DEODORIZING METHOD AND DEODORIZING CATALYST

Abstract: The present invention provides a deodorizing method for removing stinking components by oxidative destruction with ozone in the presence of a catalyst comprising the prescribed metal oxide and at least one selected from the group consisting of titanium dioxide and silver oxide and gold, or a catalyst comprising manganese dioxide and clay. Also, the present invention provides a deodorizing catalyst of which active components is carried at the range of 10 to 200 µm in thickness of the active components on the carrier, thereby stably removing stinking components in high rate, even when the reaction conditions are changed.

Description: BACKGROUND OF THE INVENTION The present invention relates to a deodorizing method for destroying compounds of emitting an offensive smell, contained in gas or the like (hereinafter referred to as stinking components) and deodorizing catalyst for using of this present method. Examples of a conventional method of destroying the stinking components contained in gas, include (i) an adsorptive deodorizing method using a porous substance such as activated carbon, zeolite or the like, (ii) a wet-treatment deodorizing method using an oxidizing agent or a reducing agent, (iii) an ozonolysis deodorizing method and (iv) the like. However, any of the conventional deodorizing method above mentioned (hereinafter referred to as conventional methods) does not fully achieve a satisfactory deodorizing. More specifically, in the adsorptive deodorizing method, the adsorbent needs to be regenerated or the like since its adsorbing ability expires in a limited period of time. This presents the problem that the deodorizing apparatus requires much labor and expense for maintenance. The wet treatment deodorizing method involves a troublesome treatment of additives such as an oxidizing agent or the like. Finally, the ozonolysis deodorizing method includes no such problems as above mentioned, but requires decomposition of ozone contained in gas submitted to deodorizing in view of insufficient removal of the stinking components by oxidative destruction and prevention of environmental pollution which may provoke a respiratory disease or the like. The solid type catalyst of which whole is shaped by catalytic active ingredient, e.g. manganese, titanium and clay in the form of honeycomb, was used as an oxidative destruction catalyst to remove the stinking components in the ozonolysis deodorizing method. According to the conventional solid catalyst, however since the saturated absorption amount of stinking components in the catalyst is large, when the condition change is occurred in a refrigeration or the like, for example the reaction temperature is risen, concentration of stinking components becomes low, the stinking components are released from the catalyst to the air, and as a result, concentration of stinking components in the air is increased. SUMMARY OF THE INVENTION Main object of the present invention is to provide an ozonolysis deodorizing method which is superior to the conventional method in ability of decomposing and removing stinking components and by which unreacted ozone hardly remains after deodorizing treatment. Another object of this invention is to provide a deodorizing catalyst for using in the ozonolysis deodorizing method, by which stable rate of decomposing stinking compounds can be obtained, even if changing the reaction condition e.g. rising the reaction temperature, lowering the concentration of stinking component or the like. To achive the object above mentioned, the deodorizing method in accordance with the present invention (hereinafter referred to as the present method) is adapted to remove stinking components by oxidative destruction with ozone in the presence of a catalyst comprising (i) at least one of metal oxide, each metal of which is selected from the group consisting of copper, manganese, cobalt, iron and nickel, and (ii) at least one selected from the group consisting of titanium dioxide, silver oxide and gold, or comprising manganese dioxide and clay. The deodorizing catalyst for using in this present invention comprises an inactive carrier, and active components carried on said inactive carrier at the range from 10 to 200 µm of thickness. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a flowsheet of a catalyst activity test emplyed in Examples. DETAILED DESCRIPTION OF THE INVENTION Examples of the stinking components to be removed by the present method include ammonia, trimethyl amine, hydrogen sulfide, methyl mercaptan, methyl sulfide, methyl disulfide, acetaldehyde, styrene, methyl ethyl ketone, acrolein, propionaldehyde, butyl alchol, phenol, cresol, diphenyl ether, acetic acid, propionic acid, n-pentanoic acid, metylamine, dimethylamine, skatole, dimetyltioether, dimetyl mercaptan, hydrogen chloride and allyl chloride. The present method may be used for deodorizing an exhaust gas dischanged, for example, from sewage disposal plants, refuse disposal plants, printing factories, plating factories, general chemical factories and the like. The catalyst comprising (i) at least one of metal oxide, each metal of which is selected from the group consisting of copper, manganese, cobalt, iron and nickel, and (ii) at least one of selected from the group consisting of titanium dioxide and silver oxide, and gold, include binary-catalyst such as MnO₂-TiO₂, CuO-TiO₂, Co₃O₄-TiO₂, Fe₂O₃-TiO₂ and Fe₂O₃-Au, and ternary catalyst such as MnO₂-Co₃O₄-TiO₂, CuO-MnO₂-Ag₂O, MnO₂-Co₃O₄-Ag₂O, NiO-MnO₂-TiO₂ or the like. A preferable concentration (% by weight) of at least one of metal oxide, each metal of which is selected from the group consisting of Cu, Mn, Co, Fe and Ni, is in a range from 25 to 95 % as converted into the concentration of the metal alone. When the concentration of at least one of metal oxide is less than 25% as converted into the concentration of the metal alone, the catalyst cannot remove the stinking components sufficiently. When the concentration of at least one of metal oxide is more than 95% as converted into the concentration of the metal alone, the catalyst does not have enough durability. A preferable concentration (% by weight) of at least one of metal oxide, each metal of which is selected from the group consisting of Ti and Ag, and/or Au, is in a range from 5 to 75% as converted into the concentration of the metal(s) alone. When the concentration of at least one of metal oxide is less than 5% as converted into the concentration of the metal alone, the catalyst does not have enough durability. When the concentration of at least one of metal oxide is more than 75% as converted into the concentration of the metal alone, the catalyst cannot remove the stinking components sufficiently. In the catalyst comprising of manganese dioxide and clay, or manganese dioxide, clay and titanium dioxide, a preferably concentration (% by weight) of the manganese dioxide is in the range from 20 to 90 %. When concentration of the manganese dioxide is less then 20 %, the catalyst does not have enough active component. When concentration of the manganese dioxide is more then 90 %, capacity of the catalyst is not improved in proportion to addition of manganese dioxide. Also, the capacity of above mentioned catalyst is improved by substituting a part of manganese to at least one of metal oxide, each metal of which is selected from the group consisting of Cu, Co, Fe, Ni and Ag. A preferably rate of the substitution as converted into oxide, is in a range from 1 to 30 %. When the rate of substitution is less than 1 %, the capacity of the catalyst is not improved. When the substitution rate is more than 30 %, capacity of the catalyst is not improved in proportion to the substitution. The substituted catalyst mentioned above, includes MnO₂-CuO-clay, Mn0₂-Co₃O₄-clay, Mn0₂-Fe₂O₃-clay, MnO₂-NiO-clay, MnO₂-Ag₂O-clay, MnO₂-CuO-clay-TiO₂, Mn0₂-Co₃O₄-clay-TiO₂, Mn0₂-Fe₂O₃-clay-TiO₂, MnO₂-NiO-clay-TiO₂, MnO₂-Ag₂O-clay-TiO₂ and the like. The above mentioned clay is the bedded clay mineral which is mainly composed of biroferait, talc, mica, chlorite, montmorillonite, caolin, hairosaite and the like. Example of the clay is Kibushi clay, Gairome clay or the like. The catalyst for using in the present method is not particularly limited in shape, but may be in any form such as honeycomb, pellet, cylinder, plate, pipe or the like. The concentration (% by weight) of an active componets contained in the catalyst is preferably 50% or more, and more preferably 75 % or more. When the concentration of the active componets in the catalyst is less than 50 %, the catalyst cannot remove the stinking components sufficiently. The catalyst may be manufactured by a known method suitably selected out of impregnation, kneading, coprecipitation, precipitation, oxide mixing and the like. In production of the catalyst, there may be added (i) a forming assistant such that the catalyst easily gets into shape, or (ii) a reinforcing agent such as inorganic fiber or an organic binder to improve the mechanical strength or the like. Also, the catalyst of this invention can be produced by supporting active components on the carrier. The carrier is not particularly limited in shape, but may be in any form such as honeycomb, pellet, cylinder, plate, pipe or the like. The carrier is not particularly limited in material, but may be made of urethane foam, clay or the like. The preferable thickness of the active components on the carrier is in the range from 10 to 200 µm. When the thickness of that is in the range, saturated absorption amount of stinking components in the catalyst is adjusted appropriately. Accordingly, the catalyst presents stable removing rate of stinking component, even if changing the reaction condition, e.g. rising the reaction temperature, lowering the concentration of stinking components or the like. When the thickness of that is more than 200 µm, the saturated absorption amount of stinking components in the catalyst is too much. And when the condition changed likely to above mentioned, the stinking compound absorbed in the catalyst is released from the catalyst to the air, as a result, the catalyst becomes generator of stench. When the thickness of that is less than 10 µm, the catalyst does not have enough capacity removing the stinking components. A suitable amount of ozone (O₃) which is used together with the catalyst at the time of deodorizing, depends on the types and concentrations of stinking components to be removed, the reaction temperature, the type and amount of the catalyst, and the like. For example, when gas containing H₂S as the stinking components is to be deodorized, it is preferable that 1 to 2 mols of O₃ coexists per mol of H₂S. For gas containing NH₃ as the stinking components, it is preferable that 1 to 3 mols of O₃ coexists per mol of NH3. For gas containing methyl mercaptan as the stinking components, it is preferable that 1 to 4 mol of O₃ per mol of methyl mercaptan. If gas to be deodorized contains stinking components in high concentration, the concentration O₃ may exceed the preferable range above mentioned to improve the stinking component removing rate. However, if excessive, surplus O₃ may remain after deodorizing. Accordingly, attention should be paid such that no excessive O₃ coexists to prevent the generation of such residue. The reaction temperature at time of deodorizing is preferably in a range from 0 to 40 °C and more preferably in a range from 10 to 30 °C. The temperature less than 0 °C causes the reaction speed to be slower, while the temperature exceeding 40 °C requires an additional energy for increasing the temperature, resulting in poor economy. Preferably, the catalyst comes in contact with the reaction gas in a range of area velocity (AV) from 5 to 50. The area velocity less than 5 requires a greater amount of