WO2014125405A1 - Appareil et procédé de captage de potentiel osmotique, et procédés de réalisation et d'utilisation correspondants - Google Patents

Appareil et procédé de captage de potentiel osmotique, et procédés de réalisation et d'utilisation correspondants Download PDF

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Publication number
WO2014125405A1
WO2014125405A1 PCT/IB2014/058861 IB2014058861W WO2014125405A1 WO 2014125405 A1 WO2014125405 A1 WO 2014125405A1 IB 2014058861 W IB2014058861 W IB 2014058861W WO 2014125405 A1 WO2014125405 A1 WO 2014125405A1
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WO
WIPO (PCT)
Prior art keywords
hfs
opposed
brine
initial
feed
Prior art date
Application number
PCT/IB2014/058861
Other languages
English (en)
Inventor
Maher KELADA
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Kelada Maher
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 Kelada Maher filed Critical Kelada Maher
Priority to JP2015557541A priority Critical patent/JP6277560B2/ja
Priority to CA2898084A priority patent/CA2898084C/fr
Priority to GB1512092.6A priority patent/GB2525335A/en
Priority to AU2014217502A priority patent/AU2014217502B2/en
Publication of WO2014125405A1 publication Critical patent/WO2014125405A1/fr
Priority to HK15112548.5A priority patent/HK1211894A1/xx

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B01D63/026—Wafer type modules or flat-surface type modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B01D63/04—Hollow fibre modules comprising multiple hollow fibre assemblies
    • 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
    • B01D61/002—Forward osmosis or direct osmosis
    • 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
    • B01D63/021—Manufacturing thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/08—Flow guidance means within the module or the apparatus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/14—Specific spacers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/20—Specific housing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/21—Specific headers, end caps
    • 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
    • B01D2313/243—Pumps
    • 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
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/36—Energy sources
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/36—Energy sources
    • B01D2313/367—Renewable energy sources, e.g. wind or solar sources
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2315/00—Details relating to the membrane module operation
    • B01D2315/06—Submerged-type; Immersion type
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • TITLE Apparatus and Methods for Harnessing Osmotic Potential and Methods of Making and Using Same
  • the present application provides a unique hollow fiber (HF) or tubular semipermeable membrane element (hereafter “HF membrane element”), apparati comprising the HF membrane element, and methods for using the HF membrane element and apparatus.
  • HF membrane element tubular semipermeable membrane element
  • Osmosis has been used to treat industrial wastewaters, to concentrate landfill leachate, and to treat liquid foods in the food industry with low salinity content. Recent developments in material science also have allowed the use of osmosis in controlled drug release and in dialysis.
  • osmosis Compared to other industrial separation processes, osmosis has the advantage of operating at low to no hydraulic pressure; rejecting a wide range of contaminants; possibly having a lower membrane fouling propensity; and, using relatively simple, basic equipment.
  • the application provides a method comprising:
  • the application provides a method comprising:
  • the application provides a method comprising: providing a power train comprising the claimed apparatus comprising a
  • concentration water at the initial end cell producing a concentration field across the plurality of cells comprising a progressively increasing concentration and osmotic pressure ratio bounded by water of low to no salt concentration at the initial end cell and by a concentrated brine at the opposed end cell, thereby producing a power train cycle comprising a controlled concentration-pressure loop wherein the concentration field: (a) osmotically induces a continuous and constant flow rate of substantially salt-free permeate flux throughout the power train; (b) maintains a salt concentration difference across the semipermeable membrane shared by the adjacent cells in the plurality of cells; (c) defines a salt concentration ratio within each cell that ensures a net positive power generation; and, (d) discharges the concentrated brine at the opposing end cell; and
  • the application provides a method of making a membrane element comprising:
  • Figure 3 is a perspective view of an array for use in a power train, the array comprising a plurality of alternating perpendicularly oriented pairs of panels.
  • Figure 3A is an exploded view of panels from the array of Fig. 3.
  • Figure 3A-1 is a frontal view of a vertical fiber panel.
  • Figure 3A-2 is a side view illustrating fluid flow across the array of Fig. 3A-1.
  • Figure 3B is an exploded view of panels from a desalination array.
  • Figure 3C is a perspective view of a desalination array.
  • Figure 3D is a cross-section of a fiber reinforced plastic (FRP) panel for a hollow fiber panel.
