Total solution for water treatments
All pollutants dissolved or existed in water can be grossly classified as ionized and neutral species. The former includes inorganic and organic ions, while the latter contains inorganic molecules, organic molecules and organisms. Using flow through capacitor for performing capacitive deionization (CDI), the ionic contaminants can be effectively and economically removed from water. Whereas the neutral contaminants are not retained in the static electric field of CDI, they can be decomposed upon flowing through an electrolytic ozonator. Either gaseous or ionic products will be generated at the ozone treatment, and the ionic byproducts can be subsequently removed by CDI. By integrating the electrolytic ozone reactor with flow through capacitor, the O3/CDI hybrid technique becomes a total solution for eliminating hazardous materials in water. Both the reactor of in-situ ozone and the flow-through capacitor (FTC) of CDI are operated in energy conservative and pollution free conditions, so the detoxification of water is highly cost effective.
Latest Patents:
- METHODS AND COMPOSITIONS FOR RNA-GUIDED TREATMENT OF HIV INFECTION
- IRRIGATION TUBING WITH REGULATED FLUID EMISSION
- RESISTIVE MEMORY ELEMENTS ACCESSED BY BIPOLAR JUNCTION TRANSISTORS
- SIDELINK COMMUNICATION METHOD AND APPARATUS, AND DEVICE AND STORAGE MEDIUM
- SEMICONDUCTOR STRUCTURE HAVING MEMORY DEVICE AND METHOD OF FORMING THE SAME
1. Field of the Invention
This invention relates to the elimination of ionic and neutral contaminants from water by using low power consumption without secondary pollution. More specifically, the invention relates to an integration of two techniques, low voltage ozone (O3) reactor and capacitive deionization (CDI) reactor, into a continuous flow-through system for reducing the conductivity and toxicity of various water.
2. Background of the Related Art
Water bound contaminants may stay as a free form, an emulsified form, dissolved but not dissociated, or dissolved and dissociated species in water. Charge is the main property to differentiate ionic pollutants from neutral ones. The objectives of all water treatments are the reduction of total dissolved solid (TDS), chemical oxygen demand (COD) and biological oxygen demand (BOD), as well as colony forming unit (CFU) of bacteria and viruses. TDS is a measure of ionic species, whereas the other indexes are important for indicating the pollution degree of water by neutral contaminants. In the removal of COD and BOD, N- and P-containing nutrients and organic substances are the subjects to be eliminated from domestic, industrial, agricultural and animal wastewater. Among the foregoing contaminants, ammonia (NH3) is the commonest compound produced from manufacturing processes or biological activities. Ammonia dissolves easily in water as unionized form (NH3) and ionized form (NH4+). The unionized form is toxic to fish and other aquatic life, while the ionized form is not. However, both forms of ammonia will cause eutrophication to rivers, lakes and dams jeopardizing water sources for human use. Currently, ammonia is widely removed from water by using biological treatment as seen in U.S. Pat. Nos. 6,572,773; 6,929,942; 6,936,456; 6,936,708; 6,984,317; 6,984,323; 6,991,931; 7,001,516 and 7,001,519. Through adsorption or precipitation, ammonia is removed chemically as described in U.S. Pat. Nos. 5,294,348; 6,838,069; 6,994,793 and 7,005,072. The chemical treatment requires the use of expensive chemicals, and the chemicals in turn become a source of pollution. Not only a carbon source, a chemical, is needed for the growth of microbes, also the biological treatment is a slow process conducted in a prescribed conditions of pH, temperature, oxygen content and ammonia level. Besides, the microbes can only take care ammonia at a concentration of 700 mg/liter or lower.
