WO2001083379A1 - Electrodialysis membrane and gasket stack system - Google Patents

Electrodialysis membrane and gasket stack system Download PDF

Info

Publication number
WO2001083379A1
WO2001083379A1 PCT/US2001/012212 US0112212W WO0183379A1 WO 2001083379 A1 WO2001083379 A1 WO 2001083379A1 US 0112212 W US0112212 W US 0112212W WO 0183379 A1 WO0183379 A1 WO 0183379A1
Authority
WO
WIPO (PCT)
Prior art keywords
electrodialysis
membrane
cell stack
gasket
electrode plate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US2001/012212
Other languages
French (fr)
Inventor
Ernst Schmidt
Brian M. Schmidt
Erich Schmidt
James Schmidt
Michael E. Williams
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LIQUITEK CORP
Original Assignee
LIQUITEK CORP
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=24240439&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2001083379(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by LIQUITEK CORP filed Critical LIQUITEK CORP
Priority to AU2001253499A priority Critical patent/AU2001253499B2/en
Priority to CA002407599A priority patent/CA2407599A1/en
Priority to AU5349901A priority patent/AU5349901A/en
Priority to EP01927003A priority patent/EP1284933A4/en
Priority to JP2001580816A priority patent/JP2004517709A/en
Publication of WO2001083379A1 publication Critical patent/WO2001083379A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/50—Stacks of the plate-and-frame type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Definitions

