WO2003082748A1 - Procede de regeneration de resines echangeuses d'ions - Google Patents

Procede de regeneration de resines echangeuses d'ions Download PDF

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Publication number
WO2003082748A1
WO2003082748A1 PCT/AU2003/000405 AU0300405W WO03082748A1 WO 2003082748 A1 WO2003082748 A1 WO 2003082748A1 AU 0300405 W AU0300405 W AU 0300405W WO 03082748 A1 WO03082748 A1 WO 03082748A1
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WO
WIPO (PCT)
Prior art keywords
resin
water
ion
doc
chloride salt
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PCT/AU2003/000405
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English (en)
Inventor
Hung V. Nguyen
Matthew W. Carr
Luisa C. Pentland
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Orica Australia Pty Ltd
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Filing date
Publication date
Application filed by Orica Australia Pty Ltd filed Critical Orica Australia Pty Ltd
Priority to AU2003213862A priority Critical patent/AU2003213862A1/en
Publication of WO2003082748A1 publication Critical patent/WO2003082748A1/fr

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Classifications

    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
    • B01J20/28002—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their physical properties
    • B01J20/28009—Magnetic properties
    • 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
    • B01J49/57—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents for anionic exchangers
    • 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

Definitions

  • the present invention relates to water treatment, and in particular to water treatment processes which involve the use of ion-exchange resins.
  • the invention relates to a process for regenerating ion-exchange resin used in such processes, and especially, magnetic ion- exchange resin.
  • the invention will be described with reference to the treatment of raw water to produce potable water for distribution and consumption, however it is to be understood that the invention may also be used in other industrial applications, such as in the treatment of sewage and effluent from industrial processes.
  • DOC dissolved organic carbon
  • Substitute Sheet The production of safe potable water from a raw water supply often requires treatment of water to make it aesthetically acceptable, as well as being safe to drink.
  • the removal of suspended matter and DOC is an important aspect of this treatment.
  • Two approaches are commonly used for the removal of suspended matter and DOC. One involves coagulation and the other membrane filtration.
  • a coagulant is applied to destabilise and combine with suspended matter and DOC so that they coalesce and form a floe, which can then be physically removed by methods such as floating, settling, filtration or a combination thereof.
  • Coagulants such as alum (aluminium sulphate), various iron salts and synthetic polymers are commonly used in processes for water treatment.
  • many raw water sources have high levels of DOC present, which reacts with the coagulant requiring a higher coagulant dose than would be required for removal of suspended matter alone.
  • the bulk of the floe formed may then be removed by sedimentation or flotation and the water containing the remainder of the floe passed through a filter for final clarification.
  • the treated water may contain as much as 30-70% of the initial DOC.
  • MF Microfiltration
  • UF Ultrafiltration
  • NF Nanofiltration
  • RO Reverse Osmosis
  • DOC dissolved organic carbon
  • Substitute Sheet Ion-exchange resins can also be used for removing DOC present in raw water.
  • Ion- exchange techniques conventionally involve passing water through a packed bed or column of ion-exchange resin.
  • Target species DOC
  • Ion-exchange resins can be used to remove up to 90% of the DOC in raw water.
  • Ion-exchange resins may also be used in conjunction with other methods of water purification including those mentioned previously. Sufficient resin may be added to remove a percentage of the DOC such that the cost of any subsequent treatment used to meet water quality objectives is minimised. For example, the use of ion-exchange resin for the removal of DOC can facilitate the reduction of the amount of coagulant required to achieve acceptable product water quality. Ion-exchange resin may also aid in significantly reducing the capital and operating costs of membrane filtration.
  • ion-exchange resins are preferably recyclable and regenerable. Recyclable resins can be used multiple times without regeneration and continue to be effective in adsorbing DOC. Regenerable resins are capable of being treated to remove adsorbed DOC, and as such, these regenerated resins can be reintroduced into the treatment process.
  • Ion-exchange resins incorporating dispersed magnetic particles readily agglomerate due to the magnetic attractive forces between them. This property renders them particularly useful as recyclable resins as the agglomerated particles are more readily removable from the water.
