GB1583881A

GB1583881A - Water clarification

Info

Publication number: GB1583881A
Application number: GB18565/77A
Authority: GB
Original assignee: Commonwealth Scientific and Industrial Research Organization CSIRO
Current assignee: Commonwealth Scientific and Industrial Research Organization CSIRO
Priority date: 1976-05-03
Filing date: 1977-05-03
Publication date: 1981-02-04
Also published as: NL7704854A; JPS622843B2; NL190840B; NL190840C; CA1097605A; MY8200238A; FR2350303A1; DE2719529C2; JPS52135553A; DE2719529A1; FR2350303B1

Description

(54) WATER CLARIFICATION (71) We, COMMONWEALTH SCIENTIFIC AND INDUSTRIAL RESEARCH ORGANISATION, a Body Corporate established under the Science and Industry Research Act 1949, carrying on scientific and industrial research of Limestone Avenue Campbell, Australian Capital Territory, Commonwealth of Australia, do hereby declare the invention for which we pray that a Patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement: This invention is concerned with a method for removing suspended impurities and colour from water by coagulation and adsorption. The method involves the use of a material which gives more rapid and better clarification and decolourisation than the conventional alum treatment and uses only a small proportion of any of the usual amount of coagulant required for such treatments. In its preferred form, the invention utilizes magnetized or magnetizable material to facilitate the settling of the sludge and the recovery and re-use of the coagulant.

The currently standard process for the clarification and decolourisation of turbid waters and effluents involves a coagulation process followed by sand filtration. The water is mixed with an appropriate amount of an aluminium salt, or a ferric salt, (the coagulant) and adjusted to a pH were the metal forms insoluble, positively-charged hydrolysis products. For aluminium sulphate (alum), the optimum pH will range from 5 to 7, depending on the water.

Negatively-charged colloids in the feed water (e.g. bacteria, virus, clays, etc) and the natural colouring matter in water (humic and fulvic acids) become attached to and entrapped within the floc and settle with it. Settling normally takes place in a settling tank and residual floc in the overflow from the settling tank is removed by passage through a sand filter to produce a sparkling clear water. Once the pressure drop through the sand filter becomes excessive the bed is backwashed to remove the deposited floc.

In practice, the coagulation process is usually carried out in three distinct zones. First, the coagulant, and any acid or alkali required for pH adjustment, are rapidly mixed with the incoming feed water for a short time to form micro-flocs of the metal hydroxide. These are next gently agitated with the water to promote attachment of the colloids to the floc; excessive agitation is avoided as it dispersed the fragile flocs. Finally, the mixture passes to a settling zone where the flocs are settled out.

This prior art process has several problems: First, the flocs are fragile and do not settle rapidly so that a large residence time must be allowed in the settling tank and the equipment is correspondingly large. Even so, settling is never complete and the overflow must be clarified by sand filtration.

Second, chemicals are expended in forming the floc and account for the major cost of the process.

Third, the final sludge is not composed solely of the clays, etc. removed from the water but contains as well a much larger volume of the hydrous metal hydroxide. Not only does the disposal of this sludge create problems but it also entrains a substantial amount of water which is lost from the feed water.

There have been a number of attempts to improve settling rates. For example, a small amount of an appropriate linear polyelectrolyte flocculant can be added to create bridges between the flocs and thereby facilitate settling. An alternative is to add a finely divided solid to the feed water so that it becomes entrapped with the floc and, by raising its density, settling is facilitated. A variant of the latter is to use a ferromagnetic particle so that the floc can be removed by magnetic means; however, this does not reduce significantly the amount of coagulating chemical needed to produce satisfactory flocs.

The principal objects of this invention include the provision of a method for the clarification of water, and the removal of colour and micro-organisms such as bacteria, virus and algae, which eliminate the use of coagulant or at least enables the use of much less than hitherto to achieve a given degree of clarification, which produces a sludge which for the most part is composed of the particulate matter removed from the water and which accelerates settling of the floc. Other objects include the provision of such a method which facilitates removal by magnetic means and which eliminates the need for a sand filter.

We have found that three conditions must be met for the attachment of colloids to a particulate surface.

1. The surface should carry a charge of opposite sign to that of the colloids (as measured by zeta potential), 2. The surface must be such that the colloid can be held by multipoint attachment, and 3. The particle to which the colloids are to attach must be small. For example, an anoinic exchange resin, having the normal degree of crosslinking, will not absorb clay particles on to its surface to any signficant extent even though the clay has an opposite zera potential charge and the resin is very finely divided. Likewise finely divided magnetite has a positively charged surface but will only weakly absorb large colloids of opposite charge, such as clay for example.

However, we have found that if micron size particles are treated so as to produce a hydroxylated surface thereon (such a particle being referred to herein as a "gel particle") and are suspended in turbid water with the pH adjusted so that the particle surface has a positive zeta potential, then the negatively charged colloids normally present in natural waters and many effluents will readily attach to the surface. Provided sufficient gel particles are present to provide an adequate surface area then it is possible to effect substantial or even virtually complete removal of the colloids.

In accordance with the present invention, therefore, we provide a method for clarifying water by removing suspended impurities and coloured substances contained in it in which the water is contacted with a particulate mineral material to coagulate and absorb thereon the impurities and coloured substances (hereinafter referred to as a "coagulant/absorbent"), the individual particles of which coagulant/absorbent have a particle size of less than 10 microns and have been treated to produce a hydroxylated surface layer having a positive zeta potential at the adsorption pH (as hereinafter defined) and the thus treated water is then separated from the coagulant/absorbent.

As used herein the term "adsorption pH" means the pH of the water under treatment; it must be within the range of pH where the colloidal matter in the water retains some of its negative charge.

