Abstract: A process for the removal of sulfur compounds and benzene of a catalytically cracked petroleum naphtha comprising benzene, organic sulfur compounds and olefins, by fractionating the cracked naphtha into a relatively low boiling range, olefinic, light catalytic naphtha (LCN) and an olefinic heavy catalytic naphtha (HCN) which boils above the range of the LCN the boiling ranges of the LCN and the HCN being defined by a cut point selected to maintain most of the benzene in the cracked naphtha in the LCN together with olefins in the boiling range of the LCN. The LCN is subjected to an optional non-hydrogenative desulfurization step followed by a fixed bed alkylation step in which the benzene in the LCN is alkylated with the olefins contained in this fraction. The HCN is treated by a similar an alkylation step using the olefins contained in this fraction to alkylate the sulfur compounds, forming alkylated products which boil above the gasoline boiling range.

Abstract: Described is an apparatus for, and a method of, recovering linear butenes from a mixed feed comprising providing a first mixed feed comprising linear butenes and isobutene; contacting the first mixed feed with an oligomerization catalyst such as an MWW family zeolite in a first oligomerization reactor to produce a second mixed feed comprising the linear butenes, C8 olefins and higher oligomers, and a reduced amount of isobutene relative to the first mixed feed; and separating the second mixed feed to produce a first effluent of first purified linear butenes, and a second effluent of C8 olefins and higher oligomers. The oligomerization reactor may be a converted isobutene-to-methyl-t-butylether reactor.

Abstract: A process for the production of high octane number gasoline from light refinery olefins, typically from the catalytic cracking unit, and benzene-containing aromatic streams such as reformate. A portion of the light olefins including ethylene and propylene is polymerized to form a gasoline boiling range product and another portion is used to alkylate the light aromatic stream. The alkylation step may be carried out in successive stages with an initial low temperature stage using a catalyst comprising an MWW zeolite followed by a higher temperature stage using a catalyst comprising an intermediate pore size zeolite such as ZSM-5. Using this staged approach, the alkylation may be carried out in the vapor phase. Alternatively, the alkylation may be carried out in the liquid phase using the heavier olefins (propylene, butene) dissolved into the aromatic stream by selective countercurrent extraction; a separate alkylation step using the ethylene not taken up in the extraction is carried out at a higher temperature.

Abstract: A process for the production of high octane number gasoline from light refinery olefins and benzene-containing aromatic streams such as reformate. The process achieves good utilization of both the ethylene and the propylene present in the mixed olefin feed from the unsaturated gas plant while reducing gasoline benzene levels. The light olefins including ethylene and propylene are reacted with the light aromatic stream containing benzene and other single ring aromatic compounds to form a gasoline boiling range product containing akylaromatics. The reaction is carried out with a two-catalyst system which comprises a member of the MWW family of zeolites and an intermediate pore size zeolite such as ZSM-5 using a fixed catalyst bed in both stages. Use of the two catalyst system enables the conversion of the ethylene and propylene components of the olefin feed to be converted to alkylaromatics under favorable conditions.

Abstract: A process for the production of high octane number gasoline from light refinery olefins and benzene-containing aromatic streams such as reformate. Light olefins including ethylene and propylene are extracted from refinery off-gases, typically from the catalytic cracking unit, into a light aromatic stream such as reformate containing benzene and other single ring aromatic compounds which is then reacted with the light olefins to form a gasoline boiling range product containing akylaromatics. The alkylation reaction is carried out in the liquid phase with a catalyst which preferably comprises a member of the MWW family of zeolites such as MCM-22 using a fixed catalyst bed.

Abstract: A process for the removal of sulfur compounds and benzene of a catalytically cracked petroleum naphtha comprising benzene, organic sulfur compounds and olefins, by fractionating the cracked naphtha into a relatively low boiling range, olefinic, light catalytic naphtha (LCN) and an olefinic heavy catalytic naphtha (HCN) which boils above the range of the LCN the boiling ranges of the LCN and the HCN being defined by a cut point selected to maintain most of the benzene in the cracked naphtha in the LCN together with olefins in the boiling range of the LCN. The LCN is subjected to an optional non-hydrogenative desulfurization step followed by a fixed bed alkylation step in which the benzene in the LCN is alkylated with the olefins contained in this fraction. The HCN is treated by a similar an alkylation step using the olefins contained in this fraction to alkylate the sulfur compounds, forming alkylated products which boil above the gasoline boiling range.

Abstract: A method of rejuvenating a deactivated molecular sieve catalyst, deactivated by use in an olefin oligomerization or aromatics alkylation process, which method comprises contacting the deactivated catalyst with a stream of rejuvenation gas comprising a hydrocarbon product fraction from the process at an elevated temperature and pressure for a time sufficient to effect an increase in catalytic activity of the deactivated catalyst.

