DECONTAMINATION OF WATER BY PHOTOLYTIC OXIDATION/REDUCTION UTILIZING NEAR BLACKBODY RADIATION

Abstract: A reactor system for decontamination of water by photolytic oxidation utilizing near blackbody radiation is disclosed. The system comprises a reaction chamber housing (202) defining an internal space with an inlet (220) and an outlet (224); and a plurality of broadband radiators (230) generating radiant energy with wavelengths between about 150 nm and about 3 mu m, the broadband radiators (230) disposed within the reaction chamber housing (202) such that a sufficient dosage of broadband radiation deeply penetrates the water matrix and irradiates the contaminants and/or the oxidant within the internal space of the reaction chamber housing (202) thereby causing photolytic oxidation of the contaminants.

Description: Title: DECONTAMINATION OF WATER BY PHOTOLYTIC OXIDATION /REDUCTION UTILIZING NEAR BLACKBODY RADIATION FIELD OF THE -INVENTION The present invention relates to decontaminauon of water, and more parucuiarly to methods and apparatus for decontaminauon of grouπdwater. surface water or waste water through the use of a highly efficient flashiamp or other source of high peak power, high average power, broadband, continuum output ultraviolet (UV)-rich blackbody or near-blackbody radiation for rapidly and efficiently reducing and/or oxidizing (redox-ing) contaminants, including organic and inorganic molecules and for microbial sterilization of groundwater. surface water or waste water. BACKGROUND OF THE INVENTION Abundant quantities of ciean. fresh water have long been available in the United States. The unfortunate introduction of pesticides, pathogens, and highly volatile gasoline components, such as MTBE. into the aquifers of many drinking water systems is now a senous constraint to economic expansion in developed countries, and a matter of survival for 20% of the world's population. As an example, the U.S. Environmental Protection Agency announced November 26 th , 1997, that it will be issuing a new health advisory citing cancer data and drinking water contaminaϋon relating to MTBE. and will recommend maximum levels as low as 5 parts per billion in dπnkiπg water. There exists a need for cost effective method to reduce MTBE levels to meet these standards. Current water purification technologies, including distillation, reverse osmosis, and carbon filtration usually produce suitable water quality, but their high capital, operating and maintenance costs have limited their use to only those situations where water shortages are most extreme or where cost is less important. Water contaminated with pesticide or gasoline contaminants are especially difficult and costly to remove with conventional technologies. The $5.5 billion annual worldwide water purification market is growing, depending on market segment between 5% and 25% per year. Thirty-three percent (33% or $ 1 8 billion) is for purification of fresh water for commercial, industrial and residential use. Waste water reclamation and re-punfication. currently about SI 0 billion annually, is the fastest growing segment. The overall market demand is currently constrained by the high cost of water purification products. Availability of low-cost alternatives could cause the market to reach $ 18 billion by the year 2002. Both advantages and disadvantages of the pπor art technologies are summarized below: Vapor compression (VC), including distillation technology systems are positive on drinking water for both pathogen and chemical contammauon remediation, remove total dissolved solids (TDS) and are excellent for desalinization. Drawbacks include a relatively high pπce. a generally large sue. non portability and fairly complex construction and operation. Reverse osmosis (RO) removes TDS with a relatively simple mechanism. Removal of non-volatile orgamcs and pathogens is easy. However, the systems are subject to contaminating product water if feed water pressure and turbidity are out of operating parameters, involve a high pπce rate, does not remove dissolved organic compounds and are complex and sophisticated Air stripping (AS) is generally the least expensive form of water remediation and is fairly good at removmg volatile orgamcs However, these systems are also large, very noisy and unsightly, do not remove non-volatile orgamcs, do not remove pesticides or pathogens, depend on ancillary technology, like the use of granulated activated carbon (below), resulting in more O&M cost as well as air pollution (the volatile orgamcs are transferred mto the atmosphere) Granulated activated carbon (GAC) acts positively on volatile and non-volatile orgamcs like pesticides, is positive on pathogens, and can be reactivated in most cases However. GAC also requires re- supply of heavy, bulky mateπal. typically has a large adsorption ratio, such as about 1000 pounds GAC to 1 pound contaminant, and itself becomes a source of contamination of product water if allowed to saturate. Furthermore, saturated GAC is a hazardous waste product and must be handled as such, especially when considering issues such as transportation, disposal or reactivation cost Low and medium pressure mercury vapor ultraviolet (UV) radiation is also effective at reducing pathogen levels, but only very slightly effective at breaking down or removing organic or synthetic organic compounds at practical flow rates Sometimes UV is used as part of a polishing loop on larger treatment systems. However, as a practical matter, use of UV radiation m the past has been impossible These systems are not practical for chemically contaminated water, the required low pressure lamps are typically not self cleaning, would require hundreds of lamps to equal the dosage of a lamp of the present invention. and provide a larger footprint for any type of remediation application Furthermore, current UV technology is not energy efficient To remediate chemically contaminated water, himdreds of thousands of watts are needed for low flows such as 240 gallons per mmute In adώtion to said power requirement, enormous amounts of additional oxidants, such as hydrogen peroxide often at rates of as many as tons of additional oxidant per year, must be added which also contributes to the high operating cost. Ozone saturation is positive on pathogens and leaves no dangerous chemicals in the water. However, providing a system which injects ozone into a water supply or stream requires a physically rather large footprint and is complex to build and operate, involves high operation and maintenance costs, involves the production of ozone - a dangerous and reactive gas. and is not practical on chemical contaminants alone. Finally, the use of chlorine (Cl) is known to kill or otherwise render pathogens harmless, but has no remedial effect on chemical contaminated water except for elimination of cyanides. Current competing technologies for chemical contamination of groundwater include reverse osmosis (RO), air stnpping, and Activated Carbon filtration. Although the populanty of reverse osmosis has gamed substantially in market share in recent years, different technology solutions contmue to dominate the vaπous mches. RO membrane production is dominated by a few compames ( DuPont. Dow-Filmtec. Fluid Systems. Toyoba, etc.). but there are thousands of compames that act as mtegrators of RO systems. Few. with the notable exception of Ionics, Osmonics. and U.S. Filter exceed SI 00 million m revenues. Air stnpping is a fairly low technology alternative and is highly cost-effective, but is noisy, unsightly, pollutes the air. and has limited effectiveness in removmg MTBE to EPA standard levels. Activated Carbon Filtration involves large quantities of carbon supplied by compames like Calgon. Inc. Pathogen removal is typically accomplished with the addition of chlorine, distillation techniques, or the use of banks of low or medium pressure ultraviolet lamps. Distillation suppliers include large European. Japanese, and Korean contractors and this technology excels at the removal of TDS. Current ultraviolet lamp suppliers include Aquafine. Fisher & Porter, and Puress. Inc. There exists a need for technology which is more energy efficient and can simultaneously remove pathogens and chemical contamination. Such equipment could also be used to post-treat water at desalination facilities to remove chemical contaminants. Traditional UV technology relies on low and medium pressure UV lamps, similar to the fluorescent lamps used in office buildings. Medium pressure lamps operate at higher power levels than do the low- pressure lamps and consequently, are slightly more efficient than the standard low-pressure vaπety The typical low-pressure power ranges from 30 to 100 watts while the medium pressures average 3000 watts. Both lamp types are known as atomic line radiators They produce light energy in very narrow wavelength bands at 10-20% electπcal efficiency Both types operate with A/C current and are controlled by electπcal ballast Though the lamp life is generally very long, maintenance cost are generally very high, especially in the case of low-pressure lamps Cleaning is the mam problem Lamps become fouled in the water environment from precipitated dissolved solids and scum This fouling action gradually reduces the UV output making the lamp useless Therefore, these lamps must be removed on peπodic bases and manually cleaned Further more, low and medium pressure lamps do not produce the radiative power levels to effectively dissociate the chemical bonds of contaminants They find their principle usage in the wastewater reclamation mdustry for biological degradation At a smgle installation, these lamps are used hundreds and sometimes thousands at a time, thus amplifying the operating and maintenance (O&M) costs Improvements to this type of technology include enhanced chemical dopmg of the lamp to mcrease its UV conversion efficiency, unproved cold cathodes to mcrease lamp life and improved reaction chambers or effluent channels to maximize dosage and throughput and to minimize head loss The following U S patents are deemed relevant to the field of the present invention Patent No Issue Date Inventor 4,141,830 Feb 27. 1979 Last 4.179,616 Dec 18, 1979 Coviello et al 4,230,571 Oct. 28, 1980 Dadd 4,273,660 Jun. 16, 1981 Beitzel 4.274.970 Jun. 23, 1981 Beitzel 4,437,999 Mar 20. 1984 Mayne 4,595,498 Jun. 17, 1986 Cohen et al 4,787.980 Nov 29, 1988 Ackermann et al 4.792.407 Dec 20, 1988 Zeff et al 4,836,929 Jun. 6, 1989 Baumann et al. 4,849,114 Jul. 18. 1989 Zeffet al. 4,849,115 Jul. 18, 1989 Cole et al. 4,913,827 Apr. 3. 1990 Nebel 4,124.051 Jun. 23. 1992 Bircher et al. 5,130,031 Jul. 14, 1992 Johnston 5,151,252 Sep. 29. 1992 Mass 5,178,755 Jan. 12. 1993 LaCrosse 5,308,480 May 3, 1994 Hinson et al. 5,466,367 Nov. 14, 1995 Coate et al. 5,330,661 Jul. 19, 1994 Okuda et al. 5,547,590 Aug. 20, 1996 Szabo Last teaches an apparatus for puπfying liquid such as water, in which as ultraviolet light source irradiates air passmg through a first chamber surroundmg the source, and then irradiates the liqmd passmg through the second chamber surrounding the first chamber. The air from the first chamber is ozonated by the UV light and this air is bubbled into the water in the second chamber to maximize the purification through simultaneous ultraviolet and ozone exposure. Beitzel teaches water treatment by passmg a mixture of water and air and/or ozone through a nozzle which compresses and breaks up bubbles within the fluid mixture m a radiation housmg, a hollow. cylindπcal chamber located around an elongated UV light source. Beitzel also teaches water treatment by passmg a thin film of water in contact with a bubble of air containing air and ozone while concurrently radiating both the water film and the air/ozone bubble with UV radiation. Mayne teaches a method of feeding an insoluble organic solid mateπal m the form of an organic resin or biological matter containing contaminating mateπal such as radioactive waste from a nuclear facility or from treatment of animal or plant tissue m a laboratory or medical facility into a vessel containing water and. to which ultraviolet light and ozone, preferably by spargmg, are applied. Cohen et al. teaches a water puπfication system which includes an ion-exchange unit for producmg high-resistivity water, followed by ozone exposure and ultraviolet steπlizer umts that oxidize orgamcs and also reduce resistivity, followed by a vacuum degassification unit to restore high resistivity. Ackermann et al. is directed to a hydraulic multiplex unit for receiving continuously one or more samples of liquid from a liquid puπfication system distπbution system and redirecting such sample or samples randomly or in sequence to one or more analytical instruments. Zeffet al. teaches a method of oxidizmg organic compounds in aqueous solutions by usmg in combination ozone, hydrogen peroxide and ultraviolet radiation. Zeffet al. also teaches a method of oxidizmg toxic compounds including halogenated and/or partially oxygenated hydrocarbons and hvdrazine and hvdrazine deπvatives in aqueous solutions by using in combination ozone, hydrogen peroxide and ultraviolet radiation. Baumann et al. teaches a process for breaking down organic substances and/or microbes in pretreated feed water for high-puπty recirculation systems usmg ozone which is generated m the anode space of an elertrochemical cell and treated with ultraviolet rays and/or with hydrogen (H 2 ) generated in the cathode space of the same cell or hydrogen (H : ) supplied from outside, for use in reducmg elementary oxygen in any form to harmless water. Cole et al. teaches a process and apparatus for oxidizmg organic residues in an aqueous stream, compπsmg a chamber with an inlet and an outlet and dividers therebetween creating subchambers, each subchamber having a source of ultraviolet light disposed therein, and means for controlling flow including flow through subchambers and means for controlling radiation to the fluid, such as when the subchambers are closed and flow is interrupted, and not when the subchambers are open such as during peπods of flow thereinto or therefrom. Nebel teaches a method for producing highly puπfied pyrogen-free water compπsmg dissolving ozone in water, separating the gas and liquid phases, and exposmg the ozone-contammg water to ultraviolet radiation to destroy pyrogen in the water. Bircher et al. teaches a process for treating aqueous waste or groundwater contaminated with nitro- containing organic chemicals to degrade the compound sufficiently to permit disposal of the waste or groundwater. Johnston teaches a process for removing halogenated organic compounds from contaminated aqueous liquids which comprises contacting the contaminated liquid with a photocatalyst while simultaneously exposing the contaminated liquid to both acoustic energy and light energy to efficiently decompose the halogenated organic compounds. Mass teaches a reactor for the treatment of a fluid with a substantially uniform dosage of light from a line-type light source, and not a blackbody radiator, in a reactor housing with a central photochemical treatment region. LaCrosse teaches an ultraviolet-enhanced ozone wastewater treatment system in which ozonated water is mixed within a multi-stage clarifier system with wastewater to be treated and suspended solids are removed. The clarified effluent is filtered and exposed to ultraviolet radiation. Ozone is injected into a contact tower, where reaction takes place, and the UV irradiated, ozonated and clarified liquid is recirculated through an ozone injector and discharged through a mixer plate into a purge chamber, from where a portion is re-diverted to the system and a poπion is discharged through a diverter valve through a carbon filter and out the system. Hinson et al. teaches a two-stage, multiphase apparatus for the purification of water which may contain solid wastes. Gaseous oxidant comprising ozone and oxygen initially removes the solids, and then resaturation with oxidant breaks down and destroys chemical and biological contaminants, prior to UV radiation, degassification and rejection from the system. Coate et al. teaches a portable system which minimizes the addition of solids to be disposed of through the use of ozone for contaminant reduction to basic elements after the pH value of the waste water to be treated is properly adjusted. Ozone is combined with ultrasound to cause coagulation and precipitation. In another stage, ozone and UV light are used in a reduction process. Ion alignment using a magnetic field and an electrochemical flocculation process to which the waste water is subjected causes further coagulation and precipitation. Okuda et al. teaches decomposition of an organochlorine solvent contained in water by adding at least one of hydrogen peroxide and ozone to the water and then radiating ultraviolet rays to the water. A catalytic amount of a water-insoluble barium titanate substance is caused to co-exist in the water. Szabo teaches a UV based water decontamination system with dimmer-control, in which a UV based or dual mode water system operates under household water pressure to provide a batch treatment of contaminated water. Treated water is stored in a pressurized reservoir from which it may be released for use. A pressure drop, or discharge of a sufficient amount of the treated water initiates another treatment cycle. A pressure gauge linked to a UV lamp dimmer detects the pressure drop and causes the UV lamp output to change from a reduced-output standby mode to an operative mode, lamp output is also linked to filter backwash. The UV light may also be used to produce ozone which is placed in contact with the fluid through a helical tube. OBJECTS AND ADVANTAGES OF THE PRESENT INVENTION Thus, it is an object and an advantage of the present invention to provide a system for decontamination of water by photolytic oxidation reduction which requires a drastically reduced operating footprint. It would be desirable to provide one lamp which can provide the same dosage that would take hundreds of mercury UV lamps and can do so more efficiently in that most of the lamp's blackbody radiation spectrum is used (80%). In contrast the mercury lamps of the prior art use a very narrow band of UV energy with an energy efficiency of 15-20%. Another object and advantage of the present invention is for decontamination of water by photolytic oxidation/reduction to provide UV blackbody radiation that ranges from about 0.75 million to about 9.0 million watts of ultraviolet power (-50% of peak power generated) at average powers ranging from about 2,500 watts to about 18,750 watts per lamp. These power levels would easily provide enough energy per pulse to dissociate chemical bonds and a sufficient number of pulses per second will sustain the 10 free radical chain reaction necessary to oxidize/reduce the contaminants. Another object and advantage of the present invention is to provide a system for decontamination of water by photolytic oxidation reduction thousands of times more dosage to destroy pathogens, at a lower energy cost, than the standard, currently marketed. UV technology Another object and advantage of the present invention is to provide a system for decontamination of water by photolytic oxidation/reduction having a unique reaction chamber design which overcomes the problems of light absorption based on water quality In this way. water that has a high level of dissolved solids, that wouid normally absorb little light energy, can be used without any extra filtering or pretreatment Another object and advantage of the present invention is to provide a system for decontamination of water by photolytic oxidation/reduction which can be produced m volume and mexpensively. resulting m lower capital cost per unit Another object and advantage of the present mvention is to provide a system with low operating and maintenance costs Such systems would operate automatically with minimal maintenance Another object and advantage of the present mvention is to provide a svstem for decontamination of water by photolytic oxidation/reduction to generate longer wavelength blackbody radiation power (P) output ranging between about 0 45 million and about 2 7 million watts (-30% of the energy generated) Another object and advantage of the present mvention is to provide a system for decontamination of water by photolytic oxidation/reduction usmg high intensity broadband radiation to provide the absorption wavelengths necessary for disruption of essentially and effectively all orgamc bonds, resulting in high efficiency orgamc bond dissociation, with as much as or more than 80% of the total light energy generated used to oxidize the constituent contaminants Yet a further object and advantage of the present invention is to provide a system for decontamination of water by photolytic oxidation/reduction m which an oxidant such as hydrogen peroxide 11 is produced or formed m the reactor spontaneously or throughout the course of the process, thereby enhancing the efficacy of the current systems Yet a further object and advantage of the present mvention is to provide a system for decontamination of water by photolvtic oxidation/reduction in which deep penetration of radiation, especially through the important microbial kill bands, of the water matrix m the system is achieved. SUMMARY OF THE INVENTION This invention is based on the ability of a high-energy flashiamp to photodegrade chemical contammants and destroy toxic and other orgamsms in water By adjusting the mput energy, pulse duration, and pulse shape waveform of the energy applied to the flashiamp, blackbody radiation mode, which peaks in the deep UV. is attainable The ionization of the flashlamp ' s plasma is predominately caused by free- bound and bremsstrahlung continuum transitions in which the bound-bound lme transitions are superimposed The plasma, bemg mostly continuum in nature, yields a high emissmty ( 98<e<l) across the UV-VIS-IR bands Sigmficant differences between the lamps used m the present invention and traditional UV lamps are that (1) the UV lamps have no phosphor coatings which otherwise essentially serve to convert the UV energy mto visible light and (2) the lamp envelope is made from high puπty or extremely high puπty or synthetic forms of quartz having SiO**. > 98%. or similar properties, which allow the UV energy to pass through A multi-pass reaction chamber design couples the high-energy light pulse to the contaminated water Each reaction chamber, containing at least one lamp, takes advantage of the 360-degree circumferential radial radiation pattern of the lamp The reaction chamber also takes advantage of the non- Lambertian volume-emitter radiation profile of the lamp, at least to the extent of the quartz-water total internal reflectance (TIR) At 185 nm. the light intensity degrades by only 4% at 40° from lamp normal. In 12 a Lambert-an source, the intensity falls to 15% of maximum Since the system is modular, extending the reaction chambers m a parallel or seπes fashion provides more reaction area and exposure time to accommodate higher flow rates and contaminant concentrations However, for more efficient oxidation, a method of adjusting the oxygen concentration, TDS and turbidity of the water to optimal levels should be used before the water reaches the reaction chamber The process can clean groundwater. surface water, and wastewater of toxic chemicals and dangerous pathogens quicklv and mexpensivelv Chemical contammants are redox-ed to smaller, less complex molecules and are finally redox-ed into safer compounds such as C0 2 . H 0. and low level orgamc acids, which pose no health or aesthetic threat to dπnking water In super high concentrations, the contaminant concentration is drastically reduced to safe levels as established by the EPA In the case of pathogens, the DNA/RNA of the bacteπa or virus are destroyed instantly by the intense UV energy This level of destruction prevents the pathogens from reproducmg Unlike other forms of water remediation, the pulsed flashiamp photolytic redox technology is small, compact and environmentally fπendlv Because the svstem does not generate loud or obnoxious sounds and is not unsightly, it can be placed m quiet neighborhoods, busmess districts, and "environmentally sensitive " ' areas such as national parks or other scemc areas A sigmficant advantage of the present invention is mcreased UV flux With the present system, just one lamp can generate up to or above 10 megawatts of UV radiation having a continuous range of wavelengths from between about 185 nm to about 400 nm in a smgle pulse lastmg only a fraction of a second These pulses can be applied at a rate of about 5 to about 100 pulses per second resultmg in ultraviolet dosages ranging from about 50 joules/cnr to about 2000 joules/cπr One lamp provides about 50 to about 550 times the UV dosage as compared to low and medium pressure lamps Current technology uses hundreds of lamps to achieve similar UV dosage 13 It should also be pomted out that due pπmaπly to a phenomenon called atomic l ne radiation, the low and medium pressure mercury UV lamps of the pπor art radiate at a few narrow wavelengths m the UV, namely about 185 nm (on special lamps), 254 nm, and 365 nm Typically, there are other wavelengths present but their energy levels are negligible for purposes of utility in a practical application On the other hand, the lamps of the present mvention radiate m the ultraviolet domain essentially continuously between about 185 nm and about 400 nm, encompassmg all the wavelengths m between in a blackbody radiation profile (continuum radiation) The present lamps also radiate in the visible and infrared domains essentially continuously from between about 400 nm and about 3 um. at sigmficant energy levels, in accordance with the blackbody radiation profile The present system uses one UV enhanced flashiamp. and greatly outperforms the systems of the pπor art. One UV enhanced flashiamp of the present mvention is equivalent to about 250 of the pπor art lamps However, the pπor art lamps only radiate at a few distinct wavelengths in the UV, while the lamp of the present mvention radiates at all the UV wavelengths, as well as. the visible and infrared, thereby providing a match for all of the sigmficant atomic absorption bands of the contammants The UV efficiency of a typical lamp of the present mvention is about 48% to about 52% This corresponds with the amount of the output spectrum compπsed of ultraviolet radiation The visible efficiency is between about 25% and about 30% while the infrared is generally about 5% to about 10% On contrast, current UV technology is about 5 to about 15% UV efficient at the three predominate wavelengths and these only radiate at rates in the millijoules/cnr range. In a preferred embodiment the system for decontamination of water by photolytic oxidation/reduction achieves deep penetration of radiation, especially through the important kill bands, mto the water matπx. This is especially useful in the waste water mdustry where a greater distance between lamps is possible Because preferred embodiments of the present system operates with only a few lamps, not 14 hundreds, it is very compact. It can easily be placed in an area such as a gas station, business park, apartment complex, pπvate home, or even a national park and not be an eye-sore or source of obnoxious noise. This has a tremendous advantage over other technologies like air-stπpping or carbon filtration, as these systems occupy a large amount of space and. in the case of air-stπpping, generate great amounts of noise An application to which the present mvention is particularly well suited is the photodegradation of methyl t-butyl ether (MTBE), an ether compound Its pπmary use is as a gasolme additive Its primary function is to mcrease the available oxygen during combustion while maintaining the octane rating of the fuel The terminal end of this molecule is electronegative making it very soluble in water and therefore difficult to remove by conventional ion filtering or air-stπppmg In a preferred embodiment the irradiation of water with blackbody irradiation, high m UV and other photoreactive bands, causes production of oxidizing intermediaries such as hydrogen peroxide and free hydroxyl radicals As opposed to systems which require mjection or meteπng of such oxidizmg agents mto the contaminated water to be puπfied. such as in an oxidizmg reactor, the present mvention utilizes the broadband radiation used for photo-decomposition and degradation of contaminants to form its own oxidizing agents from the water itself, resulting m increased, enhanced and residual oxidative decontamination function as well as lowered operating costs Embodiments of the present mvention range m size and capacity between small under-sink home umts and large 700+ gallon per mmute systems for mstallation on municipal wells Flashiamp replacement is at time intervals, typicallv from between about monthly on the large scale svstems and about yearly on the home products In a preferred embodiment a 20 gallon per mmute product addresses a high pπoπty market l e , MTBE plume remediation This embodiment can be used in conjunction with a shallow well that pumps groundwater from the contaminated aquifer, such as from beneath leaking gas station storage tanks, treats 15 the water to remove the MTBE and then discharges the water back into the aquifer. The embodiment is small, self contained, weighs about 350 pounds, or more or less, and utilizes safety and self diagnostic features to ensure effective water treatment. Similar embodiments are used to target the small scale drinking and waste water treatment markets. In another embodiment a 700 gallon per mmute embodiment services large-scale domestic and foreign markets. When connected directly to the well head of a mumcipal water supply, for example, this energy efficient embodiment will run continuously under the most adverse and varying conditions. Numerous other advantages and features of the present mvention will become readily apparent from the followmg detailed descπption of the mvention and the embodiments thereof, from the claims and from the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is the blackbody response relative spectral exitance of a preferred embodiment a blackbody radiator of the present mvention. FIG. 2 illustrates the blackbody dosimetry response over the UV interval of a preferred embodiment a blackbody radiator of the present mvention. FIGS. 3 and 4 illustrate representative selected pulse durations and power density and lifetime curves. FIG. 5 illustrates general coefficient of absorption (CoA) curves for ground water. FIG. 6 is a representative field layout drawing of a preferred embodiment of the present mvention showing photolytic redox method and apparatus for contaminated water remediation. FIG. 7 is a representative sensor layout drawing of a preferred embodiment of the present mvention for contaminated water remediation. FIG. 8 is a representative isometπc view of a preferred embodiment of a reaction chamber of the 16 present mvention. FIG 9 is a representative front end view of a preferred embodiment of a reaction chamber such as shown m FIG. 8 FIG 10 is a representative section view of a preferred embodiment of a reaction chamber such as shown in FIG. 8 FIG 11 is a representative section view of a preferred embodiment of a lamp head of the reaction chamber such as shown m FIG 8 FIG 12 is a representative detail view of the lamp head of FIG 11 FIG 13 is a flow chart that shows a prefeπed method of the present mvention FIG 14 illustrates a typical spectral absorbance response curve of a preferred embodiment of the present mvention for relatively light TDS concentration FIG 15 illustrates a typical spectral absorbance response curve of a preferred embodiment of the present mvention for a heavy TDS concentration FIG 16 shows spectral absorbance data of borderline blackbody radiation and blackbody radiation at a wavelength of about 254 nm m tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention FIG 17 shows spectral absorbance data of borderlme blackbody radiation and blackbody radiation at a wavelength of about 265 nm m tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention FIG. 18 shows spectral absorbance data of borderlme blackbody radiation and blackbodv radiation at a wavelength of about 400 nm in tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention FIG 19 shows spectral absorbance data of borderlme blackbody radiation at a wavelength of about 254 nm m tap water obtamed under test conditions from a preferred embodiment of the blackbody 17 radiator of the present mvention and Lambert's law using the calculated CoA at the same wavelength. FIG 20 shows spectral absorbance data of borderlme blackbody radiation at a wavelength of about 265 nm in tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention and Lambert's law usmg the calculated CoA at the same wavelength FIG. 21 shows an analysis of spectral absorbance data of borderlme blackbody radiation at a wavelength of about 400 nm m tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention and Lambert's law usmg the calculated CoA at the same wavelength FIG 22 shows an analysis of spectral absorbance data of borderlme blackbody radiation and blackbody radiation at a wavelength of about 254 nm in bπne water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention FIG 23 shows an analysis of spectral absorbance data of borderlme blackbody radiation and blackbody radiation at a wavelength of about 400 nm in bπne water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention FIG 24 shows an analysis of spectral absorbance data of blackbodv radiation at vaπous wavelengths in tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention FIG. 25 shows an analysis of spectral absorbance data of blackbody radiation at vaπous wavelengths m bπne water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT Near-Blackbody Radiator Means In a preferred embodiment of the present mvention. a near-blackbodv radiator means compπses a 18 high peak power, high average power Xenon-gas filled flashiamp. Such a radiator means is capable of delivering up to 12 MW of peak power with average power up to 50 KW. The use of this type of flashiamp for photolytic decontamination of water is heretofore unknown. The power density of the Xenon-gas plasma generated inside the lamp produces a strong continuum output. Depending on the selected pulse duration and input energy, this continuum output will peak in the near to far UV region. The Xenon-gas plasma temperature, again depending on the selected pulse duration and other factors, can range as high as 15.000°K or higher. The diameter of the piasma is kept relatively small so that conversion efficiencies, particularly m the shorter wavelengths, are maximized. The term "blackbody * ' denotes an ideal body which would, if it existed, absorb all and reflect none of the radiation falling upon it; i.e., its reflectivity would be zero and its absorptivity would be 100%. Such a body would, when illuminated, appear perfectly black and would be invisible, except its outline might be revealed by the obscuπng of objects beyond. The chief mterest attached to such a body lies in the character of the radiation emitted by it when heated, and the laws which govern the relations of the flux density and the spectral energy distπbution of that radiation with varying temperature. The total emission of radiant energy from a blackbody radiator takes place at a rate expressed by the Stefan-Boltzmann (fourth power) law. while its spectral energy distπbution is descnbed by Planck's equation and other empiπcal laws and formulas. Planck ' s law. often referred to as the fundamental law of quantum theory, expresses the essential concept that energy transfers associated with radiation such as light or x-rays are made up of definite or discrete quanta or mcrements of energy proportional to the frequency of the corresponding radiation. This propomonality is usually expressed by the quantum formula E = hv (1) in which E is the value of the quantum in umts of energy and υ is the frequency of the radiation. The constant of proportionality, h. is the elementary quantum of action, or Planck 's constant. The relationship: 19 E λ- hc 3 dλ λ u he kλl is known as Planck's radiation formula, where E x dλ is the intensity of radiation m the wavelength band between λ and (λ + dλ), h is Planck's constant, c is the velocity of light, k is the Boltzmann constant and T is the absolute temperature. This formula descπbes the spectral distπbution of the radiation from a complete radiator or blackbody This equation can be wπtten m other forms, such as m terms of wavenumber instead of wavelength. It may also be wπtten m terms of wavenumber instead of wavelength intensity The emissivity of the volume emitter (flashiamp plasma) is difficult to estimate accurately because of its strong dependence on temperature, wavelength and depth. Nonetheless, smce the plasma reaches thermodynamic equilibπum very quickly duπng the pulse, and the depth, for all practical purposes, remains nearly constant duπng the peπod of eqiulibπum, the emissivity ε can be descnbed accordmg to wavelength interval Hence, the expression "'near-blackbody radiator " ' The flashiamp is designed to withstand these pulse durations over a long life, providing pulse to pulse reliability In general, to achieve a higher plasma temperature, for a given power rating the application of shorter pulses of energy will be useful. Radiative heat transfers are proportional to differences m temperature to the fourth power: q « r - T (3) The electron temperature T of the resulting gas plasma inside the lamp is a function of the mput energy E . the inside surface area of the lamp A. and the pulse duration t„ and is given by the formula: 20 TM -) 4 e σA (*) where σ is the Stefan-Boltzman constant equivalent to 5.67 x 10' 12 watt/cm 2 /K 4 . Total blackbody irradiance, a function of the pulse duration and the electron plasma temperature, is given by the formula: (5) Rt iTx^oTx * Furthermore, the total power density of the lamp, i.e., the total power emitted by the lamp, including radiation from the emitter as well as thermal energy, will be given by the formula: (6) E o p *A In a typical application, taking into account the lamp envelope and flow-tube losses, a preferred embodiment of the flashiamp system of the present invention will generate a radiant flux of broadband continuum radiation of about 12 MW peak power output. The spectral breakdown is as follows: Approximately 51.2% of this radiant flux (6.2 MW) will be UV (185-400 nm). Radiant exitance: 59,678 watt/cm 2 , Dose exitance: 13.8 joule/cm 2 , Dose flux: 1440 joule. Approximately 24.6% (3.0 MW) will be m the VIS (400-700 nm). Radiant exitance: 28,908 watt/cm 2 , Dose exitance: 6.7 joule/cm 2 , Dose flux: 697 joule. Approximately 11.4% (1.39 MW) will be IR (700 nm-3 μ ). Radiant exitance: 13,313 watt/cm 2 . Dose exitance: 3.1 joule/cm 2 , Dose flux: 322 joule. 