WO2020072080A1

WO2020072080A1 - Induced symbiotic osmosis systems of 3-5 cascading circulation loops of semipermeable membranes, for salt water brines power generation or desalination

Info

Publication number: WO2020072080A1
Application number: PCT/US2018/054740
Authority: WO
Inventors: Maher Isaac Kelada
Original assignee: Maher Isaac Kelada
Priority date: 2018-10-05
Filing date: 2018-10-05
Publication date: 2020-04-09

Abstract

The present technology essentially includes an induced symbiotic osmosis system and method for symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis. The system includes a reverse osmosis membrane assembly to create potable water from saline water or brine. The membrane assembly includes a hollow fiber or flat sheet membrane and headers to transfer desalinated water therefrom. A frame having an open end receives the membrane assembly, and a shell encloses the frame so that an annulus is created between therebetween allowing the saline water or brine to flow into the open end of the frame and through the hollow fiber or flat sheet membrane. The system can be utilized with a geological depression in communication with a saline water source. An osmotic power generation unit can create electrical power by receiving and utilizing saline water from the source and brine water from the brine storage.

Description

INDUCED SYMBIOTIC OSMOSIS SYSTEMS OF 3-5 CASCADING CIRCULATION LOOPS OF SEMIPERMEABLE MEMBRANES, FOR SALT WATER BRINES

POWER GENERATION OR DESALINATION

TECHNICAL FIELD

[001] The present technology relates to induced symbiotic osmosis systems, processes and plants for use in connection with symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis, employing innovative system designs, configurations and/or operations. More particularly, the present technology relates to induced symbiotic osmosis systems of 3-5 cascading circulation loops of semipermeable membranes for salt water brines power generation or desalination.

BACKGROUND ART

[002] In a typical conventional example of seawater desalination, pretreated brackish or seawater is desalinated by reverse osmosis (RO) employing tubular high-pressure housing, often known as vessels of few inches in diameter, but generally less than 12 inches (about 30 centimeters). These membrane housing are typically mounted horizontally, on series of pipe racks, in a dedicated section of water treatment and processing buildings.

[003] The use of framed flat sheet membranes or framed hollow fiber membranes with reverse osmosis is known in the prior art. For example: U.S. Patent Number 8,545,701; U.S. Patent Number 8,852,432; U.S. Patent Number 9,156,003; and International Application Number PCT/IB2014/058861. Wherein these systems are mounted in high-pressure vessel and towers, that can be of one meter or larger in diameter and at a length or height of several meters.

[004] While the above-described devices fulfill their respective, particular objectives and requirements, the aforementioned patents do not describe an induced symbiotic osmosis systems and processes that allows symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis.

[005] Therefore, a need exists for a new and improved induced symbiotic osmosis systems and processes that can be used for symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis. In this regard, the present technology substantially fulfills this need. In this respect, the induced symbiotic osmosis systems and processes according to the present technology substantially departs from the conventional concepts and designs of the prior art, and in doing so provides an apparatus primarily developed for the purpose of symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis.

SUMMARY OF INVENTION

[006] In view of the foregoing disadvantages inherent in the known types of reverse osmosis systems and processes now present in the prior art, the present technology provides an improved induced symbiotic osmosis systems and processes, and overcomes the above-mentioned disadvantages and drawbacks of the prior art. As such, the general purpose of the present technology, which will be described subsequently in greater detail, is to provide a new and improved induced symbiotic osmosis systems and processes and method which has all the advantages of the prior art mentioned heretofore and many novel features that result in a induced symbiotic osmosis systems and processes which is not anticipated, rendered obvious, suggested, or even implied by the prior art, either alone or in any combination thereof.

[007] According to one aspect of the present technology, the present technology essentially includes an induced symbiotic osmosis system for symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis, the induced symbiotic osmosis system can include at least one reverse osmosis membrane assembly configured to receive saline water or brine, the membrane assembly including at least one hollow fiber or flat sheet membrane and at least one header configured to receive desalinated water from the hollow fiber or flat sheet membrane. A frame having an open end can be configured to receive the membrane assembly. A shell can be configured to receive and enclose the frame and the membrane assembly so that an annulus is created between the shell and the frame allowing the saline water or brine to flow into the open end of the frame and through the hollow fiber or flat sheet membrane. The shell can include a waste collecting section configured to receive an effluent from the hollow fiber or flat sheet membrane.

[008] According to another aspect of the present technology, a method of induced symbiotic osmosis can be utilized. The method can include the preparing a geological depression for receiving saline water. Then communicating the geological depression with a source of saline water, with the geological depression being at an elevation lower than the source. After which, desalinating the saline water utilizing a reverse osmosis system comprising a tower enclosing at least one hollow fiber or flat sheet membrane including at least one header configured to receive desalinated water from the hollow fiber or flat sheet membrane, and a frame having an open end configured to receive the membrane assembly. An annulus can be created between the tower and the frame allowing the saline water to flow into the open end of the frame and through the hollow fiber or flat sheet membrane. Then, discharging brine effluent from the tower into brine storage.

[009] According to yet another aspect of the present technology, an induced symbiotic osmosis processing plant system including a geological depression in communication with a source of saline water. The geological depressing being configured or configurable to receive saline water from the source. A reverse osmosis system comprising a tower enclosing at least one hollow fiber or flat sheet membrane including at least one header configured to receive desalinated water from the hollow fiber or flat sheet membrane, and a frame having an open end configured to receive the membrane assembly. An annulus can be created between the tower and the frame allowing the saline water to flow into the open end of the frame and through the hollow fiber or flat sheet membrane. Brine storage can be configured or configurable to receive brine water from the reverse osmosis system. An osmotic power generation unit can be in communication with the source and the brine storage, and configured to create electrical power by receiving and utilizing saline water from the source and brine water from the brine storage.

[010] There has thus been outlined, rather broadly, features of the invention in order that the detailed description thereof that follows may be better understood and in order that the present contribution to the art may be better appreciated.

[Oil] The invention may also include (brief description of additional elements and features). There are, of course, additional features of the invention that will be described hereinafter and which will form the subject matter of the claims attached.

[012] Numerous objects, features and advantages of the present technology will be readily apparent to those of ordinary skill in the art upon a reading of the following detailed description of presently preferred, but nonetheless illustrative, embodiments of the present technology when taken in conjunction with the accompanying drawings. In this respect, before explaining the current embodiment of the invention in detail, it is to be understood that the invention is not limited in its application to the details of construction and to the arrangements of the components set forth in the following description or illustrated in the drawings. The invention is capable of other embodiments and of being practiced and carried out in various ways. In addition, it is to be understood that the phraseology and terminology employed herein are for the purpose of descriptions and should not be regarded as limiting.

[013] As such, those skilled in the art will appreciate that the conception, upon which this disclosure is based, may readily be utilized as a basis for the designing of other structures, methods and systems for carrying out the several purposes of the present technology. It is important, therefore, that the claims be regarded as including such equivalent constructions insofar as they do not depart from the spirit and scope of the present technology.

[014] It is therefore an object of the present technology to provide a new and improved induced symbiotic osmosis systems and processes that has all of the advantages of the prior art reverse osmosis systems and processes and none of the disadvantages.

[015] These together with other objects of the invention, along with the various features of novelty that characterize the invention, are pointed out with particularity in the claims annexed to and forming a part of this disclosure. For a better understanding of the invention, its operating advantages and the specific objects attained by its uses, reference should be made to the accompanying drawings and descriptive matter in which there are illustrated embodiments of the invention.

BRIEF DESCRIPTION OF THE DRAWINGS

[016] The invention will be better understood and obj ects other than those set forth above will become apparent when consideration is given to the following detailed description thereof. Such description makes reference to the annexed drawings wherein:

[017] FIG. 1 is perspective views of prior art high capacity hollow fiver (HFM) frame design.

[018] FIG. 2 is perspective views of prior art flat sheet RO panel assembly and flat sheet RO panels frame.

[019] FIG. 3 is perspective views of prior art flat RO membrane frame.

[020] FIG. 4 is a cross-sectional view of prior art of a Type 1 frame layout for small vessels- single size membranes that occupies 64% of the vessel’s section.

[021] FIG. 5 is a cross-sectional view of prior art of a Type 2 frame layout with two membrane sizes.

[022] FIG. 6 is a cross-sectional view of prior art of a Type 3 frame layout with multiple membrane sizes that occupies a large exchange surface. [023] FIG. 7 is a cross-sectional view of prior art of a stack of flat RO membrane panels.

[024] FIG. 8 is a perspective view of a flat RO membrane frame with multiple panels of the present technology.

[025] FIG. 9 is a cross-sectional view of a flat RO membrane rectangular frame of one or more flat RO membrane panels of FIG. 8 of the present technology.

[026] FIG. 10 is a cross-sectional view of a twin RO staked sequential or independent desalination frames of the present technology.

