METHOD AND CATALYST FOR PURIFICATION OF GAS

Abstract: A catalyst for the purification of a gas containing ozone or a component of offensive odour composed of: (A) a composite oxide of (a) titanium and (b) at least one element selected from the group consisting of Si, Zr, and P; and (B) at least one element selected from the group consisting of Mn, Fe, Co, Ni and Ag oxides and Pt, Pd and Rh metals.

Description: This invention relates to a method for the purification of a gas and a catalyst for use in the purification. More particularly, it relates to a method for catalytically decomposing ozone contained in a gas or catalytically decomposing a component of offensive odor in a gas through oxidation with ozone and to a catalyst used for the decomposition. Description of the Prior Art: Ozone possesses a strong oxidizing ability and, on decomposition, converts itself into harmless oxygen. Thus, it has found extensive utility in various applications aimed at deodorizing, sterilizing, and bleaching various substances and even lowering the COD level of plant effluents. Unfortunately, since part of the ozone so used in varying treatments is released in its unaltered form into the air, the stray ozone has the possibility of giving rise to secondary environmental pollution such as, for example, generation of a photochemical smog. In the case of an airplane in flight through the stratosphere, since the air containing ozone is drawn into the interior of the airplane, the passengers and the crew aboard the airplane may possibly be exposed to the adverse effect of the ozone in the air. Further, the issue of ozone from machines incorporating therein various high voltage generating devices such as, for example, xerographic copying machines has been recently posting a problem. Since these machines are installed mainly in rooms, the ozone so generated pollutes the interiors of the rooms, though the amount of the ozone so generated is very small. The odour of ozone can be perceived even when the ozone is present in a concentration of not more than 1 ppm. When ozone is present in the air in a concentration exceeding 2 ppm, it stimulates the respiratory system of a person inhaling the air and does harm to the person's body. The air which contains the ozone issuing from a varying ozone sources must be detoxified by removal of the ozone. As conventional techniques used for disposal of spent ozone, the method using activated carbon, the method using a liquid detergent, and the method resorting to thermal decomposition have been available. When the activated carbon method is utilized for the treatment of air containing ozone in a low concentration, the activated carbon must be replenished as it is consumed in consequence of progress of the decomposition of ozone . When this method is used for the treatment of air containing ozone in a high concentration, the activated carbon must be handled attentively because it has the possibility of being ignited and burnt by the heat of reaction. The liquid detergent method resides in purifying air containing spent ozone with the aqueous solution of a reducing substance. Thus, the treatment costs much and gives rise to a problem of waste water disposal. The thermal decomposition method has the disadvantage that it requires application of heat to a temperature of not less than 300°C for the purpose of enhancing the efficiency of decomposition, necessitates an expensive application of heat for the disposal of a large volume of waste gas, and encounters a high cost of treatment. In recent years, as one approach to the disposal of spent ozone. the method which resorts to catalytic decomposition has been the subject of researches. It is held that this method constitutes an advantageous way of removing ozone by decomposition at a low cost because it has no possibility of inducing ignition or explosion and obviates the necessity for waste water disposal. Regarding the decomposition of ozone, a catalyst using the oxides of nickel, manganese, cobalt, etc. is disclosed as exhibiting an outstanding ability to effect efficient decomposition of ozone in the specification of Japanese Patent Laid-Open SHO 60(1985)-97,049. For the purpose of practical adoption, however, the necessity for developing a catalyst exhibiting high activity in the range of much lower temperatures has been finding growing recognition. In recent years, the pollution of air with offensive odor has arisen as a serious social problem and has been urging development and adoption of new techniques for combatting the offensive odour. Heretofore, deodorization of foul air has been carried out by the method of washing with a detergent., the method of adsorption, the method of direct combustion, the method of catalytic combustion, the method of oxidation with ozone. etc. These methods invariably have both mertis and demerits of their own and have much to be desired for the purpose of practical adoption. The detergent method yields a large volume of waste water and incurs a large cost for the disposal of waste water. The adsorption method which mostly uses activated carbon as an adsorbent has the disadvantage that devices such as for replacement of activated carbon are difficult to maintain because the adsorbent is liable to catch fire and is quickly deprived of the deodorizing effect. The direct combustion method requires to use fuel and, therefore, entails a high running cost, demands a careful consideration on safety of operation, and suffers a great expense for a voluminous plant. In the case of the catalytic combustion method, though the plant can be maintained relatively easily, the temperature of the catalyst bed must be maintained in the range of 300° to 450°C. When the gas to be treated has a low temperature or the flammable substance is contained in a low concentration, therefore, this method suffers from the disadvantage that the running cost is inevitably high. The ozone oxidation method effects elimination of a component of offensive odour by making use of the powerful oxidizing action of ozone Since this method effects the treatment at low temperature in the neighborhood of normal room temperature, it enjoys a low running cost as compared with the various methods mentioned above. Since the reaction of ozone with the component of offensive odour in the gaseous phase proceeds slowly, this method necessitates adoption of a long and voluminous reactor. The method further suffers from the disadvantage that the unaltered portion of ozone is released into the atmosphere possibly to induce secondary air pollution. Two new methods have been proposed as means of overcoming the aforementioned drawbacks of the various conventional methods. The first method effects deodorization of a foul gas by the use of an apparatus provided with an ozone generator and an ozone decomposition filter (Japanese Patent Laid-Open SHO 61(1986)-29,358.) This method has no possibility of causing secondary air pollution because the unaltered portion of ozone is forcibly decomposed before it is releasted into the atmosphere. Since both the unaltered portion of ozone and the component of offensive odour are decomposed in the gas phase, the reactor to be used is required to possess a large capacity for the reason mentioned above. If the reactor has a small capacity, there ensues the disadvantage that no sufficient deodorizing effect is obtained because the foul gas under treatment passes the ozone decomposition filter before it is thoroughly deodorized. The second method resides in using a catalyst for the purpose of accelerating the reaction of ozone with the component of offensive odour thereby ensuring thorough oxidation of the component of offensive odour and, at the same time, effecting catalytic decomposition of the unaltered portion of ozone. As catalysts available for this method, a catalyst having a metal oxide deposited on a carrier made of a carbonaceous material (Japanese Patent Laid-Open SHO 54(1979)-119,371) and a catalyst having a metal oxide deposited on a carrier of activated alumina (Japanese Patent Laid-Open SHO 53(1978)-30,978) have been disclosed. In the case of the former catalyst, the carrier is consumed by the combustiton of carbon with ozone and the carrier possesses such a large adsorbing capacity as to adsorb the product of oxidation and, as an inevitable result, the catalyst suffers from rapid deterioration and fails to offer an ample service life. The latter catalyst cannot be expected to offer an ample service life because