In order to expedite the treatment speed of ammonia, as well as to lower the cost of treatment, electrolytical techniques are developed in U.S. Pat. Nos. 6,348,143; 6,712,947 and 6,984,326. As a matter of fact, the electrolytical treatment utilizes the reaction between halide ions and ozone to form hypohalite ions as the reagent to oxidize ammonia. In terms of oxidizing power, ozone is more potent than the hypohalite ions. It would be more effective and convenient to use ozone directly for the decomposition of ammonia, organic substances and pathogens. Ozone is used to control the growth of red tide organisms on the surface of seawater in U.S. Pat. No 6,984,330, and the gas is applied on mails and shipping parcels for reducing the biological load including anthrax in U.S. Pat. No. 6,984,361. All of the foregoing patents of ozone applications rely on corona discharge for the generation of ozone. In addition to high operating voltage (>2000 Volts), the silent discharge requires an oxygen supply system, an ozone delivery system and a protective shield against gas leak. As ozone does not dissolve easily in water, the gas can only be dispersed water into fine bubbles for effective oxidation. The high cost and the low ozone solubility limit the corona-discharge ozone for broad utilization in water treatments. To solve the foregoing problems, ozone is directly generated in water by using a low voltage in conjunction with a high current to electrolyze water as elaborated in U.S. Pat. Nos. 6,984,295 and 6,984,304. But there are rooms for improving the overall efficiency of ozone generation and decontamination in the electrolytic ozone. For example, an ion-exchange membrane is used in '304 to separate hydrogen from ozone. The membrane is expensive and vulnerable to fouling. On the other hand, patent '295 needs multiple electrodes and a design for wastewater to flow through the reactor, so that ammonia and other neutral contaminants can be decomposed concurrently with the formation of ozone bubbles.
Two steps of reaction, that is, nitrification and denitrification, are involved in the biological removal of ammonia. Firstly, two bacteria species (Nitrosomonas and Nitrobacter bacteria) are used to exothermically oxidize ammonia to nitrite (NO2−) and nitrate (NO3−) under aerobic conditions. Next, the anions are reduced by denitrifying bacteria (facultative anaerobes) to nitrogen under anaerobic conditions. As ammonia is completely ionized, the byproducts can be quickly removed by a technique other than biological or chemical treatments. In lieu of the complexity of wastewater, reverse osmosis (RO) and ion exchange are not appropriate for the removal of ionic contaminants from the water. The foregoing two methods are particularly forbidden, if the ionic species are treated following the ozone oxidation in a continuous sequence without using chemicals and extravagant pretreatments. Both the membranes of RO and the resins of ion exchange are easily fouled and impaired by scaling, organic fouling, particulate fouling, and biofouling. Virtually all wastewater can guarantee the occurrence of one or all types of fouling. Capacitive deionization (CDI) is more fouling-resistant than RO and ion exchange, and CDI is very effective on removing the ionic species from water. CDI utilizes a flow through capacitor (FTC) and a static electric field to purify water containing ionized substances. As the wastewater pass through the charged electrodes of FTC, the ions will be adsorbed on the surface of electrodes. The power consumption of CDI treatment is very minimal at ion removal, and the residual electricity can be directly recovered at the regeneration of FTC electrodes as revealed in U.S. Pat. Nos. 6,580,598 and 6,661,643. It is the capacity of FTC that mainly determines the capability of CDI. In U.S. Pat. No. 7,000,409, a commercial FTC is used to remove NO3− and SO42− for converting condensed water of engine exhaust into potable water as a water source at arid areas, such as, desert. Only a small range of TDS is reduced in '409 indicating that the FTC employed is not suitable for large-scale treatment of wastewater. A FTC of high throughput is needed for integrating with the flow-through ozone reactor into a continuous treatment system for on-line mass purification of miscellaneous water containing both ionic and neutral pollutants.
SUMMARY OF THE INVENTIONThe present invention offers a continuous water-treatment system consisting of flow-through ozone reactor, parallel-packed flow-through-capacitor (FTC) for performing CDI, and supercapacitor for the power management of both ozone reactor and FTC. The ozone reactor and FTC each has a novel electrode set having the same configuration and construction. However, different active materials are used for the electrodes of ozone reactor and FTC.
The novel electrode set includes a plurality of identical first metal sheets longitudinal parallel to each other; a plurality of identical second metal sheets longitudinal parallel to the first metal sheets, wherein the first metal sheets and second metal sheets are arranged alternately; a first electrical rod penetrating the first and second metal sheets and electrically connecting the first metal sheets to a power supply, wherein the first electrical rod and the first metal sheets form a first electrode; a second electrical rod penetrating the first and second metal sheets and electrically connecting the second metal sheets to the power supply, wherein the second electrical rod and the second metal sheets form a second electrode; a plurality of first insulators disposed on the first electrical rod for providing electrical insulations between the second metal sheets and the first electrical rod and disposed on the second electrical rod for providing electrical insulations between the first metal sheets and the second electrical rod.
