[go: up one dir, main page]

WO2009051612A1 - Appareil d'électrogénération et procédé de traitement de l'eau - Google Patents

Appareil d'électrogénération et procédé de traitement de l'eau Download PDF

Info

Publication number
WO2009051612A1
WO2009051612A1 PCT/US2008/005195 US2008005195W WO2009051612A1 WO 2009051612 A1 WO2009051612 A1 WO 2009051612A1 US 2008005195 W US2008005195 W US 2008005195W WO 2009051612 A1 WO2009051612 A1 WO 2009051612A1
Authority
WO
WIPO (PCT)
Prior art keywords
chamber
water
electrode
resin
cation exchange
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/US2008/005195
Other languages
English (en)
Inventor
David F. Rath
James E. Bolton
Christopher S. Putka
Lyle Edward Kirman
Christopher L. Hansen
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.)
Kinetico Inc
Original Assignee
Kinetico Inc
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
Priority claimed from PCT/US2007/022204 external-priority patent/WO2008048656A2/fr
Application filed by Kinetico Inc filed Critical Kinetico Inc
Priority to US12/445,848 priority Critical patent/US8337686B2/en
Publication of WO2009051612A1 publication Critical patent/WO2009051612A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/02—Column or bed processes
    • B01J47/06—Column or bed processes during which the ion-exchange material is subjected to a physical treatment, e.g. heat, electric current, irradiation or vibration
    • B01J47/08—Column or bed processes during which the ion-exchange material is subjected to a physical treatment, e.g. heat, electric current, irradiation or vibration subjected to a direct electric current
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
    • B01J49/30—Electrical regeneration
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • 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
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
    • 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
    • C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/46115—Electrolytic cell with membranes or diaphragms
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4612—Controlling or monitoring
    • C02F2201/46125—Electrical variables
    • C02F2201/4613—Inversing polarity
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4612—Controlling or monitoring
    • C02F2201/46125—Electrical variables
    • C02F2201/46135—Voltage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/043—Treatment of partial or bypass streams
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents

Definitions

  • the present invention relates generally to water treatment processes and in particular to a method and apparatus for removing cations and anions from water using ion exchange resins and membranes and using electricity to regenerate the resins.
  • a water softening apparatus such as that disclosed in U.S. Patent No. 3,891,552 is an example of a water treatment system that is used to remove certain "hard” ions in order to produce softened water.
  • the resin When substantially all of the ion sites in the water softening resin hold a "hard” ion, the resin must be regenerated.
  • a resin tank containing a water softening resin is utilized.
  • the "hard” water is passed through the resin tank where the water exchanges its "hard” ions of calcium, magnesium, etc. for "soft” sodium or potassium ions located at the resin ion exchange sites.
  • the resin is selected to have a greater affinity for the calcium and magnesium ions and thus releases the sodium or potassium ions in favor of the calcium and magnesium ions carried by the water.
  • a brine solution is flushed through the resin bed to regenerate the resin.
  • the high concentration of sodium or potassium ions in the brine solution forces the resin bed to release the calcium and magnesium ions which are discharged to a drain.
  • the ion exchange sites in the resin bed each hold sodium or potassium ions.
  • the regeneration cycle typically lasts about an hour and needs to be done several times a week. More frequent regenerations may be required in periods of greater than normal water usage.
  • a water softener of the type described produces a waste stream during regeneration that contains brine. In some locations of the country, the discharge of a brine solution from a water treatment system is restricted or may be prohibited in the future.
  • Deionization or demineralization systems are also available in the prior art for removing both cations and anions from a water supply.
  • An example of such a deionization system can be found in U.S. Patent No. 4,427,549.
  • separate cation and anion resin tanks are used to remove cations and anions, respectively from the water being treated.
  • the cation and anion tanks contain respective cation and anion exchange resins.
  • the resin tanks of the deionization apparatus must be regenerated periodically to flush the captured ions from the resins.
  • the cation resin is regenerated by an acid regeneration solution which drives the cations from the resin bed and replaces them with hydrogen ions (H ⁇ +).
  • the anion resin is regenerated by an alkaline solution which flushes the anions from the resin bed and replaces them with hydroxyl ions (OH ⁇ -).
  • two waste streams are produced during regeneration, one being an acid solution, the other being an alkaline solution. A water deionization system where waste streams of this type are eliminated or substantially reduced is desirable.
  • EDI electrodeionization
  • Conventional EDI water producing methods as described in U.S. Patent 7,033,472 contain an ion depletion chamber partitioned by a cation exchange membrane on one side and anion exchange membrane on the other side.
  • the depletion chamber is packed with an ion exchange material.
  • Concentrate chambers are provided on both sides of the depletion chamber with the cation exchange membrane and anion exchange membrane in between.
  • the depletion chamber and the concentration chambers are disposed between an anode chamber having an anode and a cathode chamber having a cathode.
  • the depletion and concentrating chambers are stacked in multiples to achieve the desired flow rate by having cation exchange membranes and anion exchange membranes, separated from one another, alternately arranged and an ion exchange material filling every other chamber formed by the cation exchange membrane and anion exchange membrane. Ion exchange material may also be in the concentrate chambers as well.
  • Water to be processed is supplied to the depletion chamber while applying a voltage. Concentrate water is sent to a concentrate chamber to remove impurity ions from the water to be processed, whereby deionized water is produced.
  • Another example of an EDI system is disclosed in US Patent No. 4,871,431. An EDI apparatus as described in U.S.
  • Patent 6,607,647 describes EDI as a process that removes ionizable species from liquids using electrically active media and an electrical potential to influence ion transport.
  • EDI the ability of the resin to rapidly transport ions to the surface of the ion exchange membranes is much more important than the ion exchange capacity of the resin. Therefore resins are not optimized for capacity but for other properties that influence transport, such as water retention and selectivity.
  • the present invention provides a new and improved water treatment apparatus and method that utilizes electricity to regenerate the cation and anion exchange resin chambers while maintaining a relative scale free environment. It also improves on the current electrochemical device designs by lowering the voltage required, eliminating the requirement of continuous electricity during product water flow and also eliminating the requirement of product water flow when electric potential for the regeneration of the resin chambers is applied.
  • the water treatment apparatus includes at least one cation exchange chamber and at least one anion exchange chamber that contain respective cation and anion exchange resins.
  • a bipolar interface is located between the cation and anion exchange chambers.
  • a first primary electrode chamber which may comprise a cathode is associated with the cation exchange chamber. The electrode chamber communicates with the cation exchange chamber through a cation exchange membrane.
  • the cathode is surrounded by a cation exchange membrane which is located in or adjacent the cation exchange resin chamber.
  • the apparatus further includes a second primary electrode which may be an anode that is associated with the anion exchange chamber.
  • the second electrode communicates with the anion exchange chamber through an anion exchange membrane and, in a more preferred embodiment, the second electrode (i.e., anode) is surrounded by an anion exchange membrane).
  • the bipolar interface can be a bipolar membrane.
  • the bipolar interface defines a zone of water disassociation.
  • the water treatment apparatus is configured in a plate and frame design, and with this configuration, the cathode and anode resin chambers are at least one inch thick.
  • the water treatment apparatus can be configured in an annular design wherein the membranes, electrodes and chambers are arranged in an annular, layered design.
  • the water treatment apparatus may include a baffle which may comprise a cation exchange membrane located within the cation exchange resin chamber.
  • This baffle divides the resin chamber into a highly exhausted resin region and a highly regenerated resin region.
  • the baffle improves efficiency.
  • the baffle causes the incoming water to flow initially through the exhausted resin before flowing through the highly regenerated resin.
  • the exhausted resin region is located adjacent or next to the associated electrode, and as a result, virtually all current flow generated by the electrode flows through the exhausted resin before flowing through the region of the chamber where highly regenerated resin is still present.
  • a compact and efficient design is provided.
  • the design unlike the prior art, does not require multiple cation and anion exchange resin chambers in a given cell.
  • a cell with five chambers, three membranes plus bipolar interface configuration and with three electrodes is disclosed as contrasted with the first embodiment (that includes a cell with four chambers, two or three electrodes, and two membranes plus a bipolar interface).