  • a particularly useful magnetic ion-exchange resin for the treatment of raw water is described in WO96/07675, the entire contents of which is incorporated herein by reference.
  • the resin disclosed in this document has magnetic particles dispersed throughout the polymeric beads such that even when they become worn through repeated use, they retain their magnetic character.
  • Ion exchange beads of the type disclosed in this document are available from Orica Australia Pty. Ltd. under the trademark, MIEX ® .
  • Substitute Sheet WO 96/07615 describes a process for removing DOC from water using an ion-exchange resin which can be recycled and regenerated. This process is particularly useful in treating raw water with magnetic ion-exchange resin of the type described in WO96/07675.
  • the preferred ion-exchange resins disclosed in WO96/07675 are magnetic ion-exchange resins which have, throughout their structure, cationic functional groups which provide suitable sites for the adso ⁇ tion of DOC. These cationic functional groups possess negatively charged counter-ions which are capable of exchanging with the negatively charged DOC. Accordingly, the negatively charged DOC is removed from the raw water through exchange with the resin's negative counter ion. As a result of this process DOC becomes bound to the magnetic ion-exchange resin and the function of the ion-exchange resin is reduced. Such resins are referred to herein as used or loaded ion-exchange resins. For producing potable water for distribution and consumption it is particularly important to be able to regenerate the used magnetic ion-exchange resin in an efficient and cost effective manner.
  • WO 96/07615 discloses a process for regenerating magnetic ion-exchange resin by contacting it with brine (which is substantially a NaCl solution).
  • brine which is substantially a NaCl solution.
  • the by-product of this regeneration process referred to as the "spent regenerant”
  • the spent regenerants of this process are either ultimately disposed of as land fill or discharged into the ocean.
  • the spent regenerant is usually disposed of by land application when the water treatment is carried out in inland areas where ready access to the ocean is not available. It has been estimated that in the process described in WO96/07615, every million litres of raw water treated per day, generates approximately 200-400 litres of spent regenerant depending on the raw water quality. This method for disposing of spent regenerant can be environmentally unacceptable in many inland areas. In particular, the large concentrations of deposited brine which are produced as a by-product cause degradation of soil quality.
  • Substitute Sheet 26 RO AU Studies have also attributed the high concentrations of sodium in the spent regenerant to an increase in soil salinity and water logging.
  • the present invention provides a process for regenerating ion-exchange resin which has been previously used to remove DOC from water in a water treatment plant, which process comprises contacting the ion-exchange resin with an aqueous solution of a chloride salt for a time and under conditions sufficient to regenerate the resin, wherein said chloride salt is selected from KC1, NH 4 C1, MgCl 2 or CaCl 2 or mixtures thereof.
  • the invention provides an industrial scale process for the removal of DOC from water containing DOC, said process comprising:
  • the present invention provides an industrial scale process for the removal of DOC from water containing DOC, said process comprismg:
  • Substitute Sheet (ii) separating the resin loaded with DOC from the water;
  • step (iii) regenerating at least a portion of the separated resin and recycling the remainder to step (i), wherein the resin is regenerated by contacting the resin with an aqueous solution of a chloride salt for a time and under conditions sufficient to regenerate the resin, wherein the said chloride salt is selected from KC1, NH C1, MgCl 2 or
  • step (v) recycling the regenerated resin back to step (i).
  • the process according to the second and third aspects may further include additional steps associated with ion-exchange processes for water treatment, as would be understood by a person skilled in the art.
  • regenerating ion-exchange resin refers to a process in which the ion-exchange capacity of a used ion-exchange resin is returned to a level whereby it is rendered suitable for use in subsequent ion-exchange processes.
  • the ion- exchange resins used in the removal of DOC have cationic groups which provide suitable sites for the adsorption of the DOC. These cationic groups have associated anions which exchange with the DOC during the ion-exchange process.
  • the regeneration process of the present invention involves the displacement (or exchange) of the adsorbed DOC with chloride ions.