[027] FIG. 11 is a cross-sectional view of an improved piperack mounting with counter-current of the present technology.

[028] FIG. 12 is a cross-sectional view of an exemplary mounting of the piperack of FIG. 11 for 50% desalinated water recovery.

[029] FIG. 13 is a cross-sectional view of an exemplary mounting of the piperack of FIG. 11 for 75% desalinated water recovery.

[030] FIG. 14 is a cross-sectional view of membrane modules for ISOP or SRO plants utilizing hollow fiber membrane frame or flat sheet membrane to sustain a flow Reynolds Number of 3,000- 3,5000.

[031] FIG. 15 is a cross-sectional view of agitated axial flow sheet membranes with variable flow RO scheme of the present technology.

[032] FIG. 16 is a cross-sectional top view of a vessel well RO with a Type 1 membrane of the present technology.

[033] FIG. 17 is a cross-sectional view of an axial flow vertical well RO with a Type 1 flat membrane of the present technology.

[034] FIG. 18 is a cross-sectional view of a single or multiple stages for filtration and desalination towers or vertical wells of the present technology.

[035] FIG. 19 is a perspective view of a multi-compartmented Type 2 membrane frame assembly of the present technology.

[036] FIG. 20 is a perspective view of an enclosure for the multi-compartmented Type 2 membrane frame assembly of FIG. 19.

[037] FIG. 21 is a perspective view of a Type 2 membrane frame of the present technology assembly for desalination fluids of a single solute.

[038] FIG. 22 is a perspective view of an enclosure for the multi-compartmented Type 2 membrane frame assembly of FIG. 21.

[039] FIG. 23 is a cross-sectional view of an operating train utilizing multiple sequential hypersalinity RO flat sheet membrane towers of the present technology.

[040] FIG. 24 is a cross-sectional view of a multi-staged RO axial flow brackish water desalination tower of the present technology for about 85% recovery

[041] FIG. 25 is a cross-sectional view of a flat sheet membrane vessel utilizing a segmented slip-on pressure vessel shell of the present technology.

[042] FIG. 26 is a side view of the segmented slip-on pressure vessel shell exploded from the flat sheet membrane vessel of FIG. 25.

[043] FIG. 27 is a cross-sectional view of a simplified vertical tower flat sheet membrane seawater desalination plant for large seawater desalination plants of the present technology.

[044] FIG. 28 is a diagram of an exemplary simplified symbiotic osmosis seawater desalination plant of the present technology utilizing multiple trains.

[045] FIG. 29 is a diagram of an exemplary closed ISO power system of the present technology.

[046] FIG. 30 is a diagram of an exemplary closed ISO power system of the present technology utilizing operating units.

[047] FIG. 31 is a top elevational view of an exemplary natural or manufacture geological depression that can be utilized with the present technology.

[048] FIG. 32 is a top elevational diagram of the induced symbiotic osmosis and solar energy renewable energy development of the present technology being utilized with the geological depression.

[049] FIG. 33 is a top elevational diagram of the geological depression being utilized with the induced symbiotic osmosis and solar energy renewable energy development of the present technology.

[050] FIG. 34 is a flow diagram of an exemplary operation utilizing the renewable energy development of the present technology.

[051] FIG. 35 is a top elevational diagram of the induced symbiotic osmosis and solar energy renewable energy development of the present technology being utilized with a geological depression located in Morocco’s Medallion Island.

[052] FIG. 36 is a top elevational diagram of the induced symbiotic osmosis and solar energy renewable energy development of the present technology being utilized with a geological depression located in Great Australian Bight.

[053] FIG. 37 is a flow diagram of an exemplary operation utilizing the renewable energy development of the present technology utilized in FIG. 36.

[054] FIG. 38 is a top elevational diagram of the present technology being utilized with a geological depression located in Gilbert Bay, and a flow diagram of an exemplary operation utilizing the renewable energy development of the present technology in Gilbert Bay.

[055] FIG. 39 is a top elevational diagram of the present technology being utilized with a geological depression located in Mauritania, and a flow diagram of an exemplary operation utilizing the renewable energy development of the present technology in Mauritania.

[056] FIG. 40 is a top elevational diagram of the present technology being utilized with a geological depression located in Alexandria, and a flow diagram of an exemplary operation utilizing the renewable energy development of the present technology in Alexandria.

[057] FIG. 41 is a top elevational diagram of the induced symbiotic osmosis and solar energy renewable energy development of the present technology being utilized with a geological depression located in the Cara Bogaz KOL Sea.

[058] FIG. 42 is a flow diagram of an exemplary operation utilizing the renewable energy development of the present technology utilized in FIG. 41.

[059] FIG. 43 is a top elevational diagram of the present technology being utilized with a geological depression located in the Tunisia Salt Lakes, and a flow diagram of an exemplary operation utilizing the renewable energy development of the present technology in the Tunisia Salt Lakes.

[060] FIG. 44 is a flow diagram of an exemplary operation utilizing a global ISO-Power and Salt Harvesting of the present technology.

[061] FIG. 45 is a geographical cross-sectional view of salt domes in Texas and Caspian that can be utilized in the present technology.

[062] FIG. 46 is a flow diagram of an exemplary operation utilizing a global ISO-Power and Salt Harvesting of the present technology in a salt dome.

[063] The same reference numerals refer to the same parts throughout the various figures.

DETAILED DESCRIPTION OF THE INVENTION

[064] The present subject matter will now be described with reference to the attached figures. Various structures, systems and devices are schematically depicted in the drawings for purposes of explanation only and so as to not obscure the present disclosure with details that are well known to those skilled in the art. Nevertheless, the attached drawings are included to describe and explain illustrative examples of the present disclosure. The words and phrases used herein should be understood and interpreted to have a meaning consistent with the understanding of those words and phrases by those skilled in the relevant art. No special definition of a term or phrase, i.e., a definition that is different from the ordinary and customary meaning as understood by those skilled in the art, is intended to be implied by consistent usage of the term or phrase herein. To the extent that a term or phrase is intended to have a special meaning, i.e., a meaning other than that understood by skilled artisans, such a special definition will be expressly set forth in the specification in a definitional manner that directly and unequivocally provides the special definition for the term or phrase.

[065] In one embodiment, the application provides systems and processes of making same, for efficiently exchanging low or no solute solutions with high or hypersolute aqueous solutions. In one embodiment, the low or no solute solutions are saline solutions. The system may be used in a large variety of processes, including but not necessarily limited to water micro filtration, ultra-filtration, nanofiltration purification (reverse osmosis), extraction, salinity power generation and gas mixture separation (landfill gases as an example), and combinations thereof.

[066] Referring now to the drawings, and particularly to figures 1 -7, known systems and methods are described. Hollow fibers are generally more economical than other types of membrane design. Hollow fibers have the advantage of allowing for a large membrane area per unit volume. Accordingly, hollow fiber systems may be relatively compact systems. As best shown in FIG. 1, the hollow fiber (HF) panel 10 includes a frame 12 comprising a header 16, an opposed header 16a, and the membrane element 3000 retained within the frame 12. The membrane element 3000 includes a HF stack comprising a plurality of loosely packed hollow fibers (HFs) 14 comprising first ends extending through one contact structure 906 and opposed ends extending through an opposed contact structure 906a, each HF comprising an elongated lumen extending between the one contact structure 906 and the opposed contact structure 906a and comprising a hydrophilic semipermeable membrane adapted to achieve salt rejection of 98.5% or more and exhibiting a surface tension of 35 dynes/cm or more. The membrane element 3000 is adapted to be encased in a frame 12 for a HF panel 10 of FIG. 1. The plurality of loosely packed HFs 14 are adapted to be submersed in a first fluid and to sustain turbulence flow across and along surfaces of the plurality of loosely packed HFs 14 at a Reynolds' Number of about 3000 or more

[067] The loosely packed HF s 14 engaged at each end by the first and second contact structure (906, 906a) 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 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.

[068] In one embodiment, the frame 12 may have a variety of shapes (in frontal view) including, but not necessarily limited to circular, elliptical, triangular, and rectangular. In the embodiment shown in FIGS. 1 and 2, the frame 12 is square (in frontal view) and comprises a first header 16 and an opposed header 16a, and a first support 19 and second support 19a. In one embodiment, one or both of the first header 16 and the opposed header 16a have a depth 18.

[069] The plurality of HFs 14 comprises a plurality of loosely packed individual HFs comprising a semipermeable membrane defining a lumen. In one embodiment, the semipermeable membrane is adapted to retain its mechanical integrity at higher feed pumping pressures across the lumens and higher process fluid pressures inside of the lumens compared to low pressure microfiltration and ultrafiltration HF membranes currently in use in the industry.

[070] The stack of loosely packed HFs 14 (the HF stack) in the membrane element 3000 has a width 3002, a height 3004, and a depth 3005. In one embodiment, the HF stack width 3002 is the same as the HF stack height 3004. In one embodiment, the HF stack width 3002 is about 3 meters. In one embodiment, the HF stack has a depth 3005 of from 40 to about 80 mm.

