Electrochemical system and method for the treatment of water and wastewater

Abstract

Contaminants are removed from untreated raw water or discharge water by applying direct current through an array of spaced, alternately charged electrodes positioned within and electrically isolated from a housing to eliminate or minimize clogging of the electrodes with precipitated contaminants. The housing is surrounded with container structure that cooperates with the housing to define an inlet chamber positioned between the source of untreated water and the housing containing the spaced array of electrodes. The container structure further includes an outlet chamber defined between the housing and the container structure for accumulating and draining water treated by the spaced electrode array.

Claims

1. A system for removing contaminants from raw water or waste water, the system including at least one electrochemical treatment module comprising: a housing having an inlet for untreated water and an outlet for treated water that has been treated within the housing; an array of electrodes within the housing, the electrodes having space therebetween of a selected distance, the space being greater than about 0.25 inch (0.635 cm); a source for applying direct current the electrodes to charge one portion of the array positively and another portion of the array negatively so as to create an electrical gradient between the portions of the array, the direct current being sufficient to oxidize and to neutralize small particle surface charges in an aqueous solution, and container structure adjacent the housing, the container structure having an inlet chamber and an outlet chamber, the inlet chamber accumulating untreated water and delivering the untreated water to the inlet of the housing, an outlet of the housing being connected to the outlet chamber of the container and an outlet line being connected to the outlet chamber to drain away the treated water, wherein the housing and container structure are both made of dielectric material with air gaps disposed between the inlet line for untreated water and untreated water accumulated in the inlet chamber and between the outlet of the housing and treated water accumulated in the outlet chamber.

2. The system of claim 1 wherein the container structure has an inner wall and the housing is polygonal with at least two pairs of vertically extending corners, each of which corners engage the inner wall to provide first and second housing walls that cooperate with the inner wall of the container structure to define the inlet and outlet chambers.

3. The system of claim 1 wherein the inlet opening extends horizontally with respect to a lower edge of the first wall of the housing and the outlet extends horizontally with respect to the second wall of the housing.

4. The system of claim 3 wherein two side chambers are formed in addition to the inlet and outlet chambers.

5. The system of claim 3 wherein a plurality of cells each defined by a module within a container are arranged in parallel to treat contaminated water flowing to each of the cells through a feed line from the source of contaminated water.

6. The system of claim 1 wherein a plurality of cells each defined by a module within a container are arranged in parallel to treat contaminated water flowing to each of the cells through a feed line from the source of contaminated water.

7. The system of claim 1 wherein a plurality of cells each defined by a module within a container are arranged in parallel to treat contaminated water flowing to each of the cells through a feed line from the source of contaminated water.

8. The system of claim 2 wherein a plurality of cells each defined by a module within a container are arranged in parallel to treat contaminated water flowing to each of the cells through a feed line from the source of contaminated water.

9. The system of claim 1 wherein the arrays of the electrodes are formed by rod sheets.

10. The system of claim 9 wherein the rod sheets are configured as a grate and wherein the grate has rod portions separated by voids.

11. The system of claim 10 wherein the voids in the grate are arranged in rows and columns.

12. The system of claim 11 wherein there are at least two rows each containing at least two voids and at least two columns each containing at least two voids.

13. The system of claim 10 wherein the voids occupy at least 50% of the area of the grate.

14. The system of claim 10 wherein the voids are in the shape of regular polygons, circles, or ovals.

15. The system of claim 10 wherein there are multiple grates.

16. A system for removing contaminants from raw water or waste water, the system including at least one electrochemical treatment module comprising: a housing having an inlet for untreated water and an outlet for treated water that has been treated within the housing; an array of electrodes within the housing, the electrodes having space therebetween of a selected distance, the space being greater than about 0.25 inch (0.635 cm); a source for applying direct current the electrodes to charge one portion of the array positively and another portion of the array negatively so as to create an electrical gradient between the portions of the array, the direct current being sufficient to oxidize and to neutralize small particle surface charges in an aqueous solution, and container structure adjacent the housing, the container structure having an inlet chamber and an outlet chamber, the inlet chamber accumulating untreated water and delivering the untreated water to the inlet of the housing, an outlet of the housing being connected to the outlet chamber of the container and an outlet line being connected to the outlet chamber to drain away the treated water, wherein the first housing wall defines an inlet opening at the bottom thereof and the second wall defines an outlet opening at the top thereof with the outlet opening being larger in area than the inlet opening.

17. The system of claim 16 wherein the housing and container structure are both made of dielectric material with air gaps disposed between the inlet line for untreated water and untreated water accumulated in the inlet chamber and between the outlet of the housing and treated water accumulated in the outlet chamber.

18. The system of claim 16 wherein the inlet opening is an undercut of the first wall and the outlet opening is an overcut of the second wall.

19. The system of claim 18 wherein the housing and container structure are both made of dielectric material with air gaps disposed between the inlet line for untreated water and untreated water accumulated in the inlet chamber and between the outlet of the housing and treated water accumulated in the outlet chamber.

