WO2000072949A1 - Filtration utilisant un recipient sous pression avec canaux de filtration multiples - Google Patents

Filtration utilisant un recipient sous pression avec canaux de filtration multiples Download PDF

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Publication number
WO2000072949A1
WO2000072949A1 PCT/US2000/003107 US0003107W WO0072949A1 WO 2000072949 A1 WO2000072949 A1 WO 2000072949A1 US 0003107 W US0003107 W US 0003107W WO 0072949 A1 WO0072949 A1 WO 0072949A1
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WO
WIPO (PCT)
Prior art keywords
filtration system
filters
inner casings
filter
disposed
Prior art date
Application number
PCT/US2000/003107
Other languages
English (en)
Inventor
Dennis Chancellor
James Jensen
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 US10/019,066 priority Critical patent/US6942797B1/en
Priority to AU32241/00A priority patent/AU3224100A/en
Publication of WO2000072949A1 publication Critical patent/WO2000072949A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • 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
    • B01D63/02—Hollow fibre modules
    • B01D63/025—Bobbin units
    • 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
    • B01D63/10—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
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/24—Specific pressurizing or depressurizing means
    • B01D2313/246—Energy recovery means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/02—Forward flushing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/20—By influencing the flow
    • B01D2321/2008—By influencing the flow statically
    • B01D2321/2016—Static mixers; Turbulence generators

