METHODS OF MAKING FLAT SHEET MEMBRANE ELEMENT ADAPTED FOR USE IN SYMBIOTIC FLUIDS FACTIONATION, WATER TREATMENT, AND OSMOTIC PROCESSES
The present application introduces design methodology and manufacturing procedures employing conventional permeable and semipermeable membrane flat sheet membrane apparatus [FSM], adapted for use in symbiotic fluids fractionation, water treatment, symbiotic osmotic processes of brine desalination and osmotic power generation, where flat sheet membranes are manufactured in the form of plurality of spaced apart, encaged self-supported unrolled membrane of flat surface panel (leaf) in three (3) categories, including; methodology for assembly of pre-cut flat sheet membrane panels, tube-like blown or rolled membrane film methodology, and blanketing membrane sheet methodology. Further assembling these flat sheet membranes in large membrane frames, where symbiotic reverse osmosis or symbiotic osmosis power generation membrane panels varies from about 250 mm (˜10 inch) to 1.00 m (˜40 inch) in width and 250 mm to 2.00 m (˜10-80 inch) in length or larger for a new unique approach in desalinating various water salinity sources. Where, desalinated seawater recovery can exceed 85%, where water and chemicals can be recovered for reuse in Ecologically Sustainable Hydraulic Fracturing [ES-FRAC] processes of underground waters, and where generating osmotic power from brines can be achieved at 10-25 KW/liter-sec, depending on the source.
The inventor's U.S. Pat. Nos. 8,545,701, 8,852,432, 8,974,668, 9,156,003 and PCT/IB2014/058861 are all deals with Induced Osmotic Potential [ISO] for salinity power generation employing hollow fiber membranes.
THE FIELD OF THE INVENTIONThe current invention is intended to expand this field of technology by employing conventional Flat Sheet Membranes not only in the broad field of symbiotically harnessing the potential of aqueous electrolytic solutions by means of the natural phenomenon of osmosis, but also for fractionation of hydrocarbon and industrial gases, microfiltration, ultrafiltration and nanofiltration, as well as all processes that are based on hollow fiber or spiral wound membranes. In essence, it is the inventor's attempt to standardize many of the technologies for molecular exchange or manipulation of fluids that are currently in use in water, solutions and gases technologies in just one adaptable technology.
Specifically, the invention introduces a unique process concept applicable in several processes including maximizing power generation, as in the case of Induced Symbiotic Osmosis [ISO] for salinity water power generation, seawater desalination recovery of 75% or higher, hypersaline water reverse osmosis, heatless solutes recovery by means of chemical potential dissimilarity of solutions, as well as fractionation of gases based on the kinematic diameters of molecules, employing series of semipermeable flat membrane cells operating in symbiotic fashion, where each process is formed of closed hydraulic loops operating within a concentration potential field.
In regard to osmosis, this invention particularly promotes the design of Large Scale Renewable Resources (LSRR) anywhere natural or manmade physical domains or ecological topography allows for cycling of waters of dissimilar salt concentration, preferably via accumulation-evaporation by natural renewable resources. This invention allows for generating power from world endorheic (dead ended) saline water, salt deposits, saline aquifers, dry salt lakes, formulated ionizable Inorganic salt solutions, as well as with a fully closed ISO systems relying essentially on daily solar heat cycle.
Semipermeable membranes are effective and economical process for water purification or desalination by osmosis. However, current semipermeable membranes technologies, particularly for seawater (3.5% salinity) desalination are limited to two types of commercial designs; spiral wound of flat sheet membrane and hollow fiber membrane, where the later type membrane is monopolized by only one Japanese company. Regardless, the inventor offers several other technologies and applications that employ the currently manufactured flat sheet membrane. However, these flat membranes have to be structured, assembled and operated as rectangular frames of multi-panels or leaves to meet the inventor's vision for developing several new water and gases novel applications.