catalyst, while the area velocity exceeding 50 causes the decomposition efficiency to be lowered, failing to achive the desired decomposition efficiency. it is here noted that the area velocity refers to a value obtained by dividing the reaction amount (Nm³/u, u:Hr) by the gas contact area per catalyst in unit volume (m²/m³). EXAMPLES The following description will discuss, in more detail, examples of the present invention. It is noted that the present invention should not be limited to the following examples. Example 1 Kibusushi clay was dried for 18 hours at 100 °C, after that it was crushed by a sample mill having the 0.5 mm / screen. 20 kg of the results was mixed with 1 kg of methyl cellulose type binder (Yuken Industry Co., YB-32) and water. The mixture was kneaded thoroughly by a neader. After that, the mixture was put into the orga-screw type extruder, the honeycomb was obtained. In such a case, the water content was adjusted so as to have 30 - 35 kg/cm² of pressure. The obtained honeycomb was air-dried at ordinary temperature, and it was heated up to 500 °C at the rate of 5 °C by a hour. After it keep 500 °C for 3 hours, it was cooled down at the rate of 10 °C by a hour. Thus, the honeycomb type carrier having open area rate of 64 % and pitch of 4.0 mm was obtained. 704 g of MnO₂ having a specific surface area of 48 m²/g was added to 1034 ml of a titania sol (TiO₂ concentration : 150 g/ℓ). To the mixture, 250 g of grass bead was added to adjust the degree of milling. The resultant mixture was agitated and mixed for 30 minutes. The grass bead was apart from the mixture to produce the slurry. After the slurry was diluted with 300 ml of water, the slurry was impregnated into the corrugated honeycomb. The exceeded slurry was excluded from the honeycomb, and the honeycomb was air-dried and baked. Thus, there was prepared a binary-catalyst carrying 10 µm in thickness of MnO₂-TiO₂ (weight ratio of 82 :18) with 43 % of carry rate. The open area rate of the catalyst is 63 %, the area contacted with gas at a volume (hereinafter referd to as AP) is 795 m²/m³. The thickness of the MnO₂-TiO₂ was measured by electron probe micro analyser (EPMA). Example 2 There was prepared a binary-catalyst carrying MnO₂-TiO₂ having open area range 60% and Ap 775 m²/m³, in the same manner as that of Example 1, except that carry weight rate of the catalyst was 26.5 % and average thickness of MnO₂-TiO₂ was about 50 µm in Example 2. Example 3 There was prepared a binary catalyst carrying MnO₂-TiO₂ having open area rate 56% and Ap 750 m²/m³, in the same manner as that of Example 1, except that MnO₂-TiO₂ sol slurry was not diluted with water, average carry weight rate of catalyst was 40.7 % and average thickness of MnO₂-TiO₂ was about 100 µm in Example 3. Example 4 There was prepared a binary-catalyst carrying MnO₂-TiO₂ having open area rate 49% and Ap 700 m²/m³, in the same manner as that of Example 1, except that MnO₂-TiO₂ sol slurry was not diluted with water, carry weight rate of the catalyst was 65.1 % and average thickness of MnO₂-TiO₂ was about 200 µm in Example 4. Example 5 There was prepared a binary-catalyst carrying MnO₂-TiO₂ having open area rate 64% and Ap 798 m²/m³, in the same manner as that of Example 1, except that carry weight rate of the catalyst was 2.2 % and average thickness of MnO₂-TiO₂ was about 5 µm in Example 5. Example 6 There was prepared a binary-catalyst carrying MnO₂-TiO₂ having open area rate 46% and Ap 675 m²/m³, in the same manner as that of Example 1, except that MnO₂-TiO₂ sol slurry was not diluted with water, carry weight rate of the catalyst was 72.8 % in and average thickness of MnO₂-TiO₂ was about 250 µm Example 6. Catalyst Activity Test Each catalyst of Examples 1 to 6 was submitted to a catalyst activity test with the use of the test method having a flowsheet as shown in Fig. 1, under reaction conditions discussed later. In Fig. 1, stinking components H₂S, NH₃ and methyl amine contained in gas