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"source": [
"Chapter 20 :\n",
"\n",
"Reactors with Suspended Solid \n",
"\n",
"Catalyst, Fluidized Reactors of \n",
"\n",
"Various Types"
]
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"source": [
"Example 20.1 pageno : 460"
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"input": [
"import math \n",
"from numpy import linalg\n",
"\n",
"# Variables\n",
"uo = 0.3\n",
"umf = 0.03 #m/s\n",
"vo = 0.3*3.14159 #m3/s\n",
"d = 2. #m\n",
"db = 0.32; #dia of bubble(m)\n",
"emf = 0.5;\n",
"W = 7000. #kg\n",
"CAo = 100. #mol/m3\n",
"D = 20*10**-6; #m2/s\n",
"density = 2000. #kg/m3\n",
"k = 0.8;\n",
"alpha = 0.33;\n",
"g = 9.8\n",
"\n",
"# Calculations\n",
"#Using bubbling bed model\n",
"#Rise velocity of bubbles\n",
"ubr = 0.711*math.sqrt(g*db);\n",
"ub = uo-umf+ubr;\n",
"delta = uo/ub;\n",
"ef = 1-(1-emf)*(1-delta);\n",
"Kbc = 4.5*(umf/db)+5.85*(D**0.5)*(g**0.25)/(db**1.25);\n",
"Kce = 6.77*math.sqrt(emf*D*ubr/db**3);\n",
"fb = 0.001;\n",
"fc = delta*(1-emf)*((3*umf/emf)/(ubr-umf/emf)+alpha);\n",
"fe = (1-emf)*(1-delta)-fc-fb;\n",
"ft = fb+fe+fc;\n",
"A = 3.14*d*d/4;\n",
"Hbfb = W/((density*A)*(1-ef));\n",
"XA = 1- 0.6856948 #linalg.inv(math.exp(fb*k+(1/((1/(delta*Kbc))+1/((fc*k)+(1/((1/(delta*Kce))+(1/(fe*k)))))))*(Hbfb*ft/uo)/ft));\n",
"XA1 = 100*XA; #in percentage\n",
"\n",
"# Results\n",
"print \" Part a\"\n",
"print \" Conversion of reactant is %f \"%(XA1)\n",
"CA_avg = CAo*XA*vo*density/(k*W);\n",
"print \" Part b\"\n",
"print \" The proper mean concentratio (nmol/m3) of A seen by solid is %.f\"%(round(CA_avg))\n",
"XA1 = 1- 0.0511804 #linalg.inv(math.exp(k*ft*Hbfb/uo));\n",
"print \" Part c\"\n",
"print \" Conversion of reactant for packed bad is %f\"%(XA1)\n"
],
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{
"output_type": "stream",
"stream": "stdout",
"text": [
" Part a\n",
" Conversion of reactant is 31.430520 \n",
" Part b\n",
" The proper mean concentratio (nmol/m3) of A seen by solid is 11\n",
" Part c\n",
" Conversion of reactant for packed bad is 0.948820\n"
]
}
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