IN A GASEOUS STREAM

FIELD OF THE INVENTION

The present invention relates to pollutant control and more particularly to methods and systems for the reduction of nitrogen dioxide (NO2) to nitric oxide (NO) in a NO ₂ -containing gaseous stream.

BACKGROUND OF THE INVENTION

ΝΟχ generally refers to a mixture of nitric oxide (NO), nitrogen dioxide (NO2) and nitrous oxide (N ₂ O). The lifespan of NO _x components in the atmosphere typically ranges from one to seven days for NO and NO2, and to 170 years for N ₂ O. NO has no color, odor, or taste, and is relatively non-toxic. In the presence of air, NO is rapidly oxidized to NO2. NO2 is a reddish brown pollutant with high reactivity. NO2 is also a strong oxidizing agent that can form the corrosive nitric acid, as well other toxic organic nitrates. Further, NO2 is a well-known pulmonary irritant affecting the human respiratory system, which may exacerbate asthma and other respiratory conditions. Still further, NO2 absorbs light, is a main component of smog, and is sometimes seen as the yellow- brown haze hanging over cities or as the yellow plume in the stack downstream of a gas turbine. In such instances, NO ₂ may be found in concentrations above 10-12 ppm.

Numerous technologies exist to reduce NO _x components in gaseous streams, particularly exhaust streams from the combustion of fuel. Many of those solutions primarily focus on the reduction of the NO _x components down to N ₂ . Moreover, NO2 tends to be more abundant in exhaust streams at start up, lower temperatures, and part loads. The reduction of NO2 to NO (NO2 -> NO + ½ O2), however, is poorly understood and controlled. In one study, Bamwenda et al., React. Kinet. Catal. Lett. 63:1 pp. 53-59 (1998) examined the reduction of NO2 by C3H6 in the presence of O2 over alumina- supported Au, Rh and Pt. The authors, however, only achieved a reduction efficiency of up to 50% at 400° C before gradually falling off with temperature. Further, a drawback of injecting a substantial amount of an organic compound into an exhaust stream is the formation of hydrocarbons and other byproducts that need to be treated in order to comply with environmental regulations, as well as any excess of the organic compound itself in the stream. Improved solutions for reducing NO2 to NO are thus needed to reduce NO ₂ to NO with higher efficiency without generating significant pollutants.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention is explained in the following description in view of the drawings that show:

FIG. 1 is a schematic view of a system for carrying out a process for reducing NO2 to NO in accordance with an aspect of the present invention.

FIG. 2 shows the NO ₂ to NO conversion efficiency with an inlet CO concentration of about 75 ppm.

FIG. 3 is a graph showing NO2 to NO reduction efficiency (when CO is used as a reducing agent) and CO to CO2 conversion efficiency versus temperature at transient conditions (about 1 .4° C/minute).

DETAILED DESCRIPTION OF THE INVENTION

In one aspect, the present inventor has surprisingly found that the presence of effective amounts of both carbon monoxide and an organic compound in a NO ₂ - containing gaseous stream synergistically improves the efficiency of the reduction of NO2 to NO over a platinum group catalyst relative to that of known methods and relative to the use of the reducing agents (CO and an organic compound) individually.

Advantageously, the processes and systems described herein may achieve about 75% and even up to about 99% NO ₂ reduction efficiency across a low to high temperature range, such as from about 50° C to about 600° C. In particular embodiments, the processes provide high efficiencies at low temperatures (less than about 150° C), thereby providing an excellent NO2 reduction tool during start up of a gas turbine or its operation at low loads. In addition, the present inventor has found that certain organic compounds, utilized with or without CO, can provide excellent reduction efficiencies for NO2 across a range of temperatures. In particular embodiments, the organic compound may comprise an alcohol, such as methanol; an aldehyde such as formaldehyde; and/or an aromatic hydrocarbon, such as toluene. As described in detail below, these particular organic compounds had particularly surprising results, with or without CO, to reduce NO ₂ to NO.

Further, the present inventor has surprisingly found that organic compounds, including hydrocarbons, and carbon monoxide, if present, in the subject gaseous stream can also be efficiently oxidized to CO ₂ and water, particularly at temperatures greater than about 150° C. CO oxidation efficiency may, in fact, reach levels of about 90% at about 270° C, and higher oxidation efficiencies may be realized in the range of about 420° C to about 600° C. Thus, the processes and systems described herein can substantially reduce NO ₂ levels, particularly at low temperatures, e.g., less than about 150° C, and can reduce NO2, CO, and organic compound emissions across a large temperature range of about 150° C to about 600° C, thereby resulting in a substantially cleaned gaseous stream.