20. The system of claim 18 wherein the two side chambers are filled with solid foam.

21. The system of claim 20 wherein the housing and container structure are both made of dielectric material with air gaps disposed between the inlet line for untreated water and untreated water accumulated in the inlet chamber and between the outlet of the housing and treated water accumulated in the outlet chamber.

22. The system of claim 18 wherein a plurality of cells each defined by a module within a container are arranged in parallel to treat contaminated water flowing to each of the cells through a feed line from the source of contaminated water.

23. The system of claim 17 wherein the housing containing the array of electrodes is square and the container defines a cylindrical inner wall.

24. The system of claim 17 wherein a plurality of cells each defined by a module within a container are arranged in parallel to treat contaminated water flowing to each of the cells through a feed line from the source of contaminated water.

25. The system of claim 16 wherein a plurality of cells each defined by a module within a container are arranged in parallel to treat contaminated water flowing to each of the cells through a feed line from the source of contaminated water.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) The novel features which are believed to be characteristic of the present invention, as to its structure, organization, use and method of operation, together with further objectives and advantages thereof, will be better understood from the following drawings in which presently preferred embodiment(s) of the invention are now illustrated by way of example. It is expressly understood, however, that the drawings are for the purpose of illustration and description only and are not intended as a definition of the limits of the invention. Embodiments of this invention are described by way of example in association with the accompanying drawings in which:

(2) FIG. 1 is a schematic view of an electrochemical water and wastewater treatment system in accordance with the systems, apparatus and methods of the present invention;

(3) FIG. 2 is a side view of an electrochemical treatment cell according to an initial embodiment of the invention oriented horizontally;

(4) FIG. 3 is a side view partially in elevation taken along lines 3-3 of FIG. 2 showing an array of electrodes within the electrochemical treatment cell;

(5) FIG. 4 is an end view, partially in elevation, taken along lines 4-4 showing of FIG. 3 a charge distribution on the array of electrodes shown in FIG. 3;

(6) FIG. 5 is an end view similar to FIG. 4 showing a reversed charge distribution on the array of electrodes of FIGS. 3 and 4;

(7) FIG. 6 is a side elevational view of the electrochemical treatment cell of FIGS. 2-5 with the housing removed showing details of an arrangement for mounting the electrodes;

(8) FIG. 7 is a side view of an electrochemical treatment cell similar to that of FIG. 2 but oriented vertically;

(9) FIG. 8 is a perspective, exploded view of a second embodiment of an electrochemical treatment cell, according to the invention, shown partially in section;

(10) FIG. 9 is a top view of the treatment cell of FIG. 8;

(11) FIG. 10 is a side elevation of the electrochemical cell of FIG. 9, taken along lines 10-10;

(12) FIG. 11 is a perspective view of an electrode rod sheet used with the electrochemical treatment cell of FIGS. 8-10;

(13) FIG. 11A is a front view of another embodiment of the electrode sheet of FIG. 11;

(14) FIG. 12 is an enlarged view of a connector used with the electro rod sheet of FIG. 11;

(15) FIG. 13 is a perspective view, partially in section, of a reaction chamber formed of the electrochemical cell of FIGS. 8-12 inserted into a container;

(16) FIG. 14 is a top view of the reaction chamber of FIG. 13;

(17) FIG. 15 is a side elevation of the reaction chamber taken along lines 15-15 of FIG. 14, and

(18) FIG. 16 is a schematic view of a plurality of reaction chamber cells arranged in parallel to treat a source of untreated water.

DETAILED DESCRIPTION OF EMBODIMENTS OF THE INVENTION

(19) A variety of organic and inorganic contaminants in water or wastewater are capable of undergoing direct electrochemical oxidation or reduction without the involvement of other substances or catalysts, except for the possible release of electrode material. A general understanding of this phenomenon is available from the following considerations of chemical equations and unbalanced portions of chemical equations.

(20) Electrolysis of Water

(21) In addition to organic and inorganic contaminants, water itself is also capable of undergoing electrochemical transformation including electrolysis and dissociation as follows:
2H.sub.2O.fwdarw.O.sub.2+4H.sup.++4e.sup.Reaction at the Anode (Oxidation)
2H.sub.2+2e.sup..fwdarw.H.sub.2+2OH.sup.Reaction at the Cathode (Reduction)

(22) The reaction at the cathode results in the production of both hydrogen gas and an abundance of free hydroxyl radicals. Conveniently, the hydrogen gas becomes useful for the ultimate flotation of and separation of precipitated chemical floes, suspended and colloidal solids and fats, oils and grease from the aqueous solution. Conveniently, the free hydroxyl radicals serve as reducing agents for removal of such contaminants as heavy metals and to raise the pH of the water. This reaction is below to be helpful for: Precipitation of Phosphorous Precipitation of Heavy Metals Oxidation of Nitrate and Nitrogen Compounds Bacterial Kill Oxidation of Iron
Fe2e.sup..fwdarw.Fe.sup.+2
Fe.sup.+2e.sup..fwdarw.Fe.sup.+3
Oxidation of Organic Compounds (General)

