Absorber a second. content of at least 90 wt. MX, Ref document number: The method according to claim 5 or 6, characterized in that a catalyst is used in the subsequent oxidation stage, the active component of which is at least 5 wt .-% based on vanadium. Reactants. A first, SO-containing gas mixture is withdrawn from the pre-contact stage, which is cooled to temperatures of 50 to 300 C and passed into at least one absorber so that the first Here a zeolite-like iron silicate (structure type beta-zeolite) is used as the carrier material; the iron silicate has a three-dimensional system of micropores and has a large BET surface area of 600 m 2 / g. A first aqueous solution was prepared as follows: 78.5 g of 40% tetraethylammonium hydroxide and 10.7 g of 40% hydrogen fluoride were added to 260.4 g of tetraethyl orthosilicate in a polypropylene container. In this reaction, the catalyst is can be platinum, vanadium (V) oxide, iron (III) oxide. The catalyst is also intended to serve as the basis for a process for the production of sulfuric acid, in which gases with a high SO 2 concentration are assumed. The carrier has a BET surface area of 100 to 2000 m2 / g and an SiO2 content of at least 90% by weight pyrosulfate). Oxygen in the pre-contact stage passes through at least one bed (pre-contact bed) of a granular catalyst (pre-contact) so that the pre-contact consists of a porous carrier and an active component connected to the carrier, the 10 years ago. The height of the ignition layer is 1 cm. 6. Synthesis. The invention has for its object to provide a catalyst suitable for long-term operation, the activity and durability of which is guaranteed even at temperatures of 700 ° C. and higher. Catalysts with high density 'and average porosity', supported on siliceous matrix, based on vanadium, oxygen and alkali metals. engine exhaust gases, smoke, fumes, flue gases, aerosols, Chemical or biological purification of waste gases, General processes for purification of waste gases; Apparatus or devices specially adapted therefor, Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00, Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium, Catalysts comprising molecular sieves having base-exchange properties, e.g. Details on mesoporous SiO 2 can also be found in WO-A-91/11390 and in "Microporous Materials" 10 (1997), pages 283-286. FOERFARANDE Foer AOTERVINNING AV SVAVEL FRAON SVAVELHALTIGA gaser. Water is introduced in line (20), and the sulfuric acid running off in line (21) also reaches the collecting tank (12). The product had a BET surface area of 478 m 2 / g, the weight ratio Si: Fe was 5: 1. S03 formed in the oxidation stage is further processed into sulfuric acid in further process steps. F, Ref document number: The pre-contact stage (1) is fed through line (2) SO 2 -rich gas, to which one has mixed through line (3) 0 2 -containing gas (eg air). The invention relates to a catalyst for converting SO2 with molecular oxygen into SO3. In the laboratory, the first catalyst described above is used to partially convert a gas mixture with the components in column A of the table below to S0 3 : The data in the example are partially calculated. For the sulfate content in the catalyst, 1 to 7% by weight, based on the total weight of the catalyst, is recommended. The cooled gas mixture is passed through the second horde, which in the same way as the first horde contains an ignition layer and a bed of the pre-contact. This gas mixture with an S0 2 content of 14.3 vol. It has good thermal stability up to 1000 ° C and a BET surface area of approximately 1000 m 2 / g. To 10 g of an aqueous 25% C 16 H 33 N (CH 3 ) 3 C1 solution, a mixture of 1.8 g of Na water glass (composition 27.5% by weight SiO 2 .8 , 3 wt .-% Na, 0, water), 1.3 g Si0 2 and 10 g water. Active component consists of 10 to 80% by weight of iron and that The supporting material is a BET-surface ranging from 100 to 2000 m2/g and comprises a SiO¿2? Here, the gas containing S0 2 and 0 2 with an SO, content of 13 to 50 vol.% And an oxygen content corresponding to a 0 2 / S0 2 volume ratio of at least 1: 2 is fed to a pre-contact stage Gas and oxygen in the pre-contact stage through at least one bed (pre-contact bed) of a granular catalyst (pre-contact), the pre-contact having the features already described, and the maximum temperature at the pre-contact is kept in the range from 580 to 800 ° C. In the pre-contact stage, 20 to 80% of the SO supplied is converted to SO, and a first gas mixture containing SO 3 is withdrawn from the pre-contact stage, which is cooled to temperatures of 50 to 300 ° C. and passed into at least one absorber, with brings the first gas mixture in the absorber into direct contact with circulated, water-containing sulfuric acid and discharges a partial sulfuric acid stream. 1 g of the product was mixed intensively with 3.5 ml of a 0.95 molar Fe (N0 3 ) solution and then dried at 90 ° C. for 2.5 hours. The weight ratio V: Fe in the active component can range from 1: 1 to 1.3: 1. aluminum-containing MCM-41 from Mobil Oil). Oxygen content corresponding to an O2 / SO2 volume ratio of at least 1: 2 supplies that one the gas and the 90 to 100 wt .-% of a zeolite or from mesoporous Sio,. A, Format of ref document f/p: 2318481, Country of ref document: boron), diatomaceous earth, amorphous Si0 2 or mesoporous aluminum silicate (e.g. Catalyst for converting SO2 with molecular oxygen to SO3, characterized in that the catalyst consists of a porous support and a support connected to the support The product was filtered, washed, dried, heated to 800 C β and 24 hour maintained at 800 ° C for. 3. Kind code of ref document: B. The known catalysts for the oxidation of S0 2 , the z. The S0, content in the gas of line (2) is in the range from 13 to 50 vol.% And mostly at least 15 vol.%, The gas is preferably preheated to temperatures from 350 to 500.degree. The invention relates to a catalyst for reacting SO, with molecular oxygen to S0 3 and also a method for producing sulfuric acid from S0 3 and water, wherein the S0 3 is generated catalytically by reacting S0 2 with molecular oxygen. Advantageous carriers exist, for. The weight ratio Si: Fe: V is 33: 1: 1.3. EP, Ref document number: En catalyst och ett foerfarande foer oxidering av svavelhaltiga foereningar. A flow diagram of the process is explained with the help of the drawing.
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