As used herein, the term "about" refers to values that are ± 1 % of the stated value.

As used herein, the term "aldehyde" refers to a compound comprising at least one unsaturated carbonyl group (C=O).

As used herein, the term "alcohol" refers to a compound comprising at least one carbon bonded to at least one hydroxyl group.

As used herein, the terms "amount effective," "effective amount," or the like means an amount or concentration necessary to achieve the desired result(s).

As used herein, the term "aromatic hydrocarbon" preferably means a molecule comprising carbon atoms and hydrogen atoms, and having one or more aromatic rings.

As used herein, the term "organic compound" refers to a carbon-based

compound. It is noted, however, that the term "organic compound" does not include carbon-based molecules that are considered inorganic, such as carbon monoxide, carbon dioxide, carbonates, cyanides, cyanates, carbides, and thyocyanates.

In one aspect of the present invention, there is provided a process for reducing NO2 to NO in a NO2-containing gaseous stream. The process comprises contacting the gaseous stream with a catalyst bed comprising a catalyst selected from a platinum group metal in the presence of (a) carbon monoxide; (b) an organic compound; or (c) carbon monoxide and an organic compound. FIG. 1 illustrates an exemplary system for carrying out this process. It is understood, however, that the invention is neither so limited to the illustrated system of FIG. 1 nor are all shown components in FIG. 1 required. It would be readily appreciated by one skilled in the art that a greater or lesser number of components may be utilized.

Referring again to FIG. 1 , there is shown a system 10 comprising a gas turbine 1 1 that produces a gaseous stream 12, e.g., exhaust gas 14, which comprises NO2 and which may be directed to a heat recovery steam generator (HRSG) 16 as is known in the art, which includes or is otherwise located upstream of a catalyst bed 18 (or SCR bed 18). Typically, the catalyst bed 18 is positioned at a location suitable for a desired SCR temperature operating range. The exhaust gas 12 passes to the catalyst bed 18 where one or more catalysts promote the reduction of NO2 to NO and the oxidation of CO and organic compounds to CO ₂ and water in the presence of an organic compound and/or CO as shown. Alternatively, the reduction of NO2 to NO may take place in the presence of the organic compound or CO individually, and the excess organic compound or CO may be oxidized. A cleaned exhaust gas 20 is emitted from an outlet of the SCR bed 18.

To provide the organic compound to the exhaust stream 12, the system 10 optionally includes one or more injectors for injecting the organic compound 22 into the exhaust stream 14 from a suitable organic compound source. It is understood that in certain embodiments, a sufficient amount of CO for the reaction may already be included within the exhaust stream 12. Alternatively, one or more injectors for injecting all or a portion of the required carbon monoxide 24 into the exhaust stream 14 from a suitable CO source may also be provided as shown. In certain embodiments, oxygen 26 may further be added to the exhaust stream 14 via one or more injectors as shown. Optionally also, a controller may be associated with one or more sensors and valves to sense the amount of carbon monoxide and/or organic compound present in the gaseous stream 12 at any location and point in time (not shown). In this way, the controller may maintain desired amounts of the components in the gaseous stream 12. As is described in more detail below, the catalyst bed 18 comprises a catalyst system 28 having long-term stability for reducing NO2 to NO, and optionally oxidizing organic compounds and CO to CO2 and water, when exposed to the exhaust stream 14.

Although the gaseous stream 12 comprises a flowing exhaust stream 14 that is the result of a combustion process in FIG. 1 , it is understood that the gaseous stream 12 may comprise any other gaseous phase or a mixture of a gaseous and a liquid phase comprising at least an amount of NO2 - whether flowing or stationary. It is also appreciated that the gaseous stream 12 may include other components, such as carbon monoxide, carbon dioxide, molecular nitrogen, water vapor, molecular oxygen, O-, S-, and N-containing compounds, and incompletely combusted fuel, for example.

The catalyst bed 18 comprising a catalyst system 28 may be disposed in any suitable form. In one embodiment, the catalyst bed 18 is a selective catalytic reduction (SCR) bed as is well-known in the art. The catalyst bed 18 may be in a geometric form that allows for high NO _x reduction efficiency along with a minimal pressure drop.

