CATALYSTS AND METHODS FOR LOW-TEMPERATURE DESTRUCTION OF VOCs IN AIR AND SELECTIVE REMOVAL OF CO

Abstract: Catalyst compositions useful for destruction of volatile organic carbons (VOCs) in an oxygen-containing gas stream at low temperatures and for selective oxidation of carbon monoxide from a hydrogen-containing gas comprising: one or more first metals selected from the group consisting of: Ce and Zr; and at least one of: a) one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; b) one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and c) one or more fourth metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and Ir are provided. Catalyst compositions provided may be single-phase, mixed-metal oxides, or multi-phase.

Description: CATALYSTS AND METHODS FOR LOW-TEMPERATURE DESTRUCTION OF VOCs IN AIR AND SELECTIVE REMOVAL OF CO BACKGROUND OF THE INVENTION This invention relates generally to catalysts useful for destruction of volatile organic compounds (VOCs) and selective removal of carbon monoxide. Contamination ofthe environment by volatile organic compounds (VOCs) is of great concern. VOCs originate in many ways, including spray painting and engine maintenance (degreasing and fuel li i repair), indoor air decontamination, dry cleaning, food processing (grills and deep fryers), fume hoods, residential use and solvent-intensive industrial processes. VOCs have direct and secondary (e.g. photochemical smog) effects on health and the environment. Direct methods for removing VOCs from contaminated air require heating the air stream to relatively high temperatures to incinerate the contaminants. The cost required to maintain such elevated temperatures (around 815 to 925 °C) and to cool the surroundings can be unacceptably high. Various catalysts have been studied for their use in lower-temperature removal of VOCs (see, for example, Spivey, JJ. (1987) Ind. Eng. Chem. Res. 26:2165-2180). The catalytic properties of ceria and Ceθ2 containing materials have been reviewed (Trovarelli, A. (1996) Catal. Rev. Sci. Eng. 38(4):439-520; Bernal, S. et al. (1999) Catal. Today 50:175; Trovarelli, A. et al. (1999) Catal. Today 50:353-356). Pure Ceθ2 is reported to be active for the oxidation of CO over the temperature range of 200° to 500°C (Liu, W. and Flytzani-Stephanopoulos, M. (1995) J. Catal. 153:304-316). However, temperatures of at least 300°C were reported to be necessary for methane oxidation using compositions such as Ceo.2Zro.sOχ 3 Cuo.θ8[Ce(La)]o.92θ x , Cun.5[Ce(La)]o.5θ x and Cuo.5Zro.5Ox (where Ce(La) indicates cerium containing 1.5 wt% lanthanum) (Liu, . and Flytzani-Stephanopoulos, M. (1995) J. Catal. 153:304-316). Cerium oxide doped with 10% Zr, 50% Zr, 4.5% La or 10% La, and cerium oxide (doped with Zr or La as above)-supported silver (2-5% Ag) or copper (5-15%) catalysts have been studied for the combustion of methane (Kundakovic, Lj. and Flytzani-Stephanopoulos, M. (1998) J. Catal. 179:203-221). Temperatures of at least 400°C were required for any appreciable oxidation of methane using these materials. Ceθ2~Zrθ2 mixed oxides in proportions of Ceo.92Zro.O8O2 to Ceo.5Zro.5O2, and Ceo.76Zro.l9(Mn or Cu)o.θ5θ2-χ have been reported for use in oxidation of C1-C4 hydrocarbons (Terribile, D. et al. (1999) Catal. Today 47:133-140). Temperatures of about 650 to about 800K were reported to be required for 50% conversion of methane, ethane, propane, butane and isobutane. United States Patent No. 5,283,041 describes a ternary compound of vanadium oxide (0.01 to 20 weight percent), zirconium oxide (40 to 88 weight percent) and either manganese oxide, cerium oxide and cobalt oxide (3 to 48 weight percent). Platinum, palladium and rhodium may also be present from 0.01 to 5 weight percent. This compound is used to treat gas streams containing halogenated organic compounds with temperatures of 175 °C to 550° C. United States Patent No. 5,491,120 describes an inert carrer with a BET surface area of at least 10 m^/g used to support a coating of bulk ceria with a BET surface area of at least 10 rn^/g and one or more bulk metal oxides which are either titania, zirconia, ceria-zirconia, silica, alumina-silica or α- alumina metal oxide for oxidizing components of a gas stream, in particular a diesel engine exhaust. United States Patent No. 5,851,948 describes an inert porous support such as alumina or silica having a surface area of 10 - 400 m2/g used to support a catalyst composition of 0.5 to 15 wt % of chromium, cobalt, copper, cerium or iron oxide covered with a thin (at most 0.1 mm thick) layer of Pd, Pt, Ru or Rh (concentration of 0.01 to 2 wt %). United States Patent No. 5,627,124 describes a composition of ceria and alumina (each having a surface area of at least 10 m^/g and being 5 to 95 percent ofthe composition) coated on a refractory carrier for pollution abatement of exhausts containing unburned fuel or oil. United States Patent No. 5,882,616 describes perovskites ofthe formula XYO3, where X is lanthanum, cerium or yttrium, and Y is a transition metal such as copper, chromium, manganese, iron, cobalt and nickel supported on a support such as alumina, silica, magnesium aluminate, titanium oxide, zirconium oxide and mixtures thereof. Even with somewhat advanced materials, the technologies currently used for reduction of VOCs from contaminated air still require heating the air stream to relatively high temperatures to reduce the concentration of VOCs. Hydrogen powered polymer electrolyte membrane fuel cells (PEMFCs) are useful for power generation due to their high efficiency and power density, low emissions, low operating temperature, small size, and portability. Because of these characteristics, hydrogen PEMFCs are being developed for both mobile and stationary applications. Natural gas or methanol are more practical fuels than hydrogen for commercial devices because of storage and transportation issues. If natural gas or methanol is used as fuel sources for PEMFCs, a reforming step is first used to convert the fuel to hydrogen prior to entering the cell. Unfortunately, the carbon monoxide which is produced along with hydrogen in the reforming step degrades PEMFC performance. The vast majority of published work addressing the catalytic oxidation of CO has not considered selectivity in the presence of hydrogen. In the early 1980s, Stark et al. reported that Pt supported on SnO x was an effective CO oxidation catalyst. Hoflund et al. also studied the Pt/SnO x system and compared it to Au/MnO x . They reported that Au/MnO x was more active and had a longer lifetime than Pt/SnO x . The most significant results reported were that the Au/MnO x catalyst produced nearly 60% conversion of CO to CO 2 at only 35 °C and increasing the temperature to 55°C produced over 80% conversion to C0 2 . Haruta et al. also have performed extensive testing on supported Au catalysts for oxidation of CO. Using ultra-fine gold particles dispersed on the oxides of Fe, Co and Ni, they reported activity for the oxidation of CO at only -70°C. Since Au alone is known to be inactive towards oxidation, and the metal oxides used in the above studies have very limited activity, the results obtained by Hoflund et al. and Haruta et al. underscore the synergistic effects between the metal and support material. Selective CO oxidation in the presence of H has not been as thoroughly investigated as low- temperature oxidation activity. Oh and Sinkevitch studied performance for noble metals (Ru, Rh, Pt) supported on A1 2 0 3 . At high temperatures (~170°C) Ru/Al 2 0 3 and Rh/Al 2 0 3 were reported to demonstrate nearly 100% conversion of CO with approximately 5% conversion of H 2 for optimum inlet 0 2 concentrations. These results were superior to those reported for Pt/Al 2 0 3 , which was reported to produce almost 20% conversion of H 2 with 100% conversion of CO. At lower temperatures (~140°C) the better reported performance of Ru and Rh relative to Pt was even more pronounced, and Ru was significantly more selective than Rh. Kahlich et al. observed a similar trend between Ru/Al 2 O 3 and Pt/Al 2 0 3 ; however, the authors reported that Au/Fe 2 0 3 generated comparable activities and selectivities at temperatures 70 °C lower. Haruta et al. also noted high activity of Au/Fe 2 0 3 , as well as Au supported on Co 3 0 4 , NiO, Be(OH) 2 , and Mg(OH) 2 . Moreover, the authors reported that Au supported on selected metal oxides was more selective for CO oxidation relative to H 2 than Pt and Pd catalysts. Furthermore, Bethke and Kung recently reported that selectivity for CO oxidation could be improved by decreasing Au particle size, and the authors suggested that the optimal particle size is between 5-10 nm. Finally, Sekizawa et al. reported that the water-gas shift catalyst Cu/Al 2 O 3 - ZnO has promise for selective removal of CO from methanol reformate under appropriate conditions. Despite these apparent successes, current catalysts for selective CO oxidation lack sufficient activity and selectivity at temperatures compatible with PEMFCs (i.e., around 90- 110°C) and require careful control of 0 2 concentration in the feed for optimum performance. Methods for removal of carbon monoxide from hydrogen fuel include adsorption, reduction and oxidation. Adsorption methods remove carbon monoxide by trapping it on a suitable substrate. Although this method is effective, a portion of the purified hydrogen stream must be used as a sweep gas to regenerate the adsorbent, which decreases the amount of fuel available for the cell. Furthermore, large quantities of adsorbent are needed and heat must be applied to the adsorbent to liberate carbon monoxide during regeneration. Alternatively, carbon monoxide can be removed by catalytic reduction to methane. Unfortunately, catalysts that promote this reaction also promote undesirable side reactions that result in generation of more carbon monoxide. There remains a need for materials and processes that destroy VOCs at low concentrations at ambient- or near-ambient temperatures under oxygen-rich conditions. These materials should have high oxygen storage capacity, optimal surface oxygen mobility, stability against feedstream poisons, active sites with a propensity for π-bond systems as well as VOCs in general, and should not require high temperatures to reduce the concentration of VOCs in air. There is also a need for catalysts which selectively remove CO from hydrogen-containing gases. One particular use for such catalysts is to remove CO from a reformate gas feedstream with minimal reduction in hydrogen content. BRIEF SUMMARY OF THE INVENTION Catalyst compositions comprising: at least one of cerium and zirconium with at least one member ofthe group consisting of: Gd, La, Sc, Sr, Cr, Zr, Ti, V, Mn, Fe, Co, Ni, Au, Ag, Cu, Pt, Pd, Rh, Ru, Re, Os and lr are provided. Catalyst compositions ofthe invention may comprise mixed oxides, single-phase materials, or multi-phase materials. Catalyst compositions further comprising a supporting material are also provided. The catalysts in this invention are multi-component metal oxides with or without noble metals. These catalysts are useful, for example, to selectively oxidize carbon monoxide in the presence of hydrogen and are also useful for destruction of VOCs in an oxygen containing gas. The hydrogen may be present in a large excess. One specific application ofthe materials ofthe invention is improving fuel quality for hydrogen PEMFCs. One class of compounds ofthe invention comprise less than 50% of cerium and/or zirconium with at least one member ofthe group consisting of: Gd, La, Sc, Sr, Cr, Zr, Ti, V, Mn, Fe, Co, Ni, Au, Ag, Cu, Pt, Pd, Rh, Ru, Re, Os and lr, provided that the composition is not [Laq Zr r O] 1 _t M , where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. One class of compounds ofthe invention include catalyst compositions comprising one or more first metals selected from the group consisting of: Ce and Zr; and at least one of ((a) (b) or (c)) Page 4 < where (a) is one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; (b) is one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and (c) is one or more fourth metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr. In this class of compounds, preferably the second metals are one or more of Gd, Sr and La. Preferably the third metals are one or more of Cu, Au, Fe, Co and Mn. The second and third metals together preferably comprise less than about 80% of said catalyst composition, more preferably together comprise less than about 50% ofthe catalyst composition, and most preferably together comprise between about 5 and 50% ofthe catalyst composition. Preferably the fourth metals are Pt, Pd and mixtures thereof, with Pt being more preferred than Pd. The fourth metals preferably comprise less than about 25% of said catalyst composition, and more preferably comprise less than about 5% of said catalyst composition, and most preferably comprise less than about 2% of said catalyst composition. One class of compounds ofthe invention has one member from the group of second and third metals combined. Another class of compounds ofthe invention has one member from the group of second metals and one member from the group of third metals. Another class of compounds ofthe invention has more than one member from the group of second metals. Another class of compounds ofthe invention has more than one member from the group of third metals. Another class of compounds ofthe invention has more than one member from the group of second and third metals combined. Each ofthe above classes may optionally contain one or more members ofthe group of fourth metals. In all catalyst compositions listed herein, unless otherwise specified, all intermediate ranges of components are included. All catalyst compositions known in the art are not included in the compositions ofthe invention. Another class of compositions provided are the catalyst compositions with the formula: nN / Ceι_χ Zr c A a A' a . A" a » B b B' b . B" b - 0 2 _δ wherein n is a percentage from 0 to 25; N is one or more metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr; x = a + a' + a" + b + b' + b" + c; a, a', a", b, b', b" and c are each, independently of one another, 0 to 0.9; δ is a number which renders the composition charge neutral; A, A' and A" are independently selected from the group consisting of Gd, La, Sr and Sc; B, B' and B" are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; provided that when n is zero, at least one of a, a', a", b, b', b" or c is nonzero. In this class of compounds, preferably, N is selected from the group consisting of Pt and Pd. Preferably, n is a percentage from 0 to 10, more preferably, n is a percentage from 0 to 5, and most preferably, n is a percentage from 0 to 2. In this class of compounds, preferably A, A' and A" are selected from the group consisting of Gd, La and Sr. In this class of compounds, preferably B, B' and B" are selected from the group consisting of Mn, Cu, Fe, Co and Cr. Preferably, c is between 0 to 0.2. Preferably, a + a' + a" is between 0 and 0.1. Preferably b + b' + b" is between 0.05 and 0.5. Specific examples of this class of compounds include catalyst compositions of formula: Ceι_ Cufθ2-δ wherein f is about 0.001 to about 0.5 and δ is a number which renders the composition charge neutral. Specific examples of compounds of this formula include Ceo.9Cu 0.lθ2-δ an d Ceo.sCuo.2 02-δ- Other specific examples of this class of compounds include catalyst compositions with fonnula Cei.g Mng θ2-δ, wherein g is about 0.001 to about 0.8. Specific examples of compounds with this formula include catalyst composition of formula: Ceo.s no.2θ2-δ aιχ d Ceo.5Mno.5θ2_δ- Other specific examples of this class of compounds include catalyst compositions with formula: Ce0.5Fe0.lCu 0.4θ2-δ> Ceo.475Zro.05 Mno.475 02-δ, Ceo.45Zr 0.05 Mn o.45 Cuo.θ5θ2-δ a d Ceo.δZr 0.05 Cu 0.15 02-δ. Another class of compounds included in the invention are those having formula: nN / Ceι_χ Zr c A a A' a . B b B' . 0 2 -δ wherein n is a percentage from 0.01 to 15; N is one or more metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr; x = a + a' + b + b' + c; a, a', b, b' and c are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A and A' are independently selected from the group consisting of Gd, La, Sr and Sc; B and B' are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; provided that when n is zero, at least one of a, a', b, b' or c is nonzero. In this class of compounds, preferably, N is Pt or Pd, or mixtures thereof. Preferably, n is a percentage from 0.01 to 10, more preferably, n is a percentage from 0.01 to 5, and most preferably, n is a percentage from 0.01 to 2. In this class of compounds, preferably A and A' are one or more of Gd, La and Sr, and preferably B and B' are one or more of Mn, Cu, Co, Cr and Fe. Specific examples of catalyst compositions of this class include 5%Pt/Ceo.8 Cu o.2 ^2-δ l%Pt/Ce 0 .8 Cu 0.2 0 2 -δ, 5%Pt/Ce 0 . 8 Sr 0 .2 0 2 -δ, l%Pt/Ce 0 .8 Sr 0 .2 0 2 -δ, 5%Pt/Ce 0 .8 Au 0 .2 02- ; l%Pt/Ceo.8 Au 0.2 02-δ, 5%Pt/Ceθ2_δ andl%Pt/Ceθ2-δ- Another class of compounds of this invention include those having formula: nN/m Ceι_χ A a A' a , B B' b . 0 2 _δ/ Zrι_ z A" a - A'V B" b .B" 0 2 -δ wherein n is a percentage from 0 to 15; m is a percentage greater than 0; N is one or more metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr; x = a + a' + b + b'; z = a" + a'" + b" + b"'; a, a', a", a'", b, b' 5 b" and b'" are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A, A', A" and A'" are independently selected from the group consisting of Gd, La, Sr and Sc; B, B', B" and B'" are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu ; provided that when n is zero, at least one of a, a', a", a'", b, b', b" or b'" is nonzero. In this class of compounds, preferably, N is selected from the group consisting of: Pt and Pd and mixtures thereof. Preferably, n is a percentage from 0.01 to 10, more preferably, n is a percentage from 0.01 to 5, and most preferably, n is a percentage from 0.01 to 2. Preferably m is a percentage from 0.5 to 25. In this class of compounds, preferably A, A', A" and A'" are independently selected from the group consisting of Gd, La and Sr, and B, B', B" and B"' are independently selected from the group consisting of Mn, Cu, Co, Cr and Fe. A specific example of compounds of this class include those of formula: 1% Pt/12%Ce O2 / Zr O2. Another class of compounds of this invention include those having formula: nN /m (Cβ θ2y p (A a A' a Α" a " Bb B B"b"θ2-δ) / q (A ", a'"A"" a " » A a B" "B "" b""B b θ2- δ ) wherein n, p and q are percentages from 0 to 50; m is a percentage greater than 0; N is one or more metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr; a, a\ a", a"", a"", a""", b, b", b", b"", b"" and b" Λ " are each, independently of one another, 0 or 1; δ is a number which renders the composition charge neutral; A, A", A", A"", A ,Λ " and A" " are independently selected from the group consisting of Gd, La, Sr and Sc; B, B", B", B"", B"" and B"" Λ are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; provided that when n is zero, at least one of p and q is nonzero and at least one of a, a\ a", a"", a"", a"" , b, b b", b"", b"" and b""" is nonzero. In this class of compounds, preferably N is selected from the group consisting of Pt and Pd and mixtures thereof. In this class of compounds, A, A Λ , A" , A" " , A"" and A""" are preferably Gd, La and Sr, and B, B", B", B"\ B"" and B""" are preferably Mn, Cu, Co, Cr and Fe. Preferably, p and q are less than 50%. Preferably m is 10% to 50%. Preferably n is 5% or less. Specific examples of compounds of this class include those with formula Ce 02.5 10% CuO and Ce θ2-δ/ 10% Mnθ2- The catalyst composition classes listed above are particularly useful in reducing the concentration of VOCs in a hydrogen-containing gas. More preferred catalysts ofthe invention are mixtures of cerium and/or zirconium with one or more metals selected from the group consisting of: Pt, Pd, Cu, Gd, Mn, Fe, Zr, La, Co, Sr, Au, and Cr. Preferably, these metals are present in a concentration of about 5% to 50%. This class of catalysts is particularly useful in reducing the concentration of VOCs in an oxygen containing gas. Catalyst compositions useful in the methods ofthe invention include those with a surface area ranging from about 20 to about 220 rn^/g. Another class of catalysts ofthe invention have the formula: hN/Ceι-.