Abstract:
Disclosed is an improved catalyst having a high thermal stability including a solid catalyst support having a layer of catalytically active carrier material, either as a coating on a non-catalytically active support or as particles of catalytically active carrier material, and a catalytically active metal component upon the carrier, wherein the improved aspect resides in between about 0.2 and 15% by weight of zinc in the form of zinc oxide contained in the catalytically active carrier material. Also disclosed are a method for preparing the improved catalyst and a method for utilizing the catalyst for purifying automobile exhaust gas and industrial waste gas.

Description:
BACKGROUND OF THE INVENTION 
     The present invention relates to improved catalysts, and more especially, to a catalyst having high thermal stability, particularly a catalyst based upon ceramic and/or metal supporting elements, as well as to a process for manufacturing the catalyst and to a process for using the catalyst, in particular for the purification of industrial waste gases and automobile exhaust gases. 
     Loose particulate bed catalysts and also reticulated or honey-comb catalysts can be employed for the catalytic removal of harmful components from industrial waste gases and automobile exhaust gases. Both types are comprised of a carrier and catalytically active components. Reticulated, e.g., honey-comb, structures of catalytically inert material, for example, ceramic or metal, are suitably coated with a catalytically active layer of a carrier material and one or more catalytically active metals, particularly noble metals, whereas particulate catalyst bodies can be prepared in such a manner that these support bodies are formed from the catalytically active carrier material, upon which one or more catalytically active metals are then brought. 
     Particulate loose bed catalysts and reticulate catalysts have differing advantages; however, both types possess the same type disadvantage that they loose their activity when subjected to the high and continual thermal stress to which exhaust gas catalysts, in particular, are exposed. This effect may be traced back to a recrystallizaion of the catalytically active components and to their diffusion into the region of the catalyst body which lies outside of the depth of penetration of the reactants. Accordingly, there exists a definite need for particulate and reticulated catalysts which exhibit enhanced thermal stability. 
     SUMMARY OF THE INVENTION 
     It is therefore an object of the present invention to provide catalysts which exhibit an improved degree of thermal stability. 
     It is also an object of the present invention to provide both particulate catalysts as well as reticulated catalysts which are particularly suitable for withstanding thermal stress. 
     Another object of the present invention resides in the provision of catalysts suitable for the purification of industrial waste gases and automobile exhaust gases, which catalysts in addition exhibit excellent thermal stability. 
     Another object of the present invention resides in the provision of a process for the preparation of catalysts having excellent thermal stability, including both particulate catalysts intended for use in loose bed catalyst systems as well as reticulate catalyst systems. 
     It is yet another object of the present invention to provide a method for purifying industrial waste gases and automobile exhaust gases by contacting such gases with the improved catalyst provided in accordance with the invention. 
     In accomplishing the foregoing and other objects, there has been provided in accordance with the present invention an improved catalyst having a high thermal stability, including a solid catalyst support bearing a layer of catalytically active carrier material and a catalytically active metal component being deposited upon the carrier, and wherein the improvement comprises between about 0.2 and 15% by weight, preferably between about 0.5 and 8% by weight of zinc in the form of zinc oxide contained in the catalytically active carrier material. The solid catalyst support may be either a solid reticulated structure of catalytically inert material, such as ceramic or metal, bearing a layer of catalytically active carrier material, or alternatively the solid support may comprise a bed of discrete solid particles which are formed entirely or in part from the catalytically active carrier material. Preferably the catalytically active carrier material comprises aluminum oxide and the catalytically active metal component comprises a noble metal. 
     In another aspect of the present invention, there has been provided a process for the preparation of an improved catalyst having a high thermal stability, comprising the steps of mixing together a catalytically active carrier material and zinc oxide, forming a layer of the zinc oxide-containing carrier material on a solid catalyst support, drying the support at a temperature between about 100° and 250° C., calcining the dried support at a temperature between about 600° and 1200° C. and thereafter applying a catalytically active metal component to the carrier. In the case of producing a reticulated catalyst structure, the catalytically active carrier material is preferably aluminum oxide hydrate, and an aqueous suspension of highly dispersed zinc oxide and the hydrate is produced, which suspension is then coated upon a catalytically inert support member. Where the catalyst is a particulate bed catalyst system, the process involves forming discrete solid particles from the mixture of carrier material, preferably aluminum oxide, and the zinc oxide. 
