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DESIGN CALCULATIONS OF MULTI

# DESIGN CALCULATIONS OF MULTI - DESIGN CALCULATIONS OF...

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DESIGN CALCULATIONS OF MULTI-TUBULAR FIXED BED REACTOR Heating fluid out Heating fluid in Feed Stream Product Stream

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Volume of Reactor Volumetric flow rate of feed to reactor = V o = 2500 m 3 /hr V/FA 0 = 1/kCA 0 [(1+ε) ln 1/ (1-X) - εX] CA 0 = 0.0347 Kmol/m 3 FA 0 = 0.0241kmol/s ε = 0.9 k = 0.2996 m 3 gas/ m 3 reactor s Volume of reactor = 8.26m 3 Space Time τ = 1/k [(1+ε) ln 1/ (1-X) - εX] = 11.898 sec Weight of Catalyst (Nickle Oxide Catalyst on Alumina Support of size 2 mm of granules shape is used) Volume of reactor = 8.26 m 3 Porosity for granules = 0.4 So volume of catalyst = 0.6 × 8.26 = 4.956 m 3 Particle Density of catalyst = 2500 Kg/m 3 mass of catalyst = 2500 × 4.956 = 12390 Kg
Number of Tubes Length of tube = 20 ft = 6.098 m To calculate tube dia As we know that to prevent deviation from plug flow assumption D t /D p > 15 Where D t = dia of tube D p = dia of particle Let inside dia of tube = 2.204 in = 55.98 mm D t /D p = 55.98/2 = 27.99 which is satisfactory Volume of one tube = π /4 × D t 2 × L t = 3.14/4 × (55.98/1000) 2 × 6.098 = 0.0278 m 3 As total volume = 8.26 m 3 So number of tubes required = 668 tubes Diameter of Shell To calculate shell dia eq. (from Ludwig) ( 29 ( 29 ( 29 ( 29 2 t 4 3 1 s t 2 2 1 s T P 1.223 K nK K - D P - K 4 π K - D N +

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DESIGN CALCULATIONS OF MULTI - DESIGN CALCULATIONS OF...

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