|Publication number||US20030155243 A1|
|Application number||US 10/080,302|
|Publication date||Aug 21, 2003|
|Filing date||Feb 21, 2002|
|Priority date||Feb 21, 2002|
|Also published as||CA2476638A1, DE60327171D1, EP1476247A1, EP1476247A4, EP1476247B1, US7138045, US20050150768, WO2003072229A1|
|Publication number||080302, 10080302, US 2003/0155243 A1, US 2003/155243 A1, US 20030155243 A1, US 20030155243A1, US 2003155243 A1, US 2003155243A1, US-A1-20030155243, US-A1-2003155243, US2003/0155243A1, US2003/155243A1, US20030155243 A1, US20030155243A1, US2003155243 A1, US2003155243A1|
|Original Assignee||Eet Corporation|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (5), Referenced by (22), Classifications (17), Legal Events (1)|
|External Links: USPTO, USPTO Assignment, Espacenet|
 Not Applicable
 Not Applicable
 1. Field of Invention
 This invention pertains to a method and apparatus for the purification and reuse or disposal of polluted liquids.
 More particularly, this invention pertains to an electrodialysis stack for the removal and concentration of ions from aqueous solutions and certain aqueous/organic solutions.
 2. Description of the Related Art
 There are presently a number of systems for treating and recycling aqueous and aqueous/organic waste streams on the market. Present state of the art systems, including de-ionization methods that are available to industrial waste stream generators, are deficient in their ability to consistently and economically produce a cleansed fluid of sufficient quality that can be continuously recycled and reused, especially in the case of small to medium volume liquid waste generation. The initial high cost of purchasing many of these systems is beyond the economic resources of many businesses, thus prohibiting cost-effective recycling for environmental compliance or beneficial reuse.
 Multi-cell electrodialysis stacks are normally built up of membrane sheets separated from each other by suitable gaskets. For efficient separations, the distance (gap) between the sheets is as small as possible. In most designs, a spacer is introduced between the individual membrane sheets, both to assist in supporting the membrane and to help control the liquid flow distribution. The stacks for most electrodialysis processes are assembled in the same fashion as a plate-and-frame filter press, the gaskets corresponding to the frames and the membrane sheets corresponding to the plates. The manifolds that are needed to distribute the process fluids to the various compartments or channels are formed by ingenious patterns of mating holes and slots punched in the gaskets and sometimes in the membranes themselves, prior to assembly of the stack. Several different gasket and spacer materials and arrangements and channel geometries have been utilized or proposed.
 In typical electrodialysis systems, the flow pattern within each compartment (i.e., between any two successive membranes) is determined by the configuration of the spacer element used between the membranes. Two distinctively different flow arrangements are typically used. One is known as the tortuous-path design; the other makes use of the sheet-flow principle. The most serious design problem for both flow arrangements for multi-membrane and multi-cell stacks is that of assuring uniform fluid flow to the various compartments and effective transport of the ions to the membrane surfaces. These difficulties are the major obstacles to simple, single stage demineralization of brackish liquids.
 In particular, reducing concentration polarization is one of the most important design issues for electrodialysis. Concentration polarization is the reduction of ion concentrations near the membrane surface compared to those in the bulk solution flowing through the membrane compartment. With substantial concentration polarization, electrolytic water splitting in order to provide the requisite electric current carriers through the membranes occurs due to the deficiency of solute ions adjacent to the membranes that can carry the current. This water splitting is extremely detrimental to electrodialysis efficiency. The tendency of concentration polarization to take place at the surface of the membranes is due to the hydrodynamic characteristic of channel flow, in which there is a central turbulent core of flow bounded by thin viscous boundary layers adjacent to the confining surfaces. These viscous boundary layers impose a resistance to the passage of ions much greater than that of a layer of like thickness in the turbulent core, and hence increase the likelihood of polarization at the membrane surfaces. Polarization is objectionable not only from the standpoint of the inefficient increase in energy consumption, but also the change of pH of the concentrate stream as a result of water splitting, which tends to cause scale deposition.