The metal sheet used in the ozone reactor is in the form of mesh, screen, or porous plate. The holes on the electrodes allow water to flow through in a closed housing. Or, the ozone reactor without a housing can be submerged in an open water body to perform in-situ detoxification. Each of the first and second electrodes of the ozone reactor is attached to a separate electrical rod. Though a plurality of metal sheets are disposed in a stack configuration, the metal sheets of the same polarity are connected in parallel on one electrical rod. The polarities of the electrical rods are switched at a selected time interval, therefore, each metal sheet can become anode to generate ozone. Not only the throughput of ozone can be increased, but also the lifetime of electrodes can be prolonged, and the electrodes can be protected from fouling. Platinum metal, iridium oxide or synthetic diamond can be selected as the active material deposited in thin film on the metal sheets for generating ozone. The high current required for the generation of ozone is delivered by supercapacitors via PWM (pulse width modulation). During operation, the ozone reactor can work continuously without the need of regeneration. The operational voltage, ranging from 24 V to 3 V DC, of the ozone reactor depends on the conductivity of water, while the operational current is adjusted at a balance between the ozone production and electrode life. High current is beneficial to the ozone throughput, but it is detrimental to the adherence of the deposited or plated film of active material.
FTC is the heart of CDI treatment with respect to both performance and cost of the technique. The present invention provides a stack configuration electrode set similar to that of the ozone reactor for FTC. Therefore, the FTC can be operated in a closed system, or it can be submerged in an open water body to adsorb ions continuously as long as a DC current is supplied to the electrodes of FTC. There are two distinctions between FTC and the ozone reactor. One is the active material and the other is the regeneration of electrodes. In FTC, an active material with large surface areas, such as, activated carbon, carbon nanotube or fullerene (C60), is employed for adsorbing ions. Because of quick saturation of the electrodes by the adsorbed ions, FTC requires constant regeneration. Otherwise, the saturated FTC electrodes have no room for ion removal. The CDI treatment comprises a series of charging and discharging swings of FTC. Electricity can be directly recovered in the regeneration of FTC with automatic de-sorption of ions that require a rinsing water to exit the FTC. Obviously, incomplete flush of ions will jeopardize the water quality of CDI treatment. Elimination of cross contamination of CDI treatment is one objective of the present invention. Similar to the ozone reactor, supercapacitor is also employed in the power management system of CDI. The capacitor performs a dual function of energy storage and energy delivery in the reduction of TDS.
As described above, supercapacitor is a key component in making CDI energy effective, as well as allowing ozone formation on a small potential source. With quick charging and discharging property, supercapacitor can serve as a power amplifier and power buffer to deliver power needed at ozone oxidation and ion removal, as well as to store energy at FTC available for recuperation. An appropriate utilization of the effective energy of supercapacitor will further improve the efficiency of power consumption in ozone oxidation and CDI treatment.
A further aspect of the present invention is to integrate the flow-through ozone with CDI into O3/CDI hybrid treatment system for purifying water in a continuous operation. After a simple filtration, all neutral contaminants existing in the intake water will be first oxidized by the on-line O3 reactor into gaseous and ionic products. The ion-loaded stream is then directed into the FTC units for ion removal to become potable, reusable, or dischargeable water. In the operation of O3/CDI hybrid water treatment system, O3 will provide an oxidation equivalent to incineration to neutral substances and microorganisms, while CDI will adsorb all charged species with high recovery rate of water and lower power consumption. The O3/CDI hybrid water treatment can singly remove both ionic and neutral species, the most abundant pollutants in water. No chemical is required for either O3 or CDI treatment, thus, no secondary pollution will incur.
The present invention is best understood by reference to the embodiments described in the subsequent section accompanied with the following drawings.
The preferred embodiments of each component of the O3/CDI hybrid water treatment system of the present invention are presented in the subsequent sections.
FTC (Flow Through Capacitor)FTC is the heart of CDI where ions are removed so that the TDS of water can be reduced to the desired levels.
-
- 1. Water distribution at the holes of the central water inlet is non-uniform resulting in a low efficiency of electrode utilization. In other words, not every area of the electrode surface provided has been utilized for ion adsorption leading to ion removal and TDS reduction.
- 2. At the regeneration of FTC, the desorbed ions are difficult to flush out, and some of them are trapped inside the FTC, which significantly contaminate the water quality at the next run of ion removal.
