CATALYTIC PLASMA REDUCTION OF NOx

Abstract: The present invention is based upon the discovery that microporous catalysts, especially zeolites in the class of metallic Faujasites, Linde Type A (LTA) and combinations thereof having a pore size greater than 3 angstroms in combination with a plasma are capable of catalyzing conversion of NOx to N2 in a real or actual exhaust stream without any gas phase additive.

Description: CATALYTIC PLASMA REDUCTION OF NOχ FIELD OF THE INVENTION The present invention relates to catalytic plasma reduction of nitrogen oxide (NOχ). More specifically, the present invention relates to selection of a microporous catalyst to obtain conversion of the nitrogen oxide to nitrogen gas without external addition of any gas phase additive. As used herein, the phrase and similar phrases to "without external addition of any gas phase additive" refers to the absence of any non-exhaust input. As used herein, the term "pore size" is the network ring opening size in the absence of a charge compensating cation or a "bare" material. As used herein, the term "free aperture" is the size of an opening through the pore after a cation has been inserted into the pore of the bare material. BACKGROUND OF THE INVENTION Combustion exhaust theoretically should be simply carbon dioxide and water vapor. However, because most fuels are complex compounds, and because the source of oxidant is the atmosphere with about 21 vol.% nitrogen, combustion exhaust generally contains unburned hydrocarbons and one or more versions of nitrogen oxide (NO x ) converted from the nitrogen. Even a methane or hydrogen fuel source can have unburned fuel and produce nitrogen oxide. There has been much effort expended to obtain both the greatest possible energy from a fuel and achieve a clean exhaust free of hydrocarbons and nitrogen oxide. One approach toward achieving clean exhaust has been plasma assisted catalytic reduction operated downstream of the combustion chamber. An example of this approach is U.S. patent 5,711,147 to Vogtlin et al. wherein a non-thermal plasma gas is combined with γ-AI 2 O 3 catalyst and a stream of added hydrocarbon to achieve an 80% reduction of NO x . A disadvantage of this method is the added hydrocarbon defeating the goal of maximizing energy extraction from the fuel. The U.S. patent 5,715,677 to Wallman et al. achieves an unspecified reduction of nitrogen oxide (NO x ) from diesel exhaust by collecting particulate and NO x onto an adsorbent bed with bead size from 5-10 mm then exposing the adsorbent bed to plasma. Materials for the adsorbent bed included metal oxides, dolomite, zeolites of ZSM-5, Cu-ZSM-5, and H-mordenite, and perovskites. A disadvantage of this method is the semi-batch or non-continuous mode of operation requiring separate adsorption and plasma exposure steps. The U.S. patent 5,746,984 to Hoard is directed to treating cold-start emissions by adsorbing the cold start emissions on a storage device then desorbing them as the exhaust temperature increases followed by destroying the desorbed cold start emissions in a non-thermal plasma. A honeycomb monolith is prepared to receive a coating of an adsorbing material as the storage device. Adsorbing materials are recited as oxides of copper, barium and lanthanum, and CuZSM-5 zeolite. Hoard reports that operation of the plasma reactor consumes no more than about 2% of engine energy consumption. However, it has been shown in Analysis of Plasma-Catalysis for Diesel NOX Remediation, J Hoard, ML Balmer, Diesel Engine Emissions Reduction Workshop Proceedings, 1998 that in the case of Cu-ZSM-5 placed either in the plasma or downstream of (after) the plasma, converts the gas phase species back to NOχ, an undesirable product. Thus, Hoard's report of 2% consumption is not for complete conversion of NOχ to N 2 . The U.S. patent 5,458,748 to Breault et al. show NO x conversion as a function of applied voltage for the plasma, with conversion up to about 98%. However, no catalyst other than plasma is used and the products of conversion include HNO 3 which is corrosive unless removed. In addition it has been shown by BM Pentrante, WJ Pitz, MC Hsaio, BT Merritt, and GE Vogtlin, in the Proceedings for the 1997 Diesel Engine Emissions Reduction Workshop