to be deodorized are introduced into a catalyst layer 2. The stinking components thus introduced are decomposed by ozone O₃ introduced from an ozone generator 1 to the catalyst layer 2. A portion of the gas after decomposed and deodorized is introduced into an ozone analysis 3, in which the remaining ozone O₃ is subjected to quantitative analysis. The remaining potion of the gas after decomposed and deodorized is introduced to a stinking component analysis meter 4 including two gas chromatographs (designed for analyzing H₂S or methyl amine) and one NH₃ meter. These devices are adapted to carry out quantitative analysis of stinking components. (Reaction Conditions I) Space velocity : 20,000/Hr Reaction temperature : 20 °C Concentration of Stinking components /Concentration of ozone components : H₂S/ozone : 10/20 ppm NH₃/ozone: 10/30 ppm methyl mercaptan/ozone 5/10 ppm (Reaction Conditions II) After catalyst Activity Test was carried out for 24 hours under Reaction Condition I, reaction temperature was risen to 50 °C. After 5 minutes, concentrations of stinking components and ozone were measured. (Reaction Conditions III) After catalyst Activity Test carried out for 24 hours under Reaction Condition I, concentration of stinking components was changed to the following. After 5 minutes, concentrations of stinking components and ozone were measured. concentration of H₂S : 1 ppm concentration of NH₃ : 1 ppm concentration of methyl mercaptan : 1 ppm The test result are shown in the Table 1. As apparent from Table 1, any of catalyst obtained in Example 1 to 6 presents high and stable rate of removing stinking components. Especialy, the catalyst obtained in Example 1 to 4, which has 10 to 200 µm in thickness of active components on carrier, presents stable rate of removing stinking components. Example 7 30 g of Mn0₂ having a specific surface area of 48m²/g and 70 g of anatase type Ti0₂ having a specific surface area of 85 m²/g were added to 170 ml of a titania sol (Ti0₂ concentration : 150 g/ℓ). The mixture was agitated and mixed for 30 minutes to produce slurry, which was impregnated into a corrugated honeycomb made of ceramic fibers having open area rate of 81% and pitch of 4.0 mm. Thus there was prepared a binary-catalyst carrying about 50 µm in average thickness of MnO₂-TiO₂ (mol ratio of 24 : 76) with a carry rate of 101%. Example 8 There was prepared a binary-catalyst carrying about 50 um in average thickness of CuO-TiO₂ (mol ratio of 24 : 76) with a carry rate of 91%, in the same manner as that of Example 7, except that CuO having a specific surface area of 62 m²/g was used in Example 8, instead of 30 g of Mn0₂ having a specific surface area of 48m²/g used in Example 7. Example 9 There was prepared a binary-catalyst carrying about 50 µm in average thickness of Co₃O₄-TiO₂ (mol ratio of 24 : 76) with a carry rate of 91%, in the same manner as that of Example 7, except that Co₃O₄ having a specific surface area of 53 m²/g was used in Example 9, instead of 30 g of Mn0₂ having a specific surface area of 48m²/g used in Example 7. Example 10 There was prepared a binary-catalyst carrying about 50 µm in average thickness of Fe₂O₃-TiO₂ (mol ratio of 24 : 76) with a carry rate of 78 %, in the same manner as that of Example 7, except that Fe₂O₃ having a specific surface area of 53 m²/g was used in Example 10, instead of 30 g of Mn0₂ having a specific surface area of 48m²/g used in Example 7. Example 11 There was prepared 500 ml of a water solution containing 112 g of manganese acetate (4 hydrates), 182 g of cobalt nitrate (6 hydrates) and 63 g of metatitanic acid (Ti0₂ concentration of 40%). while the solution was agitated, ammonia water was gradually added to the solution, causing the same to be neutrized. Thus, a slurry-like precipitate was produced with the final pH of 7.0. The slurry was impregnated into the same corrugated honeycomb as in Example 7 was then impregnated with this precipitate. The honeycomb was calcined