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US2848403A - Process for electrodialyzing liquids - Google Patents

Process for electrodialyzing liquids Download PDF

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Publication number
US2848403A
US2848403A US428072A US42807254A US2848403A US 2848403 A US2848403 A US 2848403A US 428072 A US428072 A US 428072A US 42807254 A US42807254 A US 42807254A US 2848403 A US2848403 A US 2848403A
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chambers
stream
diluting
solution
concentrating
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US428072A
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English (en)
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Norman W Rosenberg
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Veolia WTS Systems USA Inc
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Ionics Inc
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Priority to NL104346D priority Critical patent/NL104346C/xx
Priority to NL59498D priority patent/NL59498C/xx
Application filed by Ionics Inc filed Critical Ionics Inc
Priority to US428072A priority patent/US2848403A/en
Priority to GB11970/55A priority patent/GB792623A/en
Priority to DEI10172A priority patent/DE1150656B/de
Priority to FR1138740D priority patent/FR1138740A/fr
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Publication of US2848403A publication Critical patent/US2848403A/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
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING OR TREATMENT THEREOF
    • A23C9/00—Milk preparations; Milk powder or milk powder preparations
    • A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
    • A23C9/144—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by electrical means, e.g. electrodialysis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
    • B23F—MAKING GEARS OR TOOTHED RACKS
    • B23F23/00—Accessories or equipment combined with or arranged in, or specially designed to form part of, gear-cutting machines
    • B23F23/08—Index mechanisms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
    • B23Q—DETAILS, COMPONENTS, OR ACCESSORIES FOR MACHINE TOOLS, e.g. ARRANGEMENTS FOR COPYING OR CONTROLLING; MACHINE TOOLS IN GENERAL CHARACTERISED BY THE CONSTRUCTION OF PARTICULAR DETAILS OR COMPONENTS; COMBINATIONS OR ASSOCIATIONS OF METAL-WORKING MACHINES, NOT DIRECTED TO A PARTICULAR RESULT
    • B23Q16/00—Equipment for precise positioning of tool or work into particular locations not otherwise provided for
    • B23Q16/02—Indexing equipment
    • B23Q16/04—Indexing equipment having intermediate members, e.g. pawls, for locking the relatively movable parts in the indexed position
    • B23Q16/06—Rotary indexing
    • B23Q16/065—Rotary indexing with a continuous drive
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B20/00—Purification of sugar juices
    • C13B20/18—Purification of sugar juices by electrical means
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/4604—Treatment of water, waste water, or sewage by electrochemical methods for desalination of seawater or brackish water
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis

Definitions

  • the present invention relates to improved method employing electrical energy to effect migration of electrolytes from one solution to another across ion selectively permeable membranes.
  • the invention utilizes a membrane demineralizer having a set of diluting chambers (for a first electrolyte-containing solution) alternately disposed between a set of concentrating chambers (for a second such solution) and in addition at least two electrode chambers in which the current enters and leaves the demineralizer.
  • Washing chambers if so desired to minimize contamination from the products of the electrode chambers, may be interposed adjacent the cathode and anode chambers of the cell and their respective concentrating and diluting chambers and may be hydraulically independent or manifolded to diluting or concentrating streams.
  • the aforementioned chambers are separated by barriers of intrinsically electrolytically-conductive hydraulically-impermeable ionselective permeable membranes through which dissolved electrolyte is transferred from the diluting chambers to the concentrating chambers by means of a direct electric current in series across the membranes and the chambers defined between them.
  • Such apparatus are more fully described in a copending application to W. E. Katz and N. W. Rosenberg bearing Serial No. 300,302 filed July 22, 1952. It will be apparent that such a membrane demineralizer may consist of an extremely expanded arrangement wherein a great number of concentrating and diluting chambers are employed, for example, 100 or more of each, but nevertheless having two end chambers containing the cathode and anode.
  • the spacers can be of different thickness so that at equal pressures the flow rates and velocities are not necessarily the same in both diluting and concentrating streams. It is easily seen that the hydraulic pressure required to cause solution to flow at the required rate in such a spacer is much increased over that required for a spacer having no such tortuosity.
