AU4458199A - Water treatment process - Google Patents

Description

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AUSTRALIA

PATENTS ACT 1990 DIVSIONAL APPLICATION NAME OF APPLICANT(S): Orica Australia Pty Ltd AND South Australian Water Corporation ADDRESS FOR SERVICE: DAVIES COLLISON CAVE Patent Attorneys 1 Little Collins Street Melbourne, 3000.

INVENTION TITLE: Water treatment process The following statement is a full description of this invention, including the best method of performing it known to us: Q:\OPER\NEA\705434.D1V 20/9/99 -lA- WATER TRAM TPROCEss The present invention relates to water treatment, in Particular to a process for the removal of dissolved organic carbon from water.

The processes used in water treatment are largely a function of raw water quality.

Potable water supplies often contain unacceptably high levels of organic compounds dissolved, dispersed or suspended in raw water. These organic compounds are refer-red to herein as dissolved organic carbon (DOC). Other, terms used to describe DOG include total organic carbon, organic colour, colour and natural organic matter. DOG often includes compounds such as hurnic and fulvic acids.

Humic and fulvic acids are not discrete organic compounds but mixtues of organic compounds formed by the degradation of plant residues.

15 The removal of DOC from water is necessary in order to provide high quality water *suitable for distribution and consumption. A majority of the compounds and materials which constitute DOG are soluble and not readily separable from the *water. The DOG present in raw water renders conventional treatment difficult and expensive.

The provision of a safe potable water supply often requires treatment of water to make it aesthetically acceptable. The removal of suspended matter and colour is an important aspect of this treatment. Two approaches are commonly used for the removal of suspended matter and colour. One involves coagulation and the other membrane filtration.

In the process involving coagulation, a coagulant is applied to destabilise suspended matter and colour so that they coalesce and form a floc, which can then be physically removed by methods such as floating, settling, filtration or a combination thereof. Coaguilants such as alum (aluminiumn sulphate), various iron salts and synthetic polymers are commonly used in processes for water treatment. However, many raw water sources have high levels of DOG present, which is the main cause -2 of the colour, and the DOC reacts with the coagulant requiring a higher coagulant dose than would be required for removal of suspended matter alone. The bulk of the floc formed may then be removed by sedimentation or flotation and the water containing the remainder of the floc passed through a filter for final clarification.

However, even after such treatment the treated water may contain as much as of the initial DOC.

In the membrane filtration process the water is filtered through a membrane system. However, where the water contains high levels of DOC the membranes tend to be fouled by the DOC, thereby reducing the flux across the membrane, *.reducing the life of the membranes and increasing operating costs. Metmbrajie systems designed to handle water containing high levels of DOC have much higher capital and operating costs than conventional membrane systems used for the production of potable water.

Ion-exchange resins have been used in water treatment processes for the removal of DOC by passing water treated to remove turbidity and other suspended particles 9* through ion-exchange resin packed in columns or the like. Passing untreated water through a packed resin can cause the packed resin to become clogged and 9:::20 ineffective, problems similar to those faced in membrane filtration.

The present invention provides a process for the reduction or elimination of DOC from water using ion-exchange resins which can be conveniently separated from the water prior to subsequent treatment and its distribution and consumption.

Accordingly, we provide a process for the removal of dissolved organic carbon from water, which process includes the following steps: a. adding an ion-exchange resin to water containing dissolved organic carbon; b. dispersing the resin in the water to enable adsorption of the dissolved organic carbon onto the resin; and 3 C. separating the resin loaded with the dissolved erganic carbon from the water.

The ion-exchange resin is dispersed in the water so as to provide the maximum surface area of resin to adsorb the DOC. Dispersal of the ion-exchange resin may be achieved by any convenient means. Typically the resin may be dispersed by mechanical agitation such as stirrers and the like, mixing pumps immersed in the water or. air agitation where a gas is bubbled through the water. Sufficient shear needs to be imparted on the water to achieve dispersal of the resin.

10 In some small scale operations for the ion exchange resin may be dispersed in a *.semi-fluidized bed provided pumping costs are not economically unfeasable. The ueof a semi-flidized bed is not onya convenient means for dsealofthio exchange resin but provides for the ready separation of the loaded resin from the water once DOC is adsorbed onto the ion exchange resin.

4 .Separating the resin loaded with DOC from the water may be achieved by settling or screening or a combination thereof. Screening of' the loaded resin from the water may be achieved by any convenient means. The screens may be selected with 0.00 consideration for the size of resin particles to be removed from the water. The 20 configuration of the screens may be such that clogging of the screens is reduced.

In a preferred embodiment, the ion-exchange resin may be more dense than the water and tend to settle to the bottom of the tank. This settling facilitates the convenient separation of the loaded resin from the water. Settling may be facilitated by the use of tube settlers and the like. The resin may then be collected by various means including vacuum collection, filtration and the like. It is preferable that the separation and collection means do not cause mechanical wear which may lead to attrition of the resin.

When a continuous fully suspended system is used, the resin may conveniently be separated from treated water by gravity settling. Based on resin characteristics, very effective >99% solids removal) gravitational settling is achieved in high-rate -4 settling modules with retention times less than 20 minutes.

In a preferred process for separating the ion-exchange resin from the water the bulk of resin particles settle out in the first quarter of the separating basin length which is devoid of bettler modules ("free -fl owi ng" settling). Further removal of resin particles ("enhanced" settling) from treated water is performed in the settler compartment filled with modules which may be either, tilted plates or tubular modules. The bottom of the settler is designed for collection of resin particles in cylindrical, conical or pyramidal hoppers from which the resin particles are pumped back to the front of the process. In this preferred process some mixing of the settled resin in the hoppers may be required to keep it in a fluid condition and to ensure uniform resin concentration of resin in the recycle system.

The ion-exchange resins suitable for use in the process of the present invention have cationic functional groups. The cationic functional groups provide suitable sites for the adsorption of the DOG.

It is preferred that the ion-exchange resins have a diameter less than 100pM, preferably in the range of from 25pM to 75pM. This size range provides an ionexchange resin which can be readily dispersed in the water and one which is suitable for subsequent separation from the water. The size of the resins affects the kinetics of adsorption of DOC and the effectiveness of separation. The optimal size range for a particular application may be readily determined by simple experimentation.

It is preferred that the ion-exchange resin is macroporous. This provides the resins with a substantially large surface area onto which the DOC can be adsorbed.

Water treatment processes involve the movement of water by stirring, pumping and other operations which can deleteriously effect the ion-exchange resin. It is preferred that the resin is manufactured from tough polymers with polystyrene crosslinkage. The resin may be selected to give the optimum balance between toughness and capacity.

In the process of the present invention the amnount of ion-exchange resin necessary to remove DOC from water is dependent on a number of factors including the level of DOG initially present in the water to be treated, the nature of the DOC, the desired level of DOC in the treated water, salinity, temperature, pH, the number of cycles of the resin prior to regeneration and the rate at which it is desired to treat the water to remove DOG. Typically, the amount of ion-exchange resin used to remove DOG from water will be in the range from 0.5 to 5m1 of wet resin per litre of raw water, preferably 0.5 to 3m1. Higher resin concentrations may also be useful in removing DOG. Such higher concentrations allow shorter contact times .and more effective DOG removal.

High doses of resin can be used to remove up to 90% of the dissolved organic -carbon but the relationship is non linear and it may not be economical under normal conditions to add resin at these high doses. Sufficient resin may be added to remove a percentage of the dissolved organic carbon such that the cost of any *5 subsequent treatment used to meet water quality objectives is mninimised. For -exmpewe have found that removal of dissolved organic carbon reduces the amount of coagulant required to achieve acceptable product water quality. It may also significantly reduce the capital and operating costs of membrane filtration processes.

Preferred ion-exchange resins are 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 treatment to remove adsorbed DOG and such regenerated resins can then be re-introduced into the treatment process.

We have found that, depending on the amount of resin being employed in the treatment process, the resin can be effectively recycled at least 10 times prior to regeneration and in fact at least 20 times depending on water quality. Thus, in a -6 continuous process only 10% or less of the loaded resin, even merely has to be taken for regeneration, the remainder can be recycled back into the treatment process.

