US2689826A - Electrodialytic apparatus - Google Patents

Electrodialytic apparatus Download PDF

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Publication number
US2689826A
US2689826A US175127A US17512750A US2689826A US 2689826 A US2689826 A US 2689826A US 175127 A US175127 A US 175127A US 17512750 A US17512750 A US 17512750A US 2689826 A US2689826 A US 2689826A
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chambers
cells
diaphragms
fluid
flow
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US175127A
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English (en)
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Kollsman Paul
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Individual
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Priority to BE504756D priority Critical patent/BE504756A/xx
Priority to NL96481D priority patent/NL96481C/xx
Priority to NL7810787.A priority patent/NL162669C/xx
Priority to US175127A priority patent/US2689826A/en
Application filed by Individual filed Critical Individual
Priority to GB16533/51A priority patent/GB694223A/en
Priority to CH300582D priority patent/CH300582A/de
Priority to FR1045890D priority patent/FR1045890A/fr
Priority to DEK10696A priority patent/DE931944C/de
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Publication of US2689826A publication Critical patent/US2689826A/en
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    • 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
    • B01D61/463—Apparatus therefor comprising the membrane sequence AC or CA, where C is a cation exchange membrane
    • 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

Definitions

  • This invention relates to the art of modifying the chemical composition of substances by a transfer of ions under the influence of an electric current in a process commonly called electrodialysis.
  • this process involves a transfer, or removal, of ions of one volume of fluid through anion impeding and cation impeding dia- ⁇ phragms into another volume of iiuid under the influence of ⁇ an electrical bias or potential causing the ions to travel in predetermined directions.
  • the volume of the rst iiuid is thus depleted of ions and the volume of the second fluid is enriched.
  • the present invention provides improvements in, and refinements of, the method of electrodia'lysis as well as of apparatus for practicing the method, making method and apparatus more efficient, resulting in products of higher purity, and greater uniformity, even with dia-lysis diaphragms of moderate quality.
  • the invention also consists of certain new and original features of construction and combination of parts, as well as of steps and combination ⁇ of steps, as hereinafter set forth and claimed.
  • Figure 1 is a diagrammatic representation, in vertical cross section of an improved apparatus embodying the present invention and adatped to ⁇ carry out the improved method disclosed herein;
  • Figure 2 is an elevational view taken on line 2-2 of Figure 1, and showing, in addition, further details of the apparatus.
  • Figure l is a diagrammatic illustration of an apparatus particularly designed for increasing and decreasing the salinity of water by clectrodialysis, but it may be used for the treatment or production of other fluids and compositions.
  • a tank II is subdivided into a plurality of chambers or cells by separating ion discriminating walls or diaphragms composed of a suitable composition or material imparting to the walls or diaphragme ion discriminating characteristics.
  • certain diaphragms I2 are anion-permeable V and cation-repellent, while other diaphragms I3 have theopposite characteristic of being cation-permeable and anion-repellent.
  • the diaphragms are arranged in alternating sequence with respect to traverse of the tank from one end to the other so that an anion-permeable diaphragm follows a cation-permeable diaphragm and is, in turn, followed by an anion-permeable diaphragm, and so forth.
  • the chambers of cells may be classified into two terminal cells Il and I5 containing electrodes I6 and il, and a plurality of intermediate cells I8 and I9.
  • the electrode Iii ⁇ is connected to the negative pole of a source of electric energy 2li by a lead 2i thus becoming a cathode, and the electrode Il is connected to the positive pole of a source 2i) by a lead 22 making the electrode Il an anode.
  • the intermediate cells I8 may conveniently be termed concentration cells, and the intermediate cells I9 may ⁇ be called dilution cells, according to the character of the electrodialytic action taking place therein.
  • the dilution cells I 9 are preferably narrower than the concentration Acells I8, width being measured between the bordering diaphragms.
  • the cells have inlet ports 23 at, or near, the bottom admitting fluid into the dilution cells from an inlet duct 24 which is suitably manifolded with respect to all the dilution cells.
  • the endmost diaphragms extend above the tops of the intermediate diaphragms to corinne between them a common pool 25 with which the open ends 26 of the cells I9 communicate freely.
  • a large outlet port 2l determines the height to which the liquid level 28 may rise.
  • An outlet duct 29 ( Figure 2) leads from the port 2l to discharge processed uid from the processing tank II.
  • the terminal diaphragms have ports 30 and 3
  • Fluid in the pool may freely enter the concentration chambers I8 which are open at the top at 36.
  • the fluid iiows through the concentration chambers in a downward direction, opposed to the direction of flow through the chambers I8, and leaves the concentration chambers through restricted metering passages 3l which form discharge ports for these chambers.