sulphur compounds (such as methyl mercaptan and hydrogen sulphide ) which are representative ingredients of the component of offensive odour are oxidized into SO₃ and this product of oxidation is deposited cumulatively on the active alumina of the carrier. As described in detail above, with the conventional methods, it is difficult to attain deodorization to a thorough extent and effect substantial elimination of the leakage of the unaltered ozone into the atmosphere. An object of this invention, therefore, is to provide a novel method for the purification of a gas and a catalyst to be used therefor. Another object of this invention is to provide, for catalytic decomposition of ozone contained in a gas into oxygen, an inexpensive ozone decomposition catalyst excellent in low-temperature activity and, for removal of the component of offensive odour of a gas by catalytic oxidative decomposition of the offensive odour component with ozone, a method for inexpensive deodorization capable of producing a stable and efficient deodorizing effect over a long period and substantially eliminating release of the unaltered portion of ozone into the atmosphere and a catalyst to be used therefor. Thus, component B may be an oxide of manganese, iron, cobalt, nickel and/or silver, or may be metallic platinum, palladium and/or rhodium. Component A may be an oxide of (a) titanium and (b) silicon and/or zirconium, preferably a TiO₂ -SiO₂ composite oxide. Optionally, 5 to 90% by weight of the component A in the catalyst may be substituted with an activated carbon. The catalyst of the present invention is such that the oxide of the component A thereof exhibits an outstanding ability to effect ozone decomposition and deodorization at low temperatures not exceeding 60 °C and the catalyst obtained by addition of the component B to the component A manifests high activity in the ozone decomposition and the deodorization at extremely low temperatures in the range of -10 to 25°C. A preferred catalyst contemplated by the present invention is characterized by using as a catalytic component thereof a binary composite oxide comprising titanium and silicon (hereinafter referred to as "TiO₂-SiO₂"), a binary composite oxide comprising titanium and zirconium (hereinafter referred to as "TiO₂-ZrO₂"), a binary composite oxide titanium and phosphorus comprising titanium and phosphorus (hereinafter referred to as "TiO₂-P₂O₅"), a ternary composite oxide comprising titanium, silicon, and zirconium (hereinafter referred to as "TiO₂-SiO₂-ZrO₂"), a ternary composite oxide comprising titanium, silicon, and phosphorus (hereinafter referred to as "TiO₂-SiO₂-P₂O₅"), a ternary composite oxide comprising titanium, zirconium, and phosphorus (hereinafter referred to as "TiO₂-ZrO₂-P₂O₅"), or a quaternary composite oxide comprising titanium, silicon, zirconium, and phosphorus (hereinafter referred to as "TiO₂-SiO₂-ZrO₂-P₂O₅")-(component A). Generally, the binary composite oxide comprising titanium, and silicon, from the report of Kozo Tabe "Catalyst," Vol. 17, No. 3, page 72 (1975), has been widely known as a solid acid. It exhibits conspicuous acidity now found in either of the component oxides thereof and possesses a large surface area. The TiO₂-SiO₂ is not a mere mixture of titanium dioxide with silicon dioxide but is a product which is inferred to manifest the peculiar physical attributes mentioned above because titanium, and silicon are combined to form the so-called binary type oxide. Further, the TiO₂-ZrO₂, TiO₂-P₂O₅, TiO₂-SiO₂-ZrO₂, TiO₂-SiO₂-P₂O₅, TiO₂-ZrO₂-P₂O₅, and TiO₂-SiO₂-ZrO₂-P₂O₅ are characterized as composite oxides possessing the same qualities as TiO₂-SiO₂. The composite oxides, on analysis by the X-ray diffraction, are found to possess an amorphous or substantially amorphous microstructure. The mechanism which is responsible for the outstanding activity the catalyst of this invention manifests in ozone decomposition and deodorization particularly at low temperatures has not been fully elucidated. It is, however, considered that the various properties of the composite oxides produce desirable effects on their activity in ozone decomposition and deodorization. It is further considered that the complex oxide, by addition thereto of any of such elements as manganese, iron, nickel, cobalt, silver, platinum, palladium, and rhodium or the compounds thereof, are enabled to manifest their activity in ozone decomposition more effectively. The TiO₂-SiO₂, TiO₂-ZrO₂, TiO₂-P₂O₅, TiO₂-SiO₂-ZrO₂, TiO₂-SiO₂-P₂O₅, TiO₂-ZrO₂-P₂O₅and TiO₂-SiO₂-ZrO₂-P₂O₅ one of which is selected to constitute the component A of the catalyst of this invention are desired to have a surface area exceeding 30 m²/g, prefereably falling in the range of 100 to 250 m²/g. The component A of the catalyst brings about better results when it has a percentage composition such that the TiO₂ accounts for a proportion in the range of 20 to 95 mol% and the SiO₂, ZrO₂ P₂O₅, or the sum of SiO₂ and ZrO₂, that of SiO₂ and P₂O₅, that of ZrO₂ and P₂O₅, or that of SiO₂, ZrO₂, and P₂O₅ accounts for a proportion in the range of 5 to 80 mol% (invariably based on the sum of TiO₂ + ZrO₂ + SiO₂ + P₂O₅ taken as 100 mol%), preferably the former oxide accounts for a proportion in the range of 30 to 90 mol% and the latter oxide a proportion in the range of 10 to 70 mol%. The catalyst of this invention includes the the range of 0 to 100 parts by weight of the component B, desirably 10 to 60 parts, where the element to be selected is manganese (Mn), silver (Ag). iron (Fe), cobalt (Co) or nickel (Ni) as an oxide, or in the range of 0 to 10 parts, desirably 0.2 to 5 parts where the element is platinum (Pt), palladium (Pd), or rhodium (Rh) as the metal, respectively based on 100 parts of the component A as oxide. From the point of activity in ozone decomposition and durability of the catalyst, component B preferably includes manganese oxide, more preferably β type manganese oxide, or it is preferably used palladium. The objects described above are accomplished by a catalyst for the purification of an ozone-containing gas, comprising as catalytic components, a component A being at least one composite oxide selected from the group consisting of TiO₂-SiO₂, TiO₂-ZrO₂, TiO₂-P₂O₅, TiO₂-SiO₂-ZrO₂, TiO₂-SiO₂-P₂O₅, TiO₂-ZrO₂-P₂O₅, and TiO₂-SiO₂-ZrO₂-P₂O₅, and a component B composed of at least one element selected from the group consisting of manganese, iron, cobalt, nickel, silver, platinum, palladium, and rhodium, wherein the amount of component B is a proportion in the range of 0 to 150 parts by weight as an oxide where the element selected is manganese, iron, cobalt, nickel or silver, or in the range of 0 to 10 parts by weight as the metal where the element selected is platinum, palladium or rhodium, the portions respectively being based on 100 parts by weight of component A as oxide. The objects are also accomplished by passing an ozone-containing gas through a bed of the catalyst. These objects are further accomplished by continuously adding ozone to a gas containing a component of offensive odour and passing the resulting mixed gas through a bed of the catalyst. In the removal of a component of offensive odour from a gas containing the offensive odour component by introduction of ozone into the gas and consequent decomposition of the offensive odour component, the objects mentioned above are accomplished by setting up a catalyst bed in a path for the flow of the gas and intermittently introducing ozone into the gas flowing through the catalyst bed. In accordance with this invention, the catalyst bed brings about desirable results when the above catalyst is used. The catalyst is suitable for use in the decomposition of ozone and for the removal of - a component of offensive odour from a gas, and is preferably in the form of honeycombs or pellets. If the proportion of the component B falls outside the range mentioned above, the activity of the catalyst manifested in ozone decomposition and deodorization is not sufficient and where the element to be selected is platinum, palladium, or rhodium, cost of raw materials increases, so sufficient effect cannot be obtained. In the preparation of the TiO₂-SiO₂ or use in the present invention, the titanium source may be selected from among inorganic titanium compounds such as titanium chloride and titanium sulfate and organic titanium compounds such as titanium oxalate and tetraisopropyl titanate and the silicon source from among inorganic silicon compounds such as colloidal silica, water glass, and silicon tetrachloride and organic silicon compounds such as tetraaethyl silicate. Some of the raw materials enumerated above contain a minute amount of extraneous substance. The inclusion of the extraneous substance does not matter very much so long as it has no appreciable effect upon the qualities of the TiO₂-SiO₂. Preferably, the preparation of the TiO₂-SiO₂ is attained by any of the following methods. 