We have found that the used (or spent) resin may be readily treated to remove the adsorbed DOC. Accordingly, we provide a process which incorporates the following additional steps for regenerating spent ion-exchange resin: a. adding the spent resin to brine; b dispersing the spent resin in the brine for the desorption of the DOC from the resin; and C. separating the regenerated resin from the brine.

It will be understood that the term brine means any high concentration salt solution capable of causing the desorption of DOC from the resin. High concentration sodium chloride solutions are particularly useful as brine in the present process.

The spent resin may be dispersed in the brine by any convenient means. We have found agitation by mechanical stirring or gas bubble agitation to be particularly convenient.

Separation can be achieved by allowing the regenerated resin to settle or by simply filtering through a mesh of appropriate porosity. We have found that the brine can be recycled and used to regenerate resin for a number of times before it becomes unsuitable for use in the regeneration process. The spent brine can itself be regenerated by passage through a reverse osmosis membrane to separate the DOG from the brine. The DOC thus produced is a useful source of huxmc and fulvic acids.

An alternative process for regenerating spent or loaded ion exchange resin which 7requires much less brine for the regeneration process may be particularly useful in a number of applications. We have found that the spent ion exchange resin may be packed into a column and the passage of a relatively small quantity of brine through it can effectively regenerate the ion exchange resin. Accordingly, we provide a process for regenerating spent ion exchange resin including the following steps: a. packing the spent resin into a column; and b. passing brine through the packed column for the desorption of the DOC from the resin.

*l reeeaino h*pn o xhng ei codn oti rcs Teoregeoneration DOfrhe setinxhne resin. Whaefudtaccording this process -the recyclability of the resin prior to subsequent regenerations is substantially improved.

Further, the humic and fulvic acids are present in significantly higher concentrations in the elutants from the column and thus are a more convenient and economic source of humic and fulvic acids.

The process of the present invention for removal of DOG from water is particularly useful in water treatment applications for the production of potable water.

However, the process could also successfully be applied to other aqueous streams where DOG removal is required, eg: industrial use applications, hospital facilities, mining applications or food processing. The process may also be applied to the treatment of waste water. A variety of organic materials, such as toxins or other contaminants, may be removed from waste water.

We have found that a class of ion-exchange resins is particularly suited to use in the process of the present invention. Ion-exchange resins incorporating magnetic M 0 1

M

-8 particles, known as magnetic ion-exchange resins agglomerate, sometimes referred to as "magnetic flocculation", due to the magnetic attractive forces between them.

This property renders them particularly swted for this application as the agglomerated particles are more readily removable from the water. Accordingly, we provide a process for the removal of dissolved organic carbon from water, which process includes the following steps: a. adding a magnetic ion-exchange resin to water containing dissolved organic carbon; dispersing the resin in the water to enable adsorption of the dissolved organic carbon onto the magnetic ion-exchange resin; C. agglomerating the magnetic ion-exchange resin loaded with the dissolved i organic carbon; and 0 d. separating the agglomerated magnetic ion-exchange resin loaded with the dissolved organic carbon from the water.

The magnetic ion-exchange resin may be dispersed in the water by any of the means described above. Sufficient shear needs to be imparted on the water to overcome the magnetic forces which cause the magnetic ion-exchange resin to agglomerate.

Agglomeration of magnetic ion-exchange resin loaded with DOC is achieved by removing the shear which causes the resin to disperse. In an unstirred tank, the magnetic particles in the resin cause the resin to agglomerate. The agglomeration may be facilitated by the use of tube settlers and other means known to those skilled in the art.

Typically the wet magnetic ion-exchange resin is more dense than the water and once agglomeration has commenced the resin tends to settle quickly to the bottom of the tank. This settling facilitates the convenient separation of the loaded resin 9from the water. The resin may then be collected by various means including vacuum collection, filtration, magnetic transport such as belts, pipes, disks and drums, pumps and the like. We have found vacuum collection particularly convenient. It is preferable that the separation and collection means do not cause mechanical wear which may lead to attrition of the resin.

It is preferred that the ion-exchange resins have a diameter less than 100p, preferably in the range of from 25pM to 75 pM. The size of the magnetic ionexchange resin affects the kinetics of absorption of DOC and the effectiveness of agglomeration and settling. The optimal size range for a particular application may be readily determined by simple experimentation.

V'Te magnetic ion-exchange resin can have a discrete magnetic core or have 6*68 magnetic particles dispersed throughout the resin. In resins which contain dispersed magnetic particles it is preferred that the magnetic particles are evenly dispersed throughout the resin.

A particularly preferred magnetic ion-exchange resin is described in the copending *sees' provisional application number PM8070 now filed as a PCT application designated all states including the United States of America and entitled

TM

olyrner beads and method for preparation thereof' which application is ,in the names of Commonwealth Scientific and Industrial Research Organisation and ICI Australia Operations Pty Ltd.

The spent magnetic ion-exchange resin may be treated to remove the adsorbed DOG. Accordingly, we provide a process for regenerating spent magnetic ionexchange resin including the following steps: a. adding the spent magnetic ion-exchange resin to brine; b. dispersing the spent magnetic ion-exchange resin in the brine for the desorption of the DOC from the magnetic ion-exchange resin; 10 C. agglomerating the regenerated magnetic ion-exchange resin; and d. separating the regenerated magnetic ion-exchange resin from the brine.

An alternative process for regenerating spent or loaded magnetic ion-exchange resin which requires much less brine for the regeneration process may be particularly useful in a number of applications. We have found that the spent magnetic ionexchange resin may be packed into a column and the passage of a small quantity of brine through it can effectively regenerate the magnetic ion exchange resin- Accordingly, we provide a process for regenerating spent magnetic ion exchange resin including the following steps: a. packing the spent resin into a column; and b. passing brine through the packed column for the desorption of the DOC from the resin.

The regeneration of the spent magnetic ion exchange resin according to this process employing a packed column of spent magnetic resin enables particularly high rates of desorption of the DOG from the magnetic resin. We have found that by using this process the recyclability of the magnetic resin prior to subsequent regenerationis is substantially improved.

Further, the humic and fulvic acids are present in significantly higher concentrations in the elutants from the column and thus are a more convenient and economic source of humic and fulvic acids.

The process for the removal of DOG from water is useful in water treatment applications for the production of potable water. The treated water is generally disinfected prior to distribution. The levels of DOG can be as much as 70% of the initial DOC after treatment with conventional processes. This DOC may react with any applied disinfectant to produce by-products. Chlorine is often the preferred 11 disinfectant due its cost, ease of use and the fact tha't a chlorine residual can be maintained throughout the distribution system to inactivate any contamination that may be introduced after the primary disinfection. Chlorine, however, may react with DOC to form a range of by-products, the most well known being trihalomnethanes (THMs). THMs have been identified as possible carcinogens and together with the other possible by-products are identified as a health risk in water treatment guidelines throughout the world. Not only can the DOC form such by-products but the oxidation of the DOC into smaller more biodegradable organics, particularly by the use of ozone as a disinfectant, provides a ready food source for bacteria and be. 10 may result in the regrowth of bacteria in water storages or distribution systems.

Accordingly, we provide a process for water treatment, which includes the following steps: a. adding an ion-exchange resin to water containing dissolved organic carbon; 0 b. dispersing said resin in the water for the adsorption of the dissolved organic 9carbon onto the resin; c. separating the resin loaded with the dissolved organic carbon from the water; ad d. disinfecting the water.

The steps of adding, dispersing and separating the ion-exchange resin may be accomplished by the methods described above. The water may be disinfected by any convenient means. It is particularly preferred that chlorine or chioramines are used to disinfect the water prior to its storage and/or distribution.

The magnetic ion-exchange resins may preferably be used in this process.

Accordingly, we provide a process for water treatment, which includes the following steps: 12 a. adding a magnetic ion-exchange resin to water containing dissolved organic carbon; b. dispersing said magnetic ion-exchange resin in the water for the adsorption of the dissolved organic carbon onto the magnetic ion-exchange resin; c. agglomerating the magnetic ion-exchange resin loaded with the dissolved organic carbon; d. separating the agglomerated magnetic ion-exchange resin loaded with the dissolved organic carbon from the water; and e. disinfecting the water.

S 15 The steps of adding, dispersing, agglomerating and separating the magnetic ion exchange resin may be accomplished by the methods described above.