 When dealing with fluids with very low total dissolved solids (TDS), back diffusion can take place. Back diffusion occurs when the ion concentration in the concentrate stream is substantially higher than the ion concentration in the de-mineralized stream. The result is that some of the ions from the concentrate stream diffuse back through the membrane, against the force of the DC potential, into the de-mineralized stream.
 The number of cells in a stack is limited mainly by the practical considerations of assembly and maintenance requirements. Since the failure of a single membrane can seriously impair stack performance, the necessity to be able to disassemble and reassemble a stack to replace a membrane, and the necessity to be able to perform this quickly and easily, effectively limits the number of membranes that can be practically utilized in a stack. As a result, it is often desirable to use several smaller modular-size stacks rather than one large one. This problem has been attacked by using several small subassemblies or packs containing about 50 to 100 cell pairs (CP), and arranging as many as 10 of these packs in series in a single clamping press. A single set of electrodes may be used for the entire assembly (stack) or several electrodes may be used to provide electric staging. However, use of single electrodes for larger assemblies typically causes end-cell heating that results in rapid membrane deterioration.
 The present invention serves to expand the possible applications of electrodialysis in that it represents an efficient, small scale electrodialysis system with a configuration allowing cost-effective small-scale applications, while making the large scale applications even more cost-competitive than they currently are.
 In accordance with the present invention, a unique gasket design reduces hydraulic pressure drop across the cell stack assembly by eliminating narrow inlet/outlet manifold cutouts inherent with conventional designs. The reduction of hydraulic pressure permits the use of higher flow rates that further reduce concentration polarization, as well as thinner membranes, resulting in improved desalting efficiency, especially for sparingly conductive solutions, and also less sensitivity to the presence of suspended matter.
 The novel multiple split cell design can be operated in parallel as a roughing de-mineralizer (or operated in a batch recirculation mode) or operated in series allowing for single-pass continuous flow. When operated in the series mode, the split cell design permits separate voltage and flow control when a higher purity fluid is desired. The split cell design permits separate cell control of concentrate stream salinity content. The roughing cell may be operated with a higher concentrate stream TDS, with the salinity of the polish cell concentrate stream correspondingly reduced to the salinity content of the de-mineralized stream. This prevents back diffusion and allows for efficient removal of ions in feed water of low TDS. In short, the split cell design incorporates the benefits of hydraulic and electrical staging without the inherent complexity and expense of commercial electrodialysis systems.
 The split cell design minimizes the voltage potential across the stack, thereby reducing end-cell heating that leads to membrane deterioration.
 It is an object of the present invention to provide a simpler stack assembly of low production cost. Stack assembly cost is reduced as a result of the novel split cell/gasket geometry. A reduced number of expensive machined components are required. Simpler and lighter components lower material costs for a given membrane area. Inexpensive center bolts provide an alternative to typical hydraulic force application arrangements, which also improves the uniformity of the clamping force distribution on the gasket area. Threaded bolts also reduce assembly labor time, i.e., it is easier to hold the configuration in place and also facilitate change-out of membranes when they are spent, as the cell geometry reduces stress on the end points as is found inherent with some conventional stack assemblies.
 It is another object of the present invention to provide an apparatus and method that allows for the cost-effective arrangement of two or more split membrane cells that enables the ingenious arrangements of plumbing for optimizing deionization processing.
 The cell gasket geometry can be more easily and inexpensively fabricated from a larger range of materials in comparison to conventional designs, allowing the process to be used in more harsh environments through the use of a wide range of chemically resistant materials. It is still another object of the present invention to provide an apparatus and method that combines a unique arrangement of small to intermediate scale unit operations for the economical recovery/reclamation of a wide range of fluids and that can also be scaled to a large system size, further improving the economics of large scale electrodialysis systems by reducing both capital and operating costs.
 According to one embodiment of the present invention, a dialysis stack is provided in which each generally planar gasket defines a first cell and a second cell. A membrane is located adjacent to each side of each gasket. A turbulence spacer is located within each cell. Each cell is provided with an inlet and an outlet to provide fluid access into and out of each cell. Fluid flows sequentially through the two cells defined in each gasket. Preferably, the fluid flows through a plurality of first cells defined by a plurality of spacers and then flows through a plurality of second cells defined in the plurality of spacers. Separate anodes and cathodes provide electrical energy to the two parallel sets of first cells and second cells. Separate rectifiers can be used to apply specific electric potential across the first set of cells and second cells when operated in series, or a single rectifier can power both the first and second cell sets when operated in parallel. A system of bolts extending through parallel compression plates are used to secure the plurality of spacers and interleaved membranes in register to define conduits extending between the plurality of cells.