  • FRP fiber reinforced plastic
  • Figure 3E is a cross-section of a steel frame or FRP for a hollow fiber panel
  • Figure 3F is a cutaway/transparent frame perspective view of a panel 10 (Fig. 2) comprising the header 16 and an adjacent header 26 (Fig. 2).
  • Figure 3G is a perspective view of a vertical baffle and a horizontal baffle.
  • Figure 4 is a cross section through a plurality of conventionally packed hollow fibers.
  • Figure 5 is a cross section through of a plurality of loosely packed hollow fibers.
  • Figure 6 is a frontal view of a rectangular vessel at a vertical panel, the rectangular vessel being adapted for use with high pressures inside of the hollow fibers and low pressures outside of the hollow fibers.
  • Figure 7 is a cross section through a cylindrical vessel at a vertical panel, the cylindrical vessel being adapted for use with low pressures inside of the hollow fibers and high pressures outside of the hollow fibers.
  • Figure 9B is another schematic top view of a space saving arrangement for a power train.
  • Figure 10 is a top view of a power train comprising three cells of segmented arrays limited by maximum allowable operating pressure of the plurality ofHFs.
  • Figure 11 is a top view of a last cell in a power train comprising multiple cells comprising a pressure vessel comprising a plurality of segments of progressively differing diameters.
  • Figure 12 is a top view of a final two cells in a power train comprising multiple cells having the configuration of Fig. 11.
  • Figure 13 is a top view of a final cell of an exchanger comprising multiple pressure vessels having the structure generally described in Figure 11.
  • Figure 14 is a top view of cell similar to Figure 11 comprising flexible feed conduits, the cell fitted with electromagnetic vibrators for concentration polarization control.
  • Figure 15 is a top view of an integrated plant comprising the last cell of a large scale induced symbiotic osmosis (ISO) power train and a seawater desalination cell comprising an array similar to that of Figure 3C.
  • ISO large scale induced symbiotic osmosis
  • Figure 16 is a side view of a three cell water extraction- water recovery system 300 for concentrating diluted fluids by extracting its water content, particularly water contaminated with radioactive material.
  • Figure 18 is a cross section through a contact structure adapted to retain opposed ends of the HFs.
  • Figure 18A is a cross section of a HF indicating an inner and outer diameter.
  • Figure 19 is a cross section through the rows of HFs 34 that extend between contact structures in an intermediate phase during assembly with spacers therebetween.
  • Figure 21 is a cross section through the assembly of Fig. 20 with only two HFs, depicting the HFs as weighted.
  • Figure 24 is a cross section through an assembly comprising spacers adapted to form a potting structure, minus HF roll or loom heddle.
  • Figure 25 is a top view of one embodiment of a spacer.
  • Figure 26 is a perspective view of the HF membrane element comprising opposed contact structures with layers of HFs extending therebetween.
  • Figure 27A is a cross section through Fig. 27 at line X-X before injecting potting material.
  • Figure 27B is a cross section through Fig. 27 at line X-X after injecting and curing potting material.
  • Fig. 28C is a perspective view of an assembly for manufacturing the membrane element comprising multiple spools of HFs.
  • Fig. 28D is a schematic top view of an assembly comprising a first spool row comprising an even number of HFs alternating with a second spool row comprising an odd number of HFs.
  • Fig. 28E is perspective view of an assembly for manufacturing reels of HFs from a plurality of spools.
  • Fig. 28F is a schematic top view of an assembly comprising a plurality of adjacent reels of HFs which may be spaced, as required, to produce the alternating rows of odd an even HFs.
  • Fig. 28G is a schematic view of a wrap beam assembly with the plurality of HFs extended from HF reels or spools being brought from different sources.
  • Fig. 29A and Fig. 29B together, are an exploded view of a membrane element separated from a frame of one embodiment of a hollow fiber panel. Definitions
  • Chemical potential The energy potential associated with the activity of ions of an ionizable substance.
  • the chemical potential is equal to the rate of change of free energy, known as Gibbs free energy, in a system containing a number of moles of such substance, when all other system parameters; temperature, pressure and other components are held constant.
  • Gibbs free energy the rate of change of free energy, known as Gibbs free energy, in a system containing a number of moles of such substance, when all other system parameters; temperature, pressure and other components are held constant.