The process of the present invention is readily incorporated into exidsting water -treatment facilities. For example, it may be used in conjunction with membrane filtration to improve the effectiveness of the membranes, increase the flux across membranes and reduce operating costs. For new installations it may either replace membrane filtration, or if membrane filtration is still required, significantly reduce the size and hence capital and operating costs of a membrane filtration plant. In fact, 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.

Accordingly, in a further aspect the invention provides a process for the treatment of water which includes the following steps: 13 a. adding an ion-exchange resin to water containing dissolved organic carbon; b. dispersing said resin in the water to enable adsorption of the dissolved organic carbon onto the ion-exchange resin; C. separating the ion-exchange resin loaded with the dissolved organic carbon from the water; and d. subjecting the water to membrane filtration.

In an alternative process, steps c. d. above may be combined so that the membrane effects separation of the resin while simultaneously filtering the water.

Many water treatment facilities use a coagulation /sedimentation step in their water 15 -purification process. For example, in South Australia a six stage process, which is a typical conventional water treatment process, is used to treat the source water for distribution. The six stages are as follows: Coagulation/Flocculation; Sedimentation; Filtration; Disinfection;- Storage and Distribution; and Sludge Dewatering and Disposal.

The process of the present invention may be incorporated into this water treatment process most effectively prior to coagulant addition. Typically, coagulants such as alum (aluminium sulphate), iron salts and synthetic polymers are used. The removal of DOG by the present process results in a substantial reduction in the quantity of coagulant required- In addition the removal of DOC reduces the requirement for subsequent chemnical additions and improves the efficiency and/or rate of coagulation, sedimentation and disinfection. This has a beneficial impact on the 14 water quality produced and the size of most facilities required within the water treatment plant including sludge handling facilities. These impacts are particularly convenient in the retrofitting of the process of the present invention as they enable the present process to be conveniently incorporated without substantial change in the overall size of the water treatment plant. Accordingly, in a further aspect the invention provides a process for the removal of dissolved organic carbon from water, which process includes the following steps: a. adding an ion-exchange resin to water containing dissolved organic carbon; b dispersing the resin in the water to enable adsorption of the dissolved ~.organic carbon onto the resin, 0% 0 C. separating the resin loaded with the dissolved organic carbon from the water; and d. subjecting the water to coagulation/ sedimnentation.

Utilising the process of the present invention to remove a high proportion of the #3.3 20 dissolved organic carbon, reduces the coagulant dose required and may allow the lower volumes of floc produced to be removed from the water directly by filtration, without the need for prior sedimentation.

Some water treatment processes employ activated carbon as a final polishing treatment to alleviate problems with taste and/or odour, to remove disinfection byproducts or to remove any other pollutants. The life of the activated carbon is substantially reduced by the presence of DOC in the treated water. Accordingly, a further advantage of our process is that the useful life of activated carbon may be significantly increased. Accordingly, another useful aspect of the present invention includes the further step of subjecting the treated water to activated carbon.

On greenfield sites the use of the process of the present invention wil allow 15 significantly smaller footprint water treatment plants to be designed and constructed. The reduction/ elimination of DOG from the water using the process of the present invention may be effected in a relatively small volume basin. This is due to the fast reaction and settling rates of the process. This enables the amount of coagulant used in coagulation /sedmentation processes to be reduced which consequently reduces the size of the sedimentation facilities and the size -and cost of the water treatment plant. Likewise the size and cost of membrane systems in membrane filtration plants may be reduced which in turn make membrane filtration systems more economically viable when compared with coglto seietto plants.

Throughout this specification and Lhe claims which follow, unless the context requires otherwise, the word "'comprise", or variations such as "comprises" or Hcomprising", will be understood to imply the inclusion of a stated integer or group of integers but not the exclusion of any other integer or group of integers.

The invention will now be further described with reference to the following nonlimiting examples. All percentages used herein are by weight unless otherwise stated. The following test methods were used unless otherwise stated.

1. The turbidity was determined (in nephelometric turbidity units) by direct measurement using a nephelometer (Hach Ratio Turbidimeter [Model 18900]).

2. The pH was determined by glass electrodes in combination with a reference potential provided by a silver/silver chloride or saturated calomel electrode.

3. The colour was calculated by comparison of the absorbance of the sample at 456 nm with a calibration curve of Pt-Co standard solutions at the same wavelength. The colour was recorded in Hazen units (HU) whereby 1 HU equals 1 ppm of platinum.

16 4. The UV Absorbance was determined spectrophotometrically at 254 nm using distilled water as a reference.

A Skalar SK12 organic carbon analyser was used to measure DOC levels.

The analyser used a peristaltic pump to continually aspirate samples and mix them with reagents.

The sample was filtered through Whatman No. 1 filter paper overlain with 0.45 pm membrane. The sample was then acidified with sulphuric acid and sparged with nitrogen. This liberated and dispersed any inorganic or volatile organic carbon. The sample solution was then mixed with a persulphate/tetraborate reagent (34g sodium tetraborate decahydrate and 12g potassium persulphate dissolved in 1 litre of water) and passed through a UV digestion coil. This process oxidised the organic carbon to CO 2 The 15 CO 2 was expelled from solution by acidifying and sparging, and then mixed with hydrogen (H 2 and passed over a Ni catalyst at 400 C. This reduced the CO 2 to methane which was measured with a flame ionisation detector.

20 6. Total Aluminium and Total Iron were determined by inductively coupled plasma spectrometry.

7. Standard Jar Tests: The raw water and resin treated water were subjected to jar tests which enable the evaluation of various coagulants and coagulant aids used in water treatment by simulating a conventional water treatment process, consisting of coagulation, flocculation, sedimentation and filtration. Equal volumes of water (1500 ml) were entered into jars.

The multiple stirrer operated at the "flash mix" speed, approximately 200 rpm. The test solutions of coagulant were added as quickly as possible and I/ flash mixed for a minute.

The speed of the mixer was reduced to the minimum required to maintain the floc uniformly suspended. Slow mixing was continued for a further 14 minutes. Towards the end of the flocculation time, the floc size was recorded.

After the slow mixing period, the paddles were quickly withdrawn and the settling of the floc particles observed.

After 15 minutes quiescent settling, approximately 60 ml of each solution was withdrawn from the sampling tap (the first 20 ml was discardd nnd t e settled water turbidity and pH determined on the remaining volume.

The remaining supernatant was then carefully gravity filtered through a ~:Whatinan No. 1 filter paper. The first 50 ml of filtrate was discarded. The turbidity, colour and aluminium residuals of the filtered solution was then recorded.

20 8. Jar Testing Under Direct Filtration Conditions.

Jar testing was performed under the following direct filtration conditions: room temperature (approx alum and water were flash mixed for 1 minute.

the stirring reduced to 25rpm for 4 minutes (flocculation time) for floc formation.

no settling of floc in contrast to Standard Jar Test.

water clarified by filtration with Whatman No. 1 papers prior to analysis.

9. Method for the Determination of Chlorine Demand 18 A method for determining the chlorine demand of a water sample, by standard addition of chlorine and direct measurement using DPD/FAS titration.

Reagents: Chlorine demand free water Phosphate Buffer Solution (pH N,N-Diethyl-1-4-phenylene diamine sulphate (DPD) Indicator Solution Standard Ferrous Ammonium Sulphate (FAS) Titrant Standard Chlorine Solution A chlorine solution (approx. 1000 mg/L) of measured concentration is prepared from stock sodium hypochlorite solution (approx. 10% available chlorine after filtering through 0.45 pm membrane).

Two 100 mL volumetric flasks are filled with sample water and accurately dosed with standard hypochlorite solution to produce doses equivalent to 10, 15 or 20 mg/L. A different dose is employed for each of the flasks, with the two doses adjacent in the series.

The samples are then left to stand in the dark at 200C for the required contact time after which the concentration of residual chlorine is measured by the DPD/FAS titration method.

The chlorine demand is calculated as being the difference between the amount of chlorine in the original dose and residual chlorine concentration.

The results from the titrations are averaged to obtain the demand.

NOTE: If 50.0ca 3 sample used Residual 2 x Titre Calculation and Expression of Results 19 From the titration, amount of chlorine is read directly from the titre FAS titrant: 1 mL FAS 100 ug Cl as Cl 2 Therefore for 100 mL sample 1.00 mL standard FAS titrant 1.00 mg/L available residual chlorine.