  • the five chamber design is comprised of a first primary electrode chamber which in the illustrated embodiment is a cathode/anode chamber, a second primary electrode chamber which in the illustrated embodiment is an anode chamber, a cation exchange resin chamber containing cation exchange media, an anion exchange resin chamber containing anion exchange media, and a fifth chamber that is an auxiliary electrode chamber that contains an auxiliary electrode that can function as either a cathode or as an anode.
  • the bipolar interface separates the cation exchange resin chamber and the anion exchange resin chamber.
  • the first and second primary electrode chambers and the auxiliary electrode chamber also containing an electrode are separated from each other and the cation and anion exchange resin chambers by ion exchange membranes that are selectively permeable either to cations (positively charged ions) or anions (negatively charged ions), but not both.
  • Each of the chambers that contain an electrode may also contain ion exchange media and also may communicate with a reservoir and recirculation pump.
  • the auxiliary electrode chamber is located either between the anode chamber and the anion exchange resin chamber or between the cathode/an ion chamber and the cation exchange resin chamber.
  • the auxiliary electrode in the auxiliary electrode chamber may be operated in conjunction with the other two electrodes in many different ways.
  • the auxiliary electrode can be operated intermittently with the cathode/anode in the cathode/anode chamber to create a de-scaling or cleaning cycle for either the auxiliary electrode chamber or the cathode/anode chamber in the following manner. In the first case, during the normal operation cycle, only the primary anode and the primary cathode/anode are energized and the auxiliary electrode is not energized.
  • the bipolar junction is actively splitting water into H+ and OH- ions which regenerate the cation ion exchange media in the cation exchange chamber and the anion exchange media in the anion exchange chamber, respectively, and the ions also move toward the oppositely charged electrodes under the applied electric field.
  • the primary anode is de-energized and the auxiliary electrode is energized as an anode by means of a switching device.
  • the auxiliary electrode In order to lower the pH of the auxiliary electrode chamber and thereby prevent scaling or to de-scale the auxiliary electrode chamber, the auxiliary electrode is energized as an anode, and the first primary electrode continues to function as a cathode. At the auxiliary electrode, oxygen gas and H+ ions are formed
  • the hydrogen ions reduce the pH of the water in the auxiliary electrode chamber, and thereby dissolve any scale that has formed. In order to make this pH change occur rapidly, it is also desirable to reduce or stop the flow of water through the auxiliary electrode chamber when the electrode is energized as an anode.
  • the auxiliary electrode is energized as a cathode and the first primary cathode is temporarily energized as an anode by means of a switching device.
  • the pH of the water in the cathode/anode chamber is lowered by the H + ions generated in the chamber and the first primary electrode (energized as a cathode) chamber is de-scaled.
  • the electric field resulting from this operation also results in lowering the pH of the anion membrane surface on the side facing the auxiliary electrode chamber, thereby dissolving or separating any scale that may form at this surface.
  • the second primary electrode i.e.an anode
  • the second primary electrode i.e.an anode
  • the second primary electrode is not energized and there is no electrical potential across the bipolar junction. Accordingly, there is no water splitting or regeneration of the cation exchange media in the cation exchange resin chamber and no regeneration of the anion exchange media in the anion exchange resin chamber during the de-scaling cycles as described above. Since regeneration of the ion exchange media does not occur during the de-scale cycles, it is desirable that the de-scale time interval be as short as possible in relation to the normal service cycle. Cycle times for the normal service cycle and one or more de-scale cycles may be variable and may also be combined with changes to the flow rates through the electrode chambers, and/or changes to the applied current.
  • auxiliary electrode in an auxiliary electrode chamber can be beneficially cycled, these descriptions are not intended to limit the scope of this invention regarding the ways that this feature can be used, only as two examples of the many different ways which are part of this invention.
  • the auxiliary electrode may function as the cathode with the cathode/anode de-energized during normal service without departing from the spirit of this invention.
  • Figure 1 is a schematic representation of a water treatment system constructed in accordance with one preferred embodiment of the invention
  • Figure 2 is a sectional view, shown somewhat schematically, of an electroregeneration water treatment device constructed in accordance with a preferred embodiment of the invention
  • Figure 3 is a sectional view, shown somewhat schematically, of an electroregeneration water treatment device constructed in accordance with a preferred embodiment of the invention commonly known as the plate and frame design
  • Figure 4 shows the components used to construct an electroregeneration water treatment device in accordance with one preferred embodiment of the invention commonly referred as the annular design
  • Figure 4A is a sectional view of the apparatus shown in Figure 4 as seen from the plane indicated by the line 4A-4A;
  • Figure 5 A is schematic representation of a water treatment system constructed in accordance with another preferred embodiment of the invention
  • Figures 5B and 5C are illustrations of the exhaustion patterns of the resin with and without a baffle added to the system, respectively;
  • FIG 6 is a schematic representation of a water treatment system constructed in accordance with another preferred embodiment of the invention.
  • Figure 1 schematically illustrates a water treatment system for removing both cations and anions from a water supply.
  • the water to be treated (or raw water) is first fed through a prefilter 10 to remove sediment and other particulates carried by the water. From the prefilter, the water to be treated is conveyed to an electroregeneration deionization cell or vessel indicated by the phantom line 14.
  • the cell 14 includes a cation exchange resin chamber 20 and an anion exchange resin chamber 24 through which the raw water is passed.
  • a cation exchange resin 20a (only shown in Figure 2) and an anion exchange resin 24a contained within the chambers 20, 24 (shown in Figure 1), respectively operate to remove some or all of the cations and anions carried by the raw water.
  • filtered raw water is communicated to an inlet of the cation exchange resin chamber 20 via conduit or flow path 30 and branch conduit 30a.
  • cations carried by the water such as calcium and magnesium are attracted to, and held within the chamber 20 by the cation exchange resin 20a (shown in Figure 2).
  • the decationized water flows to the anion exchange resin chamber 24 via conduit or flow path 34.
  • the decationized water may flow into the anion exchange resin chamber 24 via the flow path 35 (as will be further explained).
  • the anion resin 24a shown in Figure 2 within the chamber 24 attracts anions such as sulfates, chlorides, etc. and removes them from the water traveling through the resin chamber 24.
  • the resulting "deionized" water is then conveyed to a delivery point such as a faucet indicated generally by the reference character 36 via conduit or flow path 38.
  • the flow path 38 may optionally include a storage tank 40 for accumulating deionized water and/or a post treatment device 42.
  • the post treatment device 42 may comprise a post filter such as a carbon filter or a device for adding minerals or chemicals such as fluoride to the deionized water prior to dispensing.
  • the water produced by the apparatus was termed “deionized” water.
  • the primary function of the disclosed apparatus is to remove hardness ions from incoming water and do this without requiring pre-treatment of the water to remove certain ions prior to processing as is the case with conventional EDI systems.