this invention pertains to Permeable and Semipermeable Flat Sheet Membranes (FSM) novel applications such as:
1. Agitated Axial Flow Reverse Osmosis,
2. Agitated Oscillating Flow Reverse Osmosis,
3. Agitated Axial Flow Vertical Wells Reverse Osmosis,
4. Agitated Axial Flow Underground Vertical Wells Reverse Osmosis,
5. Induced Symbiotic Osmatic [ISO] For Salinity Power Generation,
6. Symbiotic Hypersaline Water Reverse Osmosis,
7. Induced Symbiotic Osmosis (ISO) For Solutes Recovery/Fluids Concentration,
8. Symbiotic Gases Fractionation Processes.
Definitions of Claimed InventionIn aqueous solution, osmosis is the spontaneous movement of water, through a semipermeable membrane that is permeable to water but impermeable to solute, where water moves from a solution in which solute is less concentrated to a solution in which solute is more concentrated.
the driving force of the flow movement is the difference in the chemical potential on the two sides of the semipermeable membrane, with the solvent moving from a region of higher potential (generally a lower solute concentration) to the region of lower potential (generally higher solute concentration).
“Chemical Potential” appears to be an ambiguous and elusive terminology. In fact, it is one of the most important partial molar quantities. It is the energy potential associated with the activity of the ions of an ionizable substance. It is equal to the rate of change of system's free energy, known as “Gibbs Free Energy”, of a system containing a number of moles of such substance, when all other system parameters; temperature, pressure and other components are held constant. Simply, chemical potential is a form of energy like other kinds of potential; electrical, gravitational, momentum, magnetic, surface tension, etc. where, it is spontaneous and in the direction from high to low.
the difference in chemical potential of a substance in two adjacent phases separated by a semipermeable membrane determines the direction in which the substance diffuses spontaneously. When the components of a mixture have the same chemical potential no chemical transport or reaction takes place, and no mutual diffusion will occur, because there is no driving force. The chemical potential is an intensive property of a substance in a phase.
to prevent this movement of water across the semipermeable membrane, a pressure has to be imposed to equalize the force created by the difference in the chemical potential of the solution across said membrane. This force is named osmotic pressure. If the imposed pressure exceeds this limit, then water begins to flow from the region of higher solute concentration to the region of lower solute concentration. In this case, the force is named reverse osmosis pressure.
regarding the title of this invention, the inventor believes that osmosis is nature's one of the two gifts to life; Photosynthesis and Osmosis. It is the vehicle to transport fluids in all living cells and without it, all biological functions and all forms of life cease to exist! This phenomenon is attracting the attention of researchers as a means to generate power. They tend to describe it in industrial terms such as forward osmosis, ordinary osmosis, direct osmosis, pressure retarded osmosis, etc.
In order to harness this natural phenomenon, the inventor believes that relevant potential fields should be established to induce and bring about the wonders of this phenomenon. Therefore, the inventor prefers to describe all applications that utilize the power of osmosis for the benefit of mankind as “Induced Osmosis”.
Further, the term “Symbiosis” although a biological phenomenon, its generic or metaphorical concept refers to a mutually relationship of cyclic reverberation, without altering or modifying any of the specific components of the involved systems. In industrial applications, symbiosis is a process whereby a waste or less valuable byproduct in one industry is turned into a resource for use in one or more other industries. In essence, Symbiosis is the process of optimizing functions of interrelated systems and achieves their ultimate availability.
Therefore, the inventor is naming the process of using osmosis to transfer water spontaneously from low salinity water to high salinity water across a membrane in interrelated sequence of cells as “Induced Symbiotic Osmosis” and is abbreviated here by the acronym “ISO”.
DETAILED DESCRIPTION OF THE INVENTIONthe proposed technology introduces rather new unique approach to desalinate or recover energy from hyper saline waters and entitled “Induced Symbiotic Osmosis Process [ISO]”. ISO comprises series of cells, each forming a closed hydraulic loop comprising pumping and power recovery; generation turbine or pressure exchanger, sharing semipermeable membranes between pre and post cells. Here, each cell is charged with brine of specified salt quantity and type, operated at progressively increasing concentration and osmotic pressure ratio, all cells in the series function simultaneously in symbiotic mode. Transport within cells is chemically driven under the influence of concentration potential field bounded by water of low salt concentration (LC) and by natural or manmade brine of high salt concentration (HC), thermodynamically approaching reversibility between cells.
this invention is rooted in the field of physics and pertains to the development of a chemical engineering conceptual process design, presenting new vision in the energy field. The inventor believes that understanding the basic physics and thermodynamics pertain to solutions and osmosis and their industrial application in this alternative green energy field have comprehensive value in appreciating this proposed technology. Therefore, it is the objective of the inventor to present his vision in concise, simple presentation and easy to follow explanation of the subject process, without entanglement in equipment and parts numbers. Further, all operating conditions and units of measurement and analyses are clearly defined and stated to avoid controversial opinions when relevant arts are examined. This application is rather large and it is the intention to describe it in logical steps starting with theoretical and mathematical background, substantiated with examples and analytical evaluation, then followed by several large scale potential applications of different complexity.
the first law of thermodynamics rules out the possibility of constructing a machine that can spontaneously create energy. However, it places no restrictions on the possibility of transferring energy from one form into another.
Then, osmotic pressure mathematical general form can be presented as:
Δπ=Δp=RTΔCs (Eq. 01)
The osmotic pressure it was originally proposed by Nobel Laureate Van't Hoff and modified to include Staverman's osmotic reflection coefficient to become;
π=ΦicRT (Eq. 02)
π=osmotic pressure or force imposed on the membrane given in bars, atm, psi, etc.
Φ=Osmotic Reflection Coefficient (NaCl=0.93, CaCl2=0.86, Mg CaCl2=0.89, etc.),
i=Ions concentration per dissociated solute molecule (Na+ and Cl− ions=2),
c=molar concentration of the salt ions,
R=gas constant (0.08314472 liter bar/(k·mol)),
T=ambient temperature in absolute Kelvin degrees (20° C.+273°=293° K).
In the case of sea water, the amount of average concentration of oceans salt is about 3.5% (35 gram/liter) mostly in the form of sodium chloride (NaCl). For simplicity of calculation, it is assumed that seawater contains 35 grams NaCl/liter. The atomic weight of sodium is 23 grams, and of chlorine is 35.5 grams, so the molecular weight of NaCl is 58.5 grams. The number of NaCl moles in seawater is 35/58.5=0.598 mol/liter and the osmotic pressure of seawater is
π=[0.93][2][0.598 mol/liter][0.08314 liter·bar/(k·mol)][293 K]=27.11 bar
Since one bar=100,000 Pascal (Pa) and one kilogram (force) per square centimeter (kgf/cm2)=98066.5 Pascal, computation of osmotic pressure, π and energy, SWE, LWE can be presented in several forms:
π=[27.1×105 Pa]/[98066.5 Pa/(kgf/cm2)]=27.63 kgf/cm2
π=[27.63 kgf/cm2][m/100 cm][1000 cm3/liter]=276.3 kgf·m/liter
SWE=[276.3 kgf·m/liter][9.80665 Joule/kgf·m]=2711 Joule/liter=2.711 MJ/m3 a.
SWE=[2711 Joule/liter][1 cal/4.184 J][1 kcal/1000 cal]=0.6479 kcal/liter b.
SWE=[2711 Joule/liter][1000 liter/m3]=2.710 MJ/m3=0.751 kWh/m3 c.
In case of generating power continuously (1 m3 per sec, every second per day), which is the case with power generation systems, the theoretical potential power capacity of this system is:
[2.711 MJ/m3][1 m3/s][3600 s]=9.759×109J=[9.759×109 W·s][h/3600 s]=2,711 kWh d.
SWE=[2,711 kWh][24 hrs/day][365 days/year]=23.75×106 kWh annually. e.
In the case of hyper saline lake such as in Gunnison Bay of the Great Salt Lake-USA, the amount of average salt concentration is about 24% (240 gram/liter) mostly in the form of sodium chloride (NaCl). Lake water osmotic pressure is calculated as:
π=[0.93][2][4.1026 mol/liter][0.08314 liter·bar/(k·mol)]·[293 K]=185.88 bar
For continuous power generation by exchanging Gunnison Bay brine with Bear River fresh water, at a rate of 1 m3 per sec, the theoretical potential power capacity of the lake water (LW) of such system where; 1 W=J/s, 1 W·s=J, 1 kWh=3.6×106 J, then:
LWE=[18.2286 MJ/m3][1 m3/s][3600 s]=[65.623×109J][1 kWh/3.6×106J]=18,228.6 kWh
LWE=[18,228.6 kWh][24 hrs/day][365 days/year]=159.682×106 kWh/year.