  • chemical potential is spontaneous energy that flows in a direction from high to low.
  • osmotic pressure In order to prevent water from moving across a semipermeable membrane, a pressure must be imposed to equalize the force created by a given difference in the chemical potential of the solution across said membrane. This force is named osmotic pressure.
  • LSRE Large Scale Renewable Energy
  • the HF panel 10 comprises: the frame 12 comprising a header 16, an opposed header 16a, and the membrane element 3000 (Fig. 29A, described above) retained within the frame 12.
  • the membrane element 3000 (Fig. 29A) comprising the plurality of loosely packed HFs 14 engaged at each end by the first and second contact structure (906, 906a, Fig. 29A) is adapted to provide fluid communication between lumens of the plurality of loosely packed HFs 14, the header 16, the opposed header 16a, and any adjacent frames and panels.
  • the HF panel 10 is adapted for submersion in a first fluid and for induced osmosis between lumens of the plurality of loosely packed HFs 14 in the membrane element 3000 (Fig. 16, Fig. 29A) and the first fluid.
  • the HF panel 10 has sufficient mechanical integrity to sustain turbulence flow across and along surfaces of the plurality of loosely packed HFs 14 at the Reynolds' Number of about 3,000 or more and to maintain said mechanical integrity at feed pumping pressures of 30 bars or higher.
  • the actual feed pressure to which the HF panel 10 comprising the HF membrane element 3000 (Fig. 19A) will be exposed will differ depending upon the process being performed, the initial salinity of the process fluid and the feed, and the tie-line flow. Induced osmosis of water having salinity of 1% generates an osmotic head equivalent to 7.75 bars. At 6% salinity, the osmotic head is equivalent to 46.5 bars. In general, the sustainable feed pumping pressure must be sufficiently high to overcome this osmotic head.
  • MF microfiltration
  • UF ultrafiltration
  • NF nanofiltration
  • RO reverse osmosis
  • MF typically is used to separate or remove suspended or colloidal particulates having a maximum diameter of from about 0.1 to about 1.0 microns (about 1,000 to about 10,000 angstroms).
  • UF typically is used to separate or remove dissolved materials depending upon solute size, which typically comprise a maximum diameter of from about 0.001 microns to about 0.1 microns (about 10 angstroms to about 1,000 angstroms).
  • NF and RO typically are used to separate or remove materials having a maximum diameter of less than about 0.001 micron (about 10 angstroms).
  • the hydrophilic semipermeable membrane material is cellulose acetate.
  • Cellulose acetate has a surface tension of 44 dyne per centimeter (dyne/cm).
  • the hydrophilic semipermeable membrane is a cellulose triacetate (CTA) membrane.
  • CTA cellulose triacetate
  • a suitable CTA semipermeable membrane is commercially available from the Japanese corporation, Toyobo Co, Ltd.
  • the plurality of HFs 14 in each frame are retained in a loosely packed configuration by one or more horizontal baffles 720 and/or one or more vertical baffles 710.
  • the plurality of HFs 14 in each frame are retained in a loosely packed configuration by a plurality of spaced horizontal baffles 720 and/or vertical baffles 710.
  • the baffles may be external baffles which are removable from the HF frame 12, or the baffles may be integrated into the HF frame 12, as described more fully below.
  • the spikes or wire loops 722 in a horizontal baffle are spaced from about 6 to 12 inches apart. Once inserted through the plurality of HFs, the spikes or wire loops 722 reduce movement of the plurality of HFs.
  • the horizontal baffles 720 are spaced apart across the plurality of HFs. The space between the horizontal baffles 720 is effective to retain the plurality of HFs running vertically in a loosely packed configuration and to prevent sagging. In one embodiment, the space between horizontal baffles 720 is from about 20 cm to about 30 cm.
  • each vertical baffle comprises backing 710 comprising a plurality of appropriately spaced wire loops 712.
  • the spikes or wire loops 712 are spaced along the backing 710 at intervals that are effective to retain the plurality of HFs running horizontally in a loosely packed configuration and to prevent sagging when the spikes or wire loops 712 are inserted through the plurality of HFs.
  • the intervals between spikes or wire loops 712 may vary.
  • the spikes or wire loops 712 in a vertical baffle are spaced at smaller intervals than in a horizontal baffle.
