MXPA97005473A - Method and apparatus for removing volatile organic compounds by oxidation in f - Google Patents

Abstract

A method and apparatus for reducing, knocking down and destroying volatile organic compounds (V.O.C) contained in an air stream are described. The air stream is mixed with an activated air mist or mist in aqueous solution, while the mixture is repeatedly exposed to ultraviolet radiation in chambers along a tunnel. Activated air contains oxidants that are formed by exposing ultraviolet light air. The activated air is generated under conditions that prevent prolonged ozone existence and improve the generation of highly active oxidants such as hydroxyl radicals. the aqueous solution is formed by dispersing the activated air in water, in cooling tanks that include ultraviolet lamps to maintain a high level of oxidants in the aqueous solution. The tunnel includes catalyst plates that act as scavengers and which are exposed to ultraviolet light in the tunnel to provide hydrogen to improve the generation of the hydroxyl radicals. The tunnel includes scrubbers that remove particulate water and V.O.C., which are collected in a supply tank and recirculated to the spray tanks and then back to the tunnel. The tunnel also includes carbon filters that collect V.O.C. for surface reaction in the presence of more ultraviolet light. Before discharge from the tunnel, the air stream is supplied to a coal bed system, where the V.O.C. the remaining are captured and oxidatively destroyed

Description

METHOD AND APPARATUS FOR -RETRACTING VOLATILE ORGANIC COMPOUNDS BY OXIDATION IN FRXO FIELD OF THE INVENTION This invention relates in general to controlling environmental contamination and more particularly to a method and apparatus reducing and destroying volatile organic components (V.O.C.). BACKGROUND OF THE INVENTION The V.O.C. For many years they have been a major source of air pollution as an unavoidable pollutant, which is discharged from many industrial processes including, for example, large industrial paint shops employed in the automotive industry. Legislative efforts have established emission standards to control the emission of V.O.C. in the environment. The current and future compliance with these standards imposes a continuous demand on the industry and creates a continuous need to reduce, degrade and eventually destroy V.O.C emissions. in a way that is not prohibitive in cost. This is particularly critical for manufacturers in industrialized countries that compete against sources that operate in countries that do not have strict laws for air pollution control. In automotive paint shops, large volumes of solvent-charged air (VOC) must be removed from paint spray booths, and to a lesser extent, from other paint shop operations, such as retention and silent zones, and the furnaces for painting. For automotive paint shops, large amounts of solvent charged air must be processed. Various techniques and combinations of them to date have been used to abate V.O.C. in painting workshops. Typically, scrubbers are used to capture inorganic chemicals and particulate paint from process discharge air using liquids pumped through the scrubber. Any remaining paint particles are then removed from the discharge air by filter banks with progressively increased efficiencies. Less expensive filters are used in the initial stages to trap most of the larger paint particles. After filtering, the discharge air stream is heated to reduce humidity for a subsequent adsorption process. In adsorption processes, solvent charged air is concentrated in smaller amounts, typically 10% of the main discharge air stream, and then processed. Typically, the concentration is achieved by adsorbing V.O.C. in a coal bed and then desorb the coal bed with hot air, hot inert gas or steam. The concentrated desorption product can then be finally processed through chemical treatment, solvent recovery or incineration.

Various incineration apparatuses can be used to oxidize the solvents in a concentrated air-solvent mixture that is taken from the coal beds. However, typically the mixture is heated to temperatures exceeding 760"C (1,400" F). When these temperatures are maintained, the solvents react with oxygen, with the final reaction production products theoretically being water vapor and harmless carbon dioxide. Various types of heat exchangers for thermal regeneration and the like are used to recover heat from the incinerator discharge to improve thermal efficiency. Direct incineration can be employed but generally has low thermal efficiency, particularly for processing large volumes of air charged with V.O.C .. However, these prior art systems require high capacity coal beds and have high energy costs by incineration. Except in the most advanced systems, some off-site and / or waste treatment is often required. For smaller installations, in contrast to large assembly or automotive plants, off-site charcoal desorption may be more cost-effective. In general, coal beds when used alone are not effective or cost efficient to process large volumes of air charged with V.O.C .. Special systems are required to desorb coal beds and for many applications, this is achieved off-site. Additionally, the desorption concentrate must still be treated for solvent removal and / or incineration. The incineration generally generates NOx or carbon monoxide and without thermal recovery systems, it has a direct thermal impact on the environment as well as requiring off-site disposal. More importantly, prior art systems that rely on high temperatures to complete oxidation are costly to operate and may still require off-site disposal. These disadvantages, particularly when coupled with control of environmental pollution and anticipated air and current, which give a continuous need for improved abatement of V.O.C .. Another technique that has been used for abatement of V.O.C. in industrial process air involves the use of ultraviolet light (uv) to decompose V.O.C. directly and to form activated air that contains oxygen in the form of ozone and other oxidants that also work to break V.O.C. As used herein, "activated air" will be understood to refer to air that has been treated, either by exposure to ultraviolet light or some other method to increase the concentration of oxidants in the air. Commercial systems are available that employ this technique for abatement of solvents contained in the process air discharged from industrial paint booths, ovens, conformed coating areas, etc. A typical system includes a two-stage prefilter, a photolytic reactor, an aqueous reactor, a purifier, and a pair of granular carbon beds. Particles of one size and larger in size are collected and removed from the process air and pre-filters. The air flow then passes through the photolytic reactor, where it is exposed to adjusted ultraviolet light. The exposure of process air to ultraviolet light results in photochemical reactions that form ozone from the oxygen contained in the air, as well as peroxides of the moisture content within the air. Oxidative degradation begins in the photolytic reactor due to both the newly formed oxidants and the direct exposure of the V.O.C. in ultraviolet light. The air stream is then purified with ozonated water in the aqueous reactor. Ozonated water is generated by submitting air to ultraviolet light and then injecting and mixing the activated air in the water. In this stage, water-soluble hydrocarbons will be collected in the water and thus removed from the air stream. After passing through the aqueous reactor, the water vapor contained in the air stream is removed by the purifier. The final step in this process is to pass the air stream through a carbon bed for adsorption of any V.O.C. remaining. A second coal bed is used, so that while one coal bed is in line to adsorb the VOCs, the other is in the process of regenerating using ozone containing activated air, hydrogen peroxide and other photo-produced oxidants. by exposure of clean air to ultraviolet light.

The use of ultraviolet light to generate ozone containing activated air has also been implemented in various systems to treat water. For example, the following U.S. patents. each one addresses the use of ozone and other oxidants in the wash water of a laundry system: 3,065,620, granted on November 27, 1962 to P.H. Houser; 3,130,570, granted on April 28, 1964 to P.M. Rentzepis; 3,194,628, granted on July 13, 1965 to P. Camión; 5,097,556 granted on March 24, 1992 to R.B. Engel et al; and 5,241,720 granted on September 7, 1993 to R.B. Engel et al. In these systems, ozone is produced by exposing air to ultraviolet radiation that occurs either corona discharge or ultraviolet lamp. The activated air that contains, ozone and in some cases hydrogen peroxide, is mixed with washing water to improve laundry cleaning and reduce or even eliminate the need for detergents. The literature also suggests that substantial laboratory efforts have been directed toward using ultraviolet radiation for other types of water treatment. See Legrini, Oliveros and Braun, "Photochemical Processes for Water Treatment", Chem. Rev. 1993 to pages 671 to 698, American Chemical Society Document No. 0009-2665 / 93 / 0793-0871. Ultraviolet radiation for water treatment is potentially useful not only to treat drinking water, but also to treat contaminated surface water, groundwater, and wastewater. However, based on the 221 biographical references cited and reviewed, the author suggests that most of this laboratory experimentation, with a few notable exceptions, has not been evaluated on a prototype basis much less commercially. Although the Chemical Review article addresses water treatment in contrast to V.O.C. in industrial process air, some of the mechanics of oxidative degradation there considered to be useful as background for the present invention. For example, Table I on page 674 (reproduced as "TABLE 1" below) confirms the oxidative potential of various oxidants that are considered available from the activated air and undoubtedly generated elsewhere in the system and process of the present invention. as will be described. TABLE 1 Oxidation Potentials of Some Oxidants Species Oxidation potential (V) fluorine 3.03 hydroxyl radical 2.80 atomic oxygen 2.42 ozone 2.07 hydrogen peroxide 1.78 perhydroxyl radical 1.70 TABLE 1 (cont.) Oxidation Potentials of Some Oxidants Potential Oxidation (V) ) permanganate 1. 8 hypobromic acid 1.59 chlorine dioxide 1.57 hypochlorous acid 1.49 hypoiodose acid 1.45 chlorine 1.36 bromine 1.09 iodine 0.54 Each of the above references, as well as the literature describing the commercially available air treatment systems described above, all adopt the same principles. virtues of ozone and the use of ultraviolet radiation to generate that ozone. However, as illustrated in Table 1 above, ozone has a oxidation potential lower than hydroxyl radicals. In this way, ozone has less tendency to cause oxidation of V.O.C. than the hydroxyl radical; that is, it is less active than the hydroxyl radical. The patent of the U.S.A. No. 4,214,962, granted on July 29, 1980 to A.J. Pincon establishes other disadvantages of creating ozone in addition to other oxidants formed by ultraviolet radiation; that is, the increase in surface tension of water with which it is mixed and the possible formation of carcinogenic substances. In this patent, an apparatus is described for using ultraviolet light under 200 nanometers to generate an activated oxygen product not described, without the production of ozone. When used to treat water for human consumption or for swimming pools, the apparatus may include a polyvinyl chloride enclosure to allow free chlorine release, to provide water chlorination. Not unexpectedly, however, since the Pincon patent is aimed at the use of ultraviolet radiation for water treatment, it does not address the problems associated with processing large amounts of industrial process air charged with VOC, much less offers direct solution to the problems and disadvantages of the various commercial processes that are based at least in part on the presence of ozone for abatement of VOC in the discharge of paint spray booths. SUMMARY OF THE INVENTION The invention provides a method and apparatus for reducing, collapsing and destroying volatile organic compounds on a continuous basis, wherein a stream of air charged with V.O.C. It is mixed with and held in an activated mist or mist of air in an aqueous solution, while the mixture is repeatedly exposed to ultraviolet radiation in a series of chambers along a tunnel. The activated air contains oxidants such as hydroxyl radicals, hydroperoxy radicals and hydrogen peroxide. Preferably, some of the activated air is introduced into the tunnel in gaseous form. The activated air is generated by exposing humid air to ultraviolet radiation and the activated air is then dispersed in an aqueous solution in spray tanks. The spray tanks also include ultraviolet light lamps to generate and maintain a high level of oxidant in the aqueous solution and promote other reactions just before the aqueous reaction is introduced into the tunnel as fog or mist. Preferably, before discharge of the tunnel, the air stream is still in a highly active state and is supplied through an expansion chamber to large coal beds, where the V.O.C. The remaining ones are captured and destroyed additionally in oxidative form. Clean air and water vapor and possibly harmless carbon dioxide are discharged from the coal beds into the atmosphere. Preferably, two coal beds are used in such a way that a coal bed is in line to capture any V.O.C. remaining, while the second coal bed is regenerated. Activated air is used to regenerate the coal beds, so that the regeneration not only desorbs the coal bed but also deposits and replenishes the coal bed with oxidizers of the activated air. This regeneration ensures that oxidants are available for surface reactions with any M. O.C. remaining when the regenerated coal bed is carried in line. Preferably exhaust gases from the regeneration process are recirculated back through the tunnel, together with the activated air that is vented from the spray tanks in such a way that any reaction products generated in the coal beds are treated continuously, while they are recirculated through the system. The final products of the cold oxidation process of the present invention are considered water (H20) and carbon dioxide (C02) as in an ideal incineration process. However, although some water vapor and harmless carbon dioxide gas are undoubtedly released into the environment, most of the water is retained in the system. Compared to incineration, less carbon dioxide than expected is discharged from the coal bed that is in line. In any event, the discharge of the system to the environment is not a thermal pollutant. While not assigned to any theory, it is strongly considered that the present invention destroys V.O.C. by a combination of two phenomena, which undoubtedly produce a synergistic effect. First, the activated air that is generated by ultraviolet radiation and additional ultraviolet radiation of the active mist, produces highly reactive oxidants that later decompose and destroy in a subsequent oxidative way the V.O.C .. In second, the direct ultraviolet photolysis of the V.O.C. causes chemical decomposition of V.O.C. with the resulting products that interact with oxygen, the oxidants and other intermediate radicals in the activated air and the activated air mist in the tunnel and preferably in the spray tanks and the coal beds. These two phenomena occur alone and in combination to varying degrees, not yet fully determined in the various stages described above, mainly: 1. Reaction of V.O.C., intermediates and oxidants in the vapor stage, which occurs in the tunnel chamber; 2. Reactions with V.O.C., intermediates and oxidants in the tanks of oxidation by aqueous spraying; 3. Surface reaction and final destruction of V.O.C. in the coal beds; and 4. To a lesser degree, reactions of the intermediates and oxidants in the supply tanks and PVC piping used through the system. Improvement of the activity level of the activated air is considered to occur by one or more effects that serve to decompose ozone generated by the irradiation of the ultraviolet lamps and in this way allow the oxygen of released air that is combined with the available atomic hydrogen to form hydroxyl radicals. These effects include photolysis of ozone using ultraviolet light at a wavelength of 254 nm, degradation of ozone as a result of creating and maintaining activated air in a high humidity environment, and ozone degradation by radicals such as Cl ", available from the ultraviolet radiation of a PVC or other catalyst, regardless of precisely where and how the total destruction of VOC occurs and how it progresses, no waste residue is regenerated, due in part to the continuous recirculation of the aqueous solution through the tunnel, the storage tank, the spray tanks and the circulation of the discharge air from the coal bed to the tunnel, components of the cold oxidation system, and particularly the tunnel, are of modular construction to achieve original economic installation, future expansion of system and modification during its serial production of existing systems with minimal capital expenditure and time It is not operative, although it is particularly suitable for abatement of V.O.C. of discharge air in paint spray booths for which they were designed, the method and apparatus of the present invention are potentially useful for destruction of V.O. in discharge air from many other industrial and laboratory processes, for example electro-coating, phosphating and other bath-type treatment processes and the manufacture of powder resins and other resin propagation processes. Still further, the present invention is potentially useful for destroying a wide variety of V.O.C. different from those commercially used in paint solvents, for example various harmful carcinogens and unwanted hydrocarbons.

