diff options
Diffstat (limited to 'Fluidization_Engineering/ch17.ipynb')
| -rw-r--r-- | Fluidization_Engineering/ch17.ipynb | 451 |
1 files changed, 451 insertions, 0 deletions
diff --git a/Fluidization_Engineering/ch17.ipynb b/Fluidization_Engineering/ch17.ipynb new file mode 100644 index 00000000..a51249d4 --- /dev/null +++ b/Fluidization_Engineering/ch17.ipynb @@ -0,0 +1,451 @@ +{ + "metadata": { + "name": "ch17" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 17 : Design of Catalytic Reactors" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 1, Page 434\n" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "#Reactor Development Program\n", + "\n", + "#Variable Declaration\n", + "dt=[0.081,0.205,3.6]; #Reactor diameter for the three reactors in m\n", + "dte=[0.04,0.12,0.70]; #Equivalent diameters for the three reactors in m\n", + "db=[0.05,0.057,0.07]; #Estimated bubble size in the three reactors in m\n", + "Kr1=1.3889; #Kinet1ic constant for Reaction 1 in s**-1\n", + "Kr2=0.6111; #Kinetic constant for Reaction 2 in s**-1\n", + "Kr3=0.022; #Kinetic constant for Reaction 3 in s**-1\n", + "dp=60.; #Particle size in micrometer\n", + "ephsilonm=0.50; #Void fraction of fixed bed\n", + "ephsilonmf=0.55; #Void fraction at minimum fluidized condition\n", + "umf=0.006; #Velocity at minimum fluidization condition in m/s\n", + "D=2E-5; #Diffusion coefficient of gas in m**2/s\n", + "gammab=0.005; #Ratio of volume of dispersed solids to that of bubble phase\n", + "uo=0.2; #Superficial gas velocity in m/s\n", + "XA=0.9; #Conversion\n", + "g=9.81; #Acceleration due to gravity in square m/s**2\n", + "\n", + "#CALCULATION\n", + "Kr12=Kr1+Kr2;\n", + "n=len(dt);\n", + "i=0;\n", + "ubr = [0,0,0]\n", + "ub = [0,0,0]\n", + "delta = [0,0,0]\n", + "ephsilonf = [0,0,0]\n", + "gammac = [0,0,0]\n", + "gammae = [0,0,0]\n", + "Kbc = [0,0,0]\n", + "Kce = [0,0,0]\n", + "Kf12 = [0,0,0]\n", + "Kf3 = [0,0,0]\n", + "KfA = [0,0,0]\n", + "KfAR = [0,0,0]\n", + "KfAR1 = [0,0,0]\n", + "tou = [0,0,0]\n", + "y = [0,0,0]\n", + "SR = [0,0,0]\n", + "XA1 = [0,0,0]\n", + "y1 = [0,0,0]\n", + "y2 = [0,0,0]\n", + "tou2 = [0,0,0]\n", + "Lf = [0,0,0]\n", + "Lm = [0,0,0]\n", + "XA2 = [0,0,0]\n", + "\n", + "import math\n", + "while i<n:\n", + " #Preliminary Calcualtions\n", + " ubr[i]=0.711*(g*db[i])**0.5;#Rise velocity of bubble from Eqn.(6.7)\n", + " ub[i]=1.55*((uo-umf)+14.1*(db[i]+0.005))*dte[i]**0.32+ubr[i];#Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)\n", + " delta[i]=uo/ub[i];#Fraction of bed in bubbles from Eqn.(6.29)\n", + " ephsilonf[i]=1-(1-delta[i])*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n", + " fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n", + " gammac[i]=(1-ephsilonmf)*((3/(ubr[i]*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n", + " gammae[i]=((1-ephsilonmf)*((1-delta[i])/delta[i]))-gammab-gammac[i];#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n", + " Kbc[i]=4.5*(umf/db[i])+5.85*((D**0.5*g**0.25)/db[i]**(5/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n", + " Kce[i]=6.77*((D*ephsilonmf*0.711*(g*db[i])**0.5)/db[i]**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n", + " #Effective rate constant from Eqn.(12.32)\n", + " Kf12[i]=(gammab*Kr12+1/((1/Kbc[i])+(1/(gammac[i]*Kr12+1/((1/Kce[i])+(1/(gammae[i]*Kr12)))))))*(delta[i]/(1-ephsilonf[i]));\n", + " #Rate of reaction 2 for fluidized bed from Eqn.