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diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/10-Gas_Dispersion_and_Gas_Interchange_in_Bubbling_Beds.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/10-Gas_Dispersion_and_Gas_Interchange_in_Bubbling_Beds.ipynb new file mode 100644 index 0000000..f8796a7 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/10-Gas_Dispersion_and_Gas_Interchange_in_Bubbling_Beds.ipynb @@ -0,0 +1,237 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 10: Gas Dispersion and Gas Interchange in Bubbling Beds" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 10.1: Estimate_Interchange_Coefficients_in_Bubbling_Beds.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-10, Example 1, Page 253\n", +"//Title: Estimate Interchange Coefficients in Bubbling Beds\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"umf=[0.01;0.045];//Velocity at minimum fluidization condition in m/s\n", +"ephsilonmf=[0.5;0.5];//Void fraction at minimum fluidization condition\n", +"D=[2E-5;7E-5];//Diffusion coefficient of gas in m^2/s\n", +"g=9.81;//Acceleration due to gravity in m/s^2\n", +"\n", +"//CALCULATION\n", +"db=[5;10;15;20];\n", +"n=length(umf);\n", +"m=length(db)'\n", +"for i = 1:n\n", +" for j = 1:m\n", +" Kbc(i,j)=4.5*(umf(i)/db(j))+5.85*((D(i)^0.5*g^0.25)/db(j)^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(27)\n", +" Kce(i,j)=6.77*((D(i)*ephsilonmf(i)*0.711*(g*db(j))^0.5)/db(j)^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(34)\n", +" Kbe(i,j)=(Kbc(i,j)*Kce(i,j))/(Kbc(i,j)+Kce(i,j));//Gas interchange coefficient between bubble and emulsion from Eqn.(14)\n", +" end;\n", +"end\n", +"\n", +"//OUTPUT\n", +"i=1;\n", +"j=1;\n", +"k=1;\n", +"while k<=m*n\n", +" printf('\n\t\tKbc for fine particles and He');\n", +" printf('\tKbc for coarse particles and ozone');\n", +" printf('\tKbe for fine particles and He');\n", +" printf('\tKbe for coarse particles and ozone');\n", +" while j<=m\n", +" mprintf('\ndb=%fm',db(j)*10^-2);\n", +" while i<=n\n", +" mprintf('\t%f',Kbc(k));\n", +" mprintf('\t\t\t%f',Kbe(k));\n", +" i=i+1; \n", +" k=k+1;\n", +" printf('\t\t\t');\n", +" end\n", +" i=1;\n", +" j=j+1;\n", +" end\n", +"end\n", +"Kbe=Kbe';\n", +"Kbc=Kbc';\n", +"plot2d('ll',db,[Kbc Kbe]);\n", +"xtitle('Plot of Kbc,Kbe vs db','db',['Kbc','Kbe']);\n", +"printf('\nComparing the points with the plot of Kbc,Kbe vs db in Fig.(12), we can conlcude the following:');\n", +"printf('\nKbc for fine particles and helium: line 2 in Fig.(12)');\n", +"printf('\nKbc for coarser particles and ozone: line 3 in Fig.(12)');\n", +"printf('\nKbe for fine particles and helium: line 4 in Fig.(12)');\n", +"printf('\nKbe for coarser particles and ozone: line 5 in Fig.(12)');\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 10.2: Compare_the_Relative_Importance_of_Kbc_and_Kce.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-10, Example 2, Page 254\n", +"//Title: Compare the Relative Importance of Kbc and Kce\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"D=0.69;//Diffusion coefficient of gas in cm^2/s\n", +"umf=1.0;//Velocity at minimum fluidization condition in cm/s\n", +"ephsilonmf=0.5;//Void fraction at minimum fluidization condition\n", +"db=[5;15];//Equilibrium bubble size in cm\n", +"g=980;//Acceleration due to gravity in cm/s^2\n", +"\n", +"//CALCULATION\n", +"n=length(db);\n", +"i=1;\n", +"while i<=n\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.(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.(34)\n", +" Kbe(i)=(Kbc(i)*Kce(i))/(Kbc(i)+Kce(i));//Gas interchange coefficient between bubble and emulsion from Eqn.(14)\n", +" e(i)=(Kce(i)-Kbe(i))/Kbe(i);//Error when minor resistance is ignored\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\ndb(cm)');\n", +"printf('\t\tCalculated Kbc');\n", +"printf('\tCalculated Kce');\n", +"printf('\t\tKbe from Eqn.(14)');\n", +"printf('\tErron when minor resistance is ignored (in percentage)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',db(i));\n", +" mprintf('\t%f',Kbc(i));\n", +" mprintf('\t%f',Kce(i));\n", +" mprintf('\t\t%f',Kbe(i));\n", +" mprintf('\t\t%f',e(i)*100);\n", +" i=i+1; \n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 10.3: Compare_Interchange_Rates_for_Adsorbed_and_Nonadsorbed_Gases.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-10, Example 3, Page 255\n", +"//Title: Compare Interchange Rates for Adsorbed and Nonadsorbed Gases\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Kbe=[0.028;0.05];//Reported range for gas interchange coefficient between bubble and emulsion\n", +"uo=0.30;//Superficial gas velocity in m/s\n", +"db=0.13;//Equilibrium bubble size in m\n", +"m=7;\n", +"ephsilonmf=0.5;//Void fraction at minimum fluidization condition\n", +"umf=0.0018;//Velocity at minimum fluidization condition in m/s\n", +"D=[9E-6;22E-6];//Diffusion coefficient of gas in m^2/s\n", +"g=9.81;//Acceleration due to gravity in m/s^2\n", +"\n", +"//CALCULATION\n", +"n=length(Kbe);\n", +"i=1;\n", +"while i<=n\n", +" Kbem(i)=(6/db)*Kbe(i);//Gas interchange coefficient between bubble and emulsion from Eqn.(19)\n", +" Kbc(i)=4.5*(umf/db)+5.85*((D(i)^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(27)\n", +" Kce(i)=6.77*((D(i)*ephsilonmf*0.711*(g*db)^0.5)/db^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(34)\n", +" Kbe(i)=(Kbc(i)*Kce(i))/(Kbc(i)+Kce(i));//Gas interchange coefficient between bubble and emulsion from Eqn.(14)\n", +" c(i)=(Kbem(i)/Kbe(i));\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nKbe from Eqn.(19)');\n", +"printf('\tKbc from Eqn.(27)');\n", +"printf('\tKce from Eqn.(34)');\n", +"printf('\tKbe from Eqn.(14)');\n", +"printf('\tComparison of Kbe from Eqn.(19) and that from Eqn.(14)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',Kbem(i));\n", +" mprintf('\t\t%f',Kbc(i));\n", +" mprintf('\t\t%f',Kce(i));\n", +" mprintf('\t\t%f',Kbe(i));\n", +" mprintf('\t\t%f',c(i));\n", +" i=i+1; \n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/11-Particle_to_Gas_Mass_and_Heat_Transfer.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/11-Particle_to_Gas_Mass_and_Heat_Transfer.ipynb new file mode 100644 index 0000000..3b0aae6 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/11-Particle_to_Gas_Mass_and_Heat_Transfer.ipynb @@ -0,0 +1,295 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 11: Particle to Gas Mass and Heat Transfer" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 11.1: Fitting_Reported_Mass_Transfer_Data_with_the_Bubbling_Bed_Model.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-11, Example 1, Page 265\n", +"//Title: Fitting Reported Mass Transfer Data with the Bubbling Bed Model\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"db=0.37;//Equilibrium bubble size in cm\n", +"dp=0.028;//Particle size in cm\n", +"rhos=1.06;//Density of solids in g/cc\n", +"ephsilonmf=0.5;//Void fraction at minimum fluidization condition\n", +"phis=0.4;//Sphericity of solids\n", +"gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase\n", +"rhog=1.18E-3;//Density of air in g/cc\n", +"myu=1.8E-4;//Viscosity of gas in g/cm s\n", +"D=0.065;//Diffusion coefficient of gas in cm^2/s\n", +"Sc=2.35;//Schmidt number\n", +"etad=1;//Adsorption efficiency factor\n", +"y=1;\n", +"umf=1.21;//Velocity at minimum fluidization condition in cm/s\n", +"ut=69;//Terminal velocity in cm/s\n", +"g=980;//Acceleration due to gravity in square cm/s^2\n", +"uo=[10;20;30;40;50];//Superficial gas velocity in cm/s\n", +"\n", +"//CALCULATION\n", +"n=length(uo);\n", +"i=1;\n", +"Rept=(dp*ut*rhog)/myu;\n", +"Shstar=2+(0.6*(Rept^0.5)*(Sc^(1/3)));//Sherwood no. from Eqn.(1)\n", +"Kbc=4.5*(umf/db)+5.85*((D^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of the bubble\n", +"while i<=n\n", +" x(i)=(uo(i)-umf)/(ubr*(1-ephsilonmf));//The term delta/(1-epshilonf) after simplification\n", +" Shbed(i)=x(i)*[(gammab*Shstar*etad)+((phis*dp^2*y)/(6*D))*Kbc];//Sherwood no. from Eqn.(11)\n", +" Rep(i)=(dp*uo(i)*rhog)/myu;//Reynolds of the particle\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nThe desired result is the relationship between Shbed and Rep The points gives a straight line of the form y=mx+c');\n", +"printf('\nRep');\n", +"printf('\t\tShbed');\n", +"i=1;\n", +"while i<=n\n", +" printf('\n%f',Rep(i));\n", +" printf('\t%f',Shbed(i));\n", +" i=i+1;\n", +"end\n", +"plot(Rep,Shbed);\n", +"xlabel('Rep');\n", +"ylabel('Shbed');\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 11.2: The_Effect_of_m_on_Bubble_Emulsion_Interchange.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-11, Example 2, Page 267\n", +"//Title: The Effect of m on Bubble-Emulsion Interchange\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"umf=0.12;//Velocity at minimum fluidization condition in cm/s\n", +"uo=40;//Superficial gas velocity in cm/s\n", +"ub=120;//Velocity of the bubble in cm/s\n", +"D=0.7;//Diffusion coefficient of gas in cm^2/s\n", +"abkbe1=1;//Bubble-emuslion interchange coefficient for non absorbing particles(m=0)\n", +"abkbe2=18;//Bubble-emuslion interchange coefficient for highly absorbing particles(m=infinity)\n", +"g=980;//Acceleration due to gravity in square cm/s^2\n", +"\n", +"//CALCULATION\n", +"//For non absorbing particles m=0,etad=0\n", +"Kbc=(ub/uo)*(abkbe1);\n", +"dbguess=2;//Guess value of db\n", +"function[fn]=solver_func(db)//Function defined for solving the system\n", +" fn=abkbe1-(uo/ub)*(4.5*(umf/db)+5.85*(D^0.5*g^0.25)/(db^(5/4)));//Eqn.(10.27)\n", +"endfunction\n", +"[d]=fsolve(dbguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(10.27) for db\n", +"//For highly absorbing particles m=infinity, etad=1\n", +"M=abkbe2-(uo/ub)*Kbc;\n", +"//For intermediate condition\n", +"alpha=100;\n", +"m=10;\n", +"etad=1/(1+(alpha/m));//Fitted adsorption efficiency factor from Eqn.(23)\n", +"abkbe3=M*etad+(uo/ub)*Kbc;\n", +"\n", +"//OUTPUT\n", +"mprintf('\nFor non absorbing particles:\n\tDiameter of bubble=%fcm\n\tBubble-cloud interchange coefficient=%fs^-1',d,Kbc);\n", +"mprintf('\nFor highly absorbing partilces:\n\tM=%f',M);\n", +"mprintf('\nFor intermediate condition:\n\tFitted adsorption efficiency factor:%f\n\tBubble-emuslion interchange coefficient:%fs^-1',etad,abkbe3);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 11.3: Fitting_Reported_Heat_Transfer_Data_with_the_Bubbling_Bed_Model.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-11, Example 3, Page 273\n", +"//Title: Fitting Reported Heat Transfer Data with the Bubbling Bed Model\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhos=1.3;//Density of solids in g/cc\n", +"phis=0.806;//Sphericity of solids\n", +"gammab=0.001;//Ratio of volume of dispersed solids to that of bubble phase\n", +"rhog=1.18E-3;//Density of air in g/cc\n", +"Pr=0.69;//Prandtl number\n", +"myu=1.8E-4;//Viscosity of gas in g/cm s\n", +"Cpg=1.00;//Specific heat capacity of gas in J/g K\n", +"ephsilonmf=0.45;//Void fraction at minimum fluidization condition\n", +"kg=2.61E-4;//Thermal concuctivity of gas in W/cm k\n", +"dp=0.036;//Particle size in cm\n", +"umf=6.5;//Velocity at minimum fluidization condition in cm/s\n", +"ut=150;//Terminal velocity in cm/s\n", +"db=0.4;//Equilibrium bubble size in cm\n", +"etah=1;//Efficiency of heat transfer\n", +"uo=[10;20;30;40;50];//Superficial gas velocity in cm/s\n", +"g=980;//Acceleration due to gravity in square cm/s^2\n", +"\n", +"//CALCULATION\n", +"Nustar=2+[((dp*ut*rhog)/myu)^0.5*Pr^(1/3)];//Nusselt no. from Eqn.(25)\n", +"Hbc=4.5*(umf*rhog*Cpg/db)+5.85*((kg*rhog*Cpg)^0.5*g^0.25/db^(5/4));//Total heat interchange across the bubble-cloud boundary from Eqn.(32)\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of the bubble from Eqn.(6.7)\n", +"n=length(uo);\n", +"i=1;\n", +"while i<=n\n", +" x(i)=(uo(i)-umf)/(ubr*(1-ephsilonmf));//The term delta/(1-epshilonf) after simplification\n", +" Nubed(i)=x(i)*[gammab*Nustar*etah+(phis*dp^2/(6*kg))*Hbc];//Nusselt no. from Eqn.(36)\n", +" Rep(i)=(dp*uo(i)*rhog)/myu;//Reynolds of the particle\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nThe desired result is the relationship between Nubed and Rep which is in the form of a straight line y=mx+c');\n", +"printf('\nRep');\n", +"printf('\t\tNubed');\n", +"i=1;\n", +"while i<=n\n", +" printf('\n%f',Rep(i));\n", +" printf('\t%f',Nubed(i));\n", +" i=i+1;\n", +"end\n", +"plot(Rep,Nubed);\n", +"xlabel('Rep');\n", +"ylabel('Nubed');\n", +" \n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 11.4: Heating_a_Particle_in_a_Fluidized_Bed.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-11, Example 4, Page 274\n", +"//Title: Heating a Particle in a Fluidized Bed\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhog=1.2;//Density of air in kg/m^3\n", +"myu=1.8E-5;//Viscosity of gas in kg/m s\n", +"kg=2.6E-2;//Thermal concuctivity of gas in W/m k\n", +"dp=1E-4;//Particle size in m\n", +"rhos=8920;//Density of solids in kg/m^3\n", +"Cps=390;//Specific heat capacity of the solid in J/kg K\n", +"ephsilonf=0.5;//Void fraction of the fluidized bed\n", +"umf=0.1;//Velocity at minimum fluidization condition in m/s\n", +"uo=0.1;//Superficial gas velocity in m/s\n", +"pi=3.14\n", +"\n", +"//CALCULATION\n", +"to=0;//Initial temperature of the bed\n", +"T=100;//Temperature of the bed\n", +"t=0.99*T;//Particle temperature i.e. when it approaches 1% of the bed temperature\n", +"mp=(pi/6)*dp^3*rhos;//Mass of the particle\n", +"A=pi*dp^2;//Surface area of the particle\n", +"Rep=(dp*uo*rhog)/myu;//Reynold's no. of the particle\n", +"Nubed=0.0178;//Nusselt no. from Fig.(6)\n", +"hbed1=(Nubed*kg)/dp;//Heat transfer coefficient of the bed\n", +"t1=(mp*Cps/(hbed1*A))*log((T-to)/(T-t));//Time needed for the particle approach 1 percentage of the bed temperature in case(a)\n", +"hbed2=140*hbed1;//Since from Fig.(6) Nup is 140 times Nubed\n", +"t2=(mp*Cps/(hbed2*A))*log((T-to)/(T-t));//Time needed for the particle approach 1 percentage of the bed temperature in case(b)\n", +"\n", +"//OUTPUT\n", +"printf('\nCase(a):Using the whole bed coefficient from Fig.(6)');\n", +"mprintf('\n\tTime needed for the particle approach 1 percentage of the bed temperature is %fs',t1);\n", +"printf('\nCase(b):Uisng the single-particle coefficient of Eqn.(25),also shown in Fig.(6)');\n", +"mprintf('\n\tTime needed for the particle approach 1 percentage of the bed temperature is %fs',t2);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/12-Conversion_of_Gas_in_Catalytic_Reactions.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/12-Conversion_of_Gas_in_Catalytic_Reactions.ipynb new file mode 100644 index 0000000..273c27d --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/12-Conversion_of_Gas_in_Catalytic_Reactions.ipynb @@ -0,0 +1,344 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 12: Conversion of Gas in Catalytic Reactions" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 12.1: Fine_Particle_Geldart_A_Bubbling_Bed_Reactor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-12, Example 1, Page 293\n", +"//Title: Fine Particle (Geldart A) Bubbling Bed Reactor\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Kr=10;//rate constant in m^3 gas/m^3 cat s\n", +"D=2E-5;//Diffusion coefficient of gas in m^2/s\n", +"dpbar=68;//Average partilce size in micrometers\n", +"ephsilonm=0.5;//Void fraction of fixed bed\n", +"gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase\n", +"ephsilonmf=0.55;//Void fraction at minimum fluidization condition\n", +"umf=0.006;//Velocity at minimum fluidization condition in m/s\n", +"db=0.04;//Equilibrium bubble size in m\n", +"Lm=0.7;//Length of the bed in m\n", +"uo=0.1;//Superficial gas velocity in m/s\n", +"dbed=0.26;//Diameter of the bed in m\n", +"g=9.81;//Acceleration due to gravity in square m/s^2\n", +"\n", +"//CALCULATION\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)\n", +"Kbc=4.5*(umf/db)+5.85*((D^0.5*g^0.25)/db^(5/4));//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", +"delta=uo/ub;//Fraction of bed in bubbles from Eqn.(6.29)\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", +"ephsilonf=1-(1-delta)*(1-ephsilonmf);//Void fraction of fixed bed from Eqn.(6.20)\n", +"Lf=(1-ephsilonm)*Lm/(1-ephsilonf);//Length of fixed bed from Eqn.(6.19)\n", +"Krtou=Kr*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)\n", +"Kf=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Raction rate for fluidized bed from Eqn.(14)\n", +"XA=1-exp(-1*Kf*Lf/ub);//Conversion from Eqn.(16)\n", +"\n", +"//OUTPUT\n", +"mprintf('\nThe dimnesionless reaction rate group: %f',Krtou);\n", +"mprintf('\nThe reaction rate for fluidized bed: %fs^-1',Kf);\n", +"mprintf('\nConversion: %f',XA);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 12.2: Commercial_Sized_Phthalic_Anhydride_Reactor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-12, Example 2, Page 298\n", +"//Title: Commercial-Sized Phthalic Anhydride Reactor\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"umf=0.005;//Velocity at minimum fluidization condition in m/s\n", +"ephsilonm=0.52;//Void fraction of fixed bed\n", +"ephsilonmf=0.57;//Void fraction at minimum fluidization condition\n", +"DA=8.1E-6;//Diffusion coefficient of gas in m^2/s\n", +"DR=8.4E-6;//Diffusion coefficient of gas in m^2/s\n", +"Lm=5;//Length of the bed in m\n", +"dte=1;//Diameter of tube in m\n", +"Kr1=1.5;//rate constant in m^3 gas/m^3 cat s\n", +"Kr3=0.01;//rate constant in m^3 gas/m^3 cat s\n", +"gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase\n", +"uo=0.45;//Superficial gas velocity in m/s\n", +"db=0.05;//Equilibrium bubble size in m from Fig.