that in the absence of a catalyst, the plasma chemistry primarily converts NO to NO 2 with some NO x disappearing to unmeasured products NO x species converted in the plasma are converted back to NO. U.S. patent 5,609,736 to Yamamoto describes a vessel formed of opposing conductive plates and opposing dielectric plates between the opposing conductive plates. The volume of the vessel is filled with beads having a catalytic coating thereon. Catalytic coatings specified are oxidation catalysts of noble metals and metallic oxides. Removal of carbon tetrachloride is reported. Nitrogen oxide conversion is mentioned but not quantitatively reported. UK patent application GB 2,274,412 A describes a chamber filled with pellets held between screens that act as electrodes and showing removal of toluene from a gas stream. The pellets are Pb or Ba niobate, titanate or zirconate. Nitrogen oxide removal is not quantified. Japanese Kokai JP 6-269635 describes a plasma exhaust gas processing apparatus and absorbent apparatus connected in order. No catalyst is used. The conversion product NO 2 is absorbed in the absorbent apparatus. A disadvantage of this technique is the need to regenerate the absorbent apparatus. The German Offenlegungsschrift DE 195 10 804 A1 discusses combining an exhaust gas stream with a reduction agent that is made into a plasma and contacted with a catalyst. The reduction agent is a nitrogen compound, for example nitrogen, ammodia, hydrazine or cyanuric acid or is aliphatic or olefin hydrocarbon or hydrogen. The catalyst may be zeolites doped with elements of the platinum group, copper group, or iron group, oxides doped with elements of the platinum-, aluminum-, titanium- or lanthanide groups or their mixtures, mixed oxides of wolfram, chrome, or vanadium. NO x reduction is not quantified. A disadvantage of this process is the addition of a reduction agent. The paper PLASMA-ASSISTED HETEROGENOUS CATALYSIS FOR NOχ REDUCTION IN LEAN-BURN ENGINE EXHAUST, BM Penetrante, MC Hsiao, BT Merritt, GE Vogtlin, Proceedings of the 1997 Diesel Engine Emissions Reduction Workshop discusses the advantage of using plasma in combination with "a new class of catalysts that are potentially more durable, more active, more selective and more sulfur tolerant". Because the inventors of 5,711 ,147 (discussed above) are included as authors of this paper, and the paper was published after the patent application was filed, it is hypothesized that the "new class of catalysts" includes gamma alumina mentioned in the patent and possibly other catalyst materials mentioned in the literature. FIG. 4(b) of the paper shows maximum conversion of NOχ to N 2 of 77% at about 25 J/L energy density in real diesel exhaust. It is assumed that the added hydrocarbon mentioned in the patent is also used to obtain the data in the paper although an added hydrocarbon is not specifically mentioned in the paper. The abstract of the paper CATALYST ASSISTED REACTION BY USING NON-THERMAL PLASMA ON NITRIC OXIDES REMOVAL, K Shimizu, T Oda, 1997, identifies Na-ZSM-5 as an effective catalyst in combination with non- thermal plasma for NO x removal. FIG. 4 of the paper shows a maximum removal rate of less than 55% for input power up to 30 W. Japanese patent application Hei 6-106025, K Isogai et al. discusses a plasma reactor with catalyst material for decomposition of NOχ. Catalyst material is metal oxide, and zeolites of H-ZSM-5, H-Y, H-Mordenite, Na-ZSM-5, and Cu-ZSM-5. Decomposition rate is not shown. The ineffectiveness of Cu- ZSM-5 because of reconversion to NO was mentioned above. Japanese patent application Hei 6-15143 K Isogai discusses a plasma reactor with a photocatalytic dielectric material. The photocatalytic dielectric material may be TiO 2 , ZnO, SrTiO 2 , and ZnS. Nitrogen oxide destruction is not quantified. As may be seen from the review of prior art literature provided herein, the energy efficiency of NOχ conversion is often not reported and when it is reported, it is difficult to compare because of different bases of quantification. The destruction rate of NOX decreases logarithmically with energy density as shown in Tonkyn (Vehicle Exhaust Treatment Using Electrical Discharge methods, " Tonkyn, Barlow, Balmer, Orlando, Hoard, and