Abstract:
A method for treating water including intaking a first amount of water into a plurality of treatment blocks, treating the first amount of water, outputting aqueous treated water streams from each of the plurality of treatment blocks, separating the aqueous treated water streams from each of the plurality of treatment blocks into aqueous permeate streams and concentrate reject streams, monitoring each of the aqueous permeate streams, controlling the operation of at least one of the plurality of treatment blocks based on predefined water-characteristic tolerances that fall within a predetermined concentration range based on the different qualities of the aqueous permeate streams, combining the aqueous permeate streams of at least two of the plurality of treatment blocks based on the identified characteristics and the predefined water-characteristic tolerances, and outputting the product water stream and the at least one concentrate reject stream.

Description:
BACKGROUND OF INVENTION 
       [0001]    1. Field of the Invention 
         [0002]    Embodiments disclosed herein relate generally to methods and control devices for production of consistent water quality from membrane-based water treatment for use in improved hydrocarbon recovery operations. 
         [0003]    2. Background Art 
         [0004]    Hydrocarbons accumulated within a subterranean hydrocarbon-bearing formation are recovered or produced therefrom through production wells drilled into the subterranean formation. When production of hydrocarbons slows, improved recovery techniques may be used to force the hydrocarbons out of the formation. One of the simplest methods of forcing the hydrocarbons out of the formation is by direct injection of fluid into the formation. This enhances production by displacing or sweeping hydrocarbons through the formation so that they may be produced from production well(s). 
         [0005]    As shown in  FIG. 1 , a prior art system for recovering hydrocarbons from a formation consists of an offshore rig  12  connected to a well  10 , which is completed in a subterranean hydrocarbon-bearing formation  14 . Generally, fluid is injected directly into the subterranean hydrocarbon-bearing formation  14  (indicated by the down arrow) and forces the hydrocarbons through the formation and out of the well  10  (indicated by the up arrow) via a production well, which may be the same or a different well. One type of such recovery operation uses water (e.g., seawater, produced water) as the injection fluid, which is referred to as a waterflood. Water is injected, under pressure, into the formation via injection wells, driving the hydrocarbons through the formation toward production wells. 
         [0006]    Injection water used in waterflooding for offshore wells is typically seawater and/or produced water because of the low-cost availability of seawater and/or produced water at offshore locations. Another motivation for using produced water as an injection water offshore is the difficulty in some locations in disposing the produced water offshore. In any case, seawater and produced water are generally characterized as saline, having a high ionic content relative to fresh water. For example, the fluids are rich in sodium, chloride, sulfate, magnesium, potassium, and calcium ions, to name a few. Some ions present in injection water can benefit hydrocarbon production. For example, certain combinations of cations and anions, including K + , Na + , Cl − , Br − , and OH − , can stabilize clay to varying degrees in a formation susceptible to clay damage from swelling or particle migration. 
         [0007]    However, it has also been found that certain ions, including calcium and/or sulfate, present in the injection water may have harmful effects on the injection wells and production wells and can ultimately diminish the amount or quality of the hydrocarbon product produced from the production wells. Specifically, sulfate ions can form salts in situ when contacted with metal cations such as barium and/or strontium, which may be naturally occurring in the reservoir. Barium and strontium sulfate salts are relatively insoluble and readily precipitate out of solution under ambient reservoir conditions. Solubility of the salts further decreases as the injection water is produced to the surface with the hydrocarbons because of temperature decreases in the production well. The resulting precipitates accumulate as barium sulfate scale in the outlying reservoir, at the wellbore of the hydrocarbon production wells, and downstream thereof (e.g., in flow lines, gas/liquid separators, transportation pipelines, etc). The scale reduces the permeability of the reservoir and reduces the diameter of perforations in wellbores, thereby diminishing hydrocarbon recovery from the hydrocarbon production wells. Divalent cations are particularly effective at stablizing sensitive clays. 
         [0008]    It has also been reported that a significant concentration of sulfate ions in injection water promotes reservoir souring. Reservoir souring is an undesirable phenomenon whereby reservoirs are initially sweet upon discovery, but turn sour during the course of waterflooding and attendant hydrocarbon production from the reservoir. Souring contaminates the reservoir with hydrogen sulfide gas or other sulfur-containing species and is evidenced by the production of quantities of hydrogen sulfide gas along with the desired hydrocarbon fluids from the reservoir via the hydrocarbon production wells. The hydrogen sulfide gas causes a number of undesired consequences at the hydrocarbon production wells and downstream of the wells, including excessive degradation and corrosion of the hydrocarbon production well metallurgy and associated production equipment, diminished economic value of the produced hydrocarbon fluids, an environmental hazard to the surroundings, and a health hazard to field personnel. 
         [0009]    The hydrogen sulfide is believed to be produced by an anaerobic sulfate-reducing bacteria. The sulfate-reducing bacteria is often indigenous to the reservoir and is also commonly present in the injection water. Sulfate ions and organic carbon are the primary feed reactants used by the sulfate reducing bacteria to produce hydrogen sulfide in situ. The injection water is usually a plentiful source of sulfate ions, while formation water is a plentiful source of organic carbon in the form of naturally-occurring low molecular weight fatty acids. The sulfate reducing bacteria effects reservoir souring by metabolizing the low molecular weight fatty acids in the presence of the sulfate ions, thereby reducing the sulfate to hydrogen sulfide. Stated alternatively, reservoir souring is a reaction carried out by the sulfate reducing bacteria which converts sulfate and organic carbon to hydrogen sulfide and byproducts. 
         [0010]    A number of strategies have been employed in the prior art for remediating reservoir souring with limited effectiveness. These prior art strategies have primarily been single pronged attacks against either the sulfate reducing bacteria itself or against a specific food nutrient of the sulfate reducing bacteria. For example, many prior art strategies have focused on killing the sulfate reducing bacteria in the injection water or within the reservoir. Conventional methods for killing the sulfate reducing bacteria or limiting their growth may include ultraviolet light, biocides, and chemicals such as acrolein and nitrates. Other prior art strategies for remediating reservoir souring have focused on limiting the availability of sulfates or organic carbon to the sulfate reducing bacteria. 
         [0011]    More recently, strategies for remediating reservoir souring have included the use of membranes to reduce the concentration of sulfate ions in injection water. For example, U.S. Pat. No. 4,723,603 shows that specific membranes can effectively reduce the concentration of sulfate ions in injection water, thereby inhibiting sulfate scale formation. As taught by the prior art, nanofiltration (NF) membranes are often preferred to reverse osmosis (RO) membranes because nanofiltration membranes generally permit a higher passage of sodium chloride compared to reverse osmosis membranes. Consequently, nanofiltration membranes are advantageously operable at substantially lower pressures and operating costs than reverse osmosis membranes. Furthermore, nanofiltration membranes also maintain the ionic strength of the resulting injection water at a relatively high level, which desirably reduces the risk of clay instability and correspondingly reduces the risk of water permeability loss through the porous substrata of the subterranean formation. 
         [0012]    However, in addition to the problems associated with sulfate ions being present in the injection water, it has also been found that the salinity of an injection water can have a major impact on the recovery of hydrocarbons during waterfloods, with increased recovery resulting from the use of injection water of lower salinity than natural seawater but sufficient ionic strength to prevent clay instability. Depending on the type of formation, injection fluids having higher salinity may cause the reservoir wettability to become more oilwet. This is because the multivalent cations in the brine, such as Ca +2  and Mg +2 , are believed to act like bridges between the negatively charged oil and the negatively charged clay minerals that typically line the pore walls of the formation. The oil reacts with the clay particles to form organo-metallic complexes, which results in the clay surface being extremely hydrophobic and oilwet. As the oilwetness of the reservoir rock increases, hydrocarbons will adsorb onto the surface of the rock and thereby flow less easily from the formation, relative to water, which results in less hydrocarbon product being produced. 
         [0013]    Lowering the electrolyte content (i.e., lowering the ionic strength) by lowering the overall salinity and especially reducing the concentration of multivalent cations in the formation reduces the screening potential of the cations. This results in increased electrostatic repulsion between the clay particles and the oil. Once the repulsive forces exceed the binding forces via the multivalent cation bridges, the oil particles are desorbed from the clay surfaces and the clay surfaces become increasingly waterwet. If, however, the electrolyte content is reduced too much (i.e., the formation fluid salinity is too low), the clay particles may be stripped from the pore walls (clay deflocculation), which will damage the formation. Thus, although it is desirable to have lower salinity injection water, it is important that the salinity levels be kept within a specified range. 
         [0014]    Lower salinity water, however, is not often available at a well site. Lower salinity water is typically prepared, for example, by reducing the total ion concentration of higher salinity water using membrane separation technology (e.g., reverse osmosis). In known seawater desalination plants operating according to the reverse osmosis process, the seawater to be desalinated is subjected to a separation process by means of a semi-permeable membrane. Such a membrane is understood to be a selective membrane, which is permeable to a high degree to the water molecules, but only to a very low extent to the salt ions dissolved therein. 
         [0015]    Membrane separation techniques used in the preparation of low salinity injection water use reverse osmosis (RO) membrane elements. Membrane separation techniques used in the preparation of low sulfate injection water and softened water use specialized nanofiltration (NF) membrane elements. The RO and NF processes use hydraulic pressure to produce lower salinity water from feed water through a semipermeable membrane. Depending on the membrane type, pressure and water conditions, an amount of salt also passes across the membrane, but the overall salinity of the product water is less than that of the feed water. Current RO technology can be used for desalinating both seawater and brackish water. The membranes used in the RO process are generally either made from polyamides or from cellulose sources. 
         [0016]    The water to be treated is typically pretreated using cartridge filters, media filtration, microfiltration, or ultrafiltration methods, which are known to separate solids/particulates from the water based on their size. The water is then fed to the reverse osmosis and/or nanofiltration vessel using a high-pressure pump. The required pressure from the high-pressure pump is a function of the osmotic pressure, the temperature, the flux (i.e., the rate at which the water passes through a unit area of the membrane), and the volume of the feed water to be produced with a specific membrane area. The product water (i.e., the permeate) is discharged from the membrane module by way of a permeate conduit. A concentrate conduit serves for discharging concentrated ionic water. 
         [0017]    Typically, conventional systems are only concerned with producing water having certain characteristics in amounts higher or lower than a predetermined level. Such systems focus only on a maximum allowable limit of a contaminant and treatment occurs as long as, and only if, the amount of the particular characteristic is above the set limit. Otherwise, the water is deemed acceptable for use. Most often, such a treatment plant will include several treatment blocks connected in series and/or parallel. In such systems, water is passed through as many of the multiple blocks, or through a particular block as many times, as is necessary for the particular characteristic in the water to reach the amount deemed acceptable for use. 
       SUMMARY OF INVENTION 
       [0018]    In one aspect, embodiments disclosed herein relate to a method for treating seawater or other water sources for injection, the method including intaking a first amount of water into a plurality of treatment blocks, treating the first amount of water, outputting aqueous treated water streams from each of the plurality of treatment blocks, separating the aqueous treated water streams from each of the plurality of treatment blocks into aqueous permeate streams and concentrate reject streams, monitoring each of the aqueous permeate streams, controlling the operation of at least one of the plurality of treatment blocks based on predefined water-characteristic tolerances that fall within a predetermined concentration range based on the different qualities of the aqueous permeate streams, combining the aqueous permeate streams of at least two of the plurality of treatment blocks based on the identified characteristics and the predefined water-characteristic tolerances, and outputting the product water stream and the at least one concentrate reject stream. Treating the first amount of water includes pumping at least a portion of the first amount of water through the plurality of treatment blocks. Monitoring each of the aqueous permeate streams includes identifying different characteristics of the aqueous permeate streams. 
         [0019]    According to another aspect, there is provided a membrane-based water treatment system, the system including a water intake system that intakes a first amount of water and a plurality of treatment blocks. Each of the plurality of treatment blocks includes at least one pump, a membrane pressure vessel, a monitor, and a controller. The pump feeds the first amount of intake water through the membrane pressure vessel. The membrane pressure vessel comprises at least one membrane element and separates the first amount of intake water into at least an aqueous permeate stream and a concentrate reject stream. The monitor is used to identify different characteristics of each of the aqueous permeate streams, monitor blending of the aqueous permeate streams from two or more treatment blocks, and to monitor the blended aqueous permeate streams from the two or more treatment blocks based on the identified characteristics and predefined water-characteristic tolerances. 
         [0020]    Other aspects and advantages of the invention will be apparent from the following description and the appended claims. 
     