In order to solve the cross contamination and to improve the electrode utilization rate, the present invention offers an innovative design for the configuration of FTC.
Both types of FTC as depicted in
The present invention also applies the electrode set of stacking configuration as
-
- 1. Titanium metal is the substrate for the ozone reactor, whereas the FTC can use a cheaper substrate, such as, stainless steel. The environments in the ozone reactor is extremely harsh, thus, titanium is required to resist the oxidative corrosion.
- 2. Platinum, iridium oxide, or synthetic diamond film is the active material for the ozone reactor, whereas carbonaceous material serves as the ion-adsorbing medium for the FTC. Ozone is generated on the aforementioned precious material when the material is charged as anode.
- 3. The electrodes of the ozone reactor can be in the form of mesh, screen or plate, whereas the electrodes of FTC has smaller openings relatively.
- 4. The ozone reactor can remove numerous neutral contaminants resulting in the reduction of BOD and COD through complete oxidation, whereas the FTC removes ionic species resulting in the reduction of TDS via surface adsorption.
- 5. The ozone reactor can continuously remove BOD and COD without the need of regeneration, whereas the FTC requires frequent cleaning.
- 6. The ozone reactor provides a non-selective and destructive treatment, whereas the FTC offers a non-destructive treatment, and different ions may be adsorbed and released at different stages of CDI operation.
- 7. Power is consumed at the ozone reactor, whereas residual power can be directly, without energy conversion, recovered from the FTC during regeneration.
- 8. The electrode polarities of the ozone reactor are switched at a preset time interval, whereas the FTC is switched between charging (to adsorb ions) and discharging (to regenerate the electrodes) at a longer time interval.
In addition to the same configuration of electrode assembly, the ozone reactor and the FTC of the present invention also share the use of supercapacitor as a key component for power management. For saving energy, both of the ozone reactor and the FTC are operated using PWM (pulse width modulation) instead of continuous power provision. Not only the water treatments are more energy effective on using PWM, a balance state that may exist in ozone formation and ion adsorption can be disrupted via the intermittent power supply. As a result, water treatments for reducing TDS, COD and BOD of water using CDI and flow-through ozone may be facilitated by applying the PWM technique. Similar to the FTC of
-
- 1) Every electrode disposed in the reactor can serve as the anode to generate ozone in water.
- 2) Since the electrodes work only “half” of the operation time as anode, their service life can be prolonged.
- 3) Fouling of electrodes is inhibited due to every electrode will become the anode thereon deposits will be destroyed by ozone.
The innovative ozone reactor of the present invention does not use any ion exchange membrane. Although the membrane can separate ozone from hydrogen resulting in a higher oxidant concentration, but the membrane is expensive and vulnerable to scaling and particulate fouling. If a membrane is employed in the new ozone reactor of the present invention, neither the closed mode ozonation, wherein water flows through the reactor sitting in a housing, nor the open mode ozonation, wherein the reactor is submerged in an open body of water at any depth, is allowed due to the blockage of water flow by the membrane or quick fouling of membrane, respectively. During either mode of ozonation, the ozone reactor is surrounded by contaminants, and the latter will react with ozone as soon as the micro bubbles of the oxidative gas are formed. Because of the close proximity, the reaction between contaminants ozone will be faster than that between ozone and hydrogen. In other words, there is a plentiful amount of ozone in water for the in-situ destruction of contaminants. The in-house studies have found the distinctive odor of ozone in the water stream after it passed the ozone reactor. On the other hand, the presence of hydrogen may be beneficial to the removal of any reducible pollutants in the water to be treated. Ozone can provide a complete oxidation with destructive effect equivalent to incineration, therefore, all neutral contaminants will be converted to gaseous, ionic, or a mixed products in a less toxicity than the original pollutants. Once the pollutants become ionic species, the FTC will quickly remove the ionic byproducts from water. Similar to the CDI treatments, the operational voltage of the ozone reactor depends on the conductivity of water to be treated. Generally, the voltage is less than 24V DC. If the treated water is extremely conductive, for example, seawater, it is preferred set the voltage no more than 5V DC to avoid an excess current applied to the ozone reactor. When the current density is above 1 A/cm2, the ozone forming materials, such as, platinum and iridium oxide, may peel off the titanium substrate. Ozone concentration in water is sensitive to water temperature, and low water temperature can stabilize the presence of ozone in water. Thus, water circulation due to the flow-through operation will keep the water temperature of the ozone reactor low and constant, and the water movement will promote the oxidation of pollutants as well. Under the condition of high halide ion concentrations, for example, 50 ppm or above, the flow-through ozonation of the present invention will generate hypohalite ions in addition to ozone. Nevertheless, the hypohalite ions are also potent oxidants for the removal of BOD and COD. The hypohalite ions can stay in water at a much longer time than ozone, and water containing the disinfecting anions is good for storage and transportation as a bactericide. More importantly, the hypohalite ions of the present invention are produced on-line and the residual ions after the disinfection can be removed by CDI.
