A method for producing para-xylene (PX) includes introducing a C8 aromatic-containing composition to a xylene rerun column to separate the C8 aromatic-containing composition into a xylene-containing effluent and a heavy effluent and passing the xylene-containing effluent to a PX processing loop that includes a PX recovery unit operable to separate a PX product from the xylene-containing effluent, a membrane isomerization unit operable to convert a portion of the MX, OX, or both from the xylene-containing effluent to PX, an EB dealkylation unit operable to dealkylate EB from the xylene-containing effluent to produce benzene, toluene, and other C.sub.7 compounds, and a membrane separation unit operable to produce a permeate that is PX-rich and a retentate that is PX-lean. The permeate is passed to the PX recovery unit for recovery of PX, which the retentate is bypassed around the PX recovery unit circulated through the xylene processing loop.

A method for producing para-xylene (PX) includes introducing a C8 aromatic-containing composition to a xylene rerun column to separate the C8 aromatic-containing composition into a xylene-containing effluent and a heavy effluent and passing the xylene-containing effluent to a PX processing loop that includes a PX recovery unit operable to separate a PX product from the xylene-containing effluent, a membrane isomerization unit operable to convert a portion of the MX, OX, or both from the xylene-containing effluent to PX, an EB dealkylation unit operable to dealkylate EB from the xylene-containing effluent to produce benzene, toluene, and other C.sub.7 compounds, and a membrane separation unit operable to produce a permeate that is PX-rich and a retentate that is PX-lean. The permeate is passed to the PX recovery unit for recovery of PX, which the retentate is bypassed around the PX recovery unit circulated through the xylene processing loop.

Processes and apparatus for making xylenes and phenol are described. Phenol and alkyl phenols are separated from coal derived liquid. The phenol is separated from the alkyl phenols. The alkyl phenols can be reacted with aromatics such as benzene and toluene to make xylenes. The xylenes and other aromatics are then separated from the phenol and alkyl phenols. Para-xylene is separated and recovered using a xylene separation process, and meta-xylene and ortho-xylene are optionally converted to para-xylene through an isomerization reaction.

Processes and apparatus for making xylenes and phenol are described. Phenol and alkyl phenols are separated from coal derived liquid. The phenol is separated from the alkyl phenols. The alkyl phenols can be reacted with aromatics such as benzene and toluene to make xylenes. The xylenes and other aromatics are then separated from the phenol and alkyl phenols. Para-xylene is separated and recovered using a xylene separation process, and meta-xylene and ortho-xylene are optionally converted to para-xylene through an isomerization reaction.

Provided is a hybrid process for producing high-purity para-xylene from a feedstock of aromatic hydrocarbon isomer fractions having 8 carbon atoms, in a liquid phase. The process includes a liquid chromatography separation step and a crystallization step of the para-xylene from the purified stream of para-xylene obtained at the separation step.

Provided is a hybrid process for producing high-purity para-xylene from a feedstock of aromatic hydrocarbon isomer fractions having 8 carbon atoms, in a liquid phase. The process includes a liquid chromatography separation step and a crystallization step of the para-xylene from the purified stream of para-xylene obtained at the separation step.

Provided is a hybrid process for producing high-purity para-xylene from a feedstock of aromatic hydrocarbon isomer fractions having 8 carbon atoms, in a liquid phase. The process includes a liquid chromatography separation step and a crystallization step of the para-xylene from the purified stream of para-xylene obtained at the separation step.

A diamondoid fuel comprising a cage structure including 10, 14, 18, or 22 carbons. The diamondoid fuel also includes one of one to four cyclopropyl groups bonded to the cage structure or two to four functional groups bonded to the cage structure where the functional groups are an alkyl group, an allyl group, a cyclopropyl group, or combinations thereof. Additionally, at least one functional group is an allyl group and at least one functional group is a cyclopropyl group.

In a process for separating dimethyl biphenyl isomers a mixture comprising one or more 3,3, 3,4- or 4,4-dimethyl biphenyl isomers, one or more 2,X-dimethyl biphenyl isomers (where X=2, 3, or 4) and one or more further hydrocarbon components is contacted with a first adsorbent, thereby selectively adsorbing one or more of the dimethyl biphenyl isomers within the first adsorbent. A first raffinate stream containing less selectively adsorbed components is withdrawn from the first adsorbent and a first extract stream containing selectively adsorbed dimethyl biphenyl isomers is withdraw. The selectively adsorbed dimethyl biphenyl isomers comprise one or more of 3,3-, 3,4- or 4,4-dimethyl biphenyl isomers and one or more of 2,X-dimethyl biphenyl isomers (where X=2, 3, or 4).

In a process for separating dimethyl biphenyl isomers a mixture comprising one or more 3,3, 3,4- or 4,4-dimethyl biphenyl isomers, one or more 2,X-dimethyl biphenyl isomers (where X=2, 3, or 4) and one or more further hydrocarbon components is contacted with a first adsorbent, thereby selectively adsorbing one or more of the dimethyl biphenyl isomers within the first adsorbent. A first raffinate stream containing less selectively adsorbed components is withdrawn from the first adsorbent and a first extract stream containing selectively adsorbed dimethyl biphenyl isomers is withdraw. The selectively adsorbed dimethyl biphenyl isomers comprise one or more of 3,3-, 3,4- or 4,4-dimethyl biphenyl isomers and one or more of 2,X-dimethyl biphenyl isomers (where X=2, 3, or 4).