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
         [0021]      FIG. 1  shows a prior art offshore production well. 
           [0022]      FIG. 2  shows a seawater treatment process according to one or more embodiments of the present invention. 
           [0023]      FIG. 3A  is a diagram of a seawater treatment unit on a vessel according to one or more embodiments of the present invention. 
           [0024]      FIG. 3B  is a diagram of a seawater treatment unit on an off-shore rig according to one or more embodiments of the present invention. 
           [0025]      FIG. 3C  is a diagram of a rig, a vessel, and a seawater treatment unit on the seafloor according to one or more embodiments of the present invention. 
           [0026]      FIG. 4A  shows another seawater treatment process according to one or more embodiments of the present invention. 
           [0027]      FIG. 4B  shows a treatment block according to one or more embodiments of the present invention. 
           [0028]      FIG. 4C  shows a spiral wound membrane element according to one or more embodiments of the present invention. 
           [0029]      FIG. 4D  shows a schematic for a hollow fine fiber membrane element according to one or more embodiments of the present invention. 
           [0030]      FIG. 4E  shows another seawater treatment process according to one or more embodiments of the present invention. 
           [0031]      FIG. 5  shows an improved oil recovery system according to one or more embodiments of the present invention. 
           [0032]      FIG. 6A  shows a configuration for a system or method according to one or more embodiments of the present invention. 
           [0033]      FIG. 6B  shows a configuration for a system or method according to one or more embodiments of the present invention. 
           [0034]      FIG. 7  shows a configuration for a system or method according to one or more embodiments of the present invention. 
       
