Catalytic Oxidation of Organic Nitrogen-Containing Compounds

The present invention relates generally to catalytic oxidation processes and particularly to the catalytic oxidation of gaseous nitrogen-containing compounds typically present in industrial off-gas streams.

Volatile nitrogen-containing organic compounds, referred to herein as VNC's, such as amines and nitriles, for example, must be removed from industrial off-gas streams prior to venting the gas stream into the atmosphere. Thermal incineration and catalytic oxidation are two destructive methods which may be used for controlling off-gas emissions. Thermal incineration of off-gas streams containing VNC's generate both thermal and chemical nitrogen dioxide (NO.sub.2) and nitric oxide (NO) (hereinafter referred to collectively as NO.sub.x) which are the most prevalent forms of nitrogen oxide which are present in measurable quantities in the atmosphere.

Thermal generated NO.sub.x gases are the result of the oxidation of nitrogen (N.sub.2) and occurs at high operating temperatures, while chemical generated NO.sub.x gases result from reactions involving the atomic nitrogen associated with volatile nitrogen containing compounds.

It is well-known that NO.sub.x gases are a leading constituent of smog and acid rain. Further, they have been linked to depletion of stratospheric ozone. While these gases are produced from natural sources, man-made sources can result in higher than desirable concentrations and therefore control of these emissions is desirable. The use of thermal incineration to decompose VNC's requires a costly NO.sub.x abatement process to be employed to control the NO.sub.x emissions.

Catalytic oxidation process for decomposition of VNC's have the advantage of operating at much lower temperatures than incineration processes and thus remove the mechanism to generate thermal NO.sub.x. However, there is still the potential to produce chemical NO.sub.x due to the nitrogen associated with the VNC's. Recent studies by Lester and Homeyer presented at 1993 Meeting of the American Chemical Society in Denver Colo. have reported the catalytic oxidation of a number of VNC's over a proprietary supported platinum catalyst on behalf of Allied Signal, Inc. This catalyst was able to readily destroy the VNC's tested, however, very significant quantities of NO.sub.x were generated. Therefore use of this catalyst in a process to destroy VNC's would also require an additional abatement treatment of the NO.sub.x gases generated.

Kuwabara et al (Chem. Lett., 1992) describe the use of copper-exchanged zeolites as catalysts to oxidatively destroy trimethylamine without the formation of significant amounts of NO.sub.x. The apparently most successful catalyst used was a copper-containing ZSM-5 which is a crystalline molecular sieve. However, such a catalyst is subject to poisoning by sulfur or halogen compounds often found in industrial off-gas streams. Further, crystalline zeolite molecular sieves are relatively costly to prepare for industrial applications.

A 1993 article by Rosenburg et al provides an overview of selective catalytic reduction of NO.sub.x emissions involving the addition of ammonia to a NO.sub.x stream in the presence of a catalyst consisting of vanadium supported on titania. These processes are useful to control NO.sub.x emissions with the addition of ammonia being necessary. However this process is not useful to oxidatively destroy VNC's without the formation of NO.sub.x.

There is a need to develop improved catalytic oxidation processes capable of destroying VNC's which do not generate NO.sub.x emissions and thereby do not require further costly NO.sub.x abatement operations such as the one described in Rosenburg et al.

The present invention relates to a process for oxidatively decomposing VNC's without producing significant amounts of NO.sub.x emissions. The process of the present invention comprises catalytically oxidizing VNC's using a catalyst which includes a noble or base metal deposited on a catalyst support comprising zirconia or titania and promoted by additions of vanadium, molybdenum or tungsten in the presence of an oxidizing agent. Lanthanum is a preferred addition for thermal stabilization of the catalyst.

More particularly, a gaseous stream containing one or more VNC's is passed through a catalyst bed at a selected temperature range to obtain an oxidation reaction which selectively produces CO.sub.2, H.sub.2 O, N.sub.2, N.sub.2 O and trace amounts, if any of NO.sub.x products. The process may be operated at temperatures ranging from about 200 to 500 degrees C. depending upon the particular composition of the catalyst described above, the residence time, and the particular constituents present in the incoming gas stream as well as the concentration thereof.

Further, the process according to the present invention also is effective to decompose VNC's in a gas stream which includes certain gaseous hydrocarbons or NO.sub.x or a mixture thereof, wherein the compounds are reacted without producing significant amounts of NO.sub.x, and the NO.sub.x component in the feed stream is reduced.

