TW200927272A - Low energy system and method of desalinating seawater - Google Patents

Abstract

A low energy water treatment system and method is provided. The system has at least one electrodialysis device that produces partially treated water and a brine byproduct, a softener, and at least one electrodeionization device. The partially treated water stream can be softened by the softener to reduce the likelihood of scale formation and to reduce energy consumption in the electrodeionization device, which produces water having target properties. At least a portion of the energy used by the electrodeionization device can be generated by concentration differences between the brine and seawater streams introduced into compartments thereof. The brine stream can also be used to regenerate the softener.

Description

200927272 IX. INSTRUCTIONS: [Technical Fields of the Invention] The present invention relates to a system and method for seawater desalination, and in particular to a sectional electrodialysis device and a deionization device having a concentration-based potential energy half-cell pair Low energy consumption systems and methods for seawater desalination. [Prior Art] Ο

Desalination is governed by thermal processes such as vapor compression distillers, multiple distillations, and the like. Most of the thermal facilities are located where there is ample power to dilute the seawater. Electrodialysis is generally used to desalinate or desalinate salt water. The reverse osmosis desalination system is now more mainstream because it has lower power consumption and lower capital and operating and maintenance costs than thermal systems. The use of energy recovery devices in reverse osmosis systems has further reduced energy consumption. However, the reverse osmosis technique generally requires at least about 2. 5 仟 watt hours / cubic meter. The thermal program continues to be high power consumption due to the phase changes required for desalination. If waste heat is available, procedures such as thin film distillation can be as low as 1. 5 watt hours / cubic meter of electricity demand. SUMMARY OF THE INVENTION The electrodialysis device of the present invention using low power consumption conditions, and the electrodialysis device potential energy generating half-cells provide a desalination system that has relatively low energy requirements compared to conventional reverse osmosis seawater desalination systems. One or more aspects of the present invention may be directed to an electrodeionization apparatus comprising a first depletion chamber fluidly connected to a source of water having dissolved solids therein, the depletion chamber being at least partially comprised of a cation selective membrane and a first anion a selective membrane defining; fluidly connecting a first 200927272 aqueous liquid source having a first dissolved solids concentration downstream, and ionicly connecting the first concentrating chamber of the first consuming chamber via the cation selective membrane; and fluidly connecting to have a second dissolution A second aqueous liquid source downstream of the solids concentration (which is greater than the first dissolved solids concentration) and is ionicly coupled to the second depleting compartment of the first depleting compartment via the second anion selective membrane. One or more aspects of the invention may be directed to a device for treating water having dissolved ionic species therein. In some embodiments, the apparatus can comprise a first depletion chamber fluidly coupled to the water source and at least partially defined by the first anion selective membrane and the first cation selective membrane; fluidly coupled to have a first dissolution a first concentration chamber of a first aqueous solution of a solid concentration; wherein the first concentration chamber is generally ionicly coupled to the first depletion chamber via one of the first anion selective membrane and the first cation selective membrane; and the fluidly coupled second a second consumption chamber of a second aqueous solution source having a dissolved solids concentration (which is greater than the first dissolved solids concentration), wherein the second depleting chamber is ionicly coupled to the second anion selective membrane by a second cation selective membrane A concentrating chamber. One or more aspects of the present invention may be directed to a seawater desalination system. The desalination system can include at least one first electrodialysis device including at least one first depletion chamber (having a first depletion chamber inlet fluidly connected to the seawater source, with the first depletion chamber outlet), and at least one first concentration a chamber (having a first concentrating chamber inlet and a first concentrating chamber outlet); at least one second electrodialysis unit comprising at least one second consuming chamber (having a second consuming chamber inlet fluidly connected to the seawater source, and a second consumption a chamber outlet), and at least one second concentrating chamber (having a second concentrating chamber 200927272 inlet fluidly connected to the seawater source) and at least one ion exchange unit having a fluidly connected first consuming chamber outlet and a second At least one of the outlets of the chamber exits the inlet of the exchanger, and the outlet of the ion exchanger; and at least one electrodeionization.  The device 'having a first depletion chamber fluidly connected to the outlet of the ion exchanger (this depletion chamber is at least partially defined by the first cation selective membrane and the first anion selective membrane), fluidly connecting the source of seawater and passing through the first The cation selective membrane is ionicly coupled to the first concentrating compartment of the first consuming compartment, to the second consuming compartment fluidly coupled downstream of the brine outlet and ionically coupled to the first concentrating compartment via the second anion selective membrane. One or more aspects of the present invention can be directed to a desalination system comprising a source of water that can have, at least in part, or seawater; for first reducing a concentration of a monoselective species in the first seawater stream to produce a first a means for diluting a stream; means for increasing the concentration of dissolved solids in the second seawater stream to produce a brine stream; means for exchanging at least a portion of the divalent species in the first dilution stream into a monovalent species, wherein the exchange means generally has a second dilution stream outlet; and an electrochemical separation device. The electrochemical separation apparatus generally has a means for fluidly connecting the second diluent outlet and a ionic connection consuming chamber for providing concentration evoked potential energy. One or more further aspects of the present invention may be directed to an electrodeionization apparatus comprising a depletion chamber fluidly connected to a source of water having dissolved solids therein, wherein the depletion chamber is at least partially selected by a cation selective membrane and a first anion The membrane is defined, and the concentration of the ionic connection chamber is half-cell pair. The concentration half-cell pair generally comprises a fluid source connected to a first aqueous liquid source having a first dissolved solids concentration, and is coupled to the first body of the first cation-free 200927272 selective membrane by an ionic selective membrane. a second aqueous liquid source having a second dissolved solids concentration (which is greater than the degree) downstream of the source.  The second half of the membrane is ionicly coupled to the first half-cell chamber. One or more further aspects of the invention include reducing the desalinated portion of the seawater production portion during the first demineralization stage; At least the concentration of the total dissolved solids concentration in the seawater; introducing a portion of the demineralized water into the electrically driven separation device to promote at least a portion of the dissolved species from the chamber of the partial cell of the depleting compartment, and inducing the potential energy in the electrically driven separation device. [Embodiment] The present invention relates to a processing system which may be a water treatment system in some instances or configurations. The invention may be directed to seawater treatment techniques involving seawater treatment or desalination. The systems and techniques of the present invention advantageously provide treated water by utilizing one or more mobile solubilization conditions in the water to be treated. The present invention provides a system for the treatment of water from seawater or salt water. One or more aspects of the present invention provide a drinking water that conforms to the instructions of the woven fabric, which can be manufactured from the total energy consumption of water produced by a typical seawater feed/m3. . It is possible to use a cell chamber which utilizes a difference in concentration for ion separation, and a second anion selective chamber which is concentrated in the first dissolved solid. Regarding the concentration of a monovalent species of seawater desalination, wherein the total dissolved solids of the brine solution is twice in the consumption chamber; and the separation of the brine to the concentration of the concentrated phase of the battery to produce a certain aspect, the implementation of some special favorable system Or the desalination system and the difference in concentration produce a further aspect of the potential energy or power that is beneficial to the body. Or more than 1 in the World Health Organization.  5 kW small Other aspects of the invention Combined electrodialysis and continuous 200927272 Electrodeionization system and device, and novel continuous electrodeionization configuration. Some embodiments of the invention may involve the use of an electrodialysis (ED) device to desalinate seawater to a total dissolved solids (TDS) concentration or salt concentration in the range of from about 3,500 to about 5500 ppm, followed by ion exchange (IX) softening, and finally borrowing a new version Continuous electrodeionization (CEDI) is a multi-step procedure that dilutes to a TDS level of less than about 1,000 PPm salt content. The system and program of the present invention may involve a unique combination of prior and novel techniques, wherein each component is used by advantageously using synergies between different components and unit operations collectively overcoming the individual limitations of current ED and CEDI devices. Reduce or even minimize total energy consumption. For example, because of the energy efficiency of the ED device. Generally, as the TDS level of the product decreases to less than 5 5 00 ppm (usually due to concentration polarization and water cleavage), it can be replaced with a CEDI device and further with a higher relative efficiency. 5500 ppm) of water is desalted because the latter device utilizes an ion exchange resin. In order to address the scale concerns, the softener removes or reduces the concentration of non-monovalent scale formation species. The use of a monovalent selective membrane in, for example, a second parallel electrodialysis train can be used to produce a regeneration stream for the softening stage, which typically has a high concentration of monovalent species, thereby at least reducing, if not excluding, any need for external salt stream storage. Further advantages may include improved water recovery. Some further aspects of the invention may relate to ED and CEDI devices that can operate at sufficiently low current densities such that concentration polarization and water cracking are limited, which reduces power requirements. For example, a seawater desalination system can include a first stage of treatment that preferably reduces the concentration of dissolved species, such as one or more dissolved solids. One of the inventions 200927272 These specific aspects are described with reference to seawater. However, the invention is not limited to treating or desalinating seawater' and one or more of its principles can be used to treat a liquid having a target species to be removed therefrom. .  One or more aspects of the present invention may be directed to an electrodeionization apparatus comprising a first depletion chamber fluidly connected to a source of water having dissolved solids therein. The depleting compartment is at least partially comprised of a cation selective membrane and a first anion a selective membrane defining; fluidly connecting to the first aqueous liquid source having a first dissolved solids concentration downstream, and ionicly connecting the first concentrating chamber of the first consuming chamber via the cation selective membrane; and fluidly connecting with the second dissolved solid a concentration of the second aqueous liquid at a concentration greater than the first dissolved solids concentration. And swimming and ionicly connecting the second depleting chamber of the first depleting chamber via the second anion selective membrane. In some embodiments of the invention, the first aqueous liquid is seawater, which typically has less than about 4% by weight, typically about 3. 3 wt% to 3. 7 wt% of the first dissolved solids concentration, and in some cases the second aqueous liquid is brine having a second dissolved solids concentration of at least about 10% by weight. In one or more further particular embodiments, the depleting compartment is fluidly connected to a source of water having a dissolved solids concentration of less than about 2,500 ppm, or a second dissolved solids concentration to a first dissolved solids concentration of at least about 3. One or more aspects of the invention may be directed to a device for treating water having dissolved ionic species therein. In some embodiments, the apparatus can include a first depletion chamber fluidly coupled to the water source and at least partially defined by the first anion selective membrane and the first cation selective membrane; fluidly coupled to have a first dissolved solid a first concentration -10-200927272 chamber of a first aqueous solution of a concentration, wherein the first concentrating chamber is ionicly coupled to the first consuming chamber via a first anion selective membrane and one of the first cation membranes, and The connector has a second dissolved solids concentration (which is greater than the first dissolved solids concentration).  The liquid-derived second consuming chamber' wherein the second consuming chamber is typically ionicly coupled to the first chamber via one of the second positive selective membrane and the second anion selective membrane. In some embodiments of the invention, the apparatus is further fluidly connectable to a third aqueous solution source having a third dissolved solids concentration (which is less than the second dissolved concentration) and at least one of the first aqueous solution sources. The concentrating chamber is ionicly coupled to the second consuming chamber via one of the second anion selective membrane and the first ion selective membrane. The second concentration, but not necessarily, is ionicly linked to the first depletion chamber via the first cation selective membrane. In a further configuration of some aspects of the invention, the apparatus includes a salt bridge that is, for example, ionicly coupled to the first depleting compartment and the second enrichment in other further embodiments of the invention, the apparatus being Fluidly connecting a source of the second aqueous solution to at least a third depletion chamber having a fourth aqueous solution source having a fourth dissolved solids (which is greater than the third dissolved solids concentration), wherein the third depleting compartment is generally ionicly coupled via a third cation selective membrane Two concentrating chambers. The apparatus may further comprise fluidly coupled to the first aqueous source source, the third aqueous solution source, and the fifth aqueous solution source having a fifth solution concentration (which is less than any second dissolved solids concentration and fourth dissolved solidity) The third concentrating chamber is ionicly connected to the third consuming chamber via the third anion selective membrane. The concentrating chamber may be ionicly coupled to the first consumer via a first cation selective membrane, and the second aqueous chamber containing solids may be concentrated in the first or second chamber. One of the concentration of the step package is selectively condensed to concentrate the third chamber, -11- 200927272 and in some cases, the third concentrating chamber is ionicly connected to the first chamber via a salt bridge. Therefore, in some configurations, this device does not provide an external electromotive potential - the electrode or structure that can pass through its chamber. - In other configurations of the device, the first depleting chamber is fluidly connected downstream of the same source as the first concentrating chamber. One or more aspects of the present invention may be directed to a seawater desalination system. The desalination system can include at least one first electrodialysis unit including at least one first depletion chamber (having a first depletion chamber inlet fluidly connected to the seawater source, with the first depletion chamber outlet), and at least one first concentration chamber (having a first concentrating compartment inlet and a first concentrating compartment outlet): at least one second electrodialysis unit comprising at least one second consuming chamber (having a second consuming chamber inlet fluidly connected to the seawater source, and a second consuming chamber An outlet) with at least one second concentrating compartment (having a second concentrating compartment inlet fluidly connected to the seawater source, and a brine outlet): at least one ion exchange unit having fluidly connected to the first consuming chamber outlet and the second consuming chamber Having at least one of an ion exchanger inlet and an ion exchanger outlet; and at least one electrodeionization device having a first consuming chamber fluidly connected to the ion exchanger outlet (the consuming chamber can be at least partially comprised of the first cation The selective membrane is defined by the first anion selective membrane), is fluidly connected to the seawater source and is selectively oxidized by the first cation Connecting a first ion-concentrating compartment of the first consumer chamber, fluidly connected with the outlet downstream of saline and connected via a second anion selective membrane ionic - concentrating compartment of the second consumer chamber. In one or more embodiments of the desalination system, at least one of the first concentrating compartment and the second consuming compartment is free of ion exchange resin. -12- 200927272 In other configurations of the desalination system, a second concentrating compartment is further included, which is at least a membrane-defined and fluidly connected.  