FIELD OF THE INVENTION The present invention relates to a method for preparing a purified aqueous solution which is adapted to rapidly replace body fluids. In particular, the present invention relates to a method of generating an aqueous solution comprising an electrocratic colloidal complex extracted from peat as well as the product produced by the method.

BACKGROUND OF THE INVENTION Water is necessary for all life. After oxygen, this essential nutrient is involved in all bodily functions.

Water helps in the digestion and absorption of food, maintains body temperature, helps to carry nutrients within the blood, and removes toxins and wastes from the body. Water also serves as a cushion for joints, organs, and spinal cord.

As the human body is about 60% water, it is important to drink enough water everyday in order to maintain good health. When the body does not receive enough water, dehydration occurs causing dizziness, lack of concentration, fatigue, and constipation. Unfortunately, most sources of potable water including all municipal water supplies contain contaminating material, both naturally occurring and introduced, which pollutes the water. Contaminates often found in water include chlorine, lead, asbestos, trihalomethane, lindane, 2,4-D and other herbicides and pesticides, cysts (Giardia, Cryptosporidium) and volatile organic chemicals.

In order to provide"clean"potable water many municipal water suppliers have used treatment methodologies such as chlorination. The addition of chlorine to the water supply

began in the 1890's to eradicate microorganisms that cause water-borne diseases such as cholera and typhoid. However, chlorine also reacts with organic matter such as leaves and debris to create substances, such as formaldehyde.

Moreover, chlorinated water also kills animal cells.

Another additive to scheme water is chloramine, which is a combination of chlorine and ammonia.

Public concern regarding water quality peaked in the early 1980's and since that time we have seen an increase in the volume of sales of bottled water. However, even though bottled water is usually filtered, the bottled water can legally contain minimum levels of contaminants such as bacteria, algae, lead, etc. Indeed, in 1991, the U. S.

House Energy and Commerce Commission conducted a study on bottled water and found that 25% of all bottled water originated from the same water sources as most public "scheme"water and 31% exceed tap water limits for microbiological contamination. However, despite these findings, the popularity of bottled water continues to increase.

There are a number of techniques that have been used to purify water previously, including distillation, reverse osmosis, ozonation and filtration through carbon filters.

However, the use of these techniques in isolation often create more problems than they solve. For example, while distillation removes minerals and some chemicals, other chemicals can vaporise and recondense in the water.

Moreover, distillation is an expensive system that uses a lot of electricity. Reverse osmosis uses a semi-permeable membrane to filter out small particles. However, while reverse osmosis can remove all the minerals found in the water this may not be entirely healthy to drink.

Ozone units use super-oxygenated water to kill bacteria.

However, chemicals, lead, asbestos, and particulate matter are not removed. Also ozone units are expensive to purchase and maintain. Ozonated water can also create high amounts of toxic by-products such as formaldehyde and ketones.

However, the answer is not simply to remove all chemicals, minerals and elements from the water. Indeed, ultra-pure water would not be a good long-term replacement for "natural"water as the animal body does need to replace minerals and salts lost through perspiration and the like.

The need to replace salts and minerals as well as provide "clean"drinking water has seen the recent raise in the amount of bottled mineral water. However, bottled mineral water generally suffers from the same problems as discussed above ie legally containing minimum levels of contaminants such as bacteria, algae, lead, etc, they also can often contain inorganic matter that the body cannot process or utilise. This inorganic matter, rather than helping the body replace minerals and salts actually can compound some of the problems. Accordingly, there is a continuing need for natural water, which is both clean and is capable of replacing lost salts and minerals.

One source of natural minerals and salts is peat. Peat, which is generated by the decomposition of vegetation, has been recognised for a number of years as having health promoting or medicinal properties. Torfott^, for example, is a medicinal product used for ophthalmic diseases extracted from cotton grass-sedge peat. However, while peat has been recognised as having health promoting benefits for many years it is not usually used in its native form, but is normally processed to at least remove large particulate matter and other undesirable components.

Various processes for extracting peat are known, for example, US Pat. No. 5,747, 050 to Tolpa, et al. ; US Pat.

No. 5,713, 967 to Hamerlinski ; US Pat. No. 5,360, 117 to Tolpa, et al. and US Pat. No. 5,290, 554 to Tolpa, et al., which are all incorporated in their entirety herein by reference.