Therefore the process and catalyst composition employed in accordance with the present invention can effectively decompose VNC's at relatively low operating temperatures without generating NO.sub.x in any significant amounts to permit control of VNC's and NO.sub.x emissions into the atmosphere in an economical manner which does not need a separate and costly NO.sub.x abatement operation.

FIG. 1 is a table showing the reaction products of a process according to the present invention decomposing hydrogen cyanide as a function of temperature using the method described in Example II over a selected temperature range.

The present invention relates to a novel catalytic oxidation process to control VNC emissions from industrial off-gas streams vented to the atmosphere without generating significant amounts of NO.sub.x. The process according to the present invention employs a catalyst composition which comprises a noble or a base metal supported on titania or zirconia and may be promoted with selected amount of molybdenum, tungsten, or vanadium. This catalyst composition has been discovered to possess the ability to effectively destroy VNC's in oxidizing environments without generating significant NO.sub.x emissions over selected relatively low temperature ranges.

In general, the catalyst compositions of the present invention range from about 70% to about 98% by weight zirconium oxide, titanium oxide, or combinations thereof.

In general, effective catalyst compositions contain about 0.03 to 5% of a noble metal or about 0.1 to 10% of a base metal which is impregnated onto either a titania or zirconia support. Between about 1 to 20% of molybdenum, tungsten or vanadium, or a combination thereof, is added as a promoter of the selective oxidation reaction and about 1 to 10% lanthanum is a preferred addition to promote thermal stability of the catalyst and appears to enhance the selectivity towards the formation of nitrogen among the reaction products. Generally, the catalyst may comprise about 0.1 to 10% by weight lanthanum. All percentages of catalyst components expressed herein are on a weight basis of the total formulation unless otherwise specifically designated.

A preferred catalyst formulation contains between 0.1 to 3% of a noble metal, such as palladium or platinum and between about 3 to 7% vanadium impregnated onto a titania support which forms the balance of the formulation. It is more preferred to include between 1 to 5% lanthanum. Tungsten can be substituted for vanadium or molybdenum but is less preferred than either of these components in the formulation.

The catalyst may be used in any configuration or size which sufficiently exposes the catalyst to the gas stream being treated. Preferably, the titania or zirconia support possesses a high surface area to obtain better dispersion of the components of the catalyst. The catalyst may be configured in many typical and well-known forms, such as for example, pellets, granules, rings, spheres or cylinders, or it may take the form of a coating on an inert carrier, such as spheres or monoliths. The monolithic form may be preferred when it is desired to reduce the pressure drop through the system or minimize attrition or dusting.

The catalytic components may be dispersed onto either the titania or zirconia support by means well known to the art. In general, it is desired that the promoters be impregnated onto the support first, followed by impregnation of the noble or base metals. For example, molybdenum, tungsten, or vanadium, or a combination of these, may be dispersed onto either the titania or zirconia support by impregnating granules with a solution containing one or both of these compounds. Following impregnation, the granules may be dried and/or calcined at the desired temperatures, then impregnated with a solution containing a base or noble metal. In both instances, the solution may be either aqueous or non-aqueous. Once the impregnation step is completed, the resulting catalyst may be dried and/or calcined.

When it is desired to add lanthanum to the catalyst, lanthanum may be added to the solution containing the molybdenum, tungsten and/or vanadium. Alternatively, the lanthanum impregnation may be performed either prior to or following impregnation with molybdenum, tungsten and/or vanadium.

If a monolithic form of the catalyst is desired, a slurry or solution of titania, zirconia, titania plus promoters or zirconia plus promoters may be first coated onto the monolith by means well known to the art. It is desirable that the amount of support material plus the promoters coated onto the monolith be in the range of about 25 to about 350 g/liter. The noble or base metal can be added in any convenient manner to the other components, but preferably is added last using well-known conventional means to accomplish uniform impregnation of the metal onto the coated monolithic support.

The process involves passing a gas stream containing VNC's plus an oxidizing agent, such as air, through a catalyst bed consisting of the catalyst described herein. The flow rates through the system should be sufficient to allow for greater than at least 90% and preferably greater than 95% destruction of the VNC's and any other undesirable compounds of interest. Thus, the gas hourly space velocity (GHSV) can vary significantly over a range of about 1,000 to about 300,000 hr.sup.-1 and preferably over a range of about 5,000 to about 60,000 hr.sup.-1.