Goulette, SAE Paper 971716, May 1997), specifically ■ E/β [NO] = [NO] 0 *e •E/β [NO x ] = [NO x ] f + ([NO x ] o - [NOχ] f ) * e where β (or beta parameter) is the first order decay parameter in Joules/standard liter, [NOχ] 0 is the initial NOx concentration and [NO x ] f is the final NO x concentration. The beta parameter is therefore a quantitative measure of energy consumption of the conversion of NOχ to N 2 . In general, a low beta value indicates that the energy efficiency is high, or alternatively, that the amount of energy expended to achieve the maximum NOχ destruction is relatively low. The overall NOχ destruction efficiency is affected by both the type of plasma reactor and the type of catalyst. Other measures of conversion efficiency include percent of total fuel consumption, and percent destruction for a given power (Watts). Although much attention and work has been done to clean up combustion gas exhaust streams, there is still a need in the art for an apparatus and method that is capable of converting NOχ to N 2 in a real or actual exhaust stream without any gas phase additive and with greater energy efficiency. SUMMARY OF THE INVENTION The present invention is based upon the discovery that microporous materials having a free aperture greater than 3 angstroms in combination with a plasma are capable of catalyzing conversion of NOχ to N 2 in a real or actual exhaust stream without any gas phase additive. It is an object of the present invention to provide a method of NOχ conversion to N 2 using a plasma in the presence of a microporous catalyst. It is a particular advantage of the present invention that the optimum performance is achieved at temperatures and gas compositions typically found in the exhaust of light duty vehicles. The subject matter of the present invention is particularly pointed out and distinctly claimed in the concluding portion of this specification. However, both the organization and method of operation, together with further advantages and objects thereof, may best be understood by reference to the following description taken in connection with accompanying drawings wherein like reference characters refer to like elements. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a cross section of a single stage apparatus of the present invention. FIG. 2A is a cross section of a two-stage apparatus of the present invention. FIG. 2B is a cutaway of a tube array reactor encased in a metallic housing. FIG. 2C is a cutaway of an alternate tube array reactor. FIG. 3 is a single stage NOχ conversion graph for Z-Y-Na. FIG. 4 is a single stage NOχ conversion graph for Z-Y-K. FIG. 5 is a single stage NOχ conversion graph for Z-Y-Cs. FIG. 6 is a single stage NOχ conversion graph for Z-Y-Ga. FIG. 7 is a single stage NOχ conversion graph for Z-Y-Co. FIG. 8 is a single stage NOχ conversion graph for Z-Y-Ag. FIG. 9 is a single stage NOχ conversion graph for Z-Y-Ni. FIG. 10 s a single stage NOχ conversion graph for Z-X-Na. FIG. 1 1 s a two-stage NOχ conversion graph for Z-Y-Na. FIG. 12 s a double single stage NOχ conversion graph for Z-Y-Na. FIG. 13 s a single stage NOχ conversion graph for LTA-K. FIG. 14 s a single stage NOχ conversion graph for LTA-Na. FIG. 15 s a single stage NOχ conversion graph for LTA-Ca. FIG. 16 s a single stage NO x conversion graph for ETS-10. DESCRIPTION OF THE PREFERRED EMBODIMENT(S) The present invention shown in FIG. 1 includes a method and an apparatus for catalytic plasma removal of at least one nitrogen oxide from an exhaust gas stream 100 containing the at least one nitrogen oxide by converting the at least one nitrogen oxide to a nitrogen gas (N 2 ). The method and apparatus rely upon a vessel 102 with an inlet 104 and an outlet 106, the vessel 102 having a microporous catalyst 108 therein together with electrodes 110 for creating a plasma. The exhaust gas stream 100 is passed into the inlet 104 through the vessel 102 and contacted with the microporous catalyst 108 and the plasma thereby converting the at least one nitrogen oxide to a nitrogen gas, forming a nitrogen oxide reduced exhaust gas stream 112, and flowing the nitrogen oxide reduced exhaust stream 112 through the outlet 106. If the dielectric constant of the microporous catalyst 108 is not