for three hours at 450 °C. Thus, there was prepared a ternary-catalyst carrying about 50 um in average thickless of MnO₂-Co₃O₄-TiO₂ (mol ratio of 25 : 50 : 25) with a carry rate of 89 % and having a specific surface area of 72 m²/g. Example 12 There was prepared 500 ml of a water solution containing 17.8 g of manganese acetate (4 hydrates), 288 g of cobalt nitrate (6 hydrates) and 1.5 g of silver nitrate. While the solution was agitated, a water solution of ammonium carbonate was added to the first mentioned solution, causing the same to be neutrized, Thus, a slurry-like precipitate was produced with the final pH of 7.0. The slurry was impregnated into the same corrugated honeycomb as in Example 7. The honeycomb was then calcined for three hours at 450 °C. Thus, there was prepared a ternary-catalyst carrying about 50 µm in average thickness of Co₃O₄-MnO₂-TiO₂ (mol ratio of 20 : 40 : 1) with a carry rate of 92% and having a specific surface area of 65 m²/g. Example 13 There was prepared 500 ml of a water solution containing 74.4 g of cupric nitrate (6 hydrates), 17.8 g of manganese acetate (4 hydrates) and 1.5 g of silver nitrate. While the solution was agitated, a water solution of ammonium cabonate was added to the first mentioned solution, causing the same to be nutrized, Thus, a slurry like precipitate was produced with the final pH of 7.0. This slurry was impregnated into the same corrugated honeycomb as in Example 7. The honeycomb was then calcined for three hours at 450 °C. Then, there was prepared a ternary-catalyst carrying about 50 µm in average thickness of CuO-MnO₂-Ag₂O (mol ratio of 20 : 40 : 1) with a carry rate of 87% and having a specific surface area of 71 m²/g. Example 14 There was prepared 500 ml of a water solution containing 112 g of manganese acetate (4 hydrates), 195 g of nickel nitrate (6 hydrates) and 63 g of metatitanic acid (TiO₂ concentration of 40%). while the solution was agitated, ammonia water was gradually added to the solution. Thus, a slurry-like precipitate was produced with the final pH of 7.0. The slurry was impregnated into the same corrugated honeycomb as in Example 7. The honeycomb was was calcined for three hours at 450 °C, Thus, there was prepared a ternary-catalyst carrying about 50 um in average thickless of MnO₂-Co₃O₄-TiO₂ (mol ratio of 25 : 50 : 25) with a carry rate of 94 % and having a specific surface area of 80 m²/g. Example 15 There was prepared ternary-catalysis carrying about 50 um in average thickness of NiO-MnO₂-TiO₂ (mol ratio of 20 : 40 : 1) with specific surface area of 77 m²/g, a carry rate of 98 %, in the same manner of Example 12, except that 309 g of Nickel nitrate (4 hydrates) used in Example 15, instead of 288 g of cobalt nitrate (6 hydrates) in Example 12. Example 16 There was prepared binary-catalysis carrying about 50 um in average thickness Fe₂0₃-Ag₂O (mol ratio of 95 : 5) with a carry rate of 104 % , in the same manner of Example 7, except that Au colloid which was produced by 30 % hydrogen peroxide added to chloroauric acid at pH 8.0 used in Example 16, instead of 70 g of anatase type Ti0₂ and 170 ml of a titania solution used in Example 12. Comparative Example 1 30 g of MnO₂ having a specific surface area of 48 m²/g and 70 g of a mixture (MiO₂ : SiO₂ = 1 : 1) of titanium tetrachloride with a silica sol were agitated and mixed. While agitating and mixing, ammonia gas was blown such that the resultant mixture was neutrized, thereby to produce a slurry like precipitate. After sufficiently washed with water, the precipitate was then calcined for three hours at 500 °C. Thus, there was prepared a ternary catalyst MnO₂-TiO₂-SiO₂ (mol ratio of 3 : 3.5 : 3.5) having a specific surface area of 162 m²/g. Comparative Examples 2 100 g of TiO₂ having a specific surface area of 85 m²/g was calcined for 3 hours at 500 °C. Thus, a catalyst which is consisted of TiO₂ was obtained. Comparative Example 3 100 g of MnO₂ having a specific surface area of 