  • the restricted passages 31 are dimensioned to permit only a fraction of the volumetric iiow admitted through the inlet ports 23 to pass into a common discharge duct 43 as will also be explained later in greater detail.
  • the ⁇ fluid of the terminal chambers is preferably handled separately because of certain electro-chemical reactions which may be induced by the physical presence of the electrodes in the chambers, making it generally undesirable to mix the product of the terminal cells with the products of other cells.
  • Fluid is supplied through the inlet duct 24 at a predetermined controlled slow rate which is maintained sufliciently slow to insure a pre- ⁇ determined degree of dilution, by reason of iondepletion, to take place, during the ow of the fluid from the bottom of the cells to the top.
  • the flow through the concentration cells is preferably maintained at a fraction of the total volumetric flow passing through the dilution cells, a preferred range of ratios being that in which the ow through the concentration cells is restricted to between one-half and one-twelfth the volumetric flow passing through the dilution cells. This is preferably accomplished by installation of flow restricting passages 31 of the proper dimension.
  • the volumetric flows through the dilution and the concentration cells by reference to the volume entering the dilution cells through the inlet duct 24 and to the volume leaving the concentration cells through the discharge duct 43 into which the restricted passage 31 lead.
  • the volume of fluid entering the dilution cells includes that portion of fluid which permeates the diaphragms of the dilution cells
  • the volume withdrawn from the concentration cells includes 4 the fluid gain due to passage of fluid through the diaphragms into the concentration cells.
  • the supply of fluid through the inlet duct 24 may conveniently be maintained at a predetermined volumetric rate by use of supply tank 38 ( Figure 2) connected to the duct 24.
  • the liquid level 39 in the supply tank is maintained constant by a supply valve 4I) controlled by a iioat 4I admitting sufcient fluid from a supply pipe 42 to maintain the liquid level slightly above the liquid level 28, the difference in the two levels being so selected as to provide for a predetermined static pressure which, in turn, results in a predetermined rate of flow through the chambers I9. It is thus possible to control the rate of ilow through the dilution cells by adjustment of the float 4I.
  • the operation of the apparatus may be conveniently explained by a specic example. It may be assumed that the apparatus is being used for the production of fresh water of a high degree of purity and the simultaneous production of concentrated sea water or brine. When the operation of the device as applied to Water purification is understood, it will easily be seen how other compounds in solution may be treated in the apparatus.
  • an electrical potential is applied at the electrodes at the time salt-containing raw water enters through the inlet duct 24 into the apparatus whose concentration cells are also filled with water, preferably containing a slight amount of salt in order to cause a current to ow through the cells from one electrode to the other.
  • the raw water fed into the apparatus is preferably rst filtered to free it from mechanical impurities.
  • the raw water ows slowly through the dilution cells from the bottom towards the top and is gradually deionized by reason of the action of the electric current causing the ions of the raw water to permeate the diaphragms.
  • the positively charged sodium cations tend to travel towards the cathode I5.
  • the sodiu'm cations pass through the cations permeable diaphragms I3 and accumulate in the concentration cells I8 which they are unable to leave because of the cation-blocking properties of the diaphragms I2 which bar their path.
  • chlorine anions pass through the anion permeable diaphragm I2 and accumulate in the concentration cells I3 from which their exit is barred by the anion-blocking properties of the diaphragms I3.
  • the sodium and chlorine ions in the concentration cells recombine as sodium chloride and cause the salt concentration in the cells I3 to increase, while simultaneously the salt concentration in the dilution cells decreases.
  • the purication of water flowing through the dilution cells may be carried to a very high degree, and Water leaving through the outlet port 2l has a particularly high degree of purity.
  • the flow through the concentration cells takes place at a volumetric rate which is only a fraction of the volumetric rate of flow through the dilution cells. For this reason the salt enrichment per volumetric unit of fluid in the concentration cells reaches a higher degree than the salt depletion in the dilution cells. Assuming, .for example, that the volumetric ilow through the 5, concentration cells is one sixth of the volumetric :dow through the dilution cells,.itlis evident Vthat the concentration taking place ⁇ in the concentration compartment ⁇ is six times as great per volumetric unit of fluid as the loss of salt in the dilution cells so that the water leaving the concentration ⁇ compartment through the discharge ports contains six times the amount of salt as the sea water entering the dilution cells.
  • the loss of fluid appears to be proportional to the transfer of ions
  • the presence of a higher ion concentration near the bottom of the concentration cells lessens the loss of fluid from the dilution cells in which the greatest loss also tends to occur near the bottom.