21 These radiant values indicate that one lamp can greatly exceed the dose requirements (0.6 watt'sec/cπr at 185 nm) to dissociate the bonds of organic molecules. Over the range of 185-400 ran, resonance bands for most organic interatomic bonds, dose values can be eighty times as high. One lamp provides dosage ranging from 50 to 6900 times greater than what is required for bacteria, mold, protozoa, yeast, and viruses. In the case of photolytic redox, total oxidizable carbon (TOC) levels are reduced by the UV light creating free hydroxyl radicals ( H), hydroxyl ions (OH') and peroxy radicals such as 0 2 ' and H0 2 from water or oxidant additives. During the free radical chain mechanism performing electron or hydrogen atom abstraction, organic molecules are either dissociated or unsaturated and then oxidized into C0 2 , HO, and in some cases, into various intermediate species. These intermediate species are prevalent in halogenated compounds such as the chlorinated solvents, pesticides, and herbicides. These intermediate compounds may include low concentrations of simple acids such HCl and HOCI. Compounds that are more complex may be formed if the free radical chain mechanism is not sustained. The flashiamp UV system of the present invention is a relatively inexpensive way of destroying these dangerous chemicals. The lamplife is rated at 18-50 milhon shots, or for approximately 1000 to 2800 hours. Target flow rates for a single-lamp system are between about 1.0 and about 5.0 million gallons/day (MGD) depending on the contaminant level. The process of flashiamp photodegradation referred to in this paper as including photolytic oxidation reduction (redox), is a complex series of steps taken in a specific order. Listed below are primary concerns of photolytic redox of contaminants in water. Dosage The contaminant-bearing water must receive the proper amount of ultraviolet light. The longer the contaminated water is exposed to the actinic radiation, the greater the dosage, and hence, the longer the free 22 radical chain mechanism can be sustained for complete redox reactions. Coefficient of Absorption (CoA) Lambert's law describes the decrease in light intensity with distance penetrated into a medium. Increase levels of TDS and turbidity exacerbate this problem of light transmission. The multi-pass reaction chamber design overcomes this obstacle by repeatedly bringing the water into close proximity with the lamp. For water exhibiting a high coefficient of absorption (CoA) levels, this insures that during at least one-third of the retention time in the reaction chamber, the water is receiving 70% to 98% of the maximum light intensity available. Experimental Method To attain the spectral data, a 1/8 M 1200 L/mm grating monochromator with 280 μm slits for 2 nm resolution was used. The output of the monochromator was coupled to an UV enhanced silicon diode circuit. The UV light was generated by a specialized flashiamp. The lamp arc-length was 335 mm with a bore of about 10.0 mm. The predominant fill gas was Xenon with a total gas fill pressure less than about 1.0 Atm absolute. The cathode work function was about 1.1 eV. The lamp was driven using a multi- sectioned PFN with pulse repetition rates ranging from between about 1 pps and about 5 pps at full rated energy. In order to measure and easily adjust parameters such as dosages, CoA and temperature, the reaction chamber was a scaled bench-top model. Testing of the water samples was performed by independent environmental laboratories using EPA approved 8010 and 8020 water testing methods. Flashiamp Blackbody Radiation 23 A continuum mode of radiation is created by strongly ionizing the gas within the flashiamp. This continuum radiation approaches a high-emissivity blackbody radiation pro ile with increasing flashiamp power density. Power density is defined as: p -f (7) where: E 0 = lamp discharge energy (joules); t = pulse duration at full duration half maximum (FDHM) in seconds; and A, = lamp bore surface area (cm 2 ). Attaining a high emissivity ultraviolet blackbody response requires that power densities exceed about 50,000 watt/cm 2 with t ≤ about 1 msec. This can be considered a threshold power density for blackbody radiators. In a preferred embodiment of the present invention, power densities in test power densities ranged from about 127,000 watt/cπrto about 246,000 watt/cm 2 - with about 155,000 watt/cm 2 being optimal. As the power density increases, the emissivity approaches unity in the UV bands. In the VIS and IR bands, high emissivity is easily achieved. Equation (7) shows that as the pulse duration increases, the power density decreases. It is thus apparent that if E 0 and A, are held constant, (t) becomes the primary method of adjusting the UV response of the lamp, principally by affecting the plasma temperature. Using the minimum bound of 50,000 watt/cm 2 , the upper bound, when expressed as wavelength, must be greater than the UV-cutoff of the lamp's envelope material. This is calculated by minimizing the percentage of UV generated that falls below the rriinimum UV-cutoff wavelength of the envelope J This energy is simply wasted in the lamp walls as heat, thus reducing lamplife and conversion efficiency. Within this narrow pulse interval, one can calculate the exitance response of the lamp from Wien's Displacement Law and Plank's Radiation Law as follows. Plasma temperature is determined by finding the peak wavelength over the UN interval and then applying Wien ' s Displacement Law: 24 2898 T = "ptak (8) where: T in degrees Kelvin; and λ pn *- in microns. Using Plank's Radiation Law to determine the exitance over each selected bandwidth: 37418 rø = J (9) AT C - 1 where: λ = total wavelength interval, [.185 ... 3.00] μm; λ- = shorter wavelength in question; λ 2 = longer wavelength in question; and T = plasma temperature as determined by equation (8). The normalized exitance over a selected bandwidth is given by Equation 10: >A A- i — (10) σT 4 where: σ = Stefan-Boltzmann constant 5.67x10 "12 J cm '2 K sec "1 ; and T = plasma temperature as determined by equation (8). The exitance at anv waveienεth is described bv the Stefan-Boltzmann Law corrected for bandwidth concentrations: R{T) = {εsσT uH b „ (i i) where: = average emissivity (.98); = average radiation efficiency (.85); 25 σ = Stefan-Boltzmann constant, 5.67xl0' 12 J cm '2 K "4 sec '1 ; and T = plasma temperature as determined by equation (7). Using the lamp at 147 μsec, 232 μsec, and 285 μsec pulse durations, the plasma temperatures as determined by Wien's Displacement Law are about 14057 K, about 12536 K, and about 11916 K, respectively The followmg table summarizes the data: Intervals: UV [185 πm-400 nm] VIS [400 nm-700 nm] IR [700 nm-3 0 μm] t λpea T Hb Exitance Dosage Flux R,(λ) uv 147 206 14057 52.0% 95896 14.1 1466 vis 20.6% 38268 5 6 582 IR 8.7% 16122 2.4 250 R b (λ) uv 232 231 12536 51.2% 59678 13.8 1435 vis 24.6% 28908 6 7 697 IR 11.4% 13313 3 1 322 R (λ) UV 285 243 11916 50.1% 47729 13 6 1414 vis 26.5% 25345 7 2 749 IR 12.8% 12193 3 5 364 Table 1 It is immediately apparent from the tabulated data that the UV exitance values vary from about 95896 watt/cm 2 at about 147 μsec to about 47729 watt/cm 2 at about 285 μsec. twice the value as 147 μsec. However, the dosage and conversion efficiency vanes by no more than 4% m the UV band. This is a key design pomt. The shorter pulse greatly reduces the explosion energy maxunum of the lamp thereby reducing lamplife. There is no sigmficant gam m UV dosage by dπvmg the lamp harder, i.e.. by usmg shorter pulse durations. However, there is a significant decrease m lamplife. FIGS. 1 and 2 show the blackbody response at the three selected pulse durations FIG 1 is the relative spectral exitance and FIG. 2 illustrates the dosimetry response over the UV interval. Flashiamp Lifetime 26 The flashiamp must be optimized to deliver the maximum amount of useful radiation with good conversion efficiency while still maintaining a useful long lamplife. Driving the lamp harder to produce even more UV shortens the lamplife considerably and may not be necessary. Careful attention must be paid to optimizmg this trade-off of UV intensity and lamplife by adjusting pulse shape, duration, repetition rate, and energy mput. In order to maintain reasonable lamplife, the flashiamp 's explosion energy must be kept below 18% of the theoretical smgle-shot explosion energy limit. The followmg formulas show how the explosion energy is related to the lamp geometry, envelope mateπal. input energy and pulse duration. The dimensions and envelope mateπai of the flashiamp are used to develop a numencai coefficient that will aid in the calculation of the lamp-life. This number is the explosion-energy constant (K.): K, =Aa)ld (12) where- f(d) = quartz power function, based on. inter aha. mateπal transparency, thermal conductivity, wall thickness, and bore. W sec ! : cm \ 1 = discharge length of the flashiamp. cm. and d = bore of the flashiamp. cm. The single-shot explosion energy- = K (13) where: t = pulse duration at FDHM in seconds. The lamp lifetime, in number of shots, is approximated by 27 NOT FURNISHED UPON FILING 28 keeping the pulse duration confined to the mterval [t-,--, 1---J, reliable lamplife is msured The percentage of smgle-shot explosion energies for 147 μsec, 232 μsec. and 285 μsec are 18 6%, 14 8%. and 13 4%, respectively REACTION CHAMBER METHODOLOGY Coefficient of Absorption The TDS in water will determine how well the actinic radiation penetrates The intensity (I) decreases with the distance (z) penetrated mto the water accordmg to Lambert ' s Law (K π\ (17) I=Ae~ λ J where I 0 = mcident radiation. K = constant of proportionality, λ = wavelength- (cm), and z = distance penetrated into medium (cm) The quotient compπses the coefficient of absorption (α) FIG. 5 shows that at a maximum distance (z) from the flashiamp. only about 40% of the energy reaches the contaminants. However, the water flows perpendicular and parallel to the lamp on several passes through the chamber, always insuring close contact with the lamp for at least 1/3 of the total retention time of the water in the chamber This multi-pass design allows heavy TDS water to receive high dosages of UV In such high TDS water, the energy delivered to the flashiamp will be high as compared to conditions of low TDS water One way to improve system efficiency is to momtor the CoA through differential wavelength- selective measurements By knowing the CoA and anticipated contammant levels, adjustments can be made 29 to the energy and/or pulse duration to reduce power cost and preserve the lamplife For measurement purposes, the wavelength (λ) is known but (K) is not Neither is TDS The CoA (α) can be expressed as K- - π a- ^ (18) Then, by substitution mto Equation (17) I=I ? (19) And solving for α - / a = w» Δr (20) The value of (I 0 ) is normalized to the value of (I) Therefore. (I) is the closest sensor to the flashiamp The sensors are filtered for 254 nm naπow bandpass and placed as far from each other as possible (Δz) but along the same axis Once having solved for (α), (K) can now be determined r . a - A K = (21) 4 - π At this point a CoA curve can be generated for any wavelength by usmg Equation ( 17) This information can then be used by a control processor to adjust the flashiamp energy and/or pulse duration as needed, as well as flow and oxidant infusion rates, to enhance system efficiency Reaction Chamber Dosing 30 To provide the proper dosimetry to the contaminated water, the water must stay in contact with the light energy for some predetermined peπod of time. In addition, to be cost effective, the flow rate through the reaction chamber must be reasonably high. The typical minimum target flow rate for typical mumcipalities is about 1 MGD (690 gpm), or more or less. In a preferred embodiment of the present mvention, the pulse repetition rate is about 5 pps. The volume of the reaction chamber must be large enough to retain the water for a sufficient peπod of time so that proper dosmg takes place. By way of example, a preferred embodiment compπses a scaled bench-top model which parallels the phase-2 prototype reaction chamber In the prototype, the retention time is 7 7 seconds and the pulse factor is 38.5 pulses at 690 gpm. Retention time is given by V, Tre ' βowrate < 22 > where: V rc = reaction chamber volume (gal); and flowrate = gal/sec. The number of pulses per T r . t (pulse factor) pf= prr T re( (23) where: prr = pulses per second. Dose time. =Pf' t (24) 31 where: t = pulse duration FWHM (seconds). The UV dose is found bv 374 I S D(λ) = ε - s - t / 14388 ' (25) A e^ " " ' - 1 where: X = total wavelength mterval. [ 185 . 