The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.

A process for dehydrating alkanes in which such feedstock mixtures may be used having a high proportion of olefins, i.e. approximately 1% by weight to 10% by weight. Specifically, alkenes having two to five carbon atoms are generated from alkanes having the same carbon length where the number of carbon atoms not change during by the dehydrogenation. The process is intended to be feasible on an industrial scale. A basic concept of the invention consists of hydrogenating alkenes present in the feedstock to the corresponding alkanes before they come in contact with the dehydrogenation catalyst. This avoids an undesired coke deposit. The hydrogenation is effected by minimal addition of hydrogen (80% to 120% of the stoichiometrically required amount). The hydrogenation is effected either over a dehydrogenation catalyst, or over the dehydrogenation catalyst itself.

A process for dehydrating alkanes in which such feedstock mixtures may be used having a high proportion of olefins, i.e. approximately 1% by weight to 10% by weight. Specifically, alkenes having two to five carbon atoms are generated from alkanes having the same carbon length where the number of carbon atoms not change during by the dehydrogenation. The process is intended to be feasible on an industrial scale. A basic concept of the invention consists of hydrogenating alkenes present in the feedstock to the corresponding alkanes before they come in contact with the dehydrogenation catalyst. This avoids an undesired coke deposit. The hydrogenation is effected by minimal addition of hydrogen (80% to 120% of the stoichiometrically required amount). The hydrogenation is effected either over a dehydrogenation catalyst, or over the dehydrogenation catalyst itself.

A molecular sieve having the framework structure of ZSM-5 is described comprising crystals having an external surface area in excess of 100 m.sup.2/g (as determined by the t-plot method for nitrogen physisorption) and a unique X-ray diffraction pattern.

A molecular sieve having the framework structure of ZSM-5 is described comprising crystals having an external surface area in excess of 100 m.sup.2/g (as determined by the t-plot method for nitrogen physisorption) and a unique X-ray diffraction pattern.

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.

An endothermic catalytic dehydrogenation process conducted in gas phase in system including a reactor with a catalyst bed including an inorganic catalytic material and a first inert material including the steps of: feeding a first stream having an alkane of the formulae I C.sub.nH.sub.2n+1R.sup.1 with n?3 and R.sup.1?H or aryl to be dehydrogenated into the reactor, and simultaneously or subsequently feeding a second stream including a mixture of an inert gas and a reactive gas selected from the group of alkanes of the formulae II C.sub.mH.sub.2m+2 with m?2, or alkenes of the formulae III C.sub.mH.sub.2m with .sub.m?2. The alkane to be dehydrogenated of formulae I in first stream has at least one more carbon atom than the alkane of formulae II and alkene of formulae III in the second stream.

An endothermic catalytic dehydrogenation process conducted in gas phase in system including a reactor with a catalyst bed including an inorganic catalytic material and a first inert material including the steps of: feeding a first stream having an alkane of the formulae I C.sub.nH.sub.2n+1R.sup.1 with n?3 and R.sup.1?H or aryl to be dehydrogenated into the reactor, and simultaneously or subsequently feeding a second stream including a mixture of an inert gas and a reactive gas selected from the group of alkanes of the formulae II C.sub.mH.sub.2m+2 with m?2, or alkenes of the formulae III C.sub.mH.sub.2m with .sub.m?2. The alkane to be dehydrogenated of formulae I in first stream has at least one more carbon atom than the alkane of formulae II and alkene of formulae III in the second stream.