85 m²/g was baked for 3 hours at 500 °C. Thus, a catalyst which is consisted of MnO₂ was obtained. Catalyst Activity Test Each catalyst of Examples 7 to 16 and Comparative Examples 1 to 3 was submitted to a catalyst activity test with the use of the test method having a flowsheet as shown in Fig. 1, under reaction conditions discussed later. (Reaction Conditions) Space velocity : 20,000/Hr Reaction temperature : 20 °C Stinking components : H₂S, NH₃ or methyl mercaptan The test result are shown in the Table 2. As apparent from the Table 2, any of the catalysts obtained in Examples 7 to 16 presents a higher stinking component removing rate than the catalysts obtained in Comparative Example 1 to 3. Except for the catalyst of Example 7, any of the catalysts obtained in Example 7 to 16 presents a lower ozone residual rate than the catalysts obtained in Comparative Example 1 to 3. Example 17 704 g of MnO₂ having a specific surface area of 48 m²/g and 155 g Kibushi clay were mixed with 1 ℓ of water. To the mixture, 250 g of grass bead was added to adjust the degree of milling, and was agitated and mixed for 30 minutes to produce slurry. The slurry was impregnated into a corrugated honeycomb made of ceramic fibers having open area rate of 81% and pitch of 4.0 mm. Thus, there was prepared a binary-catalyst carrying about 50 µm in average thickness of MnO₂-clay (weight rate of 82 : 18) with a carry rate 95%. Example 18 There was prepared a ternary-catalyst carrying about 50 µm in average thickness of MnO₂-TiO₂-clay (weight rate of 82 : 9 : 9) with carry rate of 95 %, in the same manner as that Example 17, except that 78 g of Kibushi clay and 517 ml of titania sol (TiO₂ concentration : 150 g/ℓ) was mixed with 500 ml of water in Example 18, instead of 704 g of MnO₂ and 155 g Kibushi clay mixed with 1 ℓ of water in Example 17. Example 19 There was prepared a binary-catalyst carrying 50 µm in average thickness of MnO₂-clay (weight ratio of 24 : 76) with carry rate of 103 %, in the same manner as that Example 17, except that 95 g of Kibushi clay and 30g of MnO₂ was mixed with 500 ml of water in Example 20, instead of 704 g of MnO₂ and 155 g Kibushi clay mixed with 1 ℓ of water in Example 17. Example 20 There was prepared a ternary-catalyst carrying 50 µm in average thickness of MnO₂-TiO₂-clay (weight ratio of 24 : 20 : 56) with carry rate of 101 %, in the same manner as that Example 19, except that 70 g of Kibushi clay, 30g of MnO₂ and 170 ml of titania sol was mixed with 500 ml of water in Example 20, instead of 95 g of Kibushi clay and 30g of MnO₂ mixed with 500 ml of water in Example 19. Example 21 There was prepared a ternary-catalyst carrying 50 µm in average thickness of MnO₂-CuO-clay (weight ratio of 77 : 5 : 18) with carry rate of 97 %, in the same manner as that Example 17, except that 43 g of CuO and 661 g of MnO₂ used in Example 21, instead of 704 g of MnO₂ used in Example 17. Example 22 There was prepared a ternary-catalyst carrying 50 µm in average thickness of MnO₂-Co₃O₄-clay (weight ratio of 80 : 2 : 18) with carry rate of 101 %, in the same manner as that Example 17, except that 17 g of Co₃O₄ and 687 g of MnO₂ used in Example 22, instead of 704 g of MnO₂ used in Example 17. Example 23 There was prepared a ternary-catalyst carrying 50 µm in average thickness of MnO₂-Fe₂O₃-clay (weight ratio of 74 : 8 : 18) with carry rate of 98 %, in the same manner as that Example 17, except that 70 g of Fe₂O₃ and 634 g of MnO₂ used in Example 22, instead of 704 g of MnO₂ used in Example 17. Example 24 There was prepared a ternary-catalyst carrying 50 µm in average thickness of MnO₂-NiO-clay (weight ratio of 76 : 6 : 18) with carry rate of 100 %, in the same manner as that Example 17, except that 50 g of NiO and 654 g of MnO₂ used in Example 24, instead of 704 g of MnO₂ used in Example 17. Example 25 There was prepared a ternary-catalyst carrying 50 µm in average thickness of MnO₂-Ag₂O-clay (weight ratio of 80 : 2 : 