## 3 Results
### Commercial Distillation Test Results  
Table 2 summarizes the operating conditions in the FCC feed hydrotreating section during the commercial test with and without processing H-Oil heavy distillates in the FCC feed hydrotreater stabilization column. For a better understanding of the meaning of the process parameters shown in Table 2, a more detailed diagram of the FCC feed hydrotreating section stabilization column and the stripping column is given in Figure 6. \begin{table}
\begin{tabular}{l c c c} \hline \hline
**Process Parameters in the LNB FCC Feed Hydrotreating Section** & **Unit** & **Case 1** & **Case 2** \\ \hline Charge heater inlet temperature & \({}^{\circ}\)C & 339 & 340 \\ Inlet pressure in the charge heater & bar & 44 & 44 \\ First hydrotreating reactor inlet temperature & \({}^{\circ}\)C & 357 & 357 \\ First hydrotreating reactor inlet pressure & bar (g) & 41 & 41 \\ Inlet temperature in the heater, heating the stabilization column feed & \({}^{\circ}\)C & 301 & 302 \\ Stabilization column feed inlet temperature & \({}^{\circ}\)C & 374 & 375 \\ Stabilization column top temperature & \({}^{\circ}\)C & 100 & 100 \\ Stabilization column first packing bed temperature & \({}^{\circ}\)C & 182 & 175 \\ Stabilization column second packing bed temperature & \({}^{\circ}\)C & 293 & 298 \\ Stabilization column bottom temperature & \({}^{\circ}\)C & 359 & 355 \\ Stabilization column top pressure & bar (g) & 0.39 & 0.4 \\ Stabilization column bottom pressure & bar (g) & 0.52 & 0.52 \\ Steam rate in the bottom of the stabilization column & kg/h & 3852 & 3952 \\ Steam rate in the stripping column & kg/h & 120 & 120 \\ Hydrotreated VGO (bottom) product temperature & \({}^{\circ}\)C & 374 & 376 \\ Fuel gas rate in the heater, heating the stabilization column feed & nm\({}^{3}\)/h & 1562 & 1779 \\ Stabilization column wash oil rate & m\({}^{3}\)/h & 9.0 & 11.6 \\ First pump around rate (below the first packing bed) & m\({}^{3}\)/h & 127 & 125 \\ Second pump around rate (below the second packing bed) & m\({}^{3}\)/h & 30 & 31 \\ First pass rate during the heater, heating the stabilization column feed & m\({}^{3}\)/h & 72 & 69 \\ Second pass rate during the heater, heating the stabilization column feed & m\({}^{3}\)/h & 68 & 69 \\ Third pass rate during the heater, heating the stabilization column feed & m\({}^{3}\)/h & 83 & 83 \\ Fourth pass rate during the heater, heating the stabilization column feed & m\({}^{3}\)/h & 74 & 77 \\ Fifth pass rate during the heater, heating the stabilization column feed & m\({}^{3}\)/h & 131 & 126 \\ Sixth pass rate during the heater, heating the stabilization column feed & m\({}^{3}\)/h & 134 & 128 \\ Feed flow rate of the FCC feed hydrotreating section & t/h & 160 & 160 \\ Flow rate of H-Oil heavy distillate blend & t/h & 0 & 39 \\ Percent of opening the valve providing recycling during the heater, heating the stabilization column feed & \% & 19 & 3 \\ \hline \hline \end{tabular}
\end{table} 
Table 2: Operating conditions during the commercial test without (Case 1) and with (Case 2) processing of H-Oil heavy distillates in the FCC feed hydrotreater stabilization column. Figure 5: HTSD and physical vacuum distillation (ASTM D 1160) data for H-Oil HAGO (**a**), and LVGO (**b**). Figure 6: Process diagram of the LNB FCCPT stabilization column. It is evident from the data in Table 2 that the operating conditions in the FCC feed hydrotreating section were almost the same for both studied cases. This may imply that any additional quantity of produced diesel in the FCC feed hydrotreating section should come from the additional H-Oil VGO blend processed in the stabilization column. Table 3 presents data of the material balance of the LNB FCC feed hydrotreating section (called also FCC pretreater) for both studied cases in this research: Case 1--without processing H-Oil heavy distillates (VGO = vacuum gas oil); and Case 2--with processing H-Oil VGO.