WO2007048814A1 - Procede d’adoucissement de l’eau a l’aide d’un echangeur de cations et regeneration de l’echangeur de cations - Google Patents

Procede d’adoucissement de l’eau a l’aide d’un echangeur de cations et regeneration de l’echangeur de cations Download PDF

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Publication number
WO2007048814A1
WO2007048814A1 PCT/EP2006/067779 EP2006067779W WO2007048814A1 WO 2007048814 A1 WO2007048814 A1 WO 2007048814A1 EP 2006067779 W EP2006067779 W EP 2006067779W WO 2007048814 A1 WO2007048814 A1 WO 2007048814A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
regeneration
exchanger
carbon dioxide
eluate
Prior art date
Application number
PCT/EP2006/067779
Other languages
German (de)
English (en)
Inventor
Wolfgang HÖLL
Klaus Hagen
Uwe Sauer
Original Assignee
Forschungszentrum Karlsruhe Gmbh
Krüger-Wabag GmbH
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
Application filed by Forschungszentrum Karlsruhe Gmbh, Krüger-Wabag GmbH filed Critical Forschungszentrum Karlsruhe Gmbh
Priority to EP06807551A priority Critical patent/EP1937599A1/fr
Publication of WO2007048814A1 publication Critical patent/WO2007048814A1/fr

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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • B01J49/50—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents
    • B01J49/53—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents for cationic exchangers
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/02—Non-contaminated water, e.g. for industrial water supply
    • 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
    • C02F2301/046—Recirculation with an external loop
    • 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
    • C02F2301/06—Pressure conditions
    • C02F2301/066—Overpressure, high pressure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/16—Regeneration of sorbents, filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage

Definitions

  • the invention relates to a method for softening water.
  • US Pat. No. 3,691,109 likewise discloses a method in which the regeneration of a basic and an acidic ion exchanger is carried out by flushing each other.
  • the present invention has accordingly set itself the task of providing a method for softening water, which does not have the described disadvantages of the prior art.
  • the precipitation of the calcium carbonate should be avoided.
  • the process should be suitable for operation in industrial reactors.
  • This object is achieved by a method for softening water in a technical reactor, in particular drinking water, with a weakly acidic cation exchanger, wherein the exchanger is regenerated after receiving alkaline earth ions by water containing dissolved carbon dioxide under pressure.
  • the carbon dioxide is preferably dissolved in water at a pressure of 2 to 10 bar, more preferably 4 to 5 bar. Accordingly, the regeneration process is performed under this pressure.
  • the regeneration is carried out in the flow.
  • the corresponding flow rates are 1 to 7 m 3 / m 2 h, preferably about 5 m 3 / m 2 h.
  • in flow means that the water used for regeneration is introduced into the reactor through one or more inlets on one side of the cation exchanger, passes through the cation exchanger, and exits the reactor through one or more outlets other than the cation exchanger ,
  • the rinse water is recycled in the process of the invention for immediate use. That is, the rinse water, after passing through the filter containing the ion exchanger, is directly supplied to a buffer from which it can be taken immediately for the next regeneration.
  • the pre-filtrate is preferably fed for reuse. That is, the pre-filtrate is fed to a buffer and used for the next regeneration.
  • the eluate produced in the regeneration can be treated with a membrane filter unit and the resulting permeate can be recycled.
  • the concentrate is fed to a receiving water or a sewage treatment plant or the like.
  • the released in the first stage of the degassing of pure water CÜ2 is collected and in turn fed to the regeneration.
  • the eluate of the regeneration and possibly the rinse water is treated by means of a vacuum degasser and the carbon dioxide removed is returned.
  • the carbon dioxide released in the second stage of the degassing of the pure water is collected and recycled for regeneration.
  • a softening of water depending on the raw water by up to 70% can be achieved.
  • the process of the invention is carried out in a preferred variant at pressures of 5 to 15 bar.
  • the inventive method is preferably carried out at temperatures of 10 to 20 ° C, particularly preferably between 10 and 15 ° C.
  • the process according to the invention is carried out in industrial reactors.
  • Technical reactor means a volume of 2 to 150 cubic meters (in 3 ), preferably 20 to 60 cubic meters (in 3 ).
  • the process according to the invention is preferably used in the treatment of drinking water and / or process water, in particular drinking water treatment.
  • the process according to the invention is preferably used in the treatment of water in breweries.
  • a preferred application is still the treatment of water in a sewage treatment plant. Also applicable is the inventive method for water treatment in a power plant. There, the water is not used as drinking water, but reaches drinking water quality.
  • the operation of at least two water-softening reactors is preferred as the "alternating reactor system."
  • Reactor further used for softening.
  • the drawing shows a process scheme for the softening of water.
  • a well 1 raw water is removed and either used directly or promoted in a raw water tank 2.
  • the water to be treated is supplied via a raw water pipe 3 to a filter system consisting of one or more filters 4, 5.
  • the two filters 4 shown in the drawing on the right are in operation, while the filter 5 shown on the left is regenerated.
  • the filters 4.5 are filled with a weakly acidic cation exchanger.
  • a portion of its salt content primarily the content of alkaline earth ions, is removed from the raw water by contact with the ion exchanger material.
  • the softened pure water enters a two-stage pure water deaerator 6 to adjust the lime-carbonic acid balance.
  • a vacuum degasser 7 is expelled from the pure water by applying a negative pressure CO2. Subsequently, the pure water of the second stage is fed to a Rieselentgaser 8, in the air blown. The degassed pure water is discharged via a pure water storage 9 or directly to the end user. Optionally, the vacuum degasser stage 7 can be dispensed with.
  • the loaded ion exchanger is regenerated by water which contains carbon dioxide dissolved under a pressure of 3-7, preferably 5-6, bar.
  • the regeneration is carried out at a flow rate of 3-7 m 3 / m 2 h.
  • the regeneration water is prepared in a reaction storage 10, in the from above water from the raw water pipe 3 or possibly water from the pure water storage 9 and from below CO2 from a CO 2 tank 1 1 and from the returns from the vacuum degasser 7 and the later described Eluatentgaser 13 fed.
  • the regeneration water is added via a line 12 from below, ie counter to the desalting in the filter 5 to be regenerated.
  • the eluate formed in the regeneration is fed, after passing through the filter 5, to an eluate degasser 13 operated under reduced pressure, where CO2 is expelled from the eluate.
  • the degassed eluate is either fed directly to a receiving water 24 or temporarily stored in an eluate storage 23, from which it is made evenly distributed to the surface water.
  • a portion of the eluate may be added via an eluate line from a further buffer 14 in the reaction memory 10, where it can be used in the regeneration.
  • the expelled in the Eluatentgaser 13 from the eluate CO2 is collected and added via a line 16 in the reaction memory 10.
  • the CO 2 produced in the vacuum degasser stage 7 of the pure-water deaerator 6 is returned via a line 17 to the reaction storage tank 10.
  • the CO2 released in the trickle degasser 8 is either fed via a line 18 into the eluate / rinse water / prefilterate stored in the buffer 14, whereby a further precharging of this water with CO2 is achieved or sent directly to the outside.
  • the regenerated filter 5 is rinsed with rinsing water in order to free the ion exchangers from the residues of the regeneration water.
  • the rinse water is removed from the raw water.
  • the spent rinse water is returned after exiting the filter 4.5 in the buffer 14 and kept ready for the next regeneration.
  • the pre-filtrate, which leaves first a regenerated filter 4,5, is not discharged as pure water. Instead, this prefilter is also fed via a prefilter line 20 into the buffer 14 and used for the next regeneration.
  • a separate CO 2 circuit 19 serves to loosen the ion exchanger material.
  • the eluate contains the salt cargo, which was extracted from the raw water. To increase the yield, the eluate can be fed completely or partially to a membrane filter unit 22.
  • the membrane filter unit 22 operates according to the method of reverse osmosis, nanofiltration or electrodialysis.
  • the permeate obtained in the membrane filter unit 22 is either fed to the raw water reservoir 2, or admixed with the raw water to be treated in the filter system or the pure water after the filter 4.5 has run out.
  • the saline concentrate is fed to the receiving water 24 or a sewage treatment plant.
  • the process according to the invention makes it possible to work only with the use of a weakly acidic cation exchanger.
  • a strongly-based anion exchanger can be dispensed with. This surprisingly allows softening of the water without causing solids, e.g. Calcium carbonate precipitate.
  • the omission of the anion exchanger does not adversely affect the process.
  • the water hardness could be lowered from 28 ° dH to 13 ° dH.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treatment Of Water By Ion Exchange (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne un procédé d’adoucissement de l’eau dans un réacteur technique, notamment d’eau de boisson, à l’aide d’un échangeur de cations acides faibles, ledit échangeur étant régénéré après absorption des ions alcalino-terreux par l’eau, l’eau étant sous pression et comprenant du dioxyde de carbone.
PCT/EP2006/067779 2005-10-27 2006-10-26 Procede d’adoucissement de l’eau a l’aide d’un echangeur de cations et regeneration de l’echangeur de cations WO2007048814A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP06807551A EP1937599A1 (fr) 2005-10-27 2006-10-26 Procede d'adoucissement de l'eau a l'aide d'un echangeur de cations et regeneration de l'echangeur de cations

