Assume the hydrogen makeup stream (usually from the naphtha reformer) is 92 %
mole pure.
The makeup gas stream required ¼
2,053,567
0:92
¼ 2,232,000 Scf=CD or, as usually
expressed, about 240 scf per bbl of feed.
The material balance over the unit is shown in Tables 22, and 23.
Heavy gas oil hydrotreater on LVGO operation. Feed to hydrotreater is as
follows:
LVGO = 5,425 BPCD
SG at 60
F = 0.8789
Pounds/gal = 7.309
100
−10
90
80
70
60
50
Mid Volume %
40
30
20
10
80
70
60
50
40
30
°API Gravity
20
10
0
0
Fig. 10 Thermal cracker
effluent gravity curve
Petroleum Products and a Refinery Configuration
101
mole pure.
The makeup gas stream required ¼
2,053,567
0:92
¼ 2,232,000 Scf=CD or, as usually
expressed, about 240 scf per bbl of feed.
The material balance over the unit is shown in Tables 22, and 23.
Heavy gas oil hydrotreater on LVGO operation. Feed to hydrotreater is as
follows:
LVGO = 5,425 BPCD
SG at 60
F = 0.8789
Pounds/gal = 7.309
100
−10
90
80
70
60
50
Mid Volume %
40
30
20
10
80
70
60
50
40
30
°API Gravity
20
10
0
0
Fig. 10 Thermal cracker
effluent gravity curve
Petroleum Products and a Refinery Configuration
101