  • ion-exchange sites in a resin it is not necessary for all ion-exchange sites in a resin to be regenerated for an ion-exchange resin to be considered "regenerated" for the purpose of the present invention. It is sufficient that the regeneration process has occurred to an extent that ion- exchange resin is useful in subsequent ion-exchange processes. Preferably more than 80% of the ion-exchange sites previously taken up by the DOC or other compounds are
  • Substitute Sheet regenerated, more preferably greater than 90% and most preferably greater than 98%.
  • the ion-exchange resin which is subjected to the regeneration process of the present invention is resin having cationic groups which has been previously used in a water treatment plant to remove DOC from water.
  • the water treatment plant may be a plant for producing potable water for distribution and consumption, or may be a plant for the treatment of sewage, or industrial waste water containing DOC.
  • An industrial water treatment plant may be associated with food processing, pharmaceutical production, electronic component manufacture, membrane plant reject, hospital application and the like. While the present invention is useful in any large scale water treatment facility, it is particularly preferred for use in the treatment of a water source to produce potable water for distribution and consumption.
  • the used or loaded ion-exchange resin (which is bound by DOC) may be contacted with the aqueous solution of the chloride salt (hereinafter referred to as "the regenerant") in any convenient way which allows the chloride ions to exchange with DOC adsorbed on the resin.
  • the regenerant is contacted with the ion-exchange resin in a way which allows the recovery of the regenerated ion-exchange resin from the regenerant.
  • the regenerant will be added to the used resin and dispersed for a time and under conditions sufficient to allow desorption of the DOC from the resin.
  • the resin may be dispersed in the regenerant by any convenient means, preferably with agitation by mechanical stirring or gas bubble agitation.
  • Separation of the resin from the regenerant can be achieved by allowing the resin to settle or by filtering through a mesh of appropriate porosity.
  • the regenerant can be recycled and reused to regenerate resin a number of times before it becomes unsuitable for use in the regeneration process.
  • Substitute Sheet is particularly suitable for the resin described in WO96/07675 due to its structure. This process also enables high rates of desorption of the DOC from the resin and improves the recyclability of the resin.
  • the preferred resins for the regeneration according to the present invention are magnetic ion-exchange resins, such as the resin disclosed in WO96/07675. These ion-exchange resins which contain magnetic particles agglomerate in a process sometimes referred to as “magnetic flocculation", due to the attractive magnetic forces between them. This property renders them particularly suited to this application as the agglomerated particles are more readily removable from the regenerant.
  • magnetic flocculation In dispersing the magnetic ion-exchange resin in the regenerant it is important that sufficient shear is applied to overcome the magnetic attractive forces which cause agglomeration. Agglomeration of the resin is achieved by removing the shear causing the resin particles to disperse.
  • the magnetic ion-exchange resin is more dense than the regenerant such that it has a tendency to settle quickly to the bottom of the regeneration tank. This also facilitates the separation of the resin from the regenerant.
  • the resin may be collected by various means including vacuum collection, filtration, magnetic transport such as belts, pipes, dishes, drums, pumps and the like.
  • the resin is separated from the regenerant by either vacuum filtration of the regenerant through a filter cloth or mesh of appropriate porosity or by decanting off the regenerant sitting on top of the settled resin or a combination of both.
  • the separation and collection means do not cause undue mechanical wear which may lead to alteration of the resin.
  • the regenerant of the present invention is preferably a concentrated aqueous chloride salt solution selected from KCl, NH 4 C1, MgCl 2 or CaCl 2 .
  • the chloride salt is KCl,
  • regenerant salt is KCl or NH 4 C1.
  • Substitute Sheet preferred regenerant salt is KCl.
  • the concentrated aqueous chloride salt solution used in the process of the present invention are preferably solutions in which the chloride salt concentration is more than 1.5M or more preferably 2M or greater.
  • the main advantage of the present invention is that the spent regenerants do not contain high levels of sodium and therefore do not contribute to increased salinity when disposed of by land application.
  • the present invention provides an environmentally friendly alternative to the prior art processes. This is of particular benefit for inland water processing plants which do not have ready access to allow for the spent regenerant to be discharged into the ocean.
