Disclosed is a process for recovering paraxylene in which a first simulated moving bed adsorption unit is used to produce two extract streamsone rich in paraxylene and a paraxylene-rich extract stream that is lean in ethylbenzene and an ethylbenzene-rich extract stream that is lean in paraxylene- and a paraxylene-depleted raffinate stream. A significant amount of the ethylbenzene is removed in the ethylbenzene-rich extract stream (at least enough to limit buildup in the isomerization loop), so the paraxylene-depleted raffinate stream may be isomerized in the liquid phase. Avoiding vapor phase isomerization saves energy and capital, as liquid phase isomerization requires less energy and capital than the vapor phase isomerization process due to the requirement of vaporizing the paraxylene-depleted stream and the use of hydrogen, which requires an energy and capital intensive hydrogen recycle loop.

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.

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.

The present invention provides a process for preparing a zeolite by hydrothermal heating of silica precursor and alumina precursor along with a combination of two structure-directing organic templates, N,N-dimethyl formamide and 1,6-diaminohexane in the presence of an alkali. The use of two structure-directing organic templates, not only reduces the crystallization time but also enables the preparation of more catalytically active ZSM-22 of submicron crystallite size. The present invention also provides a process of preparing a noble metal containing zeolite catalyst for hydroisomerization of long chain n-paraffins.

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating neohexane and/or neoheptane to produce neopentane. The neohexane and/or neoheptane may be provided by the isomerization of C.sub.6-C.sub.7 paraffins.

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating neohexane and/or neoheptane to produce neopentane. The neohexane and/or neoheptane may be provided by the isomerization of C.sub.6-C.sub.7 paraffins.

Systems and methods of producing olefins via catalytic cracking are disclosed. Hydrocarbons of a naphtha stream are isomerized by converting straight chain Cn hydrocarbons to branched Cn hydrocarbons, thereby forming an isomerized naphtha stream. The isomerized naphtha stream is subsequently fed to a catalytic cracking unit such that the hydrocarbons of the isomerized naphtha stream form olefins. In the catalytic cracking process, the reaction temperature can be kept lower than 680? C., thereby increasing the reactivity and minimizing catalyst deactivation in the catalytic cracking process.

Disclosed herein are processes for recovering paraxylene in which a first simulated moving bed adsorption unit is used to produce a paraxylene-rich extract stream that also contains a significant amount of the ethylbenzene and a paraxylene-depleted raffinate stream. Because a significant amount of the ethylbenzene is removed in the paraxylene-rich extract stream (at least enough to limit buildup in the isomerization loop), the paraxylene-depleted raffinate stream may be isomerized in the liquid phase. Avoiding vapor phase isomerization saves energy and capital, as liquid phase isomerization requires less energy and capital than the vapor phase isomerization process due to the requirement of vaporizing the paraxylene-depleted stream and the use of hydrogen, which requires an energy- and capital-intensive hydrogen recycle loop.

Disclosed herein are processes for recovering paraxylene in which a first simulated moving bed adsorption unit is used to produce a paraxylene-rich extract stream that also contains a significant amount of the ethylbenzene and a paraxylene-depleted raffinate stream. Because a significant amount of the ethylbenzene is removed in the paraxylene-rich extract stream (at least enough to limit buildup in the isomerization loop), the paraxylene-depleted raffinate stream may be isomerized in the liquid phase. Avoiding vapor phase isomerization saves energy and capital, as liquid phase isomerization requires less energy and capital than the vapor phase isomerization process due to the requirement of vaporizing the paraxylene-depleted stream and the use of hydrogen, which requires an energy- and capital-intensive hydrogen recycle loop.

A liquid phase isomerization process comprising cofeeding molecular hydrogen at a feeding rate ?100 ppm by weight can effectively convert a C8 aromatic hydrocarbon isomerization feed in the presence of an isomerization catalyst with a very low deactivation rate of the catalyst, even at high WHSV ?5 hour.sup.?1.