Equipment Calculations HDS_rahul

Equipment Calculations HDS_rahul - 1.5 m 1.7 m 1 m 15.93 m...

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Unformatted text preview: 1.5 m 1.7 m 1 m 15.93 m 2.1 m 4.2 m 60 o C 380 o C T out T int 370 o C Heat Exchanger Furnace Question 1: Catalyst volume required With the information of WHSV and feed rate Catalyst volume follows as = Vc Feed RateWHSV Where feed rate includes Recycle and Fresh gas Flow = . . = Vc 268 751 1 244 m3 Question 2: Adiabatic Temperature Rise Assuming that Recycle and Fresh gas has no Sulphur, Adiabatic temperature rise can be calculated by the use of Enthalpy graph for reactant charge / effluent streams and with the knowledge of amount of sulphur converted. = * . = Sulphur in 6000 0 017 102td = . * = . Sulphur removed 0 9 102 91 8td = . Heat Released 88 3MJt = . * = Total Heat Released 88 3 6450 569535MJd = . Inlet Enthalpy @ 370 C 4 15 E06 MJd = . + = . Outlet Enthalpy 4 15 E06 569535 4 72 E 06 MJd = Outlet Temperature from graph 390 C Question 3: Reactor Sizing superficial velocity (hot liquid load at reactor inlet) is 40 m/h , and that the velocity can be calculated as volumetric flow rate over section: And Cross sectional area can be calculated as Taking density from given graph at average temperature of 375 C 380 o C, (485 Kg/m3) and dividing the inlet mass flow rate by it, volumetric flow rate follows as Volumetric Flow = 554 m3/hr C S area = 13.9 m2 From Circular section, the reactor diameter found is D = 4.2 m Taking into account that Volume = Section Length Length of catalyst bed = 17.7 m Taking into account the inter bed, top tray arrangement and hemi spherical top/bottom height total vessel length follows as Total vessel height = 25.5 m Where Catalysts to catalyst height = 1m Height required for top tray arrangement = 1.5 mHeight required for top tray arrangement = 1....
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Equipment Calculations HDS_rahul - 1.5 m 1.7 m 1 m 15.93 m...

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