3 00] μm, λ, = UV cutoff of envelope mateπal (μm): λ 2 = 400 μm. T = plasma temperature as determined by equation (2), έ = average emissivity ( 98). s = average radiation efficiency ( 85); and t, = dose time (seconds). PHOTOLYTIC OXIDATION/REDUCTION Redox Requirements Photodegradation of contaminated water is not necessaπly a straightforward process. The contamination may be due to any vaπety of hydrocarbon compounds including halocarbons, orgamc mtrogen, orgamc sulfiir, and orgamc phosphorus compounds, or it may be microbial or morgamc m nature. The contamination may even be a combination of two or more of the groups just mentioned. This leads to intermediary species formed, either more or less transiently, during the photo-redox process, some of which are actually more hazardous than the onginal contammant. In the case of halocarbons. vinyl chloπde or ketones may be produced. In the case of MTBE. ternary butyl alcohol (TBA), formic acid, acetic acid are produced., although the latter two are not particularly dangerous in low concentrations One way to avoid large surpluses of unwanted intermediate oxidized species is to provide the 32 followmg m adequate quantity 1 Dosage. a) Intense UV energy per pulse; b) High pulse repetition rate, c) High retention time and high flow rate (l e , large volume reaction chamber); and d) Multi-pass configurations to insure those CoA extinctions are greatly minimized. 2 Oxidant a) Optimal amount of oxidant is available with the UV dose to sustain the free radical cham mechamsm This process is necessary to oxidize the contammants as completely as possible. and b) The blackbody UV radiation response provides [185 nm. 400 nm] at megawatt levels This in turn can generate l Hydrated electron e „., π Smglet oxvgen O 2 from ground state tπplet 3 0 2 . in Hydroxyl radical -OH. and iv Peroxy radical 0 2 or its conjugate acid H0 2 The choice of oxidant will be dependent on the type and concentration of contammant Saturated oxygen, 0 3 or H 2 0 2 all have their uses When these oxidants are use m conjunction with intense UV radiation, the above mentioned radicals are produced When the oxidants are not irradiated, their effectiveness is greatly reduced, as there is no formation of the free radicals A common but somewhat expensive method- at least for high contammant concentrations, is the photolvsis of H 2 0 2 to be used as the oxidant. The followmg reaction illustrates this 33 H,0, + hv - 2 -0H (26) Two moles of hydroxyl free radical (*OH) are created from one mole of hydrogen peroxide (H : 0 2) . The oxidation potential of OH is E° = +3.06 v, which makes it even more reactive than 0 3 , in which E° = +2.07 v. However, the cost effectiveness of using H 2 0 2 has to be examined closely. In general, the costs associated with such oxidants are relatively high, and add significant in operations. The blackbody radiator of this invention produces H 2 0 2 and 0 3 , such as by direct photolysis of the water and oxidation by molecular oxygen. This property reduces the amount of additional oxidant required for neutralization and degradation of organic compounds. Oxidation of MTBE In the course of testing, focus was on MTBE (methyl t-butyl ether). MTBE is made by reacting methanol from natural gas with liquid phase isobutylene and heating with an acid catalyst at 100° C. CH, CH, CH,OH + CH,=CCH, CH, O CH, (27) CH, Again, by way of example, by applying die 285 μsec puise as shown m Table 1 and scaling the dosage for 1 MGD. the following results were obtained: Initial MTBE H 2 0 2 Dose Final MTBE 1 45 40 225 >5 (ND) 2 1800 700 335 >15 (ND) 3 23000 26000 335 (ND) 34 Table 3 ND = Not Detectable In tests 1 and 2. no intermediate species were found followmg the 8020 test procedure. Minimal testing for intermediate species was performed. In test 3. no intermediate species were tested for Intermediate species mciude be low levels of formic and acetic acids System Layouts FIG. 6 is a representative field layout diagram of an embodiment of the present mvention showing photolytic oxidation method and apparatus for contaminated water remediation FIG 7 is a representative sensor layout drawing of a preferred embodiment of the present mvention for contaminated water remediation Water to be treated 102 enters the system 100 via mam flow control valve A. As descnbed above, it is understood that such water to be treated 102 mcludes surface water from lakes, farmmg ponds and/or flooded areas, ground water including natural and artificial and /or otherwise created aquifers, storage tank water from pnvate and public water supplies, effluent from water treatment facilities, such as a polishing loop in a chemical or procεssmg plant effluence stream, and other specialized water source remediation and preparation sources, including semiconductor water supplies, and biomedical and pharmaceutical water supplies. Proportioning valve D and isolation valves B and C and E control flow of water to be treated 102 through the system. Oxidant storage vessel 104 stores chemical oxidant which can be metered mto the system 100. Such chemical oxidant mateπal could be liquid hydrogen peroxide which is used as the oxidizing agent in the case of heavily contaminated water and/or for high flow rates thereof Chemical oxidant from storage vessel 104 is metered through oxidant mjector F mto oxidant mixing vessel 106 The precise amount of chemical oxidant metered through mjector F is controlled by the system controller. The reqmred amount of chemical oxidant. such as hydrogen peroxide, is determined based upon, at least m part. one or more of the followmg- 35 1. H 2 0 2 concentration; 2. Contaminant concentration; 3 Flow rate of the treatable water: (a) Retention time m the reaction chamber; (b) Average dosimetry of each element of the flow; 4 Total dissolved solids (TDS) concentration; 5 Turbidity/optical density of the treatable water: 6 Temperature of the treatable water: and 7 Lamp output energy Withm oxidant mixing vessel 106. chemical oxidant such as H 2 0 2 is diffused evenly mto the flow. Vessel 106 has sufficient volume to allow several seconds of turbulent mixing to help insure equilibration with the solute before entering reaction chamber 108 Lamp head 110 is mounted withm reaction chamber 108. Heat exchanger 112 uses at least part of the high flow rate of treatable water to remove excess heat from the closed-loop lamp coolmg circuit of the system 100 A coolmg fluid stream circulates through lamp head 110. according to system controller 116 Portions of the water to be treated 102 are directed through heat exchanger 112 to remove heat from the coolmg fluid stream. By usmg this technique, no additional power or equipment is needed, with the possible exception of use of chillers m some applications, thereby saving energy and equipment cost. The heat exchanger 112. optionally, is small and contains no moving parts. Proportioning valve D divides the influent flow 120 past mam flow control valve A so that some of the flow completes a circmt through heat exchanger 112. with flow of treatable water mto heat exchanger 112 as shown by directional arrow 122 and flow out of heat exchanger 112 as shown by directional arrow 124. In a preferred embodiment, proportioning valve D does not mcrease the pressure head against the 36 influent pump 130, or any gravity feed system, because the flow rate is not diminished but only divided between the two flow paths, flowing through either (a) valve D or (b) both valves B and C. Thus, heat is removed from the lamp head 110 cooling circuit and returned to the main flow. It will be understood that the treatable water is not contaminated by the cooling fluid passmg through heat exchanger 112. Additionally, the slight additional heat added to the treatable water 102 enhances chemical decomposition and degradation of contaminants. Flow of purified water 140 is controlled by isolation valve I. UV Dosage Reaction chamber 108 contains the high-intensity UV-VIS near-blackbody radiator pulsed light sources, hydraulic baffles, self cleaning mechanism, as well as optical and mechanical sensors and other measuring devices. It is demonstrated, therefore, how the volume selected for the reaction chamber 108 determines, at least in part and to a greater or lesser degree depending upon other considerations, effective retention time for the treatable water 102. In preferred embodiments of the present invention, while baffle design is a factor which determines. to a rather large degree, dosage of energy from the light source within the reaction chamber 108. baffle design is less directly related to retention time in the chamber 108. With more particular regard thereto. total dosimetry is defined as: n - - - prr (28) A where: (i) E = per pulse lamp radiation energy; (ii) T rn = retention time in reaction chamber: (iii) prr = pulse repetition rate; and (iv) A = surface area: lamp surface area, exposure area. etc. Additionally, wavelength dependent dosimetry is defined as: 37 37418 A^)=| ε-s-t, ( 1438a (29) Λ -1 where: (i) λ - total wavelength mterval. [.185 ... 3.00] μm; (ii) λ, = shorter wavelength of interval; (iii) λ 2 = longer wavelength of interval: (iv) T = plasma temperature as determined by Wien ' s displacement law: (v) e = average emissivity of flashiamp plasma: (vi) s = average radiation efficiency: and (vh) t, = t • T ret • prr. where: 1. t = pulse duration; 2. T m = retention time in reaction chamber; and 3. prr = pulse repetition rate. System Control A preferred embodiment of system controller 116 provides a signal from simmer supply circuit 150 to firing circuit 152. Output from chargmg supply circmt 154 is mput to pulse forming network 156 which also is used in system control by firing circuit 152. System controller 116 additionally compπses lamp - *cooling pump control circuit 158 and controller 160. A vanety of electπcal voltage and current sensors are provided m the system. In a preferred embodiment ambient air temperature sensor AAT is an analog temperature sensor. Sensor AAT momtors for and determines freezing conditions which may effect the system, with a reference point established for purposes of control parameter calculations, etc.. such as m normal operation. Housmg temperature sensor 38 HT, also an analog sensor in a preferred embodiment, is provided for purposes such as deteπnination of excessive power dissipation, such as to ensure adequate heat to overcome ambient freezing conditions. A safety circuit, in a preferred embodiment, would include a reaction chamber interlock RCI for preventing potentially hazardous or otherwise harmful radiation from being generated within reaction chamber 108 in the event a peripheral subsystem or component sensor failed to operate properly, and to interrupt operation or reaction therewithin in the event of failure of any peripheral subsystem or component. The reaction chamber interlock RCI is typically a digital sensor, and is associated with a digital signal indicator, such as part of the safety circuit. In a preferred embodiment, the system shuts down and dumps energy if the reaction chamber is opened or leaks. Such safety system would also include, in preferred embodiments, an overall ground fault circuit interrupter GFCI and associated or independent housing interlock HI circuits or controllers, as part of system controller 116 as shown. The overall ground fault circuit interrupter GFCI is typically a digital sensor, and is associated with a digital signal indicator, such as a redundant part of the safety circuit. In a prefeπed embodiment the system shuts down and dumps energy if a ground fault is detected. The independent housing interlock HI is typically a digital sensor, and is associated with a digital signal indicator, such as a redundant part of the safety circuit. In a preferred embodiment the system shuts down and dumps energy if power supply housing is opened or otherwise disturbed during operation. System controller would also include capacitor voltage A sensor CVA and capacitor voltage D sensor CVD as input signal generators to pulse forming network circuit 156, lamp simmer voltage sensor LSV as input signal generator for simmer supply circuit 150. and charging waveform voltage sensor CWV as input signal generator to charging supply circuit 154. Capacitor voltage A sensor CVA. typically an analog signal device, is useful for monitoring energy use. such as to ensure operation with the specifications for driving the lamps of the present invention. Sensor CVD such as a digital signal indicator, is also part of a safety circuit. Capacitor voltage D sensor CVD actuates a solenoid lock while the system 39 is being charged and an energy dump circmt (EDC) is not actuated or is malfunctioning. Lamp sunmer voltage sensor LSV determmes whether the flashiamp is simmering or not and if so, whether or not the simmer voltage is withm normal operating specifications Chargmg waveform voltage sensor CWV is used for determining quench timing, and to determme whether or not the voltage is withm normal