  • the contact structures 906, 906a (or 1006 in Fig. 3E) at each end of the loosely packed HFs 14 have a length 3006, a width 3008, and a thickness 3010.
  • the contact structure length 3006 is slightly larger than the HF stack width 3002
  • the contact structure width 3008 is slightly larger than the HF stack depth 3005 to allow for proper support of the HF stack 14 on the frame of Fig. 29B.
  • the HF stack depth 3005 is 40-80 mm.
  • the HF stack depth 3005 is about 3 A of the contact structure width 3008.
  • the contact structure thickness 3010 is from about 20 to 60 mm, depending on operating pressure.
  • the opposed header 16a of the HF panel 10 abuts the first support member 29 of the adjacent HF panel 20; the header 16 of the HF panel 10 abuts the opposed support member (not shown) of the adjacent HF panel 20; the support member 19 of the HF panel 10 abuts the first header 26 of the adjacent HF panel 20; and the support member 19a abuts the opposed header 26a of the adjacent HF panel 20.
  • the headers and supports comprise a material and structure having sufficient mechanical integrity to retain the plurality of HFs 24, 25 when exposed to a substantially perpendicular flow of feed at a specified operating pressure.
  • the frame 12, as well as other components, such as the array casing, may be made of a variety of materials including, but not necessarily limited to fiber reinforced plastic (FRP).
  • FRP fiber reinforced plastic
  • Fiber-reinforced plastic (FRP) also sometimes called fiber-reinforced polymer
  • Common fibers include, but are not necessarily limited to glass, carbon, basalt, aramid, paper, wood, asbestos, and the like.
  • the fibers are selected from the group consisting of glass, carbon, basalt, aramid, and combinations thereof.
  • Common polymers include, but are not necessarily limited to thermosetting plastics selected from the group consisting of epoxy, vinyl ester, polyester, phenol-formaldehyde resins, and combinations thereof.
  • Suitable FRP's meet or exceed the mechanical properties of steel.
  • the FRP exhibits superior thermo-mechanical properties, is light weight, is relatively low cost, exhibits corrosion resistance, and is easy to maintain.
  • headers and supports are made of the same material.
  • the headers and supports are made of different materials.
  • the headers and/or supports are made of steel ( Figure 3E).
  • the headers and/or supports are made of FRP.
  • the headers and the supports are made of FRP.
  • the process fluid is seawater.
  • the feed is brackish water or agricultural drainage.
  • water spontaneously permeates from the feed (brackish water or agricultural drainage) to the seawater in the HF lumens, diluting the seawater.
  • the second modified process fluid flows through the plurality of HFs 34b, producing a third modified process fluid 33c that flows into the header 36e.
  • the third modified process fluid 33c flows through an aperture 32c-l into header 36f, from header 36f (Fig. 3) through the plurality of HFs 34c into opposed header 36g, producing a fourth modified process fluid (not shown).
  • the fourth modified process fluid flows from header 36g through abutting apertures (not shown) into adjacent header 36h, through the plurality of HFs 34d to produce a fifth modified process fluid 33d.
  • process fluid is introduced into the header 41 and flows through the HFs to an opposed header 41a.
  • a high salinity brine feed 43 is charged to the array 45, and flows from and across a tail panel 47a to and across an initial panel 47b of the array 45.
  • the total area (width x length) of the frontal view across which the feed flows is up to 100 times larger than the corresponding area across which the feed flows in a conventional, commercially available tube-like high pressure membrane array.
  • the modified feed 43a exiting the array 45 is a low salinity product, typically at a higher flow rate than the high salinity brine feed 43.
  • FIG. 3B depicts a typical cross flow pattern in a desalination array 3.
  • the desalination panels operate relatively independently.
  • a brine feed 44 is charged at a relatively high pressure to and across the desalination array 3.
  • the brine feed 44 is seawater. Where the brine feed 44 is seawater, the seawater 44 passes across the array and water passes from the seawater into the HFs, producing desalinated seawater 47.
  • a relatively high salinity brine 44a exits the array.
  • Spaced horizontal baffles 720a, 720b, 720c and spaced vertical baffles 710a, 710b, 710c are visible the respective panels. The baffles are described in more detail below.
  • the process fluid travels through the headers via a pipe structure.
  • the pipe structure may have a variety of configurations.
  • Figure 3D is a cross section at 900'-900" in Figure 3A illustrating one embodiment 900 of a pipe structure.