     In a further embodiment of the present invention, there has been provided a process for purifying automobile exhaust gas and industrial waste gas, comprising contacting the gas with the improved catalyst described hereinabove at an elevated temperature sufficient to cause conversion of the undesirable components in the gas. 
     Other objects, features and advantages of the present invention will become apparent from the following detailed description of several preferred embodiments of the invention. 
    
    
     DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS 
     In accordance with the present invention, it has quite unexpectedly been discovered that a content of between about 0.2 and 15%, preferably between about 0.5 and 8% by weight of zinc in the form of zinc oxide in the catalytically active carrier material, which preferably comprises aluminum oxide, results in a stabilizing effect which enables the activity of the catalyst to remain undiminished even after longer calcining by temperatures up to 1100° C. Thus, in the case of particulate bed catalysts, the zinc is added in the form of its oxide, in a highly dispersed condition, having a particle size in the range from 0.5 to 5 μ, preferably 1-3 μ, before the pressing, granulation or other preparation method to the aluminum oxide hydrate, which may be used, for example, as the catalytically active carrier material. In the case of a reticulated catalyst body, the zinc oxide is added before the coating of the catalyst support member to the aqueous suspension which serves for the preparation of the catalytically active carrier material and which preferably contains highly dispersed aluminum oxide hydrate. 
     A catalyst composition consisting of aluminum oxide and zinc oxide without any other catalytically active component had been described in U.S. Pat. No. 3,674,423. The scope of this invention is to reduce nitrogen oxides in waste gases, zinc oxide being the only catalytically active component. The scope of the present invention is a high temperature and long time stable catalyst based on a carrier material consisting of aluminum oxide and zinc oxide and supported thereon, active metal components. In the unused, virgin state, as may be seen from the examples 17-19 and tables 1-3, there is no difference of catalytic activity in the catalysts compounded with or without zinc oxide. 
     A further difference of the U.S. Pat. No. 3,674,423 and the present invention is the method of preparing the catalysts. According to the USP the aluminum oxide is impregnated with zinc nitrate and then heated to 550° C. This method produces a nearly molecular dispersion of the zinc oxide. According to the present invention the zinc oxide is added as a fine powder of e.g. 1 to 3 μ. 
     The catalyst in accordance with the present invention can, for example, be produced in accordance with the following process: 
     If the catalyst is to be prepared as a particulate bed catalyst, then aluminum oxide, preferably pseudoboehmite, is mixed with from about 0.2 to 15%, preferably from about 0.5 to 8% by weight of zinc in the form of its oxide in highly dispersed condition. Optionally, conventional additives such as water, acids, porosity agents and/or lubricants may be added where desired. Then the mixture is granulated, extruded or tabletized, as desired, the resulting particles dried and finally calcined under conditions of conventional temperature increase between 700°  and 1200° C, preferably between about 900° and 1100° C. The final step involves impregnating the catalyst carrier with one or more catalytically active metals. Pseudoboehmite is a poorly crystallized aluminum oxide hydroxide (see I. W. Newsome Alumina Properties, Technical Paper No. 10, Aluminum Company of America, 1960). 
     If the carrier is to be employed in the form of ceramic reticulated structures, such as honey-comb structures, then the coating of the catalyst support, e.g., formed of cordierite, spodumen, corundum for mixtures of these materials, is carried out with an aqueous suspension which contains between about 5 and 25%, preferably between about 8 and 15% by weight of highly dispersed aluminum hydroxide, having a particulate size in the range from 0.5-5 μ, preferably 1-3 μ and between about 0.01 and 3% preferably between about 0.25 and 1.5% zinc in the form of its oxide, having a particle size in the range from 0.5-5 μ, preferably 1-3 μ. The aluminum hydroxide is preferably present as pseudoboehmite. Subsequently, the reticulated structure is dried at a temperature of between about 100° and 250° C, preferably at approximately 200° C, and is thereafter calcined at a temperature between about 600° and 1200° C, preferably between about 800° and 1000° C. Finally, the catalyst support bearing the layer of catalyst carrier is impregnated with one or more catalytically active metals. 