Objectives, features and advantages of the present invention are to provide a method and apparatus for abatement of air pollution of: V.O.C., which overcome the disadvantage of the prior art for abatement of V.O.C. in discharge gases; that effectively and efficiently, both in cost and results, reduce, reduce and / or destroy volatile organic compounds before discharging into the environment; that effectively destroy volatile organic compounds in discharge gases at levels well below accepted norms; that facilitate installation, operation and maintenance at a relatively low cost; that provide fast and cost efficient installation, part replacement, system expansion and modification during serial production, with low capital expenditures and short non-operational times; which do not produce any NOx, carbon monoxide and / or ozone or other harmful gases, detectable, discharged into the atmosphere or undesirable final reaction products such as nitrogen oxides and nitrous acid, which either remain in the system and / or they will require treatment for off-site disposal; that will reduce the size of capacity and cost of the coal bed, in contrast to coal beds of the prior art used with or without subsequent incineration; that operate on a continuous basis, with high volumes of polluted air and eliminate batch processing; that do not require high oxidation temperatures and are energy efficient; and that are particularly effective in cost and efficient for abatement of V.O.C. in industrial processes involving large quantities of discharge air charged with V.O.C., particularly automotive and other large industrial and similar paint shops. BRIEF DESCRIPTION OF THE DRAWINGS A preferred exemplary embodiment of the present invention will now be described in conjunction with the accompanying drawings, where like designations denote like elements, and: Figure 1 is a schematic diagram of a V.O.C. of the present invention which is useful for carrying out the method of the invention; Figure 2 is a diagrammatic view of a primary treatment tunnel of the abatement system of Figure 1 showing the location and relative placement of the various components used in the tunnel; Figure 2A is a perspective view of an ultraviolet and baffle lamp used in the tunnel of Figure 2; Figure 3 is a schematic diagram of a liquid subsystem used in the abatement system of Figure 1 to generate activated haze and continuously recirculate liquid through the system; Figure 4 is a sectional view through a spray tank of the liquid subsystem of Figure 3; Figure 5 is a view, partially broken away and in section, of a cell for generating activated air in the systems of Figures 1 and 3; Figure 6 is a perspective view of a deflector plate sub-assembly of the regenerative cell of Figure 5; Figure 7 is a schematic view of an air flow system for regenerating coal beds and discharging recirculation in the abatement system of Figure 1; and Figure 8 is a schematic view of a regeneration pipe for the coal beds of Figure 7. DETAILED DESCRIPTION General View of the Abatement System of V.O.C. Figure 1 schematically shows a preferred embodiment of a V.O.C. 10 of the present invention as it will be used to handle large volumes of process air loaded with V.O.C., discharged from large automotive paint spray booths. As illustrated in Figure 1, an air stream charged with V.O.C. 12 is directed through a primary treatment tunnel 14 between an inlet 16 and an outlet 18 using a large centrifugal impeller blower 20. The tunnel 14 continuously treats the air stream to destroy the V.O.C. within the air stream by oxidative degradation and photolysis. In general, this is achieved inside tunnel 14 by mixing the air stream with activated air and by direct exposure of the air stream to ultraviolet light. The blower 20 pushes the tunnel that discharges air 14, together with any V.O.C. in an expansion chamber 22 and then through a carbon bed absorption tower-reactor system 24, which discharges to the environment through the discharge chimney 26. As will be described in more detail below, a generator activated air 28 produces activated air which is supplied by a second impelling blower 30 to the coal bed system 24 and the upstream end of the tunnel 14. The coal bed system 24 comprises a pair of separate and isolated carbon beds 32 , 34, such that when one of the coal beds is in line in the process and treating discharge air from the tunnel 14, the other coal bed is regenerated using the activated air from the regenerator 28. The activated air of the regenerator 28 contains a high level of oxidants that desorb and regenerate the coal bed out of line. Primary Treatment Tunnel With reference again to the primary treatment tunnel 14, activated air containing a high level of oxidants is fed from the second activated air generator 40 via the pipe 42 to a courtyard of spray tanks 44, which using ultraviolet radiation generates an aqueous solution loaded with recently generated and reactivated oxidants. The oxidant-laden solution is then fed via pipe 46, solenoid-operated valve 48 and header 50 to various select modular sections Sl to S15, where it is introduced as an active mist in various selected tunnel chambers Cl to C15, to maintain a high humidity environment, enriched with oxidants inside the tunnel 14. This high humidity environment enriched with oxidants performs several important functions, as will be described later in greater detail. The oxidant-laden solution of the spray tank yard 44 is also fed by the pipe 46, solenoid valve 52 and pipe 54 to a set of nozzles 56 that also provide a high humidity environment, enriched with oxidants, downstream of an assembly of primary particulate filters 66 at the inlet 16 of the tunnel 14. Also located downstream of inlet 16 is a set of activated air nozzles 68, which is connected to a bypass 74 to receive partially spent activated air, discharged from the regeneration of the Carbon bed system 24. In this way, any VOC contained in this regeneration discharge gas will be recirculated through the abatement system 10. These nozzles also receive activated air which is vented from the spray tank yard 44, as will be described below. In addition, these nozzles are also connected to a second branch 72 that can be used to provide freshly generated activated air from the generator 28 in the event that even greater oxidative activity is required in the tunnel 14.

