In fluid coking $($see Figure below$),$ bitumen is sprayed into a hot fluidized bed of coke particles to form thin liquid

films. At high reactor temperatures, these films undergo thermal cracking reactions to form fresh coke and volatile

products. The mass of fresh coke deposited on the hot coke particles is usually about $3$ wt$\%$ per pass through the

reactor. Based on the data given below, estimating the following:

$1)$ Coke circulation rate.

$2)$ Required volume of the coker $($assuming total volume being twice of the coke volume in the coker$).$

$3)$ Minimum volume of the burner $(20\%$ greater than the volume of the coke in the burner$).$

$4)$ Flowrate of coke product exiting the system and the ultimate coke yield of the system.

DATA:

Feed to coker $=2,000$ bbl$/$h $(103$

Kg$/$m$3$

$)$ Steam temperature $=180$ oC$,$ saturated

Coke particle density $=1450$ Kg$/$m$3$

Steam flow: enough to keep fluidization

Coke bulk density $=800$ Kg$/$m$3$

Ambient air temperature $=15$ oC

Coke heat capacity $=1\mathrm{.}6$ KJ$/$Kg Ambient air relative humidity $($RH$)=60\%$

Coke heat of combustion: $29\mathrm{.}5$ MJ$/$kg Operating temperature of coker $=530$ oC

Coke yield in coking $=22\%$ mass Operating temperature of burner $=630$ oC

Coke average residence time in coker $=6$ minutes

Coke average residence time in burner $=7$ minutes