[071] The contact structures 906, 906a or 1006 at each end of the loosely packed HFs 14 have a length 3006, a width 3008, and a thickness 3010. In one embodiment, the contact structure length 3006 is slightly larger than the HF stack width 3002, and 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. 19B. In one embodiment, the HF stack depth 3005 is 40-80 mm. In one embodiment, the HF stack depth 3005 is about ¾ of the contact structure width 3008. In one embodiment, the contact structure thickness 3010 is from about 20 to 60 mm, depending on operating pressure.

[072] The frame 12 has a header 16 and an opposed header 16a. The frame has a frame width 3012, a frame height 3014, and a frame depth 3016. In one embodiment, the frame width 3012 is the same as the frame height 3014. In one embodiment, the frame depth 3016 is from about 1.5-2 times the contact structure width 3008 for proper support of the membrane element 3000.

[073] 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. In one embodiment, the solid structure 1000 is an elongated rectangular structure. The bore 1008 also may have a variety of shapes. In one embodiment, the solid structure 1000 is an elongated rectangular structure with an elongated cylindrical bore 1008 therethrough.

[074] The solid structure 1000 may be made of any suitable material. In one embodiment, the solid structure 1000 is made of steel. In one embodiment, the steel is coated with a suitable corrosion protection material. Substantially any corrosion protection material may be used. In one embodiment, the corrosion protection material is Teflon. In one embodiment, the corrosion protection material is epoxy. In one embodiment, the solid structure 1000 is made of fiber reinforced plastic. In one embodiment, a portion of a side of the solid structure comprises a contact structure 1006 adapted to retain the plurality of HFs 14 in a loosely packed arrangement. The contact structure 1006 may be any suitable material. In one embodiment, the contact structure 1006 comprises a suitable thermosetting material. In one embodiment, the contact structure 1006 is selected from the group consisting of epoxy, polyurethane, and combinations thereof.

[075] In one embodiment, the plurality of hollow fibers 14 extend through a contact structure 906 or 1006 adapted to retain the plurality of HFs 14 in a loosely packed arrangement. The contact structure 906 or 1006. In one embodiment, the contact structure 906 or 1006 comprises a suitable thermosetting material. In one embodiment, the contact structure 906 is selected from the group consisting of epoxy, polyurethane, and combinations thereof. The ends of the hollow fibers 14 empty into the pipe 904.

[076] The actual feed pressure to which the HF panel 10 comprising the HF membrane element 3000 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 equivalentto 46.5 bars. In general, the sustainable feed pumping pressure must be sufficiently high to overcome this osmotic head. For example, in the case of desalination of seawater (3.5% salinity) by reverse osmosis, where concentrated brine leaves at 6% salinity and produces an osmotic pressure of 46.5 bars, the sustainable feed pumping pressure must be higher than the osmotic head of 6%.

[077] The actual feed pressure to which the HF panel 10 comprising the HF membrane element

3000 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 equivalentto 46.5 bars. In general, the sustainable feed pumping pressure must be sufficiently high to overcome this osmotic head. For example, in the case of desalination of seawater (3.5% salinity) by reverse osmosis, where concentrated brine leaves at 6% salinity and produces an osmotic pressure of 46.5 bars, the sustainable feed pumping pressure must be higher than the osmotic head of 6%.

[078] In one embodiment, the semipermeable membrane maintains mechanical integrity at a feed pressure of: 30 bars or higher, 31 bars or higher; 32 bars or higher; 33 bars or higher; 34 bars or higher; 35 bars or higher; 36 bars or higher; 37 bars or higher; 38 bars or higher; 39 bars or higher; 40 bars or higher; 41 bars or higher; 42 bars or higher; 43 bars or higher; 44 bars or higher; 45 bars or higher; 46 bars or higher; 47 bars or higher; 48 bars or higher; 49 bars or higher; or, 50 bars or higher.

[079] As illustrated in FIG. 3, the HF panel 10 can abut an adjacent HF panel having a similar structure. The adj acent HF panel comprises a plurality of hollow fibers. The adj acent HF panel has a square frame comprising a first header and an opposed header, a first support and an opposed support. In one embodiment, the lengths of the plurality of hollow fibers in the adjacent HF panel can be parallel with or at an angle relative to the lengths of the plurality of hollow fibers 14 in the HF panel 10. The lengths two of the plurality of hollow fibers in the adjacent HF panel can be oriented substantially perpendicular to the lengths of the plurality of hollow fibers 14 in the HF panel 10. In this embodiment: the opposed header 16a of the HF panel 10 abuts the first support member of the adjacent HF panel; the header 16 of the HF panel 10 abuts the opposed support member (not shown) of the adjacent HF panel; the support member 19 of the HF panel 10 abuts the first header of the adjacent HF panel; and the support member 19a abuts the opposed header of the adj acent HF panel.

[080] In one embodiment, header 16 comprises a first aperture 22 adjacent to support 19 and the opposed header 16a comprises an aperture 23 adjacent to opposed support 19a. The apertures 22, 23 may have a variety of shapes including, but not necessarily limited to circular, elliptical, triangular, rectangular, and combinations thereof. In one embodiment, the apertures 22, 23 are circular. In one embodiment of a power train, the aperture 22 communicates with a source of process fluid (not shown).

[081] In one embodiment, the HFs are loosely packed between the first header 16 and the opposed header 16a, respectively. In one embodiment, the packing is sufficiently loose for feed to flow across the array substantially perpendicular to the HF panels at a given flow rate and feed capacity without stagnation, but sufficiently tight to provide the desired processing capacity. The frame 12 of the HF panel 10 comprises the headers 16, 16a and the supports 19, 19a, the frame of adjacent HF panel comprises the headers, and the support (and the opposed support, not shown).

[082] The headers and supports comprise a material and structure having sufficient mechanical integrity to retain the plurality of HFs 14 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). Fiber-reinforced plastic (FRP) (also sometimes called fiber-reinforced polymer) is a composite material made of a polymer matrix reinforced with fibers. Common fibers include, but are not necessarily limited to glass, carbon, basalt, aramid, paper, wood, asbestos, and the like. In one embodiment, 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.

[083] Suitable FRP's meet or exceed the mechanical properties of steel. In one embodiment, the

FRP exhibits superior thermo-mechanical properties, is lightweight, is relatively low cost, exhibits corrosion resistance, and is easy to maintain. In one embodiment, headers and supports are made of the same material. In one embodiment, the headers and supports are made of different materials. In one embodiment, the headers and/or supports are made of steel. In one embodiment, the headers and/or supports are made of FRP. In one embodiment, the headers and the supports are made of FRP.

[084] The membrane element and HF panel are useful in a variety of ISO systems and processes. Suitable ISO systems and processes include, but are not necessarily limited to those for ISO power generation, reverse osmosis, desalination, and water extraction from diluted organic, contaminated groundwater and industrial solutions. The HF panel 10 is particularly useful to perform large scale ISO processes. In one embodiment, the process fluid (or fluid inside of the HF lumen) is at a relatively high pressure and the feed (or fluid outside of the lumen) is at a relatively low pressure.

[085] The salinity (or solute concentration) of the process fluid and the feed will vary. The process fluid for an extraction process typically has a moderate salinity. In one embodiment, the moderate salinity is from about 3% to about 7%. The process fluid for osmotic power generation and/or seawater desalination by reverse osmosis will have a low salinity, typically less than about 3%. In one embodiment, the process fluid is at a relatively low pressure and the initial feed is at a relatively high pressure. In one embodiment, the process fluid is at a relatively low pressure of from about 3 bars to about 5 bars and the feed is at a relatively high pressure of from about 10 bars to about 60 bars or more, depending of on feed salinity

[086] FIGS. 4-6 illustrate an enclosure cage capable of enclosing a variety of membrane frame configurations including different configurations and/or widths of HF panels secured in the frame. FIG. 4 best illustrates a Type 1 simple frame layout for small vessels utilizing single size HF membranes that occupy about 64% of the vessel’ s interior volume or section. FIG. 5 best illustrates a Type 2 frame layout for small vessels utilizing two HF membrane sizes that occupies more of the vessel’s interior volume or section than Type 1. FIG. 6 best illustrates a Type 3 frame layout for large exchange surface utilizing multiple HF membrane sizes that occupies more of the vessel’s interior volume or section than Type 2.

[087] Referring to FIG. 7, this illustrates a top cross-section of a stack of flat RO membrane panels. The back and front sides of the frame can be perforated allowing for entry and exit of saline water flow. The sides of the HF panels are capable of allowing a side flow of the saline water.

[088] The above known systems and processes are defined herein and more fully described in U.S. Patent Number 8,545,701; U.S. Patent Number 8,852,432; U.S. Patent Number 9,156,003; and International Application Number PCT/IB2014/058861.