(23) Electrochemical oxidation of organic compounds occurs within an electrochemical cell when sufficient electrical potential differences (voltage) are applied to the anode and cathode electrodes. Due to the fact that organic compounds usually contain one of more high strength ionic and covalent bonds their oxidation proceeds simultaneously with the production of O.sub.2 from the electrochemical oxidation of H.sub.2O. The following formula provide a generic form of oxidation of organic compounds.
Orge.sup..fwdarw.Oxidation products
CN+2OH.sup.CNO.sup.+H.sub.2O+2e.sup.Oxidation of Cyanide
Oxidation of Arsenic

(24) Arsenic in groundwater is usually in the form of arsersite (As.sup.3). In the electrochemical cell fitted with iron electrodes the arsenite undergoes oxidation to arsenate (As.sup.5). In addition the iron released from the anodes combines with the arsenate to form the insoluble precipitate ferric arsenate as follows.
2H.sub.3AsO.sub.3+2H.sub.2O.fwdarw.2H.sub.3AsO.sub.4.sup.+H.sub.2
2Fe.sup.+22e.sup..fwdarw.2Fe.sup.+3
2Fe.sup.+3+6H.sub.2O.fwdarw.2FeOH.sub.3+H.sup.2
2FeOH.sub.3+2H.sub.3AsO.sub.4.sup..fwdarw.2FeAsO.sub.4+6H.sub.2O
Carbonates

(25) Two major contaminants which cause water hardness are calcium bicarbonate, Ca(HCO.sub.3).sub.2, and magnesium bicarbonate, Mg(HCO.sub.3).sub.2. In a first electrochemical cell according to the invention, the bicarbonates are broken down by oxidation into the corresponding carbonate, water and carbon dioxide.
Ca(HCO.sub.3).sub.2.fwdarw.CaCO.sub.3+H.sub.2CO.sub.3

(26) The calcium, carbonate is insoluble and will be captured by a filter. As the carbonates are strongly electronegative, some may plate out onto the anodes in the electrochemical cells. However, most of the carbonates do not adhere to the anodes. The carbonate acid, H.sub.2CO.sub.3, reacts with any calcium carbonate scaling in the downstream pipes re-dissolving it to soluble calcium bicarbonate. Over a period of time, scale will be removed.
CaCO.sub.3(as scale)+H.sub.2CO.sub.3(dissolved CO.sub.2).fwdarw.Ca(HCO.sub.3).sub.2

(27) As a result, the water undergoes a softening process and the downstream scaling is slowly dissolved.

(28) Nitrogen Oxides

(29) As nitrogen oxides such as NO.sub.3, NO.sub.2 and NO undergo reduction in the electrochemical cells, the nitrogen oxides undergo the following reactions:
2NO.sub.3+12H.sup.++10e.sup..fwdarw.N.sub.2+6H.sub.2OCathode:
2H.sub.2O.fwdarw.2H.sup.++O.sub.2+4e.sup.Anode:

(30) These reactions are simplified versions of a multi-step process in which the nitrogen oxides are reduced. The nitrogen oxides are converted to nitrogen gas. In cases where contamination of the treated water is severely high, the amount of gas formed may be high enough to require evacuation from the system. In such cases, the gases are trapped in the head of the filter vessel onto which an air vent connected to the outdoors may be mounted.

(31) In a further alternative, the iron anode may be replaced with an aluminum anode. When the current is applied to the electrochemical cell, the aluminum anode releases activated alumina into the solution. The activated alumina reacts with the arsenate to form aluminum arsenate. Aluminum arsenate is insoluble and will be captured in a downstream filter.

(32) The foregoing discussion provides a theoretical basis as for the success of the method and system, described herein.

(33) In the present invention the laws of physics, chemistry, electricity, thermodynamics and hydraulics are applied in a cost effective way to treat water and wastewater electrochemically while avoiding the problems and pitfalls of the past. The key to successful electrochemical treatment of water and wastewater at atomic and molecular levels is properly applying combinations of voltage, amperage, hydraulic retention time and electrode material to provide effective electrical charge densities on electrodes and electrical potential between the electrodes to then produce desired electrochemical reactions. The system described herein utilizes parallel or substantially parallel electrode array configurations for incorporating the individual treatment units into a horizontal or vertical manifold to achieve both redundancy and provide for greater system capacity.

FIGS. 1-7

(34) FIG. 1 is a schematic overall view of a water or wastewater electrochemical treatment system 20 configured in accordance with the present invention. Water 21 from a raw water source 22, or from a wastewater source 23, is screened at a screening station 24 to remove large solids which could damage downstream apparatus. The raw water source 22 can be a drilled or dug well or a body of water, such as but not limited to, a river, stream, lake, reservoir or any other source of potentially potable water. If the water 21 is from a wastewater source 23, the water can be from, a sewage plant, an industrial wastewater site or from any other source of accumulated or flowing wastewater.