  • the invention relates to an apparatus and a system of operation of a plurality of ion- exchange membranes. More specifically, the invention relates to an apparatus and system of operation of a plurality of electrodialysis membranes and gaskets stacked for separation of components from liquids passing through the membranes.
  • Prior methods of treatment for separating polar components in liquid mixtures having contaminants have been utilized to purify water, to desalinate water, and to purify ethylene glycol or other mixtures of chemicals.
  • One method utilizes ion exchange resins for separation of polar components on granular ion exchange resins, which require chemical regeneration of the resins and/or disposal ofthe resins.
  • Another treatment method for separating polar components in liquid mixtures include micro-porous membranes which selectively allow smaller polar compounds to pass through the membrane, while denying passage of larger sized polar compounds.
  • Another treatment method includes ion exchange membranes having anion and cation exchange membranes assembled in an alternating configuration in a unit of membranes.
  • Prior purifying and recycling devices include a plurality of ion exchange bipolar membranes separating solution compartments, and gasket separators secured together in face-to-face contact in a configuration of a multi-layered, stacked plate.
  • the gasket separators between the membranes provide sealing at the edges ofthe stacked plate of membranes, and enable a fluid to flow into and out ofthe stacked plate and through the individual solution compartments between the stacked plate of membranes.
  • the ion exchange bipolar membranes can contain an anode and a cathode electrode at the respective ends ofthe stack of membranes in order to provide an electrical input for maintaining a differential voltage between the anode end and the cathode end.
  • the ions contained in the solution to be purified will migrate in a direction in relation to the current depending on the charge of each ion in the solution.
  • the cations move toward the cathode or negative electrode, while the anions move toward the anode or positive electrode.
  • an operator induces the movement ofthe cations and anions in different directions across the stack of membranes, thereby operating the purifying and recycling system to remove contaminants from ethylene glycol, water, and/or other liquid solutions.
  • At least three types and sizes of stacks of electrodialysis membrane units are utilized in prior purifying and recycling devices, including an electrodialysis concentration cell having a cation membrane, a dilution or feed compartment, an anion membrane, and a concentrate or product compartment which forms a unit utilized for desalinating of brine solutions.
  • a second type of electrodialysis membrane unit includes a two-compartment cation cell having a bipolar membrane, a feed compartment, a cation membrane, and a base or product compartment.
  • a third type of electrodialysis membrane unit includes a two-compartment anion cell having a bipolar membrane, a product compartment, an anion membrane, and a feed compartment.
  • Electrodialysis membranes can include any combination of layers ofthe above three types to form a plurality of cation and anion membranes, interspersed with compartments and gaskets separating the compartments.
  • Electrodialysis designs for flow through the stacks of electrodialysis membranes include sheet flow and tortuous flow. Sheet flow stacks induce liquid flow across the length or width ofthe active membrane surface area, and generally are utilized for low linear velocity conditions in the range of 5 to 10 cm/sec. Tortuous flow stacks induce liquids to take a long flow path around gaskets, and are utilized for higher linear flow velocity conditions in the range of 30 to 50 cm/sec.
  • An apparatus and system of operation for the separation of polar components, inorganic contaminants, and organic contaminants within liquid mixtures.
  • the apparatus and system of operation for purification and deionizing liquid mixtures includes an operation of pretreatment by utilizing filtration for removal of inorganic contaminants and organic contaminants utilizing oil/water separation methods and settling methods for removal of suspended solids.
  • the system of operation includes an operation of adsorption treatment for the filtrate effluent ofthe pretreatment operation.
  • the adso ⁇ tion operation includes removing organic contaminants by utilizing activated carbon adso ⁇ tion methods.
  • the system of operation further includes an operation of deionizing for treating ofthe effluent liquids from the adso ⁇ tion operation.
  • the deionizing operation includes a system utilizing an apparatus having an electrodialysis cell stack including a plurality of disparate layers being stacked together, the electrodialysis cell stack having a first end and a second end, with the plurality of disparate layers stacked contiguous between the first end and second end.
  • a support frame supports the cell stack and encloses a perimeter ofthe plurality of disparate layers, with the layers being disposed in a repetitive sequence of layers between the first outer end and second outer end of the support frame.
  • the plurality of disparate layers of materials are disposed contiguous, having a first outer layer at the first end, and a second outer layer at the second end, with the plurality of disparate layers interdisposed therebetween.
  • the plurality of disparate layers include at least two electrodialysis membranes, the first ofthe electrodialysis gaskets being positioned as the first outer layer at the first end, opposite the second ofthe electrodialysis gaskets being positioned as the second outer layer at the second end.
  • a cathode electrode plate is positioned proximate to the first end and interior ofthe first electrodialysis gasket.
  • An anode electrode plate is positioned proximate to the second end and interior ofthe second electrodialysis gasket at the second end.
  • a voltage generating means is connected to the cell stack for application of an electrical voltage differential between the cathode electrode plate and the anode electrode plate
  • the plurality of disparate layers are disposed between the cathode and anode electrode plates and include a series of layers of differing permeability, the layers selected from a group comprising a first electrodialysis membrane gasket, a first turbulence promoter, an anion membrane, a second electrodialysis membrane gasket, a second turbulence promoter, a cation membrane, a third electrodialysis membrane gasket, and a third turbulence promoter, whereby the plurality of disparate layers can be repeated in series as required.
  • a connecting means provides connection of the plurality of disparate layers within the support frame, the connecting means including removably attachable connectors to allow the plurality of disparate layers to be replaced, and/or additional series of layers of differing permeability to be added to the electrodialysis cell stack.
  • the electrodialysis cell stack can further include the series of layers being repeated as required for removal of polar components and/or additional contaminants, with additional turbulence promoters being added to increase the dispersion ofthe liquid mixtures therethrough to increase the efficiency of removal of contaminants upon application of electrical voltage differential between the cathode electrode plate and the anode electrode plate.
  • the electrodialysis cell stack of disparate layers and enclosing frame ofthe deionizing operation provides continuous purifying of ethylene glycol and glycol/water mixtures, provides for continuous desalinating of water, and/or provides for continuous deionizing of water to generate ultra-pure water or other purified liquid mixtures.
  • the deionizing operation can be followed by an evaporation system for removal of excess water from the purified ethylene glycol or other liquid mixtures, with the purified liquids and/or deionized liquids being available for recycle and reuse.
  • the combination of treatment operations and the deionizing operation provides a continuous operating system with minimized down-time and improved efficiencies over prior methods for purification and deionizing liquid mixtures.
  • Figure 1 is a flow diagram illustrating the operations ofthe present invention for purification and deionizing liquid mixtures utilizing an electrodialysis operation
  • Figure 2 is a process schematic of one embodiment of a plurality of disparate layers of an electrodialysis cell stack of ion exchange membranes ofthe deionizing operation of Figure 1;
  • Figure 3 is a perspective view of a plurality of disparate layers ofthe electrodialysis cell stack of Figure 2;
  • Figure 4 is a process schematic of Figure 2 of a plurality of disparate layers illustrating the flow of liquid mixtures through and across the disparate layers;
  • Figure 5 is a perspective view of Figure 3 of a plurality of disparate layers illustrating the flow of liquid mixtures through the stacked disparate layers;
  • Figure 6 is a top view of an assembled plurality of disparate layers ofthe electrodialysis cell stack of Figure 2;
  • Figure 7 is a side view ofthe assembled electrodialysis cell stack of Figure 6;
  • Figure 8 is a front view ofthe assembled electrodialysis cell stack of Figure 7.
  • Figure 9 is a rear view ofthe assembled electrodialysis cell stack of Figure 8.
  • FIG. 1 illustrates the plurality of operations 10 for adequate operation of one embodiment ofthe deionizing system 122 ofthe present invention ofthe apparatus and system of operation, including an operation of pretreatment for a volume of contaminated liquids 108 by utilizing filtration for removal of inorganic contaminants and organic contaminants removal utilizing oil/water separation of suspended solids in a plurality of storage tanks 110.
  • the pretreatment operation 1 12 utilizes an oil/water separator 112 and storage containers known to those skilled in the art.
  • the system of operation includes an operation of adso ⁇ tion 1 16, 118 for treating ofthe effluent liquids from the pretreatment operation.
  • the adso ⁇ tion operation includes removing organic contaminants by utilizing activated carbon adso ⁇ tion compounds known to those skilled in the art.
  • the system of operation further includes an operation of deionizing 122 for treating ofthe effluent liquids from the adso ⁇ tion operation.
  • the deionizing operation includes an apparatus including an electrodialysis membrane cell stack 12 having a plurality of ion exchange membranes and separating gaskets for selectively removing contaminant ions from the effluent liquids.
  • the membrane cell stack 12 includes a first end 14, a central stack of a plurality of disparate layers being stacked on top of each layer (see Fig. 1), or being stacked side-by-side (see Fig. 6), and a second end 18 opposed from the first end 14 and enclosing the plurality of disparate layers.
  • a support frame 20 utilizing connecting members such as a pair of connectors bolts 16, 16' through the perimeter ofthe central stack provides a partially enclosing frame for the plurality of disparate layers that are disposed contiguous within the support frame 20.
  • the support frame 20 includes a first end proximate the first end 14 ofthe central stack, and a second end proximate the second end 18 ofthe central stack.
  • the plurality of disparate layers of materials are disposed contiguous, having a first outer layer at the first end 14, and a second outer layer at the second end 18, with the plurality of disparate layers interdisposed therebetween (see Figure 2 and 3).
  • the plurality of disparate layers include at least two electrodialysis gaskets composed of ethylene propylene diene monomer (EPDM), the first EPDM gasket 22 being positioned as the first outer layer proximate the first end 14, with a second EPDM gasket 24 being positioned as the second outer layer proximate the second end 18.
  • EPDM ethylene propylene diene monomer
  • the first electrodialysis EPDM gasket 22 and the second electrodialysis EPDM gasket 24 are each about 0.031 inches thick, and have the following dimensions.
  • Each gasket 22, 24 includes an exterior width of about 1' 5 3/8", and an exterior length of about 2' 3 7/8", with a 3/4" diameter off-center hole through an area about 2 11/16 " distance inward to the center ofthe off-center hole from a first side ofthe gaskets 22, 24, and the center ofthe off-center hole about 1' 5 7/16"along the length from the top edge ofthe gaskets 22, 24.
  • a cathode electrode plate 26 is positioned proximate the first end 14 ofthe plurality of disparate layers.
  • the cathode electrode plate 26 can be composed of a stainless steel plate and is positioned within the first electrodialysis gasket 22.
  • An anode electrode plate 28 is positioned proximate the second end 18, can be composed of a titanium and platinum alloy, and is positioned inwardly within the second electrodialysis gasket 24.
  • the cathode electrode plate 26 and the anode electrode plate 28 are about 0.030 inches thick, and have the following dimensions.
  • the plates 26, 28 have an exterior width of about 1' 5 3/8", and an exterior length of about 2' 3 7/8", with an off- center 3/8" threaded rod through an area about of 2 11/16 " distance inward to the center ofthe off- center rod from a first side of the plates 26, 28, and the center ofthe off-center rod about 1' 5 7/16"along the length from the top edge ofthe plates 26, 28.