(12.14)\n", + " Kf3[i]=(gammab*Kr3+1/((1/Kbc[i])+(1/(gammac[i]*Kr3+1/((1/Kce[i])+(1/(gammae[i]*Kr3)))))))*(delta[i]/(1-ephsilonf[i]));\n", + " #Rate of raection with respect to A from Eqn.(12.35)\n", + " KfA[i]=((Kbc[i]*Kce[i]/gammac[i]**2+(Kr12+Kce[i]/gammac[i]+Kce[i]/ \\\n", + " gammae[i])*(Kr3+Kce[i]/gammac[i]+Kce[i]/gammae[i]))*delta[i]*Kbc[i] \\\n", + " *Kr12*Kr3/(1-ephsilonf[i]))/(((Kr12+Kbc[i]/gammac[i])* \\\n", + " (Kr12+Kce[i]/gammae[i])+Kr12*Kce[i]/gammac[i])*((Kr3+Kbc[i]/gammac[i])* \\\n", + " (Kr3+Kce[i]/gammae[i])+Kr3*Kce[i]/gammac[i]));\n", + " KfAR[i]=((Kr1/Kr12)*Kf12[i])-KfA[i];#Rate of reaction from Eqn.(12.34)\n", + " KfAR1[i]=((Kr1/Kr12)*Kf12[i]);#Since KfA is small\n", + " #(b)Relate Selectivity with conversion in three reactors\n", + " x=-math.log(1-XA);#The term Kf12*tou in Eqn.(12.26)\n", + " tou[i]=x/Kf12[i];#Residence time from Eqn.(12.26)\n", + " y[i]=(KfAR1[i]/(Kf3[i]-Kf12[i]))*(math.exp(-x)-math.exp(-tou[i]*Kf3[i]));#CR/CAi from Eqn.(12.27)\n", + " SR[i]=y[i]/XA;#Selectivity of R\n", + " #(c)Relate exit composition to space time\n", + " tou1=5;#Space time in s\n", + " XA1[i]=1-math.exp(-Kf12[i]*tou1);#Conversion from Eqn.(12.26)\n", + " y1[i]=((KfAR1[i]/(Kf12[i]-Kf3[i]))*(math.exp(-Kf3[i]*tou1)-math.exp(-Kf12[i]*tou1)));#CR/CAi R from Eqn.(12.27)\n", + " #(d)Calculate height of bed needed to maximize production\n", + " y2[i]=(KfAR1[i]/Kf12[i])*(Kf12[i]/Kf3[i])**(Kf3[i]/(Kf3[i]-Kf12[i]));#CRmax/CAi R from Eqn.(12.37)\n", + " tou2[i]=math.log(Kf3[i]/Kf12[i])/(Kf3[i]-Kf12[i]);#Space time from Eqn.(38)\n", + " Lf[i]=(uo/(1-ephsilonf[i]))*tou2[i];#Length of bed at fully fluidized condition from Eqn.(12.5)\n", + " Lm[i]=Lf[i]*(1-ephsilonf[i])/(1-ephsilonm);#Length of bed when settled\n", + " XA2[i]=1-math.exp(-Kf12[i]*tou2[i]);#Conversion from Eqn.(12.26)\n", + " i=i+1;\n", + "\n", + "#OUTPUT\n", + "print 'Let Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively'\n", + "print '(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo)',\n", + "print '\\tReactor No.\\tKf12(s**-1)\\tuo(m/s)'\n", + "i=0;\n", + "while i<n:\n", + " print '\\t%1.0f'%i\n", + " print '\\t\\t%f'%Kf12[i],\n", + " print '\\t%f'%uo\n", + " i=i+1;\n", + "\n", + "print '\\n(b)Relation between selectivity with conversion'\n", + "print '\\n\\tReactor No.\\tKf12(s**-1)\\tSR(mol R formed/mol A reacted)'\n", + "i=0\n", + "while i<n:\n", + " print '\\t%1.0f'%i,\n", + " print '\\t\\t%f'%Kf12[i],\n", + " print '\\t%f'%SR[i]\n", + " i=i+1;\n", + "\n", + "print '(c)Relation between exit compostion and space time',\n", + "print '\\tReactor No.\\tXA\\t\\tCR/CAi'\n", + "i=0;\n", + "while i<n:\n", + " print '\\t%1.0f'%i,\n", + " print '\\t\\t%f'%XA1[i],\n", + " print '\\t%f'%y1[i]\n", + " i=i+1;\n", + "\n", + "print '(d)Height of bed needed to maximize the production of acrylonitrile',\n", + "print '\\tReactor No.\\tLm(m)\\t\\tXA'\n", + "i=0;\n", + "while i<n:\n", + " print '\\t%1.0f'%i,\n", + " print '\\t\\t%f'%Lm[i],\n", + " print '\\t%f'%XA2[i]\n", + " i=i+1;\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Let Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively\n", + "(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo) \tReactor No.