operating specifications. Current sensors mclude lamp current sensor LI. lamp simmer current sensor LSI and average chargmg current sensor ACI. Lamp current sensor LI determmes whether the current supplied to the lamp is withm normal operating specification, and is also useful for monitoring for reverse current conditions. Lamp sunmer current sensor LSI determmes whether the flashiamp is sunmeπng or not and if so, whether or not the simmer current is withm normal operating specifications Sensor LSI also determmes the retπgger status of the system. Capacitor temperature sensor CT. typically a digital sensor, is associated with a digital signal mdicator. such as part of the safety circuit. In a preferred embodiment the system is associated with an interlock and is designed to shut down if the capacitors overheat. Integrated Optical Feedback The integrated optical feedback system implemented in a prefeπed embodiment of the present mvention has capability for determination of the opacity and/or optical density of the treatable water at vaπous wavelengths by using differential photo-feedback analysis (DPFA) This information is then used to determme the optimum flow rate and oxidant doping rate. In addition, the quality of light can be assessed to aid in system troubleshooting. Sensors mounted on or adjacent to reaction chamber 108 mclude a near photo feedback sensor NPF and a far photo feedback sensor FPF The near photo feedback sensor NPF and the far photo feedback sensor FPF are used for differential analysis of the treatable water ' s total dissolved solids (TDS) concentration The DPFA is a double photo-type detector that has been narrow-pass and neutral density filtered for a specific wavelength (such as 254 nm) or band of wavelengths (such as 185 nm to 400 nm. etc.). One detector is placed adjacent or very close to the lamp, and the other is placed closer to or adjacent the outer 40 edge of the reaction chamber. The distances between them as well as the wavelengths involved are known or can be determined. Relative voltages and or currents are generated from each of the detectors that are directly proportional to the light intensity at the specific wavelength, the closer detector generating more voltage and/or current than the farther one. For calculation purposes, the voltages and/or currents can be numerically normalized, such as to the voltage and or current value of the closer detector. By using this differential method, recalibration due to lamp aging is not necessary. The differential voltage and/or cuπent values indicate the degree of attenuation experienced by the light as it travels to the outer walls of the reaction chamber 108. This is the coefficient of absorption (CoA). By applying Lambert's law, the amount of absorption achieved at various distances can be calculated. This information is then used to adjust flow and energy. Thus, the detectors, especially the one closest to the lamp, can be used to determine the absolute output of the lamp after the CoA (or α) of the flow is determined. This will aid in determining the optimum flow as well as monitoring the lamp performance. Pressure and Flow Water pressure and flow of fluid through the system and system components are measured and adjusted with transducers and solenoid valves. Optimum performance is achieved by adjusting the flow via the solenoid valves based on the feedback mformation from the DPFA as well as pressure transducers. Pump head pressure sensor PHP is positioned to read the pressure of the water to be treated 102, and is useful for maintaining the pump head pressure within safety and operating limits. Heat exchanger flow rate HEF measures the flow of fluid from heat exchanger 112 through isolation valve C and the pressure in the heat exchanger 112 is measured by heat exchanger pressure gauge sensor HEP. Heat exchanger pressure gauge sensor HEP is used, in a preferred embodiment, to ensure operation within safety boundaries. Heat exchanger flow rate sensor HEF is used to determine adequate flow of cooling 41 water for heat removal from the lamp head 110 heat exchanger Lamp coolmg water flow rate is measured by lamp coolmg flow sensor LCF and lamp coolmg water temperature is measured, in a preferred embodiment adjacent at least one pomt, such as by lamp coolmg flow inlet temperature sensor LCI Lamp coolmg flow meter sensor LCF. typically a digital sensor, is associated with a digital signal mdicator, such 5 as part of the safety circuit In a preferred embodiment, the system is associated with an interlock and is designed to shut down power to the lamp if flow is inadequate Sensor LCI is useful for ensuring adequate coolmg of die lamp Oxidant level sensor OXL measures the level or other value related to the remaining liqmd oxidant m oxidant storage vessel 104. and oxidant flow meter OXF determmes flow rate of oxidant from storage 10 vessel 104 to oxidant mixing vessel 106 Sensor OXL also determmes if oxidant storage vessel 104 needs rechargmg The signal from meter OXF is useful m reaction balance determmations. and for measurmg and controlling the oxidant volume consumed by the system Oxidant infusion pressure sensor OXIP measures the pressure of the oxidant at or near the pomt of infusion of oxidant mto oxidant mixing vessel 106, as indicated OXIP is, m a preferred embodiment, an analog pressure gauge, useful in determination of i. - reaction rates, and to ensure operation withm safetv and other parameters Treatable water flow meter TWF measure flow rate of treatable water downstream of isolation valve H pπor to entry mto reaction chamber 108 Sensor TWF is preferablv analog, is useful for determination of reaction rates, pump head boundaπes and treatment rates The temperature of the treatable water feeding reaction chamber 108 is measured by treatable flow inlet temperature sensor TFI. typically an analog sensor TFI is an important factor in the determination of reaction rates, with a reference point typically established m the system The temperature of the treated water leavmg reaction chamber 108 is measured by treatable water flow outlet temperature sensor TFO. also typicallv an analog sensor A reference pomt is also typically established relative to the TFO Reaction chamber 108 operating pressure is measured by reaction chamber pressure sensor RCP An analog sensor for the reaction chamber pressure 42 sensor RCP is typically used, such as for determination of reaction rates, safety limits of operation, and treatment rates. The temperature of the treated water is measured downstream of reaction chamber 108, preferably between reaction chamber 108 and isolation valve I. Reaction Chamber and Lamp Assembly Design FIG. 8 is a representative isometπc view of a preferred embodiment of a reaction chamber of the present mvention FIG. 9 is a representative front end view of a preferred embodiment of the reaction chamber such as shown in FIG 8 FIG. 10 is a representative section view of a preferred embodiment of the reaction chamber such as shown m FIG. 8 Reaction chamber 200 is formed of an essentially cylmdncal housmg 202 with inlet side end plate 204 and outlet side end plate 206. Peπpheral flanged portions 208 and 210 of cylindπcal housmg 202 and inlet side end plate 204. respectively, are coupled together m the familiar bolted, gasket optional, configuration as shown, as are peπpheral flanged portions 212 and 214 of cylindπcal housmg 202 and outlet side end plate 206, respectively Treatable fluid flow inlet 220 has a flanged face 222 and is mounted onto the inlet side end plate 204 Treated fluid flow outlet 224 also has a flanged face 226 and is mounted onto the outlet side end plate 206 Near photo-feedback sensor NPF and far photo-feedback sensor FPF are mounted as shown. A lamp assembly 230 is mounted to and between the inlet side end plate 204 and outlet side end plate 206. such that flashiamp tube 232 is disposed essentially centrally and aligned axially with the cylmdncal housmg 202. An internal baffle assembly is compπsed of a plurality of operatively spaced baffle elements 240 Such baffle elements have any operative size and geometry, although it will be understood that as shown, a preferred embodiment of the baffle elements 240 is essentially round and mounted withm cylmdncal housmg 202 In a multi-pass design, the plurality of individual baffle elements 240 are mounted alternatingly spaced adjacent the inner wall 242 of cylmdncal housmg 202 and adjacent the flashiamp tube 232. Thus, flow of fluid, such as water, be g treated withing reaction chamber 200 43 flows into reaction chamber 200 through inlet 220, following a route defined by directional arrows C, and through outlet 224. FIG. 11 is a representative section view of a preferred embodiment of a lamp head of a reaction chamber such as shown in FIG. 8. FIG. 12 is a representative detail view of a lamp head such as shown in FIG. 11. As will be understood, the lamp assembly 230 shown in FIGS. 8-10 comprises a Teflon or other essentially non-conductive material end caps 250 mounted within either inlet side end plate 204 or outlet side end plate 206. Electrical power supply 252 is connected to the lamp via conductive connector element 254. Leaf-type spring members 256, optionally made of a beryllium-copper or other suitable alloy, form an excellent electrical and mechanical contact with the machined end, anode or cathode ferrules 258. Compressible ring lug 260 forms a seal between the end of conductive connector element 254 and power supply 252. Ceramic or other sturdy, non-conducting material end caps 260 support the assembly with bolts 262 or other retaining means which mount the assembly onto central flange portion 264 of either inlet side end plate 204 or outlet side end plate 206. Such central flanged portions 254 of the inlet side end and outlet side end plates 204 and 206 are made of a sturdy material such as steel. As shown, the lamp tube 270 of the assembly 230 is disposed within flow tube 272. Cooling water is circulated through flow tube 272, entering the assembly through input ports 274 and passing through the annular region 276 between lamp tube 270 and flow tube 272, in direction D as shown. It will be understood that for illustrative purposes only one end of the lamp assembly 230 is shown in FIG. 12 and that flow of cooling fluid between lamp tube 270 and flow tube 272 will in most cases be from one end, such as the cathode end or the anode end. to the other end of the lamp assembly 230. Since adhesions of contaminants in various states of decomposition may tend to foul the outer surface 280 of flow tube 272, a flow tube wiping system has been implemented in the preferred embodiment of the present invention. Rotating drive shafts 282 mount within end caps 260. By providing axial positioning means, such as a helically threaded groove on the outer surface of the drive shafts 282, a 44 brush member 284 with corresponding helically threaded πdge therein can be made to move m direction E by rotating dπve shafts 282 m a first direction. Reversal of said first direction will therefore cause motion of the brush member 284 m the opposite direction. It will be understood, however, that the descnbed means for lateral wiping motion of the brush member 284 can be replaced or augmented by other suitable mechanical, electπcal or hydraulic means. Photo Feedback Based Control Flowchart FIG 13 is a flow chart that shows a preferred method of the present invention. The chart shown how flow rate, lamp power and oxidant infusion, among other operatmg parameters, are adjusted from predetermined values to calculated values based on differential photo feedback signals obtamed duπng operation. It will be understood based upon the foregoing and followmg that the operating parameters selected and descnbed with regard to the preferred embodiment of the present mvention are only representative of a very large number of possible different parameters, and that, therefore, other combinations will be possible and known to those skilled the art. In a first step, a counter is initialized. Lamp operation, including normal pulsmg. is confirmed m a second step. It will be understood that while in certain embodiments of the present mvention there may be a smgle. normal operation mode, others will mclude plural, cascaded, parallel, senal or sequential, or other or multiple normal lamp operations, including but not limited m any way to vaπous modes of operation such as normal operation, low-, medium- or high-pulse rate operation, programmed sequence operation, remote operation and/or control, stand-by operation, test operation, start-up operation, maintenance cycle, etc. Thirdly, data is collected. A sequence is begun to measure voltages from detectors as amplified by transimpedence amplifiers, etc. This mcludes the fourth step of mcrementmg the index, and the fifth step of measurmg and storing the light energy values. In the case of a measurmg cycle set to 30 seconds and a pulse rate of 5 pulses