(χ+ y- ι- z ) A x A' y A" z 02_δ where A, A', A" are independently selected from the group consisting of: Zr, Gd, La, Sc, Sr, Co, Cr, Fe, Mn, V, Ti, Cu and Ni; N is one or more members ofthe group consisting of Pt, Pd and Au; n is a weight percent between 0 and 25; x, y and z are independently 0 to 0.9; x + y + z is 0.1 to 0.9; and δ is a number which renders the composition charge neutral. These catalyst compositions are also useful in the methods ofthe invention and are particularly useful for selective oxidation of carbon monoxide. Another class of catalyst compositions of the invention have the formula: nN/(MO x ) y (Ce0 2 _δ) y , where M is one or more members of the group selected from: Zr, Co, Cr, Fe, Mn, V, Ti, Ni and Cu; N is one or more members of the group consisting of Pt, Pd and Au; n is a weight percent between 0 and 25; y is 0.1 to 0.9; and x and δ make the compositions charge neutral. These catalyst compositions are also useful in the methods of the invention and are particularly useful for selective oxidation of carbon monoxide. Another class of compounds of the invention which is useful in the methods of the invention for selective removal of carbon monoxide in a hydrogen-containing gas comprises Ce and at least one of ((a) or (b)) where (a) is one or more second metals selected from the group consisting of: Zr, Gd, La, Sc, and Sr; (b) is one or more third metals selected from the group consisting of: Co, Cr, Fe, Mn, V, Ti, Cu and Ni. Another class of compositions useful in the methods of the invention are catalyst compositions with the formula: nN / Ce.. x Zr c A a A', A",.B b B'„. B" b „ 0 2 . δ wherein n is a weight percentage from 0 to 25; N is one or more metals selected from the group consisting of Au, Pt, and Pd; x = a + a' + a" + b + b' + b" + c; a, a', a", b, b', b" and c are each, independently of one another, 0 to 0.9; δ is a number which renders the composition charge neutral; A, A' and A" are independently selected from the group consisting of Gd, La, Sr and Sc; B, B' and B" are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; provided that at least one of a, a', a", b, b', b" or c is nonzero. These catalyst compositions are also useful in the methods of the invention and are particularly useful for selective oxidation of carbon monoxide. In this class of compounds, preferably n is a weight percentage from 0 to 10, more preferably, n is a percentage from 0 to 5, and most preferably, n is a percentage from 0 to 3. In this class of compounds, preferably A, A' and A" are selected from the group consisting of Gd, La and Sr. In this class of compounds, preferably B, B' and B" are selected from the group consisting of Mn, Cu, Fe, Co and Cr. Preferably, c is between 0 to 0.2. Preferably, a + a' + a" is between 0 and 0.1. Preferably b + b' + b" is between 0.05 and 0.5. Another class of compounds useful in the methods of the invention are those having formula: nN / Ce^Zr c A a A , ..B b B , b .O z< 5 wherein n is a weight percentage from 0.01 to 15; N is one or more metals selected from the group consisting of Pt, Pd, and Au; x = a + a' + b + b' + c; a, a', b, b' and c are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A and A' are independently selected from the group consisting of Gd, La, Sr and Sc; B and B' are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; provided that at least one of a, a', b, b' or c is nonzero. These catalyst compositions are also useful in the methods of the invention and are particularly useful for selective oxidation of carbon monoxide. In this class of compounds, preferably n is a percentage from 0.01 to 10, more preferably, n is a percentage from 0.01 to 5, and most preferably, n is a percentage from 0.01 to 3. In this class of compounds, preferably A and A' are one or more of Gd, La and Sr, and preferably B and B' are one or more of Mn, Cu, Co, Ci and Fe. Another class of compounds useful in the methods of this invention include those having formula: nN/m Ce s A a A', B b B O^/Zr^A' A"> B'VB'V Q 2 . δ wherein n is a percentage from 0 to 15; m is a percentage greater than 0; N is one or more metals selected from the group consisting of Pt, Pd, and Au; x = a + a' + b + b'; z = a" + a'" + b" + b"'; a, a', a", a'", b, b', b" and b"' are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A, A', A" and A'" are independently selected from the group consisting of Gd, La, Sr and Sc; B, B', B" and B'" are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu ; provided that at least one of a, a', a", a'", b, b', b" or b'" is nonzero. These catalyst compositions are also useful in the methods of the invention and are particularly useful for selective oxidation of carbon monoxide. In this class of compounds, preferably n is a percentage from 0 to 10, more preferably, n is a percentage from 0 to 5, and most preferably, n is a percentage from 0 to 3. Preferably m is a percentage from 0.5 to 25. In this class of compounds, preferably A, A', A" and A'" are independently selected from the group consisting of Gd, La and Sr, and B, B', B" and B'" are independently selected from the group consisting of Mn, Cu, Co, Cr and Fe. Another class of compounds useful in the methods of this invention include those having formula: nN /m (Ce 0 2 )/p (A a A\-A ^ a .- B b B\-B ^ b ..0 2 . δ ) / q (A ^ \-A ^ ^ a --A a B -B ^ V -B b 0 2-δ ) wherein n, p and q are percentages from 0 to 50; m is a percentage greater than 0; N is one or more metals selected from the group consisting of Au, Pt and Pd; a, a s , a" , a s , " ^ " a" v N v , b, b" , b" v , b N , b" and b are each, independently of one another, 0 or 1; δ is a number which renders the composition charge neutral; A, A A v \ A" \ A and A s " x are independently selected from the group consisting of Gd, La, Sr and Sc; B, B , B s B" " " , B and B v are independently selected from the group consisting of Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; provided that when n is zero, at least one of p and q is nonzero and at least one of a, a a" " , a , a x a , b, b b N b N " b" and b x is nonzero. These catalyst compositions are also useful in the methods of the invention and are particularly useful for selective oxidation of carbon monoxide . In this class of compounds, A, A A" A" A" and A" " " are preferably Gd, La and Sr, and B, B\ B" , B"", B"" and B""" are preferably Mn, Cu, Co, Cr and Fe. Preferably, p and q are less than 50%. Preferably m is 10% to 50%. Preferably n is 5% or less. The catalysts particularly useful for selective removal of carbon monoxide can contain between 0 and 25 weight percent of Pt, Pd and Au, or combinations of these metals and any intermediate value therein. Preferably, the amount of Pt, Pd and Au is as small as possible, because the metals are expensive. Preferably, less than about 10 weight percent of these metals are present. If present, Pt and Au are in the metallic state and Pd can be in the metallic state or as an oxide. One class of catalysts consist of finely dispersed Au and/or Cu on nanocrystalline multi- component metal oxides. For Cu-containing analogs, the Cu is believed to be present as groups of atoms forming clusters, or stabilized surface Cu ions. The composite catalyst can be denoted by the general formula Mχ(M'Oy) z (Ceθ2-δ)l-(χ+z) > where M represents particles or clusters of Cu or Au, M' is a transition metal oxide or mixtures of transition metal oxides selected from Zr, Co, Cr, Fe, Mn, V, Ti, Ni, and Cu, and 0.5 ≤ (x+z) < 1. One class of catalyst compositions ofthe invention include combinations of ceria and/or zirconia optionally combined with platinum and/or palladium. Another class of catalyst compositions ofthe invention include combinations of ceria and/or zirconia at least one metal from the group consisting of: Gd, La, Sc, Cr, Ti, V, Mn, Fe, Co, Ni, Au, Ag and Cu, optionally combined with platinum and/or palladium. Catalyst compositions ofthe invention include those with predominantly fluorite crystal structures. Other structures that may be present include defect fluorite, pyrochlore (A2B2O7) and perovskite-like phases. Cerium and zirconium oxide with some amount of dopants are generally present as fluorite structures. Dopants may also be present as oxides. A class of catalyst compositions ofthe invention are those that do not require an inert support, such as alumina or carbon. Another class of catalyst compositions ofthe invention include a support material such as a honeycomb matrix having inner and outer surfaces, wherein said catalyst material is present on the inner surfaces of said honeycomb matrix. Preferably, the support material is fabricated from ceramic materials, but may also be fabricated from metals or ceramic or metal fibers. Catalysts that are particularly useful for destruction of carbon monoxide include those having constituents with a preference for carbon monoxide. Such constituents include: copper, manganese and gold. Particularly useful materials include finely dispersed Au or Cu within composite metal oxides. Activity is believed to be promoted by high dispersion of these metals and synergy with the composite metal oxide support. Selectivity is achieved through preferential interaction of CO with polarizable Cu clusters and Au particles, as well as stabilized surface Cu ions. One class of compounds of the invention contains finely dispersed Au within composite metal oxides. Another class of compounds of the invention includes finely dispersed Cu within composite metal oxides. One class of catalysts of the invention include: Ce 0 . 5 Cu 0 . 5 O 2 .δ; Ce 0 . 475 Zro. 05 Mno. 475 0 2 . δ; Ce 0 . 5 Mno. 5 O 2 _δ; Ceo. 45 Zro.05M1-o. 45 Cuo.05 0 2 _δ; and Another class of catalysts of the invention includes: Mi-o 5 Fe 0 . 5 O x ; Ce 0 .ι Mn 0 45 Cu 0 . 45 θ x ; Ce 0 . ! Mno. 45 Fe 0 . 45 O x ; Ce 0 3 Mno. 7 0 2 . δ; and Ce 0 3 Mr-o. 65 Zr 0 05 0 2 _δ. x is a value which depends on the crystal structure of the composition, as known in the art. One class of compounds of the invention contains cerium at less than about 50 atomic percent of the metal components. Another class of compounds of the invention contains cerium at more than about 50 atomic percent of the metal components. Another class of compounds of the invention contains cerium at about 50 atomic percent of the metal components. Another class of compounds of the invention contains cerium at less than about 40 atomic percent of the metal components. Another class of compounds contains between 1-35 atomic percent Ce0 2 . Another class of compounds of the invention contains cerium at less than about 30 atomic percent of the metal components. Another class of compounds of the invention contains cerium at less than about 25 atomic percent of the metal components. Another class of compounds of the invention contains cerium at less than about 65 atomic percent of the metal components. All intermediate ranges of cerium are included in the invention, as long as the compositions selectively remove carbon monoxide in the presence of hydrogen or reduce the concentration of at least one VOC in an oxygen-containing gas. Also provided are methods for reducing the concentration of VOCs in an oxygen-containing gas containing at least one VOC which comprises the step of contacting said gas with a catalyst composition ofthe invention, whereby the concentration of at least one VOC in said gas is reduced. These methods may further comprise heating either said gas or said catalyst composition, or both, to a temperature sufficient to reduce the concentration of at least one VOC in said gas to a selected value. The catalyst compositions may be held in a reactor at temperatures of from about ambient temperature to about 250 °C. Preferably, the temperatures are from about ambient temperature to about 150°C. The gases may contain the normal components of air, hydrocarbons and halogen- containing materials. The gas may also contain substances including water vapor, sulfur-containing gases and other substances. Also provided are methods of decomposition of VOCs in a gas, comprising the steps of providing a reactor containing a catalyst composition ofthe invention; and passing the gas through the reactor to decompose the VOCs. Also provided is a catalytic reactor for decomposition of VOCs in a gas which comprises: a casing having an entrance port, an exit port and a passage therebetween for the movement of said gases from said entrance port to said exit port with a catalyst composition ofthe invention in said passage. In the catalytic reactor, the gases preferably contact said catalyst before exiting said casing. Also provided are methods for selectively removing carbon monoxide in a hydrogen- containing gas which comprise the step of contacting said gas with a catalyst composition ofthe invention. These methods may further comprise heating either said gas or said catalyst composition, or both, to a temperature sufficient remove the desired amount of carbon monoxide in said gas. The catalyst compositions may be held in a reactor at temperatures of from about ambient temperature to about 250°C. Preferably, the temperatures are from about ambient temperature to about 150°C. Preferably, temperatures from about 150°C to about 30°C are used. Most preferably, temperatures of about 120°C and below are used. Also provided are methods of selectively removing carbon monoxide in a hydrogen- containing gas, comprising the steps of providing a reactor containing a catalyst composition ofthe invention; and passing the gas through the reactor to remove the carbon monoxide. Also provided is a catalytic reactor for selectively removing carbon monoxide from a hydrogen-containing gas which comprises: a casing having an entrance port, an exit port and a passage therebetween for the movement of said gases from said entrance port to said exit port with a catalyst composition ofthe invention in said passage. In the catalytic reactor, the gases preferably contact said catalyst before exiting said casing. The catalyst compositions ofthe invention may be used to reduce the concentration of carbon monoxide in a gas mixture. The components ofthe gas mixture may include methane, carbon dioxide, carbon monoxide, oxygen, water, nitrogen, argon, native components of air, hydrogen and other hydrocarbons, or any mixture ofthe foregoing. The gas may also include other substances, as known in the art, for example other components of a fuel cell feed. The gas mixture must contain some oxygen, preferably not a large excess of oxygen. The gas mixture preferably contains a stoichiometric amount of oxygen. The catalysts ofthe invention function in the presence of potentially interfering substances, such as water, sulfur-containing gases and halogens. The catalysts of this invention are suitable for use in any reactor system, including those known in the art and particularly with either fixed and fluid bed reactors and can be prepared as powders or pressed into plugs, pellets and other shapes suitable for use in a given reactor configuration, as known in the art. VOCs destroyed by the catalyst compositions ofthe invention include, but are not limited to: acetates, alkanes, alkenes, alcohols, aldehydes, ethers, esters, aromatics, carboxylic acids, ketones, and halogenated hydrocarbons. The catalyst compositions ofthe invention may be used to reduce the concentration of VOCs in a gaseous atmosphere. Preferably, the VOCs are converted to carbon dioxide and water. Preferably, the gaseous atmosphere is oxygen-containing, and most preferably, the gaseous atmosphere is air. Catalyst composition ofthe invention may be used to reduce the concentration of VOCs in gases containing any concentration of VOCs. In one application, catalyst compositions of the invention may reduce the concentration of VOCs in air where there is an excess of oxygen and between between 10 ppm and percent levels of VOCs. The catalysts ofthe invention are useful to reduce the concentration of VOCs in gases at low temperatures (from about 200°C and below). Preferably, temperatures from about 150°C to about 30°C are used. Most preferably, temperatures of about 100°C and below are used. The catalysts ofthe invention function in the presence of potentially interfering substances, such as water, sulfur-containing gases and halogens. The catalysts are preferably preconditioned prior to said gases contacting said catalyst. The preconditioning treatment is useful to desorb moisture and change the oxidation state of some species. More preferably, the catalysts are preconditioned at a temperature of between about 150°C to 400°C. Catalyst compositions of the invention are preferably preconditioned under a flow of air or VOC for a time sufficient to maximize activity, preferably for one hour or more. The preferred preconditioning time is longer at lower temperatures and can be as long as 24 hours at temperatures of 100° C or less. Catalysts ofthe invention have long lifetimes and can be regenerated by heating for a sufficient time to drive off adsorbed organics and moisture. For example, catalysts ofthe invention may be regenerated by heating at a temperature of about 150°C. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is the crystallographic structure of doped fluorite-type oxides. Figure 2 is a schematic diagram showing the processes believed to lead to oxidation of toluene on a Pt/Ceθ2-δ catalyst. Figure 3 shows XRD patterns for Zrθ2 and Ceθ2- Figure 4 shows XRD patterns for Ceo.8Sro.2θ2-δ and CeQ.8Auo.2θ2-δ- Figure 5 shows XRD patterns for CeCoo.5Cuo.5θ2-δ prepared by co-precipitation and from the constituent oxides using ceramic processing. Figure 6 shows an overlay ofthe EDX spectra for Ceθ2 and Zrθ2- Figure 7 shows the EDX spectra for Zrθ2 wash-coated with Ceθ2 (25 wt.%Ceθ2/ rθ2). Figure 8 shows the EDX spectra for Ceo.sZro.2θ2-δ- Figure 9 contains the EDX spectra for Ceo.8Gdo.2θ2-δ • Figure 10 shows an overlay ofthe EDX spectra for 1 wt.-%Pt, 5 wt.-%Pt, and 10 wt.-%Pt on Ceθ2- Figure 11 shows typical FTIR spectra of a catalyst before exposure to VOCs, and after screening with MEK, toluene, and 1-butanol at temperatures below 100°C. Figure 12 shows FTIR spectra of 5%Pt/Ceθ2 prepared by different methods. Figure 13 shows one apparatus useful in screening catalysts for VOC destruction. Figure 14 shows a plot of percent conversion of toluene to CO2 for 5% Pt on Ceθ2 and Zrθ2- Figure 15 is a comparison ofthe percent conversion of toluene to CO2 by 1% Pt and 1% Pd on Ceθ2- Figures 16A and 16B show the percent removal of toluene and MEK, and the percent conversion of VOCs to CO 2 at l50°C. Figure 17 is a plot of percent conversion of toluene to CO2 versus time for 5%Pt/Ceo.8Sro.2θ2-δ- Figure 18 is a plot of catalyst activity as a function of time for 5%Pt/Ceo.8Cuo.2θ2- - Figure 19 is a plot showing the effect of Cu doping level on the activity for conversion of toluene and MEKto C0 2 . Figure 20 is a plot showing the effect of Sr doping level on the activity for conversion of toluene and MEKto C02. Figure 21 shows XRD results for Ceι_ x Cu x θ2- without Pt, where x is 0.1 (A), 0.2 (B), 0.3 (C), 0.4 (D), and 0.5 (E). Figure 22 shows the XRD pattern for Ceo.6Cuo.4O1. precipitated with NaOH. Figure 23 shows a schematic diagram of a catalytic monolith for low-temperature oxidation of VOCs. Figure 24 shows a schematic illustration of a ceramic honeycomb monolith coated with active catalyst. Figure 25 shows a cross-section diagram of a quartz reactor tube packed with catalyst-coated pellets. Figure 26 is a plot showing the % conversion of MEK to CO2 for a monolith coated with l%Pt/Ceθ2. The solid line is for the catalyst-coated monolith, and the dashed line is for a blank (no catalyst) monolith. Figure 27 shows one apparatus useful in screening catalysts for selective carbon monoxide removal. Figure 28 shows selective catalytic oxidation of carbon monoxide in the presence of hydrogen. Percent conversion represents oxidation of carbon monoxide to carbon dioxide and oxidation of hydrogen to water. The catalyst was Ceo.475Zro.θ5 no.475θ2-χ and the space velocity was -24,000 hr 1. The average reactor inlet concentrations were 0.15 vol.% CO, 2.5 vol.% for H2, and approximately 0.2 vol.% O2 with a balance of Ar. Figure 29 shows selective catalytic oxidation of carbon monoxide in the presence of hydrogen. Percent conversion represents oxidation of carbon monoxide to carbon dioxide and oxidation of hydrogen to water. The catalyst was Ceo.45Zro.θ5 no.45Cuo.θ5θ2-χ and the space velocity was -24,000 hr"l. The average reactor inlet concentrations were 0.3 vol.% CO, 2 vol.% for H2, and approximately 0.3 vol.% O2 with a balance of Ar. Figure 30 shows selective catalytic oxidation of carbon monoxide in the presence of hydrogen. Percent conversion represents oxidation of carbon monoxide to carbon dioxide and oxidation of hydrogen to water. The catalyst was Ceo.5MnQ.5θ2-χ and the space velocity was -24,000 hr 1. The average reactor inlet concentrations were 0.1 vol.% CO, 1 vol.% for H2, and approximately 0.1 vol.% O2 with a balance of Ar. Figure 31 shows selective catalytic oxidation of carbon monoxide in the presence of hydrogen. Percent conversion represents oxidation of carbon monoxide to carbon dioxide and oxidation of hydrogen to water. The catalyst was Ceo.475Zro.05Mno.475O2.-x and the space velocity was -24,000 hr 1. The average reactor inlet concentrations were 0.1 vol.% CO, 1 vol.% for H2, and approximately 0.1 vol.% O2 with a balance of Ar. Figure 32 is a photograph showing a section of bare monolith and a catalyst-coated monolith inside a reactor tube. DETAILED DESCRIPTION OF THE INVENTION Catalyst compositions ofthe invention include those with predominantly fluorite crystal structures. Other structures that may be present include defect fluorite, pyrochlore (A2B2O7) and perovskite-like phases, or phases resulting from other metal oxides in the catalyst such as oxides of Cu, Mn, Cr and Co. Cerium and zirconium oxide with some amount of dopants are generally present as fluorite structures. Dopants may also be present as oxides. A class of catalyst compositions ofthe invention are those that do not require an inert support, such as alumina or carbon. Another class of catalyst compositions ofthe invention include a support material such as a honeycomb matrix having inner and outer surfaces, wherein said catalyst material is present on the inner surfaces of said honeycomb matrix. Preferably, the support material is fabricated from ceramic materials, but may also be fabricated from metals or ceramic or metal fibers. As used herein, "selective removal of carbon monoxide in the presence of hydrogen" means that more carbon monoxide is removed from a gas than hydrogen is removed. It is preferred that as much carbon monoxide is removed as possible, while the level of hydrogen is maintained to as great an extent as possible. The carbon monoxide does not need to be all removed for the removal to be encompassed by the term, as long as the carbon monoxide is reduced more than the hydrogen is reduced. The desired amount of carbon monoxide which is removed is dependent on the particular application ofthe catalyst or method. The amount of carbon monoxide which is removed is dependent on the temperature ofthe reaction, the catalyst composition, the flow rates, the composition ofthe inlet stream, and other parameters as known in the art. In some applications, it is preferred that the concentration of carbon monoxide be removed to less than 10 ppm in the gas mixture. The catalyst compositions of this invention are useful to selectively remove carbon monoxide from a hydrogen-containing gas. The catalyst compositions useful in the methods ofthe invention may be prepared by methods known in the art, or the methods described herein or modifications of methods known in the art or modifications ofthe methods described herein. The catalysts described in this invention can be prepared by coprecipitation, impregnation, precipitation deposition, ceramic processing, or hydrothermal processing techniques, or other methods known in the art, including the method comprising: (a) treating a mixture of selected metal salt precursors with a precipitating reagent to form a precipitate; (b) drying said precipitate; (c) calcining said precipitate at a temperature of about 300°C or higher; (d) contacting one or more solutions of one or more metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr (preferably Pt or Pd or mixtures thereof) with said precipitate; (e) reducing said composition (preferably at temperatures of about 200 °C or higher); and optionally (f) oxidizing said composition (preferably at temperatures of between about 80 °C to about 800°C). The catalyst compositions useful in the methods ofthe invention may also be prepared by the method comprising the steps: (a) mixing selected metal oxides; (b) ball milling said metal oxides; and (c) calcining in air (preferably at temperatures of about 300°C or higher). The catalyst compositions may be coated onto a support material by any method which produces a suitable coating of catalyst composition, including the method of: (a) treating a mixture of metal salt precursors with a precipitating reagent to form a precipitate; (b) preparing a slurry of said precipitate; (c) coating said slurry onto said support; and (d) calcining said slurry. The catalyst compositions may also be coated onto a support material by: (a) mixing a solution of metal salt precursors with the support; and (b) calcining said precursors. The catalyst compositions may also be coated onto said support material by: (a) mixing the support with one or more metal salt precursors to form a mixture; (b) treating said mixture with a precipitating reagent to form a precipitate; and (c) calcining said precipitate. The methods above may also further comprise the steps of: adding one or more metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr metal to form a composition; reducing said composition (preferably at temperatures of about 200 °C or higher); and optionally oxidizing said composition (preferably at temperatures of between about 80°C to about 800°C). As used herein, "catalyst composition" includes those compositions ofthe invention. The catalyst compositions are useful for example, in destruction of VOCs in a gas or selective removal of carbon monoxide in a hydrogen-containing gas. Catalyst compositions comprise at least one of cerium and zirconium with at least one member ofthe group consisting of: Gd, La, Sc, Sr, Cr, Zr, Ti, V, Mn, Fe, Co, Ni, Au, Ag, Cu, Pt, Pd, Rh, Ru, Re, Os and lr. Catalyst compositions ofthe invention are useful in reducing the concentration of at least one VOC in gas, or selectively removing carbon monoxide from a hydrogen-containing gas. As used herein, "destruction" of a VOC refers to the transformation of a VOC into another substance, preferably carbon dioxide and water. As used herein, "mixed metal oxides" include one or more metal oxides. As used herein, "single-phase material" is a material that comprises a single crystallographic phase. As used herein, "multi-phase material" refers to a material wherein some components are single-phase and other components are mixed metal oxides. As used herein, a "precipitating reagent" is a substance or mixture of substances that causes precipitation of a desired substance. Preferred precipitating reagents include NH4OH, (NH )2Cθ3, Na2C03, NaOH, urea and K2CO3. As used herein, "contacting" substances is meant to indicate that substances are physically near each other, but is not intended to mean a homogeneous solution is formed. Preferably, reducing occurs in a hydrogen-containing atmosphere and oxidation occurs in air, but any reaction conditions that produce the desired result may be used. In the catalyst compositions ofthe invention, if a metal selected from the group consisting of: Pt, Pd, Rh, Ru, Re, Os and lr and mixtures thereof is present, the metal(s) is preferably dispersed onto the metal oxide surface, and preferably the incipient wetness impregnation method is used. Catalysts described in this invention are believed to remove carbon monoxide by selectively oxidizing it to carbon dioxide. Carbon dioxide does not affect the performance of hydrogen PEMFCs. Furthermore, the catalysts described in this invention are distinct from other reported selective carbon monoxide oxidation catalysts since they do not rely on noble metals or metals supported on traditional carriers such as AI2O3. Some significant and distinct aspects of catalysts in this invention are that they are multi-component metal oxides tailored to generate selective oxidation of carbon monoxide in the presence of hydrogen, including a large excess of hydrogen, and the compositions do not require expensive noble metals to be effective. The oxidation catalysts described in this invention are useful for reducing the concentration of VOCs at lower temperatures than previously reported. High activity for the destruction of VOCs is achieved through a combination of appropriate catalyst elements and preparation procedures that optimize material qualities such as oxygen mobility, oxygen storage capacity, resistance to poisons, textural properties, metal dispersion, and active sites for a range of organic functional groups. Some ofthe applications of these VOC oxidation catalysts include removal of VOCs from ventilated work spaces used in spray painting, fuel line maintenence, and vapor degreasing. These catalysts can also be used to treat vapor effluents from chemical processing, computer chip/device manufacturing, air-stripping towers and catalytic wet-air oxidation, dry cleaning, and restaurants. Furthermore, these catalysts can be used to decontaminate residential and workplace office air, in air filtration devices used in face masks for firefighting and underground mines, and for the destruction of biohazardous materials. Finally, these catalysts can be used to remove CO from feedstreams in hydrogen/oxygen fuel cells, where CO poisons the anode electrocatalyst, and as CO oxidation catalysts for CO2 lasers, where the catalyst would increase the CO2 CO ratio, improving the laser performance. The specific components of these catalysts can be separated into four categories. The first category includes Ce, which comprises the major portion ofthe metal oxide component either as Ceθ2 or doped Ceθ2- This component acts both as a support in synergy with noble metals, and an active metal oxide oxidation catalyst. An equilibrium between Ce? + and Ce4+ results in an exceptionally high oxygen storage and release capacity that facilitates catalytic combustion by providing oxygen directly to catalytically active sites. Furthermore, Ceθ2-containing catalysts are less susceptible to deactivation from water vapor and more resistant to sintering than catalysts employing inactive metal oxide supports such as AI2O3. Also included in this category is Zr, which has qualities similar to Ce and improves the low-temperature reducibility of Ceθ2- The second category includes the metals Gd, La, Sc, and Sr which are incorporated as dopants in Ceθ2 to promote oxygen vacancies and increase oxygen mobility within the catalyst. The oxygen vacancy association energy for these elements increases in the order Gd<La<Sc<Sr; therefore, varying the identity and concentration of these dopants allows control over the bulk oxygen mobility. The third category includes the metals Ti, V, Co, Cr, Ni, Mn, Fe, and Cu. These metals contain multiple oxidation states and the corresponding oxides are also good oxidation catalysts. When combined with Ceθ2, they provide additional catalytic active sites with metal oxygen bond strengths conducive to complete destruction of VOCs. Finally, the fourth category includes the metals Pt, Pd, Au, Ag, Rh, Re, Os, Ru, and lr. These elements are included in the catalysts mostly in the reduced state dispersed over the surface and within the pores ofthe metal oxide. Generally, inclusion of one of these fourth category metals in the composition significantly improves activity at low temperatures. Both Pt and Au are present in the metallic state whereas Pd can be present as a metal or an oxide. Although inclusion of this fourth category in catalyst compositions improves catalyst oxidation activity, it is not necessary and is deemphasized due to the high cost of these metals. High oxidation activity of these materials results from judicious selection of specific compositions. The compositions are selected based on the qualities described above, as well as results of catalyst testing, such as that described herein, or known in the art. However, catalyst activity must be balanced with selectivity for preferential interaction of CO with catalyst active sites. Using fluorite-type oxides (such as Ceθ2 and Zrθ2) with appropriate dopants, in combination with other materials that have high oxygen exchange rates and demonstrated oxidation activity as metal supports (such as MnO x and Fe2θ3), significant improvements in the materials used for supported metal catalysts are achieved. The crystallographic structure for a doped defect fluorite oxide is shown in Figure 1. The fluorite-type metal oxides have a face-centered-cubic structure, with each tetravalent metal atom (O) surrounded by eight Cβ- ions (A) forming the vertices of a cube. Doping fluorite oxides with divalent or trivalent metals (M n+ ) produces high oxygen vacancy concentrations, which can be controlled by the degree of doping and the specific dopant used. Therefore, choosing dopants with lower association energies will produce oxides with higher oxygen mobility. Not desiring to be bound by theory, based on the range of compositions of these catalysts, several general mechanisms for VOC destruction are believed to be involved. The general mechanistic strategy for the catalytic decomposition of VOCs using the catalysts described in this work can be viewed in terms ofthe Mars-van Krevelen mechanism, (Gangwal, S.K. et al. (1988) Appl. Catal. 36:231-247): VOC + oxidized catalyst - CO2 + H2O + reduced catalyst O2 + reduced catalyst - oxidized catalyst The specific mechanism will depend on the identity ofthe VOC and catalyst, and for metals deposited onto active supports, it is likely that several mechanisms are occurring simultaneously and in concert. A general concept for the oxidation of VOCs by precious metals on active supports is shown in Figure 2 for the oxidation of toluene on Pt/Ceθ2. For such noble metal-containing catalysts, there is a contribution to the overall oxidation from the noble metal alone. Assuming a Langmuir-Hinshelwood process, the first step is adsorption of toluene and oxygen onto the Pt surface, as shown in section A of Figure 2. Toluene adsorbs parallel to the surface (flat) to produce a Pt complex, which activates the toluene for further reaction (Barresi, A.A. and Baldi, B. (1994) Ind. Eng. Chem. 33:2964-2974). Oxygen adsorbs on adjacent Pt atoms, followed by dissociation. The oxidation of toluene then proceeds by reaction with atomic oxygen to produce CO2 and H2O. Similarly, toluene and oxygen also adsorb on the Ceθ2 surface, followed by reaction to produce CO2 and H2O. However, on the Ceθ2 surface, oxidation also can proceed by reaction with lattice oxygen resulting in the reduction of Ce4+ to Ce3+, as shown in section B of Figure 2. The Ce^+ is then oxidized back to Ce4+ by reaction with gas-phase oxygen. The fact that this process occurs readily on Ceθ2 surfaces is partly responsible for the activity of this material for oxidation reactions. Furthermore, the presence of Pt on the Ceθ2 surface facilitates the reduction of Ce4 + . which is the rate limiting step in the oxygen uptake process, as shown in section C. An additional contribution to the overall oxidation comes from reaction of toluene and oxygen at the three-phase-boundary ofthe Pt, Ceθ2 and gas phase (Liu, W. Flytzani-Stephanopoulos (1995) J. Catal. 153:317-332). In this process toluene either adsorbs to acidic sites on the Ceθ2 and reacts with oxygen originating on the Pt surface, (Barresi, A.A. and Baldi, B. (1994) Ind. Eng. Chem. Res. 33:2964-2974) or toluene adsorbed on the Pt reacts with oxygen supplied by the Ceθ2, as shown in section D of Figure 2 (Haruta, M. et al. (1993) J. Catal. 