Definitions

  • the present invention relates generally to filtration of fluids, including especially filtration of water.
  • filtration Aside from distillation techniques, purification of water and other fluids is commonly satisfied by filtration. There are many types of filtration, including reverse osmosis (RO), which may involve ultra-filtration or hyper-filtration. and all such technologies are referred to herein using the generic term, "filtration.”
  • RO reverse osmosis
  • Reverse osmosis involves separation of constituents under pressure using a semi- permeable membrane.
  • 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
  • FIG. 1 A more generalized schematic of a prior art filtration system employing an energy recovery turbine is shown in Figure 1.
  • a filtration system 10 generally comprises a pump 20, a plurality of parallel permeators 30, an energy recovery turbine 40. and a permeate or filtered fluid holding tank 50.
  • the fluid feed lines are straightforward, with an intake line (not shown) carrying a feed fluid from a pretreatment device (not shown) to the pump 20, a feed fluid line 22 conveying pressurized feed fluid from the pump 20 to the permeators 30, a permeate collection line 32 conveying depressurized permeate from the permeators 30 to the holding tank 50, a waste fluid collection line 34 conveying pressurized waste fluid from the permeators 30 to the energy recovery turbine 40, and a waste fluid discharge line 42 conveying depressurized waste fluid from the energy recovery turbine 40 away from the system 10.
  • a system according to Figure 1 may be relatively energy efficient, but is still somewhat complicated from a piping standpoint.
  • each permeator 30 has at least three pressure connections - one for the feed fluid, one for the waste fluid , and one for the permeate. In a large system such fluid connections may be expensive to maintain, especially where filtration elements in the permeators need to be replaced every few years.
  • US 5470469 to Eckman (Nov. 1995) describes a pressure vessel that houses one or more hollow fiber membrane cartridges.
  • the outer circumference of the membranes do not extend completely to the inner wall of the production vessel, allowing convenient replacement of the cartridges, and also providing an annular space between the outer portion of the filters and the inner wall of the production vessel that is used as part of the waste fluid flowpath.
  • the annular space is only continuous along a single cartridge, however, and is interrupted between adjacent cartridges by an annular sealing ring at one end of each cartridge.
  • WIPO publication 98/46338 discloses an improvement over Eckman in which the annular spaces between the outer portion of the membranes and the inner wall of the production vessel can be continuous past multiple modules (cartridges).
  • the improvement extends the convenient replacement benefits of the Eckman design to spiral wound filters.
  • Both US 5470469 and WIPO 98/46338 are also advantageous in that they reduce the ratio of couplings relative to the number of filters.
  • three couplings are required to provide fluid flow paths to a single membrane, one coupling for each of the feed fluid, waste fluid, and permeate flow paths. The ratio is thus 3: 1.
  • the US 5470469 and WIPO 98/46338 designs only three couplings are still required to provide fluid flow paths to multiple membranes. Thus, if the pressure vessel contains three membranes, the ratio is 3:3, and if the pressure vessel contains five membranes, the ratio is 3:5.
  • the present invention is directed to modularized filtration systems in which an elongated outer casing houses a plurality of elongated inner casings, which in turn house a plurality of filters (membranes).
  • the outer casing, inner casings, and filters are disposed relative to one another to provide a three-flow channel system that provides additional feed fluid at one or more of the membrane couplings between membranes of the same inner casing.
  • the feed fluid flow path comprises an annular space between the inner casings and the filters contained in such casings, and in more preferred embodiments the annular space is substantially continuous past multiple filters of the same inner casing.
  • the inner casings may advantageously have openings that fluidly communicate with the lumen of the outer casing, thereby reducing the ratio of couplings relative to the number of filters (the coupling/filter ratio).
  • the coupling/filter ratio ⁇ 1 :2 in more preferred embodiments the coupling/filter ratio ⁇ 1 :3, and in still more preferred embodiments the coupling/filter ratio ⁇ 1 :4.
  • Fig. 1 is a schematic of a prior art filtration system employing an energy recovery turbine.
  • Fig. 2 is a schematic of a preferred filtration system employing an energy recovery device.
  • Fig. 3 is a schematic of a filtration system employing a field of outer casings.
  • Fig. 4 is a schematic of a preferred end cap for an inner casing.
  • Fig. 5 is a cross-section of a preferred inner casing, in which waste fluid from an upstream filter is supplemented by fresh feed fluid before being fed into a downstream filter, and both waste fluid and permeate streams exit the inner casing at the same end.
  • Fig. 6 is a cross-section of an alternative preferred inner casing, in which waste fluid from an upstream filter is supplemented by fresh feed fluid before being fed into a downstream filter, and the waste fluid and permeate streams exit the inner casing at the opposite ends.
  • Fig. 7 is a cross-section of another alternative preferred inner casing, in which waste fluid from an upstream filter is supplemented by fresh feed fluid before being fed into a downstream filter, and ail three of the feed fluid, waste fluid and permeate streams enter or exit the inner casing at the same end.
  • a preferred filtration system 200 generally comprises an outer casing 210 containing multiple internal casings 220A - 220G in which filters (not shown) are disposed. and a pump/energy recovery unit 230. Feed fluid is fed to the end plate subassembly 21 1 of the outer casing 210 from feed fluid line 240, and passes into the internal casings 220A - 220G via openings 224 in the walls of the internal casings 220A - 220G.
  • the feed fluid is filtered by the filters, with permeate being removed from the internal casings 220A - 220G at end plate subassembly 212 via permeate manifold 252 and permeate line 250, and waste fluid being removed from the internal casings 220A - 220G via waste fluid line 260.
  • Arrows 241 and 242 depict fluid flow in line 240
  • arrow 261 depicts fluid flow in line 260.
  • the outer casing 210 advantageously comprises a hollow cylinder, although other elongated shapes including those having triangular, rectangular, or octagonal cross sections are also contemplated.
  • the dimensions of the outer casing 210 depend upon the rate of fluid being filtered, with larger dimensions accommodating greater production flows. Outside dimensions of commercial systems employed in purifying brine are contemplated to fall between about 0.5 meters to several meters in diameter, and between about three to forty or fifty meters in length.
  • Outer casing 210 may be fabricated from metal, plastic, composite, concrete, reinforced concrete, or any other materials that are strong enough to withstand pressure differentials produced by the pump/energy recovery unit 230, and that cannot readily be solubilized by the fluid being processed.
  • the outer casing 210 is preferably maintained above ground for easy access, but in alternative embodiments may also be placed below ground, or underwater. Horizontal, vertical, and all other possible dispositions are contemplated.
