6F级燃蒸汽热水联合循环设计计算表

燃气轮机部分计算,,,,,,,余热锅炉部分计算,,,,,,,,汽轮机部分,,,,除氧器部分,,,,冷凝器部分,,,,烟筒部分,,,,二号加热器,

,,,,,,,,,,,,,,,汽机高压进气量D0ˊ(t/h),126,,,,,,,,,,,,,,,,

已知及选取值：,,,,,,,,,,,,t/h,,,汽机低压进气量D0〞(t/h),17.20202138,,,,,,,,,,,,,,,,

燃气轮机轴功率Pgt（KW）,77100,,燃料热值Hu（KJ/Kg),56263,,,输入烟气焓Qr(KJ/Kg）,1075.0079,,总烟气利用能（KJ/s）,151509.4563,,,,汽机高压蒸汽进气压力P0′(MPa),8,,,出水量,160.519623,,,排气冷凝后温度,30,,,烟筒中烟气进气温度,130,,,进汽温度,86

大气温度Ta（K）,288,,进气道压损率εc,0.01,,,排烟温度tpy（℃）,130,,锅炉高压蒸汽最高流量（Kg/s）,43.04563868,154.9642993,,,汽机高压蒸汽进气温度t0′(℃),550,,,出水压力,0.12,,,排气冷凝后焓值,125.6643,,,烟气进气焓,210,,,进汽压力,0.06

大气压力Pa（Mpa）,0.1013,,燃烧室压损率εb,0.03,,,排烟焓hpy（KJ/Kg）,210,,锅炉低压蒸汽最高流量（Kg/s）,51.30174933,184.6862976,,,汽机高压蒸汽进气焓h0′（KJ/Kg）,3519.74,,,出水温度,104,,,冷却水进入温度,15,,,烟气进气流量(t/h),634.5,,,进汽焓,2434.9419

压气机内效率ηc,0.9,,排气道压损率εt,0.03,,,排烟损失q2,0.195347402,,取高压蒸汽流量（Kg/s）,35,126,,,汽机低压蒸汽进气压力P0″(MPa),0.72,,,出水焓,435.95,,,冷却水进入焓,63.5142,,,烟气排气温度,80,,,热水进入温度,44.64

透平内效率ηt,0.92,,烟气泄露系数μc1,0.05,,,散热损失q5,0.005,,低压蒸汽流量（Kg/s）,9.588784174,34.51962303,,,汽机低压蒸汽进气温度t0″(℃),250,,,除氧器加热给水参数：,,,,冷却水排出温度,20,,,烟气排气焓,128.5,,,热水进口焓,187.3783

燃烧室内效率ηb,0.98,,压缩比π,17,,,灰渣损失q6,0,,,,,,,汽机低压蒸汽进气焓h0″（KJ/Kg）,2953.3,,,压力,0.72,,,冷却水排出焓,83.9548,,,烟气排气流量（t/h）,634.5,,,热水出口温度,60

整体效率ηm,0.99,,燃烧温度T3﹡(K）,1623,,,化学未完全燃烧损失q3,0,,,,,,,高压进气处熵值S0′（KJ/(Kg.K)),6.8775,,,温度,250,,,冷却水量(t/h),6643.867328,,,换热器换热量(KW),14364.375,,,热水出口焓,251.1591

Cpa[KJ/(Kg*K)],1.03,,ka,1.386,,,机械未完全燃烧损失q4,0,,,,,,,在1MPa进汽处：,,,,比焓,2953.3,,,冷却水密度,1000,,,热水进入温度,20,,,热水流量（t/h）,500

Cpg[KJ/(Kg*K)],1.2,,Kg,1.315,,,锅炉总损失∑q,0.200347402,,,,,,,查P-S图可知：,,,,0.06MPa抽汽加热后参数：,,,,冷却水流速（m/s),1.5,,,热水进口焓,83.9548,,,换热量(KW),8858.444444

燃料碳氢比x,3.72,,过量空气系数α,1.1,,,锅炉热效率ηgl,0.799652598,,,,,,,抽汽温度t1′(℃),238.93,,,压力,0.06,,,所需流通截面,1.230345801,,,热水流量（t/h）,500,,,蒸汽冷凝后出口温度,70

