A process for production of gasoline comprising separating a naphtha feed in a naphtha splitter into a stream comprising i-C.sub.5, a stream comprising C.sub.6 and lighter boiling hydrocarbons, a C.sub.7 stream comprising C.sub.7 hydrocarbons, and a heavy stream comprising C.sub.8 and heavier hydrocarbons; isomerizing at least a portion of the stream comprising C.sub.6 and lighter boiling hydrocarbons in a C.sub.5-C.sub.6 isomerization zone at isomerization conditions to form a C.sub.5-C.sub.6 isomerization effluent; dehydrogenating at least a portion of the stream comprising C.sub.7 hydrocarbons to form a C.sub.7 dehydrogenation effluent comprising C.sub.7 olefins; reforming the heavy stream in a reforming zone under reforming conditions forming a reformate stream; and blending one or more of the stream comprising i-C.sub.5, the C.sub.5-C.sub.6 isomerization effluent, the C.sub.7 dehydrogenation effluent and the reformate stream to form a gasoline blend.

In a process for upgrading paraffins and olefins, a first feed comprising C.sub.14 olefins is contacted with an oligomerization catalyst in a first reaction zone under conditions effective for oligomerization of olefins to higher molecular weight hydrocarbons. Deactivated catalyst is removed from the first reaction zone at a first temperature and is contacted with an oxygen-containing gas and a hydrocarbon-containing fuel in a regeneration zone to regenerate the catalyst and raise the temperature of the catalyst to a second, higher temperature. A second feed comprising C.sub.14 paraffins is contacted with the regenerated catalyst in a second reaction zone to convert at least some of the paraffins in the second feed to a reaction effluent comprising olefins, aromatic hydrocarbons and regenerated catalyst; and the reaction effluent is supplied to the first reaction zone. A system for performing such a process and a product of such a process are also provided.

In a process for upgrading paraffins and olefins, a first feed comprising C.sub.14 olefins is contacted with an oligomerization catalyst in a first reaction zone under conditions effective for oligomerization of olefins to higher molecular weight hydrocarbons. Deactivated catalyst is removed from the first reaction zone at a first temperature and is contacted with an oxygen-containing gas and a hydrocarbon-containing fuel in a regeneration zone to regenerate the catalyst and raise the temperature of the catalyst to a second, higher temperature. A second feed comprising C.sub.14 paraffins is contacted with the regenerated catalyst in a second reaction zone to convert at least some of the paraffins in the second feed to a reaction effluent comprising olefins, aromatic hydrocarbons and regenerated catalyst; and the reaction effluent is supplied to the first reaction zone. A system for performing such a process and a product of such a process are also provided.

An integrated process for production of gasoline has been described. The process includes a C.sub.5-C.sub.6 isomerization zone, two C.sub.7 isomerization zones separate by a deisoheptanizer, and a reforming zone. The use of two C.sub.7 isomerization zones eliminates the need for the large recycle stream from the deisoheptanizer. The low temperature in first C.sub.7 isomerization zone favors the formation of multi-branched C.sub.7 paraffins and cyclohexanes and maximizes C.sub.5.sup.+ yield. The separation between paraffin and cycloalkane in deisoheptanizer becomes easier due to conversion of cycloalkanes to cyclohexanes in the first C.sub.7 isomerization zone. Further, the high temperature in second C.sub.7 isomerization zone favors the formation of higher octane cyclopentanes over cyclohexanes. An aromatic-containing stream can be introduced to second C.sub.7 isomerization zone. The saturation of the aromatics in the second C.sub.7 isomerization zone provides heat that increases the reactor outlet temperature in the isomerization reactors to favor cyclopentanes.

An integrated process for production of gasoline has been described. The process includes a C.sub.5-C.sub.6 isomerization zone, two C.sub.7 isomerization zones separate by a deisoheptanizer, and a reforming zone. The use of two C.sub.7 isomerization zones eliminates the need for the large recycle stream from the deisoheptanizer. The low temperature in first C.sub.7 isomerization zone favors the formation of multi-branched C.sub.7 paraffins and cyclohexanes and maximizes C.sub.5.sup.+ yield. The separation between paraffin and cycloalkane in deisoheptanizer becomes easier due to conversion of cycloalkanes to cyclohexanes in the first C.sub.7 isomerization zone. Further, the high temperature in second C.sub.7 isomerization zone favors the formation of higher octane cyclopentanes over cyclohexanes. An aromatic-containing stream can be introduced to second C.sub.7 isomerization zone. The saturation of the aromatics in the second C.sub.7 isomerization zone provides heat that increases the reactor outlet temperature in the isomerization reactors to favor cyclopentanes.

An integrated process for production of gasoline has been described. The process includes a C.sub.5-C.sub.6 isomerization zone with an associated deisohexanizer, two C.sub.7 isomerization zones separated by a deisoheptanizer, and a reforming zone. The use of two C.sub.7 isomerization zones eliminates the need for the large recycle stream from the deisoheptanizer. The C.sub.6 cycloalkanes and heavies from the deisohexanizer are fed to the second C.sub.7 isomerization zone to increase the amount of 95 RONC gasoline produced. A higher percentage of 95 RONC gasoline may be achieved by further recycling C.sub.6 from deisoheptanizer overhead back to C.sub.5-C.sub.6 isomerization zone. Higher gasoline yields and higher percentage of 95 RONC gasoline is achieved over the whole naphtha complex with operating costs savings by fully integrating the C.sub.5-C.sub.6 isomerization zone, two C.sub.7 isomerization zones, deisohexanizer and deisoheptanizer columns.

An integrated process for production of gasoline has been described. The process includes a C.sub.5-C.sub.6 isomerization zone with an associated deisohexanizer, two C.sub.7 isomerization zones separated by a deisoheptanizer, and a reforming zone. The use of two C.sub.7 isomerization zones eliminates the need for the large recycle stream from the deisoheptanizer. The C.sub.6 cycloalkanes and heavies from the deisohexanizer are fed to the second C.sub.7 isomerization zone to increase the amount of 95 RONC gasoline produced. A higher percentage of 95 RONC gasoline may be achieved by further recycling C.sub.6 from deisoheptanizer overhead back to C.sub.5-C.sub.6 isomerization zone. Higher gasoline yields and higher percentage of 95 RONC gasoline is achieved over the whole naphtha complex with operating costs savings by fully integrating the C.sub.5-C.sub.6 isomerization zone, two C.sub.7 isomerization zones, deisohexanizer and deisoheptanizer columns.

The present invention relates to unsaturated carboxylic acid ester obtained from or through the use of a source material defined below in formula (I):
A.sub.(0.9-1.2)(B+C).sub.(1.0)(I)
wherein the figures set in parentheses indicate the molar proportion of source material A to the sum of source materials B and C, and
wherein the following meanings apply:
A: unsaturated dicarboxylic acid,
B: a hard diol segment,
C: a soft diol segment selected from among compounds having a continuous chain between two hydroxyl groups, which have a length of 5 to 30 atoms, wherein the molar ratio of B:C is between 5:95 and 95:5. Furthermore, it relates to unsaturated polyester resin comprising said unsaturated carboxylic acid ester as defined above and a reactive diluents as well as molded articles, coatings, and surface textiles coated, saturated, laminated, and impregnated from or with a thermoset, which was obtained by hardening said unsaturated polyester resin.

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.