The consuming chamber is selected by the second cation chamber and has a concentrating chamber, a second consuming chamber, and a second concentrating unit that are fluidly connected to at least one of the brine outlet and the second concentrating chamber outlet. ® In some advantageous configurations, the one or more brine storage tanks of the sea, the outlet of one or more chambers and the outlet of the second consumption chamber to the storage tank may each comprise an outlet, at least one of which is at least one ion The exchange unit, or in other configurations, the seawater desalination dialysis unit has a third depletion chamber fluidly connected upstream of the unit. A system of further analysis devices having a fourth depletion chamber upstream of the fluid interconnecting exchange unit. In some advantageous configurations of this system, a monovalent selective membrane disposed in at least one first depletion zone is included. In addition, the ion exchange medium is electrically removed (eg, an ion exchange resin may be water or salt water in some further aspects of the invention. In one or more of the present invention, at least one electrodeionization device is partially selected from the first anion to select the source of the seawater source Fluidly connecting the second concentration port, the outlet of the first concentration chamber, and the inlet. In some cases, at least the water desalination system of the first chamber and the third consumption chamber may further comprise a fluidly connectable portion One of the less concentrated ones. One or more brine reservoirs may be fluidly connected or connected to other units of the system. The system may further comprise a third electricity-consuming chamber downstream and the ion exchange configuration may involve a fourth electroosmosis A mixed bed downstream of the second depleting chamber and the ions, the at least one first electrodialysis chamber and the first depleting chamber of the at least one first depleting chamber sub-assembly may be included. In relation to pre-treated water, preferably in a sea configuration, the desalination system may further comprise at least one pre-treatment unit operation fluidly connected downstream of the source of water to be treated (which may be seawater or salt water), and Preferably, it is fluidly connected or connectable to at least one of the first electrodialysis device, the at least one second electrodialysis device, and the at least one of the at least one electrodeionization device. At least one pretreatment unit operation may comprise at least one secondary system selected from the group consisting of a filtration system, a chlorination system, and a dechlorination system. In some configurations of this system, the pre-processing unit operation may include at least one of a microfilter, a sand filter, and a specific filter. In some cases, the pretreatment system may also include a pressure driven system that selectively removes bivalent species such as sulfate. For example, a nanofiltration system utilizing a FILMTECTM membrane from Dow Chemical Company of Midland, Mich., can be used to reduce the concentration of at least a sulfate species, which should be further operated by one or more downstream units (eg, any electrodialysis unit with Electric deionization device) reduces power consumption. In still other configurations of one or more of the systems of the present invention, at least one of the at least one electrodeionization device comprises an anionic species collector, a cationic species collector, and a salt bridge ionicly connecting the anode to the cathode collector. The ionic species collector can be a chamber that is at least partially defined by an ion selective medium. Advantageously, at least one of the at least one electrodeionization device, the at least one first electrodialysis device, and the at least one second electrodialysis device comprise an anode chamber fluidly connected downstream of the source of the aqueous solution having dissolved chlorine species, the electrode chamber comprising One of the chlorine exports and hypochlorite exports. Further configuration may involve at least one electrodeionization device, at least one first electrodialysis device, and at least one of the at least one second electrodialysis device comprising a second -14-200927272 electrode chamber having an alkali outflow port. One or more aspects of the invention may relate to a desalination system that may at least partially have or be a source of water for seawater;  Means for producing a first set of concentrations of a single selective species in the first seawater stream; means for increasing the concentration of dissolved solids in the second seawater stream: means for diverting at least a portion of the first dilution stream to a monovalent species Wherein the exchange device can have a first port; and an electrochemical separation device. The electrochemical separation device is generally connected to a consuming chamber of the second dilution stream outlet and ionicly coupled to the device for providing concentration evoked potential energy. In some configurations of the desalination system, the means for increasing the concentration of the dissolved solids comprises a fluid An electrodialysis unit that is connected to the seawater chamber, and a monovalent selective membrane and a consuming chamber. An electrodialysis unit for fluidly connecting a concentration chamber of a seawater source for increasing the concentration of dissolved solids in the second seawater stream. a first half cell chamber connecting the first half cell feed stream source (which has a first body concentration) and a fluidly connected second flow source (which has a greater than first total dissolved solids) for providing a concentration evoked potential energy fluid The second half of the battery compartment of the concentration of the first body concentration. The first half of the battery chamber is generally seawater source and the second half of the battery chamber is fluidly connected to the brine source. One or more further aspects of the invention may be directed to a chamber comprising a fluid chamber in which the dissolved solids are fluidly connected, the consuming chamber At least in part consisting of a cation selective membrane and a system comprising selectively reducing the dilution stream, a brine stream valence species exchange, a dilute effluent having a fluid consuming chamber, and a concentrating separation of the source in a seawater stream may comprise And the provision of a salt device may comprise - total dissolved solid half cell feed two total dissolved solid fluid connection 〇 electrically deionized source of consumption of the first anion -15 - 200927272 selective membrane definition 'and at least one ionic connection consumption The pool is thick. The concentration half-cell pair generally comprises a fluid source connected to a first aqueous liquid source having a first body concentration, and the first chamber of the consuming chamber is ionicly coupled via one of the cation selective anion selective membranes, and the fluidly connected second a second aqueous liquid source downstream of the dissolved solids concentration (which is greater than the concentration of the solid solution), and the second half of the first half-cell chamber is ionicly coupled via the first sub-selective membrane in some configurations of the electrodeionization device, The first aqueous liquid water. The second aqueous liquid can be a brine stream having a second body concentration of at least about 0.001% by weight. Thus, in some embodiments of the invention, the two dissolved solids concentrations are at least about 3 for the first dissolved solids concentration. One or more further aspects of the invention may be directed to a method of the sea, including the first a salt phase that reduces the monovalent species of seawater to produce a portion of the demineralized water; a salt solution produced from seawater, at least twice the total dissolved solids concentration in the seawater of the brine solution, the total dissolved solids portion of the demineralized water introduced into the depleting compartment of the electrically driven separation device; A portion of the dissolved species is transported from the depleting compartment to the concentration chamber, and the generating capacity is generated in the concentration of the electrically driven separation device. The method may further comprise a monovalent species concentration of water in the first demineralization stage. Previously, at least a portion of the seawater is passed through the filtration system. In some aspects, the method can further comprise dissolving the non-monovalent species by dissolving at least a portion of the monosubstituted portion of the brine. The semi-electrolyzed solid film and the first half of the first solvent The second body is separated from the chamber. The body is dissolved in the sea, and the first concentration has a degree of lighter than the water; At least the battery concentration reduces the halon price of the species to reduce the sea-16-200927272 The monovalent species concentration of water may involve selectively reducing the concentration of the dissolved monovalent species in the electrodialysis unit. The manufacture of the brine solution may involve promoting at least a portion of the dissolved species. From the seawater transport to the second seawater stream flowing into the concentrating compartment of the electrodialysis unit. The water desalination method may further comprise electrolysis in an electrode chamber (typically an anode chamber) of at least one of the electrolysis device, the electrodialysis device and the electrically driven separation device Generating one of a salt and a hypochlorite species, and electrolytically producing a base stream in one or more chambers of at least one of the electrolysis device, the electrodialysis device, and the electrically driven separation device. Further, the desalination method may also include at least a portion of the seawater At least partially sterilized with the chlorine produced, the hypochlorite species produced, or both. Some specific aspects, embodiments, and configurations of the systems and techniques of the present invention may relate to systems as exemplified in FIG. Water is treated in 1000. The processing system 100 can be fluidly connected or can be connected to a source of liquid 110 to be treated. The liquid to be treated has a mobile ionic species. For example, the liquid to be treated may be or contain water having a salt such as dissolved solids. In a particular application of the invention, the liquid to be treated may be seawater, seawater, or indeed seawater. In other instances, the liquid to be treated may be salt water, contain salt water, or may actually consist of salt water. The processing system 100 may include a first processing stage 120 that fluidly connects the liquid source 110 to be treated. The processing system 100 may further comprise The second stage 130, in the advantageous and third processing stage 140, produces a processed product using point 190. The first processing stage modifies at least a portion of the properties or characteristics of the liquid to be treated. Preferably, the first processing stage 120 is reduced. The at least a portion of the one or more target species in the liquid is to be treated to provide at least a portion of the treatment liquid. Example -17- 200927272 If the first treatment stage 120 can utilize one or more unit operations from source 110 to remove at least a portion of the dissolved species in the seawater, the manufactured salinity content is less than .  The water or water stream 121 is at least partially treated by seawater. A preferred configuration provides at least a portion of the treated water stream 1 2 1 having a salinity content that is at least 5% by weight less than the source of seawater. Other preferred configurations provide at least partially treated water that is at least 10% by weight smaller than seawater. It may utilize a first treatment stage 120 or a target change © or a difference designed to provide a relative concentration or salinity between a liquid to be treated (e.g., seawater) and an at least partially treated liquid stream (e.g., at least partially treated water). The target concentration difference provided by the first processing stage 120 can be based, at least in part, on a number of factors or conditions including, but not limited to, one or more downstream unit operation capabilities, one or more downstream unit operations, one or more requirements In some cases and any one or more of the total water requirements of the processing system 100. For example, the concentration change (e.g., salinity change) provided by the first treatment stage 120 can be determined by desalinating seawater, while providing at least partially treated water that facilitates the treatment of the electrodeionization device, the nanofiltration device, or both. Other factors that may affect the design of the first-processing stage 120 may be indicated, at least in part, by economic or operational considerations. For example, the first processing stage 120 can be designed to provide at least partial processing of water using the available power of existing facilities. Further configurations or alternatives to the first processing stage 120 may involve one or more unit operations for selectively removing one or more targets or predetermined species from the liquid to be treated. For example, the first processing stage can comprise or utilize one or more unit operations that at least partially selectively remove or reduce the concentration of dissolved monovalent species in the liquid to be treated. In other cases, the first processing stage can include or utilize one or more unit operations that provide a product stream in which the concentration of one or more dissolved species is greater than the concentration of dissolved species in the liquid to be treated -18-200927272. In still other cases, the first treatment stage can provide a concentration of dissolved species greater than the auxiliary stream.  The second product stream 123 (which may be a stream of unit operations from the processing system 100 that is not associated with unit operations). For example, the auxiliary stream can be a downstream by-product of one or more sources (not shown). In other cases, the concentration or salinity change provided by the first processing stage 120 in at least a portion of the process stream 102 may be dependent on providing a second stream 123 that is operable to process one or more downstream units of the system 100. In still other cases, the first processing stage 120 provides a salinity greater than the seawater salinity (typically about 3. The second product stream 123 of 5% salinity) is preferably at least about 5% of the second product stream 123, although some specific embodiments of the invention may involve a salinity of at least about 9%. Two product streams 123. For example, the second product stream 123 can be a brine stream having a dissolved solids concentration of at least about 10%, or at least about 99,000 ppm. In other exemplary embodiments, the ratio of dissolved solids concentration in the second product stream 123 to one or more other processing streams of the processing system 100 can be at least about 3, preferably at least about 5, and in certain advantageous situations, For example, a concentration difference V or gradient may be required, which is at least about 10. The second stage 130 can have at least one operating unit that further processes the product stream 121 at least partially. In some embodiments of the invention, the second stage 130 may include one or more unit operations that adjust at least a portion of the features of the process stream 121 from the first stage 121 to provide a second, at least in part, The product stream or modified liquid 1 3 1 is treated. Preferably, the second stage 130 modifies at least two features of the stream 121 to produce a stream. 13 1» -19- 200927272 The third processing stage 140 may modify one or more of the properties or features of one or more of the inlet streams. In a particularly advantageous configuration in accordance with one or more aspects of the present invention, the third processing stage 140 can include one or more unit operations that utilize at least one stream modification from at least one upstream unit operation from one or more The other stream of upstream unit operations, while using point 190, provides a product stream having at least one desired property or characteristic. Further specific configuration of the third processing stage 140 may involve one or more unit operations that produce a product stream 141 that facilitates processing the potential energy difference of the process of stream 13 1 at least in part. In yet a further preferred configuration, the third processing stage can produce another product stream 142 that can be used to process one or more upstream units of system 100. For example, another product stream 142 can be a by-product, or be operated by one or more units of the second stage 130, for example, as a second product stream of the inlet stream in its step or operation, which at least partially facilitates at least partial processing of the stream The conversion of 121 provides a product stream 131 having at least one desired property or characteristic. Further preferred embodiments or configurations of the third processing stage 140 may involve differences in the nature or characteristics of the product stream depending on the nature or characteristics of the liquid to be treated relative to the non-attached unit operation or upstream stage or unit operation from the processing system 100. The unit operates, and at least partially facilitates processing to provide a product stream. For example, the third processing stage 140 can utilize the salinity of the seawater from the source 110 (e.g., stream 1 1 1 ) relative to the salinity of the stream 1 22 The difference is at least partially beneficial to reduce the concentration of one or more target species in stream 131, while producing product water 141 having at least one desired characteristic (e.g., purity). Figure 2 depicts an exemplary water treatment system 200 in accordance with one or more aspects of the present invention. Processing system 200 can include a first processing stage that includes -20 - 200927272 first unit operation 220 and second unit operation 222, each preferably, but not necessarily, fluidly connecting the water source 110 to be treated via its respective inlet. The processing system 200 further includes a fluid connection to receive (generally at its entrance) from the first. - a second phase 230 of each product stream of unit operations 220 and second unit operations 222 (generally from their respective outlets). The processing system 200 can further include a third having an inlet fluidly coupled to the outlet of the second stage 230, an outlet of one or more of the first processing stages, an inlet of the water to be treated, and an inlet of at least one of the non-attached unit operations Stage 240 is processed to provide product water, for example, using or using storage point 190. As described in the specific embodiment of FIG. 2, the first unit operation 220 may provide a first portion of treated water and combine processing water from another portion of the unit operation 222 to produce a partially processed product stream 221. The first stream of water from the outlet of unit 220 may have one or more features that are different from the second stream of water from unit 222. The first and second unit operations are preferably designed to provide at least partially treated water stream 221 having at least one target property for further modification or processing in the second stage 230. The second unit operation 222 can provide a second product stream 223 that preferably has one or more specific or target features. Accordingly, some configurations of the present invention contemplate the overall provision of at least partially treated water stream 221 having one or more particular features while further providing a second product aqueous stream 223 having one or more features generally different from those of stream 221. Unit operations 220 and 222. The first processing stage may utilize a water treatment unit operation, apparatus or system such as, but not limited to, an electrodialysis unit and an electrodeionization unit. A further particular embodiment of the invention may involve a first unit operation that operates at a lower power consumption operation than the second single -21 - 200927272. The first unit operation 220 is operable to produce total dissolved solids from seawater at a water recovery of about 30%.  