  • the pipe structure 3D comprises fiber reinforced plastic.
  • the header comprises a rectangular support structure 902.
  • a pipe 904 is retained within the rectangular support structure 902.
  • the rectangular support structure 902 is a solid structure defining a bore therethrough.
  • the rectangular support structure 902 is a frame with a pipe 904 extending therethrough.
  • the rectangular support structure 902 and the pipe 904 comprise fiber reinforced plastic.
  • Figure 18 is a cross section through a contact structure 906 at line A- A' in Fig. 29A.
  • the contact structure 906 or 1006 (Fig. 3E) comprises cured potting material 2000 with embedded alternating rows of HFs 34.
  • the embedded alternating rows of HFs 34 form abutting rows of hexagonal structures 2006 around a central HF 34c.
  • the contact structure 906 or 1006 (Fig. 3E) may be made in any desired size.
  • the contact structure 906 or 1006 has a width 2003 (3008 in Fig. 29A) of about 55-105 mm.
  • the contact structure 906 or 1006 has a thickness (3010 in Fig. 29 A) of about 20-60 mm.
  • the contact structure 906 or 1006 has a length 2001 (3006 in Fig. 29 A) of up to 3,000 mm (3m).
  • the HFs 34 have an inner diameter (Di) of about: 0.05 mm; 0.06 mm; 0.07 mm; 0.08 mm; 0.09 mm;0.1 mm; 0.2mm; 0.3mm; 0.4 mm; 0 5 mm; 0.6 mm; 0.7 mm; 0.8 mm; 0.9 mm; 1 mm; 1.1 mm; 1.1 mm; 1.2 mm; 1.3 mm; 1.4 mm; 1.5 mm.
  • the size of the space between HFs (2007, Fig 19) will vary depending upon parameters of the process for which the HF panel 10 will be used, particularly the flow dynamic analysis (Reynolds number).
  • Figs. 20-27 and 28A-28G illustrate suitable assemblies and processes for making the structures depicted in Figs. 18 and 19.
  • the HF's may be provided in a variety of forms. Such forms include, but are not necessarily limited to rolls, spools, reels, or wrap beam assemblies.
  • Fig. 28A is a side view of an embodiment in which a first roll 2050a comprises HF's having a first spacing (in one embodiment, an even number of HFs), and a second row 2050b comprising HFs having an alternating spacing (an odd number of HFs).
  • the roll 2050a is sufficiently wide (line 2052) that a plurality of HF stacks 2054, 2054a are made using a single roll 2050a.
  • a HF assembly platform 2018 is provided adjacent to the HF loom heddle 2016. Referring to Fig. 21, in one embodiment, a first spacer 2014a is provided on the HP assembly platform 2018. In one embodiment, a first row comprising an odd number of spaced HFs 34o is extended lengthwise across the first spacer 2014a. In one embodiment, the opposed ends 2015 of HFs opposite to the loom heddle 2016 are weighted or engaged to maintain the HFs extended along the length of the HF assembly platform 2018. In one embodiment, the opposed ends 2015 of the HFs are weighted or engaged sufficiently to extend the HFs. In one embodiment, one or more of the opposed ends 2015 of the HFs are engaged by a suitable clamp (not shown).
  • these elastic materials have a Young's Elasticity Modulus of less than lGPa and specific gravity of less than 1000 kg/m 3 .
  • the elastic material is rubber.
  • all of the opposed ends 2015 of the HFs are engaged in a single clamp having a suitable width and sufficient weight or tension to straighten the HF on the HF assembly platform 2018, but without stretching the HFs.
  • HF stack depth (2027 in Fig. 23, 3005 in Fig. 29A) is 40 mm.
  • the HFs have an outer diameter (D 0 ) of less than 0.5 mm, and the stack comprises from about 64 to about 80 rows of HFs. Processes using HFs having a smaller diameter of 0.5 mm or less would include ISO power generation and reverse osmosis.
  • suitable provisions are made to prevent the potting material 2000 (Fig. 18) from filling unintended areas.
  • a petroleum based malleable sealant is applied to the surfaces of the potting chambers 2020a-2020d defined by the slots, including any gaps at the surfaces.
  • the petroleum based malleable sealant is smoothed using any suitable method to avoid damaging the HFs or the contact structure 906 during separation after curing the contact structure 906.