  • the disclosed apparatus is effective in producing "softened” water directly from a water supply that has not been pre-treated. Because the apparatus is using an electric potential in its operation, an anode is required to create the required electric field and, as a result, some anions are also removed from the water. However, the apparatus is not intended to produce ion-free or "deionized" water as that term is defined in the water industry.
  • the system may include an optional mixing valve 45 which is used, if desired, to mix filtered raw water with treated water.
  • an optional branch conduit 47 feeds filtered raw water to the mixing valve 45 which can be operated to feed a predetermined amount of raw water via an outlet conduit 49 to the storage tank where the raw water is mixed with treated water.
  • the cation exchange resin chamber 20 is separated from a cathode chamber 50 by way of a cation exchange membrane 52.
  • the cathode chamber 50 houses a cathode 54 which is connected to a negative terminal of a direct electrical current power source 54a.
  • a flushing and dilution fluid flows through the cathode chamber 50 from an inlet indicated generally by the reference character 56 and flows to a waste conduit 58.
  • the flushing and dilution fluid is untreated water from the raw water source.
  • the anion exchange resin chamber 24 is separated from an anodic electrode chamber 60 via an anion exchange membrane 62.
  • the anode chamber contains an anode 64 connected to a positive terminal of a direct electrical current power source 64a.
  • the flushing fluid enters the anode chamber via a conduit 63 and leaves the anode chamber 60 via a waste connection or outlet conduit 68.
  • Both conduits 58 and 68 communicate with a drain or other waste connection. Conduits 58 and 68 may also be joined together and then connected to a drain or other waste connection.
  • the cation exchange resin chamber 20 and the anion exchange resin chamber 24 are in adjacent fluid communication.
  • an interface between the anion resin chamber and cation resin chamber, indicated generally by the reference character 90 is operative to split water at the interface into hydrogen and hydroxyl ions as illustrated schematically in Figure 1.
  • the anion and cation resin chambers 20, 24 are separated by a bipolar interface (indicated by the reference character 90).
  • This interface could be a bipolar membrane which maintains the mechanical separation between the anion and cation exchange resins 20a, 24a, while allowing the hydrogen and hydroxyl ions to pass through the resin and membrane to the oppositely charged electrode.
  • the bipolar interface 90 may also allow some decationized water to pass directly from the cation exchange resin chamber 20 to the anion exchange resin chamber 24 (indicated by the flow arrow 35) independent of the decationized water conveyed along the flow path 34.
  • FIG. 2 illustrates, in more detail, one preferred embodiment of an electrodeionization cell or vessel 14 that integrates the cathode chamber, cation exchange resin chamber, anion exchange resin chamber and anode chamber.
  • the portions of the deionization cell 14 shown in Figure 2 that correspond to the block diagram shown in Figure 1 will be given the same reference character followed by an apostrophe.
  • the components of the cell 14 shown individually in Figure 1 are all housed in a single vessel housing 100.
  • the lower half of the vessel is a cation exchange portion 100a whereas the upper half of the vessel is an anion exchange portion 100b.
  • the cation exchange portion 100a includes the cation exchange resin chamber
  • the cation exchange resin chamber 20' which contains the cation resin 20a.
  • the cation exchange resin chamber 20' is separated from the cathode chamber 50' by a cation exchange membrane 52'.
  • Water to be treated enters the cation exchange resin chamber 20' via the inlet connection 30a'.
  • the water to be treated flows upwardly through the cation exchange resin 20a as indicated by the process flow arrow 1 10, from a region of completely or partially exhausted resin near the cation exchange membrane 52' to a region of highly regenerated resin near the bipolar interface 90'.
  • the anion exchange portion 100b of the cell 14 located in the upper half of the vessel includes the anion exchange resin chamber 24' and the anode chamber 60'.
  • the anode chamber 60' is separated from the anion exchange resin chamber 24' via the anion exchange membrane 62'.
  • the decationized water When the decationized water leaves the cation exchange resin chamber 20', it may either pass through the interface 90' which may be termed a bipolar interface and enter the anion exchange resin chamber 24' or it will exit the cation resin chamber 20' via conduit 34' and enter the anion resin chamber via conduit 34'. If the decationized water enters the anion resin chamber via 34', then the decationized water flows through the anion exchange resin 24a as indicated by the process flow arrow 1 14. The anions carried in the decationized water are held or captured in the anion exchange resin 24a and thus deionized water is discharged from the anion exchange resin chamber 24' via the outlet connection 38'.
  • the interface 90' which may be termed a bipolar interface and enter the anion exchange resin chamber 24' or it will exit the cation resin chamber 20' via conduit 34' and enter the anion resin chamber via conduit 34'.
  • the decationized water If the decationized water enters the anion resin chamber via 34',
  • a voltage potential is applied across the cathode 54' and anode 64' thus creating an electric field within the cell.
  • This voltage potential may, or is preferably, less than 40 volts.
  • the electric field causes water in this region to disassociate into hydrogen and hydroxyl ions.
  • the electric field maintained between the cathode 54' and anode 64' also causes cations removed by the cation exchange resin 20a to migrate towards the cathode 54'. This migration of cations or "cation flux" is indicated by the arrow 120.
  • the anions removed from the water flowing through the anion exchange resin chamber 24' are attracted to and tend to migrate towards the anode 64' and into the anode chamber 60'.
  • the anion exchange membrane 62' allows this "anion flux,” as indicated by the flow arrow 126, to flow into the anode chamber 60'.
  • the ions that migrate into the cathode and anode chambers 50', 60' are flushed from the chambers by fluid communicated to the chambers via the respective inlets 56', 63' and are discharged through respective outlets 58', 68'.
  • the membranes 52', 62' that separate the cathode and anode chambers 50', 60' from the respective cation exchange resin and anion exchange resin chambers 20', 24' substantially prevents the cross flow of water and flushing fluid between the chambers.
  • the hydrogen ions produced near the bipolar interface 90' are also attracted to the cathode 54'. As these hydrogen ions travel through the cation exchange resin 20a they tend to displace the captured cations from the cation exchange resin 20a so that they can flow into the electrode chamber 50'. In effect, these hydrogen ions "regenerate" the cation exchange resin 20a. This regeneration can occur both during the processing of water (as water flows through the vessel 14) and more importantly, occurs when water is not flowing through the vessel, i.e. when treated water is not being called for at the dispensing point or faucet 36 (shown in Figure 1). In effect, the cation exchange resin 20a may be continuously regenerated.
  • the hydroxyl ions produced near the bipolar interface 90' are attracted by and move towards the anode 64'.
  • the anion exchange resin 24a they tend to replace anions such as sulfate or chloride ions from the resin so that these undesirable ions are free to flow into the anode chamber 60' where they are removed by the flushing fluid communicated to the anode chamber 60'.