  • the spent regenerant when using KCl or NH C1 as the regenerant the spent regenerant may be utilised as a fertiliser or stock feed. Accordingly, another advantage of using the alternative regenerants of the present invention is that the spent regenerant can be beneficially used in other industries as products such as a fertiliser, a component of a balanced fertiliser or a stock feed. Further processing of the spent regenerant, using processes such as evaporation or membrane treatment may produce a DOC concentrate suitable for other applications such as a soil conditioner or a health supplement. It has also been implied that fulvic acids (a DOC) may find value as a medicament, in particular, as an antioxidant or to increase the functioning of the immune system. Accordingly, the present invention may provide products which are useful in themselves, or which can be further processed to provide pharmaceutically or agriculturally beneficial compounds.
  • a DOC fulvic acids
  • the spent regenerant of the present invention generally consists of an aqueous solution of the regenerant salt and DOC. Depending on the concentration of the regenerant, the nature of the resin and the process in which the resin was used, the spent regenerant will generally have the regenerant salt and DOC in a weight ratio of around 9:1.
  • the DOC contaminated salt by-products do not adversely affect their use as fertilisers or stock feeds.
  • the regenerant may be added, either as a solid or liquid, as a supplement during the manufacture of a stockfeed.
  • the spent regenerant when used as a stockfeed or fertilizer may be used directly, diluted with an acceptable diluent, or concentrated. It may also be washed prior to use, or used as a dry cake or wet cake (which still contains some moisture).
  • the regeneration process of the present invention is readily incorporated into existing water treatment facilities which utilise ion-exchange resins.
  • it may be used in conjunction with membrane filtration techniques where ion-exchange resins are incorporated to improve the effectiveness of the membranes, increase the flux across membranes and reduce operating costs.
  • ion-exchange resins are incorporated to improve the effectiveness of the membranes, increase the flux across membranes and reduce operating costs.
  • new installations it may be used where existing membrane filtration techniques are replaced with ion-exchange techniques. If membrane filtration techniques are still required, the present invention can be used where ion- exchange processes are incorporated to significantly reduce the size and hence capital and operating cost of a membrane filtration plant.
  • the reduction in capital and operating costs may enable consideration to be given to the installation of membrane filtration rather than coagulation/ sedimentation plants thereby substantially reducing the size of the plant and enabling the production of potable water without the addition of chemicals other than for disinfection purposes.
  • Examples of water treatment processes involving ion-exchange are disclosed in WO96/07615, and the present regeneration process can be readily incorporated into these processes.
  • Substitute Sheet sedimentation, coagulation and filtration may be necessary.
  • the raw water is generally fed into a continuously stirred tank (contactor) which has a nominal residence time usually of between about 5 and 60 minutes.
  • the magnetic ion-exchange resin is added either directly into this tank or into the raw water in the pipeline feeding this tank. It is in this tank that the majority of the ion-exchange process occurs.
  • the water Prior to treatment with the ion-exchange resin the water will generally have been screened to remove large particles to protect pumps involved in pumping the water to the treatment plant. It is also possible that the water will have been subjected to one or more pretreatment steps, such as coagulation/ flocculation and subsequent clarification.
  • the resin and water (resin suspension) is generally passed to a separating stage (settler) where the resin is recovered and recycled.
  • a separating stage settler
  • Magnetic ion-exchange resins have a strong tendency to agglomerate to form large and fast settling particles, when shear is removed (as occurs in the settler).
  • the agglomerated resin particles settle rapidly and are collected on the bottom of the settler where they may be transferred (e.g. by pumping) back to the head of the treatment plant for reuse in the process. At least a portion (and generally a small portion) of the flow which is to be recycled back to the head of the plant is removed and subjected to the regeneration process.
  • fresh, regenerated resin is added to the contactor to make up for the resin not being returned. This ensures the performance of the process is maintained.
  • the resin, after it has been regenerated, may be sent to a "fresh" resin tank before it is added back into the process to make up for resin being sent for regeneration.
