Patent GB-580087-A (GB)
Title: Improved process for the catalytic conversion of hydrocarbon oils
IPC: C10G11/18
Filed: 1943-01-16
Abstract: Aviation gasoline of low acid heat and high octane number is obtained by cracking a high boiling oil, e.g., a gas oil, in presence of catalysts at temperatures of 875-100 DEG F. for a period of time that from 40-80 per cent. of the oil is converted into other constituents, fractionating the products to segregate a fraction having an upper boiling point of 200 DEG F., subjecting this fraction to further catalytic conversion at temperatures between 600 and 800 DEG F. and fractionating the product obtained to segregate a fraction suitable for use as aviation gasoline.  The charge oil, after vaporisation if desired in a heated coil 11 and separator 12, is passed <PICT:0580087/III/1> through line 17 into a reactor 15 in the form of an elongated vertical chamber having a conical base and a perforated grid acting as distributor for the oil vapours and support for the catalyst which is introduced through a stand pipe 16 from a regenerator 68 arranged above the reactor; contaminated catalyst being removed through a stand pipe 62 and mixed with oxidising gases fed through a pipe 66 to the regenerator.  The cracked products pass through a pipe 18 to a fractionating tower 19 operative under such condition that fractions boiling below 200 DEG F. are taken overhead while a gas oil fraction is collected on plate 25, a kerosene or heavy naphtha boiling between 300 and 400 DEG F. fraction is collected on plate 26, and a 200-300 DEG F. boiling range fraction is collected on plate 28 and may be used to blend with the aviation distillate.  The overhead condensate, separated from gases in receiver 32, is passed through line 37 to a debutanising tower 38 from which the debutanised fraction is removed at the bottom and with or without heating in coil 43 is passed into the reforming-polymerising catalytic chamber 46 from which the reformed vapours pass to a fractionating tower 49 where they are fractionated to recover overhead gases and vapours boiling in the aviation range which are condensed in cooler 55 and collected in receiver 56. Bottom and intermediary fractions are recovered through lines 51, 53. Specification 551,663, [Group IV], is referred to.  The Specification as open to inspection under Sect. 91 stated that the fractions subjected to the further reforming-polymerisation treatment may comprise (1) the 200 DEG F. end point naphtha with light constituents formed in the process; (2) the above naphtha fraction together with C3 and C4 constituents (3) a debutanised and/or depentanised 200 DEG F. end point naphtha (4) the total naphtha fraction boiling up to 300 DEG F. with or without other lighter constituents and with or without prior debutanisation (5) a heavy naphtha fraction boiling above 300 DEG F. mixed with a light fraction boiling up to 200 DEG F.  This matter does not appear in the Specification as accepted.ALSO:<PICT:0580087/IV/1> Aviation gasoline of low acid heat and high octane number is obtained by cracking a high boiling oil, e.g. a gas oil in presence of catalysts at temperatures of 875-1000 DEG  F. for a period of time that from 40-80 per cent of the oil is converted into other constituents, fractionating the products to segregate a fraction having an upper boiling point of 200 DEG  F., at temperatures between 600 DEG  and 800 DEG  F. and fractionating the product obtained to segregate a fraction suitable for use as aviation gasoline.  The charge oil after vaporization, if desired, in a heated coil 11 and separator 12 is passed through line 17 into a reactor 15 in the form of an elongated vertical chamber having a conical base and a perforated grid acting as distributer for the oil vapours and support of the catalyst which is introduced through a stand pipe 16 from a regenerator 68 arranged above the reactor; contaminated catalyst being removed through a stand pipe 62 and mixed with oxidising gases fed through pipe 18 to a fractionating tower 19 operative under such condition that fractions boiling below 200 DEG F. are taken overhead while a gas oil fraction is collected on plate 25, a kerosene or heavy naphtha boiling between 300 DEG  and 400 DEG F. is collected on plate 261 and a 200-300 DEG  F. boiling range fraction is collected on plate 28 and may be used to blend with the aviation distillate.  The overhead condensate separated from gases in receiver 32 is passed through line 37 to a debutanising tower 38 from which the debutanised fraction is removed at the bottom and with or without heating in coil 43 is passed into the reforming-polymerizing catalytic chamber 46 from which the reformed vapours pass to a fractionating tower 49 where they are fractionated to recover overhead gases and vapours boiling in the aviation range which are condensed in cooler 55 and collected in receiver 56.  Bottom and intermediary fractions are recovered through lines 51, 53. Specification 551,663 is referred to.  The Specification as open to inspection under Sect. 91 states that the fractions subjected to the further reforming-polymerizing treatment may comprise (1) the 200 DEG F. end point naphtha with light constituents formed in the process; (2) the above naphtha fraction together with C3 and C4 constituents; (3) a debutanised and/or depentanised 200 DEG  F. end point naphtha. The following fractions may also be reformed: (4) the total naphtha fraction boiling up to 300 DEG  F. with or without other lighter constituents and with or without prior debutanisation; (5) a heavy naphtha fraction boiling above 300 DEG  F. mixed with a light fraction boiling up to 200 DEG  F.  This subject-matter does not appear in the Specification as accepted.