Abstract: The invention relates to a tubular reactor for carrying out catalytic gas-phase reactions, containing a catalyst tube bundle (8) that is traversed by the relevant reaction gas mixture, is filled with a catalyst, extends between two tube sheets (4, 148) and around which flows a heat transfer medium contained within a surrounding reactor jacket (6). The reactor also comprises gas entry and discharge hoods (2; 60) that cover the two tube sheets for supplying the relevant process gas to the catalyst tubes and for discharging the reacted process gas from the catalyst tubes. Together with all the parts that come into contact with the process gas mixture, the reactor is designed to have an appropriate strength for withstanding the deflagration and explosive pressures that are to be taken into account during its operation. The volume available to the process gas mixture prior to its entry into the catalyst tubes is restricted as much as possible in construction and flow engineering terms.

Abstract: The invention relates to a tubular reactor for carrying out catalytic gas-phase reactions, containing a catalyst tube bundle (8) that is traversed by the relevant reaction gas mixture, is filled with a catalyst, extends between two tube sheets (4, 148) and around which flows a heat transfer medium contained within a surrounding reactor jacket (6). The reactor also comprises gas entry and discharge hoods (2; 60) that cover the two tube sheets for supplying the relevant process gas to the catalyst tubes and for discharging the reacted process gas from the catalyst tubes. Together with all the parts that come into contact with the process gas mixture, the reactor is designed to have an appropriate strength for withstanding the deflagration and explosive pressures that are to be taken into account during its operation. The volume available to the process gas mixture prior to its entry into the catalyst tubes is restricted as much as possible in construction and flow engineering terms.

Abstract: A tubular reactor (2) for catalytic reactions with a heat carrier that inside a reactor jacket (10) circulates around a contact tube bundle (8), which extends between a tube plate (4; 6; 80; 82) at the reaction gas inlet side and one at the reaction gas outlet side with gas inlet and gas outlet hoods (12, 14) spanning the face sides of the two tube plates and containing reaction-inhibiting media in the zone of the tube plate on the gas inlet side, characterize themselves in that the reaction-inhibiting media consist entirely or in part of a heat insulation layer (46; 50; 64; 80) with openings for the tube cross-sections on at least one of the two sides of the respective tube plate (4; 60; 82). In this manner, either the respective tube plate (4; 60; 82) is insulated against the hot heat carrier or the reaction gas entering into the reactor is prevented from having contact with the comparatively hot tube plate in order to prevent harmful secondary reactions at the reactor inlet.

Abstract: A tube reactor (2) for performing exothermic gas phase reactions comprising a reaction tube bundle (8), that extends in a sealed manner between two tube end plates (4, 6), that carries a reaction gas and is surrounded by a heat carrier inside a surrounding reactor shell (10). The tube reactor also includes a cowl (18, 20) that spans the respective tube plates (4, 6) and is connected to a gas inlet and a gas discharge line, respectively. Inside the cowl (18) on the gas inlet side adjacent to a first gas supply chamber (28), connected to the inside of the reaction tubes (16), is located a separately fed second gas supply chamber (30) with its own tube end plate (32) that is connected to separate gas supply tubes (34) suitable for a second reaction gas. The separate gas supply tubes reach into the gas inlet end or reach to directly before the gas inlet ends of the reaction tubes (16).

Abstract: A process for producing styrene by the dehydrogenation of ethyl benzene whereby the ethyl benzene in a mixture with steam is introduced into a tubular reactor, the tubes of which are heated by molten salts. The structural parameters of this process are the tube diameter which should be 20 to 35 millimeters, the temperature of the molten salts which should be 580.degree. to 660.degree. C. and at most 20.degree. C. higher than the reaction temperature at the catalyst and the weight ratio of steam to ethyl benzene of the feed stock which should be 0.5 to 1. The process saves energy and increases efficiency by reducing the steam consumption.

Abstract: A process and system are provided for economic utilization of solar energy. Solar energy is absorbed and converted to thermal energy by means of at least two systems, operating in different temperature ranges, for circulating a primary fluid heat transfer medium through separate collector sections of a solar receiver to recover solar heat and through separate output heat exchangers to supply heat to a second heat transfer medium functioning as a working medium, with heat storage means being associated with each system for the purpose of satisfying the heat requirements of the working fluid and also to prevent cooling down of the collector during the time that little or no solar radiation is available.