(6.8)\n", +"ub=1.5;//Velocity of bubbles in bubbling bed in m/s from Fig.(6.11(a))\n", +"g=9.81;//Acceleration due to gravity in square m/s^2\n", +"\n", +"//CALCULATION\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"KbcA=4.5*(umf/db)+5.85*((DA^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n", +"KceA=6.77*((DA*ephsilonmf*0.711*(g*db)^0.5)/db^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n", +"KbcR=4.5*(umf/db)+5.85*((DR^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n", +"KceR=6.77*((DR*ephsilonmf*0.711*(g*db)^0.5)/db^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n", +"delta=uo/ub;//Fraction of bed in bubbles from Eqn.(6.29)\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", +"ephsilonf=1-(1-delta)*(1-ephsilonmf);//Void fraction of fixed bed from Eqn.(6.20)\n", +"Lf=(1-ephsilonm)*Lm/(1-ephsilonf);//Length of fixed bed from Eqn.(6.19)\n", +"Krtou=Kr1*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)\n", +"Kr12=Kr1;//Since the reactions are a special case of Denbigh scheme\n", +"Kr34=Kr3;\n", +"Kf1=(gammab*Kr12+1/((1/KbcA)+(1/(gammac*Kr12+1/((1/KceA)+(1/(gammae*Kr12)))))))*(delta/(1-ephsilonf));//Rate of reaction 1 for fluidized bed from Eqn.(14)\n", +"Kf3=(gammab*Kr34+1/((1/KbcR)+(1/(gammac*Kr34+1/((1/KceR)+(1/(gammae*Kr34)))))))*(delta/(1-ephsilonf));//Rate of reaction 2 for fluidized bed from Eqn.(14)\n", +"Kf12=Kf1;\n", +"Kf34=Kf3;\n", +"KfA=[[KbcR*KceA/gammac^2+(Kr12+KceA/gammac+KceA/gammae)*(Kr34+KceR/gammac+KceR/gammae)]*delta*KbcA*Kr12*Kr34/(1-ephsilonf)]/[[(Kr12+KbcA/gammac)*(Kr12+KceA/gammae)+Kr12*KceA/gammac]*[(Kr34+KbcR/gammac)*(Kr34+KceR/gammae)+Kr34*KceR/gammac]];//Rate of raection with respect to A from Eqn.(35)\n", +"KfAR=Kr1/Kr12*Kf12-KfA;//Rate of reaction from Eqn.(34)\n", +"tou=Lf*(1-ephsilonf)/uo;//Residence time from Eqn.(5)\n", +"XA=1-exp(-Kf1*tou);//Conversion of A from Eqn.(26)\n", +"XR=1-((KfAR/(Kf12-Kf34))*[exp(-Kf34*tou)-exp(-Kf12*tou)]);//Conversion of R from Eqn.(27)\n", +"SR=(1-XR)/XA;//Selectivity of R\n", +"\n", +"//OUTPUT\n", +"\n", +"mprintf('\nRate of reaction 1 for fluidized bed:%f',Kf1);\n", +"mprintf('\nRate of reaction 2 for fluidized bed:%f',Kf3);\n", +"mprintf('\nRate of reaction 1 with respect to A:%f',KfA);\n", +"mprintf('\nThe Conversion of Napthalene:%f percentage',XA*100);\n", +"mprintf('\nThe selectivity of Phthalic anhydride:%f percentage',SR*100);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 12.3: Bubbling_Bed_Reactor_for_Intermediate_Sized_Reactor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-12, Example 3, Page 302\n", +"//Title: Bubbling Bed Reactor for Intermediate Sized Reactor\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Kr=3;//rate constant in m^3 gas/m^3 cat s\n", +"db=0.12;//Equilibrium bubble size in m\n", +"D=9E-5;//Diffusion coefficient of gas in m^2/s\n", +"dpbar=68;//Average partilce size in micrometers\n", +"ephsilonm=0.42;//Void fraction of fixed bed\n", +"uo=0.4;//Superficial gas velocity in m/s\n", +"Lm=0.8;//Length of the bed in m\n", +"ephsilonmf=0.45;//Void fraction at minimum fluidization condition\n", +"umf=0.21;//Velocity at minimum fluidization condition in m/s\n", +"gammab=0;//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", +"\n", +"//CALCULATION\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)\n", +"ubstar=ub+3*umf;//Rise velocity of the bubble gas from Eqn.(45)\n", +"delta=(uo-umf)/(ub+umf);//Fraction of bed in bubbles from Eqn.(6.46)\n", +"Kbe=4.5*(umf/db);//Interchange coefficient between bubble and emulsion from Eqn.(47)\n", +"Lf=Lm*(1-ephsilonm)/((1-delta)*(1-ephsilonmf));//Length of fixed bed\n", +"phi=[(Kr/Kbe)^2*{(1-ephsilonmf)-gammab*(umf/ubstar)}^2+((delta/(1-delta))+umf/ubstar)^2+2*(Kr/Kbe)*{(1-ephsilonmf)-gammab*(umf/ubstar)}*((delta/(1-delta))-umf/ubstar)]^0.5;//From Eqn.(52)\n", +"q1=0.5*Kr/umf*{(1-ephsilonmf)+gammab*(umf/ubstar)}+0.5*Kbe/umf*{((delta/(1-delta))+umf/ubstar)-phi};//From Eqn.(50)\n", +"q2=0.5*Kr/umf*{(1-ephsilonmf)+gammab*(umf/ubstar)}+0.5*Kbe/umf*{((delta/(1-delta))+umf/ubstar)+phi};//From Eqn.(50)\n", +"si1=0.5-0.5*((1-delta)/delta)*[umf/ubstar-Kr/Kbe*{(1-ephsilonmf)-gammab*(umf/ubstar)}-phi];//From Eqn.(51)\n", +"si2=0.5-0.5*((1-delta)/delta)*[umf/ubstar-Kr/Kbe*{(1-ephsilonmf)-gammab*(umf/ubstar)}+phi];//From Eqn.(51)\n", +"XA=1-(delta/(1-delta))*(1/(uo*phi))*[(1-si2)*{si1*delta*ubstar+(1-delta)*umf}*exp(-q1*Lf)+(si1-1)*{si2*delta*ubstar+(1-delta)*umf}*exp(-q2*Lf)];//Conversion from Eqn.(49)\n", +"Krtou=Kr*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)\n", +"\n", +"//OUTPUT\n", +"mprintf('\nCOmparing the values of 1-XA = %f and Krtou = %f with Fig.(6), we can conlcude that this operating condition is shown as point A in Fig.(3)',1-XA,Krtou);\n", +"printf('\nLine 2 gives the locus of conversions for different values of the reaction rate group for this fluidized contacting');\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 12.4: Reaction_in_the_Slow_Bubble_Regime.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-12, Example 4, Page 305\n", +"//Title: Reaction in the Slow Bubble Regime\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"uo=0.25;//Superficial gas velocity in m/s\n", +"db=0.025;//Equilibrium bubble size in m\n", +"Kr=1.5;//rate constant in m^3 gas/m^3 cat s\n", +"umf=0.21;//Velocity at minimum fluidization condition in m/s\n", +"Lm=0.8;//Length of the bed in m\n", +"ephsilonm=0.42;//Void fraction of fixed bed\n", +"g=9.81;//Acceleration due to gravity in square m/s^2\n", +"\n", +"//CALCULATION\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)\n", +"delta=(uo-umf)/(ub+2*umf);//Fraction of bed in bubbles from Eqn.(55) since ub/umf<<1 \n", +"XA=1-exp(-Kr*Lm*((1-ephsilonm)/uo)*(umf/uo)*(1-delta));//Conversion from Eqn.(57)\n", +"Krtou=Kr*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)\n", +"\n", +"\n", +"//OUTPUT\n", +"mprintf('\nComparing the values of 1-XA = %f and Krtou = %f with Fig.(6), we can conlcude that this operating condition is shown as point B in Fig.(3)',1-XA,Krtou);\n", +"printf('\nLine 3 gives the locus of conversions for different values of the reaction rate group for this fluidized contacting');\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 12.5: Conversion_in_the_Freeboard_of_a_Reactor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-12, Example 5, Page 307\n", +"//Title: Conversion in the Freeboard of a Reactor\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"uo=0.3;//Superficial gas velocity in m/s\n", +"Lf=1.1;//Length of fixed bed in m\n", +"Hf=1.2;//Length of freeboard in m\n", +"db=0.04;//Equilibrium bubble size in m\n", +"umf=0.006;//Velocity at minimum fluidization condition in m/s\n", +"ephsilonmf=0.55;//Void fraction at minimum fluidization condition\n", +"gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase\n", +"Kr=10;//rate constant in m^3 gas/m^3 cat s\n", +"D=2E-5;//Diffusion coefficient of gas in m^2/s\n", +"g=9.81;//Acceleration due to gravity in square m/s^2\n", +"\n", +"//CALCULATION\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)\n", +"Kbc=4.5*(umf/db)+5.85*((D^0.5*g^0.25)/db^(5/4));//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", +"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", +"Kf=(gammab*Kr)+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Raction rate for fluidized bed from Eqn.(14)\n", +"XA=1-exp(-1*Kf*Lf/ub);//Conversion at the top of dense bed from Eqn.(16)\n", +"etabed=(Kf*delta)/(Kr*(1-ephsilonf));//Reactor efficiency from Eqn.(22)\n", +"a=0.6/uo//Since uoa = 0.6s^-1 from Fig.(5)\n", +"adash=6.62;//From Fig.(5)\n", +"XA1=1-1/(exp(((1-ephsilonf)*Kr/(uo*a))*[(1-exp(-a*Hf))-((1-etabed)/(1+(adash/a)))*(1-exp(-(a+adash)*Hf))]));//Conversion from Eqn.(64)\n", +"XA2=1-(1-XA1)*(1-XA);//Conversion at the exit from Eqn.(64)\n", +"\n", +"//OUTPUT\n", +"printf('\nThe conversion:');\n", +"mprintf('\n\tAt the top pf the dense bed: %f percentage',XA*100);\n", +"mprintf('\n\tAt the reactor exit: %f percentage',XA2*100);\n", +"\n", +"//Disclaimer: The value of kf deviate from the one given in textbook, where as it is close to the value obtained by manual calculation. \n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/13-Heat_Transfer_between_Fluidized_Beds_and_Surfaces.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/13-Heat_Transfer_between_Fluidized_Beds_and_Surfaces.ipynb new file mode 100644 index 0000000..a8623b8 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/13-Heat_Transfer_between_Fluidized_Beds_and_Surfaces.ipynb @@ -0,0 +1,275 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 13: Heat Transfer between Fluidized Beds and Surfaces" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 13.1: h_on_a_Horizontal_Tube_Bank.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-13, Example 1, Page 331\n", +"//Title: h on a Horizontal Tube Bank\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dp=57;//Particle size in micrometer\n", +"rhos=940;//Density of solids in kg/m^3\n", +"Cps=828;//Specific heat capacity of the solid in J/kg K\n", +"ks=0.20;//Thermal conductivity of solids in W/m k\n", +"kg=0.035;//Thermal concuctivity of gas in W/m k\n", +"umf=0.006;//Velocity at minimum fluidization condition in m/s\n", +"ephsilonmf=0.476;//Void fraction at minimum fluidization condition\n", +"do1=0.0254;//Outside diameter of tube in m\n", +"L=1;\n", +"uo=[0.05;0.1;0.2;0.35];//Superficial gas velocity in m/s\n", +"nw=[2;3.1;3.4;3.5];//Bubble frequency in s^-1\n", +"g=9.81;//Acceleration due to gravity in square m/s^2\n", +"\n", +"\n", +"//CALCULATION\n", +"dte=4*do1*L/2*L;//Hydraulic diameter from Eqn.(6.13)\n", +"db=(1+1.5)*0.5*dte;//Rise velocity of the bubble\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"phib=0.19;//From Fig.(15) for ks/kg=5.7\n", +"ke=ephsilonmf*kg+(1-ephsilonmf)*ks*[1/((phib*(ks/kg))+(2/3))];//Effective thermal conductivity of bed from Eqn.(3) \n", +"n=length(uo);\n", +"i=1;\n", +"while i<=n\n", +" ub(i)=uo(i)-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)\n", +" delta(i)=uo(i)/ub(i);//Fraction of bed in bubbles from Eqn.(6.29)\n", +" h(i)=1.13*[ke*rhos*(1-ephsilonmf)*Cps*nw(i)*(1-delta(i))]^0.5;//Heat transfer coefficinet from Eqn.(18)\n", +" i=i+1;\n", +"end \n", +"\n", +"//OUTPUT\n", +"printf('\nSuperficial gas velocity(m/s)');\n", +"printf('\tHeat transfer coefficient(W/m^2 k)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',uo(i));\n", +" mprintf('\t\t\t%f',h(i));\n", +" i=i+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 13.2: Effect_of_Gas_Properties_on_h.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-13, Example 2, Page 332\n", +"//Title: Effect of Gas Properties on h\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dp=80;//Particle size in micrometer\n", +"rhos=2550;//Density of solids in kg/m^3\n", +"Cps=756;//Specific heat capacity of the solid in J/kg K\n", +"ks=1.21;//Thermal conductivity of solids in W/m k\n", +"kg=[0.005;0.02;0.2];//Thermal concuctivity of gas in W/m k\n", +"ephsilonmf=0.476;//Void fraction at minimum fluidization condition\n", +"\n", +"//CALCULATION\n", +"delta=0.5*(0.1+0.3);//For a gently fluidized bed\n", +"nw=3;//Bubble frequency in s^-1 from Fig.(5.12) at about 30cm above the distributor\n", +"n=length(kg);\n", +"i=1;\n", +"while i<=n\n", +" x(i)=ks/kg(i);//To find different values of ks/kg\n", +" i=i+1;\n", +"end\n", +"phib=[0.08;0.10;0.20];//From Fig.(15) for different values of ks/kg\n", +"i=1;\n", +"while i<=n\n", +" ke(i)=ephsilonmf*kg(i)+(1-ephsilonmf)*ks*[1/((phib(i)*(ks/kg(i)))+(2/3))];//Effective thermal conductivity of bed from Eqn.(3)\n", +" h1(i)=1.13*[ke(i)*rhos*(1-ephsilonmf)*Cps*nw*(1-delta)]^0.5;//Heat transfer coefficinet from Eqn.(18)\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nThermal conductivity of Gas(W/m K))');\n", +"printf('\tMax. heat transfer coefficient(W/m^2 k)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',kg(i));\n", +" mprintf('\t\t\t\t%f',h1(i));\n", +" i=i+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 13.3: Effect_of_Particle_Size_on_h.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-13, Example 3, Page 332\n", +"//Title: Effect of Particle Size on h\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhos=2700;//Density of solids in kg/m^3\n", +"Cps=755;//Specific heat capacity of the solid in J/kg K\n", +"ks=1.2;//Thermal conductivity of solids in W/m k\n", +"kg=0.028;//Thermal concuctivity of gas in W/m k\n", +"ephsilonmf=0.476;//Void fraction at minimum fluidization condition\n", +"dp1=10E-3;//Particle size for which h=hmax in m\n", +"hmax=250;//Max. heat transfer coefficient in W/m^2 K \n", +"nw=5;//Bubble frequency in s^-1\n", +"delta=0.1;//Fraction of bed in bubbles\n", +"deltaw=0.1;//Fraction of bed in bubbles in wall region\n", +"dp=2E-3;//Diameter of particle in m\n", +"\n", +"//CALCULATION\n", +"x=ks/kg;\n", +"phib=0.11;\n", +"phiw=0.17;\n", +"ke=ephsilonmf*kg+(1-ephsilonmf)*ks*[1/((phib*(ks/kg))+(2/3))];//Effective thermal conductivity of bed from Eqn.(3)\n", +"hpacket=1.13*[ke*rhos*(1-ephsilonmf)*Cps*nw/(1-deltaw)]^0.5;//Heat transfer coefficient for the packet of emulsion from Eqn.(11)\n", +"ephsilonw=ephsilonmf;//Void fraction in the wall region\n", +"kew=ephsilonw*kg+(1-ephsilonw)*ks*[(phiw*(ks/kg)+(1/3))^-1];//Effective thermal conductivity in the wall region with stagnant gas from Eqn.(4)\n", +"y=(2*kew/dp1)+(hmax*hpacket)/(((1-deltaw)*hpacket)-hmax);//Calculating the term alphaw*Cpg*rhog*uo from Eqn.(16) by rearranging it\n", +"h=(1-deltaw)/((2*kew/dp+y*(dp/dp1)^0.5)^-1+hpacket^-1);//Heat transfer coeeficient from Eqn.(11) by using the value of y \n", +"\n", +"//OUTPUT\n", +"mprintf('\nThe heat transfer coefficient for paricle size of %fm = %fW/m^2 K',dp,h);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 13.4: Freeboard_Heat_Exchange.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-13, Example 4, Page 334\n", +"//Title: Freeboard Heat Exchange\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Hf=4;//Height of freeboard in m\n", +"uo=2.4;//Superficial gas velocity in m/s\n", +"ho=350;//Heat transfer coefficient at the bottom of freeboard region in W/m^2 K\n", +"hg=20;//Heat transfer coefficient in equivalent gas stream, but free of solids in W/m^2 K\n", +"\n", +"//CALCULATION\n", +"zf=[0;0.5;1;1.5;2;2.5;3;3.5;Hf];//Height above the top of the dense bubbling fluidized bed\n", +"hr=0;//Assuming heat transfer due to radiation is negligible\n", +"a=1.5/uo;//Since decay coefficient from Fig.(7.12), a*uo=1.5s^-1 \n", +"n=length(zf);\n", +"i=1;\n", +"while i<=n\n", +" h(i)=(hr+hg)+(ho-hr-hg)*exp(-a*zf(i)/2);//Heat transfer coefficient from Eqn.(24) for zf=Hf\n", +" i=i+1;\n", +"end \n", +"hbar=(hr+hg)+2*(ho-hr-hg)*(1-exp(-a*Hf/2))/(a*Hf);//Mean heat transfer coefficient for the 4-m high freeboard from Eqn.(26)\n", +"\n", +"//OUTPUT\n", +"printf('\nThe required relationship is h(W/m^2 K) vs. zf(m) as in Fig.(9a)');\n", +"printf('\nHeight above the dense bubbling fluidized bed(m))');\n", +"printf('\tHeat transfer coefficient(W/m^2 k)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',zf(i));\n", +" mprintf('\t\t\t\t\t\t%f',h(i));\n", +" i=i+1;\n", +"end\n", +"mprintf('\n\nThe mean heat transfer coefficient for the 4-m high freeboard =%fW/m^2 K',hbar);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/14-The_RTD_and_Size_Distribution_of_Solids_in_Fluidized_Beds.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/14-The_RTD_and_Size_Distribution_of_Solids_in_Fluidized_Beds.ipynb new file mode 100644 index 0000000..9b3c420 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/14-The_RTD_and_Size_Distribution_of_Solids_in_Fluidized_Beds.ipynb @@ -0,0 +1,333 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 14: The RTD and Size Distribution of Solids in Fluidized Beds" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.1: Flow_with_Elutriatio.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-14, Example 1, Page 343\n", +"//Title: Flow with Elutriation\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Fo=2.7;//Feed rate in kg/min\n", +"Fof=0.9;//Feed rate of fines in feed in kg/min\n", +"Foc=1.8;//Feed rate of coarse in feed in kg/min\n", +"W=17;//Bed weight in kg\n", +"kf=0.8;//Elutriation of fines in min^-1\n", +"kc=0.0125;//Elutriation of coarse in min^-1\n", +"\n", +"//CALCULATION\n", +"F1guess=1;//Guess value of F1\n", +"function[fn]=solver_func(F1)//Function defined for solving the system\n", +" fn=F1-(Fof/(1+(W/F1)*kf))-(Foc/(1+(W/F1)*kc));//Eqn.(17)\n", +"endfunction\n", +"[F1]=fsolve(F1guess,solver_func,1E-6);//Inbuilt function fsolve to solve for F1\n", +"F1f=Fof/(1+(W/F1)*kf);//Flow rate of fines in entrained streams from Eqn.(16)\n", +"F1c=Foc/(1+(W/F1)*kc);//Flow rate of coarse in entrained streams from Eqn.(16)\n", +"F2f=Fof-F1f;//Flow rate of fines in overflow streams from Eqn.(9)\n", +"F2c=Foc-F1c;//Flow rate of coarse in overflow streams from Eqn.(9)\n", +"tbarf=1/((F1/W)+kf);//Mean residence time of fines from Eqn.(12)\n", +"tbarc=1/((F1/W)+kc);//Mean residence time of coarse from Eqn.(12)\n", +"\n", +"//OUTPUT\n", +"mprintf('\nFlow rate in entrained stream:\n\tFines:%fkg/min\n\tCoarse:%fkg/min',F1f,F1c);\n", +"mprintf('\nFlow rate in overflow stream:\n\tFines:%fkg/min\n\tCoarse:%fkg/min',F2f,F2c);\n", +"mprintf('\nMean residence time:\n\tFines:%fmins\n\tCoarse:%fmins',tbarf,tbarc);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.2: Flow_with_Elutriation_and_Change_in_Density_of_Solids.