    
    
     DETAILED DESCRIPTION 
       [0035]    One or more embodiments of the present invention will be described below with reference to the figures. In one aspect, embodiments disclosed herein relate to systems and methods for treating seawater or other water source using customizable membrane technology to prepare an aqueous fluid having specific water characteristic tolerances that fall within predefined threshold values. In another aspect, embodiments disclosed herein relate to a water treatment process having a customizable membrane system that may include a bypass blend line which may be used depending on the water outputted from the customizable membrane system to achieve predefined threshold values. In yet another aspect, embodiments disclosed herein relate to the treatment of seawater using a customizable treatment system to produce an aqueous fluid which has specifically tailored properties and which is capable of being used as an injection fluid to be used in improved oil recovery operations. In yet another aspect, embodiments disclosed herein relate to blending treated fluids which have specifically tailored properties. In yet another aspect, embodiments disclosed herein relate specifically to improved oil recovery operations in offshore wells. 
         [0036]    Seawater Treatment 
         [0037]    Typically, seawater treatment systems are based on several factors. Most importantly, seawater treatment systems depend on the quality of the seawater (e.g., the temperature, salinity, and/or specific chemical composition of the water). In particular, the input water temperature variance of the seawater is the most common factor that varies to which the treatment system must react in order to produce consistent water quality. Water temperature impacts the treatment performance as a function of the water and salt transport property variation of the membranes. Warmer water will result in treated water with higher salinity than the same treatment of cooler water. In addition, as the membrane used in the treatment system ages, its performance changes, thereby impacting the water and salt transport properties and the resulting treated water quality. According to embodiments of the present invention, depending on these factors, a treatment system may be customized to produce any quality of output water desired. 
         [0038]    As used herein, the term “predefined water-characteristic tolerances” is used to refer to the desired output water quality that falls within predefined threshold values for any system which will be using the treated water. For example, in downhole applications, it may be desired to produce a water having a salinity of between about 1,000 mg/L and about 30,000 mg/L, a sulfate ion content of between about 5 mg/L and 2,000 mg/L and hardness content of between 5 mg/L and 300 mg/L. 
         [0039]    According to one or more embodiments of the present invention, a seawater treatment system may be used to produce water having predefined water-characteristic tolerances, for example, by controlling pumps within the system to ensure that any water having characteristics outside the predefined threshold values is appropriately blended either with treated or untreated (or both) filtered water to produce a water that has characteristics falling inside the predefined threshold values. 
         [0040]    In one embodiment, a treatment system comprising multiple membrane blocks may be modified so as to change the operation of each of the membrane blocks themselves so they produce different quality water streams based on the predefined water-characteristic tolerances. These different quality water streams may then be blended together to form a product water stream having predefined water-characteristic tolerances. Alternatively, the product water stream may be further blended with untreated filtered seawater from a blend/bypass line. 
         [0041]    In particular, control devices may be used (e.g., a monitor and/or transmitter) to modify or vary the operational parameters of each block based on the outputted permeate water streams. Operational parameters to be modified may include input feed pressure, flux, temperature, flowrate, and water recovery. 
         [0042]    Referring to FIGS.  2  and  3 A-C, a seawater treatment system according to one or more embodiments is shown. As shown in  FIG. 2 , the present invention provides a seawater treatment system  200  that may include a water intake system  201 , a membrane system  210 , permeate transfer and treatment system  220 , a concentrate discharge system  230 , a control system  240 , and a power source  290 . Water intake system  201  may include water intake(s)  202 , water intake pump(s)  204 , pre-filter(s)  206 , and membrane/media-filter(s)  208 ; membrane system  210  may include variable speed high-pressure pump(s)  212 , blend/bypass line(s)  225 , either a reverse osmosis and/or nanofiltration membrane(s)  214 , and monitor/transmitter(s)  226 ; the concentrate discharge system  230  may include a plurality of discharge ports; and permeate transfer and treatment system  220  may include permeate transfer pump(s)  222 . While in the exemplary embodiments shown, certain components may be shown by a single block/symbol, those skilled in the art will appreciate that each system described may be comprised of a plurality of such elements. 
         [0043]    As shown in  FIGS. 3A-C , the seawater treatment system  200  may be provided on a vessel  300 , on a rig  312 , and/or on the seafloor  316 . Alternatively, in one or more embodiments, the seawater treatment system  200  may be used onshore. 
         [0044]    Additionally, according to one or more embodiments, treatment block  260  may be used to describe the system that includes, for example, membrane system  210 , blend/bypass line  225 , concentrate discharge system  230 . 
         [0045]    The treatment block  260  is in communication with the water intake system  201  and the permeate transfer and treatment system  220 . Both the control system  240  and the power source  290  are in communication with one another, as well as in communication with the water intake system  201 , the permeate transfer and treatment system  220 , and treatment block  260  (i.e., membrane system  210  and concentrate discharge system  230 ). As used herein, the terms “communicate” or “communication” mean to mechanically, electrically, or otherwise contact, couple, or connect by direct, indirect, or operational means. 
         [0046]    Within the water intake system  201 , water intake pump  204  pumps the intake water through pre-filter  206  to remove any large contaminants (e.g., sand, rocks, plants, debris, etc.) and then through a low pressure membrane or media filter  208  to remove large molecules (e.g., suspended solids, colloids, macromolecules, bacteria, oils, particulate matter, proteins, high molecular weight solutes, etc.). One of ordinary skill in the art will appreciate that depending on the specifications of the equipment and the type and density of particulate matter to be removed, various types of filters, including for example, sand or media filters, cartridge filters, ultra filters, and/or micro filters may be used. 
         [0047]    Furthermore, the water intake system  201  may include one or more variable-depth extension members capable of extending into the body of water so as to intake water from a desired depth. Additionally, the extension member may include one or more intake screens designed to help prevent fouling of the intakes by marine life or other particles. One of ordinary skill in the art will appreciate that depending on the intended body of water from which water is being taken, other equipment may also be employed. 
         [0048]    After passing through water intake system  201 , the filtered seawater may be provided to blend/bypass line  225  and transferred directly to permeate treatment and transfer system  220  where it may then be combined with a permeate stream produced from membrane  214 . Additionally, the filtered seawater may be provided to treatment block  260  wherein a variable speed high-pressure pump  212  pushes the filtered seawater through to membrane  214 , whereby a concentrate is created on the high pressure side of the membrane  214  and a permeate stream is created on the low pressure side of the membrane  214 . 
         [0049]    The permeate stream produced from membrane  214  may comprise predefined water-characteristic tolerances, i.e., water that has specific ions and/or molecules removed therefrom, for example, the permeate stream may have lower sulfate ion content and/or lower salinity compared to the filtered seawater produced from water intake system  201 . The permeate stream may then be transferred, for example, from vessel  300  to rig  312 , from seafloor  316  to rig  312 , and/or from rig  312  to well  310 , through permeate transfer and treatment system  220 . 
         [0050]    Alternatively, the permeate stream produced from membrane  214  may not comprise the desired predefined water-characteristic tolerances and may need to be further treated in order to reach the predefined water-characteristic tolerances. For example, the permeate stream may be blended with other permeate streams and/or untreated filtered seawater from the blend/bypass line. However, based on the quality of the permeate stream produced from membrane  214 , it may be necessary to change the operation of the membrane block itself so it will produce a different quality water stream based on the outputted permeate stream produced from the membrane and based on predefined water-characteristic tolerances. Such a change may be made by using a monitor  226  to first determine the quality of the outputted permeate stream and second to vary or change the operation of the membrane block itself (e.g., by controlling the pump  212  that pumps water into the membrane block  214  and/or a concentrate line valve  223 ), thereby changing the quality of the outputted permeate stream for subsequent batches of water. 
