Process for production of a catalyst having excellent heat resistance for use in purifying exhaust gases from internal combustion engines

Abstract: An exhaust gas purifying catalyst having excellent heat resistance comprises a platinum-group element, active alumina, cerium oxide, a barium compound and a zirconium compound on a monolithic support. The barium compound is preferably barium hydroxide, barium oxide or barium carbonate. The zirconium compound is preferably zirconium oxide.

Description: This invention relates to a catalyst for purifying exhaust gases discharged from internal combustion engines of automobiles, etc., and a process for its production. More specifically, it relates to a process for producing a catalyst which shows better exhaust gas purifying ability than conventional catalysts even after it has been exposed for a long period of time to high temperatures (900 to 1100°C) immediately below the manifold, for example, and to a process for its production. Three-way catalysts for simultaneously removing hydrocarbons, carbon monoxide and nitrogen oxides in exhaust gases discharged from internal combustion engines or automobiles, etc. now mainly contain platinum-group elements such as platinum and rhodium and for increasing low-temperature activity, cerium oxide having an oxygen storing effect. One property required of the present-day catalysts is heat resistance at high temperatures of 900 to 1100°C. This is because the place of installing the catalysts tends to be immediately below the manifold near the engine, and during high speed driving, the temperature of the exhaust gases increases. However, catalysts containing platinum-group elements or cerium oxide are susceptible to degradation at such high temperatures. The addition of oxides of rare earth metals and alkaline earth metals has heretofore been known as a method of increasing the heat resistance of the catalysts (for example, Japanese Laid-Open Patent Publications Nos. 99988/1975 and 31994/1977). It is also stated that the addition of lanthanum and calcium to inhibit thermal degradation of cerium oxide at high temperatures can result in an increase in the heat resistance of catalysts (for example, Japanese Laid-Open Patent Publications Nos. 631333/1982 and 46247/1986). Since the temperature of exhaust gases has recently shown a rising tendency as a result of high-speed operation of automobile engines, the catalysts described in the above-cited patent documents do not have sufficient activity after use at high temperatures. It has been desired therefore to develop an excellent catalyst whose activity after use at high temperatures does not decrease so much as in the conventional catalysts. EP-A-0171151 (Engelhard Corporation) discloses a three-way catalyst for lean exhaust systems and a process for the preparation thereof. The catalyst comprises rhodium dispersed on particles of gamma alumina, an amount of rare earth oxide such as ceria, and a second platinum group metal such as platinum or palladium. The rhodium is dispersed on gamma alumina particles which are substantially rare-earth oxide free. The second platinum group metal, may be dispersed on rare-earth oxide particles, or on gamma alumina particles containing rare-earth oxide. The catalyst is made by separately coating one batch of particles with rhodium and a second batch of particles with the second platinum-group metal, followed by combining the batches to form the catalyst. The catalyst may then be suspended in a slurry and coated onto a monolithic support, if desired. FR-A-2449475 (Deutsche Gold- und Silber- Scheideanstalt) discloses catalysts for use in catalytic convertors for exhaust gases. The catalysts comprise rhodium and platinum dispersed on stabilised gamma alumina, cerium oxide, zirconium oxide, iron oxide and optionally barium oxide. The catalysts are obtained by multi-step deposition of the catalyst constituents on a monolithic substrate followed by reduction in a hydrogen stream. It is an object of this invention to provide a process for producing a catalyst which shows excellent exhaust gas purifying ability even after it has been exposed to high temperatures of 900 to 1100°C for a long period of time. The present inventors have made extensive investigations in order to solve the above problems, and have found a process for producing a catalyst, which catalyst comprises a combination of at least platinum and rhodium, active alumina, cerium oxide, a barium compound and a zirconium compound, and which combination is very effective for maintaining the excellent catalyst activity of an exhaust gas purifying catalyst even after it has been exposed to high temperatures of 900 to 110°C. The present invention provides a process for producing an exhaust gas purifying catalyst comprising the steps of: preparing an alumina powder containing a plurality of platinum-group elements by treating active alumina separately from the other components of the slurry defined below with