     If, on the other hand, the carrier is to be employed in the form of metallic reticulated structures, then the catalyst support member of a non-rusting, scale-free and heat resistant metallic material is first coated with an elastic priming layer of aluminum silicate, preferably in the form of aluminum silicate fibers. The thickness of the primer layer is typically between about 5 and 100 μ, and more preferably between about 10 and 50 μ. After coating the metallic skeleton with the primer layer and after drying at a temperature between about 100° and 250° C, preferably at approximately 200° C, the primed skeleton is coated with a layer of catalytically active carrier material. This involves the step of coating with an aqueous suspension which contains highly dispersed aluminum hydroxide (e.g., particle size in the range from 1-3 μ, which is preferably present as pseudoboehmite and between about 0.01 and 3%, preferably between about 0.25 and 1.5% by weight of zinc in the form of its oxide in a highly dispersed condition (e.g., particle size in the range from 1 to 3 μ. The thickness of this coating ranges between about 2 and 50 μ and preferably between 5 and 15 μ and preferably between about 5 and 15 μ. Subsequently, the reticulated metal body is dried at a temperature between about 100° and 250° C, preferably about 200° C, and is calcined at a temperature between about 600° and 1000° C, preferably between about 800° and 1000° C. Finally, the dried and calcined catalyst support is impregnated with one or more catalytically active metals. 
     For waste gas and/or exhaust gas catalysts, there may be employed as catalytically active metals, for example, between about 0.01 and 1%, preferably between about 0.02 and 0.5% by weight of platinum and/or palladium, whereby mixtures of the two metals preferably contain a platinum:palladium ratio of between about 9:5 and 4:3 by weight. Furthermore, there may be employed up to about 0.5% by weight each of ruthenium and platinum, whereby the ratio of ruthenium to platinum ranges between about 1:3 and 1:0.15. Alternatively there may be employed up to about 0.5% by weight platinum in combination with ruthenium, rhodium and rhenium, and in this case the ratio of platinum to ruthenium to rhodium to rhenium ranges between about 1:1:1:1 and 1:0.25:0.25:0.25. 
     In the case of reticulated catalyst structures, the noble metal components can also be applied simultaneously with the catalytically active carrier material comprising aluminum oxides and zinc oxide. Similarly, in the case of particulate catalyst beds or the like, the noble metal components can be mixed into the aluminum hydroxide-zinc oxide mixture prior to formation of the carrier structure. 
     Of the catalysts described hereinabove, the type which contains only platinum and/or palladium is particularly suitable for the oxidation of carbon monoxide and uncombusted hydrocarbons in automobile exhaust gases and industrial waste gases. The ruthenium- and platinum-catalyst types are especially suitable for the reduction of nitrogen oxides in the aforementioned waste and exhaust gases. On the other hand, for the simultaneous conversion of carbon monoxide, uncombusted hydrocarbons and nitrogen oxides in automobile exhaust gases, which result in the case of nearly stoichiometric adjustment and maintenance of the fuel-air ratio in the automobile engine, there has been found particularly suitable, for example, the catalyst type which contains platinum, ruthenium, rhodium and rhenium (a single bed catalyst process). The operating temperature range of the catalysts is in the range of the automobile exhaust gases, namely 200° to 1000° C. 
     The following Examples are presented to more fully explain the manufacture and application of the catalyst in accordance with the present invention, being understood that the examples are intended as merely illustrative and in no sense limitative. 
     EXAMPLE 1 
     An aluminum hydroxide which consists essentially of pseudoboehmite with portions of a morphous hydroxide is dried, ground up and mixed with 3% by weight of zinc oxide which has a particle size of less than 3 μ. Granulation of the mixture is accomplished in accordance with the process described in German Offenlegungsschrift No. 2,308,890, the disclosure of which is incorporated herein by reference. According to this process, the aluminum oxide is treated with between 30 and 60 weight percent of a 0.1 to 2% ammonia solution prior to being formed into granules and dried, and preferably also has added thereto between 0.01 and 1% by weight of carbon black. The granulated material is calcined in a rotating drum under conditions of conventional temperature increase for 15 minutes between 1030° and 1050° C, and after cooling is impregnated with a solution at its boiling temperature which contains an amount of platinum tetrammine hydroxide and palladium tetrammine hydroxide which is sufficient to produce a finished catalyst No. 1 containing 0.045% by weight platinum and 0.017% by weight palladium after drying at 120° C and calcining at 800° C. 