  • the high ion concentration in the concentration cells tends to reduce the loss of fluid from the dilution cells.
  • the high concentration of the fluid leaving the concentration cells makes the fluid suitable for further commercial use, which it might not have, if the concentration were less.
  • the resultant brine may be used for manufacture of dry salt and other uses.
  • the volumetric rate of flow through the dilution cells I9 may be controlled either by control of the fluid pressure or by the dimensions of the ports 2l, or both, in such a way that the fluid leaving the device through the outlet lduct 29 has the desired degree of dilution, and the volumetric flow through the concentration compartment is so controlled, as to maintain the ion enrichment at a predetermined ratio with respect to the ion depletion in the adjoining cells.
  • the ratio may be one to six or one to ten, or any other gure, as conditions ⁇ may require. This is conveniently effected by control of the out-flow, for example by installation of suitably restricted discharge ports 2B.
  • a particular feature of the counter flow arrangement of the illustrated apparatus is its favorable effect on the current density near the bottom of the cells in order to remove the greatest possible number of ions per unit of time from the ilow entering the dilution cells.
  • a high current density near the bottom of the cells is promoted by the concentration cells in which the greatest concentration and hence the :greatest conductivity is likewise near the bottom, and not near the top, as it would be in an ⁇ installation which does notemploy the principle of opposite ilow on opposite sides of the diaphragms.
  • the rate of flow through the individual dilution cells is controlled inA such a way that the product at the tops 2.6 of "all the cells ⁇ Il) is of 6. uniform purity. It is rather di'icult to control the ⁇ rate of flow through the individual dilution cells E9 by proper dimensioning of their individual inlet ports 23 in such a way that the volumetric flows through all the dilution cells I9 is ⁇ precisely the same.
  • Nonmuniformity of flow has certain disadvantages, as will be seen from the followin specific examples:
  • ⁇ It may be assumed, that the volumetric ilow through all the cells is equal with the exception of one cell through which the ow passes at a slower rate. Under these circumstances all the cells, except the one, yield a product of insufficient purity, since the uid in the one cell becomes deionized sooner than the fluid in the other cells. As soon as the fluid in the one cell becomes deionized its conductivity' approaches zero and the current ceases to flow. Deionization in the other cells ceases, and the fluid discharged from them has a lower degree of purity, than desired. I
  • the gravity control may be carried out in an extremely simple manner by using the weight of the liquid columns as the controlling means.
  • the specic gravity of each fluid column proper in the individual dilution cells retards or accelerates the flow through the cells. It has been found that extremely small differences in gravity are suificient to provide a very effective control of the rate of flow.
  • the control operates as follows:
  • the fluid ows at a more rapid rate through one cell than through the other.
  • the rapid flow in the one cell causes the iluid to be exposed to the dialyzing current for a shorter time than in the other cells, resulting in less deionization and a higher specic gravity of the fluid in the one cell than in the others.
  • the greater weight of the fluid column in the one cell causes less liuid to enter the cell, thus retarding the flow.
  • the retarded iicw is subject to the dialyzing current for a longer period of time whereby a proportionately greater number of ions is removed therefrom, causing the weight of the fluid column to become less and the ow rate to increase. In this manner a proper mean rate of flow is automatically maintained in each cell resulting in a yield of fluid from all the dilution cells which is of substantially uniform purity,
  • a fluid of a particularly high degree of purity for example, if drinking water is to be produced from sea water, it is preferable to subject the iluid to the action of a dialyzing current more than once.
  • a dialyzing current more than once.
  • the product of all the dilution cells I9 is collected in the pool 25 and withdrawn through the port 21 and the duct 29.
  • the now of the treated fluid through the duct 29 involves intimate mixing of the products of the several dilution cells so that the fluid is of uniform concentration or dilution as it enters a second dialyzer tank Ill through an inlet duct H24.
  • the dialyzer III corresponds in all details to the dialyzer shown in Figure 1, but the potential applied to its electrodes may be higher because of the low ion concentration of the iiuids to be treated. A lead l2
  • the fluid After ow of the fluid through the dilution cells of the second dialyzer the fluid is again collected in a pool and is then withdrawn through a duct
  • 29 is of a high degree of purity and the second step of dialyzation is efflcient and economical, since the products of the cells of the rst dialyzer are not individually subjected to the second treatment, but only after thorough mixing. This is important since no unduly high voltages need be employed to overcome the effects of the presence of a more highly purified product in some of the cells, resulting in a greater ohmic resistance, than in the others.