18) with carry rate of 100 %, in the same manner as that Example 17, except that 17 g of Ag₂O and 687 g of MnO₂ used in Example 25, instead of 704 g of MnO₂ used in Example 17. Example 26 There was prepared a quartery-catalyst carrying 50 µm in average thickness of MnO₂-CuO-TiO₂-clay (weight ratio of 77 : 5 : 9 : 9) with carry rate of 103 %, in the same manner as that Example 21, except that 78 g of Gairome clay and 517 g of titania sol used in Example 26, instead of 155 g of Kibushi clay used in Example 17. Example 27 There was prepared a quartary-catalyst carrying 50 µm in average thickness of MnO₂-Ag₂O-TiO₂-clay (weight ratio of 80 : 2 : 9 : 9) with carry rate of 103 %, in the same manner as that Example 17, except that 78 g of Gairome clay and 517 g of titania sol used in Example 27, instead of 155 g of Kibushi clay in Example 17. Comparative Example 4 100 g of Kibushi clay having a specific surface area of 56 m²/g was calcined for 3 hours at 500 °C. Thus, a catalyst consisted in Kibushi clay, was obtained. Catalyst Activity Test Each catalyst of Examples 17 to 27 and Comparative Examples 4 were submitted to a catalyst activity test with the use of the test method having a flowsheet as shown in Fig. 1, under the same reaction conditions as the Example 7 to 16. The test result are shown in the Table 3. As apparent from Table 3, any of the catalysts obtained in Example 17 to 27 presents a higher removing rate of stinking component than that of the catalysts obtained in Comparative Example 1 to 4. And any of the catalysts obtained in Example 17 to 27 presents a lower ozone residual rate than that of the catalyst obtained in Comparative Example 1 to 4. These results of the Catalyst Activity Test present that the method of the present invention is effective to remove stinking components in high rate, and unreacted ozone hardly remains after deodorizing treatment.

Claims: A deodorizing method for removing stinking components by oxidative destruction with ozone in the presence of a catalyst comprising, as active components; at least one of metal oxide, each metal of which is selected from the group consisting of copper, manganese, cobalt, iron and nickel; and at least one selected from the group consisting of titanium dioxide, silver oxide and gold. A deodorizing method according to Claim 1, wherein the catalyst is selected from the group consisting of MnO₂-TiO₂, CuO-TiO₂, Co₃O₄-TiO₂, Fe₂O₃-TiO₂, Fe₂O₃-Au, MnO₂-Co₃O₄-TiO₂, CuO-MnO₂-Ag₂O, MnO₂-Co₃O₄-Ag₂O and NiO-MnO₂-TiO₂. A deodorizing method according to Claim 1, wherein the concentration of said metal oxide, each metal of which is selected from the group consisting of Cu, Mn, Co, Fe and Ni, in said active components is in a range from 25 to 95% by weight as converted into the concentration of the metal alone. A deodorizing method for removing stinking components by oxidative destruction with ozone in the presence of a catalyst comprising manganese dioxide and clay as active components. A deodorizing method according to Claim 4, wherein the catalyst includes titanium dioxide in addition to manganese dioxide and clay. A deodorizing method according to Claim 4, wherein the the catalyst includes at least one of metal oxide, each metal of which selected from the group consisting of copper, manganese, cobalt, nickel and silver in addition to manganese dioxide and clay. The use of a catalyst for removing stinking components by oxidative destruction with ozone, the catalyst being formed of an inactive carrier supporting a layer of active components having a thickness of 10-200 µm, the active components being: (i) at least one metal oxide in which the metal is selected from copper, manganese, cobalt, iron and nickel; and (ii) at least one of titanium dioxide, silver oxide and gold.

Inventors: NAGANO, KAZUHIKO, NAKATSUJI, TADAO, YOSHIMOTO, MASAFUMI
Applicants: SAKAI CHEMICAL INDUSTRY CO., LTD.,
Application year: 1989
Main classification: A61L9
IPC codes: A61L9, B01D53