The present invention provides a process for the preparation of 1,4-butanediol and tetrahydrofuran said process comprising contacting furan with hydrogen and water in the presence of a supported catalytic composition comprising at least one first metal selected from those in groups 8 to 10 of the periodic table and a further metal selected from manganese, molybdenum, niobium and tungsten.

Utilization of CO.sub.2 for the alkylation of aromatic hydrocarbons is one of the green and sustainable routes for the production of valuable alkylated aromatics like xylenes. Aspects of the present invention deal with the development of single-step catalytic process for the production of alkylated aromatics using CO.sub.2 as a carbon source and alkylation reagent and methylcyclohexane as a hydrogen atom donor as well as source of toluene. In presence of the metal functionalized zeolite catalyst, methylcyclohexane undergoes dehydrogenation to produce toluene and hydrogen; hydrogen reacts with CO.sub.2 to form active alkylating species which triggers the alkylation of toluene. Additionally, a novel process is disclosed for the production of xylene-rich alkylated aromatics from methylcyclohexane and CO.sub.2 using single multi-functional catalyst possessing dehydrogenation, hydrogenation and acid functionalities.

A novel catalyst composition and its use in the dehydrogenation of alkanes to olefins. The catalyst comprises a Group VIII noble metal and a metal selected from the group consisting of manganese, vanadium, chromium, titanium, and combinations thereof, on a support. The Group VIII noble metal can be platinum, palladium, osmium, rhodium, rubidium, iridium, and combinations thereof. The support can be silicon dioxide, titanium dioxide, aluminum oxide, silica-alumina, cerium dioxide, zirconium dioxide, magnesium oxide, metal modified silica, silica-pillared clays, silica-pillared micas, metal oxide modified silica-pillared mica, silica-pillared tetrasilicic mica, silica-pillared taeniolite, zeolite, molecular sieve, and combinations thereof. The catalyst composition is an active and selective catalyst for the catalytic dehydrogenation of alkanes to olefins.

A catalyst comprising a Group IIIA metal, a Group VIII noble metal, and an optional promoter metal, on a support selected from silica, alumina, silica-alumina compositions, rare earth modified alumina, and combinations thereof, doped with iron, a Group VIB metal, a Group VB metal, or a combination thereof, offers decreased reactivation time under air soak in comparison with otherwise identical catalysts. Reducing reactivation time may, in turn, reduce costs, both in inventory and capital.

A catalytic composite for a cyclic process of adiabatic, non-oxidative dehydrogenation of an alkane into an olefin, comprising a dehydrogenation catalyst, a semimetal and a carrier supporting the catalyst and the semimetal. During the reduction and/or regeneration stages of the adiabatic process, the semimetal releases heat which can be used to initiate the dehydrogenation reactions, which are endothermic in nature, thereby reducing the need for hot air flow and combustion of coke as heat input. The semi-metal is inert towards the dehydrogenation reaction itself, alkane feed and olefin product as well as other side reactions of the cyclic process such as cracking and decoking.

Processes for producing mono-methyl alkylbenzenes from natural oils are described. The processes includes a linear selective cracking process to crack C14+ chains into C9 to C14 chains which are useful for making linear alkylbenzene for use in detergents and a hydroisomerization step to produce paraffins with mono-methyl branching which can be reacted with benzene to form the mono-methyl alkyl benzenes.

Catalysts for the hydrogenolysis of butane are described. A supported catalyst for hydrogenolysis of butane to ethane can include a support and a catalytic crystalline bimetallic composition that can include a molybdenum-iridium (MoIr) crystalline composition attached to the support. The supported catalyst has a BET specific surface area of at least 100 m.sup.2/g, preferably 100 m.sup.2/g to 500 m.sup.2/g. Method of use and methods of making the catalyst are also described.

Producing a product hydrocarbon includes subjecting a feed mixture containing a feed hydrocarbon and oxygen to selective oxidation to obtain a product mixture containing product hydrocarbon and water. A subsequent mixture is formed from a portion of the product mixture by separating a portion of the water. Oxygen in the feed mixture is partially converted during the selective oxidation, so that the product mixture has a first residual oxygen content and the subsequent mixture has a second residual oxygen content. Detection of the first and/or the second residual oxygen content is performed using a first measuring device. A second measuring device at the end of the catalyst bed detects temperature. Using a process control and/or evaluation unit, measurement data of the first and/or second measuring device(s) are detected and are evaluated and/or processed while obtaining follow-up data. Process control is carried out on the basis of the follow-up data.

A process for producing an ether including treating (a) an ester with (b) hydrogen in the presence of (c) a heterogeneous catalyst to reduce the ester by hydrogenation to form an ether product.