Patent GB-778220-A (GB)
Title: Improvements in or relating to the cracking of crude petroleum oils
IPC: C10G9/32
Filed: 1954-06-22
Abstract: In a process wherein crude petroleum oil or topped crude oil is passed into a vaporization zone where it is brought into contact with fluidized inert solid particles at a temperature up to about 1100 DEG F. so that the gas oil and lighter components of <PICT:0778220/III/1> the crude oil are rapidly vaporized leaving a carbonaceous residue on the particles, and the particles charged with residue are then transferred to a zone where they are maintained as a hot dense fluidized bed whereby the carbonaceous residue is converted into vapours and coke, some of the vapours leaving the coking zone are passed, directly or after catalytic cracking, through the vaporization zone in order to assist in vaporizing the feed.  The vapours leaving the vaporization zone are fractionated to obtain gas oil and lighter components; the bottoms from the fractionator may be introduced into the coking zone.  The preferred inert particulate material is coke; but sand, clay, spent catalyst, metal shot, glass beads, or ceramic beads, may also be used. Crude oil is fed into transfer line 1 through inlets 3 and 5; and a stream of coke particles at about 1000 DEG F. is also introduced into the transfer line through line 53, there being about 6 to 20 pounds of hot solids per pound of feed, which is ample to vaporize the gas oil and lower boiling constituents of the feed.  The particles are carried up line 1 by steam introduced through inlets (not shown).  The mixture is discharged from the transfer line into cyclone separator 7, where the vapours are separated from the solids.  The total contact time is less than 5 seconds.  The vapours are passed to fractionator 10, either directly via line 15 or via cooler 12.  When cooler 12 is employed the effluent therefrom, which contains condensed heavy gas oil, is passed to gas/liquid separator 20.  From here the uncondensed vapours are taken to the fractionator, while the liquid is sent via line 23 to a catalytic cracking bed 63 in reactor 33.  Coke particles coated with residue are withdrawn from separator 7 and passed through U-bend 27 into the botom of fluidized coking bed 31 in the lower part of reactor 33.  Here the charged coke particles are mixed with hotter coke particles supplied from heater 47 via U-bend 35. The mixture remains in coking bed 31 for 3 to 20 minutes, the temperature of the bed being about 950 DEG F.  The bed is fluidized in part by vaporous coker products and in part by steam.  The spent coke overflows partition 41 into zone 43 where occluded vapours are stripped therefrom by steam introduced through line 45.  The stripped bend 49. Part of the coke from stripper 43 may be diverted through U-bend 51 into transfer line 1.  The coke in heater 47 is maintained as a fluidized bed; and is heated either by passing air through it or by burning extraneous fuel therein. The reheated solids are stripped in zone 37; and then passed in part to transfer line 1 via U-bend 35. By adjustment of the valves in lines 51 and 53 the temperature of the solids in transfer line 1 may be accurately controlled.  Coke produced in excess of operating requirements is withdrawn from the system through line 50.  The vapours from coker bed 31 pass upwards through grid 61 into a fluidized bed of cracking catalyst 63.  The catalytically cracked products are withdrawn from the reactor via cyclone 65, and are passed in part into transfer line 1 via lines 71 and 73, the remainder being introduced directly into the fractionator via line 15.  Catalyst is withdrawn from bed 63 via line 76, and is passed to a regenerator (not shown).  The regenerated catalyst, mixed if desired with gas oil from separator 20, is returned to the reactor via line 77.  The bottoms from the fractionator may, if desired, be returned to the coker.