Results are quoted to one decimal place.

Example Resin 1 Magnetic polymer beads were prepared in accordance with the process of the 10 copending application in the name of CSIRO and ICI using the following raw materials: 1. Water: this is the continuous medium in which the organic phase is dispersed and then reacted.

15 2. Gosenhol GH 17: this is a high molecular weight polymeric surfactant, a polyvinyl alcohol, that disperses the organic phase in the water as droplets.

3. Terice N9: this is a low molecular weight surfactant that is added to further reduce the particle size of the dispersed organic phase.

9 4. Cyclohexano this is the major porogen: it is a solvent for the monomers, but a non-solvent for the polymer, and it promotes the formation of voids and internal porosity in the resin beads.

5. Dodecanol: this is the minor porogen.

6. Solsperse 2400Q it is a solid phase dispersing agent and is a block copolymer of poly(hydroxystearic acid) and poly(ethyleneimine).

7. Pferrox 2228HC y-Fe 2 P, gamma iron oxide (maghemite). This is the magnetic oxide that makes the resin beads magnetic.

20 8. DVB-50 (divinyl ben.hene): this is the monomer that crosslinks the beads.

9. GMA (glycidyl methacrylate): this is the monomer that is first polymerised to incorporate it into the beads, then it is quaternized to place quaternary amrm''ium groups into the beads, thereby creating the ion exchange sites: polvmen zation AIBN, hear quatem azation -N HCI see* 0 0 so*** 0. 0 0> In 0 0 HO C1

N

0 15 10. AIIBN: this is the catalyst that initiates polyrnerisation when the mixture is heated above 501C.

11. Trimethylarnine: this is the amine that reacts with the epoxy group of the glycidyl methacrylate to form quaternary ammonium ion exchange sites.

12. Hydrochloric acidk this is used to neutralise the high pH due to the trimethylamine.

13. EthanoL this is used as a rinse and as a wetting agent.

Method Water (6.3L) was charged to a 20L reactor and the stirrer and nitrogen purge started. Next Gosenhol *8 GH-17 (30g) and Teric 0 N9 (l5g) were added, and the water phase heated to W0C to dissolve the surf actants. While the water was heating cyclohexanol (1755g) was charged to a separate stirred mix tank and the stirrer turned on. Dodencanol (195g), SOLSPERSE 24000 (63g), Pferrox 2228 21 H"IC y-Fe20 3 (936g), divinylbenzene (410g), and glycidyl methacrylate (1541g) were added in turn. This mixture was stirred and sonicated for one hour.

Azoisobutyronitrile (8g) was added and the mixture was stirred for a further five minutes before adding it to the heated water phase. The resulting dispersion was held at 801C for two hours, during which time polymerisation occurs and the solid resin beads (4.17kg) were formed. The nitrogen purge is then stopped and the trimethylamine and the hydrochloric acid are added to aminate the resin. These two materials can either be pre-mixed (with great caution due to the exotherm), or added in such a way as to maintain the pH between 6 and 8. The reaction mixture is then held at 80°C for three hours. The mixture is then cooled to room temperature, and the beads separated from the excess y-Fe 2

O

3 by repeated cycles of washing, settling and decanting (the beads settle much faster than the free oxide particles). The resin beads are then filtered, redispersed in ethanol, then filtered and washed with additional ethanol, then acetone, and dried with an air stream.

Photomicrographs of the polymer beads produced by this example are shown in Figures 1A and lB. As can be seen, especially from Figure 1B which is a photomicrograph of cracked beads, the solid particles are evenly dispersed throughout the polymer beads.

*Q

The maghemite was well dispersed throughout the resin beads produced in this S"Example Example Resin 2 Magnetic polymer beads were prepared in accordance with the process of the copending application in the name of CSIRO and ICI using the following raw materials: 1. Water. this is the continuous medium in which the organic phase is dispersed and then reacted.

2. Gosenhol GH 20. this is a high molecular weight polymeric surfactant, a 22 polyvinyl alcohol, that disperses the organic phase in the water as droplets.

3. Cyclohexanol this is the major porogen: it is a solvent for the monomers, but a non-solvent for the polymer, and it promotes the formation of voids and internal porosity in the resin beads.

4. Toluene: this is the minor porogen.

Solsperse 24000 it is a solid phase dispersing agent and is a block 10 copolymer of poly(hydroxystearic acid) and poly(ethyleneimine).

6. Pferrox 2228HC y-Fe 2 0 3 gamma iron oxide (maghemite). This is the magnetic oxide that makes the resin beads magnetic.

15 7. KRATON D1102 this is a low molecular weight rubber, incorporated into the organic phase to toughen the polymer beads.

8. DVB-50 (divinyl benzene): this is the monomer that crosslinks the beads.

20 9. GMA (glycidyl methacrylate): this is the monomer that is first polymerised to incorporate it into the beads, then it is quaternized to place quaternary ammonium groups into the beads, thereby creating the ion exchange sites.

VASO 67: this is the catalyst that initiates polymerisation when the mixture is heated above 50 0

C.

11. Trimethylamine this is the amine that reacts with the epoxy group of the glycidyl methacrylate to form quaternary ammonium ion exchange sites.

12. Hydrochloric acid: this is used to neutralise the high pH due to the trimethylamine.

23 Method Water (2333g) was charged to a 5 L reactor and the stirrer and nitrogen purge started. Next, Gosenhol GH20 (10g) was added, and the water phase heated to 80'C. While the water was heating Toluene (130g), DVB-50 (130g) and a first portion of Cyclohexanol (130g) were charged to a separate mix tank and the stirrer turned on. The Sotsperse 24000 (21.8 4 g) and the Pferrox 2228 HC y-Fe 2

O

3 (325g) were added in turn, then the mixture was stirred and sonicated for 20 minutes to thoroughly disperse the magnetic oxide. Kraton D 1102 was then added and the mixture stirred for a further hour to dissolve the toughening agent. The remaining Cyclohexanol (390g) and the VAZO 67 (2.65g) were then added and the mixture was stirred for a further five minu...s before adding it to the heated water phase.

The resulting dispersion was then stirred and held at 80 0 C for two hours. The nitrogen purge was stopped and a mixture of triinethylaniine (687g; 25% w/w) and -hydrochloric acid (294 g; 36% w/w) added, then the mixture was then stirred and held at 80'~C for a further three hours. The mixture was then cooled and the resulting polymer beads cleaned as in Example 1. Photomicrographs of the beads are shown in Figures 3A and 3B. Again, the solid magnetic oxide is well dispersed -throughout the beads, and the beads are qualitatively tougher than those of 20 Example 1. Further, the size distribution of the polymer beads was relatively narrow.

Example 1 Raw water was obtained from the Myponga Reservoir, South Australia. The raw water was pumped into a stirred vessel and was dosed with resin manufactured according to Example Resin 1 at a rate of 2.6m1 of wet resin per litre of raw water.

Resin and water were stirred in a flow through system for an average time of minutes before settling for 10 minutes in a plate settler. The water passed up through the plate settler and the clarified water overflowed for collection. The temperature of the water during this process was in the range of from 14 to 16 C.

24 In the continuous process resin was recycled maintaining the 2.6 ml of wet resin per litre of raw water dose rate. 90% of the resin was recycled without regeneration.

The remaining 10% was sent for regeneration (see Example 2).

The raw water and resin treated water were subjected to Standard Jar Tests.

Analyses including DOC, UV absorption and iron were also undertaken. The results of the jar tests on the resin treated water are set out herein in Table 1 and jar tests on raw-water are set out herein in Table 2.

to

I.

4•

S

S S 'a S .0 S S S *S *5 -s 55. S .5 S 555 Table 1

DOSE

tng/L

FLOC

SIZE

mm UNFI LTERED

FILTERED

*1 I Turbidi ty

NTU

Turbidity

NTU

Colour

HU

t t t .9 Resin Treated -2 -2 -3 -3 -4 2.3 2.9 1.1 0.9 0.9 0.6 0.6 7.9 7.6 7.4 7.3 7.2 7 6.9 1.2 1. 1 0.2 0.12 0.13 0.11 0.11 Ultraviolet Absorbance (254 nm) 0.217 0.165 0.073 0.064 0.061 0.061

DOC

ing /L Total Aluminium mg /L 4.7 f0.068 t 0o.637 4.6 3.5 3.3 3.2 3.1 0.563 0.084 0.052 0.042 0.035 0.355 0.026 0.016 0.016 0.015 Total Iron mg/ L I z 1 0.

b I [_______iiiiiiiiiiiiiiiiii::ii 0.024 _0.012 0* ,s e U U U

US

U. Ut U

U

U S U S U*U *U '1 UU* U U as.