per second, a 150-pulse sequence is begun. Voltage or other determined value is read 45 from a first channel, CHI for each of values CH1 to CHI,, with the determined value stored in the t Λ index of vector CHI . This will correspond with the first pulse of the 150-pulse measuring cycle or sequence. Simultaneously, voltage or other determined value is read from a second channel, CH2 for each of values CH2, to CH2„ with the determined value stored in the 7 th index of vector CH2. This also corresponds with the first pulse of the 150-pulse measuring cycle or sequence. Therefore, when CHI is a closer detector to the lamp (about 0.5" for example), and CH2 is a more distally positioned detector (such as about 5-15" or more or less), the distance ΔZ is the distance between the detectors and is known and is constant. In a sixth step, lamp operation is confirmed, and, as in step 2, normal operation may be a function of a pre-programmed or programmable operation or other mode. In the event the lamp is not operating, for whatever reason, data collected to that point in operation will be collected and evaluated. Proceed to step 8. Otherwise, if lamp operation and/or function is normal, proceed to step 7. Step 7 determines whether the counter has reached the end of its cycle, namely does 7=150. If the 150 th index of channel 1 and 2 vectors has been filled, proceed to step 8. Otherwise, check to see if a user- caused or system-caused interruption in data collection has occurred (step 3), and if not proceed through sequence step 4, step 5, step 6 and step 7 until finished filling vectors for CHI and CH2. In step 8, vectors are averaged over the number of valid indexes. Step 9 is a calculation of the absorption coefficient . For example, 254 is the absorption coefficient at 254 nm, and the detector response is optimized for 254 ± 20 nm. Based upon Lambert's law of equation (17): ' " " \ ^ fι Η / r Δ ~ l ) X J -=- - Ϊ: (30 In step 10, the absorption coefficient at lower wavelengths (such as at about 185 nm) and at upper wavelengths (such as at about 400 nm) is calculated. Since the 2 detectors are optimized for about 254 nm. 46 neither opacity at about 185 nm nor at about 400 nm can be measured directly. More detectors could be added, but that would be a costly solution, with greater chance for error with more detectors and more software compute cycles to be performed. A better solution is to calculate the other opacities based on Maxwell's equations. The absorption coefficients α* 8 j and α 400 can be found by comparing Lambert's law results for the decrease in light intensity with distance ΔZ penetrated into a medium, — <A - Λ -≥ r = J 0 (3. (31) with the equations for the mtensity obtamed from the solution of Maxwell's equations. Smce Maxwell's equations predict that for a wave traveling through a medium or matπx in die ΔZ direction: όC"^ - 2 s-) (32) where: z \ A x _ U_y / , • A\ = r - ' — L - j k ) (33) By substitution of equation (33) into equation (32): and simplifying: _ C^ -7 ; , /-. . ii •. >, (35) 47 Therefore, the wave amplitude decreases exponentially with distance ΔZ. The intensity of radiated light is proportional to the square of the field (wave) amplitude. Thus, ignoring the complex term in equation (34): <*•- / • £; C- - 2 A - 0 ^ (36) ^ 2 (37) o A. <A By substituting into Lambert's law: (38) c_ and comparing equations (31) and (38): i ~ι ^<--^ f ^ (39) G^~ ~ c in which ω is the angular frequency: (40) Thus, by substituting equation (40) into equation (39): _ - (41) 48 By applying the known value for a^ (calculated α) and solving for K h ~ (42) Thus, the absorption coefficients for the upper wavelengths (such as at about 400 nm) and for the lower wavelengths (such as at about 185 nm) can be calculated- oA . i o R & (43) Ό n 5 ~ - _ - (44) By calculating this '"expanded" information, a better determination can be made as to exactly what photomc energy is bemg dosed. By way of example only, m situations where no additional chemical or other oxidant is bemg used, those wavelengths below about 254 nm will be important Principally, wavelengths at or about 185 nm will cause photolysis mto water yielding hydroxyl free radicals -OH As another example, at or about 220 nm ozone is produced from dissolved oxygen (0 2 + 0 2 -* 0 3 + 0). The O is very reactive and plays a pan m the atomic abstraction of orgamc contammants. Therefore. if these wavelengths are bemg attenuated because of high total dissolved solids, then the flow rate can be lowered so as to allow for a higher dosage rate Thus, dosage is proportional to mtensity and time, or to lamp power, or to pulse repetition rate. Furthermore, if these wavelengths are bemg attenuated because of normal or abnormal lamp agmg. then flow rate can be lowered to an acceptable limit. In the cases where an adjunct chemical or other oxidant is used, higher energy, shorter wavelengths are also important. The 49 oxidant can often or usually be stimulated at longer wavelengths which are not so easily absorbed by the total dissolved solids. Therefore, oxidation can occur at higher flow rates In step 11. actual calculation of the opacity of the water matπx at the selected wavelengths can be made: -_. — - A ~- _^Δ * 5* W - W. ≤ z C ffl - e. <45) In step 12. a determination is made as to whether or not transmission is below a threshold setpomt or not. This determination is made based upon measured opacity If a low transmission is determined. proceed to step 13 If not. the preset, predetermined or otherwise previously adjusted flow rate, flashiamp power and oxidant infusion rates are maintained. Optionally, the counter can be reset at this pomt to a value of 1 and the measurmg cycle repeated If not. proceed to step 14 In step 1 . therefore, flow rate, flashiamp power and oxidant infusion rates are readjusted to approach and hopefully achieve the optimum dosage, and step 14 is an optional operator or system interrupt m the measuπng cycle Oxidant Insuring that there is enough oxidant available m the water to oxidize the contaminants is important. TDS can be measured to determme. directly or mdirectlv. amount or type of contammants. TDS are known to absorb ultraviolet and are likewise oxidized. TDS include dissolved metals such as iron. manganese, zmc. sodium, calcium magnesium, alummum. and copper Sulfates and sulfur compounds and nitrates as well as the heavy metals lead and mercury can also be present In a preferred embodiment the irradiation of water with blackbody irradiation, high m UV and other kill bands, causes production of oxidizmg mtermedianes such as hydrogen peroxide and free hydroxyl radicals. As opposed to systems which require mjection or meteπng of such oxidizing agents mto the 50 contaminated water to be puπfied. such as m an oxidizmg reactor, the present mvention utilizes the broadband radiation used for photo-decomposition and degradation of contaminants to form its own oxidizing agents from the water itself, resulting m increased, enhanced and residual oxidative decontamination function as well as lowered operating costs Experimental Data - Hydrogen Peroxide Production By way of example, the followmg results at a flow rate of about 3 8 GPM were obtamed. Test Lamp quality Baffles Pulse Rate (pps) Initial phenol (pp j Final phenol (ppm) Final H-O- (ppm) 1 opaque - used 0 4 1 0 0 4 ND 2 opaque - used 3 3 1 0 0 1-0 2 ND 3 clear - new 3 3 1 0 0 1-0 2 ND 4 clear - new 3 4 1 0 ND 0 3-04 J ' able 4 ND = Not Detectable Analysis Thus, it is demonstrated that the blackbody radiator of the present mvention produces broad band, high UV radiation which, by atomic abstraction, breaks down water and other intermediary species mto further oxidizmg mtermedianes. including hydrogen peroxide Because of this property, any residual contammants which may be present in the water after processmg are subject to oxidation by exposure to the generated volumes of hydrogen peroxide. This also reduces the overall adjunct chemical oxidant demand of the system, thereby reducing startup and capital, overhead and operatmg costs. The total amount of hydrogen peroxide produced by this process may be rather difficult to calculate It is possible that hydrogen peroxide or other meta-stable mtermedianes are formed duπng the process However, aside from the transient species, a well-defined concentration develops and is detectable as indicated in the table as the final value This spontaneous formation and production of hydrogen peroxide mtermedianes essentially prevents re-contamination of the water due to the residual oxidizmg 51 power due to the end-point steady state hydrogen peroxide content. Experimental Data - Absorbance FIGS. 16-18 show spectral absorbance data of borderline blackbody radiation and blackbody radiation at wavelengths of about 254, about 265 and about 400 nm, respectively, in tap water obtained under test conditions from a preferred embodiment of the blackbody radiator of the present invention. In the experimental tests, degree of filter transmission at different wavelengths is as follows: T 2J4 = 0.16, T 265 - 0.15 and T 400 = 0.44: and detector response at different wavelengths is as follows: ds- 254 = 0.39, ds 265 = 0.37 and ds^ = 0*50. The following equations were used to calculate output voltages corrected for degree of transmission, gain and distance from the lamp, normalized to an amplifier gain of A = 10 4 . for test run #4: SL ScL , := . ΑL (46) T 254- s 254 10 and: SH ScH AH — I 2 *•>5*-- d ass 254 10 * (47) Based on equations (46) and (47), the following measured low power and high power output voltages and calculated low power and high power signals were obtained in test run #4: Test 4 D 4 , AL 4| AH*, SL 4l SH 4l ScL 4l ScH 4) 1.5 10 4 10 4 1.46 2.36 23.397 37.821 52 6.5 10 3 10 4 7.444 1.70 1 1.923 27.244 22.0 10* 10 5 1.05 4.64 1.683 7.436 35.0 10 3 10 5 0.296 1.30 0.474 2.083 51.0 10 3 10 3 0.092 0.408 0.147 0.654 65.0 10 3 10 5 0.036 0.160 0.058 0.256 72.0 10° 10 3 0.220 0.088 0.035 0.141 Table 5 These results are shown in FIG. 16. The following equations were used to calculate output voltages coπected for degree of transmission, gain and distance from me lamp, normalized to an amplifier gain of A = 10". for test run #3: S ScL A 3 ι (48) WT 265 ' ds 265 . 10 4 / and: SH ScH AH -τ 265 ' ds 265 (49) ■ vr Based on equations (48) and (49). the followmg measured low power and high power output voltages and calculated low power and high power signals were obtained in test run #3: Test 3 D* AL 3 , AH 3l SL 3 , SH 3 , ScL 3 , ScH 3 , 1.5 10 4 10 4 2.48 3.24 44.685 58.378 6.5 10 4 10 4 1.92 2.80 34.595 50.450 22.0 10" 10 4 1.24 1.84 22.342 33.153 35.0 10 5 10 4 5.12 1.18 9.225 21.261 51.0 10 3 10 3 2.2 7.36 3.964 13.261 65.0 10 3 10 3 1.26 4.56 2.270 8.216 72.0 10 3 10 s 1.02 3.72 1.838 6.703 Table 6 These results are shown in FIG. 17. 53 NOT FURNISHED UPON FILING 54 SL ScL s *- • (52) /AL 254 ' ds 254 10" and: SH ScH 5. - ■ AH 5. (53) 254 ' d α s s 254 10" Based on equations (52) and (53), the following measured low power and high power output voltages and calculated low power and high power signals were obtained in test run #5: Test 5 D 5 , AL 5 , AH 5 , SL 5 , SH 5I ScL 5 , ScH 5l 2.0 10 4 10 4 1.26 2.16 20.192 34.615 8.0 10 3 10 3 3.18 12.16 5.096 19.487 20.0 10 3 10 3 0.468 2.12 0.750 3.397 33.0 10 3 10 3 0.090 0.412 0.144 0.660 45.0 10 3 10 3 0.026 0.112 0.042 0.179 60.0 10 3 10 ό 0.005 0.224 0.008 0.036 74.0 10° 10 ό 0.053 0.144 0.008 0.023 Table 8 These results are shown in FIG. 19. FIG. 20 shows spectral absorbance data of borderline blackbody radiation and blackbody radiation at a wavelength of about 400 nm in brine water obtained under test conditions from a preferred embodiment of the blackbody radiator of the present invention. The following equations were used to calculate output voltages corrected for degree of transmission, gain and distance from the lamp, normalized to an amplifier gain of A = 10 4 . for test run #6: SL , ScL , AL (54) ' : T 400 ds 400 10" and: 55 SH 6. ScH 6. - ■ AH 6. (55) — 4(Jo ds 400 10" / Based on equations (54) and (55), the followmg measured low power and high power output voltages and calculated low power and high power signals were obtamed in test run #6: Test 6 D SI AL 6I AH,, SL 6 , SH,, ScL 6 , ScH., 1.5 10 4 10 4 2.30 3 00 10.455 13.636 6.5 10 4 10 4 1 64 2.32 7 455 10.545 22 10 3 10 4 5 20 1.20 2.364 5 455 35 10 3 10° 2.14 7 68 0.973 3.491 51 10 3 10 J 0.832 3 00 0 378 1.364 65 10 J 10° 0 504 1 82 0.229 0.827 72 w w 0.348 1 26 0.158 0.573 Table 9 These results are shown m FIG. 20. Analysis As shown in FIGS. 16-20. the output signals conesponding to depth of penetration of the radiation mto the water or bπne matnces by the higher power blackbody radiator of the present mvention is stronger, at essentially all wavelengths tested, than the response of a borderline blackbody radiator for essentially all tested distances from the lamp FIG. 21 shows an analysis of spectral absorbance data of borderline blackbody radiation at a wavelength of about 254 nm in tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present mvention and data from Lambert ' s law usmg the calculated CoA at the same wavelength. The followmg equations were used to calculate CoA for test run #4- 0.000 ' ScH 0.050 -In 0.074 ScH (56) <zH αH 0.083 D 0.080 0.077 0.078 56 and: ι = 2 ιτH 4m 6 (57) αH 4m = 0.074 Thus, αH 4ra = 0.074. Therefore, to determine the corresponding output voltage I based on Lambert's law at 33.870 ' calculated CoA: ,, . .. 