 The electrodialysis stack is included in an electrodialysis system. The system includes a mixing tank for the solution being processed. Mixed solution is passed through filters for removing particulate matter and potential precipitants. The filtered solution is collected in a dilute tank. Concentrated fluid is collected in a concentrate tank. Electrolyte is provided from an electrolyte tank to an anode chamber and to a cathode chamber. The anode chamber and the cathode chamber have an electrically conductive fluid connection through the cell stack. The membranes alternate between anion exchange membranes and cation exchange membranes. The cells alternate between concentrate stream cells and dilution stream cells.
 The above-mentioned features of the invention will become more clearly understood from the following detailed description of the invention read together with the drawings in which:
FIG. 1 is a laterally exploded view of a cell stack embodying various of the features of the present invention;
FIG. 2 is a plan view of a cell stack embodying various features of the present invention;
FIG. 3 is a side elevation view of a cell stack embodying various features of the present invention;
FIG. 4 is an end elevation view of a cell stack embodying various features of the present invention;
FIG. 5 is an elevation view of an electrodialysis system embodying various features of the present invention;
FIG. 6 is a flow diagram of an electrodialysis system embodying various features of the present invention;
FIG. 7a is a schematic diagram of split cell spacer having two cells arranged in series;
FIG. 7b is a schematic diagram of split cell spacer having two cells arranged in parallel;
FIG. 7c is a schematic diagram of split cell spacer having three cells arranged in series;
FIG. 7d is a schematic diagram of split cell spacer having three cells arranged in parallel;
FIG. 7e is a schematic diagram of split cell spacer having four cells with two parallel cells arranged in series with two parallel cells;
FIG. 7f is a schematic diagram of split cell spacer having four cells arranged in series; and
FIG. 7g is a schematic diagram of split cell spacer having four cells with three cells arranged in parallel arranged in series with a single polish cell.
 Referring to the drawings, wherein similar reference numbers denote similar elements throughout the several drawings, there are disclosed a method and an apparatus for electrodialysis treatment of a fluid in which a salt is dissolved. One example of such a fluid is used antifreeze, which can be cleaned and recycled in accordance with the present invention.
 In FIG. 1 there is illustrated one embodiment of an electrodialysis cell stack 10, exploded laterally. At one end is an electrode stream spacer 12 defining two rectangular apertures 14 and 14′. In the depicted embodiment the electrode stream spacer is approximately 14 inches by 24 inches, though it will be recognized that various sizes may be used. Also defined in the electrode stream spacer 12 are eight conduit apertures 16 a, 16 b, 16 c, 16 d, 16 e, 16 f, 16 g and 16 h.
 Adjacent to the electrode stream spacer 12 is an anion exchange membrane 18, many of which are well known in the art. One commercially available material is Neosepta AFN produced by Tokuyama Corporation. The anion exchange membrane 18 is shaped and sized substantially identically to the electrode stream spacer 12 and includes conduit apertures 19 a-h in register with the conduit apertures 16 a-h defined in the electrode stream spacer 12.
 Adjacent to the anion exchange membrane 18 is a concentrate split cell spacer 20 defining two apertures 22 and 22′. Each of the apertures 22 and 22′ has the shape of an abbreviated rectangle in which two squares have been removed from diagonally opposed corners and all corners have been rounded. Conduit apertures 24 a, 24 c, 24 e and 24 h are defined in the concentrate split cell spacer. The concentrate split cell spacer 20 is shaped and sized substantially identical to the electrode stream spacer 12. The aperture 22 is in register with the rectangular aperture 14 and the aperture 22′ is in register with the rectangular aperture 14′.
 A concentrate turbulence spacer 28 is located within the aperture 22 and a concentrate turbulence spacer 28′ is located within the aperture 22′. Each of the concentrate turbulence spacers 28 and 28′ are formed from a mesh to maintain turbulence within the apertures 22 and 22′ as concentrate fluid passes through the apertures 22 and 22′.