         [0051]    Additionally, permeate streams from various treatment blocks  260  may be blended together, and may be blended with untreated filtered seawater from the blend/bypass line  225  to produce water having predefined water-characteristic tolerances. Each treatment block can use the same or a different type of RO or NF membrane requiring its respective pressure from the high-pressure pump  212 . Blending the various permeate streams from each treatment block can then provide a very specific composition of mono- and divalent ions as a function of optimum reservoir performance. According to one or more embodiments, this very specific composition may then be mixed with water from the blend/bypass line  225 . 
         [0052]    According to one or more embodiments of the present invention, a monitor  226  may be used to detect the characteristics of the output permeate streams. Based on these characteristics, one or more monitor  226  may be used to change the operation of the membrane block  214 , for example, by controlling the variable speed high-pressure pump  212  in real-time to change the amount of water being pumped through membrane  214 , so as to produce different quality water having predefined water-characteristic tolerances. Additionally, based on these characteristics, untreated filtered seawater from the blend/bypass line  225  may be blended in with the output permeate streams in order to achieve a water having even more specific water-characteristics tolerances. 
         [0053]    In one or more embodiments, a permeate stream from a treatment block  260  can be further treated using forward osmosis (FO) or other treatment, which impacts the chemical composition of the water to further refine the ionic balance as a function of achieving optimum reservoir performance. 
         [0054]    In one or more embodiments, instead of seawater as the source of water through intake system  201 , brackish water or produced water could be the feed water, thereby allowing the flexibility to switch between brackish water, produced water, and seawater treatment. 
         [0055]    The permeate transfer and treatment system  220  may be capable of transferring the permeate produced to a permeate delivery system comprising a pipeline in communication with the permeate transfer and treatment system  220 . The pipeline may transfer the permeate, for example, from vessel  300  to rig  312 , from seafloor  316  to rig  312 , and/or from rig  312  to well  310 . The permeate transfer and treatment system  220  may also be capable of treating the permeate produced either prior to, during, or after the permeate is transferred. Treatment of the permeate may include “post-treatment,” for example, chemical addition (e.g., in line chemical injection) and/or deaeration (e.g., in a vacuum system). 
         [0056]    The concentrate created on the high pressure side of the membrane  214  comprises the ions and/or molecules removed by membrane  214 . The concentrate is then disposed of, for example, through a plurality of concentrate discharge ports within the concentrate discharge system  230 . However, before the concentrate is disposed of, an energy recovery device (not shown) may be used to capture the energy possessed by the concentrate and return such energy to the variable speed high-pressure pump  212 . 
         [0057]    Furthermore, the concentrate may be diluted or otherwise treated prior to disposal. For example, in one or more embodiments, the concentrate discharge system  230  may be configured to increase the mixing of the concentrate discharged into the surrounding body of water. The plurality of discharge ports of the concentrate discharge system  230  may be physically located above or below the water line  318  of the vessel  300  and/or the rig  312 . Also, the discharge ports may be disposed on a variable-depth extension member that can be positioned so as to promote dispersion of the concentrate into the body of water. 
         [0058]    In one or more embodiments, the effluent from membrane  214  (either the permeate stream or the concentrate) may take one or more subsequent passes through membrane  214  and concentrate streams may be recycled to earlier positions in the treatment scheme. 
         [0059]    According to one or more embodiments of the present invention, separate power source(s) may provide power to each of the water intake system  201 , permeate transfer and treatment system  220 , treatment block  260  (i.e., membrane system  210  concentrate discharge system  230 ), monitor  226 , and propulsion device  302 . For example, each of the water intake pump  204 , variable speed high-pressure pump  212 , monitor  226 , and permeate transfer pump  222  may be in communication with a separate power source. 
         [0060]    According to one or more embodiments, the seawater treatment system  200  may be land-based or provided on a vessel. Where the seawater treatment system  200  is provided on a vessel  300 , vessel  300  may further comprise a propulsion device  302  in communication with the power source  290 . The vessel  300  may be a self-propelled ship, a moored, towed, pushed or integrated barge, or a flotilla or fleet of such vessels. The vessel  300  may be manned or unmanned. The vessel  300  may be either a single-hull or double-hull vessel. 
         [0061]    Alternatively, in one or more embodiments, a single power source may provide power to a combination of two or more of the water intake system  201 , membrane system  210 , permeate transfer and treatment system  220 , concentrate discharge system  230 , monitor  226 , and/or propulsion device  302  where the seawater treatment system  200  is provided on a vessel  300 . For example, electric power for the variable speed high-pressure pump  212  may be provided by a generator driven by the power source for the vessel&#39;s propulsion device, such as a vessel&#39;s main engine. In such an embodiment, a step-up gear power take off or transmission would be installed between the main engine and the generator in order to obtain the required synchronous speed. 
         [0062]    Further, an additional coupling between the propulsion device and the main engine allows the main engine to drive the generator while the vessel is not under way. Moreover, an independent power source (not shown), such as a diesel, steam, or gas turbine, renewable energy generator, or combinations thereof, may power the treatment block  260 , the propulsion device  302 , or both. 
         [0063]    In other embodiments, the power source for seawater treatment system  200  may be dedicated solely to the seawater treatment system  200 . 
         [0064]    In one or more embodiments, the plurality of concentrate discharge ports of the concentrate discharge system  230  may act as an auxiliary propulsion device for the vessel  300  or act as the sole propulsion device for the vessel  300 . Some or all of the concentrate may be passed to propulsion thrusters to provide idling or emergency propulsion. 
         [0065]    In one or more embodiments, the power source  290  may comprise electricity producing windmills and/or water propellers that harness the flow of the air and/or water to generate power for the seawater treatment system  200  and/or the operation of the vessel  300  and/or rig  312 . 
         [0066]    For embodiments where the seawater treatment system  200  is on a vessel  300 , the water intake system  201  may be capable of taking in seawater from the water surrounding the vessel  300  and providing it to the treatment block  260 . In such embodiments, the water intake  202  of the water intake system  201  may include one or more apertures in the hull of the vessel  300  below the water line  318 . An example of a water intake  202  is a sea chest (not shown). Water is taken into the vessel  300  through the one or more apertures (i.e., water intake  202 ), passed through the water intake pump  204 , pre-filter  206 , membrane/media filter  208 , and either supplied to the variable speed high-pressure pump  212  or supplied to the blend/bypass line  225 , or both. 
         [0067]    For embodiments where the seawater treatment system  200  is on an offshore rig  312 , the water intake system  201  may be capable of taking in seawater from the water surrounding the rig  312  and providing the seawater to the treatment block  260 . In such embodiments, the water intake  202  of the water intake system  201  may include an intake riser(s), screen(s), and external or submerged pump(s). 
         [0068]    For embodiments where the seawater treatment system  200  is on the seafloor  316 , the water intake system  201  may be capable of taking in seawater from the water surrounding the seawater treatment system  200  and providing it to the membrane system  210 . In such embodiments, the water intake  202  of the water intake system  201  may include an intake well or riser, screen(s) and pump(s). 
         [0069]    The membrane system  210  may comprise a variable speed high-pressure pump  212 , a membrane  214 , a blend/bypass line  225 , and a monitor  226 . 