sufficient to prevent arcing between the electrodes 110, a dielectric barrier 114 may be added. If the microporous catalyst 108 is not self supporting, a support frit 116 may be used. The microporous catalyst 108 may be supported in a binder including but not limited to attapulgite clay, alumina and combinations thereof. It is important that the binder permit gas (hydrocarbon and NOχ) access to the microporous catalyst 108. The vessel 102 may have separate chambers as shown in FIG. 2A, a plasma chamber 200 and a catalyst chamber 202. Alternatively, two vessels 102 having microporous catalyst 108 therein may be placed in series (not shown) as a double single stage configuration, or a double two-stage configuration. The plasma chamber may comprise a packed bed reactor or a tube array reactor. Packed bed reactors suffer from electrical current flow across the particles of the packed bed and higher pressure drop through the packed bed which contribute to higher energy requirements than are needed with tube array reactors. The tube array is the preferred reactor for the plasma chamber due to its lower energy requirement and higher efficiency design resulting from factors such as a higher transfer of electrical energy into the plasma and the openness of the tube array design which facilitates a lower pressure drop across the tube array. A tube array reactor 250 encased in a metallic housing 252 is shown in Fig. 2B. Dielectric tubes 254 are metalized on the inside 256 and electrified by fused contacts 258 to a high voltage power source (not shown). In this tube array design, the exhaust gas stream enters the chamber inlet 260 and flows in a transverse direction across the dielectric tubes before exiting the chamber outlet 262. In an alternate configuration shown in Fig. 2C, taken from U.S. Patent 5,458,748, the exhaust gas stream enters the chamber inlet 260 and flows through the tubes 254 in a parallel direction with the tubes 254. A preferred microporous catalyst is a zeolite in the class of metallic Faujasites, Linde Type A (LTA) and combinations thereof. The microporous catalyst may have all pores as microporous (pore size of 15 angstroms or less) or may have mixed micropores (15 angstroms or less) and mesopores (greater than 15 angstroms). The metallic Faujasite must be crystalline and has a structure selected from the group of zeolite X, zeolite Y and combinations thereof. Microporous material composition includes but is not limited to aluminosilicate and titanosilicate. Other network site cations include iron, gallium, germanium and combinations thereof. The metal in the exchange site of metallic Faujasite may be alkali, including but not limited to Mg, Li, Na, K, Rb, Cs, alkali earth, including but not limited to Ca, Sr, Ba, transition metals including but not limited to Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Re, Fe, Ru, Os, Co, Rh, Os, Co, Rh, Ir, Ni, Pd, Pt, Cu, Ag, Au, rare earths and combinations thereof. Rare earths include but are not limited to Ce and Sm. The amount of metal atoms in the metallic Faujasite may range from about 5% to about 100% of available sites for metal atoms. The metallic Faujasite has a micropore size of at least 6 angstrom units. Generally, zeolite Y has a pore size of about 7 angstroms and zeolite X has a pore size of about 10 angstroms. Metallic Faujasite in or after plasma converts more than 55% of NOχ to N 2 for certain cations at a temperature of about 180 °C. The optimum temperature is from about 150°C to about 250°C. This is an advantage because diesel exhaust from a light duty vehicle is typically near 150°C to 200°C. Free aperture size greater than 3.5 angstrom units permits flow of unburned hydrocarbon into the pores of the metallic Faujasite during conversion with at least one benefit of preventing the formation of nitric acid. Free aperture size greater than 6 angstrom units is preferred. The catalyst structure may be a perforated or porous monlith, beads, powder or combination thereof. Zeolites of Linde Type A (LTA) are characterized by pore sizes on the order of 4 angstroms. Small cations, including but not limited to Li, Na, Ca and combinations thereof permit NO x conversion to N 2 . Large cations, for example K, fill the pore preventing entrance