For membrane selection in osmotic processes, several types of semipermeable membranes such as stirred cell membrane, flat sheet tangential flow membrane, tubular membrane, spiral-wound membrane and hollow fiber membrane can be used for the ISO technology applications. In this invention, high pressures Semipermeable Flat Sheet Membranes (SFSM) that are intended for seawater and brine desalination are being adopted. Such membranes should operate with salinity that is less than salt saturation point to minimize concentration polarization, as well as maintaining relatively even flow distribution through the flat membrane panels.
Commercially available permeable and semipermeable flat sheet membrane elements of conventional sizes (generally 40 inch×60 inch, ˜1.0 m×1.5 m), or commercially available suitable membrane of other sizes are being adopted in this invention for water filtration, gases fractionation,
brackish water and seawater desalination, fluid extraction and solute recovery, symbiotic salinity power generation, symbiotic Hypersalinity reverse osmosis, where flat sheet membrane elements are adapted for use as flat plates in the form of rectangular panels, mounted in rectangular frames comprising top and bottom water collecting headers, where said frames assembly is mounted within one or more sequential or parallel pressure vessels.
In case of water desalination, the membrane elements are subjected externally to pressurized untreated water at a pumping pressure that is higher than its osmotic pressure, as in case of reverse osmosis, where treated water is collected in the frame headers and transported to storage for future use, while the rejected saline water outside the membrane is disposed.
In case of osmotic power generation, the membrane elements are subjected externally to saline water operating at a pumping pressure that it is relatively less than its osmotic pressure, to enhance treated low or no salinity water flowing in the frame headers to be induced spontaneously across the flat semipermeable membrane into the saline water, where the combined flows of both the saline water and the permeated induced water, being at the initial saline water pumping pressure, is circulated through a turbine to generate power that exceeds the power that is consumed to pump the saline water. The same cycle is repeated in the subsequent cells, but at different concentrations and pumping pressures.
The subject technology is adaptable to the various specifications of flat sheets membranes and is a companion technology to the inventor's U.S. Pat. No. 8,974,668 for hollow fiber applications.
Concentration polarization results of accumulation of dissolved salt at the membrane surface, creating relatively high localized osmotic gradient, reducing osmotically driven normal permeate diffusion and hinders membrane flux. However, since ISO cells are charged with circulated brine of formulated salt content in closed loops, membranes are less susceptible to concentration polarization. Pretreatment is required for inlet water feed, particularly when organic fouling is anticipated. In general, membranes operating in induced osmosis mode are less susceptible to this phenomenon due to the low pressure imposed on membrane as compared with membranes in reverse osmosis service.
Energy, as equated to the water head, of this stream is now higher than the potential energy of the seawater feed, where it is preferentially used to generate energy.
Symbiotic Osmosis Power Generation is a grassroots technology. Inventor's U.S. Pat. No. 8,545,701 should be consulted in any attempt to evaluate the potential of the various domains. Since the objective here is to generate power, each system must be analyzed based on equitable and technically sound criterion to determine validity of assumptions and merits of such processes. Therefore, several parameters and means of measurements are defined by the inventor in the following to facilitate systems simulation:
Specific gravity, SG is estimated at 20° C., using the inventor's following relation:
[SG=1+0.0077×C %],
where C is salt concentration in the form of sodium chloride, since saline waters contain mostly this salt.
Turbine Energy (MJ)=(η)(ρ)(g)(h)(Q),
where η: turbine efficiency (<1.0), ρ: density (kg/m3), g: acceleration of gravity (9.81 m/s2), h: water column height, head (m), Q: water or brine flow (m3/s), MJ: Mega Joule, Watt=Joule (J)/second.
