Abstract:
An insulating end cap for a cylindrical electrolysis cell the type comprising at least two tubular electrodes with a cylindrical membrane arranged co-axially between them, comprises a first annular section with first and second axial ends, having at its first axial end a circular seating or one end of an outer cylindrical electrode and at its second end a circular aperture, of smaller diameter than the circular seating and co-axial therewith, to accommodate one end of the membrane. A second annular section of the end cap is detachably secured to the first and has a central circular aperture of smaller diameter than the central aperture of the first section and co-axial therewith, to accommodate one end of the inner cylindrical electrode. The two part construction of the end cap facilitates the assembly of the cell, and reduces the likelihood of breakage of the fragile ceramic membrane.

Description:
BACKGROUND OF THE INVENTION  
       [0001]     1. Field of the Invention  
         [0002]     This invention relates to an insulating end cap construction for a cylindrical electrolysis cell of the type comprising at least two tubular electrodes arranged coaxially, one within the other, with a cylindrical membrane arranged coaxially between them.  
         [0003]     2. Description of the Prior Art  
         [0004]     Cells of the type to which the invention relates can be used for example for sanitising water through electrolysis for drinking purposes, or electrolysing brine solutions to make a powerful biocide. Many types of electrochemical activation and electrolysis cells exist for this purpose, and generally comprise two concentric cylindrical electrodes, one of which acts as a cathode and the other as an anode, an ion-permeable membrane being located coaxially between them to separate the space between the electrodes into anode and cathode compartments. An electrolyte such as brine is passed through the anode and cathode compartments, separately or successively. When brine is electrolysed in this way, under suitable conditions, it can produce a sporicide solution of high strength and long shelf life, which is ecologically and human friendly.  
         [0005]     One type of concentric cylindrical cell of the type to which the invention relates is disclosed in published European Patent Application No. 922788. This discloses an electrolytic cell in which the two concentric electrodes and the membrane are received in unitary end bushes, each having a central aperture for passage of the inner electrode with surrounding concentric seatings for the membrane and the outer electrode. Cells of this type function quite well, but a problem arises in their construction. A high degree of craft skill is required to assemble them, and in particular to assemble the cell components in the end bushes, and there is a high breakage rate. With brittle ceramic cylindrical membranes, damage rates can be as high as 1 in 5.  
         [0006]     It is accordingly an object of the present invention to provide an end cap for an electrolytic cell which is easy to fit and reduces the likelihood of breakages.  
         [0007]     It is another object of the present invention to provide a cylindrical cell which is leak-free and pressure-resistant. Many existing cells start leaking over a period of time as component parts are mechanically sealed with gaskets. During the lifetime of a cell, component parts become brittle, shrink or expand, causing leakages.  
       SUMMARY OF THE INVENTION  
       [0008]     The present invention provides an insulating end cap for a cylindrical electrolysis cell of the type comprising at least two tubular electrodes arranged coaxially one within the other with a cylindrical membrane arranged coaxially between them, said end cap comprising: 
        a first annular section of insulating material with first and second axial ends, having at its first axial end a circular seating for one end of an outer cylindrical electrode and at its second end a circular aperture, of smaller diameter than said circular seating and coaxial therewith, to accommodate one end of a cylindrical membrane; and     a second annular section of insulating material detachably secured to the first and having a central circular aperture, of smaller diameter than the central aperture of the first section and coaxial therewith to accommodate one end of an inner cylindrical electrode.        
 
         [0011]     With the insulating end caps of the invention, the assembly of the cell can be greatly simplified, avoiding damage to components and allowing easier visual inspection at all stages of construction. Craft skills are not necessary, and sealants can more easily be used, avoiding the need for mechanical gasket or O-ring seals. The use of such non-toxic sealants helps to avoid leakages and imparts increased pressure resistance.  
         [0012]     The sealants and the end caps can be made of a plastics material that is approved for medical purposes, and can be in contact with drinking water. The preferred sealants are two-part epoxy sealants which possess a high chemical resistance as well as a high degree of flexibility, so that seals are maintained even when components shrink or expand during the electrolysis process.  
         [0013]     The second annular section is preferably secured to the first by means of a screw thread. This means that the end cap can be assembled and secured to the cylindrical cell components without the need to apply force to overcome friction.  
         [0014]     In a preferred embodiment of the invention, a third annular section is secured to the second section, this third section having a central circular aperture of similar diameter to that of the aperture in the second section and serving to enhance a sealing engagement between the end cap and an inner cylindrical electrode passing through said apertures of the second and third sections. This third section is preferably secured to the second section by means of a screw thread, for the same reasons as discussed above in connection with the first and second sections.  
         [0015]     One or both of the first and second sections of the end cap may be provided with lateral inlets through their outer walls, for the passage of electrolyte into or out of the cell compartments defined between the electrodes and the membrane. In the first section, the inlets can be provided axially between the seating for the first electrode and the circular aperture through which the membrane passes. In the second section the inlet can be provided axially between the first and second ends. In each case the lateral inlets are preferably arranged for tangential feed into the cell compartments so that a spiral flow pattern of the electrolyte through the anode or cathode chamber is achieved.  
         [0016]     The electrolyte inlets are preferably equipped with John Guest fittings for sealing connections to electrolyte inlet or outlet pipes.  
         [0017]     According to a further aspect of the invention, there is provided a cylindrical electrolysis cell comprising at least two tubular electrodes arranged coaxially, one within the other, with a cylindrical ion-permeable membrane arranged coaxially between them, wherein there is provided at at least one end of the cell an insulating end cap as defined above, one end of a radially outer electrode of the cell being located in the circular seating at the first end of the first annular section, one end of the cylindrical membrane being located in the circular aperture at the second end of the first section and one end of an inner tubular electrode being located in the central aperture of the second section. This arrangement is preferably provided at both ends of the cell.  
         [0018]     The cell membrane is preferably a ceramic ion-permeable membrane, more preferably comprising alumina and/or zirconia. One preferred type of membrane comprises Al 2 O 3  particles with a mean particle size of 3 to 5 μm and ZrO 2  particles with a mean particle size of 0.3 to 0.8 μm. The preferred ratio of Al 2 O 3  to 5 wt % of Al 2 O 3  and 15 wt % ZrO 2 . The end cap construction of the present invention means that relatively fragile membranes can be used. The membrane preferably has a thickness of 1-2 mm. The membrane can be made as a slip and fixed in cylindrical form.  
         [0019]     Conventional electrolysis cells of the type to which the invention relates typically have an anode made of titanium, the cathode being of a different metal. In the preferred embodiments of the present invention, both the anode and the cathode can be made from titanium, and at least the anode is preferably coated with a mixed oxide for enhanced performance. In more preferred embodiments, both the anode and the cathode are made from titanium and coated with a mixed oxide. The preferred coating structures are made from platinum or platinum metal oxides, which may be mixed with other transition metal oxides. Preferred coatings will be discussed in more detail below.  
         [0020]     Various different biocidal liquids can be produced in the electrolysis cells of the present invention, depending on the pipework configuration (flow pattern through the cell). For example, the electrolyte can be fed to the anode and cathode compartments and the electrolysed liquid can then be collected from each of these compartments separately. Alternatively, the electrolyte can be fed through both electrode chambers successively. Other factors which can be used to vary the biocidal liquid include the voltage applied to the electrodes, the electrical power absorbed, the electrode coating and physical size of the electrode, the shape of the electrodes and distances between them and the spacing and material of the membrane. The membrane material is also an important feature since it affects the mobility of ions passing between the electrodes.  
         [0021]     The preferred mixed oxide coated electrodes comprise a titanium base activated with a coating structure which may comprise platinum, preferably in finely divided form such as platinum black, or platinum metal oxide mixed with oxides of one or more other transition metal oxides such as those of titanium, tantalum, niobilum, iridium, ruthenium, rhodium or palladium oxides, or mixtures thereof. The particular coating selected will depend on the application. By depositing a number of layers, one upon the other, a noble metal mixed oxide coating can be obtained on the titanium substrate. Each layer may be less than 1 μm thick. In a preferred process for reducing the coatings, the metal compounds are dissolved in organic solvents, applied to the surface and decomposed after drying. The titanium base is thus shielded and an electrode is obtained with a small internal resistance, high loading capacity for the electric current, a constant electrode potential over the life of the electrode and a low rate of wear.  
         [0022]     When the electrode is to be used for the electrolysis of brine, for example sea water, for the production of biocidal liquids the preferred coating is a ruthenium mixed metal oxide or a platinum-iridium oxide coating on the titanium anode, depending on for example the temperature of the sea water and its salinity.  
         [0023]     Where the electrolyte feed liquid comprises a brine feed of mains water mixed with sodium chloride for the production of biocidal liquids, a ruthenium mixed metal oxide coating is preferably applied to the titanium electrode. This is to ensure an optimal conversion of electrolyte into biocidal liquid. Deposits of electrolyte or brine in the biocidal liquid are minimised, and the content of active chlorine is maximised.  
         [0024]     For sanitising water in order to make a sterile anti-oxidant drink, the preferred electrodes are coated with a platinum-iridium oxide coating or a ruthenium mixed metal oxide coating. This is to ensure the maximum production of oxygen within the electrolytic cell.  
         [0025]     The biocidal liquids produced in the electrolytic cell can have a pH varying from 2 to 8.5 and an essentially positive redox potential, typically in the range from +600 to +1200 mV. Alternatively, a wetting alkaline liquid can be produced with a strongly negative redox potential, typically in the range from −800 mV to −1100 mV, depending on the conditions applied to the cell.  
         [0026]     The negatively charged alkaline liquids are not stable and last only for about 48 hours before losing their charge. They have been used as a powerful anti-oxidant within the bodies of fish and mammals to boost the immune system. They have many other uses. The positively charged biocidal liquids can be sustained in what are stable solutions for up to two years given certain production conditions within the electrolytic cell. Although many large users of biocides may find it advantageous to manufacture fresh biocidal liquids, it can be shown that a sporicidal effect can be achieved with biocidal liquid blends for up to five months.  
         [0027]     This invention sets out to produce an electrolytic cell with some unique features that address the problems of robustness, general reliability, cost, performance, ease of manufacture and quality control (traceability and usage of approved materials).  
         [0028]     Some particular applications of the cells of the present invention will now be described.  
         [0000]     Electrochemical Activation of Mineralised Water  
         [0029]     The system used allows for two things to happen: 
    (1) It sterilises the water passing through the cell housing.     (2) It imposes an electrical charge on the water passing through the cell housing.    
 
         [0032]     Sanitising water for drinking purposes is achieved using a diaphramatic electrolyses cell and an active-coal filter, in which water is purified in several stages:  
         [0033]     First stage is the oxidation of water and its substances. Bacteria, viruses and organic substances are destroyed (oxidised). The water is saturated with short-lived oxidants, such as HClO, ClO 2 , O 3 , O 2 , H 2 O 2 , OH.  
         [0034]     The second stage takes place in a reaction chamber, where oxidation processes continue. The third stage consists of catalytic destruction of active chlorine compounds; removal of organic substances, taste and taint using activated coal as a sorbent.  
         [0035]     The final stage consists of reduction of tap water and its substances. Toxic heavy metal ions and hazardous organic substances such as herbicides, pesticides, phenols and dioxins are transformed into non-toxic hydroxyls. The water is saturated with anti-oxidants: OH − , HO 2   −  and O 2 .  
         [0036]     Electrolysis of water take place at the surface of mixed-oxide noble metal coated electrodes within the electrolytic cell. Free radicals are released during electrolysis like hydroxyls, oxidants, such as oxygen and ozone to sanitize the water passing through the anode and cathode chamber of an electrolytic cell. In order to “plate” out metals and break down organic molecules into harmless components an anthracite and activated carbon chamber are fitted next to the electrolytic cell. Part of this sanitizing process puts a predominantly negative charge on the water. This property makes the water an anti-oxidant. Anti-oxidants have many uses.  
         [0037]     The two main properties listed give this technology a wide range of uses: 
    (1) Sterilisation and purification of water sources.     (2) Potable/hot water systems/water features;     (3) Additive in the food industry harnessing the anti-oxidant properties.     (4) As a fodder assimilator and health promoter in pigs and poultry.     (5) As a skin treatment for a range of dermatitis disorders.     (6) As a health drink for humans (anti-oxidant booster of the immune system).    
 