23.44a 7.499 ' " H 4m-°-l, 1 4 := ScH 4 e 2.883 0.889 (58) 0.317 0.190 Thus, solving equation (58) for I, the following results were obtained for test run #4: Test 7 αH, I 4 0.000 33.870 0.050 23.448 0.074 7.499 0.083 2.883 0.080 0.889 0.077 0.317 0.078 0.190 Table 10 These results are shown in FIG. 21. FIG. 22 shows an analysis of spectral absorbance data of borderline blackbody radiation at a wavelength of about 265 nm in tap water obtained under test conditions from a preferred embodiment of the blackbody radiator of the present invention and data from Lambert's law using the calculated CoA at the same wavelength. The following equations were used to calculate CoA for test run # 3 : 0.000 ' ScH 3. 0.029 In ScH 0.038 (59) αH αH 0.034 3. 0.032 0.032 0.030 57 and: αH 3, i Σ= 2 αH 3m = (60) αH 3m 0.032 Thus, αH 3m = 0.032. Therefore, to determine the corresponding output voltage I based on Lambert's law at 55.608 ' calculated CoA: 49.644 35.900 — " Sin 0 .-*-) I 3 := ScH 1 3 = 22.076 V 13.143 (61) 7.824 _ 5.658 Thus, solving equation (61) for I, the following results were obtained for test run #3: Test 3 αH 3 Is 0.000 55.608 0.029 49.644 0.038 35.900 0.034 22.076 0.032 13.143 0.032 7.824 0.030 5.658 Table 11 These results are shown in FIG. 22. FIG. 23 shows an analysis of spectral absorbance data of borderline blackbody radiation at a wavelength of about 400 nm in tap water obtained under test conditions from a preferred embodiment of the blackbody radiator of the present invention and data from Lambert's law using the calculated CoA at the same wavelength. The following equations were used to calculate CoA for test run #7: 0.000 ' ScH 7 0.063 -In i ScH 0.052 (62) αH 7. αH 0.070 0.074 0.070 0.068 58 and: αH i = 2 αH 7m (63) αH 7rπ = 0.066 Thus, αH 7m = 0 066. Therefore, to determme the corresponding output voltage I based on Lambert's law at 10.537 ' calculated CoA. 7.570 4.038 - 'αH 7m u 7, 2.379 7 • = ScH 7, » 7 S 0.773 (64) 0.268 0.099 Thus, solving equation (64) for I. the followmg results were obtamed for test run #7 Test 7 αH 7 I 0 000 10.537 0.063 7 570 0.052 4 038 0 070 2.379 0 074 0 773 0 070 0 268 0 068 0 099 Table 12 These results are shown m FIG. 23. As shown in FIGS 19-21, the measured output signals, corresponding to absorbance levels at vaπous distances from the lamp, from the near or border blackbody radiators of the present mvention are very close to those which would be deπved from Lambert's law usmg the calculated CoA. FIG. 24 shows an analysis of spectral absorbance data of blackbody radiation at vaπous wavelengths in tap water obtamed under test conditions from a preferred embodiment of the blackbody radiator of the present invention. FIG 25 shows an analysis of spectral absorbance data of blackbody radiation at vaπous wavelengths in bπne water obtamed under test conditions from a preferred embodiment 59 NOT FURNISHED UPON FILING 60 wavelengths between about 240 and about 280 nm with a peak kill zone between about 260 and about 265 nm. Mercury vapor lamps which produce 254 nm radiation have been used in the past, however, the use of the near blackbody radiation of the present invention, including the domain between about 260 nm and about 265 nm, provides many times greater penetration depth into the water matrix, thus translating into greater kill efficiency over the range of output, specifically within the cited domain. Microbial kill is enhanced by absorption of the VIS as well as the IR bandwidths as well. According to the following equations : aH 4m 254 254 - 4*ιι (69) k ^.-r α1 := 254 (70) and k 254- -π α2 := 40 ° (71) the following values are obtained: k^ ****- 1.486571; αl = 0.074; α2 = 0.047; and αH 7m = 0.066. Similarly, according to the following equations: k k 265 - . - αH _3_m 2 "_ (72) 61 NOT FURNISHED UPON FILING 62 ScH 3. (78) 8cH 3norm. i ScH 3max the following results are obtained: scϋ-^-^yo) D 4 ScI . (%) D 3 100.000 1.500 100.000 1.500 72.034 6.500 86.420 5.000 19.661 22.000 56.790 15.000 5.508 35.000 36.420 30.000 1.729 51.000 22.716 46.000 0.678 65.000 14.074 62.000 0.373 72.000 11.481 72.000 Table 13 By assuming that a distance of 1.5" is equivalent to the lamp surface, then radiation attenuation can be determined by solving the followmg equations: (79) M φdπa. : ~ * dna ScH 4noιm and 03 φdπa. := * dna ScH 3norm. (80) the following results show that radiation attenuation degrades according to Lambert ' s law as follows: D4 φDNA (J/cnr) D3 φDNA (J/cnr) 0.000 10.537 0.063 - 7.570 0.052 4.038 0.070 2.379 0.074 0.773 0.070 0.268 0.068 0.099 Table 14 63 respectively, can be made by solving the followmg equations: ScH H34. - ScH (81) and ScH 3. H37. ScH (82) Results are as follows: ΔH 34 ΔH 37 1.544 5.017 1.852 6.529 4.459 6.512 10.205 9.910 20.282 23.340 32.043 38.296 47.528 77.610 Table 15 Lamp Spacing As has been determined, the required dosage A to kill bacteria, in particular the organism Paramecium caudatum as an example, is about 30000 x 10 "6 watt sec/cπr or about 0.030 joule/cm : . For typical, low-pressure mercury vapor-type lamps, this requires a lamp spacing of at most 3". As has been determined experimentally, however, the irradiance of wavelengths effective at disrupting DNA φ DNA is about 1.38 jouie/cm : and an exitance value of about 32.98 joules has been observed. Furthermore, with respect to the UV bands, φuv is about 4.84 joule/cnr with an exitance value of about 115.86 joules. 64 As mentioned above, an example of an application is in remediation of industrial waste water. Because of the greater distance that the blackbody radiation is able to penetrate mto the water/contaminant matrix, a greater distance between lamps is possible. As shown above, as opposed to a lamp spac g of only between about 3 and about 6 mches usmg low or medium pressure lamps, an increased spacmg of between about 18 and about 24 inches is now possible This greatly reduces the number of lamps, system head losses as well as operating and maintenance costs. Variable Flow Rates Another advantage of the present mvention is the efficacy of the blackbody radiators duπng peπods of both high flow rate as well as low flow rates. In the past, a fairly constant flow rate through a water purification module has been required, based on design characteπsυcs of systems utilizing the low and medium pressure mercury vapor lamps of the pπor art. In the present invention, however, a very broad range in flow rate through a given lamp module can be accommodated with resultant highly efficient water puπfication throughout the range of variability. It will be understood by those skilled in die art that lamp modules can be installed m parallel, senal or other configurations. Thus, duπng times of high flow rate, short circuiting of water due to increased depth of flow over the lamps is not significant because of the deep penetration of the blackbody radiation the kill and decontamination zones. Typical system configurations are descnbed more fully m the following documents: Water Disinfection with Ultraviolet Light- Aquafme Wedeco Environmental Systems. Inc. brochure. 1996: and Ultraviolet - UV Disinfection in Power Cogeneration. Ultrapure Water. Vo. 12. No. 5. July/August 1995 Unless defined otherwise, all technical and scientific terms used herem have the same meaning as commonly understood by one of ordinary skill in the art to which this mvention belongs. Although any mediods and materials similar or equivalent to those described can be used in the practice or testmg of the 65 present mvention, the preferred methods and mateπals are now descnbed. All publications and patent documents referenced m this application are incorporated herem by reference While the principles of the mvention have been made clear m illustrative embodiments, there will be immediately obvious to those skilled m the art many modifications of structure, arrangement proportions, the elements, mateπals. and components used m the practice of the invention, and otherwise, which are particularly adapted to specific environments and operative requirements without departing from those prmciples The appended claims are mtended to cover and embrace any and all such modifications, with the limits only of the true purview, spiπt and scope of the mvention

Claims: 66 I claim:: 1. A system for photolytic decontamination of water utilizing near blackbody radiation comprising: a reaction chamber defining an internal space with an inlet and an outlet: and a broadband radiator which generates radiant energy, at least a portion of which is delivered in a pulsed mode, over a continuum of wavelengths between about 150 nm and about 3 μm. the broadband radiator disposed withm the reaction chamber such that a sufficient dosage of broadband radiation penetrates a sufficient distance mto the contaminated water withm the mtemal space. 2. The system of Claim 1 m which hydroxyl radicals m the form of hydrogen peroxide or similar oxidants are formed m the contaminated water, thereby decreasmg the need for use of adjunct chemical or other oxidants. 3 The system of Claim 1 m which the near blackbody radiation compπses ultraviolet radiation over a contmuum of wavelengths between about 260 nm and about 265 nm. 4. The system of Claim 1 adapted for use m conditions under which flow rates through the system vary significantly. 67 1 5. A system for photolytic decontamination of water utilizing near blackbody radiation, the system compπsmg: 3 a reaction chamber adapted for decontamination of water under varying flow conditions; and I* a broadband radiator which generates radiant energy, at least a portion of which is delivered in a ' pulsed mode, over a continuum of wavelengths between about 150 nm and about 3 μm, the broadband radiator disposed withm the reaction chamber such that a sufficient dosage of broadband radiation penetrates a sufficient distance mto the contaminated water withm the reaction chamber 6. A reactor for photolytic decontamination of groundwater utilizing near blackbody radiation, the reactor compπsmg: a reaction chamber defining an mtemal space with an inlet and an outlet; and a plurality of flashiamp type broadband radiators which generate pulsed radiant energy at a rate of between about 1 and about 500 pulses per second with wavelengths between about 150 nm and about 3 μm at between about 1 KW and about 15 MW peak power which provides a dosage rate of broadband radiation between about 1 joule/cπr and about 5000 joules/cm : , the broadband radiator disposed withm the reaction chamber to penetrate irradiate the contaminated water withm the mtemal space of the reaction chamber, the plurality of flashlamps having a minimum spacmg between about 12 inches and about 24 inches. /// 68 7 A method for photolytic decontamination of water utilizing near blackbody radiation, the method utilizmg a reactor compπsmg a reaction chamber with an mtemal space, an inlet and an outlet and at least one flashiamp type broadband radiator which generates pulsed radiant energy at a rate of between about 1 and about 500 pulses per second with wavelengths between about 150 nm and about 3 μm at between about 1 KW and about 15 MW peak power, the method compπsmg the following steps- oxidizmg components withm the contaminated water by providing a sufficient dosage of broadband radiation between about 1 joule/cnr and about 5000 jouies/cπr; and forming hydroxyl radials m the form of hydrogen peroxide or other similar oxidants m the contaminated water. 8 A method for steπlization of water utilizmg near blackbody radiation, the method compπsmg the steps of pulsmg at least one flashiamp type broadband radiator at a rate of between about 1 and about 500 pulses per second at between about 1 KW and about 15 MW peak power, and delivering ultraviolet radiation having a contmuum of wavelengths between about 260 nm and about 265 nm to the water. 9 A system for steπhzation of water utilizmg near blackbody radiation, the system compπsmg at least one flashiamp type broadband radiator pulsed at a rate of between about 1 and about 500 pulses per second at between about 1 KW and about 15 MW peak power to deliver ultraviolet radiation having a continuum of wavelengths between about 260 nm and about 265 nm to the water and a penetration depth of between about 40 times and about 50 times greater than that of a mercury vapor lamp ///

Inventors: BENDER JIM, BENDER, JIM
Applicants: NEW STAR LASERS INC, NEW STAR LASERS, INC.
Application year: 1999
Main classification: C02F1
IPC codes: A61L2, C02F1