The process described according to the present invention is also applicable to the injection of liquid nitrogen-containing compounds into a gas stream consisting of inert compounds plus an oxidizing agent, air for example. The gas stream flow rate and temperature, and rate of liquid injection are such as to allow for the vaporization of the nitrogen-containing compounds. The gas stream containing the vaporized nitrogen-containing compounds is then contacted with the catalyst described herein.

It should be noted that in the formulation of the catalyst, the components, particularly the noble or base metal, should be highly dispersed throughout the particular configuration used. The degree of metal dispersion can effect the efficiency of the chemical reaction desired. Further, the dispersion of the components on the form used can also effect the temperature range and the residence time required to obtain the desired conversion percentage of the VNC's being treated. Alternatively, the better dispersion of the metals can reduce the quantity of the components needed to achieve a given efficiency of the reaction at the same operating temperature and residence time.

It should also be noted that after the gas stream has been treated in accordance with the present invention, further treatment, if desired, may be effected to remove the smaller quantities of N.sub.2 O which may be required to achieve a future emission standard. Also halogen containing organic compounds included in the gas stream, including those containing atomic nitrogen, also can be oxidized in accordance with the present invention resulting in the production of acid gases. If the concentration of such acid gases in the exiting gas stream are deemed unacceptable, conventional collection or abatement processes may be employed to avoid venting acid gases directly into the atmosphere.

The reaction temperature range within which the process is operated is based on a number of factors which include the concentration of the target VNC to be decomposed, the reactivity level of the target VNC, the space velocity and the percentage of the noble or base metal associated with the catalyst. Generally, lower operating temperatures may be employed for VNC compounds which are readily oxidized by the catalyst or for those present in relatively low concentrations in the incoming gas stream, less than about 500 ppm for example. Further, the operating temperature may be reduced by decreasing the space velocity of the incoming gas stream and/or increasing the percentage of the base or noble metal component associated with the catalyst.

It should also be pointed out that the process parameters noted herein which include varying the composition of the catalyst with respect to the percentages of the promoter elements, such as molybdenum, tungsten and vanadium for example, also alter the selectivity of the nitrogen containing reaction products generated. This provides one the ability to design the process to achieve the most desirable result when actual operation in a particular industrial application tends to set certain limits on process parameters. Using certain catalyst compositions demonstrate, for example, that selectively producing very low percentages of NO.sub.x occur within a given temperature range and therefore higher or lower operating temperatures need to be avoided unless other operating parameters are appropriately adjusted, such as space velocity, for example. The relatively wide range of suitable operating conditions which produce useful results is a significant advantage in using the process according to the present invention.

It should also be noted that since oxidation reactions of the VNC's are exothermic, the temperature of the incoming gas stream to be treated should be adjusted to take into account the potential for the reaction temperature at the catalyst bed to be higher due to the heat generated by the chemical reactions so that the catalyst temperature does not exceed a level such that NO.sub.x formation becomes significant.

The composition of the catalyst reported in the following examples of the present invention is stated in percent by weight and was calculated based upon the elements described in the catalyst. Therefore an appropriate amount of a salt is used so that the weight percent of the metal component derived from the salt is included in the catalyst as described in the examples. When the solution of the salt is evaporated, the salt remains associated with the titania or zirconia support until calcination. At this point, the salts converted to metal and/or metal oxides. No formal analysis, such as atomic absorption, was performed to obtain an accurate measure of the catalyst composition. In view of the relatively wide range of catalyst formulations found to be operable within the general ranges disclosed, highly precise determinations of the catalyst compositions were not deemed necessary.

The selectivity of the nitrogen containing reaction products as noted herein is calculated on the basis of the available atomic nitrogen present in the VNC in the incoming stream.

The concentrations of CO.sub.2, N.sub.2 O, and N.sub.2 in the reactor effluent in the following examples described herein were determined using gas chromatographic techniques which employed packed columns to perform the separation and a thermal conductivity detector to quantitatively determine the product concentration. The concentration of VNC in the feed and effluent streams was determined using gas chromatographic techniques which employed a packed column to perform the separation. A flame ionization detector was used to provide quantitative analyses. The concentration of NO.sub.x in the reactor effluent was determined using a chemiluminescent NO/NO.sub.x analyzer which employed an optical filter and photomultiplier. These analytical techniques are well known to those skilled in the art.