[089] These together with other obj ects of the present technology, along with the various features of novelty that characterize the present technology, are pointed out with particularity in the claims annexed to and forming a part of this disclosure. For a better understanding of the present technology, its operating advantages and the specific objects attained by its uses, reference should be made to the accompanying drawings and descriptive matter in which there are illustrated embodiments of the present technology. Whilst multiple objects of the present technology have been identified herein, it will be understood that the claimed present technology is not limited to meeting most or all of the obj ects identified and that some embodiments of the present technology may meet only one such obj ect or none at all.

[090] Referring now to the drawings, and particularly to FIGS. 8-46, an embodiment of the induced symbiotic osmosis systems and processes of the present technology is shown and generally designated.

[091] In FIG. 8, a new and novel RO membrane 30 of the present technology is illustrated and will be described. More particularly, the RO membrane 30 includes a frame 32 including a top header 34, an opposed bottom header 36, a perforated or porous frame back side 38, a perforated or porous frame front side 40, and one or more flat RO panels 42.

[092] The headers 34, 36 each include a guiding bar 44 extending outwardly therefrom. The frame front site 40 can include a foldable, pivotable, retractable or removable handle 46. It can be appreciated that the handle 46 can be included with the frame back side 38. The guide bars 44 can be configured to be slidable received in a corresponding slot, groove or channel in an enclosure configured to receive the RO membrane 30.

[093] The frame back and front sides 38, 40 are configured to allow saline water to flow therethrough. The RO panels 42 are configured to allow saline water to flow perpendicularly therethrough to create a saline water side flow, and laterally to create a saline water flow between the back and front sides 38, 40 and to the headers 34, 36. The top and bottom headers 34, 36 are configured to operate at or with an external pressure of 1000 psi or greater.

[094] Referring to FIG. 9, the top header 34 defines an interior cavity configured to receive a desalinated water flow from the RO panels 42. A desalinated water outlet 48 is associated with the top header 34 and is in communication with the cavity to provide an outlet flow of desalinated water. The bottom header 36 defines an interior cavity configured to receive a desalinated water flow from the RO panels 42. A desalinated water outlet 50 is associated with the top header 36 and is in communication with the cavity to provide an outlet flow of desalinated water.

[095] A screen 52 can be provided on either side of the RO panel 42, or which is received and/or secured with the top and bottom headers 34, 36. The screen 52 is configured to reinforce and protect the RO panel 42, while allowing side flow of saline water.

[096] In use, saline water inlet flow can enter the RO membrane 30 from the perforated front side

40, then travels across the length the RO panel 42, where the saline water is desalinated into a desalinated water outlet and a brine water outlet flows. The desalinated water outlet flow travels to the top and bottom headers 34, 36 and exits through their corresponding outlets 48, 50. The brine water outlet flow travels toward and exits the frame back side 38.

[097] A RO membrane frame mounting 54 can be utilized to receive one or more RO membranes 30. The frame mounting 54 includes a slot, channel or notch that is configured to longitudinal receive at least one of the frame guiding bars 44. Rollers or ball bearings 56 are associated with the frame mounting 54 to facilitate sliding in/out of the RO membrane 30. It can be appreciated that the frame mounting 54 can be utilized with the top and/or bottom headers 34, 36, and can be used in a stacking configuration to allow multiple RO membranes 30 to be utilized in series.

[098] The handle 46 provides for easy insertion and/or removal of the RO membrane 30 from the frame mounting 54. The edges of the RO panels 42 can be sealed to their respective side frames 38, 40 by a vertical edge epoxy sealing sleeve.

[099] Referring to FIG. 10, a twin RO staked sequential or independent desalination frame is described, which includes a RO membrane pressure vessel 60 that receives ultra-filtered saline water 62 by way of a pump (P) and valve. Inside the pressure vessel 60 is one or more frame enclosures or cages 64 featuring a closed end 66 and an open end configured to slidable receive a connected pair or stacked RO membranes 30.

[0100] The top headers 34 of the twin stacked RO membranes 30 are in communication with a desalinated water top collector header 68. The bottom headers 36 are in communication with a desalinated water bottom collector header 70. The desalinated water collector headers 68, 70 position the twin RO membranes 30 in a spaced apart relationship, while inserted in the enclosure 64.

[0101] The saline water 62 flows into the pressure vessel 60, around the enclosure 64 and into its open end. The saline water then flows through the perforated frame flow entry side 40 of a first RO membrane 30, then passes through the RO panel 42 with desalinated water entering the top and bottom headers 34, 36 and then to their respective desalinated water collector headers 68, 70. Saline or brine water exits the first RO membrane 30v via its perforated frame flow exit side 38, and then enters the second RO membrane 20 by way of its perforated frame flow entry side 38. The saline or brine water then passes through the RO panel 42 with desalinated water entering the top and bottom headers 34, 36 and then to their respective desalinated water collector headers 68, 70. Brine water exits the second RO membrane 30 via its perforated frame flow exit side 40 and exits the enclosure 64 by way of a brine outlet back pressure control 72. [0102] Regarding FIG. 11, this embodiment represents a design of a membrane exchanger for pipe rack installation of a piperack mounted co-current or counter-current hollow fiber membrane module 74, including hollow fiber or flat sheet exchangers for fluids filtration and osmotic processes. The hollow fiber or flat sheet exchangers can be based on rolling a layer 76 (10-15 mm) of segregated hollow fibers or flat sheet membranes, of large width to header depth ratio. The rolled membrane bundle 76 can be inserted or received in conventional membranes cylindrical vessel or shell 77. The bundle 76 can be made by forming a pad of about 10-15 mm of segregated hollow fibers and rolling the pad in the form of a cylinder of a desired diameter, forming a membrane module of several centimeters in diameter (10-30 cm i.e., 4-12 inches). The shell 77 can be rated at around 800 psi operations or greater.

[0103] Such assembly and fabrication of membranes enhance exchanger efficiency, retard fouling and improve membrane cleaning, particularly when the raw water pumping pressure is frequently isolated according to a programed cycle to flush the membrane.

[0104] Segregation of hollow fibers is essential and can be done by randomly distributed, flexible PVC or CPE glued filaments or strips with OD or depth of about 1 mm or less. Then, the assembled rolled membrane module 76 can be inserted in the cylindrical vessel 77 of the type being currently used in osmotic processes. Framed flat sheet membranes may be used in large dimeter vessels, where membrane surface width is significantly wider than the said membrane framing headers.

[0105] The closed vessel 77 includes a low pressure low salinity feed 78, a low pressure high salinity output 80, a high pressure diluted bring high flow 82, and a high pressure high salinity brine flow 84.

[0106] Localized mounted, low pressure reversible flow pumps 86 enhances turbulence and reduce membranes fouling. Flexible PVC, CPE turbulence baffles 88 can be placed inside the shell 77 to further enhance turbulence and reduce membranes fouling. An HF epoxy sheet (potting seal) 90 can be utilized at the ends of the rolled bundle 76, which can seal against an interior surface of the shell 76.

[0107] This ISO Module 74 can be also mounted vertically on a structural base with some modifications of inlet and outlet flow ports. Such system can potentially replace conventional seawater RO rolled membrane sheets.

[0108] In this process, interrupting the desalination cycle for few minutes, will allow some of the desalinated salt free water to reverse flow across the membrane to flush the accumulated sludge on the raw water side of the membrane by“osmosis”, where this sludge would be directed to waste water disposal facility.

[0109] Flat sheet membranes of variable circumferential length, in the form of a continuous folded sheet, or assembly of segregated variable height plates can be also used.

[0110] Operation considerations of the piperack mounting counter-current module 74 can be associated with an osmotic system. Hollow Fiber-ISO Module material is based on food grade polyvinyl chloride (PVC), chlorinated polyethylene(CFE) or equivalent that are used for forming filaments of porous mesh between membrane hollow fiber layers, as well as for providing semi- ridged baffles for controlling flow pattern and prevent areas of stagnation.

[0111] The module 74 can be used potentially in more than one application.

[0112] 1) Power Generation Mode

In the case described earlier, desalinated water crosses membranes from“the low pressure-low salinity tube feed” 78 to“the high pressure, high salinity-high flow rate vessel shell side” 84 by osmosis, where such high flow-high pressure stream can drive a hydraulic turbine to generate osmotic power and low pressure reduced salinity flow.

[0113] 2) Desalination Mode ( = =►): In another case, the same vessel can be used to desalinate brackish and seawater. Here, the outlet of high pressure diluted brine-high flow 82 will be used to flow high rate of brackish water or seawater on the shell side, in a reverse order to the power generation case, where the desalinated water crosses flat sheet or hollow fiber membranes and exists from the low pressure low salinity side 78 and the concentrated brine exists from the high pressure high salinity brine shell side port 84.