The activated aqueous solution introduced into the tunnel 14 by the nozzles 56 and nozzle head 50, which precipitates, condenses and / or is filtered out of the air stream 12, is collected in a supply tank 60 from which it can be recirculated through a pump 62 and pipe 64 back to tank yard 44, where it is mixed again with activated air from generator 40 and exposed to ultraviolet radiation to provide a continuous recirculating supply of oxidant enriched mist to tunnel 14. Advantageously, each of the modular sections, S1-S15 can be constructed totally or partially off-site. The modular sections include racks, structural members, pipes, fittings and some electrical wiring for the various functional components, ie UV lamps, fog nozzles, Viledon filters, carbon filters and catalyst plates, some of which can also be preassembled in the modules. The spray tank yard 44 and the coal bed system 24 can also be partially assembled off-site as modules. External housing panels for the tunnel 14 are fabricated and assembled on site, preferably of sheet metal of stainless steel to form the C1-C15 chambers. After completing all the fabrication of sheet metal and ducts, the necessary pipes, valves and electrical wiring connections are made and the system is cleaned and washed by dragging before final installation of nozzles and ultraviolet lamps. Although an understanding of the present invention will be more fully apparent from the following detailed description in general, the air stream with V.O.C. 12 entering the tunnel 14 is separated in the filters 66 to remove paint on particles and other particles. It is then mixed with the oxidized enriched mist of the nozzles 56 and with gaseous activated air from the nozzles 68. The mixture then enters an expansion chamber 76 which allows the air stream to equilibrate and charge the unit to a steady flow . As the air stream continues to move from left to right as seen in Figure 1, it passes through the series of treatment chambers, Cl to C15, defined between corresponding modular sections Sl to S15, where the V.O.C. at least it is partially destroyed by photo-decomposition and oxidative degradation. According to the current loaded with V.O.C. 12 passes through chambers Sl to S15, is repeatedly exposed to ultraviolet radiation in the high humidity environment, loaded with oxidants. The activated air mist is replenished repeatedly by the head 50 in the selected modular sections Sl to S15. According to the air flow charged with V.O.C. it moves through various filters, precipitators and purifiers, water in particles, together with water-soluble compounds, are collected in the supply tank 60. Preferably, selected purifiers are perforated plates coated with a catalyst, such as dioxide. titanium, which provides hydrogen for the production of hydroxyl and other oxidants, in order to improve the oxidative degradation of VOCs Perforated plates and, to a lesser extent, filters, also act as purifiers to mix and carry the activated air mist, oxidants and VOC in intimate contact with each other. Preferably, various other components in the system are made of PVC to serve co or catalysts. The water from the supply tank 60 is recirculated to the spray tank yard 44, mixed with the activated air from the generator 40, exposed to additional ultraviolet radiation, and reintroduced to the tunnel 14. Except for the high humidity vapor discharged from the tunnel, together with the air charged with VOC The remaining water and any water-soluble intermediates of the V.O.C. reactions are recirculated in a substantially closed system until all the remaining intermediate reaction products are reduced in water and / or carbon dioxide. Activated Air As will be described in more detail below, the activated air that is supplied to the generator 40 is produced by exposing moist air to ultraviolet radiation to produce oxidizing radicals, preferably under turbulent flow conditions and in the presence of a catalyst to improve generation of oxidants and produce additional oxidants. Normally, the air in the plant is used as a supply of fresh air to the generator 40 with a humidity level of 85% that is typical. If necessary, moisture can be introduced into the air in the generator 40 for example by absorption by capillarity of water in the air of the plant. The ultraviolet light preferably includes wavelengths of 184.9 nm and 254 n, which can be achieved by circumscribing an ultraviolet lamp in a convenient quartz lens, as will be described later. Table 2 lists the relative percentages of the various oxidants and other constituents that are considered in the activated air. The percentages given indicate the relative amounts in approximately 20% of the activated air that includes oxygen and oxygen-containing compounds. TABLE 2 Percent by volume of Constituent Air Excluding Nitrogen Nitrogen Dioxide (NO-,) >0.1% Atomic Oxygen (0X) > 4.4% Hydrogen Peroxide (H202) > 12.6% Radical Hydroperoxy (H02) > 29.4% Radical Hydroxy (HO) > 6.0% Oxygen (02) > 45.5% TABLE 2 (Continued) Percent by volume of Constituent Air Excluding Nitrogen Other Oxidants such as N02, N20 > 1.0% Other gases such as NH2, NH3, C2, N2, HCN, Cl > 1.0% As indicated in Table 2 above, even when the ultraviolet light includes wavelength 184.9 n which is known to cause ozone formation (03) in air, there is no ozone present in the resulting active air that is produced by the generator. This is considered to result from the presence of moisture in the supply air that provides a hydrogen-rich environment, which allows any ozone to almost immediately separate and form hydroxyl radicals. This is also considered to result from the photolysis of ozone caused by ultraviolet light of 254 nm. When active air is generated by exposure to ultraviolet radiation in the presence of a catalyst, such as polyvinyl chloride, it is considered that the following additional radicals are produced: TABLE 3 Radicals C2C1"Cl" Cl2 C10H "H203C1" H2C1"HOC1" These radicals also help to separate the ozone, releasing oxygen that can be combined with available hydrogen to form the highly active hydroxyl radicals. Without wishing to be limited by some theoretical explanation, it is considered that, by separating the ozone almost as soon as it is generated, the oxygen of the ozone is available to form hydroxyl radicals that have a higher oxidation potential and therefore are more effective than ozone to destroy the VOC In this way, the activity level of the activated air can be improved. In addition, the produced oxidants are negatively charged and this is considered to result in improved degradation of V.O.C. Preferably, the relative humidity of the plant or other fresh air used to generate activated air is at least 25% and more preferably is within the range of 75-100% and even more preferably in the range of 90-100%.

The activated air is then dissolved as best as possible in an aqueous solution in the spray tank yard 44. The resulting activated aqueous solution is then introduced into the tunnel 14 as an active mist, which is mixed with the air stream charged with V.O.C. 12 which passes through tunnel 14. The air stream is maintained at a high level of activity by direct ultraviolet radiation in the high humidity environment. The photo-decomposition is initiated by breaking the V.O.C. and oxidative degradation begins at least in the first Cl chamber. As the air stream moves through the tunnel, breaking down the compounds and continuing the oxidative destruction at an accelerated rate as the reaction products in the solution are filtered and precipitated from the air stream and return to supply tank 60. As indicated above, the destruction of the V.O.C. according to the present invention it is considered that it occurs by a combination of two phenomena, ie oxidative degradation of V.O.C. by oxidants contained in the activated air in the gaseous and fog states, and by photolysis that occurs simultaneously and undoubtedly synergistically in the tunnel 14 which, due to repeated exposure of the air stream charged with V.O.C. to ultraviolet radiation in a high humidity environment. Consequently, the tunnel 14 will be useful in and of itself to provide abatement of the V.O.C. acceptable without further treatment in carbon beds 32, 34.

Tunnel Chambers In general, tunnel 14 incorporates particle filtration, fogging or mist formation, ultraviolet light activation, purifier, carbon filters for surface reactions and preferably one or more catalysts. One or more of these functions is incorporated in each of the modular sections Sl to S15. In addition, these functions are carried out in a predetermined sequence, such that the processes and reactions that occur in cameras Cl to C15, individually and in sequence, optimize the destruction of V.O.C. occurring in tunnel 14. As illustrated in Figure 2, modular sections Sl to S15 in tunnel 14 are as follows: Section Sl: fog nozzles, mixing cones and ultraviolet lamps. Section S2: Ultraviolet lamps and fog nozzles. Section S3: Ultraviolet lamps and fog nozzles. Section S4: Viledon filters and ultraviolet lamps. Section S5: Carbon filters, ultraviolet lamps and fog nozzles. Section S6: Ultraviolet lamps and fog nozzles. Section S7: Perforated catalyst plates, ultraviolet lamps and fog nozzles. Section S8: Perforated catalyst plates, ultraviolet lamps and fog nozzles.

Section S9: Viledon filters and ultraviolet lamps. SIO Section: Carbon filters, ultraviolet lamps and fog nozzles. Section Sil: Ultraviolet lamps and fog nozzles. Section S12: Ultraviolet lamps and fog nozzles. Section S13: Perforated catalyst plates, UV lamps and fog nozzles. Section S14: Double Viledon filters and ultraviolet lamps. Section S15: Carbon filters and ultraviolet lamps. The illustrated mode is based on an airflow flow rate of 10,620 to 16,992 lt / sec (22,500 to 36,000 ACFM), to an average over-spray of 9,988 kg (22 pounds) per hour to reduce V.O.C. from more than 100 ppm to no more than 12 ppm per volume, which is less than half of current 25 ppm EPA standards. This system is manufactured in modular sections in such a way that it can easily be adjusted to any flow or volume expense of V.O.C. For example, for smaller flows (10,620 to 16,992 lt / sec (22,500 ACFM to 36,000 ACFM)), a single generator 40, tank yard 44 and tunnel 14 can be used. For larger flows (23,600 lt / sec (50,000) ACFM)), a pair of tunnels 14 can be connected in parallel and run from a single generator 40 and tank yard 44. For very large flows (33,984 lt / sec (72,000) ACFM)), a pair of tunnels can be used with a pair of generators 40 that supply activated air to the tank yard 44 at the required speed, to provide a convenient level of activated air within the water that is provided to the two tunnels. For a capacity of (16,992 lt / sec (36,000) ACFM)), tunnel 14 is 3.66 m (12 ft) wide, 3.66 m (12 ft) high and 17.07 m (56 ft) long, preferably constituted in two modular sections, each 8.53 (28 feet) long. The walls and ceiling are made of stainless steel, with airtight welding. The inlet sections are manufactured separately to house the filters 66, activated air nozzles 68, mist nozzles 56 and expansion chamber 76. In the embodiment described, the inlet 16 is designed such that the cross sectional velocity is not exceeds 137.16 m / min (450 feet per minute) and three separate filter sections are used to progressively separate particulate paint filtrate, for example the average efficiency of the first filter is seventy-two percent (72%) in paint particles of size 4 microns and larger, the second filter has an average efficiency of eighty-five percent (85%) in paint particles with a size of 2 microns and larger, and the third filter has an average efficiency no greater than ninety and six percent (96%) in paint particles of size 1 and larger. All the filters were made of synthetic organic fibers to operate at a relative humidity of one hundred percent (100%) without deterioration or detachment of the fibers. Filters can be constructed of sections, approximately .61 x .61 (two by two feet) with 5.08 to 10.16 cm (two to four inches) deep to fill the cross section of the tunnel, for example six filters across a width of 3.66 m (12 feet) and six high filters for a height of 3.66 (12 feet). Suitable filters are available from Eaton Air Filter of 2338 Cole Street, Birmingham, Michigan 48009. Similar filter sections are typically employed in coal bed systems of the prior art with incineration. The set of activated air nozzles 68 consists of forty-eight nozzles capable of delivering up to approximately 4,248 m3 / min (150 cubic feet per minute) of air from the tank yard 44, bypass 74 and / or generator 28 by the bypass 72 An electronically controlled, normally open valve 78 is used to control the air flow to the nozzles 68. The nebulizer nozzle assembly 56 at the inlet 16 is designed to instantaneously achieve high humidity in the expansion chamber 76, for example at use 192 fogging nozzles such as stainless steel nozzles, with ruby hole to produce a mist, ASI # 006 at 60.65 1 / min (0.033 gallons per minute) at 703 kg / cm2 (1,000 psi). The expansion chamber 76 can be approximately .61 (approximately two feet) long, to allow the air stream 12 to compensate and charge the system to a uniform air flow.