Further, the addition of the promoters to the catalyst composition described herein have a slight retarding effect on the catalytic activity, however these components have been found to dramatically minimize NO.sub.x formation in the process according to the present invention. Also, the inclusion of a noble or base metal in the catalyst composition not only significantly enhances the reactivity of the catalyst, but further dramatically minimizes the formation of NO.sub.x in the reaction products. If either the noble or base metal or the promoters described herein are omitted from the catalyst composition, the generation of NO.sub.x in the reaction products is increased several hundred fold or the oxidation of the VNC is decreased several hundred fold under the same processing conditions. Therefore both of these constituents are required in the catalyst composition and cooperate to achieve the improved results of effectively decomposing VNC's while minimizing generation of NO.sub.x among the reaction products.

In view of the above description and the examples of the process according to the present invention which follow, it should be understood by those skilled in the art that the present invention provides a process and catalyst formulation which very effectively destroys VNC's without generating significant amounts of the undesirable NO.sub.x gases. Further, the catalyst formulations disclosed herein are not readily subject to poisoning by many organic compounds which may be present in a wide variety of industrial off-gas applications. The economic impact of such a process which does not require costly additional NO.sub.x abatement operations represents a novel and valuable contribution to the state of the art.

A catalyst was prepared on a weight basis containing nominally 1% platinum, 5% vanadium, 5% lanthanum with the balance titania as follows: 25 g of primarily anatase phase titania (Degussa p-25) with a surface area of approximately 50 m.sup.2 /g was slurried in 250 ml distilled, deionized water. To the slurry was added 2.9 g lanthanum nitrate hydrate dissolved in 30 ml distilled water. The slurry was then placed in a rotary evaporator at 45 degrees C. and the water was evaporated from the slurry overnight. The remaining solid was dried at 125 degrees C. for 2 hours, then crushed and sieved to 25/60 mesh granules. The granules were then calcined at 450 degrees C. for four hours. Approximately 8 g of the resulting granules were slurried in 200 ml distilled, deionized water. To the slurry was added approximately 0.9 g ammonium metavanadate dissolved in 80 ml distilled, deionized water. The slurry was then placed in a rotary evaporator at 60 degrees C. and the water was evaporated overnight. The remaining solids were dried at 125 degrees C. for two hours, then calcined at 450 degrees for four hours. Approximately 2.0 g of the resulting granules were slurried in 50 ml distilled, deionized water. Then 0.04 g tetraammineplatinum nitrate dissolved in 25 ml distilled, deionized water was added to the slurry. The slurry was placed in a rotary evaporator at 60 degrees C. and the water was evaporated overnight. The resulting material was dried at 125 degrees C. for two hours, then reduced in a hydrogen environment for two hours at 450 degrees C., then calcined at 450 degrees C. for two hours. Approximately one gram of the resulting material containing nominally 1% Pt, 5% V, 5% La supported on TiO.sub.2 was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 350 degrees C. At this temperature, the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 8 ppm NO.sub.x, 100 ppm N.sub.2 O, 970 ppm N.sub.2 and 2,100 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected.

A catalyst was prepared containing nominally 1% palladium, 5% vanadium, 5% lanthanum with the balance titania as follows: Approximately 2.0 g of the granules prepared containing (nominally) 5% vanadium, 5% lanthanum with the balance titania according to example I were slurried in 50 ml distilled, deionized water. Approximately 0.05 g tetraamminepalladium chloride dissolved in 10 ml distilled, deionized water was added to the slurry. The slurry was placed in a rotary evaporator at 60 degrees C. and the was evaporated overnight. The resulting material was dried at 125 degrees C. for two hours then reduced in a hydrogen environment at 450 degrees C. for two hours, then calcined at 450 degrees C. for two hours. Approximately one gram of the resulting material containing nominally 1% Pd, 5% V, 5% La supported on TiO.sub.2 was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min. The catalyst was exposed to the feed stream described at temperatures between 350 and 450 degrees C. The concentration of the reaction products formed at ten degree intervals are listed in FIG. 1. In the temperature range between 350 to 420 degrees C., greater than 99.95% of the hydrogen cyanide was destroyed without generation of more than 5 ppm of NO.sub.x. The catalyst was then exposed to 2,000 ppm hydrogen cyanide continuously for 24 hours at 370 degrees C. The conversion of hydrogen cyanide was greater than 99.95% throughout the duration of the run. The NO.sub.x selectivity was less than 1% throughout the duration of the run.