  • the electrodes IB and I1 are lmade of a material resisting decomposition. Carbon and graphite are suitable materials for the anodein an apparatus for purifying wa-ter, and iron or nickel-chromium may serve as material for the cathode.
  • the dilution cells represent a greater ohmi'c resistance per unit of width than the concentration cells, -the dilution cells may be made narrower than the concentration cells.
  • the thickness of the fluid lms in the ycells is considerably less than shown in the drawings in which many dimensions are exaggerated or reduced for the sake of clearness. It has been found particularly advantageous toA make the spaces between the diaphragms narrower than the thickness of the diaphragms and to employ diaphragms of high electric conductivity. For example, a spacing of one or two millimeters has 'been found advantageous ⁇ for diaphragms of a thickness of three millimeters.
  • the height of the cells is not shown in its correct -proportion with respect to the other dimensions.
  • the height of the ycells may natu ⁇ rally be considerably greater than shown so that the fluid columns in the cells are of substantial length.
  • flows of fluid to be deionized are confined between flows of fluid into which ions are to be transferred through ion-discriminating diaphragms.
  • the fluids are maintained in ythe state of flux in opposite directions ⁇ past the diaphragms and the volumetric flow of the iiuid into which ions are to be transferred' is maintained smaller than -the volumetric flow of the iiuid to be deionized.
  • the volume of fluid withdrawn from the ⁇ concentration cells may be supplied in part from the output of the dilution cells, but may be replenished entirely by fluid transfer through the diaphragms. It is evident that in the treatment of fluids in steps or stages by passage, in succession, through several ion exchange units as represented by Figures 1 and 3, the fluid supplied to the concentration cells in the rst stage or unit need not be as highly purified as in the succeeding stages, since the purity of the fluid at the top of the concentration cells need not be greater than the desired purity of the iiuid leaving the dilution cells.
  • the flow of iiuid to be deionized is split into a plurality of substantially equal branches all of which are subjected to the same current. It follows that the rate of deionization per inch of flow is the same in all -the branches assuming that the flows are equal. This is conveniently -controlled by proper adjustment of the individual ports lthrough which the fluid enters or leaves the cells.
  • ion-discriminating diaphragm is used in the claims to identify membranes which have the inherent property of being permeable to ions of one sign and passage resistant to ions of the opposite sign.
  • An apparatus for increasing and decreasing the ion ycontent of liquids comprising means forming a plurality of chambers, not less than ve, the -chambers being arranged in line; aniondiscriminating and cation-discriminating ⁇ diaphragms between said chambers for establishing a selective path for ions from one chamber into an adjoining ichamber under the inuence of an electrical potential, said diaphragms being arranged in substantially vertical position and in alternating sequence with respect to traverse from one terminal chamber through the intermediate chambers to the other terminal cham-.
  • An apparatus for increasing and decreasing the ion content of liquids comprising means forming a plurality of chambers, not less than ve, the chambers being arranged in line; aniondiscriminating and cation-discriminating diaphragms between said chambers for establishing a selective path for ions from one chamber into an adjoining chamber under the inuence of an electrical potential, said diaphragms being arranged in substantially vertical position and in alternating sequence with respect to traverse from one terminal chamber through the intermediate chambers to the other terminal chamber; an electrode in each of the terminal chambers, one electrode to serve as an anode, the other electrode to serve as a cathode; means including inlet ports near the bottom of certain alternate chambers for supplying raw liquid to be deionized into said alternate chambers; means forming a common space above, and in communication with, all of said intermediate chambers, said common space lying above the upper ends of said diaphragms for collecting liquid from said alternate chambers rising into said common space by reason of flow and reduced
  • An apparatus for increasing and decreasing the ion content of liquids comprising means forming a plurality of chambers, not less than five, the chambers being arranged-in line; aniondiscriminating and cation-discriminating diaphragms between said chambers for establishing a selective path for ions from one chamber into an adjoining chamber under the iniiuence of an electrical potential, said diaphragms being arranged in substantially vertical position and in alternating sequence with respect to traverse from one terminal chamber through the intermediate chambers to the other terminal chamber; an electrode in each of the terminal chambers, one elecl trode to serve as an anode, the other electrode to serve as a cathode; means including inlet ⁇ ports near the bottom of certain alternate chambers for supplying raw liquid to be deionized into said alternate chambers; means forming a common space above, and in communication with, all of said intermediate chambers, said common space lying above the upper ends of said diaphragms for collecting liquid from said alternate chambers rising

