Abstract: In producing C2-C4 olefins, in particular propylene, from an educt mixture containing steam and oxygenates, such as methanol and/or dimethyl ether, the educt mixture is reacted in a reactor on a catalyst to a reaction mixture comprising low-molecular olefins and gasoline hydrocarbons, which in a first separating device is separated into a mixture rich in C5? olefins, a mixture rich in C5+ gasoline hydrocarbons, and an aqueous phase. To increase the yield of propylene the mixture rich in C5+ gasoline hydrocarbons is supplied to a second separating device, in which the aromatics contained in the mixture are separated. The residual stream largely free from aromatics is at least partly recirculated to the reactor.

Abstract: An apparatus for producing dimethyl ether by catalytic dehydration of methanol and by distillation of the dehydration product includes a first DME reactor having at least a first reaction stage and a last reaction stage connected in series, the first reaction stage being configured to at least partially perform catalytic dehydrogenation of methanol. A cooling apparatus is disposed between at least the first reaction stage and the last reaction stage and is configured to cool a reaction mixture conveyed from the first reaction stage disposed upstream of said cooling apparatus. A DME column is disposed downstream of, and operatively coupled to, the last reaction stage and is configured to separate dimethyl ether from the reaction mixture conveyed from the last reaction stage. A methanol column is also operatively coupled to a bottom of the DME column and is configured to separate the dimethyl-free reaction mixture into methanol and water.

Abstract: The present disclosure relates to a method and apparatus for producing dimethyl ether by catalytic dehydration of methanol and by distillation of the dehydration product. The method is characterized in that the catalytic dehydration takes place in at least two reaction stages which are connected in series and of which at least the first reaction stage is operated adiabatically, wherein a cooling of the reaction products takes place at least between the first and the second reaction stages.

Abstract: The present disclosure relates to a method and apparatus for producing dimethyl ether by catalytic dehydration of methanol and by distillation of the dehydration product. The method is characterized in that the catalytic dehydration takes place in at least two reaction stages which are connected in series and of which at least the first reaction stage is operated adiabatically, wherein a cooling of the reaction products takes place at least between the first and the second reaction stages.

Abstract: For the production of olefins from dimethyl ether gaseous dimethyl ether in a purity of 70-100 wt-% together with recycle gas, which contains olefinic, paraffinic and/or aromatic hydrocarbons, as well as steam is charged to a first catalyst stage of a re actor. To render the temperature profile over the catalyst stages as flat as possible, but close to the optimum operating temperature, gaseous dimethyl ether in a purity of 70-100 wt-% together with recycle gas, which contains olefinic, paraffinic and aromatic hydrocarbons, is charged to at least one downstream catalyst stage, wherein this downstream catalyst stage additionally is fed with product gas from the upstream catalyst stage.

Abstract: A reactor is described for the production of C2 to C8 olefins from gaseous oxygenate and H2O and one or more material flows containing C2 C4, C5, C6, C7, C8 olefin and paraffin at 400° to 470° C., wherein several reaction stages which the material flow can pass through from the top to the bottom, each consisting of a support base with a catalyst layer situated on it, are arranged in a closed, upright container.

Abstract: For the production of hydrocarbons, in particular C2-C4 olefins, using a combined plant with a steam cracker and at least one reactor for converting an educt mixture which includes steam and at least one oxygenate, the respective intermediate product streams of the steam cracker and of the reactor are at least partly combined. To increase the yield of valuable products, a shape-selective zeolite material is used as catalyst in the reactor for oxygenate conversion and at least a part of the product streams obtained downstream of the combined plant is recirculated to the steam cracker and/or the reactor.

Abstract: The invention relates to a reactor for the production of C2 to C8 olefins from gaseous oxygenate and H2O and one or more material flows containing C2 C4, C5, C6, C7, C8 olefin and paraffin at 400° to 470° C., wherein several reaction stages which the material flow can pass through from the top to the bottom, each consisting of a support base with a catalyst layer situated on it, are arranged in a closed, upright container.

Abstract: In producing C2-C4 olefins, in particular propylene, from an educt mixture containing steam and oxygenates, such as methanol and/or dimethyl ether, the educt mixture is reacted in a reactor on a catalyst to a reaction mixture comprising low-molecular olefins and gasoline hydrocarbons, which in a first separating device is separated into a mixture rich in C5? olefins, a mixture rich in C5+ gasoline hydrocarbons, and an aqueous phase. To increase the yield of propylene the mixture rich in C5+ gasoline hydrocarbons is supplied to a second separating device, in which the aromatics contained in the mixture are separated. The residual stream largely free from aromatics is at least partly recirculated to the reactor.

Abstract: Disclosed is a method for the production of synthetic fuels, wherein, in a first step, a gas mixture consisting of methanol and/or dimethyl ether and/or another oxygenate and water vapor is reacted at temperatures of 300-600° C. in order to form olefins with, preferably, 268 carbon atoms. In a second step, the olefin mixture thus obtained is oligomerized at an elevated pressure to form higher olefins with predominantly more than 5, preferably 10-20 carbon atoms. According to said method, a) the production of olefins in the first step is carried out in the presence of a gas flow which essentially consists of saturated hydrocarbons which are separated from the product flow of the second step and returned to the first step, and (b) the production of olefins is carried out in the second step in the presence of a flow of water vapor which is separated from the product flow of the first step and returned to the first step.

Abstract: In a method for the production of propylene, a charge stream containing C4 to C6 olefins is evaporated, superheated, mixed with hot water vapor, the olefins vapor mixture converted on a zeolite catalyst, the reaction mixture formed thereby cooled, and then partially condensed. In order to increase the yield of propylene, the gaseous phase containing ethylene, propylene, C4 to C8 olefins, and additional hydrocarbons that is accumulated during the partial condensation is compressed, the gaseous and liquid phase containing propylene, ethylene, and other light hydrocarbons that exit from the compression step is separated into a gaseous phase containing propylene, ethylene, and other light hydrocarbons and a liquid phase containing C4+ olefins, and the liquid phase is separated into a fraction containing C4 to C6 olefins and a fraction containing C7+ olefins.

Abstract: In a method for the production of propylene, a charge stream containing C4 to C6 olefins is evaporated, superheated, mixed with hot water vapor, the olefins vapor mixture converted on a zeolite catalyst, the reaction mixture formed thereby cooled, and then partially condensed. In order to increase the yield of propylene, the gaseous phase containing ethylene, propylene, C4 to C8 olefins, and additional hydrocarbons that is accumulated during the partial condensation is compressed, the gaseous and liquid phase containing propylene, ethylene, and other light hydrocarbons that exit from the compression step is separated into a gaseous phase containing propylene, ethylene, and other light hydrocarbons and a liquid phase containing C4+ olefins, and the liquid phase is separated into a fraction containing C4 to C6 olefins and a fraction containing C7+ olefins.

Abstract: The granular, form-selective zeolite catalyst used as bed in a process of producing lower olefins from a feed mixture of higher olefins must be decoked from time to time. This is effected such that the reactor is rinsed with a nitrogen stream heated to 460 to 500° C. for expelling the hydrocarbons, the reactor is then cooled with a nitrogen stream heated to 420 to <460° C., a nitrogen/air mixture heated to 460 to 500° C. then flows through the reactor until complete decoking, and subsequently the reactor is rinsed with a nitrogen stream heated to 460 to 500° C.