  • Connector rods 16, 16' of about four inches in length are utilized to connect the plates 26, 28 and plurality of layers between together.
  • a voltage generating means (not shown) is connectable to the cathode electrode plate 26 and separately to the anode electrode plate 28 ofthe membrane cell stack 12 for application of an electrical voltage differential between the cathode electrode plate 26 and the anode electrode plate 28.
  • the voltage generating means can include a voltage generator and an electrode 134 inserted to contact the cathode electrode plate 26, and a separate electrode 134' inserted to contact the anode electrode plate 28.
  • the application of an electrical voltage differential provides for improved removal of polar contaminants from concentrated liquids directed across the cation membranes 50, 66 (discussed below) that are located between the cathode electrode plate 26 and the anode electrode plate 28.
  • the third layer positioned inwardly from the first end 14 is an outer electrodialysis EPDM gasket 30 positioned next to the cathode electrode plate 26, with another outer electrodialysis EPDM gasket 36 positioned next to the anode electrode plate 28 near the second end 18.
  • the outer electrodialysis EPDM gaskets 30, 36 are about 0.062 inches thick (70 Duro), and have the following dimensions.
  • the EPDM gaskets 30, 36 include an exterior width of about 1' 8", and an exterior length of about 3' 1 ", with about four spaced apart end holes of about 1 " diameter through an area in the upper portion of each gasket 30, 36, with each end hole center being about 2 3/4" down from the upper edge ofthe gasket gaskets 30, 36.
  • the interiors 32, 38 ofthe respective gasket gaskets 30, 36 are open to allow for optional placement of a layer of an appropriately sized turbulence promoter 34, 40 against the gaskets 30, 36.
  • Each interior 32, 38 includes inside dimensions of a width of about 1' 5 l ⁇ ", and a length of about 2' 4 3/4".
  • Each turbulence promoter 34, 40 is sized with a width of about 1' 5 3/8", and a length of about 2' 4 3/8".
  • the turbulence promoters 34, 40 if utilized in the membrane cell stack 12, are composed of a polypropylene fabric of about 0.030 inches thick.
  • the turbulence promoters 34, 40 can be combined with additional back-to-back stacked turbulence promoters 68, 70 (see Fig. 5) to create additional turbulence in liquids moving through and past the respective gasket gaskets 30, 36.
  • the fourth layer inwards from the first end 14 includes an anion membrane 42.
  • the anion membrane 42 includes an anion membrane 42.
  • the anion membrane 42 is the first of approximately six layers of a series of layers that can be repeated as often as desired by the operators ofthe electrodialysis system 10 for improved efficiency and flow of liquids through the membrane cell stack 12.
  • the anion membrane 42 is about 0.031 inches thick, and includes the dimensions of about 1' 8" wide and about 3' 1" long with four spaced apart end holes of about 1 " diameter through an area in the upper portion ofthe anion membrane 42 with each end hole center being about 2 3/4" down from the upper edge ofthe anion membrane 42.
  • Additional membranes, EPDM gaskets, and plate layers ofthe series of layers can include a fifth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added), composed of an electrodialysis EPDM gasket 44 having an offset interior opening 46.
  • the EPDM gasket 44 is about 0.031 inches thick (60 Duro), and the dimensions of an exterior width of about 1'
  • the interior opening 46 includes an upper interior corner opening offset from the upper exterior side ofthe first or right side of about 8 3/4", and is offset downwards of about 3" from the upper exterior side of gasket 44.
  • a similar sized offset in the interior opening 46 is within the opposed lower interior corner and includes an offset from the exterior side ofthe second or left side of about 8 3/4", and is offset upwards about 3" from the lower exterior side of gasket 44 (see Figs. 2-5).
  • a sixth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of a turbulence promoter 48 having an offset shape having an appropriate size for insertion into the interior opening 46 of EPDM gasket 44.
  • the outer dimensions of promoter 48 includes a width of about 1 ' 5 3/8", and a length of about 2' 10 3/8", with offset extensions sized appropriately to be insertable into the interior opening 46 of EPDM gasket 44.
  • a seventh layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of a cation membrane 50 having a generally rectangular size of a width of about 1' 8", and a length of about 3' 1 ".
  • the cation membrane 50 includes four spaced apart end holes of about 1" diameter through an area in the upper portion ofthe cation membrane 50 with each end hole center being about 2 3/4" down from the upper edge ofthe cation membrane 50, and four spaced apart end holes of about 1" diameter through an area in the lower portion ofthe cation membrane 50 with each end hole center being about 2 3/4" up from the lower edge ofthe membrane 50.
  • An eighth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of another electrodialysis EPDM gasket 52 having an offset interior opening 54.
  • the EPDM gasket 52 includes generally the dimensions of EPDM gasket 44, with the interior offset dimensions ofthe upper and lower opposed corners of opening 54 being a mirror image of interior opening 46.
  • a ninth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of another turbulence promoter 56 having an offset shape for insertion into the interior opening 54 of EPDM gasket 52.
  • the plurality of disparate layers, fourth through ninth layers, can be repeated after EPDM gasket 52 and/or turbulence promoter 56, as required to improve efficiency of removal of polar components.
  • a repeat set of disparate layers can include anion membrane 42, EPDM gasket 44 having opening 46, and turbulence promoter 48 being sized for insertion into opening 46.
  • Cation membrane 50 is followed by EPDM gasket 52 having opening 54, and turbulence promoter 56 being sized for insertion into opening 54.
  • anion membrane 58 Following one or more sets of disparate layers 42 - 52, another anion membrane 58 is positioned, the anion membrane 58 having the dimensions of anion membrane 42 described above.
  • the anion membrane 58 is followed by EPDM gasket 60 having opening 62 sized and shaped comparable to EPDM gasket 44 and opening 46.
  • Turbulence promoter 64 is sized and shaped to fit closely against EPDM gasket 60, with a cation membrane 66 following in series.
  • Cation membrane 66 is sized and shaped comparable to cation membrane 50.
  • the second end layers include the layers discussed above of second electrodialysis EPDM gasket 36, having opening 38 therethrough, followed by turbulence promoter 40, or additional stacked turbulence promoters, followed by the outer second end layers of anode electrode plate 28, and the second electrodialysis EPDM gasket 24.
  • Concentrate C liquid streams and dilute D liquid streams are directed through the cell stack 12 by passage through a plurality of end holes 72 in each ofthe following layers: 30, 42, 44, 48, 50, 52, 56, 58, 60, 64, 66, and 36.
  • Concentrate C liquid streams and dilute D liquid streams can be directed into the cell stack 12 at the first end 14, as shown in Figure 1, for passage through the plurality of end holes 72, and exiting at the second end 18, or alternatively can be directed into the end proximate the anode plate 28, as shown in Figure 5, for passage through the plurality of end holes 72, and exiting at the end proximate cathode plate 26.
  • a connecting means such as a support frame 20 known to those skilled in the art is connected by connection rods 16, 16' through the outer edges ofthe layers including EPDM gasket 30, the EPDM gasket 36, for containment ofthe membrane cell stack 12 positioned within the support frame 20.
  • a method of operation including a system for electrodialysis treatment of contaminated liquid mixtures including the operations of feeding a volume of contaminated liquids
  • the pretreatment system 112 can inco ⁇ orate an oil-water separator known to those skilled in the art, for generating a filtrate effluent 1 14 that is processed by an adsorbing operation 116, 118 for adsorbing organic contaminants from the filtrate effluent utilizing activated carbon adso ⁇ tion 116, and/or polishing with carbon particles in a polishing step 118, with the adsorbing operation 116, 1 18 generating a liquid fraction 120 for transfer to electrodialysis deionizing operation 122.
  • the electrodialysis membrane cell stack 126 includes a plurality of disparate layers enclosed within a support frame 20 supported by end plates 132, 132'.
  • the end plates 132, 132' can be composed of generally rigid PVC materials.
  • Connector members such as a pair of connector bolts 16, 16' of about 7/8 inch threaded diameter and having lengths of about four inches long fasten the cell stack 126 together.
  • the cell stack 126 (see Fig. 4 - 7) can accept multiple input streams such as dilute D input streams 128, 128', and concentrate C input streams 130, 130'.
  • the dilute D input streams 128, 128' are directed through the cell stack 126 through the plurality of end holes 72 forming an outer passage at each opposed end of a plurality ofthe layers of the cell stack to follow a tortuous flowpath at about the middle portions ofthe cell stack 126, due to the influence of turbulence promoter 56 and EPDM gaskets 52 and 60.
  • the dilute D streams pass through the outer passage holes of stacked membranes and gaskets for exit ofthe dilute D exit streams 138, 138' from the cell stack 126 at exit valves 142" and 142'" (see Fig. 4 and 5).
  • Electrode 134 is inserted through front end plate 132, and extends through EPDM gasket 22, for contact with, and maintenance of an electrical charge on cathode plate 26. Electrode 134' is inserted through rear end plate 132', and extends through EPDM gasket 24, for contact with, and maintenance of an electrical charge on anode plate 28.
  • the electrodes are about 3/8 inch diameter threaded rods.
  • an electrolyte E stream is injected in one side into at least one intake valve 136 of front end plate 132, for flow across the cathode plate 26 near the first end 14, and flow across the anode plate 28 near the second end 18, for exit from at least one exit valve 136' in the back end plate 132' ofthe cell stack 126 without mixing with the dilute D streams or the concentrate C streams.
  • the electrolyte E stream can be composed of a salt solution that provides a conducting solution to each cathode plate 26 and anode plate 28 ofthe cell stack 126 for improved performance of each electrically charged plate 26, 28.
  • the electrodialysis deionizing operation 122 selectively removes contaminant ions from the liquid fraction during the continuous passage ofthe liquid fraction through the cell stack 126.
  • the electrodialysis cell stack ofthe deionizing operation provides continuous purifying for ethylene glycol or for glycol/water mixtures, for continuous desalinating of water, and/or for continuous deionizing of water to generate ultra-pure water or other purified liquid mixtures.
  • the deionizing operation can be followed by an evaporation system 144 for removal of excess water from the purified ethylene glycol or other liquid mixtures, with the purified liquids and/or deionized liquids being available for combining with distilled water in a dilution process 146, for recycle and reuse ofthe purified and deionized liquid effluent 148.
  • an evaporation system 144 for removal of excess water from the purified ethylene glycol or other liquid mixtures, with the purified liquids and/or deionized liquids being available for combining with distilled water in a dilution process 146, for recycle and reuse ofthe purified and deionized liquid effluent 148.
  • the combination of treatment operations and the deionization operation provides a continuous operating system with minimized down-time and improved efficiencies over prior methods for purification and deionizing of liquid mixtures.
  • Analytical results demonstrate the efficiency ofthe deionizing operation utilizing the electrodialysis stack having a plurality of ion exchange membranes and separating gaskets as illustrated in Figures 2 and 3.
  • the analytical results were obtained by testing ofthe electrodialysis membrane stack design utilizing four cells in parallel, versus a baseline design of cells without the improved electrodialysis membrane cell stack 126 design.
  • the percent reduction in processing time is based on average overall deionizing time, and based on average conductivity change per time per unit of four cells.
  • the results can be summarized that four cells with the improved membranes instead of four cells having prior art membrane stack designs, plus operating in parallel the improved electrodialysis membrane cell stack 12 design to provide about 42% to about 44% decrease in processing time for a 5,000 gallon batch of liquids compared to prior membrane stack designs.
  • the average processing time for a 5,000 gallon batch of liquids is estimated to be about 20.5 hours per batch, reduced from an average of about 36.9 hours per batch for prior art membrane stack designs.
  • the benefits ofthe apparatus and system of operation disclosed is a reduction in overall processing times for the separation of polar components within liquid mixtures for purification and deionization of liquid mixtures, an ease of assembly for reduction in assembly times, and a simplified assembly with a lesser amount of parts.

Landscapes

  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Health & Medical Sciences (AREA)
  • Urology & Nephrology (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)

Abstract

An apparatus and system of operation of an electrodialysis membrane and gasket stack for separation of components in liquid mixtures is disclosed. The system of operation for purification and deionizing liquids (108) includes an operation of pretreatment (112) by filtration for removal of inorganic contaminants, includes an operation of adsorption (116, 118) for removing organic contaminants by activated carbon adsorption, and includes an operation of deionizing (122) for removing ions from the effluent liquids. The deionizing operation includes an apparatus having an electrodialysis stack (12) of a plurality of ion exchange membranes (42, 50, 58, 66) and separating gaskets (22, 30, 44, 52, 60, 36, 24) for selectively removing contaminant ions. The electrodialysis stack of ion exchange membranes and separating gaskets provides continuous operations for purifying ethylene glycol and glycol/water mixtures, for continuous desalinating of water, and/or for continuous deionizing of water to generate ultra-pure water or other purified liquid mixtures. The combination of treatment operations and the deionizing operation provides a continuous operating system with minimized down-time and improved efficiencies over prior methods for purification of liquid mixtures.

Description

TITLE OF INVENTION Electrodialysis Membrane And Gasket Stack System CROSS-REFERENCE TO RELATED APPLICATIONS Not Applicable.
STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT
Not Applicable.
BACKGROUND OF INVENTION
1. Field of Invention
The invention relates to an apparatus and a system of operation of a plurality of ion- exchange membranes. More specifically, the invention relates to an apparatus and system of operation of a plurality of electrodialysis membranes and gaskets stacked for separation of components from liquids passing through the membranes.
2. Description of the Related Art
Prior methods of treatment for separating polar components in liquid mixtures having contaminants have been utilized to purify water, to desalinate water, and to purify ethylene glycol or other mixtures of chemicals. One method utilizes ion exchange resins for separation of polar components on granular ion exchange resins, which require chemical regeneration of the resins and/or disposal ofthe resins. Another treatment method for separating polar components in liquid mixtures include micro-porous membranes which selectively allow smaller polar compounds to pass through the membrane, while denying passage of larger sized polar compounds. Another treatment method includes ion exchange membranes having anion and cation exchange membranes assembled in an alternating configuration in a unit of membranes.
Prior purifying and recycling devices include a plurality of ion exchange bipolar membranes separating solution compartments, and gasket separators secured together in face-to-face contact in a configuration of a multi-layered, stacked plate. The gasket separators between the membranes provide sealing at the edges ofthe stacked plate of membranes, and enable a fluid to flow into and out ofthe stacked plate and through the individual solution compartments between the stacked plate of membranes. The ion exchange bipolar membranes can contain an anode and a cathode electrode at the respective ends ofthe stack of membranes in order to provide an electrical input for maintaining a differential voltage between the anode end and the cathode end. When a direct current is passed through the multi-layered stacked plate, the ions contained in the solution to be purified will migrate in a direction in relation to the current depending on the charge of each ion in the solution. The cations move toward the cathode or negative electrode, while the anions move toward the anode or positive electrode. By controlling the electrical input, and therefore the differential voltages, an operator induces the movement ofthe cations and anions in different directions across the stack of membranes, thereby operating the purifying and recycling system to remove contaminants from ethylene glycol, water, and/or other liquid solutions.
At least three types and sizes of stacks of electrodialysis membrane units are utilized in prior purifying and recycling devices, including an electrodialysis concentration cell having a cation membrane, a dilution or feed compartment, an anion membrane, and a concentrate or product compartment which forms a unit utilized for desalinating of brine solutions. A second type of electrodialysis membrane unit includes a two-compartment cation cell having a bipolar membrane, a feed compartment, a cation membrane, and a base or product compartment. A third type of electrodialysis membrane unit includes a two-compartment anion cell having a bipolar membrane, a product compartment, an anion membrane, and a feed compartment. Additional types of electrodialysis membranes can include any combination of layers ofthe above three types to form a plurality of cation and anion membranes, interspersed with compartments and gaskets separating the compartments. Electrodialysis designs for flow through the stacks of electrodialysis membranes include sheet flow and tortuous flow. Sheet flow stacks induce liquid flow across the length or width ofthe active membrane surface area, and generally are utilized for low linear velocity conditions in the range of 5 to 10 cm/sec. Tortuous flow stacks induce liquids to take a long flow path around gaskets, and are utilized for higher linear flow velocity conditions in the range of 30 to 50 cm/sec. Utilization ofthe electrodialysis designs as described above in stacks of membranes for purifying and recycling of ethylene glycol solutions, or for purifying water and desalinating water require a plurality of multiple membranes having complicated configurations. There is a need for a simplified design of a series of electrodialysis membranes in stacked configurations for improved removal efficiencies of contaminants in a purification and deionizing system. Therefore, it is an object ofthe present invention to provide an improved membrane cell stack for purification of liquid mixtures.
It is another object ofthe present invention to provide a method of operation for an electrodialysis treatment system providing increased efficiency for ion-removal of liquid mixtures.
It is another object ofthe present invention to provide a membrane and gasket cell stack system having reduced assembly time.
It is another object of the present invention to provide a system having a plurality of membranes and interchangeable gaskets for improved efficiency for removal of contaminants by electrodialysis deionizing of liquid mixtures.
It is another object ofthe present invention to provide an improved system having a plurality of membranes and interchangeable gaskets for improved efficiency for deionizing liquid mixtures by an electrodialysis apparatus.
BRIEF SUMMARY OF INVENTION An apparatus and system of operation is disclosed for the separation of polar components, inorganic contaminants, and organic contaminants within liquid mixtures. The apparatus and system of operation for purification and deionizing liquid mixtures includes an operation of pretreatment by utilizing filtration for removal of inorganic contaminants and organic contaminants utilizing oil/water separation methods and settling methods for removal of suspended solids. The system of operation includes an operation of adsorption treatment for the filtrate effluent ofthe pretreatment operation. The adsoφtion operation includes removing organic contaminants by utilizing activated carbon adsoφtion methods.
The system of operation further includes an operation of deionizing for treating ofthe effluent liquids from the adsoφtion operation. The deionizing operation includes a system utilizing an apparatus having an electrodialysis cell stack including a plurality of disparate layers being stacked together, the electrodialysis cell stack having a first end and a second end, with the plurality of disparate layers stacked contiguous between the first end and second end. A support frame supports the cell stack and encloses a perimeter ofthe plurality of disparate layers, with the layers being disposed in a repetitive sequence of layers between the first outer end and second outer end of the support frame. The plurality of disparate layers of materials are disposed contiguous, having a first outer layer at the first end, and a second outer layer at the second end, with the plurality of disparate layers interdisposed therebetween. The plurality of disparate layers include at least two electrodialysis membranes, the first ofthe electrodialysis gaskets being positioned as the first outer layer at the first end, opposite the second ofthe electrodialysis gaskets being positioned as the second outer layer at the second end. A cathode electrode plate is positioned proximate to the first end and interior ofthe first electrodialysis gasket. An anode electrode plate is positioned proximate to the second end and interior ofthe second electrodialysis gasket at the second end. A voltage generating means is connected to the cell stack for application of an electrical voltage differential between the cathode electrode plate and the anode electrode plate The plurality of disparate layers are disposed between the cathode and anode electrode plates and include a series of layers of differing permeability, the layers selected from a group comprising a first electrodialysis membrane gasket, a first turbulence promoter, an anion membrane, a second electrodialysis membrane gasket, a second turbulence promoter, a cation membrane, a third electrodialysis membrane gasket, and a third turbulence promoter, whereby the plurality of disparate layers can be repeated in series as required. A connecting means provides connection of the plurality of disparate layers within the support frame, the connecting means including removably attachable connectors to allow the plurality of disparate layers to be replaced, and/or additional series of layers of differing permeability to be added to the electrodialysis cell stack.
The electrodialysis cell stack can further include the series of layers being repeated as required for removal of polar components and/or additional contaminants, with additional turbulence promoters being added to increase the dispersion ofthe liquid mixtures therethrough to increase the efficiency of removal of contaminants upon application of electrical voltage differential between the cathode electrode plate and the anode electrode plate.
The electrodialysis cell stack of disparate layers and enclosing frame ofthe deionizing operation provides continuous purifying of ethylene glycol and glycol/water mixtures, provides for continuous desalinating of water, and/or provides for continuous deionizing of water to generate ultra-pure water or other purified liquid mixtures.
The deionizing operation can be followed by an evaporation system for removal of excess water from the purified ethylene glycol or other liquid mixtures, with the purified liquids and/or deionized liquids being available for recycle and reuse. The combination of treatment operations and the deionizing operation provides a continuous operating system with minimized down-time and improved efficiencies over prior methods for purification and deionizing liquid mixtures.
BRIEF DESCRIPTION OF SEVERAL VIEWS OF DRAWINGS The above-mentioned objects and advantages ofthe present invention are readily apparent from the description of the invention contained herein, and by reference to the claims, read together with the drawings in which:
Figure 1 is a flow diagram illustrating the operations ofthe present invention for purification and deionizing liquid mixtures utilizing an electrodialysis operation; Figure 2 is a process schematic of one embodiment of a plurality of disparate layers of an electrodialysis cell stack of ion exchange membranes ofthe deionizing operation of Figure 1;
Figure 3 is a perspective view of a plurality of disparate layers ofthe electrodialysis cell stack of Figure 2;
Figure 4 is a process schematic of Figure 2 of a plurality of disparate layers illustrating the flow of liquid mixtures through and across the disparate layers;
Figure 5 is a perspective view of Figure 3 of a plurality of disparate layers illustrating the flow of liquid mixtures through the stacked disparate layers;
Figure 6 is a top view of an assembled plurality of disparate layers ofthe electrodialysis cell stack of Figure 2; Figure 7 is a side view ofthe assembled electrodialysis cell stack of Figure 6;
Figure 8 is a front view ofthe assembled electrodialysis cell stack of Figure 7; and
Figure 9 is a rear view ofthe assembled electrodialysis cell stack of Figure 8.
DETAILED DESCRIPTION OF THE INVENTION In accordance with the present invention, there is disclosed an apparatus and system of operation for the separation of polar components, inorganic contaminants, and organic contaminants within liquid mixtures for purification and deionizing liquid mixtures. Figure 1 illustrates the plurality of operations 10 for adequate operation of one embodiment ofthe deionizing system 122 ofthe present invention ofthe apparatus and system of operation, including an operation of pretreatment for a volume of contaminated liquids 108 by utilizing filtration for removal of inorganic contaminants and organic contaminants removal utilizing oil/water separation of suspended solids in a plurality of storage tanks 110. The pretreatment operation 1 12 utilizes an oil/water separator 112 and storage containers known to those skilled in the art.
The system of operation includes an operation of adsoφtion 1 16, 118 for treating ofthe effluent liquids from the pretreatment operation. The adsoφtion operation includes removing organic contaminants by utilizing activated carbon adsoφtion compounds known to those skilled in the art.
The system of operation further includes an operation of deionizing 122 for treating ofthe effluent liquids from the adsoφtion operation. The deionizing operation includes an apparatus including an electrodialysis membrane cell stack 12 having a plurality of ion exchange membranes and separating gaskets for selectively removing contaminant ions from the effluent liquids. The membrane cell stack 12 includes a first end 14, a central stack of a plurality of disparate layers being stacked on top of each layer (see Fig. 1), or being stacked side-by-side (see Fig. 6), and a second end 18 opposed from the first end 14 and enclosing the plurality of disparate layers. A support frame 20 utilizing connecting members such as a pair of connectors bolts 16, 16' through the perimeter ofthe central stack provides a partially enclosing frame for the plurality of disparate layers that are disposed contiguous within the support frame 20. The support frame 20 includes a first end proximate the first end 14 ofthe central stack, and a second end proximate the second end 18 ofthe central stack. The plurality of disparate layers of materials are disposed contiguous, having a first outer layer at the first end 14, and a second outer layer at the second end 18, with the plurality of disparate layers interdisposed therebetween (see Figure 2 and 3). The plurality of disparate layers include at least two electrodialysis gaskets composed of ethylene propylene diene monomer (EPDM), the first EPDM gasket 22 being positioned as the first outer layer proximate the first end 14, with a second EPDM gasket 24 being positioned as the second outer layer proximate the second end 18.
The first electrodialysis EPDM gasket 22 and the second electrodialysis EPDM gasket 24 are each about 0.031 inches thick, and have the following dimensions. Each gasket 22, 24 includes an exterior width of about 1' 5 3/8", and an exterior length of about 2' 3 7/8", with a 3/4" diameter off-center hole through an area about 2 11/16 " distance inward to the center ofthe off-center hole from a first side ofthe gaskets 22, 24, and the center ofthe off-center hole about 1' 5 7/16"along the length from the top edge ofthe gaskets 22, 24.