144:175-192). The relatively high activity of Pt/Ceθ2 catalyst systems for oxidation of VOCs, therefore, is likely partially the result of synergistic effects between the Pt metal and Ceθ2 support. Additionally, adsorbed O2 can react with gas-phase VOCs according to the Eley-Rideal mechanism. The supply of O2 to the noble metal surface comes from the gas phase or spillover from the metal oxide. Similar mechanisms also likely occur on the metal oxide surface; however, the VOCs can react either with adsorbed oxygen or lattice oxygen. One application for the materials and methods described herein is selective removal of carbon monoxide from reformate fuel for hydrogen powered polymer electrolyte membrane fuel cells (PEMFC). Since even low levels of carbon monoxide can degrade hydrogen PEMFC performance, use of these catalysts will improve fuel cell operation when using fuel sources other than pure hydrogen. Although Applicants do not wish to be bound by theory, and the mechanism for selective oxidation of carbon monoxide on these materials is not known, it is believed that the first step involves adsorption of oxygen from the feedstream onto a surface metal cation to form a superoxide (O2'). The superoxide likely converts to a peroxide species (O^'), which has been suggested to be the active form of surface oxygen for similar materials. The peroxide ion may associate with two reduced-state metal cations or an oxygen vacancy. Simultaneously, carbon monoxide can selectively adsorb from the feedstream to a metal particle, cluster, or ion, and migrate to the three-phase boundary between the specific active site, metal oxide surface, and gas phase. At this three-phase boundary, reaction with 02^" can occur to produce CO2. This process will remove deleterious carbon monoxide from the reformate fuel without combusting hydrogen. Those of ordinary skill in the art will appreciate that methods, techniques, and components other than those specifically described herein can be employed in the practice ofthe invention without departing from its spirit scope. The following examples illustrate the invention and are in no way intended to limit its scope. EXPERIMENTAL A. Catalyst Synthesis The doped Ceθ2 and mixed-oxide catalysts in this invention can be prepared by methods known in the art, including coprecipitation, hydrothermal synthesis, calcination, wash-coating, impregnation-deposition or ceramic processing. Methods of making the catalysts are described herein or are well known in the art, or readily adapted from the methods described herein or those methods well known in the art by one of ordinary skill in the art without undue experimentation. Such methods known in the art are described, for example, in Perego, C. and Villa, P., (1997) Catalysis Today, 34:281-305. Preparation of Powder Supports. Many powder support materials were prepared by co- precipitation. In this procedure the metal nitrate precursors were dissolved in water (cerium-based) or methanol (zirconium-based) in the appropriate molar ratios. The concentration ofthe primary metal cation for each support (i.e. cerium and zirconium) before precipitation was approximately 0.4 M. Zirconyl nitrate had to be gently heated with stirring overnight in methanol for dissolution. The precipitant used may be NΗ4OH, NaOH, KOH, a2Cθ3, urea, K2CO3, sodium or potassium oxylate, or any other substance able to perform the desired precipitation. In the preparation of most ofthe powder supports the precipitant used was NH4OH in concentrations as low as 1 M. During precipitation, the mixture was stirred vigorously. Precipitant was added beyond the calculated stoichiometric equivalence point, until the supernatant liquid tested basic. The resulting precipitates were vacuum filtered and washed three times with room-temperature deionized water, then dried at 90-110 °C for several hours. The dried powders were finely ground and heated in air at temperatures of 200-900°C for 2-12 hours to produce the metal oxide support. After oxidation, the powders were reground and passed through a 150-μm sieve. To decrease particle size, the powder is thoroughly milled to nanometer dimensions using a Spex Certiprep 8000 Mixer/Mill. Hydrothermal synthesis also involves the precipitation ofthe oxide from the precursor salts with a base; however, the reaction is carried out at temperatures between 100° and 350°C in a sealed vessel. Preferably a pressure of less than 15 MPa is used, and the samples are aged for 5 to 60 minutes. Following crystallite formation, the crystallite powders are filtered, washed and dried. The hydrothermal process tends to produce ultra fine powders with a very narrow distribution of particle sizes and shapes. As an example of a mixed oxide, wash-coated catalyst Ceθ2/Zrθ2 in Table 1 was prepared by forming a suspension of Zrθ2 in a solution of Ce(Nθ3)3, followed by precipitation ofthe cerium, filtering, and oxidation in air as described above. Alternatively, for the impregnation/decomposition method, 2 g of Zrθ2 was placed in a beaker, and an appropriate volume of a 0.2 M Ce(N03)3 solution was added slowly with continuous stirring and gentle heating. Addition ofthe nitrate solution was slow enough that the mixture had a paste- like consistency with no standing liquid. After addition ofthe nitrate solution the mixture was dried at ~90°C overnight, ground to a fine powder, then heated at 400°C in air for four hours. After cooling to room temperature, the powder was again ground and passed through a 150 μm sieve. For ceramic processing, a mixture ofthe oxides or carbonates in the appropriate stoichiometric ratios was ball milled for 24 hours, then passed through a 355-μm and a 90- m sieve. The powder was then calcined in a ceramic crucible at 1200 °C for 6 hours. After cooling, the support powder was passed through a 150-μm sieve. This process eliminates problems associated with selective precipitation that might be encountered with coprecipitation; however, the high processing temperatures generally result in catalysts with much lower surface areas. Catalysts are calcined in air prior to any additional treatment, and the calcination temperature and duration is used to adjust the crystallographic properties ofthe material as described above. In particular, the calcination temperature affects the ratio of surface metal to the metals in the bulk oxide, as well as the surface cluster size. However, for Cu-containing analogs reductive pretreatment is used to affect the nature ofthe Cu active sites. For example, Tschδpe et al. showed that after reduction of Cuo.l5CeQ.85θ2-δ at 200°C, the Cu content was 100% Cu + .52 Increasing the reduction temperature to 300° C divided the Cu content to 70% Cu + and 30% CuO, and reduction at 400°C produced 100% CuO. Since Cu + has been suggested to be the active site for CO oxidation, low-temperature reduction is likely favored for similar systems. However, the above discussion only relates to activity for CO oxidation and not selectivity over H2. Since high activity already is easy to achieve, improvements in selective CO oxidation are gained through alternative treatments that enhance selectivity. Accordingly, promising catalyst compositions are tested after exposure to both oxidative and reductive conditions over the temperature range of 100° to 850°C. The catalyst metals Pt and Pd were added to the support powders primarily by incipient wetness/impregnation. For the impregnation method, three approaches were used. In the first approach, 1-mL increments of a 10-mg/mL Pt solution were added to the support powder creating a suspension. The suspension was gently heated and stirred until the water evaporated, followed by addition of another 1 mL of Pt solution. This process was repeated until the desired Pt loading was achieved. In the second approach, only a few drops ofthe Pt solution were added at a time, so that the solution was completely absorbed by the powder. As above, this process was repeated with occasional stirring until the desired metal loading was achieved. For the third approach, the desired volume of Pt precursor solution was mixed with the support powder and rotated under reduced pressure until dry. Following impregnation, the Pt was reduced in a furnace at 300°C for 3 hours under H2 flowing at 100-200 mL/min. Several ofthe catalysts were prepared by adding platinum before the co-precipitation step. For this simultaneous addition method, the appropriate amount of platinum salt was added to the metal nitrate solution before precipitation with the NH4OH so that the Pt was incorporated into the precipitate rather than only on the support surface. Prior to testing, all catalysts were heated at 100 to 200 °C under a flow of air overnight. B. Catalyst Characterization Catalysts were characterized using various methods, including B.E.T. surface area measurements, particle size measurement, metal particle dispersion, Fourier transform infrared absorption (FTIR), X-ray diffraction (XRD), energy dispersive X-ray spectroscopy (EDX), and scanning electron microscopy (SEM). Other methods, including oxygen temperature programmed desorption (TPD) may also be used. Surface Area Analysis. Table 1 presents a summary ofthe surface area measurements for several ofthe catalysts investigated. The surface area analysis was performed using a Micromeritics ASAP-2000 surface area analyzer/porosimeter with nitrogen/helium mixtures. For this work, surface areas were determined from nitrogen volume/partial pressure isotherms using the B.E.T. method. From the table the following can be seen: (i) the Zrθ2 and Zrθ2-containing support materials tended to have much higher surface areas than the Ceθ2 analogs; (ii) incorporation of dopants into Ceθ2 substantially increased the surface area, with Co and Cu giving the greatest increase; (iii) addition of Pt slightly increased the surface area of Ceθ2 supports, decreased the surface area of Zrθ2 supports, and had no effect on the surface area of doped-Ceθ2 supports. Pore size distribution of catalysts was also determined from the multipoint nitrogen isotherm. Initially, it is assumed that adsorption can occur in the micropores ofthe particles. This behavior is manifested as BET-type adsorption at relatively low values of x, followed by a saturation-type (Langmuir) adsorption as the relative pressure is increased, and the pores fill with adsorbate. The adsorption isotherm in this case is expressed in terms of a quantity possessing units of length. Particle Size Measurement. Catalyst particle size measurements were performed using a Shimadzu SALD-2001 Particle Size Analyzer. Measurements were obtained by dispersing catalyst powder in ultra-pure water, which was then passed through a flow cell. A collimated beam from a diode laser was directed through the flow cell and the light diffracted and scattered by the particles was detected by sensors in appropriate positions to detect light from all angles. This arrangement of sensors allows detection of light diffracted and scattered from large and small particles, which enables a particle size range of 0.03 μm to 700 μm to be measured. Laser beam intensity distributions were converted into particle size distributions using Shimadzu software that combines Fraunhofer, Mie and side-scatter processing methods. Information from this technique was used to correlate catalyst particle sizes and distributions to preparation methods and catalytic activity. Metal Particle Dispersion. Group VIII metals used in this work generally adsorb H2 and CO irreversibly at room temperature. The stoichiometry is approximately one H atom or one CO molecule per metal atom, which allows adsorption of these gasses to be used to calculate metal surface area. Based on the determined surface area ofthe metal and the known amount of metal present, the dispersion of metal particles can be calculated. However, two major factors regarding the catalysts in this work must be considered when interpreting such adsorption data. First, Ceθ2 and presumably Ceθ2-based materials adsorb H2 (and O2) which leads to erroneously high dispersion calculations. Second, Ceθ2-supported Pt possibly will have some activity for the oxidation of CO to CO2, even at low temperatures. This second consideration highlights a major factor leading to ambiguous results for dispersion measurements on supported metals, which is the effect of strong support-metal interactions. It has been demonstrated that such interactions produce unpredictable adsorption stoichiometry characteristics leading to inaccurate calculations of metal dispersion. This effect is particularly pronounced for metals deposited onto supports with reductive pretreatment. More than one method may be used to determine metal dispersion. First, CO can be used as the probe molecule and a correction for the amount CO converted to CO2 can be made based on mass spectrometer measurements. Second, transmission-electron microscopy can be used to image the metal particles on the support surface. Measurement ofthe particle diameters will yield a particle size distribution that can be correlated to particle dispersion by making assumptions about the particle shapes. Finally, XRD data can be used to estimate the metal particle sizes, t, according to the Scherrer equation, t = 0.9λ/Bcosθβ where λ is the incident wavelength, B is the peak width at one half of the maximum intensity, and θβ is Bragg angle. This method is only effective for small particle sizes, and is difficult to use at very low metal loading. XRD. XRD analysis was performed on the support powders to confirm their anticipated crystal structures, and determine if the materials are single phase. Diffraction patterns were obtained using wither a Rigaku Miniflex X-ray Diffractometer (Model CN2005) or a Philips PW 1830 with CuK α line radiation (λ = 1.5418 A). Peak positions in the diffraction pattern are determined experimentally as 20 values. Using Bragg's law, the interplanar spacings, d, are determined. Using commercial software (Micro-Index, Materials Data, Inc.), the crystal lattice symmetry and lattice parameters are calculated from the interplanar spacing. This information allows correlation of catalyst powder activity with crystallographic structural parameters, and allows determination if the support materials are single phase or mixed oxides. Figure 3 shows the XRD patterns for Ceθ2 and Zrθ2, and indicates that the ceria is primarily a single-phase fluorite structure material, whereas the Zrθ2 is mostly amorphous. The majority of the doped Ceθ2 support powders demonstrated XRD patterns like Ceθ2, and were determined to be primarily single phase. Examples of these materials include Ceo.8Zro.2θ2-δ > Ceo.8Gdo.2θ2_ 3 Ceo.8Coo.2θ2-δ, Ceo.sCuo.2θ2-δ, and Ceo.8Feo.2θ2-δ, Ceo.48Zro.θ5 Mn 0.48θ2-δ> and Ceo.45 ro.θ5Mno.45Cuo.θ5θ2- - However, examples of catalysts with significant multi-phase contributions include Ceo.8Sro.2θ2-δ and Ceo.sAuo.2θ2-δ (shown in Figure 4) as well as mixed oxide cataysts such as 10%CuO/Ceθ2. The asterisks in Figure 4 identify peaks from the fluorite phase and the x identifies other phases. The broad peak at 2Θ values less than 25 in Figure 4 is a background signal from the sample holder used for small sample sizes. The second phase in the Ceo.8Auo.2θ2-δ powder is from metallic gold; however, the identity ofthe additional phase(s) in the pattern for Ceo.8Sro.2θ2-δ ls not clear. Comparison to XRD patterns for precursors and oxides indicated that the additional peaks were not from SrCθ3 or SrO. Figure 5 shows the XRD patterns for CeCoo.5Cuo.5θ2_δ prepared by co-precipitation from the metal nitrates, and from the metal oxides using ceramic processing. Both samples demonstrated primarily a fluorite structure (indicated with asterisks); however, the sample prepared from the oxides had much greater crystallinity resulting from the higher processing temperatures. Furthermore, contributions from other phases are clearly evident in the latter sample. Specifically, the peaks between 2Θ values of 30 and 50 are from C03O4 and CuO. Table 1. Support and Catalyst B.E.T. Surface Area Measurements EDX. EDX measurements were obtained on a PGT (Princeton Gamma-Tech) X-ray fluorescence detector in combination with a JEOL JSM T200 Scanning Electron Microscope. Figure 6 shows an overlay ofthe EDX spectra for Ceθ2 and Zrθ2- For comparison, Figures 7 and 8 show the spectra for Zrθ2 wash-coated with Ceθ2 (25 wt.%Ceθ2/Zrθ2) and Ceo.8Zro.2θ2- ; respectively. For the wash-coated sample, the Ceθ2 covers the majority ofthe surface ofthe Zrθ2 particles, and the EDX spectra over most ofthe sample surface show peaks only for Ce. However, the spectrum in Figure 7 is from a recess in the surface, and peaks from Zr also are present. The XRD pattern for this support powder (data not shown) shows broad peaks corresponding to the fluorite structure, but the crystallinity appears intermediate between the Zrθ2 and Ceθ2 XRD patterns shown in Figure 3, as would be expected. Alternatively, the EDX spectrum of Ceo.8 ro.2θ2-δ shown in Figure 8 generates peaks for both Ce and Zr over the entire surface, and the XRD pattern demonstrates a crystallinity equivalent to the undoped Ceθ2- These results suggest successful doping of Zr into the Ceθ2 lattice, and are indicative ofthe structural differences between the two materials. Figure 9 contains the EDX spectra for Ceo.8Gdo.2θ2-δ an d clearly indicates the dopants. EDX spectra for other conmpositions, such as Ceo.8Cuo.2θ2- > Ceo.sAuo.2θ2-δ> e 0.8F e 0.2θ2- δ,Ceo.8Coo.2θ2-δ, Ceo.48ZrQ.θ5 no.48θ2-δ, and Ceo.45Zro.θ5Mnθ.45 c uθ.05°2-δ are not shown, but also clearly indicate the dopants present. Since the XRD patterns for these materials corresponded to a single-phase fluorite structure (except for Ceo.8Auo.2θ2-δ) 5 it is assumed that incorporation ofthe dopants by co-precipitation was successful. EDX also was used to qualitatively confirm the relative amounts of Pt loading on the support materials. Figure 10 shows an overlay ofthe EDX spectra for 1 wt.-%Pt, 5 wt.-%Pt, and 10 wt.-%Pt on Ceθ2- The baselines are offset for clarity. The peaks for Ce are visible in all three spectra; however, only the 5% and 10% Pt samples show peaks for Pt. The spectral intensities are not normalized, so a ratio ofthe most intense Ce peak, Ic e , to the most intense Pt peak, Ip t , in each spectrum was used to compare the metal loading. From this data, the Ipt Ice f° r me 10%Pt/Ceθ2 catalysts was more than 1.5 times the value for the 5%Pt/Ceθ2 catalyst, which suggests the incipient wetness/impregnation method for incorporation of Pt was successful. FTIR. The FTIR system used was a Nicolet Impact 410 spectrometer. This system employs a mid-IR source, a Michelson interferometer, and a deuterated triglycine sulfate (DTGS) detector. Calibration ofthe FTIR for peak height, area, and position was accomplished using 38.1- and 76.2- polystyrene films. The catalyst samples were prepared for FTIR analysis by grinding approximately 1 mg of catalyst powder with 75 mg of KBr and pressing the mixture into a pellet. The spectrum of a pellet with KBr only was subtracted from the background of all spectra. Figure 11 shows typical FTIR spectra of a catalyst (here, 5% Pt/Ceθ2) before exposure to VOCs, and after screening with MEK, toluene, and 1-butanol at temperatures well below 100°C. The features in the spectra were very broad, which made identification of specific vibrational bands difficult. The spectra are characterized by absorbance bands between 1250-1402 cnr 1 (a), 1480-1590 cm" 1 (c), and 1580-1680 cnr 1 (d). After screening with VOCs, a peak between 1350-1480 cm - 1 (b) grows in, and this peak is present regardless ofthe VOC used. Essentially the same spectrum has been observed by Haruta et al. for Au/Tiθ2 catalysts exposed to CO (Haruta, M. et al. (1993) J. Catal. 144:175-192) In Haruta's work, peaks (a) and (c) are attributed to carboxylate species that accumulated during the experiment. However, in the present work, peaks in the same region are present even before exposure to VOCs. Peak (b) also can be attributed to symmetric CO2 stretching, however, one would then expect it to correlate with peaks (a) and (c), and be present also before exposure to VOCs. Alternatively, peak (b) could be a combination of methylene CH2 scissoring and CH3 asymmetric bending, and aromatic ring stretching could contribute to both peaks (b) and (c). Peak (a) is from water and also is observed in the spectrum of KBr alone. But peak (a) is much stronger in the spectra ofthe samples than the background, as is the OH stretching between 3000-3600 cm'l (not shown). Additionally, catalysts exposed to toluene and 1-butanol sometimes show bands at 2930 and 2850 cm _ l from aliphatic CH2 stretching. In total, spectra were acquired on seven different catalysts before and after screening with VOCs and all samples showed peak (b) after screening. For comparison, spectra were acquired on bare Ceθ2 and Zrθ2 before and after screenmg with toluene. The bare supports, which were not active at 100°C, showed no difference in spectra before and after screening, and did not show peak (b). An additional peak from NO3" asymmetric stretching at - 1380 cnr 1 was observed in the FTIR spectra of many ofthe support powders and catalysts. Figure 12 shows FTIR spectra of 5%Pt/Ceθ2 prepared under thorough (Preparation #1) and moderate (Preparation #2) Pt reduction conditions. Preparation #2 shows the NO3" asymmetric stretching peak and Preparation #1 does not. It was determined that the presence of this peak was indicative of incomplete thermal decomposition of residual nitrates from the precursors, which also resulted in much lower catalytic activity. Once this fact was determined, several ofthe catalysts were reproduced under more-thorough heat treatment, and those catalysts demonstrated dramatic improvements in activity relative to their earlier analogs. The presence or absence of this peak in the FTIR spectra of catalysts may be used to assess the quality ofthe catalyst preparation. C. Performance Testing and Optimization of Heterogeneous Catalysts for VOC removal Screening Apparatus. Performance testing ofthe catalysts was accomplished using the apparatus shown in Figure 13. The apparatus shown in Figure 13 illustrates two channels for testing in the same apparatus. The following description describes the operation of one channel (A), however the same description applies to channel B, which is identical to channel A. VOC gas cylinder (5) is connected to on/off valve (18) through connecting tubing (70). On/off valve (18) is connected to needle valve (24) through connecting tubing (70). Needle valve (24) is connected to flow meter (30) through connecting tubing (70). Air cylinder (10) is connected to on/off valve (19) through connecting tubing (70). On off valve (19) is connected to needle valve (25) through connecting tubing (70). Needle valve (25) is connected to flow meter (31) through connecting tubing (70). Flowmeters (30 and 31) are connected to port (33) by connecting tubing (70). Connecting tubing (80) connects port (33) to 4-way switch valve (35). 