SupercapacitorsAs described in the foregoing sections, supercapacitor is a key component for managing the power utilization in the operations of the new FTC and the new ozone reactor of the present invention. Supercapacitor receives its name of “super” from its capability of storing hundreds to thousands times energy of the conventional capacitors. Like the latter, supercapacitor is a passive energy-storage device with fast charging and discharging rates. However, due to the large capacitances in a small volume, supercapacitors have the following unique properties as added values.
-
- 1. Within the rated working voltages, the capacitors can be charged with any magnitude of currents. Henceforth, the residual current of saturated FTC units, large or small electricity, can be quickly and completely transferred to supercapacitors for storage for latter use. By discharging the saturated FTC units in series, the transfer of the residual energy of FTC to supercapacitors can be expedited. Desorption of the adsorbed ions from the electrodes of FTC is promoted as well.
- 2. When the FTC units and the ozone reactors of the present invention demand large currents for operation, supercapacitors can fulfill the needs in a real-time response. This will save the cost of water treatments for a power supply with large current output, for example, 50 A or above, is very expensive. By the provision of low currents from an economical potential source, supercapacitors can deliver tens times of current for large-scale water treatments. Because the load for the potential source is low, fire hazard is thus prevented.
- 3. Supercapacitors can deliver a power at many folds of an input power without energy conversion and electrical components, such as, transformer and converter. On the other hand, supercapacitors can serve as energy buffer for storing the energy recovered from the regeneration of FTC. The energy storage of supercapacitors is conversion free as well. Energy is directly deposited and withdrawn at a very minimal loss. Using supercapacitors for the power management of water treatments, the energy consumption of the treatments will be highly cost effective.
- 4. Supercapacitors have a long lifetime without maintenance. The capacitors also have good temperature characteristics and outdoor suitability. Supercapacitors are known to assist the ignition of engines at frigid temperatures.
- 5. The working voltage of supercapacitors is low, which is consistent with the low operational voltages of the FTC and the ozone reactor of the present invention. Low operational voltage allows the water treatments to be driven by batteries, fuel cells, and renewable energies (e.g., solar cells and wind turbines). The latter potential sources are generally low in power output that can be easily compensated by the use of supercapacitors.
As a matter of fact, the FTC as depicted in
The flow through ozone reactor, the FTC, and DC power supplies using the supercapacitors operated via CD swing are integrated to form a preferred embodiment of compact and self-sustained water treatment system as shown in
The ozone reactor and FTC of the present invention utilize the same configuration of electrode stack as shown in
The practice of the present invention can be better understood by reference to the following examples, which are provided to illustrate the performance of ozone reactor and FTC unit individually and collectively.
