PSD of SO treated in 1st chamber
PSD of SO treated in 2nd chamber
20
20
15
15
10
10
5
5
0
0
nm(10 m) -9
nm(10 m) -9
PSD of solids removed in 1st chamber
PSD of solids removed in 2nd chamber
80
40
60
30
40
20
20
10
0
0
nm(10 m) -9
nm(10 m) -9
Figure 2 PSD of solids removed in first and second UMF chambers/slurry oil exiting first and second UMF chambers
2 , where SO exiting the first chamber contained mainly 6-500 nm particles, but still had 20% 6,000+ nm par - ticles. SO exiting second chamber contained only 9-44 nm particles (no 6,000+ nm particles). Most larger par - ticles (2,600-6,000+ nm [63.3%]) were removed by the first chamber. Smaller particles (800-6,000+ nm [33.4%]) were removed by the second chamber. Figure 3 compares the PSD of the original (SO-O), treated (SO-1), and dupli - cate treated (SO-1A) slurry oil, based on the analysis of all samples collected from the experiments. The result confirmed that any solid particles having a size larger than 50 nm (44.3 nm) were successfully removed from the slurry oil by MagAFS process technol - ogy. It is also possible to provide low-cost and convenient
on-site testing by installing a small portable MagAFS unit through a slip-stream connection without disruption to normal FCC unit operations. Q What FCC and hydrotreater modifications are needed to increase refinery coprocessing of renewable feedstocks? A Francy Barrios, Technology Engineer in FCC and Sweetening Processes, Axens Renewable feeds available for co-processing in FCC units present different properties and impurities compared to conventional feedstock, impacting operation, heat bal - ance, catalyst activity, and unit performance. This impact will even depend on the co-processing ratio. The main
80
Original
Treated
Duplicate treated SO-1A
60
SO-O
SO-1
40
20
0
nm(10 m) -9
Figure 3 Comparison of PSD of original and treated slurry oil
13
PTQ Q1 2025
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