Abstract: There is proposed a process for producing short-chain olefins by conversion of oxygenates in a multi-stage fixed-bed reactor (OTO reactor) with reaction zones each operated adiabatically, in which the individual stages or reaction zones are covered with beds of a granular, form-selective zeolite catalyst which previously has been subjected to a steam pretreatment in an external, isothermally or quasi-isothermally operated steam pretreatment reactor. By means of the external steam pretreatment according to the invention, higher lifetimes of the catalyst used are obtained as compared to a steam pretreatment in the OTO reactor. The availability of the OTO reactor for the olefin production is increased.

Abstract: In a process for producing synthetic fuels from an educt mixture containing hydrogen and oxygenates, such as methanol and/or dimethyl ether, the educt mixture is reacted on a catalyst in a first process stage to obtain a hydrocarbon product containing olefins with preferably 2 to 8 carbon atoms. In a second process stage the hydrocarbon product is oligomerized to long-chain olefins, from which gasoline and Diesel products are obtained. The hydrocarbon product obtained in the first process stage is separated into a liquid phase and a gaseous phase. The gaseous phase is supplied to the second process stage. The liquid phase is separated into a mixture rich in C6? hydrocarbons and a mixture containing C7+ hydrocarbons and aromatics. The mixture rich in C6? hydrocarbons is supplied to the second process stage. The mixture containing C7+ hydrocarbons ?+ and aromatics can be admixed to the gasoline product for quality improvement.

Abstract: In a process for producing synthetic fuels from an educt mixture containing hydrogen and oxygenates, such as methanol and/or dimethyl ether, the educt mixture is reacted on a catalyst in a first process stage to obtain a hydrocarbon product containing olefins with preferably 2 to 8 carbon atoms. In a second process stage the hydrocarbon product is oligomerized to long-chain olefins, from which gasoline and Diesel products are obtained. The hydrocarbon product obtained in the first process stage is separated into a liquid phase and a gaseous phase. The gaseous phase is supplied to the second process stage. The liquid phase is separated into a mixture rich in C6? hydrocarbons and a mixture containing C7+ hydrocarbons and aromatics. The mixture rich in C6? hydrocarbons is supplied to the second process stage. The mixture containing C7+ hydrocarbons ?+ and aromatics can be admixed to the gasoline product for quality improvement.

Abstract: In the presence of a catalyst, at least one isoparaffin having 4 to 6 C atoms per molecule is reacted with at least one olefin having 2 to 6 C atoms per molecule in a liquid phase to obtain a product containing alkylate, a suspension containing isoparaffin and a granular zeolite catalyst being supplied to the upper region of a reaction column. Below the point where the catalyst-containing suspension is supplied, an isoparaffin-olefin mixture is introduced into the reaction column, the temperatures in the reaction column being maintained in the range from 50 to 120° C. From the bottom region of the reaction column a product mixture containing alkylate is withdrawn, and in a separation by distillation alkylate product is recovered therefrom. Preferably, isoparaffin and catalyst are recovered from the separation by distillation and at least partly recirculated to the upper region of the reaction column.

Abstract: In the presence of a catalyst, at least one isoparaffin having 4 to 6 C atoms per molecule is reacted with at least one olefin having 2 to 6 C atoms per molecule in a liquid phase to obtain a product containing alkylate, a suspension containing isoparaffin and a granular zeolite catalyst being supplied to the upper region of a reaction column. Below the point where the catalyst-containing suspension is supplied, an isoparaffin-olefin mixture is introduced into the reaction column, the temperatures in the reaction column being maintained in the range from 50 to 120° C. From the bottom region of the reaction column a product mixture containing alkylate is withdrawn, and in a separation by distillation alkylate product is recovered therefrom. Preferably, isoparaffin and catalyst are recovered from the separation by distillation and at least partly recirculated to the upper region of the reaction column.