  • the petroleum based malleable sealant is smoothed using a brush or air stream.
  • the petroleum based malleable sealant is applied between HFs in spaces 2006, 2007 (Fig. 19) between HFs.
  • the method comprises:
  • the header comprises a solid structure 1000 with a bore 1008 therethrough.
  • the solid structure 1000 may have a variety of shapes. Suitable shapes include, but are not necessarily limited to, triangular shapes, rectangular shapes, pentagonal shapes, hexagonal shapes, cylindrical shapes, oblong shapes, and the like.
  • the solid structure 1000 is an elongated rectangular structure.
  • the bore 1008 also may have a variety of shapes.
  • the solid structure 1000 is an elongated rectangular structure with an elongated cylindrical bore 1008
  • the sealing encasement 71 is effective to prevent leakage or seeping of the high pressure relatively unprocessed raw feed (37, Fig. 3) to the processed feed flowing through the HF array (37a, Fig. 3) at relatively lower operating pressures.
  • This embodiment is useful under a variety of conditions.
  • a circular or elliptical pressure vessel is useful with a relatively high pressure process fluid inside of the HFs and a relatively low pressure feed.
  • the initial modified feed 85b is fed to an adjacent array 87c having a larger diameter than the initial array 87d contained in an adjacent segment 82c of the pressure vessel 80 that has a larger diameter than the initial segment 82d.
  • the adjacent array 87c produces a second modified feed 85c having a lower salinity, a higher flow rate, and a slightly lower pressure than the initial modified feed 85b.
  • the array 88 is surrounded by an array casing 88a.
  • array casing 88a comprises an open tail end 88b.
  • the initial feed 85a flows into the array 88 at the open end 88a at a given pressure.
  • the diameters of the segments 82a-d of the array casing 88a maintain the pressure of the feed sufficiently high to flow across the array 88.
  • the diameters of the segments 82a-d are effective to maintain the pressure drop from the feed 85 entry point to feed 85 a entry point of less than 1 bar.
  • the electromagnetic vibrators 104a and 104b provide further control of fouling. In one embodiment, the electromagnetic vibrators 104a and 104b also provide further control of concentration polarization. In one embodiment, depicted in Figure 14A, spring supports 108 and 108a are provided at intervals along the length of the exchanger. In one embodiment, support members 110, 110a are provided at intervals along the length of the exchanger. [000173]
  • Figure 11 A illustrates an induced symbiotic osmosis power generation train comprising 3 cells, forming low pressure exchanger section 370, and a high pressure exchanger section 372.
  • the low pressure exchanger section 370 comprises two sequential segmented exchangers comprising a first segmented exchanger 374 and a second segmented exchanger 376 of a design described in Fig. 8, with a cross section similar to Fig. 6.
  • These exchangers 374, 376 have generally low operating pressure of 5 bars or less, with a HF lumen pressure (process fluid pressure) that is higher than its external pressure (feed pressure).
  • Exchangers are limited in size- typically having diameters or 4 meters or less for cylindrical pressure vessels and 12 square meters or less for rectangular low pressure HF membrane housing.
  • Cell 2 operates in a similar fashion as Cell 1, but at relatively higher salinity conditions and higher pressure.
  • feed stream 396a enters the low pressure shell side of HF exchanger 376 external to the hollow fiber, while relatively higher salinity water (process fluid) is pumped at relatively high pressure by means of P3 via stream 391 through the relatively high pressure HF lumens of exchanger 376.
  • the feed 383a to HF exchangers 378, 380 operates at a pressure of 30 bars or more, while the process fluid in the HF lumens operates at a low pressure of 5 bars or less.
  • high salinity brine potentially approaching saturation (35% in case of sodium chloride) is pumped with high pressure pump P4 as a feed brine 383a from an evaporation /concentration pond 390, through the four pressure vessel segments surrounding the encased hollow fiber arrays as shown in Figs.7 and 14A.
  • Freshwater is always preferable for its better efficiency and low cost of treatment.
  • seawater is abundant, but a large volume is required to extract the salt-free water that is needed to run the HF train.
  • Figure 13 illustrates a final cell 120 of an ISO power generation exchanger, the cell 120 comprising multiple pressure vessels 122, 124, 126 having the structure generally described in Figure 11.