of unburned hydrocarbons and substantially reduce conversion to the point of inoperability. Other microporous materials with structures different from Faujasite or Type A including titanosilicate (ETS-10) templated mesoporous materials with micropores have been found useful for NOχ conversion to N 2 . Experimental Apparatus and Method for Examples Simulated exhaust gas streams were obtained from gas tanks with mass flow controllers. The exhaust gas test conditions were 100 °C to 300 °C in a lean mix of 0 2 (2-8 vol%), C0 2 (< 7 vol%), H 2 0 (2-10 vol%), CO (<1 vol%), hydrocarbon (25-3100 ppm (as propylene or nonene, etc.)), and NO (10-500 ppm) at a space velocity of 2,000 - 45,000 hr "1 . Two catalyst configurations were used, either a single stage of a packed bed of catalyst material in the plasma region or two-stages of a plasma region followed by a packed bed of the catalyst material (FIG. 2). NO and NOχ were monitored with a chemiluminescent NOχ detector with differences attributed to N0 2 . End products of C0 2 and N 2 were monitored with a mass spectrometer and gas chromatograph. Example 1 Catalysts known in the prior art were used to measure NO x conversion with plasma. The amount of C0 2 was less than 4 vol%. The catalyst was in the form of a bead or pellet with particles held with a binder. Table E1-1 shows the catalysts and conversion results. NOχ conversion excludes thermal NO x reduction for Temp > 200 C B Conversion high at onset is close to 67%, however rapid degradation of activity observed after several hours. In general, protonated zeolites adsorbed large amounts of hydrocarbon then failed by deactivation or conduction. c Sample adsorbs large amounts of hydrocarbon and possibly NOX, the reactor (plasma) fails due to conduction. io . Example 2 Metallic Faujasites according to the present invention were used for NOχ conversion. The Z-X materials were obtained from Aldrich Chemical Milwaukee, Wl. Zeolite Y (Z-X materials) with a Na as the exchange cation was obtained from Zeolyst International Valley Forge, PA. To obtain zeolite Y with other cations, an ion exchange or solution impregnation technique was used on the Zeolyst material. Pellets were made from powders using either a gamma alumina binder or an attapulgite clay binder and 500°C heat treatment. The Z-Y with sodium was tested on a monolith honeycomb. The others were in the form of a bead or pellet secured with a binder. The single stage, conditions typically were: Temp. 180 °C, space velocity 12,000 hr "1 (4 L/min), 0 2 (8 vol%), C0 2 (7 vol%), H 2 0 (7 vol%), CO (0.0 vol%), hydrocarbon (C 3 H 6 525 ppm, C 3 H 8 75 ppm), and NO (250 ppm). In addition, there was argon (9,000 ppm) and hydrogen (130 ppm). For 2-stage experiments, the conditions were similar with water content reduced to 2 vol%, NO reduced to 150 ppm, and hydrocarbon levels reduced to C 3 H6 400 ppm. Results are shown in Table E2-1 and FIG.'s 3-12. The Z-Y with sodium was tested on a monolith honeycomb as well as in pellet and bead form. The others were in the form of a bead or pellet secured with a binder. FIG.'s 3-10 are for single stage operation with various cations. Single stage operation achieves 36-88% conversion with beta parameters ranging from 20-78 J/L. For Ag zeolite Y, which converts 73% of NOx at 50 J/L, or 3.3 Watts, or an equivalent of approximately 5% of the vehicle fuel would be used to reduce NO x to N 2 . For two-stage operation using Z-Y-Na, 29-81 % conversions are obtained for the beta parameter ranging from about 2 to 13 (fuel equivalent range from about 0.7% to about 4%). In FIG. 9 the beta parameter is 5 for a catalyst in the two stage configuration that achieves 81 % NOχ destruction at 20J/L, or 0.35 Watts, or 0.002 J/gram NOχ, or an equivalent of approximately 2% of the vehicle fuel would be used to reduce NOχ to N 2 nitrogen (a Ford Taurus was used to calculate fuel equivalent). For comparison, current catalytic converter systems need to operate at stoichiometric air/fuel ratios which results in a reduction of fuel efficiencies of about 6%. - No Data ! Reactor temperature different from the catalyst temperature A FIG. 3 B FIG. 5 C FIG. 6 D FIG. 7 E FIG. 8 F FIG. 9 G FIG. 10 H PB is packed bed and TAR is tube array reactor. For a double