         [0070]    In one or more embodiments, membrane  214  is an ion selective membrane, which may selectively prevent or at least reduce hardening or scale-forming ions (e.g., divalent ions including sulfate, calcium, and magnesium ions) from passing across it, while allowing water and other specific ions (e.g., monovalent ions including sodium, chloride, bicarbonate, and potassium ions) to pass across it. The selectivity of the membrane may be a function of the particular properties of the membrane, including pore size and charge characteristics of the polymeric structure comprising the membrane. For example, a polyamide membrane, a cellulose acetate membrane, a nano-embedded membrane, a piperazine-derivative membrane and/or other membrane innovation may be used to selectively prevent or at least reduce sulfate, calcium, and magnesium ions from passing across it. In one or more embodiments, membrane  214  may reduce up to about 99% of the sulfate ions. 
         [0071]    In one or more embodiments, membrane  214  is a desalting membrane, which may lower the total salinity or ionic strength of the filtered seawater by preventing or at least reducing ions (e.g., sodium, chloride, calcium, potassium, sulfate, bicarbonate, and magnesium ions) from passing across it. 
         [0072]    In one or more embodiments, membrane  214  is a nanofiltration membrane. Examples of commercially available nanofiltration membranes suitable for use in the treatment process of the present disclosure may include, for example, FILMTEC™ SR90 Series, NF 200 Series, NF90 Series which is available from The Dow Chemical Company (Minneapolis, Minn.), or membranes with similar rejection properties from other membrane manufacturers. 
         [0073]    In one or more embodiments, membrane  214  is a reverse osmosis membrane. Examples of commercially available reverse osmosis membranes suitable for use in the treatment process of the present disclosure may include, for example, FILMTEC™ SW 30 Series, which is available from The Dow Chemical Company (Minneapolis, Minn.), or other membranes with similar rejection properties from other membrane manufacturers. 
         [0074]    As shown in  FIGS. 4A-B , the seawater treatment system  200  may include a membrane system  210  that includes a plurality of membrane pressure vessels (shown as  214 ,  216 , and  218 ), which may be arranged in parallel. Although three membrane pressure vessels are shown, other embodiments may include more or less than three membranes. According to one or more embodiments, each membrane pressure vessel  214 ,  216 ,  218 , may include a plurality of membrane elements  250  installed therein. Although six elements  250  are shown in each membrane pressure vessel, other embodiments may include more or less than six elements  250 . 
         [0075]    Further, in one or more embodiments, at least one of each of a conductivity sensor  224 , a flow sensor  226 , and a hardness sensor  227  may be disposed on the blend/bypass line  225 . In one or more embodiments, each of the conductivity sensor  224 , the flow sensor  226 , and the hardness sensor  227  may be disposed on the blend/bypass line  225  to measure conductivity, flow, and hardness of water, respectively, passing through the blend/bypass line  225  on each permeate of the membrane pressure vessel. For example, as shown in  FIG. 4A , each of the conductivity sensor  224 , the flow sensor  226 , and the hardness sensor  227  may be disposed on the blend/bypass line  225  to measure conductivity, flow, and hardness of water, respectively, in the blend/bypass line  225  after the water passes through each membrane pressure vessel  214 ,  216 ,  218 . Those having ordinary skill in the art will appreciate that each of the conductivity sensor  224 , a flow sensor  226 , and a hardness sensor  227  may be any conductivity sensor, flow sensor, or hardness sensor known in the art. 
         [0076]    Furthermore, in one or more embodiments, the seawater treatment system  200  may include a desalination water controller  265 . In one or more embodiments, the desalination water controller  265  may take signals from desalination plant sensors and output signals to the main plant  240 . 
         [0077]    As shown in  FIGS. 4B-C , according to one or more embodiments, each element  250  may comprise, for example, reverse osmosis membrane elements, nanofiltration membrane elements, or other membrane elements known in the art. Membrane elements  250  may comprise one of several configurations known in the art, for example, spiral wound (SW) and/or hollow fine fiber (HFF). 
         [0078]    As shown in  FIG. 4C , according to one or more embodiments, elements  250  may comprise spiral wound elements  250 . Spiral wound elements  250  may be constructed from flat sheet membranes  254  and  256  and may include a backing material  258  to provide mechanical strength. The membrane material may be cellulosic (i.e., cellulose acetate membrane) or non-cellulosic (i.e., composite membrane). For cellulose acetate membranes, the two layers may be different forms of the same polymer, referred to as “asymmetric.” For composite membranes, the two layers may be completely different polymers, with the porous substrate often being polysulfone. 
         [0079]    In the spiral wound design, the membrane is formed in an envelope that is sealed on three sides. A supporting grid, called the product water carrier, is on the inside. The envelope is wrapped around a central collecting tube  261 , with the open side sealed to the tube. Several envelopes, or leaves, are attached with an open work spacer material  262  between the leaves. This is the feed/concentrate, or feed-side spacer. The leaves are wound around the product water tube  261 , forming spirals if viewed in cross section. Each end of the unit may be finished with a plastic molding, called an “anti-telescoping device,” and the entire assembly may be encased in a thin fiberglass shell (not shown). Feed water may flow through the spiral over the membrane surfaces, roughly parallel to the product water tube  261 . Product water flows in a spiral path within the envelope to the central product water tube  261 . A chevron ring (not shown) around the outside of the fiberglass shell may force the feed water to flow through the element  250 . 
         [0080]    As shown in  FIG. 4D , according to one or more embodiments, elements  250  may comprise hollow fine fiber elements  270 . The design of the hollow fine fiber elements  270  may include a plurality of hollow fiber membranes  272  being placed in a membrane pressure vessel  280 . The hollow fine fiber may be a polyaramid or a blend of cellulose acetates. The membranes  272  may have an outside diameter of about  100  to about  300  microns and in inside diameter between  50  and about  150  microns. The fibers may be looped in a U-shape, so both ends are imbedded in a plastic tubesheet  274 . The pressurized seawater may be introduced into the vessel (indicated by arrow  276 ) along the outside of the hollow fibers. Under pressure, desalted water passes through the walls of the hollow fiber membranes  272  and flows down the inside of the fiber membranes  272  to a permeate collection tube  278  for collection (as indicated by arrow  282 ), while the separated concentrate is removed from the membrane pressure vessel  280  (as indicated by arrow  284 ). 
         [0081]    According to one or more embodiments, all of the membrane pressure vessels in membrane system  210  may comprise elements  250  having only reverse osmosis membrane elements installed therein. In another embodiment, all of the membrane pressure vessels in membrane system  210  may comprise elements  250  having only nanofiltration membrane elements installed therein. In other embodiments, one or more membrane pressure vessel (e.g., membrane pressure vessel  214 ) may comprise elements  250  having either nanofiltration or reverse osmosis membrane elements installed therein while the remaining membrane pressure vessels (e.g., membrane pressure vessels  216  and  218 ) comprise elements  250  having only reverse osmosis or nanofiltration membrane elements installed therein. While specific examples of combinations of membrane pressure vessels and membrane element types are listed here, these examples are not intended to be exhaustive and other combinations may be used. Those skilled in the art will appreciate other appropriate examples and combinations, which are intended to be encompassed by one or more embodiments. 
         [0082]    As shown in  FIGS. 3A-C , one or more treatment blocks  260  may be installed on the deck  304  of a vessel  300 , on the platform  305  of a rig  312 , and/or on the seafloor  316 , depending on the location of the seawater treatment system  200 . Additionally, the one or more treatment blocks may also be installed in other parts of the vessel  300  and/or the rig  312 , or even on multiple levels of the vessel  300  and/or the rig  312 . For example, each treatment block may be installed in a separate container. Several containers can be placed on top of each other to optimize the use of the deck  304  and/or platform  305  to decrease the time and expense associated with construction of the seawater treatment system on the vessel  300  and/or rig  312 . The one or more treatment blocks may be installed in series or in parallel. 
         [0083]    Within the water intake system  201 , water intake pump  204  pumps the intake water through pre-filter  206  to remove any large contaminants (e.g., sand, rocks, plants, debris, etc.) and then through filter  208  to remove large molecules (e.g., suspended solids, colloids, macromolecules, bacteria, oils, particulate matter, proteins, high molecular weight solutes, etc.). After passing through water intake system  201 , the filtered seawater is provided to treatment block  260  by variable speed high-pressure pump  212 . Although only one treatment block  260  is shown, according to one or more embodiments, there may be more than one treatment block arranged in series and/or in parallel. 