  • the multiple pressure vessels 122, 124, 126 do not comprise flexible support members. In one embodiment, the multiple pressure vessels 122, 124, 126 (Fig. 13) do comprise flexible support members, described more fully in connection with Fig. 14. [000192] Referring again to Fig. 13, diluted brine 128 discharged from the turbine of a prior cell is fed as process fluid to initial panels 130, 132, 134 of the exchangers in the respective pressure vessels 122, 124, 126. In one embodiment, the diluted brine 128 has a relatively low pressure. A high salinity brine feed 135 is fed from a source 140 into each pressure vessel 122, 124, 126 at 131a-c.
  • the TL is optimized and the efficiency of power generation is optimized by evaluating salinity distribution across adjacent cells in the train.
  • greater efficiency is realized by using three ISO cells having the following salinity ranges: [10% -2%] ce n i, [20% -4%] cell 2 , [30% -6%] C eii 3, with a constant tie line flow of 4 m 3 /s. [000199] Optimization of ISO power trains becomes more complicated when the source of Tie-Line flow is brackish or seawater, due to the lower salinity operating margin available; between 3.5% and 6%.
  • the cell 204b comprises four pressure vessels.
  • the pressure vessel 206a has smaller diameter than pressure vessel 206b; the pressure vessel 206b has a smaller diameter than pressure vessel 206c; and, the pressure vessel 206c has a smaller diameter than the pressure vessel 206d.
  • solutions comprising radioactive contamination generally comprise solutes having higher molecular weights; accordingly, such solutions tend to have a relatively low osmotic pressures.
  • Radioactive contamination may take different forms.
  • the radioactive contamination comprises Cesium-137.
  • the feed 321 has a pressure sufficiently high to create a pressure differential of 50 bar (720 psi) or higher between the feed and the process fluid in the HF lumens in the second cell 300b.
  • a pressure differential of 50 bar (720 psi) or higher between the feed and the process fluid in the HF lumens in the second cell 300b.
  • water passes from the feed 321 into the process fluid in the HF lumens of the second array 322.
  • the result is a concentrated radioactive stream 334 and a first decontaminated process fluid 332.
  • the concentrated hazardous chemicals or radioactive substance stream 334 is safely disposed.
  • the third radioactive waste water 342 is recycled to the second pressure exchanger 318a.
  • water passes from the feed 321a into the process fluid in the HF lumens of the third reverse osmosis array 324.
  • the result is a concentrated radioactive stream 336 and a second decontaminated process fluid 338.
  • the decontaminated process fluid 338 is used as process fluid 310.
  • the decontaminated process fluid 338 may be used for a variety of purposes.
  • the decontaminated process fluid 338 is used as freshwater.
  • An intermediate salinity product 734a flows from the extraction array 702 into a second loop 701a.
  • the intermediate salinity product 734a is split into a first stream 715 and a second stream 718.
  • the first stream 715 is fed to a pressure exchanger 716 and the second stream 718 is fed to a pump 720.
  • the pump 720 uses about 6.38 K Joule of energy to increase the pressure of the second stream 718, producing an increased pressure second stream 718a.
  • the first stream 715 is fed to a pressure exchanger 716.
  • the pressure exchanger recovers pressure from the first stream 715 for subsequent use, and produces a relatively high pressure first stream 715a.
  • the second product 724 is split into a first stream 726 and a second stream 728.
  • the relatively high pressure of first stream 726 is fed to a pressure exchanger 716 where the pressure is recovered by pressurizing first stream 715 to produce an increased pressure first stream 715a, a reduced pressure second stream 732, and approximately 6.38 K Joule of recovered energy.
  • the relatively high pressure first stream 728 is retained by a back pressure control valve 730, and a reduced pressure first stream 731 is combined with the reduced pressure second stream 732 to form return stream 734 to the extraction array 702.
  • the return stream 734 has a salinity of about 6% and a flow rate of about 1 liter/sec.
  • the second feed 722 is exchanged with feed 758 across membranes of the first reverse osmosis array 704, to produce a reduced salinity second product 740, which serves as a feed to a third loop 701b.
  • the function of this third loop 701b is identical to the function of the second loop.
  • ⁇ osmotic pressure or force imposed on the membrane given in bars, atm, psi, etc.
  • ⁇ dynamic viscosity (Ns/m 2 , Ib r Js ft) e.