1 A method which comprises mixing titanium tetrachloride with silica sol, adding ammonia to the resulting mixture thereby inducing precipitation, separating and washing the resulting precipitate, drying the washed precipitate, and calcining the dry precipitate at a temperature in the range 350° to 650°C, preferably 300° to 600°C. 2 A method which comprises adding an aqueous sodium silicate solution to titanium tetrachloride, causing them to react with each other and give rise to a precipitate separating and washing the precipitate, drying the washed precipitate, and calcining the dry precipitate at a temperature in the range of 300° to 650°C. preferably 350° to 600°C. 3 A method which comprises adding ethyl silicate [(C₂H₅O)₄Si] to a water-alcohol solution of titanium tetrachloride thereby causing hydrolysis and consequent precipitation, separating and washing the resulting precipitate, drying the washed precipitate, and calcining the dry precipitate at a temperature in the range of 300° to 650°C, preferably 350° to 600°C. 4 A method which comprises adding ammonia to a water-alcohol solution of titanium oxygen chloride (TiOCl₂) and ethyl silicate thereby giving rise to a precipitate, separating and washing the precipitate, drying the washed precipitate, and calcining the dry precipitate at a temperature in the range of 300° to 650°C, preferably 350 to 600°C. Among in the preferred methods cited above, the method of (1) proves to be particularly desirable. Specifically, this method is carried out as follows: Compounds selected severally from the groups of typical examples of the titanium source and the silicon source are weighed out in amounts to form a composite oxide consisting of TiO₂ and SiO₂ in a prescribed ratio, mixed in the form of an acidic aqueous solution or as a sol containing titanium and silicon in a concentration in the range of 1 to 100 g/liter, preferably 10 to 80g/liter as oxide, and then held at a temperature in the range of 10° to 100°C. The solution or so is kept stirred, with aqua ammonia added dropwise thereto meanwhile as a neutralizing agent, for a period of 10 minutes to three hours until a coprecipitate composed of titanium and silicon is formed at a pH in the range of 2 to 10. This coprecipitate is separated by filtration, thoroughly washed, then dried at a temperature in the range of 80° to 140°C for a period of 1 to 10 hours, and calined at a temperature in the range of 300° to 650°C, preferably 350° to 600°C for a period of one to 10 hours, pereferably 2 to 8 hours, to give birth to TiO₂-SiO₂. The TiO₂-ZrO₂-SiO₂ is prepared by the same method as used for the preparation of the TiO₂-SiO₂. In this case, the zirconium source may be selected from among inorganic zirconium compounds such as zirconium chloride and zirconium sulfate and organic zirconium compounds such as zirconium oxalate. Specifically, by handling a zirconium compound and a titanium compound suitably selected by the same method as described above, there can be easily prepared the TiO₂-ZrO₂-SiO₂. The amount of zirconium to be present in this ternary composite oxide is desired to be not more than 30% by weight as ZrO₂, based on the total amount of the TiO₂ + ZrO₂ + SiO₂. The preparation of the TiO₂-ZrO₂ can be carried out in the same manner as described above. For the preparation of the TiO₂-P₂O₅, the titanium source may be selected from among inorganic titanium compounds such as titanium chloride and titanium sulfate and organic titanium compounds such as titanium oxalate and tetraisopropyl titanate and the phosphorus source from among phosphorus compounds such as ammonium phosphate, phosphoric acid, and phosphorus pentoxide. Some of the raw materials enumerated above contain a minute amount of extraneous substance. The inclusion of the extraneous substance does not matter very much so long as it has no appreciable effect upon the qualities of the TiO₂-P₂O₅. Desirably, the preparation of the TiO₂-P₂O₅ is carried out as follows. Compounds selected severally from the aforementioned groups of typical examples of the titanium source and the phosphorus source are weighted out in amounts to form a composite oxide consisting of TiO₂ and P₂O₅ in a prescribed ratio, stirred to give a mixture containing titanium and phosphorus in a concentration in the range of 1 to 100 g/liter, preferabaly 10 to 80 g/liter as oxide, and left aging at a temperature in the range of 10° to 100°C thereby giving rise to a precipitate. The precipitate is separated by filtration, thoroughly washed, then, dried at a temperature in the range of 80° to 200°C, for one to 10 hours, and calcined at a temperature in the range of 300° to 800°C, preferably 350° to 600°C, for one to 10 hours, preferably 2 to 8 hours, to give birth to TiO₂-P₂O₅ The TiO₂-SiO₂-P₂O₅, TiO₂-ZrO₂-P₂O₅, and TiO₂-SiO₂-ZrO₂-P₂O₅ can be prepared by adopting the same method as described above. From the TiO₂-SiO₂, TiO₂-ZrO₂, TiO₂-P₂O₅, TiO₂-SiO₂-ZrO₂, TiO₂-SiO₂-ZrO₂, TiO₂-ZrO₂-P₂O₅, or TiO₂-SiO₂-ZrO₂-P₂O₅, a final catalyst can be obtained by the following method. For example, the catalyst is obtained by mixing TiO₂-SiO₂ with a molding aid, kneading the resulting mixture with a suitable amount of water. molding the resulting blend in the form of pellets or a honeycomb, with an extrusion molder, drying the molded article at a temperature in the range of 50° to 120°C, and thereafter calcining the dry molded article at a temperature in the range of 300° to 800°C, preferably 350° to 600°C, for one to 10 hours, preferably 2 to 6 hours under a current of air. Optionally, 5 to 90% by weight, preferably 10 to 60% by weight, of the aforementioned component A may be substituted with activated carbon for the purpose of enabling the catalyst of this invention to manifests the activity in deodorization and ozone decomposition to a greater extent. For this substitution, the activated carbon generally in use to date can be employed. It may be used in a chemically or physically modified form. In the catalyst of this invention produced as described above, the component A is desired to account for a proportion in the range of 95 to 100% by weight and the activated carbon for a proportion in the range of 5 to 90% by weight. If the proportion of the activated carbon is less than 5% by weight, the ability of the catalyst to deodorize is not sufficient. If this proportion exceeds 90% by weight, the catalyst fails to effect ample removal of such basic component of offensive odor such as ammonia and possesses insufficient physical strength in withstanding various impacts exerted threreon during actual use thereof. From the component A, i.e. the TiO₂-SiO₂, TiO₂-ZrO₂, TiO₂-SiO₂-ZrO₂, etc. prepared as described above, a final deodorant can be obtained by the following method. For example, the deodorant is produced by thoroughly mixing TiO₂-SiO₂ powder with activated carbon optionally further with a molding aid, blending the resulting mixture with a suitable amount of water, molding the resulting blend in a desired shape, then drying the shaped blend, and calcining the dry shaped blend when necesarry. Though the activated carbon is generally used in the form of powder, it may be used partly in the form of short fibers. The molding can be effected by any of the various known methods represented by compression molding and extrusion molding. The drying of the shaped composite is effected at a temperature in the range of 50° to 200°C and the calcining of the dry shaped composite is desirably carried out in a non-oxidizing atmosphere because the shaped composite contains a flammable activated carbon. When the flammable subtance is contained in a low concentration, this calcination may be carried out in the air. The calcination is performed at a temperature in the range of 200° to 600°C, preferably 200° to 400°C, for a period of 1 to 10 hours, preferably 2 to 8 hours. When the calcination is not required, it can be omitted rather advantageously. Though the calcination performed at high temperatures results in improvement of the strength of the shaped composite, it has the possibility