PACKED BED CATALYTIC REACTOR - MATEEN 2392.08 mol% at %...

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MATEEN total kg /hr in 2392.08 mol% at % conversion 0.5 Hf inlet condition g.mol outlet condition g.mol j/mol CH4 15234 0.31 CH4 7617 -74776.02 S 67000 0.69 S 36532 0 impurities 153.58 0 H2S 15234 -19938.6 82387.58 1 CS2 7617 117499.8 temp. 973 K 67000 Qin Qp Qr CH4 -542786630.13 2065516096.49 ### S -2683549754.6 Qin total -3226336384.73 25.42 We know that for adiabatic operation Qr +Qp+Qin =0 so 0.3 GRAPH PLOT 0.1 0.5561117 0.2 0.6952169 0.3 0.8939746 0.4 1.1921793 0.5 1.6694491 ra (total area under curve 0.44 now in g mol CH4 15234.0 S2 33500.0 IMP 153.580 TOTAL n 48887.580 Tin 973.000 Pin 3.000 TOTAL VOLUME 1300.99 m3/hr FA0 48887.5800 Mmol/h Coh4 0.01 mol/L CoS2 0.03 mol/L Xa 0.5 M 2.2 LOG k 3.85 K 7029.49 0 hr T = volume of catalyst/volumetric flow rate 17.66 sec SPACE VELOCITY s=1/T 203.81 so volume of catalyst = T*volumetric flow rate 6.38 m3 density of catalyst ρp = 750 kg/m3 4787.62 kg φ porosity 0.4 hr -1 Weight of catalyst = ρp x Volume of catalyst Volume of Reactor = Vol. of catalyst x (1+φ) 0.1 0.15 0.2 0.25 0.3 0.35 0.4 0.0000000 0.2000000 0.4000000 0.6000000 0.8000000 1.0000000 1.2000000 1.4000000 1.6000000 1.8000000
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8.94 m3 To find length and diameter take L/D = 6 so V =π/4(5D3) so D 3= 1.9 D = 1.24 m so L = 6.19 Extra length added for porcelin balls to support the catalyst = 0.2 So actual length = 7.43 PRESSURE DROP CALCULATIONS using urgun eq Where mass velocity of feed= G = Mass flow rate / Cross sectional area
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PACKED BED CATALYTIC REACTOR - MATEEN 2392.08 mol% at %...

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