The water product or stream is at least partially treated at about 2,500 ppm. The second unit operation 222 is operable to produce about 10% saline solution having a dissolved solids concentration greater than about 99,000 ppm from seawater. In another embodiment (not shown), the second stage 130 can include two or more unit operations that receive streams from the first and second unit operations 22 and 222, respectively. One or more of the preferred configurations of the second phase 23 may involve one or more unit operations that alter at least one property of the inlet stream 221 from at least one of the first processing stages. The second stage thus provides a third product stream 23 1 having one or more target characteristics and which can be further processed in a third processing stage 240. Other embodiments of the invention may be directed to an ion exchange unit comprising an anion exchange resin in the form of chloride ions, which exchanges at least a portion of the sulfate species with chlorine species to further reduce the power requirements of one or more downstream unit operations, and in some cases further This downstream unit operation reduces the possibility of scale formation. Thus the exchange unit may involve a cation exchange resin that at least partially reduces the concentration of non-monovalent cationic species (such as Ca2+ and Mg2+) with a monovalent cationic species (such as Na+), and preferably further comprises a monovalent anionic species (eg Cl_) An anion exchange resin that at least partially reduces the concentration of non-monovalent anionic species (e.g., S042.), which reduces the processing power requirements of one or more downstream unit operations. Regeneration of any ion exchange resin type can be carried out, for example, with a waste brine stream that dissolves Na + and cr. The third processing stage 240 can include one or more unit operations utilizing the second product water or the -22-200927272 aqueous stream 223 and other streams from the source 110 (eg, water stream ill) to facilitate processing the third water product stream 231 and Use or storage point 190 provides treated product water. A further preferred configuration of the third processing stage 240 may involve the manufacture of by-product water or aqueous stream 241 that may be used in one or more upstream or downstream stages of the processing system 200. For example, a by-product stream can be used in the second stage 230 for one or more unit operations as an input or reactant during its operation. The third processing stage may utilize one or more unit operations, devices or systems such as, but not limited to, an electrodialysis unit and an electrodeionization device. Figure 3 depicts a seawater desalination system 300 in accordance with one or more aspects of the present invention. The desalination system 300 generally includes a first train having at least one first electrodialysis unit 321A, preferably and at least one second electrodialysis unit 322B. The desalination system 300 can further include a second train having at least one third dialysis unit 323A, preferably at least one second electrodialysis unit 324B. The desalination system 300 can also include at least one ion exchange subsystem 330 having at least one ion exchanger inlet fluidly coupled to the outlet of at least one of the upstream electrodialysis units 321A, 322B, 323A, and 324B. The desalination system 300 can also include a third processing stage 340 that can further process at least a portion of the treated water 331 from the at least one ion exchanger outlet of the ion exchange subsystem 330. The first electrodialysis unit 321A has at least one consuming chamber 321D1 having an inlet fluidly connected to the seawater source 310. The first electrodialysis device 321A also includes at least one concentrating chamber 321C1, which is preferably fluidly connected to the seawater source 310»the second electrodialysis device 322B of the first train, generally comprising at least one consuming chamber 322D2 and at least one concentrating chamber 322C2 . The first -23-200927272 outlet of the consuming chamber 321D1 is fluidly connected to the inlet of the at least one consuming chamber 322D2 and the at least one concentrating chamber.  At least one of the entrances. In some particular embodiments, the inlet of at least one concentrating compartment 322C2 of the second set 322B is a fluid water source 310. A first train having at least one means for treating water 31 in a small portion is preferably produced in accordance with some aspects of the invention, particularly and at least partially. For example, the first train of the desalination electrodialysis device preferably selects 0 dissolved solid species from the seawater, and produces a dissolved non-monovalent dissolved solid species having a lower than seawater and relatively high seawater, and dissolves the single species, and lowers The water stream 321 is at least partially treated by dissolving any one or more of the monovalent species concentrations. In particular embodiments in which selective devalence species are sought, they may at least partially define a depletion chamber using one or more unit prices, and are preferably at least partially chambers. For example, the electrodialysis unit 3 2 1 A may have a portion that is at least partially separated from the first depletion chamber by a monoselective membrane 381 and a monovalent cation selective membrane (not shown) and a monovalent anion selective membrane 381 A concentrating chamber 3 2 1 C 1 , optionally and a second concentrating compartment of the meridional selective membrane (not shown). The second electrodialyte may also be optionally designed to have one or more monovalent selective membranes which facilitate the selective removal or consumption of monovalent species from the water stream introduced therein and accumulated in its concentrating compartment. During operation of the first and second electrodialysis units, the seawater stream is used, fed to the concentrating chambers 321C1 and 322C2, and the 322C2 322C2 electrodialyticly connected to the sea embodiment is characterized in that the water is partially The corresponding ratio of the ratio of the selected species to the solid concentration is determined by the solubility of the monovalent membrane. The first sub-linkage is determined by the concentration of the anion. The first sub-linkage is 185. The consumption chamber or the plurality of singles can be concentrated as one or more -24-200927272 The species removed from the stream in the chamber. The concentrated stream exiting chambers 321C1 and 322C2 and containing species removed from the depleting compartment can be discharged as waste or discarded, or can be used in other non-attached procedures R. At least one third electrodialysis unit 323 A can be designed to provide a product stream that can be used to operate downstream units of the desalination system 300. According to a specific embodiment, the third electrodialysis unit 3 23 A may have at least one consuming chamber 3 23 D1 and at least one concentrating chamber 323C1 ionicly connected to at least one of the consuming chambers 3 23 D1 via the ion selective membrane 3 82 . Preferably, the current applied via the third electrodialysis unit 3 23 A provides sufficient potential energy to provide a product water stream having one or more predetermined or targeted characteristics from the concentrating chamber 3 23 C1. For example, the third electrodialysis unit 323A can also be separated but provides a monovalent selective membrane constituting the ionic connection between the depleting chamber 323 D1 and the concentrating chamber 323C1. The at least one fourth electrodialysis chamber 324B can comprise at least one at least partially an anion. The consuming compartment 3 24D2 defined by the cationically selective membrane and the at least one concentrating compartment 324C2 of at least one of the ionic interconnecting consuming chambers 3 24D2. During the operation of the system 300, the product from the consuming chamber 3 2 3 D1 Water can be introduced into the depleting compartment 324B to further process the seawater from the source 310 and to facilitate the at least partially treated water 22 1 . As exemplarily illustrated, the product water from the depleting compartment 324D2 can combine the product water from the depleting compartment 322D2 321 is configured to at least partially treat the water 221 for further processing. The first train comprising the first and second electrodialysis devices 321A and 322B is operable to produce a target total dissolved solids concentration at a water recovery of about 30% (eg, about 2,500 ppm) of water. The first and second electrodialysis units 321A and 322B can utilize a monovalent anion selective membrane and a cation selective membrane to -25 - 20092727 2 less, and preferably at least the first electrodialysis device 321A ion selective membrane and monovalent cation selective membrane, which should be at least .  Any pot scale may be. A brine stream comprising third and fourth electrodialysis units 323A and 324B operable to produce a target salinity content of about 10% (NaCl) in a concentrated stream from one or more of its concentrating compartments. Preferably, the dialysis unit produces a sufficient degree of salinity brine when operated at a water recovery of about 70%. The fourth electrodialysis unit 3 24B is operable to recover at least a portion of the target dissolved solids content of about 2,500 ppm and preferably at a recovery of about 48%. In some embodiments of the invention, the total recovery of the second train may be about 40%. The ion exchange subsystem 330 can be designed to receive at least one partially treated water 22 1 and to convert or modify at least one of its specific one or more aspects. Some embodiments relate to the concentration of a target dissolved species that selectively treats water. At the same time, at least partially transporting at least a portion of the non-target or other dissolved species, while the dissolved species replaces at least a portion of the retained dissolved species. For example, water, water 221 can have a relatively high concentration of non-monovalent dissolved species, magnesium, and is treated to exchange at least a portion of the non-monovalent species (e.g., sodium). Some configurations of the exchange subsystem 330 may involve an exchange train (not shown) of the catalyst or ion exchange media bed. The first train may comprise a leading ion exchange bed, which in turn may replace the non-monovalent dissolved species (e.g., Ca2+ and Mg2+) in the water with a monovalent dissolved species (e.g., Na+). The second ion is reduced by the unit price, and the second train is made to have the third electricity. At least the target is manufactured with the treated water, and the specific specific fraction is at least. The origin of the reduction is intended to be retained or suppressed. The target is compared to the sea (such as calcium and the formation of two soft-ion exchange exchanges, and a small part of the exchange train -26-200927272 can similarly contain the tandem connection and backward An ion exchange bed. In operation, one of the first and second ion exchange trains may have a fluid connection port to receive at least a portion of at least a portion of the treated water 221 and an exchanged water stream having a lower concentration of monovalent dissolved species. The first ion delivery is saturated by a non-monovalent species, such as a non-monovalent versus monovalent ion exchange procedure, a second ion exchange train can be utilized. The first train can then borrow an aqueous stream of a rich monovalent dissolved species to replace at least a portion of the combined Regeneration of the non-monovalent species of the ion exchange medium of the bed. Ion exchange ❹ may comprise a regeneration of a mixed bed ion exchange medium of an ion exchange resin such as the commercially available AMBERLITETM and AMBERJETTM resins from Rohm and of Philadelphia, Pennsylvania. This is carried out by using a brine solution 261 having a sufficient salinity (e.g., about 10%) from a brine storage tank. Stream 332 can be discharged as a reject. The salinity of the ion exchange medium can be greater than the thermal resistance of the non-monovalent species exchange matrix. The third treatment stage 3 40 can include one or more electrodeionization devices. In some embodiments of the present invention, the third processing stage may include at least one of the conventional electrodeionization device described above and the modified electronic device described in FIG. 5. In accordance with one or more of the present invention In a further configuration of the aspect, the third processing stage may comprise one or more electrodeless continuous devices. The electrodeionization device described in FIG. 4 generally comprises at least one ocean 411 and at least one adjacent consuming chamber 411. Once configured, 14 1 2. Each of the consumption and concentrating chambers is at least partially selected by any anion selection period. The junction is replaced by the sub-unit Haas 0 260. It is sufficient to join the other ions. The ventricular ventricular membrane -27- 200927272 AEM is defined by the cation selective membrane CEM. In contrast to the electrodialysis unit, the chamber of the electrodeionization device contains a cation exchange resin and an anion exchange resin. .  During the current application operation, the cationic species (e.g., Na+) generally moves to the cathode (-) of the device, and the anionic species (e.g., C1·) move toward the anode (+) of the device 400. The anion selective membrane AEM and the cation selective membrane CEM capture moving or transported dissolved species (Na + and Cl_) in each concentration chamber 412 into a reject stream R. The feed to one or more of the depleting compartments is typically a softened water stream 331 from ion exchange subsystem 330. The product water from the depleting compartment can then be stored or transported to the point of use. One or more power sources (not shown) typically provide electrical energy or power to the electrodeionization device 400 that facilitates separation of the target dissolved species. In some cases, a portion of the electrical energy is used to separate the hydrolysis into H + and 0 species. The power supply can be controlled to provide the desired or target electrical flow, the desired or target voltage or potential level, and the current polarity. Figure 5 illustrates, by way of example, a modified electrodeionization apparatus 500 that can be used in a third processing stage of a processing system. Apparatus 500 includes at least one first depleting chamber 511 (which is generally at least partially defined by first cation selective membrane 521C' and first anion selective membrane 531A), at least one first concentrating compartment 52 1 , and at least one first Concentration chamber 54 1 (which may be at least partially defined by second anion selective membrane 5 3 2 A and ionicly coupled to first consumable chamber 511 via at least a portion of first cation selective membrane 521C). The apparatus 500 can further include a second depleting chamber 512 that is at least partially coupled to the first concentrating compartment 541 via at least a portion of the second anion selective membrane 532A and at least a portion of the second anion selective membrane 532A. Electrodeionization apparatus 500 can further comprise a second concentrating compartment 542 that is at least partially defined by third cation selective membrane 523C -28-200927272. The second concentrating chamber 542 is preferably at least partially ionicly coupled to the first consuming chamber 511 via the first anion selective membrane 531A. Electricity .  The deionization device 500 can further comprise a third depleting compartment 513, preferably defined by a third anion selective membrane 533A. The third depleting chamber 513 is preferably at least partially ionically coupled to the second concentration chamber 5 42 via the third cation selective membrane 523C. The electrodeionization apparatus 500 generally has an anode chamber 562 surrounding the anode and a cathode chamber 564 surrounding the cathode. According to other aspects of the invention, the electrodeionization apparatus 500 includes a first deuterium consuming chamber 511' comprising a cation exchange medium and an anion exchange medium, such as a cation exchange resin CX and an anion exchange resin AX, and at least partially The cation selective membrane 521C is defined by a first anion selective membrane. In some cases, only the first depleting compartment, or the chamber downstream of any depleting chamber that only receives or fluidly connects the electrodialysis unit to the ion exchange unit, contains an electroactive medium such as an ion exchange resin, and the other chambers are free of ion exchange media. For example, in some configurations of the electrodeionization apparatus 500, the one or more first consumption chambers 511 each comprise a mixed bed of ion exchange resins, and one or more of the first concentration chambers 541, one or more second consumptions The chamber 512, the one or more second concentrating chambers 542, and the one or more third consuming chambers 513 are each free of ion exchange media. In operation, power from a power source (not shown) provides electrical energy to an electric field typically generated by the anode and cathode across the electrodeionization device 500. The water to be treated, for example, from the outlet of the first stage ion exchange unit 330, enters the depleting chamber 511 through its inlet. The water to be treated has dissolved species that are movable in the electrodeionization device 500 under the influence of an electric field. Because of the ion exchange procedure of unit operations 〇 -29- 200927272, water stream 331 generally contains a relatively high amount of the target dissolved monovalent species (Na + and C1·) relative to the non-monovalent species. Thus, the additional energy and operating costs of the second stage 330 can be reduced (if not excluded) because the energy associated with facilitating the transport of the monovalent species can be relatively less than the energy associated with facilitating the transport of the non-monovalent species. The monovalent species generally moves to the corresponding attracting electrode and further passes through the anion or cation selective membrane to one of the first concentrating compartment and the second concentrating compartment. For example, the cationic Na+ species can be attracted to the cathode and generally pass through the cation selective membrane 52 1C, while the anionic species C1- can be attracted to the anode, and generally through the anion selective membrane 531A. The product stream from the outlet of the consuming chamber 331 typically has a reduced concentration of the target dissolved solid species. In some configurations of the invention, a stream having a first dissolved solids concentration can be used as a concentrated stream to collect moving target dissolved solid species. For example, the salinity is about 3. The 5% seawater stream 111 can serve as a concentrated stream introduced into the first concentration chamber 541. The stream leaving the first concentrating compartment 541 is thus generally rich in mobile cationic or anionic species. This stream can be discharged into waste or abandoned stream R. Also during operation, it generally introduces another feed stream to the second concentration chamber 512 and the third concentration chamber 5 13 . The electrodeionization apparatus 500 may further include a first concentrated battery pair 531, and optionally a second concentrating battery pair 523, each of which is preferably ionicly coupled to the first consuming chamber 511. The first concentrated battery pair 531 may include a first half cell chamber 541 (which is fluidly connected to a first aqueous liquid source having a first dissolved solids concentration and fluidly connected to the depleting chamber 511 via the first cation selective membrane 521C), and The second half of the battery compartment 512. The second half of the battery room is generally -30-