(35) After the screening station 24 has removed large solids from the water 21 to prevent downstream damage, the water is pulled by a flow regulating pump 26 and conveyed to an electrochemical treatment unit 28 configured in accordance with the principles of the present invention. A monitor and control module 27 attached to the flow regulating pump 26 determines the hydraulic residence time within the electrochemical treatment unit 28, and thus depending upon applied electrical parameters, helps determine electrical charge density within the electrochemical treatment unit. A DC power unit 30 controlled by a controller 33 converts AC line current to DC and applies DC to the electrochemical treatment unit 28 while a polarity reverser 32 allows the DC to be reversed periodically in order to minimize the possibility of clogging in the electrochemical unit 28. A selected contaminate or multiple contaminates are removed form the water stream 21 by the electrochemical treatment unit 28 while an uncontaminated water stream 21A flows to a clarification/filtration station 36. If a gas, such as nitrogen (N.sub.2), is separated from the water stream 21 in the electrochemical treatment unit 28, the gas may vented by a vent 34.

(36) If the treated water stream 21A still contains suspended solid particulates precipitated by the electrochemical treatment unit 28, the suspended solid particulates are removed by a clarification/filtration station 36, which comprises either a gravitational or centrifugal separation unit 37, or a filtration unit 38. In some situations it may be necessary to use both gravitational or centrifugal separation, as well as filtration in order to provide an uncontaminated water stream 21B which may be for initial use or reuse, or for disposal back into the environment.

(37) FIGS. 2-6 illustrate an initial embodiment of an electrochemical module 40 for use as the electrochemical treatment unit 28, or for use as a stand alone electrochemical treatment unit. The module 40 is an initial prototype of an electrochemical treatment unit formed as a cell, which may be combined with other similar cells when practicing the invention. The module 40 has a horizontal orientation in FIG. 2 and has successfully demonstrated that dissolved nitrogen and dissolved phosphorous compounds are removed from a water stream contaminated therewith when mechanical parameters such as electrode spacing, speed of the pump 26 and volume of the module 40 are considered in combination with electrical parameters, such as potential, amperage and rates of polarity change. Using the module 40, Applicant was able to decontaminate a water flow 21 without clogging of the module, a drawback that has prevented current commercial use of electrochemical decontamination for water treatment.

(38) As is seen in FIG. 2, module 40 is aligned, or substantially aligned, with a horizontal axis 41. The module 40 comprises a cylindrical chamber 42 made of a dielectric material such as polyvinylchloride (PVC) and having at a first end portion 43 an inlet 44 that receives an influent in the form of the water stream 21. At a second end portion 45, an outlet 46 releases an effluent stream in the form of the water stream 21A in which previously dissolved contaminants have been separated from the water and exist in the form of relatively small particulates that are subsequently filtered, or in the form of gas that is subsequently vented. The first and second ends 43 and 45 of the chamber 42 are closed by end caps 50 and 52, respectively, made of a dielectric material such as PVC. The end caps 50 and 52 are bolted by bolts 54 to inverting rings 56 and 58, respectfully, that are received around the first and second ends 43 to 45 of the chamber 42 and are positioned in abutment with end sleeves 60 and 61 fixed to the cylindrical chamber 42. Positively charged and negatively charged leads 64 extend from the second end cap 52 on the cylindrical chamber 42 and are attached to electrodes within the chamber.

(39) Referring now to FIGS. 3-5, it is seen that within the chamber 42 an array 66 of electrodes 68, configured as rods, are imbedded in a separator 70 of insulating material adjacent to the first end cap 50, and imbedded in an insulator 72 of insulating material, at the second end cap 52 so that the electrodes 68 are electrically isolated from one another. In order to ionize and remove dissolved contaminates, it is necessary to set up electrical charge gradiants within the chamber 42 by negatively charging one portion of the array 66 of electrodes 68 and positively charging another portion of the array 66 of electrodes 68.

(40) As is seen in the end views of FIGS. 4 and 5, one array of electrodes 68A has a negative charge () while another array of electrodes 68B has a positive charge (+). This creates ionization within the water 21 being treated. In order to prevent clogging of electrodes 68B attracting negatively charged ions, the polarity of the arrays 66A and 66B are periodically reversed, as is shown by comparing FIGS. 4 and 5. By applying DC current at low voltage and keeping the influent water 21 moving though the chamber 42 at a selected speed so that hydraulic retention time is sufficient to obtain, ionization of contaminates suspended in particulate form in the water 21 being treated, and by periodically reversing the polarity of the electrode arrays, clogging of the space between electrodes array 66A and 66B is avoided. Since the particulate contaminates remain suspended, the particulates can be removed by settlement and filtration at station 36 of FIG. 1.

(41) Further with respect to the embodiment of FIGS. 2-6, FIG. 6 shows a practical way in which to install the electrode array 66 wherein the electrodes 68 are retained by the first insulator 70 located at end cap 50 using bushings 80 and retained by the second insulator 72 at second end cap 52 by bushings 82. In the arrangement of FIG. 6, the end caps 50 and 52 are made of an insulating material such as PVC.

(42) While the module 40 is shown aligned with a horizontal axis in FIG. 2, the module 40 is oriented with a vertical axis 41 in the second embodiment of the invention shown in FIG. 7. This takes advantage of the tendency of gas to flow upwardly allowing gas to vent via a vent 34 now disposed proximate the upper end 43 of the chamber 42 of the module 40.