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Health & Medical Sciences (AREA)
  • Urology & Nephrology (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
US175127A 1950-07-21 1950-07-21 Electrodialytic apparatus Expired - Lifetime US2689826A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
BE504756D BE504756A (hu) 1950-07-21
NL96481D NL96481C (hu) 1950-07-21
NL7810787.A NL162669C (nl) 1950-07-21 Werkwijze voor de bereiding van een fluorpolymeer.
US175127A US2689826A (en) 1950-07-21 1950-07-21 Electrodialytic apparatus
GB16533/51A GB694223A (en) 1950-07-21 1951-07-12 Apparatus for modifying the chemical composition of substances by ion transfer
CH300582D CH300582A (de) 1950-07-21 1951-07-13 Verfahren zur Elektrodialyse und Vorrichtung zur Durchführung des Verfahrens.
FR1045890D FR1045890A (fr) 1950-07-21 1951-07-16 Modification de la composition chimique de substances
DEK10696A DE931944C (de) 1950-07-21 1951-07-21 Verfahren zum kontinuierlichen elektrodialytischen Trennen von Loesungen in Mehrzellenapparaten und Vorrichtung zum Durchfuehren des Verfahrens

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US175127A US2689826A (en) 1950-07-21 1950-07-21 Electrodialytic apparatus

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US2689826A true US2689826A (en) 1954-09-21

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US175127A Expired - Lifetime US2689826A (en) 1950-07-21 1950-07-21 Electrodialytic apparatus

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US (1) US2689826A (hu)
BE (1) BE504756A (hu)
CH (1) CH300582A (hu)
DE (1) DE931944C (hu)
FR (1) FR1045890A (hu)
GB (1) GB694223A (hu)
NL (2) NL162669C (hu)

Cited By (30)