 Adjacent to the concentrate turbulence spacer 28 is a cation exchange membrane 29, many of which are well known in the art. One commercially available material is Neosepta CMX produced by Tokuyama Corporation. The cation exchange membrane 29 is shaped and sized substantially identical to the electrode stream spacer 12 and includes conduit apertures 30 a-h in register with the conduit apertures 16 a-h defined in the electrode stream spacer 12.
 Adjacent to the cation exchange membrane 29 is a dilution stream split cell spacer 32 defining two apertures 34 and 34′. Each of the apertures 34 and 34′ has the shape of an abbreviated rectangle in which two squares have been removed from diagonally opposed corners and all corners have been rounded. The apertures 22 and 22′ are mirror images of the apertures 34 and 34′. Conduit apertures 36 b, 36 d, 36 e and 36 g are defined in the dilution stream split cell spacer 32. The dilution stream split cell spacer 32 is shaped and sized substantially identically to the electrode stream spacer 12. The aperture 34 is in register with the rectangular aperture 14 and the aperture 34′ is in register with the rectangular aperture 14′ to provide electrically conductive fluid connection to the apertures 14 and 14′, respectively.
 A dilution stream turbulence spacer 38 is located within the aperture 34 and a concentrate turbulence spacer 38′ is located within the aperture 34′. Each of the concentrate turbulence spacers 38 and 38′ is formed from a mesh to maintain constant turbulence within the apertures 34 and 34′ as dilution fluid passes through the apertures 34 and 34′.
 Adjacent to the dilution stream turbulence spacer 38 is an anion exchange membrane 40, which is identical to anion exchange membrane 18. The anion exchange membrane 40 defines conduit apertures 42 a-h in register with the conduit apertures 16 a-h defined in the electrode stream spacer 12.
 Adjacent to the anion exchange membrane 40 is a concentrate split cell spacer 44 defining two apertures 46 and 46′. The concentrate split cell spacer is identical to the concentrate split cell spacer 20 and defines conduit apertures 48 a, 48 c, 48 f and 48 h. The aperture 46 is in register with the rectangular aperture 14 and the aperture 46′ is in register with the rectangular aperture 14′ to provide electrically conductive fluid connection to the apertures 14 and 14′, respectively
 A concentrate turbulence spacer 50 is located within the aperture 46 and a concentrate turbulence spacer 50′ is located within the aperture 46′. Each of the concentrate turbulence spacers 50 and 50′ is formed from a mesh to maintain constant turbulence within the apertures 46 and 46′ as concentrate fluid passes through the apertures 46 and 46′.
 Adjacent to the concentrate turbulence spacer 50 is a cation exchange membrane 52, many of which are well known in the art. The cation exchange membrane 52 is shaped and sized substantially identically to the electrode stream spacer 12 and includes conduit apertures 54 a-h in register with the conduit apertures 16 a-h defined in the electrode stream spacer 12.
 Adjacent to the cation exchange membrane 52 is an electrode stream spacer 56 defining two rectangular apertures 58 and 58′. The electrode stream spacer 56 is substantially identical to the electrode stream spacer 12. Also defined in the electrode stream spacer 56 are eight conduit apertures 60 a-h, which are in register with the conduit apertures 16 a-h respectively.
 A first end section 62 b of the aperture 22 overlays the conduit apertures 19 b and 30 b to cooperatively define a concentrate outlet port for the aperture 22. A diagonally opposed second end section 62 e overlays conduit apertures 19 e and 30 e to cooperatively define a concentrate inlet for the aperture 22. A first end section 62 d of the aperture 22′ overlays the conduit apertures 19 d and 30 d to cooperatively define an outlet port for the aperture 22′. A diagonally opposed second end section 62 g of the aperture 22′ overlays the conduit apertures 19 g and 30 g to cooperatively define an inlet port for the aperture 22′.