(conci) (concl) ~nF 200927272 Ionically connected to the first d via the anion selective membrane 532A The second concentrated battery pair 532 may comprise a third half cell - cell chamber 513. The third half of the cell chamber is typically connected to the consuming chamber 511 via an anion. The fourth half cell compartment generally has a membrane 52 3 C ionicly coupled to the third half cell compartment 542. A further advantageous feature of the invention may involve a difference in concentration between the pools of different dissolved components by the respective feed streams. The difference in concentration produces a potential energy that can be at least partially quantified, such as an electromotive force potential (volts η Ε = - where cowci is the concentration of the stream introduced into the second half-cell 512, and co«c2 is introduced into the first half-cell 541 The flow concentration, which is a gas constant of 8.314 joules / (K·mole), is 298 K, "the number of electrons transferred in the reaction of the battery" and some preferred groups of the Faraday constant of 96,498 coulombs/momming. The state may involve a solution I 223 for use in the seawater stream 111 introduced into the first depleting compartment. It may be used with a salinity of generally at least about 8%, preferably and more preferably at least about 12%, or at least about preferably at least Preferably, the salt water of at least 99,400 ppm, and more preferably at least the dissolved solids concentration, is introduced as the second semi-electricity: preferably the second and fourth half-cells 512 and 513 are also introduced into the fourth half-cell chamber 513. 3 battery chamber 541. The chamber 542 is selected from the fourth half! The selective membrane 531A is similar in composition to the cation selective supply, and the dissolved solid enthalpy of the dissolved solid 111 adjacent to the Nernst equation 223 is established as a temperature. Generally, for sea water and salt water. Thus, the brine stream having a large concentration of dissolved solids concentration in accordance with the present invention is at least about 10%, 80,000 ppm > more than about 1 20,000 ppm in tank 512, and stream 223. Each leaving still has water relative to sea-31 - 200927272 a high brine concentration, and can be directed to a brine storage tank for introduction into the first half-cell chamber 54 1 and, optionally, the third half-cell. The feed stream 1 1 1 can be seawater or have a salinity of about 3. 5 % or an aqueous stream having a solubility of less than about 36,000 ppm. The above example shows that the concentrated battery pair is about 0.026 volts. Therefore, the present invention can be advantageous for the potential energy of real estate seawater treatment or desalination. Example 1 below provides for utilization in concentration. In the first stream and the second stream, based on the predicted capacity of the exemplary conditions, wherein the dissolved solids concentration of the second stream is greater than the dissolved temperature of the first stream. In some cases, the concentration of one or more devices in the third processing stage is sufficient. The battery pair provides a substantially all potential energy required to dilute the product stream, 331. In this configuration, the device can sub-connect a salt bridge (not shown) of the half cell chamber of the device, wherein General Qualitative, such as potassium chloride or sodium chloride. For example, the first end of the salt bridge can be separated from the second half of the battery chamber 512 and the fourth half of the 513 with the second chamber 513 » V Figure 6A and 6B depict the electrodeless continuous The ion device 610, which may be a Dunant potential or a Dunant enhanced EDI device, according to still further aspects of the invention. The device 600 may include a housing 60 surrounding the at least one consuming chamber 611 (each having a liquid to be treated 331 introduced therein) 1. The apparatus can further comprise at least one first concentration (each having a first feed stream 111 introduced therein), and at least one depletion chamber 612 (each having a second feed stream 223 introduced therein). The device further comprises at least one second concentrating chamber 622, each of which has a 260 chamber 542 solid concentration for each of the battery-converted potential solids, including a sufficient degree to contain an electronically connected battery chamber 600 and an auxiliary unit. The first cylindrical chamber 62 1 is secondarily 600 having a third -32 - 200927272 feed stream 112 introduced therein. The first depleting chamber 611 can be defined by an anion selective membrane 64 1A and a cation selective membrane 651C. The first concentrating compartment 621 can be defined by an anion selective membrane (e.g., membrane 641A) and a second cation selective membrane 652C. As exemplarily described, the first depleting chamber is ionicly coupled to the first depleting chamber via membrane 641A. The second depleting compartment 612 can be defined by a cation selective membrane and a second anion selective membrane 642A. Preferably, the second depleting chamber 612 is ionicly coupled to the first concentrating chamber 621 via the cation selective membrane 652C. The second concentrating compartment 622 can be defined by an anion selective membrane and a cation selective membrane boundary. Preferably, the second concentrating compartment is ionicly coupled to the second consuming chamber 61 by the second anion selective membrane 642A. A further preferred configuration may involve a second concentrating chamber having a first consuming chamber 611 ionically coupled to one of the first cation selective membranes 651C via a salt bridge. Member 66 1 provides ion and electrical insulation and structural support for the chamber. The second feed stream 223 typically has a dissolved solids concentration greater than the first feed stream hi and is preferably a dissolved solids concentration that is also greater than the dissolved solids concentration of the third feed stream 112. The dissolution of each of the first feed stream and the third feed stream ❹ solid concentration may be the same as or less than the dissolved solids concentration in the liquid to be treated 331. As noted above, the concentration between the paired half cells 612 and 621, and 612 and 622 can produce a potential for facilitating the transport of Na+ and C1 species from the depleting chamber 611, as described, to produce a product stream. Like the electrodeless device 600, the device 610 depicted in Figure 6B includes a second battery pair 'which includes a depleting chamber 613 and a concentrating chamber 623 each having a feed stream 113 and 114. Feed stream 113 can be brine' from, for example, electrodialysis unit 323a and feed stream 114 can be seawater from source 310. Dolly-33-200927272 The consumption and concentration chambers of the seawater and brine streams advantageously produce a potential energy sufficient to drive at least a portion of the treated water having a dissolved solids concentration of, for example, about 2,500 ppm, and is manufactured to have, for example, about 500 ppm. The target dissolves the product water in solid concentration. Other configurations may involve at least partially including any one or more of the feed streams and H4 that at least partially treat the water 331, which may provide a greater concentration difference relative to the brine stream 223. Further significant differences include the direction of countercurrent flow of some of the flow through the chamber. As described, the second stream 1 1 1 can be introduced into the first concentrating chamber countercurrently into the flow in the first consuming chamber 61 1 or, in some cases, in the direction of the third stream 223 in the second consuming chamber. 621. The difference in concentration between the second and third streams produces the potential energy driven by the half-cell reaction of the dissolved species (e.g., Na + and Cl_). Any of the membranes in units 00 and 610 can be monovalent anion selective or monovalent cation selective. In some configurations of the invention, an electrolysis device (not shown) can be used to produce an aqueous solution comprising a disinfecting species such as chlorine, chloride, hypochlorite, and hypobromite. In other configurations, at least one of the electrodeionization device and any one or more electrodialysis devices can be used to produce any one or more of an acidic solution, an alkaline solution, and a disinfecting solution. For example, a relatively pure water stream can be introduced into the anode chamber (+) to collect and agglomerate the H + species to produce an acidic outlet stream having a pH of less than 7. Chlorine-containing solutions can be introduced into the cathode compartment in the feed stream to facilitate the production of sterile species such as chlorine and hypochlorite species. Gaseous hydrogen by-products can be vented or discharged. Any of various subsystems, stages, trains, and unit operations of the present invention - 34- 200927272 may utilize one or more controllers to facilitate, monitor, and/or adjust its operation. Preferably, the controller (not shown) monitors, and in some cases controls, the components of the system of the present invention. The controller can be implemented using one or more computer systems. The computer system can be, for example, a general purpose computer such as an Intel PENTIUM® based processor, a Motorola PowerPC® processor, a Sun UltraSPARC® processor, a Hewlett-Packard PA-RISC® processor, or any other type of processor or combination thereof. . Alternatively, the computer system may include special stylized special purpose hardware, such as an application integrated circuit ASIC or a controller intended for use in an analysis system. The computer system can include one or more generally connected one or more memory devices (which can include, for example, any one or more of a disk drive memory, a flash memory device, a RAM memory device, or other storage for storing data) Processor of the device). Memory devices are typically used to store programs and data during operation of the processing system and/or computer system. For example, a memory device can be used to store historical data about the parameters over time, as well as operational data. The software (including the code for implementing a specific embodiment of the present invention) can be stored in a computer readable and/or writable non-volatile recording medium and then generally copied to a memory device, where it can then be processed by the processor carried out. This code can be written in any one or more programming languages, such as Java, Visual Basic, C, C# or C++, Fortran, Pascal, Eiffel, Basic, COBAL, or any combination thereof. The components of the computer system can be connected to an interconnection mechanism that can include, for example, one or more bus bars between components integrated into the same device, and/or between networks (e.g., between components on separate discontinuities). Interconnect mechanisms generally -35 - 200927272 allow, for example, information, instructions to be exchanged between their components for communication. The computer system may also include one or more input devices such as a keyboard, mouse, trackball, microphone, trackpad, valve, position indicator, fluid sense, temperature sensor, conductivity sensor, pH sensing And the composition analyzer 'and one or more output devices' such as printing devices, display screens, or horns, actuators, power supplies, and valves. In addition, the computer system can include one or more interfaces not shown which can additionally connect the computer system to a communication network or to a network that can be formed by one or more system components. In accordance with one or more embodiments of the present invention, one or more input devices may include sensors for measuring one or more parameters of the processing system. Or sensors, metering valves and/or pumps, or all of these components can be connected to a communication network that is operatively connected to the computer system. For example, the sensor can be designed to be directly connected to the input device of the computer system, and the metering valve and/or pump can be designed to connect to the output device of the computer system, and any one or more of the other computer systems or components can be connected to the communication network and the computer. System communication. This configuration allows a sensor to be placed at a long distance from other computers or to distance any sensor from any secondary system and/or controller while still providing data between them. The controller can include one or more computer storage media, such as readable and/or writable non-volatile recording media, in which signals defining programs to be executed by one or more processors can be stored. The media can be, for example, a disk or a flash memory. In a typical operation, one or more processor packages may cause data (such as encoding of one or more embodiments of the present invention) to be read from a storage medium to a memory structure that may cause one or more processors Get information faster than the media. This memory structure is generally a volatile random access memory (such as dynamic memory DRAM or static memory SRAM), or other suitable device that facilitates the transfer of information back and forth from the processor. Although a computer system, such as a computer system that can perform various aspects of the present invention, is exemplified, it should be understood that the present invention is not limited to computer systems implemented in software or by way of illustration. In fact, in addition to being implemented, for example, in a general purpose computer system, a controller, or a component or subsystem thereof, it may be implemented in a proprietary system or in a decentralized control system with a dedicated programmable logic controller PLC. Furthermore, it is to be understood that one or more features or aspects of the invention can be implemented in the form of a soft body, a hardware or a s. For example, one or more of the algorithms that the controller can execute can be implemented in separate computers, which in turn can communicate via one or more networks. The functions and advantages of these and other embodiments of the present invention can be further understood from the following examples which describe the benefits and/or advantages of one or more of the systems and techniques of the present invention, but are not intended to illustrate the full scope of the present invention. . Example 1 In this example, a concentration battery pair is utilized in some configurations of the apparatus of the present invention to produce the desired potential energy. Table 1 below provides the calculated potential energy based on the flow equation introduced into the half cell chamber according to the Energy equation at room temperature. The table below shows that the ratio of feed stream concentration is preferably as large as possible to increase the potential energy produced. For example, the concentration ratio can be at least about 2, preferably at least about 3', more preferably at least about 5, and even more preferably at least about 1 Torr. -37- 200927272 Table 1 CONC1 CONC2 E (volts) E (millivolts) 1 1 0 0 10 1 0.059 59.1 100 1 0.118 118.2 1,000 1 0.177 177.4 10,000 1 0.024 236.5 2 1 0.018 18.8 3 1 0.028 28.2 4 1 0.036 35.6 5 1 0.041 41.3 6 1 0.046 46.0 7 1 0.050 ' 50 8 1 0.053 53.4 9 1 0.056 56.4 5.68 1 0.044 44.6 2.3 1 0.021 21.4 The table below provides the ion concentration of typical seawater. The main cationic species in seawater are Na+, K+, Ca + 2, and Mg + 2, and the main anionic species are (1_ and S042'. The concentration of bicarbonate and carbonate species depends on the pH of water. Set. -38 - 200927272

Species concentration (ppm) Chloride 19,353 Sodium 10,781 Sulfate 2,712 Magnesium 1,284 Potassium 399 Calcium 412 Carbonate/Bicarbonate 126 Bromine 67 缌7.9 Boron 4.5 Fluoride 1.28 Lithium 0.173 Iodine 0.06 钡 less than 0.014 Iron ' Less than 0.001 猛 less than 0.001 0.001 Cobalt less than 0.001 Copper less than 0.001 Nickel less than 0.001 Selenium less than 0.001 Vanadium less than 0.002 Zinc less than 0.001 Molybdenum less than 0.01 Aluminum less than 0.001 Lead less than 0.001 Arsenic less than 0.002 Cadmium less than 0.001 Nitrate 1.8 Phosphate 0.2 Example 2 This example is illustratively provided in accordance with the present invention Some of the aspects can be used to electrodialysis trains. -39 - 200927272 Figure 10A exemplarily depicts an electrodialysis unit train that can be used in the first train 220 of the first processing stage. Train 220 can include multiple stages, each of which operates at an optimum voltage and current density to minimize energy usage. As described, train 220 can have four electrodialysis unit stages. In the first train, the consuming chambers can be connected in series and the dilution streams are cascaded to feed the product from one stage as a feed to the downstream consuming chamber. Fresh seawater is used as the feed to each concentration chamber in each stage to minimize any difference in concentration between the dilution and concentration chambers in each stage. ® There are also several ED modules that operate in parallel at each stage. The second train 222 can also include a multi-electrodialysis unit stage having a consumable chamber connected in series. The consuming chambers may also be connected in series to increase the concentration of agglomerated NaCl in the brine stream therefrom to a salt concentration of about 10%. As depicted in Figure 10B, the second train 222 can have four electrodialysis stages, each preferably utilizing a monovalent selective membrane. The third train (not shown) may also involve multiple electrodialysis stages to facilitate reducing the dissolved solids concentration of the water stream to a range of from about 3,500 ppm to about 5,500 ppm. Example 3 This example describes an expected performance of desalinating seawater at a rate of about 8,000 cubic meters per hour using a system substantially as shown in Figure 3 of the present invention and the apparatus depicted schematically in Figure 4. It simulates two electrodialytic (ED) device trains with finite components with softeners and electrodeionization (EDI) devices. Several stages are used for finite element simulation; Stages 1-5 are designed to produce a brine system with at least 10% NaCl; -40-200927272 and the last two stages are designed to absorb dissolved solids from the softener and electrodeionization streams . Tables 2 and 3A-3C below are listed. Calculation results. Table 4 summarizes the predicted energy requirements of the ED/EDI system. Figure 7 graphically depicts the projected energy required for seawater desalination to produce various target waters. It is assumed that the incoming seawater has a TDS of about 35,700 ppm (TDS) after pretreatment with a commercially available pretreatment device for filtration (not shown). It should be noted that extensive prior processing (e.g., generally with reverse pretreatment) is not necessary for the ED/CEDI procedure of the present invention to pass water through the membrane. The feed water is divided into ED train 1, ED train 2, and the concentrated stream (salt water) of the vehicle 2 is designed to be fed to the CEDI column | ED train 1 passes through two stages to elect each stage. Train 1 manufactures 2,500 ppm at approximately 30% recovery. It is expected to use a standard electrodialysis module for this train. The use of a monovalent selective ion exchange membrane in Section 1 should minimize the concentration chamber 〇 v energy. ED train 2, stage 1 is designed to make a (salt) solution in a concentrated stream. The brine is used to regenerate one of the concentrated streams downstream of the softener and in the module. This electrodialysis stage uses a monovalent exchange membrane to make a 10% NaCl solution in a concentration chamber. The ED train was operated at about 70% recovery to produce a brine solution. ED | 48% estimated recovery. The total recovery of the ED train 2 is approximately at least partially treated with product water having a reduced production simulation parameter of about 2,500 ppm. The standard feature produces a total dissolved solids infiltration system of 10 microns before, because in this ED column, the 0 0 force utilizes the optimum TDS quality to produce 10% NaCl in the scale of the train. As a CEDI selective ion exchange: Phase 1 of Phase 1 Wall segment 2 has a TDS of 40% ,, and -41 - 200927272 has a high calcium and magnesium ion content from the second train. The water stream is at least partially treated to soften in the softener or ion exchange unit to exchange calcium and magnesium ions for sodium ions. The softened feed from the softener to the downstream CEDI train should not have the tendency to form scale during the desalination to the target water quality. The softener is periodically regenerated by the ED train 2, the 10% brine solution supplied in phase 1. An electrodeionization device provides for the transport of Na+ and C1· ions from the brine stream (10% NaCl) to the abandon stream. Transporting the counter ion self-dilution stream to the abandon stream 3 should maintain electrical neutrality. The net thermodynamic voltage across the flow is reduced because at least a portion of the DC voltage is generated by the half cell pair. Although not depicted, any EDI reject stream can be recycled for feeding into the ED unit. > The eluate from the brine chamber can be discharged to a storage tank as a softener regenerant. Some simulation parameters (TDS concentration and flow rate) are included (refer to Figures 2 and 3): • Inlet 35,700 ppm 海水 Seawater inlet: 25,277 m3/h First stage