In each of the modular sections Sl to S15, the lamp portion of the modular section includes a set of 16 ultraviolet lamps 80, one of which is illustrated in Figure 2A. Each of the lamps includes a SOa lamp tube made from quartz LH with high ozone output, which allows radiation transmission in the wavelength range from 184.9 to 254 nanometers. Lamps of this type are available from Voltrac Technologies, 186 Lin ood Avenue, Fairfield, Connecticut 06420-0688. The lamps are 1.22 m (four feet) long and are mounted in a two-section frame, each frame section supports eight lamps that extend in a vertical direction. Alternatively, the lamps 80 may be mounted so as to extend in the horizontal direction, with access openings in the tunnel sides 14 to allow the lamps to be changed from the outside of the tunnel 14 without having to interrupt operation of the system 6. Each lamp 80 also has an upstream shield or shield 82, which is cut from 7.62 cm (3 inches) PVC pipe, leaving a radiant section of 240"intact and a 120" window through from which radiation is emitted to the downstream chamber. The PVC deflector operates as a catalyst, providing the various radicals listed previously in Table 3 that aid in the destruction of V.O.C. within the air stream 12. Preferably, the PVC employed is caliber 80, which will provide the desired radicals, however it is dense and will not break too fast. Section Sl includes a set of mixing cones 70, comprising 180 relatively small double cone venturis, to optimize the mixing of the air stream charged with V.O.C. 12 with the aqueous mist of the nozzles 56 and gaseous activated air from the nozzles, 68. These cones homogenize the air stream charged with V.O.C. with activated haze and activated air from nozzles 56 and 68 respectively, to form a homogeneous mixture. The nozzle portion of sections S1-S3, S5-S8 and S10-S13 each includes thirty-five nozzles directed downstream and mounted in seven vertical heads with five nozzles per head. The seven vertical heads are staggered between the eight vertical lamps, in the space between the lamp shields. As the air stream moves through the tunnel 14, it is deflected around the lamps and into the mist leaving the nozzles. The nozzles section is made of stainless steel mounted on stainless steel columns. Again, the mist nozzles are 'stainless steel with a ruby hole to produce a mist, ASI # 006 at 60.65 l / min. (0.033 gallons per minute) to 703 kg / cm2 (1,000 psi). In the filter sections and lamps S4, S9 and S14, the filter can be constituted by 25 sections with approximately 60.96 x 60.96 x 2.54 cm (24 inches x 24 inches x 1 inch) thickness, mounted on stainless steel frames and backed in both sides by stainless steel wire mesh. A suitable filter material is Viledon, which is sold commercially by Eaton Air Filter of Birmingham, Michigan. Preferably, Viledon filters remove water in particles and other particles at least five microns in size and even more preferably at about one micron in size. The ultraviolet lamp portions of these sections may be identical to the previously described set of lamps, and may be located immediately downstream of the filters. In each modular section S5, SIO and S15, twenty-five coconut charcoal filters with approximately 60.96 x 60.96 x 4.763 cm (24 x 24 x 1-7 / 8 inches) thick, are installed in a stainless steel frame in such a way that all the air moving through the tunnel 14 must pass through the carbon filters. Preferably, the filters have interior transverse reinforcements and are backed on the downstream side by a perforated steel plate that holds the coconut charcoal filters and ensures that all air moving in the tunnel 14 passes through the filters of coal. In the modular sections S5 and S10, the portion of ultraviolet lamps and the mist nozzle portions, are immediately downstream of the carbon filters and have the construction previously described. . r Perforated catalyst plate portions of sections S7, S8 and S13 each are fabricated from six standard ferrous punch plates, each approximately 1.22 x 1.83 m (4 x 6 ft), 16 gauge, punched with holes of .635 cm (1/4 inch), offset to .635 cm (1/4 inch) and mounted on a frame to fill the tunnel. The perforated plates are heavily coated with a high displacement hydrogen catalyst, for example titanium dioxide applied with an ultraviolet resistant adhesive. Other catalysts may be employed, including a titanium-ferrous catalyst mixture, a copper-zinc catalyst mixture, a catalytic copper-silver mixture and a zinc-silver copper catalyst mixture. The lamp and nozzle portions of sections S7, S8 and S13 are of the same construction as previously established and are located just downstream of the perforated catalyst plates. Preferably, only the surfaces upstream of the plates are coated with the catalyst, leaving the ferrous material on the inner surface of the perforations and the back side of the exposed plates. By providing an exposed ferrous surface, ultraviolet light and peroxide radicals can react with the iron in the plates to release the hydrogen required to produce the highly active hydroxyl radicals.

With the tunnel assembly 14 described previously, as soon as the air stream charged with V.O.C »12 between the tunnel 14, wetting the V.O.C. and oxidants and some oxidative degradation start immediately on the air stream 12 by mixing with the activated air from the nozzles 68 and the activated mist from the nozzles 56. This step can be seen as a pre-treatment for further oxidative degradation and photolysis at tunnel 14 and may not be required for some applications. In the illustrated embodiment, this initial stage provides a preferred convenient location for recirculating some of the active solution in the supply tank 60, in a closed loop through the spray tank yard 44 and the tunnel 14. Similarly, the inlet 16 of tunnel 14 provides a preferred location for introducing ventilated activated air from the tank yard 44 and also for continuously recirculating partially depleted activated air which is discharged from the coal bed system 24. As the air stream advances through the chambers Cl to C15, is treated progressively and continuously by direct exposure to ultraviolet light and mist loaded with oxidants. The ultraviolet radiation in the Cl chamber not only continues to activate the mist by regenerating oxidants but also begins the photolysis of the V.O.C., at least initiating the humidification, rupture and photodecomposition of the V.O.C. The simultaneous oxidative decomposition of V.O.C. occurs due to the high level of oxidants in the activated mist. Greater oxidative degradation and photolysis occur as air stream 12 passes through chambers C2 and C3. As the current passes the chamber C3 and through the Viledon filters in section S4, the filters remove particulate water, together with water-soluble intermediate radicals, compounds and the like, and the filtrate is collected in the supply tank. Viledon filters only let moisture pass, VOC gaseous and air activated in gaseous form to pass to chamber C5 where the air stream is again irradiated by ultraviolet radiation even in a high humidity environment but without dense activated haze. This is considered to improve more direct irradiation of V.O.C. due to the dispersion and reduced absorption of the radiation, compared to a dense haze environment. However, the humidity in the C5 chamber is sufficiently high (95-100% relative humidity) to cause formation of the new hydroxyl radicals from any ozone generated there by the ultraviolet lamps. Furthermore, it is considered that the oxidants are continuously deposited on the carbon filter surfaces in Section S5 at the downstream end of the C4 chamber for surface reaction with V.O.C. photodecomposed. To some degree, these surface reactions can be influenced by ultraviolet radiation reaching the carbon filters.

In chambers C5 and C6, the air stream again moves through a dense, high humidity environment with prolonged activation by ultraviolet radiation. This causes greater oxidant generation and oxidative and photochemical decomposition of V.O.C. As the airstream reaches section S7 at the downstream end of chamber C6, the catalytic plates serve as scavengers for forcing activated haze, oxidants and V.O.C., in intimate contact with each other. The activated mist is also condensed in the catalytic plates to remove water-soluble compounds, intermediate radicals and the like. The reactions that occur have been found to be improved by the presence of the catalysts. It is considered that the catalysts cause a high displacement of hydrogen that promotes rupture of V.O.C. , oxidative degradation and / or generation of oxidants. The cameras C7 and C8 are also highly active due to ultraviolet radiation combined with additional infusions of activated mist. The rupture, photochemical and oxidative wetting and decomposition continue, probably at an accelerated rate, before being filtered in section S9. In chamber C9, as in chamber C4, the air stream enters a condition of high humidity but no active dense fog. As in the C4 chamber, the ultraviolet irradiation of the V.O.C. It is more direct and efficient. Fresh oxidants are produced, photochemical and oxidative decomposition continues, but ozone production is still inhibited. The carbon filters at the upstream end of the SIO section perform as in section S5, followed by a high level of activity in the C10-C12 chambers, as in the C5 and C6 chambers, due to activated dense fog replenished and repeated ultraviolet radiation. As levels of V.O.C. concentration continue to decline, photochemical and oxidative decomposition are undoubtedly more effective and efficient as V.O.C. They migrate through the activated mist and are exposed to ultraviolet radiation and oxidants in the C10-C12 chambers. In section 13, as in section S7, the air stream, oxidants and mists are purified and coalesced in the presence of a catalyst with perforated catalyst plates with any condensation flowing into tank 60. Prolonged exposure to ultraviolet radiation and haze dense active is repeated in the C13 camera, as in the C8 camera, progressively achieving even more VOC destruction photochemical and oxidative, before filtering in section S14. In section S14, particulate water is removed by Viledon filters, together with water-soluble reaction radicals, like compounds. In chamber C14, as in cameras C4 and C9, the air stream is exposed to ultraviolet radiation, in a high humidity environment, but without dense fog before passing through the carbon filter in section S15. The chamber 14 therefore provides a direct and efficient irradiation of the V.O.C. remaining, not only in the air stream but also on the surface of the carbon filters in section S15. The reactivation of the air current in cameras C14 and C15 by ultraviolet radiation continues the destruction of V.O.C. and provides additional oxidants that aid in any oxidative destruction of V.O.C. additional required in the coal bed system 24. As will be apparent from the above process description, repeated ultraviolet radiation of the air stream charged with V.O.C. 12 occurs in a high humidity environment, either as a dense fog, as in chambers C1-C3, C5-C8 and C10-C13, or as gaseous moisture such as in chambers C4, C9, C14 and C15. This ensures a continuous replenishment of oxidants for reaction with V.O.C. photochemically decomposed. Additionally, sustainable ozone formation, as would be expected with air except, does not occur in the high humidity environment that is maintained through tunnel 14. Experimental analysis has not revealed any detectable ozone leaving tunnel 14. The analysis confirms that the gas that leaves the camera C15 does not contain ozone. It is considered that any ozone produced is rapidly decomposed by one or more of a variety of phenomena, including the presence of high humidity, photolysis by ultraviolet radiation at 254 nm, and rupture due to chlorine and other radicals that are released by catalysts as result of exposure to ultraviolet light.