(43) The key to successful electrochemical treatment of waste and raw water at atomic and molecular levels is effective application of voltage, amperage, hydraulic retention time and electrode material in combination to provide electrical charge densities on the electrodes and electrical potential between the electrodes to produce a desired electrochemical reaction. The power applied is determined according to the mass of material to be removed, i.e., watts/pounds removed.

(44) The following Charts A, B and C cite test data from testing the prototype illustrated in FIGS. 2-7 of the drawings. The parameters used occur within testing ranges initially selected by the inventor, which ranges do not limit the scope of the inventor's invention. The test data establish that the inventor has eliminated, or at least minimized, clogging of spaces between electrodes 68 by contaminants when electrochemically removing contaminants from water within the module 40.

(45) As is evident from the charts, preferred test ranges are as follows;

(46) DC Voltage: about 10 volts to about 50 volts.

(47) DC Amperage: about 15 amps to about 35 amps,

(48) Hydraulic retention time: about 2 minutes to about 5 minutes.

(49) Spacing between electrodes; about 0.75 inch (1.90 cm), and

(50) Polarity switching cycle: performed manually at intervals of about 5 minutes,

(51) The ranges and specific parameter values recited in the Charts A, B and C are within larger contemplated ranges as follows: DC Voltage: about 10.0 volts to about 60 volts, DC Current: about 5.0 amps to about 50.0 amps. Hydraulic Retention Time: about 30 seconds to 5 minutes, about 2 minutes, 30 seconds being preferred Electrode Diameters: about 0.25 inch (0.635 cm) is preferred, but the electrodes may be effective at other diameters Electrode Spacing: preferably >0.25 inch (0.635 cm) Electrode Materials: iron, copper, carbon, aluminum. Electrode Shape: The electrodes may have any shape effective to accomplish the invention, such as but not limited to: cylindrical rods, perforated or imperforated flat plates, undulating plates or rods. Polarity Change Cycle: about 1 minute to 15 minutes.

(52) While the cylindrical module 40 used to demonstrate the effectiveness of the invention has a length of 25 inches (63.5 cm) and a diameter of 6 inches (15.24 cm), a module used to practice the invention may have any dimensional configuration that achieves similar useful results. The electrodes 68 of the illustrated electrode array 66 are iron rods that are circular in cross section and have a diameter of inch (2.54 centimeters). The cylindrical module 40 has dimensions which are suitable for intermittent flow wherein the water being treated remains in the module for a time sufficient to apply various voltages and amperages to achieve a range of test results such as those of the Charts A, B and C.

(53) A preferable practice is to have an array of modules, configured to achieve results similar to the module 40, wherein individual modules can be readily replaced if necessary. The module can be arranged with other modules in parallel or serial arrays, or unparallel and serial arrays, to accomplish removal of contaminants from waste water or raw water. In order to increase hydraulic retention time, recycling of partially decontaminated water can be performed in order to further decontaminate already treated water.

(54) Module construction can be scaled up to a much, larger individual size, for example, a size suitable to decontaminate waste water discharged from sewerage plants. Also, module construction can be scaled much smaller, for example to decontaminate tap water or water entering a home or a community, so as to remove endocrine disrupting compounds and personal care products from potable water. Modules scaled even smaller and using DC current from batteries and/or solar cells are usable to decontaminate raw water for drinking by campers, hunters and hikers, as well as to decontaminate raw water for military personnel.

(55) The principles of the present invention, as exemplified in by the module 40 of FIGS. 2-7, can be used, to treat waste water and/or bilge water prior to discharge from ships and pleasure boats to remove contaminants. It is also contemplated that these principles are applicable to removing salt from sea water when sea water is used as a source of raw water for ships or perhaps agriculture, and for removing urea from urine recirculated to provide drinking water for astronauts.

(56) Charts A, B and C are test results establishing the effectiveness of the method and system in removing various contaminants from water and aqueous solutions.

(57) TABLE-US-00001 CHART A Electrochemical Treatment of Municipal Wastewater Plant 1 Contaminant Raw BOD.sup.1 Raw Phos Raw TKN.sup.2 Electrode Material Iron Iron Iron Electrode Spacing (inches; 0.75; 1.905 0.75; 1.905 0.75; 1.905 centimeters) Power Supplied to the System 120 Volt AC 120 Volt AC 120 Volt AC DC Voltage Applied Low 10 10 10 Medium 30 30 30 High 50 50 50 Amperage Applied Low 15 15 15 Medium 25 25 10 High 35 35 15 Hydraulic Retention Time (minutes) Low 1 1 1 Medium 3 3 3 High 5 5 5 Untreated Concentration (mg/l) 350 6.9 62 EC Treated Concentration (mgl) Low 52 4.4 44 Medium 34 1.3 39 High 26 0.8 31 Percent Removal Low 85 36 29 Medium 90 81 37 High 93 88 50 Contaminant Effluent Effluent Primary Nitrate E Coli Phos Electrode Material Iron Iron Iron Electrode Spacing (inches; 0.75; 1.905 0.75; 1.905 0.75; 1.905 centimeters) Power Supplied the System 120 Volt AC 120 Volt AC 120 Volt AC DC Voltage Applied Low 10 10 10 Medium 30 30 30 High 50 50 50 Amperage Applied Low 15 15 5 Medium 25 25 10 High 35 35 15 Hydraulic Retention Time (minutes) Low 1 1 1 Medium 3 3 3 High 5 5 5 Untreated Concentration (mg/l) 16.8 >1,600 2.3 EC Treated Concentration (mgl) Low 0.2 0 0.8 Medium 0.2 0 0.3 High 0.2 0 0.3 Percent Removal Low 99 99+ 65 Medium 99 99+ 87 High 99 99+ 87 .sup.1BODBiochemical Oxygen Demand .sup.2TKNTotal Kjeldahl Nitrogen (sum of organic nitrogen, ammonia and ammonium)