A catalyst was prepared containing nominally 5% chromium, 5% vanadium, 5% lanthanum with the balance titania as follows: Approximately 2.0 g of the (nominally) 5% V/5% La/TiO.sub.2 granules prepared according to example I were slurried in 50 ml distilled, deionized water. Approximately 0.76 g chromium nitrate nonahydrate dissolved in 25 ml distilled, deionized water was added to the slurry. The slurry was placed in a rotary evaporator at 60 degrees C. and the water was evaporated overnight. The resulting material was dried at 125 degrees C. for two hours, then reduced in a hydrogen environment at 450 degrees C. for two hours, then calcined at 450 degrees C. for two hours. Approximately one gram of the resulting material containing nominally 5% Cr, 5% V, 5% La supported on TiO.sub.2 was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 400 degrees C. At 400 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 19 ppm NO.sub.x, 560 ppm N.sub.2 O, 585 ppm N.sub.2 and 2,250 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at this temperature.

A catalyst was prepared containing nominally 1% palladium, 3% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 350 degrees C. At 350 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 7 ppm NO.sub.x, 75 ppm N.sub.2 O, 950 ppm N.sub.2 and 2,285 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at this temperature.

A catalyst was prepared containing nominally 1% palladium, 7% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 350 degrees C. At 350 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 11 ppm NO.sub.x, 221 ppm N.sub.2 O, 750 ppm N.sub.2 and 2,275 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at this temperature.

A catalyst was prepared containing nominally 1% palladium, 5% vanadium, with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 350 and 400 C. At 400 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 3.9 ppm NO.sub.x, 275 ppm N.sub.2 O, 725 ppm N.sub.2 and 2,200 ppm CO.sub.2. At 350 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 4.1 ppm NO.sub.x, 350 ppm N.sub.2 O, 675 ppm N.sub.2 and 2,200 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at either temperature.

A catalyst was prepared containing nominally 0.1% palladium, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 400 C. At 400 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 2.6 ppm NO.sub.x, 200 ppm N.sub.2 O, 665 ppm N.sub.2 and 1,825 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at either temperature.

A catalyst was prepared containing nominally 3% palladium, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 350 C. At 350 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of less than 0.5 ppm NO.sub.x, 135 ppm N.sub.2 O, 800 ppm N.sub.2 and 2,025 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at this temperature.

A catalyst was prepared containing nominally 1% palladium, 7% molybdenum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 330 and 370 degrees C. At 370 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 2.1 ppm NO.sub.x, 60 ppm N.sub.2 O, 825 ppm N.sub.2 and 1,950 ppm CO.sub.2. At 330 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 5.8 ppm NO.sub.x, 100 ppm N.sub.2 O, 850 ppm N.sub.2 and 2,000 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at either temperature.

A catalyst was prepared containing nominally 1% palladium, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,350 ppm (v/v) diethylamine in 21% O.sub.2 /He flowing at 200 ml/min at 350 degrees C. At 350 degrees C., the conversion of diethylamine was greater than 99.95%. The reaction product distribution consisted of 7.8 ppm NO.sub.x, 120 ppm N.sub.2 O, 850 ppm N.sub.2 and 7700 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at either temperature.

A catalyst was prepared containing nominally 1% palladium, 5% vanadium, 5% lanthanum with the balance zirconia in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 380 and 320 degrees C. At 380 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 50 ppm NO.sub.x, 100 ppm N.sub.2 O, 600 ppm N.sub.2 and 1950 ppm CO.sub.2. At 320 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of less than 0.5 ppm NO.sub.x, 80 ppm N.sub.2 O, 500 ppm N.sub.2 and 1,820 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at either temperature.

A catalyst was prepared containing nominally 1% palladium, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide and 750 ppm NO.sub.x in 21% O.sub.2 /He flowing at 200 ml/min at 350 and 390 degrees C. At 390 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The concentration of nitrogen and carbon species in the reactor effluent was as follows: 21 ppm NO.sub.x, 175 ppm N.sub.2 O, 1150 ppm N.sub.2 and 2,200 ppm CO.sub.2. At 350 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The concentration of nitrogen and carbon species in the reactor effluent was as follows: less than 0.5 ppm NO.sub.x, 100 ppm N.sub.2 O, 1225 ppm N.sub.2 and 2,175 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at either temperature. Results demonstrate that the catalyst and process are capable of reducing NO.sub.x in a process stream containing NO.sub.x, hydrogen cyanide and oxygen.