The first ED train 22 0, the first ED device 321A and the second ED device 322B 3, 100 cubic meters / hour 5, 1 67 cubic meters 7 hours 49,929 ppm 10,000 ppm The inlet seawater concentrating chamber 321C1 inlet seawater from the consumption chamber 321D1 comes from Inlet of the concentrating chamber 3 2 1 C 1 of the abandonment consuming chamber 322D2: 3,1 0 0 m 3 /hr -42 - 200927272 2,067 m 3 /hr 49,929 ppm 2.500 ppm 99.500 ppm Concentration chamber 322C2 inlet seawater: From Abandonment of chamber 322C2: product water 321 from chamber 322D2: brine from ED train 222:

Second ED train 222, third ED unit 323A and fourth ED unit 324B 4,900 cubic meters / hour 2,100 cubic meters / hour 99,467 ppm (10% salinity) 10,000 ppm 5,277 cubic meters / hour 42,664 ppm 2.500 ppm 2.500 ppm Inlet seawater of the consumption chamber 323D1: Concentration chamber 3 2 3 C 1 inlet seawater: outlet brine from chamber 323C1: 入口 inlet of the consumption chamber 324D2: inlet water of the concentration chamber 324C2: abandon flow from the chamber 3 24 C2: chamber 324D2 The outlet: • the inlet of the second stage softener 330: • the third treatment stage of the electrodeionization device 340 The inlet of the consumption chamber 511: 8,000 cubic meters / hour The inlet of the first concentration chamber 541 seawater: 2,667 cubic meters /hour chamber 5 12 inlet (salt water): 2,100 cubic meters / hour (10% salinity) outlet brine from chamber 512: 91,848 ppm • product 500 ppm from chamber 5 1 1 exit: -43 - 200927272 Table 2 TDS in the total ED total ED/EDI product stream feed 35,700 ppm 35,700 ppm TDS in the feed stream 35,700 ppm 35,700 ppm Recovery 39.9% 32.9% Flow rate by membrane area (flux) 1.79 gfd 0.0030 m/hr 1.60 gfd 0.0027 m/h r Product TDS 2,500 ppm 500 ppm Abandoned TDS - Stage 1 to 5 99,467 ppm Abandoned TDS - Stage 6 and 7 42,664 ppm Total power 1,706 kW 1,799 kW Total energy required per unit of production 1.39 kWh/m3 5.27 kWh/Kgal 1.47 kWh/m3 5.56 kWh/Kgal Membrane area by flow rate 0.560 ft2/gpd 329.9 m2/(m3/hr) 0.627 ft2/gpd 369.1 m2/(m3/hr) Product flow rate 1,225 m3/hr 1,225 m3/hr Flow rate Stage 1 to 5 525 m3/hr Discharge flow rate Stages 6 and 7 1,319 m3/hr Discharge flow rate, total ED 1,844 m3/hr Discharge flow rate, total ED/EDI 2,504 m3/hr Total projected membrane area 404,068 m2 452,171 m2 - 44- 200927272

Table 3A Stage 1 2 3 TDS in the product stream feed 35700 ppm 30000 ppm 25000 ppm TDS in the feed stream 35700 ppm 52800 ppm 64467 ppm Total voltage difference per cell pair 0.0584 Volt 0.0632 Volt 0.0744 Volt Recovery 75.0 % 70.0 % 70.0 % Flow rate by membrane area (flux) 25.0 gfd 0.0174 gpm/ft2 0.0424 m/hr 25.0 gfd 0.0174 gpm/ft2 0.0424 m/hr 25.0 gfd 0.0174 gpm/ft2 0.0424 m/hr Product TDS 30000 ppm 25000 ppm 20000 ppm Discharge TDS 52800 ppm 64467 ppm 76133 ppm, total power 196.7 kW 186.8 kW 220.1 kW Total energy required per unit of production 0.161 kWh/m3 0.61 kWh/Kgal 0.153 kWh/m3 0.58 kWh/Kgal 0.180 kWh/m3 0.68 kWh /Kgal Membrane area by flow rate 0.04 ft2/gpd 23.56 m2/(m3/hr) 0.04 ft2/gpd 23.56 m2/(m3/hr) 0.04 ft2/gpd 23.56 m2/(m3/hr) Product flow rate 1225 m3/hr 1225 m3/hr 1225 m3/hr Flow rate 408 m3/hr 525 m3/hr 525 m3/hr Total projected cation membrane area 28862 m2 28862 m2 28862 m2 Total projected anion membrane area 28862 m2 28862 m2 28862 m2 Total projection membrane area 57724 M2 57724 m2 57724 m2 -45 - 200927272

Table 3B Stage 4 5 6 TDS in product stream feed 20000 ppm 15000 ppm 10000 ppm TDS in the feed stream 76133 ppm 87800 ppm 35700 ppm Total voltage difference per battery pair 0.0892 Volt 0.1110 Volt 0.1160 Volt Recovery rate 70.0% 70.0% 65.0% Flow rate by membrane area (flux) 25.0 gfd 0.0174 gpm/ft2 0.0424 m/hr 25.0 gfd 0.0174 gpm/ft2 0.0424 m/hr 25.0 gfd 0.0174 gpm/ft2 0.0424 m/hr Product TDS 15000 ppm 10000 ppm 5000 ppm Discharge TDS 87800 ppm 99467 ppm 44986 ppm Total power 263.8 kW 328.2 kW 342.9 kW Total energy required per unit of production 0.215 kWh/m3 0.82 kWh/Kgal 0.268 kWh/m3 1.01 kWh/Kgal 0.280 kWh/m3 1.06 kWh/ Kgal Membrane area by flow rate 0.04 ft2/gpd 23.56 m2/(m3/hr) 0.04 ft2/gpd 23.56 m2/(m3/hr) 0.04 ft2/gpd 23.56 m2/(m3/hr) Product flow rate 1225 m3/hr 1225 M3/hr 1225 m3/hr Flow rate 525 m3/hr 525 m3/hr 660 m3/hr Total projected cation membrane area 28862 m2 28862 m2 28862 m2 Total projected anion membrane area 28862 m2 28862 m2 28862 m2 Total projection membrane area 57724 m2 57724 m2 57724 m2 -46 - 200927272

Table 3C Stage 7 EDI product feed TDS in the 5000 ppm 2500 ppm TDS in the feed stream 35700 ppm 35700 ppm Total voltage difference per cell pair 0.1133 Volt 0.0788 Volt Recovery 65.0% 70.0% 25.0 gfd 60.0 gfd Membrane area flow rate (flux) 0.0174 gpm/ft2 0.0417 gpm/ft2 0.0424 m/hr 0.1019 m/hr Product TDS 2500 ppm 500 ppm Abandoned TDS 40343 ppm 40367 ppm Total power 167.5 kW 93.2 kW Required per unit of production Total energy 0.137 kWh/m3 0.52 kWh/Kgal 0.076 kWh/m3 0.29 kWh/Kgal Membrane area by flow rate 0.04 ft2/gpd 23.56 m2/(m3/hr) 0.02 ft2/gpd 9.82 m2/(m3/hr) Product flow rate 1225 m3/hr 1225 m3/hr Flow rate 660 m3/hr 525 m3/hr Total projected cation membrane area 28862 m2 24052 m2 Total projected anion membrane area 28862 m2 24052 m2 Total projection membrane area 57724 m2 48103 m2 -47 - 200927272 4 ED train 1 ED train 2 combined ED stage EDI stage combination ED and EDI product flow rate, cubic meters / hour 8,000 power demand * 仟 3,938 6,824 10,762 628 11,390 Energy demand per cubic meter of product, 仟 / cubic meter 0 .492 0.853 1.345 0.079 1.424 Example 4 This example describes a Dunant enhanced EDI device in accordance with one or more aspects of the present invention. Figure 8 shows a simplified diagram of the Dunant Enhanced EDI program with four batteries shown as "repeating units" in the module. When no electric field is applied, the anion in the brine stream B1 is transferred across the separated anion exchange membrane to the right concentrated stream C1B due to the difference in concentration between the brine and the concentrated stream. In order to maintain electrical neutrality, the equivalent amount of cationic species in charge generally moves across the cation selective membrane CM from the dilution stream D1 to the concentrate stream C1B. Similarly, the cationic species typically moves from the brine stream B1 across the other cation selective membrane CM to the concentrate stream C1A. In order to maintain electrical neutrality, the anionic species typically migrate across the anion selective membrane AM self-diluting stream D2 into the concentrate stream C1A. In fact, the transfer of ions from the brine stream to the adjacent concentrated stream due to the difference in concentration can be considered to promote the ionic species moving from the dilute stream to the concentrated stream to maintain electrical neutrality. The dilution stream is therefore deionized.