\tKf12(s**-1)\tuo(m/s)\n", + "\t0\n", + "\t\t0.410042 \t0.200000\n", + "\t1\n", + "\t\t0.270620 \t0.200000\n", + "\t2\n", + "\t\t0.128980 \t0.200000\n", + "\n", + "(b)Relation between selectivity with conversion\n", + "\n", + "\tReactor No.\tKf12(s**-1)\tSR(mol R formed/mol A reacted)\n", + "\t0 \t\t0.410042 \t0.641507\n", + "\t1 \t\t0.270620 \t0.618358\n", + "\t2 \t\t0.128980 \t0.558283\n", + "(c)Relation between exit compostion and space time \tReactor No.\tXA\t\tCR/CAi\n", + "\t0 \t\t0.871292 \t0.564802\n", + "\t1 \t\t0.741562 \t0.484243\n", + "\t2 \t\t0.475286 \t0.313823\n", + "(d)Height of bed needed to maximize the production of acrylonitrile \tReactor No.\tLm(m)\t\tXA\n", + "\t0 \t\t3.056064 \t0.956404\n", + "\t1 \t\t4.137401 \t0.939139\n", + "\t2 \t\t7.049378 \t0.897005\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 2, Page 438\n" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "#Design of a Commercial Acrylonitrile Reactor\n", + "\n", + "#Variable Declaration\n", + "deltaHr=5.15E8; #Heat of reaction in J/k mol\n", + "W=5E4; #Weight of acrylonitirle produced per 334-day year in tonnes\n", + "db=0.07; #Estimated bubble size in m\n", + "dte=0.7; #Equivalent diameter in m\n", + "Kf12=0.35; #Effective rate constant in s**-1 from Example 1\n", + "dp=60; #Particle size in micrometer\n", + "ephsilonm=0.50; #Void fraction of fixed bed\n", + "ephsilonmf=0.55;#Void fraction at minimum fluidized condition\n", + "T=460; #Temperature in reactor in degree C\n", + "Pr=2.5; #Pressure inside reactor in bar\n", + "#Feed gas composition\n", + "x1=1; #Propylene\n", + "x2=1.1; #Ammonia\n", + "x3=11; #Air\n", + "do1=0.08; #OD of heat exchanger tubes in m\\\n", + "L=7; #Length of tubes in m\n", + "ho=300; #Outside heat transfer coefficient in W/m**2 K\n", + "hi=1800; #Inside heat transfer coefficient in W/m**2 K\n", + "Tc=253.4; #Temperature of coolant in degree C\n", + "pi=3.14;\n", + "\n", + "#CALCULATION\n", + "#Preliminary calculation\n", + "uo=0.46;#Superficial gas velocity from Fig.E1(a) for the value of Kf12 & db\n", + "tou=8;#Space time from Fig.E2(b) for highest concentraion of product R\n", + "Lm=uo*tou/(1-ephsilonm);\n", + "y=0.58;#CR/CAi from Fig.E1(c) for the value of tou & Kf12\n", + "XA=0.95#From Fig.E1(c) for the value of tou & Kf12\n", + "SR=y/XA;#Selectivity of R\n", + "\n", + "#Cross-sectional area of the reactor\n", + "P=W*10**3/(334*24*3600);#Production rate of acrylonitrile\n", + "F=(P/0.053)/(SR*XA/0.042);#Feed rate of propylene\n", + "V=((F*22.4*(T+273)*(x1+x2+x3))/(42*273*Pr));\n", + "At=V/uo;#Cross-sectional area of reactor needed for the fluidized bed\n", + "\n", + "#Heat exchanger calculation\n", + "q=F*XA*deltaHr/42;#Rate of heat liberation in the reactor\n", + "U=(ho**-1+hi**-1)**-1;#Overall heat transfer coefficient\n", + "deltaT=T-Tc;#Driving force for heat transfer\n", + "Aw=q/(U*deltaT);#Heat exchanger area required to remove q\n", + "Nt=Aw/(pi*do1*L);\n", + "li1=(At/Nt)**0.5;#Pitch for square pitch arrangement\n", + "dte1=4*(li1**2-(pi/4)*do1**2)/(pi*do1);\n", + "if dte1>dte:\n", + " li=(pi/4*dte*do1+pi/4*do1**2)**0.5;#Pitch if we add dummy tubes\n", + "import math\n", + "f=li**2-pi/4*do1**2;#Fraction of bed cross section taken up by tubes\n", + "dt1=math.sqrt(4/pi*At/(1-f));#Reactor diameter including all its tubes\n", + "\n", + "#OUTPUT\n", + "print 'Superficial gas