  • Substitute Sheet With processes involving the use of MIEX ® resin, pre-treatment is not usually required to remove solids and turbidity from the water, although the raw water may be screened to remove large particulate matter before it is introduced into a water treatment process.
  • the water may be subjected to a coagulation/ flocculation step followed by clarification. This may be done in a gravity settler.
  • the water may also be subjected to one or more of the filtration steps described above, as well as disinfection.
  • the disinfectant may be added at any stage during the water treatment process. Usually however, disinfectants are added during or at the end of the treatment process such that there is residual disinfectant present in the water supplied to the consumer. This is known as secondary disinfection and most commonly involves the use of chlorine, chloramines and chlorine dioxide.
  • potassium permanganate, peroxone, UV radiation and combinations of the above can also be used as primary disinfectants.
  • the water treatment process may also be used in conjunction with other unit processes such as ozonation and treatment using granular activated carbon (GAC).
  • GAC granular activated carbon
  • the regeneration processes of the present invention may be utilised in the above described treatment processes or similar water treatment processes, where an ion-exchange process is incorporated prior to or instead of coagulant addition.
  • coagulants such as alum (aluminium sulphate), iron salts and synthetic polymers are used following the ion- exchange step.
  • the removal of DOC by ion-exchange results in a substantial reduction in the quantity of coagulant required.
  • the removal of DOC reduces the requirement for subsequent chemical additions and improves the efficiency and/or rate of coagulation, sedimentation and disinfection. This has a beneficial impact on the water quality produced and the size of most facilities required within the water treatment plant
  • Substitute Sheet including sludge handling facilities. Since most plants have equipment for regenerating the ion-exchange resin by contacting with brine, the process of the present invention can be conveniently incorporated without significant change in the overall structure or size of the water treatment plant.
  • the regeneration process of the present invention can be conveniently adapted for use in continuous ion-exchange processes that presently use brine as a regenerant.
  • the continuous process differs significantly from conventional ion-exchange process.
  • conventional ion-exchange columns the water quality produced deteriorates as the ion- exchange capacity is progressively exhausted.
  • the leakage of undesired ions eventually reaches the point where the product water is not potable. In such an instance, the column must be taken-off line and the resin regenerated.
  • a continuous process differs in that the overall ion-exchange capacity is continuously maintained. This leads to the production of water with consistent quality as well as the DOC being controlled at predetermined levels.
  • the ability to maintain the quality of water in such processes stems directly from the incorporation of resin recycling and regeneration steps.
  • Such processes usually incorporate a means for removing and recycling the resin to the front end of the process. However, a small amount of the recycled resin is usually removed to be regenerated. The regenerated resin from the regeneration process is subsequently added to the front end of the process.
  • the present invention can be incorporated into such continuous processes.
  • Figure 1 is a plot of tannic acid released (mass) from the resin as a function of time for NaCl, KCl, NH 4 C1 and MgCl 2 .
  • Figure 2 is a plot of tannic acid concentration (cumulative) in the regenerant as a function of the number of regenerations for KCl, NaCl and NH C1.
  • Figure 3 is a plot of tannic acid released (mass) from the resin as a function of the number of regenerations for NaCl, KCl and NH 4 C1.
  • Figure 4 is a plot of absorbance at 254nm of the regenerant as a function of the number of regenerations for NaCl, KCl and NH C1.
  • Figure 5 is a plot of pH of regenerant contacted with resin as a function of the number of regenerations by NaCl, KCl and NH C1.
  • Figure 6 is a plot of TOC (Total Organic Carbon) of regenerant contacted with resin as a function of the number of regenerations by NaCl, KCl andNH 4 Cl.
  • Figure 7 is a plot of TOC of regenerant contacted with resin as a function of the absorbance at 254nm for NaCl, KCl and NH 4 C1.
  • Figure 8 is a plot of the chloride concentration of the regenerant contacted with resin as a function of the number of regenerations for the regenerants NaCl, KCl and NH C1.
  • Example 1 Kinetics of Single Regeneration of MIEX® DOC Resin Loaded with Tannic Acid using Various Regenerants.