 A first end section 64 a of the aperture 34 overlays the conduit apertures 30 a and 42 a to cooperatively define a dilution outlet port for the aperture 34. A diagonally opposed second end section 64 f overlays conduit apertures 30 f and 42 f to cooperatively define a dilution inlet for the aperture 34. A first end section 64 c of the aperture 34′ overlays the conduit apertures 30 c and 42 c to cooperatively define an outlet port for the aperture 34′. A diagonally opposed second end section 64 h of the aperture 34′ overlays the conduit apertures 30 h and 42 h to cooperatively define an inlet port for the aperture 34′.
 A first end section 66 b of the aperture 46 overlays the conduit apertures 42 b and 54 b to cooperatively define a concentrate outlet port for the aperture 46. A diagonally opposed second end section 66 e overlays conduit apertures 54 e and 42 e to cooperatively define a concentrate inlet for the aperture 46. A first end section 66 d of the aperture 46′ overlays the conduit apertures 42 d and 54 d to cooperatively define an outlet port for the aperture 46′. A diagonally opposed second end section 66 g of the aperture 46′ overlays the conduit apertures 42 g and 54 g to cooperatively define an inlet port for the aperture 46′.
 In FIGS. 2 and 3 the cell stack 10 is depicted as it is mounted with threaded bolts 68 between an opposed pair of electrolyte flow distribution endplates 70 a and 70 b. Preferably, the bolts 68 are coated with a plastic or other high electrically resistant material. The threaded bolts 68 are arranged around the periphery of the end plates 70 a and 70 b and also extend through the space between the split cells as shown in FIG. 4. As depicted in FIG. 5, a cathode 72 extends through the endplate 70 a and an anode 74 extends through the endplate 70 b. A rectifier 75 applies a potential between the cathode 72 and the anode 74. An electrolyte solution supplied to the endplates 70 a and 70 b, a concentrate stream sequentially supplied to the apertures 22, 22′, 46′ and 46 and a dilution stream sequentially supplied to the apertures 34 and 34′ provide electrically conductive fluid connection between the cathode 72 and the anode 74.
 The split-cell spacers comprise EPDM (ethylene propylene diene terpolymer) sold under the name Nordel by E. I. Du Pont de Nemours and Company. When assemble and secured with threaded bolts 68 no glue or other adhesive is required between the membranes and the spacers.
 Referring now to FIG. 6, there is depicted a flow diagram of an electrodialysis system adapted for using the cell stack described hereinabove. The system is portable and may be easily moved to locations where fluids require cleaning. For example, used antifreeze is stored in a mixing tank 76, where it is mixed with a metal reducing agent to precipitate metals in the fluid. The mixing tank 76 is in flow communication with a desalinated tank 78 through a filter pump 80, a 1 micron filter 82, a carbon adsorber 84 and a second 1 micron filter 86.
 The desalinated tank 78 is in flow communication by conduits, through a pump 88 to the conduit apertures 60 f, 54 f, 48 f and 42 f (in series) to enter the inlet of aperture 34. The outlet of the aperture 34 is connected in flow communication with the inlet of the aperture 34′ by a conduit 91. The outlet of the aperture 34′ is in flow communication with the desalinated tank by conduit apertures 30 c, 24 c, 19 c and 16 c.
 An electrolyte is stored in an electrolyte rinse tank 90, which is connected through conduits to the inlets 92 a and 92 b of the end plates 70 a and 70 b, respectively. The outlets 94 a and 94 b from the endplates 70 a and 70 b, respectively, are connected back to the electrolyte rinse tank 90. A pump 96 circulates the electrolyte.
 A pump 100 sends concentrated brine from a concentrate brine tank 98 through the conduit apertures 60 e and 54 e to enter the inlet of aperture 46. From the outlet of the aperture 46 the brine is directed through the conduit apertures 42 b, 36 b and 30 b to the inlet of the aperture 22. From the outlet of the aperture 22 the brine is directed through the conduit apertures 19 e and 16 e, a conduit 102, and conduit apertures 60 g and 54 g to the inlet of aperture 46′. From the outlet of the aperture 46′ the brine is directed through the conduit apertures 42 d, 36 d and 30 d to the outlet of the aperture 22′. From the outlet of the aperture 22′ the brine is directed back to the concentrated brine tank 98 via the conduit apertures 19 g and 16 g. The concentrated brine tank 98 is in flow communication with a concentrate neutralization tank 104.
