换热器模型原程序（C语言）.doc

管壳式换热器数学模型模拟与计算换热器模型原程序（C语言）#include #include float density(float t,float d) float x,z; x=1+(t/100); z=0.942+0.248*x+0.174*d*d+0.0841/(x*d)-0.312*x/d-0.556*exp(-x); z=z*1000; return(z); /*以下为比热容的计算：*/ float hcap(float t,float d) float cp; cp=(0.7072+(0.00147-0.000551*d)*t-0.318*d)*(0.055*12.5+0.35); cp=cp*4186; return(cp); /*以下为热导率的计算：*/ float hcon(float t,float d) float cn; cn=0.1008*(1-0.00054*t)/d; cn=cn*4186/3600; return(cn); float nianc(float t,float d) float ni; ni=exp(exp(22.81142-3.68738*log(t+273)-1.22; ni=ni*density(t,d)*0.000001; return(ni); float nianh(float t,float d) float ni; ni=exp(exp(18.9173-2.92782*log(t+273)-1.22; ni=ni*density(t,d)*0.000001; return(ni); main() int n,N; float tc1,tc2,th1,th2,k,q,e,h,hi,ho,ntu,rei,reo,pri,pro,wc,tao, wh,tmc,tmh,ai,ao,twi,two,cpc,cph,rdc,rdh,ndc,ndh,di,dou,dk, d1,d2,s1,s2,cmin,cmax,de,p,l,v1,v2,rs,rt,thx,tx,ty,thy,tcx,tcy;tc1=160; th1=280; wh=29.5; N=324; wc=37.5; di=0.021; dou=0.025; dk=0.8; l=6.0; p=0.032; n=0; rs=0.0005; rt=0.0001; thx=th1; do tmh=(th1+thx)/2; cph=hcap(tmh,0.919); q=wh*cph*(th1-thx); tcx=tc1; do tmc=(tc1+tcx)/2; tc2=tc1+q/(wc*hcap(tmc,0.850); tcy=tcx; tcx=tc2; while(fabs(tc2-tcy)0.1); tmc=(tc1+tc2)/2; d1=density(tmc,0.850); d2=density(tmh,0.919); cpc=hcap(tmc,0.850); rdc=hcon(tmc,0.850); rdh=hcon(tmh,0.919); ndc=nianc(tmc,0.850); ndh=nianh(tmh,0.919);s1=3.1415926*0.25*di*di*N*0.5; v1=wc/d1/s1; ai=3.1415926*di*N*l; rei=di*v1*d1/ndc; pri=cpc*ndc/rdc; s2=0.230*dk*(1-dou/p); v2=wh/d2/s2; de=4*(p*p-3.1415926*0.25*dou*dou)/(3.1415926*dou); reo=de*v2*d2/ndh; pro=cph*ndh/rdh; ao=3.1415926*dou*N*l; h=0.023*pow(rei,0.8)*pow(pri,0.33)*rdc/di; hi=h; twi=tmc+q/(h*ai); dohi=h*pow(ndc/nianc(twi,0.850),0.14); tx=twi; twi=tmc+q/(hi*ai); while(fabs(twi-tx)0.5); hi=h*pow(ndc/nianc(twi,0.850),0.14);if(reo2000)h=0.36*pow(reo,0.55)*pow(pro,0.33)*rdh/de; if(reo0.5); ho=h*pow(ndh/nianh(two,0.919),0.14); k=1/(1/hi+rt)*ao/ai+1/ho+rs); cmin=wh*cph; cmax=wc*cpc; ntu=k*ao/(wh*cph); tao=ntu*sqrt(1+(cmin/cmax)*(cmin/cmax); e=2/(1+(cmin/cmax)+sqrt(1+(cmin/cmax)*(1+exp(-tao)/(1-exp(-tao); th2=th1-e*(th1-tc1);tc2=tc1+(cmin/cmax)*(th1-th2); thy=thx; thx=th2; n+; printf(output of the recycle %d:n,n); printf(Rei=%f,rei); printf(Reo=%f,reo); printf(Pri=%f,pri); printf(Pro=%fn,pro); printf(Hi=%f,hi); printf(Ho=%f,ho); printf(Th2=%f,th2); printf(Tc2=%fn,tc2); printf(e=%fn,e); printf(NTU=%fn,ntu); printf(K=%fn,k); while(fabs(th2-thy)0.1); 现采用一管壳式换热器，以蒸馏塔釜排出的渣油预热原油。已知换热器结构为双管程单壳程，壳内径为0.8m，管束规格为252mm，长度为6.0m，共324根，材质为碳钢。管束的管子按正方形排列，管心距为32mm。壳程设有切除25%的折流板，间距为230mm，原油走管程，渣油走壳程。已知冷物流的条件有： 渣油：流量Wh=106200/h，温度Th1=280；原油：流量Wc=135000/h，温度Tc1=160；污垢热阻：渣油侧：Rs=0.0005m2/W；原油侧：Rt=0.0001 m2/W；相对密度：式中 , Tm-定性温度, D20-20时油品相对密度，可查取或实测; 对渣油，K渣油=12.5，对原油，K原油=12.5定压热容：热导率： Kcal/（ mh）粘度： 厘泊-温度为t1时的运动粘度，厘泊；-温度为t2时的运动粘度，厘泊。如选t1=50，t2=100，可查得1渣油=1500，2渣油=120，1原油=90， 2原油=13将已知条件各数值赋予程序中相应的变量，运行后可得如下结果：即：output of the recycle 1:Rei=5459.146973,Reo=7749.009277,Pri=52.925968,Pro=70.550148Hi=499.244751,Ho=805.451111,Th2=245.832932,Tc2=190.821411e=0.284726NTU=0.409956K=235.563385output of the recycle 2:Rei=7134.744629,Reo=6253.752930,Pri=41.856537,Pro=84.399651Hi=617.473083,Ho=729.976990,Th2=243.293076,Tc2=191.539963e=0.305891NTU=0.455251K=255.301697output of the recycle 3:Rei=7265.567383,Reo=6151.324219,Pri=41.198006,Pro=85.579514Hi=625.540039,Ho=723.879333,Th2=243.161789,Tc2=191.541321e=0.306985NTU=0.457643K=256.173096output of the recycle 4:Rei=7272.351562,Reo=6146.061035,Pri=41.164467,Pro=85.641144Hi=625.955139,Ho=723.561829,Th2=243.1