Although beads, extrudates, etc. are suitable geometric forms employed in commercial applications, a monolith is a preferred form. The monolithic form and the use of a monolith as a catalyst carrier are well known to one skilled in the art. A monolith comprises a series of straight, non-interconnecting channels. Typically, a thin layer of a catalyst-containing material, termed "washcoat" by the trade, is coated onto the walls of the monolith.

In certain embodiments, the catalyst system 28 may comprise at least one catalyst, a binder, washcoat particles, and optionally, a promoter. The catalyst may comprise one or more members of the platinum group metals, namely ruthenium, rhodium, palladium, osmium, iridium, and platinum. In one embodiment, the catalyst comprises one or more of the palladium-group platinum group elements (Rh, Pt, Pd). In a particular embodiment, the catalyst comprises platinum. It is appreciated that additional catalysts known in the art may be included in the catalyst system 28. The inventor has found that a catalyst system comprising at least a platinum catalyst provides optimum results for reducing NO2, and also for oxidizing CO and organic compounds. Typically, the catalyst is provided in an amount effective to optimally facilitate the reduction of NO ₂ to NO, and also the oxidation of CO to CO ₂ and organic compounds to CO2 and water. In one embodiment, the platinum group catalyst is provided in an amount from about 0.5 to about 20 wt % of the catalyst bed 18, and in a particular embodiment from about 0.5 to about 5 wt % of the catalyst bed 18.

The washcoat particles may be any suitable particles known in the art, such as well-known metal oxide (e.g., Al, Mg, and/or Si oxides) or zirconia-based washcoat particles. In one embodiment, the washcoat particles comprise alumina particles. In another embodiment, the washcoat particles comprise zirconia, sulfated-zirconia, and/ or sulfated-zirconia-silica oxides.

Binders may be used to adhere the solid catalyst support material to the substrate, e.g., monolithic substrate. Conventional binders include clays, aluminas, silicas, zirconias, and the like. In one embodiment, the binder comprises a pre-sulfated zirconia binder as was described in U.S. Patent Application Publication No.

20090285735, the entirety of which is hereby incorporated by reference. The binder may be provided in the catalyst system 28 in any suitable quantity, such as a mass ratio of the binder to the catalyst system of between about .001 and about .04. Optionally, the catalyst system 28 may also comprise a promoter. The promoter may comprise one of tungsten, zinc, titanium, and combinations thereof, for example. In one embodiment, the promoter is tungsten and the tungsten loading is in the range of from about 0.5 to about 5.0 wt. % of the catalyst system 28. It is appreciated that the addition of a small amount of a promoter may aid in reducing the oxidation efficiency of the catalyst when desired.

The present inventor has found that effective amounts of carbon monoxide, an organic compound, or an organic compound and carbon monoxide, significantly improve the reduction efficiency of the conversion of NO ₂ to NO over a platinum group metal catalyst, particularly at low temperatures (about 150° C or less). In certain embodiments, the reduction of NO2 to NO takes place in the presence of effective amounts of both an organic compound and carbon monoxide. The present inventor has surprisingly found that the presence of effective amounts of both carbon monoxide and an organic compound in a NO2-containing gaseous stream dramatically improves the reduction efficiency of the conversion of NO2 to NO over a platinum group catalyst relative to that of known methods and relative to the use of the reducing agents (CO and an organic compound) individually. As shown in the Examples below, for example, 75 ppm of CO alone at 50° C provided a reduction efficiency of 0% (See Table 1 ) while 10 ppm of toluene alone at 50° C provided a reduction efficiency of 31 % (See Table 2). Added together, however, 75 ppm of CO and 10 ppm of toluene at 50°C provided a substantially greater than additive effect and synergistically provided a reduction efficiency of 98% (See Table 3). These results show that, in one aspect, effective amounts of CO and an organic compound may be utilized to reduce NO2 to NO over a platinum group catalyst even at very low temperatures, e.g., 50° C. As shown in Examples 5 and 6, effective amounts of methanol and formaldehyde, respectively, in combination with an effective amount of CO also provided desirable results.

In addition, the present inventor has found that the reduction efficiency may be improved over known methods, with or without CO, when the organic compound is in the form of an alcohol, an aldehyde, and/or an aromatic hydrocarbon, such as one or more of methanol, formaldehyde, and/or toluene. In contrast, the inventor found that certain aliphatic hydrocarbons, such as methane, did not provide the same optimal reduction efficiencies for NO2. In one embodiment, the organic compound comprises an alcohol, and the alcohol comprises methanol. In another embodiment, the organic compound comprises an aldehyde, and the aldehyde comprises formaldehyde. In still another embodiment, the organic compound comprises an aromatic hydrocarbon, and the aromatic hydrocarbon comprises toluene.