Embodiments of the invention will now be described and discussed in detail. Reference will be made to the accompanying drawings, in which: Figures la and ib are diagrammatic representations showing the effect of multivalent cations on the absorption of colloids by the hydroxylated surface of the gel particle; Figure 2 is a flow diagram showing a preferred method of water treatment in accordance with the invention.

Figure 3 is a diagram of a solids contact clarifier for use in the method of the invention.

Figure 4 is a diagram showing a preferred form of apparatus for carrying out the method of the invention.

The coagulant/absorbent materials used in the invention may be of two notionally different types: (I) those in which the hydroxylated layer is derived directly from the substance of the particles; and (II) those in which the layer is derived from another substance.

The preferred coagulant/absorbent materials are those of type I and these can be derived from a wide variety of minerals and clays provided the nature of the mineral is such as to permit the ready formation of the hydroxylated surface. In this respect oxides and silicates are particularly useful. Examples of such minerals include zinc oxide, and clay minerals such as mica, china clay and pyrophillite. This list is not exhaustive, however, and may other minerals are suitable for use in this invention.

In the most preferred embodiment of this invention, the particulate material should be a magnetic or magnetisable material. For this purpose iron oxides, such as gamma iron oxide or magnetite, which are eminently suitable, or ferrites, such as barium ferrite or spinel ferrite, can be used.

The particles should be preferably in very finely divided form in order to be fully effective in removing colloids from solution. The particles should be less than 10 micron in size, preferably l to 5 micron.

The preparation of the gel particles of type I is simply carried out, usually by suspending the particles in alkali solution for a short period of time, preferably in the presence of air. Sodium hydroxide is probably most suitable, but potassium hydroxide or aqueous ammonia may also be used. Generally. alkali concentrations should be at least 0.0 iN, preferably about 0.05N to 0. iN, at which level the treatment is effective after about 10 minutes. Shorter treatment times can be achieved by the use of elevated temperatures and/or higher alkali concentrations. A suggested temperature range is 40-60"C. For example, a satisfactory material is produced using either 0.1N sodium hydroxide at room temperature (i.e. about 20"C) for ten minutes, or 0.05N sodium hydroxide solution at about 60"C for five minutes.

Because the hydroxylated layer of the type II materials is provided by another substance, the range of starting materials is broader. A wide variety of minerals and clays can be used provided the nature of the mineral or clay is such as to permit the ready deposition of a hydroxide gel on its surface. In this respect oxides, sulphates, silicates and carbonates are particularly useful. Examples of such minerals include calcium sulphate, calcium carbonate, zinc oxide, barium sulphate, silica and siliceous materials such as sand and glass and clay minerals such as mica, china clay and pyrophillite. This list is not exhaustive, however, and many other minerals are suitable for use in this invention. In some cases, pre-treatment of the surface of the mineral may be required to produce a satisfactory deposition of the gel. Yet another alternative is to use hollow microspheres, e.g. of glass for the production of gel particles which can be separated from the water, after treatment, by flotation rather than sedimentation.

The hydroxylated layer of the gel particles of type II can be provided by any of a number of metal hydroxides, the requirements being substantial insolubility in water, a valency preferably of three or more, and a positive zeta potential at the adsorption pH, where the colloids retain negative charge. Suitable metals with this characteristic are ferric iron, aluminium, zirconium and thorium. Ferric hydroxide is preferred because it is cheap, and exceptionally insoluble, over a wide pH range. For example, it does not readily dissolve at high pH, as does aluminium hydroxide.

The preparation of the gel-coated particle of type II is also simply carried out, usually by suspending the particles in water, adding a salt of a suitable metal followed by an alkaline material, preferably in aqueous solution which will precipitate the metal hydroxide which then forms a coating on the particle. Typically, chlorides, sulphates, nitrates and the like are suitable salts of the metals, thus ferric chloride or aluminium sulphate could be employed.

The alkaline material may be sodium hydroxide, calcium hydroxide ammonia or similar soluble material. The concentration at which the preparation is carried out is generally not critical.

In the case of where magnetitie or other iron oxide materials are used as the basis for tyep II particles, the metal salt which is employed to produce the hydroxide layer may be obtained by first adding acid to the suspension of the particles (to give ferric and/or ferrous salts in solution from the iron oxide) and then adding the alkaline material.

It has been found advantageous, when forming the gel particles of type II to provide means for increasing the degree of polymerization of the gel. Polymerization occurs due to the elimination of water and the establishment of oxygen ("ol") linkages between the metal atoms: 2MOH MOM + H20 This process occurs on standing, but can be accelerated by heating.

After preparation, it is best if the gel-coated particles are not permitted to dry out. This can be avoided by keeping them under water.

The invention thus offers a method which uses a cheap, readily-prepared recyclable coagulant/ absorbent which removes colloidal particles, micro-organisms and colouring matter from water quickly and more economically, producing a sludge which is little different to the impurities removed from the water and is therefore readily disposable without environmental problems.

An important feature of the process of the present invention is that the gel particles can be recycled many times. To achieve this, the adsorbed material is removed by raising the pH of a suspension of the adsorbent in water. In the case of type I coagulant/adosrbents, the coagulating properties may be regenerated by treatment with alkali solution; these two treatments may be combined.

The gel particles may be used simply by adding them to the water to be treated, either in a batch process or in a continuous process by mixing them with the incoming water, stirring them for a sufficient period to allow the colloids and colouring matter to adhere to the particles and then permitting the particles to settle. The clarified water can be removed and the particles regenerated to the addition of a solution of a suitable alkaline material. To meet the requirement mentioned earlier, the pH of the water to be treated might have to be adjusted after addition of the particles.