4-way switch valve (35) is inside insulated box (75). 4-way switch valve (35) is connected to catalyst chamber (55) through comiecting tubing (85). Catalyst chamber (55) is connected to another 4-way switch valve (35) through connecting tubing (85). 4-way switch valve (35) is connected through connecting tubing (85) to sample port (45). Sample port (45) is connected to gas chromatograph (65) through through ten- port switch valve (60) which enables alternating on-line GC measurements between the A and B sides ofthe catalyst screening apparatus. Air cylinder (10) is also connected to on/off valve (20) through connecting tubing (70). On/off valve (20) is connected to needle valve (26) through connecting tubing (70). Needle valve (26) is connected to flow meter (32) through connecting tubing (70). Flowmeter (32) is connected to 4-way switch valve (35) through connecting tubing (70). 4-way switch valve (35) is connected to blank reactor (50) which contains no catalyst through comiecting tubing (85). Blank reactor (50) is connected to another 4-way switch valve (35) through comiecting tubing (85). 4-way switch valve (35) is connected through connecting tubing (85) to sample port (45). Bubble meter (40) is attached to 4-way switch valve (35) through connecting tubing (70). In operation, gas from VOC gas cylinder (5) containing a selected concentration of VOC (typically 200 ppm VOC in a balance of air) flows through connecting tubing (70) to on/off valve (18), needle valve (24) and flow meter (30). Air from air cylinder (10) flows through connecting tubing (70) to on/off valve (19), needle valve (25) and flow meter (31). The VOC and air streams pass through port (33) into insulated box (75) through comiecting tubing (80). The concentration of VOC is controlled by mixing the effluent from the VOC cylinder with an appropriate amount of air. The mixture flows through 4-way switch valve (35) into the catalyst reaction chamber (a 10-cm long by 0.4-cm i.d. tubular quartz cell (55) containing approximately 0.2 g of catalyst was used for each run, which created a 1-cm catalyst column in the reactor) , which was packed between two pads of quartz wool, and held in place with two narrower inner tubes. After passing through catalyst reaction chamber (55), the gas flows through connecting tubmg (85) into 4-way switch valve (35) into sample port (45). Sample port (45) allows passage ofthe sample into gas chromatograph (65) through ten- port switch valve (60) which enables alternating on-line GC measurements between the A and B sides ofthe catalyst screening apparatus. Air from air cylinder (10) also passes through on/off valve (20), needle valve (26) and flow meter (32) into insulated box (75) through tubing (70), where the air is passed through blank reactor (70) which contains no catalyst. Bubble meter (40) is attached to 4- way switch valve (35) through connecting tubing (70). Flow rates through the catalyst and blank lines were confirmed using a bubble meter (40), and equilibrated by varying the packing density of quartz wool in the blank. Comparison ofthe gas mixture through the blank reactor to the catalyst reactor allows determination ofthe amount of VOC removal. The majority ofthe apparatus is enclosed in an insulated box and heated with heat tape for temperature control. External gas lines are also wrapped in heat tape to minimize condensation of VOCs. The online GC (Shimadzu GC-14A) is equipped with a flame ionization detector (FID) for analysis ofthe unreacted VOC as well as other hydrocarbon reaction products. Sampling ports are installed on the exit ofthe system for analysis of CO2 product from the catalytic destruction. The CO2 was analyzed on a second GC (Hewlett-Packard 5890) equipped with a thermal conductivity detector (TCD). For determining the concentrations of VOCs, generally calibration curves of peak height and area as a function of VOC concentration were prepared over the range of 1 to 200 ppm. Concentrations were controlled by mixing effluent from the 200 ppm VOC/air cylinder (5) with air from a second line (10), shown in the apparatus diagram. For CO2 calibration, a cylinder of 1000 ppm CO2 was used to prepare a calibration curve over the concentration range of 5 to 1000 ppm. Detection limits for the FID GC were below 1 ppm and for the TCD GC were below 5 ppm. Space velocities, V s , were calculated based on the volume ofthe catalyst in the reactor and the gas stream flow rate, L, according to the equation, v,= 4L πD 2 H where D is the inner diameter ofthe reactor tube, and His the height ofthe catalyst bed. Typically, 0.2 g of catalyst were used for each analysis, which produces a catalyst bed - 1 cm long in a 0.4-cm-diameter reactor tube. Flow rates across the catalyst were typically between 2 and 20 mL/min which produced space velocities between 1000 and 15,000 hr 1. Alternatively, each channel may be enclosed in a separate heater to control the temperature of each reactor individually enabling different measurement temperatures or separate experiments to be conducted simultaneously. Different gases may be used. Poisons may be added to determine their effect on the catalysts. Other embodiments ofthe testing apparatus may also be used, as easily determined by one of ordinary skill in the art without undue experimentation. Performance Testing ofPt- or Pd- containing catalysts. Table 2 contains a summary ofthe performance evaluation for some ofthe catalysts investigated that contain Pt or Pd. The following VOCs were tested: toluene, methyl ethyl ketone (MEK) and 1-butanol. The VOC concentrations on the inlet stream typically were between 50-200 ppm in air, and the space velocities were between 1000-7000 hr 1. Table 2. Performance Evaluation for Some Catalysts Containing Pt and Pd* *VOC concentrations were between 100-200 ppm in air, and space velocities were between - 1000-7000 hr-1. **This composition is most likely a combination of Ceι_ x Cu x 02- and CuO. Comparison ofCeθ2 andZrθ2 Supports. From Table 2, most ofthe catalysts from #1-12 gave greater that 70% conversion of toluene to CO2 at 150° C, and the Pt-based catalysts generated between 40 and 88% conversion at 100°C. Furthermore, the 5% Pt/Zrθ2 and 5% Pt/Ceθ2 catalysts produced between 40 and 50% conversion at 80 °C. For the bare support materials (absent Pt or Pd) Ceθ2 produced 45% conversion of toluene to CO2 at 200°C, and 7% conversion at 150°C. However, despite having a much higher surface area, Zrθ2 produced only 27% conversion at 200 °C, and 4% conversion at 150° C. Figure 14 demonstrates the effect ofthe Ceθ2 versus the Zrθ2 support materials on the catalytic behavior as a function of time for 5% Pt-loaded catalysts at several temperatures. The space velocity was about 2000 hr 1. The first points for each line were obtained at 150°C, and the activity was established within the first 15 to 30 minutes. The temperature was then dropped to 100°C, which is concurrent with the drop in % conversion to less than 10% for second set of data points. However, over the next several hundred minutes activity was reestablished, which is seen with the third and fourth data points for each line. The temperature was then reduced to 80°C. At 80°C, activity was again established and the drop-off in the curve with time is from the deactivation ofthe catalyst. The induction period necessary to reach full activity is apparent in Figure 14 for 100° C and 80 °C. Once activity had stabilized, a reduction in temperature caused the activity to drop off, followed by reestablishment of activity. The time period for stabilization generally was longer at lower temperatures, which is also visible in Figure 14. The 5% Pt/Ceθ2 catalyst demonstrated good agreement for toluene destruction based on toluene removal and CO2 production, with an approximate difference of 10%. The toluene removal percentage generally followed the same trend for CO2 production with the 5% Pt/Ceθ2 catalyst, but did not demonstrate an induction period after reducing the temperature . The 5% Pt/Zrθ2 catalyst showed a greater than 95%) toluene removal throughout the duration ofthe experiment This is compared with the much lower values based on CO2 production. Despite this large difference in values between the two curves for 5% Pt/Zrθ2, no other product species were identified in the chromatograms. The disparity of values of % toluene removal and CO2 production is likely due to the facilitation of adsorption and retention of toluene as well as the production of nonvolatile material on the Zrθ2 catalysts by the high surface area ofthe 5% Pt/Zrθ2 catalyst. In fact, the catalyst deactivation at 80 °C is much steeper for the Zrθ2-supported Pt than the Ceθ2-supported Pt (see Figure 14). Furthermore, although observed only qualitatively, upon ramping the catalyst materials back up to 100°C large amounts of toluene were liberated from the Zrθ2 catalyst relative to the Ce0 2 - Comparison ofPt andPd. Figure 15 is a comparison ofthe percent conversion of toluene to CO2 by 1% Pt and 1% Pd on Ceθ2- For the Pt catalyst, activity was established immediately at 150°C, whereas the Pd catalyst increased in activity slowly over the first day of testing. As in Figure 14, reducing the temperature to 100°C dropped the activity to only a few percent. Testing was not continued beyond this point for the Pd catalyst, but the activity for the Pt catalyst was reestablished to almost 40%. This trend is also observed when comparing the l%Pt/12%Ceθ2/Zrθ2 and 5%Pt/12%Ceθ2/Zrθ2 catalysts to the l%Pd/12%Ceθ2/Zrθ2 and 5%Pd/12%Ceθ2/Zrθ2 catalysts in Table 2 (#13-16). For example, at 100°C the l%Pt/12%Ceθ2/Zrθ2 generated nearly complete conversion of toluene to CO2, whereas the l%Pd/12%Ceθ2/Zrθ2 generated only 10%) conversion. Comparison of Preparation Methods. By far the most significant step in the catalyst preparation procedure was determined to be associated with the exact conditions during the reduction ofthe catalytic metals (Pt and Pd) on the support powder. It is critical that the conditions are carefully controlled to ensure that a thoroughly reductive environment and adequate temperatures are maintained. It was determined that the catalysts with the highest activity were being reduced in a low- volume furnace with very even heating profiles, and no potential sources for leaks to the exterior atmosphere. Conversely, the catalysts with low activity were reduced in a furnace with opposite qualities. With this knowledge, the 5%Pt/Ceθ2 catalyst in addition to several doped-Ceθ2 catalysts were re-synthesized and screened for both toluene and MEK destruction. These materials are in Table 2 as catalysts #39-44. The first catalyst in the series (5%Pt CeCoo.5Cuo.5θ x ) showed only minor improvements, i.e. 61% conversion of toluene to CO2 at 100°C compared to 52% for the original analog. However, most ofthe other catalysts demonstrated more significant improvements. Specifically, the original 5%Pt/Ceθ2 (#4) catalyst demonstrated high activity for destruction of toluene, 1-butanol and MEK. However attempts to reproduce those results with batches prepared in a different reduction furnace failed (see batch #35 and 38 in Table 2). However, once the problem was identified, the results were reproduced and are shown in Table 2 for batch #40. The 5%Pt/Ceo.8 ro.2θ2- catalyst (#26 and #41) showed only modest improvement in toluene destruction, but the MEK destruction went from 0% to 35% at 80°C. Similarly, the 5%Pt/CeQ.sCuo.2θ2-δ catalyst (#28) previously demonstrated 35%) and 14% conversion of toluene and MEK to CO2 at 80°C, respectively; whereas, the resynthesized analog (#42) demonstrated 61% conversion of toluene and 39% conversion of MEK. The Fe-doped catalyst previously demonstrated negligible activity at 100°C (#31). However, the resynthesized batch (#43) had significant activity for both toluene and MEK destruction at 80 °C, and for MEK destruction at 60 °C. Finally, the first batch ofthe 5%Pt/Ceo.8Coo.2θ2-δ catalysts (#33) gave only 2% conversion of toluene to CO2 at 80°C, whereas the resynthesized batch (#44) gave 10% conversion of toluene, and 25% conversion of MEK at 80°C. In addition to the fact that the catalysts reduced in the preferred furnace demonstrated greater activity for VOC destruction, these catalysts also did not showNθ3 _ asymmetric stretching in the FTIR spectra. Nearly all ofthe catalysts presented were prepared by coprecipitation. As mentioned earlier, this method results in much higher surface area materials, and therefore a greater number of catalytically active sites. However, with coprecipitation it is possible that some ofthe components are selectively precipitated to a greater extent than others, and the resulting material composition might not be what was intended. In Table 2, the activity of 5%Pt/CeCoo.5Cuo.5θ2-δ prepared by coprecipitation (#39) can be compared to the same material prepared by ceramic processing from the constituent oxides (#45) for the destruction of toluene. At 150°C, the catalyst from coprecipitation gave 100% conversion to CO2 compared to 85% for the material from the oxides. At 80 °C, the coprecipitated and oxide-generated materials gave 11% and 3% conversion, respectively. Given the large differences in the material surface areas, the resulting catalytic activities are surprisingly similar. The method of metal addition to the support materials also was briefly investigated for Pt and Pd on the 12%Ceθ2/Zrθ2 supports. In the first method, which was used almost exclusively in this project, the Pt and Pd was added to the support powder from the appropriate Pt or Pd salt solution as described above. In the second method (simultaneous addition), the Pt or Pd nitrate was dissolved in the Ce nitrate solution before co-precipitation onto the Zrθ2- Based on results reported in the literature, in was anticipated that the simultaneous addition method would result in greater metal particle dispersion, and thus greater activity (Haruta, et al. (1989) J. Catal. 115:301-309). However, as evident in Table 2 (catalysts #13-20), the first method resulted in much higher activity. It is likely that the simultaneous method results in a relatively large quantity ofthe Pt or Pd being buried in the Ceθ2 wash coat, and therefore not available for interaction with VOCs in the gas stream. Metal Loading. To investigate the effect of Pt loading on Ceθ2 for the oxidation of VOCs, catalysts composed of 1%, 5%, and 10%Pt/Ceθ2 were prepared and screened under identical conditions. The EDX data for all three catalysts were presented earlier in Figure 10, and demonstrated a relative increase in peak intensity for Pt as a function of loading. Table 3 shows the results for % conversion of MEK to CO2 as a function of Pt loading for 80°C and 60°C, and demonstrates a maximum in activity for 5% Pt. This reduction in activity at higher Pt loading is probably the result of a decrease in Pt dispersion. Table 3. Comparison of catalytic activity for MEK destruction as a function of Pt loading for a Pt/Ceθ2 support.* *The MEK concentration was -100 ppm in air and the space velocity was ~1000 hr 1. However, a different trend is observed for Pt on a 12%Ceθ2/Zrθ2 support as demonstrated in Table 4. For this catalyst, significantly higher % conversions of toluene to CO2 were observed for only 1%) Pt loading at both 100°C and 80 °C. Furthermore, Table 5 demonstrates that the dependence of catalytic activity on metal loading is dependent on the specific VOC. In this case, the exact same catalysts screened in Table 4 were screened for destruction of 1-butanol, and maximum activity was observed for the 5% Pt loading. Table 4. Comparison of catalytic activity for toluene destruction as a function of Pt loading for a Pt/12%Ceθ2/Zrθ2 support.* *The toluene concentration was -100 ppm in air and the space velocity was -1000 hr 1. Table 5. Comparison of catalytic activity for 1-butanol destruction as a function of Pt loading for a Pt/12%Ceθ2/Zrθ2 support.* *The 1-butanol concentration was -100 ppm in air and the space velocity was -1000 hr 1. Generally, activity reaches a maximum between 3% and 5% loading by weight. Toluene and MEK Mixtures. To investigate catalytic activity toward mixtures of VOCs, an experiment was performed that followed the simultaneous decomposition of toluene and MEK, and the results are shown in Figures 16A and 16B. For this experiment the toluene concentration was held roughly constant, and the MEK concentration was gradually increased while monitoring the removal of both VOCs and the production of CO2. In actuality, dilution ofthe toluene stream occurred significantly at the higher MEK concentrations. This problem is somewhat unavoidable if a constant total flow rate is to be maintained using ball-type flow meters. This problem may be alleviated by using bubble flow meters. This experiment was ran at 150°C with the 5%Pt/Ceθ2 catalyst. The figures are divided into eight sections (a through h) that differ in the toluene and MEK concentrations as follows: (a) toluene -212 ppm, MEK -0 ppm, (b) toluene -205 ppm, MEK -0.9 ppm, (c) toluene -203 ppm, MEK -2.6 ppm, (d) overnight heating with air only, (e) toluene - 199 ppm, MEK -7.5 ppm, (f) toluene -177 ppm, MEK -19 ppm, (g) overnight heating with air only, (h) toluene -132 ppm, MEK -56 ppm. The percent activity was calculated based on the removal of each VOC, and from the conversion ofthe total VOC concentration to CO2. The small dips in the curves for CO2 in sections (c) and (f) are the result of bypass measurements. In order to determine the toluene and MEK concentrations entering the reactor, the flow was diverted to a bypass line and replaced with a flow of air over the catalyst. Thus, reestablishment of VOC flow over the catalyst resulted in a small induction period to regain activity. Similarly, the catalysts were maintained at 150°C under a flow of air overnight, which resulted in greater induction periods at the beginning of the day in sections (a), (e), and (f). Figure 16A shows that the total percent conversion of toluene and MEK to CO2 reaches a maximum of greater than 80% for each set of concentrations. This experiment used a sample of catalyst prepared under non-optimal reduction conditions. The % conversion would be greater if the catalyst was prepared under optimal reduction conditions. Additionally, the percent removal of toluene and MEK remains above 95% for each set of concentrations. The curves for toluene and MEK removal are shown expanded in Figure 16B. The data in Figure 16B also show an induction period for each set of concentrations, and suggest that there is a slightly larger percent removal of toluene than MEK. The difference in percent removal of these two VOCs appears to decrease as the difference in their concentrations is reduced. Despite the relatively high temperature of this experiment (150°C) there remains about a 16%) difference between the activity based on VOC removal and CO2 production. At most, a few percent of this difference can be attributed to other oxidation products observed in the chromatograms during the early part ofthe experiment (sections b, c, and e in Figures 16A and 16B). However, the identity ofthe other oxidation products varied between chromatograms. Based only on retention times, some ofthe other products may be acetone, benzene, and hexanone. Catalyst Preconditioning. Figure 17 demonstrates the effect