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-14, Example 2, Page 344\n", +"//Title: Flow with Elutriation and Change in Density of Solids\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dt=4;//Diameter of reactor in m\n", +"ephsilonm=0.4;//Void fraction of static bed\n", +"rhos=2500;//Density of solid in the bed in kg/m^3\n", +"Lm=1.2;//Height of static bed in m\n", +"Fo=3000;//Feed rate in kg/hr\n", +"beta1=1.2;//Increase in density of solids\n", +"dp=[3;4;5;6;7;8;9;10;11;12;3;14;16;18;20;22;24;26;28;30]*10^-2;//Size of particles in mm\n", +"po=[0;0.3;0.8;1.3;1.9;2.6;3.5;4.4;5.7;6.7;7.5;7.8;7.5;6.3;5.0;3.6;2.4;1.3;0.5;0];//Size distribution of solids in mm^-1\n", +"k=[0;10;9.75;9.5;8.75;7.5;6.0;4.38;2.62;1.20;0.325;0;0;0;0;0;0;0;0;0]*10^-4;//Elutriation constant in s^-1\n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"W=(pi/4*dt^2)*Lm*(1-ephsilonm)*rhos;//Weight of solids in bed\n", +"n=length(dp);\n", +"i=1;\n", +"F1guess=1000;//Guess value for F1\n", +"F1c=2510:10:2700;\n", +"while i<=n\n", +" function[fn]=solver_func(F1)//Function defined for solving the system\n", +" if k(i)==0 then x(i)=0; break \n", +" else x(i)=(po(i)/(W*k(i)/F1))*log(1+(W*k(i)/F1)); \n", +" end\n", +" fn=F1/(Lm*Fo)-x(i);\n", +" endfunction\n", +" [F1(i)]=fsolve(F1guess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(20) for F1\n", +" c(i)=F1c(i)/(Lm*Fo);\n", +" if F1(i)==0 then a(i)=0;\n", +" else a(i)=(po(i)/(W*k(i)/F1(i)))*log(1+(W*k(i)/F1(i)));\n", +" end \n", +" i=i+1;\n", +"end\n", +"plot(F1,a,F1,c);\n", +"xtitle('F1 vs a,c','F1','a,c');\n", +"F1n=2500;//The point were both the curves meet\n", +"F2=beta1*Fo-F1n;//Flow rate of the second leaving stream\n", +"j=1;\n", +"m=length(dp);\n", +"while j<=m\n", +" p1(j)=(1/F1n)*((Fo*po(j))/(1+(W/F1n)*k(j)));//Size distribution of stream 1 in mm^-1 from Eqn.(16)\n", +" p2(j)=k(j)*W*p1(j)/F2;//Size distribution of stream 2 in mm^-1 from Eqn.(7)\n", +" if p1(j)==0 & p2(j)==0 then tbar(j)=0;\n", +" else if p1(j)==0 then tbar(j)=(W*p1(j))/(F2*p2(j));\n", +" else if p2(j)==0 then tbar(j)=(W*p1(j))/(F1n*p1(j));\n", +" else tbar(j)=(W*p1(j))/(F1n*p1(j)+F2*p2(j));//Average time in hr from Eqn.(11)\n", +" end\n", +" end\n", +" end\n", +" j=j+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nFlow rate of stream 1:%fkg/hr',F1n);\n", +"printf('\nFlow rate of stream 2:%fkg/hr',F2);\n", +"j=1;\n", +"mprintf('\ntbar(hr)');\n", +"while j<=m\n", +" mprintf('\n%f',tbar(j));\n", +" j=j+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================\n", +"//DISCLAIMER: The value obtained for tbar is deviating highly form the one given in textbook. However, the value obtained by manual calculation is close to the ones obtained from the program." + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.3: Single_Size_Feed_of_Shrinking_Particles.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-14, Example 3, Page 351\n", +"//Title: Single-Size Feed of Shrinking Particles\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dp=1;//Particle size in mm\n", +"Fo=10;//Feed rate in kg/min\n", +"k=0.1;//Particle shrinkage rate in mm/min\n", +"\n", +"//CALCULATION\n", +"R=k/2;//Particle shrinkage rate in terms of radius\n", +"W=(Fo*dp/2)/(4*R);//Bed weight from Eqn.(42)\n", +"\n", +"//OUTPUT\n", +"printf('\nWeight of bed:%fkg',W);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.4: Wide_Size_Distribution_of_Shrinking_Particle.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-14, Example 4, Page 352\n", +"//Title: Wide Size Distribution of Shrinking Particle\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dpi=[1.05;0.95;0.85;0.75;0.65;0.55;0.45;0.35;0.25;0.15;0.05];//Mean size in mm\n", +"Fo=[0;0.5;3.5;8.8;13.5;17.0;18.2;17.0;13.5;7.3;0]*10^-2;//Feed rate in kg/s\n", +"k=[0;0;0;0;0;0;0;0;2.0;12.5;62.5]*10^-5;//Elutriation constant in s^-1\n", +"R=-1.58*10^-5;//Rate of particle shrinkage in mm/s\n", +"deldpi=0.1;//Size intervals in mm\n", +"\n", +"//CALCULATION\n", +"n=length(dpi);\n", +"m=2;//Starting with the largest value size interval that contains solids\n", +"W(m-1)=0;\n", +"while m<=n\n", +" W(m)=(Fo(m)-R*W(m-1)/deldpi)/(k(m)-R/deldpi-3*R/dpi(m));//From Eqn.(33)\n", +" m=m+1;\n", +"end\n", +"Wt=sum(W);//Total sum\n", +"\n", +"//OUTPUT\n", +"printf('\nTotal mass in the bed:%fkg',Wt);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.5: Elutriation_and_Attrition_of_Catalyst.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-14, Example 5, Page 353\n", +"//Title: Elutriation and Attrition of Catalyst\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dpi=[0.17;0.15;0.13;0.11;0.09;0.07;0.05;0.03;0.01];//Mean size of particles in mm\n", +"a=[0;0.95;2.45;5.2;10.1;23.2;35.65;20.0;2.45]*10^-2;//Feed composition Fo(dpi)/Fo\n", +"y=[0;0;0;0;0;0;0.625;10.225;159.25]*10^-6;//Elutriation and cyclone efficiency k(dpi)(1-eta(dpi))\n", +"F=0.01;//Rate at which solids are withdrawn in kg/s\n", +"W=40000;//Weight of bed in kg\n", +"dp1=0.11//Initial size in mm\n", +"dp2=0.085;//Size after shrinking in mm\n", +"dpmin=0.01;//Minimum size in mm\n", +"deldpi=2*10^-2;//Size inerval in mm\n", +"t=20.8;//Time in days\n", +"si=1;\n", +"\n", +"//CALCULATION\n", +"kdash=log((dp1-dpmin)/(dp2-dpmin))/(t*24*3600);//Rate of particle shrinkage from Eqn.(24)\n", +"n=length(dpi);\n", +"m=2;\n", +"Fo=0.05;//Initial value of Fo\n", +"F1(m-1)=0;\n", +"s=0;\n", +"c=0;\n", +"t=1E-6;\n", +"while m<=n\n", +" R(m)=-kdash*(dpi(m)-dpmin);//Rate of size change\n", +" x(m)=(a(m)*Fo-W*R(m-1)*F1(m-1)/deldpi)/(F+(W*y(m))-(W*R(m)/deldpi)-3*W*R(m)/dpi(m));//Eqn.(34)\n", +" F1(m)=x(m)*F;\n", +" c=c+x(m);\n", +" m=m+1;\n", +" if abs(c-1)<t then break\n", +" end\n", +" Fo=Fo+0.0001;//Incrementing Fo\n", +"end \n", +"\n", +"//OUTPUT\n", +"mprintf('\nFeed rate with deldpi=%fmm is %fg/hr',deldpi,Fo);\n", +"i=1;\n", +"mprintf('\nBed composition');\n", +"while i<=n\n", +" printf('\n%f',x(i)*100);\n", +" i=i+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/15-Circulation_Systems.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/15-Circulation_Systems.ipynb new file mode 100644 index 0000000..723a984 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/15-Circulation_Systems.ipynb @@ -0,0 +1,354 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 15: Circulation Systems" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 15.1: Circulation_Rate_when_Deactivation_Controls.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-15, Example 1, Page 369\n", +"//Title: Circulation Rate when Deactivation Controls\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"thalf=1;//Half life of catalyst in s\n", +"F=960;//Feed rate of oil in tons/day\n", +"W=50;//Weight of the bed in tons\n", +"a=0.5;//Activity after time equal to half life\n", +"abar=0.01;//Average activity of the catalyst\n", +"\n", +"//CALCULATION\n", +"Ka=-log(a)/thalf;//Rate constant is s^-1, assuming I order kinetics from Eqn.(12)\n", +"Fs=Ka*W*abar/(1-abar);//Circulation rate of solids from Eqn.(16)\n", +"x=(Fs*60*60*24)/F;//Circulation rate per feed of oil\n", +"\n", +"//OUTPUT\n", +"mprintf('\nSolid recirculation per feed of oil =%ftons of solid circulated/ton feed oil',x);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 15.2: Circulation_Rate_when_Heat_Duty_Controls.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-15, Example 2, Page 370\n", +"//Title: Circulation Rate when Heat Duty Controls\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"deltaHr1=1260;//Enthalpy change during endothermic reaction in kJ/kg\n", +"deltaHr2=-33900;//Enthal[y change during exothermic reaction in kJ/kg\n", +"H1=703;//Enthalpy of feed oil in kJ/kg\n", +"T1=260;//Temperature of feed oil in degree celcius\n", +"H3=1419;//Enthalpy of cracked product in kJ/kg\n", +"T3=500;//Temperature of cracked product in degree celcius\n", +"Ta=20;//Temperature of entering air in degree celcius\n", +"Cpa=1.09;//Specific heat of entering air in kJ/kg K\n", +"Cpf=1.05;//Specific heat of flue gases in kJ/kg K\n", +"Cps=1.01;//Specific heat of solids in kJ/kg K\n", +"Cpv=3.01;//Specific heat of vaporized feed in kJ/kg K\n", +"T4=[520;540;560;580;600;620;640;660];//Temperature of flue gas in degree celcius\n", +"V=22.4;//Volume of 1 mole of Carbon dioxide gas in N-m^3\n", +"M=12;//Molecular weight of carbon in kg\n", +"rho=1.293;//Density of carbon dioxide gas in kg/N-m^3\n", +"xa=0.21;//Mass fraction of oxygen in air\n", +"betac=0.07;//Mass fraction of carbon\n", +"\n", +"//CALCULATION\n", +"n=length(T4);\n", +"i=1;\n", +"\n", +"x2min=betac*(V*rho/(M*xa));//Minimum amount of air required for complete combustion\n", +"while i<=n\n", +" x1(i)=(deltaHr1+0.93*H3-H1)/(Cps*(T4(i)-T3));//Fs/F1 by simplifying the overall energy balance\n", +" x2(i)=[(0.07*(-deltaHr2)-(deltaHr1+0.93*H3-H1))/(Cpf*(T4(i)-Ta))]-0.07;//F2/F1 by simplifying the energy balance for regenerator\n", +" if x2(i)>x2min then excess_air(i)=(x2(i)-x2min)/x2min; //Excess air used\n", +" else excess_air(i)=0;\n", +" end\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT \n", +"printf('\nT4(degree celcius)');\n", +"printf('\tFs/F1');\n", +"printf('\t\tF2/F1');\n", +"printf('\t\tExcess air(percentage)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',T4(i));\n", +" mprintf('\t\t%f',x1(i));\n", +" mprintf('\t%f',x2(i));\n", +" mprintf('\t%f',excess_air(i)*100);\n", +" i=i+1;\n", +"end\n", +"\n", +"//Disclaimer: The values of F2/F1 obtained by manual calculation has close correspondance to the ones obtained as the output, whereas it deviates largely from the values given in textbook.\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 15.3: Aeration_of_Fine_Particle_Downcomer.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-15, Example 3, Page 379\n", +"//Title: Aeration of Fine Particle Downcomer\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Fs=100;//Solid flowrate in kg/s\n", +"ephsilon1=0.55;\n", +"ephsilon2=0.5;\n", +"p1=120;//Pressure at upper level in kPa\n", +"rhos=1000;//Density of solid in kg/m^3\n", +"rhog=1;//Density of gas in kg/m^3\n", +"gc=1;//Conversion factor\n", +"g=9.81;//Acceleration due to gravity in m/s^2\n", +"di=0.34;//Diameter of downcomer in m\n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"x=(ephsilon1/ephsilon2)*((1-ephsilon2)/(1-ephsilon1));//To find pressure at lower level using Eqn.(30)\n", +"p2=x*p1;//Pressure at lower level using Eqn.(30)\n", +"deltap=p2-p1;\n", +"ephsilonbar=0.5*(ephsilon1+ephsilon2);\n", +"deltah=(deltap*10^3*gc)/(rhos*(1-ephsilonbar)*g);//Static head height from Eqn.(28)\n", +"At=0.25*pi*di^2;//Area of downcomer\n", +"Gs=Fs/At;//Flux of solids in downcomer\n", +"Gg=Gs*(ephsilon1/(1-ephsilon1))*(rhog/rhos)*(x-1);//Required gas aeration rate from Eqn.(31)\n", +"Fg=Gg*At;//Flow rate of gas required\n", +"\n", +"//OUTPUT\n", +"mprintf('\nThe required flow rate of gas required for location of %fm below downcomer is %fkg/s',deltah,Fg);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 15.4: Circulation_in_Side_by_Side_Beds.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-15, Example 4, Page 380\n", +"//Title: Circulation in Side-by-Side Beds\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Fs=600;//Solid circulation rate in kg/s\n", +"dpbar=60;//Mean size of solids in micrometer\n", +"pA=120;//Pressure in vessel A in kPa\n", +"pB=180;//Pressure in vessel B in kPa\n", +"LfA=8;//Bed height in vessel A in m\n", +"LfB=8;//Bed height in vessel B i m\n", +"//Bulk densities in kg/m^3\n", +"rho12=100;\n", +"rho34=400;\n", +"rho45=550;\n", +"rho67=200;\n", +"rho78=200;\n", +"rho910=400;\n", +"rho1011=400;\n", +"rho1112=550;\n", +"rho13=100;\n", +"deltapdA=7;//Pressure drop across the distributor in regenerator in kPa\n", +"deltapdB=8;//Pressure drop across the distributor in reactor in kPa\n", +"deltap12=(9+4);//Friction loss and pressure difference required to accelerate the solids in transfer lines in kPa\n", +"deltap78=(15+3);//Friction loss and pressure difference required to accelerate the solids in transfer lines in kPa\n", +"deltap45=20;//Friction loss across the reactor's stripper downcomer in kPa\n", +"deltap1112=4;//Friction loss across the regenerator's downcomer in kPa\n", +"deltapvA=5;//Pressure drop assigned for the control valve in regenerator in kPa\n", +"deltapvB=15;//Pressure drop assigned for the control valve in reactor in kPa\n", +"deltah12=15;//Height of the riser in m\n", +"deltah86=30;//Height of the riser in m\n", +"deltah1011=7;//Height difference h10-h11 in m\n", +"g=9.81;//Acceleration due to gravity in m/s^2\n", +"gc=1;//Conversion factor\n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"Gs=900;//From Fig.(8), to find dt\n", +"dt=sqrt((4/pi)*Fs/Gs);//Diameter of the downcomer\n", +"//Height of downcomer A from Eqn.(7)\n", +"deltahA=(1/(rho1112*g))*[(pB-pA)*gc*(10^3)+(deltap12+deltapdB+deltap1112+deltapvA)*gc*10^3-rho12*g*(-deltah12)-rho34*g*(-LfB)-rho1011*g*deltah1011];\n", +"//Height of downcomer B from Eqn.(8)\n", +"deltahB=(1/(rho45*g))*[-(pB-pA)*gc*10^3+(deltap45+deltapvB+deltap78+deltapdA)*gc*10^3+rho78*g*deltah86+rho910*g*LfA];\n", +"\n", +"//OUTPUT\n", +"printf('\nHeight of downcomer for:');\n", +"mprintf('\n\tRegenerator:%fm',deltahA);\n", +"mprintf('\n\tReactor:%fm',deltahB);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 15.5: Steam_Seal_of_a_Coarse_Particle_Downcomer.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-15, Example 5, Page 381\n", +"//Title: Steam Seal of a Coarse Particle Downcomer\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dp=10^-3;//Particle diameter in m\n", +"dt=0.8;//Diameter of reactor in m\n", +"us=0.15;//Descend velocityo of solids in m/s\n", +"L=15;//Length of downcomer\n", +"deltap1=300;//Pressure in lower vessel in kPa\n", +"deltap2=240;//Pressure in upper vessel in kPa\n", +"phis=0.8;//Sphericity of solids\n", +"ephsilonm=0.45;//Void fraction of bed\n", +"myu=4E-5;//Viscosity of gas in kg/m s\n", +"rhogl=2;//Density of gas in lower vessel in kg/m^3\n", +"rhogu=1.6;//Density of gas in upper vessel in kg/m^3\n", +"rhogbar=0.5*(rhogl+rhogu);//Average density in kg/m^3\n", +"gc=1;//Conversion factor\n", +"\n", +"//CALCULATION\n", +"//(a)Without steam seal\n", +"deltapfr=(deltap1-deltap2)*10^3;//Frictional pressure drop between two levels in Pa\n", +"deluguess=50;//Guess value of deltau\n", +"function[fn]=solver_func(delu)//Function defined for solving the system\n", +" fn=(deltapfr*gc/L)-(150*(1-ephsilonm)^2*myu*delu/(ephsilonm^2*(phis*dp)^2))-(1.75*(1-ephsilonm)*rhogbar*delu^2/(ephsilonm*phis*dp));\n", +"endfunction\n", +"[delu]=fsolve(deluguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(25) for deltau\n", +"uo=(delu-us)*ephsilonm;//Superficial gas velocity\n", +"Fg=rhogbar*uo*(pi/4)*dt^2;//Flow rate of gs up the tube\n", +"\n", +"//(c)With steam seal\n", +"//For section 1 to 3\n", +"L1=10;\n", +"deluguess1=50;//Guess value of deltau\n", +"function[fn]=solver_func1(delu1)//Function defined for solving the system\n", +" fn=(deltapfr*gc/L1)-(150*(1-ephsilonm)^2*myu*delu1/(ephsilonm^2*(phis*dp)^2))-(1.75*(1-ephsilonm)*rhogbar*delu1^2/(ephsilonm*phis*dp));\n", +"endfunction\n", +"[delu1]=fsolve(deluguess1,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(25) for deltau\n", +"uou=(delu1-us)*ephsilonm;//Upward superficial gas velocity\n", +"Fgu=rhogbar*uou*(pi/4)*dt^2;//Upward flow rate of gs up the tube\n", +"//For section 3 to 2\n", +"ugd=0.15;//Downward velocity of gas\n", +"uod=ugd*ephsilonm;//Downward superficial gas velocity\n", +"Fgd=rhogbar*uod*(pi/4)*dt^2;//Downward flow rate of gas up the tube\n", +"Fgt=Fgu+Fgd;//Total flow rate of gas\n", +"\n", +"//OUTPUT\n", +"printf('\nWithout steam seal');\n", +"printf('\n\tFlow rate of gas up the tube:%fkg/s',Fg);\n", +"printf('\nWith steam seal');\n", +"printf('\n\tTotal flow rate of gas:%fkg/s',Fgt);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/16-Design_for_Physical_Operations.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/16-Design_for_Physical_Operations.ipynb new file mode 100644 index 0000000..676b88f --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/16-Design_for_Physical_Operations.ipynb @@ -0,0 +1,413 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 16: Design for Physical Operations" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 16.1: Single_Stage_Limestone_Calciner.