single stage operation with Z-Y-Na with a conversion of 36%, FIG. 12 shows a beta parameter of about 6 which are about the same as a two-stage configuration. Example 3 An experiment was conducted to demonstrate the effect of free aperture on the present invention. The catalyst was zeolite LTA with a Si:AI ratio of 1 :1 in pellet form. For the single stage, conditions were Temp. 180 °C, space velocity 12,000 hr -1 (4 L/min), 0 2 (8 vol%), C0 2 (7 vol%), H 2 0 (7 vol%), CO (0.0 vol%), hydrocarbon (C 3 H 6 525 ppm, C 3 H 8 75 ppm), and NO (250 ppm). In addition, there was argon (9,000 ppm) and hydrogen (130 ppm). Results are shown in Table E3-1. Table E3-1 NOχ conversion with Various Free Aperture B FIG. 12 C FIG. 13 Results are further shown in FIG.'s 13-15 for single stage conversion showing both NO and NOχ conversion. FIG. 13 is for zeolite LTA with potassium (K), FIG. 14 is for zeolite LTA with sodium (Na), and FIG. 15 is for zeolite LTA with calcium (Ca). For conversion rates from 4-57%, the beta parameter ranges from 10 to 30 respectively. Example 4 An experiment was conducted to demonstrate titanosilicate as a catalyst for NOχ conversion to N 2 . Catalyst beads were synthesized from the titanosilicate ETS-10 powder (obtained from Engelhard corporation, Iselin, NJ) using an attalpulgite clay or alumina binder. The free aperture of this catalyst was oval shaped with opening of 4.9Ax7.6A. The titanosilicate catalyst in a single-stage configuration with 8% water, at 180 °C achieved 47% NOχ conversion with a beta parameter of 39 (FIG. 16). CLOSURE While a preferred embodiment of the present invention has been shown and described, it will be apparent to those skilled in the art that many changes and modifications may be made without departing from the invention in its broader aspects. The appended claims are therefore intended to cover all such changes and modifications as fall within the true spirit and scope of the invention.

Claims: CLAIMS We claim: 1. A method of catalytic plasma conversion of at least one nitrogen oxide from an exhaust gas stream containing said at least one nitrogen oxide to a nitrogen gas, comprising the steps of: (a) providing a vessel with an inlet and an outlet, the vessel having a zeolite catalyst selected from the group of metallic Faujasite, Linde Type A and combinations thereof therein together with electrodes for creating a plasma, said zeolite catalyst containing a metal in an exchange site; (b) passing said exhaust gas stream into the inlet through said vessel and contacting said exhaust gas stream with said catalyst and said plasma thereby converting said at least one nitrogen oxide to said nitrogen gas, forming a nitrogen oxide reduced exhaust gas stream; and (c) flowing said nitrogen oxide reduced exhaust stream through the outlet. 2. The method as recited in claim 1 , wherein said metallic Faujasite has a structure selected from the group of zeolite X, zeolite Y and combinations thereof. 3. The method as recited in claim 2, wherein said metal is selected from the group of alkali, alkali earth, transition metal and combinations thereof. 4. The method as recited in claim 1 , wherein said zeolite catalyst contains metal atoms from about 5% to about 100% of available sites. 5. The method as recited in claim 1 , wherein said zeolite catalyst has a pore size of greater than 3 angstrom units. 6. The method as recited in claim 5, wherein said metallic Faujasite has a pore size of at least 6 angstrom units. 7. The method as recited in claim 1 , wherein said metal in said Linde Type A is a cation selected from the group consisting of Li, Na, Ca and combinations thereof. 8. The method as recited in claim 1 , wherein said exhaust gas is at a temperature of at least 100 °C. 9. The method as recited in claim 1 , wherein said zeolite catalyst has a metal selected from the group consisting of Na, Cs, Ca, Co, Ag, Ni, and K. 10. The method as recited in claim 1 , wherein said electrodes are arranged in a tube array. 