         [0084]    According to one or more embodiments, within treatment block  260 , there may be one or more membrane pressure vessels (e.g.,  214 ,  216 , and  218 ). In one embodiment, the pressurized seawater may be pushed through the first membrane pressure vessel (e.g.,  214 ) having one or more elements  250  with membrane elements installed therein, thereby creating a first permeate stream and a first concentrate stream. The first permeate stream may comprise water that has specific ions removed therefrom, for example, the first permeate stream may have lower sulfate ion content and/or lower salinity compared to the filtered seawater produced from water intake system  201 . The first concentrate stream may comprise the ions and/or molecules removed by the membrane elements in the first membrane pressure vessel (e.g.,  214 ). The first concentrate stream may then be disposed of, for example, through a plurality of concentrate discharge ports within the concentrate discharge system  230 . However, before the first concentrate is disposed of, an energy recovery device (not shown) may be used to capture the energy possessed by the first concentrate stream and return such energy to the variable speed high-pressure pump  212 . 
         [0085]    According to one or more embodiments, one or more monitors  226  may be used to determine the characteristics of the output permeate streams created by the one or more membrane pressure vessels  214 ,  216 ,  218 . According to one or more embodiments, one or more monitors  226  may be used to determine the characteristics of the streams created by blending the output permeate streams with the blend/bypass lines. Based on these characteristics, monitors  226  may be used to change the performance of the membranes in pressure vessels  214 ,  216 ,  218  to produce different quality water by controlling the variable speed high-pressure pumps  212  to change, real-time, the amount of water being pumped through membrane pressure vessels  214 ,  216 ,  218 . Similarly, based on these characteristics, monitors  226  may be used to control the amount of untreated filtered seawater water provided to the blend/bypass line  225 , i.e., monitors  226  may be used to trigger an amount of untreated filtered seawater water being blended in with the output permeate streams in order to achieve a water having even more specific characteristics. 
         [0086]    According to one or more embodiments, this process may continue for as many membrane pressure vessels as there are in the treatment block  260 . Additionally, this process may continue for as many treatment blocks  260  as there are in the treatment system  200 , until a final permeate stream, optionally having untreated filtered seawater water blended therein, is produced from a final membrane pressure vessel. The final permeate stream may then be transferred, for example, from vessel  300  to rig  312 , from seafloor  316  to rig  312 , and/or from rig  312  to well  310 , through the permeate transfer and treatment system  220 . 
         [0087]    In one or more embodiments, the membrane elements installed within the membrane pressure vessels (e.g.,  214 ,  216 , and  218 ) are all ion selective membrane elements that lower the salinity or ionic strength of the seawater by selectively preventing or at least reducing certain ions (e.g., sodium, calcium, potassium, and magnesium ions) from passing through the membrane elements, while allowing water and other specific ions (e.g., sulfate, calcium, magnesium, and bicarbonate ions) to be produced for use and/or further treatment. In other embodiments, the membranes elements are all ion selective membranes that selectively prevent or at least reduce hardening or scale-forming ions (e.g., sulfate, calcium, magnesium, and bicarbonate ions) from passing through the membrane elements, while allowing water and other specific ions (e.g., sodium and potassium ions) to be produced for use and/or further treatment. 
         [0088]    In one or more embodiments, the seawater treatment system  200  may include multiple treatment blocks  260 , wherein the multiple treatment blocks  260  each comprise different membrane pressure vessels. For example, in one embodiment, one or more treatment block  260  may include membrane pressure vessels (e.g.,  214 ,  216 , and  218 ) having membrane elements installed therein wherein the membrane elements comprise only nanofiltration membrane elements, while one or more separate treatment block  260  includes membrane pressure vessels (e.g.,  214 ,  216 , and  218 ) having membrane elements installed therein wherein the membrane elements comprise only reverse osmosis membrane elements. Additionally, one of ordinary skill in the art would recognize that the number of treatment blocks in a system may vary in one or more embodiments. Further, one of ordinary skill in the art in possession of the present disclosure will recognize that the membrane elements may vary and may be, for example, spirally wound, hollow fiber, tubular, plate and frame, or disc-type. 
         [0089]    According to one or more embodiments, the variable speed high-pressure pump that operates to push the pretreated water through the treatment block  260  may be controlled by monitor  226  and may comprise any pump suitable to generate the hydraulic pressure necessary to push the water through the one or more membrane pressure vessels. However, the pump discharge pressure must be controlled in order to maintain the designated permeate flow and, more importantly, to not exceed the maximum allowed feed pressure for the membrane elements being used. This is of particular importance because if the maximum allowed feed pressure is exceeded, the membrane element may blow out and thereby fail prematurely. Because the maximum allowed feed pressure for nanofiltration elements is typically much less than the maximum allowed feed pressure for reverse osmosis element, conventional membrane systems having more than one type of membrane (e.g., nanofiltration and reverse osmosis) typically require more than one pump (i.e., a pump for each type of membrane). Conventional systems with nanofiltration membranes installed cannot change to reverse osmosis membranes due to this pressure differential. 
         [0090]    However, according to one or more embodiments, the treatment block  260  may include a variable-speed high-pressure pump  212  that is controlled by monitor  226  and that provides the filtered seawater to more than one membrane pressure vessel. Because the membrane pressure vessels may vary in size and/or may include different types of membrane elements, and therefore require varying feed pressures, the high-pressure pump  212  must be able to provide an adjustable feed pressure based on the type of system being used and based on the water characteristics detected by the monitor  226 . In one or more embodiments, the variable speed high-pressure pump may comprise, for example, a positive displacement pump. 
         [0091]    In one or more embodiments, a pump may be used to provide approximately 16,068 m 3 /d (or 670 m 3 /hr or 2950 gpm) at varying pressures. Specifically, for a seawater reverse osmosis (SWRO) treatment system with an energy recovery device (ERD), the lowest needed pressure is about 26.5 bar and the highest needed pressure may be about 30.2 bar. For an NF system with no ERD, the lower required pressure is about 27 bar while the highest required pressure may be about 39 bar. For a sulfate reducing nanofiltration (SRNF) system with no ERD, the lowest needed pressure may be about 14 bar and the highest required pressure may be about 19 bar. 
         [0092]    One or more embodiments of the present invention may also include variable frequency drives (VFD) on the high-pressure pump. The VFD are systems that control the rotational speed of an alternating current (AC) electric motor by controlling the frequency of the electrical power supplied to the motor. By employing VFD, the pressures created by the variable speed high-pressure pump can also be varied according to the specific needs of the system at any time, for example, as a function of operation, membrane type, water quality objectives, and/or seawater temperature and salinity. 
         [0093]    Referring to  FIG. 4E , in one or more embodiments, a slip stream line  295  may be included in the system. Like elements of the system shown in  FIG. 4E  to the elements shown and described in other embodiments are given like reference numerals and detailed description thereof is omitted. In embodiments including a slip stream line  295 , the controller  260  may also control valves  296  connecting the slip stream line  295  to other lines in the system for addition of specially-treated water. The valves  296  may be located at various positions in the system, e.g., at the entrances of the system pumps, at water blending points in the system, etc. For instance, the slip stream line  295  may contain water having an additive acid or base to assist with balancing the quality of the water being processed. Additionally, the slip stream line may contain warmer or cooler water than the water in the system to assist with balancing the temperature of the water being processed. Controller  260  may blend water from slip stream  295  so as to improve overall system efficiency, reduce power consumption, etc. 
         [0094]    Accordingly, one or more embodiments provide a seawater treatment system having the flexibility to switch between multiple membrane elements using high-pressure pumps that may be varied, real-time, by a controller that monitors the characteristics of the output permeate streams and then transmits a signal to the high-pressure pumps to either pump more or less water through the membrane elements and/or blend in untreated filtered seawater from the blend/bypass line to achieve a water having specifically tailored properties without having to pass through multiple treatment systems. For example, as shown in  FIGS. 4A-4B , VFDs  212 A may be integrated into the seawater treatment system  200  and may allow the pressures created by the high-pressure pumps  212  to be varied according to the specific needs of the seawater treatment system  200  at any time. 