compounds of the plurality of platinum-group elements, said plurality of platinum-group elements comprising platinum and rhodium; preparing a slurry comprising a single said alumina powder containing a plurality of platinum-group elements, cerium oxide, a barium compounds and a zirconium compound; depositing the slurry on a monolithic catalyst support, and calcining the catalyst support with the slurry deposited thereon, and wherein the weight of the platinum is from 0.1 to 10g per liter of the finished catalyst, the weight of the rhodium is from 0.02 to 2g per liter of the finished catalyst, the weight of active alumina is from 30 to 200g per liter of the finished catalyst, the weight of the cerium oxide is from 10 to 150g per liter of the finished catalyst, the weight of the barium compound is from 0.1 to 20g calculated as barium oxide per liter of the finished catalyst and the weight of the zirconium compound is from 0.1 to 30g calculated as zirconium oxide per liter of the finished catalyst. The present invention will now be described below in detail. In the present invention, the addition of various barium compounds and zirconium compounds shows an effect of inhibiting sintering of the platinum-group elements and cerium oxide and maintains the oxygen storage effect of cerium oxide and produces favorable results in maintaining the activity of the catalyst after it has been used at high temperatures of 900 to 1100°C. First, the catalyst obtained by the process of this invention will be described. The exhaust gas purifying catalyst obtained by the process of this invention comprises a monolithic support and being present thereon, platinum, rhodium, active alumina, cerium oxide, a barium compound and a zirconium compound as catalyst components. The monolithic support is comprised of a refractory metal oxide or a refractory metal and is, for example, of a honeycomb-like or three-dimensional network structure. The monolithic support may also be a foamed support. Examples of the refractory metal oxides are cordierite mullite, alpha-alumina, sillimanite, magnesium silicate, zircon, pentalite, spodumene and aluminosilicates. Examples of the refractory metals are iron-base alloys, refractory nickel-base alloys and refractory chromium-base alloys. Of these monolithic supports, a honeycomb-shaped support composed of cordierite is most preferably used. Platinum and rhodium are contained as the platinum-group element in order to purify CO, HC and NO x at the same time. The weight of platinum is from 0.1 to 10 g, preferably 0.1 to 3 g, per liter of the catalyst. The weight of rhodium is 0.02 to 2 g, preferably 0.02 to 0.7 g, per liter of the catalyst. Active alumina is preferably gamma-alumina. It desirably has a specific surface area of 10 to 300 m²/g. Its weight is 30 to 200 g, preferably 40 to 120 g, per liter of the catalyst. Cerium oxide has an oxygen storing effect, and is used to reduce the amount of the platinum-group element used and maintain the same purifying ability. Its weight is 10 to 150 g, preferably 10 to 50 g, per liter of the catalyst. Desirably, cerium oxide has a specific surface area of 10 to 300 m²/g. The barium compound is preferably, barium hydroxide, barium oxide and barium carbonate. Its weight is 0.1 to 20 g, preferably 3 to 15 g, more preferably 5 to 10 g, calculated as barium oxide. The zirconium compound is preferably zirconium oxide, and its weight is 0.1 to 30 g, preferably 5 to 25 g, more preferably 7 to 20 g, per liter of the catalyst. [B] The process for producing the exhaust gas purifying catalyst of this invention will be described. Preparation of active alumina containing the platinum-group element Active alumina (for example, gamma-alumina) is put in a mixer. The particle diameter of the active alumina is 1 to 100 microns, preferably 1 to 50 microns, more preferably 1 to 30 microns. Part of cerium oxide may be incorporated in the active alumina. A platinum compound (such as an amine solution of hexahydroxoplatinic acid, or chloroplatinic acid) is added to the active alumina. The platinum compound may be added little by little while gamma-alumina is stirred in the mixer, or it may be added at a time. The platinum compound may be added as a solution (such as an aqueous solution) or a suspension (such as an aqueous suspension). The weight of the platinum compound added may be 1 to 100 g calculated as platinum, or 100 to 500 ml as a solution of the platinum compound, per kilogram of the active alumina. A rhodium compound (such as rhodium nitrate or rhodium chloride) may be added little by little or at a time to a mixture containing the active alumina and the platinum compound. The rhodium compound may be added as a solution or suspension. The weight of the rhodium compound added may be 0.2 to 50 g calculated as rhodium, or 100 to 500 ml as a solution of the rhodium compound, per liter of the active alumina. Subsequently, a solution of acetic acid, preferably a 10-40% by weight aqueous solution