However, the majority of these extraction processes are either destructive to the active agents being extracted or the extracted material becomes contaminated with residual extraction chemicals. For example, one known extraction process utilises steam distillation to extract material from peat ; however, this process produces a product which is heavily contaminated with a variety of volatile compounds including phenols, amines, and saturated carboxylic acids. Other extraction processes use either acid extraction or acid degradation of peat, which results in the destruction of many of the active agents being extracted.

Another problem with some of the previous known processes of extracting peat is the inability to industrialise the extraction processes as they either involve costly filtration equipment or lengthy extraction protocols. For example, the extraction of large quantities of peat has previously been done using static extracts. These processes are typically carried out in extracting tubs, optionally equipped with mechanical stirrers. Such tubs are loaded with peat and the extracting solvent is added.

Periodically, the mixture of peat and solvent is stirred to keep the extracting fluid in contact with the peat material for a time sufficient to obtain a saturated solution of the desired substance or substances in the extracting medium. The peat particles are then allowed to settle and either the extract is decanted or collected from the bottom of the extractor through a screen.

When such a process is applied the extraction process has a number of problems, namely: 1). It is time consuming, as the"leaching process" requires sufficient time for the extracting solvent to penetrate the peat ; 2). It is easily contaminated by the mud found in peat ; and 3). The peat extract, when collected by decanting, is easily contaminated with particulate material.

Some of the problems identified above can be overcome by more intensive stirring of the mixture to increase the contact of the peat with the extracting solvent. However, this procedure also results in increased turbidity from the disturbed mud and renders decantation of a clear extract impossible.

Other more dynamic extraction processes that have been proposed, eg. in W092/16600, are carried out in extractors with a stationary peat bed and a continuously flowing stream of extracting solvent. However, these methods are also unsatisfactory, both in the quality and quantity of extracted material as well as the speed of extraction.

One process used to overcome the slowness of the tub/stirrer processes disclosed above is disclosed in US Pat. No. 5,290, 554. In this process, the extracting solvent is introduced under pressure, which results in increased contact of the extraction solvent with the peat.

However, frequently, the pressure of the extracting solvent is so high that the whole peat bed is either pushed upwards or remains dry during the extraction, because the solvent forms flow channels through the peat bed, or else moves between the peat bed and the extractor walls.

Other apparatus and processes for extract peat have been shown to be more dynamic, see, for example, US Pat. No.

5,713, 967 to Hamerlinski and US Patent No. 5,360, 117 to Tolpa, et al.

One of these known processes is described in US Pat. No.

5,747, 050 to Tolpa, et al. According to this prior art process, peat-derived bioactive products are obtained by mixing peat with a highly concentrated aqueous solution of inorganic salts, especially of sodium chloride and then diluted with demineralised water and subjected to reverse osmosis in order to desalinate the solution, inorganic salts being removed, and wherein the resulting solution is concentrated and clarified, and, optionally, in at least one further step, sterilised and/or spray-dried. Another known process uses primary and secondary alkaline hydrolysis of an air-dried raw peat material, followed by acidification and separation of insoluble solid parts with subsequent second alkalisation, acidification of the clear liquid phase and elimination of ballast substances by means of alcohol and ether extraction. In this process, the aqueous phase from the organic extraction is a liquid peat-derived bioactive product.

In both of these known processes the resulting product is discoloured or a highly concentrated, nearly saturated aqueous solution of sodium chloride. The products are unstable when stored for a long time and, moreover, contains undesirable materials such as solvents.

Alkaline drinking water ie water with a pH above 7.0, more preferably above pH 9, is known to have certain health benefits, including antioxidant properties. See, for example, US Patent No. 6,572, 902, which is incorporated herein by reference. Alkaline drinking water is usually produced by electrolysis of potable source water, which results in separate alkaline and acidic (pH below 7.0)

streams of water; however, alkaline drinking water can be produced by adding alkaline minerals to potable source water, such as tap water.

However, while alkaline drinking water is generally more beneficial than ordinary tap water or even bottled water or bottled mineral water, the health benefits are often lost from alkaline drinking water upon storage.

Consequently, there is a continuing need for a purified drinking water, which also contains the health promoting benefits typically associated with alkaline water without the concomitant problems.

SUMMARY OF THE INVENTION The broadest aspect of the present invention relates to an improved type of alkaline drinking water which comprises an electrocratic colloidal complex extracted from peat, which greatly increases the rate of adsorption of fluid.

