Catalysts are disclosed having metal oxide support structures and acidic reaction sites. The reaction sites may be according to the general formula M.sub.xO.sub.yAlBr.sub.zX].sup.H.sup.+ where x is one or two; y is one or two; z is one or two; X is selected from Br or Cl; M is Al or Si and one or more of M, O and Al has a molecular bond with the metal oxide support structure.

A method includes brominating a butanes feed stream including i-butane in a bromination reactor to form a bromination effluent stream including t-butyl bromide. The method includes dehydrobrominating the t-butyl bromide to form isobutylene. Another method includes brominating a mixed pentanes feed stream including i-pentane and n-pentane in a bromination reactor to form a bromination effluent stream including t-pentyl bromide. The method includes dehydrobrominating the t-pentyl bromide to form isoamylene and HBr.

A method includes brominating a butanes feed stream including i-butane in a bromination reactor to form a bromination effluent stream including t-butyl bromide. The method includes dehydrobrominating the t-butyl bromide to form isobutylene. Another method includes brominating a mixed pentanes feed stream including i-pentane and n-pentane in a bromination reactor to form a bromination effluent stream including t-pentyl bromide. The method includes dehydrobrominating the t-pentyl bromide to form isoamylene and HBr.

Catalysts are disclosed having metal oxide support structures and acidic reaction sites. The reaction sites may be according to the general formula M.sub.xO.sub.yAlBr.sub.zX].sup.H.sup.+ where x is one or two; y is one or two; z is one or two; X is selected from Br or Cl; M is Al or Si and one or more of M, O and Al has a molecular bond with the metal oxide support structure.

A process of tuning a hydrocarbon product composition is described. The process involves selecting paraffins for reaction. The equilibrium constants for reactions of the selected paraffins can be used to select appropriate feed ratios, or an equilibrium composition as function of C/H molar ratio. A selected feed is reacted to obtain the product. Equilibrium product compositions and non-equilibrium product compositions can be obtained using the process.

A method includes brominating a butanes feed stream including i-butane in a bromination reactor to form a bromination effluent stream including t-butyl bromide. The method includes dehydrobrominating the t-butyl bromide to form isobutylene. Another method includes brominating a mixed pentanes feed stream including i-pentane and n-pentane in a bromination reactor to form a bromination effluent stream including t-pentyl bromide. The method includes dehydrobrominating the t-pentyl bromide to form isoamylene and HBr.

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.

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.

Disclosed herein are embodiments of a process which generally includes contacting i) a monomer or mixture of monomers, ii) a haloaluminate ionic liquid, and iii) one or more halide components in a reaction zone, and oligomerizing the monomer or mixture of monomers in the reaction zone to form an oligomer product. The combination of the haloaluminate ionic liquid and halide component can constitute a catalyst system which is used in embodiments of the process to produce the oligomer product.