  • demineralizers having effective spacer tortuosity that relatively high hydraulic pressures are required to achieve the necessary velocity for the passage of the required current, for example, 15 or 20 or more lbs. per square inch. It will be obvious that in the absence of solution pressure through the concentrating chambers of such a demineralizer, the diluting chamber pressure will be applied across the membrane bounding said diluting chamber. It is well known that suitable demineralizers of this type should use as thin membranes and as thin spacers as are practically attainable or operable, in order to minimize ohmic power loss. When a thin membrane, for example, a material of between 0.1 and 1 mm.
  • the spacer forming the concentrating chamber be substantially similar in tortuosity but not necessarily of the same thickness as that of the diluting chamber and that means he provided to flow the concentrating solution in parallel to the diluting solution and at a velocity sufficient so that the hydraulic pressure through the concentrating chamber shall vary in similar fashion to that in the diluting and thus everywhere oppose with an equal pressure that pressure resulting from the flow of solution in the diluting chambers. While my present preferred range of flow pressures in the unit is from 5 to p. s. i., a pressure range of 2 to 50 p. s. i. is also feasible.
  • Substantially similar configurations of spacers in this sense are defined as configurations in which the pressure drop across a membrane at any point thereof can either be substantially equalized or can represent only a small fraction, such as less than 20% of the manifold-to-manifold pressure drop, when the inlet manifold pressures of both (or all streams) are equalized and when the outlet manifold pressures of both (or all) streams are equalized.
  • operation of this invention yielded an unexpected result; i. e. that the effects of back diffusion are entirely unimportant in operating the present unit at high current densities and that a far more important consideration is the maintenance of equalized pressures across all membranes to prevent deformation and back leakage.
  • a demi'neralizer may be made by utilizing a single expanded membrane demineralizer having many pairs of diluting and concentrating chambers and a single pair of electrodes by causing the solution which is to be diluted to recirculate, preferably from a reservoir, through the diluting chambers of the demineralizer at a velocity sufficiently high to permit the required electrical current density to be applied without polarization, and periodically discharging the contents of the reservoir and diluting chambers automatically when they have obtained the required extent of demineralization.
  • a continuous product can be obtained by adjusting a bleed from the dilute reservoir at a lower rate than the recirculation rate through the unit.
  • Recirculation is 'anideal'method of permitting such high current densities to be utilized in a unit containing deformable membranes. Especially,'it offers a highly versatile method of varying the concentrate and dilute feed rates to theapparatus as a whole over very wide ranges relative to one another without significantly affecting the hydraulic pressure balance within the chambers of the unit.
  • the concentrating solution be recycled, preferably through a reservoir tank to permit its repeated use in the concentrating chambers. This stream may be periodically or continuously charged and recharged as described above for the diluting solution.
  • efliuents from the electrode chambers are collected in a common reservoir which combined effluent is then recycled to the electrode chambers, after the electrode gases are disengaged. I simultaneously bleed in required quantities of feed solution and permit the overflow of a similar volume of waste from the electrode reservoir.
  • I bleed in quantities of acid suflicient to insure that the solution leaving the cathode chamber I will have a pH of less than 5 and preferably not less than 1.
  • a suitable acid maybe HCl acid although sulfuric acid and acid sodium sulfate may be used if the feed solution to the recycling electrode stream does not contain such a high concentration of calcium that the introduction of sulfate ion would cause precipitation of CaSO
  • the concentrating and electrode feed streams for obvious reasons should not be the industrial solution to be demineralized.
  • an appropriate feed to the concentrate stream is a tap water, and the feed to the electrode stream could be a dilute sodium acid sulfate solution or sodium sulfate solution.
  • Figure 1 is a schematical representation of the complete system which includes a concentrating and diluting cell unit and the circulatory system in connection therewith.
  • Figure 2 is a perspective view of the elements of a pair of concentrating and diluting chambers in exploded relationship.
  • a concentrating and diluting cell unit U shown schematically in Figure 1 consists, in general, of a series of parallel alternating diluting and concentrating chambers, and 13 respectively, divided by alternating membranes selectively permeable to cations K and anions A, defining end electrode chambers S and 9a with cathode and anode electrodes 7 and 5 attached thereto on one side thereof and a pair of washing chambers 11 adjacent thereto on the other side.