     EXAMPLE 2 
     The carrier described in Example 1 is treated with a platinum tetrammine hydroxide solution at its boiling temperature which contains an amount of platinum sufficient to provide a finished catalyst No. 2 containing 0.1% by weight platinum after drying at 120° c C calcining at 800° C. 
     EXAMPLE 3 
     The carrier described in Example 1 is treated with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxy-chloro-hydroxide at its boiling temperature which contains an amount of platinum and ruthenium which is sufficient to provide the finished catalyst No. 3 with 0.15% by weight platinum and 0.075% by weight ruthenium after drying at 120° C and calcining at 800° C. 
     EXAMPLE 4 
     The carrier described in Example 1 is treated first with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxy-chloro-hydroxide at its boiling temperature which contains an amount of platinum and ruthenium sufficient to provide the catalyst with 0.05% by weight platinum and 0.05% by weight ruthenium after drying at 120° C. and calcining at 800° C. In the second step, the catalyst is impregnated with a solution of rhodium-III-nitrate and ammonium perrhenate at its boiling temperature which contains an amount of rhodium and rhenium sufficient to provide the catalyst after drying at 120° C. and calcining at 800° C. with 0.05% by weight each of rhodium and rhenium. After reduction in a stream of hydrogen at a temperature of 500° C., the final catalyst No. 4 contains 0.05% by weight each of platinum, ruthenium, rhodium and rhenium. 
     EXAMPLE 5 
     A honey-comb shaped support structure manufactured from a 50 μ thick steel sheet of non-rusting, scale-free and thermally stable steel material is dipped in a degreased and clean condition into an aqueous suspension which contains fibrous aluminum silicate and colloidal silicic acid. A commercially available product marketed under the designation &#34;Fiberfrax QF 180&#34; by the Carborundum Company is employed as the aluminium silicate. After drying at 200° C., the catalyst body is dipped in a suspension which contains 10% by weight of highly dispersed pseudoboehmite (particle size less than 3 μ) and 0.62% by weight of highly dispersed zinc oxide (particle size less than 3 μ) in water. After drying at 200° C. and calcining at 900° C., the catalyst support is treated with a solution at its boiling temperature which contains an amount of platinum tetrammine hydroxide and palladium tetrammine hydroxide which is sufficient to provide the finished catalyst No. 5 with 0.18% by weight platinum and 0.1% by weight palladium after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 6 
     The carrier described in Example 5 which is coated with aluminum silicate, aluminum hydroxide and zinc oxide is treated with a platinum tetrammine hydroxide solution at its boiling temperature which contains an amount of platinum sufficient to provide a finished catalyst No. 6 with 0.18% by weight platinum after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 7 
     The carrier described in Example 5 which is coated with aluminum silicate, aluminum oxide and zinc oxide is treated with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxy-chloro-hydroxide at its boiling temperature which contains an amount of platinum and ruthenium which is sufficient to provide the finished catalyst No. 7 with 0.15% weight platinum and 0.075% by weight ruthenium after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 8 
     The carrier described in Example 5 which is coated with aluminum silicate, aluminum hydroxide and zinc oxide is treated first with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxy-chloro-hydroxide at its boiling temperature which contains an amount of platinum and ruthenium sufficient to provide the catalyst with 0.05% by weight platinum and 0.05% by weight ruthenium after drying at 120° C. and calcining at 800° C. In the second step, the catalyst is impregnated with a solution of rhodium-III-nitrate and ammonium perrhenate which contains an amount of rhodium and rhenium sufficient to provide a content of 0.05% by weight each of rhodium and rhenium based upon the catalyst which is dried at 120° C. and calcined at 800° C. After reduction in a stream of hydrogen at a temperature of 500° C., the finished catalyst No. 8 contains 0.05% by weight each of platinum, ruthenium, rhodium and rhenium. 