It has been determined empirically that the present invention effectively and efficiently destroys the V.O.C. at levels well below the standards currently accepted as indicated in Table 4. TABLE 4 REDUCTION INPUT 1 BEFORE BED BED OUT OF SYSTEM. OF CARBON1 CARBON2 DA1 §No tunnel 14 56 ppm 56 ppm 50, 000 ppm3 14 ppm MAK (2: 1) 25,000 ppm3 Xylene With tunnel 14 56 ppm 30 ppm 0. 180 ppm3 0.688 ppm MAK (2: 1) 0. 170 ppm3 Xylene 1 Measured by Photorae ionization instrument averaged over a 33-hour run. Measured by an independent laboratory, Swanson Environmental Inc. 3 Samples were removed after 8 hours of V.O.C. before regeneration. The quantities therefore represent the residual amount remaining in coal before the regeneration process. Although the present invention preferably uses additional oxidative degradation in the coal bed system 24, it will be apparent from Table 4 that the treatment in tunnel 14 only results in a reduction from 56 parts per million to 30 parts per million that even without subsequent treatment in the coal bed system 24, it may be more suitable to comply with the applicable standards. Liquid System Now with reference to Figure 3, fresh water, preferably filtered filtered water, is supplied to tank 60 through a solenoid valve 102 and inlet pipe 104. Valve 102 is opened and closed by a level control of convenient liquid, including a liquid level detector operated by float 106, to initially fill the tank 60 and maintain a liquid level between an upper limit 108 and a lower limit 110. The upper limit 108 is established by an outlet pipe of spill 107 which is also connected to a normally closed solenoid valve 109, such that tank 60 can be discharged. Fresh water can also be supplied to tank 60 by a manual valve 112. Tank liquid 60 is supplied to four low pressure sprinkler tanks 114, 116, 118 and 120 in the tank yard 44 via pipe 122, pump 62, valves normally open solenoid 126, 128, a low pressure filter 130, normally open solenoid valve 132 and pipes 64 discharging liquid in the upper portion of the tank 114. The filter 130 can be bypassed by a normally closed solenoid valve 138 and discharged to the supply 60 by a normally closed solenoid valve 140. Tank 114 can also be supplied directly with fresh running water by a normally closed valve 141 to discharge the system. The liquid pumped to tank 114 is transferred by gravity to tank 116 through line 142, from tank 116 to tank 118 through spill line 144, and tank 118 to tank 120 through line 146. Pump 62 is a pump high capacity, low pressure. The spill from the tank 120 is returned to the tank 60 by the spill pipe 152 and a normally open solenoid valve 154. Each spray tank 114-120 has a sight glass 156, such that an operator can visually verify the liquid level at each one of the tanks. The spray tanks 114-120 can be discharged into the tank 60 through the discharge pipe 189 and the normally closed valves 190, 192, when it is desired to purge or flush the system. Tank liquid 120 is supplied with nozzle assembly 56 and nozzle head 50 through line 172, filter 176, pump 182, and normally open valves 170, 174, 178, 180, 184, 48 and 52. The filter 176 can be bypassed by a normally closed valve 186 and discharged to tank 60 by the normally closed valve 188. Preferably, the filter 176 traps particles greater than 1 miera to ensure that the particles do not enter the tunnel 14 and prevent clogging of the nozzles. The head 50 feeds nozzles N1-N3, N5-N8 and N10-N13, in corresponding modular sections S1-S3, S5-S8 and S10-S13, as previously described in connection with Figures 1 and 2, to maintain a high humidity environment through the tunnel 14. As was generally described in connection With the total system of Figure 1, the liquid supplied to the nozzle head 50 and nozzle assembly 56 is an aqueous solution containing dispersed bubbles of activated air charged with oxidants from the generator 40. As illustrated in greater detail in the Figure 3, the compressed air is supplied to the generator 40 from a fresh plant air source 194, through a filter and purifier 196, a compressor 198, a variable Venturi flow regulator 200 and a normally open solenoid valve 202. The filter 196 is used to remove particulate moisture and oil to sizes of 0.01 miera. Air entering the generator 40 passes in series through a series of individually activated air cells 210 (Figures 3, 5 and 6) where it is exposed to ultraviolet radiation to generate the various oxidants. Activated air from the generator 40 is then supplied by the header pipe 42 to each of the spray tanks 114-120 by an associated variable flow regulator 212. The regulators 212 control the activated air entering each tank and balance the distribution to all tanks Since tanks 114-120 are similar in construction, only tank 116 will be described in detail. Compressed activated air, at a relatively low volume and low pressure, enters the lower portion of the tank 116 through an inlet tube 214 and a piece with radial arms of the spray pipes 216. The spray pipes 216 cause the activated air to disperse in small bubbles and agitate the liquid in the tank 116. As illustrated by dotted lines in Figure 3 and in cross-section in Figure 4, four UV lamps 213 are mounted on the top of the tank 116 and extend down through of a main portion of the tank, ending just above the piece with radial arms of spray pipes 216. The lamps 218 also consist of an ultraviolet lamp tube, protected from tank liquid 116 by a separate quartz lens tube 217 and can eer identical to the lamps 80 used in the tunnel 14. Each of the quartz lens tubes 217 is preferably made from the same material LH of high performance ozone used to produce the lamps 218. For purposes of simplification, a power source 219 is illustrated with connections to only two of the lamps 218 in each of the tanks 114, 116, it being understood that the source 219 is connected to all the lamps in all the tanks. As the activated air in the radially spaced part of spray tubes 216 bubbles somewhat violently and migrates upwardly through the tank 116, the activated air bubbles are exposed to more ultraviolet radiation to generate and reactivate oxidants. The generation and reactivation of oxidants not only occurs as activated fresh air is introduced into each tank, but also as activated liquid moves progressively through the tanks. Additionally, ultraviolet radiation from the aqueous solution in tanks 114-120 is also considered to contribute to the total destruction of V.O.C. by promoting greater intermediate and radical reactions that occur after photochemical degradation of V.O.C. in tunnel 14. As mentioned above, relatively large amounts of water are required to maintain high humidity in tunnel 14. In the illustrated embodiment, tank 60 contains 3890.98 liters (1,028 gallons) with pump 62 that provides 227.1 liters (60 gallons) per minute at low pressure and pump 182 delivers 48.07 liters (12.7 gallons) per minute at 703 kg / cm2 (1,000 psi). To supply approximately 48.07 liters (12.7 gallons) per minute to pump 182, tanks 114-120 can have capacities of approximately 427.7-757 liters (113-200 gallons) per tank with compressed activated generator air 40 that is introduced into each tank at a rate of .708 It / sec (1.5 cubic feet per minute) at .703 to 1.05 kg / cm2 (ten to fifteen psi) per minute. Progressive circulation through the tanks 114-120 as described herein, ensures an adequate supply of liquid charged with freshly activated oxidant which is required to keep the dense activated air mist and high humidity in the tunnel 14. Most of the The pipe in the low pressure portions of the system of Figure 3 is made of PVC, which is considered to provide one. catalytic action for reactions occurring in the liquid as the liquid recirculates tank 60 through tank yard 44, resides in tunnel 14 as a mist, and then rushes back to tank 60. As illustrated in Figures 1 and 3, activated air that is collected at the top of each of the spray tanks 114-120, is vented to a line 79 that supplies the activated air to the air nozzles 68 together with regenerated discharge air that is supplied from the coal bed system by a branch 74. Preferably, approximately 47.2 to 56.64 lt / sec (100-120 cubic feet per minute) is supplied to the nozzles 68, with the tanks 114-120 supplying approximately 5.7 to 7.55 lt / sec (12-16 cubic feet per minute) at .703 kg / cm2 (10 psi) and approximately 42.5 to 47.2 lt / sec (90-100 ACFM) through branch 74. Activated Air Generating Cells With reference to Figures 5 and 6 are illustrated with greater detail one of the generating cells 210 in generator 40. Each cell includes an ultraviolet lamp 220, which may be the same as lamps 80 in tunnel 14 and lamps 218 in tank yard 44. Each lamp 220 is generally concentrically retained in a tubular outer shell 221 of its associated cell 210. Compressed air from the generator 40 enters the cell 210 through an inlet fitting 226 in an end cap 222 and is discharged from the cell 210 through an outlet fitting 228 in an end cap 224. The lamp 220 is transported in a sub-assembly 230, slidably received in the enclosure 221 and comprising a plurality of baffle plates 232 that provide a serpentine flow path that introduces turbulence to the air stream. which flows through the cell 210. The baffles 232 are mounted on three rods 234 that are spaced apart and extend axially within the enclosure 221 relative to the lamp 220. Each baffle 232, in general, is a circular disk having a flat edge in section 236 and the baffles are mounted on rods 234 with alternating planes 236 facing in opposite directions to provide the serpentine flow path. All deflectors 232, except an end deflector 232 ', have a central spacing hole 238 through which lamp 220 is received, with one end of lamp 220 being received in and held by a plug 240 in the deflector of end 232 '. The lamp 220 is energized at its other end by the terminals 242, 244, cables 246, 248 and plug 250. The enclosure 221 has an axial-to-inner diameter ratio, from 1 to 8 and 1 to 16, and preferably about 1 to 12. To ensure turbulent flow, preferably the baffles 232 are equidistant and the distance between half and one times the inside diameter of the enclosure 221. Preferably, the area of the cutting fins 236 is not greater than about 10% of the baffle plate area to improve turbulent flow and to provide a debugging action. Preferably the enclosure 221, the end caps 222, 224, the baffles 232 and the retainer rods 234 are made of PVC for the reasons stated above to resist oxidation and are also considered to serve as a catalyst. With this construction, the deflectors 232 are cemented to the rods 234 and the sub-assembly 230 adheres to the enclosure 221 with PVC cement. In a practical construction of the generator cell 210, enclosure 221 is made from commercially available PVC pipe having a nominal outside diameter of 15.24 cm (six inches) and with end caps 222, 224 a total length of approximately 1,676 m (5-1 / 2 feet) ). The sub-assembly of baffles is also made of PVC, has 14 baffles that have an approximate diameter of 15.24 cm (six inches) and a thickness of .1875 cm (3/16 inch). Approximately .95 cm (3/8 inch) are removed to form fins 236. A convenient ultraviolet lamp tube having a total length of about 155 cm (61 inches) is commercially available from Voltarc Technologies of Fairfield, Connecticut. A regenerator 40 of twelve of these cells connected in series has an output of approximately 19.82 lt / sec (42 standard cubic feet per minute) when operated with a compressed inlet air pressure of approximately 1,406 kg / cm2 (20 psi). The activated air produced by this generator is considered to typically have the same oxidants as other radicals in the proportions stated in Tables 2 and 3. Bacterial maintenance is not required due to biological treatment by ultraviolet radiation by lamps 220 in the cells 221, lamps 218 in the tank yard 44 and the various ultraviolet lamps in chamber 14. Coal Bed Regeneration In previous applications using carbon beds for VOC abatement, when air of low concentration, high volume, is passed through of the coal bed, the VOCs They are absorbed in the bed. The bed is subsequently desorbed by steam, etc., resulting in an effluent with higher concentration, of smaller volume, which then must be further processed by incineration or some other solvent removal techniques. For some previous applications, carbon bed desorption must be done off-site and other previous applications require off-site disposal of waste products. Still further, when using the method and apparatus of the present invention, coal beds may not require all applications where the treatment in tunnel 14 has reduced V.O.C. enough to comply with the applicable standards. When the carbon beds 32, 34 are used in accordance with the present invention, they can be constructed in a manner similar to that of the carbon beds of the prior art. However, the use and function of the carbon beds according to the preferred embodiment of the present invention differ significantly from the carbon beds of the prior art used only as an absorber. Again with reference to Figure 1, it will be recalled that in the preferred embodiment, the air vapor exiting the tunnel 14 has just been reactivated with ultraviolet radiation in the chambers C14 and C15 and filtered by carbon filters in the modular section. The air vapor entering the expansion chamber 22 is still highly active with oxidants, together with some VOCs and more likely, intermediate compounds resulting from oxidative and photochemical degradation in the tunnel 14. Continuous oxidation activity at a high level can be maintained by using additional ultraviolet lamps in the expansion chamber 22. Preferably, two coal beds 32, 34 of modular construction and off-site assemblies are used. During final site assembly, the beds 32, 34 are circumscribed by a convenient external housing, generally designated 266 and insulated from each other by an internal gap 267. An inlet chamber 268 for the bed 32 is connected to the expansion chamber 22 by an inlet duct 270 and an inlet damper 272. The bed dump 32 to the discharge chimney 26 is through an outlet duct 274 and the outlet damper 276. Similarly, an inlet chamber 277 for bed 34 is connected to the expansion chamber 22 via a duct 280 and damper 282 and the bed 34 is discharged to the chimney 26 through an outlet duct 284 and an outlet damper 286. The bed 32 is brought in line upon opening the shock absorbers 272, 276 and closing the dampers 282, 286 and the bed 34 is carried in line when opening the dampers 282, 286 and closing the dampers 272, 276. Each of the carbon beds 32 and 34 includes a respective template 290 and 292 located just upstream of the buffers 276 and 286, respectively. Each of the templates 290 and 292 provide a restriction in the flow path that results in a back pressure within its associated carbon bed. This back pressure compensates for the flow through the carbon filters to help maximize the effectiveness of the carbon beds. Each of these templates can be implemented, using a pair of perforated plates with the degree of alignment and perforations that are varied as necessary to obtain the desired back pressure. Also with reference to the schematic of Figure 7, the blower 30 removes fresh plant air 300 through a filter 302 and the generator 28 through a five-door manifold 304. Each manifold door 304 feeds a respective row of seven series-connected activated air cells 306 whose discharge streams flow through respective solenoid-operated valves 308 to a five-port discharge manifold 310 and then through line 312 to the inlet of the plenum blower 30. The blower impeller 30 supplies compressed air at approximately 141.6 lt / sec (300 ACFM) to activate air bypass 72 through supply line 314 and solenoid valve 316; to the perforated tube assemblies 320, 321 in the coal bed 34 by pipe 314 and respective solenoid valves 318, 319; and the perforated tube assemblies 326, 328 in the carbon bed 32 through the pipe 314 and respective solenoid valves 322, 324. Preferably, each of the perforated tube assemblies 320, 321, 326 and 328 have multiple rows of perforated outlet tubes, for example arranged in a vertical assembly of three tubes 330, 332, 334 as illustrated in Figure 8, for assembly 328. This assembly uniformly dispersed activated air in the carbon beds during regeneration. In the exemplary embodiment described, each carbon bed 32, 34 can be fabricated into two modular sections each with approximately 9.14 m long x 3.05 wide x 3.05 m high (30 feet long x 10 feet wide x 10 feet wide). high) and finally join in end-to-end site in a unit of 18.29 m (60 feet). The carbon bed base material can be 14.15 m3 (500 cubic feet) of activated carbon shell with natural grain coconut.