Furthermore, we have also discovered, in accordancd with a further aspect of this invention, that if a small quantity of multi-valent cation having a valency of three or more (e.g. Fe 3+ or Al3+) is added to the water after the addition of the gel particles, then the amount of the cation added is substantially less than would be required to produce water of comparable clarity by using the cation alone, with appropriate addition of alkali or acid, to form an absorptive floc as in the usual process of water coagulation. In many situations, but not all, the optimum economic situation will be to use the gel particles in combination with a small amount of such a cation.

It is thought that after the gel particles have absorbed some of the colloidal particles, the addition of limited amounts of the multivalent cation suppresses, but does not completely eliminate, the negative charge on the remaining colloids so that when part of their negative surface binds to the positive region of the gel particle, electrostatic repulsion between neighbouring colloids on the gel particle surface is reduced. Consequently the colloids can pack together more closely on the gel particle surface so that less of the latter is required. This is shown diagrammatically in Figure 1. When the colloid's negative charge is neutralized by monovalent cations such as Na+ (Figure la) the colloid has a high zeta potential and there is strong repulsion between adjacent colloids on the gel surface. When the colloid absorbs on to the surface of the gel particle, some of its Na+ counter ions are replaced by the positive charges on the gel surface and electrostatic binding results, no double assisted by hydrogen bonding and the like. If the remainder of the Na+ is replaced by aluminium, or other multivalent ions, then the elctrostatic repulsion is suppressed and the particles can pack more closely together (Figure lib).

The final sludge from this process consists essentially of the colloids removed from the original water, but when multivalent cations are added to facilitate the process these colloids are rejected with multivalent cations replacing most of the monovalent cations which were present in the diffuse double layer of the original colloid. Thus the presence of the voluminous iron or aluminium hydroxide floc in the sludge of the conventional process is avoided and disposal of the sludge is greatly facilitated. For example, if river water is being clarified the sludge could be returned to the river with little environmental harm. After desorption, the regenerated gel particles can be recycled for the adsorption of more colloids at a lower pH.

Thus the net multivalent ion requirement of the process is greatly reduced.

The positively-charged nature of the coated adsorbent particles also leads to the adsorption of the acidic materials which comprise the natural colouring matters often present in water.

Thus the application of the present process results in substantial or complete removal of such colour from water, often to an extent which cannot be achieved by conventional alum treatment.

As indicated above, a much better purification is usually achieved in high turbidity water if a suitable coagulant is also added to the water. For this purpose, aluminium sulphate (alum) is the most convenient, but other materials such as ferric chloride or an organic polyelectrolyte may be used. This addition is best made shortly after the gel particles have been added, and the pH of the water has been adjusted. The mixture is stirred for a suitable time and then the sludge allowed to settle.

There is a striking difference in behaviour when an untreated finely divided mineral particle (e.g. magnetite) is added to turbid water along with coagulant chemicals, compared with the behaviour of the gel particles. In the former case the mineral coprecipitates with the colloids, and whilst its presence will accelerate settling it is only possible to reduce the amount of coagulant a slight amount to achieve comparable clarification. On vigorous shaking the floc and colloids separate from the magnetite. When the gel particles of the invention are added, however, each particle is observed to be a separate entity and to be completely coated with colloids; a large reduction in the amount of coagulant can be achieved. At the same time the colloids are very firmly attached to the particles and remain so even under vigorous conditions of stirring. When the gel particles are magnetic, they are readily removed by magnetic means in a magnetic separator, or by applying a magnetic field to cause the particles to flocculate and settle rapidly; a sparking clear supernatant can be obtained. Under similar conditions, the agglomerate produced by untreated magnetite tends to disperse under the agitation conditions and a cloudy supernatant results. Thus by using the gel particles of the invention water of high clarity can be obtained simply by permitting the particles to separate by sedimentation or by using a magnetic separator; a sand filter is not required. If simple sedimentation is to be used then the mineral core of the gel particle can be any inert material, e.g. sand. However. it is preferable to use a soft ferromagnetic material (e.g. magnetite) to permit accelerated removal of the gel particles with attached colloids by magnetic means. In such a case the gel particles should preferably not be magnetized whilst the colloids are being absorbed but can be subsequently magnetized prior to separation from the water. There is advantage in collecting the particles by passing the slurry through a magnetized wire packing to which they adhere. Later they can be removed by switching off the magnetic field. This mode of operation reduces abrasion between the particles with consequent removal of the gel coat and so facilitates their mechanical handling.

Regeneration of the gel particles is simple and merely requires adjustment of the pH of the sludge to about pH 10, separation of the adsorbed material and, in the case of the type I material, treatment of the gel particles by the same process as was described for their preparation.

While at least some of the benefits of the above-described coagulant/adsorbent material can thus be obtained by application of known procedures, the full advantages are more readily realizable with a procedure and apparatus which therefore we have specifically designed for this purpose. This method and apparatus will now be described in more detail with reference to Figures 2 to 4 of the accompanying drawings, which relate to water treatment using type I coagulant/adsorbents.

As illustrated in Figure 2, at Stage 1 feed water to be treated is contacted with the coagulant/ absorbent in any suitable liquid solid contactor. Alum is then added, if necessary or desirable at stage 1A, and after further mixing the clarified water is separated from the coagulant/adsorbent in the separation stage 2. The spent coagulant/absorbent is then treated with dilute caustic soda at stage 3 to free the coagulant/adsorbent from the adsorbed contaminants. After a further separation stage 4, the contaminants pass to waste as effluent, while the coagulant/adsorbent passes to a regeneration stage 5 where it is treated with 0.1N caustic soda which is continuously recycled (with make-up when necessary). The coagulant/absorbent is then washed at stage 6 with water. The washings (dilute caustic soda) are recycled to stage 3 while the regenerated coagulant/absorbent is recycled to stage 1.

