CH CH CH CH
Perylene CH
Tetradecylcyclohexane C 0 H 0
Butyl perylene C 0 H
H H
Eicosane nC 0 H
H
H
H
H
H H
H H
H
H
H
H
H
H
H
H
H H
H
BP = 358˚C H = 14.3 wt% H/C = 2.0 d = 0.8219
BP = 343˚C H = 15 wt% H/C = 2.1 D = 0.787 g/cc Best Olen yields
BP = 407˚C H = 7.0 wt% H/C = 0.9 d = 1.13
BP = 468˚C H = 4.8 wt% H/C = 0.6 d = 1.3
Worst Olen yields
Very Low coking
Very High coking
Figure 4 Characterisation of different C₂0 species
5 for crude cracking. Desalted crude is preheated to mod- erate temperatures in the convection section and sent to the HOPS unit. Here, the crude feed is mixed with super- heated dilution steam. The HOPS unit contains trays and/ or packing. Dilution steam reduces the hydrocarbon partial pressure and reduces the vapourisation temperature. The overhead temperature is controlled, and only the vapour (vapourised hydrocarbons + dilution steam) is sent to the lower portion (hot flue gas region) of the convection sec - tion for further superheating and then cracked in the radi- ant section.
With the improved HOPS design, the cut-point overlap is significantly reduced. First-generation HOPS units have been successfully operating since the 1990s for conden- sate cracking. Condensates are like light crudes with the tail portion end boiling point well over 700ºC. The bottom frac- tion of the HOPS unit (unvapourised crude) can be sent to another heater for further preheating and then to another HOPS tower and/or processed further by different technol- ogies, such as hydrocracking, fluid catalytic cracking, and delayed coking. When using a second HOPS, it is known as two-stage HOPS. One can consider two or three stages
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