(58) TABLE-US-00002 CHART B Electrochemical Treatment of Municipal Wastewater Plant 2 Contaminant Filter Eff Filter Eff BOD.sup.1 TOC.sup.3 Effluent Ph Electrode Material Iron Iron Iron Electrode Spacing (inches; 0.75; 1.905 0.75; 1.905 0.75; 1.905 centimeters) Power Supplied to the System 120 Volt AC 120 Volt AC 120 Volt AC DC Voltage Applied Low 10 10 10 Medium 30 30 30 High 50 50 50 Amperage Applied Low 15 15 15 Medium 25 25 10 High 35 35 15 Hydraulic Retention Time (minutes) Low 1 1 1 Medium 3 3 3 High 5 5 5 Untreated Concentration (mg/l) 4 34 6.4 EC Treated Concentration (mgl) Low <2 28 6.9 Medium <2 27 8.0 High <2 8.3 Percent Removal Low 50+ 18 NA Medium 50+ 21 NA High 50+ NA Contaminant Effluent Effluent Primary Nitrate E Coli Phos Electrode Material Tron Tron Tron Electrode Spacing (inches, 0.75; 1.905 0.75; 1.905 0.75; 1.905 centimeters) Power Supplied to the System 120 Volt AC 120 Volt AC 120 Volt AC DC Voltage Applied Low 10 10 10 Medium 30 30 30 High 50 50 50 Amperage Applied Low 20 15 5 Medium 30 25 10 high 40 35 15 Hydraulic Retention Time (minutes) Low 1 1 1 Medium 3 3 3 High 5 5 5 Untreated Concentration (mg/l) 16.7 >1,600 3.5 EC Treated Concentration (mgl) Low 10.1 0 0.6 Medium 0.1 0 0.3 High 0.3 0 0.2 Percent Removal Low 40 99+ 83 Medium 99 99+ 91 High 98 99+ 94 .sup.1BODBiochemical Oxygen Demand .sup.3TOCTotal Organic Carbon (includes, but is not limited to, pharmaceutical products, such as antibiotics and endocrine disrupting compounds exemplified estrogen compounds, and to personal and household care products, such as cosmetics and deodorant sprays).

(59) TABLE-US-00003 CHART C Electrochemical Treatment of Beverage Plant Wastewater Contaminant Phosphorous Copper pH Electrode Material Iron Iron Iron Electrode Spacing (inches, 0.75; 1.905 0.75; 1.905 0.75; 1.905 centimeters) Power Supplied to the System 240 Volt AC 240 Volt AC 240 Volt AC DC Voltage Applied Low 10 10 10 Medium 30 30 30 High 50 50 50 Amperage Applied Low 5 10 10 Medium 20 20 20 High 35 30 30 Hydraulic Retention Time (minutes) Low 1 1 2 Medium 3 3 High 5 5 5 Untreated Concentration (mg/l) 3.50 0.075 6.3 EC Treated Concentration(mgl) Low 1.64 ND 7.0 Medium 1.04 ND 8.3 High 0.62 ND 8.9 Percent Removal Low 53 99+ NA Medium 70 99+ NA High 82 99+ NA

(60) The electrodes 66 used to develop She data of charts A, B, and C are circular iron electrodes having a diameter of inch (0.635 cm). For purposes of this invention the electrodes have a preferable range of inch (0.317 cm) to 5/16 inch (0.794 cm), however, the diameter may be substantially smaller wherein the electrodes have diameters which are measured in terms of wire gauge.

FIGS. 8-12

(61) Referring now to FIGS. 8-12 there is shown another embodiment of an electrochemical cell, but configured as a polygonal, preferably rectangular, conductive module 100 having an increased water treatment capacity over that of FIGS. 2-7. The conductive module 100 is within a dielectric housing 102, which is preferably square in cross section and made of a dielectric material such as fiberglass. Influent, such as but not limited to, untreated water 21 from a raw water source 22 or a waste water source 23 (see FIG. 1) is introduced by an inlet 103 provided at the bottom end 104 of the dielectric housing 102 of the conductive module 100. Treated exfluent 21A exits the conductive module 100 through an outlet 105 provided by the open top end of the dielectric housing 102.