of acetic acid, is added to a mixture containing the platinum compound and the active alumina. The acetic acid solution is preferably added little by little while the mixture is stirred in the mixer. The amount of acetic acid added may be 100 to 300 ml per kilogram of active alumina. Preparation of a slurry Active alumina containing the platinum-group elements obtained by the above method, cerium oxide, the barium compound, the zirconium compound, acetic acid and deionized water were introduced into a mill and pulverized to form a slurry. The weight of cerium is 50 to 500 g, preferably 150 to 400 g, per kilogram of active alumina. The barium compound is preferably barium hydroxide, barium acetate or barium oxide. Its weight is 1.0 to 310 g, preferably 45 to 225 g, more preferably 60 to 150 g. The zirconium compound is preferably zirconyl acetate or zirconyl hydroxide. Its weight is 1.0 to 430 g, preferably 70 to 350 g, more preferably 100 to 290 g, per kilogram of the active alumina calculated as zirconium oxide. Acetic acid is used preferably in an amount of 50 to 300 ml per kilogram of the active alumina as a 60-90 wt.% aqueous solution. The amount of deionized water may be 50 to 1000 ml per kilogram of the active alumina. By the above pulverization in the mill, the average particle diameter of the mixture in the slurry can be adjusted to 0.1 to 10 microns, preferably 1 to 5 microns. The resulting slurry was transferred to a vessel, and deionized water was added to form a slurry having a predetermined specific gravity which may, for example, be 1.20 to 1.85 g/ml. Deposition of the slurry on a monolithic support The slurry is deposited on a monolithic support which is described in section [A] above. The slurry is deposited on the monolithic support for a period of, for example, 1 to 60 seconds, preferably 3 to 10 seconds, and then the excess of the slurry in the cells is removed by an air blow. Then, the support having the slurry deposited thereon is dried with hot air preferably at a temperature of 20 to 100 °c to remove at least 50%, preferably at least 90%, of water. After removing the water, the support may be calcined at a temperature of 200 to 900 °C, preferably 300 to 800 °C, for 10 minutes to 10 hours, preferably 15 to 60 minutes, in air, for example. When the temperature of the support is to be gradually raised in calcination, the above drying (removal of water) may be omitted. By the above slurry deposition step, there is deposited per liter of the finished catalyst 30 to 200 g of alumina, 0.1 to 10 g of platinum, 0.02 to 2 g of rhodium, 10 to 150 g of cerium oxide, 0.1 to 20 g of the barium compound calculated as barium oxide, and 0.1 to 30 g of the zirconium compound calculated as zirconium oxide. The following examples illustrate the present invention in more detail. (a) Active alumina (1.2 kg) having a BET specific surface area of 150 m²/g and an average particle diameter of 30 microns was put in a mixer, and with stirring, 300 ml of an aqueous amine solution of hexahydroxoplatinic acid containing 20.4 g of platinum was added dropwise little by little and dispersed uniformly. Subsequently, 150 ml of an aqueous solution of rhodium nitrate containing 4.1 g of rhodium was added dropwise little by little and uniformly dispersed. Finally, 100 ml of 25% by weight acetic acid was added little by little and uniformly dispersed to prepare an alumina powder (Pt/Rh=5/1) containing platinum and rhodium. (b) The alumina containing platinum and rhodium obtained in step (b) (532 g as the dry weight), 304 g of cerium oxide having an average particle diameter of 15 microns, 117 g of barium hydroxide octahydrate (57 g calculated as barium oxide), 535 g (107 g calculated as zirconium oxide), 71 ml of 90% by weight acetic acid and 100 ml of deionized water were put in a mill and pulverized and mixed to form an alumina slurry. The pulverizing time was such that at least 90% of the particles in the slurry had a particle diameter of not more than 9.0 microns. (c) Deionized water was addd to the slurry obtained in step (b) to adjust its specific gravity to 1.66 g/ml to form a diluted slurry. A cylindrical monolithic carrier of cordierite (volume 1.0 liters, 300 cells/in²) having a length of 147.5 mm in length and 93 mm in diameter was immersed for 5 seconds in the diluted slurry, withdrawn from the diluted slurry, and then subjected to an air blow to remove the excess of the slurry. It was further dried at 30 to 60 °C, and then calcined at 500 °C for 30 minutes to obtain a catalyst A. The catalyst A obtained by a series of steps (a), (b) and (c) contained 1.4 g of platinum and rhodium, 70 g of alumina, 40 g of cerium oxide, 7.5 g, calculated as barium oxide, of the barium compound and 14 g of zirconium oxide per liter of the finished catalyst. COMPARATIVE EXAMPLE 1 A catalyst B was prepared in the same way as in Example 1 except that barium hydroxide and zirconyl acetate were not added in step (b). COMPARATIVE EXAMPLE 2 A catalyst C was prepared in the same way as in Example 1 except that in step (b), zirconyl acetate was not added. COMPARATIVE EXAMPLE 3 A catalyst D was prepared in the same way as in Example 1 except that in step (b), barium hydroxide was not added. COMPARATIVE EXAMPLE 4 A catalyst E was prepared in the same way as in Example 1 except that in step (b), cerium oxide was not added. EXAMPLE 2 A catalyst F was prepared in the same way as in Example 1 except that in step (b), barium oxide in the same amount calculated as barium oxide was used instead of barium hydroxide. EXAMPLE 3 A catalyst G was prepared in the same way as in Example 1 except that in step (b), the amount of the barium hydroxide was changed to 83 g from 117 g. The catalyst G contained 5.3 g of the barium compound calculated as barium oxide per liter of the finished catalyst. EXAMPLE 4 A catalyst H was prepared in the same way as in Example 1 except that in step (b), the amount of the barium hydroxide added was changed to 156 g from 117 g. The catalyst H contained 10 g of the barium compound calculated as barium oxide per liter of the finished catalyst. EXAMPLE 5 A catalyst I was prepared in the same way as in Example 1 except that in step (b), the amount of the barium hydroxide added was changed to 55 g from 117 g. The catalyst I contained 3.5 g of the barium compound calculated as barium oxide per liter of the finished catalyst. EXAMPLE 6 A catalyst J was prepared in the same way as in Example 1 except that in step (b), zirconyl hydroxide in nearly the same amount calculated aa zirconium oxide was used instead of zirconyl acetate. EXAMPLE 7 A catalyst K containing 20 g of zirconium oxide per liter of the finished catalyst was prepared in the same way as in Example 1 except that in step (b), the amount of zirconyl acetate added was changed to 764 g from 535 g. EXAMPLE 8 A catalyst L containing 7 g of zirconium oxide per liter of the finished catalyst was prepared in the same way as in Example 1 except that in step (b), the amount of zirconyl acetate added was changed to 268 g from 535 g. EXAMPLE 9 A catalyst M containing 25 g of cerium oxide per liter of the finished catalyst was prepared in the same way as in Example 1 except that in step (b), the amount of cerium oxide added was changed to 190 g from 304 g. EXAMPLE 10 A catalyst N containing 55 g of cerium oxide per liter of the finished catalyst was prepared in the same way as in Example 1 except that in step (b), the amount of cerium oxide added was changed to 418 g from 304 g. TEST EXAMPLE 1 The catalysts (sample designations A to N) obtained in Examples 1 to 10 and Comparative Examples 1 to 4 were each subjected to a durability test by the following method, and their catalytic performances were evaluated. Durability test. Each of the catalysts was filled into a stainless steel multiconverter. Under the following conditions, an exhaust gas was passed through the multiconverter for 50 hours. Air-fuel ratio (A/F): 16.2 Temperature of the catalyst bed: 950 °C. Fuel: Gasoline (lead-free) Test for evaluating catalytic performance The performance of each catalyst was evaluated by filling the catalyst into the same multiconverter as above fitted with a sampling tube, and analyzing inlet and outlet gas components by means of MEXA 8120 (made by Horiba Seisakusho). An exhaust gas was used, and the test was carried out under the following conditions. Air-fuel ratio: 14.55, 14.7, 14.85 ( A/F=±0.5) Space velocity (SV): 133,000 hr⁻¹ Temperatre at the inlet of the catalyst: 500 °C Frequency: 2.0 Hz The ratio of purifying the components (CO, HC, NO x ) are shown by average values of the purification ratios at each of the above A/F ratios. The results are shown in Tables 1 to 6. Table 1 shows that the catalyst A containing cerium oxide, the barium compound and the zirconium compound simultaneously had excellent purifying ability even after the high temperature durability test at 950 °C; but that absent at least one of these additives, the purifying ability of the catalyst after the high temperature durability test at 950 °C was markedly decreased. Table 2 shows that when the barium compound, irrespective of its type, was present together with the other additives (cerium oxide and the zirconium compound), excellent purifying ability was manifested after the high-temperature durability test. Table 3 shows that the effect of adding the barium compound was noted even when its amount was small, but the optimum range of its amount is 0.1 to 20 g/liter, preferably 3.0 to 15.0/liter, more preferably 5.0 to 10 g/liter, calculated as barium oxide. Table 4 shows that when the zirconium compound, irrespective of its type, was present together with the other additives (cerium oxide and the barium compound), excellent purifying ability was manifested after the high-temperature durability test. Table 5 shows that the effect of adding the zirconium compound was noted even when its amount was small, but the optimum range of its