[0114] 3) Desalination Mode ( ^=^), the same vessel can be used to desalinate brackish and seawater. Here the diluted high flow brine or seawater and brackish water are pumped in the shell side under pressure to desalinate such stream by reverse osmosis, leaving from the inlet that was used for high pressure, high salinity brine 84, meanwhile desalinated water crosses hollow fiber membranes and exists from the low pressure high salinity brine port 80, as in the case of power generation.

[0115] Here Case 2 and 3 are shifting the side of the exchanger that can be used.

[0116] FIG. 12 is exemplary of the piperack mounting, counter-current module 74, with parallel, same size, hollow fiber ISO modules with 50% desalinated water recovery, per FIG. 11. This system can be also mounted vertically if adequate space is available. Localized flow turbulence are not shown. [0117] In operation, saline water is pumped at 4 volumes into the high pressure salinity flow 84 of each of the parallel modules 74, resulting in each module receiving 2 saline water volumes. The saline water proceeds through each rolled bundle 76, where brine exits via flows 82 at 7.0% brine and 2 volumes. Desalinated water exits from each of the low pressure low salinity sides 78 at 1 volume.

[0118] FIG. 13 is exemplary of the piperack mounting, counter-current module 74, with cascade, variable size, hollow fiber ISO module or flat sheet-ISO module for 67% desalinated water recovery, per FIG. 11. This system can be also mounted vertically if adequate space is available.

[0119] In operation, saline water is pumped at 4 volumes into the high pressure salinity flow 84 of a first of the cascading modules 74. The saline water proceeds through the rolled bundle 76 of the first module 74, where brine exits via flow port 82 at 7.0% brine and 2 volumes, which then enters the high pressure salinity flow 84 of a second of the cascading modules 74. Desalinated water exits from the low pressure low salinity sides 78 of the first module 74 at 2 volumes.

[0120] The saline water proceeds through the rolled bundle 76 of the second module 74, where brine exits via flow port 82 at 10.50% brine and 1.33 volume. Desalinated water exits from the low pressure low salinity sides 78 of the second module 74 at 0.67 volumes.

[0121] Typical membrane modules design of induced symbiotic osmosis power [ISOP] or symbiotic reverse osmosis [SRO] plants employing hollow fiber membrane frame [HFM] or flat sheet membrane (FSM) to sustain flow Reynolds Number of 3,000-3,500. The System can be mounted indoor or outdoor, on piperack, or vertically mounted.

[0122] Referring to FIG. 14, represents an embodiment of a membrane module 92 including axial flat sheet membranes (FSM) of variable flow reverse osmosis scheme, relying on step change in the vessel diameter to sustain flow velocity and avoiding excessive membrane fouling by sustaining Reynolds Number requirement. The module 92 includes a high pressure exchanger shell 94 featuring varying diameter sections, preferable decreasing in size from one end to another end. Each section of the shell 94 encloses a hollow fiber array encasement 96, with each encasement employing Hollow Fiber Membrane Frame (HFM), Flat Sheet Membrane (FSM) or rolled membranes. Each encasement 96 is located within its corresponding section to define an annulus between an outer surface the encasement 96 and the shell 94.

[0123] Typical membrane modules design of ISOP or SRO Plants employ HFM or FSM to sustain flow Reynolds Number of 3,000-3,500. The System can be mounted indoor or outdoor, on piperack, or vertically mounted.

[0124] A hydro turbine low pressure discharge drum 98 feeds high pressure diluted brine into a first HF array encasement of a first diameter, while high pressure high salinity brine is pumped (Pi) from a final HF array encasement 96 via a return line 100. The final HF array encasement has a diameter, which is smaller than the first diameter. The high pressure high salinity brine then travels to a prior cell 102, which dilutes the brine. The high pressure diluted brine from the prior cell 102 to travels to a turbine (T ) which produces electricity, and then exits to the discharge drum 98.

[0125] Diluted brine exits the first FH array encasement 96 via line 104, and then travels to a turbine (T₂) which produces electricity, and then exits to a brine evaporation lake or pool 106. High salinity brine at high pressure is pumped (P₂) from the evaporation lake 106, through a filter, and then enters the annulus of adjacent the first HF array encasement 96. The high salinity brine travels along the annulus to the final HF array encasement and enters the final HF array encasement. The high salinity brine then travels through each cascading HF array encasement 96 where it exits as diluted brine via line 104.

[0126] FIG. 15 represents an agitated axial flat sheet membranes (FSM) variable flow reverse osmosis scheme 110, which can provide fouling control of membranes. This scheme can include horizontal vessels 112 each including a diameter sized to maintain relatively the same velocity in every vessel. Internal circulation pumps (P₂, P₃, P₄, P_?) are utilized for maintaining flow recycle at a Reynold’s number above 3000 to mitigate fouling. Each vessel 112 includes the twin RO staked sequential or independent desalination modules 64 of FIG. 10.

[0127] An automated backflush of the membrane can be achieved with desalinated water, while releasing pressure on seawater supply and returning it to pretreatment. Backflush is activated by inadvertent reduction in desalinated water flow rate, changes in its salinity or changes in seawater pressure.

[0128] Low Pressure (LP) treated seawater can enter a pressure exchanger (PX) 114 for brine pressure power recovery, via a pump (Pi). A control valve (CV) controls the flow of the treated seawater leaving the pressure exchanger 114 to a seawater treatment plant and/or to one of the vessels 112, with control valve being controlled by an attribute of a flow in a connection line leading from the first vessel to the second vessel.

[0129] The high pressure seawater enters an annulus of the first vessel 112, and is processed through the twin RO modules 64, as described above. Desalinated water exits the closed end of the frame enclosure of the first vessel 112 and enters an annulus of the second vessel 112. Internal circulation pump (P₂) recirculates flow from the closed end of the frame enclosure of the first vessel 112 to the space defined between the twin RO membranes 30. While circulation pump (P₃) recirculates flow from the space defined between the twin RO membranes 30 to an area adjacent the open end of the frame enclosure. Desalinated water can exit the top collector header 68 and the bottom collector header 70. The desalinated water exiting the top collector header 68 can be in communication with the bottom collector header 70 of the RO module 68 of the second vessel 112.

[0130] The desalinated water entering the annulus of the second vessel 112 is processed through its twin RO module 64, as described above. Internal circulation pump (P₄) recirculates flow from the closed end of the frame enclosure of the second vessel 112 to the space defined between the twin RO membranes 30. While circulation pump (P₅) recirculates flow from the space defined between the twin RO membranes 30 to an area adjacent the open end of the frame enclosure. Desalinated water can exit the top collector header 68 and the bottom collector header 70.

[0131] High pressure brine exits the closed end of the frame enclosure of the second vessel 112 and enters the pressure exchanger 114, which reduces its pressure and exits as low pressure brine disposal.

[0132] Referring to FIGS.16 and 17, an axial flow vertical well RO flat membrane Typel vessel well 114 for a RO Type 1 membrane 122 is illustrated and will be described. The vessel 114 is configured to receive an enclosure 122 featuring a closed end and an open end. The RO Type 1 membrane 124 is received in the enclosure 122, and it includes one or more RO panels and headers 126, as described above. Ultra-filtered saline water is pumped (P) into an annulus of the vessel 114 to the fill the vessel. Saline water will spill over atop edge of the enclosure 122 thereby entering the RO membrane 124. Desalinated water exits the RO membrane 124 via the headers 126, and then exits the vessel 120. Brine exits from the bottom of the RO membrane 124, and then exits the vessel. Lifting lugs 128 can be utilized with the frame of the RO membrane 124 and/or the vessel 120

[0133] FIG. 18 represents a single or multiple stages for filtration and desalination towers or vertical wells. Axial flow applicable design for macro, micro, ultra and Nano- filtration, as well as present technology osmotic power generation and salinity reverse osmosis employing Type 1, 2 and 3 membrane processes.

[0134] A pressure vessel 130 includes a top retention plate 132, a vessel head 134 (in closed position) covering an open top end of the vessel, and a bottom end drain 136. The vessel 130 can be a polymeric carbon fiber reinforced vessel or equivalent. The vessel head 134 can include a pressure regulating valve (PRV). A flat sheet membrane (FSM) 140 is received in an enclosure or cage 138, which is receivable in the vessel 130. The enclosure 138 and/or the FSM 140 can be supported by a resting mount located adj acent and above the drain 136. The FSM 140 includes a frame and headers 142, as described above. Lifting lugs 144 can be utilized with the enclosure 138, a frame of the RO membrane 140 and/or the vessel head 134.

[0135] Filtered saline water is supplied to an annulus of the vessel 130 via a pump (P) and valve. The saline water fills the vessel 130 and spills over the enclosure 138 and enters into the FSM 140 to be processed as describe above. Filtered water exits the FSM 140 via the headers 142 and then exits the vessel via line 146. Brine exits from the bottom of the FSM 140, and then exits the vessel 130 via a pressure exchanger (PX) as waste. The pump (P) is associated with the pressure exchanger. Brine can further be drained using the drain 136.