The amount of the organic compound present should be any amount effective to reduce an amount of NO2 to NO with a greater efficiency than without the organic compound. In one aspect, when the gaseous stream 12 is in contact with the catalyst bed 18, the amount of the organic compound in the gaseous stream 12 is at least 1 ppm, and in a particular embodiment is at least 5 ppm.

If present, the amount of CO present for the reduction of NO to NO2 is at least an amount effective to increase the reduction efficiency of NO ₂ to NO relative to the reduction efficiency of NO2 to NO of the associated process without CO. In one embodiment, the amount of the CO in the gaseous stream 12 present during the contacting of the gaseous stream with the catalyst is at least about 5 ppm. In a particular embodiment, the amount of the CO present is at least about 75 ppm. In embodiments where both CO and an organic compound are utilized for the reduction of NO2 to NO, the ratio of the CO to the organic compound present may be any suitable amount effective to reduce an amount of NO2 to NO. In one embodiment, the ratio of CO to organic compound is at least about 2:1 . This may be based upon the ppm of each component in the gaseous stream 12, although the invention is not so limited.

It is appreciated that in certain embodiments, a portion of CO and/or the organic compound for the reduction of NO2 to NO may already be present in the gaseous stream 12, particularly when the gaseous stream 12 is an exhaust stream 14 from the combustion of a natural gas-containing fuel. Thus, it is contemplated that, in certain embodiments, a portion of the CO and/or the organic compound may not be required to be intentionally added to the gaseous stream 12, e.g., exhaust stream 14, as was shown in FIG. 1 . In a particular embodiment, when CO is also used as a reducing agent, the effective amount of CO for the reduction of NO ₂ to NO is already present in the exhaust stream 14.

Advantageously, the reduction of NO2 and NO may take place over a wide range of temperatures. In one embodiment, aspects of the present invention are particularly beneficial in reducing NO ₂ to NO at a temperature of from about 50° C to about 600° C. In a particular embodiment, the contacting of the gaseous stream 12 with the catalyst bed 18 in the presence of CO, an organic compound, or CO and an organic compound, is done at a temperature of about 150° C or less. In this way, the reduction of NO2 utilizing CO and/or an organic compound, and a platinum group metal catalyst can occur at temperatures associated with the start up of a combustion engine or its operation at part or low loads where NO2 levels are generally relatively high. As can be seen in the examples below, the reduction efficiency of NO2 to NO rapidly increases starting from 50 to 75° C in the presence of CO, an organic compound, or CO and an organic compound, over a platinum group catalyst. Thus, the reduction efficiency can be very high even at lower temperatures.

It is appreciated that at least a portion to all of an effective amount of oxygen may already be present in the gaseous stream 12. In one embodiment, the oxygen is added to the gaseous stream 12 at a point upstream from the catalyst bed 18 as was shown in FIG. 1 ; however, it is understood that the present invention is not so limited. In certain embodiments, the effective amount of oxygen is at least about 1 % by volume of the gaseous stream 12. In other embodiments, the amount of oxygen may be at least about 10% by volume of the gaseous stream.

While the present inventors have found that the presence of CO in combination with an organic compound aids in reducing NO2 to NO, it may also be desirable for excess of the organic compound(s), any byproducts, such as hydrocarbons, and CO in the gaseous stream 12 to be oxidized before release into the environment. The presence of oxygen in certain embodiments thus assists in the oxidation of the organic compound(s) and CO to a product comprising CO2. As shown in the examples below, for example, the CO and the organic compound rapidly increase NO2 to NO reduction efficiency at temperatures of about 150° C or less. At a temperature of about 150° C, the conversion efficiency of NO ₂ to NO plateaus and the conversion of CO to CO ₂ rapidly increases until about 300° C, and then even further increases at a temperature of from about 400 to about 600° C. Thus, at temperatures lower than about 150 ^° C, the CO aids in the reduction of NO2 to NO. Thereafter, particularly at temperatures of about 150 to about 600 ^° C, CO (and also organic compounds) may be oxidized to a product comprising CO2.