  • a direct current for passage through the cell is obtained through leads 1 and 3 from a suit-able source (not shown).
  • the membranes A and K are electrically conductive, as well as selectively permeable to anions and cations, respectively. Suitable membranes for this purpose are described in the copending application to W. E. Katz and Norman W.
  • the washing and electrode chambers do not function directly in the concentrating and diluting process, but are provided to minimize contamination of the solutions in the concentrating and diluting chambers by the products of electrolvsis.
  • the washing chambers maybe omitted if desired.
  • the concentrating, diluting, washing, and end electrode chambers are fed in parallel with the washing chambers being fed and removed in the concentrate stream.
  • the washing chambers could also be hydraulically independent if desired.
  • the anode and cathode streams are fed separately in parallel and removed in a single stream.
  • the anode and cathode streams could also be removed separately from the unit U into separate electrode reservoir tanks if desired.
  • the circulatory systems for the three streams employed in the system of the disclosed embodiment of the invention are designated broadly by D (diluting stream), C (concentrating), and E (electrode stream). These are separate streams which originate from their sources 2, 50 and 100, into feed'tanks 4, 52 and 102, respectively. They enter and leave the electrodialysis cell unit U through conduits 38 and 40; 80 and 82; and 128 and 130, respectively.
  • the diluting stream D originates from a source 2 supplying feed tank 4, is pumped by centrifugal pump 6 through filter 10 which has pressure gages 8 and 12 on both sides thereof to indicate the degree of exhaustion of said filter.
  • Feed valev 14 is normally kept in a closed position to prevent the raw feed stream from entering the recirculating diluting system but opened periodically to fill reservoir tank 18. This valve may be,
  • the batch of solution to be diluted in reservoir diluting tank 18 is pumped through conduit 44, by centrifugal pump 30, throttled through valve 32, and passed through flowrator 34. Its pressure is measured on pressure gage 36, and it then flows through main conduit'38 to the diluting chambers of the electrodialysis cell unit through main conduit 40, passes through conductance measuring cell 28 and normally open valve 20 (valve 22 being normally closed), returning to the diluting reservoir tank 18 for recirculation. cell 28 indicates satisfactory dilution has been achieved, valve 20 is closed and normally closed valve 22 is opened. The product steam leaving the unit is thus by-passed through conduit 46 into product tank 24 by means of pump 22, and diluting reservoir tank 18 empties through outlet 26 therefrom. When tank 18 is almost empty,
  • a float switch therein opens valve 14, allowing a fresh batch of raw solution to be diluted to enter the stream by pump 30. Because of its initial high con- When the conductance ductivity when the raw solution to be diluted enters conductance cell 28, valve 22 is normally closed and valve 20 is normally open. Diluting tank 18 then refills the raw solution to be diluted and when full, valve 11 is closed, cutting oif'further entry of raw solution to be diluted. The unit continues to demineralize this new batch in tank 18 until it is sufficiently pure agains initiating the cycle, This method of operation is. referred to hereinafter as batch circulation.
  • An alternative method of operating the diluting circuit is to adjust valve 14 to a partially open position thereby continuously feeding solution to be diluted through flowrator 16 and continuously withdrawing product at exit overflow 19 in which case valve 20 is continuously open, and valve 22, conduit 46, and product tank 24 are eliminated.
  • This method of operation is referred to as continuous circulation and removal of the diluting stream as opposed to the batch recirculation described in the preceding description, Note especially that the recirculation rate through fiowrator 34 and the feed rate through flowrator 16 are completely independent of one another and may be varied relative to one another.
  • the concentrating stream C originates from conduit 50 into concentrating stream feed tank 52 and is then pumped through centrifugal pump 54, through filter 58 which has pressure gages 56 and 60 on both sides thereof for determining the extent of exhaustion thereof.
  • the concentrating stream is then passed through partially open valve 62 and flowrator 64 which measures the feed rate of the concentrate feed stream.
  • the conductance cell 70 would indicate the highest permissible concentration and would signal the opening of valve 62. If this concentration were exceeded, the opening of valve 62 would introduce a quantity of solution to be concentrated at a lower concentration than that being removed through conduit 86. It is clear that these various instruments may either function automatically or be manually controlled.