[0136] Filtered water exiting the vessel 130 via line 146 is pumped into a second vessel 130, of similar configuration to the preceding vessel. The second vessel 130 includes a multi-stage FSM 150. The filtered water enters and second vessel and is processed in a similar manner to that of the preceding vessel and multi-stage FSM 150. Desalinated water exits the multi-stage FSM 150, while brine exits from the bottom of the multi-stage FSM 150, and then exits the second vessel 130 via a pressure exchanger (PX) as waste. The pump (P) of line 146 is associated with a pressure exchanger (PX). Brine can further be drained from the second vessel using the drain 136.

[0137] Referring to FIGS. 19 and 20, a multi -compartments Type 2 membrane frames and enclosure assembly is illustrated and described. A frame assembly 160 can be utilized for the Type 2 membrane, wherein multiple Type 2 membranes can be utilized in sequence, as best illustrated in FIG. 19. An enclosure or cage 162 can be used to enclose the multiple Type 2 membrane frame assemblies 160, as best illustrated in FIG. 20. The enclosure 162 can include a saline water inlet 164, and a brine or waster outlet 166.

[0138] Referring to FIGS. 21 and 22, a single compartment Type 2 membrane frames and enclosure assembly preferably for desalination fluids of a primarily a single solute/seawater, is illustrated and described. A frame assembly 170 can be utilized for a single Type 2 membrane, as best illustrated in FIG. 19. An enclosure or cage 172 can be used to enclose the single Type 2 membrane frame assembly 170, as best illustrated in FIG. 22. The enclosure 172 can include a saline water inlet 174, and a brine or waster outlet 176.

[0139] FIG. 23 represents an operating train 180. Generally, a train 180 comprises 2-5 sequential hypersalinity reverse osmosis flat sheet membrane towers (HRO-FSM) 182, which can be incorporated for various brine desalination applications. It can be appreciated that these vessels are ideally mounted outdoor, in groups of 3 -5 vessels, depending on the nature and the operating salinity of the process fluids, such as but not limited to, brackish water, seawater, brine or mixed solutions, etc. The towers 182 can include a vessel and multi-stage FSM 184 similar to that illustrated in FIG. 18.

[0140] Ultra-filtered saline water can enter the first tower 182 at 6% salinity, and is processed through the first tower to produce filtered water at 4% salinity. The 4% filtered water exits the first tower and is pumped (P) into a second tower 182, where it is processed to produce filtered water at 2% salinity. The 2% filtered water exits the second tower and is pumped (P) into a third tower 182, where it is processed to produce filtered water at 0.001% salinity.

[0141] Brine exits from the bottom of the multi-stage FSM in the third or final tower 182, and then exits the third tower via a third pressure exchanger (PX) at 6% salinity. The 6% brine then enters the second tower and is further processed by the multi-stage FSM in the second tower 182. Brine exits from the bottom of the multi-stage FSM in the second tower 182, and then exits the second tower via a second pressure exchanger (PX) at 12% salinity. The 12% brine then enters the first tower and is further processed by the multi-stage FSM in the first tower 182. Brine exits from the bottom of the multi-stage FSM in the first tower 182, and then exits the first tower via a first pressure exchanger (PX) at 18% salinity. It can be appreciated multiple towers 182 can be utilized in this train, instead of the three towers illustrated.

[0142] FIG. 24 represents a multi-stages FSM reverse osmosis axial flow brackish water desalination tower 190 with escalating pumping pressure to overcome salinity osmotic pressure rise. Raw water is pumped through a macro, micro and ultra filtration membranes 192, and then passed through a pressure exchanger (PX), before entering the tower 190.

[0143] The tower 190 includes multiple stages of FSM 194 connected in series, with a top FSM receiving the filtered raw water. The filtered raw water is sequentially processed through each FSM stage 194. A pressure exchanger (PX) or circulating pump 196 can be utilized between FSM stages to increase pumping pressure for overcoming salinity osmotic pressure rise. Additional pressure exchanger may be incorporated on each stage to sustain a desired Reynold Number. [0144] Filtered or desalinated water exits the headers from each of the FSM stages 194 and is discharged 198 from the tower 190. Brine exits from each FSM stage 194 and is either used an input for the next FSM stage or is passed through the pressure exchanger (PX) or circulating pump 196, which is then inputted into the next FSM stage. NaCl brine at less than 7% salinity is discharged from the final FSM stage through the pressure exchanger (PX) associated with the filtration membranes 192. The NaCl brine exiting the tower 190 can be passed to seawater RO desalinations.

[0145] FIGS. 25-27 represent a FSM vessel with a segmented slip-on pressure vessel shell, and illustrate an assembly of process and structural sections. Flat sheet membranes 200 can include compartment angular alignment structures 202 located a corners of the FSM 200, as best illustrated in FIG. 25, which includes cross-section of one of the FSM 200. Multiple FSM’s 200 can be stacked one on top of the other and enclosed by the slip-on vessel shell. The slip-on vessel shell includes a vessel’s primary equipment base segment 204, comprising all required connections and operation controls, internal piping not shown.

[0146] A segmented slip-on pressure vessel shell 206 can be positioned over the stacked FSM 200 so at to abut or rest on the base segment 204, as best illustrated in FIG. 26. The shell 206 can include lifting lugs.

[0147] With the shell 206 placed in position over the stacked FSM 200 and secured to the base segment 204, as best illustrated in FIG 27, completion of the tower is complete for use with large seawater desalination plants operating a flows, such as but not limited to, 1-10 m³/sec.

[0148] FIG. 28 represents a simplified symbiotic osmosis seawater desalination plant 210 utilizing multiple trains. Seawater can be pumped at 1-2 m’/sec from a source into a pretreatment/clarification system 212. After which, the clarified seawater is passed through micro and ultrafiltration towers 214. Waste from the pretreatment/clarification system 212 and micro and ultrafiltration towers 214 are discharged 218. The filtered seawater from the micro and ultrafiltration towers 214 can then be stored in feed storage 216.

[0149] High pressure pumps 220 transfers the ultra-filtered water from storage 216 to multiple HSM or FSM trains 222, with operation containment, flow circulation pumps, piping and controls not shown. Desalinated water from each of the FSM trains 222 are directed to storage 224 for use.

[0150] Brine at 28-30% salinity is discharged from each of the FSM trains 222, which is then processed in a brine vacuum evaporation-salt drying / packaging system 226 and/or an osmotic salinity power 228. The farm or plant 200 can include offices 230 and shops/warehouses 232. It is projected that the plant 200 will produce 56E6 m’/yr or l5E9 gal/yr. It is further projected that the brine vacuum evaporation-salt drying / packaging system 226 will produce 1-2 million metric tons per year of food grade salt.

[0151] FIG. 29 represents a closed ISO power system 240 that can be utilized with the present technology plants or farms, the system 240 includes a natural gas backup heater 242 that supplies heated distilled water to a multi-effect evaporator 244. The evaporator 244 discharges distilled water to a distilled water storage 246, with the storage providing distilled water to an osmotic power generation unit 248 and a solar panel array 250. The solar panel array 250 provides distilled water to the natural gas backup heater 242 and/or bypass the backup heater.

[0152] The power generation unit 248 is in communication with the evaporator 244, which then discharges brine into a brine storage 252. The brine storage 252 provides brine to the power generation unit 248.

[0153] FIG. 30 represents closed ISO power system-operating units 260 that can be utilized with the present technology plants or farms. The units 260 includes a parabolic solar panel assembly 262 including the backup gas heater 242 that is configured to receive a flow from a steam drum 266 and/or the distilled water storage 246 via a pump (P) and filter (F). Heated water is then passed to a trim cooling exchanger and multi -effect evaporator assembly 270, which includes multiple staged evaporators 244 and cooling exchangers 268. Heated water sequentially flows through each stage, with a first cooling exchanger 268 discharging to a condition drum 266 of the solar panel assembly 262. The condition drum 266 provides water to the solar panel array 250 via a pump (P), which then provides water to the steam drum 264. Concentrated brine the all the evaporators 244 is collected in the brine storage 252

[0154] The ISO power generation unit 248 includes a 1-2 MW ISO power train featuring multiple cells. Each cell includes a pump (P) and a turbine (T), with a first train receiving brine from the brine storage 252, and discharging from the turbine into an exchanger 274 feeds into the last exchanger 268 of the multi-effect evaporator assembly 270. The power generation unit 248 can receive UV treated water from the water storage 246. The last exchanger 268 can further receive flow from a vacuum vent storage 272 that collects discharge from the evaporators 244.