  • Substitute Sheet approximately 43 quantities of IL of deionised water to ensure that there were no resin fines.
  • 210ml of the above resin was placed in a sintered glass column, and was loaded with a solution of lOOg of tannic acid (a surrogate material for DOC) in 2L of deionised water.
  • the tannic acid solution was passed through the column over a period of 2 hours. After 30 minutes, the effluent changed in colour from clear to brown.
  • the resin was assumed to be fully loaded with tannic acid after 2 hours.
  • a 50ml sample (30 mins settling) of the tamiic acid loaded resin was taken and washed thoroughly with deionised water before it was added to a 150ml stirred solution (i.e.: 3 bed volumes) of NaCl, which had a chloride concentration of 2.05M. Samples were taken at various time intervals by filtering the suspension through a 3 micron filter cartridge. A sample of the regenerant before resin addition was also taken. The pH was monitored at various times during the contact.
  • the samples were diluted by a factor of 250, and the concentration of tannic acid in solution was determined by using a Varian Cary 50 Probe UV-VIS spectrophotometer at 275 nm. A standard curve was generated, using standards of 0, 5, 10, 20 and 30 mg/L tannic acid.
  • Example 2 Efficiency of Alternative Regenerants after Multiple Regenerations of MIEX ® DOC Resin Loaded with Tannic Acid.
  • the resin sample was stirred in 10L of 20g/L tannic acid solution (ie.:100mg/mL resin) at 450rpm for 1 hour. Samples of the tannic acid solution were taken prior to and after contact with MIEX® DOC resin for UV analysis. The resin was washed with 12L of deionised water and set aside for regeneration. The samples were diluted by 500 times, buffered to pH 7 and the absorbance of each sample at 275nm measured with the UN-NIS spectrophotomer. The amount of tannic acid loaded onto the resin was therefore calculated.
  • 20g/L tannic acid solution ie.:100mg/mL resin
  • regenerant 500ml of regenerant solution was made containing 2M chloride content. A sample of regenerant solution was taken for UV analysis. Nine 50ml samples of loaded resin were prepared. The first 50ml resin sample was filtered to remove excess water and was then added to the 150 ml of the above regenerant solution and stirred at 300rpm in a 200ml beaker for 30 minutes. The regenerant was then filtered from the resin, and a 5g sample taken for UV analysis. The chloride concentration of the remaining regenerant was adjusted before the following regeneration by adding and dissolving 4g NaCl, 5g KCl or 3.6g NH C1. This ensured that the chloride concentration was kept at above 2M.
  • the volume was then readjusted to 150ml with deionised water. The volume and mass of extra water required was noted.
  • the regenerant was then contacted with the second 50ml resin sample, as outlined above. A total of nine regenerations were performed for each regenerant. The pH was measured prior to the first, and after the ninth regeneration using pH paper.
  • the regenerant samples were diluted by 250 times, and pH 7 buffer was added during the dilution to ensure the pH was kept at 7 during UN measurement.
  • the absorbance of each sample was measured. Standards containing 1, 5, 10, 20 and 40mg/l tannic acid, buffered to pH 7 were made. Each sample's absorbance was then converted to mass tannic acid released per volume resin, correcting for the dilutions made after each regeneration.
  • the concentration of tamiic acid in the regenerant is plotted as a function of the number of regenerations in Figure 2, while the amount of tannic acid released in a cycle is plotted as a function of the number of regenerations in Figure 3.
  • Substitute Sheet Example 3 Efficiency of Alternative Regenerants after Multiple Regenerations of MIEX" DOC Resin Loaded with DOC from Real Water.
  • regenerant solution 500 ml was made containing 2M chloride. A 5g sample of regenerant solution was taken for UV analysis, Total Organic Carbon (TOC) analysis and pH measurement.
  • TOC Total Organic Carbon
  • regenerant was then filtered from the resin, and a 5g sample taken for UV, TOC and pH analysis. The mass and volume of the remaining solution were recorded.
  • regenerant salt was added to ensure that the cliloride concentration of the final diluted regenerant would be 2M.
  • Substitute Sheet 8 The volume was then readjusted to 150ml with deionised water. The final volume and mass of the regenerant were noted.
  • regenerant was then contacted with the next 50ml resin sample, as outlined in steps 3 to 8 above. A total often regenerations were performed.
  • regenerant was added to a 100ml volumetric flask, and diluted to the mark with deionised water. (Note: 1ml regenerant in 100ml flask used for KCl and NH C1 regenerants).
  • regenerant samples were diluted 1000 times and buffered to pH 7. (i.e., 1.0 ml of sample was placed in a 50ml volumetric flask, and diluted to the mark with deionised water. 2.5ml of this diluted solution was placed in a 50ml volumetric flask, 5ml of pH