of preconditioning the catalysts at elevated temperatures before screening. The upper and lower curves both correspond to activity based on conversion of toluene to CO2 for the 5%Pt/Ceo.8Sro.2θ2-δ catalyst. The difference between the two curves is that the catalyst for the upper curve was screened at 130°C for almost 200 minutes under a flow of toluene before the temperature dropped to 100°C. For the lower curve, the catalyst screening was started at 100°C. The activity for the experiment in the upper curve is substantially higher, and shows the characteristic induction period at each temperature. This same trend also was observed for the catalysts l%Pt/12%Ceθ2/Zrθ2 and l%Pt/Ceo.8Cuo.2θ2- - F° r l%Pt/12%Ceθ2/Zrθ2, starting the catalyst screening at 100°C produced greater than 90% conversion to CO2, and reducing the temperature to 80°C produced greater than 45% conversion. However, for the same catalyst started at 80°C, the highest achievable conversion was only 17%. Similarly, for l%Pt/Ceo.sCuo.2θ2-δ starting at 130°C gave greater than 50% conversion, and reducing to 100°C still gave greater than 17% conversion. The same catalysts started at 100°C gave a maximum activity of only 9% conversion to CO2. Therefore, the data from the screening of these three catalysts suggest that to optimize activity at lower temperatures, the catalysts should be first exposed to temperatures high enough to obtain significant conversion to CO2. The significance ofthe catalyst preconditioning is underscored by the data for MEK destruction by 5%Pd/Ceθ2 shown in Figure 18. This plot shows the preconditioning at 150° C under a flow of MEK, followed by screening at 80°C (the induction period for 80 C C is not shown). The activity at 80°C dies off slowly over 2844 minutes (-2 days) from 28% to 11%. However, heating the catalyst at 150°C for 288 minutes under a flow of MEK (break in the plot) restored activity and resulted in even higher conversions to CO2 of 35%. During the reconditioning cycle initial CO2 concentrations greater than 2000 ppm were observed, followed by a rapid decrease. These results suggest that deactivation ofthe catalyst results from build up of organic material that can be removed from the catalyst surface by high temperature cycling. The data shown in Figures 17 and 18 demonstrated that pretreating the catalysts at elevated temperatures under a flow of VOCs resulted in much higher catalytic activity. Based on these results, it is possible that an activated intermediate necessary for the complete destruction of VOCs is being generated more quickly at the higher temperatures, which then facilitates the catalytic combustion when the temperature is reduced. To test this possibility, the experiments were repeated, but the catalyst conditioning was performed in a flow of air only. It was determined that conditioning in air had the same beneficial effect as conditioning in a VOC flow, and that catalytic activity could be restored after deactivation by heating in air at 150°C. Therefore, it is likely that the heat treatment is simply oxidizing and desorbing hydrocarbons, oxidation products, and water, that are occupying active sites on the catalyst. In fact, a fresh catalyst sample was heated at 180° C for several hours under air, and liberated -50 ppm of CO2 initially, which gradually dropped off to zero after about 2.5 hours. FTIR results supporting these conclusions are not shown. Effect of Dopant Concentration. The effect ofthe dopant concentration on the catalytic activity for Ceθ2-based supports was determined for both Cu and Sr dopants, and the results are presented in Figures 19 and 20, respectively. Figure 19 shows the % conversion of toluene and MEK to CO2 at both 150°C and 80°C for 5%Pt/Ceι_ x Cuχθ2_ 5 where x = 0.1, 0.2, and 0.5. A direct comparison between the toluene and MEK data was not possible since the toluene runs were performed at a space velocity of -4000 hr 1, and the MEK runs were performed at -2600 hr 1. However, for each curve the maximum activity was obtained with the 5%Pt/Ceo.8Cuo.2θ2-δ catalyst. Similarly, Figure 20 shows the results for 5%Pt Ceι-.χSrχθ2-δ with x = 0.1, 0.2, and 0.5. Although the difference between the catalysts was not a great as for the Cu-doped catalysts, the 5%Pt/Ceo.8Sro.2θ2-δ had generally greater activity. For 1-butanol, the 5%Pt/Ceθ2 catalyst gave 95% conversion to CO2 at only 60°C, with light-off temperatures (50% conversion to CO2) between 40°C and 60°C. For MEK, this catalyst demonstrated light-off temperatures between 60 °C and 80 °C. For toluene, which is typically more difficult to oxidize, the light-off temperature was between 80°C and 100°C. However, doping the Ceθ2 with small amounts of Cu resulted in over 60% conversion of toluene to CO2 at 80°C. Additionally, a catalyst with only 1% Pt loading on a mixed Ceθ2/Zrθ2 support generated near light-off conversion of toluene at 80°C, and near complete conversion at 100°C. Three major factors affecting the activity of noble metal containing catalysts were determined." 1) there is a temperature-dependent induction period for these materials to reach full activity for conversion ofthe representative VOCs to CO2, 2) the catalysts should be pre-conditioned at temperatures of approximately 150°C or greater under either oxidizing or reducing conditions, and 3) the exact conditions during the reduction ofthe catalytic metals (Pt and Pd) must be carefully controlled to ensure that a thoroughly reductive environment and adequate temperatures are maintained. These factors were not appreciated during the screening of all ofthe catalysts, and the conversion values for many of them do not represent optimal conditions. Specifically, catalysts #1-12 in Table 2 were prepared under adequate conditions, and they were inadvertently preconditioned by screening at relatively high temperatures. However, once conversion rates substantially above the light-off value were achieved the temperature was reduced. This factor explains why higher conversion values are reported at lower temperatures for several ofthe materials (catalysts #2 and #4, in Table 2, for example). The reported conversion values for the block of catalysts from #13-34 in Table 2 are likely well below the optimal values, since none ofthe above three factors were considered in the screening. Performance Testing of Metal Oxide Catalysts Without Noble Metals Table 6 contains a summary of some ofthe catalysts screened that did not contain noble metals. For each catalyst, the table contains the composition, preparation method, and percent conversion of 100 ppm toluene (in air) to CO2 at 200 °C and a space velocity of approximately 6,000 hr 1. The percent conversion values are averages from steady state conditions over an approximately 24-hour period. Except where noted, these catalysts maintained activity over the duration ofthe tests. Most ofthe mixed oxide catalysts in the table used commercial metal oxides as the support (e.g. Ceθ2, CuO, Fβ2θ3, etc.), and have BET surface areas below 40 m^/g. However, as indicated, several ofthe mixed oxide catalysts used Ceθ2 prepared by precipitation ofthe corresponding nitrate, and these materials have higher surface areas. The first ten catalysts listed in Table 6 are either mixed Cu and Ce oxides or Cu-doped Ceθ2- The first two catalysts compare the effect of using either CuO or Ceθ2 as the support. Although the 10%Ceθ2/CuO (No. 1) produced a higher mean activity (33%), this catalyst was one of only two that showed significant deactivation over the test period. Alternatively, 10%CuO/Ceθ2 (No. 2) demonstrated a very stable conversion rate of 19%. Catalysts No. 2 through 5 all had the same composition, except the surface areas and preparation methods differed. Catalysts No. 2 and 3 compared the effect of preparation method on the lower surface area materials, and demonstrated that ppt/dep produced about twice the activity for toluene destruction as imp/dec. Catalysts No. 4 and 5 compared the effect of preparation method on the higher surface area materials, and demonstrated the reverse behavior. In this case the preparation method was much more significant, and the imp/dec catalyst (No. 4) gave 100% conversion of toluene to CO2. It is possible that for the higher surface area Ceθ2 support powder, the precipitant (NH4OH) did not effectively penetrate the crevasses of the surface roughness features. Subsequent washing ofthe precipitate would have removed excess nitrate, and resulted in less CuO in contact with the Ceθ2 support after the oxidation step. The Ceι-. x Cuχθ2-δ catalysts (No. 6 through 10) had the highest surface areas and overall highest activity. It should be noted that the FTIR spectra of Ceo. Cuo.2O1.8 indicated the presence of NO3", which was determined to inhibit catalyst activity. Finally, X-ray diffraction (XRD) analysis of this series of catalysts on very small sample sizes with a low-resolution instrument showed the characteristic pattern for Ceθ2 without contributions from CuO. A comparison of catalysts containing Mn also was performed (No. 11 through 14). As with the Cu-containing catalysts, No. 11, 12, and 13 compared the effect of using Ceθ2 versus Mnθ2 as the support (Mnθ2 is actually a combination of Mn^ + and Mn4+). Each catalyst was stable, but the Ceθ2-supported Mnθ2 (No. 12 and 13) had much higher activity. Furthermore, the 10%Mnθ2/Ceθ2 catalyst prepared by imp/dec (No. 12) was more active and much more stable than the analog prepared by ppt/dep (No. 13). Finally, the higher surface area analog of 10%Mnθ2/Ceθ2 (No. 14) prepared by ppt/dep was significantly less active than the lower surface area versions prepared by ppt/dep and imp/dec. A higher surface area 10%Mnθ2 Ceθ2 catalyst has been prepared by imp/dec. The Fe-, Co-, and Zr-containing catalysts (No. 15 through 22) were much less active than the Cu and Mn analogs. Also, the 10%Zrθ2/10%MeO x /Ceθ2_δ catalysts, where Me is Cu, Mn, Fe, or Co, all had low or negligible activity (No. 23 through 26). Lastly, a Gd-doped ceria catalysts has been screened (No. 27) and demonstrated an 80% conversion. Table 6. Summary of Catalyst Screenin g of Catalysts without Noble Metals BET Surface Preparation % Conversion of Toluene No. Composition Area (rn^/g) Method* to CO 2 at 200°C** 33 1 10%CeO 2 /CuO 8 Imp/Dec (deactivated) 2 10%CuO/Ceθ2 11 Imp/Dec 19 3 10%CuO/Ceθ2 12 Ppt/Dep 44 10%CuO/CeO 2 41 Imp/Dec 100 4 (higher surface area ceria) 10%CuO/CeO 2 5 41 Ppt/Dep 8 (higher surface area ceria) 91 6 Ceo.9Cuo.iO1.9 85 Co-ppt (sv > 12,000 l r-1) 7 Ceo.8Cuo.2θι.8 120 Co-ppt 31 8 Ceo.7Cuo.3O1.7 125 Co-ppt 48 9 Ceo.6Cuo.4O1.6 179 Co-ppt 100 10 Ceo.5Cuo.5OL5 172 Co-ppt 100 11 10%Ceθ2/Mnθ2 12 Imp/Dec 7 12 10%MnO 2 /Ceθ2 12 Imp/Dec 62 58 13 10%Mnθ2/Ceθ2 12 Ppt/Dep (slowly deactivated) 10%MnO2/Ceθ2 14 32 Ppt Dep 16 (higher surface area ceria) 15 10%Ceθ2/Fe2θ 11 Imp/Dec 4 16 10%Fe2θ3/CeO 2 19 Imp/Dec 46 17 10%Fe2θ3/Ceθ2 23 Ppt/Dep negligible 18 10%Ceθ2/Cθ3θ4 9 Imp/Dec 23 19 10%Cθ3θ4/Ceθ2 15 Imp/Dec negligible 20 10%Cθ3θ4/Ceθ2 16 Ppt/Dep negligible 21 10%ZrO 2 /CeO 2 18 Imp/Dec negligible 22 10%Zrθ2/Ceθ2 26 Ppt/Dep negligible 23 10%ZrO /l 0%CuO/CeO 2 27 Imp/Dec 19 24 10%Zrθ2/l 0%Mnθ2/CeO 2 36 Imp/Dec negligible BET Surface Preparation % Conversion of Toluene No. Composition Area (m^/g) Method* to CO 2 at 200°C** 25 10%ZrO 2 /10%Fe 2 θ3/Ceθ2 35 Imp/Dec 15 26 10%ZrO 2 /l 0%Co 3 04/Ce02 33 Imp/Dec negligible 27 Ceo.95Gdo.05Ol.98 78 Co-ppt 80 imp/dec = impregnation decomposition; ppt/dep = precipitation/deposition; co-ppt : coprecipitation. Toluene concentration was approximately 100 ppm in air, and the space velocity was approximately 6,000 hr 1, except where noted. Screening period was at least 24 hours. Table 7 contains a data indicating the activity of some metal oxide catalysts screened for conversion of toluene to CO2 at 150° C. The concentration of toluene was - 100 ppm in air, the space velocity was at least 6,000 hr 1, and the temperature was 150°C. Additive-free Ceθ2 and Mnθ2 are included in the graph for comparison. Many ofthe catalysts had activity between or below Ceθ2 and Mnθ2; however, Ceo.8Mno.2θ2- and Ceo.5Feo.lCuo.4θ2-δ demonstrated significant improvements with 50% and 75% conversion of toluene to CO2, respectively. These conversion values were very stable over the 48-hour test period. Table 7. Summary of screening data for catalytic conversion of toluene to CO2 for various catalyst compositions. A series of catalysts also were screened for conversion of 1-butanol to CO2, and these results are shown in Table 8. Again, the temperature was 150°C, the concentration of 1-butanol was - 100 ppm in air, and the space velocity was at least 6,000 hr" 1 . Each of these catalysts gave high activity for destruction of 1-butanol, but the results for Ceo.48Zro.θ5 no.45θ2_δ were particularly good. In addition to generating 100% conversion at 150°C, this catalyst gave 42% conversion at 100°C, and 15%> conversion at only 80°C. Moreover, the 15% conversion achieved at 80°C was very stable over a 96-hour test period. The results for Ceo.48Zro.θ5Mno.45θ2_δ are summarized in Table 9. Table 8. Summary of screening data for catalytic conversion of 1-butanol to CO2 for various catalyst compositions. Table 9. Percent conversion of 1-butanol to CO2 as a function of temperature for Ceo.48Zro.05 Cu 0.48θ2-δ-* *The 1-butanol concentration was -100 ppm in air, the space velocity was at least 6,000 hr 1, and the temperature was 150°C. Performance Testing ofCeθ2~Based Catalysts Incorporating Cu Activity Measurements and Characterization. The catalyst screening results for conversion of toluene to CO2 are shown in Table 10 for a series of Ceθ2-based catalyst incorporating Cu. The catalysts were either Cu-doped Ceθ2, or mixed Cu and Ce oxides. The results are presented for both Pt-free and Pt-containing analogs. The concentration of toluene in the feedstream was approximately 100 ppm (in air) and the space velocity was approximately 6000 hr 1. Table 10 contains the catalyst compositions and percent conversion of toluene to CO2 at each temperature. Most ofthe catalysts were prepared by coprecipitation ofthe constituent metal nitrates using NH4OH; however, as indicated in the table, an analog of Ceo.6Cuo.4Oi 6 also was precipitated using NaOH. Incorporation of Pt was performed by incipient wetness impregnation. Table 10. Summary of Screening Results for Ce/Cu-Based Catalysts* For most ofthe catalysts in Table 10 there was a clear increase in activity upon addition of 1% Pt. The most active catalyst in Table 10 was l%Pt/Ceo.7Cuo.3θι.7, which produced a very stable 32% conversion of toluene to CO2 at 100°C. For the Pt-free materials there was a dip in activity for the 20% and 30% Cu doped catalysts, in contrast to 5% Pt-loaded Ceι_χCu x θ2- - However, for the 1% Pt-loaded catalyst, there was no discernable trend in activity. These observations likely are the result of subtle differences in the Pt addition step that result in incongruities in the exact Pt loading and dispersion between samples. To gain insight into properties ofthe Cu-doped Ceθ2 catalysts, the catalysts were characterized by X-ray diffraction (XRD), Fourier-transform infrared (FTIR) spectroscopy, and energy dispersive X-ray spectroscopy (EDX). The XRD results are shown in Figure 21 for Ceι_ χCu χ θ2-δ without Pt, where x is 0.1 (A), 0.2 (B), 0.3 (C), 0.4 (D), and 0.5 (E). The catalysts were prepared by coprecipitation using NH4OH. The peaks marked with an asterisk are due to the Ceθ2 fluorite structure and the peaks marked bg are background from the aluminum sample holder. As the Cu content increases from x = 0.1 to x = 0.5, there is a broadening ofthe peaks indicating a reduction in crystallinity. However, there is no shift in peak positions, so it is not clear if Cu is being incorporated into the Ceθ2 lattice, or if it is in the form ofthe oxide (CuO or Cu2θ). The XRD patterns (not shown) for the Pt-loaded Ceι_ x Cu θ2-δ analogs over the narrow range of 39° < 2Θ ≤ 41 °, show the peak for Pt at approximately 39.8°. The EDX spectra (not shown) for the Pt-free Ceι_ x Cu x θ2- catalysts showed large peaks for Ce, but peaks for Cu were only visible once a doping level of 40% was reached. The height ratio of the most intense Cu peak to the most intense Ce peak for 40% and 50% Cu doping was approximately the same (Cu/Ce - 0.11). The FTIR spectrum for the Pt-free Ceo.9Cuo.1O1 9 catalyst shows a majority ofthe peaks in the spectrum from carbonate species, which are located at approximately 850, 1058, 1350, 1530, and 1640 cm"l. Also, there was a broad weak peak for chemisorbed CO centered at -2050 cm _ l. An intense broad peak between -2700 to 3700 cm ~ l was mostly from undissociated water, but OH stretching from hydrogen bonding also was seen at -3400 cm"l and -3600 cm-l . The most significant peak in the FTIR spectra for the catalysts was the NO3" asymmetric stretching located at 1385 cm - 1 . It was detennined that the presence of NO3" resulted in a dramatic decrease in oxidation activity for Pt-loaded catalysts. The NO3" peak was most intense for Ceo.8Cuo.2Oi.8, so this factor might have contributed to the reduced activity of that catalyst. However, Ceo.9Cuo.1O1 9 was rather active and, as shown in the figure, also had a substantial NO3" peak. The Ceo. Cuo.4O 6 and Ceo.5Cuo.5O1 5 catalysts had the weakest NO3" peaks and had the highest activity. Based on these results, in the future the oxidation step during catalyst syntheses will be performed at higher temperatures or for longer periods of time to ensure complete decomposition ofthe nitrate precursors. Comparison ofNH40HandNaOHPrecipitants. The amount of Cu in the catalysts prepared by coprecipitation using NH4OH might be overestimated due to complex formation between NH4 "1" and Cu2+. This expectation was qualitatively confirmed by the deep blue color ofthe filtrate after precipitation. To circumvent this problem, an analog of Ceo.6Cuo.4O1 6 was prepared using NaOH as the precipitant. In this case, the filtrate was very pale blue indicating much more Cu was precipitated with NaOH than NH4OH. Further confirmation was attained by comparing the XRD patterns for the two analogs. Figure 22 shows the XRD pattern for Ceo.6Cuo.4O . precipitated with NaOH, and the pattern for the version precipitated with NH4OH was shown in Figure 21. In both figures the characteristic fluorite peaks are visible; however, in Figure 22 two peaks for CuO also are present (marked with an X), which is expected for 40% Cu doping. Moreover, the EDX spectra for both materials (not shown) indicates a higher relative amount of Cu for the analog prepared using NaOH (Cu/Ce - 0.31) compared to the one prepared using NH4OH (Cu/Ce - 0.11). Referring back to Table 10, the analog prepared using NaOH produced only 38% conversion of toluene to CO2 at 200°C compared to 100% for the analog prepared using NH4OH. Therefore, although NaOH results in much greater precipitation of Cu, high levels of Cu result in a suppression of catalytic activity. Furthermore, residual sodium must be thoroughly rinsed from the precipitate when using NaOH. Performance Testing of Ce/Zr-Based Catalysts Table 11 contains a summary of some ofthe Ce/Zr-based catalysts studied with and without Pt. The activity ofthe Pt-free analogs were comparable the Pt-free Cu-doped Ceθ2 catalysts. However, the FTIR spectra (not shown) of these catalysts showed evidence of large amounts of residual nitrates, and even greater activity will be achieved by oxidizing the materials at higher temperatures. The Pt-loaded Ce/Zr catalysts were much more active than the Cu-doped catalysts. All ofthe Pt/Ce/Zr catalysts produced complete destruction of toluene at 150° C, and had very high activity at 100°C. Furthermore, measurable and sustainable activity was achieved at 80°C for the 3% and 5% Pt-loaded analogs. These results are shown in Table 12. At 100°C, activity is at a maximum for 3% Pt loading, whereas at 80°C the activity is maximized at 5% loading. Table 11. Summary of Screening Results for Ce/Zr-Based Catalysts* ■ oluene concentration was -100 ppm. Space velocity at least 6,000 hr Table 12. Catalyst activity as a function of Pt loading for a Pt/Ceo.95Zro.