  • a solution appropriate for use in the electrode stream e. g. sodium sulfate or any natural water such as sea water, is introduced through conduit 100 into electrode feed tank 102. From this tank it is pumped through centrifugal pump 104, through filter 108 which has pressure gages 106 and 110 at each end to indicate the degree of exhaustion of the filter, is then passed through partially open throttle valve 112, and through flowrator 114 where it is joined by the main recirculating electrode stream from electrode reservoir tank 118 through conduit 116.
  • a solution appropriate for use in the electrode stream e. g. sodium sulfate or any natural water such as sea water
  • the combined stream is then passed through centrifugal pump 120, throttle valve 122, fiowrator 124, its pressures measured on gage 126, and introduced into the electrodialysis unit U through main conduit 128, removed therefrom through return conduit 130 at which point it is returned to the electrode stream recirculating reservoir 118.
  • a continuous overflow from the electrode reservoir tank 118 is provided through conduit 132.
  • a small stream of acid may be added to electrode reservoir 118 from acid container 134 through throttle valve 136, and introduced into the recirculating stream through conduit 138 to maintain a pH of the electrode solution at such a value that precipitation will not occur in the electrode compartments. It is obvious that batch operation of this electrode stream could also be untilized.
  • Figure 1 shows three separate streams 38, 80, and 128, feed to electrodialysis unitU and threeseparate streams 40, 82 and 130 leaving the unit.
  • Alternating individual chambers 13 and 15 are shown bounded by cation and anion permeable membranes K and A wherein entrys are affected at points 25 and 29 and the solution leaving individual chambers at points 27 and 31 respectively (see Figure 2).
  • the rate of flow through conduit equal the rate of flow through conduit 38 and therefore the pressure drop encountered between 25 and 27 will not necessarily equal the pressure drop occurring between 29 and 31.
  • recirculation rates in the system described in Figure 1 can be chosen completely independently of the desired feed rates to the dilute stream, concentratestream, and the electrode stream, which are determined respectively by the setting of valves 14, 62, and 112 or by the set points indicated on conductance cells 28 and 70. In other words, recirculation rates are chosen to maintain balanced forces across all membranes whereas feed rates are chosen in accordance with the requirements of the streams to be processed.
  • Figure 2 shows an exploded perspective view of a pair of concentrating and diluting chambers of the electrodialysis cell unit (U) of Figure 1, like numerals for like parts being employed.
  • Numerals 21 and 23 indicate one form of baffle employed to effect a tortuous path for the flow streams in the concentrating and diluting chambers. It is apparent that the multiple chambers could very well be expanded into several hundred of such chambers.
  • the embodiment of the recirculation system of Figure 1 shows the diluting stream to be batch recirculation while both the concentrating and electrode streams are continuous recirculation systems, but it should be appreciated that many varied combinations of the diluting and concentrating streams in conjunction with the electrode stream is contemplated herein as noted above.
  • EXAMPLE 1SEA WATER In a unit constructed as shown in Figure 1 (with broken line conduits 42 and 84 in operation), the following performance was obtained using an 80 cell pair demineralizer stack with .10 cm. thick spacers except at electrodes which were .32 cm. thick.
  • Raw sea water at 40 F. was contained in tank 4, which had a capacity of 500 gallons.
  • Valve 14 is normally in the closed position.
  • the diluting stream was recirculated from the ten-gallon reservoir tank 18 through the electrodialysis unit (U) and by means of valve 32 was adjusted to a flow of 300 G. P. H. measured on flowrator 34 at a pressure read on gage 36 of 12 p. s. i., returning to the diluting reservoir tank 18.
  • Recycle of the concentrating stream from S-gallon tank 68 was at a 300 G. P. H. flow and 12 p. s. i. pressure, equal to the pressure on the dilute recirculating stream.
  • Raw sea water fed to the concentrate stream and measured through fiow rator 64 was adjusted by valve 62 to 20 G. P. H. when the pressure read on gage 12 was 15 p. s. i.
  • Recycle of the electrode stream was 25 G. P. H. through flowrator 124 at a pressure reading on gage 126 of 12 p. s. i., equal to the pressure on the dilute recirculating stream.