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US2708658A (en) * 1952-07-18 1955-05-17 Ionics Apparatus for removing electrolytes from solutions
US2777814A (en) * 1954-12-02 1957-01-15 Gen Electric Water heating and demineralizing apparatus
US2794777A (en) * 1956-08-27 1957-06-04 Clayton Manufacturing Co Electrolytic deionization
US2799638A (en) * 1954-08-17 1957-07-16 Dorr Oliver Inc Purification of solutions by ionic transfer
US2828257A (en) * 1954-02-17 1958-03-25 Robert E Briggs Multi-compartment electrolytic cell
US2897130A (en) * 1956-01-18 1959-07-28 Tno Apparatus for electrodialyzing liquids
US2987472A (en) * 1955-09-22 1961-06-06 Kollsman Paul Method of and apparatus for increasing and decreasing the ion content of fluids by ion transfer
US3030287A (en) * 1957-10-26 1962-04-17 Benckiser Gmbh Joh A Method for the removal of small quantities of strong electrolytes from solutions of weak electrolytes
US3164540A (en) * 1961-02-17 1965-01-05 American Mach & Foundry Electrodialyzer
US3296112A (en) * 1957-07-16 1967-01-03 Kollsman Paul Method of modifying the chemical composition of substances by ion transfer
US3323653A (en) * 1963-03-20 1967-06-06 Robert E Lacey Multimembrane apparatus for demineralizing liquids
US3323652A (en) * 1963-03-20 1967-06-06 Everett L Huffman Multimembrane apparatus for demineralizing liquids
US4196069A (en) * 1978-05-19 1980-04-01 Hooker Chemicals & Plastics Corp. Means for distributing electrolyte into electrolytic cells
US4415424A (en) * 1981-01-16 1983-11-15 Creusot-Loire Device for supply and discharge of liquid electrolyte for an electrolyzer of filterpress type
US5292422A (en) * 1992-09-15 1994-03-08 Ip Holding Company Modules for electrodeionization apparatus
US5308466A (en) * 1990-12-17 1994-05-03 Ip Holding Company Electrodeionization apparatus
WO1994014538A1 (de) * 1992-12-24 1994-07-07 Grünbeck Wasseraufbereitung GmbH Verfahren und anlage zur behandlung einer wässrigen lösung durch ionenaustausch
US5558753A (en) * 1994-05-20 1996-09-24 U.S. Filter/Ionpure, Inc. Polarity reversal and double reversal electrodeionization apparatus and method
EP0803474A2 (en) 1996-04-26 1997-10-29 Millipore Corporation Electrodeionization apparatus and process for purifying a liquid
US20030146090A1 (en) * 2002-02-02 2003-08-07 Mack Bernard R. EDI and related stacks and method and apparatus for preparing such
US20030173222A1 (en) * 2002-03-13 2003-09-18 Kannan Srinivasan Water purifier and method
US20040027100A1 (en) * 2002-08-07 2004-02-12 Zhejiang Omex Environmental Engineering Ltd. EDI module with stabilizing DC current
US20040055887A1 (en) * 2002-07-30 2004-03-25 Xiang Li EDI device with composite electrode
US20040112752A1 (en) * 2002-07-30 2004-06-17 Xiang Li EDI device with resin seepage-proof inserts
US20040154916A1 (en) * 2002-07-30 2004-08-12 Zhejiang Omex Environmental Engineering Ltd. Dilute support frame for an EDI device
US20060157422A1 (en) * 2003-11-13 2006-07-20 Evgeniya Freydina Water treatment system and method
US8377279B2 (en) 2003-11-13 2013-02-19 Siemens Industry, Inc. Water treatment system and method
US8658043B2 (en) 2003-11-13 2014-02-25 Siemens Water Technologies Llc Water treatment system and method
US9011660B2 (en) 2007-11-30 2015-04-21 Evoqua Water Technologies Llc Systems and methods for water treatment
US9023185B2 (en) 2006-06-22 2015-05-05 Evoqua Water Technologies Llc Low scale potential water treatment