         [0095]    As discussed above, seawater has a high ionic content relative to fresh water. For example, seawater is typically rich in ions such as sodium, chloride, sulfate, magnesium, potassium, and calcium ions. Seawater typically has a total dissolved solids (TDS) content of at least about 30,000 mg/L. According to one or more embodiments, it is preferred that the permeate stream have a total dissolved solids content of between about 1,000 mg/L and about 30,000 mg/L. 
         [0096]    Improved Oil Recovery 
         [0097]    As noted above, improved oil recovery processes commonly inject water into a subterranean hydrocarbon-bearing reservoir via one or more injection wells to facilitate the recovery of hydrocarbons from the reservoir via one or more hydrocarbon production wells. The water can be injected into the reservoir as a waterflood in a secondary oil recovery process. Alternatively, the water can be injected into the reservoir in combination with other components as a miscible or immiscible displacement fluid in a tertiary oil recovery process. Water is also frequently injected into subterranean oil and/or gas reservoirs to maintain reservoir pressure, which facilitates the recovery of hydrocarbons and/or gas from the reservoir. 
         [0098]    According to one or more embodiments, injection fluids may include aqueous solutions (e.g., seawater) that have been treated according to methods disclosed above. In a particular embodiment, the seawater may first undergo filtration in a water intake system whereby the seawater is pumped through a first filter to remove any large contaminants (e.g., sand, rocks, plants, debris, etc.) and then through a second filter to remove large molecules (e.g., suspended solids, colloids, macromolecules, bacteria, oils, particulate matter, proteins, high molecular weight solutes, etc.). One of ordinary skill in the art will appreciate that depending on the specifications of the equipment and the type and density of particulate matter to be removed, various types of filters, including for example, sand or media filters, cartridge filters, ultra filters, and/or micro filters may be used. 
         [0099]    After passing through the water intake system, the filtered seawater may be provided to a seawater treatment system such as the one depicted in the figures of the present disclosure. Specifically, as shown in  FIGS. 4A-B , the filtered seawater may be provided to a treatment block  260  and either sent through blend/bypass line  225  or pumped by variable speed high-pressure pump  212 , which pushes the filtered seawater through to one or more membrane pressure vessels (e.g.,  214 ,  216 , and  218 ), thereby creating a permeate stream and a concentrate stream. 
         [0100]    The permeate stream may comprise water that has specific ions and/or molecules removed therefrom, for example, the permeate stream may have lower sulfate ion content and/or lower salinity compared to the filtered seawater produced from the water intake system. A monitor may be used to detect the characteristics of the permeate stream and, based on these characteristics, control the high-pressure pumps and blend line and effectively produce a water that is customized for a very specific purpose. As shown in  FIG. 5 , the permeate stream may then be transferred, for example, from vessel  300  to rig  512 , from seafloor  516  to rig  512 , and/or from rig  512  to well  510 , through permeate transfer system  520  and used as an injection fluid for improved recovery of hydrocarbons from a subterranean hydrocarbon-bearing formation  514 . 
         [0101]    The concentrate stream may comprise the ions and/or molecules removed by the membrane elements within the one or more membrane pressure vessels. The concentrate stream may then be disposed of, for example, through a plurality of concentrate discharge ports within the concentrate discharge system. However, before the concentrate is disposed of, an energy recovery device may be used to capture the energy possessed by the concentrate stream and return such energy to variable speed high-pressure pump. Also, the concentrate may be diluted or otherwise treated prior to disposal. 
         [0102]    In one or more embodiments, the effluent from the one or more membrane pressure vessels (either the permeate stream and/or the concentrate stream) may take one or more subsequent passes through treatment block  260 . Additionally, in some embodiments, more than one treatment block and/or more than one blend/bypass line may be used in the seawater treatment system. 
         [0103]    In one or more embodiments, a method for recovering hydrocarbons from a subterranean hydrocarbon-bearing formation  514  may include injecting the permeate stream into a hydrocarbon-bearing formation  514  via an injection well  560 , displacing hydrocarbons with the permeate towards an associated hydrocarbon production well  580 , and recovering the hydrocarbons from the formation  514  via the hydrocarbon production well  580 . 
         [0104]    Preferably, the methods of one or more embodiments may result in an increase in hydrocarbon recovery from a hydrocarbon bearing formation, for example in the range of about 2% to about 40%, when compared with a waterflood treatment using untreated high salinity injection water. 
         [0105]    As shown in  FIGS. 6A-B , the systems and methods of one or more embodiments of the present invention may be included in various configurations. Specifically, as shown in  FIGS. 6A-B , a system and/or method of the present invention may be configured so that the variable speed high-pressure pump  212  pushes the filtered seawater  611  through one or more treatment blocks, thereby creating a concentrate stream  634  and a permeate stream (not shown), wherein the permeate stream may then be analyzed using a monitor (not shown) to determine the characteristics of the output permeate stream. Based on these characteristics, the monitor may be used to control the variable speed high-pressure pump  212  real-time by varying the amount of water being pumped through membrane  214 . Additionally, based on these characteristics, untreated filtered seawater from the blend/bypass line  225  may be blended in with the permeate stream in order to achieve a water having specific characteristics. 
         [0106]    The concentrate stream  634  may then be disposed of, for example, through a plurality of concentrate discharge ports within the concentrate discharge system. However, before the concentrate stream  634  is disposed of, an energy recovery device  232  may be used to capture the energy possessed by the concentrate stream  634  and return such energy to variable speed high-pressure pump  212 . Also, the concentrate stream  634  may be diluted or otherwise treated prior to disposal. Alternatively, as shown in  FIG. 6B , a system and/or method of the present invention may be configured so that the concentrate stream  634  bypasses the concentrate discharge system, for example, via elbow piping  613 . 
         [0107]    Additionally, in other embodiments of the present invention, the systems and/or methods of the present invention may be capable of switching back and forth between systems shown in  FIGS. 6A-B . For example, when blending of untreated filtered seawater with the permeate streams is desired, the monitor may be used to control the variable speed high-pressure pump so as to pump an appropriate amount of water through one or more treatment blocks and produce one or more permeate streams which may then be blended with untreated filtered seawater from the blend/bypass line; however, when blending of untreated filtered seawater is not required, the blend/bypass line may be bypassed. 
         [0108]    Furthermore, as shown in  FIG. 7 , a system and/or method according to one or more embodiments of the present invention may include both an energy recover device  232  and elbow piping  613 , wherein the energy recover device  232  and the elbow piping  613  are connected via valves  614 . In one embodiment, the valves  614  may be left open so as to allow the concentrate stream  634  to be piped directly in to the energy recover device  232 . In another embodiment, some valves  614  may be closed so as to bypass the energy recover device  232 . Also, the concentrate stream  634  may be diluted or otherwise treated prior to disposal. 
       EXAMPLES 
       [0109]    The following examples are provided to further illustrate the application and use of the methods and systems disclosed herein for treating seawater. 
       Example 1 
       [0110]    A system comprised of a treatment block of seawater reverse osmosis membranes and a treatment block of seawater nanofiltration membranes is configured such that the flowrates to each treatment block and the respective high-pressure pump to each block can be regulated. The treatment block is comprised such that it produces approximately 60% of the permeate flow using the nanofiltration block operating at 42% recovery and 40% of the permeate flow using the reverse osmosis block operating at 40% recovery. In this example, the specific (target) salinity (total dissolved solids) of the blended permeate is 2,900 mg/L (+/−100 mg/L) and the maximum allowable hardness is 60 mg/L (as defined by the combined calcium and hardness ion concentration, in mg/L). The operating range of the system is 25 to 30° C. 
         [0111]    Exhibit 1 provides the natural deviation of the salinity and hardness of a conventional system, comprised of 60% nanofiltration and 40% reverse osmosis, over the temperature range. 
         [0000]    
       
