Licensor guarantees middle of run sulfur removal as 99 % wt.
Then lbs/CD sulfur removed = 2,631 lbs/CD. This generates 2,795 lbs/CD of
H 2 S.
There is no significant amount of naphtha made, nor is there significant amount
of hydrogen needed for saturation. The hydrogen makeup required is
82 mol/CD or 82 Ä 0.92 = 89 mol/CD reformer gas. This amounts to 33,780
Scf/CD.
iii. Summary of Kero operation
In
Kero feed
4,545 BPCD
1.280 mm lbs/CD
Hydrogen
89 moles/CD
979 lbs/CD ref gas
Total
1,280,979 lbs/CD
Out
Kero product
4,539 BPCD
1,277,342 lbs/CD
Hydrogen sulfide
82 mol/CD
2,788 lbs/CD
Losses from stripper
813
Total
1,280,166 lbs/CD
Naphtha consolidation and treating. Summary of naphtha and light ends streams
to treating processes.
From
Stream
BPCD
CDU
Gas to C 5
855
Lt naphtha to 212
F
5,219.5
Hvy naphtha to
380
F
7,100
Thermal cracker
Gas to C 5
852
Lt naphtha to 212
F
436.5
Hvy naphtha to
380
F
577.7
The hydrotreaters
Gas to C 5
Mostly H 2 S to
treating
Lt naphtha to 212
F
323.5
Hvy naphtha to
380
F
940.5
Unstabilized naphtha feed to naphtha
hydrotreater
Gas to C 5
1,707
Light naphtha
5,981
Heavy naphtha
8,618
Total
16,306
Light naphtha to gasoline pool
Total
5,970
Heavy naphtha feed to cat reformer
Total
8,618
The naphtha hydrotreater (HDS) material balance is in Table 33.
Catalytic reformer operation. The reformer will operate at a severity of 91 RON
and at a reactor pressure of 350 psig.
106
D.S.J. Jones and S.A. Treese