         [0044]     To serve the needs outlined above where the quantity requirements are diverse a simple robust system for making the desired water is required. This invention seeks to use a standard cylindrical electrolysis cell which has been developed for water or brine electrolysis. Take advantage of the modular nature of the electrolytic cell and try to create an electrochemical activation process which can be tailored to address the many diverse applications.  
         [0000]     Electrolysis of Brine  
         [0045]     This electrochemical activation of a brine solution is achieved using a cylindrical diaphragm electrolysis cell (an electrolytic cell).  
         [0046]     The electrolytic cell can produce various biocidal liquids, depending on the electrical power supply, the current drawn, brine feed and flow pattern convention.  
         [0047]     In the cathode chamber, e.g. the following reactions take place: 
 
2H 2 O+2 e =H 2 +2OH − 
 
2H 3 O+2 e =H 3 +2H 2 O 2  
 
         [0048]     In the anode chamber, e.g. the following reactions take place: 
 
2Cl=Cl 2 +2 e  
 
3H 2 O=½O 2 +2H 3 O − +2 e   − 
 
2OH=½O 2 +H 2 O+2 e  
 
 and the formation of active chlorine: 
 
Cl 2 +H 2 O+HClO 
 
HClO+H + +ClO 
 
 As well as the formation of hypochlorite, as minor by-product: 
 
HClO+NaOH=NaClO+H 2 O 
 
         [0049]     Several cylindrical cells exists where a water or brine solution to be processed flows upwards through valves in the lower part of the electrolysis cell. Electrochemically received anolyte and catholyte leave the electrolysis cell by separate channels in the upper part of the electrolysis cell. The disadvantage of these electrolysis cells is the possibility of gas-filled zones forming in the upper part of electrode chambers, so that considerable losses of electricity occur which are due to counter-flow of electrochemically obtained gases and electrolytes.  
         [0050]     When the electrolytic cells of the invention are used for electrolysis of the potable water, water to be electrolysed is preferably supplied to both chambers in the lower part of an electrolytic cell, and the anolyte and catholyte received are removed separately from the upper parts of the separated chambers.  
         [0051]     A spiral feed of electrolyte into the anode and cathode chambers leads to turbulization of the electrolytes in the chambers of the electrical cell, prolongs influence of electrolysis over elementary amounts of the processed water solutions, simplifies removal of gaseous and liquid products of electrolysis and reduces possible formation of gas-filled zones in the upper points of electrode chambers.  
         [0052]     The space between outer cylindrical electrode and membrane, and between membrane and inner cylindrical electrode form separated electrode chambers whose geometric dimensions preferably satisfy the following: 
 
 D   D &gt;0.835 D S  
 
 D   B &gt;0.695 D S  
 
 D S —inner diameter of outer cylindrical electrode, mm; 
        D D —inner diameter of membrane, mm     D B —outer diameter of inner cylindrical electrode, mm        
 
         [0055]     In terms of surface area the relation between the anode and the cathode (ion exchange area) should preferably be roughly 1:1.40-1:1.50 respectively with a spacing between the electrodes (separated from the membrane) of 9 mm to 21 mm depending on the capacity of the electrolytic cell and the product requirements. The length of the ion exchange area can be varied depending on the volume required. 
     
    
     BRIEF DESCRIPTION OF THE DRAWINGS  
       [0056]     Further objects and advantages of the invention will become apparent from the following detailed description, when read with reference to the accompanying drawings which illustrate preferred embodiments thereof.  
         [0057]     In the Drawings:  
         [0058]      FIG. 1  is a side elevation of an electrolytic cell having a pair of multiple end caps according to the present invention;  
         [0059]      FIG. 2  is a cross-section on the line II-II of  FIG. 1 ;  
         [0060]      FIG. 2   a  is an enlarged detail of a part of  FIG. 2 ;  
         [0061]      FIG. 3  is a partially cutaway bottom plan view of the cell of  FIG. 1 ;  
         [0062]      FIG. 4  is a partially cutaway plan view of a first section of one of the end caps of the cell of  FIG. 1 ;  
         [0063]      FIG. 5  is a cross-section on the line V-V of  FIG. 4 ;  
         [0064]      FIG. 6  is a partially cutaway plan view of the second section of a modification of one of the end caps of the cell of  FIG. 1 ;  
         [0065]      FIG. 7  is a cross-section on the line VII-VII of  FIG. 6 ; and  
         [0066]      FIG. 8  is a schematic flow diagram of an electrolytic process using cells in accordance with the present invention. 
     