θ5θ2-δ support. Performance Testing of Additional Catalysts Table 13 contains a summary of some ofthe additional catalysts screened. For the Pt-free analogs in this table, the Ceθ2-based catalysts doped with Co or Mn demonstrated the greatest activity, generating complete destruction at 200°C. The catalyst CeCoo.5Cuo.5θ2_δ had the highest activity at 150°C, generating 22% destruction of toluene. Undoped Ceθ2 prepared by coprecipitation also showed significant activity (89%) destruction), however, Ceθ2 prepared by hydrothermal synthesis was not very active (33% destruction). The most active Pt-free catalyst in this table was Mnθ2, which produced 33% destruction of toluene at 150°C. Most ofthe Pt-loaded analogs generated 100% conversion of toluene to CO2 at 150°C, and the l%Pt/Ceo.95Lao.θ5θι.95 generated 20% destruction at 100°C. As with the Ce/Cu and Ce/Zr catalysts, many ofthe Pt-free analogs contained residual nitrates from the corresponding precursors. Greater activity will be seen from these materials after oxidation under more severe conditions. Table 13. Summary of Catalyst Screening Results for Additional Catalysts * % Conversion of Toluene to CO2 a Composition 200°C 150°C 100°C 80°C Ce0 2 89 Ceθ2 (hydrothermal) 33 CuO negligible C03O4 55 Mnθ2 (Mn2θ3) 100 33 1 CeCoo.5Cuo.5θ2_δ 100 22 CeMno.5Cuo.5θ2-δ 75 5 1% Pt-Loaded Analogs l%Pt/Ce 0 .95Gd 0 .05θ2-δ 57 l%Pt/Ce 0 .8Co 0 .2θι.8 25 l%Pt/Ceo.95Mno.θ5θl .95 100 8 2 l%Pt/Ceo.8Mno.2θι.8 44 9 l%Pt/Ce 0 .75 z r0.2Cu 0 .05θl.95 negligible l%Pt/Ce0 2 100 17 l%Pt/Mnθ2 100 5 0 l%Pt/CeCo 0 .5Cuo.5θ2-δ 100 11 l%Pt/CeMn 0 .5Cu 0 .5θ2-δ negligible l%Pt CeFe 0 .5Cu 0 .5θ2-δ 50 l%Pt/Ce 0 .5Coo.iCu 0 .4θ2-δ 100 2 l%Pt/Ceo.5Mno.lCuo.4θ2-δ 40 l%Pt/Ce 0 .5Feo.ιCu 0 .4θ2-δ 100 0 0 l%Pt/Ce 0 .95La 0 .05θl.95 100 20 1 *Toluene concentration was - 100 ppm. Space velocity at least 6,000 hr 1. Catalysts Incorporated into Ceramic Monoliths In order to incorporate catalysts into an air decontamination device, the active materials must be structurally supported in a way that allows adequate exposure ofthe catalyst to the contaminated air stream, without producing excessive back pressure. This condition is diagramed in Figure 23 for the destruction of VOCs on a catalyst-coated monolith. The monolith contains narrow channels running parallel to the length ofthe tube. Coating the interior walls ofthe monolith with catalyst provides a compromise between high VOC-catalyst contact and high flow rates. The goal for supporting the catalysts will be to produce an evenly-distributed high-surface area catalyst coating without plugging the pores ofthe support. The following support techniques may be used: a) ceramic monoliths, b) pellets, and c) irregular porous clusters. As with the catalyst powders discussed above, several techniques for incorporating the catalysts with the supports, and for preactivating the supported catalysts may be used. Overall, activity per gram of catalyst determine the optimum supported configuration. Preparation and Evaluation of Supported Catalysts a. Monolith Supports Ceramic Cordierite monoliths were obtained from commercial sources (Corning) with a cell density of 400/in2. Sections ofthe monolith blocks were cut to fit inside a 13.8-mm i.d. quartz tube, and the tube was incorporated into the reactor assembly described above. The length ofthe monolith (catalyst bed depth) was approximately 25 mm. Coating ofthe ceramic monoliths with catalyst may be performed by four methods, 1) dip- coating the monolith in a slurry ofthe catalyst in a solvent, 2) decomposition of metal precursors onto the monolith, 3) precipitation-deposition of catalyst onto the monolith, and 4) wash-coating the monolith with nano-scale dispersions of catalysts. The objective is to form an evenly-distributed catalyst layer on the inside ofthe monolith cells as diagramed in Figure 24, without creating a prohibitive pressure drop. More detailed morphological and compositional information is obtained using SEM and EDX. The catalyst loading is determined by weighing the monolith sections before and after deposition. Slurry Coating. For slurry coating, 0.2 g ofthe catalyst powder was mixed with several drops of 1,2-butanediol. The 1,2-butanediol had sufficient viscosity to maintain suspension ofthe catalyst particles, while allowing thorough coating ofthe monolith surface. The slurry was added dropwise to one end ofthe monolith and allowed to flow through the monolith lengthwise. Between additions, the slurry-coated monolith was dried in air at 120° C for several hours. After drying, the coated monolith was calcined in air at 300° C for 4 hours. This method resulted in a very uneven and unstable catalyst coating, and after calcining, the catalyst was easily removed from the monolith with gentle tapping. The calcination temperature was kept low to avoid sintering ofthe catalyst; however, sintering at higher temperatures would have resulted in a more stable coating. Decomposition ofthe Nitrate Precursors. For this method, a section ofthe monolith was completely submerged for 15 seconds in a -0.5 M solution of Ce(N03)3, then dried in air at 120°C for several hours. This process was repeated until a 50 wt.% loading of Ce(N03)3 relative to the weight ofthe monolith was achieved. The coated monolith was then calcined in air at 1000°C for 3 hours resulting in a very stable 23 wt.-% loading of Ceθ2- Next, one end ofthe coated monolith was dipped into 1 mL of a 10- mg/mL Pt solution causing the solution to wick into the monolith. The monolith was dried at 100°C, then reduced under H2 at 300°C for 3 hours, resulting in a Pt loading of 1% relative to the weight of Ceθ2- The resulting catalyst layer was very evenly distributed and relatively rugged. Precipitation-Deposition. This method will combine the metal precursor-decomposition technique above, with the coprecipitation technique described above. Specifically, the monolith will be submerged in a 1 M solution ofthe appropriate metal precursors in the necessary stoichiometric ratio. Next, a precipitating reagent will be added to produce the metal hydroxides. Decomposition at elevated temperatures in air will generate a metal oxide coating on the monolith surface. As with the above method, the catalyst metal can be incorporated with the original precursor solution, or added in a second step. It is anticipated that adding the metal in a second step will reduce the amount enveloped by the metal oxide layer, and lead to higher activity at lower metal loading This method should yield surface structure and particle size characteristics similar to the coprecipitated powders. Wash Coating. The wash coating technique described above may also be used to coat the ceramic monolith. b. Ceramic Pellets Catalyst pellets can be prepared either by pressing the catalyst material into a ceramic body ofthe desired shape, or by coating the outside of pre-pressed pellets with catalyst. The former type will have greater structural integrity; however most ofthe catalyst material is incorporated on the inside ofthe pellet and is not contributing to the activity. The later pellet configuration will be more susceptible to degradation from loss of catalyst from the surface; however, much less catalyst is required, which is more desirable for catalysts containing precious metals. Two types of pellet configurations will be investigated, although others are possible. For the first type of pellet configuration, inert pellets of alumina and silica with approximately 6-mm particle diameters will be obtained from commercial sources and coated with catalyst for use as large-grain structural supports. Smaller grain pellets will be prepared by crushing and sieving the 6-mm diameter pellets to 4- and 2- mm diameters. The method of incorporation ofthe catalyst onto the pellets likely will be critical to the resulting activity, stability, and pressure drops observed for the system. Therefore, the exact same methods described for coating the monolith supports also will be compared for coating pellets. As with the monoliths, the objective is to obtain a well-distributed, reproducible layer of catalyst on the pellet surface. The resulting catalyst-coated pellets will be loosely packed in a quartz tube to form a structure similar to the coated monolith, as shown in Figure 25. From the figure, it is evident that the size ofthe pellets will be an important variable to overall performance. Pellets that are to large will lead to bypassing and channeling ofthe gas stream; whereas pellets that are too small might lead to impractical pressure drops in the reactor. The second type of pellet configuration will involve preparing pellets from the active powder supports, then depositing the catalytic precious metal(s) on the exterior ofthe pellet. The pellets will be formed by mixing approximately 1 g of powder support with 1 to 3 wt-% of a ceramic binder (e.g. methylcellulose) and drying in an oven. The resulting powder will be introduced into a pellet press and pressed at 25,000 to 60,000 psi for 1 to 5 minutes. The green pellets of each material will be sintered in a bed ofthe same material in alumina or zirconia crucibles. Sintering temperatures of 1200°C to 1900°C will be used to achieve greater than 90% ofthe theoretical density, as determined from unit cell volumes calculated from the XRD patterns. Once the pellets are centered, they will be ground to the desired size range, and immersed into a solution ofthe catalytic metal precursor, followed by drying and heating under a flow of H2 at 300°C for 3 hours. The high sintering temperatures will be used to achieve high material densities, which will be desirable to minimize the amount of metal precursor that wicks into the support. However, is should be pointed out that the high temperatures required for sintering will not be compatible with many ofthe doped Ceθ2 materials in this program due to insolubility ofthe phases. c. Catalyst Clusters Catalyst clusters will be prepared by spreading out a layer of active support in a Pyrex dish, and spraying a fine mist of catalytic metal precursor over the powder using an air brush paint sprayer. Mechanical agitation ofthe dish during the spraying process will result in clustering ofthe catalyst. The degree of metal loading in the clusters will be controlled by varying the concentration and amount of precursor solution applied to the powder. The resulting clusters will be oven dried, and sintered to produce structural rigidity. Then, the catalytic metal will be reduced under a flow of H2 at 300°C for 3 hours. The exact sintering conditions will be detennined experimentally. Again, if high temperatures are required to attain acceptable integrity, this method might not be compatible with the doped Ceθ2 materials. Results for catalytic monoliths The results for screening monolith-supported l%Pt/Ceθ2 with MEK are presented in Figure 26. The concentration of MEK was - 150 ppm in air, and the flow rate through the section of monolith (with dimensions described above) was -9 mL/min. At 150° C, there was an increase in conversion over 1600 minutes to -95%. The supported catalyst was then heated at 150°C under a flow of air for several hours, and the temperature was dropped to 80 °C. Initially, a conversion rate of 30% was achieved, but the conversion dropped over -400 minutes to a steady value of -8%. This conversion rate was maintained for -1000 minutes before gradually dropping to 6%. For comparison, the results for a bare monolith (no catalyst) run in parallel under the exact same conditions also is shown in the figure. At 80 °C, the blank monolith did not decompose any MEK. Other catalyst compositions and structural supports may be used to optimize the conversion of VOCs using the methods described herein, or by modification ofthe methods described herein, or the methods well known to the art. D. Testing of catalysts for selective carbon monoxide oxidation in a hydrogen containing gas Catalyst Screening Apparatus. A schematic diagram of a single reactor to be used for catalyst screening is shown in Figure 27. The actual catalyst screening apparatus incorporates six reactors, which enables rapid catalyst screening. Important components ofthe reactor include an electric furnace surrounding a 4-mm i.d. quartz tube containing the catalyst sample. The catalyst is held in place by a plug of quartz wool and a narrower inner-tube, and the temperature is monitored and adjusted using a controller paired with a thermocouple touching the top the catalyst bed. The quartz reactor tube is coupled to 1/8" stainless steel inlet and outlet tubes using Swagelok fittings with Teflon ferrules. Simulant reformate fuel is prepared by mixing H2, CO, and O2 from cylinders with a balance of N2 or Ar. Flow rates are controlled by needle valves and monitored using both ball-type and bubble flow meters. Sampling ofthe inlet and outlet gas stream is achieved through ports located on opposite sides ofthe reactor. Catalyst Screening Conditions and Procedure. Approximately 0.2 g of catalyst is used for each evaluation, which corresponds to a cylindrical catalyst volume of -0.13 cm^. Catalysts are screened at temperatures between 50 - 200°C and space velocities between 10,000 - 20,000 hr 1 (contact times between 0.4 - 0.2 seconds), which requires flow rates between 20 - 40 mL/min. The CO concentration in the feedstream is maintained at -2000 ppm. To simulate H2-rich reformate, the H2 concentration is between 10,000 - 50,000 ppm. The O2 concentration is a variable in catalyst performance evaluation, and ranges between 0 - 6,000 ppm. The concentrations of species in the inlet and outlet streams (i.e., CO, H2, and CO2) are determined by chromatographic analysis of 1-mL samples using a Hewlett-Packard 5890 GC with thermal-conductivity detection. Chromatographic separation is performed with an Alltech CTR-1 column, and peak areas are determined using a Hewlett-Packard 3396A integrator. Calibration is performed by measuring chromatographic peak area as a function of concentration over the relevant concentration ranges for each gas. For each catalyst, activity and selectivity are determined over a range of temperatures for a fixed O2 concentration approximately equal to the CO concentration. The temperature required for 50% and 100% CO oxidation is determined from the data, and the catalysts are screened at these temperatures for a variable 0 2 concentration. Conversion values, %C, for CO are determined based on CO removal and C0 2 production according to, (5) and (6) where [CO],„ to , [CO] 0 „ rtø , and [C0 2 ] 0itftø are the inlet and outlet CO concentrations, and the outlet C0 2 concentration, respectively. Consumption of H 2 is determined using an equation analogous to Equation 5. For each set of data, selectivity is highlighted by plotting %C versus H 2 consumption. Figures 28-31 show selective catalytic oxidation of carbon monoxide in the presence of hydrogen for four catalysts. Catalyst Optimization. Catalyst optimization is performed by careful variation of catalyst constituents and concentrations in the material, as well as preparation and pretreatment conditions. Optimization is also performed using statistical methods known in the art. Supported catalysts. Catalyst compositions are also tested on traditional cordierite monolith and alumina pellet supports. The ceramic monoliths are obtained from commercial sources (Corning) and have a cell density of 400/in 2 . Alumina pellets also are obtained from commercial sources (Aldrich) and have a particle diameter of -6 mm. Since the method of incorporating the catalysts onto the support structures is anticipated to have a dramatic effect on the resulting activity, several methods are investigated: i) slurry coating, ii) decomposition of precursors, and iii) deposition-precipitation. Each of these methods, as well as the procedures for evaluating structurally-supported catalysts, is described below. Slurry Coating. Catalyst powder slurries are prepared by mixing approximately 2 g of 0.2 to 2-μm catalyst powder in 1,4-butanediol. The 1,4-butanediol has sufficient viscosity to maintain suspension of the catalyst particles, while allowing thorough coating of the support surface. The uncoated support is immersed in the slurry, then removed and dried at ~100°C for 12 hours, followed by calcining in air for 2 hours at temperatures between 200 and 900°C. As with the powder catalysts, exact calcination temperatures and pretreatment conditions are determined experimentally, and depend on the specific catalyst being used. To obtain the desired loading, this process may be repeated several times, and variation of the slurry thickness is another way to control the catalyst loading and microstructure. Furthermore, the surface area of the monolith may be increased before application of the catalyst. This task is achieved by wash-coating with A1 2 0 3 from a bohemite solution, followed by drying and heating at 400 °C. Decomposition of Precursors. For this method, an aqueous solution of metal precursors in the appropriate stoichiometric ratios is prepared at a concentration of at least IM. Depending on the solubility of the precursors, it is desirable to have the concentration as high as possible. As with the slurry-coating technique, the support is submerged into the solution for a defined period of time, then removed, dried, and weighed. This process is repeated until there is no weight gain (usually 3 or 4 applications), then calcined in air to produce the catalyst coating. Deposition-Precipitation. This method combines the decomposition technique above with the coprecipitation technique. Specifically, the support is submerged in a solution of the appropriate precursors in the necessary stoichiometric ratio. Next, NH 4 OH (or other precipitating reagent) is added slowly with mixing to produce the corresponding metal hydroxides, which coats all surfaces of the support materials. Since this step normally results in production of a thick gel, the concentration of the precursor solution and NH 4 OH need to be low to avoid pore clogging with monoliths. The metal hydroxide layer is then decomposed to the oxide by calcining in air. For noble metal-containing catalysts, the metal oxide can be deposited first, then the noble metal can be deposited using the procedure. Evaluation. For monolith supports, small sections of monolith are cut to fit inside a 13.8-mm i.d. quartz tube, and the tube is incorporated into the reactor assembly shown in Figure 1. A photograph of a section of bare monolith is shown next to a catalyst-coated monolith within the reactor tube in Figure 32. The length of the monolith (catalyst bed depth) is - 25mm. Approximately 0.2 - 0.4 g of catalyst can be deposited onto a monolith of these dimensions using the techniques above. For pellet supports, the catalyst-coated pellets simply replace the monolith in the assembly. Evaluation of the supported catalysts is performed according to the conditions described above. Although the description above contains many specificities, these should not be construed as limiting the scope ofthe invention but as merely providing illustrations of some ofthe presently- preferred embodiments ofthe invention. For example, other methods of preparing catalysts may be used. Also, different components than described in the Examples may be incorporated. Also, different apparatuses may be used, as known to one of ordinary skill in the art. Thus, the scope ofthe invention should be determined by the appended claims and their legal equivalents, rather than by the examples given. Those of ordinary skill in the art will appreciate that methods, techniques, and components other than those specifically described herein can be employed in the practice of the invention without departing from its spirit scope. All references included herein are hereby incorporated by reference to the extent not inconsistent with the disclosure herein. Those of ordinary skill in the art will appreciate that optimization procedures and selection procedures are well within the skill of one with ordinary skill in the art using the guidance herein and the knowledge in the art. References 1. Gardner, S. D.; Hoflund, G. B.; Davidson, M. R.; Laitinen, H. A.; Schryer, D. R.; Upchurch, B. T. 