Total sulfur in feed ¼ 9,275 Â 42 Â 7:678 Â 0:031
¼ 92,720 lbs per calendar day:
85 % wt of the sulfur is to be removed. This amounts to 78,812 pounds of sulfur or
2,462.9 mol/CD.
Hydrogen required for sulfur removal in the gas oil is estimated as follows:
Hydrogen contained in H 2 S only ¼ 92,720 Â 0:85=32 ¼ 2,462:9 mols=CD:
¼ 2,462:9 Â 379
¼ 933,439 Scf standard cuft at 60
F and 14:7 psia
ð
Þ :
Hydrogen is also required for nitrogen removal and to close ruptured hydrocarbon
rings due to the sulfur removal. This reaction also produces light ends at the
Table 19 Yield of thermal cracker product streams
Streams
% vol on feed % vol on total products Mid vol% on total product
H 2 S
0.18
0.17
–
Gas to C 6
7.81
7.40
3.87
Naphtha C 6 –380
F
9.51
9.02
12.08
Gas oil 380–650
F
13.91
13.19
23.12
Cracked resid +650
F 74.08
70.22
71.49
Total
105.49
100.00
–
Table 20 Cracked product properties
Stream
BPCD
SG
Sulfur % wt
Vis at 100
F
Vis at 210
F
Gas to C 5
852
0.465
3.47
a
À
–
Naphtha
1,014.2
0.724
1.58
Gas oil
1,483.5
0.825
2.55
5.4
0.2
Residue +650
F
7,900.6
1.046
6.19
110
12.5
Total
11,250.3
0.944
5.35
a
Includes 3,362 lbs/CD sulfur as H 2 S
Table 21 Sulfur balance over the thermal cracker
Streams
BPCD
lbs/gal
MM lbs/CD
% Sulfur
lbs sulfur/CD
Feed in
10,665
8.38
3.756
5.35
200,964
Streams out
Gas to C 5
852
4.21
0.151
3.47
5,243.7
Naphtha
1,014.2
6.03
0.257
1.58
4,058.3
Gas oil
1,483.5
6.87
0.428
2.55
10,914.0
Cracked res
7,900.6
8.80
2.920
6.19
180,748.0
Total
11,250.3
7.94
3.756
5.35
200,964.0
Petroleum Products and a Refinery Configuration
99
¼ 92,720 lbs per calendar day:
85 % wt of the sulfur is to be removed. This amounts to 78,812 pounds of sulfur or
2,462.9 mol/CD.
Hydrogen required for sulfur removal in the gas oil is estimated as follows:
Hydrogen contained in H 2 S only ¼ 92,720 Â 0:85=32 ¼ 2,462:9 mols=CD:
¼ 2,462:9 Â 379
¼ 933,439 Scf standard cuft at 60
F and 14:7 psia
ð
Þ :
Hydrogen is also required for nitrogen removal and to close ruptured hydrocarbon
rings due to the sulfur removal. This reaction also produces light ends at the
Table 19 Yield of thermal cracker product streams
Streams
% vol on feed % vol on total products Mid vol% on total product
H 2 S
0.18
0.17
–
Gas to C 6
7.81
7.40
3.87
Naphtha C 6 –380
F
9.51
9.02
12.08
Gas oil 380–650
F
13.91
13.19
23.12
Cracked resid +650
F 74.08
70.22
71.49
Total
105.49
100.00
–
Table 20 Cracked product properties
Stream
BPCD
SG
Sulfur % wt
Vis at 100
F
Vis at 210
F
Gas to C 5
852
0.465
3.47
a
À
–
Naphtha
1,014.2
0.724
1.58
Gas oil
1,483.5
0.825
2.55
5.4
0.2
Residue +650
F
7,900.6
1.046
6.19
110
12.5
Total
11,250.3
0.944
5.35
a
Includes 3,362 lbs/CD sulfur as H 2 S
Table 21 Sulfur balance over the thermal cracker
Streams
BPCD
lbs/gal
MM lbs/CD
% Sulfur
lbs sulfur/CD
Feed in
10,665
8.38
3.756
5.35
200,964
Streams out
Gas to C 5
852
4.21
0.151
3.47
5,243.7
Naphtha
1,014.2
6.03
0.257
1.58
4,058.3
Gas oil
1,483.5
6.87
0.428
2.55
10,914.0
Cracked res
7,900.6
8.80
2.920
6.19
180,748.0
Total
11,250.3
7.94
3.756
5.35
200,964.0
Petroleum Products and a Refinery Configuration
99