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-16, Example 1, Page 404\n", +"//Title: Single-Stage Limestone Calciner\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"T=1000;//Operating temperature of calciner in degree celcius\n", +"deltaHr=1795;//Heat of reaction in kJ/kg\n", +"M1=0.1;//Molecular weight of Calcium carbonate in kg/mol\n", +"M2=0.056;//Molecular weight of CaO in kg/mol\n", +"M3=0.044;//Molecular weight of Carbon dioxide in kg/mol\n", +"M4=0.029;//Molecular weight of Air in kg/mol\n", +"M5=0.029;//Molecular weight of Combustion gas in kg/mol\n", +"Cp1=1.13;//Specific heat of Calcium carbonate in kJ/kg K\n", +"Cp2=0.88;//Specific heat of CaO in kJ/kg K\n", +"Cp3=1.13;//Specific heat of Carbon dioxide in kJ/kg K\n", +"Cp4=1.00;//Specific heat of Air in kJ/kg K\n", +"Cp5=1.13;//Specific heat of Calcium carbonate in kJ/kg K\n", +"Tf=20;//Temperature of feed in degree celcius\n", +"ma=15;//Air required per kg of fuel in kg\n", +"Hc=41800;//Net combustion heat of fuel in kJ/kg\n", +"Tpi=20;//Initial temperature of solids in degree C\n", +"Tgi=1000;//Initial temperature of gas in degree C\n", +"\n", +"//CALCULATION\n", +"mc=1;//Based on 1 kg of Calcium carbonate\n", +"B=(1/(Hc-(ma+mc)*Cp5*(T-Tpi)))*[M3*Cp3*(T-Tf)+M2*Cp2*(T-Tf)+deltaHr]//Fuel consumption(kg fuel/kg calcium carbonate)\n", +"B1=B*M3/M2;//Fuel consumption(kg fuel/kg Cao)\n", +"H=Hc*B1;//Heat required for calcination\n", +"eta=deltaHr/(B*Hc);//Thermal efficiency\n", +"\n", +"//OUTPUT\n", +"mprintf('\nFuel consumption:%f kg fuel/kg Cao',B1);\n", +"mprintf('\nHeat requirement for calcination:%f kJ/kg Cao',H);\n", +"mprintf('\nThermal efficiency:%f percentage',eta*100);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 16.2: Multistage_Limestone_Calciner.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-16, Example 2, Page 405\n", +"//Title: Multistage Limestone Calciner\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"F=400;//Feed rate of Calcium carbonate in tons/day\n", +"T=1000;//Operating temperature of calciner in degree celcius\n", +"deltaHr=1795;//Heat of reaction in kJ/kg\n", +"M1=0.1;//Molecular weight of Calcium carbonate in kg/mol\n", +"M2=0.056;//Molecular weight of CaO in kg/mol\n", +"M3=0.044;//Molecular weight of Carbon dioxide in kg/mol\n", +"M4=0.029;//Molecular weight of Air in kg/mol\n", +"M5=0.029;//Molecular weight of Combustion gas in kg/mol\n", +"Cp1=1.13;//Specific heat of Calcium carbonate in kJ/kg K\n", +"Cp2=0.88;//Specific heat of CaO in kJ/kg K\n", +"Cp3=1.13;//Specific heat of Carbon dioxide in kJ/kg K\n", +"Cp4=1.00;//Specific heat of Air in kJ/kg K\n", +"Cp5=1.17;//Specific heat of Combustion gas in kJ/kg K\n", +"Tf=20;//Temperature of feed in degree celcius\n", +"ma=15;//Air required per kg of fuel in kg\n", +"uo=0.8;//Superficial gas velocity in m/s\n", +"Hc=41800;//Net combustion heat of fuel in kJ/kg\n", +"Tpi=20;//Initial temperature of solids in degree C\n", +"Tgi=1000;//Initial temperature of gas in degree C\n", +"rhoa=1.293;//Density of air in kg/m^3\n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"mc=1;//Based on 1 kg of Calcium carbonate\n", +"Bguess=2;//Guess value of B\n", +"function[fn]=solver_func(B)//Function defined for solving the system\n", +" phi=((ma+mc)*Cp5*B+(M3*Cp3))/Cp1;\n", +" T3=(Tpi+(phi+phi^2+phi^3)*Tgi)/(1+phi+phi^2+phi^3);\n", +" phiplus=30.6*B\n", +" Tr=(T+Tpi*phiplus)/(1+phiplus);\n", +" fn=Hc*B+Cp3*(T3-Tpi)+ma*B*Cp4*(Tr-20)-(ma+mc)*Cp5*(T-Tpi)-M3*Cp3*(T-Tpi)-M2*Cp2*(T-Tpi)-deltaHr;\n", +" //fn=(1/20800)*(2470-T3-13.34*(Tr-20));\n", +"endfunction\n", +"[B]=fsolve(Bguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou\n", +"phi=((ma+mc)*Cp5*B+(M3*Cp3))/Cp1;\n", +"//Temperature of various stages\n", +"T1=(Tpi+(phi)*Tgi)/(1+phi);\n", +"T2=(Tpi+(phi+phi^2)*Tgi)/(1+phi+phi^2);\n", +"T3=(Tpi+(phi+phi^2+phi^3)*Tgi)/(1+phi+phi^2+phi^3);\n", +"phiplus=30.6*B\n", +"Tr=(T+Tpi*phiplus)/(1+phiplus);\n", +"eta=deltaHr/(B*Hc);//Thermal efficiency\n", +"H=B*Hc/M2;//Heat requirement\n", +"//For lower heat recovery section\n", +"Ql=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(Tr+273)));//Volumetric flow rate of gas in the lower heat recovery section\n", +"dtl=sqrt(4/pi*Ql/uo);//Diameter of lower bed\n", +"//For calcination section\n", +"Qc=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T+273)));//Volumetric flow rate of gas in the calcination section\n", +"dtc=sqrt(4/pi*Qc/uo);//Diameter of calcination section\n", +"//For I stage\n", +"Q1=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T1+273)));//Volumetric flow rate of gas in the I stage\n", +"dt1=sqrt(4/pi*Q1/uo);//Diameter of I stage\n", +"//For II stage\n", +"Q2=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T2+273)));//Volumetric flow rate of gas in the II stage\n", +"dt2=sqrt(4/pi*Q2/uo);//Diameter of II stage\n", +"//For III stage\n", +"Q3=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T3+273)));//Volumetric flow rate of gas in the III stage\n", +"dt3=sqrt(4/pi*Q3/uo);//Diameter of III stage\n", +"\n", +"//OUTPUT\n", +"printf('\nDiameter of lower bed:%fm',dtl);\n", +"printf('\nDiameter of calcination section:%fm',dtc);\n", +"printf('\nBed no.\t\t1\t2\t\t3');\n", +"printf('\nDiameter(m)%f\t%f\t%f',dt1,dt2,dt3);\n", +"\n", +"//The value of diameter of each section is largely deviating from the values in the textbook. This is because the fuel consumption B have not been included in the energy balance equation. And the value of molecular weight is wrong by one decimal point.\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 16.3: Multistage_Adsorber.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-16, Example 3, Page 413\n", +"//Title: Multistage Adsorber\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"T=20;//Temeprature in degree C\n", +"M=0.018;//Molecular weight of water in kg/mol\n", +"Q=10;//Flow rate of dry air in m^3/s\n", +"R=82.06E-6;//Universal gas constant\n", +"pi=0.0001;//Initial moisture content in atm\n", +"pj=0.01;//Final moisture content in atm\n", +"\n", +"//CALCULATION\n", +"a=Q*(273+T)/273;//Term At*uo\n", +"b=a*M/(R*(T+273));//Term C*At*uo\n", +"//The value of slope can be found only by graphical mehtod. Hence it has been taken directly from the book(Page no.414,Fig.E3)\n", +"m=10.2;\n", +"Fo=b/m;//Flow rate of solids\n", +"Q3=(b/Fo)*(pj-pi);//Moisture content of leaving solids\n", +"\n", +"//OUTPUT\n", +"printf('\nMoisture content of leaving solids:%f kg H2O/kg dry solids',Q3);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 16.4: Dryer_Kinetics_and_Scale_up.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-16, Example 4, Page 422\n", +"//Title: Dryer Kinetics and Scale-up\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Qfi=0.20;//Initial moisture fraction\n", +"Qfbar=0.04;//Average final moisture fraction\n", +"rhos=2000;//Density of solid in kg/m^3\n", +"Cps=0.84;//Specific heat of solids in kJ/kg K\n", +"Fo=7.6E-4;//Flow rate of solids in kg/m^3\n", +"Tsi=20;//Inital temperature of solids in degree C\n", +"rhog=1;//Density of gas in kg/m^3\n", +"Cpg=1;//Specific heat of gas in kJ/kg K\n", +"uo=0.3;//Superficial gas velocity in m/s\n", +"Tgi=200;//Initial temperature of gas in degee C\n", +"L=2370;//Enthalpy of liquid in kJ/kg\n", +"Cpl=4.2;//Specific heat of liquid in kJ/kg K\n", +"dt=0.1;//Diameter of reactor in m\n", +"Lm=0.1;//Length of fixed bed in m\n", +"ephsilonm=0.45;//Void fraction of fixed bed\n", +"pi=3.14;\n", +"Fo1=1;//Feed rate for commercial-scale reactor in kg/s\n", +"\n", +"//CALCULATION\n", +"//(a)Bed temperature\n", +"Teguess=50;//Guess value of Te\n", +"function[fn]=solver_func(Te)//Function defined for solving the system\n", +" fn=(pi/4)*dt^2*uo*rhog*Cpg*(Tgi-Te)-Fo*(Qfi-Qfbar)*[L+Cpl*(Te-Tsi)]-Fo*Cps*(Te-Tsi);\n", +"endfunction\n", +"[Te]=fsolve(Teguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(53) for Te\n", +"\n", +"//(b)Drying time for a particle\n", +"xguess=2;//Guess value of x, ie term tou/tbar\n", +"function[fn]=solver_func1(x)//Function defined for solving the system\n", +" fn=1-(Qfbar/Qfi)-(1-exp(-x))/x;\n", +"endfunction\n", +"[x]=fsolve(xguess,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(61) for x\n", +"W=(pi/4)*dt^2*Lm*(1-ephsilonm)*rhos;//Weight of soilds in bed\n", +"tbar=W/Fo;//Mean residence time of solids from Eqn.(59)\n", +"tou=tbar*x;//Time for complete drying of a particle\n", +"\n", +"//(c)Commercial-scale dryer\n", +"W1=Fo1*tbar;\n", +"Atguess=5;//Guess value of area\n", +"function[fn]=solver_func3(At)//Function defined for solving the system\n", +" fn=At*uo*rhog*Cpg*(Tgi-Te)-Fo1*(Qfi-Qfbar)*[L+Cpl*(Te-Tsi)]-Fo1*Cps*(Te-Tsi);\n", +"endfunction\n", +"[At]=fsolve(Atguess,solver_func3,1E-6);//Using inbuilt function fsolve for solving Eqn.(53) for At\n", +"dt1=sqrt(4/pi*At);//Diameter of commercial-scale dryer\n", +"Q1=At*uo*rhog;//Flow rate necessary for the operation\n", +"\n", +"//OUTPUT\n", +"printf('\nBed temperature:%f degree C',Te);\n", +"printf('\nTime for complete drying of particle:%fs',tou);\n", +"printf('\nFlow rate of gas necessary for Commercial-scale dryer:%fkg/s',Q1);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 16.5: Solvent_Recovery_from_Polymer_Particles.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-16, Example 5, Page 425\n", +"//Title: Solvent Recovery from Polymer Particles\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhos=1600;//Density of solid in kg/m^3\n", +"Cps=1.25;//Specific heat of solids in kJ/kg K\n", +"Fo=0.5;//Flow rate of solids in kg/s\n", +"Tsi=20;//Inital temperature of solids in degree C\n", +"Qwi=1;//Initial moisture fraction in water\n", +"Qwf=0.2;//Final moisture fraction in water\n", +"Qhi=1.1;//Initial moisture fraction in heptane\n", +"Qhf=0.1;//Final moisture fraction in heptane\n", +"Tgi=240;//Initial temperature of gas in degee C\n", +"Te=110;//Bed temperature in degree C\n", +"ephsilonm=0.45;//Void fraction of fixed bed\n", +"ephsilonf=0.75;//Void fraction of fluidized bed\n", +"uo=0.6;//Superficial gas velocity in m/s\n", +"di=0.08;//Diameter of tubes in m\n", +"li=0.2;//Pitch for square arrangement\n", +"hw=400;//Heat transfer coefficient in W/m^2 K\n", +"Tc=238;//Temperature at which steam condenses in degree C\n", +"//Specific heats in kJ/kg K\n", +"Cwl=4.18;//Water liquid\n", +"Cwv=1.92;//Water vapor\n", +"Chl=2.05;//Heptane liquid\n", +"Chv=1.67;//Heptane vapor\n", +"//Latent heat of vaporization in kJ/kg\n", +"Lw=2260;//Water\n", +"Lh=326;//Heptane\n", +"//Density of vapor in kg/m^3 at operating conditions\n", +"rhow=0.56;//Water\n", +"rhoh=3.1;//Heptane\n", +"Lf=1.5;//Length of fixed bed in m\n", +"t=140;//Half-life of heptane in s\n", +"L=1.5;//Length of tubes in heat exchanger\n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"//(a) Dryer without Internals\n", +"xw=(Qwi-Qwf)/(Qhi-Qhf);//Water-heptane weight ratio\n", +"xv=((Qwi-Qwf)/18)/((Qhi-Qhf)/100);//Water-heptane volume ratio\n", +"T=(Qwi-Qwf)/18+(Qhi-Qhf)/100;//Total volume\n", +"rhogbar=((Qwi-Qwf)/18)/T*rhow+((Qhi-Qhf)/100)/T*rhoh;//Mean density of the vapor mixture\n", +"Cpgbar=(((Qwi-Qwf)/18)/T)*rhow*Cwv+(((Qhi-Qhf)/100)/T)*rhoh*Cwv;//Mean specific heat of vapor mixture\n", +"//Volumetric flow of recycle gas to the dryer in m^3/s from Eqn.(53)\n", +"x=(Cpgbar*(Tgi-Te))^-1*[Fo*(Qwi-Qwf)*[Lw+Cwl*(Te-Tsi)]+Fo*(Qhi-Qhf)*[Lh+Chl*(Te-Tsi)]+Fo*(Cps*(Te-Tsi))];\n", +"r=Fo*[(Qwi-Qwf)/rhow+(Qhi-Qhf)/rhoh};//Rate of formation of vapor in bed\n", +"uo1=uo*(x/(x+r));//Superficial velocity just above the distributor\n", +"At=x/uo1;//Cross-sectional area of bed\n", +"dt=sqrt(4/pi*At);//Diameter of bed\n", +"B=-log(Qwf/Qwi)/t;//Bed height from Eqn.(63)\n", +"tbar=((Qhi/Qhf)-1)/B;//Mean residence time of solids\n", +"W=Fo*tbar;//Weight of bed\n", +"Lm=W/(At*(1-ephsilonm)*rhos);//Static bed height\n", +"Lf=(Lm*(1-ephsilonm))/(1-ephsilonf);//Height of fluidized bed\n", +"\n", +"//(b) Dryer with internal heaters\n", +"f=1/8;//Flow rate is 1/8th the flow rate of recirculation gas as in part (a)\n", +"x1=f*x;//Volumetric flow of recycle gas to the dryer in m^3/s from Eqn.(53)\n", +"uo2=uo*(x1/(x1+r));//Superficial velocity just above the distributor\n", +"Abed=x1/uo2;//Cross-sectional area of bed\n", +"q=[Fo*(Qwi-Qwf)*[Lw+Cwl*(Te-Tsi)]+Fo*(Qhi-Qhf)*[Lh+Chl*(Te-Tsi)]+Fo*(Cps*(Te-Tsi))]-Abed*uo2*Cpgbar*(Tgi-Te);//Heat to be added from energy balance of Eqn.(53)\n", +"Aw=q*10^3/(hw*(Tc-Te));//Total surface area of heat exchanger tubes\n", +"Lt=Aw/(pi*di);//Total length of tubes\n", +"Nt=Lt/L;//Total number of tubes\n", +"Atubes=Nt*(pi/4*di^2);//Total cross-sectional area of tubes\n", +"Atotal=Abed+Atubes;//Total cross-sectional area of tube filled dryer\n", +"d=sqrt(Atotal*pi/4);//Diameter of vessel\n", +"li=sqrt(Atotal/Nt);//Pitch for square array of tubes\n", +"\n", +"//OUTPUT\n", +"printf('\n\t\t\tBed diameter(m)\tRecycle vapor flow(m^3/s)');\n", +"printf('\nWithout internal heater\t%f\t%f',dt,x);\n", +"printf('\nWith heating tubes\t%f\t%f',d,x1);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/17-Design_of_Catalytic_Reactors.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/17-Design_of_Catalytic_Reactors.ipynb new file mode 100644 index 0000000..07db9ca --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/17-Design_of_Catalytic_Reactors.ipynb @@ -0,0 +1,371 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 17: Design of Catalytic Reactors" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 17.1: Reactor_Development_Program.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-17, Example 1, Page 434\n", +"//Title: Reactor Development Program\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\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;//Kinetic 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=length(dt);\n", +"i=1;\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)/gammae(i))*(Kr3+Kce(i)/gammac(i)+Kce(i)/gammae(i))]*delta(i)*Kbc(i)*Kr12*Kr3/(1-ephsilonf(i))] /[[(Kr12+Kbc(i)/gammac(i))*(Kr12+Kce(i)/gammae(i))+Kr12*Kce(i)/gammac(i)]*[(Kr3+Kbc(i)/gammac(i))*(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", +" \n", +" //(b)Relate Selectivity with conversion in three reactors\n", +" x=-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)))*(exp(-x)-exp(-tou(i)*Kf3(i)));//CR/CAi from Eqn.(12.27)\n", +" SR(i)=y(i)/XA;//Selectivity of R\n", +" \n", +" //(c)Relate exit composition to space time\n", +" tou1=5;//Space time in s\n", +" XA1(i)=1-exp(-Kf12(i)*tou1);//Conversion from Eqn.(12.26)\n", +" y1(i)=((KfAR1(i)/(Kf12(i)-Kf3(i)))*[exp(-Kf3(i)*tou1)-exp(-Kf12(i)*tou1)]);//CR/CAi R from Eqn.(12.27)\n", +" \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)=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-exp(-Kf12(i)*tou2(i));//Conversion from Eqn.(12.26)\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nLet Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively'); \n", +"printf('\n(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo)');\n", +"printf('\n\tReactor No.\tKf12(s^-1)\tuo(m/s)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%1.0f',i);\n", +" mprintf('\t\t%f',Kf12(i));\n", +" mprintf('\t%f',uo);\n", +" i=i+1;\n", +"end\n", +"printf('\n(b)Relation between selectivity with conversion');\n", +"printf('\n\tReactor No.\tKf12(s^-1)\tSR(mol R formed/mol A reacted)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%1.0f',i);\n", +" mprintf('\t\t%f',Kf12(i));\n", +" mprintf('\t%f',SR(i));\n", +" i=i+1;\n", +"end\n", +"printf('\n(c)Relation between exit compostion and space time');\n", +"printf('\n\tReactor No.\tXA\t\tCR/CAi');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%1.0f',i);\n", +" mprintf('\t\t%f',XA1(i));\n", +" mprintf('\t%f',y1(i));\n", +" i=i+1;\n", +"end\n", +"printf('\n(d)Height of bed needed to maximize the production of acrylonitrile');\n", +"printf('\n\tReactor No.\tLm(m)\t\tXA');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%1.0f',i);\n", +" mprintf('\t\t%f',Lm(i));\n", +" mprintf('\t%f',XA2(i));\n", +" i=i+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 17.2: Design_of_a_Commercial_Acrylonitrile_Reactor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-17, Example 2, Page 438\n", +"//Title: Design of a Commercial Acrylonitrile Reactor\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\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 then li=(pi/4*dte*do1+pi/4*do1^2)^0.5;//Pitch if we add dummy tubes\n", +"end\n", +"f=li^2-pi/4*do1^2;//Fraction of bed cross section taken up by tubes\n", +"dt1=sqrt(4/pi*At/(1-f));//Reactor diameter including all its tubes\n", +"\n", +"//OUTPUT\n", +"printf('\nSuperficial gas velocity=%fm/s',uo);\n", +"printf('\nNo. of %1.0fm tubes required=%1.0f',L,Nt);\n", +"printf('\nReactor diameter=%fm',dt1);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 17.3: Reactor_Regenerator_with_Circulating_Catalyst_Catalytic_Cracking.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-17, Example 3, Page 444\n", +"//Title: Reactor-Regenerator with Circulating Catalyst: Catalytic Cracking\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\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;//Temperature of reactor in degree C\n", +"T2=580;//Temperature of regenerator in degree C\n", +"Fs=F1*23.3;//Solid circulation rate from Ex.(15.2)\n", +"rhos=1200;//Density of catalyst in kg/m^3\n", +"dpbar=60;//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;//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^(5/4));//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", +"\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=-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", +"n=length(a1bar1);\n", +"i=1;\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)+(1/(gammae*x1(i))))))))*(delta/(1-ephsilonf));//Effective rate constant from Eqn.(12.14)\n", +" tou1(i)=-log(1-XA)/Kf1(i);//Space time from Eqn.