In addition, in one embodiment, the alkaline drinking water is further stabilised for storage by the addition of silica which maintains a millivolt charge in the alkaline drinking water for a greater period of time.

Accordingly, in a first aspect, the invention provides an alkaline drinking water, which water has a millivolt charge of between about-150 to about-400 millivolts, wherein said charge is maintained for greater than 30 hours.

Preferably, the millivolt charge is maintained with the addition of silica.

In a second aspect the invention provides an alkaline drinking water comprising an electrocratic colloidal complex extracted from peat.

Preferably, the alkaline drinking water is prepared by a method comprising the step of electrolysis.

Accordingly, in a third aspect the invention provides a method of producing alkaline drinking water comprising the steps of: i). filtering potable source water to produce purified water ; ii). directing the purified source water through a water softening system to produce ultra-pure water; iii). oxygenating said ultra-pure water ; iv). electrolysing the oxygenated water to produce alkaline water with a pH greater than 7; and v). adding silica to the alkaline water so that the resulting alkaline water maintains a millivolt charge of between about-150 to about-400 millivolts.

Preferably, the step of filtering the potable water involves a sand filter and/or an activated charcoal filter. Furthermore, the water softening system is preferably reverse osmosis. The step of oxygenating the water is preferably accomplished by exposing the ultra- pure water to ozone. In one preferred embodiment steps iii) and iv) are interchanged ie the water is oxygenated after electrolysis.

In a fourth aspect the invention provides a method of producing alkaline drinking water comprising the steps of: i). filtering potable source water through sand and activated charcoal filters to remove particulate matter and produce purified water ; ii). directing the purified source water through an reverse osmosis filter to produce ultra-pure water; iii). exposing said ultra-pure water to ozone to produce oxygenated water ; iv). electrolysing the oxygenated water to produce alkaline water with a pH in the range of 8 to 10;

v). adding silica to the alkaline water so that the resulting alkaline water maintains a millivolt charge of between-150 to-400 millivolts.

Preferably, the method further comprises the step of adding an electrocratic colloidal complex extracted from peat. More preferably, the step of adding the electrocratic colloidal complex occurs after step v).

In a fifth aspect the present invention provides a process for producing an electrocratic colloidal complex extracted from peat comprising: i). Exposing peat to an extracting solvent for a period of time sufficient to release nutrients and minerals into said extracting solvent thereby producing a peat extract ; and ii). Filtering said peat extract through a crossflow filter to produce filtered peat extract.

In one embodiment, the process further comprises exposing the filtered peat extract to a magnetic field to produce an electrocratic colloidal complex having a millivolt charge corresponding to between-350 and +800 mV.

Preferably, the magnetic field is between 100,000 to 120,000 gauss and the millivolt charge corresponds to about-300 mV.

In another embodiment, the process further comprises exposing the electrocratic colloidal complex to sterilisation. Preferably, the sterilisation is exposure to ultraviolet light. More preferably, the ultraviolet light is at a wavelength between 200nm to 300nm and at a dose of between 43,000 and 63, 000 uW sec/cm2 (43 mJ/cm2 and 63 mJ/cm2.

Preferably, the period of time sufficient to release the nutrients and minerals from the peat is greater than 10

minutes. More preferably, the period of time is between 10 minutes and 48 hours. Even more preferably, the period of time is between 5 hours and 24 hours.

While any extracting solvent may be used in the present invention, the solvent will preferably be non-toxic.

Accordingly, the solvent is preferably water. More preferably, the water is filtered water. Even more preferably, the water is substantially free of chlorine.

Most preferably, the water is in a microstructured form, which is substantially free of negative electrolytes as well as being in a 6 cluster molecular form.

The step of exposing the peat to an extracting solvent may utilise any of the known methods of mixing solvent and peat. However, preferably, the method uses either a batch method or a continuos flow method. In one embodiment, the peat is retained so that large particular matter or contaminating material such as stones, detritus and the like does not contaminate the electrocratic colloidal complex. Preferably, the restraint includes a permeable fabric sack.

Once the nutrients and minerals have been released or extracted from the peat, the peat extract is then filtered to remove any further contaminating material. The filtering step is preferably via a crossflow filter of less than 10 microns to produce a filtered peat extract.

Preferably, the crossflow filter is made of fabric with a pore size distribution of between 1 to 8 micron. Most preferably, the fabric is a densely woven filament fabric such as Dacron polyester, which only allows particles of 3 microns or less to pass through.