     EXAMPLE 9 
     A ceramic honey-comb structure of a cordierite composition is put in a suspension which consists of 10% by weight of highly dispersed pseudoboehmite (particle size less than 3 μ) and 0.62% by weight of highly dispersed zinc oxide (particle size less than 3 μ) in water. After drying at 200° C. and calcining at 900° C. the catalyst support body is treated with a solution at its boiling temperature which contains an amount of platinum tetrammine hydroxide and palladium tetrammine hydroxide which is sufficient to provide the finished catalyst No. 9 with a content of 0.12% by weight platinum and 0.065% by weight palladium after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 10 
     The carrier described in Example 9 which is coated with aluminum oxide and zinc oxide is treated with a platinum tetrammine hydroxide solution at its boiling temperature which contains an amount of platinum sufficient to provide the finished catalyst No. 10 with a content of 0.12% by weight platinum after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 11 
     The carrier described in Example 9 which is coated with aluminum oxide and zinc oxide is treated with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxy-chloro-hydroxide at its boiling temperature which contains an amount of platinum and ruthenium sufficient to provide the finished catalyst No. 11 with a content of 0.1% by weight platinum and 0.05% by weight ruthenium after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 12 
     The carrier described in Example 9 which is coated with aluminum oxide and zinc oxide is treated first with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxy-chloro-hydroxide at its boiling temperature which contains an amount of platinum and ruthenium sufficient to provide the catalyst, after drying at 120° C. and calcining at 800° C., with a content of 0.033% by weight platinum and 0.033% by weight ruthenium. In the second step, the catalyst is impregnated with a solution of rhodium-III-nitrate and ammonium perrhenate which contains an amount of rhodium and rhenium so that the content of rhodium and rhenium based upon the catalyst dried at 120° C. and calcined at 800° C. amounts to 0.033% by weight for each. After reduction of the catalyst of the catalyst in a hydrogen stream at 500° C., the finished catalyst No. 12 contains 0.033% by weight each of platinum, ruthenium, rhodium and rhenium. 
     EXAMPLE 13 (COMPARATIVE) 
     In order to provide proof that a catalyst having a carrier of aluminum oxide which does not contain the addition of zinc in accordance with the present invention possesses an essentially lower resistance to thermal aging, a honey-comb support structure prepared from a 50 μ thick sheet of a non-rusting, scale-free and heat resistant steel material is dipped in a defatted and cleaned condition into a suspension which is comprised of fibrous aluminum silicate in aqueous colloidal silicic acid. A commercially available product available under the designation &#34;Fiberfrax QF 180&#34; from the Carborundum Company is employed as the aluminum silicate. After drying at 200° C. the catalyst body is dipped in a suspension which is comprised of 10% by weight of highly dispersed pseudoboehmite (particle size 3 μ) in water. After drying at 200° C. and calcining at 900° C., the catalyst body is treated with a solution at its boiling temperature which contains an amount of platinum tetrammine hydroxide and palladium tetrammine hydroxide sufficient to provide the present catalyst No. 13 with a content of 0.18% by weight platinum and 0.1% by weight palladium after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 14 (COMPARATIVE) 
     The carrier described in Example 13 is treated with aluminum silicate and aluminum oxide is treated with a platinum tetrammine hydroxide solution at its boiling temperature which contains an amount of platinum sufficient to provide the finished catalyst No. 14, after drying at 120° C. and calcining at 800° C. with a content of 0.18% by weight of platinum. 
     EXAMPLE 15 (COMPARATIVE) 
     The carrier described in Example 13 which is coated with aluminum silicate and aluminum oxide is treated with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxy-chloro-hydroxide at its boiling temperature which contains an amount of platinum and ruthenium sufficient to provide the catalyst No. 15 with a content of 0.15% by weight platinum and 0.075% by weight ruthenium after drying at 120° C. and calcining at 800° C. 
     EXAMPLE 16 (COMPARATIVE) 
     The carrier described in Example 13 which is coated with aluminum silicate and aluminum oxide is treated with a mixed solution of platinum tetrammine hydroxide and ruthenium tetrammine-hydroxo-chloro-hydroxide at the boiling temperature which contains an amount of platinum and ruthenium sufficient to provide the catalyst after drying at 120° C. and calcining at 800° C., with a content of 0.05% by weight platinum and 0.05% by weight ruthenium. In the second step, the catalyst is impregnated with a solution of rhodium-III-nitrate and ammonium perrhenate which contains an amount of rhodium and rhenium sufficient to provide a metal content based upon the catalyst dried at 120° C. and calcined at 800° C. of 0.05% by weight each of rhodium and rhenium. After reduction of the catalyst in a hydrogen stream of 500° C., the finished catalyst No. 16 contains 0.05% by weight each of platinum, ruthenium, rhodium and rhenium. 