  • L characteristic length (m,ft) also known as the hydraulic diameter, d h for ducts, passageways, annuli, etc.

Landscapes

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

Abstract

L'invention concerne un appareil et des procédés correspondants de fabrication et d'utilisation. Cet appareil comprend un élément à membrane comprenant un empilement de fibres creuses constitué d'une pluralité de fibres creuses faiblement tassées définissant des premières extrémités traversant une structure de contact, et des extrémités opposées traversant une structure de contact opposée. Chaque fibre creuse, qui comporte une lumière de forme allongée allant d'une structure de contact à la structure de contact opposée, comprend une membrane hydrophile semi-perméable conçue pour réaliser un rejet de sels d'au moins 98,5% et pour présenter une tension superficielle d'au moins 35 dynes/cm. L'élément à membrane est conçu, d'une part pour être monté dans un châssis, d'autre part pour être plongé dans un premier fluide, et enfin, pour réaliser une osmose induite entre les lumières de la pluralité de fibres creuses faiblement tassées et le premier fluide. Quand il est monté dans le châssis et plongé dans le premier fluide, l'élément à membrane présente une intégrité mécanique suffisante pour entretenir, au travers et le long des surfaces de la pluralité de fibres creuses faiblement tassées, un flux de turbulence d'un nombre de Reynolds d'au moins 3.000, et pour conserver ladite intégrité mécanique sous des pressions de pompage d'alimentation d'au moins 30 bars.
PCT/IB2014/058861 2013-02-15 2014-02-07 Appareil et procédé de captage de potentiel osmotique, et procédés de réalisation et d'utilisation correspondants WO2014125405A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
JP2015557541A JP6277560B2 (ja) 2013-02-15 2014-02-07 浸透ポテンシャルを利用する装置、装置の作製方法、及び使用方法
CA2898084A CA2898084C (fr) 2013-02-15 2014-02-07 Appareil et procede de captage de potentiel osmotique, et procedes de realisation et d'utilisation correspondants
GB1512092.6A GB2525335A (en) 2013-02-15 2014-02-07 Apparatus and methods for harnessing osmotic potential and methods of making and using same
AU2014217502A AU2014217502B2 (en) 2013-02-15 2014-02-07 Apparatus and methods for harnessing osmotic potential and methods of making and using same
HK15112548.5A HK1211894A1 (en) 2013-02-15 2015-12-21 Apparatus and methods for harnessing osmotic potential and methods of making and using same

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US201313768228A 2013-02-15 2013-02-15
US201361765268P 2013-02-15 2013-02-15
US61/765,268 2013-02-15
US13/768,228 2013-02-15

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WO2016190166A1 (fr) * 2015-05-28 2016-12-01 東洋紡株式会社 Module de membrane à fibres creuses de type à immersion et procédé de traitement d'eau à osmose avant dans lequel celui-ci est utilisé
US20230133424A1 (en) * 2020-03-20 2023-05-04 Oliver Piestert Method for performing working using osmosis

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DE102016211903A1 (de) * 2016-06-30 2018-01-04 membion Gmbh Verfahren zur Herstellung eines Membranfilters

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US5104535A (en) * 1990-08-17 1992-04-14 Zenon Environmental, Inc. Frameless array of hollow fiber membranes and module containing a stack of arrays
US6790360B1 (en) * 1999-11-18 2004-09-14 Zenon Environmental Inc. Immersed membrane element and module
US20110127209A1 (en) * 2008-07-24 2011-06-02 Siemens Water Technologies Corp. Frame System for Membrane Filtration Modules
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WO2016190166A1 (fr) * 2015-05-28 2016-12-01 東洋紡株式会社 Module de membrane à fibres creuses de type à immersion et procédé de traitement d'eau à osmose avant dans lequel celui-ci est utilisé
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US20230133424A1 (en) * 2020-03-20 2023-05-04 Oliver Piestert Method for performing working using osmosis

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JP2016514035A (ja) 2016-05-19
GB201512092D0 (en) 2015-08-19
HK1211894A1 (en) 2016-06-03
AU2014217502A1 (en) 2015-08-27
GB2525335A (en) 2015-10-21
CA2898084A1 (fr) 2014-08-21
AU2014217502B2 (en) 2017-09-14
CA2898084C (fr) 2021-04-13
JP6277560B2 (ja) 2018-02-14

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