of decreasing the specific surface area of the deodorant and lowering the deodorizing ability thereof. The catalyst of the present invention which comprises the component A and the activated carbon may additionally incorporate therein a carrier or some other known deodorant. The conversion of the TiO₂-SiO₂ to a final catalyst by the addition thereto of manganese, iron, nickel, cobalt, silver, platinum, palladium, or rhodium is effected by impregnating a shaped article of TiO₂-SiO₂ with an aqueous solution of the salt of the metal, drying the impregnated shaped article, and calcining the dry shaped article. Alternatively, this conversion may be accomplished by adding the aqueous solution of metal salt in conjunction with a molding aid to the TiO₂-SiO₂ powder, kneading them, and molding the resulting blend. Further, the catalyst of this invention permits use of a carrier. Examples of the material usable for the carrier are alumina, silica, silica-alumina, bentonite, diatomaceous earth, silicon carbide. titania, zirconia, magnesia, cordierite, mullite, pumice, activated carbon, and inorganic fibers. The combination of the catalyst with the carrier can be effected, for example, by preparing a slurry comprising the TiO₂-SiO₂ and other components of the catalyst and impregnating granular silicon carbide with the slurry thereby depositing the catalyst on the carrier. These are not the only methods available for the production of the catalyst of this invention. The conceivable shapes of the catalyst include not only the pellets and the honeycomb mentioned above but also cylinder, tube, plate, ribbons, corrugated sheet, pipe, doughnut, lattice, and integral mass. Among thereof it is preferred to use the honeycomb catalyst having a nominal diameter of penetration pore in the range of 0.7 to 3mm, wall thickness of cells is in the range of 0.2 to 0.5mm, and aperture ratio thereof is not less than 50%, preferably in the range of 50 to 80%. In case of using a deodorizating catalyst, ozone decomposition is also often limitted in setting up place. Therefore, the reactor for catalyst is required to be small one. In any case it is further required to avoid choking a bed of catalyst by dust containing treated gas, or loss of pressure and to maintain a high activity of the catalyst. All of these requirement is satisfied by using honeycomb catalyst above-mentioned. If the nominal diameter of penetration pore of catalyst is less than 0.7mm, at the same time of increasing the loss of pressure, choking the bed of catalyst intends to be occured. If the diameter is above 3mm, it is not preferable to cause decreasing a ratio of ozone decomposition or deodorization on account of decreasing a geometric surface area. It is the same reason why the aperture ratio is required to be more than 50%. The starting material for the component B which is used in combination with the component A in the catalyst of the present invention can be suitably selected from among oxides, hydroxides, inorganic acid salts, and organic acid salts, particularly ammonium salts, oxalates, nitrates, sulfates, and halogenates. In the ozone-containing gas to be effectively treated by the catalyst of the present invention, the ozone concentration is roughly in the range of 0.01 to 10,000 ppm, though not critically. Even when other binary through quaternary composite oxide is used as the component A, the deposition of the component B on a carrier is effected in the same manner as the TiO₂-SiO₂ composite oxide. The deodorizing catalyst contemplated by the present invention can be used for the treatment of any of various foul gases emanating from food storages, garbage dumps, septic tanks, sewage disposal plants, trash incinerators, cleaning shops, printing shops, painting shops, and chemical plants in general. As examples of the component of offensive odor, there can be cited hydrogen sulfide, methyl sulfide, methyl mercaptan, methyl disulfide, ammonia, methylamine, dimethylamine, trimethylamine, ethylamine, diethylamine, triethylamine, isobutylamine, pyridine, acetone, methylethyl ketone, butyric acid, acetaldehyde, acrolein, phenol, benzene, xylene, toluene, and butenes. Gases containing these substances can be substantially completely deodorized by the method of this invention. In the ozone-containing gas to be effectively treated by the catalyst of the present inveniton, the ozone concentraton is roughly in the range of 0.01 to 10,000 ppm, though not critically. The ozone decomposing agent of the present invention can be used for both gases and aqueous solutions containing ozone. The use of this agent is generally accomplished by passing a gas or solution under treatment through a bed packed with the ozone decomposing agent. The space velocity of the gas or solution for this passage generally falls in the range of 1,000 to 100,000 hr ¹ , preferably 3,000 to 50,000 hr ¹ . The method which uses packed beds of the ozone decomposition agent of this invention and packed beds of the conventional ozone decomposing agent in a multistage system brings about highly desirable results. When a bed of activated carbon is used for the removal of ozone from a waste gas containing ozone in a high concentration, for example, the operation is hardly feasible because the bed may possibly encounter ignition and explosion and undergo heavy pulverization. When a bed packed with the ozone decomposing agent of the present invention is set up on the upstream side of the path for the flow of the waste gas under treatment, the system enables the ozone concentration of the waste gas to be lowered in the former bed and permits the remaining ozone in the gas to be further removed in the latter ctivated carbon catalyst bed. The deodorization of a foul gas by the use of the catalyst of this invention is accomplished by a method which comprises continuously introducing ozone at a prescribed rate into the foul gas containing a component of offensive odor and passing the resulting mixed gas over a bed of the catalyst set up on the downstream side in the path for the flow of the gas under treatment thereby effecting catalytic removal of the component of offensive odor from the gas under treatmnet. The concentration of the ozone introduced as described above into the foul gas is determined by the attributes and concentration of the component of offensive odor in the gas, other reaction conditions such as, for example, the reaction temperature, the kind of the catalyst, and the amount of the catalyst. This concentration is desired to fall in the range of 0.5 to 1,000 mols, preferably 1 to 10 mols, per mol of the component of offensive odor. The reaction temperature is in the range of -10° to 400°C, preferably 0° to 300°C. The space velocity is in the range of 1,000 to 100,000 hr ¹ , prefarably 3,000 to 50,000 hr⁻¹ . Alternatively the deodorization of a foul gas by the present invention may be attained by a method which enables the deodorizing effect to be maintained for a long period by alternately repeating the first step of deodorizing the foul gas by catching the bed of catalyst having component of offensive odor from the gas through the phenomenon of adsorption and the second step of intermittently introducing ozone into the degenerated bed of catalyst thereby decomposing the adsorbate and regenrating the bed of catalyst. The salient feature of this method resides in the fact that the introduction of ozone into the foul gas in motion of the purpose of regenerating the degenerated adsorbent can be effected without interrupting the flow of the gas under treatment. The ozone thus introduced fulfils the role of removing the component of offensive odor from the gas under treatment and, at the same time, removing the adsorbate from the bed of catalyst by decomposition. Unlike the conventional method for effecting deodorization by adsorption, the method under discussion is not required to operate alternately two columns of adsorbent beds, one for the treatment of adsorption and the other for the treatment of desorption and regeneration. For this method, it suffices to use only one column to effect simultaneously the treatments of adsorption and regeneration. The conditions for the adsorption and regeneration are suitably selected, depending on the composition of the gas under treatment and the concentration of the component of offensive odor. They can be found by a simple test. For example, the space velocity of the gas relative to the adsorbent is desirably fixed in the range of 100 to 1000 hr ¹ and the concentration of ozone during the introduction thereof for regeneration in the range of 1 to 100 ppm. When the ozone concentration is lower than the range just mentioned, the regeneration is obtained with poor efficiency. When the ozone concentration is higher than the range though the regeneration proceeds quickly, the unaltered portion of ozone leaks into the ambient air and possibly induces secondary air pollution. The intermissions and the durations of the intermittent introduction of ozone are desired to be fixed each in the range of 30 minutes to 12 hours, per a period of of roughly one to 24 hours. The intermittent introduction of ozone can be easily effected by programming the pattern of intermission in advance and combining an ozone generator and a timer in accordance with the programmed pattern. Now, the present invention will be described more specifically below with reference to working examples. It should be noted, however, that this invention is not limited to these examples. The "ozone decomposition ratio" mentioned in the working examples was calculated by the following formula. The "deodorization ratio" similarly mentioned was calculated by the following formula. Example 1 A composite oxide comprising titanium and silicon was prepared as follows. An aqueous sulfuric acid solution of titanyl sulfate having the following composition was used as a titanium source. TiOSO₄ (as TiO₂) 250 g liter Total H₂SO₄ 1,100 g/liter Separately, 28 liters of aqueous ammonia (NH₃, 25%) was added to 40 liters of water and 2.4 kg of Snowtex-NCS-30 (silica sol containing about 30% by weight of silica as SiO₂; product of Nissan Chemicals Industries Ltd.) was added further thereto. To the resulting solution, a titanium-containing aqueous sulfuric acid solution prepared by diluting 15.3 liters of the aqueous sulfuric acid solution of titanyl sulfate with 30 liters of water was gradually added dropwise while under agitation to give rise to a coprecipitate gel. The resulting reaction mixture was left standing at rest for 15 hours. The TiO₂-SiO₂ gel thus obtained was separated by filtration, washed with water, and then dried at 200°C for 10 hours. The dry TiO₂-SiO₂ gel was calcined under an atmosphere of air at 550°C for six hours. The powder thus obtained had a composition of TiO₂:SiO₂ = 4:1 (molar ratio) and a BET surface area of 185m²/g. The powder which will be referred to hereinafter as TS-1 was used to prepare an ozone decomposition catalyst as follows. In a kneader, 1.0 kg of the TS-1 powder was thoroughly mixed with 20 g of microcrystalline cellulose (produced by Asahi Chemical Industry Co., Ltd. and marketed under trademark designation of "Avicel") and a suitable amount of water. The resulting mixture was molded in the form of pellets 3.0 mm in diameter and 3.0 mm in length with an extrusion molding machine. The pellets were dried at 100°C for 10 hours and then calcined under an atmosphere of air at 500°C for six hours. Consequently, there was obtained a catalyst of formed TiO₂-SiO₂. Example 2 TiO₂-ZrO₂ was prepared as follows. In 100 liters of cold water, 1.93 kg of zirconium oxychloride (ZrOCl₂ 8H₂O) was dissolved. In the resulting solution, 7.8 liters of an aqueous sulfuric acid solution of titanyl sulfate having the same composition as used in Example 1 was added and thoroughly mixed. The mixture thus formed was kept amply stirred at a temperature of about 30°C and aqua ammonia was gradually added thereto until the pH reached 7. The resulting reaction mixture was left standing at rest for 15 hours. The TiO₂-ZrO₂ gel thus obtained was separated by filtration, washed with cold water, and then dried at 200°C for 10 hours. Then, the dry gel was calcined under an atmosphere of air at 550°C for six hours. The powder consequently obtained had a composition of TiO₂:ZrO₂ = 4:1 (molar ratio) and a BET surface area of 140 m²/g. The powder thus obtained will be referred to hereinafter as TZ-1. By using this TZ-1 and following the procedure of Example 1, there was obtained a catalyst formed of TiO₂-ZrO₂. Example 3 TiO₂-SiO₂-ZrO₂ was preapred by following the procedures of Examples 1 and 2. The powder consequently obtained had a composition of TiO₂ : SiO₂ : ZrO₂ = 80 : 16 : 4 (molar ratio) and a BET surface area of 180m²/g. The powder thus obtained will be referred to hereinafter as TSZ-1. By using this TSZ-1 and following the procedure of Example 1, there was obtained a catlyst formed of TiO₂-SiO₂-ZrO₂. Examples 4-6 Catalysts formed of TiO₂-SiO₂ were prepared by following the procedure of Example 1, excepting the molar ratio of TiO₂/SiO₂ was varied. The compositions and BET surface areas of the catalysts thus obtained were as shown in Table 1. Control 1 A TiO₂ powder was prepared by following the procedure of Example 1, excepting use of silica sol was omitted. The TiO₂ powder thus obtained had a BET surface area of 60 m²/g. By using this powder and following the procedure of Example 1, there was obtained a catalyst formed solely of TiO₂. Control 2 A powder solely of SiO₂ containing no titanium was prepared by following the procedure of Example 1. The powder thus obtained had a surface are of 250 m²/g. By using this powder and following the procedure of Example 1, there was obtained a catalyst formed solely of SiO₂. Control 3 A TiO₂ powder and a SiO₂ powder obtained by following the procedures of Controls 1 and 2 were weighed out in amounts calculated to give a molar ratio of TiO₂/SiO₂ = 4 and thoroughly mixed. The mixed powder consequently obtained had a BET surface area of 90 m²/g. By following the procedure of Example 1, there was obtained a catalyst formed of the mixed powder. Example 7 The catalyts obtained in Examples 1-6 and Controls 1-3 were tested for ozone decomposition ratio as follows. In a reaction tube made of Pyrex glass and having an inner diameter of 20 mm, 10.5 cc of pellets of catalyst 3.0 mm in diameter and 3.0 mm in length were packed. Air containing 10 ppm of ozone was introduced to the bed of catalyst at a flow rate of 0.21 Nm³/hr (space velocity 20,000 hr ¹ ) with the reaction temperature varied in the range of 20° to 100°C, to find the ozone decomposition ratio. The results were as shown in Table 2. Example 8 In a kneader, 1.0 kg of the same TS-1 powder as used in Example 1 and an aqueous solution containing 0.366 kg of manganese nitrate, Mn(NO₃)₂ 6H₂O, added thereto were thoroughly kneaded, with a suitable amount of water added thereto. By following the procedure of Example 1, the resulting mixture was molded in the form of pellets and the pellets were dried and calcined. Consequently, there was obtained a catalyst having a composition of TS-1 : MnO₂ = 90 : 10 by weight ratio as oxide. As the result of X ray diffraction, manganese obtained was structed type manganese. This catalyst was tested for ozone decomposition capacity by following the procedure of Example 7. The reuslts were as shown in Table 3. Examples 9-12 Catalysts were prepared by using the same TS-1 powder as used in Example 1 and following the procedure of Example 8, excepting the component for addition to the component A was varied. As catalyst sources, nitrates of iron, cobalt, nickel, and silver were respectively used. The catalysts were tested for ozone decomposition capactiy by following the procedure of Example 7. The catalyst compositions and the results of the test were as shown in Table 3. Example 13 In an evaporation dish, 500 cc of the catalyst (pellets 3 mm in diameter and 3 mm in length ) formed of TiO₂-SiO₂ obtained in Example 1 and 140 ml of an aqueous platinum nitrate solution containing 3.5 g of platinum (Pt) were thoroughly mixed for impregnation of the catalyst with the solution. Over a water bath, the impregnated catalyst was dried at 120°C for five hours. Then, the dry catalyst was calcined in an electric oven at 400°C for three hours. The catalyst thus obtained was tested for ozone decomposition capacity by following the procedure of Example 7. The results were as shown in Table. 3. Examples 14-15 Catalysts were prepared by following the procedure of Example 13, excepting palladium and rhodium were respectively used in the place of platinum. These catalysts were tested for ozone decomposition catalyst by following the procedure of Example 7 The catalyst compositions and the results of the test were as shown in Table 3. It is noted from the results of Tables 2 and 3 that the catalysts of this invention provide highly efficient decomposition of ozone at low temperatures not exceeding 50°C, particularly at temperatures approximating to normal room temperature. TiO₂/SiO₂ catalyst TiO₂/SiO₂ (molar ratio) Specific area (m²/g) Example 4 9 175 Example 1 4 185 Example 5 1 230 Example 6 0.42 210 Example 16 A compoisite oxide comprising titanium and phosphorus was prepared as follows. An aqueous sulfuric acid solution of titanyl sulfate having the following composition was used as a titanium source. TiOSO₄ (as TiO₂) 250 g/liter Total H₂SO₄ 1,100 g/liter A titanium-containing aqueous sulfuric acid solution prepared by diluting 10 liters of the aqueous sulfuric acid solution of titanyl sulfate with 50 liters of cold water was kept at 40°C and, while under thorough agitation, 40 liters of an aqueous solution containing 4.13 kg of diammonium hydrogen phosphate was gradually added dropwise thereto, to give rise to a precipitate. The resulting reaction mixture was left standing at rest at 80°C for six hours. The TiO₂-P₂O₅ gel consequently obtained was separated by filtration, washed with cold water, and then dried at 150°C for 10 hours. Subsequently, the dry gel was calcined under an atmosphere of air at 550°C for six horus. The powder consequently obtained had a composition of TiO₂ : P₂O₅ = 2 : 1 (molar ratio) and a BET surface area of 70 m²/g. This powder will be referred to hereinafter as TPI and was used to prepare an ozone decomposition catalyst as follows. In a kneader, 1.0 kg of the TP-1 powder and 20 g of microcrystalline cellulose (produced by Asahi Chemical Industry Co., Ltd. and marketed under trademark designation of "Avicel") added thereto were thoroughly mixed, with a suitable amount of water added therto. The reuslting mixture was molded in the form of pellets 3.0 mm in diameter and 3.0 mm in length with an extrusion molder. The pellets were dried at 100°C for 10 horus and then calcined under an atmosphere of air at 500°C for six hours. Consequently, there was obtained a catalyst formed of TiO₂-P₂O₅. Example 17-19 Catalysts formed of TiO₂-P₂O₅ were prepared by following the procedure of Example 1, excepting the molar ratio of TiO₂-P₂O₅ was varied. The compositions and the BET surface areas of the catalysts obtained were as shown in Table 4. Exmaple 20 The catalysts obtained in Examples 16-19 and Control 1 were tested for ozone decomposition ratio as follows. In a reaction tube made of Pyrex glass and having an inner diameter of 20mm, 10.5 cc of pellets of catalyst 3.0 in diameter and 3.0 mm in length were packed. Air containing 10 ppm of ozone was introduced to the catalyst bed at a flow rate of 0.21 Nm³hr (space velocity 20,000 hr ¹), with the reaction temperature varied in the range of 25° to 100°C, to find the ozone decomposition ratio. The results were as shown in Table 5. Example 21 In a kneader, 1.0 kg of the same TP-1 powder as used in Example 16 and an aqueous solution containing 0.366 kg of manganese nitrate, Mn(NO₃)₂·6H₂O added thereto were thoroughly mixed, with a suitable amount of water added thereto. By following the procedure Example 16, the resulting mixtrue was molded in the form of pellets and the pellets were dried and calcined. Consequently, there was obtained a catalyst having the composition of TP-1 : MnO₂ = 90 : 10 by weight ratio as oxide. The catalyst was tested for ozone decomposition capacity by following the procedure of Example 20. The results were as shown in Table 6. Examples 22-25 Catalysts were prepared by using the same TP-1 powder as used in Example 16 and following the procedure of Example 21, excepting the component for addition to the component A was varied. As catalyst sources, nitrates of iron, cobalt, nickel, and silver were respectively used. The catalysts were tested for ozone decomposition capacity by following the procedure of Example 20. The catalyst compositions and the results of the test were as shown in Table 6. Example 26 In an evaporation dish, 500 cc of the catalyst (pellets 3 mm indiameter and 3 mm in length) formed of TiO₂-P₂O₅ obtained in Example 16 and 140 ml of an aqueous platinum nitrate solution containing 3.5 g of platinum (Pt) were thoroughly mixed to effect impregnation of the catalyst with the solution. Over a water bath, the impregnated catalyst was dried at 120°C for five hours. Then, the dry impregnated catalyst was calcined under an atmosphere of air at 400°C for three hours. The catalyst consequently obtained had a composition of TP-1 : Pt = 99 : 1:0 (weight ratio). This catalyst was tested for ozone decomposition capacity by following the procedrue of Example 20. The resutls were as shown in Table 6. Example 27-28 Catalysts were prepared by following the procedure of Example 26, excepting palladium and rhodium were respectively used in the place of platinum. The catalysts were tested for ozone decomposition capacity by following the procedure of Example 20. The catalyst compositions and the results of the test were as shown in Table 6. It is noted from the data of Tables 5 and 6 that the catalysts of the present invention provide highly efficient decomposition of ozone at low temperatures not exceeding 60°C, particularly at low temperature approximating to normal room temperatrue. Example 29 In a kneader, 10 kg of the TS-1 powder obtained in Example 1 and a suitable amount of water added thereto were thoroughly mixed. The resulting mixtrue was thoroughly blended in a blender. The homogeneous mixture consequently obtained was molded in the form of latticshaped honeycombs having visible dimensions of 50 mm in length, 50 mm in width, and 100 mm in length (0.3 mm in wall thickness and 1.4 mm in mesh) with an extrusion molder. the honeycombs were dried at 150°C for five hours and then calcined under an atmosphere of air at 300°C for two hours. Consequently, there was obtained a deodorizing catalyst formed of TS-1H. Example 30 A catalyst formed of TZ-1H was prepared by using the TZ-1 obtained in Example 2 and following the procedure of Example 29. Example 31 A catalyst formed of TSZ-1H was prepared by using the TSZ-1 obtained in Example 3 and following the procedure of Example 29. Examples 32-34 Catalysts formed of TiO₂-SiO₂ were prepared by following the procedrue of Example 29, excepting the molar ratio of TiO₂/SiO₂ varied. The compositions and the BET surface areas of the catalysts thus obtained were as shown in Table 7. Example 35 The catalysts obtained in Examples 29-34 were tested for deodorization ratio as follows. In a reaction tube made of Pyrex glass, 250 ml of latticelike honeycombs of catalyst were packed. Steam-saturated air containing 5 ppm of trimethylamine or methyl mercaptan as a typical component of offensive odor was introduced to the catalyst bed at a flow rate of 5 Nm³/hr (space velocity of 20,000 hr ¹). Ozone was introduced in a concentration of 20 ppm to the inlet side of the catalyst bed, with the reaction temperature at 5°C. After 500 hours' use of the catalyst bed required for stabilization of the catalyst activity, the catalyst was tested for deodorization ratio. The results were as shown in Table 8. Example 36 A catalyst having a composition of TS-1 : MnO₂ = 90 : 10 by weight ratio as oxide was obtained by impregnating the latticelike honeycombs of TS-1H of Example 29 with an aqueous manganese nitrate solution, drying the impregnated honeycombs, and calcining the dry honeycombs. This catalyst was tested for deodorization capacity by following the procedure of Example 35. The results were as shown in Table 9. The ozone concentration in the outlet gas was less than 0.1 ppm. Example 37-43 Catalysts were prepared by following the procedure of Example 36, excepting the component for addition to the component A was varied. As catalyst sources, nitrates of iron, cobalt, nickel, silver, and platinum, and chlorides of palladium and rhodium were used. The catalysts were tested for deodorization capacity by following the procedure of Example 35. The compositions of the catalysts and the results of the test were as shown in Table 9. The ozone concentrations in the outlet gases were invariably less than 0.1 ppm. Controls 4-5 Catalysts were prepared by following the procedure of Example 36, excepting lattice-like honeycombs of activated alumina and lattice-like honeycombs of activated carbon were used in the place of TS-1H. The catalysts were tested for deodorization capacity by following the procedrue of Example 35. The compositions of the catalysts and the results of the test were as shown in Table 9. As shown in Table 8 and Table 9, the catalysts of the present invention permit deodorization to be