  • Each of the internal casings 220A - 220G is also contemplated to comprise an elongated shape, such as a hollow cylinder, but with the added limitation that multiple internal casings should fit within the lumen of the outer casing 210.
  • one of the fluid pathways extends through the openings 224 in the walls of the internal casings 220 A
  • the shapes of the internal casings 220 A - 220G should allow for fluid flow around the perimeters of the internal casings 220A - 220G.
  • the internal casings 220A - 220G are again preferably fabricated from metal, plastic, or composite, that is insoluble in the various fluids, but here the walls do not need to be especially strong since the openings 224 may substantially equalize the pressure differential across the walls.
  • the openings 224 are preferably dimensioned to limit the pressure inside the internal casings 220A - 220G to no more than a 20% drop relative to the pressure outside the internal casings 220A - 220G.
  • the openings 224 are positioned towards one end of each of the inner casings 220A - 220G.
  • Preferred shapes for the openings 224 are slots oriented along the long axis of the internal casings 220A
  • Contemplated filters may comprise any suitable material, including reverse osmosis membranes. Filters are preferably spiral wound, as for example, those discussed in WO
  • any other types of filters can be employed.
  • flat membrane, tubular, spiral, and/or hollow tube type filters can, for example, be deployed in a manner similar to that described in US 5,470,469 to Eckman (Nov. 1995).
  • the filters are preferably dimensioned to provide an annular space between the filters and the inside wall(s) of the inner casings 220A - 220G.
  • the term "annular” in “annular space” should be interpreted loosely, and is intended to include round spaces, oval spaces, rectangular spaces, and so forth.
  • the average thickness of the annular spaces preferably ranges from about 1 mm to about 10 cm.
  • Multiple filters are preferably serially disposed in each of the inner casings 220A - 220G. and the annular space within any given inner casing is preferably continuous across (i.e. along) the long axis of at least several consecutive filters.
  • the pump/energy recovery unit 230 forces the feed fluid in feed fluid line 240 under pressure into the outer casing 210, through the openings 224 into the lumen of the inner casings 220A - 220G, and thence to the high-pressure side of the various filters.
  • waste fluid line 260 the waste fluid line is still pressurized, and some of the energy in the pressurized waste fluid is recovered in pump/energy recovery unit 230.
  • any pump or pump system that provides adequate pumping volume and pressure may be employed in filtration system 200. This includes positive displacement pumps, impeller pumps, head pressure devices, and many others. On the other hand, some pumps and pumping systems will be more efficient than others, and such pumps and systems are particularly contemplated.
  • An especially efficient pumping system is a two stage turbine pump, in which feed fluid flows first to a relatively low-pressure turbine and then on to a relatively high-pressure turbine. It is also contemplated that the pump portion of the pump/energy recovery unit 230 may be physically separated from the energy recovery portion, or that a pump portion may be present without any energy recovery portion.
  • Filtration systems employing one or more outer casings 210 may be deployed in any suitable manner. As such, contemplated filtration systems may be disposed more or less horizontally on, above or below the surface of the ground, or in some other configuration such as a partially buried disposition. In other contemplated embodiments, for example, filtration systems may be set into a shallow well, perhaps less than 100 or even less than 50 feet deep. In still other embodiments, filtration systems may be disposed within or as part of a tower, hillside, or mountain. In yet another aspect, multiple filtration systems may be coupled together in any combination of dispositions.
  • a filtration system 300 includes four outer casings 310A - 310D, each of which contains multiple inner casings (not shown), a pump/energy recovery unit 330, a feed fluid line 340 with fluid flow depicted by arrow 341, a permeate exit line 350. and a waste fluid line 360 with fluid flow depicted by arrow 361, and end plate subassemblies 31 1 , 312, the elements of which are substantially as described above with respect to Figure 2.
  • a control panel 370 is also present to control the operation, and the entire filtration system 300 includes a base, skid, or rack 380 to facilitate placement and access.
  • an end plate subassembly 400 includes an end plate 498 coupled to a main body (not shown) of an outer casing (not shown) using bolts 499.
  • End plate subassembly 400 is similar in function and appearance to endplate subassemblies 212 and 312 of Figures 2 and 3, respectively, except that here there are only four inner casings (not shown) rather than five inner casings 220A - 220G as in Figure 2.
  • the specific number of inner casings is generally not critical to the operation.
  • the end caps 414A - 414D of the four inner casings (not shown) are coupled to the permeate manifold 462 through permeate lines 460. Waste fluid exits the outer casing though waste fluid lines 450, and waste fluid manifold 452.
  • the base, skid, or rack 480 used to facilitate placement and access is also shown to establish context.
  • Figure 5 depicts preferred details of the fluid flows and structural aspects of elements employed within a preferred inner casing, depicted here as inner casing 520, which may (for example, be the inner casing of Figure 4.
  • a feed fluid enters opening 524 (similar to openings 224 of Figure 2) along arrow 540, and travels along arrows 541 A and 54 I B to one end of a first filter 551.
  • the fluid then flows along arrows 541C through filter 551, with permeate passing through collector pores 571 into permeate collector line 570, and waste fluid flowing along arrows 541 D to act as a feed fluid for a downstream filter 552.
  • the waste fluid flowing along arrow 541 D enters the inter-filter space 555 where it joins fresh feed fluid traveling along arrows 542A, 542B to form a combined stream 542C.
  • the combined stream 542C then enters the downstream filter 552 in a manner similar to feed fluid entering along arrow 541 B entering the upstream filter 551.
  • permeate passes along arrows 542D through collector pores 571 into permeate collector line 570, and then travels along arrows 572 to exit the inner casing at arrow 550.
  • Waste fluid flows along arrows 542E. and at the end of a series of filters fluidly coupled as described immediately above, accumulated waste fluid exits the inner casing 520 at arrow 560.
  • the waste fluid of each filter experiences a drop in pressure relative to the feed fluid entering the filter, and has a correspondingly higher concentration of salts or other compounds removed by the filter.
  • a typical pressure drop may be from about 200 psi to about 190 psi across a single filter.
  • the waste fluid exiting at arrow 560 typically has a pressure of about 180 psi.
  • Permeate exiting at arrow 550 has an even lower pressure, which may typically be about 10 psi.
  • Restriction orifices 557 advantageously lower the pressure of additional feed fluid entering inter-filter space 555 along arrow 542B.
  • the amount and pressure of the additional feed fluid along arrow 542B is advantageously controlled to improve downstream membrane performance, while avoiding excessive backpressure on upstream membranes.
  • Of the 100% of fluid entering the system it is preferred that between about 50% - 70% of the fluid will enter the most upstream membrane, with about 50% - 30% being used as supplemental feed to downstream membranes.