If a DC current DC electric field is applied, in the procedure called Dunant Enhanced EDI-48 - 200927272, the ionic transfer due to the electric field may increase due to the ionic movement phenomenon due to the concentration difference between the brine-concentrated streams. • Dunan potential energy based on ion concentration _ as a result of ion-exchange membranes that are permeable to these ions. EXAMPLE 5 This example illustrates an alternative configuration of the processing system and technology of the present invention. The ED device and the softening and EDI device are used to desalinate salt water and seawater. Figures 9A and 9B show further embodiments of a system in accordance with one or more aspects of the present invention. In contrast to the system depicted in FIG. 2, the system 905 further utilizes a third train electrodialysis unit ED TRAIN 3 configured to receive at least a portion of the treated water by removing at least a portion of the target species from the water prior to ion exchange. Further processing in the third treatment (which may be Dunant Enhanced Electrodeionization (DE-EDI)). Figure 9B shows another exemplary processing system 910 that also utilizes the third train electrodialysis unit TRAIN 3, which is also configured to treat the water in a small portion and further process the water flow, but instead utilizes the conventional EDI without flow, or Polarity and flow reversal (EDIR) EDI, DE-EDI device. The EDIR unit is configured downstream of the IX softener and can have a higher hardness feed stream (which reduces softener hardness removal) or a higher breakthrough before regeneration. Higher breakthrough conditions increase the regeneration of the IX softener unit and also reduce the size and capital and operating costs of the softener. Further variations or modifications to the systems of Figures 9A and 9B may involve configuring the IX softener prior to ED TRAIN 3. In contrast to the phase difference, the treatment, at the processing stage, the ED is brought to the brine instead of the hardening: between, for example, -49- 200927272 This system can benefit seawater and from estuaries, rivers and/or even The salt water of the groundwater is desalinated. Example 6 In this example, the desalination experiment was carried out using an electrodialysis module with a standard or monovalent selective membrane. The initial feed solution is about 35,000 ppm NaCl solution or synthetic seawater with a total dissolved solids (TDS) of about 35,000 ppm. Figures 11A and 11B show ED products per cubic meter when using a standard ion selective membrane (Figure 11A) and a monovalent selective membrane (Figure 11B) to reduce the target concentration in the product stream from about 35,000 ppm to about 500 ppm. The required calculation energy. The monovalent selective membrane used was a CMS cation selective membrane and an AMS anion selective membrane obtained from Tokuyama Soda Qo., Tokyo, Japan. Figures 12A and 12B show the ratio of residual cationic species (Fig. 12A) and anionic species (Fig. 12B) to the electrodialysis stage using a monovalent selective membrane. Both types of ED modules have high energy consumption when the feed is synthetic seawater. For ED modules with standard membranes, the energy consumption of seawater is between 7% and 32% compared to synthetic Naci solution, and that of ED modules with monovalent membranes is 21%. The ED module with a monovalent selective membrane has an extremely high energy consumption, almost twice that of an ED module with a standard membrane. The energy consumption increases dramatically as the target product TDS drops below about 5,000 ppm. In addition to NaCM' seawater containing divalent ions, such as Ca + 2, Mg + 2 and S04 · 2, as listed in Example 1 above, it can affect the energy consumption of divalent ions, such as sea-50-200927272 water and synthetic NaCl solution The description of the information. Since the monovalent selective membrane preferably passes the monovalent ion to the divalent ion, it is believed that the concentration ratio of the divalent to monovalent ion in the diluting chamber increases as the seawater desalination in the ED module _ series increases. Figures 12A and 12B show the ratio of residual ions in experiments with ED modules with monovalent selective membranes. This data shows that the membrane blocks the pathway of divalent ions relative to monovalent ions. The selectivity of the anion membrane is almost 100%, which is consistent with the published data for the Tokuyama Soda monovalent selective anion membrane. The preferred selective anion membrane causes the S04 ion © to not transfer, so the residual amount of the S04 ion is still 100%. It is believed that the increase in S04 concentration is due to electro-osmotic phenomena whereby water is also transported through the membrane. Based on Figures 12A and 12B, it is believed that the higher energy consumption of the ED module with a monovalent selective membrane is due to the increase in the concentration ratio of divalent to monovalent ions. It is also expected that the removal of divalent ions in the feed water in the ED and EDI modules will reduce energy consumption. For example, the removal of divalent ions by nanofiltration (NF), such as a portion of the treatment prior to the ED step, reduces the energy consumption of the ED and EDI steps. The NF product therefore contains primarily NaCl and KC1 at a lower concentration than the starting seawater, and requires less energy to dilute to 500 ppm. Thus, in some aspects of the invention, it may utilize NF operations such as pressure drivers to facilitate recovery, and the energy consumed and remaining in the NF abandon stream further reduces system energy consumption. It is believed that the energy recovery device originally developed for reverse osmosis (R0) can also be applied to NF unit operations. Alternatively, the salt regeneration anion exchange step between the ED device or between the ED and the EDI device also reduces the total energy consumption. Some aspects of the present invention provide a desalination system -51 - 200927272 and technology via an electric drive program. Ion transfer, which is advantageous due to potential energy, is described as a fairly efficient procedure because the resistance to ion mobility is used to separate the membrane limits of purified water and waste/concentrated water. Additional features and aspects of the invention may be prior to the processing operations described herein. The present invention has been described with reference to the preferred embodiments of the present invention. In fact, some illustrative configurations of the devices, systems, and techniques of the present invention, as well as specific components implemented in the configuration, are considered a part of this disclosure. For example, each unit operation is described herein as being connectable or connectable (e.g., fluidly connected) to each of the inlet and outlet portions that provide this connectivity. Non-limiting examples of connection structures include lines, and spiral or welded flanges that are bolted to the nut and are generally sealed with a gasket. Numerous modifications and other specific embodiments are within the ordinary scope of the art and are intended to be within the scope of the invention. In particular, although many of the examples presented herein are directed to a particular combination of method acts or system components, it should be understood that these acts and these components can be combined in other ways to accomplish the same purpose. It will be appreciated by those skilled in the art that the parameters and configurations described herein are exemplary and that actual parameters and/or configurations are dependent upon the particular application in which the systems and techniques of the present invention are used. Those skilled in the art will also appreciate or be able to determine that a fixed experiment equivalent to the specified embodiment of the invention is used. It is to be understood that the specific embodiments described herein are by way of example only, and the scope of the claims In addition, it should be understood that the present invention relates to the features described herein, the system, the system, or the technology, and the two or more features, systems, subsystems, or technologies described herein. Any combination, and any combination of two or more features, systems, subsystems, and/or methods (if such features, systems, subsystems, and technology are inconsistent with each other) are deemed to be covered by the scope of the patent application. Within the scope of the invention. Further, the actions, elements, and features discussed with respect to one particular embodiment are not intended to exclude similar roles in other embodiments. The term "plurality" as used herein refers to two or more items or components. © the terms "including", "including", "having", "having", "including" and "involving", whether stated in the scope of description or patent application, are open nouns, meaning " including but not limited to". The use of this term is therefore used to include the listed items and their equivalents and additional items. The transitional terms "composition" and "actual composition" are all closed or semi-closed transitional terms. The use of generic terms such as "first", "second" and "third" in the scope of the patent application to modify the scope of the patent application element itself is not related to any priority, succession, or application of the component of the patent application. Or the order, or the chronological order in which the method is practiced, but merely distinguishes between the elements of the patent application that have the specific name and the elements that have the same name but are used in order to distinguish the components of the claim. BRIEF DESCRIPTION OF THE DRAWINGS The drawings are not intended to be drawn to scale. In the drawings, identical or nearly identical components that are described in the various figures are represented by the same reference numerals. For the sake of clarity, not all components are necessarily indicated in the drawings. In the drawings: -53 - 200927272 Figure 1 is a schematic flow diagram of a system in accordance with one or more embodiments of the present invention; Figure 2 is a diagram of one or more other embodiments in accordance with the present invention. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 3 is a schematic flow diagram of a seawater desalination system in accordance with one or more embodiments of the present invention; FIG. 4 is a diagram of one or more aspects that may be used in accordance with the present invention. A schematic view of a portion of an electrodeionization apparatus of a plurality of systems; © FIG. 5 is a schematic view of a portion of an electrodeionization apparatus in accordance with one or more aspects of the present invention; FIGS. 6A and 6B are diagrams according to the present invention. BRIEF DESCRIPTION OF THE INVENTION - or a plurality of aspects of a portion of an electrodeless continuous deionization apparatus; Figure 7 is a diagram depicting predicted energy requirements in accordance with one or more aspects of the present invention; A schematic view of a Dunan Enhanced Electrodeionization (EDI) module of one or more aspects of the invention; ® Figures 9A and 9B are schematic views of a system in accordance with one or more aspects of the present invention; 10A and 10B are diagrams of electrodialysis that can be used in accordance with one or more aspects of the present invention. A schematic view of the vehicle; FIGS. 11A and 11B are diagrams showing the treatment of the synthesis by an electrodialysis apparatus having a standard ion selective membrane (Fig. 11A) and a single selective membrane (Fig. 11B) in accordance with one or more aspects of the present invention. a graph of brine ("NaCl solution") and seawater required energy versus target product total dissolved solids concentration; and "54- 200927272 Figures 12A and 12B are diagrams showing one or more aspects of seawater treatment during seawater treatment The ratio of the ratio of the cation (Fig. 12A) to the anion (Fig. 12B) is relative to the graph of the electrodialysis stage using a single selective membrane. [Main component symbol description]

100 processing system 102 at least partially processes stream 110 to process liquid source 111 stream 112 second feed stream 113 feed stream 114 feed stream 120 first - processing stage 12 1 at least partially treats water or water stream 122 stream 123 second production Stream 13 0 Second Stage 13 1 Second At least Partially Processed Product Stream or Modified Liquid 140 Third Treatment Stage 14 1 Product Stream 142 Product Stream 190 Use Point 200 Water Treatment System 220 Unit Operation 22 1 Partially Process Product Flow -55- 200927272

222 Second unit operation 223 Second product stream 230 Second stage 23 1 Second product stream 240 Third treatment stage 24 1 By-product water or aqueous stream 260 Saline storage tank 26 1 Saline solution 300 Seawater desalination system 3 10 Seawater source 32 1 at least partially treated water 3 2 1 A first electrodialysis unit 3 2 1 C 1 concentrating chamber 32 1 D 1 consuming chamber 3 22B second electrodialysis unit 3 22C2 concentrating chamber 3 22D2 consuming chamber 3 23 A third dialysis unit 3 23 C 1 Concentration chamber 3 23 D 1 Consuming chamber 3 24B Fourth electrodialysis unit 3 24C2 Concentration chamber 3 24D2 Consumption chamber 3 3 0 Ion exchange subsystem -56 - 200927272

3 3 1 at least partially treated water 332 vent stream 340 third ΐ treatment stage 3 8 1 monovalent anion selective membrane 3 82 ion selective membrane 3 90 product 400 electrodeionization device 4 11 consuming chamber 4 12 concentrating chamber 5 00 electricity Deionization device 5 11 - consumption chamber 5 12 second: consumption chamber 5 13 third three consumption chamber 52 1 first - concentration chamber 52 1 C first - cation selective membrane 522C second cation selective membrane 5 23 C third tri-cation selective membrane 53 1 first - concentrated battery pair 53 1 A first - anion selective membrane 532 second two concentrated battery pair 5 3 2A second one negative - * rtw ion m selective film 5 3 3 A Ξ 阴离子 anion selective membrane 54 1 - - concentrating chamber 542 second concentrating chamber 5 62 anode chamber - 57 - 200927272 564 cathode chamber 600 electrodeless continuous deionization device. 60 1 cylindrical shell 6 10 Electrodeless continuous deionization device 6 11 First consumption chamber 6 12 Second consumption chamber 62 1 a concentrating chamber 622 a second concentrating chamber Ο 64 1 A anion selective membrane 642 Α a second anion selective membrane 65 1 C cation selective membrane 65 2C second cation selective membrane 66 1 member AEM anion selective membrane AX anion exchange resin CEM cation selective membrane CX cation exchange resin R abandon flow-58-

Claims (1)