The present invention also provides an electrocratic colloidal complex obtained by a process according to the fifth aspect. Accordingly, the present invention provides

a peat extract comprising an electrocratic colloidal complex, wherein said electrocratic colloidal complex comprises essential minerals, but is substantially free of humic acid.

The term"substantially free"as used herein means less than about 1 weight percent, preferably less than about 0.5 weight percent, more preferably less than about 0.01 weight percent, and most preferably less than about 0.005 weight percent.

Preferably, the essential minerals in the electrocratic colloidal complex is selected from the group consisting of Aluminium, Boron, Barium, Chromium, Calcium, Cobalt, Copper, Iron, Magnesium, Manganese, Phosphorus, Potassium, Silicon, Silver, Sodium, Strontium, Sulphur, Vanadium, Zinc and combinations thereof. More preferably, the electrocratic colloidal complex has a millivolt charge of greater than-300 mV.

The foregoing and other aspects of the present invention are explained in greater detail in the specification below.

BRIEF DESCRIPTION OF THE FIGURES Figure 1 shows a portion of a crossflow filter.

Figure 2 shows a typical analysis of the filtered electrocratic colloidal complex produced by the processes disclosed herein.

Figures 3a and 3b show a magnetic field generator.

Figure 4 shows one embodiment of the process for producing an extract from peat.

Figure 5 is a block diagram showing the sequence of steps in one embodiment of claimed process.

Figure 6 shows a comparison of reduction- oxidation potentials of various water samples.

Figure 7 shows a typical analysis of alkaline water produced by the methods disclosed.

DETAILED DESCRIPTION OF THE INVENTION Before describing the present invention in detail, it is to be understood that all publications, patents and patent applications cited herein, whether supra or infra, are hereby incorporated by reference in their entirety.

However, publications mentioned herein are cited for the purpose of describing and disclosing the protocols and reagents which are reported in the publications and which might be used in connection with the invention. Nothing herein is to be construed as an admission that the invention is not entitled to antedate such disclosure by virtue of prior invention.

Furthermore, the practice of the present invention employs, unless otherwise indicated, conventional water purification techniques, chemistry and engineering within the skill of the art. Such techniques are well known to the skilled worker, and are explained fully in the literature. See, eg. , Coligan, Dunn, Ploegh, Speicher and Wingfield"Current protocols in Protein Science" (1999) Volume I and II (John Wiley & Sons Inc.) ; and Bailey, J. E. and Ollis, D. F. , Biochemical Engineering Fundamentals, McGraw-Hill Book Company, NY, 1986.

Before the present methods are described, it is understood that this invention is not limited to the particular materials and methods described, as these may vary. It is

also to be understood that the terminology used herein is for the purpose of describing particular embodiments only, and is not intended to limit the scope of the present invention which will be limited only by the appended claims. It must be noted that as used herein and in the appended claims, the singular forms"a,""an,"and"the" include plural reference unless the context clearly dictates otherwise. Thus, for example, a reference to"a filter"includes a plurality of such filters. Unless defined otherwise, all technical and scientific terms used herein have the same meanings as commonly understood by one of ordinary skill in the art to which this invention belongs. Although any materials and methods similar or equivalent to those described herein can be used to practice or test the present invention, the preferred materials and methods are now described.

One embodiment of the present invention, relates to a process for preparing an electrocratic colloidal complex extracted from peat. As used heein the term "peat" refers to any partly decayed organic material that has formed in waterlogged, sterile or acidic conditions of bogs and fens over long periods of time. Preferably, the peat material is isolated from bogs or marshes that are at least between 1000 and 3000 years old.

Once the peat has been obtained it is"exposed"to an "extracting solvent". The terms"exposed,""exposing," "expose"and the like are used to infer that the peat is mixed with the extracting solvent or in someway brought into contact with the extracting solvent. The term "extracting solvent"refers to the solution, which is used to leach out the desirable components from the peat.

While any useful solvent may be used, in one embodiment the extracting solvent is water. The water can be any source water including normal mains scheme water, deionised water, purified water and the like.

In one embodiment the water is firstly filtered through a filter designed to remove particular matter and particular undesirable chemicals. For example, a 5 micro filter is capable of removing most particulate matter from the water. Most commonly, the water is then passed through a further filter comprising granular activated carbon or the like, which is capable of removing chlorine, organic material and other impurities.