A catalyst was prepared containing nominally 1% palladium, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 500 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 310 and 350 degrees C. At 350 degrees C., the conversion of hydrogen cyanide was greater than 99.5%. The reaction product distribution consisted of 3.9 ppm NO.sub.x, 25 ppm N.sub.2 O, 210 ppm N.sub.2 and 475 ppm CO.sub.2. At 310 degrees C., the conversion of hydrogen cyanide was approximately 95%. The reaction product distribution consisted of 5.1 ppm NO.sub.x, 27 ppm N.sub.2 O, 200 ppm N.sub.2 and 465 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at these reaction temperatures.

A catalyst was prepared containing nominally 1% palladium, 10% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 340 and 400 degrees C. At 400 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 9 ppm NO.sub.x, 140 ppm N.sub.2 O, 775 ppm N.sub.2 and 2100 ppm CO.sub.2. At 340 degrees C., the conversion of hydrogen cyanide was approximately 99.95%. The reaction product distribution consisted of less than 0.5 ppm NO.sub.x, 170 ppm N.sub.2 O, 650 ppm N.sub.2 and 2100 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at these reaction temperatures.

A catalyst was prepared containing nominally 5% iron, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 400 degrees C. At 400 degrees C., the conversion of hydrogen cyanide was greater than 99.5%. The reaction product distribution consisted of 15.3 ppm NO.sub.x, 200 ppm N.sub.2 O, 600 ppm N.sub.2 and 2100 ppm CO=. No carbon monoxide or products of partial oxidation were detected at this reaction temperature.

A catalyst was prepared containing nominally 5% nickel, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 200 ml/min at 400 degrees C. At 400 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 6.8 ppm NO.sub.x, 210 ppm N.sub.2 O, 650 ppm N.sub.2 and 2125 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at this reaction temperature.

A catalyst was prepared containing nominally 1% palladium, 5% vanadium, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately 0.87 gram of the resulting material was exposed to 2000 ppm (v/v) cyanogen chloride in 21% O.sub.2 /He with 1.5% H.sub.2 O (v/v) flowing at 175 ml/min at 200, 300 and 400 degrees C. At 200 degrees C., the conversion of cyanogen chloride was greater than 99.9%. The reaction product distribution consisted of 20 ppm NO.sub.x, less than 5 ppm N.sub.2 O, 965 ppm N.sub.2 and 1950 ppm CO.sub.2. At 300 degrees C., the conversion of cyanogen chloride was greater than 99.9%. The reaction product distribution consisted of 145 ppm NO.sub.x, less than 5 ppm N.sub.2 O, 900 ppm N.sub.2 and 1950 ppm CO.sub.2. At 400 degrees C., the conversion of cyanogen chloride was greater than 99.9%. The reaction product distribution consisted of 240 ppm NO.sub.x, 210 ppm N.sub.2 O, 575 ppm N.sub.2 and 1950 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at these reaction temperatures. No determination or measurement was made of the concentration of HCl which was present in the exiting treated gas stream.

A catalyst was prepared containing nominally 1% palladium, 3% tungsten, 5% lanthanum with the balance titania in a manner similar to that described previously. Approximately one gram of the resulting material was exposed to 2,000 ppm (v/v) hydrogen cyanide in 21% O.sub.2 /He flowing at 100 ml/min at 340 degrees C. At 340 degrees C., the conversion of hydrogen cyanide was greater than 99.95%. The reaction product distribution consisted of 75 ppm NO.sub.x, 85 ppm N.sub.2 O, 800 ppm N.sub.2 and 2,100 ppm CO.sub.2. No carbon monoxide or products of partial oxidation were detected at either temperature.

It should be noted that other formulations of the catalyst used within the parameters described herein could be successfully employed in the process according to the present invention as well as choosing other operating parameters to meet a given application and level of effectiveness suitable to the application without departing from the spirit of the present invention. The selective oxidation achieved to produce the lower levels of NO.sub.x generated in the reaction products is generally most desirable. This selectivity of the components formed by the oxidation reactions which can readily reduce the amount of NO.sub.x in the exiting treated gas stream represents a significant advantage over prior abatement processes used to treat VNC ladened gas streams.