 In operation, electrolyte is circulated between the electrolyte rinse tank 90 and the end plates 70 a and 70 b. The pH of the electrolyte is monitored for maintenance in a generally constant range. As required, neutralization acid may be added from the tank 104.
 Concentrated brine is circulated from the tank 98, sequentially through the apertures 46, 22, 46′ and 22′ and then back to the tank 98. The concentration of the brine is monitored for maintenance in a generally constant range. As required, water may be added to the tank 98. A “feed and bleed” mode of operation is provided for make-up water. The pH is also monitored and controlled.
 The fluid to be cleaned, such as used antifreeze, is entered into the mixing tank 76 where a stirrer 106 maintains agitation of the fluid with a metal reducing agent. The fluid is then pumped through the filter 82, the carbon adsorber 84 and the filter 86 to the desalinated tank 78. The fluid is circulated from the desalinated tank 78, sequentially through the apertures 34 and 34′, and then back to the desalinated tank. As is well recognized in the field of electrodialysis, the potential applied between the cathode 72 and anode 74 induce the ions of salts in the fluid to pass through the membranes into the brine solution passing through the adjacent aperture, thus increasing the concentration of salts in the brine solution and reducing the concentration of salts in the treated fluid. By cycling the fluid repeatedly through the apparatus, the concentration of salts can be reduced to the desired minimal level. A conductivity sensor 108 monitors the fluid as it leaves the pump 88 to determine when a satisfactory level has been reached. A control panel 110 provides visual readouts and controls for operating the system.
Conventional Multi- Multi-path Split Cell Parameter Compartment Stack (Operated in parallel) Glycol content % w. 40.0 40.0 Glycol Retention % 91.8 99.9 Starting conductivity 3,800 3,800 (μMho/cm) Finish Conductivity (μMho/ 1,000 1,000 cm) Cell pair Volage (V) 1.0 1.0 Membrane type Conventional Conventional Solution temperature (° F.) 76 76 Production Rate 0.44 2.0 (m3/day/m2 of membrane) Gasket Material EPDM EPDM
 (The anion exchange membrane used was Neosepta AFN produced by Tokuyama Corporation. The cation exchange membrane used was Neosepta CMX produced by Tokuyama Corporation.)
 The multi-path split cell system was substantially less costly to produce than the conventional multi-compartment stack, yet operated at a production rate over four times greater.
 Studies indicate that the configuration of the invention is a substantial improvement over traditional designs. Example 2 shows the production rate and typical % removal of NaCl for the current invention; those skilled in the art will recognize these values allow the invention to be economically competitive for a variety of feeds. Example 3 shows typical membrane area and energy requirements for desalination using traditional ED stack designs contrasted with the performance of the current invention. Those skilled in the art will recognize that the improved design of the current invention results in a stack requiring significantly less membrane area and that is significantly more energy efficient.
1. NaCl Feed Production Rate % NaCl Concentration (m3/m2 day) Removal 1.65 g/L 5.74 91 16.5 g/L 1.50 99
NaCl Feed Traditional % Concentration Designs** Split cell Reduction A. Membrane Area (m2) for 1 m3/day Capacity* 1 g/L 0.3 0.17 42% 10 g/L 1.2 0.67 44% B. Energy Requirements (kw-hr/m3 product)* 1 g/L 1.2 0.26 78% 10 g/L 3.4 2.67 21%
 An important variable describing an ED system is the current utilization efficiency. The current utilization efficiency is primarily influenced by the ED stack design and flow velocities but also to a lesser extent by the concentration and composition of the feed stream. For a given ED stack (gasket design, spacer design, etc.) and feed stream, the current efficiency is [1,2,3,4,5]:
 ξ=current utilization efficiency, %
 z=charge of ion
 F=Faraday's constant, 96,485 Amp-s/mol
 Qf=diluate flow rate, L/s
 Cd inlet=diluate ED cell inlet ion concentration, mol/L
 Cd outlet=diluate ED cell outlet ion concentration, mol/L
 N=number of cell pairs
 I=applied current, Amps.
