'une source d'eau salée ou saumâtre telle que l'océan ou un réservoir par l'intermédiaire de tuyaux pourvus de bouchons d'entrée amovibles qui résistent au colmatage, et l'on envisage de poser ces tuyaux au moyen d'un traîneau sous-marin capable simultanément de creuser une tranchée et de poser un tuyau.
PCT/US1997/015181 1996-09-03 1997-08-28 Systeme de filtration modulaire WO1998009718A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
AU42393/97A AU717474B2 (en) 1996-09-03 1997-08-28 Modular filtration system
IL12862197A IL128621A (en) 1996-09-03 1997-08-28 Modular filtration system
UA99031345A UA61925C2 (en) 1996-09-03 1997-08-28 Method for liquid purification
EP97940671A EP0930931A4 (fr) 1996-09-03 1997-08-28 Systeme de filtration modulaire
JP51274998A JP3522768B2 (ja) 1996-09-03 1997-08-28 モジュール式濾過システム
CA002264853A CA2264853C (fr) 1996-09-03 1997-08-28 Systeme de filtration modulaire
ZA981743A ZA981743B (en) 1997-08-28 1998-03-02 Modular filtration system
NO19991014A NO991014L (no) 1996-09-03 1999-03-02 Filtreringssystem oppbygget av moduler

Applications Claiming Priority (24)

Application Number Priority Date Filing Date Title
US70824996A 1996-09-03 1996-09-03
US08/708,249 1996-09-03
US72286896A 1996-09-26 1996-09-26
US08/722,868 1996-09-26
US3334296P 1996-11-21 1996-11-21
US3286396P 1996-11-21 1996-11-21
US3334396P 1996-11-21 1996-11-21
US60/033,343 1996-11-21
US60/032,863 1996-11-21
US60/033,342 1996-11-21
US3673997P 1997-01-27 1997-01-27
US3674097P 1997-01-27 1997-01-27
US60/036,739 1997-01-27
US60/036,740 1997-01-27
US83491697A 1997-04-07 1997-04-07
US08/834,916 1997-04-07
US4300197P 1997-04-14 1997-04-14
US60/043,001 1997-04-14
US4418997P 1997-04-25 1997-04-25
US60/044,189 1997-04-25
US5122397P 1997-06-30 1997-06-30
US5119297P 1997-06-30 1997-06-30
US60/051,192 1997-06-30
US60/051,223 1997-06-30

Publications (2)

Publication Number Publication Date
WO1998009718A1 true WO1998009718A1 (fr) 1998-03-12
WO1998009718A9 WO1998009718A9 (fr) 1998-07-30

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Family Applications (1)

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PCT/US1997/015181 WO1998009718A1 (fr) 1996-09-03 1997-08-28 Systeme de filtration modulaire

Country Status (10)

Country Link
EP (1) EP0930931A4 (fr)
JP (1) JP3522768B2 (fr)
KR (2) KR100422891B1 (fr)
CN (1) CN1233972A (fr)
AU (1) AU717474B2 (fr)
CA (1) CA2264853C (fr)
IL (1) IL128621A (fr)
MX (1) MX212477B (fr)
NO (1) NO991014L (fr)
WO (1) WO1998009718A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
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WO1999043421A1 (fr) * 1998-02-27 1999-09-02 Nate International Ensembles grands tubes utiles pour une osmose inverse
EP0983115A1 (fr) * 1997-04-14 2000-03-08 Nate International Systemes de filtration modulaires et procedes
WO2000072949A1 (fr) * 1999-05-27 2000-12-07 Nate International Filtration utilisant un recipient sous pression avec canaux de filtration multiples

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JP5037460B2 (ja) * 2007-09-21 2012-09-26 旭化成ケミカルズ株式会社 ヘッダ部品及び濾過装置
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KR101666718B1 (ko) * 2014-09-16 2016-10-14 임운영 해수담수화 장치 및 해수담수화 방법
FR3049196B1 (fr) * 2016-03-23 2018-03-30 Veolia Water Solutions & Technologies Support Dispositif de filtration membranaire de liquide sous pression.
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Publication number Priority date Publication date Assignee Title
EP0983115A1 (fr) * 1997-04-14 2000-03-08 Nate International Systemes de filtration modulaires et procedes
EP0983115B1 (fr) * 1997-04-14 2003-09-10 Nate International Systemes de filtration modulaires
WO1999043421A1 (fr) * 1998-02-27 1999-09-02 Nate International Ensembles grands tubes utiles pour une osmose inverse
AU741395B2 (en) * 1998-02-27 2001-11-29 Nate International Large tube assemblies for reverse osmosis
US6547965B1 (en) * 1998-02-27 2003-04-15 Nate International Large tube assemblies for reverse osmosis
WO2000072949A1 (fr) * 1999-05-27 2000-12-07 Nate International Filtration utilisant un recipient sous pression avec canaux de filtration multiples

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NO991014D0 (no) 1999-03-02
MX9901941A (en) 2000-03-31
IL128621A0 (en) 2000-01-31
IL128621A (en) 2002-02-10
AU4239397A (en) 1998-03-26
NO991014L (no) 1999-04-30
JP3522768B2 (ja) 2004-04-26
CN1233972A (zh) 1999-11-03
KR20010029459A (ko) 2001-04-06
CA2264853A1 (fr) 1998-03-12
MX212477B (en) 2003-01-09
CA2264853C (fr) 2003-08-05
EP0930931A4 (fr) 2000-07-12
AU717474B2 (en) 2000-03-30
KR20010106362A (ko) 2001-11-29
KR100422891B1 (ko) 2004-03-12
EP0930931A1 (fr) 1999-07-28
JP2002504012A (ja) 2002-02-05

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