蒸汽管道壓降溫降計算EXCEL軟件

1、名 稱符號公 式管道外徑Do管道總長度L管道始端蒸汽焓H1蒸汽始端壓力P1蒸汽始端溫度T1蒸汽終端允許壓力P2管道終端允許溫度T2管道終端允許蒸汽焓H2管道蒸汽流量V管道允許焓降HH=H1-H2假定保溫厚度假定假定管道保溫外徑D1D1=D0+2*假定管道外表面積SS=*D1*L/1000允許散熱密度qq=1000*H*V/S允許對流和輻射散熱密度q1假定：q1=q環(huán)境溫度ta假定室外常年平均風(fēng)速w保溫層材料黑度(鍍鋅鐵皮)假設(shè)管道保溫外壁溫度ts假定管道對流傳熱系數(shù)acac=72.81*w0.6/D10.4管道保溫外表面?zhèn)鳠嵯禂?shù)anan=(5.67*/(ts-ta)/(273+ts)/100)

2、4-(273+ta)/100)4)傳熱系數(shù)aa=ac+an允許保溫外表面溫度tsts=ta+q1/a管道設(shè)計溫度TT=(T1+T2)/2管道外表面溫度tt=T1管道保溫層平均溫度tmtm=(t+ta)/2保溫材料導(dǎo)熱系數(shù)=0.035+1.65*0.0001*tm+1.242*E-7*tm2保溫層熱傳導(dǎo)散熱密度q2q2=q1保溫層厚度=*(t-ts)/q2實(shí)際取用保溫厚度A實(shí)際保溫層熱傳導(dǎo)散熱密度q2q2=(t-ts)/(A/)實(shí)際取用保溫外徑D1D1=D0+2*A管道實(shí)際總外表面積SS=*D1*L/1000管道實(shí)際損失熱量QQ=q2*S/1000蒸汽焓降HH=Q/V終端實(shí)際焓H2H2=H1-H

3、終端實(shí)際溫度T2查表單 位管徑計算(426x8)管徑計算(426x8)管徑計算(426x8)管徑計算(426x8)mm426426133219m160016001000700kj/kg303230322828.273287Mpa0.850.8513.8290290200430Mpa0.50.50.83.65260260173405kj/kg3000300027753232.11t/h6050521kj/kg323253.2754.89mm100100100150mm626626333519m23145.0243145.0241045.621140.762W/m2169.580052141.31

4、67170.75812543280.6822691w/m2169.580052141.3167170.75812543280.6822691-30-302020m/s32230.250.250.250.2500304010.709628328.39691280510.8086557111.545077180.0022850510.0022850510.0133872710.0112214610.711913378.39919785610.8220429811.55629864-14.16902321-13.1749754726.5383334344.28824987275275186.5417

5、.5275275186.5417.5122.5122.5103.25218.75W/(m.K)0.0570762760.0570762760.0533602920.077036914w/m2169.580052141.3167170.75812543280.6822691mm97.32684276116.3907263120.6306861102.4328384mm100100100150w/m2165.0469105164.479545185.35601215191.6738768mm626626333519m23145.0243145.0241045.621140.762kw519.076

6、4947517.292116889.24995342218.6542751kj/kg31.1445896837.2450324164.2599664637.48359001kj/kg3000.855412994.7549682764.0100343249.516412702651704121.734104046誤差 %名 稱符 號單 位公 式管段始端壓力p1Mpa管段始端溫度t1蒸汽流量Gt/h管段始端蒸汽比容1m3/kg管段始端蒸汽焓值h1kj/kg管段末端允許壓力(假定)p2Mpa管段末端允許溫度(假定)t2管段末端蒸汽比容(假定)2m3/kg平均壓力ppjMpa平均比容pjm3/kgVp

7、j=0.5*(1+2)管道流速計算wm/sw=G/(Di/594.7)2抽汽管道管外徑(假定)Dwmm抽汽管道管內(nèi)徑Dimm抽汽管道壁厚mm介質(zhì)動力粘度1Pa.s查汽規(guī)P162165頁介質(zhì)運(yùn)動粘度m2/s=1*1雷諾系數(shù)ReRe=w*Di/管道等值粗糙度查汽規(guī)P166頁管道相對粗糙度/Di管道摩擦系數(shù)查汽規(guī)P39頁莫迪圖管道彎頭個數(shù)n1每90米一個彎管道上閥門個數(shù)n2閘閥1只單個彎頭局部阻力系數(shù)j1j1=20*(單個彎頭阻力系數(shù))彎頭處局部總阻力系數(shù)jwjw=n1*j1(彎頭局部阻力系數(shù):r/d=1)止回閥局部阻力系數(shù)j2查汽規(guī)(止回閥門阻力系數(shù)：L/Di=50)閘閥局部阻力系數(shù)j3查汽規(guī)(閘

8、閥阻力系數(shù))jfjf=j2+1*j3管道局部阻力系數(shù)jj=jw+jf管道沿程阻力系數(shù)yy=*L/Di管道總長Lm管道阻力系數(shù)tt=j+y管道壓降P1PaP1=t*w2/2*管道壓降PMPap=1.1*p1/1000000(阻力預(yù)留10%預(yù)量)終端管道實(shí)際壓力P2MPaP2=P1-P管道壓降比值Bp/p1終端壓力計算誤差 %數(shù)值1(426x8)數(shù)值1(219x6)13.82004305210.2060.08172828.273287.670.83.651704050.22110.081620.9003.7250.213550.0816624.168262615.1622815224.190944133219125200560.20.30.00160.00150.0150.020.0214256895030110.250.412.512030.2500.25312.751