管壳式换热器模拟计算~~~.doc

管壳式换热器模拟计算 （课本P40 2-5题）张锐钧 200748004 化0704程序中各参数的意义：字母意义字母意义n迭代次数niu1/2冷/热物料运动粘度Ai/Ao管内外传热面积yita1/2冷/热物料粘度D壳体直径B折流板间距L管长度t管心距Di/Do/Dm管内径/外径/平均管径niuwi/o内外表面壁温下运动粘度Ko总传热系数yitawi/o内外表面壁温下粘度De壳程当量直径Dwi/o内外表面壁温下相对密度Si管程通道截面积rouwi/o内外表面壁温下密度Smax壳程通道截面积ld管材（碳钢）热导率Wh热物料(渣油)流量b管壁厚Wc冷物料(原油)流量Hi0/Ho0管内外表面传热系数初值Th1/Tc1热/冷物料入口温度Hi/Ho管内外表面传热系数 Th2/Tc2热/冷物料出口温度Qh/Qc热/冷物料热流量Th20/Tc20热/冷物料出口温度初值Twi0/Two0热/冷物料壁温初值Cp1/Cp2热/冷物料定压比热容Twi/Two热/冷物料壁温C热容流率比(热/冷)Rs/Rt热/冷物料侧污垢热阻Tmh/Tmc热/冷物料定性温度ui/uo管/壳程流速D1/D21热/冷物料相对密度Rei/Reo管/壳程雷诺数K油品特性因数Pri/Pro管/壳程普朗特数rou1/rou2冷/热物料密度NTU传热单元数lamada1/2冷/热物料热导率E传热效率程序条文：# include # include main()double Do=0.025，Di=0.021，L=6，Wh=29.5; Th1=280，Wc=37.5， Tc1=160，Ro=0.0005,Ri=0.0001，D1,D2，D2O1=0.85，D2O2=0.919，Tc2,Th2，MD2O1，MD2O2，K=12.5,Cp1,Cp2，ramda1,ramda2，niu1,niu2，yita1,yita2,a1,b1,a2,b2,Tc20,Th20,Tmc,Tmh,C,Qc,Qh,Ho,Hi,Reo,Rei,Pro,Pri,Si,rou1,ui,Hi0,Twi0,Ai,Twi,niuwi,yitawi,Dwi,Xwi,rouwi,Ao,Smax,B=0.23,D=0.8,t=0.032,De,uo,rou2,Ho0,Two0,Two,niuwo,yitawo,Dwo,Xwo,rouwo，Ko，NTU,E,F,Cmin,Cmax，Xh,Xc，ld=44,b=0.002,Dm=0.0023，e=2.71828;int n=0;Tc2=180;Th2=260; /*给Tc2，Th2赋初值*/ do n+; printf(n=%dn,n);Th20=Th2; Tmh=(Th1+Th20)/2;doTc20=Tc2; /*Tc2的迭代*/ Tmc=(Tc1+Tc20)/2; Cp1=(0.7072+(0.00147-0.00051*D2O1)*Tmc-0.318*D2O1)*(0.055*K+0.35)*4.18*1000;Cp2=(0.7072+(0.00147-0.00051*D2O2)*Tmh-0.318*D2O2)*(0.055*K+0.35)*4.18*1000;C=Wh*Cp2/(Wc*Cp1);Tc2=Tc1+C*(Th1-Th20);while(fabs(Tc2-Tc20)=0.1); Qh=Wh*Cp2*(Th1-Th2); Qc=Wc*Cp1*(Tc2-Tc1);Ai=3.14*Di*L*324;Si=0.25*3.14*Di*Di*324/2;Xc=1+Tmc/100.0;MD2O1=pow(D2O1,2);D1=0.942+0.248*Xc+0.174*MD2O1+0.0841/(Xc*D2O1)-0.312*Xc/D2O1-0.556*exp(-Xc);rou1=1000*D1; ui=Wc/(rou1*Si);b1=log(log(90.0+1.22)/log(13+1.22)/(log(50.0+273)/(100.0+273); a1=log(log(90+1.22)-b1*log(50.0+273); niu1=exp(exp(a1+b1*log(Tmc+273)-1.22;yita1=niu1*rou1/1000000;Rei=Di*ui*rou1/yita1;ramda1=0.4213*(1-0.00054*Tmc)/D2O1/3.6;Pri=Cp1*yita1/ramda1; Hi0=0.027*pow(Rei,0.8)*pow(Pri,0.33)*ramda1/Di;Twi0=Tmc+Qc/(Hi0*Ai);do /*管壁内壁温的迭代*/ niuwi=pow(e,pow(e,a1+b1*log(Twi0+273)-1.22; Xwi=1+Twi0/100.0;Dwi=0.942+0.248*Xwi+0.174*MD2O1+0.0841/(Xwi*D2O1)-0.312*Xwi/D2O1-0.556*exp(-Xwi);rouwi=1000*Dwi;yitawi=niuwi*rouwi/1000000;Hi=Hi0*(pow(yita1/yitawi),0.14);Twi=Tmc+Qc/(Hi*Ai);Twi0=Twi;while(fabs(Twi-Twi0)=0.5); Ao=3.14*Do*L*324;Smax=B*D*(1-Do/t); De=4*(t*t-0.25*3.14*Do*Do)/(3.14*Do);Xh=1+Tmh/100.0;MD2O2=pow(D2O2,2);D2=0.942+0.248*Xh+0.174*MD2O2+0.0841/(Xh*D2O2)-0.312*Xh/D2O2-0.556*exp(-Xh);rou2=1000*D2;uo=Wh/(rou2*Smax);b2=log(log(1500+1.22)/log(120+1.22)/(log(50.0+273)/(100.0+273); a2=log(log(1500+1.22)-b2*log(50.0+273); niu2=exp(exp(a2+b2*log(Tmh+273)-1.22;yita2=niu2*rou2/1000000;Reo=De*uo*rou2/yita2;ramda2=0.4213*(1-0.00054*Tmh)/D2O2/3.6;Pro=Cp2*yita2/ramda2;Ho0=0.36*pow(Reo,0.55)*pow(Pro,0.33)*ramda2/De; Two0=Tmh-Qh/(Ho0*Ao);do /*管壁外壁温的迭代*/ niuwo=exp(exp(a1+b1*log(Two0+273)-1.22; Xwo=1+Two0/100;Dwo=0.942+0.248*Xwo+0.174*MD2O1+0.0841/(Xwo*D2O1)-0.312*Xwo/D2O1-0.556*exp(-Xwo);rouwo=1000*Dwo;yitawo=niuwo*rouwo/1000000;Ho=Ho0*(pow(yita2/yitawo),0.14);Two=Tmh-Qh/(Ho*Ao);Two0=Two; while(fabs(Two-Two0)=0.5)； Ko=1/(1/Hi+Ri)*Ao/Ai+1/Ho+Ro+b/ld*Do/Dm); /*以管外表面为基准，计算传热系数K*/Cmin=Wh*Cp2;Cmax=Wc*Cp1;NTU=Ko*Ao/Cmin; /*传热单元数*/ F=NTU*sqrt(1+pow(Cmin/Cmax,2); E=2/(1+Cmin/Cmax)+sqrt(1+Cmin/Cmax)*(1+exp(-F)/(1-exp(-F); /*传热效率*/ Th2=Th1-E*(Th1-Tc1);Tc2=Tc1+C*(Th1-Th2); printf(Th2=%.1lftTc2=%.1lfn,Th2,Tc2); printf(Rei=%.2lftPri=%.2lftHi=%.2lfn,Rei,Pri,Hi); printf(R