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Claims: CLAIMS We claim: 1. A catalyst composition comprising at least one of cerium and zirconium with at least one member ofthe group consisting of: Gd, La, Sc, Sr, Cr, Ti, V, Mn, Fe, Co, Ni, Au, Ag, Cu, Zr, Pt, Pd, Rh, Ru, Re, Os and lr. 2. A catalyst composition comprising less than 50% of at least one of cerium and zirconium with at least one member ofthe group consisting of: Gd, La, Sc, Sr, Cr, Ti, V, Mn, Fe, Co, Ni, Au, Ag, Cu, Zr, Pt, Pd, Rh, Ru, Re, Os and lr, provided that the composition is not [Laq Zr r O] _t M , where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. 3. A catalyst composition comprising one or more first metals selected from the group consisting of Ce and Zr and at least one of: (a) one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; (b) one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and (c) one or more fourth metals selected from the group consisting of: Pt, Pd, Rh, Ru, Re, Os and lr. 4. A catalyst composition, wherein less than 50% ofthe composition is one or more first metals selected from the group consisting of Ce and Zr and the balance ofthe compsition comprises at least one of: (a) one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; (b) one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and (c) one or more fourth metals selected from the group consisting of: Pt, Pd, Rh, Ru, Re, Os and lr provided that the composition is not [Laq Zr r O] ι_ Mt, where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. 5. The catalyst composition of claim 3 or 4, wherein said second and third metals comprise less than about 80% of said catalyst composition. 6. The catalyst composition of claim 3 or 4, wherein said second and third metals comprise less than about 50% of said catalyst composition. 7. The catalyst composition of claim 3 or 4, wherein said fourth metals comprise less than about 25% of said catalyst composition. 8. The catalyst composition of claim 3 or 4 which is a single-phase material. 9. The catalyst composition of claim 3 or 4 which is a multi-phase material. 10. The catalyst composition of claim 3 or 4, wherein said third metals are selected from the group consisting of Co, Mn, Fe and Cu. 11. The catalyst composition of claim 3 or 4, wherein said fourth metals are selected from the group consisting of Pt and Pd and mixtures thereof. 12. The catalyst composition of claim 3 or 4 further comprising a supporting material. 13. The catalyst composition of claim 3 with the formula: nN / Ceι_χ Zr c A a A' a - A" a » B b B' b . B" b » 0 2 _δ wherein n is a percentage from 0 to 25; N is selected from the group consisting of fourth metals and mixtures thereof; x = a + a' + a" + b + b' + b" + c; a, a', a", b, b', b" and c are each, independently of one another, 0 to 0.9; δ is a number which renders the composition charge neutral; A, A' and A" are independently selected from the group consisting of second metals; B, B' and B" are independently selected from the group consisting of third metals; and provided that when n is zero, at least one of a, a', a", b, b', b" or c is nonzero. 14. The catalyst composition of claim 3 with the fonnula: nN / Ceι_ x Zr c A a A' a - A" a » B b B' b > B 0 2 _δ wherein n is a percentage from 0 to 25; N is selected from the group consisting of fourth metals and mixtures thereof; x = a + a' + a" + b + b' + b" + c; a, a', a", b, b', b" and c are each, independently of one another, 0 to 0.9; δ is a number which renders the composition charge neutral; A, A' and A" are independently selected from the group consisting of second metals; B, B' and B" are independently selected from the group consisting of third metals; and provided that when n is zero, at least one of a, a', a", b, b', b" or c is nonzero and provided that (1-x) + c is less than 0.5 and provided that the composition is not [Laq Zr r O)ι_t M , where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. 15. The catalyst composition of claim 13 or 14, wherein N is selected from the group consisting of Pt and Pd and mixtures thereof. 16. A catalyst composition of formula: Ce ι_f Cu f θ2_δ wherein f is about 0.001 to about 0.5 and δ is a number which renders the composition charge neutral. 17. The catalyst composition of claim 13 of formula Ceo.δMn o.2 02-δ- 18. The catalyst composition of claim 13 of formula Ceo.sMn o.5 θ2-δ- 19. The catalyst composition of claim 13 of formula Ceo.sFe o.l Cu 0.4 θ2- - 20. The catalyst composition of claim 13 of formula Ceo.475Zr o.05 Mn 0.475 02-δ- 21. The catalyst composition of claim 13 of formula: Ceo.45Zr Q.05 Mn o.45 Cuo.θ5°2-δ wherein δ is a number which renders the composition charge neutral. 22. The catalyst composition of claim 13 of formula: Ce 0.8 Zr 0.05 Cu 0.15 02-δ wherein δ is a number which renders the composition charge neutral. 23. The catalyst composition of claim 3 having formula: nN / Ceι_ x Zr c A a A' a > B B' b . 0 2 -δ wherein n is a percentage from 0.01 to 15; N is selected from the group consisting of fourth metals and mixtures thereof; x = a + a' + b + b' + c; a, a', b, b' and c are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A and A' are independently selected from the group consisting of second metals; B and B' are independently selected from the group consisting of third metals; provided that when n is zero, at least one of a, a', b, b' or c is nonzero. 24. The catalyst composition of claim 3 having formula: nN / Ceι_ x Zr c A a A' a - B B' b . 0 2 _δ wherein n is a percentage from 0.01 to 15; N is selected from the group consisting of fourth metals and mixtures thereof; x = a + a' + b + b' + c; a, a', b, b' and c are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A and A' are independently selected from the group consisting of second metals; B and B' are independently selected from the group consisting of third metals; provided that when n is zero, at least one of a, a', b, b' or c is nonzero; provided that (1-x) + c is less than 0.5 and provided that the composition is not [Laq Zr r O)ι_t M , where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. 25. The catalyst composition of claim 23 wherein N is one or metals selected from the group consisting of: Pt and Pd and mixtures thereof. 26. The catalyst composition of claim 23, wherein n is a percentage from 0.01 to 10. 27. The catalyst composition of claim 23 wherein n is a percentage from 0.01 to 5. 28. The catalyst composition of claim 23 wherein n is a percentage from 0.01 to 2. 29. The catalyst composition of claim 23 of formula: 5%Pt/Ce 0 .8 Cu o.2 0 2 -δ, wherein δ is a number which renders the composition charge neutral. 30. The catalyst composition of claim 23 of formula: l%Pt/Ce 0 .8 Cu o.2 θ 2 -δ, wherein δ is a number which renders the composition charge neutral. 31. The catalyst composition of claim 23 of formula: 5%Pt/Ce 0 .8 Sr o.2 θ 2 -δ, wherein δ is a number which renders the composition charge neutral. 32. The catalyst composition of claim 23 of formula: l%Pt/Ce 0 .8 Sr o.2 θ 2 -δ, wherein δ is a number which renders the composition charge neutral. 33. The catalyst composition of claim 23 of formula: 5%Pt/Ce 0 .8 Au 0 .2 0 -δ, wherein δ is a number which renders the composition charge neutral. 34. The catalyst composition of claim 23 of formula: l%Pt/Ce 0 .8 Au 0 .2 θ2-δ, wherein δ is a number which renders the composition charge neutral. 35. The catalyst composition of claim 23 of formula 5%Pt/Ceθ2- 36. The catalyst composition of claim 23 of formula l%Pt/Ceθ2- 37. The catalyst composition of claim 3 having formula: nN/m Cei_ x A a A' a , B b B' b . 0 2 _δ/ Zrι_ z A" a . A"' a » B" b »B"V 0 2 . δ wherein n is a percentage from 0 to 15; m is a percentage greater than 0; N is selected from the group consisting of fourth metals and mixtures thereof; x = a + a' + b + b'; z = a" + a"' + b" + b"'; a, a', a", a'", b, b', b" and b'" are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A, A', A" and A'" are independently selected from the group consisting of second metals; B, B', B" and B'" are independently selected from the group consisting of third metals; provided that when n is zero, at least one of a, a', a", a'", b, b', b" or b'" is nonzero. 38. The catalyst composition of claim 3 having formula: nN/m Ceι.χ A a A' a . B b B' b , 0 2 . δ / Z . z A" a » A'V B" b , B" 0 2 . δ wherein n is a percentage from 0 to 15; m is a percentage greater than 0; N is selected from the group consisting of fourth metals and mixtures thereof; x = a + a' + b + b'; z = a" + a"' + b" + b"'; a, a', a", a'", b, b', b" and b'" are each, independently of one another, 0 to 0.5; δ is a number which renders the composition charge neutral; A, A', A" and A"' are independently selected from the group consisting of second metals; B, B', B" and B"' are independently selected from the group consisting of third metals; provided that when n is zero, at least one of a, a', a", a'", b, b', b" or b'" is nonzero; provided that (1-x) + c is less than 0.5 and provided that the composition is not [Laq Zr r O)ι_t M , where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. . 39. The catalyst composition of claim 37 wherein N is one or metals selected from the group consisting of: Pt and Pd and mixtures thereof. 40. The catalyst composition of claim 37, wherein n is a percentage from 0.01 to 10. 41. The catalyst composition of claim 37 wherein n is a percentage from 0.01 to 5. 42. The catalyst composition of claim 37 wherein n is a percentage from 0.01 to 2. 43. The catalyst composition of claim 37 of formula 1% Pt/12%Ce 0 2 / Zr O2 44. The catalyst composition of claim 3 having formula: nN/m(Ceθ2)/p(A a N^N ^B b B B" b -θ2-δ)/q(N ^ a "N" ^ a — A a B"V " B "" b""B b 0 2 _δ) wherein n, p and q are percentages from 0 to 50; m is a percentage greater than 0; N is one or more metals selected from the group consisting of fourth metals; a, a a", a"", a ", a""", b, b b", b"\ b"" and b" Λ " are each, independently of one another, 0 or 1; δ is a number which renders the composition charge neutral; A, A", A", A"\ A"" and A""" are independently selected from the group consisting of second metals; B, B", B , B"", B"" and B"" ' ' are independently selected from the group consisting of third metals; provided that when n is zero, at least one of p and q is nonzero and at least one of a, a", a", a ,a ,a , b, b , b , b ,b and b is nonzero. 45. The catalyst composition of claim 3 having formula: ri /m(Ceθ2) p(AaAVA"a"BbBVB"b"θ2.δ)/q(A"V"A"" a ""A a B" "B "' '"B b 02-δ) wherein n, p and q are percentages from 0 to 50; m is a percentage greater than 0; N is one or more metals selected from the group consisting of fourth metals; a, a", a", a"", a , a " "" 1 ", b, b b , b"", b"" andb Λ " are each, independently of one another, 0 or 1; δ is a number which renders the composition charge neutral; A, A", A", A"", A"" and A ,,λ " are independently selected from the group consisting of second metals; B, B", B", B ,, , B"" and B""" are independently selected from the group consisting of third metals; provided that when n is zero, at least one of p and q is nonzero and at least one of a, a\ a", a-"" 1 , a" "" , a" " " , b, b' , b" , fr"" 1 , b' " " and b" ' " " is nonzero; provided that the composition contains less than 50% Ceθ2 and provided that the composition is not [Laq Zr r O)ι_t Mt, where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. 46. The catalyst composition of claim 37, wherein N is selected from the group consisting of Pt and Pd and mixtures thereof. 47. The catalyst composition of claim 37 with formula Ce O2/ 10% CuO. 48. The catalyst composition of claim 37 with formula Ce O2/ 10% Mnθ2. 49. A catalyst composition with the formula: nN/Ceι-.(χ +y + z ) A x A' y A" z ©2-δ where A, A', A" are independently selected from the group consisting of: Zr, Gd, La, Sc, Sr, Co, Cr, Fe, Mn, V, Ti, Cu and Ni; N is one or more members ofthe group consisting of: Pt, Pd, and Au; n is a weight percent between 0 and 25; x, y and z are independently 0 to 0.9; x + y + z is 0.1 to 0.9; and δ is a number which renders the composition charge neutral. 50. A catalyst composition of formula: r_N/(MOχ)y (Ceθ2-δ) 1-y, where M is one or more members ofthe group selected from: Zr, Co, Cr, Fe, Mn, V, Ti, Ni and Cu; N is one or more members ofthe group selected from: Pt, Pd, and Au; n is a weight percent between 0 and 25; y is 0.1 to 0.9; and x and δ make the compositions charge neutral. 51. The catalyst composition of claim 49 or 50, wherein said catalyst composition contains one or more members ofthe group consisting of: copper, manganese and gold 52. A method for selectively removing carbon monoxide from a gas containing hydrogen comprising: contacting said gas with a catalyst composition whereby the carbon monoxide in said gas is selectively removed. 53. A reactor for selectively removing carbon monoxide from a gas which comprises: a casing having an entrance port, an exit port and a passage therebetween for the movement of said gases from said entrance port to said exit port; and a catalyst composition of claim 49 or 50 in said passage. 54. The reactor of claim 53, wherein said gas contacts said catalyst composition before exiting said casing. 55. The reactor of claim 53, wherein said reactor is a component of a polymer electrolyte membrane fuel cell. 56. The reactor of claim 53, wherein the gas in said entrance port comprises carbon monoxide, hydrogen and oxygen. 57 The reactor of claim 53, wherein said catalyst composition is coated on a support surface. 58. The method of claim 52, wherein said catalyst composition contains one or more members of the group consisting of: copper, manganese and gold. 59. A method for reducing the concentration of VOCs in a gas containing at least one VOC which comprises the step of contacting said gas with a catalyst composition ofthe formula comprising one or more first metals selected from the group consisting of Ce and Zr and at least one of: (a) one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; (b) one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and (c) one or more fourth metals selected from the group consisting of: Pt, Pd, Rh, Ru, Re, Os and lr, whereby the concentration of at least one VOC in said gas is reduced. 60. A method for reducing the concentration of VOCs in a gas containing at least one VOC which comprises the step of contacting said gas with a catalyst composition comprising less than 50% of one or more first metals selected from the group consisting of Ce and Zr and the balance ofthe compsition comprising at least one of: (a) one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; (b) one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and (c) one or more fourth metals selected from the group consisting of: Pt, Pd, Rh, Ru, Re, Os and lr provided that the composition is not [Laq Zr r O] ι_t M , where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5. 61. The method of claim 59, further comprising heating either said gas or said catalyst composition or both to a temperature sufficient to reduce the concentration of at least one VOC in said gas to a selected value. 62. The method of claim 59, wherein said gas also contains water vapor. 63. The method of claim 59, wherein said catalyst composition is held in a reactor at temperatures of from about ambient temperature to about 250°C. 64. The method of claim 59, wherein said catalyst composition is held in a reactor at temperatures of from about ambient temperature to about 150°C. 65. The method of claim 59, wherein said catalyst composition has a surface area ranging from about 20 to about 220 m 2 /g. 66. The method of claim 59, wherein said catalyst composition is prepared by the methods comprising: (a) treating a mixture of selected metal salt precursors with a precipitating reagent to form a precipitate; (b) drying said precipitate; (c) calcining said precipitate at a temperature of about 300 ° C or higher; (d) contacting one or more solutions of one or more metals selected from the group consisting of Pt, Pd, Rh, Ru, Re, Os and lr with said precipitate to form a composition; (e) reducing said composition at temperatures of about 200 °C or higher; and optionally (f) oxidizing said composition at temperatures of between about 80°C to about 800°C. 67. The method of claim 66, wherein said precipitating reagent is selected from the group consisting of: NH4OH, (NH4)2C03, NaOH, Na Cθ3, urea or K2CO3. 68. The method of claim 59, wherein said catalyst composition further comprises a support material. 69. The method of claim 68, wherein said support material is a honeycomb matrix having inner and outer surfaces, wherein said catalyst composition is present on the inner surfaces of said honeycomb matrix. 70. The method of claim 68, wherein said support material is fabricated from ceramic materials. 71. A method of decomposition of VOCs in a gas, comprising the steps of (a) providing a reactor containing the catalyst composition composition ofthe formula comprising one or more first metals selected from the group consisting of Ce and Zr and at least one of: (i) one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; (ii) one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and (iii) one or more fourth metals selected from the group consisting of: Pt, Pd, Rh, Ru, Re, Os and lr; and (b) passing said gas through said reactor to decompose the VOCs. 72. A method of decomposition of VOCs in a gas, comprising the steps of (a) providing a reactor containing the catalyst composition composition ofthe formula comprising one or more first metals selected from the group consisting of Ce and Zr and at least one of: (i) one or more second metals selected from the group consisting of: Gd, La, Sr and Sc; (ii) one or more third metals selected from the group consisting of: Ti, V, Mn, Fe, Co, Cr, Ni, Au, Ag and Cu; and (iii) one or more fourth metals selected from the group consisting of: Pt, Pd, Rh, Ru, Re, Os and lr; provided that the composition is not [Laq Zr r O)ι_t Mt, , where M is a transition metal or mixture thereof; q is between 0.45 and 0.55; r is between 0.55 and 0.45; and t is between 0 and 0.5; and (b) passing said gas through said reactor to decompose the VOCs. 73. A catalytic reactor for decomposition of VOCs in gases which comprises: a casing having an entrance port, an exit port and a passage therebetween for the movement of said gases from said entrance port to said exit port; and a catalyst composition according to claim 3 or 4 in said passage. 74. The catalytic reactor of claim 73 wherein said gases contact said catalyst composition before exiting said casing. 75. The catalytic reactor of claim 73, wherein said catalyst composition is preconditioned at a temperature of about 100°C or above prior to said gases contacting said catalyst composition. 76. The catalytic reactor of claim 73, further comprising a support material.

Inventors: ROARK SHANE E, WHITE JAMES H, ROARK, SHANE, E., WHITE, JAMES, H.
Applicants: ELTRON RES INC, ELTRON RESEARCH, INC.
Application year: 2000
Main classification: B01J8
IPC codes: A62D3, B01J23, C01B3