3,556,725 or CM-41 from Mobil Oil as pure SiO 2 material), and also such mesoporous silica gels up to 10% by weight of foreign elements (e.g. Catalyst for the oxidation of SO- to S0 2 and use of the catalyst in a process for the production of. Water is introduced in line (20), and the sulfuric acid running off in line (21) also reaches the collecting tank (12). 09600332, Country of ref document: % can be further processed in a main converter in accordance with the latest state of the art (eg Lurgi, Frankfurt), whereby SO and sulfuric acid are formed and a tail gas with an S0 2 content of less than 200 pp remains. 1998966365, Country of ref document: Catalyst according to claim 1 or 2, characterized in that the support to 90-100 wt.% Of mesoporous % iron. The result of this is that the gas which is given up to catalysis should have an S0 2 content of at most about 12% by volume, so that the exotherm of the oxidation reaction can be controlled well remains. AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE, Ref document number: A first, SO, -containing gas mixture leaves the pre-contact stage (1) in line (6) at temperatures in the range from 580 to 800 ° C. and preferably 600 to 700 ° C. This first gas mixture is cooled in the waste heat boiler (7) to temperatures of 50 to 300 ° C, valuable high-pressure steam can be obtained from water. Iron vanadate can be applied in the same way to supports with a large surface area. 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 converting SO2 with molecular oxygen into SO3. B. V 2 0 5 as an active component, preferably work in the temperature range from 380 to 620 ° C. Higher temperatures damage the catalytic converter. 0.5 ml of a fraction with particle sizes between 500 and 1000 μm was used for each catalyst Activation held at 324 ° C in a nitrogen stream for three hours. The product was heated to 200 ° C at 2 ° C per minute, held at this temperature for 3 hours, then heated to 550 ° C at 5 ° C per minute and held at this temperature for 10 hours. 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. A, Format of ref document f/p: Catalyst according to claim 1 or 2, characterized in that the support consists of 90 to 100% by weight of a zeolite. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS, Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium, Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof, Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. 580 to 800 C is that in the pre-contact stage 20 to 80% of the supplied So, is converted to SO3 and from the Samples of the three catalysts described were tested in the laboratory to determine their activity with regard to the oxidation of SO 2 to SO 3 . 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. Weight ratio carrier: Active component in the range from 1: 1 to 100: 1 is that the maximum temperature at the pre-contact DE-C-27 10 350 describes a catalyst for the conversion of S0 2 to S0 3 , which works in the temperature range from 600 to 800 ° C. The catalyst has a silicon oxide support with a tridymite structure and an active component containing iron, copper and an alkali metal. The gas flowing upward in the second absorber (14) releases sulfuric acid droplets in the droplet separator (24) and then passes through the line (25) to a heater (26) which raises the temperature of the gas to 380 to 500 ° C. 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