200927272 X. Patent application scope: 1. An electrodeionization device comprising: a fluidly connected first--chamber having a source of dissolved solid water, the depleting chamber being at least partially composed of a cation selective membrane and a first a selective membrane defining; fluidly establishing a first aqueous source downstream of the first aqueous source having a first dissolved solids concentration, and ionically connecting the first chamber via the cation selective membrane; and fluidly connecting to the second dissolved solids concentration a second aqueous liquid source downstream of the second aqueous liquid source (which is greater than the first solid concentration), and ionicly connected to the second depleting chamber of the first depleting chamber via the ion selective membrane 2. As in the electrodeionization apparatus of claim 1 Wherein the first liquid is a tank having a first dissolved solids concentration of less than about 4% by weight. 3. The electrodeionization apparatus of claim 2, wherein the second liquid is a second dissolved solid having less than about 10% by weight. Concentration of private water. 4. The electrodeionization apparatus of claim 3, wherein the first chamber is fluidly connected to a helium having a dissolved solids concentration of less than about 2,500 ppm. 5. The electrodeionization apparatus of claim 1, wherein the ratio of the second solids concentration to the first dissolved solids concentration is at least about 3. 6. The apparatus for treating water having dissolved ionic species therein comprises: fluidly connecting a source of water, and at least partially consuming the first yin consuming liquid away from the liquid - dissolved yin 水性 aqueous E water. The aqueous salt is depleted by water, the ion-59-200927272 selective membrane and the first consuming chamber defined by the first cation selective membrane: fluidly connected to the first concentrating compartment of the first aqueous solution source having the first dissolved solids concentration a first concentrating chamber is ionicly coupled to the first consuming chamber via one of the first anion selective membrane and one of the first cation selective membranes; and fluidly coupled to have a second dissolved solids concentration (which is greater than the first dissolved solids concentration) A second consuming chamber of the second aqueous solution source, the second consuming chamber is ionicly coupled to the first concentrating chamber via the second cation selective membrane and the second anion selective membrane. The device of claim 6, further comprising fluidly connecting a second aqueous solution source having a third dissolved solids concentration (which is less than the second dissolved solids concentration) to at least one of the first aqueous sources The concentrating chamber is ionicly connected to the second consuming chamber via one of the second anion selective membrane and the second cation selective membrane. 8. The device of claim 7, wherein the second concentrating compartment is ionicly coupled to the first consuming chamber via the first cation selective membrane. 9. The device of claim 7, further comprising a salt bridge ionicly connecting the first consuming chamber to the second concentrating chamber. 10. The device of claim 7, further comprising a third consumption fluidly connecting the second aqueous source source to at least one of the fourth aqueous solution source having a fourth dissolved solids concentration greater than the third dissolved solids concentration a third consuming chamber is ionicly coupled to the second concentrating compartment via a third cation selective membrane. 1 1. The device of claim 1 , further comprising fluidly connecting the first aqueous source, the third aqueous source, and having a fifth dissolved -60-200927272 solid concentration (which is less than any second dissolved solids concentration) And a third concentration chamber of at least one of the fifth aqueous solution source having a fourth dissolved solids concentration, wherein the third concentration chamber is ionically connected to the third consumption chamber via the third anion selective membrane. 12. The device of claim 11, wherein the third concentrating compartment is ionicly coupled to the first consuming chamber via the first cation selective membrane. 13. The device of claim 12, wherein the third concentrating compartment is ionicly coupled to the first consuming compartment via a salt bridge. © 14. The device of claim 6 is electrodeless. 15. The device of claim 6 wherein the first depleting compartment is fluidly connected to the first concentrating compartment downstream of the same source. 16. A seawater desalination system, comprising: at least one first electrodialysis device comprising at least one first depletion chamber having a first depletion chamber inlet fluidly connected to a source of seawater, and a first depletion chamber outlet, And at least one first concentrating compartment having a first concentrating compartment inlet and a first concentrating compartment outlet; at least one second electrodialysis unit comprising at least one second consuming compartment having a second consumption of fluidly connected seawater source a chamber inlet, and a second depleting chamber outlet; and S one less concentrating chamber having a second concentrating chamber inlet fluidly connected to the seawater source, and a brine outlet; at least one ion exchange unit having a fluid connection first An ion exchanger at least one of the outlet of the consuming chamber and the outlet of the second consuming chamber enters a port of -61-200927272, and an outlet of the ion exchanger; and at least one electrodeionization device having a first fluidly connected outlet of the ion exchanger a consuming chamber, the consuming chamber being at least partially defined by the first cation selective membrane and the first anion selective membrane, the fluid a first concentrating chamber connected to the seawater source and ionically connected to the first consuming chamber via the first cation selective membrane, and fluidly connected downstream of the brine outlet and ionicly connected to the second concentrating chamber via the second anion selective membrane Consumption room. 17. The seawater desalination system of claim 16, wherein at least one of the first concentrating compartment and the second consuming compartment is free of ion exchange resin. 1 8. The seawater desalination system of claim 16 wherein at least one electrodeionization device further comprises a second concentration chamber defined at least in part by the first anion selective membrane and having a fluidly connected source of seawater An inlet, and a third depleting chamber fluidly connected to the second concentrating chamber via the second cation selective membrane, and having at least a fluidly connected brine outlet, an outlet of the first concentrating compartment, and an outlet of the second concentrating compartment The entrance to one. 1 9. The seawater desalination system of claim 18, wherein at least one of the first concentration chamber, the second consumption chamber, the second concentration chamber, and the third consumption chamber is free of ion exchange resin. The seawater desalination system of claim 16, wherein the seawater desalination system further comprises a brine storage tank fluidly connecting at least one of an outlet of the first concentrating compartment and an outlet of the second consuming compartment. 21. The seawater desalination system of claim 20, wherein the brine storage tank comprises an outlet fluidly connectable to the at least one ion exchange unit. The seawater desalination system of claim 21, further comprising a third electrodialysis unit having a third depleting chamber fluidly connected downstream of the first depleting compartment and upstream of the ion exchange unit. 23. The seawater desalination system of claim 22, further comprising a fourth electrodialysis unit having a fourth depleting chamber fluidly connected downstream of the second depleting compartment and upstream of the ion exchange unit. A seawater desalination system according to claim 16 wherein at least one of the first electrodialysis devices comprises a monovalent selective membrane disposed between the at least one first depleting compartment and the at least one first depleting compartment. 25. The seawater desalination system of claim 24, wherein the first depletion chamber of the electrodeionization apparatus comprises a mixed bed of ion exchange medium. 26. The seawater desalination system of claim 16, further comprising at least one pre-treatment unit operating fluidly connected to the downstream of the seawater source, and at least one first electrodialysis device, at least one second electrodialysis device, Upstream with at least one of the at least one electrodeionization device. 27. The seawater desalination system of claim 26, wherein at least one of the pretreatment unit operations comprises at least one secondary system selected from the group consisting of a filtration system, a chlorination system, a dechlorination system, and a pressure driven system. 28. The seawater desalination system of claim 27, wherein the pretreatment unit operation comprises at least one of a microfilter, a sand filter, and a nanofiltration system. 2 9. The seawater desalination system of claim 16 wherein at least one electrodeionization device comprises an anode collector, a cathode collector, and a salt bridge connecting the anode and the cathode collector. 30. The seawater desalination system of claim 16, wherein at least one of the electrodeionization device, the at least one first electrodialysis device, and at least one of the at least one second electrodialysis device are fluidly connected to have a dissolved chlorine species The aqueous solution is sourced downstream of the anode chamber, which contains one of a chlorine outlet and a hypochlorite outlet. The seawater desalination system of claim 16, wherein at least one of the electrodeionization device, the at least one first electrodialysis device, and the at least one second electrodialysis device comprise at least one of the alkali flow outlets Second electrode chamber. 3 2. The seawater desalination system of claim 6, wherein the at least one ion exchange unit comprises an anion exchange resin in the form of chlorine. 3 3 · a desalination system comprising: a seawater source; a device for selectively reducing a concentration of a monoselective species in the first seawater stream to produce a first dilution stream; ◎ for increasing a second seawater stream a device for dissolving a solids concentration to produce a brine stream; a device for exchanging at least a portion of a divalent species in the first dilution stream into a monovalent species, the exchange device having a second dilution stream outlet; and an electrochemical separation device having a fluid field A consuming chamber connected to the second dilution stream outlet, and a means for ionicly connecting the consuming chamber for providing concentration evoked potential energy. -64- 200927272 34. The desalination system of claim 33, wherein the means for increasing the concentration of dissolved solids in the first seawater stream comprises an electrodialysis unit having a consumption chamber fluidly connected to the seawater source, and the unit price A concentrating compartment in which the selective membrane is separated from the consuming compartment. 35. The desalination system of claim 33, wherein the means for increasing the concentration of dissolved solids in the second seawater stream comprises an electrodialysis unit having a concentration chamber fluidly connected to the source of seawater, and a brine outlet providing a brine stream . 3 6 · The desalination system of claim 35, wherein the means for providing concentration © evoked potential energy comprises fluidly connecting the first half-cell feed stream source (which has a first total dissolved solids concentration) One half of the battery compartment, and a second half of the battery compartment fluidly connected to the second half of the battery feed stream source having a second total dissolved solids concentration greater than the first total dissolved solids concentration. 37. The desalination system of claim 36, wherein the first half of the battery compartment is fluidly connected to the seawater source and the second half of the battery compartment is fluidly connected to the salt water source. 38. An electrodeionization device comprising: a fluidly connected depletion chamber having a source of dissolved solids therein, the depletion chamber being at least partially defined by a cation selective membrane and a first anion selective membrane, and ionic linkage consumption a concentration half-cell pair, the concentration half-cell pair is fluidly connected to a first aqueous liquid having a first dissolved solids concentration - 65- 200927272 source, and is ionicly coupled to one of the first anion selective membranes via a cation selective membrane a first half of the battery chamber of the consuming chamber, and a fluidly connected second source of the second aqueous liquid having a second dissolved solids concentration (which is greater than the first dissolved solids concentration) and ionicly coupled via the second anion selective membrane The second half of the cell compartment of the half cell compartment. 39. The electrodeionization device of claim 38, wherein the first aqueous liquid is seawater. 40. The electrodeionization apparatus of claim 39, wherein the second aqueous liquid is salt water having a second dissolved solids concentration of at least about 10% by weight. 41. The electrodeionization apparatus of claim 38, wherein the ratio of the second dissolved solids concentration to the first dissolved solids concentration is at least about 3. 42. A method of seawater desalination comprising: reducing a monovalent species concentration of seawater in a first demineralization stage to produce a partial demineralized water; " producing a brine solution from seawater having at least two concentrations of total dissolved solids in the seawater Times total dissolved solids concentration: introducing a portion of the demineralized water into the depleting compartment of the electrically driven separation device; and promoting at least a portion of the dissolved species from the demineralized compartment to be transported to the chamber of the concentration cell pair, and in the electrically driven separation device The concentration evoked potential energy is generated in the concentration battery pair. 43. The method of claim 42, further comprising dissolving at least a portion of the portion of the desalinated water to dissolve the non-monovalent compound -66-200927272 species by dissolving the monovalent species. 44. The method of claim 42, wherein reducing the concentration of the monovalent species of seawater comprises selectively reducing the concentration of the dissolved monovalent species in the electrodialysis unit. 45. The method of claim 42, wherein the making of the brine solution comprises promoting the transport of at least a portion of the dissolved species from the seawater to the second seawater stream flowing into the concentrating compartment of the electrodialysis unit. 46. The method of claim 42, further comprising: electrolytically producing one of a salt and a hypochlorite species in an anode chamber of at least one of the electrolysis device, the electrodialysis device, and the electrically driven separation device, and An alkali stream is produced electrolytically in one or more chambers of at least one of the electrolysis device, the electrodialysis device, and the electrically driven separation device. 47. The method of claim 46, further comprising at least partially disinfecting at least a portion of the seawater with the chlorine or hypochlorite species produced. 4. The method of claim 42, further comprising passing at least a portion of the seawater through the nanofiltration system prior to reducing the monovalent species concentration of seawater in the first demineralization stage. -67-