  • Raw sea water fed to the concentrate stream and measured through fiow rator 64 was adjusted by valve 62 to 20 G. P. H. when the pressure read on gage 12 was 15 p. s. i.
  • Recycle of the electrode stream was 25 G. P. H. through flowrator 124 at a pressure reading on gage 126 of 12 p. s
  • the initial current was 20 amperes.
  • the electrical circuit controlled by the conductance cell 28 caused valve 20 to close and valve 22 to open, allowing tank 18 to empty into tank 24.
  • the electrical circuit controlled by the float switch therein caused valve 14 to open, and a stream of raw water entered tank 18.
  • the raw water passed through the unit it forced the purified water ahead of it from the unit into product tank 24.
  • valve 20 opened and valve 22 closed, and when tank 18 filled to the 10-gallon level, the float switch closed valve 14, allowing a new cycle to begin automatically.
  • the unit described above produced 15 gallons per hour of 4 500 p. p. m. demineralized water at a D. C. power con sumption of 1 kilowatt.
  • EXAMPLE 2BRACKISH WATER In the same unit used in Example 1, the tank 4 was filled with a brackish water containing 5000 p. p. m. of
  • EXAMPLE 3--INDUSTRIAL SOLUTIONS Cane juice of 150 G. P. H. at a pressure of 10 p. s. i. and at a temperature of 60 C.
  • Tap water was fed to the concentrate stream which stream was recycled at a flow of 300 G. P. H. to obtain a pressure of 10 p. s. i.
  • Recycle of a .1 N NaHSO stream was 25 G. P. H. through anode and through cathode chambers at a pressure of 10 p. s. i.
  • Reduction of the conductivity of the raw sugar to 10% of its original value was accomplished at 65 volts D. C. in a period of 240 minutes when the batch volume at the start of the run was 10 gallons.
  • the starting current was 5 amperes and the final current 1.2 amperes, thus indicating a production rate of 2.5 gallons per hour at an average power demand of 0.2 kw., with the ionizable ash content reduced as measured by conductance.
  • the presence of ionizable ash prevents crystallization of sucrose from the cane juice to the extent of about 1 pound of sugar retained per pound of such ash.
  • EXAMPLE 4--INDUSTRIAL SOLUTIONS Glycerine The unit described in Example 3 was operated in an identical manner on a glycerine process stream containing 30% glycerine and 3% of ionizable solids, largely NaCl.
  • the usefulness of removing the ash from glycerine is that only water need be removed to produce a glycerine suitable for industrial use. If, on the other hand, the salt is not removed the glycerine must be distilled away from the salt to produce a commercially useful product, the latter being an expensive process. Removal of the entire salt content by the usual granular ion exchange resin beds is not feasible because of the large quantity of salt present. It was found that a recirculating flow of G. P. H.
  • valves, pumps, flowrators, conductance cells, pressure gages, and safety devices including pressure points, timing switches, etc., employed in the system are well known, per se, but the assembly and incorporation of the same in conjunction with the novel present system wherein sensing and automatically controlling the operation of membrane demineralizing of liquids may be obtained are novel and may be valuable features to the commercial success of the present invention.
  • the method of modifying the concentration-of an electrolyte solution comprising passing a first feed stream through diluting chambers of an electrodialysis unit having a plurality of concentrating and diluting chambers defined between alternate anion permeable membranes and cation permeable membranes said membranes having a thickness between about 0.1 mm. and about 1 mm. and.
  • said diluting chambers having a thickness of about-0.5 mm. to about 2 mm, passing a second feed stream through the alternate concentrating chambers, passing a direct current in series across the alternating chambers and membranes, and passing the two feed streams in parallel concurrent flow through said chambers at flow rates controlled to maintain substantially equal hydraulic pressures on opposite faces of the membranes at any point thereof to prevent undue stresses or bowing of said membranes.
  • the first experiments 2 The methodof modifying the concentration; of an electrolyte solution comprising ,passing a first feed stream through diluting chambers of an electrodialysis unit having a plurality of concentrating and diluting chambers defined between alternate anion permeable membranes and cation permeable membranes, passing a second feed stream through the alternate concentrating chambers, passing a direct current in series across the alternating chambers and membranes said membranes having a thickness between about 0.1 mm. andabout 1 mm. and said diluting chambers having a thickness of about 0.5 mm. to about 2 mm., passing the two feed streams in parallel concurrent flow through said chambers, and at least partially recirculating at least one of said feed streams at a fiow rate to. maintain.substantially equal hydraulic pressures on opposite faces ofthe membranes at any point thereof to prevent undue stresses or bowing .of said membranes.