(12.16)\n", +" Lm1(i)=tou1(i)*uo/(1-ephsilonm);//Length of fixed bed for guess value of a1bar...Condition (i)\n", +" i=i+1;\n", +"end\n", +"\n", +"//Find the optimum size ratio for various a1bar\n", +"Lm=[5;6;7;8;10;12];\n", +"m=length(Lm);\n", +"i=1;\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", +"end\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", +"printf('\nBed height versus catalyst activity in reactor');\n", +"printf('\n\tAverage activity');\n", +"printf('\tLength of fixed bed(m)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%f',a1bar1(i));\n", +" mprintf('\t\t%f',Lm1(i));\n", +" i=i+1;\n", +"end\n", +"printf('\nOptimum size ratio for various activity in reactor');\n", +"printf('\n\tLength of fixed bed(m)');\n", +"printf('\tAverage activity');\n", +"i=1;\n", +"while i<=m\n", +" mprintf('\n\t%f',Lm(i));\n", +" mprintf('\t\t%f',a1bar2(i));\n", +" i=i+1;\n", +"end\n", +"printf('\nFinal design values');\n", +"printf('\n\tDiameter of reactor(m):%f',dt);\n", +"printf('\n\tBed weight for reactor(tons):%f',W11/10^3);\n", +"printf('\n\tBed weight for regenerator(tons):%f',W2/10^3);\n", +"printf('\n\tDiameter of regenerator(m):%f',dt2);\n", +"printf('\n\tSolid circulation rate(tons/hr):%f',Fs*3.6);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/18-The_Design_of_Noncatalytic_Gas_Solid_Reactors.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/18-The_Design_of_Noncatalytic_Gas_Solid_Reactors.ipynb new file mode 100644 index 0000000..99bb9ed --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/18-The_Design_of_Noncatalytic_Gas_Solid_Reactors.ipynb @@ -0,0 +1,537 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 18: The Design of Noncatalytic Gas Solid Reactors" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 18.1: Kinetics_of_Zinc_Blende_Roasting.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-18, Example 1, Page 456\n", +"//Title: Kinetics of Zinc Blende Roasting\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"xA=0.08;//Fraction of oxygen in stream\n", +"dp=[2;0.1];//Particle diameter in mm\n", +"rhos=4130;//Density of catalyst in kg/m^3\n", +"Ds=8E-6;//Diffusion coefficient of solid in m^2/s\n", +"kc=0.02;//Reaction rate constant in m/s\n", +"P=10^5;//Pressure in bar\\n", +"R=8.314;//Universal gas constant\n", +"T=900;//Temperature in degree C\n", +"mB=0.09745;//Molecular weight of ZnS in kg/mol\n", +"\n", +"//CALCULATION\n", +"b=2/3;//Stoichiometric coefficient of ZnS in the reaction equation\n", +"CA=xA*P/(R*(T+273));//Concentration of Oxygen\n", +"rhob=rhos/mB;//Molar density of pure solid\n", +"n=length(dp);\n", +"i=1;\n", +"while i<=n\n", +" kbar(i)=(kc^-1+(dp(i)*10^-3/(12*Ds)))^-1;//Average reaction rate constant from Eqn.(11)\n", +" tou(i)=rhob*dp(i)*10^-3/(2*b*kbar(i)*CA);//Time for complete reaction in seconds from Eqn.(9)\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nParticle Size(mm)\tAverage rate constant(m/s)\tTime for complete reaction(min)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f\t\t%f\t\t\t%f',dp(i),kbar(i),tou(i)/60);\n", +" i=i+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 18.2: Kinetics_of_Carbon_Burning.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-18, Example 2, Page 457\n", +"//Title: Kinetics of Carbon Burning\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"xA=0.08;//Fraction of oxygen in stream\n", +"dp=1;//Particle diameter in mm\n", +"rhos=2200;//Density of catalyst in kg/m^3\n", +"kc=0.2;//Reaction rate constant in m/s\n", +"mC=0.012;//Molecular weight of carbon in kg/mol\n", +"P=10^5;//Pressure in bar\\n", +"R=8.314;//Universal gas constant\n", +"T=900;//Temperature in degree C\n", +"\n", +"//CALCULATION\n", +"b=1;//Stoichiometric coefficient of C in the reaction equation\n", +"CA=xA*P/(R*(T+273));//Concentration of Oxygen\n", +"rhob=rhos/mC;//Molar density of pure solid reactant\n", +"tou=rhob*10^-3/(2*b*kc*CA);//Time required for complete reaction in seconds\n", +"\n", +"//OUTPUT\n", +"mprintf('\nThe time required for complete combustion:%fmins',tou/60);\n", +"\n", +"//====================================END OF PROGRAM ======================================================\n", +"\n", +"\n", +"\n", +"\n", +"\n", +"\n", +"\n", +"\n", +"\n", +"" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 18.3: Roasting_Kinetics_from_Flowing_Solids_Data.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-18, Example 3, Page 462\n", +"//Title: Roasting Kinetics from Flowing Solids Data\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dp=110;//Particle size in micrometer\n", +"T=900;//Temperature of roaster in degree C\n", +"tbar1=[3;10;30;50];//Reported average time in min\n", +"XBbarr=[0.840;0.940;0.985;0.990];//Reported value of average conversion\n", +"tbar=3;\n", +"XBbar=0.840;//Average conversion for tbar = 3 mins\n", +"\n", +"//CALCULATION\n", +"//Uniform-Reaction Model\n", +"x=(1/tbar)*(1/(1-XBbar)-1);//Term KrCA of Eqn.(20)\n", +"n=length(tbar1);\n", +"i=1;\n", +"while i<=n\n", +" XBbar1(i)=1-1/(1+x*tbar1(i));//Average conversion using calculated value of KrCA from Eqn.(20)\n", +" i=i+1;\n", +"end\n", +"\n", +"//Shrinking-Core, Rection Control\n", +"touguess=2;//Guess value of tou\n", +"function[fn]=solver_func(tou)//Function defined for solving the system\n", +" fn=(1-XBbar)-(0.25*tou/tbar)+(0.05*(tou/tbar)^2)-((1/120)*(tou/tbar)^3);\n", +"endfunction\n", +"[tou]=fsolve(touguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou\n", +"i=1;\n", +"while i<=n\n", +" XBbar2(i)=1-(0.25*tou/tbar1(i))+(0.05*(tou/tbar1(i))^2)-((1/120)*(tou/tbar1(i))^3);//Average conversion using calculated value of tou from Eqn.(23)\n", +" i=i+1;\n", +"end\n", +"\n", +"//Shrinking-Core, Diffusion Control\n", +"touguess1=2;//Guess value of tou\n", +"function[fn]=solver_func1(tou)//Function defined for solving the system\n", +" fn=(1-XBbar)-(1/5*tou/tbar)+(19/420*(tou/tbar)^2)-(41/4620*(tou/tbar)^3)+(0.00149*(tou/tbar)^4);\n", +"endfunction\n", +"[tou1]=fsolve(touguess1,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou\n", +"i=1;\n", +"while i<=n\n", +" //Average conversion using calculated value of tou from Eqn.(23)\n", +" XBbar3(i)=1-(1/5*tou1/tbar1(i))+(19/420*(tou1/tbar1(i))^2)-(41/4620*(tou1/tbar1(i))^3)+(0.00149*(tou1/tbar)^4);\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\n\t\t\t\tXBbar calculated for Models');\n", +"printf('\nReported Data');\n", +"printf('\ntbar(min)\tXBbar,obs\tUniform Reaction\tShrinking-Core, Rection Control\t\tShrinking-Core, Diffusion Control');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f\t%f\t%f\t\t%f\t\t\t\t%f',tbar1(i),XBbarr(i),XBbar1(i),XBbar2(i),XBbar3(i));\n", +" i=i+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 18.4: Scale_up_of_a_Reactor_with_Flowing_Solids.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-18, Example 4, Page 462\n", +"//Title: Scale-up of a Reactor with Flowing Solids\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"W=1;//Bed weight in kg\n", +"F1=0.01;//Solid feed rate in kg/min\n", +"dp=[200;600];//Particle size in micrometer\n", +"XBbar=[0.85;0.64];//Average conversion for corresponding particle sizes\n", +"rhos=2500;//Density of solid in kg/m^3\n", +"ephsilonm=0.4;//Void fracton of fixed bed\n", +"F11=4;//Feed rate of solids in tons/hr\n", +"XBbar1=0.98;\n", +"dp1=600;\n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"//Shrinking-Core, Rection Control\n", +"n=length(dp);\n", +"i=1;\n", +"touguess=2;//Guess value of tou\n", +"while i<=n\n", +" function[fn]=solver_func2(tou)//Function defined for solving the system\n", +" fn=(1-XBbar(i))-(0.25*tou/107)+(0.05*(tou/107)^2)-((1/120)*(tou/107)^3);\n", +" endfunction\n", +" [tou(i)]=fsolve(touguess,solver_func2,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou\n", +" i=i+1;\n", +"end\n", +"tou1=tou(2);\n", +"\n", +"//For a single stage fluidized roaster\n", +"tbar1=0.25*(tou1/(1-XBbar1))/60;//Mean residence time of solids in reactor in hr from Eqn.(24)\n", +"W1=F11*tbar1;\n", +"dtguess=2;//Guess value of tou\n", +"function[fn]=solver_func3(dt)//Function defined for solving the system\n", +" fn=W1*10^3-(pi/4)*dt^2*0.5*dt*rhos*(1-ephsilonm);//Since Lm=0.5dt\n", +"endfunction\n", +"[dt]=fsolve(dtguess,solver_func3,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou\n", +"Lm=dt/2;//Length of bed required\n", +"\n", +"//For a two-stage fluidized roaster\n", +"tbar2=tou1*sqrt(1/(20*(1-XBbar1)))/60;//Mean residence time of solids in reactor in hr from Eqn.(30)\n", +"W2=F11*tbar2;\n", +"dtguess1=2;//Guess value of tou\n", +"function[fn]=solver_func4(dt)//Function defined for solving the system\n", +" fn=W2*10^3-(pi/4)*dt^2*0.5*dt*rhos*(1-ephsilonm);//Since Lm=0.5dt\n", +"endfunction\n", +"[dt1]=fsolve(dtguess,solver_func4,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou\n", +"Lm1=dt1/2;//Length of bed required\n", +"\n", +"//OUTPUT\n", +"printf('\nSingle stage fluidized roaster');\n", +"printf('\n\tWeight of bed needed:%ftons',W1);\n", +"printf('\n\tDiameter of reactor:%fm',dt);\n", +"printf('\n\tLength of bed:%fm',Lm);\n", +"printf('\nTwo-stage fluidized roaster');\n", +"printf('\n\tWeight of bed needed:%ftons',W2);\n", +"printf('\n\tDiameter of reactor:%fm',dt1);\n", +"printf('\n\tLength of bed:%fm',Lm1);\n", +"printf('\nThese results show that this operation can be accomplished in a single bed of %ftons or in two beds of %f tons each.',W1,W2);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 18.5: Design_of_a_Roaster_for_Finely_Ground_Ore.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-18, Example 5, Page 468\n", +"//Title: Design of a Roaster for Finely Ground Ore\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"T=900;//Temperature in roaster in degree C\n", +"P=101325;//Pressure in Pa\n", +"R=8.314;//Universal gas constant\n", +"dpbar=150;//Average particle size in micrometer\n", +"rhosbar=4130;//Average particle density in kg/m^3\n", +"kc=0.015//Rate constant in m/s for reaction which follows shrinking core model\n", +"Ds=8E-6;//Diffusion coefficient of solid in m^2/s\n", +"uo=0.6;//Superficial gas velocity in m/s\n", +"D=2.3E-4;//Diffusion coefficient of gas in m^2/s\n", +"Lm=1;//Length of fixed bed in m\n", +"dte=0.4;//Equivalent diameter of bed\n", +"umf=0.025;//Velocity at minimum fluidization condition in m/s\n", +"ephsilonm=0.45;//Void fraction of fixed bed\n", +"ephsilonmf=0.50;//Void fraction at minimum fluidized condition\n", +"db=0.2;//Estimated bubble size in m\n", +"gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase\n", +"Fo=2;//Feed rate of solids in kg/s\n", +"XA=0.6677;//Conversion of Oxygen\n", +"xA=0.21;//Mole fraction of oxygen in feed\n", +"mB=0.09744;//Molecular weight of ZnS\n", +"F=0.85;//Fraction of open area\n", +"g=9.81;//Acceleration due to gravity in square m/s^2\n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"//(a)Extreme Calculation\n", +"a=3/2;//Stoichiometric coefficient of Oxygen in the reaction equation\n", +"At=(Fo/mB)*(a)/(uo*(273/(T+273))*(XA*xA)/0.0224);\n", +"dt=sqrt(At/F*4/pi);\n", +"\n", +"//(b)The Three-Step Procedure\n", +"//Step 1. Conversion of gas\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"ub=1.6*{(uo-umf)+1.13*db^0.5}*dte^1.35+ubr;//Bubble rise velocity for Geldart B particle\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=0.15;//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^(5/4));//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", +"x=delta*Lm*(1-ephsilonm)/((1-ephsilonf)*uo);//Term Lf/ub of Eqn.(12.16) from Eqn.(6.19)\n", +"CAi=xA*P/(R*(T+273));//Initial concentration of oxygen\n", +"\n", +"//Step 2.Conversion of solids\n", +"rhob=rhosbar/mB;//Density of ZnS\n", +"kbar=(kc^-1+(dpbar*10^-6/(12*Ds))^-1)^-1;//Modified rate constant from Eqn.(11)\n", +"tbar=At*Lm*(1-ephsilonm)*rhosbar/Fo;//Mean residence time of solids\n", +"Krguess=2;//Guess value of Kr\n", +"function[fn]=solver_func(Kr)//Function defined for solving the system\n", +" Kf=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Reaction rate for fluidized bed from Eqn.(14)\n", +" XA=1-exp(-x*Kf);//Conversion of oxygen from Eqn.(42)\n", +" CAbar=(CAi*XA*uo)/(Kr*Lm*(1-ephsilonm));//Average concentration of oxygen from Eqn.(43)\n", +" tou=rhob*dpbar*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)\n", +" y=tbar/tou;//Term tbar/tou\n", +" XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)\n", +" //Step 3. Material balance of both streams\n", +" fn=(Fo/mB)*XBbar-(At*uo*CAi*XA/a);//From Eqn.(44b)\n", +"endfunction\n", +"[Kr]=fsolve(Krguess,solver_func,1E-6);//Using inbuilt function fsolve for solving for Kr\n", +"Kf=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Reaction rate for fluidized bed from Eqn.(14)\n", +"XA=1-exp(-x*Kf);//Conversion of oxygen from Eqn.(42)\n", +"CAbar=(CAi*XA*uo)/(Kr*Lm*(1-ephsilonmf));//Average concentration of oxygen from Eqn.(43)\n", +"tou=rhob*dpbar*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)\n", +"y=tbar/tou;//Term tbar/tou\n", +"XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)\n", +"\n", +"\n", +"//(c) For other feed rates of solids\n", +"F1=[2;2.5;3;3.5];//Various feed rates of solids in kg/s\n", +"n=length(F1)\n", +"i=1;\n", +"Krguess1=2;//Guess value of Kr\n", +"while i<=n\n", +" tbar1(i)=At*Lm*(1-ephsilonm)*rhosbar/F1(i);//Mean residence time of solids\n", +" function[fn]=solver_func1(Kr)//Function defined for solving the system\n", +" Kf1=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Reaction rate for fluidized bed from Eqn.(14)\n", +" XA1=1-exp(-x*Kf1);//Conversion of oxygen from Eqn.(42)\n", +" CAbar1=(CAi*XA1*uo)/(Kr*Lm*(1-ephsilonm));//Average concentration of oxygen from Eqn.(43)\n", +" tou1=rhob*dpbar*10^-6*a/(2*kbar*CAbar1);//Time for complete reaction from Eqn.(9)\n", +" y1(i)=tbar1(i)/tou1;//Term tbar/tou\n", +" XBbar1(i)=3*y1(i)-6*y1(i)^2+6*y1(i)^3*(1-exp(-1/y1(i)));//Average conversion of ZnS from Eqn.(22)\n", +" //Step 3. Material balance of both streams\n", +" fn=(F1(i)/mB)*XBbar1(i)-(At*uo*CAi*XA1/a);//From Eqn.(44b)\n", +" endfunction\n", +" [Kr1(i)]=fsolve(Krguess1,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou\n", +" Kf1(i)=gammab*Kr1(i)+1/((1/Kbc)+(1/(gammac*Kr1(i)+1/((1/Kce)+(1/(gammae*Kr1(i)))))));//Reaction rate for fluidized bed from Eqn.(14)\n", +" XA1(i)=1-exp(-x*Kf1(i));//Conversion of oxygen from Eqn.(42)\n", +" CAbar1(i)=(CAi*XA1(i)*uo)/(Kr1(i)*Lm*(1-ephsilonmf));//Average concentration of oxygen from Eqn.(43)\n", +" tou1(i)=rhob*dpbar*10^-6*a/(2*kbar*CAbar1(i));//Time for complete reaction from Eqn.(9)\n", +" y1(i)=tbar1(i)/tou1(i);//Term tbar/tou\n", +" XBbar1(i)=3*y1(i)-6*y1(i)^2+6*y1(i)^3*(1-exp(-1/y1(i)));//Average conversion of ZnS from Eqn.(22)\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\nExtreme Calculation');\n", +"printf('\n\tDiameter of tube with all its internals:%fm',dt);\n", +"printf('\nThree step procedure');\n", +"printf('\n\tConversion of ZnS:%f',XBbar);\n", +"printf('\nFor other feed rates of solids');\n", +"printf('\n\tFeed(kg/s)\ttbar(s)\t\tXBbar/XA\tKrbar(s^-1)\tCAbar/CAi\ttou(s)\t\tXA\t\tXB');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%f\t%f\t%f\t%f\t%f\t%f\t%f\t%f',F1(i),tbar1(i),XBbar1(i)/XA1(i),Kr1(i),CAbar1(i)/CAi,tou1(i),XA1(i),XBbar1(i));\n", +" i=i+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 18.6: Design_of_a_Roaster_for_Coarse_Ore.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-18, Example 5, Page 471\n", +"//Title: Design of a Roaster for Coarse Ore\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"T=900;//Temperature in roaster in degree C\n", +"P=101325;//Pressure in Pa\n", +"R=8.314;//Universal gas constant\n", +"dp=750;//Particle size in micrometer5\n", +"Fo=2.5;//Feed rate of solids in kg/s\n", +"uo=0.6;//Superficial gas velocity in m/s\n", +"W=80140;//Weight of bed in kg\n", +"ephsilonmf=0.50;//Void fraction at minimum fluidized condition\n", +"umf=0.5;//Velocity at minimum fluidization condition in m/s\n", +"db=0.2;//Estimated bubble size in m\n", +"g=9.81;//Acceleration due to gravity in square m/s^2\n", +"Lm=1;//Length of fixed bed in m\n", +"ephsilonm=0.45;//Void fraction of fixed bed\n", +"xA=0.21;//Mole fraction of oxygen in feed\n", +"kc=0.015//Rate constant in m/s for reaction which follows shrinking core model\n", +"Ds=8E-6;//Diffusion coefficient of solid in m^2/s\n", +"rhosbar=4130;//Average particle density in kg/m^3\n", +"mB=0.09744;//Molecular weight of ZnS\n", +"a=3/2;//Stoichiometric coefficient of Oxygen in the reaction equation\n", +"\n", +"//CALCULATION\n", +"//Selection of models to represent reactor\n", +"ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)\n", +"f=ubr/(umf/ephsilonmf);\n", +"\n", +"//Step 1.\n", +"ub=uo-umf+ubr;//Rise velocity of bubbles from Eqn.(6.8)\n", +"delta=(uo-umf)/(ub+2*umf);//Fraction of the bed in bubbles from Eqn.(6.26)\n", +"Krguess=2;//Guess value of Kr\n", +"x=Lm*(1-ephsilonm)*umf*(1-delta)/uo^2;\n", +"CAi=xA*P/(R*(T+273));//Initial concentration of oxygen\n", +"\n", +"//Step 2.\n", +"kbar=(kc^-1+(dp*10^-6/(12*Ds))^-1)^-1;//Modified rate constant from Eqn.(11)\n", +"tbar=W/Fo;//Mean residence time of solids from Eqn.(14.2)\n", +"rhob=rhosbar/mB;//Density of ZnS\n", +"function[fn]=solver_func1(Kr)//Function defined for solving the system\n", +" XA=1-exp(-x*Kr);//Conversion from Eqn.(42)\n", +" CAbar=(CAi*XA*uo^2)/(Kr*Lm*(1-ephsilonm)*umf*(1-delta));//Average concentration of oxygen from Eqn.(43)\n", +" tou=rhob*dp*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)\n", +" y=tbar/tou;//Term tbar/tou\n", +" XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)\n", +" //Step 3.\n", +" fn=XBbar-1.2*XA;//From Table E5, for Fo=2.5kg/s\n", +"endfunction\n", +"[Kr]=fsolve(Krguess,solver_func1,1E-6);//Using inbuilt function fsolve for solving for Kr\n", +"XA=1-exp(-x*Kr);//Conversion from Eqn.