1 1. An apparatus for catalytic plasma conversion of at least one nitrogen oxide from an exhaust gas stream containing said at least one nitrogen oxide to a nitrogen gas, comprising: (a) a vessel with an inlet and an outlet; (b) the vessel having therein a zeolite microporous catalyst selected from the group of metallic Faujasite, Linde Type A and combinations thereof; together with (c) electrodes for creating a plasma; wherein (d) said exhaust gas stream passes into the inlet through said vessel and contacts said exhaust gas stream with said catalyst and said plasma, thereby converting said at least one nitrogen oxide to said nitrogen gas, forming a nitrogen oxide reduced exhaust gas stream, and said nitrogen oxide reduced exhaust stream passing through the outlet. 12. The apparatus as recited in claim 11 , wherein said metallic Faujasite has a structure selected from the group of zeolite X, zeolite Y and combinations thereof. 13. The apparatus as recited in claim 12, wherein said metallic Faujasite has a metal selected from the group of alkali, alkali earth, transition metal and combinations thereof. 14. The apparatus as recited in claim 11 , wherein said zeolite catalyst contains metal atoms from about 5% to about 100% of available sites. 15. The apparatus as recited in claim 11 , wherein said zeolite catalyst has a pore size greater than 3 angstrom units. 16. The apparatus as recited in claim 15, wherein said metallic Faujasite has a pore size of at least 6 angstrom units. 17. The apparatus as recited in claim 11 , wherein said electrodes are arranged in a tube array. 18. The apparatus as recited in claim 11 , wherein said zeolite microporous catalyst has a metal selected from the group consisting of Na, Cs, Ca, Co, Ag, Ni, and K. 19. A method of converting at least one nitrogen oxide to nitrogen gas, comprising the steps of: (a) providing a vessel with an inlet and an outlet, the vessel having a microporous catalyst of a titanosilicate with a free aperture of at least 3.5 angstroms, said free aperture defined by a base porous material impregnated with a cation selected from the group consisting of alkaline earth, alkali, transition, and combinations thereof therein together with electrodes for creating a plasma; (b) passing said exhaust gas stream into the inlet through said vessel and contacting said exhaust gas stream with said catalyst and said plasma thereby converting said at least one nitrogen oxide to a nitrogen gas, forming a nitrogen oxide reduced exhaust gas stream; and (c) flowing said nitrogen oxide reduced exhaust stream through the outlet. 20. The method as recited in claim 19, wherein said cation is selected from the group consisting of Li, Na, K, Cs and combinations thereof. 21. The method as recited in claim 19, wherein said electrodes are arranged in a tube array. 22. A method of catalytic plasma conversion of at least one nitrogen oxide from an exhaust gas stream containing said at least one nitrogen oxide to a nitrogen gas, wherein at an optimum temperature from about 150 °C to about 180 °C, NOχ reduction is greater than 52%, comprising the steps of: (a) providing a vessel with an inlet and an outlet, the vessel having a zeolite catalyst selected from the group of metallic Faujasite, Linde Type A and combinations thereof therein together with electrodes for creating a plasma, said zeolite catalyst containing a metal in an exchange site; (b) passing said exhaust gas stream into the inlet through said vessel and contacting said exhaust gas stream with said catalyst and said plasma thereby converting said at least one nitrogen oxide to said nitrogen gas, forming a nitrogen oxide reduced exhaust gas stream; and (c) flowing said nitrogen oxide reduced exhaust stream through the outlet. 23. The method as recited in claim 22 wherein said zeolite has a free aperture from 3 angstroms to 7 angstroms. 24. The method as recited in claim 22, wherein said zeolite catalyst has a metal selected from the group consisting of Na, Cs, Ca, Co, Ag, Ni, and K. 25. The method as recited in claim 24 wherein said zeolite has a free aperture from 3 angstroms to 7 angstroms. 26. The method as recited in claim 22, wherein said electrodes are arranged in a tube array.

Inventors: BALMER MARI LOU, BARLOW STEPHAN E, KIM ANTHONY Y, ORLANDO THOMAS M, TONKYN RUSSELL G, BALMER, MARI, LOU, BARLOW, STEPHAN, E., KIM, ANTHONY, Y., ORLANDO, THOMAS, M., TONKYN, RUSSELL, G.
Applicants: BATTELLE MEMORIAL INSTITUTE
Application year: 1999
Main classification: B01D53
IPC codes: B01D53, F01N3