A cathode electrode plate 26 is positioned proximate the first end 14 ofthe plurality of disparate layers. The cathode electrode plate 26 can be composed of a stainless steel plate and is positioned within the first electrodialysis gasket 22. An anode electrode plate 28 is positioned proximate the second end 18, can be composed of a titanium and platinum alloy, and is positioned inwardly within the second electrodialysis gasket 24. The cathode electrode plate 26 and the anode electrode plate 28 are about 0.030 inches thick, and have the following dimensions. The plates 26, 28 have an exterior width of about 1' 5 3/8", and an exterior length of about 2' 3 7/8", with an off- center 3/8" threaded rod through an area about of 2 11/16 " distance inward to the center ofthe off- center rod from a first side of the plates 26, 28, and the center ofthe off-center rod about 1' 5 7/16"along the length from the top edge ofthe plates 26, 28. Connector rods 16, 16' of about four inches in length are utilized to connect the plates 26, 28 and plurality of layers between together. A voltage generating means (not shown) is connectable to the cathode electrode plate 26 and separately to the anode electrode plate 28 ofthe membrane cell stack 12 for application of an electrical voltage differential between the cathode electrode plate 26 and the anode electrode plate 28. The voltage generating means can include a voltage generator and an electrode 134 inserted to contact the cathode electrode plate 26, and a separate electrode 134' inserted to contact the anode electrode plate 28. The application of an electrical voltage differential provides for improved removal of polar contaminants from concentrated liquids directed across the cation membranes 50, 66 (discussed below) that are located between the cathode electrode plate 26 and the anode electrode plate 28.
The third layer positioned inwardly from the first end 14 is an outer electrodialysis EPDM gasket 30 positioned next to the cathode electrode plate 26, with another outer electrodialysis EPDM gasket 36 positioned next to the anode electrode plate 28 near the second end 18. The outer electrodialysis EPDM gaskets 30, 36 are about 0.062 inches thick (70 Duro), and have the following dimensions. The EPDM gaskets 30, 36 include an exterior width of about 1' 8", and an exterior length of about 3' 1 ", with about four spaced apart end holes of about 1 " diameter through an area in the upper portion of each gasket 30, 36, with each end hole center being about 2 3/4" down from the upper edge ofthe gasket gaskets 30, 36. The interiors 32, 38 ofthe respective gasket gaskets 30, 36 are open to allow for optional placement of a layer of an appropriately sized turbulence promoter 34, 40 against the gaskets 30, 36. Each interior 32, 38 includes inside dimensions of a width of about 1' 5 lΛ", and a length of about 2' 4 3/4". Each turbulence promoter 34, 40 is sized with a width of about 1' 5 3/8", and a length of about 2' 4 3/8". The turbulence promoters 34, 40, if utilized in the membrane cell stack 12, are composed of a polypropylene fabric of about 0.030 inches thick. The turbulence promoters 34, 40 can be combined with additional back-to-back stacked turbulence promoters 68, 70 (see Fig. 5) to create additional turbulence in liquids moving through and past the respective gasket gaskets 30, 36.
The fourth layer inwards from the first end 14 (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added), includes an anion membrane 42. The anion membrane
42 is the first of approximately six layers of a series of layers that can be repeated as often as desired by the operators ofthe electrodialysis system 10 for improved efficiency and flow of liquids through the membrane cell stack 12. The anion membrane 42 is about 0.031 inches thick, and includes the dimensions of about 1' 8" wide and about 3' 1" long with four spaced apart end holes of about 1 " diameter through an area in the upper portion ofthe anion membrane 42 with each end hole center being about 2 3/4" down from the upper edge ofthe anion membrane 42.
Additional membranes, EPDM gaskets, and plate layers ofthe series of layers can include a fifth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added), composed of an electrodialysis EPDM gasket 44 having an offset interior opening 46. The EPDM gasket 44 is about 0.031 inches thick (60 Duro), and the dimensions of an exterior width of about 1'
8", and an interior opening width of about 1' 5 V". The interior opening 46 includes an upper interior corner opening offset from the upper exterior side ofthe first or right side of about 8 3/4", and is offset downwards of about 3" from the upper exterior side of gasket 44. A similar sized offset in the interior opening 46 is within the opposed lower interior corner and includes an offset from the exterior side ofthe second or left side of about 8 3/4", and is offset upwards about 3" from the lower exterior side of gasket 44 (see Figs. 2-5).
A sixth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of a turbulence promoter 48 having an offset shape having an appropriate size for insertion into the interior opening 46 of EPDM gasket 44. The outer dimensions of promoter 48 includes a width of about 1 ' 5 3/8", and a length of about 2' 10 3/8", with offset extensions sized appropriately to be insertable into the interior opening 46 of EPDM gasket 44.
A seventh layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of a cation membrane 50 having a generally rectangular size of a width of about 1' 8", and a length of about 3' 1 ". The cation membrane 50 includes four spaced apart end holes of about 1" diameter through an area in the upper portion ofthe cation membrane 50 with each end hole center being about 2 3/4" down from the upper edge ofthe cation membrane 50, and four spaced apart end holes of about 1" diameter through an area in the lower portion ofthe cation membrane 50 with each end hole center being about 2 3/4" up from the lower edge ofthe membrane 50. An eighth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of another electrodialysis EPDM gasket 52 having an offset interior opening 54. The EPDM gasket 52 includes generally the dimensions of EPDM gasket 44, with the interior offset dimensions ofthe upper and lower opposed corners of opening 54 being a mirror image of interior opening 46. A ninth layer (without counting the plurality of turbulence promoters 34, 68, 40, 70 that may be added) is composed of another turbulence promoter 56 having an offset shape for insertion into the interior opening 54 of EPDM gasket 52.
The plurality of disparate layers, fourth through ninth layers, can be repeated after EPDM gasket 52 and/or turbulence promoter 56, as required to improve efficiency of removal of polar components. A repeat set of disparate layers, can include anion membrane 42, EPDM gasket 44 having opening 46, and turbulence promoter 48 being sized for insertion into opening 46. Cation membrane 50 is followed by EPDM gasket 52 having opening 54, and turbulence promoter 56 being sized for insertion into opening 54.
Following one or more sets of disparate layers 42 - 52, another anion membrane 58 is positioned, the anion membrane 58 having the dimensions of anion membrane 42 described above.
The anion membrane 58 is followed by EPDM gasket 60 having opening 62 sized and shaped comparable to EPDM gasket 44 and opening 46. Turbulence promoter 64 is sized and shaped to fit closely against EPDM gasket 60, with a cation membrane 66 following in series. Cation membrane 66 is sized and shaped comparable to cation membrane 50. The second end layers include the layers discussed above of second electrodialysis EPDM gasket 36, having opening 38 therethrough, followed by turbulence promoter 40, or additional stacked turbulence promoters, followed by the outer second end layers of anode electrode plate 28, and the second electrodialysis EPDM gasket 24. Concentrate C liquid streams and dilute D liquid streams are directed through the cell stack 12 by passage through a plurality of end holes 72 in each ofthe following layers: 30, 42, 44, 48, 50, 52, 56, 58, 60, 64, 66, and 36. Concentrate C liquid streams and dilute D liquid streams can be directed into the cell stack 12 at the first end 14, as shown in Figure 1, for passage through the plurality of end holes 72, and exiting at the second end 18, or alternatively can be directed into the end proximate the anode plate 28, as shown in Figure 5, for passage through the plurality of end holes 72, and exiting at the end proximate cathode plate 26. A connecting means such as a support frame 20 known to those skilled in the art is connected by connection rods 16, 16' through the outer edges ofthe layers including EPDM gasket 30, the EPDM gasket 36, for containment ofthe membrane cell stack 12 positioned within the support frame 20.
A method of operation is disclosed including a system for electrodialysis treatment of contaminated liquid mixtures including the operations of feeding a volume of contaminated liquids
108, into a pretreating system 112 for filtration of inorganic contaminants and organic contaminants with the pretreatment operation including a pretreatment settling tank 110. The pretreatment system 112 can incoφorate an oil-water separator known to those skilled in the art, for generating a filtrate effluent 1 14 that is processed by an adsorbing operation 116, 118 for adsorbing organic contaminants from the filtrate effluent utilizing activated carbon adsoφtion 116, and/or polishing with carbon particles in a polishing step 118, with the adsorbing operation 116, 1 18 generating a liquid fraction 120 for transfer to electrodialysis deionizing operation 122.
A preferred embodiment for the method ofthe deionizing operation 122 is illustrated in Figures 4 - 9. The electrodialysis membrane cell stack 126 includes a plurality of disparate layers enclosed within a support frame 20 supported by end plates 132, 132'. The end plates 132, 132' can be composed of generally rigid PVC materials. Connector members such as a pair of connector bolts 16, 16' of about 7/8 inch threaded diameter and having lengths of about four inches long fasten the cell stack 126 together.
Multiple input streams are introduced through end plate 132, into input valves 124, 124', 124", 124'", with multiple output streams released from end plate 132', from output or exit valves 142, 142', 142", 142"'(see Fig. 6 - 9). The liquid streams requiring deionizing are directed through the cell stack 126 by passage through a plurality of end holes 72 in each ofthe following respective layers: 30, 42, 44, 48, 50, 52, 56, 58, 60, 64, 66, and 36.
The cell stack 126 (see Fig. 4 - 7) can accept multiple input streams such as dilute D input streams 128, 128', and concentrate C input streams 130, 130'. The concentrate C input streams 130,
130' are directed through the plurality of end holes 72 ofthe respective layers of cell stack 126, and the streams 130, 130' travel between cation membranes 50, 66 and anion membranes 42, 58 due to the influence of turbulence promoters 48 and 64, and EPDM gaskets 44, 52, 36 and 60, to follow a tortuous flow for exit as concentrate C exit streams 140, 140' from the cell stack 126 at exit valves 142, 142'.
The dilute D input streams 128, 128' are directed through the cell stack 126 through the plurality of end holes 72 forming an outer passage at each opposed end of a plurality ofthe layers of the cell stack to follow a tortuous flowpath at about the middle portions ofthe cell stack 126, due to the influence of turbulence promoter 56 and EPDM gaskets 52 and 60. The dilute D streams pass through the outer passage holes of stacked membranes and gaskets for exit ofthe dilute D exit streams 138, 138' from the cell stack 126 at exit valves 142" and 142'" (see Fig. 4 and 5).
Electrode 134 is inserted through front end plate 132, and extends through EPDM gasket 22, for contact with, and maintenance of an electrical charge on cathode plate 26. Electrode 134' is inserted through rear end plate 132', and extends through EPDM gasket 24, for contact with, and maintenance of an electrical charge on anode plate 28. The electrodes are about 3/8 inch diameter threaded rods.
As shown in Figures 4, 6 - 9, an electrolyte E stream is injected in one side into at least one intake valve 136 of front end plate 132, for flow across the cathode plate 26 near the first end 14, and flow across the anode plate 28 near the second end 18, for exit from at least one exit valve 136' in the back end plate 132' ofthe cell stack 126 without mixing with the dilute D streams or the concentrate C streams. The electrolyte E stream can be composed of a salt solution that provides a conducting solution to each cathode plate 26 and anode plate 28 ofthe cell stack 126 for improved performance of each electrically charged plate 26, 28.
The electrodialysis deionizing operation 122 selectively removes contaminant ions from the liquid fraction during the continuous passage ofthe liquid fraction through the cell stack 126. The electrodialysis cell stack ofthe deionizing operation provides continuous purifying for ethylene glycol or for glycol/water mixtures, for continuous desalinating of water, and/or for continuous deionizing of water to generate ultra-pure water or other purified liquid mixtures.
The deionizing operation can be followed by an evaporation system 144 for removal of excess water from the purified ethylene glycol or other liquid mixtures, with the purified liquids and/or deionized liquids being available for combining with distilled water in a dilution process 146, for recycle and reuse ofthe purified and deionized liquid effluent 148.
The combination of treatment operations and the deionization operation provides a continuous operating system with minimized down-time and improved efficiencies over prior methods for purification and deionizing of liquid mixtures.
Analytical results demonstrate the efficiency ofthe deionizing operation utilizing the electrodialysis stack having a plurality of ion exchange membranes and separating gaskets as illustrated in Figures 2 and 3. The analytical results were obtained by testing ofthe electrodialysis membrane stack design utilizing four cells in parallel, versus a baseline design of cells without the improved electrodialysis membrane cell stack 126 design. The percent reduction in processing time is based on average overall deionizing time, and based on average conductivity change per time per unit of four cells. The results can be summarized that four cells with the improved membranes instead of four cells having prior art membrane stack designs, plus operating in parallel the improved electrodialysis membrane cell stack 12 design to provide about 42% to about 44% decrease in processing time for a 5,000 gallon batch of liquids compared to prior membrane stack designs. The average processing time for a 5,000 gallon batch of liquids is estimated to be about 20.5 hours per batch, reduced from an average of about 36.9 hours per batch for prior art membrane stack designs.
The benefits ofthe apparatus and system of operation disclosed is a reduction in overall processing times for the separation of polar components within liquid mixtures for purification and deionization of liquid mixtures, an ease of assembly for reduction in assembly times, and a simplified assembly with a lesser amount of parts.
One skilled in the art will recognize the associated mechanical components which support the system are illustrated in the Figures for clarity only and other embodiments could be utilized without interfering with the objects and advantages ofthe present invention.
While a preferred embodiment is shown and described, it will be understood that it is not intended to limit the disclosure, but rather it is intended to cover all modifications and alternative apparatus configurations and systems of operation falling within the spirit and the scope ofthe invention as defined in the appended claims.