(42)\n", +"CAbar=(CAi*XA*uo^2)/(Kr*Lm*(1-ephsilonm)*umf*(1-delta))//Average concentration of oxygen from Eqn.(43)\n", +"tou=rhob*dp*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)\n", +"y=tbar/tou;//Term tbar/tou\n", +"XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)\n", +"\n", +"//OUTPUT\n", +"printf('\nSelection of models to represent reactor');\n", +"printf('\n\tSince ratio ubr/(umf/ephsilonmf)= %f <1, the reactor is operating in slow bubble regime',f);\n", +"printf('\n\tSince particle size =%f micrometer, they react according to shrinking-core model',dp);\n", +"printf('\n\tConversion obtained for %f micrometer particle:%f',dp,XBbar);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/3-Fluidization_and_Mapping_of_Regimes.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/3-Fluidization_and_Mapping_of_Regimes.ipynb new file mode 100644 index 0000000..a111bcb --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/3-Fluidization_and_Mapping_of_Regimes.ipynb @@ -0,0 +1,243 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 3: Fluidization and Mapping of Regimes" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 3.1: Size_Measure_of_Nonuniform_Solids.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-3, Example 1, Page 68\n", +"//Title: Size Measure of Nonuniform Solids\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"weight = [0;60;150;270;330;360];// Weight in grams for the oversized particles\n", +"psize = [50;75;100;125;150;175];//PSD in micrometers\n", +"\n", +"//CALCULATION\n", +"len = length(psize); // To obtain the size of input array\n", +"// Computation of sauter mean diameter for the given PSD\n", +"i = 1;\n", +"while i<len\n", +" dpi(i)=(psize(i,:)+ psize(i+1,:))/2;\n", +" weightf(i)=(weight(i+1)-weight(i))/weight(6); \n", +" dp(i)=weightf(i)/dpi(i); \n", +" i=i+1;\n", +"end \n", +"dpbar=1/sum(dp);//Calculation of average particle daimeter Eq.(15)\n", +"\n", +"//OUTPUT\n", +"mprintf('\n The Sauter mean diameter of the material with the given particle size distribution = %f micrometer',dpbar);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 3.2: Estimation_of_Minimum_Fluidizing_Velocity.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-3, Example 2, Page 76\n", +"//Title: Estimation of Minimum fluidizing velocity\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"ephsilon=0.55;//Void fraction of bed\n", +"rhog=0.0012;//Density of gas in g/cc\n", +"myu=.00018;//Viscosity of gas in g/cm s\n", +"dpbar=0.016;//Mean diameter of solids in centimeter\n", +"phis=0.67;//Sphericity of solids\n", +"rhos=2.6;//Density of solids in g/cc\n", +"g=980;//Acceleration due to gravity in square cm/s^2\n", +"\n", +"//CALCULATION\n", +"//Computation of umf using the simplified equation for small particles\n", +"umf=((dpbar^2)*(rhos-rhog)*g*(ephsilon^3)*(phis^2))/(150*myu*(1-ephsilon));//Simplified equation to calculate minimum fluidizing velocity for small particles Eq.(21)\n", +"Re=(dpbar*umf*rhog)/myu;//To calculate Reynolds number for particle\n", +"\n", +"//Computation of umf if neither void fraction of bed nor sphericity is known\n", +"c1=28.7; c2=0.0494;//Value of constants from Table 4, page 70\n", +"umf1=(myu/(dpbar*rhog))*(((c1^2)+((c2*(dpbar^3)*rhog*(rhos-rhog)*g)/(myu^2)))^0.5-c1);//Equation to calculate minimum fluidizing velocity for coarse particles Eq.(25)\n", +"err=((umf-umf1)/umf)*100;//Calculation of error from experimental value\n", +"\n", +"//OUTPUT\n", +"if Re<20 then \n", +" mprintf('\nThe particle Reynolds no = %f',Re)\n", +" printf('\nThe simplified equation used for calculating minimum fluidizing velocity is valid.');\n", +"end\n", +"mprintf('\nThe minimum fluidizing velocity by simplified equation for small particles = %fcm/s',umf);\n", +"mprintf('\nThe minimum fluidizing velocity by equation for coarse partilces = %fcm/s',umf1);\n", +"mprintf('\nThis value is %f percent below the experimentally reported value.',err);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 3.3: Estimation_of_Terminal_Velocity_of_Falling_Particles.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-3, Example 3, Page 82\n", +"//Title: Estimation of terminal velocity of falling particles\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhog=1.2e-3;//Density of air in g/cc\n", +"myu=1.8e-4//Viscosity of air in g/cm s\n", +"dpbar=0.016//Mean diameter of solids in centimeter\n", +"phis=0.67;//Sphericity of solids\n", +"rhos=2.6;//Density of solids in g/cc\n", +"g=980//Acceleration due to gravity in square cm/s^2\n", +"\n", +"//CALCULATION\n", +"dpstar=dpbar*((rhog*(rhos-rhog)*g)/myu^2)^(1/3);//Calculation of dimensionless particle size Eq.(31)\n", +"utstar=((18/(dpstar^2))+(2.335-(1.744*phis))/(dpstar^0.5))^-1;//Calculation of dimensionless gas velocity Eq.(33)\n", +"ut=utstar*((myu*(rhos-rhog)*g)/rhog^2)^(1/3);//Calculation of terminal velocity of falling particles Eq.(32)\n", +"\n", +"\n", +"//OUTPUT\n", +"mprintf('\nThe dimensionless particle size = %f', dpstar);\n", +"mprintf('\nThe dimensionless gas velocity = %f', utstar);\n", +"mprintf('\nThe terminal velocity of falling particles = %fcm/s', ut);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 3.4: Prediction_of_Flow_Regimes.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-3, Example 4, Page 91\n", +"//Title: Prediction of flow regime\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhos=1.5;//Density of Solid in g/cc\n", +"uo1=40; uo2=80;//Superficial gas velocity in cm/s\n", +"dp1=0.006; dp2=0.045;//Particle size in centimeter\n", +"rhog1=1.5E-3; rhog2=1E-3; //Density of gas in g/cc\n", +"myu1=2E-4; myu2=2.5E-4;//Viscosity of air in g/cm s\n", +"g=980;//Acceleration due to gravity in square cm/s^2\n", +"\n", +"//CALCULATION\n", +"//for smaller particles\n", +"dpstar1=dp1*((rhog1*(rhos-rhog1)*g)/myu1^2)^(1/3);//Calculation of dimensionless particle diamter Eq.(31)\n", +"uostar1=uo1*((rhog1^2)/((myu1)*(rhos-rhog1)*g))^(1/3);\n", +"uostar2=uo2*((rhog1^2)/((myu1)*(rhos-rhog1)*g))^(1/3);//Calculation of dimensionless superficial gas velocity Eq.(32)\n", +"\n", +"//for larger particles \n", +"dpstar2=dp2*((rhog2*(rhos-rhog2)*g)/myu2^2)^(1/3);//Calculation of dimensionless particle diamter Eq.(31)\n", +"uostar3=uo1*((rhog2^2)/((myu2)*(rhos-rhog2)*g))^(1/3);\n", +"uostar4=uo2*((rhog2^2)/((myu2)*(rhos-rhog2)*g))^(1/3);//Calculation of dimensionless superficial gas velocity Eq.(32)\n", +"\n", +"\n", +"//OUTPUT\n", +"printf('\nFor particle of size %f centimeter',dp1);\n", +"mprintf('\nThe dimensionless particle diameter = %f',dpstar1);\n", +"mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar1,uo1);\n", +"mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar2,uo2);\n", +"mprintf('\n\nFrom Fig.16(page 89)comparing u*=%f vs dp*=%f',uostar1,dpstar1);\n", +"mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Onset of turbulent fluidization in an ordinary bubbling bed',uo1);\n", +"mprintf('\nFrom Fig.16(page 89)comparing u* =%f vs dp* =%f',uostar2,dpstar1);\n", +"mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Fast fluidization(requires a circulating solid system)',uo2);\n", +"printf('\n\nFor particle of size %f centimeter',dp2)\n", +"mprintf('\nThe dimensionless particle diameter = %f',dpstar2);\n", +"mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar3,uo1);\n", +"mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar4,uo2);\n", +"mprintf('\n\nFrom Fig.16(page 89)comparing u*=%f vs dp*=%f',uostar3,dpstar2);\n", +"mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Bublling Fluidization',uo1);\n", +"mprintf('\nFrom Fig.16(page 89)comparing u* =%f vs dp* =%f',uostar4,dpstar2);\n", +"mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Bubbling Fluidization',uo2);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/4-The_Dense_Bed.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/4-The_Dense_Bed.ipynb new file mode 100644 index 0000000..565ff97 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/4-The_Dense_Bed.ipynb @@ -0,0 +1,266 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 4: The Dense Bed" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 4.1: Design_of_a_Perforated_Plate_Distributor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-4, Example 1, Page 106\n", +"//Title: Design of a Perforated Plate Distributor\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dt=4;//Vessel diameter in m\n", +"Lmf=2;//Length of the bed in m\n", +"ephsilonmf=0.48;//Void fraction of bed\n", +"rhos=1500;//Density of solid in kg/m^3\n", +"rhog=3.6;//Density of gas in kg/m^3\n", +"myu=2E-5;//Viscosity of gas in kg/m s\n", +"po=3;//Pressure of inlet gas in bar\n", +"uo=0.4;//Superficial velocity of gas in m/s\n", +"uorm=40;//Maximum allowable jet velocity from holes in m/s\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"gc=1;\n", +"pi=3.1428;\n", +"\n", +"//CALCULATION\n", +"//Computation of minimum allowable pressure drop through the distributor\n", +"deltapb={(1-ephsilonmf)*(rhos-rhog)*g*Lmf}/gc;//Calculation of pressure drop in bed using Eqn.(3.17)\n", +"deltapd=0.3*deltapb;//Calculation of pressure drop in distributor using Eqn.(3)\n", +"\n", +"//Computation of orifice coefficient\n", +"Ret=(dt*uo*rhog)/myu;\n", +"if Ret>=3000 then Cd=0.60;\n", +"elseif Ret>=2000 then Cd=0.61;\n", +"elseif Ret>=1000 then Cd=0.64;\n", +"elseif Ret>=500 then Cd=0.68;\n", +"elseif Ret>=300 then Cd=0.70;\n", +"elseif Ret>=100 then Cd=0.68;\n", +"end\n", +"\n", +"//Computation of gas velocity through orifice\n", +"uor=Cd*((2*deltapd)/rhog)^0.5;//Calculation of gas velocity through orifice by using Eqn.(12)\n", +"f=(uo/uor)*100;//Calculation of fraction of open area in the perforated plate \n", +"\n", +"\n", +"//Computation of number of orifices per unit area of distributor\n", +"dor=[0.001;0.002;0.004];//Different orifice diameters in m\n", +"n=length(dor);\n", +"i=1;\n", +"while i<=n\n", +" Nor(i)=(uo*4)/(pi*uor*(dor(i))^2);//Calculation of number of orifices by using Eqn.(13)\n", +" i=i+1;\n", +"end\n", +" \n", +"//OUTPUT\n", +"mprintf('\nThe pressure drop in bed:%fPa',deltapb);\n", +"mprintf('\nThe minimum allowable pressure drop in distributor:%fPa',deltapd);\n", +"if uor<uorm then mprintf('\nThe gas veleocity of %fm/s is satisfactory',uor);\n", +" else mprintf('\nThe gas veleocity of %fm/s is not satisfactory',uor);\n", +"end\n", +"if f<10 then mprintf('\nThe fraction of open area of %f percent is allowable',f);\n", +" else mprintf('\nThe fraction of open area of %f percent is not allowable',f);\n", +"end \n", +"printf('\nDiameter of orifice(m)');\n", +"printf('\tNumber of orifices per unit area(per sq.m)');\n", +"j=1;\n", +"while j<=n\n", +" mprintf('\n%f',dor(j));\n", +" mprintf('\t\t%f',Nor(j));\n", +" j=j+1;\n", +"end\n", +"printf('\nThis number can be rounded off.');\n", +"printf('\nSince orifices that are too small are liable to clog and those that are too large cause uneven distribution of gas, we choose orifice of diameter %fm',dor(2));\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 4.2: Design_of_a_Tuyere_Distributor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-4, Example 2, Page 108\n", +"//Title: Design of a Tuyere Distributor\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"lor=0.1;//Minimum allowable tuyere spacing in m\n", +"uorm=30;//Maximum allowable jet velocity from the tuyere in m/s\n", +"uo=0.4;//Superficial velocity of gas in m/s\n", +"uor=30.2;//Gas velocity through orifice,from Exa 1, in m/s\n", +"Cd=0.6;//Dicharge coefficient from Exa 1\n", +"rhog=3.6//Density of gas in kg/m^3\n", +"pi=3.1428;\n", +"\n", +"//CALCULATION\n", +"Nor=1/(lor^2);//Calculation of number of orifices per unit area by assuming minimum spacing for tuyeres\n", +"dor={(4/pi)*(uo/uor)*(1/Nor)}^0.5;//Calculation of diameter of inlet orifiec by using Eqn.(13)\n", +"\n", +"//Computation of diameter of hole for different number of holes per tuyere\n", +"q=(lor^2)*uo;//Volumetric flow rate in m^3/s\n", +"Nh=[8;6;4];//Different number of holes per tuyere\n", +"n=length(Nh);\n", +"i=1;\n", +"while i<=n\n", +" dh(i)=((((q/Nh(i))*(4/pi))/uorm)^0.5);//Calculation of diameter of holes\n", +" i=i+1;\n", +"end\n", +"deltaph=(rhog/2)*((uor/Cd)^2);\n", +"\n", +"//OUTPUT\n", +"printf('\nNumber of holes(number of holes/tuyeres)');\n", +"printf('\tDiameter of hole(m)');\n", +"j=1;\n", +"while j<=n\n", +" mprintf('\n%f',Nh(j));\n", +" mprintf('\t\t\t\t\t%f',dh(j));\n", +" j=j+1;\n", +"end\n", +"printf('\nThe design chosen is as follows');\n", +"printf('\n\tTuyeres are as shown in Fig.2(b),page 97');\n", +"mprintf('\n\tNumber of holes = %f(Since rectangular pitch is chosen for tuyeres)',Nh(2));\n", +"mprintf('\n\tDiameter of hole = %fm',dh(2));\n", +"mprintf('\n\tDiameter of incoming high-pressure-drop orifice = %fm ID',dor);\n", +"printf('\nChecking the pressure drop in tuyeres');\n", +"mprintf('\nSince pressure drop of %fPa gives sufficiently high distributor pressure drop as seen in Exa.1, use of inlet orifice can be dispensed.',deltaph);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 4.3: Power_Requirement_for_a_Fluidized_Coal_Combustor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-4, Example 3, Page 110\n", +"//Title: Power Requirement for a Fluidized Coal Combustor(FBC)\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"deltapd=[3;10]//Distributor pressure drop in kPa\n", +"deltapd2=10;//Distributor pressure drop in kPa\n", +"po=101;//Entering air pressure in kPa\n", +"To=20;//Entering air temperature in degree C\n", +"y=1.4;//Fugacity of air\n", +"deltapb=10;//Pressure drop in bed in kPa\n", +"p3=103;//Pressure at the bed exit in kPa\n", +"F=8;//Feed rate of coal in tons/hr\n", +"H=25;//Gross heatig value of coal in MJ/kg\n", +"Fa=10;//Air required at standard condition in nm^3/kg\n", +"etac=0.75;//Efficiency of compressor\n", +"etap=36;//Efficiency of plant in %\n", +"\n", +"//CALCULATION\n", +"//Calculation of volumetric flow rate of air\n", +"vo=((F*1000)*Fa*((To+273)/273))/3600;\n", +"\n", +"//Case(a) Distributor Pressure drop = 3kPa and Case(b) Distributor Pressure drop = 10kPa\n", +"n=length(deltapd);\n", +"i=1;\n", +"while i<=n\n", +" p2(i)=p3+deltapb;//Calculation of pressure at the entrance of the bed\n", +" p1(i)=p2(i)+deltapd(i);//Calculation of pressure before entering the bed\n", +" ws(i)=(y/(y-1))*po*vo*((p1(i)/po)^((y-1)/y)-1)*(1/etac);//Calculation of power required for the compressor by Eqn.(18) & Eqn.(20)\n", +" i=i+1;\n", +"end\n", +"\n", +"//Case(c) 50% of the required bypassed to burn the volatile gases. Distributor Pressure drop = 3kPa\n", +"//No change in pressure drop from case(a)\n", +"v1=vo/2;//New volumetric flow rate of air\n", +"ws1=ws(1)/2;//Power required for blower for primary air\n", +"ws2=(y/(y-1))*po*v1*((p3/po)^((y-1)/y)-1)*(1/etac);//Power required for blower for bypassed air\n", +"wst=ws1+ws2;//Total power required for the two blowers\n", +"p=((ws(1)-wst)/ws(1))*100;//Saving in power when compared to case(a)\n", +"\n", +"//OUTPUT\n", +"printf('\nCase(a)');\n", +"mprintf('\n\tVolumetric flow rate of air = %f m^3/hr',vo);\n", +"mprintf('\n\tPower required for compressor = %f kW',ws(1));\n", +"printf('\nCase(b)');\n", +"mprintf('\n\tVolumetric flow rate of air = %f m^3/hr',vo);\n", +"mprintf('\n\tPower required for compressor = %f kW',ws(2));\n", +"printf('\nCase(c)');\n", +"mprintf('\n\tVolumetric flow rate of air = %f m^3/hr',v1);\n", +"mprintf('\n\tPower required for compressor for primary air = %f kW',ws1);\n", +"mprintf('\n\tPower required for blower for bypassed air = %f kW',ws2);\n", +"mprintf('\n\tTotal power required for the two blowers = %f kW',wst);\n", +"mprintf('\n\tPower saved compared to case(a) = %f percent',p);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/5-Bubbles_in_Dense_Beds.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/5-Bubbles_in_Dense_Beds.ipynb new file mode 100644 index 0000000..114d006 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/5-Bubbles_in_Dense_Beds.ipynb @@ -0,0 +1,129 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 5: Bubbles in Dense Beds" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 5.1: Characteristics_of_a_Singe_Bubble.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-5, Example 1, Page 126\n", +"//Title: Charactersitics of a Single Bubble\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dt=60;//ID of tube in cm \n", +"dp=300;//Size of particles of bed in micrometers\n", +"umf=3;//Velocity at minimum fluidization condition in cm/s\n", +"ephsilonmf=0.5;//Void fraction of bed at minimum fluidization condition\n", +"db=5;//Diameter of bubble in cm\n", +"g=980;//Acceleration due to gravity in cm/s^2\n", +"\n", +"//CALCULATION\n", +"//Computation of rise velocity of bubble\n", +"if (db/dt)<0.125 then ubr=(0.711*((g*db)^0.5));//Rise velocity by Eqn.(3)\n", +"elseif (db/dt)<0.6 then ubr=(0.711*((g*db)^0.5))*1.2*exp(-1.49*(db/dt));//Rise velocity by Eqn.(4) \n", +"end\n", +"\n", +"//Computation of cloud thickness\n", +"Rb=db/2;//Radius of bubble\n", +"uf=umf/ephsilonmf;//Velocity of emulsion gas\n", +"Rc=Rb*((ubr+(2*uf))/(ubr-uf))^(1/3);//Radius of cloud by Eqn.(6)\n", +"\n", +"//OUTPUT\n", +"mprintf('\nThe rise velocity of the bubble=%fcm/s',ubr);\n", +"mprintf('\nThe cloud thickness=%fcm',Rc-Rb);\n", +"mprintf('\nFrom Fig.8(page 124)comparing fw vs dp, for dp = %f micrometer, wake fraction = 0.24',dp);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 5.2: Initial_Bubble_Size_at_a_Distributor.