In view of the above, there are provided numerous systems and processes for reducing NO2 to NO in a NO2-containing gaseous stream, which are particularly useful at the low temperatures associated with start up of a gas turbine and its operation at low or part loads to reduce yellow plume. In one aspect, there is provided a process for reducing NO2 to NO in a NO2-containing gaseous stream. The process comprises contacting the gaseous stream with a catalyst system comprising a catalyst selected from a platinum group metal. The contacting is done in the presence of at least an organic compound, and in certain embodiments, CO and an organic compound. The carbon monoxide and/or the organic compound may be present in an amount effective to reduce NO2 to NO in the gaseous stream with a reduction efficiency of at least about 75%. In certain embodiments, the reduction efficiency is at least about 90%, and in further embodiments is at least about 98%. In one aspect, the reduction takes place at a temperature of about 150° C or less, which is particularly suitable to reduce NO2 emissions at start up or part load of a gas turbine. In certain embodiments, the organic compound is selected from the group consisting of an alcohol, an aldehyde, an aromatic hydrocarbon, and combinations thereof. In a particular embodiment, the organic compound may be selected from the group consisting of methanol, formaldehyde, toluene, and combinations thereof.

In accordance with another aspect, there is provided a process for reducing NO2 to NO in a NO ₂ -containing gaseous stream. The process comprises contacting the gaseous stream with a catalyst system comprising a catalyst selected from a platinum group metal in the presence of an effective amount of an organic compound. The organic compound may be selected from the group consisting of an alcohol, an aldehyde, and an aromatic hydrocarbon, such as methanol, formaldehyde, and toluene, respectively.

In accordance with another aspect, there is provided a process for reducing NO2 to NO in a NO2-containing gaseous stream. In this embodiment, the process comprises intentionally adding an amount of a CO and/or an organic compound to the gaseous stream. The process also includes contacting the gaseous stream with a catalyst system comprising a catalyst selected from a platinum group metal, wherein the catalyst, carbon monoxide, and/or organic compound are present in an amount effective to reduce an amount of NO2 to NO in the gaseous stream.

Although the above invention was described in the context of the power generation field with specific emphasis on the treatment of gas turbine exhaust, the novel processes as described herein may be applied to other NO _x pollution sources comprising an amount of NO2, such as for example nitric acid plants and stationary emissions sources, with different system configurations.

In any of the embodiments contemplated herein, the processes may further comprise oxidizing an amount of CO to CO2 and/or organic compounds in the exhaust stream to CO2 and water in the presence of oxygen to lower an amount of CO and/or organic compounds in the gaseous stream 12, particularly before release of the gaseous stream 12 to the atmosphere in the case of an exhaust gas 14. In certain embodiments, the reduction efficiency of the conversion of NO2 to NO rapidly increases at a temperature of about 50° C to about 150° C while the oxidation efficiency of the conversion of CO to CO2 and organic compounds to CO2 and water rapidly increases at a temperature of from 150 to 300° C and may be carried out to 600° C.

The below examples are provided to illustrate certain aspects of the present invention and are not intended to be limiting in any respect.

EXAMPLE 1

The preparation of a catalyst bed having 5.0g Pt / ft ³ on a monolith substrate was prepared. The prepared catalyst bed was then utilized to generate the data in each of the following examples. First, a platinum metal solution was prepared by adding to a beaker 0.13 g tetraamine platinum chloride (55.46% Pt), 0.3 g TEA (Triethanolamine, Ashland), and the resulting solution was diluted to 50 g total with deionized (Dl) water. Monolithic honeycomb substrate had 1 10 CPSI (cells per square inch) and had in its composition primarily Al, Mg, and Si oxides. The monolith block was dipped in the platinum solution. The calculated loading on monolith substrate was 5.2g Pt / ft ³ .

Thereafter: 1 ) the block was microwave dried; 2) the block was placed in a furnace at 250°C; 3) the furnace was ramped to 450°C at a rate of 50°C/hr; 4) the temperature was held at 450°C for 2 hours; and 5) the furnace was ramped to 100°C at a rate of about 35°C/hr.

EXAMPLE 2 (CO alone as reducing agent)

Example 2 illustrates the conversion of NO2 to NO when CO alone is used as the reducing agent. The results and conditions are shown in FIG. 2 and Table 1 below. As shown in FIG. 2, with an inlet concentration of 75 ppm CO, the NO ₂ to NO conversion efficiency dramatically increases from 75 to 150° C. To generate the data in FIG. 2 and Table 1 , the above-described Pt catalyst was used; inlet concentration of NOx was 20 ppm; 80% of NO ₂ was in the NO _x mixture; GHSV was about 20,000 hr ^"1 ; and O ₂ concentration was about 10% by vol.; and the balance was N ₂ .