     EXAMPLE 17 
     In order to test the oxidation activity, the catalysts 1, 2, 5, 6, 9, 10, 13 and 14 are tested with a gas mixture containing: 
     
         ______________________________________300 ppm            Ethylene1 Vol.-%           Carbon monoxide10 Vol.-%          Carbon dioxide10 Vol.-%          Water vapor3 Vol.-%           OxygenRest               Nitrogen______________________________________ 
    
     The space velocity is 40000 hr. -   1 .The residual content of CO and ethylene is determined after exit from the catalyst bed with Uras (CO) and FID(ethylene) under conditions of stepwise increased gas entrance temperature, whereby the measurement is accomplished in a nearly adiabatic reactor after accomplishment of temperature equilibrium. From the curve plotted from the data points obtained, there is calculated by graphical interpolation the temperature at which 50% of the CO and 50% of the ethylene is converted. 
     This half-value temperature (T 50 ) serves as an indication of activity. After testing the catalyst in fresh condition under the above recited conditions, the catalysts are then aged in air at 24 hours respectively, at 870° C., 980° C. and partially at 1090° C. After each aging step a new activity test is carried out. The results are set forth in Table 
     
                                           TABLE I__________________________________________________________________________CATALYST        CO-CONVERSION                     C.sub.2 H.sub.4 -CONVERSIONNo.     AGING   50%       50%__________________________________________________________________________1      fresh    208       208  24 hr. 870° C.           217       220  24 hr. 980° C.           234       240  24 hr. 1090° C.           251       2592      fresh    237       240  24 hr. 870° C.           258       261  24 hr. 980° C.           281       286  24 hr. 1090° C.           298       3025      fresh    221       228  24 hr. 870° C.           230       245  24 hr. 980° C.           249       2616      fresh    252       253  24 hr. 870° C.           265       268  24 hr. 980° C.           286       2939      fresh    188       186  24 hr. 870° C.           201       208  24 hr. 980° C.           221       225  24 hr. 1090° C.           253       26410     fresh    268       272  24 hr. 870° C.           280       288  24 hr. 980° C.           291       297  24 hr. 1090° C.           307       31213     fresh    227       226  24 hr. 870° C.           254       273  24 hr. 980° C.           292       not accomplished14     fresh    252       252  24 hr. 870° C.           316       328  24 hr. 980° C.           371       not accomplished__________________________________________________________________________ 
    
     EXAMPLE 18 
     For the purpose of examining the reduction activity, the catalysts 3, 7, 11 and 15 are tested with a gas mixture containing: 
     
         ______________________________________0.1            Vol.-%      NO4              Vol.-%      CO0.5            Vol.-%      H.sub.210             Vol.-%      CO.sub.214             Vol.-%      H.sub.2 O-Vapor0-2.3          Vol.-%      O.sub.2Rest                       N.sub.2______________________________________ 
    
     The testing is carried out with a variable oxygen content between 0 and 2.3% by volume and at a space velocity of 50000 hr. -   1  and with a gas entrance temperature of 500° C. 
     The conversion value of NO as well as the ammonia produced are calculated in accordance with the formula: ##EQU1## If one sets L=1, then the oxidizing and reducing reaction participants stand in stoichomatic relationship. The activity of the catalyst is evaluated in accordance with the NO-conversion and the NH 3  -formation in the region of L=0-1, whereby the goal is a complete conversion of the NO and a very small NH 3  -formation. 
     After testing in the fresh condition under the indicated conditions, the catalysts are aged in air for 24 hrs. respectively at 870° C., 980° C., and partially at 1090° C. After each aging step, a new activity test is carried out. The results are set forth in Table 2. 