(62) The untreated water 21 flows upwardly through a bank 110 of individual electrode rod sheets 112 having individual rods 113 which are preferably circular in cross section. (See FIG. 11). The electrode rod sheets 112 are connected to eyelets 116 along one bus bar 118 of each electrode rod sheet 112. The bus bars 118 establish an electrical connection with buses 120 and 122, buses having threaded posts 124 and 126 thereon. The electrode rod sheet 112 has buses 118 and 119 which provide either a positive (+) or a negative () polarity to the rods 113 that extend therebetween. The rods 113 are preferably circular and have a spacing of about inch (1.905 cm). The buses 120 and 122 have opposite electrical charges (+ and ) thereon so that all electrode rod sheets 112 connected to the bus bar 120 have a positive charge and all electrode rod sheets 112 connected to the bus bar 122 have a negative bias. Periodically, the polarity reverser 32 (see FIG. 1) reverses polarity on the buses 120 and 122 in order to minimize the possibility of clogging within the electrode rod sheet bank 110. Within the dielectric housing 102, the electrode rod sheets 112 are electrically insulated from one another by dielectric spacers 130 (see FIGS. 8 and 9) while adjacent electrode rod sheets 112 have electrical connections 124 and 126 of different polarities so that adjacent electrode rod sheets have opposite polarities. If over time, the individual rods 113 comprising the rod sheets 112 degrade, the electrode rod sheets or panels 112 as seen in FIGS. 11 and 12 may be readily withdrawn from the dielectric housing 102 and replaced.

(63) The conductive module 300 of FIGS. 8-12 has a preferred processing rate in a range of about 35-60+ gallons per minute and has a width in a range of about 2 to 5 feet. In practicing this invention to remove remaining contaminants from untreated discharge water 21, numerous electrochemical modules, such as the conductive module 100, are connected in parallel. For example, at a rate of about 50 gallons per minute one hundred electrochemical conductive modules 100 are expected to decontaminate about seven million gallons of water per day.

(64) FIG. 11A is a perspective view of another embodiment of the invention wherein the electrode rod sheets 112 are configured as grates 127, Bach grate 127 has rod portions 128 separated by elongated voids 129. The grates 127 may be formed by stamping metal plates, such as aluminum or aluminum alloy plates, to remove metal so as to create the voids 129. In the illustrated embodiment, the plate 127 is at least substantially flat. In another embodiment, the grates 127 are made of iron or iron alloys such as steel.

FIGS. 13-16

(65) Referring now to FIGS. 13, 14 and 15, the conductive module 100 and dielectric housing 102 are inserted into a dielectric container structure 130, which in a preferred embodiment is cylindrical, to form with the dielectric container structure 130 a reaction chamber 132. The dielectric housing 102 of the conductive module 100 has vertically extending corners 134 which engage an inner cylindrical wall 136 of the container structure 130 so as to provide an inlet chamber 140 and an outlet chamber 142. The inlet chamber 140 is connected to an inlet pipe 144 for delivering untreated water 21 to the inlet chamber of the reaction chamber 132 and the outlet chamber 142 is connected to an outlet pipe 148 connected to an outlet line for discharging treated water 21A from the reaction chamber 132. A floor 149 is integral with the bottom of the cylindrical wall 136 of the dielectric container 130. In the illustrated embodiment the conductive module 100 is square in cross section and has four vertically extending corners.

(66) In order to facilitate entry of untreated structure water 21 into the conductive module 100 the dielectric housing 102 directly support the conductive module 100 has a first wall 160 having a undercut 162 defining an inlet opening 163 allowing untreated water 21 to flow from the inlet chamber 140 into the dielectric housing 102. Hydraulic pressure in the inlet chamber 140 forces the untreated water 21 to rise in the dielectric housing 102 so that the untreated water 21 is exposed to the electrode rod panels 112 for a time sufficient to remove contaminants from the untreated water 21 to produce the treated water 21A. In one example of the illustrated embodiment, the undercut 162 has a height of about 1 inch providing a 1 inch inlet opening in the dielectric housing 102 communicating with the inlet 104 of the conductive module 100.

(67) The treated water 21A then flows over a top edge 166 of a second wall 168 of the housing 102, which top edge 166 is an overcut which is lower than the top edges of the first wall 160 and two side walls 170 and 172 of the dielectric housing 102. From the top edge 166, the treated water 21A flows downward in the outlet chamber 142, and out of the outlet pipe 148 to the clarification/filtration station 36 (FIG. 1). The overcut reducing the height of the top edge 166 is substantially greater than the undercut 162. For example, the overeat over the top edge 166 is about 6 inches while the undercut 162 through the first wall 160 is about 1 inch.

(68) As is seen in FIGS. 13 and 15, there are pair of side chambers 176 and 178 which are preferably filled with foam. In this illustrated embodiment, the dielectric container structure 130 is preferably made of fiberglass and the dielectric housing 102 within the container structure 130 is preferably made of Polyvinyl Chloride (PVC) forming a dielectric support structure for the conductive module 100.

(69) As is seen in FIG. 15, there is an air gap 170 between the outlet end 171 of the inlet pipe 144 and the top surface 173 of the untreated water 21 accumulated in the inlet chamber 140. The air gap 170 electrically isolates the untreated water 21 from the upstream portion of the treatment system 20 illustrated in FIG. 1. Similarly, there is an air gap 175 between the outlet of the dielectric housing 102 formed by the over cut 166 and the top surface 177 of the treated water 21A accumulating in the outlet chamber 142. There are vents 178 and 178a through the first wall 160 and dielectric container 130 adjacent the inlet pipe 144 and a vent 179 at the top of the outlet chamber 142.