U

U *U Table 2 Table 2

ALUM

DOSE

mg/L

FLOC

SIZE

mm

UNFILTERED

FILTERED

I UNFI LTERED Turbidity

NTUJ

Turbidity Colour

HU

Ultraviolet Absorbance (254 nm)

DOG

Total Alumin- Total f i iNTU Raw Water 1.4 2 4.5 3.6 2.5 2.8 7.9 0.9 119 mg/L ium Iron mg

L

mg

L

-2 -2 -2 7.4 7.2 7.1 7 6.9 1.6 3.5 0.8 0.2 0.22 118 120 31 0.522 0.505 0.252 10.6 10.*4 1.81 2.36 0.718 0.645 10 0.127901 10 J .175.4 0.077 0.013 10 j 0.109 4.8!.6 .1 2.7 6.7 0.21 27 Example 2 The resin taken for regeneration from the process described in Example 1 was regenerated under laboratory conditions. A sample of 10 ml of loaded resin was added to 400 ml 1M sodium chloride and mixed at flash mix speed (200 rpm) over minutes at room temperature (20 The extent of the resin regeneration was measured by monitoring the increase in the ultraviolet absorbance of the regeneration solution. Ultraviolet absorbance was 10 measured at 254 nm and the results are shown at Figure 1.

Example 3 4** River Murray water sampled at Mannum, South Australia was treated with varying 15 resin concentrations under the following laboratory conditions: Water temperature during the run was 21 C.

Resin used was manufactured according to Example Resin 1.

Contacted resin and water by stirring at 100rpm for 10 minutes.

Resin removed by settling for 10 minutes and passing clarified water through a 30pm screen prior to Jar Testing. Under Direct Filtration Conditions.

-28- The results of Jar Testing under Direct Filtration Conditions are shown in Table 3.

Table 3 Alum Resin Bulk Density Dose ml resin/L water Colour Turbidity mg/l iml 2ml 3m1 1l 2ml 3ml 0 75 31 25 12 11 12 12 12 12 21 12 12 15 23 5 13 10 0.88 L 20 32 8 3 11 2.1 0.24 St.

*9*S S S S. p a 5s 4 S S

S

*5*9 4.s p. 9* a, Example 4 Water was sampled from the Millbrook Reservoir, South Australia and was treated with varying resin concentrations under the following laboratory conditions: Water temperature during the run was 14.5*C.

Resin used was manufactured according to Example Resin 2 20 Contacted resin and water by stirring at 100rpm for 10 minutes.

Resin removed by settling for approximately 20 minutes and clarified water decanted.

Jar Testing Under Direct Filtration Conditions was performed. The flocculation time however, was 9 minutes at The results of Jar Testing Under Direct Filtration Conditions are shown in Table 4.

4** 9 9 9..

ft...

4* 9 9* 49 3 4 9 4 4 .9 9. 3 4 4 4 94. 9 4 9* 4 *44 Tablie 4 Chemical Additives unfilr' M±ered Physical Chemical Properties tered I I I Y Alum Resin (mL/L) Turbidi ty Turbidity Colour UVabs (/cm,

DO

(NTU) (HIJ) (mi I I I t 4 L I raw 29.0 28.0 31.0 36.0 41.0 41.0 45.0 6.7 6.9 6.9 6.8 7.0 6.8 6.4 21.00 23.00 27.00 28.00 11.00 1.53 0.68 74.0 70.0 66.0 45.0 20.0 11.0 8.0 0.465 0.437 0.420 0.337 0.224 0.164 0.134 1 1 1 C =TMFP Al Fe 0.8 182 1.530 1.160 0.2 2.140 1.180 0.2 3.010 1.280 1.8 3.300 1.140 1.0 1.420 0.386 1.80.274 0.047 1.8 107 0.147 0.018 1.3 0.198 0.016 .3 163 1.640 1.200 1.9 2.210 1.180 1.4 2.700 1.110 1.91.660 0.536 10 40 0.207 0.046 1.4 .090 0.012

'I

4 4 4.

L

1 29.0 II 29.0 32.0 ml 37.0 II 34.0 6.7 6.4 6.4 6.8 6.7 22.00 24.00 26.00 14.00 1.20 6.0 0.330 0.309 0.278 0.157 0.111 37.0 6.5 0.40 I A ~V0Q4 9 9** 9.9 9 C 99 999 9 9 4** 9. 9 9..

9..

9 9 9 9 99.

999 *9 .9 9.

9 99. 9 9 9 9 *999 99 9. 9. 9 9 999 9 9 4 9 9 9 9 9. 9 9*9 Table 4 Cont I I

Y

Chemical Additives Unf il- Filtered Alum Resin ITurbid- pH Turbid- Colouru (mL/L) ity J ity

I(HU.)

j J(NTU) 12 28.0 27.0 29.0 33.0 33.0 7.2 7.4 7.4 7.4 7.3 21.00 22.00 23.00 22.00 0.94 I. I L I 0 3 28.0 #127.0 29.0 31.0 29.0 29.0 7.3 6.9 7.5 7.4 7.0 21002 21.00 37 21.00 34 2.00 24 2.40 7 0.37 3 Physical Chemical .Properties rVabs DOC THMFP Al Fe /cm, (mg/L) (ug/L) (mg/L) (mg/L) 5:4nm) 0.234 6.4 55 1.550 1.070 0.220 7.2 1.830 1.050 0.210 6.3 2.180 1.080 0.120 5.5 2.340 0.877 0.072 4.9 55 0.152 0.038 00 4.1 0.094 0.012 0.180 5.6 1.570 1.070 0.167 4.7 1.760 1.020 0.141 4.7 12.050 1.020 0.070 3.7 0.384 0.147 004 3.2 0.105 0.070 0.0141,6,11 3.1 0 0.061 0.017 7.0 0.25 2 I I I I I 31 Example Water sampled at North Pine Dam, Brisbane, Queensland was treated with varying resin concentrations under the following laboratory conditions: Water temperature during the run was 19 0

C.

Resin used was manufactured according to in Example Resin 2.

Contacted resin and water by stirring at 100rpm for 10 minutes.

Resin removed by settling for about 20 minutes and decanting the clarified water prior to Jar Testing under Direct Filtration Conditions.

The Jar Testing under Direct Filtration Conditions was performed. However, Ithe flocculation time was 9 minutes at 40rpm. The results of the Jar Testing under Direct Filtration Conditions are shown in Table 4i 4 a 4 4.

4 9 999 99999 9.

9 4 994 9999 9 9999 999 9. 9.

9* 99 9 9 9 9 9 *999 9. 9. 9S 9 9 999 9 9 999 9 9 99 9 *9t Table Chemical Additives Unfiltered Filtered Filtered -I t I Alum Resin (mL/L) Turbidity

(NTU)

Turbidity NTU Colour

(HU)

raw 0 1.8 7.6 0.28 7.5 0.28 16 7.4 0.25 15 7.4 0.14 10 7.6 0.08 8 7.2 0.14 8 7.1 0.08 7 7.0 0.06 5 6.9 0.06 7 0 0.5 1.0 7.5 0.31 13 7.4 0.29 12 7.4 0.12 8 7.3 0.13 10 7.2 0.09 5 7.2 0.08 6 0.05 6 Physical Chemical Properties UVabs DOC THMFP Al Fe (mg/L) (ug/L) (mg/L) (m/L) 2 54nm) 0.120 4.5 182 <0.005 0.053 0.116 4.5 3 0.331 0.061 0.088 3.9 0.414 0.047 0.076 3.7 0.192 0.038 0.07 3.7 5 0.108 0.030 0.066 3.3 0.074 0.034 0.057 3.0 0.063 0.037 0.054 2.8 0.039 0.062 0.09254 2.8 84 0.030 0.025 0.092 3.7 118 0.009 0.030 0.074 3.3 0.329 0.025 0.068 3.1 0.180 0.028 0.061 3.0 0.122 0.029 0.052 2.8 0.074 0.019 0.049 2.8 0.060 0.086 0.0671 3.2 105 <.005 0.023 0.052 2.7 0.303 0.017 0.046 2.5 0.142 0.012 0.043 2.5 0.096 0.014 0.040 2.2 0.075 0.021 0.038 2.2 0.057 0.018 0.050 0.024 1.1 7.5 7.4 7.4 7.3 7.2 7.2 7.1 0.27 0.26 0.08 0.10 0.07 0.07 0.06 7. 1 0.06 9 9*~ .9 9.