Claims

CLAIMS What is claimed is: 1. A membrane cell stack for purification of liquid mixtures having contaminants dispersed therein, and for deionization of liquid mixtures by passage through the membrane cell stack, the liquid mixtures including concentrate liquids and/or dilute liquids, said membrane cell stack comprising: an electrodialysis cell stack including a plurality of disparate layers being stacked together, said electrodialysis cell stack having a first end and a second end, said plurality of disparate layers being disposed contiguous and having a first outer layer at said first end, and a second outer layer at said second end; a support frame having a first outer end proximate said first end of said cell stack, and having a second outer end proximate said second end, with said plurality of disparate layers interdisposed therebetween said first outer end and said second outer end; at least two electrodialysis gaskets including a first electrodialysis gasket being positioned at said first outer end, and a second electrodialysis gasket being positioned at said second outer end; a cathode electrode plate being positioned proximate and interior of said first electrodialysis gasket being positioned at said first outer end; at least one anode electrode plate being positioned proximate and interior of said second electrodialysis gasket being positioned at said second outer layer; at least two membrane gaskets including a first membrane gasket being positioned proximate and interior of said cathode electrode plate, and a second membrane gasket being positioned proximate and interior of said anode electrode plate, said first membrane gasket and said second membrane gasket having a central opening therethrough and having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; said plurality of disparate layers including: an anion membrane having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; at least one electrodialysis membrane gasket having a central opening therethrough and having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; at least one turbulence promoter layer being sized to fit proximate said opening within said at least one electrodialysis membrane gasket and having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; and a cation membrane having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; whereby said plurality of disparate layers being repeated in series, the liquid mixtures being passed through said plurality of holes in respective disparate layers of said electrodialysis cell stack; and connecting means for connection of said plurality of disparate layers within said support frame; whereby said electrodialysis cell stack including said plurality of disparate layers being repeated as required for purification and deionization ofthe liquid mixtures being passed therethrough.
2. The membrane cell stack of Claim 1, wherein said electrodialysis cell stack further comprises a voltage generating means for application of an electrical voltage differential between said cathode electrode plate and said at least one anode electrode plate, said voltage generating means including a voltage generator, said electrodialysis cell stack having a first electrode in contact with said cathode electrode plate, and a second electrode in contact with said at least one anode electrode plate.
3. The membrane cell stack of Claim 1, wherein said plurality of disparate layers being stacked adjacent and having a plurality of shapes being sized for being positioned within said support frame, said plurality of disparate layers further includes a plurality of turbulence promoter plates and a plurality of electrodialysis membrane gaskets being positioned between said anion membrane and said cation membrane for direction ofthe waste liquids from the plurality of holes through each opposed end of each disparate layer to the plurality of holes through each adjacent disparate layer for passage of liquid mixtures therethrough said electrodialysis cell stack.
4. The membrane cell stack of Claim 1, wherein said first electrodialysis gasket and said second electrodialysis gasket being composed of ethylene propylene diene monomer of about 0.031 inch thickness.
5. The membrane cell stack of Claim 1, wherein said first membrane gasket and said second membrane gasket being composed of ethylene propylene diene monomer of about 0.062 inch thickness.
6. The membrane cell stack of Claim 1 , wherein said at least one turbulence promoter being composed of polypropylene fabric of about 0.030 inch thickness.
7. The membrane cell stack of Claim 1, wherein said at least one electrodialysis membrane gasket having an opening therethrough being composed of ethylene propylene diene monomer of about 0.031 inch thickness.
8. The membrane cell stack of Claim 1 , wherein said first end of said electrodialysis cell stack comprising a first input valve and a second input valve through said first end for receipt of concentrate liquids in said first input valve, and for receipt of dilute liquids in said second input valve, whereby said concentrate liquids and said dilute liquids being passed though said plurality of disparate layers of said electrodialysis cell stack.
9. The membrane cell stack of Claim 8, wherein said second end of said electrodialysis cell stack comprising a first output valve and a second output valve through said second end for passage of concentrate liquids out of said second output valve, and for passage of dilute liquids out of said first output valve, whereby said concentrate liquids and said dilute liquids having passed though said plurality of disparate layers of said electrodialysis cell stack.
10. The membrane cell stack of Claim 9, wherein said support frame having a first outer end and having a second outer end, further comprises: at least one intake valve in said first outer end; an electrolyte liquid being input into said at least one intake valve, said electrolyte liquid being in contact across said cathode electrode plate; said electrolyte liquid being in contact across said anode electrode plate; and at least one exit valve in said second outer end for removal of said electrolyte liquid from said cell stack; whereby said electrolyte liquid does not contact said concentrate liquids or said dilute liquids within said cell stack.
11. A membrane cell stack for purification of liquid mixtures having contaminants dispersed therein in concentrate liquids and/or in dilute liquids, and for deionization of liquid mixtures by passage through said membrane cell stack comprising: an electrodialysis cell stack including a plurality of disparate layers being stacked together, said electrodialysis cell stack having a first end and a second end, said plurality of disparate layers being disposed contiguous and having a first outer layer at said first end, and a second outer layer at said second end; a support frame having a first outer end proximate said first end of said cell stack, and having a second outer end proximate said second end, with said plurality of disparate layers interdisposed therebetween said first outer end and said second outer end; at least two electrodialysis gaskets including a first electrodialysis gasket being positioned at said first outer end, and a second electrodialysis gasket being positioned at said second outer end; a cathode electrode plate being positioned proximate and interior of said first electrodialysis gasket being positioned at said first outer end; at least one anode electrode plate being positioned proximate and interior of said second electrodialysis gasket being positioned at said second outer layer; at least two membrane gaskets including a first membrane gasket being positioned proximate and interior of said cathode electrode plate, and a second membrane gasket being positioned proximate and interior of said anode electrode plate, said first membrane gasket and said second membrane gasket having a central opening therethrough and having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; said plurality of disparate layers including: an anion membrane having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; a first electrodialysis membrane gasket having a central opening therethrough and having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; a first turbulence promoter layer being sized to fit proximate said opening within said first electrodialysis membrane gasket; a cation membrane having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; a second electrodialysis membrane gasket having an opening therethrough and having a plurality of holes through each opposed end for passage of liquid mixtures therethrough; and a second turbulence promoter layer being sized to fit proximate said opening within said second electrodialysis membrane gasket; whereby said plurality of disparate layers being repeated in series, the liquid mixtures being passed through said electrodialysis cell stack; connecting means for connection of said plurality of disparate layers within said support frame; and a voltage being supplied by a voltage supply means, said voltage being applied as a voltage differential between said cathode electrode plate and said anode electrode plate; whereby said electrodialysis cell stack including said plurality of disparate layers being repeated as required for purification and deionization ofthe liquid mixtures being passed therethrough.
12. The membrane cell stack of Claim 11, wherein said electrodialysis cell stack further comprises a first electrode in contact with said cathode electrode plate, and a second electrode in contact with said at least one anode electrode plate for application of said voltage differential between said cathode electrode plate and said at least one anode electrode plate.
13. The membrane cell stack of Claim 12, wherein said plurality of disparate layers being substantially parallel and being sized and shaped for being positioned within said support frame, said plurality of disparate layers further includes a plurality of turbulence promoter plates being positioned between said anion membrane and proximate said anode electrode plate.
14. The membrane cell stack of Claim 13, wherein said first electrodialysis gasket and said second electrodialysis gasket being composed of ethylene propylene diene monomer of about 0.031 inch thickness.
15. The membrane cell stack of Claim 14, wherein said first membrane gasket and said second membrane gasket being composed of ethylene propylene diene monomer of about 0.062 inch thickness.
16. The membrane cell stack of Claim 15, wherein said turbulence promoter being composed of polypropylene fabric of about 0.030 inch thickness.
17. The membrane cell stack of Claim 16, wherein said first electrodialysis membrane gasket and second electrodialysis membrane gasket being composed of ethylene propylene diene monomer of about 0.031 inch thickness.
18. A system for electrodialysis treatment of liquid mixtures including concentrate liquids and/or dilute liquids comprising the operations of: providing a pretreating operation for filtration of inorganic contaminants and organic contaminants, said pretreatment operation generating a filtrate effluent; providing an adsorbing operation for adsorbing organic contaminants from said filtrate effluent utilizing activated carbon adsoφtion, said adsorbing operation generating a liquid fraction; and providing a deionizing operation for continuous purifying of said liquid fraction from said adsorbing operation, including utilizing an electrodialysis stack having a plurality of membranes and separating gaskets, said deionizing operation selectively removing contaminant ions from said liquid fraction; whereby said deionizing operation providing said electrodialysis stack having a plurality of ion exchange membranes providing continuous purifying of said liquid fractions of ethylene glycol and glycol/water mixtures, and providing continuous purifying of water, and/or continuous purifying ethylene glycol and/or glycol and water mixtures.
19. The system for electrodialysis treatment of Claim 18, wherein said deionization operation comprises: providing an electrodialysis cell stack including a plurality of disparate layers being stacked together, said electrodialysis cell stack having a first end and a second end, said plurality of disparate layers being disposed contiguous and having a first outer layer at said first end, and a second outer layer at said second end; supporting said electrodialysis cell stack within a support frame having a first outer end proximate said first end of said cell stack, and having a second outer end proximate said second end, with said plurality of disparate layers interdisposed therebetween said first outer end and said second outer end; providing at least two electrodialysis gaskets including a first electrodialysis gasket being positioned at said first outer end, and a second electrodialysis gasket being positioned at said second outer end; positioning a cathode electrode plate proximate and interior of said first electrodialysis gasket being positioned at said first outer end; positioning an anode electrode plate proximate and interior of said second electrodialysis gasket being positioned at said second outer layer; providing at least two membrane gaskets including a first membrane gasket being positioned proximate and interior of said cathode electrode plate, and a second membrane gasket being positioned proximate and interior of said anode electrode plate, said first membrane gasket and said second membrane gasket having an opening therethrough; positioning said plurality of disparate layers in series including: an anion membrane; at least one electrodialysis membrane gasket having an opening therethrough; at least one turbulence promoter layer being sized to fit proximate said opening within said at least one electrodialysis membrane gasket; and a cation membrane; whereby said positioning said plurality of disparate layers being repeated in series; passing the liquid mixtures through said electrodialysis cell stack; and supplying a voltage differential between said cathode electrode plate and said anode electrode plate; whereby said deionizing operation purifies and deionizes the liquid mixtures being passed therethrough.
PCT/US2001/012212 2000-04-28 2001-04-13 Electrodialysis membrane and gasket stack system Ceased WO2001083379A1 (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
AU2001253499A AU2001253499B2 (en) 2000-04-28 2001-04-13 Electrodialysis membrane and gasket stack system
CA002407599A CA2407599A1 (en) 2000-04-28 2001-04-13 Electrodialysis membrane and gasket stack system
AU5349901A AU5349901A (en) 2000-04-28 2001-04-13 Electrodialysis membrane and gasket stack system
EP01927003A EP1284933A4 (en) 2000-04-28 2001-04-13 Electrodialysis membrane and gasket stack system
JP2001580816A JP2004517709A (en) 2000-04-28 2001-04-13 Electrodialysis membrane and gasket lamination system