  • the numbers are contemplated to be closer to about 50% of the fluid entering the most upstream membrane, and about 40% being used as supplemental feed to downstream membranes.
  • the preferred distribution among downstream membranes depends on the number of membranes, and generally increases as the fluid flows downstream.
  • the distribution of supplemental feed relative to the original feed entering the system may be about 7%, 8%, 1 1%, and 13%. Where there are only two downstream membranes, the distribution of supplemental feed relative to the original feed entering the system may be about 15% and 25%,
  • Figure 5 also depicts additional details that may be present in preferred embodiments such as those of Figures 2 or 3.
  • an anti-telescoping device such as ATD ribs 592.
  • the complete ATDs are made from several components, including the ribs 592, inner couplings 594, and outer couplings 595, which may simply be short lengths of plastic or other piping.
  • the filters 551 , 552 and outer couplings 595 may advantageously be centered in the casing by a series of tabs or spacers (not shown) attached to the ATD ribs 592. These tabs are intended to keep the filters from binding/sticking during insertion or removal. Seals (not shown) can be included as needed. It should be appreciated that because the ATD ribs 592 may be connected in series by inner and outer couplings 594, 595 using watertight seals 597, the internal casings may be viewed as serving mainly to align the membranes and couplings in series.
  • the internal casings can have slits or other openings along their lengths, or guide rails can be used as equivalents in place of the casings to align the membrane/coupling components, provided that the last inner coupling 594 would be sealed against the end plate of the outer casing.
  • end plate 514 (which may also be the same as any of the end plates 414A - 414D of Figure 4) is preferably coupled to a body of the inner casing 520 using a nut and bolt system 518.
  • Figure 6 depicts an alternative preferred inner casing that is similar to the case of Figure 5 except that the waste fluid and permeate streams exit the inner casing at the opposite ends rather than at the same end.
  • the numerals correspond with those of Figure 5 except that they are increased in value by 100.
  • a feed fluid enters opening 624 (similar to openings 224 of Figure 2 and opening 524 of Figure 5) along arrow 640. and travels along arrows 641 A and 641 B to one end of a first filter 651.
  • the fluid then flows along arrows 641 C through filter 651 , with permeate passing through collector pores 671 into permeate collector line 670 and thence along arrows 672, with waste fluid flowing along arrows 641 D to act as a feed fluid for a downstream filter 652.
  • the waste fluid flowing along arrow 641 D enters the inter-filter space 655 where it joins fresh feed fluid traveling along arrows 642A and 642B to form a combined stream 642C.
  • the combined stream 642C then enters the downstream filter 652 in a manner similar to feed fluid entering along arrow 641 B entering the upstream filter 651.
  • downstream filter 652 permeate passes along arrows 642D through collector pores 671 into permeate collector line 670, and waste fluid flows along arrows 642E.
  • accumulated permeate exits the inner casing 620 at arrow 650.
  • Accumulated waste fluid exits the inner casing 620 at arrow 660.
  • ATDs include ribs 692. inner couplings 694, and outer couplings 695. which may simply be short lengths of plastic or other piping. Restriction orifices 657, watertight seals 697 and a nut and bolt system 618 are also depicted.
  • Figure 7 is a cross-section of another alternative preferred inner casing 720, in which waste fluid from an upstream filter 751 is supplemented by fresh feed fluid before being fed into a downstream filter 752, and all three of the feed fluid stream 740. permeate stream 750 and waste fluid stream 760 enter or exit the inner casing at the same end.
  • a feed fluid enters opening 724 (similar to openings 224 of Figure 2 and opening 524 of Figure 5) along arrow 740, and travels along arrow 741 A and 741 B to one end of a first filter 751.
  • the fluid then flows along arrows 741C through filter 751 , with permeate passing through collector pores (not shown) into permeate collector line 770 and thence along arrows 772, with waste fluid flowing along arrows 741D to act as a feed fluid for a downstream filter 752.
  • the waste fluid flowing along arrow 74 ID enters the inter-filter space 755 where it joins with fresh feed fluid traveling along arrows 742A and 742B to form a combined stream 742C.
  • the combined stream 742C then enters the downstream filter 752 in a manner similar to feed fluid entering along arrow 74 I B entering the upstream filter 751.
  • permeate passes along arrows 742D through collector pores (not shown) into permeate collector line 770, and waste fluid is carried out of the system in channel 780 as shown by arrows 742E.
  • accumulated permeate exits the inner casing 720 at arrow 750.
  • ATDs include ribs 792, inner couplings 794, and outer couplings 795. which may simply be short lengths of plastic or other piping. Restriction orifices 757, watertight seals 797 and a nut and bolt system 718 are also depicted.
  • a major advantage is that by permitting feed water to enter at the membrane couplings between membranes of the same inner casing, the waste fluid passing from one series filter to another is diluted, thereby reducing its osmolarity and the pressure needed to operate the system. Lowered pressure allows for the use of lower cost pressure vessels, and lessens the tolerance requirements at the seals.
  • the additional feed fluid adds to the volume of fluid passing into the downstream membrane, thus increasing the flush rate and reducing the fouling potential.
  • a related benefit is that dilution of the feed fluid entering a downstream membrane reduces the concentration of compounds that may precipitate onto the membranes at higher concentrations.
  • Another benefit is that the additional feed fluid reduces the pressure drop experienced by a downstream membrane. thereby increasing the production of permeate.
  • Still another benefit is that the additional feed fluid reduces the osmotic pressure experienced by the downstream membrane, thereby increasing the rate of filtration.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Nanotechnology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un système de filtration comprenant une gaine extérieure (210) destinée à loger une pluralité de gaines intérieures allongées (220A-220F), qui sont elles-mêmes conçues pour loger une pluralité de membranes de filtration. La gaine extérieure, les gaines intérieures et les membranes de filtration sont disposées par rapport les unes aux autres afin de former un système à trois canaux d'écoulement, qui alimente en fluide un ou plusieurs raccords de membranes, placés entre des membranes à l'intérieur de la même gaine intérieure. Cette structure définit donc un trajet d'écoulement pour fluide d'alimentation permettant de diluer, à l'aide d'un autre fluide, un fluide provenant d'un filtre situé en amont et dirigé vers un filtre situé en aval.
PCT/US2000/003107 1999-05-27 2000-02-04 Filtration utilisant un recipient sous pression avec canaux de filtration multiples WO2000072949A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US10/019,066 US6942797B1 (en) 1999-05-27 2000-02-04 Filtration using pressure vessel with multiple filtration channels
AU32241/00A AU3224100A (en) 1999-05-27 2000-02-04 Filtration using pressure vessel with multiple filtration channels

