Patent GB-873004-A (GB)
Title: Thermal conversion of hydrocarbons
Inventor: METRAILER WILLIAM JOSEPH
IPC: C10G9/32
Filed: 1958-05-20
Abstract: <PICT:0873004/IV (b)/1> A process for thermally converting a petroleum oil feed to lower molecular weight liquid hydrocarbons and normally gaseous unsaturated hydrocarbons and coke by contacting the oil with a dispersed suspension of catalytically inert hot particulate solids and separating the gaseous products from solids in a first, vapour-solid separation zone, comprises the further steps of quenching the separated gaseous products with a quench medium comprising a hydrocarbon liquid product stream, to a temperature sufficiently low to terminate the thermal conversion, said quench medium containing from 1-20% volume of liquid which boils above the temperature of the gaseous stream after quenching and having a final boiling point of from 50 DEG  to 100 DEG F. above said temperature; feeding the quenched stream into a second cyclone separation zone; separating uncondensed vapours from entrained solids and a liquid stream containing quenched liquid condensate and unvaporized quench medium; separating the liquid stream from the solids; recycling a major production by weight of the liquid stream to the upper portion of the second cyclonic separation zone to wet the wall thereof and wash down adhering solids; passing the uncondensed vapours and the remaining portion of the liquid stream to a fractionating column to separate vapour and liquid product streams therefrom including the hydrocarbon liquid product stream and utilizing at least a portion of this stream for the quenching step.  A residual petroleum oil heated to 650 DEG F. is introduced through line 1 into transfer line 2 which is supplied with coke particles at 1600 DEG F. from line 3 and steam from line 4.  The contact time is 0.2 to 0.4 seconds before the products pass into cyclone 5 where the coarser solids are removed through line 8. The vapours are quenched in line 6 with liquid from line 7 from 1400 DEG F. to 650 DEG F.  The quench liquid consists of 90% volume hydrocarbons boiling below 650 DEG F. and 10% volume hydrocarbons boiling between 650 DEG F. and 750 DEG F.  Between 3 and 4 volumes of quench liquid per volume of feed are used and the conditions are such that the 10% of the quench liquid boiling above 650 DEG F. is not vaporized.  The quenched stream is passed to a second cyclone 9 whence the vapours are passed via line 10 to fractionater 16 and solids and liquids descend via dip leg 11 to solid/liquid separator 12.  Solids are removed by line 13, 90 to 95% by weight of the liquid is recycled via line 14, and the balance of the liquid is passed to fractionater 16 via line 15.  The fractionation therein is assisted by steam introduced through line 20.  The fractions obtained are a light ends (380-430 DEG F.) through line 17; a 430 to 650 DEG F. through line 18; a liquid product which contains components boiling in the same ranges as the above fractions and at least part of which is used as the quench medium, through line 19; and a 650 DEG F.+ tar through line 21.  Suitable ranges of conditions mentioned are a temperature of 1100 to 1800 DEG F., a fluidizing gas velocity of 5 to 150 f.s. and a contact time of 0.01 to 5 seconds in the transfer line reactor and a temperature of 1200 to 2300 DEG F. and a gas velocity of 0.2 to 150 f.s. in the heater. Reference has been directed by the Comptroller to Specification 819,846.ALSO:<PICT:0873004/III/1> A process for thermally converting a petroleum oil feed to lower molecular weight liquid hydrocarbons and normally gaseous unsaturated hydrocarbons and coke by contacting the oil with a dispersed suspension of catalytically inert hot particulate solids and separating the gaseous products from solids in a first, vapour-solid separation zone, comprises the further steps of quenching the separated gaseous products with a quench medium comprising a hydrocarbon liquid product stream, to a temperature sufficiently low to terminate the thermal conversion, said quench medium containing from 1-20 volume per cent. of liquid which boils above the temperature of the gaseous stream after quenching and having a final boiling point of from 50 DEG  to 100 DEG F. above said temperature; feeding the quenched stream into a second cyclone separation zone; separating uncondensed vapours from entrained solids and a liquid stream containing quenched liquid condensate and unvaporized quench medium; separating the liquid stream from the solids; re-cycling a major production by weight of the liquid stream to the upper portion of the second cyclonic separation zone to wet the wall thereof and wash down adhering solids; passing the uncondensed vapours and the remaining portion of the liquid stream to a fractioning column to separate vapour and liquid product streams therefrom including the hydrocarbon liquid product stream and utilizing at least a portion of this stream for the quenching step. A residual petroleum oil heated to 650 DEG F. is introduced through line 1 into transfer line 2 which is supplied with coke particles at 1600 DEG F. from line 3 and steam from line 4.  The contact time is 0.2 to 0.4 seconds before the products pass into cyclone 5 where the coarser solids are removed through line 8.  The vapours are quenched in line 6 with liquid from line 7 from 1400 DEG F. to 650 DEG F.  The quench liquid consists of 90 volume per cent. hydrocarbons boiling below 650 DEG F. and 10 volume per cent hydrocarbons boiling between 650 DEG F. and 750 DEG F. Between 3 and 4 volumes of quench liquid per volume of feed are used and the conditions are such that the 10% of the quench liquid boiling above 650 DEG F. is not vaporized.  The quenched stream is passed to a second cyclone 9 whence the vapours are passed via line 10 to fractionator 16 and solids and liquids descend via dip p  leg 11 to solid/liquid separator 12.  Solids are removed by line 13, 90 to 95% by weight of the liquid is recycled via line 14, and the balance of the liquid is passed to fractionator 16 via line 15.  The fractionation therein is assisted by steam introduced through line 20.  The fractions obtained are a light ends (380-430 DEG F.) through line 17; a 430 to 650 DEG F. through line 18; a liquid product which contains components boiling in the same ranges as the above fractions and at least part of which is used as the quench medium, through line 19; and a 650 DEG F.+ tar through line 21.  Suitable ranges of conditions mentioned are a temperature of 1100 to 1800 DEG F., a fluidizing gas velocity of 5 to 150 f.s. and a contact time of 0.01 to 5 seconds in the transfer line reactor and a temperature of 1200 to 2300 DEG F. and a gas velocity of 0.2 to 150 f.s. in the heater.  Reference has been directed by the Comptroller to Specification 819,846.