A process is presented for recovering the hydrocarbon components from a naphtha feed to pass to a gasoline blending pool or to change the operations to increase the production of light olefins. The process includes the separation of the naphtha feedstock into a light naphtha stream and a heavy naphtha stream. The process further includes separating the light naphtha stream to recovery high quality non-normal hydrocarbons, and to separate normal hydrocarbons to the feed to the cracking unit.

A process is presented for improving the feed to a cracking unit and a reforming unit from a naphtha feedstock. The process includes the use of a separation unit to generate a light naphtha feed and a heavy naphtha feed. The process further includes separating the light naphtha feed into a light naphtha feed comprising normal hydrocarbons and a light naphtha feed comprising non-normal hydrocarbons. The light naphtha feed comprising normal hydrocarbon is passed to the cracking unit and the heavy naphtha feed is passed to the reforming unit.

The invention relates to a process for producing benzene, comprising the steps of: (a) providing a hydrocracking feed stream comprising C5-C12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 A and a silica (SiO2) to alumina (Al.sub.2O.sub.3) molar ratio of 5-200 under process conditions including a temperature of 425-580? C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h.sup.?1 to produce a hydrocracking product stream comprising benzene, toluene and C8+ hydrocarbons, (c) separating benzene, toluene and the C8+ hydrocarbons from the hydrocracking product stream and (d) selectively recycling back at least part of the toluene from the separated products of step (c) to be included in the hydrocracking feed stream process for producing benzene from a c5-c12 hydrocarbon mixture

The invention relates to a process for producing benzene, comprising the steps of: (a) providing a hydrocracking feed stream comprising C5-C12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 A and a silica (SiO2) to alumina (Al.sub.2O.sub.3) molar ratio of 5-200 under process conditions including a temperature of 425-580? C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h.sup.?1 to produce a hydrocracking product stream comprising benzene, toluene and C8+ hydrocarbons, (c) separating benzene, toluene and the C8+ hydrocarbons from the hydrocracking product stream and (d) selectively recycling back at least part of the toluene from the separated products of step (c) to be included in the hydrocracking feed stream process for producing benzene from a c5-c12 hydrocarbon mixture

Zn-promoted and/or Ga-promoted cracking catalysts, such as cracking catalysts comprising an MSE framework zeolite or an MFI framework zeolite can provide unexpectedly superior conversion of branched paraffins when used as part of a catalyst during reforming of a hydrocarbon fuel stream. The conversion and reforming of the hydrocarbon fuel stream can occur, for example, in an internal combustion engine. The conversion and reforming can allow for formation of higher octane compounds from the branched paraffins.

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feed to the gas oil steam cracker in certain embodiments includes gas oil range intermediates from the vacuum residue hydrocracking zone. In addition, a base oil production center is integrated to provide base oils product used for production of synthetic lubes or corresponding lube oil feedstocks

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feed to the gas oil steam cracker in certain embodiments includes gas oil range intermediates from the vacuum residue hydrocracking zone. In addition, a base oil production center is integrated to provide base oils product used for production of synthetic lubes or corresponding lube oil feedstocks

The invention relates to a production and separation device and method wherein: a reforming effluent (40) is produced and fractionated in a separation unit (1) and a fractionation train (5-6-7) for extracting benzene (22), toluene (23), xylenes (24) and C9-10 aromatics; aromatics are extracted from a feedstock (41) in a liquid-liquid extraction unit (14) to produce a first raffinate (43) and a first extract (42), the first extract (42) being sent to a benzene-toluene fractionation device (5); the xylenes are separated in a xylene separation unit (10) to produce a second extract (31) containing para-xylene, and a second raffinate (32) containing ortho-xylene and meta-xylene; and the second raffinate is isomerised in an isomerisation unit (11) so as to produce an isomerate (34) enriched in para-xylene sent to a fractionation train (5-6-7).

In a method and system for treating a catalytic cracking gasoline, a catalytic cracking process, or a plant employs a fluidized reactor to carry out hydrodealkylation treatment on a catalytic cracking oil gas or catalytic cracking gasoline, so that heavy aromatics present therein can be efficiently converted into light olefins and light aromatics. The method and system can improve the yield of light olefins, allow a long-period stable operation, relieve the contradiction between supply and demand of light aromatics, and solve the problem of high content of heavy aromatics that have low value and are difficult to be utilized in aromatics present in oil gas from catalytic cracking units.

In a method and system for treating a catalytic cracking gasoline, a catalytic cracking process, or a plant employs a fluidized reactor to carry out hydrodealkylation treatment on a catalytic cracking oil gas or catalytic cracking gasoline, so that heavy aromatics present therein can be efficiently converted into light olefins and light aromatics. The method and system can improve the yield of light olefins, allow a long-period stable operation, relieve the contradiction between supply and demand of light aromatics, and solve the problem of high content of heavy aromatics that have low value and are difficult to be utilized in aromatics present in oil gas from catalytic cracking units.