         
               
             
               
               
               
               
             
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                   
               
               
                 Exhibit 1 
               
             
          
           
               
                   
                   
                 Permeate Flow 
                   
               
               
                   
                 Conventional System 
                 Distribution 
                 Membrane Flux, Lmh 
               
             
          
           
               
                   
                 TDS, mg/L 
                 Hardness 
                 NF 
                 RO 
                 NF 
                 RO 
               
               
                   
                   
               
             
          
           
               
                 25 
                 2918 
                 51.1 
                 60% 
                 40% 
                 14.57 
                 14.50 
               
               
                 30 
                 3723 
                 67.2 
                 60% 
                 40% 
                 14.57 
                 14.50 
               
               
                   
               
             
          
         
       
     
         [0112]    The results indicate that the permeate at 25° C. meets the permeate water quality specifications but the permeate produced at 30° C. does not. 
         [0113]    If the feed flows are reapportioned between the two treatment blocks such that 49% of the permeate flow originates from the nanofiltration block and 51% originates from the reverse osmosis block, with corresponding changes in membrane flux and feed pressures, then the blended permeate quality will meet the water quality specifications at 30° C., as shown in Exhibit 2. 
         [0000]    
       
         
               
             
               
               
               
               
             
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                   
               
               
                 Exhibit 2 
               
             
          
           
               
                   
                   
                 Permeate Flow 
                   
               
               
                   
                 Conventional System 
                 Distribution 
                 Membrane Flux, Lmh 
               
             
          
           
               
                   
                 TDS, mg/L 
                 Hardness 
                 NF 
                 RO 
                 NF 
                 RO 
               
               
                   
                   
               
             
          
           
               
                 25 
                 2918 
                 51.1 
                 60% 
                 40% 
                 14.57 
                 14.50 
               
               
                 30 
                 2905 
                 51.7 
                 49% 
                 51% 
                 15.76 
                 18.50 
               
               
                   
               
             
          
         
       
     
         [0114]    In Exhibit 2, approximately 25% of the NF membranes were removed from service due to lack of need, through the use of automated valve. 
         [0115]    Example 2 
         [0116]    A system comprised of a treatment block of seawater reverse osmosis membranes and a by-pass stream treatment block of seawater nanofiltration membranes is configured such that the flowrates to each treatment block and the respective high-pressure pump to each block can be regulated. The treatment block is comprised such that it produces approximately 92.8% of the permeate flow using the seawater reverse osmosis membrane block operating at 45% recovery and the remaining permeate flow using a slipstream of permeate from a multi-pass nanofiltration membrane block operating at 75%, 80% and 80% recovery, respectively, for the three-pass system. In this example, the specific (target) salinity (total dissolved solids) of the blended permeate is 2,000 mg/L (+/−50 mg/L) and the maximum allowable calcium is 10 mg/L, the maximum allowable magnesium is 10 mg/L, and the maximum allowable sulfate is 10 mg/L. The operating range of the system is 22 to 31° C. 
         [0117]    Exhibit 3 provides the natural deviation of the salinity, calcium, magnesium and sulfate over the temperature range. 
         [0000]    
       
         
               
             
               
               
               
             
               
               
               
               
               
             
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                   
               
               
                 Exhibit 3 
               
             
          
           
               
                   
                 System with Conventional Operation 
                   
               
             
          
           
               
                   
                 Ca 2+ , 
                 Mg 2+ , 
                   
                 Permeate Flow Distribution 
               
             
          
           
               
                   
                 TDS, mg/L 
                 mg/L 
                 mg/L 
                 SO 4   2−   
                 SWRO 
                 3-pass NF 
               
               
                   
                   
               
             
          
           
               
                 22 
                 1872 
                 1.0 
                 2.8 
                 2.3 
                 92.9% 
                 7.1% 
               
               
                 25 
                 2016 
                 1.4 
                 3.3 
                 2.7 
               
               
                 31 
                 2183 
                 2.0 
                 4.6 
                 3.7 
               
               
                   
               
             
          
         
       
     
         [0118]    The results indicate that the permeate produced at 25° C. meets the permeate water quality specifications but the permeate produced outside this design point does not meet the salinity requirement. 
         [0119]    If the high salinity, low hardness, low sulfate slipstream is used to adjust the salinity across the operating seawater temperature range, then the blended permeate salinity can be controlled within the setpoint of 2,000 mg/L, as shown in Exhibit 4. 
         [0000]    
       
         
               
             
               
               
               
             
               
               
               
               
               
             
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                   
               
               
                 Exhibit 4 
               
             
          
           
               
                   
                 System with Conventional Operation 
                   
               
             
          
           
               
                   
                 Ca 2+ , 
                 Mg 2+ , 
                   
                 Permeate Flow Distribution 
               
             
          
           
               
                   
                 TDS, mg/L 
                 mg/L 
                 mg/L 
                 SO 4   2−   
                 SWRO 
                 3-pass NF 
               
               
                   
                   
               
             
          
           
               
                 22 
                 2005 
                 1.1 
                 2.8 
                 2.3 
                 92.3% 
                 7.7% 
               
               
                 25 
                 2016 
                 1.4 
                 3.3 
                 2.7 
                 92.9% 
                 7.1% 
               
               
                 31 
                 2017 
                 1.9 
                 4.6 
                 3.8 
                 93.6% 
                 6.4% 
               
               
                   
               
             
          
         
       
     
         [0120]    For a 100,000 bbl/day (15,898 m 3 /day) injection system, the flowrate of the RO system will vary between 92,300 and 93,600 bbl/day (14,674 and 14,481 m 3 /day) and the NF slipstream requirements will vary between 7,700 and 6,400 bbd/day (1,224 and 1,017 m 3 /day). The control system will adjust the required flows from the respective systems to meet the conductivity setpoint and any excess water can be disposed to sea (due to its high quality) or alternatively, the production of the two systems can be dialed up or turn as needed, noting the resulting change in flux. 
         [0121]    Additionally, while the above embodiments were described as being application for offshore water treatment, one of ordinary skill in the art would appreciate that the treatment techniques may also be used in land-based operations, particularly when the feed water has a high salinity and/or high ionic content. 
         [0122]    Furthermore, one skilled in the art in possession of this specification will appreciate that the system and method are also applicable to other water treatment environments. For example, by substituting one or more treatment blocks as appropriate, municipalities could use the system and method to produce potable or otherwise treated water. 
         [0123]    Advantageously, one or more embodiments may provide one or more of the following. In offshore operations, the most common source of injection water is seawater, which has significant levels of contaminants that may be removed before the seawater can be used as an injection water. Depending on the type of formation being drilled, certain components of the seawater must be removed while others must remain in order to protect the formation from damage and to maximize the hydrocarbons produced from the formation. Using a combination of water treatment approaches may allow for water treatment processes which are able to effectively and cost efficiently prepare injection water that is specifically tailored for the formation being drilled and thereby allows for improved oil recovery. Further, water quality and specific water-characteristics can be closely controlled to ensure maximum effectiveness in varying downhole environments. Also, the water treatment processes may be used to reduce costs associated with the preparation of injection water because the most expensive component, i.e., the high-pressure pump, can be operated at variable pressures using information from the permeate streams and output streams. 
         [0124]    While the invention has been described with respect to a limited number of embodiments, those skilled in the art, having benefit of this disclosure, will appreciate that other embodiments can be devised which do not depart from the scope of the invention as disclosed herein. Accordingly, the scope of the invention should be limited only by the attached claims.