velocity=%fm/s'%uo\n", + "print 'No. of %1.0fm tubes required=%1.0f'%(L,Nt);\n", + "print 'Reactor diameter=%fm'%dt1\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Superficial gas velocity=0.460000m/s\n", + "No. of 7m tubes required=295\n", + "Reactor diameter=7.173176m\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 3, Page 444\n" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "#Reactor-Regenerator with Circulating Catalyst: Catalytic Cracking\n", + "\n", + "#Variable Declaration\n", + "db=0.08; #Estimated bubble size in m\n", + "dte=2; #Equivalent diameter in m\n", + "F1=55.6; #Feed rate of oil in kg/s\n", + "XA=0.63; #Conversion\n", + "uo=0.6; #Superficial gas velocity in m/s\n", + "T1=500.0; #Temperature of reactor in degree C\n", + "T2=580.0; #Temperature of regenerator in degree C\n", + "Fs=F1*23.3; #Solid circulation rate from Ex.(15.2)\n", + "rhos=1200.0; #Density of catalyst in kg/m**3\n", + "dpbar=60.0; #Average particle size in micrometer\n", + "ephsilonm=0.50;#Void fraction of fixed bed\n", + "ephsilonmf=0.55;#Void fraction at minimum fluidized condition\n", + "umf=0.006; #Velocity at minimum fluidization condition in m/s\n", + "dt=8.0; #Diameter of reactor in m\n", + "D=2E-5; #Diffusion coefficient of gas in m**2/s\n", + "Kr=8.6; #Rate constant for reaction at 500 degree C in s**-1\n", + "Ka1=0.06; #Rate constant for deactivatiion at 500 degree C in s**-1\n", + "Ka2=0.012; #Rate constant for regeneration at 580 degree C in s**-1\n", + "gammab=0.005; #Ratio of volume of dispersed solids to that of bubble phase\n", + "g=9.81; #Acceleration due to gravity in square m/s**2\n", + "pi=3.14;\n", + "\n", + "#CALCULATION\n", + "#Parameters for the fluidized reactor\n", + "ubr=0.711*(g*db)**0.5;#Rise velocity of bubble from Eqn.(6.7)\n", + "ub=1.55*((uo-umf)+14.1*(db+0.005))*dte**0.32+ubr;#Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)\n", + "delta=uo/ub;#Fraction of bed in bubbles from Eqn.(6.29)\n", + "ephsilonf=1-(1-delta)*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n", + "fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n", + "gammac=(1-ephsilonmf)*((3/(ubr*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n", + "gammae=((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n", + "Kbc=4.5*(umf/db)+5.85*((D**0.5*g**0.25)/db**(5.0/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n", + "Kce=6.77*((D*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n", + "import math\n", + "#Bed height versus catalyst activity in reactor\n", + "a1bar=0.07;#Guess value for average activity in reactor\n", + "x=Kr*a1bar;#Value of Kra1 to be used in the following equation\n", + "Kf=(gammab*x+1/((1/Kbc)+(1/(gammac*x+1/((1/Kce)+(1/(gammae*x)))))))*(delta/(1-ephsilonf));#Effective rate constant from Eqn.(12.14)\n", + "tou=-math.log(1-XA)/Kf;#Space time from Eqn.(12.16)\n", + "Lm=tou*uo/(1-ephsilonm);#Length of fixed bed for guess value of a1bar\n", + "a1bar1=[0.0233,0.0465,0.0698,0.0930,0.116,0.140];#Various activity values to find Lm\n", + "x1 = [0,0,0,0,0,0]\n", + "Kf1 = [0,0,0,0,0,0]\n", + "tou1 = [0,0,0,0,0,0]\n", + "Lm1 = [0,0,0,0,0,0]\n", + "\n", + "n=len(a1bar1);\n", + "i=0;\n", + "while i<n:\n", + " x1[i]=Kr*a1bar1[i];\n", + " Kf1[i]=(gammab*x1[i]+1/((1/Kbc)+(1/(gammac*x1[i]+1/((1/Kce)+ \\\n", + " (1/(gammae*x1[i])))))))*(delta/(1-ephsilonf));\n", + " #Effective rate constant from Eqn.