Figure 3 shows a form of solids contact clarifier which is suitable for the stage 1 and 2 operations described above. This apparatus is used in conventional water treatment processes and is designed to ensure efficient contact between suspended matter and reagent, such as an alum solution, by circulating water containing the suspended matter around a zone into which the reagent is introduced.

The apparatus consists of a long pipe 21 and a vessel 22. The latter is generally in the form of closed cylinder with an integral, conical base portion 23. Within the vessel 22 there is mounted an inverted cup-like housing 24 which is of generally similar shape to the vessel 22, and serves to define an inner chamber 25. Centrally located in the chamber 25 is a short vertical pipe 26. The pipe 21 is connected into the pipe 26 is a short vertical pipe 26. The pipe 21 is connected into the pipe 26 near the bottom of the latter. An impeller 27, to aid liquid circulation in the chamber is mounted within the bottom portion of pipe 26. Clarified water and settled. solids outlets 28, 29 are at the top and bottom, respectively, of the vessel 22.

In typical operation, the turbid feed water is admitted to the pipe 21, at such a rate that it would take about 5 minutes to pass to the vessel 22. Acid to adjust the pH to the optimum for the particular water, and the coagulant/ adsorbent are introduced at, or near to, the inlet end of the pipe 21. Flow in the pipe 21 is turbulent to ensure thorough mixing. The water leaving pipe 21 flows up through the central pipe 26 into the surrounding chamber 25. Alum, if required is introduced (by means not shown) into the pipe 26 and/or at or near the inlet end of pipe 21. Clear water is drawn off through outlet 28 at the top of the vessel 22 and the settled coagulant/adsorbent, together with attached impurities at the bottom outlet 29. Precipitation of the coagulant/adsorbent may be facilitated by using a magnetizable adsorbent. The equipment can be operated continuously, and the adsorbent regenerated in a separate stage (as described above) by raising the pH of the slurry to about 10.5, separating the released floc and colouring matter, and treating the adsorbent with an alkaline solution as described above.

In using the coagulant/ adsorbents in accordance with the method of this invention it will be found that maximum clarification depends on the pH of the feed water. The optimum pH may vary from sample to sample, it is therefore recommended to test samples and adjust the feed water pH to optimum by addition of acid and/or alum. When the coagulant/adsorbents are used in conjunction with alum, it will normally be found that the optimum pH for alum alone is suitable, typically about 5 or above. When the adsorbent is used along it is frequently advantageous to lower the pH to about 4.

A complete and preferred water treatment system is shown in Figure 4.

The incoming feedwater (A) and regenerated coagulant/ adsorbent (magnetite) are fed to a contactor 31, which may be a pipe as described above (21 in Figure 3) or any other suitable apparatus, for example a channel, trough or tank provided, if necessary, with stirring equipment. Where necessary alum (B) is added to the mixture as it leaves the contactor 31.

The mixture then passes to a solids clarifier 32, which may be of the type described above (Figure 3). or as shown may comprise a separate clarifier 32A and solids/liquid separator 32B.

Clarified water (C) is taken off as the overflow from the separator 32B or clarifier 32 as the case may be.

The solids underflow (D) from 32B or 32 consists of the loaded coagulant/adsorbent, i.e. associated with the colloidal and other impurities. This passes to a first regeneration mixing stage 33, where it is mixed with recycled dilute caustic soda (G) to free the coagulant/adsor bent from the impurities, and thence to another magnetic separator 34 from which emerge an effluent stream E containing the impurities and partly regenerated coagulant/adsorbent (F). The stream (F) is mixed with further dilute caustic soda (L) to bring the pH to 10.5 and passes to the second regeneration mixing stage 35 and thence to a further magnetic separator 37.

The overflow stream of dilute caustic soda (G) from 37 goes for mixing with stream (D) and the underflow solids-containing stream (H) passes to a final regeneration stage 38 where it is mixed with 0.1N caustic soda ( ) . This mixture passes to a further magnetic separator 39 from which the overflow stream (I) of caustic soda is recycled for mixing with stream (H) and the underflow solids (J) are mixed with recycled washwater (M) and pass to the first washing mixer 41.

From 41 the mixture passes to a further magnetic separator 42. The overflow liquid stream (L) of dilute caustic soda is recycled for mixing with stream (F) and the underflow solids stream (N) passes to the final washing mixer 43, where it is mixed with washwater (K), and thence to the final magnetic separator 44. The overflow stream (M) is recycled back to first washing stage for mixing with stream (J) and the underflow solids stream (0), which now contains regenerated and washed coagulant/adsorbent, is returned for mixing with further feed water (A).

Where alum is used, it may be desirable to make provision for recovery and recycling of this reagent and this optional arrangement is also shown in Figure 4. Here the effluent stream (E) from the first magnetic separator 34 is adjusted to pH 3.5 in a mixer 46. The mixture is passed to a solids/liquid separator 47 from which the stream (P) of recovered alum solution may be recycled for mixing with stream (B) and the solid sludge of effluent (Q) finally passes to waste.

The mixing stages (33, 36, 38,41,43 and 46) may be performed in any suitable apparatus, such as pipes with turbulent flow, or channel, troughs or tanks with suitable stirring or mixing equipment.

Typical contact times for the main steps in the process are: Purification - 1st stage (3) - 7 minutes - 2nd stage (32) - 5 minutes Regeneration - final stage (38) -10 minutes.

Similar apparatus and procedures to those described above may be adopted when using the type II coagulant/adsorbents. In this case, however, the regeneration stage(s) (5 in Figure 2 and 38 in Figure 4) are not required.