[0155] Referring to FIGS. 31-34, an exemplary use of the present technology with a natural or manufactured geological depression 300 is illustrated and described. For exemplary purposes, FIG. 31 illustrates the Qattara Depression 300 which is a depression located in northwestern Egypt, specifically in the Matruh Governorate. Natural or manufactured geological depressions, or manmade desert seas located near seawater or saline water source can be beneficial for location of a hypersaline osmotic power project 310. The project 310 is projected to support the life of about 10 million people, relying only on osmotic power and solar energy. Additional locations suitable for the project 310 can be found in, but not limited to, the United States, Africa, Middle East, East Europe, North Asia and Australia.

[0156] The project 310 is projected to generate 6,000 MW of renewable power by symbiotic osmosis, wind and solar power, and to produce up to 100 million cubic meter of desalinated water per day (1157 m/s). This flow equates to 41% of the allocate Egypt’s discharge rate of 2.800 m³/s to the Aswan Dam. Additional benefits from the project 310 is the constructing a man-made lake for marine life, the opportunity to create a man-made, inland marine resort, developing 150 Km of leisure lake shores south of the Qattara Sea, cultivating one million acres of developed land for various crops, no salt deposit formation or accumulation is allowed in all water ways, no combustible hydrocarbon is allowed without sequestration of emissions, no emission of regurgitating farms animals is allowed without controlled facilities, preventing the use of animals in farm work; i.e., plowing, rolling carts, etc., and venting clean carbon dioxide, not contaminated with industrial gases, is needed for vegetation.

[0157] The plant or project 310 can include a natural or manufactured cannel, waterway or pipeline 312 from the water source to a natural or manufactured lake or sea 314. In the surrounding area of the sea 314, there could be towns and cities 318, farming land 320, an industrial district 322, and wind farms 324, as best illustrated in FIG. 32.

[0158] In this Qattara example, as best illustrated in FIGS. 33 and 34, the sea 314 would result of about 150 km of seashore, and would store 8,820 km² of seawater having 4-4.5% salinity. The sea 314 could have a level of around 20 m below the seawater source. The seawater would flow into the sea 314 at around 2,570 m³/s with 3.5% salinity. An ISO-RO system 316 can be in communication with the waterway 312 to produce 600 m³/s of desalinated water.

[0159] A dam 326 would separate the sea 314 and create a brine lake 328. The brine lake 328 could be 6,905 km². Seawater at 4-4.5% salinity from the sea 314 could be pumped into a raw water treatment plant 330, and then passed through a heat exchanger 332 at 2,400 m³/s. After the heat exchanger, the seawater could then be passed through a horizontal sun -tracking parabolic solar train 334, which discharges into a solar desalination plant 336 in vertical orientation. Potable water from the solar desalination plant 336 could then pass through a turbine and heat exchanger 338 for use. It is projected that 1,800 m³/s at 0.01% salinity of potable water will be produced per day.

[0160] Brine at 600 m³/s and 16-18% salinity from the solar desalination plant 336 could be discharged through the heat exchanger 332 and to the top of the dam 326 or into the brine lake 328. The brine lake can be communication with a salinity adjustment pond 340. The brine lake 328 could have a level of around 40 m below the seawater source.

[0161] Brine water can discharge using a pumping station from the brine lake 328 back into the seawater source or other location at a rate of 300 m³/s with a maximum salinity of 32%. The discharged brine water can be diverted to an osmotic 3,000 MW ISO power generation unit 342, which receives seawater source from the waterway 312 and discharges seawater back into the seawater source at 1,050 m³/s with 5% salinity. Brine from the power generation unit 342 could discharge back to the dame 326 by way of a secondary waterway system 344 at 600 m³/s with 8.25- 16% salinity. Brine, or a portion thereof, from the secondary waterway system 344 can be diverted to the salinity adjustment pone 340 to assist in adjusting the salinity of the brine discharged back into the brine lake 328 via the secondary waterway system 344.

[0162] During a typical summer operation, a conceptual ISO plant model for the project 310 is rated at producing 3.0 GW, with low winter evaporation reducing the power output. The power plant associated with the project 310 could comprise 15 trains of 250 MW each. Energy produced for 6 summer months is estimated at 13 billion KWH. Power generation efficiency of the ISO train could exceed 50%.

[0163] The present technology relies only on natural renewable resources to achieve the above goals, while utilizing seater, saline water and/or salt as a source of energy. The above Qattara example is one possible geographical location to implement the present technology plant. FIGS. 35- 44 illustrate examples of other geological depressions with their corresponding systems and power plant.

[0164] The basic scope of the of generating osmotic power from the Qattara depression (Egypt) will be partitioned into two sections. The southern section can be used as a regular marine life habitat filled with seawater and a massive development to support human life. The northern section where salt water is concentrated by evaporation to reach salinity of -26% then exchanging this brine with seawater -3.5 salinity, across an ISO Power Systems that will be located at the north edge of the depression to generate electric power.

[0165] In this proposal, the Qattara Depression is only acting in its northern section as a large open vessel to facilitate evaporation of water to reach salt saturation point.

[0166] As the high salinity brine is exchanged with seawater via ISO Power generation system at the Northern edge of the depression to generate osmotic power. It can be appreciated that large amount of salt can be recovered for consumption or sale.

[0167] This generated osmotic power can be partially used to desalinate seawater for consumption and meet the demand of various agricultural, commercial and residential applications but as important circulate water from the Southern section of the Qattara to the Northern section of the depression to sustain marine life habitat.

[0168] Table 1 provides further exemplary locations that may include a depression near a saline water source, including estimated osmotic power potential of several worldwide hypersaline domains.

Table 1 [0169] Referring to FIG. 45, salt domes, as those located in Texas, USA and the Caspian Basin for example, can be utilized with the present technology for desalinated water and power production and salt harvesting. An exemplary plant utilizing these salt domes is best illustrated in FIG. 46. An injection and production well is introduced into the salt dome, where warm or hot seawater and/or potable water is injected into the salt dome. Brine is formed in the salt dome from the dissolving salt and injected water. The brine can then be produced at 1 m³/s at 26% brine, which then can enter a water treatment system.

[0170] The treated brine can then enter one stage of an ISO-powertrain of the present technology as discussed above at 4 m³/s and 6.5% brine. The other end of the power train is introduced with seawater or potable water at 3 m³/s and 7% brine. The power train can include multiple cells or generating estimated power of 10 MW at 1 m³/s of 26% brine.

[0171] The seawater or potable water exiting the power train can be combined with the brine exiting the power train to create a flow at 7 m³/s and 6.7% brine. This flow then can enter a solar salt harvesting or vacuum evaporation enclosure, where salt can be harvested.

[0172] Other minerals capable of being utilized by the present technology are sodium chloride or potassium chloride with a dominant mineral being sylvite mixed with halite (sodium chloride), which forms a mixed mineral called sylvanite.

[0173] The maj ority of the produced potassium chloride is used for making fertilizers. Potassium chloride is extracted from minerals sylvite, camallite, and potash, as well as extracted from salt water. The vast majority of potassium chloride is produced as agricultural and industrial grade potash. Regarding osmotic potential of potassium chloride, it can generate osmotic power, but at 78% of sodium chloride as a result of its higher molecular weight than that of sodium chloride.

[0174] In 2017, worldwide production of salt amounted to some 280 million metric tons. In that year, China was the leading salt producer worldwide with the production of 58 million tons. Thus potential for the utilization of salt with the present technology is apparent.

[0175] Generally, one cubic meter of seawater (about 1026 kilogram) of seawater contains 33-37 kilogram of salt with an average of 35 kilogram.

[0176] Based on osmotic power potential simulation of exchanging sodium chloride brines with low salinity waters 1-3.5%, the net osmotic power generation can range between 15-20 megawatt per one (1) cubic meter-Second of saturated sodium chloride solution, where 4 m³/s @ at low Salinity Water of 1-3.5% is exchanged through semipermeable with 1 m³/s @ 26% Salinity. [0177] The world’ s recovered salt from seawater in 2017 is estimated at 280 million metric tons. The amount of seawater used to recover this quantity of salt is estimated at 8 billion (8 xl09) cubic meter in that year, or 253.7 cubic meters /second of seawater containing 8,879 kilogram of salt (3.5% salinity). This seawater was generally accumulated in evaporation ponds to reach saturation of 26%, resulting in producing salt at a rate of 34.5 cubic meter /sec.

[0178] Megawatt is generally the units in use for measuring osmotic power potential in large systems: One megawatt equals one million watts, or 1,000 kilowatts, roughly enough electricity for the instantaneous demand of 750 homes at once. That number fluctuates (some say one megawatt is enough for 1,000 homes) because electrical demand changes based on the season, the time of day, and other factors.

[0179] Salinity of 280 million metric tons is equivalent to 1120 million metric tons of saline solution @ 26 % salinity and at a rate of 34.5 cubic meter/sec, potentially generating net osmotic power of 15 MW or more per 1 m³/s. At a rate of generating osmotic power of 15 megawatt per one 1 cubic meter- second, estimated system osmotic power potential is (15 MW/l m³/s x 34.5 m³/s = 518 megawatt, which can provide power to about 500,000 home, potentially occupied by 3-6 million people.