  • the anion exchange resin 24a is continuously regenerated by the hydroxyl ions produced in the zone of water disassociation 90' in the same or in substantially the same manner described above in connection with the cation resin 20a.
  • the cation and anion exchange resin chambers 20 and 24 respectively are sized to have sufficient capacity for intermittent periods of high product water flow and usage. This allows the deionization cell 14 to deionize water during higher than normal usage or usage during a power outage.
  • the deionization cell 14 is also capable of electroregeneration without producing product water due to the separate flushing streams through the cathode and anode chambers 50' and 60' respectively.
  • the chambers 20, 24 are preferably at least one inch thick.
  • the cell 14 preferably produces treated water that is less than one grain per gallon hard.
  • the vessel may include optional third electrodes 140 which can be used to control the pH of the water in the anion exchange resin chamber 24' or in the cation exchange chamber 20'.
  • Figures 3 and 4 illustrate actual implementations of the cell 14 illustrated schematically in Figure 2.
  • the cell 14 is implemented in a plate and frame configuration.
  • components shown in Figure 3 that are the same as the components shown in Figure 2 are indicated by the same reference character.
  • the flowpath 34 illustrated in Figure 3 corresponds to the flowpath 34 shown in Figure 1. With this preferred design, only one anion chamber and one cation chamber are needed in a given cell to produce sufficient quantities of treated water.
  • Figures 4 and 4A illustrate another implementation of the cell 14 shown schematically in Figure 2.
  • the apparatus shown in Figure 4 is substantially similar to that shown in Figure 3 except that cell is configured as an annular structure in which the plate-like layers shown in Figure 3 are replaced with cylindrical interfitting layers.
  • the components shown in Figures 4 and 4a that are the same as those shown in Figure 2 are indicated with the same reference characters.
  • the flowpath 34 shown in Figure 4A corresponds to the flowpath 34 shown in Figure 1.
  • Figure 5 A illustrates another embodiment of the invention.
  • the system shown in Figure 5A is shown schematically and for purposes of explanation, components in Figure 5A that are identical or substantially identical to components shown in Figure 1 are given the same reference characters.
  • the cations removed from the treated water move downwardly towards the cathode chamber, through the cation exchange membrane 52. This movement is indicated by the vertical arrow.
  • the water being treated moves generally vertically through the cation exchange resin chamber towards the bipolar junction 90 in Figure 1.
  • the movement of the water being treated and the flow of cations are generally parallel.
  • the flow of water to be treated is transverse or perpendicular to the flow of electric current, i.e., the flow of cations.
  • FIG. 5A This flow relationship is illustrated in Figure 5A.
  • a baffle 52a is employed.
  • the baffle 52a is another cation exchange membrane.
  • the placement of the cation exchange membrane 52a in the canion exchange chamber creates a region of highly exhausted resin next to the cathode chamber 50.
  • the baffle 52a confines and directs the flow of water entering the cation exchange resin chamber 20 to flow initially through the highly exhausted resin 21a before flowing around the baffle 52a and entering more highly regenerated resin region 21b.
  • the baffle 52a defines a flowpath for the water entering the chamber, the cations themselves removed from the water can flow across the baffle 52a towards the cathode 54.
  • FIG. 5B illustrates the flow pattern and relationship between the cation membrane 52 and the cation chamber 20.
  • water to be treated enters the chamber 20 via inlet 30a.
  • the baffle 52a which preferably comprises a cation membrane forces the incoming water to flow through the highly exhausted resin which is immediately adjacent the cation membrane (CM) 52a and hence the cathode 54.
  • CM cation membrane
  • FIG 5C illustrates the flow/resin relationship when the baffle 52a is not used.
  • water to be treated enters at one end of the cell and flows in a direction substantially parallel to the cathode membrane 52.
  • highly exhausted resin is formed near the chamber inlet.
  • a gradient may be formed where the resin varies from highly exhausted resin at the inlet to highly regenerated resin at the outlet. Since the current flow from the cathode membrane 52 is transverse to the water flow, a significant portion of the current flows through highly regenerated resin where it is not needed. This results in inefficient use of the cathode current.
  • the baffle cell design described above is advantageous when the flow of water is transverse or perpendicular to the flow of electric current as is the case, for example, in the plate and frame design shown in Figure 3.
  • the use of the flow baffle forces the ions to enter the ion exchange resin chamber at a point close to where they will exit through the ion exchange membrane. The ions, therefore, have less distance to travel in order exit the chamber when the baffle design is utilized.
  • resins of different ionic forms have different conductivities, such that the regenerated form of both strong acid cations and strong base anion resins are more conductive than the exhausted form of each resin.
  • the flow directing baffle 52a which is also importantly not a barrier to ion transport or electrical conductance, most of the current would pass through the already regenerated resin and be wasted in the sense that the majority of the current would not regenerate the exhausted resin as is desired.
  • the baffle 52a creates a plane of exhausted resin across the entire cross-section of the cell and forces current in the form of hydrogen ion migration to pass through the exhausted resin, thereby regenerating it. This balances out the flow of electrical current at the top, middle and bottom of the chamber and improves the electrical efficiency.
  • the third electrode was not used in this example but it is believed that a desirable pH can be obtained by using such.
  • FIG. 6 schematically illustrates another embodiment of a water treatment system for removing hard and other ions from a water supply.
  • the water to be treated (or raw water) is first fed through a prefilter 10" to
  • the cell 14" includes a cation exchange resin chamber 20" and an anion exchange resin chamber 24" through which the raw water is passed.
  • a cation exchange resin 20a (only shown in Figure 2) and an anion exchange resin 24a contained within the chambers 20", 24", respectively operate to remove some or all of the cations and anions carried by the raw water.
  • filtered raw water is communicated to an inlet of the cation exchange resin chamber 20" via conduit or flow path 30" and branch conduit 30a".
  • cations carried by the water such as calcium and magnesium are attracted to, and held within the chamber 20" by the cation exchange resin 20a (shown in Figure 2).
  • the decationized water flows to the anion exchange resin chamber 24" via conduit or flow path 34". Alternately, some or all of the decationized water may flow into another chamber or reservoir (as will be further described).
  • the anion resin 24a (shown in Figure 2) within the chamber 24" attracts anions such as sulfates, chlorides, etc. and removes them from the water traveling through the resin chamber 24".
  • the resulting "deionized” water is then conveyed to a delivery point such as a faucet indicated generally by the reference character 36" via conduit or flow path 38".
  • the flow path 38" may optionally include a conduit 38a" to a storage tank 40" for accumulating purified water and/or a post treatment device 42", or a flow conduit 38b" to a mixing valve 45" to mix filtered raw water 47" with the treated water 38".
  • the post treatment device 42" may comprise a post filter such as a carbon filter or a device for adding minerals or chemicals such as fluoride to the deionized water prior to dispensing.