EXAMPLE 110 different reagent grade salts: CuSO4, FeSO4, Ca(NO3)2. Fe(NO3)2, Al(NO3)3, NaNO3, Zn(NO3)2, K3PO4, Na3PO4 and NaCl, are individually dissolved in 1 liter deionized water to form 10 pure solutions with TDS ranging from 700 to 1000 ppm. Each solution is deionized on 5 serially connected units of cylindrical FTC, as shown in
1.5 liters of 1% ammonia (NH3) water is prepared for ozonation using an ozone reactor as revealed in U.S. Pat. No. 6,984,295, which is currently owned by the assignee of the present invention. A pair of platinum coated titanium meshes, each is 10 cm wide by 10 cm long with opening of 3.5 mm×6.5 mm, is used to form the ozone reactor. The ozone reactor is placed in the container of 1.5 liters ammonia water under the application of 8.5V average voltage and 1.75 A average current and PWM control. Only the TDS of the ammonia water during ozonation is measured, and the hourly variation of TDS is shown in
Next, the ozonated water is deionized using a single FTC unit as example 1, as well as 3V DC for deionization. TDS of the water is reduced smoothly from 600 to 150 ppm as shown in
6 g of ammonia is dissolved in 2 liters tap water, which is mixed with 1 liter of filtered seawater (TDS=35,000 ppm). The salted ammonia water as prepared is first oxidized using an ozone reactor with electrode configuration of
If 2 liters tap water is mixed with 1 liter seawater, the mixture has alkalinity of pH 7.6. As soon as ammonia is added to the foregoing mixture, pH of the mixture jumps to 10.4. With the progress of ozonation, pH of the ammonia brine is decreasing. Thus, a complete oxidation of ammonia should be reached between the 3rd and 4th hour ozonation according to Table 1. If the weight ratio between ammonia and ozone is 1:1, the ozone reactor of the present reactor should generate more than 1.5 g of ozone per hour. A neutral pH levels, all neutral ammonia molecules in water will turn ammonium (NH4+). The pH of water should be at least 10.5 for ammonia to be stripped as vapor. The applied current for ozonation is fixed at 10 A, whereas the operational voltage is automatically determined by the conductivity of water. Due to constant circulation, the water temperature varies between 23° C. and 25° C., which is very close to the ambient temperature. After ozonation, the oxidized water is subjected to deionization using stack configuration as
20 liters of wastewater of a steel plant is treated to reduce its COD from 314 ppm to below 100 ppm. The water was first oxidized then desalted on a O3/CDI hybrid unit as shown in
Table 2 indicates that the total electrode area for the ozone reactors is much smaller than that for CDI, and it is reflected by the degree of COD reduction. Since the water contains NH3, which is oxidized to NO2− or NO3− during ozonation, CDI will have a faster removal rate for the ions than the oxidation of ions by O3. The flow of water was 1.5 l/min for both treatments, and it took about 13 minutes for the treated water to pass through the FTC modules. Had the water allowed to pass the FTC units one more time, the COD would be reduced further. No chemical or bacteria is used, therefore, the treatments by O3/CD are clean, economical and fast.
From the above examples and other in-house tests, the present invention clearly provides a solution of chemical free, low energy consumption and low space area for various water treatments. Removal of TDS, COD and BOD can be completed in one line or in open water body. Expansion of the O3/CDI hybrid system for any scale of water treatment is straightforward and easy. Both of the ozone reactor and FTC unit are modular, they can be added with the increasing amount of water for treatment. All materials used for constructing the ozone reactor and FTC unit are environmental friendly, and the metal components are recyclable. Electricity is used to generate ozone, as well as to control the adsorption and desorption of ionic contaminants in a clean, fast and high efficiency state. Supercapacitor is used in the custom design of the power needs of the O3/CDI hybrid water treatment system leading to energy conservation and high dependability. As no chemical or bacteria is used, ions remain in the original states and become recyclable at the FTC unit of CDI treatment. Even the common salt of seawater is a precious resource to human life and animal life, as well as to many industrial productions. The application of the O3/CDI hybrid system of the present invention is almost endless. Most importantly, the system offers a natural and economical solution for water treatments.
Claims
1. A water treatment system for removing contaminant in subject water comprising:
- an inlet for receiving the subject water;
- at least one ozone reactor for receiving the subject water from the inlet and providing ozone by electrolyzing the subject water, the ozone reactor including:
- a first electrode set for being submerged in the subject water wherein the first electrode set comprises a first electrode and a second electrode; and
- a first power supply for applying a direct current voltage below 24V to the first electrode set, wherein the first power supply is capable of changing the polarities of the first and second electrodes at a predetermined interval of time;
- at least one flow through capacitor for performing capacitive deionization on the subject water from the ozone reactors and removing ionic contaminant from the subject water, the flow through capacitor including: a second electrode set for being submerged in the subject water wherein the second electrode set comprises a third electrode and a fourth electrode; and
- a second power supply for applying a direct current voltage about 1˜9V to the second electrode set; and
- an outlet for draining the subject water from the flow through capacitors.