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  • Environmental & Geological Engineering (AREA)
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  • Treatment Of Water By Ion Exchange (AREA)

Abstract

La présente invention concerne un procédé qui permet de regénérer une résine échangeuse d'ions qui a déjà été utilisée pour retirer le carbone organique dissous de l'eau d'une station d'épuration d'eaux. Cette résine est régénérée en étant placée en contact avec un sel de chlorure.
PCT/AU2003/000405 2002-04-03 2003-04-03 Procede de regeneration de resines echangeuses d'ions WO2003082748A1 (fr)

Priority Applications (1)

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AU2003213862A AU2003213862A1 (en) 2002-04-03 2003-04-03 Process for regenerating ion-exchange resins

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AUPS1505 2002-04-03
AUPS150502 2002-04-03

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WO2003082748A1 true WO2003082748A1 (fr) 2003-10-09

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005105677A1 (fr) * 2004-04-30 2005-11-10 Orica Australia Pty Ltd Procede de regeneration
WO2006010216A1 (fr) * 2004-07-28 2006-02-02 Orica Australia Pty. Ltd. Procédé de régénération à écoulement piston
WO2010065738A1 (fr) 2008-12-03 2010-06-10 Hydroionic Technologies Co.Ltd. Système et procédé de traitement d’eaux usées
WO2015041866A1 (fr) * 2013-09-18 2015-03-26 Purolite Corporation Procédé de régénération de résine pour réduire des contaminants organiques
WO2018072281A1 (fr) * 2016-10-21 2018-04-26 中国环境科学研究院 Dispositif pour l'extraction d'acide humique dissous hydrophobe à partir d'un corps d'eau douce
WO2018145457A1 (fr) * 2017-02-08 2018-08-16 中国环境科学研究院 Appareil d'extraction et de purification de matières organiques dissoutes hydrophobes de sol
CN110255767A (zh) * 2019-06-28 2019-09-20 吉林建筑大学 一种天然水体中有机物的分离方法

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EP2373586A1 (fr) * 2008-12-03 2011-10-12 Hydroionic Technologies Co. Ltd. Système et procédé de traitement d eaux usées
EP2373821A2 (fr) * 2008-12-03 2011-10-12 Hydroionic Technologies Co. Ltd. Système et procédé de traitement d' eaux usées
EP2373822A2 (fr) * 2008-12-03 2011-10-12 Hydroionic Technologies Co. Ltd. Système et procédé de traitement d' eaux usées
EP2373821A4 (fr) * 2008-12-03 2013-04-17 Hydroionic Technologies Co Ltd Système et procédé de traitement d' eaux usées
EP2373822A4 (fr) * 2008-12-03 2013-04-17 Hydroionic Technologies Co Ltd Système et procédé de traitement d' eaux usées
EP2373586A4 (fr) * 2008-12-03 2013-04-17 Hydroionic Technologies Co Ltd Système et procédé de traitement d eaux usées
US8761942B2 (en) 2008-12-03 2014-06-24 Hydroionic Technologies Co., Ltd. System and method for wastewater treatment
WO2015041866A1 (fr) * 2013-09-18 2015-03-26 Purolite Corporation Procédé de régénération de résine pour réduire des contaminants organiques
WO2018072281A1 (fr) * 2016-10-21 2018-04-26 中国环境科学研究院 Dispositif pour l'extraction d'acide humique dissous hydrophobe à partir d'un corps d'eau douce
WO2018145457A1 (fr) * 2017-02-08 2018-08-16 中国环境科学研究院 Appareil d'extraction et de purification de matières organiques dissoutes hydrophobes de sol
CN110255767A (zh) * 2019-06-28 2019-09-20 吉林建筑大学 一种天然水体中有机物的分离方法

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