The peat is typically allowed to remain in contact with the extracting solvent for a period of time sufficient to enable the release of nutrients and minerals from the peat. Any technique for exposing the extracting solvent may be used; however, preferably the technique is either batch or continuous flow. Batch techniques involve the use of tanks, optionally equipped with mechanical stirrers. In one preferred embodiment, the peat is encased in a fabric sack such as hessian and loaded into the tank with the extracting solvent. Periodically, the mixture of peat and solvent is stirred to keep the extracting solvent in contact with the peat material for a time sufficient to obtain a saturated solution of the desired substance or substances in the extracting solvent. The fabric sack is then removed and the extracting solvent is removed for further processing. The solvent is allowed to remain in contact with the peat for at least 10 minutes, but preferably between 4 hours and 10 hours.

The ratio of peat to extraction solvent is typically between 1: 1 to 1: 100, respectively, although different ratios may be used.

Once the extraction solvent has been removed it is filtered through a crossflow filter to produce filtered product. The term"crossflow filter"refers to the type and position of the filter used to filter the extraction

solvent. The filter is composed of any material or fabric, which has a pore size of less than 8 micron. In use the extraction solvent circulates through the crossflow filter as shown in Figure 1.

In one embodiment, the crossflow filter is made of fabric with a pore size distribution of less than 5 micron. In this regard, the fabric is typically a densely woven filament fabric such as Dacron polyester or nylon, which only allows particles of 3 micro or less to pass through.

Types of fabric that may be used in the present invention includes cloth woven from nylon yarns, usually in a ripstop weave. The term"ripstop weave"as used herein means that the weave pattern of the nylon cloth consists of reinforced ribs, in both the warp and the filling, forming a uniform pattern of squares. Some of the commercially available cloths include MIL-C-44378 Type I and Type III, which are high tenacity 30 den flO nylon fabrics. The minimum braking strength of these fabrics is 451bs/inch and the tear strengths are a minimum 51bs/inch.

Other fabrics are BSF 118 854 and BSF 118 1302, which are 50 dtex 15 fils 300 tpm Nylon 6.6 Type 143 fabrics.

Another fabric is BSF 126/1312, which is a 33 dtex flO/200 tpm Nylon 6.6 Type 143. Other fabrics include BS2F 126/254 (A374) and MIL-C 7020 H TYPE 1 (A380). All of these fabrics are commercially available from companies such as Gelvenor, Kwazulu Natal, South Africa or Perseverance Mills Ltd, Padiham, Lancashire, UK.

The crossflow filter is capable of removing much of the fumic and humic acid residues found in peat, which often creates a dark colour.

As shown in Figure 1, the crossflow filter 11 includes a plurality of elongate tubes 30 through which the extraction solvent passes during use. In the present embodiment, the crossflow filter 11 is arranged such that

extracting solvent is caused to flow in one direction along a tube 30, then to flow in a substantially opposite direction in an adjacent tube 30, and so on in repeated opposite directions until the extracted solvent passes out of the crossflow filter 11.

Each of the tubes 30 is defined by a plurality of join lines 32 produced by appropriate weaving, the join lines 32 being such that the seal between adjacent tubes 30 defined by the join lines 32 becomes increasingly more effective as the volume of extracting solvent in the tubes 30 increases.

It will be understood that since contaminants accumulate on inner surfaces 34 of the tubes 30 during use, the particle size allowed to pass through the material of the tubes 30 decreases over time and the efficiency of the crossflow filter increases over time.

In one embodiment, the individual tubes 30 of the crossflow filter 11 can be isolated or segmented so that these can be flushed, or if required the volume of filtrate can be reduced without reducing the filtration efficiency. This feature allows for optimum filtered peat extract production.

Once the extraction solvent has passed through the crossflow filter it may then be used directly or further processed. In one embodiment the further processing comprises exposing the filtered extraction solvent to a magnetic field to produce a millivolt charge in the filtered extract corresponding to between-350 and +800 mV. Preferably, the magnetic field is between 100,000 to 120,000 gauss produced by magnets, which have signals controlled and omitted at the rate of about 7.8 millivolts per second.