effected with high efficiency at such a low temperature as 5°C. Example 44 In a kneader, 750 g of the TS-1 powder obtained in Example 1 and 250 g of a commercially available activated carbon were thoroughly mixed, with a suitable amount of water added thereto. The resulting mixture was thorgouhly blended in a blender. The homogeneous mixture consequently obtained was molded in the form of pellets 5.0 mm in diameter and 6.0 mm in length with an extrusion molder. The pellets were dried at 150°C for two hours. Consequently there was obtained an ozone decomposing agent formed of TiO₂-SiO₂ Example 45 An ozone decomposing agent formed of TiO₂-ZrO₂-C was prepared by using the TZ-1 obtained in Example 2 and following the procedure of Example 44. Example 46 An ozone decomposing agent formed of TiO₂-SiO₂-ZrO₂-C was prepared by using the TSZ-1 obtained in Example 3 and following the procedrue of Example 44. Example 47-49 Ozone decomposing agents formed of TiO₂-SiO₂-C were prepared by following the procedure of Example 44, excepting the weight ratio of TiO₂-SiO₂d the activated carbon was varied. The compositions of the ozone decomposing agents consequently obtained were as shown in Table 10. Control 6 An ozone decomposing agent formd solely of activated carbon was prepared by following the procedure of Exmaple 44, excepting granular activated carbon was used in the place of the TS-1 powder. Example 50 The ozone decomposing agents obtained in Examples 44-49 and Control 6 were tested for ozone decomposition capacity as follows. In a reaction tube made of Pyrex glass and having an inner diameter of 38 mm, 200 ml of pellets of the agent 5.0 mm in diameter and 6.0 mm in length were packed. Air containing 2,000 ppm of ozone and 2% of steam was introduced to the catalyst bed at a flow rate of 0.40 Nm³/hr (space velocity 2,000 hr ¹ ) at a reaction temperature of 20°C. The gas emanating from the catalyst bed was tested for ozone concentration. The results obtained after 100 hours' passage of the gas through the catalyst bed were as shown in Table 11. Example 51 In a kneader, 10 kg of the TS-1 powder obtained in Example 1 and 10 kg of commercially available activated carbon were thoroughly mixed, with a suitable water added thereto. The resulting mixture was thoroughly blended in a blender. The homogeneous mixture consequently obtained was molded in the form of lattice-like honeycombs having visible dimensions of 50 mm in length. 50 mm in width, and 20 mm in depth (0.7 mm in wall thickness and 3.0 mm in mesh) with an extrusion molder. The honeycombs were dried at 150°C for five hours and then calcined under an atmosphere of air at 300°C for two hours. Consequently, there was obtained a deodorant formed of TiO₂-SiO₂-C. Example 52 A deodorant formed of TiO₂-ZrO₂-C was prepared by using the TZ-1 obtained in Example 2 and following the procedure of Example 51. Example 53 A deodorant formed of TiO₂-SiO₂-ZrO₂-C was prepared by using the TSZ-1 obtained in Example 3 and following the procedrue of Example 51. Example 54-56 Deodorants formed of TiO₂-SiO₂-C were prepared by following the procedure of Exmaple 51, excepting the weight ratio of the TiO₂-SiO₂ and the activated carbon was varied. The compositions of the deodoratns consequently obtained were as shown in Table 12. Control 7 A deodorant formed solely of activated carbon was preapred by following the procedrue of Example 51, excepting powdered activated carbon was used in the place of the TS-1 powder. Example 57 The various deodorants obtained in Example 51-56 and Control 7 were tested for capacity for deodorization of a foul gas as follows. A deodorant was placed in a container having an inner volume of 2 liters. Air (20°C) containing 300 ppm of ammonia or hydrogen sulfide was introduced to the deodorant. The deodorant covered with the air was left standing at rest. At intervals of 30 minutes, 60 minutes, and 90 minutes, the air was tested for residual ammonia or hydrogen sulfide concentration to determine deodorization ratio. The results of the test were as shown in Table 13. Example 58 The various deodorants obtained in Examples 51, 54, 55, and 56 and Control 7 were tested for crush strength with an Instron tester. The results were as shown in Table 14. Example 59 A tube made of Pyrex glass was packed with the lattice-like honeycombs of catalyst TS-1H obtained in Example 29 so as to preclude the incoming gas from finding a short path. Air containing 5 ppm of trimethylamine as a typical component of offensive odor was continuously introduced at a flow rate of 2.5 Nm³/hr to the catalyst bed at 25°C. After 10 hours' use of the catalyst bed, the gas at the outlet of the catalyst bed was analyzed to determine trimethylamine concentration. Then, the flow of the gas was continued. After the catalyst bed was exhausted and the concentration of the component of offensive odor in the gas at the outlet of the catalyst bed roughly equalled the concentration at the inlet, introduction of ozone to the tube interior was started. The introduction of ozone was adjusted so that the ozone concentraiton in the gas would remain at 30 ppm. The ozone introduction was continued for five hours. At the end of the ozone introduction, the gas at the outlet of the catalyst bed was analyzed for ozone and trimethylamine contents. Thereafter, the ozone introduciton was discontinued and the introduction of the gas containing the component of offensive odor was continued to effect regeneration of the catalyst bed for 10 hours. At the end of the regeneration, the gas at the outlet of the catalyst bed was analyzed. Then, the same operation of intermittently introducing ozone to the exhausted catalyst bed as described above was repeated a total of 10 times. After elapse of 10 hours, the gas at the outlet of the catalyst bed was analyzed. The analysis for trimethylamine was made by using a FID-fitted gas chromatography and that for ozone an ozone monitor. The results were as shown in Table 15. Example 60 The catalyst obtained in Example 59 was subjected to the procedure of Example 59, excepting the temperature of the catalyst bed was kept at 0°C. The results were as shown in Table 16. Example 61 The catalyst of TZ-1H obtained in Example 30 was tested for adsorption and regeneration by following the procedure of Examples 59 and 60. The results were as shown in Tables 15 and 16. Example 62 The catalyst of TSZ-1H obtained in Example 31 was tested for adsorption and regeneration by following the procedrue of Examples 59 and 60. The results were as shown in Tables 15 and 16. Example 63 A catalyst having a composition of TS-1 : MnO₂ = 90 : 10 in weight ratio as oxide was obtained by impregnating the lattice-like honeycombs of TS-1H obtained in Example 29 with an aqueous manganese nitrate solution, and drying and calcining the impregnated honeycombs. This catalyst was tested for adsorption and regeneration by following the procedure of Example 60, excepting the concentration of the introduced ozone was fixed at 20 ppm and the duration of the introduction was two hours. The results of the test were as shown in Table 17. Example 64 The catalyst obtained in Exmaple 63 was tested for adsorption and regeneration by following the procedure of Example 63, excepting the catalyst bed temperature was fixed at 25°C. The results were as shown in Table 18. Examples 65-71 Adsorbents were prepared by following the procedure of Example 63, excepting the component B for addition to the component A was varied. As raw materials for the component B, nitrates of iron, cobalt, nickel, silver, and platinum and chlorides of palladium and rohodium were used. The catalysts thus obtained were tested for adsorption and regeneration by following the procedrue of Example 63. The catalyst compositions and the results of the test were as shown in Table 17. Example 72-78 The catalysts obtained in Examples 65-71 were tested for adsorption and regeneration by following the procedure of Example 64. The catalyst compositions and the results of the test were as shown in Table 18. Controls 8-9 Catalyst were prepared by following the procedure of Example 63, excepting lattice-like honeycombs of activated alumina and lattice-like honeycombs of activated carbon were used in the palce of the TS-1H. The catalysts were tested for adsorption and regeneration by following the procedure of Example 64. The catalyst compositions and the results of the test were as shown in Table 18. Examples 79-80 Catalysts were prepared by following the procedure of Example 