Another simplified estimation is based on concentration, where turbine generated power equals [(0.658 MJ per 1% of concentration) (C %) (SG) (Q)], based on turbine hydraulic efficiency of 85% and where C, SG and Q are flow conditions at the turbine inlet.
Similarly, pumping requirement can be also based on concentration, where pump shaft energy equals [(1.033 MJ per 1% of concentration) (C %) (SG) (Q)], based on pump efficiency of 75% and where SG and Q are flow conditions at the outlet of the pump, but C is the concentration % at the inlet of the turbine, where pumping is intended to overcome the osmotic pressure leaving the membrane.
Considering as an example the power generation from the Great Salt Lake of Utah, USA, an ISO train comprises three (3) cells operating at constant cell (HC/LC) ratio of 4.0, employing 1 m3/s from Gunnison Bay with salinity of 24% salt is exchanged with 3 m3/s with negligible salinity from Bear River water, operating at equal Log Mean concentration difference (LMCD) of 4.43 across membranes would generate a net energy of about 17,000 kWh.
Fouling of membranes is a serious problem in reverse osmosis desalination and directly affect process efficiency and economics. Pall Corporation indicated that 28% Costs Improvement can be achieved by effectively protecting reverse osmosis units. Generally all types of membrane separation technology are susceptive to a certain degree of foiling. In principal, reverse osmosis is a process is intended to filter water only. Since water molecules is about 0.275 nanometer (0.275×10−9 meter), then any particle larger that this size is considered a foiled matter and has to be removed.
However, since there are different types of foiling, different types of treatment may be required; i.e., mineral deposits, organic and inorganic matter, biological matter, bacterial and algae films, dissolved chemical compounds, herbicides and insecticides, etc., it must be more than one process to remove these foreign matter before any reverse osmosis process.
In addition, there are also other significant types of foiling that takes place within and among the membranes surface.
Concentration Polarization is one type of these foiling mechanism that result in formation of salt spots or layers on the membrane surface that have higher salt concentration, increasing the osmotic pressure at the membrane surface than the feed water and causing reversed is the flow direction, reducing the separation efficiency of this membrane. For this reason, the inventor specify, in all his membrane separation technologies, that membrane contact is not allowed and flow velocity is maintained at minimum Reynolds Number of 3000. Regarding flux redistribution in multi-elements reverse osmosis system, housing has to be sized to meet Reynolds number criterion. Where Reynolds number is calculated as follows:
Re=(ρvDH)/μ
ρ=density(kg/m3),v=velocity(m/s),DH=hydraulic diameter,
μ=Dynamic viscosity kg/(m·s)
Existing technologies suffer from what is known as concentration polarization phenomenon. The use of hydrophilic semipermeable membranes in hollow fiber panels significantly mitigates this phenomenon. Hydrophilic literally means “water-loving.” Accordingly, a hydrophilic material exhibits an affinity for water, and tends to readily adsorb water.
Suitable hydrophilic semipermeable membranes have a surface tension sufficiently high (surface tension of the membrane has to be higher than the surface tension of water) to maintain materials at the surface of the semipermeable membrane in liquid form. In one embodiment, the surface tension of the hydrophilic semipermeable membrane is about 35 dyne/cm or more.
In one embodiment, the hydrophilic semipermeable membrane material has a surface tension of about 44 dyne per centimeter or more. Hydrophilic membrane materials having suitable surface tensions include, for examples, Polyepichlorohydrin (surface tension-35), Polyvinyl Chloride (PVC) (surface tension-39), Polyethersulfone (surface tension-41), Polyethylene Terephthalate (Polyester) (surface tension-43), Polyacrylonitrile (surface tension-44); Cellulose (surface tension-44), and variants thereof.
in one embodiment, the hydrophilic semipermeable membrane material is cellulose acetate. Cellulose acetate has a surface tension of 44 dyne per centimeter (dyne/cm), or 44 milli Newton/meter. In one embodiment, the hydrophilic semipermeable membrane is a cellulose triacetate (CTA) membrane. A suitable CTA seawater semipermeable membrane in the form of hollow fiber is manufactured by the Japanese corporation, Toyobo Co, Ltd, In one embodiment, a flat sheet membrane Zirfon manufactured by Agfa for alkaline waters.
the present invention may be subject to many modifications and changes without departing from the spirit or essential characteristics thereof. The present embodiment should therefore be considered in all respects as illustrative and not restrictive of the scope of the subject invention as defined by the appended claims.