  • the method .of modifying the concentration .of .an electrolytesolution comprising passing a first feed stream through diluting chambers of an electrodialysis unit having a plurality of concentrating and diluting chambers defined between alternate anion permeable membranes and cation permeable membranes, said membranes having a thickness between about 0.1 mm. and about 1 mm. and said diluting chambers having a thickness of about 0.5 mm.
  • the recirculating stream is the dilute stream and consists of continuously recirculatingv all ,of the stream and periodically removing and replacing at least part of said stream with raw feed solution.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Mechanical Engineering (AREA)
  • Urology & Nephrology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Biochemistry (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
US428072A 1954-05-06 1954-05-06 Process for electrodialyzing liquids Expired - Lifetime US2848403A (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
NL104346D NL104346C (de) 1954-05-06
NL59498D NL59498C (de) 1954-05-06
US428072A US2848403A (en) 1954-05-06 1954-05-06 Process for electrodialyzing liquids
GB11970/55A GB792623A (en) 1954-05-06 1955-04-26 Process and apparatus for electrodialyzing liquids
DEI10172A DE1150656B (de) 1954-05-06 1955-05-05 Kontinuierliche Vielkammerelektrodialyse waessriger Elektrolytloesungen unter Benutzung ionenselektiver Membranen
FR1138740D FR1138740A (fr) 1954-05-06 1955-05-06 Procédé d'électrodialyse et appareil pour sa mise en oeuvre

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US428072A US2848403A (en) 1954-05-06 1954-05-06 Process for electrodialyzing liquids

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DE (1) DE1150656B (de)
FR (1) FR1138740A (de)
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NL (2) NL59498C (de)

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US2990361A (en) * 1957-11-25 1961-06-27 Permutit Co Ltd Electrodialytic cells
US3086928A (en) * 1958-08-09 1963-04-23 Benckiser Gmbh Joh A Process of producing citric acid
US3111472A (en) * 1957-08-24 1963-11-19 Zaidan Hojin Noguchi Kenkyu Jo Process of carrying out electrochemically electrolysis
US3179583A (en) * 1960-07-26 1965-04-20 American Mach & Foundry Fluid treatment
US3223606A (en) * 1959-05-22 1965-12-14 American Mach & Foundry Electrodialysis device and method of operation
US3228867A (en) * 1959-05-22 1966-01-11 American Mach & Foundry Electrodialysis device
US3296112A (en) * 1957-07-16 1967-01-03 Kollsman Paul Method of modifying the chemical composition of substances by ion transfer
US3657106A (en) * 1969-06-05 1972-04-18 American Bioculture Electro-osmosis system
US3674669A (en) * 1970-04-01 1972-07-04 Rai Res Corp Concentration of electrolyte from dilute washings by electrodialysis in a closed system
US3676335A (en) * 1967-06-08 1972-07-11 Southern Res Inst Process for effecting changes in solution concentrations
JPS5011867B1 (de) * 1970-12-22 1975-05-07
FR2492269A2 (fr) * 1980-01-10 1982-04-23 Ionics Appareil d'electrodialyse et procede de fractionnement de melanges de proteines
JPS57204003U (de) * 1981-06-22 1982-12-25
US4802965A (en) * 1984-12-21 1989-02-07 Basf Aktiengesellschaft Concentrating aqueous solutions of organic compounds which contain salts, with simultaneous reduction of the salt content
US20050031774A1 (en) * 2000-11-30 2005-02-10 Kraft Foods Holdings, Inc. Method of deflavoring soy-derived materials using electrodialysis
US20050186311A1 (en) * 2004-02-23 2005-08-25 Loh Jimbay P. Method for acidifying and preserving food compositions using electrodialyzed compositions
US20050186312A1 (en) * 2004-02-23 2005-08-25 Kraft Foods Holdings, Inc. Shelf-stable foodstuffs and methods for their preparation