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-5, Example 2, Page 132\n", +"//Title: Initial Bubble Size at a Distributor\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"uo=15;//Superificial gas velocity in cm/s\n", +"umf=1;////Velocity at minimum fluidization condition in cm/s\n", +"lor=2;//Pitch of perforated plate in cm\n", +"g=980;//Acceleration due to gravity in cm/s^2\n", +"//CALCULATION\n", +"//Case(a) For porous plate\n", +"dbo1=(2.78/g)*(uo-umf)^2;//Initial bubble size using Eqn.(19)\n", +"\n", +"//Case(b) For Perforated plate\n", +"Nor=(2/sqrt(3))*(1/lor)^2;//Number of orifices in cm^-2\n", +"dbo2=(1.30/(g^0.2))*((uo-umf)/Nor)^0.4;//Initial bubble size using Eqn.(15) assuming inital bubble size is smaller than hole spacing\n", +"\n", +"//OUTPUT\n", +"printf('\nCase(a) For porous plate');\n", +"printf('\n\tInitial bubble size=%fcm',dbo1);\n", +"printf('\nCase(b) For Perforated plate');\n", +"printf('\n\tInitial bubble size=%fcm',dbo2);\n", +"printf('\n\tSince %f<%f, the equation used is correct.',dbo2,lor);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/6-Bubbling_Fluidized_Beds.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/6-Bubbling_Fluidized_Beds.ipynb new file mode 100644 index 0000000..ef9253c --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/6-Bubbling_Fluidized_Beds.ipynb @@ -0,0 +1,429 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 6: Bubbling Fluidized Beds" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 6.1: Bubble_Size_and_Rise_Velocity_in_Geldart_A_Beds.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-6, Example 1, Page 150\n", +"//Title: Bubble Size and Rise Velocity in Geldart A Beds\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"z=0.5;//Height of bed in m\n", +"dt=0.5;//ID of tube in m\n", +"rhos=1.6;//Density of catalyst in g/cm^3\n", +"dpbar=60;//Averge catalyst diameter in micrometer\n", +"umf=0.002;//Velocity at minimum fluidization condition in m/s\n", +"uo=0.2;//Superficial velocity in m/s\n", +"dor=2;//Diameter of orifice in mm\n", +"lor=20;//Pitch of perforated plate in mm\n", +"g=9.80;//g=980;//Acceleration due to gravity in m/s^2\n", +"\n", +"//CALCULATION\n", +"//Method 1. Procedure using Eqn.(10) & Eqn.(11)\n", +"db=(0.035+0.040)/2;//Bubble size at z=0.5m from Fig.7(a) & Fig.7(b)\n", +"ub1=1.55*((uo-umf)+14.1*(db+0.005))*(dt^0.32)+0.711*(g*db)^0.5;//Bubble velocity using Eqn.(10) & Eqn.(11)\n", +"\n", +"//Method 2. Werther's procedure\n", +"si=0.8;//From Fig.6 for Geldart A solids \n", +"ub2=si*(uo-umf)+(3.2*(dt^(1/3)))*(0.711*(g*db)^0.5);//Bubble velocity using Eqn.(9)\n", +"\n", +"//OUTPUT\n", +"printf('\nMethod 1. Procedure using Eqn.(10) & Eqn.(11)');\n", +"mprintf('\n\tDiameter of the bubble=%fm',db);\n", +"mprintf('\n\tRise velocity of the bubble=%fm/s',ub1);\n", +"printf('\nMethod 2. Werthers procedure');\n", +"mprintf('\n\tDiameter of the bubble=%fm',db);\n", +"mprintf('\n\tRise velocity of the bubble=%fm/s',ub2);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 6.2: Bubble_Size_and_Rise_Velocity_in_Geldart_B_Beds.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-6, Example 2, Page 151\n", +"//Title: Bubble Size and Rise Velocity in Geldart B Beds\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"z=0.5;//Height of bed in m\n", +"dt=0.5;//ID of tube in m\n", +"rhos=2.6;//Density of catalyst in g/cm^3\n", +"dpbar=100;//Averge catalyst diameter in micrometer\n", +"umf=0.01;//Velocity at minimum fluidization condition in m/s\n", +"uo=0.45;//Superficial velocity in m/s\n", +"dor=2;//Diameter of orifice in mm\n", +"lor=30;//Pitch of perforated plate in mm\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"pi=3.142857;\n", +"\n", +"//CALCULATION\n", +"//Part(a).Bubble Size\n", +"Nor=(2/sqrt(3))*(1/lor^2);\n", +"dbo=5.5;\n", +"\n", +"//Method 1.Werther's procedure for finding bubble size\n", +"z1=[0;5;10;20;30;50;70];\n", +"n=length(z1);\n", +"i=1; \n", +"while i<=n\n", +" db(i)=0.853*((1+0.272*(uo-umf)*100)^(1/3))*(1+0.0684*z1(i))^1.21;\n", +" i=i+1; \n", +"end\n", +"db1=0.163;//Since bubble size starts at dbo=5.5cm at z=0, we shift the curve accordingly to z=0.5m\n", +"\n", +"//Method 2.Mori and Wen's procedure for finding bubble size\n", +"dbm=0.65*((pi/4)*((dt*100)^2)*(uo-umf)*100)^0.4;\n", +"db2=dbm-(dbm-dbo)*exp(-0.3^(z/dt));\n", +"\n", +"//Part(b).Bubble Velocity\n", +"//Method 1.Procedure using Eqn.(12)\n", +"ub1=1.6*((uo-umf)+1.13*db1^0.5)*(dt^1.35)+(0.711*(g*db1)^0.5);\n", +"\n", +"//Method 2.Werther's Procedure\n", +"si=0.65;\n", +"ub2=si*(uo-umf)+2*(dt^0.5)*(0.711*(g*db1)^0.5);\n", +"\n", +"//Using Eqn.(7) & Eqn.(8)\n", +"ubr1=0.711*(g*db1)^0.5;\n", +"ubr2=0.711*(g*db2/100)^0.5\n", +"ub3=uo-umf+ubr1;\n", +"ub4=uo-umf+ubr2;\n", +"\n", +"//OUTPUT\n", +"printf('\nBubble Size');\n", +"mprintf('\nInitial bubble size from Fig.5.14 for %fm/s = %fcm',uo-umf,dbo);\n", +"printf('\n\n\tMethod 1.Werthers procedure for finding bubble size');\n", +"printf('\n\t\tHeight of bed(cm)');\n", +"printf('\t\t\tBubble size(cm)');\n", +"m=length(z1);\n", +"j=1;\n", +"while j<=m\n", +" mprintf('\n\t\t%f',z1(j));\n", +" mprintf('\t\t\t\t%f',db(j));\n", +" j=j+1;\n", +"end\n", +"printf('\n\n\tMethod 2.Mori and Wens procedure for finding bubble size');\n", +"mprintf('\n\t\tMaximum expected bubble size=%fcm',dbm);\n", +"mprintf('\n\t\tBubble size=%fcm',db2);\n", +"printf('\nBubble Velocity');\n", +"printf('\n\n\tMethod 1.Procedure using Eqn.(12)');\n", +"mprintf('\n\t\tBubble velocity=%fm/s',ub1);\n", +"printf('\n\n\tMethod 2.Werthers procedure');\n", +"mprintf('\n\t\tBubble velocity=%fm/s',ub2);\n", +"printf('\nComparing the above results with the expressions of the simple two-phase theory');\n", +"printf('\n\tWerthers bubble size');\n", +"mprintf('\tBubble rise velocity=%fm/s\tBubble velocity=%fm/s',ubr1,ub3);\n", +"printf('\n\tMori & Wens bubble size');\n", +"mprintf('\tBubble rise velocity=%fm/s\tBubble velocity=%fm/s',ubr2,ub4);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 6.3: Scale_down_of_a_Commercial_Chlorinator.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-6, Example 3, Page 153\n", +"//Title: Scale-down of a Commercial Chlorinator\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dpbar=53;//Average particle size in micrometer\n", +"s=[1;2];//Size of Bermuda rock in cm \n", +"rhosbar=3200;//Average solid density of the coke-zircon mixture in kg/m^3\n", +"ephsilonm=0.5;//Void fraction for fixed bed\n", +"ephsilonf=0.75;//Void fraction for bubbling bed\n", +"rhogbar=0.64;//Average density of gas in kg/m^3\n", +"uo=14;//Superficial gas velocity in cm/s\n", +"myu=5E-5;//Viscosity of gas in kg/m s\n", +"T=1000;//Temperature in degree C\n", +"P=1;//Pressure in atm\n", +"dt=91.5;//ID of bed in cm\n", +"sh=150;//Slumped height in cm\n", +"\n", +"//CALCULATION\n", +"rhog2=1.2;//Density of ambient air\n", +"myu2=1.8E-5;//Viscosity of ambient air\n", +"rhos2=rhog2*(rhosbar/rhogbar);//For the requirement of constant density ratio\n", +"m=((rhogbar*myu2)/(rhog2*myu))^(2/3);//Scale factor by usin Eqn.(16)\n", +"u2=(m^0.5)*uo;//Superficial gas velocity by using Eqn.(17)\n", +"//OUTPUT\n", +"printf('\nFor the model use');\n", +"mprintf('\n\tBed of ID %fcm\n\tSlumped bed height of %fcm\n\tPacked bed distributor consisting of %f-%fmm rock',m*dt,m*sh,m*s(1),m*s(2));\n", +"mprintf('\nFluidizing gas: ambient air at %fatm',P);\n", +"mprintf('\nSolids: \tzirconia, Average particle size=%fmicrometers',m*dpbar);\n", +"mprintf('\nEntering gas:\tSuperficial velocity=%fcm/s',u2);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 6.4: Reactor_Scale_up_for_Geldart_A_Catalyst.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-6, Example 4, Page 159\n", +"//Title: Reactor Scale-up for Geldart A Catalyst\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dtb=20;//ID of bench-scale reactor\n", +"dtp=1;//ID of pilot reactor\n", +"dpbar=52;//Average particle size in micrometer\n", +"ephsilonm=0.45;//Void fraction for fixed bed\n", +"ephsilonmf=0.50;//Void fraction at minimum fluidization condition\n", +"ephsilonmb=0.60;//Void fraction \n", +"uo=30;//Superficial gas velocity in cm/s\n", +"Lmb=2;//Length of fixed bed in m\n", +"umf=0.33;//Velocity at minimum fluidization condition in cm/s\n", +"umb=1;//Velocity at in cm/s\n", +"db=3;//Equilibrium bubble size in cm\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"pi=3.142857;\n", +"\n", +"//CALCULATION\n", +"ubr=0.711*(g*db/100)^0.5;//Rise velocity of bubble using Eqn.(7)\n", +"\n", +"//Bubble velocity for the bench unit\n", +"ubb1=1.55*(((uo-umf)/100)+14.1*((db/100)+0.005))*((dtb/100)^0.32)+ubr;//Bubble velocity using Eqn.(11)\n", +"si=1;\n", +"ubb2=si*((uo-umf)/100)+(3.2*((dtb/100)^(1/3)))*ubr;//Bubble velocity using Eqn.(9)\n", +"ubb=(ubb1+ubb2)/2;//Average bubble velocity\n", +"\n", +"//Bubble velocity for the pilot unit\n", +"ubp1=1.55*(((uo-umf)/100)+14.1*((db/100)+0.005))*(dtp^0.32)+ubr;//Bubble velocity using Eqn.(11)\n", +"si=1;\n", +"ubp2=si*((uo-umf)/100)+(3.2*(dtp^(1/3)))*ubr;//Bubble velocity using Eqn.(9)\n", +"ubp=(ubp1+ubp2)/2;//Average bubble velocity\n", +"\n", +"//Rise velocity of upflowing emulsion\n", +"ueb=ubb-ubr;//For the bench unit\n", +"uep=ubp-ubr;//For the pilot unit\n", +"\n", +"//Scale-Up Alternative 1.\n", +"dteb=20;//Effective bubble diameter\n", +"dib=[5;10;15;20];//Different outside diameters\n", +"n=length(dib);\n", +"i=1;\n", +"while i<=n\n", +" li(i)=sqrt(((pi*dib(i)*dteb)/4)+((pi/4)*(dib(i))^2));//Pitch using Eqn.(13)\n", +" i=i+1;\n", +"end \n", +"\n", +"//Scale-Up Alternative 2.\n", +"Lmp=Lmb*(ubp/ubb);//Static bed height of commercial unit\n", +"dtep=100;//Effective bubble diameter\n", +"dip=[10;15;20;25];//Different outside diameters\n", +"m=length(dip);\n", +"i=1;\n", +"while i<=m\n", +" lip(i)=sqrt(((pi*dip(i)*dtep)/4)+(pi/4)*dip(i));//Pitch using Eqn.(13)\n", +" i=i+1;\n", +"end \n", +"\n", +"//Height of Bubbling beds\n", +"//For bench unit\n", +"deltab=((uo/100)-(umb/100))/(ubb-(umb/100));//Fraction of bed in bubbles using Eqn.(28)\n", +"ephsilonfb=deltab+(1-deltab)*ephsilonmb;//Void fraction of bubbling bed using Eqn.(20)\n", +"Lfb=Lmb*(1-ephsilonm)/(1-ephsilonfb);//Hieght of bubbling bed usnig Eqn.(19)\n", +"//For pilot unit\n", +"deltap=((uo/100)-(umb/100))/(ubp-(umb/100));//Fraction of bed in bubbles using Eqn.(28)\n", +"ephsilonfp=deltap+(1-deltap)*ephsilonmb;//Void fraction of bubbling bed using Eqn.(20)\n", +"Lfp=Lmp*(1-ephsilonm)/(1-ephsilonfp);//Hieght of bubbling bed usnig Eqn.(19)\n", +"\n", +"//OUTPUT\n", +"mprintf('\nRise velocity of bubble=%fm/s',ubr);\n", +"printf('\nFor the bench unit');\n", +"mprintf('\n\tWith Eqn.(11), Rise velocity=%fm/s',ubb1);\n", +"mprintf('\n\tWith Werthers procedure, Rise velocity=%fm/s',ubb2);\n", +"mprintf('\n\tAverage rise velocity=%fm/s',ubb);\n", +"mprintf('\n\tRise velocity of upflowing emulsion=%fm/s',ueb);\n", +"printf('\nFor the pilot unit');\n", +"mprintf('\n\tWith Eqn.(11), Rise velocity=%fm/s',ubp1);\n", +"mprintf('\n\tWith Werthers procedure, Rise velocity=%fm/s',ubp2);\n", +"mprintf('\n\tAverage rise velocity=%fm/s',ubp);\n", +"mprintf('\n\tRise velocity of upflowing emulsion=%fm/s',uep);\n", +"printf('\nScale-Up Alternative 1.');\n", +"printf('\n\tOuter diameter of tube(cm)');\n", +"printf('\tPitch(cm)');\n", +"n=length(dib);\n", +"j=1;\n", +"while j<=n\n", +" mprintf('\n\t\t%f',dib(j));\n", +" mprintf('\t\t\t%f',li(j));\n", +" j=j+1;\n", +"end\n", +"printf('\n\tSuitable arrangement');\n", +"mprintf('\n\t\tOuter Diameter=%fcm\tPitch:Diameter ratio=%f',dib(2),(li(2)/dib(2)));\n", +"printf('\nScale-Up Alternative 2.');\n", +"mprintf('\n\tStatic bed height for commercial unit=%fm',Lmp);\n", +"printf('\n\tOuter diameter of tube(cm)');\n", +"printf('\tPitch(cm)');\n", +"n=length(dip);\n", +"j=1;\n", +"while j<=n\n", +" mprintf('\n\t\t%f',dip(j));\n", +" mprintf('\t\t\t%f',lip(j));\n", +" j=j+1;\n", +"end\n", +"printf('\n\tSuitable arrangement');\n", +"mprintf('\n\t\tOuter Diameter=%fcm\tPitch:Diameter ratio=%f',dip(2),(lip(2)/dip(2)));\n", +"printf('\n\n\t\t\t\tFraction of bed in bubbles\tVoid fraction of bed\tStatic bed height(m)\tHeight of bubbling bed(m)');\n", +"printf('\n\t\t\t\t---------------------------------------------------------------------------------------------------------');\n", +"mprintf('\nBench unit\tID=%fm\t%f\t\t\t%f\t\t%f\t\t%f',dtb/100,deltab,ephsilonfb,Lmb,Lfb);\n", +"mprintf('\nCommercial unit\tID=%fm\t%f\t\t\t%f\t\t%f\t\t%f',dtp,deltap,ephsilonfp,Lmp,Lfp);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 6.5: Reactor_Scale_up_for_Geldart_B_Catalyst.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-6, Example 5, Page 161\n", +"//Title: Reactor Scale-up for Geldart B Catalyst\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dtb=20;//ID of bench-scale reactor\n", +"dtp=1;//ID of pilot reactor\n", +"dpbar=200;//Average particle size in micrometer\n", +"ephsilonmf=0.50;//Void fraction at minimum fluidization condition\n", +"ephsilonmb=0.50;//Void fraction \n", +"uo=30;//Superficial gas velocity in cm/s\n", +"Lmb=2;//Length of fixed bed in m\n", +"umf=3;//Velocity at minimum fluidization condition in cm/s\n", +"umb=3;//Velocity at in cm/s\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"pi=3.142857;\n", +"\n", +"//CALCULATION\n", +"//In the small bench unit\n", +"c=1;\n", +"ubb=c*((uo-umf)/100)+0.35*(g*(dtb/100))^0.5;//Velocity using Eqn.(5.22)\n", +"zsb=60*(dtb)^0.175;//Height using Eqn.(5.24)\n", +"\n", +"//In the large pilot unit\n", +"ubp=c*((uo-umf)/100)+0.35*(g*dtp)^0.5;//Velocity using Eqn.(5.22)\n", +"zsp=60*(dtp*100)^0.175;//Height using Eqn.(5.24)\n", +"\n", +"//OUTPUT\n", +"printf('\nCondition at which bubbles transform into slugs');\n", +"mprintf('\nFor tha small bench unit\n\t\tVelocity=%fm/s\n\t\tHeight above distributor plate=%fm',ubb,zsb/100);\n", +"mprintf('\nFor tha large pilot unit\n\t\tVelocity=%fm/s\n\t\tHeight above distributor plate=%fm',ubp,zsp/100);\n", +"\n", +"//====================================END OF PROGRAM ======================================================\n", +"" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/7-Entrainment_and_Elutriation_from_Fluidized_Beds.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/7-Entrainment_and_Elutriation_from_Fluidized_Beds.ipynb new file mode 100644 index 0000000..745a4e8 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/7-Entrainment_and_Elutriation_from_Fluidized_Beds.ipynb @@ -0,0 +1,359 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 7: Entrainment and Elutriation from Fluidized Beds" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 7.1: Entrainment_from_fine_particle_beds_with_high_freeboard.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-7, Example 1, Page 179\n", +"//Title: Entrainment from Fine Particle Beds with High Freeboard\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhog=5.51;//Density of gas in kg/m^3\n", +"rhos=1200;//Density of solid in kg/m^3\n", +"dpbar=130;//Average size of particles in micrometer\n", +"uo=0.61;//Superficial gas velocity in m/s\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"\n", +"//CALCULATION\n", +"//Assuming that freeboard in higher than TDH, computation of entrainment rate by Zenz & Weil's method\n", +"x=(uo^2)/(g*(dpbar*10^-6)*rhos^2);//Calculation of value of x-axis for Fig.(6), page 175\n", +"y=1.2;// Value of y-axis from Fig.(6)\n", +"Gsstar=y*rhog*uo;//Computation of rate of entrainment\n", +"\n", +"//OUTPUT\n", +"mprintf('\nRate of entrainment=%fkg/m^2s',Gsstar);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 7.2: Entrainment_from_large_particle_beds_with_high_freeboard.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-7, Example 2, Page 180\n", +"//Title: Entrainment from Large Particle Beds with High Freeboard\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"x=0.2;//Fraction of fines in the bed\n", +"Gsstar=4.033320//Rate of entrainment in kg/m^2s(from Exa.1)\n", +"\n", +"//CALCULATION\n", +"Gsstar1=x*Gsstar;//Rate of entrainment by Eqn.(3)\n", +"\n", +"//OUTPUT\n", +"mprintf('\nRate of entrainment=%fkg/m^2s',Gsstar1);\n", +"\n", +"//====================================END OF PROGRAM ====================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 7.3: Entrainment_from_beds_with_a_wide_size_distribution_of_solids.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-7, Example 3, Page 181\n", +"//Title: Entrainment from Beds with a Wide Size Distribution of Solids\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhog=5.51;//Density of gas in kg/m^3\n", +"rhos=1200;//Density of solid in kg/m^3\n", +"uo=0.61;//Superficial gas velocity in m/s\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"dp=[10;30;50;70;90;110;130];//Diameter of particle in micrometer\n", +"p=[0;0.0110;0.0179;0.0130;0.0058;0.0020;0];\n", +"pi=3.142857;\n", +"dt=6;\n", +"\n", +"//CALCULATION\n", +"n=length(dp);\n", +"i=1;\n", +"while i<=n\n", +" x(i)=(uo^2)/(g*(dp(i)*10^-6)*rhos^2);//Computation of value of x-axis for Fig.(6), page 175)\n", +" i=i+1;\n", +"end\n", +"y=[40;12;6;3.2;2.;1.3;1];//Value of y-axis corresponding to each value of x-axis\n", +"y1 = y .* p;\n", +"i=1;\n", +"k=0;\n", +"while i<n\n", +" y1(i)=(y(i)*p(i));\n", +" k=k+((0.5)*(dp(i+1)-dp(i))*(y1(i+1)+y1(i)));//Integration using Trapezoidal rule\n", +" i=i+1;\n", +"end\n", +"rhosbar=k*rhog;//Computation of solid loading\n", +"te=(pi/4)*(dt^2)*rhosbar*uo;//Computation of total entrainment\n", +"\n", +"//OUTPUT\n", +"mprintf('\nSolid loading =%fkg/m^3',rhosbar);\n", +"mprintf('\nTotal Entrainment =%fkg/s',te);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 7.4: kstar_from_steady_state_experiments.