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS  
       [0067]     Referring first to  FIGS. 1 and 2 , a cylindrical electrolysis cell generally indicated by  10  comprises an outer cylindrical anode  12  enclosed on its outer surface by a cylindrical protective and insulating sleeve  14 . This electrode is preferably made of titanium, coated on its inner surface with a transition metal oxide coating as described above. An inner cylindrical cathode  16 , also preferably made of titanium and with a transition metal oxide coating on its outer surface, is arranged co-axially within the cylindrical anode, and a cylindrical ion-permeable membrane  18  is arranged co-axially between the electrodes in such a way as to define a space  20  between the anode and the membrane, which in use acts as an anolyte compartment, and a space  22  between the membrane and the cathode, which in use becomes the catholyte compartment.  
         [0068]     The ion-permeable membrane  18  is preferably a ceramic membrane, and is suitably made from allumina.  
         [0069]     An insulating end cap  23  is provided at each end of the cell, the end caps each comprising three annular sections which are co-axial with one another and secured together by means of screw threads. The three sections  24 ,  32  and  36  can best be seen in  FIG. 2 . The first annular section  24  has three circular apertures  26 ,  28  and  30 . The aperture  26  is surrounded by an annular end face  27 , against which bears one end of the insulating sleeve  14 .  
         [0070]     The aperture  26  has an inner diameter which matches the outer diameter of the cylindrical anode  12 , and is separated from the aperture  28  by an annular shoulder  27 , lying in a plane perpendicular to the longitudinal axis of the cell, and which acts as a seating for one end of the cylindrical anode  12 .  
         [0071]     The innermost circular aperture  30  of the first annular section has an inner diameter such as to match the outer diameter of the membrane  18 , such that the membrane can be slid into this section without the need to overcome substantial friction but without significant play when it is in position.  
         [0072]     A second annular section  32  of insulating material is detachably secured by a screw thread  33  to an end of the first section  24  which is remote from the seating  27  for the anode. This annular section has a circular recess within it, which is of larger diameter than the membrane  18 , so that the second section can be screwed onto the first without touching the membrane, which may be projecting axially beyond the first section.  
         [0073]     At its opposite axial end the second section of the end cap has a circular aperture  34  which accommodates one axial end of the cylindrical cathode  16 .  
         [0074]     The third annular section  36  is detachably secured to the second annular section  32  by means of a screw thread  39 , and has a central circular aperture  38  of similar diameter to that of the second section. The third annular section serves to enhance a ceiling engagement between the end cap  23  and the cathode  16 .  
         [0075]     As can be seen in  FIG. 2   a , the central circular aperture  34  of the second annular section  32  has a circumferential channel  41  accommodating a ceiling ring  43  to enhance the seal between the second section and the cathode  16 .  
         [0076]     A radially projecting terminal  48  is provided for the anode  12 , about half way along its axial length, and a similarly shaped terminal  50  is provided at one axial end of the cathode  16 .  
         [0077]     The two end cap assemblies at opposite ends of the cell are essentially the same, and each has a pair of John Guest fitting for ceiling connections of inlet and outlet pipes for electrolytes. Each of these fittings connects to a lateral inlet through one of the annular sections of the end caps, transverse to the longitudinal direction of the cell and offset from the central axis of the cell.  
         [0078]     At the lower end of the cell, an inlet fitting  40  passes through the first annular section of the end cap to the space  20  which forms the anode chamber. At the upper end, a corresponding fitting  44  is provided as an outlet connection from the anode chamber.  
         [0079]     A John Guest fitting  42  at the lower end of the cell provides an inlet connection through the second end cap section  32  to the anode chamber, and at the upper end of the cell a corresponding fitting  46  provides an outlet connection from the anode chamber.  
         [0080]     The bottom plan view of  FIG. 3  shows the electrolyte inlets in more detail. The John Guest fitting  40  connects to an inlet tube  52  which passes tangentially through the first section  24  of the lower end cap to communicate with the anode chamber  20  through an aperture  56 .  