US20050183955A1 (en) * 2004-02-23 2005-08-25 Crowley Colin P. Electrodialyzed compositions and method of treating aqueous solutions using elecrtrodialysis
US20050220969A1 (en) * 2004-02-23 2005-10-06 Kraft Foods Holdings, Inc. Shelf-stable cold-processed food compositions and methods for their preparation
US20050276904A1 (en) * 2003-10-29 2005-12-15 Kraft Foods Holdings, Inc. Method of deflavoring whey protein using membrane electrodialysis
US20060024413A1 (en) * 2004-02-23 2006-02-02 Colin Crowley Preparation of pumpable, edible composition using electrodialysis
US7887867B2 (en) 2004-02-23 2011-02-15 Kraft Foods Global Brands Llc Stabilized non-sour dairy base materials and methods for preparation
CN104562169A (zh) * 2013-10-22 2015-04-29 镇江胡氏光电科技有限公司 一种电镀液回用的装置
US11655166B2 (en) * 2017-05-08 2023-05-23 Evoqua Water Technologies Llc Water treatment of sodic, high salinity, or high sodium waters for agricultural application

Families Citing this family (1)

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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
US3296112A (en) * 1957-07-16 1967-01-03 Kollsman Paul Method of modifying the chemical composition of substances by ion transfer
US3111472A (en) * 1957-08-24 1963-11-19 Zaidan Hojin Noguchi Kenkyu Jo Process of carrying out electrochemically electrolysis
US2990361A (en) * 1957-11-25 1961-06-27 Permutit Co Ltd Electrodialytic cells
US3086928A (en) * 1958-08-09 1963-04-23 Benckiser Gmbh Joh A Process of producing citric acid
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US3228867A (en) * 1959-05-22 1966-01-11 American Mach & Foundry Electrodialysis device
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US3676335A (en) * 1967-06-08 1972-07-11 Southern Res Inst Process for effecting changes in solution concentrations
US3657106A (en) * 1969-06-05 1972-04-18 American Bioculture Electro-osmosis system
US3674669A (en) * 1970-04-01 1972-07-04 Rai Res Corp Concentration of electrolyte from dilute washings by electrodialysis in a closed system
JPS5011867B1 (de) * 1970-12-22 1975-05-07
FR2492269A2 (fr) * 1980-01-10 1982-04-23 Ionics Appareil d'electrodialyse et procede de fractionnement de melanges de proteines
JPS57204003U (de) * 1981-06-22 1982-12-25
US4802965A (en) * 1984-12-21 1989-02-07 Basf Aktiengesellschaft Concentrating aqueous solutions of organic compounds which contain salts, with simultaneous reduction of the salt content
US20050031774A1 (en) * 2000-11-30 2005-02-10 Kraft Foods Holdings, Inc. Method of deflavoring soy-derived materials using electrodialysis
US7175869B2 (en) 2000-11-30 2007-02-13 Kraft Foods Holdings, Inc. Method of deflavoring soy-derived materials using electrodialysis
US20050276904A1 (en) * 2003-10-29 2005-12-15 Kraft Foods Holdings, Inc. Method of deflavoring whey protein using membrane electrodialysis
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
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
US20050183955A1 (en) * 2004-02-23 2005-08-25 Crowley Colin P. Electrodialyzed compositions and method of treating aqueous solutions using elecrtrodialysis
US20050186312A1 (en) * 2004-02-23 2005-08-25 Kraft Foods Holdings, Inc. Shelf-stable foodstuffs and methods for their preparation
US7887867B2 (en) 2004-02-23 2011-02-15 Kraft Foods Global Brands Llc Stabilized non-sour dairy base materials and methods for preparation
CN104562169A (zh) * 2013-10-22 2015-04-29 镇江胡氏光电科技有限公司 一种电镀液回用的装置
US11655166B2 (en) * 2017-05-08 2023-05-23 Evoqua Water Technologies Llc Water treatment of sodic, high salinity, or high sodium waters for agricultural application

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GB792623A (en) 1958-04-02
NL59498C (de)
DE1150656B (de) 1963-06-27
FR1138740A (fr) 1957-06-19
NL104346C (de)

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