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-7, Example 4, Page 181\n", +"//Title: k* from Steady State Experiments\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dp=[40;60;80;100;120];//Diameter of particle in micrometer\n", +"uo=0.381;//Superficial gas velocity in m/s\n", +"\n", +"//CALCULATION\n", +"Gs=0.9;//Rate of entrainment in kg/m^2 s from Fig.3(a)\n", +"pb=(1/100)*[0.45;1.00;1.25;1.00;0.60];//Size distribution for bed particles from Fig.3(b)\n", +"pe=(1/100)*[1.20;2.00;1.25;0.45;0.10];//Size distribution for entrained particles from Fig.3(b)\n", +"n=length(dp);\n", +"i=1;\n", +"while i<=n\n", +" ki(i)=(Gs*pe(i))/pb(i);//Calculation of ki* using Eqn.(13)\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\ndpi(micrometer)');\n", +"printf('\t100pb(dpi)(micrometer^-1)');\n", +"printf('\t100pe(dpi)(micrometer^-1)');\n", +"printf('\tki*(kg/m^2 s)');\n", +"j=1;\n", +"while j<=n\n", +" mprintf('\n%f',dp(j));\n", +" mprintf('\t%f',100*pb(j));\n", +" mprintf('\t\t\t%f',100*pe(j));\n", +" mprintf('\t\t\t%f',ki(j)); \n", +" j=j+1;\n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 7.5: Comparing_predictions_for_kstar.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-7, Example 5, Page 181\n", +"//Title: Comparing Predictions for k*\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"rhog=1.217;//Density of gas in kg/m^3\n", +"myu=1.8E-5;//Viscosity of gas in kg/m s\n", +"umf=0.11;//Velocity at minimum fluidization condition in m/s\n", +"rhos=2000;//Density of solid in kg/m^3\n", +"uo=1.0;//Superficial gas velocity in m/s\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"dp=[30;40;50;60;80;100;120];//Diameter of particle in micrometer\n", +"uti=[0.066;0.115;0.175;0.240;0.385;0.555;1.0];//Terminal velocity of particles in m/s\n", +"\n", +"//CALCULATION\n", +"n=length(dp);\n", +"i=1;\n", +"while i<=n\n", +" //Using Yagi & Aochi's correlation\n", +" Ret(i)=(rhog*(uti(i))*dp(i)*10^-6)/myu;\n", +" kistar1(i)=((myu*((uo-uti(i))^2))/(g*(dp(i)*10^-6)^2))*(0.0015*(Ret(i)^0.5)+(0.01*(Ret(i)^1.2)));\n", +" //Using Wen & Hasinger's correlation\n", +" kistar2(i)=(((1.52E-5)*((uo-uti(i))^2)*rhog)/(g*dp(i)*10^-6)^0.5)*(Ret(i)^0.725)*((rhos-rhog)/rhog)^1.15;\n", +" //Using Merrick & Highley's correlation\n", +" kistar3(i)=uo*rhog*(0.0001+130*exp(-10.4*((uti(i)/uo)^0.5)*((umf/(uo-umf))^0.25)));\n", +" //Using Geldart's correlation\n", +" kistar4(i)=23.7*uo*rhog*exp(-5.4*(uti(i)/uo));\n", +" //Using Zenz & Weil's procedure\n", +" x1(i)=(uo^2)/(g*(dp(i)*10^-6)*rhos^2);//Computation of value of x-axis for Fig.(6), page 175)\n", +" y1=[12.2;8.6;6.4;4.9;2.75;1.8;1.2];//Value of y-axis corresponding to each value of x-axis\n", +" kistar5(i)=y1(i)*rhog*uo;\n", +" //Using Gugnoni & Zenz's procedure\n", +" x2(i)=(uo-uti(i))/((g*dp(i)*10^-6)^0.5);//Computation of value of x-axis for Fig.(6), page 175)\n", +" y=[5.8;5.4;3.2;2.8;1.3;0.6;0];//Value of y-axis corresponding to each value of x-axis\n", +" kistar6(i)=y(i)*rhog*uo;\n", +" i=i+1;\n", +"end\n", +"\n", +"i=1;\n", +"printf('dp(micrometer)');\n", +"printf('\tYagi & Aochi');\n", +"printf('\tWen & Hashinger');\n", +"printf('\t\tMerrick & Highley');\n", +"printf('\tGeldart et al.');\n", +"printf('\t\tZenz & Well');\n", +"printf('\t\tGugnoni & Zenz');\n", +"while i<=n\n", +" mprintf('\n%f',dp(i));\n", +" mprintf('\t%f',kistar1(i)); \n", +" mprintf('\t%f',kistar2(i));\n", +" mprintf('\t\t%f',kistar3(i));\n", +" mprintf('\t\t%f',kistar4(i));\n", +" mprintf('\t\t%f',kistar5(i));\n", +" mprintf('\t\t%f',kistar6(i));\n", +" i=i+1;\n", +"end \n", +"\n", +"//Note: There is huge deviation of the calculated answer and the answer given in the textbook for the correlation of Merrick & Highley. There is a contradiction in the correlation used in the problem and the one given in page 179. \n", +"//We tried to retrieve the original paper i.e. D.Merrick and J.Highley, AICHE J., 6, 220(1960). But the effort was not fruitful.\n", +"\n", +"//====================================END OF PROGRAM ====================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 7.6: Entrainment_from_a_short_vessel.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-7, Example 6, Page 190\n", +"//Title: Entrainment from a Short Vessel Ht<TDH\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"dpbar=60;//Average size of particles in micrometer\n", +"rhog=1.3;//Density of gas in kg/m^3\n", +"rhos=1500;//Density of solid in kg/m^3\n", +"umf=0.003;//Velocity at minimum fluidization condition in m/s\n", +"uo=0.503;//Superficial gas velocity in m/s\n", +"g=9.80;//Acceleration due to gravity in m/s^2\n", +"Hf=2;//Height at which the cyclone inlet is to be located in m\n", +"\n", +"//CALCULATION\n", +"y=(uo^2)/(g*(dpbar*10^-3)*rhos^2);//Calculation of value of y-axis for Fig.(6), page 175\n", +"x=1;//Value of x-axis from Fig.(6), page 175\n", +"Gsstar=x*rhog*uo;//Computation of rate of entrainment\n", +"Gsuo=5.0;//Ejection rate pf particles in kg/m^2 s from Fig.(11), page 188\n", +"a=0.72/uo;//From Fig.(12), page 189\n", +"Gs=Gsstar+(Gsuo-Gsstar)*exp(-a*Hf);\n", +"p=((Gs-Gsstar)/Gsstar)*100;\n", +"\n", +"//OUTPUT\n", +"mprintf('\nRate of entrainment from short bed=%fkg/m^2s',Gs);\n", +"mprintf('\nThis entrainment is %f percent higher than it would be if the gas exit were at the TDH',p);\n", +"\n", +"//====================================END OF PROGRAM ====================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/8-High_velocity_Fluidization.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/8-High_velocity_Fluidization.ipynb new file mode 100644 index 0000000..5670c0b --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/8-High_velocity_Fluidization.ipynb @@ -0,0 +1,161 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 8: High velocity Fluidization" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 8.1: Performance_of_a_Fast_Fluidized_Vessel.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"//Chapter-8, Example 1, Page 206\n", +"//Title: Performance of a Fast Fluidized Vessel\n", +"//==========================================================================================================\n", +"clear\n", +"clc\n", +"//INPUT\n", +"Lmf=2.4;//Length of bed at minimum fluidized condition in m\n", +"uo=[2;4;6];//Superficial gas velocity in m/s\n", +"GsII=100;//Solid circulation rate in kg/m^2 s for Mode II\n", +"uoIII=4;//Superficial gas velocity in m/s for Mode III\n", +"GsIII=[42;50;100;200;400];//Solid circulation rate in kg/m^2 s for Mode III\n", +"GsIV=[70;100;120];//Solid circulation rate in kg/m^2 s for Mode IV\n", +"dt=0.4;//Column diamter in m\n", +"Ht=10;//Height of column in m\n", +"rhos=1000;//Density of solid in kg/m^3\n", +"dpbar=55;//Particle diameter in micrometer\n", +"ephsilonmf=0.5;//Void fraction at minimum fluidization condition\n", +"//CALCULATION\n", +"//Mode I\n", +"ephsilonstar=0.01;//Saturation carrying capacity of gas\n", +"ephsilonsd=[0.2;0.16;0.14];//Solid holdup in lower dense region from Fig.8(b) for various uo\n", +"n=length(uo);\n", +"i=1;\n", +"Hfguess=2;//Guess value of height\n", +"while i<=n\n", +" a(i)=3/uo(i);//Decay constant\n", +" function[fn]=solver_func(Hf)//Function defined for solving the system\n", +" fn=Lmf*(1-ephsilonmf)-((ephsilonsd(i)-(ephsilonstar+(ephsilonsd(i)-ephsilonstar)*exp(-a(i)*Hf)))/a(i))-Ht*ephsilonsd(i)+Hf*(ephsilonsd(i)-ephsilonstar);\n", +" endfunction\n", +" [Hf(i)]=fsolve(Hfguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf\n", +" Hd(i)=Ht-Hf(i);//Height of lower densce region\n", +" ephsilonse(i)=ephsilonstar+(ephsilonsd(i)-ephsilonstar)*exp(-a(i)*Hf(i));//Solid holdup at exit\n", +" GsI(i)=rhos*uo(i)*ephsilonse(i);//Solid circulation rate from Eqn.(4)\n", +" i=i+1;\n", +"end\n", +"//Mode II\n", +"i=1;\n", +"Hfguess2=2;//Guess value of height\n", +"while i<=n\n", +" ephsilonseII(i)=GsII/(rhos*uo(i));//Solid holdup at exit\n", +" function[fn]=solver_func1(Hf)//Function defined for solving the system\n", +" fn=ephsilonseII(i)-ephsilonstar-(ephsilonsd(i)-ephsilonstar)*exp(-a(i)*Hf);//From Eqn.(7)\n", +" endfunction\n", +" [HfII(i)]=fsolve(Hfguess2,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf\n", +" HdII(i)=Ht-HfII(i);//Height of lower dense region\n", +" //Length of bed minimum fluidization condtion\n", +" LmfII(i)=(1-ephsilonmf)^-1*[((ephsilonsd(i)-ephsilonseII(i))/a(i))+Ht*ephsilonsd(i)-HfII(i)*(ephsilonsd(i)-ephsilonstar)];\n", +" i=i+1;\n", +"end\n", +"//Mode III\n", +"aIII=3/uoIII;//Decay constant\n", +"ephsilonsdIII=0.16;//Solid holdup at lower dense region\n", +"i=1;\n", +"m=length(GsIII);\n", +"Hfguess3=2;//Guess value of height \n", +"while i<=m\n", +" ephsilonseIII(i)=GsIII(i)/(rhos*uoIII);//Solid holdup at exit\n", +" function[fn]=solver_func2(Hf)//Function defined for solving the system\n", +" fn=ephsilonseIII(i)-ephsilonstar-(ephsilonsdIII-ephsilonstar)*exp(-aIII*Hf);//From Eqn.(7)\n", +" endfunction\n", +" [HfIII(i)]=fsolve(Hfguess3,solver_func2,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf\n", +" HdIII(i)=Ht-HfIII(i);//Height of lower dense region\n", +" //Length of bed at minimum fluidization condition\n", +" LmfIII(i)=(1-ephsilonmf)^-1*[((ephsilonsdIII-ephsilonseIII(i))/aIII)+Ht*ephsilonsdIII-HfIII(i)*(ephsilonsdIII-ephsilonstar)];\n", +" i=i+1;\n", +"end\n", +"//Mode IV\n", +"i=1;\n", +"Hfguess4=2;//Guess value of height\n", +"while i<=n\n", +" aIV(i)=3/uo(i);//Decay constant\n", +" ephsilonseIV(i)=GsIV(i)/(rhos*uo(i));//Solid holdup at exit\n", +" function[fn]=solver_func3(Hf)//Function defined for solving the system\n", +" fn=ephsilonseIV(i)-ephsilonstar-(ephsilonsd(i)-ephsilonstar)*exp(-aIV(i)*Hf);//From Eqn.(7)\n", +" endfunction\n", +" [HfIV(i)]=fsolve(Hfguess4,solver_func3,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf\n", +" HdIV(i)=Ht-HfIV(i);//Height of lower dense region\n", +" //Length of bed at minimum fluidization condition\n", +" LmfIV(i)=(1-ephsilonmf)^-1*[((ephsilonsd(i)-ephsilonseIV(i))/aIV(i))+Ht*ephsilonsd(i)-HfIV(i)*(ephsilonsd(i)-ephsilonstar)];\n", +" i=i+1;\n", +"end\n", +"//OUTPUT\n", +"printf('\nMode I');\n", +"printf('\n\tuo(m/s)\t\tephsilonse(-)\tHf(m)\t\tHd(m)\t\tGs(kg/m^2 s)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%f\t%f\t%f\t%f\t%f',uo(i),ephsilonse(i),Hf(i),Hd(i),GsI(i));\n", +" i=i+1;\n", +"end\n", +"printf('\nMode II');\n", +"printf('\n\tuo(m/s)\t\tephsilonse(-)\tHf(m)\t\tHd(m)\t\tLmf(m))');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%f\t%f\t%f\t%f\t%f',uo(i),ephsilonseII(i),HfII(i),HdII(i),LmfII(i));\n", +" i=i+1;\n", +"end\n", +"printf('\nMode III');\n", +"printf('\n\tGs(kg/m^ s)\tephsilonse(-)\tHf(m)\t\tHd(m)\t\tLmf(m)');\n", +"i=1;\n", +"while i<=m\n", +" mprintf('\n\t%f\t%f\t%f\t%f\t%f',GsIII(i),ephsilonseIII(i),HfIII(i),HdIII(i),LmfIII(i));\n", +" i=i+1;\n", +"end\n", +"printf('\nMode IV');\n", +"printf('\n\tuo(m/s)\t\tGs(kg/m^2 s)\tephsilonse(-)\tHf(m)\t\tLmf(m)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n\t%f\t%f\t%f\t%f\t%f',uo(i),GsIV(i),ephsilonseIV(i),HfIV(i),LmfIV(i));\n", +" i=i+1;\n", +"end\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/9-Solid_Movement_Mixing_Segregation_and_Staging.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/9-Solid_Movement_Mixing_Segregation_and_Staging.ipynb new file mode 100644 index 0000000..9bf2518 --- /dev/null +++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/9-Solid_Movement_Mixing_Segregation_and_Staging.ipynb @@ -0,0 +1,245 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 9: Solid Movement Mixing Segregation and Staging" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 9.1: Vertical_Movement_of_Solids.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-9, Example 1, Page 218\n", +"//Title: Vertical Movement of Solids\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"umf=0.015;//Velocity at minimum fluidization condition in m/s\n", +"ephsilonmf=0.5;//Void fraction at minimum fluidization condition\n", +"uo=0.1;//Superficial gas velocity in m/s\n", +"delta=0.2;//Bed fraction in bubbles\n", +"db=0.06;//Equilibrium bubble size in m\n", +"dt=[0.1;0.3;0.6;1.5];//Various vessel sizes in m\n", +"ub=[0.4;0.75;0.85;1.1];//Bubble velocity in m/s\n", +"Dsv=[0.03;0.11;0.14;0.23];//Reported values of vertical dispersion coefficient\n", +"\n", +"//CALCULATION\n", +"n=length(ub);\n", +"i=1;\n", +"fw1=2;//Wake fraction from Hamilton et al.\n", +"fw2=0.32;//Wake fraction from Fig.(5.8)\n", +"fw=(fw1+fw2)*0.5;//Average value of wake fraction\n", +"while i<=n\n", +" Dsv1(i)=12*((uo*100)^0.5)*((dt(i)*100)^0.9);//Vertical distribution coefficient from Eqn.(3)\n", +" Dsv2(i)=(fw^2*ephsilonmf*delta*db*ub(i)^2)/(3*umf);//Vertical distribution coefficient from Eqn.(12)\n", +" i=i+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"printf('\n\t\tVertical dispersion coefficient(m^2/s)');\n", +"printf('\nVessel Size(m)');\n", +"printf('\tFrom Experiment');\n", +"printf('\tFrom Eqn.(3)');\n", +"printf('\tFrom Eqn.(12)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',dt(i));\n", +" mprintf('\t%f',Dsv(i));\n", +" mprintf('\t%f',Dsv1(i)/10^4);\n", +" mprintf('\t%f',Dsv2(i));\n", +" i=i+1; \n", +"end\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 9.2: Horizontal_Drift_Of_Solids.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-9, Example 2, Page 222\n", +"//Title: Horizontal Drift Of Solids\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Lmf=0.83;//Length of bed at minimum fluidization condition in m\n", +"dp=450;//Average particle size in micrometer\n", +"ephsilonmf=0.42;//Void fraction at minimum fluidization condition\n", +"umf=0.17;//Velocity at minimum fluidization condition in m/s\n", +"uo=[0.37;0.47;0.57;0.67];//Superficial gas velocity in m/s\n", +"Dsh=[0.0012;0.0018;0.0021;0.0025];//Horizontal Drift Coefficient from Experiment in m^2/s\n", +"db=[0.10;0.14];//Equilibrium bubble size in m\n", +"g=9.81;//Acceleration due to gravity in m/s^2\n", +"\n", +"\n", +"//CALCULATION\n", +"n=length(uo);\n", +"m=length(db);\n", +"j=1;\n", +"i=1;\n", +"k=1;\n", +"alpha=0.77;//Since we are not dealing with Geldart A or AB solids\n", +"uf=umf/ephsilonmf;\n", +"for j = 1:m\n", +" for i = 1:n\n", +" ubr(k)=0.711*(db(j)*g)^0.5;//Rise velocity of a single bubble in m/s\n", +" ub(k)=uo(i)-umf+ubr(k);//Rise velocity of bubbles in a bubbling bed\n", +" delta(k)=(uo(i)-umf)/(ub(k)+umf);//Bed fraction in bubbles\n", +" if ubr(i)>uf then Dshc(k)=(3/16)*(delta(k)/(1-delta(k)))*((alpha^2*db(j)*ubr(k)*[(((ubr(k)+2*uf)/(ubr(k)-uf))^(1/3))-1]));//Horizontal Distribution coeff. from Eqn.(14)\n", +" else Dsh(k)=(3/16)*(delta/(1-delta))*(alpha^2*umf*db/ephsilonmf);//Horizontal Distribution coeff. from Eqn.(15)\n", +" end\n", +" Dshc(k)=(3/16)*(delta(k)/(1-delta(k)))*((alpha^2*db(j)*ubr(k)*[(((ubr(k)+2*uf)/(ubr(k)-uf))^(1/3))-1]));//Horizontal Distribution coeff. from Eqn.(14)\n", +" i=i+1;\n", +" k=k+1;\n", +" end\n", +" i=1;\n", +" j=j+1;\n", +"end\n", +"\n", +"//OUTPUT\n", +"i=1;\n", +"j=1;\n", +"k=1;\n", +"while k<=m*n\n", +" mprintf('\nSnce we do not have ub=%fm/s>>uf=%fm/s we use Eqn.(14).',ub(k),uf)\n", +" printf('\nGas Velocity(m/s)');\n", +" printf('\tHorizontal Drift Coefficient Calculated(m^2/s)');\n", +" printf('\tHorizontal Drift Coefficient from Experiment(m^2/s)');\n", +" while j<=m\n", +" mprintf('\ndb=%fm',db(j));\n", +" while i<=n\n", +" mprintf('\n%f',uo(i));\n", +" mprintf('\t\t%f',Dshc(k));\n", +" mprintf('\t\t\t\t\t%f',Dsh(i));\n", +" i=i+1; \n", +" k=k+1;\n", +" end\n", +" i=1;\n", +" j=j+1;\n", +" end\n", +"end \n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 9.3: Design_of_Baffle_Plates.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491\n", +"\n", +"//Chapter-9, Example 3, Page 232\n", +"//Title: Design of Baffle Plates\n", +"//==========================================================================================================\n", +"\n", +"clear\n", +"clc\n", +"\n", +"//INPUT\n", +"Gsup=1.5;//Solid interchange rate in kg/m^2plate s\n", +"dor=19.1;//Orifice diameter in mm\n", +"dp=210;//Particle size in micrometer\n", +"uo=0.4;//Superficial gas velocity in m/s\n", +"fopen=[0.12;0.17;0.26];//Open area fraction \n", +"pi=3.14;\n", +"\n", +"//CALCULATION\n", +"n=length(fopen);\n", +"i=1;\n", +"while i<=n\n", +" uor(i)=uo/fopen(i);//Gas velocity through the orifice\n", +" ls1(i)=Gsup/fopen(i);//Flux of solids through the holes\n", +" i=i+1;\n", +"end\n", +"ls2=[12;20;25];//Flux of solids through holes from Fig.13(c) for different uor values\n", +"fopen1=0.12;//Open area fraction which gives reasonable fit\n", +"lor=sqrt(((pi/4)*dor^2)/fopen1);//Orifice spacing\n", +"\n", +"//OUTPUT\n", +"printf('\nfopen');\n", +"printf('\t\tuor(m/s)');\n", +"printf('\tls from Eqn.(18)');\n", +"printf('\tls from Fig.13(c)');\n", +"i=1;\n", +"while i<=n\n", +" mprintf('\n%f',fopen(i));\n", +" mprintf('\t%f',uor(i));\n", +" mprintf('\t%f',ls1(i));\n", +" mprintf('\t\t%f',ls2(i));\n", +" i=i+1; \n", +"end\n", +"mprintf('\n\nFor square pitch, the orifice spacing should be %fmm',lor);\n", +"\n", +"//====================================END OF PROGRAM ======================================================" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} |