9* 99. 9 9..

9 9 9*t 9 9 9** 9** *0 99 9 9 9 .0 9 9 9 9** 9* 9 Table 5 cont...

If If If Chemical Unf ii- Filtered Physical Chemical Properties Filtered Additives 1

I

Alum Resin (mL/L) Turbidity pH Turbid- Colour UVa ity

(HU)

(NTU) I-I I I 7.4 7.4 7.3 7.2 7.1 7.1 0.32 0.16 0.06 0.07 0.04 0.05 *1 I~ I.

0.c 0.i 0.I 0.4 0.c 0.c bs DOC THMFP Al

F

M, (mg/L) (Ug/L) (mg/L) (mg/L) nm) 045 2.4 72 001 039 2.3 0.2025 0.022 )29 2.1 0.113 0.013 )29 2.0 0.071 0.042 )27 .0 0.052 0.017 )26 1.9 0.046 0.016 J261.70.034 0.014 234 JL.a5 <.005 0.018 )241.50.151 0.020 )201.40.093 0.009 )201.30.062 0.011 )20 1.3 0.055 L.005 209 1.5 0.038 0.008 119 13 5 0.30 L.0 ,3 0u3JO L0000 8 0.9 7.4 7.3 7.2 7.1 6.9 0.25 0.07 0.04 0.05 0.04 6.8 0.04 I I~I 0.04 34 Example 6 Water sampled at Lexton Reservoir, Victoria was treated with varying resin concentrations under the following laboratory conditions: Water temperature during the run was 19 0

C.

Resin used was manufactured according to in Example Resin 2.

Contacted resin and water by stirring at 100rpm for 10 minutes.

Resin removed by settling for about 20 minutes and decanting the clarified water prior to Jar Testing under Direct Filtration Conditions.

The Jar Testing under Direct Filtration Conditions was performed. However, the flocculation time was 9 minutes at 40rpm. The results of the Jar Testing under Direct Filtration Conditions are shown in Table 6.

9 *9*9 9..

.9 9 9*9 9 .9.

9 9 9999 9 9.9 9*9 9* *9 99 9 9 9 9 9999 9. *9 9 9 99. 9*9 9 9 9 99~ 9 9 99 9 9.9 Table 6 T 1

T

Chemical Additives Un f ii Filtered Physical Chemical Properties tered 1* t Alum Resin (mL/L) Turbidity Turbidi ty Colour

(HU)

UVabs (1cm, (NTU) (NTU) flY' I 20.0 raw 8.0 8.0 7.9 7.8 7.8 7.7 7.7 9.20 9 .50 10.40 10.50 9.20 6.10 2.00 159 154 156 162 140 99 50 0.593 0.580 0.580 0.582 0.518 0.416 0.314 7.7 of of of of if 12.7 7.6 7.6 7.5 7.5 7.5 8.60 9.30 7.30 0.86 0.45 119 140 114 31 24 29 0.457 0.446 0.386 0.220 0.195 DOC THMFP Al Fe (mg/L) (ug/L) (mg/L) (mg/L) 11.4 243 0.812 0.652 11 .11 90 6 80.5 142.674 0.548 98 1.400 0.3927 7.3 1.390 0.261 6.2 0.488 0.077 5.1 0.259 0.037 59 0---0320 027 7.4 0.29 I t t I It 14.0 7.6 7.6 7.6 7.6 7.7 9.00 9.00 6.90 1.68 0.61 121 129 98 39 25 0.412 0.405 0.335 0.219 0.181 7.7 0.54 21 I I 9 9.9.

990 99 9 99 999 9 9 .99.

9 9 9.. 9 9 .99 *9 99 9 9 99 9.

9 9 9 9 9 9. 09 99 9 999 *90 *99 9 9 9 9 9 *09 Table 6 Cont..

I

Chemical Additives IUnf il- Filtered Physical Chemical Properties Alum 1Resin ITurbid- 1 pH Turbid- Colour (mL/L) ity J__ity

(HU)

13.1 7.6 7.8 7.7 7.7 7.6 6.40 6.60 5.80 0.64 0.20 87 87 77 19 LlVa (Ic *254 0.: 0.: 0.: 1.: 7.6 03 if 76 6.40 106 3f 7.3 6.10 73 0.

of7.4 0.19 7 0.c 7.4 0.14 6 0. C bs DOC TIMFP Al Fe M, (Mg/L) (ug/L) (mg/L) (gL nm) (gL 301 6.6 189 0.655 0.496 298 6.4 1.230 0.491 270 6.2 1.560 0.422 137 4.6 0.367 0.077 107 4.2 0.170 0.026 )93 3.8 0.109 0.017 ~30 5.3 77 0.744 0.589 ~24 5.0 1.290 0.522 4.3 0.651 0.158 )79 3.9 0.193 0.043 ~68 3.7 0.127 0.029 ~61 3.4 0.112 0.022 88 4.4 55 0.708 0.546 0 4 11.1 7.5 6.30 460 n1. 7.

37 Example 7 Water sample at of Wanneroo Ground Water, Western Australia was treated with varying resin concentrations under the following laboratory conditions: Water temperature during the run was 19°C.

Resin used was manufactured according to in Example Resin 2.

Contacted resin and water by stirring at 100rpm for 10 minutes.

Resin removed by settling for about 20 minutes and decanting the clarified water prior to Jar Testing under Direct Filtration Conditions.

The Jar Testing under Direct Filtration Conditions was performed. However, the flocculation time was 9 minutes at 40rpm. The results of the Jar Testing under Direct Filtration Conditions are shown in Table 7.

o* 0 *0 •l 9*O C 0 eel Tablb 7 Chemical Additives Unf il- Filtered Alum Resin Turbid- pH Turbid- Colour (niL/L) ity ity

(HU)

(NTU)

raw 0 33.0 7.5 10.70 184 to7.5 11.30 190 of7.3 10.40 202 of7.3 9.00 156 40 It7.2 2.10 41 7.1 1.60 27 7.1 1.54 26 1 0.98 1 18

$I

of of of of 31.0 7.5 7.5 7.4 7.3 7.3 10.00 9.80 9.60 2.10 1.80 182 175 172 40 31 Physical Chemical Properties ;UVabs IJOC THMFP Al Fe (1cm, (mg/L) (ug/L) (mg/L) ('ng/L) -254nn) g) 0.481 7.0 395 0.288 1.145 0.468 7.0 0.867 1.210 0.463 6.8 0.564 1.210 0.379 6.0 1.69 0.831 0.150 3.8 0.185 0.167 0.116 3.4 0.122 0.116 0.103 2.9 0.133 0.105 0.082 2.7 1300. 7 0 0 7 0.408 6.0 33 0.322 1.215 0.398 6.3 0.917 1.180 0.396 5.2 11.480 0.183 0.147 3.6 0.199 0.154 0.110 3.0 0.110 0.121 0.095 2.6 144 0.124 0.121 0.352 44. 294 0.282 1.185 0.337 4.9 0.882 1.080 0.286 3.7 0.341 0.917 0.088 2.7 0.117 0.059 0.072 2.4 0.086 0.052 0.7 22114 0.100 0.084 742 28.0 7. 1 6.8 6.8 11.30 8.90 9.00 0.68 0.68 183 159 154 17 15 6.8 1.21 h~I

II

19 S.

S

U

Sb S S S S S

S

55e *5 55 S S 5955 5* @5 Se 5 S p 5 S SO 9 *5 5(5 Table 7 Cont Chemical Unf ii- Filere Physical Chemical Properties Filtered Additives 4 I

I

Alum Resin (niL!L) Turbidity Turbidity IColour

(HU)

(NTU)