  • the cation exchange resin chamber 20" is separated from an auxiliary electrode chamber chamber 163 by way of a cation exchange membrane 52" which in the preferred embodiment separates the cation exchange resin chamber 20" from the auxiliary electrode chamber 163.
  • the auxiliary electrode chamber 163 houses an auxiliary electrode 160 which by means of a switching device (not shown) can be connected to either the positive terminal or to the negative terminal of a direct electric current source 160a.
  • the auxiliary electrode chamber 163 is separated from the cathode/anode chamber 165 by an anion exchange membrane 164 which may have the identical construction as anion exchange membrane 62". Make-up water flows into the auxiliary chamber 163 through conduit 161, and exits as waste through conduit 162.
  • conduit 161 There can be various sources of the make-up water in conduit 161, and in the preferred embodiment the source of this water is the dilution water that is leaving the Cathode/Anode chamber 165 in conduit 166.
  • the source of this water is the dilution water that is leaving the Cathode/Anode chamber 165 in conduit 166.
  • cations pass into the auxiliary electrode chamber 163 through cation exchange membrane 52"
  • anions pass into the auxiliary electrode chamber through anion exchange membrane 164.
  • These ions exit the auxiliary electrode chamber as waste through conduit 162.
  • the cathode/anode chamber 165 houses an electrode 167 which by means of a switching device (not shown) can be connected either to the negative terminal or to the positive terminal of a direct electrical current power source 167a.
  • Dilution water flows through the cathode/anode chamber 165 from an inlet indicated generally by the reference character 56"and flows to an outlet conduit 166.
  • the dilution water may be decationized water from conduit 34" and may be recirculated by means of a pump(not shown) from a reservoir (not shown) through both the anode chamber 60" and the cathode/anode chamber 165.
  • the anion exchange resin chamber is separated from an anodic electrode chamber 60"via an anion exchange membrane 62".
  • the anode chamber contains an anode 64"connected to a positive terminal of a direct electrical current power source 64"a, and may at times be de-energized by means of a switching device (not shown).
  • Dilution water is also conveyed to the anode chamber 60" through the connected conduit or flow path 63" The dilution water enters the anode chamber via a conduit 63" and leaves the anode chamber 60" and is communicated to the cathode/anode chamber 165 through conduits 68" and 56".
  • an interface between the anion resin chamber and cation resin chamber, indicated generally by the reference character 90" is a bipolar interface operative to split water at the interface into hydrogen and hydroxy! ions as illustrated schematically in Figure 1.
  • the hydrogen ions and the hydroxide ions produced in the zone of water disassociation 90" move as described previously in the descriptions for Fig. 1 and Fig. 2, except that when configured as shown in Figure 6, anions also flow from the cathode/anode chamber 165 to the auxiliary electrode chamber 163 through anion exchange membrane 164.
  • the auxiliary electrode 160 can be operated intermittently with the cathode/anode 167 in the cathode/anode chamber 165 to create a de-scaling or cleaning cycle for either the auxiliary electrode chamber 163 or the cathode/anode chamber 165 in the following manner.
  • the primary anode 64" and the primary cathode 167 are energized and the auxiliary electrode 160 is not energized.
  • the bipolar junction 90" is actively splitting water into H+ and OH- ions which regenerate the cation ion exchange media in the cation exchange chamber 20" and the anion exchange media in the anion exchange chamber 24", respectively, and the ions also move toward the oppositely charged electrodes under the applied electric field.
  • the primary anode 64" is de-energized and the auxiliary electrode 160 is energized as an anode by means of a switching device.
  • the auxiliary electrode 160 is energized as an anode, and the primary cathode 167 continues to function as a cathode.
  • oxygen gas and H+ ions are formed due to the electrolysis of water by the following equation, where e ' represents a negatively charged electron. 2H 2 O - 4e " -» O 2 ( g) + 4H +
  • the hydrogen ions generated from this reaction reduce the pH of the water in the auxiliary electrode chamber 163, and thereby dissolve any scale that has formed. In order to make this pH change occur rapidly, it is also desirable to reduce or stop the flow of water through the auxiliary electrode chamber 163 when the electrode 160 is energized as an anode.
  • the auxiliary electrode 160 is energized as a cathode and the primary cathode 167 is temporarily energized as an anode by means of a switching device. In this way the pH of the water in the cathode/anode chamber 165 is lowered by the H + ions generated by the above reaction and the primary cathode chamber is de-scaled.
  • the electric field resulting from this operation also results in lowering the pH of the anion membrane surface 164 on the side facing the auxiliary electrode chamber 163, thereby dissolving or separating any scale that may form at this surface.
  • the primary anode 64" is not energized and there is no electrical potential across the bipolar junction 90". Accordingly, there is no water splitting or regeneration of the cation exchange media in the cation exchange resin chamber 20" and no regeneration of the anion exchange media in the anion exchange resin chamber 24" during the de-scaling cycles as described above. Since regeneration of the ion exchange media does not occur during the de-scale cycles, it is desirable that the de-scale time interval be as short as possible in relation to the normal service cycle. Cycle times for the normal service cycle and one or more de-scale cycles may be variable and may also be combined with changes to the flow rates through the electrode chambers, and/or changes to the applied current. Table 2
  • Table 2 describes several cycles that can be implemented with the apparatus show in Figure 6.
  • Cycle A and B There are at least two possible service cycles which are identified as Cycle A and B.
  • Service Cycle A the primary anode 64" is energized with a positive voltage, the auxiliary electrode 160 is de-energized and the cathode/anode 167 is given a negative potential.
  • the apparatus of Figure 6 will use Cycle A as its normal service cycle to produce softened water.
  • Cycle B may be chosen as the normal service cycle.
  • a positive voltage is applied to the anode 64"
  • a negative voltage is applied to the auxiliary electrode 160 and the cathode/anode 167 is de-energized.
  • Cycle C is implemented.
  • the primary anode 64" is de-energized and the auxiliary electrode is positively charged and the cathode/anode 167 is negatively charged.
  • the length of the cleaning cycle in C should be relatively short but of sufficient time to dissolve and flush away any scale in the auxiliary electrode chamber 160. If the anion exchange membrane 164 also needs cleaning, Cycle D is then implemented.
  • Cycle D the primary anode 64" is de-energized and the auxiliary electrode 160 is negatively charged, whereas the cathode/anode 167 is positively charged. It is believed that cleaning Cycle D should be relatively short but of sufficient time to allow the scale to be dissolved and flushed from the anion exchange membrane 164.
  • auxiliary electrode in an auxiliary electrode chamber can be beneficially cycled
  • these descriptions are not intended to limit the scope of this invention regarding the ways that this feature can be used, only as two examples of the many different ways which are part of this invention.
  • the auxiliary electrode may function as a primary cathode with the cathode/anode de-energized during normal service without departing from the spirit of this invention.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Molecular Biology (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)

Abstract

La présente invention concerne un appareil de traitement de l'eau qui comprend une chambre échangeuse de cations contenant une résine échangeuse de cations et une chambre échangeuse d'anions contenant une résine échangeuse d'anions. Une interface bipolaire se trouve entre les chambres contenant les résines et définit une zone de dissociation de l'eau. Une cathode communique avec la chambre échangeuse de cations par une membrane échangeuse de cations. Une anode communique avec la chambre échangeuse d'anions par une membrane échangeuse d'anions. Une eau de dilution ou de rinçage s'écoule dans les chambres contenant la cathode et l'anode et achemine les ions capturés jusqu'à un branchement de drainage ou d'évacuation autre. Une déflection peut être utilisée dans certaines configurations pour diviser une chambre contenant une résine en une région contenant la résine épuisée et une région contenant la résine régénérée et qui fait s'écouler l'eau entrante d'abord à travers la région contenant la résine épuisée. La région contenant la résine épuisée se trouve à proximité de l'électrode qui lui est associée, améliorant ainsi l'efficacité électrique de la cellule. Dans une variante de conception, l'appareil comprend une chambre contenant une cathode/anode, une chambre contenant une anode et une chambre contenant une électrode auxiliaire disposée entre la chambre contenant la cathode/anode et une chambre de milieu échangeur de cations. Une membrane échangeuse d'anions sépare la chambre contenant la cathode/anode de la chambre contenant l'électrode auxiliaire. La chambre contenant l'anode, la chambre contenant la cathode/anode et la chambre contenant l'électrode auxiliaire sont alimentées en séquences prédéterminées pour créer à la fois des cycles de service qui produisent de l'eau adoucie avec une faible teneur en ions et des cycles de nettoyage pour détartrer la chambre contenant l'électrode auxiliaire et/ou la membrane échangeuse d'anions située entre la chambre contenant la cathode/l'anode et la chambre contenant l'électrode auxiliaire.
PCT/US2008/005195 2006-10-18 2008-04-23 Appareil d'électrogénération et procédé de traitement de l'eau Ceased WO2009051612A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US12/445,848 US8337686B2 (en) 2006-10-18 2008-04-23 Electroregeneration apparatus and water treatment method

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
PCT/US2007/022204 WO2008048656A2 (fr) 2006-10-18 2007-10-18 Appareil d'électrorégénération et procédé de traitement d'eau
USPCT/US2007/022204 2007-10-18

Publications (1)

Publication Number Publication Date
WO2009051612A1 true WO2009051612A1 (fr) 2009-04-23

Family

ID=40568382

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2008/005195 Ceased WO2009051612A1 (fr) 2006-10-18 2008-04-23 Appareil d'électrogénération et procédé de traitement de l'eau

Country Status (1)

Country Link
WO (1) WO2009051612A1 (fr)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012082239A1 (fr) * 2010-12-14 2012-06-21 General Electric Company Appareil de désionisation par échange d'ions présentant une régénération électrique
US8585906B2 (en) 2006-07-14 2013-11-19 Rayne Dealership Corporation Regeneration of ion exchange resin and recovery of regenerant solution
US8627560B2 (en) 2010-11-12 2014-01-14 Siemens Water Technologies Pte. Ltd. Methods of making a cell stack for an electrical purification apparatus
EP2708514A4 (fr) * 2011-05-13 2014-06-04 Panasonic Corp Dispositif adoucisseur d'eau par régénération
KR20140074896A (ko) * 2011-09-16 2014-06-18 제너럴 일렉트릭 캄파니 스케일링 물질을 부동태화시키기 위한 전기 투석 방법 및 장치
EP2809431A4 (fr) * 2012-02-02 2015-11-04 Tangent Company Llc Déionisation de l'eau régénérée de manière électrochimique
US10301200B2 (en) 2013-03-15 2019-05-28 Evoqua Water Technologies Llc Flow distributors for electrochemical separation
CN115246671A (zh) * 2021-04-26 2022-10-28 财团法人工业技术研究院 废水处理系统及其清洗方法
RU2825947C1 (ru) * 2023-12-28 2024-09-02 Общество с ограниченной ответственностью "АКВАМИН-ТЕХНОЛОДЖИ" Электрохимическая установка обессоливания высокоминерализованных вод

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6416645B1 (en) * 1993-10-27 2002-07-09 The State Of Connecticut, As Represented By The Department Of Economic And Community Development Electrolytic process and apparatus for the controlled regeneration of modified ion exchangers to purify aqueous solutions
US20050103644A1 (en) * 2003-11-13 2005-05-19 United States Filter Corporation Water treatment system and method
US20060157422A1 (en) * 2003-11-13 2006-07-20 Evgeniya Freydina Water treatment system and method

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6416645B1 (en) * 1993-10-27 2002-07-09 The State Of Connecticut, As Represented By The Department Of Economic And Community Development Electrolytic process and apparatus for the controlled regeneration of modified ion exchangers to purify aqueous solutions
US20050103644A1 (en) * 2003-11-13 2005-05-19 United States Filter Corporation Water treatment system and method
US20060157422A1 (en) * 2003-11-13 2006-07-20 Evgeniya Freydina Water treatment system and method

Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8585906B2 (en) 2006-07-14 2013-11-19 Rayne Dealership Corporation Regeneration of ion exchange resin and recovery of regenerant solution
US9186665B2 (en) 2006-07-14 2015-11-17 Rayne Dealership Corporation System for ion exchange resin regeneration and regenerant recovery
US9481585B2 (en) 2010-11-12 2016-11-01 Evoqua Water Technologies Pte. Ltd Flow distributors for electrochemical separation
US8741121B2 (en) 2010-11-12 2014-06-03 Evoqua Water Technologies Llc Electrochemical separation modules
US9187350B2 (en) 2010-11-12 2015-11-17 Evoqua Water Technologies Pte. Ltd. Modular electrochemical systems and methods
US8627560B2 (en) 2010-11-12 2014-01-14 Siemens Water Technologies Pte. Ltd. Methods of making a cell stack for an electrical purification apparatus
US9227858B2 (en) 2010-11-12 2016-01-05 Evoqua Water Technologies Pte Ltd. Electrical purification apparatus
US9463987B2 (en) 2010-11-12 2016-10-11 Evoqua Water Technologies Pte. Ltd Methods of making a cell stack for an electrical purification apparatus
US9463988B2 (en) 2010-11-12 2016-10-11 Evoqua Water Technologies Pte. Ltd Electrical purification apparatus having a blocking spacer
US8956521B2 (en) 2010-11-12 2015-02-17 Evoqua Water Technologies Llc Electrical purification apparatus having a blocking spacer
US9138689B2 (en) 2010-11-12 2015-09-22 Evoqua Water Technologies Pte. Ltd. Method of providing a source of potable water
US9139455B2 (en) 2010-11-12 2015-09-22 Evoqua Water Technologies Pte. Ltd. Techniques for promoting current efficiency in electrochemical separation systems and methods
US9446971B2 (en) 2010-11-12 2016-09-20 Evoqua Water Technologies Pte. Ltd Techniques for promoting current efficiency in electrochemical separation systems and methods
US9187349B2 (en) 2010-11-12 2015-11-17 Evoqua Water Technologies Pte. Ltd. Modular electrochemical systems and methods
WO2012082239A1 (fr) * 2010-12-14 2012-06-21 General Electric Company Appareil de désionisation par échange d'ions présentant une régénération électrique
JP2013545612A (ja) * 2010-12-14 2013-12-26 ゼネラル・エレクトリック・カンパニイ 電気脱イオン化装置
CN103249485A (zh) * 2010-12-14 2013-08-14 通用电气公司 带有电再生的离子交换去离子设备
US8496797B2 (en) 2010-12-14 2013-07-30 General Electric Company Electrical deionization apparatus
AU2011341667B2 (en) * 2010-12-14 2016-10-06 Bl Technologies, Inc. Ion exchange deionization apparatus with electrical regeneration
KR101838770B1 (ko) 2010-12-14 2018-03-14 제너럴 일렉트릭 캄파니 전기적 재생과 함께 이온 교환 탈이온화를 수행하는 장치
EP2708514A4 (fr) * 2011-05-13 2014-06-04 Panasonic Corp Dispositif adoucisseur d'eau par régénération
KR20140074896A (ko) * 2011-09-16 2014-06-18 제너럴 일렉트릭 캄파니 스케일링 물질을 부동태화시키기 위한 전기 투석 방법 및 장치
KR101892787B1 (ko) 2011-09-16 2018-08-28 제너럴 일렉트릭 캄파니 스케일링 물질을 부동태화시키기 위한 전기 투석 방법 및 장치
US9724645B2 (en) 2012-02-02 2017-08-08 Tangent Company Llc Electrochemically regenerated water deionization
EP2809431A4 (fr) * 2012-02-02 2015-11-04 Tangent Company Llc Déionisation de l'eau régénérée de manière électrochimique
US10301200B2 (en) 2013-03-15 2019-05-28 Evoqua Water Technologies Llc Flow distributors for electrochemical separation
CN115246671A (zh) * 2021-04-26 2022-10-28 财团法人工业技术研究院 废水处理系统及其清洗方法
CN115246671B (zh) * 2021-04-26 2023-11-28 财团法人工业技术研究院 废水处理系统及其清洗方法
US12209037B2 (en) 2021-04-26 2025-01-28 Industrial Technology Research Institute Wastewater treatment system and cleaning method thereof
RU2825947C1 (ru) * 2023-12-28 2024-09-02 Общество с ограниченной ответственностью "АКВАМИН-ТЕХНОЛОДЖИ" Электрохимическая установка обессоливания высокоминерализованных вод

Similar Documents

Publication Publication Date Title
US8337686B2 (en) Electroregeneration apparatus and water treatment method
JP3416455B2 (ja) 液体を精製するための電気脱イオン方法
US6733646B2 (en) Method and apparatus for electrodeionization of water
US6896814B2 (en) Fractional deionization process
US3686089A (en) Method of separation of ions from a solution
US7582198B2 (en) Water treatment system and method
EP1299312B1 (fr) Appareil d' electrodesionisation
EP2208523B1 (fr) Dispositif d'électro-désionisation avec séparation de flux hydrodinamique
WO2009051612A1 (fr) Appareil d'électrogénération et procédé de traitement de l'eau
US20060231403A1 (en) Chambered electrodeionization apparatus with uniform current density, and method of use
AU2014212394B2 (en) Rechargeable electrochemical cells
JP2006297392A (ja) 極性逆転および二重逆転による電気消イオン装置ならびにそれらの使用法
US20100133115A1 (en) Devices and methods for acid and base generation
JP4748318B2 (ja) 電気脱イオン装置
EP1684902B1 (fr) Procedes de traitement d'eau
MXPA06005384A (en) Water treatment system and method
JP4915843B2 (ja) 電気軟化装置、軟化装置及び軟水製造方法
HK1115574A (en) Fractional deionization process
JP2003001261A (ja) 電気再生式脱塩装置

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 12445848

Country of ref document: US

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08767407

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 08767407

Country of ref document: EP

Kind code of ref document: A1