As discussed above in connection with the generator 40, the generation of activated air is preferably carried out using humid air. This moisture can be added to the fresh plant air 300 used by the generator 26. Optionally, the clean process air leaving the coal bed system 24 can be used in the plant 300 air place and therefore can be carried directly from the chimney 26 by an e-line 336 illustrated in Figure 1. This clean process air is well filtered and amounts to a moisture level of approximately 95% after only three minutes of operation of the chilling system 10. In this way, the clean process air does not require added or filtered moisture and the filter 302 can therefore be removed. As illustrated in Figures 1 and 7, coal bed regeneration discharge gases 34 are supplied to supply branch 74 through a pair of solenoid valves 340, 342, discharge head 344, pipe 346 and valves of solenoids 348, 350. The regeneration discharge gases of the bed 32 are similarly supplied to the bypass 74 through a pair of solenoid valves 352, 354, manifold 344, line 346 and solenoid valves 348. 350. The manifold of discharge 344 can also be directly connected to chimney 26 through pipe 346, valve 348 and solenoid valve 356, for applications where the regeneration discharge is clean enough to discharge directly into the environment. Advantageously, the activated air that is supplied to the coal beds 32, 34 during regeneration not only desorbs the coal beds but also deposits oxidizers on the surfaces of the coal bed for further destruction of V.O.C. by surface reactions when the regenerated charcoal bed is carried in line. Consequently, it is also desirable to recirculate the regenerative discharge gas from the coal beds 32, 34 through the branch 74 and back to the tunnel 14, to promote the continuous intermediate reactions and destroy any V.O.C. remaining and decomposition products of V.O.C. The cells 306 in the generator 28 can be constructed substantially as described in connection with the cells 210 in the regenerator 40. The cells 306 are connected in series in six respective rows so that the numbers of the cells in line can be chosen by the valves 308 in accordance with the demands of the system to regenerate either cell 32 or 34 and also supply air activated by gate 28 to activate air nozzles 68 in tunnel 14. Pumped blower 30 has a variable speed control (vfd) 370, in such a way that the outlet of the blower 30 can be varied according to the demands of the system. Photochemical and Oxidation Reactions and Results Based on the abatement system test 10, it has been shown that the present invention effectively destroys V.O.C. of the type found in an automotive paint spray booth discharge system. Much of this testing is reviewed to simulate a percentage ratio based on a commercial unit that can handle 33,984 (72,000 cfm) to 20.43 kg (45 lbs.) Of V.O.C. per hour. In order to obtain representative results for paint spray solvents, the results shown in Table 4 are for a ratio of two parts of methylamyl ketone (MA-K) to one part of Xylene. Although the trajectories of oxidative degradation and destruction of V.O.C. they have not yet been fully elucidated, the various reactions occurring for these solvents are known and the results between Table 4 show that the present invention can successfully reduce or destroy V.O.C. As an example of VOC degradation, the following reactions show reduction of methane (CH ,,) by hydroxyl (HOJ) As illustrated, this is accomplished by replacement of each hydrogen atom.The first stage is the formation of methyl alcohol ( CH3OH or H'CH20H), followed by formation of formaldehyde (HC2 (0H) 2) that by loss of water gives CH20 or H'CHO and finally the formation of formic acid (CH (? H) 3) that by loss of water gives CHO (OH) 2, HO'COOH or H2C03, CH4 + HO-? C? H3 + H20 C'H3 + HO- - >; CH30H CH30H t- HO-? C * H20 (0H) + H20 C * H20 (GHj f HO- -> C'H2 (0H) 2 i H20 C'H2 (0H) 2 + HO- - * CH402 4 H20 CH402 + HO- -r * CH20 t H20 CH20 + HO-? C * HO + H20 C'HO 1- HO-> H2C02 H2C02 + HO-? HC 02 + H20 HC ~ 02 + HO-? H2C03 H2C03 4 HO- ** H20 4 CG2 There will be it should be noted that the above reactions are representative of hydroxyl intrusion alone and that they do not consider any reactions or improvements of reactions that may occur due to intrusion of ultraviolet light, other radicals - and oxidants in the activated air, as well as photon / electron transfer A similar process of chemical reduction to water and carbon dioxide is considered and expected to occur with similar compounds, such as N-butyl alcohol, aromatic hydrocarbons, mineral spirits, 1,1,1-trichlorethylene, BTX in slight ppm, methanol.; MEK; V, M and P, Naphtha; N-butanol; perchlorethylene and butyl ether As previously indicated, the destruction of VOC in water and carbon dioxide is strongly considered. not innocuous, is achieved by the combination of doe phenomena that undoubtedly produce a synergistic effect. First, ultraviolet radiation produces highly active oxidants that then subsequently degrade oxidatively to V.O.C. The oxidants are generated not only in the active air from generators 28, 40 but are reactivated, regenerated and generated again by ultraviolet radiation in a courtyard of spray tanks 44 and within the numerous chambers in tunnel 14 that have lamps ultraviolet. The generation of the activated air is carried out in a high humidity environment and using ultraviolet wavelengths of 184.9 nm, to produce ozone and 254 nm to help quickly break down the ozone in such a way that the oxygen released can form highly hydroxyl groups assets. The generation of activated air is also carried out in the presence of a catalyst to help release hydrogen for hydroxyl radical production. The oxidants in the activated air of the generator 28 are deposited on surfaces in carbon beds 32, 34 during carbon bed regeneration and for surface reaction with V.O.C. when the coal beds are carried online in the process. These surface reactions can be improved by additional ultraviolet radiation in the expansion chamber 22, just before any V.O.C. remaining in the air stream are passed through the carbon beds 32, 34. In second, direct ultraviolet photolysis of the V.O.C. causes a chemical decomposition of the V.O.C., with the resulting products that interact with the oxidants and chemical intermediaries that are constantly generated, reactivated and reacted through the system. It will also be apparent that ultraviolet radiation for photodecomposition and for oxidant generation is carried out under a variety of conditions. In tunnel 14, ultraviolet radiation occurs in the various chambers with strong haze and also chambers where after water is filtered into particles, only highly gaseous moisture is present in the chambers just before the carbon filters. Residence time varies in different chambers. Ultraviolet radiation directly affects the catalyst plates and other components of PVC and carbon filters where surface reaction may occur. Strong homogenous mixing occurs in the cones assembly 70 and strong debugging occurs in the perforated catalyst plates. Variable degrees of turbulence also exist in tunnel 14 due to different filter assemblies and particularly to perforated catalyst plates, as well as the effect of nozzle sprays and deflection around lamp guards. Experimentation has shown that the production of oxidants as well as the destruction of V.O.C. it is improved by the catalytic action that is provided, in the example previously described, by the PVC. In addition to lamp guards and catalytic plates, various other internal supports that are exposed to the ultraviolet lamps inside the tunnel 14, can be made from catalytic materials. For example, PVC pipe can be used in the frame structure that holds the UV lamps and can be used to drive the activated air and the aqueous solution loaded with oxidants created in the tank yard 44. Due to the high level of oxidants present in the In the system, slight oxidation of PVC can also occur, with some reaction products entering the system. Undoubtedly, the analysis has generated some reaction products that confirm this and after prolonged use, a slight surface erosion can be detected in some of the PVC components. When any of the coal beds 32 or 34 are in line, the oxidants are continuously deposited on the coal bed surface for continuous destruction of any V.O.C. that remain in the air stream that passes through coal bed. During regeneration, oxidants produced by the activated air generator 28 are not only depoeited in the coal bed for destruction of V.O.C. when the coal bed is carried in line, but additionally the regeneration discharge is recirculated back to the tunnel 14 for further reactivation. In the spray tank yard 44, an aqueous solution is irradiated according to the air bubbles through the spray tank and the solution moves from tank to tank and then to tunnel 14, such that the mist or mist supplied to the tunnel 14 be highly active with oxidants. Filtered particulate water from tunnel 14 and otherwise precipitated to tank 60 is considered to be still active enough to contribute to the reactions occurring in tank 60. Oxidizers and dissolved intermediates are recirculated through the spray tank yard 44 to be exposed to ultraviolet radiation, and recirculated in tunnel 14. Some of the oxidants produced by ultraviolet radiation in generators 28, 40 and spray tanks 44 and tunnel 14, are powerful oxidizing agents but their life as radical, for example Hydroxyl radicals can be relatively short, depending on the competition for reaction and recombination through the system. Therefore, for high volume industrial processes, the production of oxidants is continuous through the system by repeated exposure to ultraviolet radiation and by the introduction of fresh oxidants from generators 28 and 40. Also, the various oxidants available in the system of abatement 10, are available not only for direct reaction with VOCs photodecomposed, but they serve as radical intermediates in radical to radical reactions, since various chain reactions occur in the system. In any event, the desired final result of total destruction of the V.O.C is achieved, giving as final products carbon dioxide and water. Since water is a necessary part of the operation and system processes, the generation of water has a beneficial result, only leaving the carbon dioxide relatively innocuous to attend to it, at least from a theoretical point of view. The analysis to date has not determined the fate of the carbon dioxide, if any, generated by the abatement system 10. Although some experimentation has not shown an expected increase in C02m, the anticipated presence of C02 increases in the discharge stack. it can not be detected effectively. This would be convenient for direct comparison of the destruction efficiency of V.O.C. by the present invention regarding the destruction efficiency of V.O.C. by incineration, whose final products are also carbon dioxide and water. However, with the system of the present invention, the absence of an expected increase detectable at C02 in the discharge chimney 26 has several possible explanations. First, it is possible, although unlikely, that carbon dioxide is not produced by the system. Second, in an environment enriched with oxidant, the carbon dioxide may well react according to the following reaction scheme as suggested, in the aforementioned Chemical Review article: HO-4 C02? HC03 HO- 4 HC03"? H20 4 C03 •" HO- I HC02 2"? HO '? C03 •" In an environment enriched with hydroxyl radical, any bicarbonate or carbonate that is formed by the interaction of water or hydroxide with C02 t it can react with the hydroxyl radical to give a carbonate radical anion. This radical anion is itself an oxidant, although of a Oxidizing potential smaller than the hydroxyl radical. Thirdly, carbon dioxide is precisely absorbed in the 5 carbon beds32,34, and this absorbed carbon dioxide is not easy to displace but will slowly come off over time. Finally, thanks to the large amount of water present and passing through the tank yard 44, the dioxide can be solubilized to the aqueous phase and never appears -fl ^) in the exhaust chimney 26. As discussed above, no There are detectable levels of ozone in the activated air produced by generators 28 and 40. Furthermore, ozone is not generated in the tank yard 44 because the air is dissolved in an aqueous solution, and ozone is generated in tunnel 14, due to the soot and high humidity present along the tunnel. It is considered that this results from one or more of the following phenomena: ** decomposition of ozone due to the presence of high humidity; selection of ultraviolet light wavelengths and, the presence of PVC catalytic radicals. It is generally considered that, in a dry environment, ultraviolet radiation at wavelengths shorter than 220 nanometers will produce ozone and decompose 02 into 0l. Ultraviolet radiation at a wavelength of 184.9 is also considered. nanometers is especially effective in the production of ozone.

