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Unformatted text preview: Post Masters Program Process and Product Design PROCESS DESIGN COURSE Eindhoven University of Technology Chemical Engineering and Chemistry Department EQUIPMENT CALCULATIONS GASOIL HDS Results by Branislav Manic Antonio M. Matarredona Ruiz Raul Velasco Pelaez Supervised by Prof. Geert Thielemans Eindhoven, 11 February 2009 Process Design Course Equipment Calculations Gasoil HDS A new 6000 t/d gasoil HDS will be built. The basic design information is provided. Feedstock 1 is the design case with fresh gas from the platformer. 1.  Calculation of required volume of catalyst From the package, it is known that WHSV = 1.1 t/(m 3 h) . As the definition for WHSV is CAT R V F WHSV = the volume of catalyst can be isolated from the former expression as WHSV F V R CAT = And as h t 250 h 24 d 1 d t 6000 F R = = then V CAT = 227.3 m 3 2.  Adiabatic temperature rise From the data available, it is known that the temperature of the reactor inlet is: T inlet =370 o C and that the heat of reaction is: _________________________________________________________________________________________ 2 Process Design Course Equipment Calculations Gasoil HDS sd MJ 10 71 . 6 sd t 6000 ton MJ 8 . 111 H 5 r = = From the figure Enthalpy of Combined Reactor Charge/Effluent, locating T=370 o C in horizontal axis and going up to the curve, in vertical axis the enthalpy of charge can be found. Adding enthalpy of reaction to this value, coming back horizontally to the curve of effluent and coming down to horizontal axis, a temperature of 400 o C is found. This way, the adiabatic temperature rise is: T ad =30 o C 3.  Sizing of reactor Overall dimensions The volume needed for the reaction is the calculated volume for the catalyst. This is: V CAT = 227.3 m 3 As it is known that 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: Section F velocity V = the section can be calculated as: velocity F Section V = _________________________________________________________________________________________ 3 Process Design Course Equipment Calculations Gasoil HDS As, taking density from figure Actual Density of Combined Reactor Charge/Effluent Liquid for an average temperature of 375 o C, h / m 5 . 515 t 485 . m 1 h 24 d 1 d t 6000 F 3 3 V = = Then, the section obtained is: Section = 12.9 m 2 And, from circular section, the reactor diameter found is: D = 4m Taking into account that Volume = Section Length The total catalyst length obtained is: L CAT = 17.6 m As the total calculated adiabatic temperature rise is 30 o C and it is only allowed a temperature rise of 10 o C, the catalyst will be divided in 3 beds . Then, two interstage cooling stages are needed....
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This note was uploaded on 02/18/2010 for the course CHEMICAL E 121 taught by Professor Rahul during the Spring '10 term at Punjab Engineering College.
 Spring '10
 Rahul
 Chemistry

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