Revise Osmosis Membranes by Some Manufacturers
Apparatus Relevant Components, Design and Specification List:
Claims
1-20. (canceled)
21. Methods of Making Flat Sheet Membrane [FSM] Apparatus Adapted for various symbiotic fluids fractionation and osmotic processes in this application comprising three distinctive methodologies for fabricating and mounting conventional permeable or semipermeable membrane sheet in the form of plurality a spaced apart, self-supported and un-rolled spiral wound configuration membrane flat surface panel (leaf), essentially employing same conventional permeable or semipermeable membrane sheets.
21a. The first methodology wherein adjacent permeable or semipermeable membrane flat sheets, in an un-rolled configuration, is formed by two adjacent permeable or semipermeable membrane flat sheets of same size and specifications, separated by flat porous permeate carrier, in the form of a hard board, comprising intermediate flow channels or permeable inert structure for communicating permeated desalinated water across said flat sheet membranes, in a horizontal pattern to the vertical side headers of a flat sheet membrane panels frame, as in case of vertically mounted enclosing vessels (FIG. 4), wherein each of the opposite membrane panel edges, top and bottom, are heat or epoxy sealed. Such flow pattern arrangement is reversed when vessels are mounted horizontally.
- Said process can be automated by laying the first permeable or semipermeable membrane flat sheet on a moving belt, followed by laying the flat hard board porous permeate carrier on to top of the first membrane sheet, then followed by laying the second permeable or semipermeable membrane flat sheet and finally seem welding the top and bottom membrane sheets with epoxy material or heat.
21b. The second methodology comprising replacement of the two membrane sheets of claim 21a, by permeable or semipermeable membrane films that can be formed as a tube, either by employing blown-film extrusion process of molten and malleable resin pellets, in a similar fashion for forming conventional plastic bags, if membrane physical and chemical specifications are adaptable for such process, or by mechanically rolled the required membrane sheet in a tube form and seal its edges.
- In either application, the circumference of said tube has to be completely and securely overlay the flat porous permeate carrier board. This implies the need to heat the membrane polymeric tube with hot dry air or nitrogen @ 40-45° C. in a heating chamber, if tube has already been formed in a roll. Then flatten the end of the malleable formed tube, while it is hot, and slide it on the flat porous permeate carrier board, which can be accomplished, preferably by using automatic bag filling and sealing machine (modified version of zipper bags filling/sealing) to open the end of the extruded polymeric tube by air suction to expand tube diameter by few millimeters, then inserted on the flat porous permeate carrier boards being mounted on a moving conveyor belt.
- As the film cools, it shrinks maintaining secure flat sheet film on both side of porous permeate carrier board. Then, the process is completed but cutting/trimming the required flat sheet membrane length for mounting in the desalinated water header of the membranes frame. This process is more suited for vertically mounted flat porous permeate carrier board assembly lines.
- For an example, a membrane tube 19 cm (7.5 inch) in diameter overlays both sides of a flat membrane panel of 30 cm (11.8 inch) wide.
21c. The method further comprising modification of flat sheet membrane of claim 21, where a plurality of spaced apart, self-supported, vertically mounted flat sheet membrane panels assembly, wherein adjacent permeable or semipermeable membrane flat sheets, in an un-rolled configuration, can be formed efficiently and economically by laying down the selected membrane film, of a sufficient width on a speed-controlled moving belt(s) of several meters long, to securely wrapping both sides of the permeate carrier board, then laying down the flat porous permeate carrier board for the full length of the belt, then automatically wrapped the two sheet edges fairly tight around the board and seal these edges by adhesive sealing, heat sealing, or ultrasonic welding, where the sealing process is followed by an automatic process to cut this long film assembly to the required Flat Sheet Membrane panel (leaf) length.
- The process is most suited for narrow and square membrane panels (leaves), where the membrane outlets width of the desalinated water discharge is at or longer than the panels' sealed sides.