It is also considered that ultraviolet radiation at a wavelength of 254 nanometers decomposes ozone. The ultraviolet lamps used to practice the present invention have a spectral wavelength distributed between 184 and 254 nanometers, with the 184.9 nm lamp that helps to generate ozone and the 254 nm lamp that helps decompose that ozone. The lamps are relatively low wattage, for example 0.425 amps at 120 volts for each lamp in each of the cells 306 in the generator 20 and the cells 210 in the generator 240. Similarly, each of the lamps is deployed in tunnel 14 and spray tank yard 44 is of relatively low wattage. It is expected that the process of the present invention can be optimized for a wide range of V.O.C. and V.O.C. different from those expected in paint spray booth applications by varying the amount (upper wattage) and radiation wavelengths, either distributed over different ranges of wavelength or possibly even monochromatic radiation at selected wavelengths. By using the modular sections, such as sections Sl to S15, when the new technology is developed, it can easily be applied retroactively in an existing system. The exposure time to ultraviolet radiation in tunnel 14 can be varied by modifying the number and length of chambers included in the tunnel and by changing turbulence in divers chambers.

The present invention effectively and efficiently achieves the desired end products, ie water and certainly some C02. Oxides, ozone or other objectionable pollutants, including thermal pollution, are not released into the environment. The original installation costs are competitive with competitive systems for various reasons. System components and system design do not have to meet the demands of high temperature systems such as incinerators. Smaller beds of coal can be used due to substantial V.O.C. reduction. and destruction that occurs in the tunnel and the destruction of V.O.C. It continues in the coal bed for surface reactions with oxidants from the generator. The apparatus of the present invention is constructed with relatively inexpensive materials, including extensive use of commercially available, low cost PVC tubing. Operating and maintenance costs are also reduced compared to competitive systems. No special chemicals are required as they could be used for chemical destruction of V.O.C. Definitely, the only "starting" materials are running water and plant air. The oxidants used, for example as illustrated in Tables 1 and 2, represent 20% of the atmosphere. The carbon bed regeneration time is reduced by using activated air, regeneration is carried out on site and large quantities of waste byproduct are not transported for treatment and / or off-site disposal. In this aspect, with the present invention, it has been noted that some small granules with an approximate size of a fine sand grain are eventually collected in tank 60, but the amount produced is negligible and possibly due to some incidental ineralization. that occur in the process. HE. they expect energy efficiencies that compare favorably with incineration, even though that comparison has not been quantified to date. In this way, it will be apparent that, according to the present invention, there has been provided a method and apparatus for abatement of volatile organic comptables that achieve the objectives and advantages specified herein. Of course it will be understood that the foregoing description is of a preferred exemplary embodiment of the invention and that the invention is not limited to the specific embodiment illustrated. Various changes and modifications will be apparent to those skilled in the art and all these changes and modifications are intended to fall within the scope of the appended claims.

Claims (70)