[0180] Megawatt is generally the units being used for measuring osmotic power potential in large systems. One megawatt equals one million watts, or 1,000 kilowatts, roughly enough electricity for the instantaneous demand for several hundred homes. Some claims that one megawatt can meet the demand of 1,000 homes, because electrical demand changes based on the season, the time of day, and other factors. With the average power per capita, worldwide is just 309 watt.

[0181] Generating osmotic power relies on large land depressions in proximity to the sea, where it can be filled with seawater and concentrated by solar energy and dry atmosphere and then exchange accumulated brine with seawater via semipermeable membranes to generate osmotic power. The process employs a high salinity osmotic power generation train, as discussed above utilizing the present technology.

[0182] It is also worth mentioning that the number of countries near or connected to a saltwater source or sea exceeds 200 with sea shores of 1,634,701 kilometers long. It seems very prudent that many of these countries, particularly in moderate temperature zones, could consider excavating one or more square kilometer from their land for the purpose of starting seawater brine basins for power generation utilizing the present technology. [0183] Confirmation of such concept, could lead to a massive expansion in using salt water for osmotic power generation on a global level by almost every country.

[0184] These proposed basins can be 2-5 meters deep of stabilized surface and with looped flow passes, to produce brine at 20-26 % salinity by solar evaporation. Each basin can be fitted with one or more simple osmotic power generation systems of 1-5 megawatt to generate free osmotic power for general community services; hospitals, schools, offices, and potentially residential buildings.

[0185] As a criterion for designing and operating such enclosed basins, few basic functions are required for managing seawater and brine:

1. An existing natural land depression, or a stable substrate of large section of land that can be excavated and filled with seawater and allow it to evaporate to reach almost saturation point @ 26% salinity is a basic requirement for such process.

2. A semipermeable membrane apparatus, comprising a hydraulic turbine system is employed to exchange the salt water of 26% salinity that is generated by evaporation in the land depressions in step (1), with fresh stream of seawater to produce relativity large diluted flow stream at high pressure that can drive a hydraulic turbine to generate electric power. As well as generating a large flow of low salinity brine, that can be re-concentrated by evaporation in the land depression, as mentioned earlier.

3. Hydraulic Turbines that are capable of recovering osmotic pressure, as it is formed as a water head when water permeates across a semipermeable membrane from low salinity water to high salinity water that is being concentrated, in the basin, by natural evaporation from seawater. Expected power generation is about 15 MW of power, but could be higher, as a result of exchanging one cubic meter of brine @ 26 salinity with 3 m’/sec of permeated salt free water from seawater feed of 6 m’/sec.

4. This proposal could be an additional option to curb global warming and prevent global drawing by sea rise, meanwhile provide a new important source of potable water for the occupants of seashores.

[0186] With the above present technology in mind, we covered the design of desalination and power generation systems. Particularly, multi-cell membranes in the form of self-standing towers (like distillation towers in chemical plants), equipment arrangement and source of water supply, etc.

[0187] It has been mentioned that the net recovered power is 15 MW at 1 m³/sec of from high salinity brine namely seawater. It can be appreciated that the power recovery could be higher, as shown and discussed above, with four membrane cells particularly if brackish water is used instead of seawater. In this case, the train may comprise five cells.

[0188] On the other hand, if the present technology is designed with a system for lower salinity water source, i.e. underground water with 15% salinity, the power recovery will be much less and the power train may comprise only 3 cells.

[0189] The use of solar power to generate electricity is large to run the present technology. The proposed system relies on integrated photovoltaic and salinity ISO Power for continuous energy supply in harsh environment, such as but not limited to the Sahara Desert, which is very hot during the day yet cold at night. The proposed system is solar tracking, water-cooled, self-cleaned, and day and night operation.

[0190] While embodiments of the induced symbiotic osmosis systems and processes have been described in detail, it should be apparent that modifications and variations thereto are possible, all of which fall within the true spirit and scope of the invention. With respect to the above description then, it is to be realized that the optimum dimensional relationships for the parts of the invention, to include variations in size, materials, shape, form, function and manner of operation, assembly and use, are deemed readily apparent and obvious to one skilled in the art, and all equivalent relationships to those illustrated in the drawings and described in the specification are intended to be encompassed by the present technology.

[0191] Therefore, the foregoing is considered as illustrative only of the principles of the invention. Further, since numerous modifications and changes will readily occur to those skilled in the art, it is not desired to limit the invention to the exact construction and operation shown and described, and accordingly, all suitable modifications and equivalents may be resorted to, falling within the scope of the invention.

Claims

CLAIMS What is claimed is:

1. An induced symbiotic osmosis system for symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis, the induced symbiotic osmosis system comprising:

at least one reverse osmosis membrane assembly configured to receive saline water or brine, the membrane assembly including at least one hollow fiber or flat sheet membrane and at least one header configured to receive desalinated water from the hollow fiber or flat sheet membrane;

a frame having an open end configured to receive the membrane assembly; and a shell configured to receive and enclose the frame and the membrane assembly so that an annulus is created between the shell and the frame allowing the saline water or brine to flow into the open end of the frame and through the hollow fiber or flat sheet membrane, the shell including a waste collecting section configured to receive an effluent from the hollow fiber or flat sheet membrane.

2. The induced symbiotic osmosis system according to claim 1, wherein the membrane assembly includes multiple interconnected hollow fiber or flat sheet membranes to create stages in the shell, with the header of each stage being in communication with each other.

3. The induced symbiotic osmosis system according to claim 2, wherein the shell is a tower with the multiple stages being stacked in a vertical relationship.

4. The induced symbiotic osmosis system according to claim 1 , wherein the system is a train including multiple sequentially connected shells, with each of the shells including the membrane assembly and the frame.

5. The induced symbiotic osmosis system according to claim 4, wherein the desalinated water of a first of the shells in the train is transferred in sequence to each succeeding the shell until exiting a last of the shells in the train, with the effluent of the last of the shells is transferred in sequence to each preceding the shell until exiting the first of the shells.

6. The induced symbiotic osmosis system according to claim 5 further comprises a pump associated with the transfer of the desalinated water, and a pressure exchanger associated with the transfer of the effluent, each of the pressure exchanger is in operable association with the pump of the same the shell.

7. The induced symbiotic osmosis system according to claim 1 further comprises an effluent processing system configured to receive the effluent from the shell, the effluent processing system being one of a brine vacuum evaporation-salt drying system, and an osmotic salinity power system.

8. The induced symbiotic osmosis system according to claim 1, wherein the shell receives the saline water or brine from a geological depression that is in communication with a saline water source.

9. The induced symbiotic osmosis system according to claim 1 further comprises a filtration system configured to filter the saline water or brine prior to entering the membrane assembly.

10. The induced symbiotic osmosis system according to claim 1, wherein the hollow fiber or flat sheet membrane includes a membrane frame including rollers configured to slidably move the membrane assembly in or out of the frame.

11. A method of induced symbiotic osmosis, the method comprising the steps of:

preparing a geological depression for receiving saline water;

communicating the geological depression with a source of saline water, the geological depression being at an elevation lower than the source;

desalinating the saline water utilizing a reverse osmosis system comprising a tower enclosing at least one hollow fiber or flat sheet membrane including at least one header configured to receive desalinated water from the hollow fiber or flat sheet membrane, and a frame having an open end configured to receive the membrane assembly, wherein an annulus is created between the tower and the frame allowing the saline water to flow into the open end of the frame and through the hollow fiber or flat sheet membrane; and

discharging brine effluent from the tower into brine storage.

12. The method according to claim 11 further comprises a solar desalination system configured to receive saline water from the geological depression and convert the saline water to desalinated water and brine water, with the brine water being discharged into the brine storage.

13. The method according to claim 11 further comprises an osmotic power generation unit configured to create electrical power by receiving and utilizing saline water from the source and brine water from the brine storage.

14. The method according to claim 11, wherein the brine storage is a portion of the geological depression formed by a dam separating the geological depression.

15. An induced symbiotic osmosis processing plant system comprising: a geological depression in communication with a source of saline water, the geological depressing being configured or configurable to receive saline water from the source; an induced symbiotic reverse osmosis system comprising a tower enclosing at least one hollow fiber or flat sheet membrane including at least one header configured to receive desalinated water from the hollow fiber or flat sheet membrane, and a frame having an open end configured to receive the membrane assembly, wherein an annulus is created between the tower and the frame allowing the saline water to flow into the open end of the frame and through the hollow fiber or flat sheet membrane; a brine storage configured or configurable to receive brine water from the induced symbiotic reverse osmosis system; and

an induced symbiotic osmotic power generation unit in communication with the source and the brine storage, the induced symbiotic osmotic power generation unit being configured to create electrical power by receiving and utilizing saline water from the source and brine water from the brine storage.