22. Wherein the panel surface is tightly wrapped by a highly porous protective woven fabric, secured by epoxy sealed sleeves, or equivalent means, at the panel both side ends, then the panel is shielded with protective rigid polymeric or rustproof metallic porous screen.
25. Wherein a stack of plurality of uniform membrane panels are mounted within detachable top and bottom of holding caps that can be securely inserted and epoxy scaled to the top and bottom headers of the flat sheet membrane frame for communicating treated water.
26. Wherein said mounted membrane panels are separated apart to maintain flow Reynold's number of 3,000-3,500 for mitigating membrane fouling, while maintaining=a minimum clearance of least of 1.0 mm (˜0.04 inch) for regular membranes maintenance procedures.
27. Wherein said flat sheet membrane panels [FSM] for osmotic processes are exceptionally large in size than that of conventional desalination membranes and uniquely designed for operating at pressures of up to 70 kg/cm2 (1,000 psi), would be mounted in frames of up to one meter in width and more than two (2) meters in length, or more;
28. Wherein, flat sheet membrane panel's frames, of essentially same configuration, but of varying specification and operating conditions are housed in large holding compartments of essentially cubical shapes that are mounted within a vertical tower or horizontal train of sequential set of vessels, for specific process applications; macro filtration, micro filtration, ultra-filtration, nano filtration and reverse osmosis.
29. Wherein flat sheet membrane in the form of polymeric sheets or ceramic sheets, as well as in the form of hollow fiber can be mounted in independent vessels within the same desalination and salinity power generation trains of multi vessels.
30. Wherein, flat sheet membrane panel [FSM] frames, of essentially the same configuration, but of varying specification and operating conditions are housed in vertical, single stage axial flow pressure vessels, mounted above or for below grade, or housed in multi stages water desalination towers (U.S. patent application Ser. No. 14/967,295),
31. Wherein, the water desalination or brine power generation operating capacity determines the size, weight and the mechanical integrity of equipment; where size and number of panels is dictated by availability of safe means to handle, operate and maintain such operating systems;
32. Wherein, small desalination operating capacity that may require 15 membrane panels, with frame header cross section of 20 cm, only one single frame of 20 cm size can be used considering the relatively light weight of the frame and its mounted panels.
33. Wherein, the large operating desalination capacity that may require multiple heavy weight frames, then the membrane panels frame header can be 10-15 cm (˜4-6 inch) in width, comprising 6-12 membrane panels; where size and number of panels is dictated by water flow rates, turbidity and salinity, availability of safe means to handle, operate and maintain such operating systems;
34. The method of claim 21 further comprises:
- A plurality of spaced apart, vertically mounted flat ceramic membrane panels assembly, wherein adjacent permeable membrane flat sheets can be used ahead of the semipermeable reverse osmosis polymeric flat sheet membranes [FSM], for water filtration and can be formed, as well, by separating these panels with flat porous permeate carrier comprising an intermediate flow channels for communicating permeated filtered water across said flat ceramic membranes,
- Wherein, said ceramic membranes are mostly suitable for macro, micro and ultrafiltration, generally has limited operating pressure of about 300 psi, but less sensitive to temperature changes,
35. The method of claim 21, 22, 23, further comprises:
- Automated or semi-automated assembly platform (assembly line) for assembling flat sheet membrane panels in sequential steps, comprising a moving belt, where the first shielding screen is laid down on the belt, followed by a feed spacer, then by a flat membrane panel, followed by a feed spacer, then by the second shielding screen, where bottom and top shielding metallic screens edges are continuously welded or epoxy sealed, if screens are of polymeric materials, where this automated process for panel's assembly could potentially construct 90-120 panels per hour.
