The present disclosure generally relates to methods and systems for reforming and isomerizing hydrocarbons. More particularly, the present disclosure relates to a novel combination of two traditionally separate reforming and isomerization reaction zones. A first hydrocarbon stream comprising C.sub.5-C.sub.6 hydrocarbons is isomerized in a first isomerization zone. A second hydrocarbon stream comprising C.sub.7+ hydrocarbons is reformed thus producing a C.sub.7 hydrocarbon stream and a C.sub.8 hydrocarbon stream. The reformed C.sub.7 stream is then isomerized in a second isomerization zone.

Naphtha compositions with enhanced reformability are provided. The naphtha compositions can be derived from biomass, can exhibit improved N+2A values, and can be used as a reformer feedstock with little or no processing.

Naphtha compositions with enhanced reformability are provided. The naphtha compositions can be derived from biomass, can exhibit improved N+2A values, and can be used as a reformer feedstock with little or no processing.

Disclosed herein are processes for the production of hydrocarbon fuel products from C.sub.2-5 alkanes. Methane is converted to ethylene in a methane thermal olefination reactor operating at a temperature of at least 900? C. and a pressure of at least 150 psig, and without a dehydrogenation catalyst or steam. C.sub.2-5 alkanes are converted to olefins in a C.sub.2-5 thermal olefination reactor operating at a temperature, pressure and space velocity to convert at least 80% of the alkanes to C.sub.2-5 olefins. The ethylene and C.sub.2-5 olefins are passed through an oligomerization reactor containing a zeolite catalyst and operating at a temperature, pressure and space velocity to crack, oligomerize and cyclize the olefins. In one aspect, methane in the effluent of the oligomerization reactor is recycled through the C.sub.2-5 thermal olefination reactor. Methods for the thermal olefination of methane are also disclosed.

Disclosed herein are processes for the production of hydrocarbon fuel products from C.sub.2-5 alkanes. Methane is converted to ethylene in a methane thermal olefination reactor operating at a temperature of at least 900? C. and a pressure of at least 150 psig, and without a dehydrogenation catalyst or steam. C.sub.2-5 alkanes are converted to olefins in a C.sub.2-5 thermal olefination reactor operating at a temperature, pressure and space velocity to convert at least 80% of the alkanes to C.sub.2-5 olefins. The ethylene and C.sub.2-5 olefins are passed through an oligomerization reactor containing a zeolite catalyst and operating at a temperature, pressure and space velocity to crack, oligomerize and cyclize the olefins. In one aspect, methane in the effluent of the oligomerization reactor is recycled through the C.sub.2-5 thermal olefination reactor. Methods for the thermal olefination of methane are also disclosed.

GCI fuel compositions and methods of making them are described. The GCI fuel compositions comprises a fuel blend having an initial boiling point in a range of about 26 C. to about 38 C. and a final boiling point in a range of about 193 C. to less than 250 C., a density of about 0.72 kg/l to about 0.8 kg/l at 15 C., a research octane number of about 70 to about 85, and a cetane number of less than about 27, the fuel blend comprising a naphtha stream and a kerosene stream.

GCI fuel compositions and methods of making them are described. The GCI fuel compositions comprises a fuel blend having an initial boiling point in a range of about 26 C. to about 38 C. and a final boiling point in a range of about 193 C. to less than 250 C., a density of about 0.72 kg/l to about 0.8 kg/l at 15 C., a research octane number of about 70 to about 85, and a cetane number of less than about 27, the fuel blend comprising a naphtha stream and a kerosene stream.

The present disclosure generally relates to methods and systems for reforming and isomerizing hydrocarbons. More particularly, the present disclosure relates to a novel combination of two traditionally separate reforming and isomerization reaction zones. A first hydrocarbon stream comprising C.sub.5-C.sub.6 hydrocarbons is isomerized in a first isomerization zone. A second hydrocarbon stream comprising C.sub.7+ hydrocarbons is reformed thus producing a C.sub.7 hydrocarbon stream and a C.sub.8 hydrocarbon stream. The reformed C.sub.7 stream is then isomerized in a second isomerization zone.

Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Recognizing that several subsets of hot sources can be identified from among the available hot sources in a large petroleum refinery, subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified.

Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Recognizing that several subsets of hot sources can be identified from among the available hot sources in a large petroleum refinery, subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified.