Hydrocarbon processing apparatuses and processes for producing n-pentane and isobutane are provided herein. In an embodiment, a process for producing n-pentane and isobutane includes providing a hydrocarbon feed stream that includes C4 and C5 hydrocarbons. A recycle stream that includes C4+ hydrocarbons and the hydrocarbon feed stream is combined to produce a combined feed stream. The combined feed stream is separated to produce an iC4 product stream, an nC5+ product stream, and an iC5/nC4 feed stream. The iC5/nC4 feed stream is simultaneously disproportionated and isomerized in an isomerization zone to produce an intermediate stream that includes C3-C6 hydrocarbons. The C3-C6 hydrocarbons in the intermediate stream are separated to produce a C3 stream and the recycle stream that includes C4+ hydrocarbons.

A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of C.sub.4 and C.sub.7 paraffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of C.sub.4 and C.sub.7 paraffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of C.sub.4 and C.sub.7 paraffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

The invention concerns an alkane metathesis catalyst, its production and use. The catalyst comprises a Group V, VI or VII metal alkyl with the metal in its highest oxidation state, preferably Ta or W, and the alkyl of C1-C4, preferably together with alkylidene and/or alkylidyne ligands, in particular -Me, CH2 and CH, on a metal oxide support, preferably silica partially dehydroxylated at 200 or 700 C. Substrates include cycloalkanes, preferably cyclooctane.

The invention concerns an alkane metathesis catalyst, its production and use. The catalyst comprises a Group V, VI or VII metal alkyl with the metal in its highest oxidation state, preferably Ta or W, and the alkyl of C1-C4, preferably together with alkylidene and/or alkylidyne ligands, in particular -Me, CH2 and CH, on a metal oxide support, preferably silica partially dehydroxylated at 200 or 700 C. Substrates include cycloalkanes, preferably cyclooctane.

The invention concerns an alkane metathesis catalyst, its production and use. The catalyst comprises a Group V, VI or VII metal alkyl with the metal in its highest oxidation state, preferably Ta or W, and the alkyl of C1-C4, preferably together with alkylidene and/or alkylidyne ligands, in particular -Me, CH2 and CH, on a metal oxide support, preferably silica partially dehydroxylated at 200 or 700 C. Substrates include cycloalkanes, preferably cyclooctane.

A circulating fluidized bed reaction regeneration device and its application method are provided. The device includes a fluidized bed reactor, a fluidized bed regenerator and a riser reactor. The fluidized bed reactor is used for introducing a naphtha feedstock and a methanol feedstock, where the naphtha feedstock is brought into contact with a catalyst from the riser reactor, so as to perform a reaction to generate a BTX-containing product gas flow and a spent catalyst, and the methanol feedstock undergoes a methylation reaction with benzene and toluene in the BTX-containing product gas flow to generate p-xylene; the product gas flow is subjected to gas-solid separation, the separated product gas is conveyed to downstream sections, unconverted naphtha is returned as a feedstock to the fluidized bed reactor, part of light alkanes is returned as a feedstock to the riser reactor, and the spent catalyst is introduced into the fluidized bed regenerator.

A circulating fluidized bed reaction regeneration device and its application method are provided. The device includes a fluidized bed reactor, a fluidized bed regenerator and a riser reactor. The fluidized bed reactor is used for introducing a naphtha feedstock and a methanol feedstock, where the naphtha feedstock is brought into contact with a catalyst from the riser reactor, so as to perform a reaction to generate a BTX-containing product gas flow and a spent catalyst, and the methanol feedstock undergoes a methylation reaction with benzene and toluene in the BTX-containing product gas flow to generate p-xylene; the product gas flow is subjected to gas-solid separation, the separated product gas is conveyed to downstream sections, unconverted naphtha is returned as a feedstock to the fluidized bed reactor, part of light alkanes is returned as a feedstock to the riser reactor, and the spent catalyst is introduced into the fluidized bed regenerator.