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US09/561,049 US6274020B1 (en) 2000-04-28 2000-04-28 Electrodialysis membrane and gasket stack system
US09/561,049 2000-04-28

Publications (1)

Publication Number Publication Date
WO2001083379A1 true WO2001083379A1 (en) 2001-11-08

Family

ID=24240439

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2001/012212 Ceased WO2001083379A1 (en) 2000-04-28 2001-04-13 Electrodialysis membrane and gasket stack system

Country Status (6)

Country Link
US (2) US6274020B1 (en)
EP (1) EP1284933A4 (en)
JP (1) JP2004517709A (en)
AU (2) AU5349901A (en)
CA (1) CA2407599A1 (en)
WO (1) WO2001083379A1 (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2198947A1 (en) 2008-12-22 2010-06-23 Aquafuel Research Limited Purification of alcohols

Families Citing this family (42)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT1313862B1 (en) * 1999-11-11 2002-09-24 Solvay EXTREMITY BOX OF AN ELECTRODIALIZER, ELECTRODIALIZER THAT INCLUDES SUCH EXTREMITY BOX AND PROCEDURE OF
US6274020B1 (en) 2000-04-28 2001-08-14 Ernst Schmidt Electrodialysis membrane and gasket stack system
US7175869B2 (en) * 2000-11-30 2007-02-13 Kraft Foods Holdings, Inc. Method of deflavoring soy-derived materials using electrodialysis
US20030155243A1 (en) * 2002-02-21 2003-08-21 Eet Corporation Multi-path split cell spacer and electrodialysis stack design
US7582326B2 (en) 2003-10-29 2009-09-01 Kraft Foods Global Brands Llc Method of deflavoring whey protein using membrane electrodialysis
US20050186311A1 (en) * 2004-02-23 2005-08-25 Loh Jimbay P. Method for acidifying and preserving food compositions using electrodialyzed compositions
US20050183955A1 (en) * 2004-02-23 2005-08-25 Crowley Colin P. Electrodialyzed compositions and method of treating aqueous solutions using elecrtrodialysis
US7887867B2 (en) 2004-02-23 2011-02-15 Kraft Foods Global Brands Llc Stabilized non-sour dairy base materials and methods for preparation
US20050186312A1 (en) * 2004-02-23 2005-08-25 Kraft Foods Holdings, Inc. Shelf-stable foodstuffs and methods for their preparation
US20050220969A1 (en) * 2004-02-23 2005-10-06 Kraft Foods Holdings, Inc. Shelf-stable cold-processed food compositions and methods for their preparation
US20060024413A1 (en) * 2004-02-23 2006-02-02 Colin Crowley Preparation of pumpable, edible composition using electrodialysis
US7501064B2 (en) * 2005-01-06 2009-03-10 Eet Integrated electro-pressure membrane deionization system
CN100349805C (en) * 2005-12-30 2007-11-21 于容朴 Dynamic micro filter membrane assembly and water treatment process method
US8277627B2 (en) 2006-06-13 2012-10-02 Siemens Industry, Inc. Method and system for irrigation
US8114259B2 (en) 2006-06-13 2012-02-14 Siemens Industry, Inc. Method and system for providing potable water
US10213744B2 (en) 2006-06-13 2019-02-26 Evoqua Water Technologies Llc Method and system for water treatment
US10252923B2 (en) 2006-06-13 2019-04-09 Evoqua Water Technologies Llc Method and system for water treatment
US20080067069A1 (en) 2006-06-22 2008-03-20 Siemens Water Technologies Corp. Low scale potential water treatment
US7820024B2 (en) 2006-06-23 2010-10-26 Siemens Water Technologies Corp. Electrically-driven separation apparatus
CN1904724B (en) * 2006-07-29 2012-10-17 汕头市华天富工业发展有限公司 Electric dialysis desalinating process for photosensitive emulsion preparing production line and device thereof
CN101306855B (en) * 2007-11-07 2010-07-21 傅叶明 Plate type electro-deionization device
AU2008331796B2 (en) 2007-11-30 2013-01-10 Evoqua Water Technologies Llc Systems and methods for water treatment
US20100037941A1 (en) * 2008-08-13 2010-02-18 E. I. Du Pont De Nemours And Company Compositions and processes for forming photovoltaic devices
DE102009001512A1 (en) * 2009-03-12 2010-09-16 Evonik Degussa Gmbh Production of high-purity suspensions containing precipitated silicas by electrodialysis
US8648219B2 (en) 2010-08-20 2014-02-11 James Cramer Method for purifying glycerin and products obtained therefrom
EP2637972A1 (en) 2010-11-12 2013-09-18 Siemens Pte Ltd. Electrical purification apparatus having a blocking spacer
PL2663388T3 (en) 2011-01-13 2020-04-30 Carlsberg A/S An electro-membrane separation system
US9339765B2 (en) 2011-09-16 2016-05-17 General Electric Company Electrodialysis method and apparatus for passivating scaling species
KR101282794B1 (en) 2012-01-06 2013-07-05 한국에너지기술연구원 Stack-type flow capacitive deionization device
CN105209159B (en) 2013-03-15 2018-06-12 懿华水处理技术有限责任公司 For the flow distributor of Electrochemical separation
US20150299002A1 (en) * 2014-04-22 2015-10-22 Purewater Medical, Inc Active carbon filter system and method
CN106045137A (en) * 2016-01-29 2016-10-26 蔡雄 Seawater desalination method and seawater desalination system
IL272679B2 (en) 2017-08-21 2023-09-01 Evoqua Water Tech Llc Treatment of saline water for agricultural and potable use
US12180103B2 (en) 2017-08-21 2024-12-31 Evoqua Water Technologies Llc Treatment of saline water for agricultural and potable use and for generation of disinfectant solution
CN108423775A (en) * 2018-03-24 2018-08-21 佛山市云米电器科技有限公司 Ionize purifier and family's management system for internet of things
US12195370B2 (en) * 2020-10-14 2025-01-14 Duke University Methods and systems for wastewater treatment
TWI740763B (en) * 2020-12-30 2021-09-21 財團法人工業技術研究院 Cassette type electrodialysis unit and module comprising the same
US12151211B2 (en) 2021-07-19 2024-11-26 Aqueous Resources LLC Electro-pressure membrane method for recovery and concentration of lithium from aqueous sources
US12172908B2 (en) 2021-08-12 2024-12-24 Robert Bosch Gmbh Water deionization cells with flow channels packed with intercalation material
US12195366B2 (en) * 2021-08-12 2025-01-14 Robert Bosch Gmbh Water deionization cells
KR102727002B1 (en) * 2021-12-21 2024-11-05 주식회사 포스코 Electrodialysis and feeding tray of electrodialysis
KR20240061105A (en) * 2022-10-31 2024-05-08 포스코홀딩스 주식회사 Electrodialysis and manufacfuring method thereof