The following Examples further illustrate the invention which is, however, not limited by these Examples. In all the Examples of water treatment, the zeta potential of the hydroxylated surface layer of the coagulant/adsorbent was positive at the pH of the water under treatment. At this pH the colloided matter in the water retains some of its negative charge.

EXAMPLE 1 - General Method of Preparation of the Type I Coagulant/Adsorbent.

A magnetite ore from Savage River, Tasmania, was crushed and classified to yield 1-5 micron particles. A 10 ml portion of the particles was added to 200 ml of sodium hydroxide solution of appropriate concentration and at an appropriate temperature. The slurry was stirred for a period, usually 5 to 10 minutes. The particles were filtered and washed with water.

A number of samples were prepared under varying conditions. These were used in following examples and were regenerated under the conditions used initially. They are identified according to the code letter shown in the table below: Code Letter NaOH Conc. Temp. Contact Time A 0. SN 60"C 5 mins B 0. 5N 25"C 5 mins C 0.05N 60"C 10 mins For comparison in some examples, magnetite was treated both initially and in regeneration by slurrying in water adjusted to pH 10.5 at 25"C for five minutes.

B. Standard Jar Test for Magnetite in Conjunction with Alum A 1l sample of water is contacted with 10 ml of magnetite for 7 min at 160 RPM after addition of the optimum amount of acid. Alum is then added and the fast stirring continucd for 2 minutes, followed by slower stirring at 75 RPM for 5 minutes. The mixing should he such as to keep the magnetite fully suspended. The stirring is then stopped and the magnetite allowed to settle for 5 minutes. The resulting unfiltered supernantant liquor is then analyzed for residual turbidity and colour. The magnetite is then separated by decantation and treated by the same method as described in Example l.

C. Standard Jar Test for Magnetite Alone A I e sample of water is contacted with 10 ml of magnetite for is minutes at I 60 RPM at the optimum pH (determined in prior experiments). The stirring is stopped and the magnetite allowed to settle for 5 minutes. The unfiltered supernantant liquor is then analysed for residual turbidity and colour. The magnetite is then separated by decantation and treated by the same method as described in Example l.

These test conditions A, B and C were found to be the most rapid to bring about optimum coagulation by each of the three methods. The total process time for each method is as follows: Method A 42 minutes Method B @ 19 minutes Method C 2() minutes EXAMPLE 3 - Treatment of High Turbidity River Water In this example, four samples of water from the Yarra River in Victoria with relatively high turbidity ranging from 18 NTU to 68 NTU and colour ranging from 55 Pt-Co units to 75 Pt-Co units were treated. Comparisons of standard alum treatment with treatments involving samples of magnetite activated according to Example 1, both with and without alum were made. The results are shown in Table I and generally are the average of a number of cycles, which have been made with magnetite regenerated after each coagulation.

EXAMPLE 4 - Treatment of Low Turbidity/High Colour Water In this example, two samples of water from the Yan Ycan rcscrvoir in Victoria were treated to remove colour. Again, treated magnetite, with and without alum added, was tested ind compared with standard alum treatment and with untreated magnetic. As in the prcvious examples, the magnetite was generally recycled and the average results are quoted. Rcsults are shown in Table II.

With this water, alum was not very effective for colour removal whereas magnetite treated according to the invention gave almost complete removal even without added alum. Othcr magnetites were largely ineffectivc.

EXAMPLE 5 - Modified Regeneration of Magnetite A modified procedure for the regeneration of magnctite was tested in comparison with the method described in Example l. In the modified method, the magnctite was washed after treatment with 0.05N sodium hydroxide and the washings kcpt. These were adjusted to pll 10.5-11 and used to treat the magnetite after the next tlocculation cycle. Ncarly all of the insoluble material was removed from the magnetite by this step, together with much of the adsorbed colouring material. The magnctite was separated from the liquor, washed and then treated with the 0.05N sodium hydroxide solution. The remainder of the colour and insoluhle material were thus removed. The magnctite was washed (and the washings retained íor the next cycle) and then reused for the next flocculation. The ().()5N sodium hydroxide solution could be used for a very large number of cycles with occasional addition of more solution to make up for losses. Magnetite treated by this modified procedure gave results in clarifying and decolourising water which were indistinguishable from those obtained with magnetite regenerated according to Example 1. This method is particularly suitable lor continuous operation.

EXAMPLE 6 Magnetites regenerated under other conditions were tested on water from the Yarra River in comparison with standard alum treatment. The regeneration was carried out by treating 10 ml of the magnetite with 40 ml of sodium hydroxide solution. The samples were identified according to the code letter shown in the table below.

CODE LETTER NaOH CONC. TEMP. CONTACT TIME E ().()5N 60"C 5 mins F ().()5N 40 C I() mins G 0. IN 25"C 10 mins The results obtained arc shown in Table Ill.

TABLE 1 Treatment Treatment Alum Final Raw Water Product Water Comments Material Method Added pH pH T C T C mg/l (NTU) (Pt-Co) (NTU) (Pt-Co) Alum A 10 5 7.1 68 55 9.5-9.8 40 Colour removal poor Alum A 20 5 7.1 68 55 < 1 5 Fe3O4A B 10 5 7.1 68 55 < 1 0 Average of six cycles.

Excellent clarity and colour Fe3O4B B 10 5 7.1 68 55 1 0 Avarage of six cycles.

Excellent clarity and colour Fe3O4D B 10 5 7.1 68 55 12 40 Average of six cycles.

Both turbidity and colour removal poor Alum A 10 5 7.0 18 55 5 40 Colour removal poor Alum A 15 5 7.0 18 55 1.7 10-15 Colour removal fair Fe3O4A B 5 5 7.0 18 55 1-1.1 0 Average of nine cycles.