1. CLAIMS 1. Method to degrade volatile organic compounds (VOC) contained in discharge air from industrial processes and the like, by a continuous flow treatment in a circumscribed tunnel that has multiple chambers throughout, comprising the steps of: continuously introducing a VOC-containing deepening air stream, at a tunnel entrance, exposing an air supply to ultraviolet radiation to produce an activated air supply having reactive oxidants, including at least hydroxyl radicals, forming an aqueous solution having the air activated there It is necessary to disperse, nebulize the aqueous solution in a first chamber to maintain an activated mist environment in the first chamber and pass the air current through the first chamber and expose the air current to ultraviolet radiation, to degrade oxidatively and phochemically. VOC in the air stream.
2. 2. Method according to claim 1, further comprising introducing the aqueous solution into the first chamber as a mist having aqueous particles in the range from 1 to 5 microns.
3. 3. Method according to claim 1, further comprising removing particulate water with dissolved reaction products from the air stream as it leaves the first chamber while passing V.O.C. gaseous, gaseous activated air and water vapor in the air stream into a chamber downstream of the first chamber.
4. 4. Method according to claim 3, further comprising exposing the air stream to ultraviolet radiation while the air stream moves through the downstream chamber.
5. 5. Method according to claim 4, wherein the downstream chamber is a second chamber downstream and contiguous with the first chamber and wherein the method further comprises: maintaining the air stream substantially free of particulate water, as air current enters the second chamber, so that the VOCs gaseous, activated air and aqueous vapors are exposed to ultraviolet radiation in a high humidity environment, but substantially no haze in a second chamber.
6. 6. Method according to claim 5, wherein the second chamber is maintained at relative humidity in the range of about 95 to 100 percent. Method according to claim 5, wherein the water is extracted from the air stream and the second chamber is substantially free of particulate water by filtering the air stream as it leaves the first chamber and enters the second chamber. camera. 8. Method according to claim 6, wherein the air stream is filtered through a filter medium that removes water in particles greater than about 5 microns. The method according to claim 5, further comprising extracting VOC reaction products from the air stream as it leaves the second chamber 10. Method according to claim 9, wherein the VOC reaction products they are extracted from the air stream as they leave the second chamber when passing the air stream through a carbon filter 11. Method according to claim 10, further comprises exposing the carbon filter to ultraviolet radiation. according to claim 5, further comprises: passing the air stream through a third chamber upstream of the first chamber, continuously fogging the aqueous solution into the third chamber to maintain an activated mist environment there, passing the current of air through the third chamber while simultaneously exposing the air stream and the haze to ultraviolet radiation in the This is done in the chamber, and stirring the nebulized air stream in the third chamber, while the nebulized air stream is contacted simultaneously as a catalyst. 13. Method of compliance with claim 12, wherein the nebulized air stream is agitated and contacted with a catalyst as the air current leaves the third chamber. Method according to claim 12, wherein the air stream is passed through the third chamber and then through at least one first chamber and then immediately through the second chamber. 15. Method according to claim 14, wherein the air stream leaving the third chamber is then passed sequentially through a plurality of first chambers adjacent to each other and then immediately passed from a last of the first sequential chambers to the second camera. 16. Method according to claim 5, further comprising: passing the air stream through another first chamber downstream of the second chamber, and then passing the air stream through another second chamber downstream of the other first chamber. camera. 17. Method according to claim 1, wherein the water and the reaction products V.O.C. that are extracted from the air stream that moves through the tunnel, recirculate back to the tunnel and nebulize inside the air stream. 18. Method according to claim 17, wherein the extracted water and the reaction products V.O.C. they are recirculated back to the air stream, by dispersing activated air in the extracted water and reaction products V.O.C. to form the aqueous solution. 19. Method according to claim 18, further comprising exposing the aqueous solution to ultraviolet radiation while simultaneously dispersing the activated air therein. 20. Method according to claim 5, further comprising passing air that is discharged from the tunnel through a carbon bed system to adsorb any V.O.C. remaining of the air stream. 21. Method according to claim 20, further comprising: passing activated air through the coal bed system to desorb the coal bed system and dispersing oxidizers in the coal bed system for a surface reaction with V.O.C. in the air stream, and then pass the tunnel discharge air through the coal bed system. 22. Method according to claim 21, wherein the air activated by desorption that is discharged from the coal bed is introduced into the tunnel. 23. Method according to claim 22, wherein the desorption discharge air is introduced to an activated haze environment in the tunnel. 24. Method according to claim 20, further comprises the step of providing a restriction to the air flow through the coal bed system. Method according to claim 3, wherein the downstream chamber is another first chamber immediately adjacent to the first mentioned chamber, and the method further comprises: introducing a mist of the aqueous solution into the other first chamber, to create an activated haze environment, pass the VOC air stream through the first adjoining chamber, while the air stream and mist are exposed to ultraviolet radiation in the other first chamber, and to extract water in particle with dissolved reaction products from the air stream as they leave the other first camera. 26. Method according to claim 25, wherein the air stream is repeatedly exposed to ultraviolet radiation in an activated haze environment, as the air stream moves sequentially through a plurality of first chambers, and particulate water. with VOC reaction products It is extracted from the air stream in each first chamber. 27. Method according to claim 26, wherein the air stream is also repeatedly exposed to ultraviolet radiation in high humidity environments, substantially free of activated haze. 28. Method according to claim 27, wherein the water vapor and V.O.C. Gases in the air stream are exposed to ultraviolet radiation in an environment substantially free of activated haze, immediately after water in particles and reaction products V.O.C. They have been extracted from the airstream and at least one of the first chambers. 29. Method according to claim 26, wherein the air stream is repeatedly exposed to ultraviolet radiation in an activated haze environment, at least several times and filtered at least several times. 30. Method according to claim 29, wherein the air stream is exposed to ultraviolet radiation in an activated haze environment, with intermediate extraction of water and reaction products V.O.C. at least five times. 31. Method according to claim 28, wherein the water vapor and V.O.C. gaseous gases exposed to ultraviolet radiation are then passed through a carbon filter before the airflow is again exposed to ultraviolet radiation in an activated haze environment at least in one of the first chambers. 32. Method according to claim 26, wherein the air stream is contacted with a catalyst before repeated exposure to ultraviolet radiation in the first chambers. 33. Method according to claim 26, further comprises: connecting particulate water that is extracted from the air stream in the tunnel, and dispersing the activated air in the collected water, to form the aqueous solution before the aqueous solution is nebulized in the air stream to in this way continuously recirculate the collected water back to the tunnel. 34. Method according to claim 26, further comprising: downloading V.O.C. gaseous and water vapor from the tunnel, and pass the tunnel discharge gases through a carbon bed system to adsorb V.O.C. remaining of the air stream. 35. Method according to claim 34, further comprising: passing activated air through the coal bed system to desorb the coal bed and dispersing oxidizers in the coal bed system for surface reaction with V.O.C. in the gassing of tunnel loading, and then passing the tunnel discharge gases through the coal bed system. 36. Method according to claim 35, further comprising: discharging air activated by desorption of the coal bed system and introducing the coal bed discharge air into the tunnel. 37. Method according to claim 35, further comprising: providing at least one pair of coal bed in the seventh carbon bed, passing exhaust air from the tunnel through a first of the carbon beds to adsorb V.O.C. of the discharge air, while activated air is simultaneously passed to the other of the beds to desorb the other bed and recharge the other bed with a fresh supply of oxidants for surface reaction with the VOCs, and then pass the discharge air from the tunnel to through the other coal bed, to adsorb the VOCs from the tunnel discharge air while simultaneously passing activated air through the first coal bed to desorb the first coal bed and recharge the first coal bed with a new supply of oxidants for surface reaction with V.O.C. 38. Method according to claim 1, wherein the activated air is introduced into the tunnel in gaseous form. 39. Method according to claim 1, wherein before exposing the air stream to ultraviolet radiation, the method further comprises: spraying aqueous solution into the air stream, and then vigorously mixing the air stream and the spray. aqueous solution to intimately contact VOCs in the air stream with the aqueous solution. 40. Method according to claim 1, wherein the air stream moving through the tunnel is contacted with a catalyst. 41. Method according to claim 40, wherein the air stream is contacted with polyvinyl chloride in an activated haze environment. 42. Method according to claim 1, wherein the V.O.C. they include ethylanilketones (MAK), xylenes and ortho-xylenes. 43. Method according to claim 1, wherein the exposure step further comprises exposing air having a relative humidity of at least 85% to ultraviolet radiation to produce euminietro of activated air. 44. Method according to claim 1, wherein the air stream ee passes through the tunnel at a volumetric expense that is in the range of 10,620 to 23,600 It / sec (22,500 to 50,000 ACFM). 45. Method according to claim 1, wherein the aqueous solution is nebulized in the tunnel at a rate exceeding 18.93 liters per minute (5 gallons per minute) to about 703 kg / cm2 (1,000 psi). 46. Method according to claim 1, wherein the air stream is exposed to ultraviolet radiation in the range from 184 to 254 nanometers. 47. Method according to claim 1, wherein the aqueous solution containing dispersed activated air there is formed by mixing activated air with a liquid to disperse bubbles of activated air in the liquid while being simultaneously exposed to the aqueous solution to radiation. ultraviolet. 48. Method according to claim 1, wherein a plurality of first chambers is maintained at one hundred percent relative humidity and the air stream is strongly saturated to provide the activated haze environment and at least one other chamber is maintained at one relatively high humidity and substantially free of particulate water from the upstream chambers. 49. Apparatus for removing volatile organic compounds (VOC) from industrial process discharge air and the like on a continuous basis, by oxidative and photochemical degradation, comprising: a generator that provides an activated air source, the generator has a plurality of electrically energized lamps that can produce ultraviolet radiation, the generator is arranged and built to receive clean air, exposes clean air to ultraviolet radiation and supplies activated air that has reactive oxidants, a mixer arranged and built to disperse activated air bubbles from the generator inside of a liquid to form an activated aqueous solution, a tunnel with walls having an inlet for receiving air having VOC, a plurality of chambers spaced over the tunnel and an outlet for discharging air after treatment in the tunnel, the tunnel is arranged and builds to confine the discharge air within a stream of air moving on a path through the tunnel, at least one of the chambers comprises a plurality of nozzles that receive activated aqueous solution from the mixer and spray the aqueous solution into said chamber to introduce an activated mist into the stream of air, a plurality of electrically energized ultraviolet lamps that are transported in said chamber to expose the air stream and activate haze to ultraviolet radiation in said chamber, and a liquid extractor to remove particulate water from the air stream as it moves outside the camera and inside an adjoining chamber downstream. 50. Apparatus as described in claim 49, wherein the plurality of chambers includes a plurality of first chambers comprising said chamber, and all first chambers have nozzles for introducing activated haze into the air stream, ultraviolet lamps for exposing the air stream and the ultraviolet radiation mist and liquid extractors to remove particulate water from the air stream, when the air stream moves outside each chamber. 51. Apparatus as described in claim 50, further comprising: a first separation extending transversely of the tunnel through the air current path and separating the first chamber from the adjoining chamber and where: the extractor comprises filters mounted in the separation, in such a way that the air current circulates through the filters inside the adjoining chamber and a • "plurality of electrically energized lamps are mounted in the downstream division of the filters to emit ultraviolet radiation within the adjoining chamber," "52. Apparatus as described in claim 51, wherein the adjoining chamber is a first chamber and the apparatus. it further comprises a plurality of nozzles that are conveyed in the downstream separation of the filter to receive activated aqueous solution from the mixer and introduce activated mist into the adjoining downstream chamber 53. Apparatus as described in claim 51, wherein the filters have characteristics of select filters to block particulate water and pass gaseous VOCs and water vapor in such a way that the air stream moves within the adjoining chamber, substantially free of particulate water and the plurality of lamps in the first separation exposes gaseous VOCs and water vapor to ultraviolet radiation in the chamber with 54. Apparatus as described in claim 53, further comprising: a second separation extending transversely of the tunnel and through the air current path at an outlet of the adjoining chamber; and second filters mounted in the second separation so that the air stream must flow through the second filters. 55. Apparatus as described in claim 54, wherein the second filters are carbon filters. 56. Apparatus as described in claim 55, wherein a plurality of second camera including the second adjacent camera are spaced over the tunnel, each of the second cameras being downstream immediately adjacent to a first camera to receive V.O.C. gaseous and water vapor, each of the second chambers has ultraviolet lamps to expose V.O.C. gaseous and water vapor to ultraviolet radiation and each of the second chambers has carbon filters mounted in second eeparations at exit ends of the second chambers. 57. Apparatus as described in the claim? 50, further comprises: a third chamber in the tunnel, immediately upstream of a first chamber, nozzles connected to the mixer and operatively associated with the third chamber for introducing activated haze into the air stream in the third chamber, electrically operated ultraviolet lamps , operatively associated with the third chamber, for exposing the nebulized air stream to ultraviolet radiation in the third chamber, and a third separation in the third chamber extending transversely from the tunnel through the air stream path, and mounted scrubbers in the third separation to create turbulence in the air stream and intimate contact between the VOCs in the air stream and oxidants in the activated mist. 58. Apparatus as described in claim -57, wherein the scrubbers include catalyst. 59. Apparatus as described in claim 57, wherein the scrubbers are perforated plates having the catalyst at least on one surface. 60. Apparatus as described in claim 49, further comprising: a collection tank arranged and positioned to receive liquid withdrawn from the air stream by the extractors, and a pumping system connected to a pumping system connected to the collection tank and the nozzles to recirculate liquid from the tank back to the air stream in the tunnel. 61. Apparatus as described in claim 60, wherein the pumping system comprises: a first pump operatively connected between the tank and the mixer to supply extracted liquid to the mixer, and a second pump operatively connected between the mixer and the nozzles, to supply the aqueous solution from the mixer to the nozzles. 62. Method according to claim 61, wherein the mixer further comprises: a housing having a liquid inlet connected to the first pump for receiving tank liquid, a bubbler operatively connected to the activated air generator and disposed and placed in the housing for dispersing bubbles of air activated in liquid in the housing, to form the activated aqueous solution, and a plurality of ultraviolet lamps mounted within the housing to expose Ultraviolet radiation the aqueous solution and the bubbles of activated air, while the activated aqueous solution is formed. 63. Apparatus according to claim 49, wherein the mixer comprises: a housing wherein the bubbles of activated air are dispersed in a liquid to form the activated aqueous solution, and a plurality of ultraviolet lamps operatively mounted within the housing to expose the aqueous solution and the bubbles of air activated to ultraviolet radiation, while the activated aqueous solution is formed. 64. Apparatus according to claim 49, wherein the tunnel comprises: a plurality of first chambers spaced over the air stream path, each of the first chambers having activated mist nozzles and ultraviolet lamps operatively associated with them to expose the air stream and mist activated to ultraviolet radiation, and liquid extractors to remove particulate water as the air stream moves out of the first respective chambers, a plurality of second chambers spaced over the air stream path with second chambers respective that are contiguously downstream of respective first chambers, filters transvereally extending from the tunnel through the air stream path between adjacent first chambers and second chambers, the filters have characteristics of filters selected to extract water from particles of the air stream q that leaves the first cameras and passes V.O.C. gaseous and water vapor from a first chamber to a second adjoining chamber, the second chambers have operatively associated ultraviolet lamps to expose V.O.C. gaseous and water vapor to ultraviolet radiation as the air current moves through the second chambers and at least one third chamber in the tunnel upstream of a first chamber and its second adjoining chamber, the third chamber has: ultraviolet and activated mist nozzles operatively associated to simultaneously expose the air and mist stream activated in the third chamber to ultraviolet radiation and catalytic perforated plates extending transversely of the tunnel in the third chamber through the air current path. 65. Apparatus according to claim 64, wherein at least two first contiguous chambers are located in the air current path upstream of the second adjoining chamber. 66. Apparatus according to claim 49, further comprising: a coal bed system circumscribed in a housing, first ducts connecting the outlet of the tunnel with the coal bed housing to supply air discharge from the tunnel to the system of coal bed for adsorption of any VOC remaining. 67. Apparatus according to claim 66, further comprising: damping assemblies for selectively interrupting the supply of tunnel discharge air to the coal bed system through the first ducts, a coal bed desorption system comprising : an activated air source, the source has a plurality of electrically energized lamps that produce ultraviolet radiation and are arranged and constructed to receive clean air, expose clean air to ultraviolet radiation to produce activated air containing oxidants, direct by pipeline by operatively connecting the active air source to the coal bed system and valve assemblies to selectively pass active air through the pipe with the coal bed system during carbon bed desorption. 68. Apparatus according to claim 67, wherein: the coal bed system includes at least the first and second coal beds, the shock mounts are operative to supply the tunnel discharge air through the first ducts to one of the coal beds and interrupt the supply from the tunnel discharge air to the other coal bed and the valve assemblies are operative to supply active air from the source through the pipe to the other coal bed to desorb the other coal bed, while the first coal bed receives discharge air from the tunnel through the ducts. 69. Apparatus according to claim 67, further comprising: a seventh return pipe connected at one end with a deepening of the coal bed system and at its other end with the tunnel to introduce coal bed discharge to the air stream. 70. Apparatus according to claim 66, wherein the coal bed system defines a path extending between an inlet and an outlet of the coal bed system and wherein the seventh carbon bed includes a flow restriction of air located in the path near the outlet, whereby the restriction of air flow creates a counter-pressure within the coal bed system. SUMMARY OF THE INVENTION A method and apparatus for reducing, knocking down and destroying volatile organic compounds (V.O.C.) contained in an air stream are described. The air stream is mixed with an activated air mist or mist in aqueous solution, while the mixture is repeatedly exposed to ultraviolet radiation in chambers along a tunnel. The activated air contains oxidants that are formed by exposing air to ultraviolet light. The activated air is generated under conditions that prevent prolonged ozone existence and improve the generation of highly active oxidants such as hydroxyl radicals. The aqueous solution is formed by dispersing the activated air in water, in tank coolers that include ultraviolet lamps to maintain a high level of oxidants in the aqueous solution. The tunnel includes catalyst plates that act as scavengers and which are exposed to ultraviolet light in the tunnel to provide hydrogen to improve the generation of the hydroxyl radicals. The tunnel includes scrubbers that remove particulate water and V.O.C., which are collected in a supply tank and recirculated to the spray tanks and then back to the tunnel. The tunnel also includes carbon filters that collect V.O.C. for surface reaction in the presence of more ultraviolet light. Upon discharge of the tunnel, the air stream is supplied to a coal bed system, where the V.O.C. The remaining ones are captured and they are also destroyed oxidatively. Two coal beds can be used, with one coal bed in line while the other is regenerated using activated air. ES b + / (11) TE1779SC