         [0081]     Similarly, John Guest fitting  42  connects to an inlet pipe  54  through an aperture  58  in the second section  32  of the end cap, to feed electrolyte into the cathode chamber  22 . A similar arrangement at the upper end of the cathode chamber  22  provides an outlet from the chamber through a John Guest fitting  46 .  
         [0082]     The inlet tubes  52  and  54  enter the respective anode and cathode chambers tangentially to impart a spiral motion to the electrolyte passing through each of the chambers. This enhances mixing of the electrolyte, with consequent benefit to the electrolysis process.  
         [0083]     The structure of the first section  24  of the end cap is shown in more detail in  FIGS. 4 and 5 , which show the screw thread  33  at the second end of the section, the three co-axial apertures  26 ,  28  and  30  and the shape of the tangential inlet ball  56  where it enters the aperture  28 . Also illustrated is the shoulder  27  which acts as a seating for the axial end of the anode.  
         [0084]      FIGS. 6 and 7  show a plan view of the second end cap section  32 , from the side which connects to the first section. This shows the inside of the screw thread  33  and the inner aperture  34 , as well as the tangential inlet  58  for the electrolyte. The cross-sectional view  7  also shows the screw thread  39  to which the third end cap section is attached.  
         [0085]     In the version shown in  FIG. 7 , instead of an annular channel  41  to receive an O-ring, there is an open seating  60  so that an O-ring or other type of annular seal can be compressed by screwing on the third end cap section.  
         [0086]     A two pack epoxy sealant is used to seal around the axial ends of the anode  12  where it seats in the end cap first section  24 , around the outside of the axial ends of the membrane where they are received in the aperture  30  of the end cap first sections and around the axial ends of the cathode  16  where they are received in the apertures  34  of the second end cap sections.  
         [0087]     The ceramic ion permeable membrane should preferably have a low hydraulic resistance and a high mechanical strength. The porosity and the pore size of the ceramic are important for electrolysis and depend on the nature of the particles in the slurry.  
         [0088]     In one preferred process, ceramic ion permeable membranes can be manufactured by cast forming a slurry of a mixture of non-metallic and/or metallic particles in a porous mould. A slurry contains fine particles, but the majority are coarse particles. Most commonly used materials for the particles are alumina, mullite and zirconium-dioxide, but other materials can be used to give the membrane specific characteristics. After the slurry is applied to a porous mould, the slurry is fired at a temperature between 1100-1300° C. Firing is executed in a controlled environment in order to sinter the membrane without formation of cracks due to shrinkage and differences in the thermal expansion coefficient of the particles.  
         [0089]      FIG. 8  shows an example of an electrolyser system and a typical flow through such a system. The process of the present invention may be operated as illustrated by and with reference to  FIG. 8  as follows:  
         [0090]     A water supply  70 , such as towns water, is fed via an optional pre-heater  72  which is typically controlled at from 30 to 40° C. through feed lines around which are wound aerials of a low band frequency radio wave transmitter  74 . The water is optionally passed through a hard salt deioniser  76 . The towns water supply feeds both the mixer column  78 , and the brine tank  80 . The towns water supply to the mixer column  78  is used to dilute the brine solution feed. The towns water supply to the brine tank is used to prepare the brine solution, typically from sodium chloride and towns water. The towns water feed line has a T-connector  75  to direct the towns water feed to the mixer column and to the brine tank. A first valve  77 , in a first feed line after the T-connector in the towns water feed line controls the flow oftowns water to the mixer column  78 ; a second valve  79 , in a second feed line after the T-connector  75 , in the towns water feed line controls the flow of towns water to the brine tank. Regulation of these valves controls the flow of towns water to the mixer column and to the brine tank. A second T-connector  81  is situated downstream of the valve  77  between the towns water supply and the mixer column. A feed line from the brine tank  80 , via this second T-connector, provides a supply of brine, via a third valve  82  to the mixer column  78 . Regulation of the first and third valves allows the concentration of brine fed to and exiting from the mixer column to be controlled. It will be appreciated that closing the third valve  82  will isolate the brine feed to the mixer column and result in only towns water being fed into the mixer column. It will also be appreciated