1~ 26.0 7.5 7.4 7.3 7.2 12.00 9.60 0.80 0.76 0.46 177 157 18 13 10 I 4-4--

I

25.0 7.2 7.3 7.4 7.4 11.50 9.40 0.33 0.22 161 148 9 UVabs DOC T H MF =A Feg) (mg/L) (ug/L) (mg/L) (m/L 2 54nm) 0.296 3.7 272 0.316 1.160 0.281 3.6 0.814 0.964 0.081 2.2 0.180 0.116 0.057 1.8 98 0.086 0.050 0.046 1.6 0.065 0.037 0.039 1.6 0.045 0.020 0.4 30183 0.274 1.070 0.232 2.7 07 0.3 0.048 1. 70.407 0. 044 0.035 1.5 0.0 0 044 0.030 1 50.0 43 0.02 3 0.210 2.4 169 0.263 0.950 0.204 2.4 0.581 0.919 0.193 2.0 0.646 0.584 0.043 1.4 73 0.119 0.3 0.033 1.3 081 0.039 0.025 1.1 0.047011 0.184 1.8 152 0.268 0.925 0.172 1.8 6 3 0.081 1.3 0.67 0.8 0.027 1.1 51 0.210 0.278 0.023 1.0 0.1069 0.020 0.019 10 0.040 0.023 0.30 0 4 27.0 7.7 11.80 157 17.7 10.80 148 to7.6 9.10 128 it7.6 0.28 7 of7.5 0.28 6 0.24 4 0 26.0 7.6 7.6 7.6 7.5 7.4 12.20 10.30 3.60 0.21 0.20 157 136 51 5 7.4 0.32 a a 3 3 Example 8 Water sampled at Happy Valley Reservoir, South Australia was treated with varying resin concentrations under the following laboratory conditions: Water temperature during the run was 18°C.

Resin used was manufactured according to Example Resin 7.

Contacted resin and water by stirring at 100rpm for 10 minutes.

Resin removed by settling for approximately 20 minutes and decanting clarified water prior to Standard Jar Testing.

The Standard Jar Testing was performed except that the coagulant used was ferric chloride at varying dosages. The results of the Standard Jar Testing are shown in Table 8.

0* 0 *ooo 4* t 4~ C- S Table a Table 8 Ferric Chloride Dose mg /L Floc Size Unflteredi Filtered I y Turbidity

NTU

Turbidity Colour

HU

Ultraviolet THF DTC Total Total ug/L mg/L Aluini- Iron nium mg/L ig IL I I I I (254nm) Raw Water T i I I r 5.7 5.9 6.3 7.4 9.1 10.7 3.8 7.2 7.0 6.8 6.7 6.5 6.4 6.2 6.0 6.2 3.70 3.80 4.10 4.90 4.40 0.78 0.48 0.35 0.23 0.289 0.370 0.429 0.390 0.222 0.134 0.108 0.084 0.076 159 159 274 132 141 87 58 47 57 21 7.2 7.6 6.8 7.2 6.0 5.4 4.9 4.8 4.5 0.328 0.302 0.303 0.283 0.185 0.087 0.027 0.044 0.02 0.298 1 .590 2.790 3.930 3.360 0.572 0.267 0.211 0.139 1.7 6.3 0.22 Y

I

<1 1ito 2 to 2.70 3.20 4.20 5.70 2.50 1 .54 7.2 7.2 ResinTreated Water (InL/L) I 2.20 35 0.182 2.40 52 0.261 3.30 14 0.119 I 0.76 7 0.089 0.41 5 0.078 0.32 4 0.068 0.23 2 0.0354 4. 0.03 0.3 211 4.8 0.264 0.282 237 4.7 0.275 1.65 195 4.6 0.243 2.65 128 3.9 0.107 0.570 118 3.5 0.037 0.235 124 3.3 0.033 0.156 2 to 0.65 7.2 9*# 0 0 0** 0 0 0** 0** 0 0

S

0** 0* S 0* *5

'S

000

S

S V. Table 8 Cont...

Ferric Chloride Dose ing /L Floc Size Unfiltered Filtered Unfiltered *1

I

Turbidity

NTU

Turbidity

NTU

Colour Ultra- TIIMFP DOC Total Total violet ug/L mg/L Alumi- Iron Absorb- nium m/ ance gL g/ (254rn) g/ T

I

LO

0 2 3 to 4 3 to 4 3 to 4 3 to 4 6.60 4.90 1.00 0.60 0.38 0.34 7.

7 7.( 7.1 7. 7.2 7.( 3.30 13 0.069 0.25 <1 0.040 0.11 <1 0.033 0.10 <1 0.032 0.09 <1 0.031 0.09 <1 0.030 0.10 0.028 52 3.8 0.284 0.238 55 3.1 0.079 0.077 14 2.5 0.031 0.023 16 1.8 0.022 0.027 12 1.9 0.018 0.032 24 1.9 0.018 0.044 9 1 9 00 1 9 0 0 4 3 to 4 0.32 7.C am m 43 Example 9 Water sampled at Myponga Reservoir, South Australia was treated with resin and the loaded resin contained approximately 6 milligrams DOG per ml of we[ resin. The loaded resin was then subjected to a number of regeneration methods employing brine solutions having varying concentrations of sodium chloride. The resin used was manufactured according to in Example Resin 1.

99In the first method the loaded resin (5S0ml) was dispersed in a sodium chloride at varying molar concentrations In the second method a 20 0m.] column was packed with loaded resin (50ml) and the sodium chloride solutions (lO0rnI) were placed on top of the packed resin and the resin and sodium chloride solution were mixed thoroughly by sparging nitrogen through the columri. In the third method a 2 0 0rnl column was packed with loaded resin (IS0mI) and the sodium chloride solutions (lO0mI) were placed on top of the packed resin. The sodium chloride solutions were allowed to pass through the packed resin.

The resultant sodium chloride solutions were measured for UV absorbance and DOC. The results are shown in Table 9 and 10 and the higher organic content of the regenerant solution demonstrates the particular effectiveness of employing a packed column to regenerate the resin.

.44- Qptiniising Regeneration With Columns Table 9 to...

to..

Regen~eration Ultraviolet Absorbance Method S odium Chloride Sodium Chloride Molar 1.5 Molar Stirred 24 hours 15.40 19.80 Column 15.60 23.80 (mixed by aeration)_ Column 24.10 29.80 (no mixing) Table Method' UV Absorbance

DOC

___mg Column 21.4 (mixed by aeration) Column 29.9 (no mixing) *Employed 1.5 Molar Sodium Chloride 45 Example Water sampled from the Myponga Reservoir, South Australia was treated with varying resin concentrations under the following laboratory conditions: Water temperature during run was about Resin used was manufactured according to Example Resin 1.

Contacted resin and water by stirring at 100rpm for 10 minutes.

Resin removed by settling for approximately 20 minutes and decanting S. clarified water. The clarified water was measured for UV absorbance and 10 DOC. Chlorine demand tests and TI-IMFP tests were subsequently conducted on the clarified water. The results are shown in Table 11.

Example 11 River Murray water sampled at Mamnun, South Australia was treated with varying resin concentrations under the following laboratory conditions: Water temperature during run was about 201C.

Resin used was manufactured according to in Example Resin 1.

'.:Contacted resin and water by stirring at 100rpm, for 10 minutes.

Resin removed by settling for approximately 20 minutes and decanting clarified water. The clarified water was measured for UV absorbance and DOC. Chlorine demand tests and THMIFP tests were subsequently conducted on the clarified water. The results are shown in Table 12.

46 Table 11 000900 0 0* *4 *Oat Resin Ultraviolet DOC Chlorine THMfFP Dose Absorbance Demand m-L/L 254nm mgIL mg/L ug7/L 00.320 8.1 41397 1 0.181 5.1 2.6 207 2 0.125 3.9 1.7 156 3 0.084 3.0 1.0 1 117 Table 12 Resin Ultraviolet DOC Chlorine THMIFP Dose Absorbance Demand mL/L 254nxn mg/L mg/L ugfL 0 0.103 4.4 3.0 21 2 1 0.057 3.1 2.0 135 2 0.041 2.7 1.5 102 3 1 0.028 2.3 1 1.5 1

S

0*aa a Sat.

a a a a 4.