At this stage the extraction solvent is termed an "electrocratic colloidal complex". The term"colloidal"as used herein refers to the state of matter in which very finely divided particles (1 to 1000nm) of one substance (the disperse phase) are suspended in another (the dispersion medium) in such manner and degree, that the electrical and surface properties acquire special importance. The divided particles do not settle out under the influence of gravity either in an electrocratic state or a lyocratic state. The term"electrocratic"as used herein means that the colloidal particles used have natural repelling action, as they have identical charged particles, and that these particles have not demonstrated any side effects.

The components of a typical electrocratic colloidal complex as produced by the process disclosed herein is shown in Figure 2.

A suitable magnetic field generator 40 is shown in Figures 3a and 3b. During use, the extraction solvent passes through a conduit 42 which extends through the magnetic field generator 40 so that the extraction solvent is exposed to a magnetic field as it flows though the conduit 42.

The magnetic field generator 40 includes a housing 44 and a plurality of magnetic field generating elements 46 disposed at spaced circumferential locations around the housing 44. In this example, three magnetic field generating elements 46 are provided, each magnetic field generating element 46 being an electro-magnet energised by a control unit 48. In the present example, the control unit 48 is arranged to energise the field generating elements 46 so that a pulsed magnetic field of approximately 7.5Mz is produced. The field generating elements 46 are arranged such that north poles of the

electromagnets are located closer to the conduit 42 than south poles of the electromagnets.

In one embodiment the electrocratic colloidal complex is also further sterilised before use. Any normal sterilisation process may be employed; however, in one embodiment the sterilisation is by ultraviolet (UV) light.

The use of UV light to sterilise water and other solutions is well known. In one preferred method, the filtered electrocratic colloidal complex is exposed to UV of a wavelength between 200nm to 300nm and at a dose of between 43,000 and 63,000 pW sec/cm2 (43 mJ/cm2 and 63 mJ/cm2).

Figure 4 shows one preferred embodiment of the invention that has been described in general terms above. However, it should be noted that Figure 4 is merely an illustration of one embodiment of the invention and should not be construed as the only process that can be used.

Referring to Figure 4, in one embodiment the process for the extraction of peat comprises a first filter 1, which is typically a 5 micro filter capable of removing most particulate matter from water, a second filter 3, which typically comprises granular activated carbon or the like, which is capable of removing chlorine from water and a peat tank 5, for extracting the electrocratic colloidal complex from the peat. The process starts with source water passing through the first filter 1 and second filter 3, into the peat tank 5, where peat is added. The peat and water are allowed to mix for a period of time then the water, including the colloidal complex, is discharged into a holding tank 7, then pump by rotary pump 9, through a magnetic field generator 23 to a crossflow filter 11. The water at this stage is termed electrocratic colloidal complex and it then either recirculates through openings 15, to the holding tank 7, or passes through pores 13, to a tray 17. The electrocratic colloidal complex at this

stage passes through a UV light generator 19, where it is sterilised, to a final product tank 21.

At this stage the electrocratic colloidal complex can be used directly or introduced into purified water as described below.

Referring to Figure 5, in one embodiment, potable water (1) from any source is passed through a sediment filter (3) in order to remove all suspended sediments greater than 5 micron in size. In one embodiment the sediment filter is a multi-media or a graded density depth filter, using sand and gravel, of various dimensions, which removes large particles and oxidized metals such as iron and manganese which may still be in the source water. Sand and gravel filters of the type used are well known in the art.

The filtered water is then processed through an activated carbon filter (5) in order to remove pesticides, herbicides and other unwanted materials such as chlorine at high levels or anything in gaseous form. Activated carbon filters are also well known in the art and are produced by Rubbermaidt^, Cameron Carbon, Inc. , Baltimore, Md. ; or HermotztM filter, Plymouth, Minn. , USA or any equivalent.

The water is then passed through a water softening system (7), which removes calcium, magnesium and iron. In one embodiment the water softening system is reverse osmosis such as described in US patent No. 6,531, 050 ("US050"), which describes the removal of nitrate ions from an aqueous solution or European Patent No. EP-A-291,330 ("EP330"), which describes a process for treating ground water. US050 and EP330 are both incorporated herein in their entirety by reference.

After filtration the water is then passed through electrolysis (9). Typical electrolysis systems include a plurality of two-chamber electrolytic cells, each cell including an anode chamber and a cathode chamber, with an ion exchange membrane serving as a diaphragm between the two chambers. One example of such an electrolytic cell is shown in U. S. Pat. No. 5,762, 779, the contents of which is hereby incorporated by reference. The membrane significantly restricts water from passing therethrough, but allows ions to readily pass through. One of the chambers is an anodic chamber, with an anode positioned therein, while the other is a cathodic chamber and has a cathode disposed therein. The cathode and the anode elements comprise, for example, platinum or carbon. Other metals could also be used.