Families Citing this family (15)

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Publication number Priority date Publication date Assignee Title
DE1183475B (de) * 1952-07-18 1964-12-17 Ionics Verfahren zur UEberfuehrung von Elektrolyten aus einer waessrigen Loesung in eine andere durch Elektrodialyse
NL82530C (hu) * 1952-10-17
DE977065C (de) * 1953-01-23 1965-01-07 Permutit Ag Verfahren zur elektrodialytischen Veraenderung des Elektrolytgehaltes von Loesungen unter Verwendung von Elektrodialysezellen, die durch aufeinanderfolgende Kationen- und Anionenaustauschermembranen in mehrere Kammern unterteilt sind
US2802344A (en) * 1953-07-08 1957-08-13 Eureka Williams Corp Electrodialysis of solutions in absorption refrigeration
DE1101364B (de) * 1953-10-05 1961-03-09 Max Planck Gesellschaft Vorrichtung zur kontinuierlichen Elektrodialyse
US2815320A (en) * 1953-10-23 1957-12-03 Kollsman Paul Method of and apparatus for treating ionic fluids by dialysis
US2758965A (en) * 1954-01-20 1956-08-14 Borden Co Electrodialysis of solutions
NL59498C (hu) * 1954-05-06
US3124522A (en) * 1955-03-22 1964-03-10 Electrodialysis processes and electro-dialysis cells
US2878178A (en) * 1955-04-15 1959-03-17 Bier Milan Continuous free-boundary flow electrophoresis
DE1095788B (de) * 1955-07-30 1960-12-29 South African Council For Scie Vielkammerelektrodialysevorrichtung
US2937126A (en) * 1957-08-13 1960-05-17 Ionics Electrodialysis demineralization
BE565776A (hu) * 1958-01-10
NL278428A (hu) * 1961-05-15 1900-01-01
JPS6058230A (ja) * 1983-09-09 1985-04-04 Babcock Hitachi Kk 排煙脱硫方法および装置

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US1986920A (en) * 1932-06-28 1935-01-08 S M A Corp Electroosmotic process and apparatus
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US1326106A (en) * 1919-12-23 Schaet fur elektro-osmose m
US1546908A (en) * 1925-01-22 1925-07-21 Vincent A Lapenta Electroendosmosis method and apparatus
US1986920A (en) * 1932-06-28 1935-01-08 S M A Corp Electroosmotic process and apparatus
US2411238A (en) * 1943-07-08 1946-11-19 Syivania Ind Corp Process and apparatus for dialyzing solutions
US2636852A (en) * 1949-07-09 1953-04-28 Ionics Method of electrodialyzing aqueous solutions and apparatus therefor

Cited By (42)