*9 47 Example 12 Treated effluent from the Handoff Sewage Treatment Works was treated with varying resin concentrations under the following laboratory conditions: Water temperature during run was approximately Resin used was manufactured according to Example Resin 2.

Contacted resin and watg; by stirring at 100rpm for 10 minutes.

Resin removed by settling for approximately 20 minutes and decanting clarified water.

a a

U

a. a o a a. a a The clarified water was then measured for UV absorbance and DOC. The results are shown in Table 13.

Table 13 Resin Ultraviolet DOC Dose Absorbance mL/L 254nm mgIL 0 0.164 1 0.131 2 0.109 3 10.0921 Examnplel13 Water sampled at Happy Valley, South Australia was subjected to membrane filtration in combination with resin treatment.

The membrane filtration unit was operated at lO0kpa at a flow rate of 5 litres per hour. The temperature of the water was about 20T 0 The effectiveness of the membrane filtration was measured on raw water and on water treated with resin under the following laboratory conditions: Water temperature during run was about -48- Resin used was manufactured according to Example 4.

Contacted 4 mL/L of wet resin and water by stirring at 100rpm for minutes.

Resin removed by settling for about 20 minutes and decanting clarified water.

The results of measurements of pH, turbidity, colour, UV absorption and DOC are shown in Table 14. It can be seen that the combination of resin treatment prior to membrane filtration results in acceptable water quality without the need 10 for additional chemicals such as coagulating agents and the like.

able 14 Table 14 9* e g 5

*S*S

a.

a 15 Analysis Raw Water Resin Treated Before After Before After Membrane Membrane Membrane Membrane pH 7.8 8.2 7.8 8 Turbidity (NTU) 5.20 0.37 5.20 0.32 Colour (HU) 60 32 12 UVabs 0.276 0.197 0.067 0.048 DOC Example 14 Some waters are prechlorinated prior to the water treatment process. Water sampled at Myponga Reservoir, South Australia was prechlorinated with varying doses of chlorine under the following laboratory conditions: Water treatment during the run was about The prechlorination occurred over 16 hours in the dark.

The prechlorinated water was treated with 1 millilitre of wet resin per 2 litres of prechlorinated water under the following laboratory conditions: Water temperature during the run was about 49 Resin used was manufactured according to Example Resin 1.

Contacted resin and water by stirring at 100rpm for 30 minutes.

Resin removed by settling for about 20 minutes and decanting clarified water.

The clarified water was measured for colour, UV absorption and DOG and the results are shown in Table 15. These results show that the process is also effective for removing chlorinated DOC from solution.

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eq..

em C. Ce *C C

C.

me

C

C

em C

C

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Table Prechiorination Colour UVabs DOC Dose 15 mg/L HU 0 mgfL 49 0.321 7.7 -3 11 39 0.274 6 "32 0.246 9 "29 0.229 7.8 20 0 mgfL resin 27 0.158 4.8 3 "118 0.136 13 0.119 4.9 9 ""17 0.115 4.8 It will be appreciated that the invention described herein is susceptible to variations and modifications other than those specifically described. It is to be understood that the invention encompasses all such variations and modifications that fall within the spirit and scope. For example, the present process may be employed for the removal of contaminants other than DOG from water. It may be necessary to select an ion-exchange resin with anionic funictional groups.

Claims (26)

1. A process for the removal of dissolved organic carbon from water, which process includes the following steps: a. adding an ion-exchange resin to water containing dissolved organic carbon; b. dispersing the resin in the water to enable adsorption of the dissolved 10 organic carbon onto the resin; and i c. separating the resin loaded with the dissolved organic carbon from the ."water.

2. A process according to Claim 1 wherein the resin is dispersed by mechanical agitation, mixing pumps immersed in the water or air agitation.

3. A process according to either Claim 1 or Claim 2 wherein the loaded resin is separated from the water by settling, screening or a combination thereof.

4. A process according to Claim 3 wherein the loaded resin is separated from the water by settling and wherein the ion exchange resin is more dense than the water.

5. A process according to Claim 4 wherein the settled resin is collected by vacuum collection.

6. A process according to either Claim 4 or Claim 5 wherein the settling is facilitated by tilted plates or tubular modules.

7. A process according to any one of Claims 1 to 6 wherein the ion-exchange resin has cationic functional groups. I M 51

8. A process according to any one of Claims 1 7 wherein the ion-exchange resins is particulate and the particles have a diameter less than 100pm.

9. A process according to Claims 8 wherein the ion-exchange resins particles have a diameter in the range of from 25pm to A process according to any one of Claims 1 to 9 wherein the ion-exchange 0040e:resin is macroporous. 060 10 11. A process according to any one of Claims 1 to 10 wherein the ion- exchange resin is manufactured from cross-linked polystyrene based polymers.

12. A process according to any one of Claims 1 to 11 wherein the ion- t.0 exchange resin is present in the water in the range of from 0.5 to 5mi of wet -resin per litre of water.

13. A process according to any one of Claims 1 to 12 wherein the resin is t* recycled and regenerated. too.

14. A process according to any one of Claims 1 to 13 wherein the process includes the resin regeneration steps: a packing the spent resin into a column, b. passing brine through the packed columnn for desorption of the dissolved organic carbon from the resin. A process according to any one of Claims 1 to 14 wh~ich comprises a process for the removal of contaminants from solution wherein the ion-exchange resin is dispersed in the contaminated water.

16. A process according to any one of Claims 1 to 15 wherein the ion- 52 exchange resin is a magnetic ion-exchange resin.

17. A process for the removal of dissolved organic carbon fromi water, which process includes the following steps: a. adding a magnetic ion-exchange resin to water containing dissolved organic carbon; dispersing the resin in the water to enable adsorption of thle dissolved 10 organic carbon onto the magnetic ion-exchange resin; C. agglomerating the magnetic ion-exchange resin loaded with the dissolved organic carbon; and separating the agglomerated magnetic ion-exchange resin loaded with the dissolved organic carbon from the water. *18. A process according to Claim 17 wherein the magnetic ion-exchange resin -is dispersed in the water with sufficient shear to maintain the magnetic ion- exchange resin in a dispersed state.

19. A process according to either Claim 17 or Claim 18 wherein the loaded resin is separated from the water by settling, screening or a combination thereof.

20. A process according to Claim 19 wherein the loaded resin is separated from the water by settling and wherein the ion exchange resin is more dense than the water.

21. A process according to Claim 20 wherein the settled resin is collected by vacuum collection.

22. A process according to either Claim 20 or Claim 21 wherein the settling is 4 -53 facilitated by tilted plates or tubular modules.

23. A process according to any one of Claims 17 to 22" wherein the ion- exchange resin has cationic functional groups.

24. A process according to any one of Claims 17 to 23 wherein the ion- exchange resin is particulate and the particles have a diameter less than 100pm. A process according to any one of Claims 17 to 24 wherein the ion- 10exchange resini prteshavenatdiaeter in the range of from 5 to rsn.e..teo wtr 2. A process according to any one of Claims 17 to 25 wherein the reini rexchcean reneratredr.s 5 327. A process according to any one of Claims 17 to 26 wherein the io-s exchang te resin semanfai tueprmcos lnkdplsyee:ae oyes 2. a proesaccordih sngt anre o lis1o2 hrin theo ion-umn exhag re ssin g bsrntin therwaerg the age cofm fr 0esorton of whe

29. A procssolaccorngitocanyon foCms 17e to28weriiteneini -54-

31. A process according to any one of Claims 17 to 30 which comprises a process for the reproval of contaminants from solution wherein the Ion-exchange resin is dispersed in the contaminated water.

32. A process according to any one of Claims 1 to 31 wherein said process includes the additional step of disinfecting the water.

33. A process according to Claim 32 wherein the water is disinfected with ***chlorine. C.0. 9:34. A process according to any one of Claims 1 to 33 wherein said process is CC.. a pre-treatment prior to subjecting the pretreated water to membrane Filtration. A process according to any one of Claims 1 to 33 wherein said process is a pretreatment prior to subjecting the pretreated water to a coagulation /sedimnentation process.

36. A process according to any one of Claims 1 to 35 wherein the process ~.includes, the additional step of treating the water with activated carbon after treatment with the ion-exchange resin.

37. A process substantially as hereinbefore described with reference to any one of the foregoing Examples.