Table 1 . Influence of CO concentration in the flow on NO2 to NO % Conversion Efficiency (%)

CO, % NO ₂ Reduction Efficiency

EXAMPLE 3 (Toluene as reducing agent)

Next, the influence of toluene concentration in the flow and temperature on NO to NO ₂ conversion efficiency (%) was determined by varying the toluene concentration and temperature under the conditions described below in Table 2.

Table 2. Influence of toluene concentration in the flow on NO ₂ to NO % Conversion Efficiency; Pt Catalyst; Inlet concentration of NOx 20 ppm; 80% of NO ₂ in the NOx mixture; GHSV - 20,000 hr ^"1 ; O ₂ ~10% by vol.; and the balance was N ₂ .

EXAMPLE 4 (Toluene and CO as reducing agents) Next, the synergistic effect of the concentration of toluene and CO in the flow on NO to NO ₂ conversion efficiency (%) was determined by varying the toluene

concentration and temperature under the conditions described below in Table 3.

Table 3. Synergetic effect of CO and toluene in the flow on NO ₂ to NO %

Conversion Efficiency; Pt Catalyst; Inlet concentration of NO _x 20 ppm; 80% of NO ₂ in the ΝΟχ mixture; GHSV - 20,000 hr ^"1 , O ₂ ~10% by vol.; and the balance was N ₂ .

I I 10 I 98j 99j

As shown, 75 ppm of CO alone at 50° C provided a reduction efficiency of 0% (See Table 1 ) while 10 ppm of toluene alone at 50° C provided a reduction efficiency of 31 % (See Table 2). Critically, 75 ppm of CO and 10 ppm of toluene at 50°C provided a substantially greater than additive effect and synergistically provided a reduction efficiency of 98% (See Table 3). This was a dramatic increase in efficiency. Also, 75 ppm of CO alone at 75° C provided a reduction efficiency of 3% (See Table 1 ) while 5 ppm of Toluene alone at 75° C provided a reduction efficiency of 90% (See Table 2). Added together, however, 75 ppm of CO and 5 ppm of toluene at 75°C also provided a greater than additive effect and synergistically provided a reduction efficiency of 99% (See Table 3).

EXAMPLE 5 (Methanol and CO as reducing agents) Next, the influence of methanol and CO concentration in the flow and

temperature on NO to NO ₂ conversion efficiency (%) was determined by varying the methanol concentration and temperature under the conditions described below in Table 4.

Table 4. Synergetic effect of CO and methanol in the flow on NO ₂ to NO %

Conversion Efficiency; Pt Catalyst; Inlet concentration of NOx 20 ppm; 80% of NO ₂ in the NOx mixture; GHSV ~ 20,000 hr ^"1 ; O ₂ ~10% by vol.; and the balance was N ₂ .

EXAMPLE 6 (Formaldehyde and CO as reducing agents) Next, the influence of formaldehyde and CO concentration in the flow and temperature on NO to NO ₂ conversion efficiency (%) was determined by varying the formaldehyde concentration and temperature under the conditions described below in Table 5. Table 5. Synergetic effect of CO and formaldehyde in the flow on NO ₂ to NO % Conversion Efficiency; Pt Catalyst; Inlet concentration of NO _x 20 ppm; 80% of NO ₂ in the NOx mixture; GHSV - 20,000 hr ^"1 ; O ₂ ~10% by vol.; and the balance was N ₂ .

EXAMPLE 7

The NO ₂ to NO conversion efficiency (%) when CO is used as a reduction agent (160 ppm) and CO conversion efficiency (%) versus temperature was measured at transient conditions (1 .4°C/min). The results are fully shown in FIG. 3. The conditions were: Pt Catalyst; Inlet concentration of NOx 20 ppm; 80% of NO ₂ in the NOx mixture; GHSV ~ 20,000 hr ^"1 , O ₂ concentration was -10% by vol.; and the balance was N ₂ . As shown, the reduction of NO ₂ to NO rapidly increases at temperatures from 50 to 150° C while the oxidation of CO to CO ₂ rapidly increases at temperatures ranging from 150 to 300° C. At temperatures of from 300° C or more, both NO ₂ is reduced and CO is oxidized at favorable efficiencies.

While various embodiments of the present invention have been shown and described herein, it will be obvious that such embodiments are provided by way of example only. Numerous variations, changes and substitutions may be made without departing from the invention herein. Accordingly, it is intended that the invention be limited only by the spirit and scope of the appended claims.