2. The water treatment system as claimed in claim 1, wherein the first electrode set comprise
- a plurality of identical first metal sheets longitudinal parallel to each other;
- a plurality of identical second metal sheets longitudinal parallel to the first metal sheets, wherein the first metal sheets and second metal sheets are arranged alternately;
- a first electrical rod penetrating the first and second metal sheets and electrically connecting the first metal sheets to the first power supply, wherein the first electrical rod and the first metal sheets form the first electrode;
- a second electrical rod penetrating the first and second metal sheets and electrically connecting the second metal sheets to the first power supply, wherein the second electrical rod and the second metal sheets form the second electrode;
- a plurality of first insulators disposed on the first electrical rod for providing electrical insulations between the second metal sheets and the first electrical rod and disposed on the second electrical rod for providing electrical insulations between the first metal sheets and the second electrical rod.
3. The water treatment system as claimed in claim 2, wherein the first and second metal sheets are in the form of plate or mesh.
4. The water treatment system as claimed in claim 2, wherein the first and second metal sheets are made of titanium and coated with platinum, iridium oxide, or synthetic diamond.
5. The water treatment system as claimed in claim 2, wherein the first insulator is a plastic screen or a plastic ring.
6. The water treatment system as claimed in claim 2, wherein the firth and second electrical rods are made of titanium.
7. The water treatment system as claimed in claim 1, wherein the first power supply including at least one supercapacitor.
8. The water treatment system as claimed in claim 7, wherein the supercapacitor can amplify an input power by 10 times or more.
9. The water treatment system as claimed in claim 7, wherein the supercapacitor includes a plurality of units that are divided into two identical modules each has the same operational voltage and capacitance to be switched reciprocally between charging and discharging for providing consistent peak power to the first electrode set.
10. The water treatment system as claimed in claim 1, the ozone reactor further comprising a housing for allowing subject water flowing through the housing.
11. The water treatment system as claimed in claim 1, wherein the ozone reactor is submerged without a housing in an open body of water.
12. The water treatment system as claimed in claim 1, wherein the second electrode set comprise
- a plurality of identical third metal sheets longitudinal parallel to each other;
- a plurality of identical fourth metal sheets longitudinal parallel to the third metal sheets, wherein the third metal sheets and fourth metal sheets are arranged alternately;
- a third electrical rod penetrating the third and fourth metal sheets and electrically connecting the third metal sheets to the second power supply, wherein the third electrical rod and the third metal sheets form the third electrode;
- a fourth electrical rod penetrating the third and fourth metal sheets and electrically connecting the fourth metal sheets to the second power supply, wherein the fourth electrical rod and the fourth metal sheets form the fourth electrode;
- a plurality of second insulators disposed on the third electrical rod for providing electrical insulations between the fourth metal sheets and the third electrical rod and disposed on the fourth electrical rod for providing electrical insulations between the third metal sheets and the forth electrical rod.
13. The water treatment system as claimed in claim 12, wherein the third and fourth metal sheets are in the form of perforated plate.
14. The water treatment system as claimed in claim 12, wherein the third and fourth metal sheets are made of titanium or stainless steel and coated with activated carbon, carbon nanotube, or fullerene (C60).
15. The water treatment system as claimed in claim 14, wherein the carbon nanotube or fullerene (C60) is directly grown on the metal sheet.
16. The water treatment system as claimed in claim 12, wherein the second insulator is a plastic screen or a plastic ring.
17. The water treatment system as claimed in claim 12, wherein the third and fourth electrical rods are made of titanium.
18. The water treatment system as claimed in claim 1, wherein the second power supply charging and discharging the second electrode set reciprocally.
19. The water treatment system as claimed in claim 1, wherein the second power supply including at least one supercapacitor.
20. The water treatment system as claimed in claim 19, wherein the supercapacitor can amplify an input power by 10 times or more.
21. The water treatment system as claimed in claim 19, wherein the supercapacitor includes a plurality of units that are divided into two identical modules each has the same operational voltage and capacitance to be switched reciprocally between charging and discharging for providing consistent peak power to the second electrode set.
22. The water treatment system as claimed in claim 1, the flow through capacitor further comprising a housing for allowing subject water flowing through the housing.
23. The water treatment system as claimed in claim 1, wherein the flow through capacitor is submerged without a housing in an open body of water.
Type: Application
Filed: May 24, 2006
Publication Date: Nov 29, 2007
Applicant:
Inventors: Lih-Ren Shiue (Hsinchu), Min-Chu Chen (Sugar Land, TX), Mu-Fa Chen (Tulsa, OK)
Application Number: 11/439,167