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US2828257A (en) * 1954-02-17 1958-03-25 Robert E Briggs Multi-compartment electrolytic cell
US2799638A (en) * 1954-08-17 1957-07-16 Dorr Oliver Inc Purification of solutions by ionic transfer
US2777814A (en) * 1954-12-02 1957-01-15 Gen Electric Water heating and demineralizing apparatus
US2987472A (en) * 1955-09-22 1961-06-06 Kollsman Paul Method of and apparatus for increasing and decreasing the ion content of fluids by ion transfer
US2897130A (en) * 1956-01-18 1959-07-28 Tno Apparatus for electrodialyzing liquids
US2794777A (en) * 1956-08-27 1957-06-04 Clayton Manufacturing Co Electrolytic deionization
US3296112A (en) * 1957-07-16 1967-01-03 Kollsman Paul Method of modifying the chemical composition of substances by ion transfer
US3030287A (en) * 1957-10-26 1962-04-17 Benckiser Gmbh Joh A Method for the removal of small quantities of strong electrolytes from solutions of weak electrolytes
US3164540A (en) * 1961-02-17 1965-01-05 American Mach & Foundry Electrodialyzer
US3323653A (en) * 1963-03-20 1967-06-06 Robert E Lacey Multimembrane apparatus for demineralizing liquids
US3323652A (en) * 1963-03-20 1967-06-06 Everett L Huffman Multimembrane apparatus for demineralizing liquids
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US4415424A (en) * 1981-01-16 1983-11-15 Creusot-Loire Device for supply and discharge of liquid electrolyte for an electrolyzer of filterpress type
US5308466A (en) * 1990-12-17 1994-05-03 Ip Holding Company Electrodeionization apparatus
US5316637A (en) * 1990-12-17 1994-05-31 Ip Holding Company Electrodeionization apparatus
US5292422A (en) * 1992-09-15 1994-03-08 Ip Holding Company Modules for electrodeionization apparatus
WO1994014538A1 (de) * 1992-12-24 1994-07-07 Grünbeck Wasseraufbereitung GmbH Verfahren und anlage zur behandlung einer wässrigen lösung durch ionenaustausch
US5736023A (en) * 1994-05-20 1998-04-07 U.S. Filter/Ionpure, Inc. Polarity reversal and double reversal electrodeionization apparatus and method
US5558753A (en) * 1994-05-20 1996-09-24 U.S. Filter/Ionpure, Inc. Polarity reversal and double reversal electrodeionization apparatus and method
EP0803474A2 (en) 1996-04-26 1997-10-29 Millipore Corporation Electrodeionization apparatus and process for purifying a liquid
US20030146090A1 (en) * 2002-02-02 2003-08-07 Mack Bernard R. EDI and related stacks and method and apparatus for preparing such
US7094325B2 (en) 2002-02-02 2006-08-22 Ionics, Incorporated EDI and related stacks and method and apparatus for preparing such
US6808608B2 (en) 2002-03-13 2004-10-26 Dionex Corporation Water purifier and method
US20030173222A1 (en) * 2002-03-13 2003-09-18 Kannan Srinivasan Water purifier and method
US20040112752A1 (en) * 2002-07-30 2004-06-17 Xiang Li EDI device with resin seepage-proof inserts
US20040154916A1 (en) * 2002-07-30 2004-08-12 Zhejiang Omex Environmental Engineering Ltd. Dilute support frame for an EDI device
US7029563B2 (en) 2002-07-30 2006-04-18 Zhejiang Omex Environmental Engineering Ltd. EDI device with composite electrode
US20040055887A1 (en) * 2002-07-30 2004-03-25 Xiang Li EDI device with composite electrode
US7097753B2 (en) 2002-07-30 2006-08-29 Zhejiang Omex Environmental Engineering Ltd. Dilute support frame for an EDI device
US7097752B2 (en) 2002-07-30 2006-08-29 Zhejiang Omex Environmental Engineering, Ltd. EDI device with resin seepage-proof inserts
US7261802B2 (en) 2002-08-07 2007-08-28 Zhejiang Omex Enviromental Engineering Ltd. EDI module with stabilizing DC current
US20040027100A1 (en) * 2002-08-07 2004-02-12 Zhejiang Omex Environmental Engineering Ltd. EDI module with stabilizing DC current
US20060157422A1 (en) * 2003-11-13 2006-07-20 Evgeniya Freydina Water treatment system and method
US8377279B2 (en) 2003-11-13 2013-02-19 Siemens Industry, Inc. Water treatment system and method
US8658043B2 (en) 2003-11-13 2014-02-25 Siemens Water Technologies Llc Water treatment system and method
US8864971B2 (en) 2003-11-13 2014-10-21 Evoqua Water Technologies Llc Water treatment system and method
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US9586842B2 (en) 2006-06-22 2017-03-07 Evoqua Water Technologies Llc Low scale potential water treatment
US9011660B2 (en) 2007-11-30 2015-04-21 Evoqua Water Technologies Llc Systems and methods for water treatment
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Also Published As

Publication number Publication date
GB694223A (en) 1953-07-15
NL162669C (nl)
BE504756A (hu)
NL96481C (hu)
CH300582A (de) 1954-08-15
DE931944C (de) 1955-08-22
FR1045890A (fr) 1953-12-01

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