(12.14)\n", + " \n", + " tou1[i]=-math.log(1-XA)/Kf1[i];#Space time from Eqn.(12.16)\n", + " Lm1[i]=tou1[i]*uo/(1-ephsilonm);\n", + " #Length of fixed bed for guess value of a1bar...Condition [i]\n", + " i=i+1;\n", + "\n", + "#Find the optimum size ratio for various a1bar\n", + "Lm=[5,6,7,8,10,12];\n", + "W1 = [0,0,0,0,0,0]\n", + "t1bar = [0,0,0,0,0,0]\n", + "t2bar = [0,0,0,0,0,0]\n", + "a1bar2 = [0,0,0,0,0,0]\n", + "m=len(Lm);\n", + "i=0;\n", + "while i<m:\n", + " W1[i]=(pi/4)*dt**2*rhos*(1-ephsilonm)*Lm[i];#Bed weight\n", + " t1bar[i]=W1[i]/Fs;#Mean residence time of solids in reactor\n", + " t2bar[i]=t1bar[i]*(Ka1/Ka2)**0.5;#Mean residence time of soilds at optimum from Eqn.(16)\n", + " a1bar2[i]=(Ka2*t2bar[i])/(Ka1*t1bar[i]+Ka1*t1bar[i]*Ka2*t2bar[i]+Ka2*t2bar[i]);#From Eqn.(15)...Condition (ii)\n", + " i=i+1;\n", + "\n", + "#Final design values\n", + "Lm4=7.3;#For satisfying condition [i] & (ii)\n", + "a1bar3=0.0744;#By interpolation\n", + "x2=a1bar3*Kr;\n", + "W11=(pi/4)*dt**2*rhos*(1-ephsilonm)*Lm4;#Bed weight for reactor\n", + "t1bar1=W11/Fs;#Mean residence time of solids in reactor\n", + "a2bar=(1+Ka1*t1bar1)*a1bar3;#Average activity in regenrator from Eqn.(10)\n", + "t2bar1=t1bar1*(Ka1/Ka2)**0.5;#Mean residence time of solids in regenerator from Eqn.(16)\n", + "W2=W11*(t2bar1/t1bar1);#Bed weight for regenerator\n", + "dt2=dt*(W2/W11)**0.5;#Diameter of regenerator assuming same static bed height for reactor and regerator\n", + "\n", + "#OUTPUT\n", + "print 'Bed height versus catalyst activity in reactor'\n", + "print '\\tAverage activity',\n", + "print '\\tLength of fixed bed(m)'\n", + "i=0;\n", + "while i<n:\n", + " print '\\t%f'%a1bar1[i],\n", + " print '\\t\\t%f'%Lm1[i];\n", + " i=i+1;\n", + "\n", + "print 'Optimum size ratio for various activity in reactor'\n", + "print '\\tLength of fixed bed(m)',\n", + "print '\\tAverage activity'\n", + "i=0\n", + "while i<m:\n", + " print '\\t%f'%Lm[i],\n", + " print '\\t\\t%f'%a1bar2[i]\n", + " i=i+1;\n", + "\n", + "print 'Final design values'\n", + "print '\\tDiameter of reactor(m):%.0f'%dt\n", + "print '\\tBed weight for reactor(tons):%.0f'%(W11/10**3)\n", + "print '\\tBed weight for regenerator(tons):%.0f'%(W2/10**3)\n", + "print '\\tDiameter of regenerator(m):%.0f'%(dt2);\n", + "print '\\tSolid circulation rate(tons/hr):%f'%(Fs*3.6);\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Bed height versus catalyst activity in reactor\n", + "\tAverage activity \tLength of fixed bed(m)\n", + "\t0.023300 \t\t11.059747\n", + "\t0.046500 \t\t7.911053\n", + "\t0.069800 \t\t6.756202\n", + "\t0.093000 \t\t6.118750\n", + "\t0.116000 \t\t5.696470\n", + "\t0.140000 \t\t5.372072\n", + "Optimum size ratio for various activity in reactor\n", + "\tLength of fixed bed(m) \tAverage activity\n", + "\t5.000000 \t\t0.097879\n", + "\t6.000000 \t\t0.086112\n", + "\t7.000000 \t\t0.076871\n", + "\t8.000000 \t\t0.069420\n", + "\t10.000000 \t\t0.058149\n", + "\t12.000000 \t\t0.050026\n", + "Final design values\n", + "\tDiameter of reactor(m):8\n", + "\tBed weight for reactor(tons):220\n", + "\tBed weight for regenerator(tons):492\n", + "\tDiameter of regenerator(m):12\n", + "\tSolid circulation rate(tons/hr):4663.728000\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file |