Excellent clarity and colour Fe3O4B B 5 5 7.0 18 55 1.5-2.0 0-5 Average of nine cycles.

Excellent clarity and colour Alum A 20 5 7.1 63 70 7.4 30 Colour removal poor TABLE 1 Contd.

Treatment Treatment Alum Final Raw Water Product Water Comments Material Method Added pH pH T C T C mg/l (NTU) (Pt-Co) (NTU) (Pt-Co) Alum A 30 5 7.1 63 70 2.7 15 Colour removal fair Alum A 35 5 7.1 63 70 2.2 10 Colour removal fiar Fe3O4C B 15 5 7.1 63 70 1.0 0 Average of six cycles.

Excellent clarity and colour Fe3O4D B 15 5 7.1 63 70 30 40 Turbidity and colour removal poor Alum A 20 5 7.1 31 75 4.2 35 Colour removal poor Alum A 30 5 7.1 31 75 2.4 20 Colour removal fair Alum A 40 5 7.1 31 75 1.9-2.2 10-15 Colour removal fair Fe3O4C B 15 5 7.1 31 75 #1 0- 5 Average of seven cycles.

Excellent result Fe3O4C C - 5 7.1 31 75 8.9 20 Fe3O4C C - 4 7.1 31 75 1.7 0- 5 Lower pH markedly improves performance. Result better than the best alum treatment for this water.

GENERAL COMMENTS. Not only does the treated magnetite give better results than alum alone, but using half or less the amount alum, but it is done in less than half the time. Removal of colour by the treated magnetite was particularly good.

TABLE II Treatment Treatment Alum Final Raw Water Product Water Comments Material Method Added pH pH T C T C mg/l (NTU) (Pt-Co) (NTU) (Pt-Co) Alum A 25 5 7.1 2.0 70 1.3 25 Colour removal poor Alum A 30 5 7.1 2.0 70 0.7 20 Colour removal poor Alum A 2.5 5.5 7.1 2.0 70 1.3 20 Colour removal poor Fe3O4C B 15 5 7.1 2.0 70 0.7 0-5 Excellent colour removal Fe3O4* C - 4 7.1 2.0 70 3.9 40 Poor result Fe3O4D C - 4 7.1 2.0 70 3.4 35 Poor result Fe3O4C C - 4 7.1 2.0 70 0.6-0.8 0-5 Excellent colour removal Alum A 15 5 7.0 1.8 60 1.5 30 Colour removal poor Alum A 15 5.5 7.0 1.8 60 1.7 20 Colour removal poor Fe3O4 C - 4 7.0 1.8 60 0.3-0.4 0 Excellent colour removal * Fresh, untreated Fe3O4 used.

TABLE III Treatment Treatment Alum Final Raw Water Product Water Material Method Added pH pH T C T C mg/ 1 (NTU) (Pt-Co) (NTU) (Pt-Co) Alum A 30 5 7 26 70 1.2 10-15 E C - 4 7 26 70 < 1 0 F C - 4 7 26 70 1-1.2 0 G C - 4 7 26 70 1.3 0 The following examples illustrate the preparation and use of the Type II coagulant/adsorbent.

EXAMPLE 7 - Preparation of the Gel Particles on Magnetite A magnetite ore from Savage River, Tasmania, was crushed and classified to yield 1 - 10 micron particles. These were slurried in water to which a hydrolysable metal salt was added (ferric chloride or aluminium sulphate in this example), followed by sodium hydroxide solution to adjust the pH to the desired level. After the precipitation of the hydroxide coating was complete, the mixture was heated to increase the polymerization of the coating - 1 hour at boiling point for a ferric hydroxide coating, 40 minutes at 80"C for an aluminium hydroxide coating. The supernatant liquor was then decanted off and the coated particles thoroughly washed by decantation with cold water.

Three samples were prepared under the conditions shown in Table IV.

TABLE IV Code No. Raw Material charges pH for precipitation Fe Mag 1 0.5 g FeCl3.6H2O/g. Fe304 11.5 in 2.5 ml water Fe Mag 4 0.085g FeCl3.6H2O/g Fe3O4 9.8 in 2.5 ml water Al Mag 2 0.5g Al2(SO4)3.16H2O/g 5.5 Fe304 in 250 ml water EXAMPLE 8 - Purification of River Water Standard jar tests were carried out with Yarra River water (turbidity 12 NTU, colour 65 Pt/Co unites) whereby aluminium sulphate (alum) plus coagulant/adsorbent, was mixed for a predetermined time, after which mixing was stopped. After a further specified time for settling the turbidity and colour of the supernatant liquid was measured. In the experiments using the coated particles the sediment was removed, regenerated by washing with NaOH solution at pH 10.5, rinsed and then recycled. After thirteen such complete cycles the results of the turbidity and colour removal for the fourteenth cycle were taken, and are shown in Table V. The amount of the coated particles added was 5 ml/l (settled volume) in all cases.

An identical run using alum alone was carried out for comparison.

TABLE VI Alum Level 5 mg/l alum 10 mg/l alum Coagulant/adsorbent T C T C Fe Mag 1 1.5 10 0.35 5 Fe Mag 4 5.0 30 0.85 10 Alum 9.9 50 3. 6 25 T = Residual Turbidity N.T.U.; C = Residual Colour Pt/Co Units It can be seen that the use of the gel-coated particles of this invention give remarkably better removal of turbidity and colour using low levels of alum than the alum alone. At the 10 mg/ l level of alum. water of acceptable quality is produced by the gel-coated particles, but not by alum alone.

A significant advantage exhibited by the treated particles was the short time required for treatment and settling. Thus the treated particle experiments required only 12 minutes total to achieve the clarification shown, whereas alum required at least 35 minutes.