In operation, the anode element in the anodic chamber is connected to the positive terminal of a DC voltage source, while the cathode element is connected to the negative terminal of the DC voltage source. An electric field is thus generated across the cell. An electrolyte such as carbon dioxide with an electrolytic salt of ammonia acetate (CH3 COONH4 are examples) may be added if necessary to initiate and/or enhance current flow between the electrodes. In general, when a DC voltage is applied between the anode and cathode at a sufficiently high voltage, an electric current is generated, flowing between the electrodes. The electric current produces electrolysis of the water. At the surface of the anode element oxygen gas is generated, producing anodic (acidic) water having a relatively low pH value, as indicated above, while at the cathode element, hydrogen gas is generated, resulting in cathodic (alkaline) water, which has a relatively high pH value. Thus, the result of the operation of the electrolytic cell is two streams of water, one of which is acidic and the other of which is alkaline.

Once the electrolysis is complete the acid water is delivered through one delivery tube (11), while the alkaline water is collected via a second delivery tube (13).

Alkaline water, produced by the above process has a number of associated health benefits. For example, by disassociation and reconstruction of the acid and alkaline waters, where the positive and negative ions have been separated, beneficial minerals such as calcium, magnesium, potassium, manganese and sodium have been segregated and concentrated. When drinking water possessing these beneficial minerals is further enhanced with the removal of acidic minerals such as, carbonic ; chlorine; sulphuric and nitric.

The basic properties of the alkaline water produced by the above process is its capacity to assist in buffering acidity, removing acidic build up, and further assisting the body in maintaining its narrow window of alkalinity of pH7.2 to pH7.4 pH. Without wishing to be bound by any particular theory or hypothesis the inventor believes that due to the smaller clustered effect of the alkaline water, it has become water that can more effectively deliver the alkaline minerals to a cellular and sub-cellular level.

Thus, the increased bioavailability of minerals through an enhanced delivery medium provides effective delivery of minerals to the cells and the body tissue. Also the ability to donate electrons allows the body to utilise the alkaline water as a mechanism to initiate antioxidant activity for minimising free radical damage.

While the alkaline water produced above may be used at this stage in one preferred embodiment it is placed in a holding tank (15), where its pH is determined.

Preferably, the pH is above 9. Also, the millivolt charge of-300 or below is determined. Figure 6 shows the effect

of water with millivolts ranging from-350 to +800 mV for tap water, alkaline water and acid water. At this stage it is also possible to expose the water to ozonation.

Ozonation is a well known technique for disinfecting water and oxygenating water. The ozonation is most effective in cold water and a small quantity of ozone will be required for disinfection. Ozone generators and ozonators of different capacities are commercially available and can be customised to the application according to specifications.

Ozonators are produced by Ozomax, Montreal, Quebec, Canada; Water Ozonator, Sota Instruments, British Columbia, Canada; and Ozoteck, Yreka, Calif. , USA, or any equivalent.

Inventor has determined that maintaining the pH and/or millivolt charge is important for alkaline water.

For alkaline water the millivolt charge should preferably be in the range from about-150mV to about-400 mV. The inventor has found that this may be maintained with the introduction of silica. In order to achieve this, the inventor typically adds a concentrate of silica. The amount of silica added is typically 50ppm. Inventor have found that the introduction of silica lengthened the normal time for holding the millivolt charge from several hours to at least 30 hours and up to 50 days.

Once the pH and millivolt levels of the alkaline water have been stabilised a volume of electrocratic colloidal complex is added (17).

It is preferred to add around 1.5 mls of the electrocratic colloidal complex per 600 mls of the final water product Once the alkaline water plus electrocratic colloidal complex has been produced it can be bottled for storage. A typical analysis of the alkaline water produced by the

methods disclosed herein is shown in Figure 7.

Throughout the specification, unless the context requires otherwise, the word"comprise"or variations such as "comprises"or"comprising", 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.

It should be noted that the methods disclosed herein are illustrative only, and should not be taken in any way as restrictive. It should be understood that various changes, modifications and substitutions can be made to the preferred embodiments without detracting from the spirit of the invention which is set forth by the claims which follow.