Device and process for the conversion of a feedstock of aromatic compounds, in which the feedstock is treated notably by means of a fractionation train (4-7), a xylene separation unit (10) and an isomerization unit (11), and in which a pyrolysis unit (13) treats a second hydrocarbon feedstock, produces a pyrolysis effluent feeding the feedstock, and produces a pyrolysis gas comprising CO, CO.sub.2 and H.sub.2; a reverse water gas shift RWGS reaction section (50) treats the pyrolysis gas and produces an RWGS gas enriched in CO and in water; a fermentation reaction section (52) treats the RWGS gas enriched in CO and in water, to produce ethanol and recycle the ethanol to the inlet of the pyrolysis unit.

Device and process for the conversion of a feedstock of aromatic compounds, in which the feedstock is treated notably by means of a fractionation train (4-7), a xylene separation unit (10) and an isomerization unit (11), and in which a pyrolysis unit (13) treats a second hydrocarbon feedstock, produces a pyrolysis effluent feeding the feedstock, and produces a pyrolysis gas comprising CO, CO.sub.2 and H.sub.2; a reverse water gas shift RWGS reaction section (50) treats the pyrolysis gas and produces an RWGS gas enriched in CO and in water; a fermentation reaction section (52) treats the RWGS gas enriched in CO and in water, to produce ethanol and recycle the ethanol to the inlet of the pyrolysis unit.

Device and process for converting a feedstock of aromatic compounds, in which the feedstock is notably treated using a fractionation train (4-7), a xylenes separating unit (10) and an isomerization unit (11), and in which a pyrolysis unit (13) treats a second hydrocarbon-based feedstock, produces a pyrolysis effluent feeding the feedstock, and produces a pyrolysis gas comprising CO, CO2 and H2; a WGS water gas shift reaction section (50) suitable for treating the pyrolysis gas and for producing a WGS gas enriched in CO2 and in hydrogen; a CO2 aromatization reaction section (52) suitable for: at least partly treating the WGS gas to produce a hydrocarbon effluent comprising aromatic compounds, and feeding the feedstock with the hydrocarbon effluent.

Device and process for converting a feedstock of aromatic compounds, in which the feedstock is notably treated using a fractionation train (4-7), a xylenes separating unit (10) and an isomerization unit (11), and in which a pyrolysis unit (13) treats a second hydrocarbon-based feedstock, produces a pyrolysis effluent feeding the feedstock, and produces a pyrolysis gas comprising CO, CO2 and H2; a WGS water gas shift reaction section (50) suitable for treating the pyrolysis gas and for producing a WGS gas enriched in CO2 and in hydrogen; a CO2 aromatization reaction section (52) suitable for: at least partly treating the WGS gas to produce a hydrocarbon effluent comprising aromatic compounds, and feeding the feedstock with the hydrocarbon effluent.

A process for converting C2-5 alkanes to higher value C5-24 hydrocarbon fuels and blendstocks. The C2-5 alkanes are converted to olefins by thermal olefination, without the use of a dehydrogenation catalyst and without the use of steam. The product olefins are fed to an oligomerization reactor containing a zeolite catalyst to crack, oligomerize and cyclize the olefins to the fuel products which are then recovered. Optionally, hydrogen and methane are removed from the product olefin stream prior to oligomerization. Further optionally, C2-5 alkanes are removed from the product olefin stream prior to oligomerization.

A process for converting C2-5 alkanes to higher value C5-24 hydrocarbon fuels and blendstocks. The C2-5 alkanes are converted to olefins by thermal olefination, without the use of a dehydrogenation catalyst and without the use of steam. The product olefins are fed to an oligomerization reactor containing a zeolite catalyst to crack, oligomerize and cyclize the olefins to the fuel products which are then recovered. Optionally, hydrogen and methane are removed from the product olefin stream prior to oligomerization. Further optionally, C2-5 alkanes are removed from the product olefin stream prior to oligomerization.

Process for the production of C6-C7 aromatic compounds from a hydrocarbon feedstock of naphtha type comprising the following stages: a) the said feedstock (1) is sent into a first fractionation unit (2) in order to obtain an upper stream (3) comprising C6 and C7 hydrocarbon compounds and a lower stream (4) comprising C8 to C10 hydrocarbon compounds; b) the upper stream (3) and a stream (12) comprising C6 and C7 aromatic compounds obtained on conclusion of stage e) are sent into a unit for extraction of the aromatics (5) in order to obtain an aromatic base (6) and a liquid effluent (7); c) the liquid effluent (7) is sent into a first catalytic reforming unit (8) in order to obtain a first reformate effluent (9); d) the said first reformate effluent (9) is sent into a reformate separation section (10) in order to obtain a first stream (11) comprising C5 hydrocarbon compounds and a second stream (12) comprising C6 and C7 aromatic compounds; e) the second stream (12) comprising C6 and C7 aromatic compounds is recycled in stage b).

Processes for increasing an octane value of a gasoline component by dehydrogenating a stream comprising C.sub.7 hydrocarbons and methylcyclohexane in a first dehydrogenation zone to form an intermediate dehydrogenation effluent, and then dehydrogenating the intermediate dehydrogenation effluent in a second dehydrogenation zone to form a C.sub.7 dehydrogenation effluent. The C.sub.7 dehydrogenation effluent has an increased olefins content compared to an olefins content of the intermediate dehydrogenation effluent. The first dehydrogenation zone is operated under conditions to convert methylcyclohexane to toluene and minimize cracking reactions. The intermediate dehydrogenation effluent may be heated before being passed to the second dehydrogenation zone.

Processes for increasing an octane value of a gasoline component by dehydrogenating a stream comprising C.sub.7 hydrocarbons and methylcyclohexane in a first dehydrogenation zone to form an intermediate dehydrogenation effluent, and then dehydrogenating the intermediate dehydrogenation effluent in a second dehydrogenation zone to form a C.sub.7 dehydrogenation effluent. The C.sub.7 dehydrogenation effluent has an increased olefins content compared to an olefins content of the intermediate dehydrogenation effluent. The first dehydrogenation zone is operated under conditions to convert methylcyclohexane to toluene and minimize cracking reactions. The intermediate dehydrogenation effluent may be heated before being passed to the second dehydrogenation zone.

A method of forming C.sub.6-C.sub.8 aromatics may include selectively dealkylating a Fluid Catalytic Cracking (FCC) heavy cut naphtha that has at least C.sub.9+ aromatics to selectively crack C.sub.2+ alkyl chains from the C.sub.9+ aromatics, thereby forming the C.sub.6-C.sub.8 aromatics. The selectively de-alkylated heavy cut naphtha is then combined with a FCC middle cut naphtha, and aromatics including the C.sub.6-C.sub.8 aromatics are separated from the combined stream. A system for forming C.sub.6-C.sub.8 aromatics may include a fluid catalytic cracking unit for producing a FCC heavy cut naphtha comprising at least C.sub.9+ aromatics; a de-alkylation reactor for selectively cracking C.sub.2+ alkyl chains from the C.sub.9+ aromatics, thereby forming the C.sub.6-C.sub.8 aromatics; and an aromatic extraction unit for extracting at least a portion of the C.sub.6-C.sub.8 aromatics.