8, excepting amount of manganese nitrate addition was varied. Consequently, there were obtained catalysts having compositions of TS-1:MnO₂=80:20 by weight ratio as oxide adn that of TS-1: MnO₂=70 : 30 by weight ratio as oxide. Example 81 A catalyst was prepared by following the procedure of Example 8, excepting TiO₂-SiO₂ (composition of TiO₂/ SiO₂=1, molar ratio) obtained in Example 5 was used in place of TS-1. Consequently, there was obtained a catalyst having a composition of TiO₂-SiO₂:MnO₂=90:10 by weight ratio as oxide. Example 82 A catalyst was prepared by following the procedure of Example 8, excepting TiO₂-SiO₂ (composition of TiO₂-/SiO₂=0.42) obtained in Example 6 was used in place of TS-1. Consequently, there was obtained a catalyst having a composition of TiO₂-SiO₂:MnO₂=90:10 by weight ratio as oxide. Example 83-86. The catalysts prepared in Examples 79-82 were tested for the activity of ozone decomposition by following the procedure of Example 20. The reaction temperature was at 2°C. The results were as shown in Table 19. Examples 87-90 The catalysts prepared in Example 79-82 were tested for deodorizing activity by following procedure of Example 35, excepting 10.5 ml of pellets of catalysts were packed in a reaction tube made of Pyrexglass having an inner diameter of 20 mm, and steam saturated air containing 5 ppm of trimethylamine and methyl mercaptan was introduced to the catalyst bed at a flow rate of 0.21 Nm³/hr (space velocity of 20,000 hr ¹)at a reaction temperature of 2°C. The results obtained were as shown in Table 20. In a reaction tube made of Pyrexglass, 250 cc of lattice-like honeycombs of catalyst were packed. Air containing 40% of relative humidity, and containing 5 ppm of ozone was introduced to the catalyst bed at a flow rate of 12.5Nm³/hr (space velocity 50,000hr-1) at room temperature. Change of ozone decomposition ratio with time was tested for 250 days. The results were shown in Table 21. Example 93 A composite oxide comprising titanium and silicon was prepared as follows. An aqueous sulfuric acid solution of titanyl sulfate having the following composition was used as a titanium source. TiOSO₄(as TiO₂) 250 g/liter Total H₂SO₄ 1,100 g/liter Separately, 280 liters of aqua ammonia (NH₃, 25%) was added to 400 liters of water and 24 kg of Snowtex-NCS-30 (silica sol containing about 30% by weight of silica as SiO₂; product of Nissan Chemicals Industries Ltd.) was added further added thereto. To the resulting solution, a titanium-containing aqueous sulfuric acid solution prepared by diluting 153 liters of the aqueous sulfuric acid solution of titanyl sulfate with 300 liters of water was gradually added dropwise while under agitation to give rise to a coprecipitate gel. The resulting reaction mixture was left standing at rest for 15 hours. The TiO₂-SiO₂ gel thus obtained was separated by filtration, washed with water, and then dried at 200°C for 10 hours. The dry TiO₂-SiO₂ gel was calcined under an atmosphere of air at 550°C for six hours. The powder thus obtained had a composition of TiO₂:SiO₂ = 4:1 (molar ratio) and a BET surface area of 185m²/g. The powder thus obtained was used to prepare deodrant formed of lattice-like honeycomb. An aqueous solution containing 3.68 kg of manganese nitrate Mn(NO₃)₂ 6H₂O was added in 10 kg of this powder. And then the resulting mixture was thoroughly blended in a blender with a suitable water added thereto. The homogeneous mixture consequently obtained was molded in the form of lattice-like honeycombs having visible dimensions of 50 mm in length, 50 mm in width, and 100 mm in depth with an extrusion molder. The honeycombs were dried at 150°C for five hours and then calcined under an atmosphere of air at 300°C for two hours. The honeycomb obtained had 1.4mm in individual diameter of penetration pores, 0.33 mm in wall thickness of cells and aperture ratio of this honeycomb was 64%. There was obtained a catalyst formed of the honeycombs having a composition of TiO₂-SiO₂ = 90:10 by weight ratio as oxide. Example 94-95 Catalysts formed of lattice-like honeycombs were prepared by using the same composition as used in Example 93 and following the procedure of Exmaple 93, excepting the form of catalyst were varied. The diameter of penetration pores, wall thickness of cells, and aperture ratio of catalysts thus obtained were shown as follows. Example 96-98 The catalysts obtained in Examples 93-95 were tested for deodorization and loss of pressure at the time as follows. In a reaction tube made of Pyrex glass, 250 ml of lattice-like honeycombs of catalyst were packed. Steam-saturated air containing 5 ppm of trimethylamine or methyl mercaptan as a typical component of offensive odor was introduced to the catalyst bed at a flow rate of 5 Nm³/hr (space velocity of 20,000 hr ¹ ). Ozone was introduced in a concentration of 20 ppm to the inlet side of the catalyst bed, with the reaction temperature at 5°C. After 500 hours' use of the catalyst bed required for stabilization of the catalyst activity, the catalyst was tested for deodorization ratio. The losses of pressure were tested at above-mentioned operating condition. The results were as shown in Table 22.

Claims: A catalyst for the purification of an ozone-containing gas, comprising as catalytic components, a component A being at least one composite oxide selected from the group consisting of TiO₂-SiO₂, TiO₂-ZrO₂, TiO₂-P₂O₅, TiO₂-SiO₂-ZrO₂, TiO₂-SiO₂-P₂O₅, TiO₂-ZrO₂-P₂O₅, and TiO₂-SiO₂-ZrO₂-P₂O₅, and a component B composed of at least one element selected from the group consisting of manganese, iron, cobalt, nickel, silver, platinum, palladium, and rhodium, wherein the amount of component B is a proportion in the range of 0 to 150 parts by weight as an oxide where the element selected is manganese, iron, cobalt, nickel or silver, or in the range of 0 to 10 parts by weight as the metal where the element selected is platinum, palladium or rhodium, the portions respectively being based on 100 parts by weight of component A as oxide. A catalyst as claimed in Claim 1 characterised in that component A comprises 20 to 95 mol% of TiO₂ and 5 to 80 mol% of at least one oxide selected from the group consisting of SiO₂, ZrO₂ and P₂O₅. A catalyst as claimed in any preceding claim, characterised in that component B is an oxide or oxides of manganese. A catalyst as claimed in any preceding claim characterised in that component A includes 5 to 90% by weight substituted with activated carbon. A catalyst as claimed in any preceding claim characterised in that the catalyst is in the form of honey combs having a nominal diameter of individual penetration pore in the range of 0.7 to 3.0mm, a wall thickness of cells in the range of 0.2 to 0.5 mm, and an aperture ratio of not less than 50%. A catalyst as claimed in any preceding Claim for the purification of gas containing component of offensive odour by means of introducing ozone into the gas characterised in that the amount of component B is a proportion in the range of 10 to 60 parts by weight as an oxide where the element selected is manganese, iron, cobalt, nickel or silver or in the range of 0.2 to 5 parts by weight as the metal where the element selected is platinum, palladium, or rhodium, the proportions respectively being based on 100 parts by weight of component A as oxide. A method for the purification of an ozone-containing gas, which comprises passing the ozone-containing gas through a bed of catalyst characterised in that the catalyst is as claimed in any preceding claim, thereby effecting decomposition of the ozone in the gas. A method for the purification of a gas containing a component of offensive odour, characterised by combining the gas with ozone and passing the resultant mixed gas through a bed of a catalyst as claimed in any of Claims 1 to 6 thereby effecting removal of the component of offensive odour by the ozone and subsequent decomposition of the ozone. A method for the deodourisation of a gas containing a component of offensive odour by means of introducing ozone into the gas thereby decomposing and removing the component of offensive odour, characterised by setting up a bed of a catalyst as claimed in any of claims 1 to 6 in a path for the gas and making the introduction of the ozone intermittently.

Inventors: INOUE, AKIRA, KANZAKI, TOSHIHIDE, KOBAYASHI, MOTONOBU, MITSUI, KIICHIRO, NANBA, YOKU, SANO, KUNIO, SUZUKI, TAKEHIKO
Applicants: NIPPON SHOKUBAI CO., LTD.
Application year: 1987
Main classification: B01D53
IPC codes: B01J23, B01J27, B01D53