36. The methods of claim 21, 22, 23 through claim 35 further comprising:
- Means for measuring fluid properties; flow rate, temperature, density, viscosity, acidity, radioactivity, etc., as well fluid sampling, flow conditioning and property adjustment for various processes. Where said Flat Sheet Membrane [FSM] apparatus is capable of processing several fluids, including: seawater and brines reverse osmosis desalination and osmotic power generation, flowback and produced water fractionation in the hydraulic fracturing process, in-situ leaching of underground soluble minerals, fractionation of alcohols mixtures, removing radioactive from water, medical solutions, fractionation of industrial gases,
37. Flat porous permeate media in claims 21, 22, 23 can be made of Polysulfone membrane support boards, less than 5 micron pores, Zirfon® with low zirconia. Also, interstitial porous aluminum oxide, woven metal screen, channels or nonwoven polyester or Polysulfone fiber mat. Epoxy sealing sleeve for right & left edges of vertically mounted membrane panels,
38. Feed Spacer can be made of Polyester or polypropylene, or comparable material;
39. Seawater, brackish water and brines desalination membranes are made of polyamide or cellulose acetate flat sheets, or comparable material;
40. The methods of claim 36 further comprising:
- Means for adjusting fluid temperature to sustain membrane mechanical integrity and fluid separation or retention of solutes, where the change of fluid temperature, as a result of atmospheric weather changes; summer and winter, on open water domains operation, can have serious implication on polymeric membrane pore size. This function is very important in the development of “Ecologically Sustainable Hydraulic Fracturing [ES-FRAC] Process” by the same applicant of the current patent application!
41. A frame configured to house the plurality of the caped (Please see FIG. 2) membrane Panels; the frame includes: a top header in communication with the first end cap and a bottom header in communication with the second end cap, each end cap configured to rest within a track formed in the bottom and top headers; a side member having a porous surface configured to permit the passage of saline water (or other saline fluids); and an outlet formed in at least one of the top header and the bottom header to allow passage of desalinated water (or other Fluids); wherein pressurized saline water is forced to passed through the porous side member of the frame through the flat sheet membranes.
42. The panel assembly of claim 21, 22, 23, 36, wherein the plurality of flat sheet membranes is configured to be suitable for at least one of filtration or fractionation function; brackish water, seawater, brines desalination, fluid extraction, solute recovery, symbiotic salinity power generation, symbiotic Hypersalinity reverse osmosis, and gas mixture fractionation.
43. The panel assembly of claim 21, 22, 23, wherein the plurality of flat sheet membranes is adapted for use in a rectangular shape.
42. The panel assembly of claim 21, 22, 23, wherein treated water is collected through the plurality of headers and the brine waste water is disposed of, or used as a source for salt, as in the case of seawater desalination.
44. The panel assembly of claim 21, 22, 23, wherein the plurality of the flat sheet membranes are made of at least one of a polyamide and a cellulose acetate, or equivalent membrane material, having a pore size suitable for filtration or desalination.
45. The panel assembly of claim 21, 22, 23, wherein the plurality of flat sheet membranes are separated by a permeate carrier.
46. The panel assembly of claim 21, 22, 23, wherein the permeate carrier is configured to resist collapse under the operating pressure of the fluid.
47. The panel assembly of claim 21, 22, 23, further comprising:
- a shielding screen coupled to a surface of the flat sheet membranes panels and configured to protect membranes from damage.
48. The panel assembly of claim 1, wherein the frame is configured to include a rolling device configured to translate the frame on the bottom header within the pressure vessel.
49. In all design cases, desalinated water collecting header has to be on the long side of the membrane panels (leaves) to avoid restricting the flow of desalinated water through the membrane.
50. This invention pertains to Permeable and Semipermeable Flat Sheet Membranes (FSM) applicant's novel applications such as:
- a. Agitated axial and oscillating flow reverse osmosis,
- b. Agitated axial flow underground vertical wells reverse osmosis,
- c. Induced symbiotic osmatic [ISOP] for salinity power generation,
- d. Symbiotic hypersaline water reverse osmosis [SRO],
- e. Induced symbiotic osmosis [ISO] for solutes recovery/fluids concentration,
- f. Symbiotic gases fractionation processes [SGF].
- g. Ecologically sustainable hydraulic fracturing process [ES-FRAC].
Type: Application
Filed: Dec 12, 2015
Publication Date: Mar 23, 2017
Inventor: Maher Isaac Kelada (Houston, TX)
Application Number: 14/967,295
