The present invention relates to a process for preparing cyclohexane by isomerizing a hydrocarbon mixture (HM1) comprising methylcyclopentane (MCP) in the presence of a catalyst. The catalyst is preferably an acidic ionic liquid. The starting material used is a stream (S1) which originates from a steamcracking process. The hydrocarbon mixture (HM1) obtained from this stream (S1) in an apparatus for aromatics removal has a reduced aromatics content compared to stream (S1), and (HM1) may optionally also be (virtually) free of aromatics. Depending on the type and amount of the aromatics remaining in the hydrocarbon mixture (HM1), especially in the case that benzene is present, the isomerization may additionally be preceded by performance of a hydrogenation of (HM1). In addition, depending on the presence of other components of (HM1), further purification steps may optionally be performed prior to or after the isomerization or hydrogenation. High-purity (on-spec) cyclohexane is preferably isolated from the hydrocarbon mixture (HM2) obtained in the isomerization, the specifications being, for example, those applicable to the use of the cyclohexane for the preparation, known to those skilled in the art, of caprolactam.

A method for producing a linear hydrocarbon, including reacting a linear aliphatic aldehyde in the presence of at least one metal ion selected from the group consisting of a vanadium ion, a manganese ion, an iron ion, a cobalt ion, an iridium ion, a copper ion, and a thallium ion.

The present disclosure provides methods to produce para-xylene, toluene, and other compounds from renewable sources (e.g., cellulose, hemicellulose) and ethylene in the presence of an acid, such as a Lewis acid. For example, cellulose and/or hemicellulose may be converted into 2,5-dimethylfuran (DMF) and 2-methylfuran, which may be converted into para-xylene and toluene, respectively. In particular, para-xylene can then be oxidized to form terephthalic acid.

The present invention relates to a process for preparing cyclohexane from methylcyclopentane (MCP) and benzene. In the context of the present invention, MCP and benzene are constituents of a hydrocarbon mixture (HM1) additionally comprising dimethylpentanes (DMP), possibly cyclohexane and possibly at least one compound (low boiler) selected from acyclic C.sub.5-C.sub.6-alkanes and cyclopentane. First of all, benzene is converted in a hydrogenation step to cyclohexane (that present in the hydrocarbon mixture (HM2)), while MCP is isomerized in the presence of a catalyst, preferably of an acidic ionic liquid, to cyclohexane. After the hydrogenation but prior to the isomerization the dimethylpentanes (DMP) are removed, with initial removal of the cyclohexane present in the hydrocarbon mixture (HM2) together with DMP. This cyclohexane already present prior to the isomerization can be separated again from DMP in a downstream rectification step and isolated and/or recycled into the process for cyclohexane preparation. Between the DMP removal and MCP isomerizationif low boilers are present in the hydrocarbon mixture (HM1)low boilers are, optionally removed. After the isomerization, the cyclohexane is isolated, optionally with return of unisomerized MCP and optionally of low boilers. Preferably, cyclohexane and/or low boilers are present in the hydrocarbon mixture (HM1), and so a low boiler removal is preferably conducted between the DMP removal from isomerization. It is additionally preferable that the removal of the cyclohexane from DMP is additionally conducted, meaning that the cyclohexane component which arises in the benzene hydrogenation and may be present in the starting mixture (HM1) is isolated and hence recovered.

A self-metathesis process for the production of unsaturated dicarboxylic fatty diacids and/or unsaturated dicarboxylic fatty diesters, wherein unsaturated carboxylic fatty acids and/or esters of unsaturated carboxylic fatty acids are reacted in the presence of at least one defined ruthenium based catalyst compound. A catalyst enhancer compound selected from a sacrificial catalyst or a non-catalyst enhancer may also be used. The process exhibits improved reaction times and/or the catalyst can be used at very low concentrations.

The present invention relates to a method for preparing an iodine-doped TiO.sub.2 nano-catalyst and use of the catalyst in heterogeneously catalyzing configuration transformation of trans-carotenoids. The iodine-doped TiO.sub.2 nano-catalyst is prepared by a sol-gel process using a titanate ester as a precursor and an iodine-containing compound as a dopant in the presence of a diluent, inhibitor and complexing agent. The catalyst exhibits high activity for isomerization of the trans-carotenoids into their cis-isomers within a short catalytic time. The catalyst can be easily prepared and is highly efficient, economical, recyclable and environmentally friendly.

The present invention relates to a process for preparing cyclohexane from methylcyclopentane (MCP) and benzene. In the context of the present invention, MCP and benzene are constituents of a hydrocarbon mixture (HM1) additionally comprising dimethylpentanes (DMP), possibly cyclohexane and possibly at least one compound (low boiler) selected from acyclic C.sub.5-C.sub.6-alkanes and cyclopentane. First of all, benzene is converted in a hydrogenation step to cyclohexane (that present in the hydrocarbon mixture (HM2)), while MCP is isomerized in the presence of a catalyst, preferably of an acidic ionic liquid, to cyclohexane. After the hydrogenation but prior to the isomerization the dimethylpentanes (DMP) are removed, with initial removal of the cyclohexane present in the hydrocarbon mixture (HM2) together with DMP. This cyclohexane already present prior to the isomerization can be separated again from DMP in a downstream rectification step and isolated and/or recycled into the process for cyclohexane preparation. Between the DMP removal and MCP isomerizationif low boilers are present in the hydrocarbon mixture (HM1)low boilers are, optionally removed. After the isomerization, the cyclohexane is isolated, optionally with return of unisomerized MCP and optionally of low boilers. Preferably, cyclohexane and/or low boilers are present in the hydrocarbon mixture (HM1), and so a low boiler removal is preferably conducted between the DMP removal from isomerization. It is additionally preferable that the removal of the cyclohexane from DMP is additionally conducted, meaning that the cyclohexane component which arises in the benzene hydrogenation and may be present in the starting mixture (HM1) is isolated and hence recovered.

A process of metathesizing a feedstock in the presence of a metathesis catalyst and at least one catalyst enhancer. The catalyst enhancer can be selected from a sacrificial catalyst or a non-catalyst enhancer. The process exhibits improved reaction times and/or the metathesis catalyst can be used at very low concentrations.

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.1 to 5 in.sup.1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.1)(gal.sup.1) to 6.0 (lb)(hr.sup.1)(gal.sup.1).

C.sub.20 trisubstituted olefins are produced from C.sub.20 2-substituted alpha olefins, which are produced from branched C.sub.10 olefins.