(70) As is seen in FIGS. 14 and 15, the inlet pipe 144 includes a PVC ball valve 180 and the outlet pipe 148 includes a PVC ball valve 182. The inlet pipe 144 has a diameter (for example 3 inches) which is larger than that of the outlet pipe 148 (for example 2 inches). A PVC drain valve 186 is placed in a portion of the floor 149 at the bottom of inlet chamber 140. Preferably, the outlet pipe 348 is beneath the portion of the floor 149 located at the outlet chamber 142. The top of the housing 102 is preferably open, to the atmosphere in order to let gases such as nitrogen vent from the water 21 being treated by the electrode rod sheets or panels 112.

(71) In order to process about 40 gallons/min of contaminated water, the reaction chamber 132 has a dielectric housing 102 with a width of about 24 inches and a height of about 30 inches, which reaction chamber 132 is contained within a dielectric container structure 130 having a diameter of about 36 inches. In a preferred embodiment, only a single input pump 26 (see FIG. 1) is connected to the inlet pipe 180; however as is seen in FIG. 15, a pump 178 may be placed on the outlet pipe 148 that provides an outlet line for drainage of the treated water 21A from, the outlet chamber 142.

(72) The inlet and outlet valves 180 and 182 are adjusted so that the level of the treated water 21A emerging from the module 100 and flowing over the overeat edge 166 does not rise above the top of the container structure 130 and overflow the container structures.

(73) A cap 185 covers the reaction chamber 132 and has a dog house vent 186.

(74) Referring now to FIG. 16, a plurality of reaction chambers 132 (a-n), each of which is as illustrated in FIGS. 13-15, are arranged in parallel (a-n) connection with a feed pipe 190 feeding a parallel array of inlet pipes 144. The inlet pump 26 (also see FIG. 1), pumps untreated wafer to each of the reaction chambers which drain through outlet pipes 148 (a-n) to a drain line 192, The drain line 192 connects to a final processing station 36 (FIG. 1) where additional clarification and/or filtration occurs before clear treated water 21B (FIG. 1) is released back into the environment or collected in holding ponds or containers for recycling.

Examples

(75) a) When using the module 100 within the dielectric container structure 130 of FIGS. 13-16, a maximum power level of about 15 Kw per module is sufficient for various applications. The actual power level applied depends on the chemical make-up of the water being treated. Preferably, the 15 Kw power supply is capable of producing direct current at 500 amps and 30 volts, or any other combination of amperage or voltage within the 15 Kw envelope.

(76) b) In a specific example, laundry water was treated at a DC power level of 400 amps and 9 volts with satisfactory results, however a higher amperage is thought to achieve better results. The satisfactory results were achieved at a pump speed of 16.5 U.S. gallons per minute (62.46 liters per minute) with a hydraulic retention time of about 2 minutes. Specifically, removal of contaminants was observed at 95 watts/gallon [9 volts400 amps/38 gallons (94.74 liters)].

(77) c) Experiments on synthetic soapy samples using the module of FIGS. 2-7 used voltages in the range of 10 v to 20 v with amperages remaining under 40 amps arrange for this purpose and utilizes a maximum voltage of 50 volts and maximum amperage of about 47 amps.

(78) d) For acidic mine drainage it was calculated that about 1 Kw per gallon (3.785 liters) is suitable.

(79) These examples are indicative of results achieved by this invention thus far. The selected ratio of voltage/amperage depends on the contaminant being removed from the water.

(80) Other variations of the above principles will be apparent to those who are knowledgeable in the field of the invention, and such variations are considered to be within the scope of the present invention. Other modifications and/or alterations may be used in the configuration and/or manufacture of the apparatus of the present invention, or in methods of practicing the present invention, without departing from the spirit and scope of the accompanying claims.

(81) Moreover, the word substantially when used with an adjective or adverb is intended to enhance the scope of a particular characteristic.

(82) Without further elaboration, it is believed that one skilled in the art can, using the preceding description, utilize the present invention to its fullest extent. The preceding preferred specific embodiments are, therefore, to be construed as merely illustrative, and not limitative of the remainder of the disclosure in any way whatsoever.

(83) In the foregoing and in the examples, all temperatures are set forth uncorrected in degrees Celsius and, all parts and percentages are by weight, unless otherwise indicated.

(84) The entire disclosures of all applications, patents and publications, cited herein and of pending U.S. application Ser. No. 12/492,367, filed Jun. 26, 2009, are incorporated in their entirety by reference herein.

(85) The preceding examples can be repeated with similar success by substituting the genetically or specifically described reactants and/or operating conditions of this invention for those used in the preceding examples.

(86) From the foregoing description, one skilled in the art can easily ascertain the essential characteristics of this invention and, without departing from the spirit and scope thereof, can make various changes and modifications of the invention to adapt it to various usages and conditions.