Abstract: A method of converting an original FCC unit of side by side configuration to a converted FCC unit for processing light feedstock by replacing an regenerator in the original FCC unit with an embodied regenerator. From the original FCC unit, the air supply assembly is removed and a centerwell is installed with a fluidization gas, fuel, and air inlet(s) through the centerwell. Distribution rings are connected to each of fluidization gas and fuel inlet(s). An internal pipe and a standpipe portion are installed, wherein a lower end of the standpipe extends into the centerwell creating a radial slot, and wherein the lower end of the standpipe is spaced above the deflector plate in the centerwell to allow flow of spent catalyst through the standpipe and provide deflection of the spent catalyst flow for mixing the spent catalyst with fuel oil that is vaporized within the centerwell.

Abstract: A low-pressure olefins recovery process and plant are described. The feed gas is compressed and distilled at a primary distillation pressure. The overhead stream is chilled at a pressure less than 30 kg/cm2 (430 psia) to partially condense the overheads. The primary distillation tower is refluxed with at least a portion of the condensate. The overhead vapor is further chilled and partially condensed and the condensate is fed to a demethanizer. The remaining vapor is cooled in a cold section and the resultant liquid is phase-separated and expanded to provide refrigeration for the cold section. The expanded vapor from the cold section is recycled to the process gas compressor. The bottoms streams from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene, ethane, propylene, propane, C4's, and C5+.

Abstract: Disclosed are compliant variable tension risers (106) to connect deep-water subsea wellheads (102) to a single floating platform (104) in wet tree or dry try systems. The variable tension risers (106) allow several subsea wellheads (102), in water depths from 1220 to 3050 meters, at lateral offsets from one-tenth to twice the depth or more, to tie back to a single floating platform (104). Also disclosed are methods to counter buoyancy and install variable tension risers using a weighted chain ballast line (228, 230).

Abstract: Disclosed is a process for the upgrading and demetallizing of heavy oils and bitumens. A crude heavy oil and/or bitumen feed is supplied to a solvent extraction process 104 wherein DAO and asphaltenes are separated. The DAO is supplied to an FCC unit 106 having a low conversion activity catalyst for the removal of metals contained therein. The demetallized distillate fraction is supplied to a hydrotreater 110 for upgrading and collected as a synthetic crude product stream. The asphaltene fraction can be supplied to a gasifier 108 for the recovery of power, steam and hydrogen, which can be supplied to the hydrotreater 110 or otherwise within the process or exported. An optional coker 234 can be used to convert excess asphaltenes and/or decant oil to naphtha, distillate and gas oil, which can be supplied to the hydrotreater 220.

Abstract: A process for the selective hydrogenation of alpha-methyl-styrene (AMS) to cumene in a two catalyst system is disclosed. A crude cumene feed stream containing up to 10% AMS by weight is supplied to the first reaction zone 112 and mixed with hydrogen in a first catalyst bed 118 containing a nickel catalyst, converting from 70 to 95 percent of the AMS to cumene. Cumene and remaining AMS are separated from hydrogen in a liquid take off tray 120. The first reaction zone 112 effluent is supplied to a second reaction zone 114, where the effluent and hydrogen gas are mixed in a second catalyst bed 126 containing a noble-metal catalyst to substantially convert any remaining AMS to cumene. Cumene is collected, separated from the hydrogen, and can be resupplied to the hydrogenation reactor 110, or supplied as feed to a phenol synthesis loop.

Abstract: Residual oil supercritical extraction (ROSE) 10 and integrated gasification combined-cycle (IGCC) power systems 70, 114 are cooperatively integrated. High-level heat from the IGCC is used via a heat transfer fluid 84 for high level process heating requirements in the ROSE unit. This can eliminate the fired heater normally required in the ROSE unit, and reduces the size of the gasifier 62 waste heat boiler 72 and/or the high-pressure steam coil 134 and steam turbine generator 144 in the IGCC.

Abstract: A catalyst regenerator for regenerating spent light FCC catalyst and heating the catalyst to supply heat to an FCC reactor. The regenerator has discharge outlets for catalyst and off gas and a valve for introducing spent catalyst through a central stand pipe portion. The regenerator houses a dense phase catalyst bed. A centerwell receives a lower end of the standpipe portion and defines an annulus therebetween. The spent catalyst is introduced through the standpipe portion into the annulus. A fuel distributor introduces fuel into the centerwell for mixing with the catalyst in the annulus. A fluidization distributor introduces fluidization gas into the centerwell for fluidizing the catalyst in the annulus. A radial slot in the centerwell introduces the catalyst and fuel mixture from the annulus below the upper surface of the dense phase bed. An air distributor located below the radial slot introduces combustion air into the dense phase bed.