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102005051388.3 2005-10-27
DE102005051388 2005-10-27

Publications (1)

Publication Number Publication Date
WO2007048814A1 true WO2007048814A1 (fr) 2007-05-03

Family

ID=37706554

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2006/067779 WO2007048814A1 (fr) 2005-10-27 2006-10-26 Procede d’adoucissement de l’eau a l’aide d’un echangeur de cations et regeneration de l’echangeur de cations

Country Status (2)

Country Link
EP (1) EP1937599A1 (fr)
WO (1) WO2007048814A1 (fr)

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3691109A (en) * 1970-05-25 1972-09-12 Marathon Oil Co Process for regenerating resins of deionization system
DE2714297A1 (de) * 1977-03-31 1978-10-05 Berger Wittmar Christoph Verfahren und vorrichtung zur regeneration schwach saurer ionenaustauscher mittels kohlensaeure bei gleichzeitiger kalziumkarbonat-faellung
EP0056850A1 (fr) * 1981-01-28 1982-08-04 Kernforschungszentrum Karlsruhe Gmbh Procédé de déminéralisation partielle d'eaux à l'aide d'une combinaison de matières échangeuses d'ions acides moderées et basiques, suivi d'une régénération de ces matières échangeuses
EP0930272A2 (fr) * 1998-01-15 1999-07-21 WABAG Wassertechnische Anlagen GmbH Procédé de déminéralisation partielle de l'eau
EP1110914A2 (fr) * 1999-11-19 2001-06-27 Rohm And Haas Company Procédé et appareil pour le traitement d' eaux
WO2002026344A1 (fr) * 2000-09-26 2002-04-04 Hydrometrics, Inc Purification d'eau produite provenant de puits de gaz naturel a couche de charbon par echange d'ions et osmose inverse

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3691109A (en) * 1970-05-25 1972-09-12 Marathon Oil Co Process for regenerating resins of deionization system
DE2714297A1 (de) * 1977-03-31 1978-10-05 Berger Wittmar Christoph Verfahren und vorrichtung zur regeneration schwach saurer ionenaustauscher mittels kohlensaeure bei gleichzeitiger kalziumkarbonat-faellung
EP0056850A1 (fr) * 1981-01-28 1982-08-04 Kernforschungszentrum Karlsruhe Gmbh Procédé de déminéralisation partielle d'eaux à l'aide d'une combinaison de matières échangeuses d'ions acides moderées et basiques, suivi d'une régénération de ces matières échangeuses
EP0930272A2 (fr) * 1998-01-15 1999-07-21 WABAG Wassertechnische Anlagen GmbH Procédé de déminéralisation partielle de l'eau
EP1110914A2 (fr) * 1999-11-19 2001-06-27 Rohm And Haas Company Procédé et appareil pour le traitement d' eaux
WO2002026344A1 (fr) * 2000-09-26 2002-04-04 Hydrometrics, Inc Purification d'eau produite provenant de puits de gaz naturel a couche de charbon par echange d'ions et osmose inverse

Also Published As

Publication number Publication date
EP1937599A1 (fr) 2008-07-02

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