The invention relates to isomerization catalysts and can be used in the petroleum processing and petrochemical industry. The catalyst contains sulfated zirconium oxide and a binderaluminum oxide in a ratio of ZrO2/SO4 to Al2O3 from 70 to 30 to 90 to 10, as well as promoter, a group II metal, Ca, in a quantity ranging from 0.01 to 1 wt % of the weight of the catalyst. The catalyst also contains platinum and/or palladium in a quantity ranging from 0.1 to 0.45 wt % of the metal. Isomerization of C4-C7 paraffinic hydrocarbons in the presence of hydrogen at a temperature of 110-200 C., a pressure of 1-5 MPa, a hydrogen:hydrocarbon ratio of 0.5-4, and a feedstock space velocity of 0.5-4 h.sup.1 is carried out on a catalyst having the claimed composition. The proposed catalyst offers an enhanced degree of isomerization, improved selectivity of the process, and increased strength of the granules.

The invention relates to isomerization catalysts and can be used in the petroleum processing and petrochemical industry. The catalyst contains sulfated zirconium oxide and a binderaluminum oxide in a ratio of ZrO2/SO4 to Al2O3 from 70 to 30 to 90 to 10, as well as promoter, a group II metal, Ca, in a quantity ranging from 0.01 to 1 wt % of the weight of the catalyst. The catalyst also contains platinum and/or palladium in a quantity ranging from 0.1 to 0.45 wt % of the metal. Isomerization of C4-C7 paraffinic hydrocarbons in the presence of hydrogen at a temperature of 110-200 C., a pressure of 1-5 MPa, a hydrogen:hydrocarbon ratio of 0.5-4, and a feedstock space velocity of 0.5-4 h.sup.1 is carried out on a catalyst having the claimed composition. The proposed catalyst offers an enhanced degree of isomerization, improved selectivity of the process, and increased strength of the granules.

A method for modification of pretreated acidic porous material via selective cation exchange using suitable solvent to obtain higher noble metal dispersion is described herein. The solvent system required for cation exchange should have its dielectric constant in the range of 25-45, wherein this solvent property is found to impart significant effect on cation loading and distribution, which in turn defines the stability, dispersion of the noble metals. The catalyst so obtained has higher noble metal dispersion and when used for hydroisomerization reaction, leads to higher selectivity even at significantly high conversion values.

A process and system is provided including hydroisomerization reaction zone for production of high octane gasoline blending components that provide high selectivity for producing high octane isomers of light paraffins. A light paraffin feed is enriched by incorporation of dissolved hydrogen, thereby permitting a reaction phase that is liquid or substantially liquid to produce high octane gasoline blending components. Accordingly, a substantially two phase isomerization reactor system is provided, with a hydrogen-enriched liquid feedstock phase and a solid phase catalyst.

The present invention relates to a process and a device for the conversion of aromatic compounds, in which the aromatic compounds of a hydrocarbon feedstock (1) comprising aromatic compounds containing 9 carbon atoms are isomerized in an isomerization unit (A) in the presence of a bifunctional isomerization catalyst having a hydro/dehydrogenating function and a hydroisomerizing function, to produce an isomerization effluent (10) enriched in trimethylbenzenes. The present invention also relates to a process and a device for the production of aromatic compounds, comprising the process and the device for the conversion of aromatic compounds.

A method for producing a hydroisomerization catalyst according to the present invention includes: a first step of preparing a catalyst to be treated, which contains a support having a one-dimensional porous structure including a 10-membered ring and at least one metal selected from the group consisting of: group 8 to 10 metals of the periodic table, Mo, and W supported on the hydroisomerization catalyst; and a second step of producing a hydroisomerization catalyst having a carbon content of 0.4 to 2.5% by mass by subjecting the catalyst to be treated to a coking treatment by means of a carbon-containing compound.

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.

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.

An alkylaromatics isomerisation catalyst, which catalyst comprises at least 50 wt % of an inorganic binder; at least 0.01 wt % of a Group VIII metal and 1-9 wt % ZSM-12 zeolite wherein the silica to alumina molar ratio (SAR) of the ZSM-12 zeolite is in the range of from 60 to 200, and a process for the isomerisation of alkylaromatics to provide a reaction mixture, said process comprising contacting a hydrocarbon stream comprising alkylaromatics with such catalyst.

An alkylaromatics isomerisation catalyst, which catalyst comprises at least 50 wt % of an inorganic binder; at least 0.01 wt % of a Group VIII metal and 1-9 wt % ZSM-12 zeolite wherein the silica to alumina molar ratio (SAR) of the ZSM-12 zeolite is in the range of from 60 to 200, and a process for the isomerisation of alkylaromatics to provide a reaction mixture, said process comprising contacting a hydrocarbon stream comprising alkylaromatics with such catalyst.