The treated particles after separation of the clear supernatant liquid were regenerated by the addition of a small quantity of approximately 0.5N sodium hydroxide. The release of the attached impurities was demonstrated by plotting pH of the slurry against turbidity-or apparent colour and iron content of the liquid layer. The results showed that as the pH is increased, colour and turbidity increased in the water layer, corresponding to their removal from the treated particles. This transfer occurs mainly at pH 9 to 10. At the same time, an amount of iron salt is removed corresponding to the amount of iron present in the original water.

EXAMPLE 9 This example illustrates the effect of recycling on the performance of the treated particles.

The flocculation was carried out as described in Example 7 (except that 15 mg/ 1 of alum was used) using a ferric hydroxide coated particulate magnetitie and one coated with aluminium hydroxide. The results obtained are shown in Table VII.

TABLE VII Cycle 1 2 3 4 5 T C T C T C T C 3.7 ml Fe Mag 1 0.78 0 0.49 0 0.46 - 0.36 - 0.38 3.6 ml Al Mag 1 0.59 0 0.73 0 1.2 - 1.3 - 1.3 The results show that the iron hydroxide treated particles improved in their performance on recycling. On the other hand, the performance of the particles coated with AI(OH)3 fell off with each successive cycle, probably the result of dissolution of the gel coat at high pH, during regeneration.

The effectiveness of regeneration on the coated particles was demonstrated by reusing the material after one flocculation without treatment with alkali. In the following cycle, normal regeneration was used. The results obtained are shown in Table VIII (amount of alum used in flocculation was 5 mg/l).

TABLE VIII Cycle 8 9 10 T C T C T C FeMag 1 5 ml 1.4 10 4.6 25 1.5 10 It can be seen that when the particles are not regenerated, the purification is poor, but regeneration before cycle 10 has restored the effectiveness.

EXAMPLE 10 This example shows the effect of increasing the amount of gel-coated particles, while keeping the amount of alum constant. Yarra River water was treated using a constant dose of 5 mg/l of alum, in conjunction with different quantities of coagulation aid (Fe Mag 4). The results are shown in Table IX.

TABLE IX Amount of Amount of Residual Residual Colour Coagulant Alum Turbidity (Pt-Co) Aid (ml/l) (mg/l) (NTU) Fe Mag 4 5 5 6.6 45 10 5 6.6 40 15 5 2.9 5 20 5 1.4 0 Alum only Nil 5 13 60 Alum only Nil 20 1.5 15 Yarra River water pH = 7.1 Turb = 14 NTU Colour = 65 Pt-Co The results show that the increase in Fe Mag 4 results in considerable improvement in the purity of the treated water. At four times the quantity, alum alone does not have as great an effect as can be achieved with Fe Mag 4/alum.

EXAMPLE 11 The physical stability of the coated particles is demonstrated in this example.

A sample of coated particles (Fe Mag 5) was prepared as in Example 7 using 0.25 g of FeCI3.6H20/g.Fe304. Portion of this material was subjected to attrition by pumping it as an aqueous slurry (200 ml coated particles, settled volume in total volume of 250 ml) through a peristaltic pump at the rate of 100 ml/minute for 5 days. This material was then tested on Yarra River Water, pH 7.3, turbidity 13 and colour 65-70. A sample of the original coated particles was also tested for comparison. The tests were carried out using 20 ml/l of the coated particles and 5 mg/ 1 of alum. The particulates were regenerated and recycled, and the results obtained on the third cycle are given in Table X.

TABLE X Flocculant Turbidity Colour Fresh 1 < 5 After pumping 5 days 0.5 0 It can be seen that the coated particles are stable to prolonged attrition.

EXAMPLE 12 - Preparation of Gel Particles from Titanium Dioxide Gel particles in were prepared by slurrying titanium dioxide (RMS, 20 g, particle size 10-20 micron in water (200 ml) and adding ferric chloride solution (60%, 5 ml) followed by sufficient dilute sodium hydroxide solution to bring the pH to 11.5. The mixture was boiled for 1 hour.

The particles were tested on the same water as in Example 11 using 5 ml/l of the material.

The treated water had a turbidity of only 6.4 NTY and colour of < SPt/Co Units.

EXAMPLE 13 - Separation of Chlorella Vulgaris In this experiment, a sample of gel-coated magnetite (Fe Mag 5 from Example 11) was used in order to separate a suspension of Chlorella Vulgaris. This was achieved by contacting 50 ml of fresh Chlorella suspension (400 mg/l suspended solids) with 8 ml of settled Fe Mag 5 for 3 minutes, during which the flask was gently agitated. The suspension was allowed to settle and the supernatant was decanted and analysed for residual suspended solids. It was found that the residual suspended solid amounted to only 30 mg/l, indicating that 92.5% of the algae had been removed.

The adsorbed algae were recovered from the precipitated sludge by increasing the pH of the sludge to about 10.5 and agitating the mixture. On standing, the heavier gel-coated magnetite particles settled readily and the algae were removed as a suspension.

Claims

WHAT WE CLAIM IS:

1. A method for clarifying water by removing suspended impurities and coloured substances contained in it, which comprises contacting the water with a particulate mineral material, to coagulate and absorb thereon the impurities and coloured substances, the individual particles of which coagulant/ adsorbent have a particle size of less than 10 microns and have been treated to produce a hydroxylated surface layer having a positive zeta potential at the pH of the water under treatment, said pH being within the range of pH where the colloidal matter in the water retains some of its negative charge, and the thus treated water is then separated from the coagulant/absorbent.

2. A method as claimed in claim 1. wherein the hydroxylated layer is derived from the substance of the particulate material.