     
                                           TABLE 2__________________________________________________________________________                Cat.No. 3                           Cat.No. 7                                    Cat.No. 11                                              Cat.No. 15     Space Vel. NO-  NH.sub.3                           NO- NH.sub.3                                    NO-  NH.sub.3                                               NO-  NH.sub.3Temp.1         Conv.  formation                Conv.                     formation                           Conv.                               formation                                    Conv.                                         formationAging° C.     hr.    L   %    ppm   %   ppm  %    ppm   %    ppm__________________________________________________________________________Fresh500  50000  0.02                100  55    100 100  100  100   100  70            0.07                100  65    100 90   100  100   100  100            0.11                100  50    100 80   100  100   100  80            0.16                100  45    100 70   100  70    100  70            0.24                100  10    100 70   100  50    100  45            0.33                100  7     100 45   100  40    100  25            0.49                100  5     100 20   100  20    100  10            0.82                100  3     100 10   100  20    100  10            0.87                100  0     100 10   100  10    100  10            0.91                100  0     100 10   100  10    100  3            0.96                100  0     100 5    100  5     100  3            1.00                100  0     100 2    100  5     100  3            1.05                30   --     34 --   50   --    54   --24 hr.870         0.02                100  60    100 100  100  40    100  70            0.07                100  70    100 100  100  50    100  120            0.11                100  65    100 80   100  65    100  100            0.16                100  55    100 70   100  60    100  80            0.24                100  30    100 60   100  55    100  50            0.33                100  15    100 55   100  35    100  40            0.49                100  8     100 50   100  25    100  15            0.82                100  3     100 10   100  15    100  5            0.87                100  1     100 10   100  15    100  5            0.91                100  0     100 10   100  15    100  3            0.96                100  0     100 5    100  15    100  2            1.00                100  0     100 5    100  5     100  2            1.05                30   --     39 --   38   --    60   --24 hr.980         0.02                100  35    100 70   100  40    50   35            0.07                100  30    100 80   100  45    79   55            0.11                100  30    100 60   100  30    72   35            0.16                100  25    100 50   100  25    68   25            0.24                100  18    100 25   100  20    59   15            0.33                100  12    100 10   100  12    53   8            0.49                100  5     100 5    100  10    43   5            0.82                100  3     100 3    100  7     33   5            0.87                100  0     100 3    100  5     30   4            0.91                100  0     100 3    100  5     25   4            0.96                97   0     100 3    100  5     18   4            1.00                96   0      99 3    100  3     16   4            1.05                15   --     35 --   30   --    14   --24 hr.1090        0.02                96   70             94   30            0.07                97   100            95   65            0.11                97   100            97   60            0.16                98   90             98   50            0.24                98   90             99   38            0.33                98   70             99   25            0.49                99   65             99   20            0.82                99   60             99   15            0.87                99   60             99   15            0.91                97   50             99   15            0.96                96   30             98   10            1.00                94   20             97   7            1.05                0    --             0    --__________________________________________________________________________ 
    
     EXAMPLE 19 
     To examine the activity for the simultaneous conversion of hydrocarbons, carbon monoxide and nitrogen oxides, the catalysts 4, 8, 12 and 16 are tested with a gas mixture which approximates in its composition an automobile exhaust gas which results by a stoichiometrically adjusted air-fuel ratio in the engine. The gas mixture contains: 
     
         ______________________________________0.1            Vol.-%      NO0.5            Vol.-%      C.sub.2 H.sub.41              Vol.-%      CO0.4            Vol.-%      H.sub.210             Vol.-%      CO.sub.214             Vol.-%      Water Vapor0.45-0.90      Vol.-%      O.sub.2Rest                       N.sub.2______________________________________ 
    
     The oxygen content is varied between 0.45 and 0.9% by volume. The space velocity is 50000 hrs. -   1  at a gas entrance temperature of 500° C. If one sets the stoichiometric ratio of the oxidizing and reducing reaction particiments equal to 1, than there results the relationship: ##EQU2## The effectiveness of the catalyst under variable L-values in the region of L=1 (stoichiometric exhaust gas composition) is determined in the following way: the degree of conversion of NO, CO and C 2  H 4  in percent are graphically plotted against the values of L. The region of L within which the degree of conversion of the three above-mentioned exhaust gas components lies above 90% is the criterion for the catalyst effectiveness and should be as large as possible. 
     After testing in the fresh condition under the conditions set forth above, the catalysts are aged in air for 24 hrs. respectively at 870° C., 980° C. and partially at 1090° C. After each aging step, a new activity test is carried out. The results are set forth in Table 3. 