Abstract: A process for the regeneration of materials used in the guard beds preceding the reactors used in an olefin conversion process which converts olefinic refinery streams to higher boiling hydrocarbon products by polymerization (oligomerization) or alkylation of aromatics including benzene. Products of the process may include olefin oligomers and alkylaromatics in the gasoline boiling range as well as alkylaromatic petrochemicals such as cumene and ethylbenzene. The process is integrated with the olefin conversion process to ensure continuous operation of the olefin conversion without sending the feedstock containing the contaminant(s) to the reactor. The process uses reaction products from the olefin conversion process to regenerate the guard bed material and so is economically attractive since it does not require the use of separate purge, regeneration feed and separation systems. A plurality of guard beds is used, each containing a material which removes catalyst poisons.

Abstract: A process unit for the zeolite-catalyzed conversion of light refinery olefins from an FCC unit such as ethylene, propylene, and butylene to gasoline boiling range motor fuels comprises at least two sequential, serially connected reactors connected in parallel to a fractionation section with at one or two fractionators for separating the reactor effluents into product fraction with an optional recycle stream or streams. The configurations according to this scheme allow the adjustment of reactor temperature and/or pressure and/or space velocity to be based on the reactivities of the olefin compounds present in the LPG streams so that the gasoline produced in each reactor will be separated immediately, to reduce over-polymerization of the gasoline in the low severity reactor and to ensure that gasoline formed in the low severity reactor will not be sent to the higher severity reactor e.g.

Abstract: A sulfated solid catalyst is provided which comprises (1) oxide or hydroxide of Group III or Group IV element, e.g. zirconium, and (2) a first metal comprising a metal or combination of metals selected from the group consisting of platinum, palladium, nickel, platinum and rhenium, and platinum and tin. The catalyst may further comprise (3) a second metal selected from the group consisting of Group VIII elements, e.g. iron. One embodiment of the invention further comprises (4) a third metal selected from the group consisting of Group V, VI and VII elements, e.g. manganese. The catalyst of the invention is useful for the isomerization of normal alkanes having 4 to 40 carbon atoms per molecule, for the naphtha upgrading of a hydrocarbon feedstock and for the hydrocracking of a hydrocarbon feedstock.

Abstract: An isomerization process is provided which process utilizes a sulfated solid catalyst comprising (1) oxide or hydroxide of Group III or Group IV element, e.g. zirconium, and (2) a first metal comprising a metal or combination of metals selected from the group consisting of platinum, palladium, nickel, platinum and rhenium, and platinum and tin. The sulfated support is calcined prior to incorporation of the first metal and subsequent to said incorporation. The catalyst may further comprise (3) a second metal selected from the group consisting of Group VIII elements, e.g. iron. One embodiment of the invention further comprises (4) a third metal selected from the group consisting of Group V, VI and VII elements, e.g. manganese. Said second and third metals are added prior to the first calcination.

Abstract: Oxidative dehydrogenation of alkanes and alkylaromatic hydrocarbons is achieved by contact with an active carbon catalyst. In various aspects of the invention, the oxidative dehydrogenation is performed at a pressure above about 100 psia, and/or at a temperature in the range from about 500.degree. C. to about 800.degree. C., and/or the active carbon catalyst contains a metal, for example, molybdenum.

Abstract: A hydrocracking process is provided which process utilizes a sulfated solid catalyst comprising (1) oxide or hydroxide of Group III or Group IV element, e.g. zirconium, and (2) a first metal comprising a metal or combination of metals selected from the group consisting of platinum, palladium, nickel, platinum and rhenium, and platinum and tin. The catalyst may further comprise (3) a second metal selected from the group consisting of Group VIII elements, e.g. iron. One embodiment of the invention further comprises (4) a third metal selected from the group consisting of Group V, VI and VII elements, e.g. manganese.

Abstract: A naphtha upgrading process is provided which process utilizes a sulfated solid catalyst comprising (1) oxide or hydroxide of Group III or Group IV element, e.g. zirconium, and (2) a first metal comprising a metal or combination of metals selected from the group consisting of platinum, palladium, nickel, platinum and rhenium, and platinum and tin. The sulfated support is calcined prior to incorporation of the first metal and subsequent to said incorporation. The catalyst may further comprise (3) a second metal selected from the group consisting of Group VIII elements, e.g. iron. One embodiment of the invention further comprises (4) a third metal selected from the group consisting of Group V, VI and VII elements, e.g. manganese. Said second and third metals are added prior to the first calcination.

Abstract: Solid superacid catalyst, for example sulfated zirconia, is used in the oxidative dehydrogenation of saturated or partially saturated hydrocarbons, for example the conversion of isobutane to isobutylene in the presence of an oxygen-containing oxidizing agent at reaction conditions typically including temperatures from 500 to 1,000 degrees Fahrenheit, superatmospheric pressures, and oxygen/alkane molar ratios from 0.2 to 20. Performance of a metal-oxide or metal-hydroxide oxidative dehydrogenation catalyst may be enhanced by pretreating a solid superacid or other catalyst containing metal oxides or hydroxides at a carbonizing temperature with an organic material, for example an oxygen-containing organic material, to form a carbonaceous layer on the surface thereof prior to use of the catalyst in oxidative dehydrogenation.