3. A method as claimed in claim 2, wherein the particulate material is an oxide or silicate.

4. A method as claimed in claim 2, wherein the particulate material is a magnetic or magnetisable material.

5. A method as claimed in claim 4, wherein the particulate material is gamma iron oxide. magnetite or a ferrite.

6. A method as claimed in claim 1, wherein the hydroxylated layer is derived from another substance.

7. A method as claimed in Claim 6. wherein the particulate material is an oxide, sulphate, silicate or carbonate mineral or a clay.

8. A method as claimed in Claim 6. wherein the particulate material is calcium sulphate, calcium carbonate, zinc oxide, barium sulphate, silica, sand, glass, mica, china clay, prophillite, gamma iron oxide, magnetite or a ferrite.

9. A method as claimed in any one of Claims 6 to 8, wherein the hydroxylated layer is a metal hydroxide gel which is substantially insoluble in water.

10. A method as claimed in Claim 9, wherein the metal hydroxide is ferric, aluminium, zirconium or thorium hydroxide.

11. A method as claimed in any one of Claims l to 5, wherein the coagulant/adsorbent is prepared by suspending the particulate material in an alkali solution for a period sufficient to form the hydroxylated layer.

12. A method as claimed in Claim 11,wherein the alkali solution is a 0.05 to 0.1N sodium hydroxide solution, and the treatment time is from 5 to 10 minutes at a temperature of from 20 to 600C.

13. A method as claimed in any one of Claims 6 to 10, wherein the coagulant/adsorbent is prepared by suspending the particulate material in water, adding a salt of a suitable metal, adding an alkaline substance to thereby precipitate the hydroxide of the metal and form a coating thereof on the surface of the particulate material.

14. A method as claimed in Claim 6, wherein the coagulant/adsorbent is prepared by suspending in water a particulate iron oxide material, adding acid to produce some ferric and/or ferrous ions in solution, then adding an alkaline substance to thereby precipitate ferric and/or ferrous particulate material.

15. A method as claimed in any one of Claims 1 to 14, wherein a substance containing a multi-valent cation is added to the water after contact with, and before separation of, the coagulant/adsorbent and the water.

16. A method as claimed in Claim 15, wherein the multi-valent cation is ferric or cluminium.

17. A method as claimed in any one of claims 1 to 14, wherein an organic polyelectrolyte is added to the water after contact with, and before separation of, the coagulant/adsorbent and the water.

18. A method as claimed in any one of Claims 1 to 16, wherein after separation from the water, the spent coagulant/ adsorbent is freed from adsorbent impurities by raising the pH of a suspension of the spent material and separating the coagulant/ adsorbent from the resulting solution.

19. A method as claimed in Claim 18 utilizing the coagulant/adsorbent defined in any one of Claims 1 to 5, wherein the coagulant/adsorbent is regenerated subsequent to or simultaneously with the step of claim 18 by treatment with an alkaline solution.

20. A method as claimed in any one of claims 1 to 19, wherein the individual particles of the particulate material have a particle size in the range of from 1 to 5 microns.

21. A method for the clarification of water by removing suspended impurities and coloured substances contained in it, which comprises the steps of: (a) contacting water with particulate mineral material to coagulate and absorb thereon the impurities and coloured substances, the invidual particles of which coagulant/ adsorbent have a particle size of less than 10 microns and have a hydroxylated surface layer which has a positive zeta potential at the absorption pH (as hereinbefore defined); (b) separating the water from coagulant/adsorbent to obtain the clarified water; (c) treating suspension of the spent coagulant/adsorbent to raise the pH to about 10.5; (d) separating the coagulant/adsorbent from the resulting. effluent solution; (e) where necessary regenerating the coagulant/adsorbent by treatment with an alkaline solution; (f) separating the coagulant/adsorbent from the alkaline solution; (g) washing the regenerated coagulant/adsorbent with water; (h) separating the coagulant/adsorbent from the water; and (i) recycling the regenerated and washed coagulant/adsorbent to step (a).

22. A method as claimed in Claim 21, wherein the washing liquor separated from the coagulant/adsorbent in step (g) is used to raise the pH in step (c).

23. A method as claimed in Claim 21 or Claim 22, wherein the coagulant/adsorbent is a magnetic or magnetisable material and the separation steps (d), (f), and (h) are carried out magneticallv.

24. A method as claimed in any one of Claims 22 to 23, wherein alum is added to the water between steps (a) and (b).

25. A method as claimed in Claim 24, wherein alum is recovered from the effluent from step (d).

26. A method according to claim 23 carried out in apparatus comprising: (a) first mixing and contacting means for contacting water to be treated with the coagulant/adsorbent; (b) separating means for separating the treated water from the spent coagulant/adsorbent; (c) mixing and contacting means for contacting the spent coagulant/ adsorbent with dilute alkali for pH adjustment; (d) magnetic separation means for separating the coagulant/ adsorbent from the resulting effluent; (e) optionally mixing and contacting means for contacting the coagulant/adsorbent with alkali for regeneration of the coagulant/absorbent where necessary; (f) magnetic separation means for separating the coagulant/ adsorbent from the alkali and recycling the latter to means (e); (g) mixing and contacting means for contacting the coagulant/adsorbent with water for washing; and (h) magnetic separation means for separating the coagulant/adsorbent from the water, recycling the water to means (c) and the coagulant/adsorbent to means (a).

27. A method as claimed in Claim 26, wherein at least one of the mixing and contacting means (a), (c), (e) and (g) comprises a long pipe with turbulent flow conditions therein when in use.

28. A method as claimed in Claim 26 or Claim 27, wherein the separating means (b) comprises a solids recirculation clarifier.

29. A method for the clarification of water carried out substantially as hereinbefore described with reference to Figure 2, 3 or 4 of the accompanying drawings.