     The results show that catalysts which are thermally exceptionally stable are obtained with the use of the carrier composition according to the present invention, irrespective of the noble metal composition and the testing procedure applied. In contrast, it is clear from the results in connection with the catalyst produced according to examples 13-16, wherein the active carrier substance does not contain zinc, that the effectiveness after 24 hrs. of aging at 980° C. is nearly completely lost (see Tables 1, 2 and 3). 
     Because the honey-comb structure utilized as the Example for a metallic support is constructed of a material having a tinder resistance value near 1000° C., the last aging step at 1090° C. is omitted in this instance. 
     
                                           TABLE 3__________________________________________________________________________                       Catalyst                              No. 4     Space Vel. NO-    CO-    HC-Temp.1         Conv.  Conv.                Conv.Aging° C.     hr.    L   %      %      %      ΔL__________________________________________________________________________fresh500  50000  0.63                100    81     95     0.26            0.86                100    90     96            0.89                100    98     97            0.95                100    99     98            1.01                92     100    99            1.08                76     100    100            1.14                60     100    100            1.20                40     100    10024 hr.870         0.63                100    77     96     0.25            0.76                100    89     96            0.89                100    97     97            0.95                99     99     99            1.01                92     100    100            1.08                72     100    100            1.14                54     100    100            1.20                38     100    10024 hr.980         0.63                100    73     87     0.21            0.76                100    87     90            0.89                100    96     93            0.95                98     99     97            1.01                90     100    99            1.08                64     100    99            1.14                30     100    99            1.20                12     100    9924 hr.1090        0.63                100    65     84     0.20            0.76                100    83     91            0.89                100    97     92            0.95                99     100    94            1.01                90     100    94            1.08                67     100    95            1.14                41     100    95            1.20                16     100    95fresh500         0.63                100    87     95     0.32            0.76                100    92     97            0.89                100    95     99            0.95                100    97     100            1.01                95     100    100            1.08                70     100    100            1.14                55     100    100            1.20                45     100    10024 hr.870         0.63                100    88     93     0.30            0.76                100    93     94            0.89                100    95     96            0.95                100    97     99            1.01                85     100    99            1.08                57     100    100            1.14                47     100    100            1.20                39     100    10024 hr.980         0.63                100    86     85     0.27            0.76                100    92     90            0.89                100    94     91            0.95                100    97     93            1.01                70     98     94            1.08                35     100    99            1.14                25     100    99            1.20                19     100    9924 hr.1090        0.63            0.76            0.89            0.95            1.01            1.08            1.14            1.20fresh500         0.63                100    85     96     0.28            0.76                100    91     96            0.89                100    94     97            0.95                100    96     99            1.01                97     98     100            1.08                73     100    100            1.14                58     100    100            1.20                41     100    10024 hr.870         0.63                100    84     92     0.27            0.76                100    92     95            0.89                100    97     97            0.95                100    99     100            1.01                82     100    100            1.08                63     100    100            1.14                47     100    100            1.20                34     100    10024 hr.980         0.63                100    82     90     0.22            0.76                100    88     91            0.89                100    95     93            0.95                100    98     93            1.01                92     100    95            1.08                70     100    97            1.14                51     100    97            1.20                40     100    9724 hr.1090        0.63                100    76     85     0.21            0.76                100    89     90            0.89                100    96     92            0.95                100    98     93            1.01                82     99     94            1.08                61     100    95            1.14                50     100    95            1.20                35     100    95fresh500         0.63                100    86     94     0.33            0.76                100    93     96            0.89                100    98     98            0.95                100    100    99            1.01                92     100    100            1.08                79     100    100            1.14                60     100    100            1.20                41     100    10024 hr.870         0.63                100    83     93     0.33            0.76                100    92     95            0.89                100    98     97            0.95                98     100    98            1.01                94     100    99            1.08                83     100    100            1.14                66     100    100            1.20                44     100    10024 hr.980         0.63                98     40     60     0.00            0.76                98     61     70            0.89                88     73     78            0.95                83     80     81            1.01                76     84     83            1.08                64     87     84            1.14                56     88     85            1.20                50     90     85__________________________________________________________________________