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US13673999P 1999-05-27 1999-05-27
US60/136,739 1999-05-27

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US10/922,060 Division US20050035048A1 (en) 1999-05-27 2004-08-18 Filtration system with anti-telescoping device

Publications (1)

Publication Number Publication Date
WO2000072949A1 true WO2000072949A1 (fr) 2000-12-07

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4064052A (en) * 1976-06-28 1977-12-20 Ladish Co. Fractionator modules having lip seals
US4083780A (en) * 1976-07-29 1978-04-11 Envirogenics Systems Company Fluid purification system
US5470469A (en) * 1994-09-16 1995-11-28 E. I. Du Pont De Nemours And Company Hollow fiber cartridge
WO1998009718A1 (fr) * 1996-09-03 1998-03-12 Nate International Systeme de filtration modulaire
WO1998023361A1 (fr) * 1996-11-26 1998-06-04 Keefer Bowie Dispositif et procede de dessalement par osmose inverse

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4064052A (en) * 1976-06-28 1977-12-20 Ladish Co. Fractionator modules having lip seals
US4083780A (en) * 1976-07-29 1978-04-11 Envirogenics Systems Company Fluid purification system
US5470469A (en) * 1994-09-16 1995-11-28 E. I. Du Pont De Nemours And Company Hollow fiber cartridge
WO1998009718A1 (fr) * 1996-09-03 1998-03-12 Nate International Systeme de filtration modulaire
WO1998023361A1 (fr) * 1996-11-26 1998-06-04 Keefer Bowie Dispositif et procede de dessalement par osmose inverse

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