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3223612A (en) * 1959-10-02 1965-12-14 American Mach & Foundry Fluid treatment
US3235481A (en) * 1960-07-25 1966-02-15 American Mach & Foundry Spacer gasket
US3405047A (en) * 1959-05-22 1968-10-08 American Mach & Foundry Electrodialysis method and apparatus having a series of cascades
US5972191A (en) * 1997-01-17 1999-10-26 Archer Daniels Midland Company Electrodialysis apparatus

Family Cites Families (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3375182A (en) * 1959-05-22 1968-03-26 American Mach & Foundry Electrodialysis method and apparatus having radially symmetrical flow paths
US3291716A (en) * 1963-06-24 1966-12-13 Ionics Noble metal coated valve metal electrodes useful in electrodialysis systems
US3412006A (en) * 1965-01-11 1968-11-19 Ionics Ion-exchange membranes
US3761386A (en) * 1971-08-02 1973-09-25 Process Research Inc Novel membrane spacer
US3878086A (en) * 1972-05-01 1975-04-15 Process Research Inc Electrodialysis stack and spacer for use therein
JPS548355B2 (en) * 1973-08-06 1979-04-14
US3993517A (en) * 1975-10-31 1976-11-23 The United States Of America As Represented By The Secretary Of The Interior Thin cell electromembrane separator
US4319978A (en) * 1980-12-30 1982-03-16 Lea Manufacturing Company Spacer for electrodialysis stack
US4427507A (en) * 1982-03-22 1984-01-24 Shell Oil Company Process for the separation of glycol from an electrolyte-containing aqueous solution
JPS6068009A (en) 1983-09-26 1985-04-18 Tokuyama Soda Co Ltd Electrodialysis cell installed with ion exchange membrane and desalting process
JPS60115503U (en) * 1984-01-09 1985-08-05 バブコツク日立株式会社 electrodialysis machine
EP0185067B1 (en) * 1984-06-18 1989-04-26 The Permutit Company Limited Fluid separation cells and spacers for use in these
GB8415463D0 (en) * 1984-06-18 1984-07-25 Permutit Boby Ltd Fluid separation cells
US4676908A (en) * 1984-11-19 1987-06-30 Hankin Management Services Ltd. Waste water treatment
US4752373A (en) * 1985-01-14 1988-06-21 Morton Thiokol, Inc. Electrodialysis apparatus for the chemical maintenance of electroless copper plating baths
US4810340A (en) * 1986-11-13 1989-03-07 Shell Oil Company Process for recovering organic values from aqueous solutions containing both organic values and scale-forming ions
US5294305A (en) * 1993-05-06 1994-03-15 Mobile Process Technology, Inc. Ethylene glycol recovery process
JPH07109492A (en) * 1993-10-13 1995-04-25 Arakawa Chem Ind Co Ltd Reclamation from waste liquid of nonhalogen detergent
US5503729A (en) 1994-04-25 1996-04-02 Ionics Incorporated Electrodialysis including filled cell electrodialysis (electrodeionization)
JPH09110770A (en) * 1995-10-12 1997-04-28 Denki Kagaku Kogyo Kk Purification of alkylene glycol alkyl ether
RU2109556C1 (en) * 1996-04-29 1998-04-27 Акционерное общество открытого типа "Капролактам" Method of preparing ethylene glycol aqueous solution from exhausted antifreezes
US6187197B1 (en) * 1998-10-28 2001-02-13 Marvin Haddock Multi-stage engine coolant recycling process
US6274020B1 (en) * 2000-04-28 2001-08-14 Ernst Schmidt Electrodialysis membrane and gasket stack system

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3405047A (en) * 1959-05-22 1968-10-08 American Mach & Foundry Electrodialysis method and apparatus having a series of cascades
US3223612A (en) * 1959-10-02 1965-12-14 American Mach & Foundry Fluid treatment
US3235481A (en) * 1960-07-25 1966-02-15 American Mach & Foundry Spacer gasket
US5972191A (en) * 1997-01-17 1999-10-26 Archer Daniels Midland Company Electrodialysis apparatus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP1284933A4 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2198947A1 (en) 2008-12-22 2010-06-23 Aquafuel Research Limited Purification of alcohols

Also Published As

Publication number Publication date
JP2004517709A (en) 2004-06-17
US6274020B1 (en) 2001-08-14
AU5349901A (en) 2001-11-12
AU2001253499B2 (en) 2004-06-24
US6537436B2 (en) 2003-03-25
US20010037942A1 (en) 2001-11-08
CA2407599A1 (en) 2001-11-08
EP1284933A1 (en) 2003-02-26
EP1284933A4 (en) 2004-10-13

Similar Documents

Publication Publication Date Title
AU2001253499B2 (en) Electrodialysis membrane and gasket stack system
AU2001253499A1 (en) Electrodialysis Membrane and Gasket Stack System
US7138045B2 (en) Multi-path split cell spacer and electrodialysis stack design
US8377280B2 (en) Microscale capacitive deionization apparatus
US20100133115A1 (en) Devices and methods for acid and base generation
JP4065664B2 (en) Electric desalination equipment
JP2002535128A (en) Electrodeionizer and electrodeionization method
CN104838043B (en) electrochemical separation system and method
US7820024B2 (en) Electrically-driven separation apparatus
US20090008269A1 (en) Electrocoagulation reactor and water treatment system and method
KR102733383B1 (en) Deionization device and method for at least partially deionizing a supply liquid containing dissolved electrolyte, and apparatus using such devices
US6998044B2 (en) Electrophoretic cross-flow filtration and electrodeionization: method for treating effluent waste and apparatus for use therewith
Dermentzis et al. Copper removal from industrial wastewaters by means of electrostatic shielding driven electrodeionization.
KR20120133229A (en) Capacitive deionization method for drinking water treatment
US20060254919A1 (en) Electrophoretic cross-flow filtration and electrodeionization method for treating effluent waste and apparatus for use therewith
KR102591796B1 (en) Capacitive seawater desalination system using ion-drive, and methdo thereof
KR100196746B1 (en) Module for two path electrodeionization apparatus
KR20230107642A (en) Electrodeionization configuration for enhanced removal of weakly ionized species

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CR CU CZ DE DK DM DZ EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

ENP Entry into the national phase

Ref document number: 2001 580816

Country of ref document: JP

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 2001927003

Country of ref document: EP

Ref document number: 2407599

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 2001253499

Country of ref document: AU

WWP Wipo information: published in national office

Ref document number: 2001927003

Country of ref document: EP

WWG Wipo information: grant in national office

Ref document number: 2001253499

Country of ref document: AU