that the first, second and third valves may be automated and controlled in response to a suitable signal from the electrolyser system. For example, the second valve  79  may be controlled by a level detector  83  in the brine tank, the valve closing when a particular pre-set level is reached. The first and third valves  79 ,  82  may be controlled by a suitable means such as a conductivity detector  84  situated before or after the mixer column which adjusts the relative flows of towns water to obtain a pre-set range of conductivity. Further the first and third valves may be controlled by a redox meter or pH meter measuring the redox or pH value of the liquid medium exiting the electrolyser(s) (E). In this example the feed liquid exiting the mixer column  78  is caused to flow into the anode chamber  85  of the first electrolyser  90  and from the anode chamber to the cathode chamber  88  of the first electrolyser. The liquid exiting the cathode chamber  88  of the first electrolyser is caused to flow into the anode chamber  92  of a second electrolyser  91  and from the anode chamber to the cathode chamber  94  of the second electrolyser. On its way from the mixer column to the first electrolyser the feed liquid is subjected to further radio waves from a generator  86 .  
         [0091]     The liquid medium exiting the electrolyser, or if more than one electrolyser the last electrolyser  91 , is caused to flow into a gas entrainment column  95  where gases such as hydrogen, oxygen, ozone and chlorine which are produced in the process are disengaged. The gas entrainment column, is typically made of glass or plastics material which is packed with an inert support, such as plastics rings.  
         [0092]     A non-foaming non-ionic surfactant held in a surfactant tank  100  may be fed into the liquid medium exiting the electrolyser  90  either before or after the gas entrainment column  95  (shown as before in  FIG. 8 ). The surfactant may be fed into the liquid medium via a T-connector  102  and using a suitable pump, such as a peristaltic pump, to transfer the surfactant. The liquid medium exiting the gas entrainment column is ready for use as a broad spectrum biocide in sterilization, disinfection, and bio-film removal applications and the like.  
         [0093]     A central power supply and control unit  150  controls the power supply to the electrolysers  90 ,  92  via transformers  152 ,  154 , and also controls the operation of the valves and radio wave generators. It will be appreciated that any number of electrolysers may be operated in series or in parallel as part of the electrolyser system. It will be further appreciated that the pipework connecting the electrolysers may be arranged in different ways to provide liquid media with different characteristics.  
         [0094]     In a second example the liquid medium exiting the anode chamber is collected via an outlet from the anode chamber (not shown in  FIG. 8 ).  
         [0095]     In a third example part of the liquid medium exiting the anode chamber is collected and part is fed into the cathode chamber via a T-connector and outlet (not shown in  FIG. 8 ). In a fourth example the feed liquid exiting the mixer column  78  is fed via a manifold device into electrolysers connected in parallel.  
         [0096]     When the electrolyte is fed successively through the anode and cathode chamber of one or more cells in accordance with the invention, the resulting solution is known as “hanolyte neutral catholyte (ANK) solution”. This typically has a pH between 7 and 8.9, preferably 7.7+/−0.5. In this mode of operation, a rectified square wave direct current is applied across the electrodes. The electrical system applies a steady current based on the saline content of the brine flowing through the cell. This is set to certain working perimeters. The current is preferably at least 20 amps, depending on the volume and length of the cell, to ensure a good sporicidal liquid flow. Minimum brine concentrations ensure that the residues in the product are at a minimum. Brine feeds to the cell of 5 to 15 millisiemens (3 to 12 g/l) with a product concentration of 6 to 16 millisiemens (4 to 13 g/l). To preserve the life of the cell, the running temperature that is generated should be below 55° C. The electrical system is self monitoring in terms of working perimeters and also has a reverse polarity feature. This enables any surface contamination to be removed, and can be activated as desired, especially when running in a neutral product mode.  
         [0097]     When running the system to produce purified water, a mineralised water feed with a TDS of about 300 microsiemens (0.3 g/l) is enough to draw sufficient current (at least 2.5 amps) to ensure that the product is germ free and negatively charged to −100 milli-volts on the redox metre. The voltage applied can be varied according to the mineralisation of the water, which should not be less than 250 microsiemens (0.25 g/l).