 Those skilled in the art will recognize that current utilization efficiencies should be >70% for efficient use of ED for desalting typical brackish water feeds, and that current utilization decreases as the product water concentration decreases. Chart 1 shows that the invention provides excellent current utilization efficiencies (>90%) over a wide range of product water concentrations. The figure also shows that good current utilizations are achieved even when producing high quality product (<5 mg/L Cl−). Also, studies indicate that the invention is capable of producing a product with extremely low conductivity levels (down to as low as 2.6 μMho/cm). Those skilled in the art will recognize that this represents a substantial improvement compared to traditional ED designs, which are typically limited to product with conductivities >30 μMho/cm. As a result, the invention would represent a new pretreatment option for production of ultrapure water.
 While the depicted embodiment has been described in terms of three split cell spacers and four membranes, it will be recognized that additional split cell spacers and membranes are desirable to speed the process. Such additional apparatus would function in substantially the same manner.
 As depicted schematically in FIGS. 7a to 7 g, the split cells may be arranged with more than two cells and the cells may be arranged in a variety of parallel, serial and parallel/serial arrangements. FIG. 7a depicts the arrangement described herein above. FIG. 7b depicts an arrangement wherein the two split cells are arranged in parallel. FIG. 7c depicts a split cell having three apertures that are arranged serially. FIG. 7d depicts a split cell having three apertures that are arranged in parallel. FIG. 7e depicts a split cell having four apertures that are arranged with two parallel cells arranged serially with another set of parallel cells. FIG. 7f depicts a split cell having four apertures that are arranged serially. FIG. 7g depicts a split cell having four apertures with three cells arranged in parallel and all three serially feeding the fourth cell. It will be recognized by those skilled in the art that the multiple cells may be arranged in a variety of ways to accommodate many different electrodialysis situations.
 Benefits of the process include a recovery rate in excess of 95%, high throughput and low capital and operating cost. The system does not generate hazardous by-products. It is easy to operate, control and automate, and easy to maintain. Also, studies indicate that the invention is capable of producing a product with extremely low conductivity levels (down to as low as 2.6 μMho/cm). Those skilled in the art will recognize that this represents a substantial improvement compared to traditional ED designs, which are typically limited to product with conductivities >30 μMho/cm. As a result, the invention would represent a new pretreatment option for production of ultrapure water.
 The multi-path split-cell spacer design permits use of a single or multiple central bolts, eliminating the need for an expensive hydraulic clamping assembly for applying central pressure on the stack and providing a uniform force distribution over the gasket area, improving the seals between membranes and improving ion removal efficiency, while also reducing assembly labor time. Expensive machined components are replaced with simpler, lighter components having lower material costs, for a given membrane area assemblies.
 In addition to the described use of the method and apparatus to clean used antifreeze, the system may be used to clean and/or recycle: wash water (vehicular, laundry, mop water, trailer/tank washout, textile rinses, metal, aqueous parts cleaners), oil and gas field fluids (glycol base natural gas dehydration fluids, glycol/water heat transfer fluids, amines from treatment of natural gas, produced water), other thermal transfer fluids (secondary coolants from HVAC systems and coolants from ice-skating rinks), cooling water reuse, nuclear wastewater, mixed (nuclear and hazardous) wastewater, hazardous wastewater, desalination of sea or brackish water, drinking water production and pretreatment for ultra-pure water production.
 While the present invention has been illustrated by description and while the illustrative embodiments have been described in considerable detail, it is not the intention of the applicant to restrict or in any way limit the scope of the appended claims to such detail. Additional advantages and modifications will readily appear to those skilled in the art. The invention in its broader aspects is therefore not limited to the specific details, representative apparatus and methods, and illustrative examples shown and described. Accordingly, departures may be made from such details without departing from the spirit or scope of applicant's general inventive concept.
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|U.S. Classification||204/520, 204/523, 204/635, 204/638, 204/636|
|International Classification||B01D63/08, B01D61/50, C02F1/469, B01D61/46|
|Cooperative Classification||B01D2313/345, B01D2313/14, B01D63/084, B01D61/50, C02F1/4693|
|European Classification||C02F1/469D, B01D61/50, B01D63/08D10|
|Feb 21, 2002||AS||Assignment|
Owner name: EET CORPORATION, TENNESSEE
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:SFERRAZZA, ALOIS;REEL/FRAME:012633/0392
Effective date: 20020221