amount is 0.1 to 30 g/liter, preferably 5.0 to 25.0 g/liter, more preferably 7.0 to 20 g/liter, calculated as zirconium oxide. Table 6 shows that the optimum range of the amount of cerium oxide added is 10 to 150 g/liter, preferably 10 to 50 g/liter. TEST EXAMPLE 2 The crystallite size of cerium oxide in each of the catalysts after the durability test was determined by using an X-ray diffraction device (RAD-IIVB made by Rigaku Denki Co., Ltd.), and the extent of thermal degradation of cerium oxide was evaluated. When thermal degradation proceeds, the crystallite size of cerium oxide gradually increases and its oxygen storing effect decreases. Hence, the activity of the catalyst is reduced. Table 7 shows that the extent of thermal degradation of cerium oxide was markedly inhibited in the catalyst containing the barium compound and the zirconium compound simultaneously. As stated hereinabove, by the presence of the platinum-group element, active alumina, cerium oxide, the barium compound and the zirconium compound as active ingredients on the monolithic support, thermal degradation of cerium oxide in the catalyst of this invention was markedly inhibited as compared with that in conventional catalysts. When the activity of the catalyst of this invention after the high-temperature durability test at 950 °C is evaluated in terms of the purifying ratios of the regulated substances at a normally used temperature (500 °C), the catalyst of this invention can increase the purifying ratio of carbon monoxide by 10 to 15%, the purifying ratio of hydrocarbons by 3 to 7% and the purifying ratio of nitrogen oxides by 10 to 15%. [Explanation of Tables] Table 1: Comparison of the effects of the additives on the purifying abilities of the catalysts after the high-temperature durability test at 950 °C. Table 2: Comparison of the effects of the type of the barium compound added on the purifying abilities of the catalysts after the high-temperature durability test at 950 °C. Table 3: Comparison of the effects of the amount of the barium compound added on the purifying abilities of the catalysts after the high-temperature durability test at 950 °C. Table 4: Comparison of the effects of the type of the zirconium compound added on the purifying abilities of the catalysts after the high-temperature durability test at 950 °C. Table 5: Comparison of the effects of the amount of the zirconium compound added on the purifying abilities of the catalysts after the high-temperature durability test at 950 °C. Table 6: Comparison of the effects of the amount of cerium oxide added on the purifying abilities of the catalysts after the high-temperature durability test at 950 °C. Table 7: Comparison of the crystallite sizes of cerium oxide in the catalysts after the high-temperature durability test at 950 °C with regard to the effect of the additives on the inhibition of thermal degradation of cerium oxide. In all tables, "Ex." stands for Example, and "CEx.", Comparative Example.

Claims: A process for producing an exhaust gas purifying catalyst comprising the steps of: preparing an alumina powder containing a plurality of platinum-group elements by treating active alumina separately from the other components of the slurry defined below with compounds of the plurality of platinum-group elements, said plurality of platinum-group elements comprising platinum and rhodium; preparing a slurry comprising a single said alumina powder containing a plurality of platinum-group elements, cerium oxide, a barium compound and a zirconium compound; depositing the slurry on a monolithic catalyst support, and calcining the catalyst support with the slurry deposited thereon, and wherein the weight of the platinum is from 0.1 to 10g per liter of the finished catalyst, the weight of the rhodium is from 0.02 to 2g per liter of the finished catalyst, the weight of active alumina is from 30 to 200g per liter of the finished catalyst, the weight of the cerium oxide is from 10 to 150g per liter of the finished catalyst, the weight of the barium compound is from 0.1 to 20g calculated as barium oxide per liter of the finished catalyst and the weight of the zirconium compound is from 0.1 to 30g calculated as zirconium oxide per liter of the finished catalyst. A process according to claim 1 wherein the monolithic catalyst support is of a honeycomb-like or three-dimensional network structure. A process according to claim 1 or 2 wherein the monolithic catalyst support is composed of cordierite. A process according to claim 1, 2 or 3 wherein the monolithic catalyst support is composed of a refractory metal. A process according to any preceding claim wherein the barium compound is barium hydroxide. A process according to any preceding claim wherein the zirconium compound is zirconyl acetate.

Inventors: FUNABIKI MASAKI, YAMADA TEIJI, FUNABIKI, MASAKI, YAMADA, TEIJI
Applicants: ENGELHARD CORP, ENGELHARD CORPORATION
Application year: 1988
Main classification: B01J23
IPC codes: B01J23, B01D53