计算部分：,,,,,,,锅炉有效利用热Q1（KJ/Kg）,859.6328605,,,,,,,抽汽焓h1′（KJ/Kg）,2918.1464,,,温度,70,,,管径（m),0.025,,,热水出口焓,187.3783,,,蒸汽冷凝后出口焓,292.9962

⑴在压缩机内,,,⑵在燃烧室中,,,,给水温度tgs(℃),104,,,,,,,抽汽量D1（t/h),60,,,比焓,292.9962,,,管数,2506.442002,,,出口热水温度,44.64,,,蒸汽抽汽量(t/h）,14.88851935

T1＊（K）,288,,T3＊（K),1623,,,给水压力Pgs（Mpa）,0.12,,,,,,,抽汽后蒸汽流量D1′,66,,,流量,14.8,,,取管数,2507,,,查得换热器换热系数,116,,,换热器换热系数,3000

T2s＊（K）,633.9742588,,qb(KJ/Kg),1255.011682,,,给水焓hgs（KJ/Kg）,435.95,,,,,,,在0.72MPa进气处：,,,,排气冷却后参数：,,,,传热系数K（W/(m2℃),3000,,,逆流时的对数平均温差,71.93651879,,,逆流时的对数平均温差,25.67867077

△Tcs（K）,345.9742588,,燃料空气比f,0.022761391,,,高压过热蒸汽压力Pgy(MPa),8,,,,,,,查P-S图可知：,,,,压力,0.005,,,热损失系数,0.98,,,温差修正系数,0.97,,,温差修正系数,0.97

△Tc（K）,384.4158431,,f在0.02~0.03之间，0.0227614符合要求,,,,高压过热蒸汽温度tgy(℃),550,,,,,,,原高压蒸汽焓h2′（KJ/Kg）,2846.327,,,温度,30,,,传热量（KW）,36969.03939,,,修正温差,69.77842323,,,有效平均温差,24.90831064

T2＊（K）,672.4158431,,,,,,高压过热蒸汽焓hgy(KJ/Kg),3519.74,,,,,,,两股蒸汽汇合后总蒸汽焓h2（KJ/Kg）,2868.443672,,,比焓,125.6643,,,逆流时的对数平均温差,13.923616,,,热损失系数,0.95,,,需要传热面积,118.5473739

压气机压缩功ωc,395.9483184,,,,,,低压过热蒸汽压力Pdy（MPa）,0.72,,,,,,,查P-h图可知：,,,,补水参数：,,,,温差损失系数,0.97,,,换热量（KW),13646.15625,,,选取管子直径（m）,0.025

,,,,,,,低压过热蒸汽温度tdy（℃）,250,,,,,,,汇合后蒸汽温度t2(℃),211.2,,,压力,0.1013,,,有效平均温差,13.50590752,,,需要的传热面积（m2),1635.320697,,,管厚,0.0025

⑶在透平内,,,⑷整体性能,,,,低压过热蒸汽焓hdy（KJ/Kg）,2953.3,,,,,,,汇合后蒸汽熵S2（KJ/(Kg.K)),6.9236,,,温度,30,,,需要传热面积,912.4165197,,,翅化率,23.4,,,热水流速（m/s),1.5

πt,15.835347,,比功ωn（KJ/Kg),466.5935406,,,高压蒸汽流量Dgy(t/h),126,,,,,,,汇合后蒸汽流量D2(t/h),83.20202138,,,比焓,138.287,,,每根管长,4.63392412,,,,,,,流通截面积(m2),0.092592593

T4s﹡（K),837.4430027,,空气流量qm(Kg/s),165.2401786,,,低压蒸汽流量Ddy(t/h),34.51962303,,,,,,,在0.06MPa抽汽处：,,,,加热除氧器用汽量,17.31760165,,,取标准长,5,,,,,,,需要管子数,188.6280807

△Tts(K),785.5569973,,燃料流量qmf（Kg/s),3.761096383,,,总蒸汽流量D（t/h）,160.519623,,,,,,,查P-S图可知：,,,,补给水流量(t/h),42.68239835,,,校正传热面积,984.4965978,,,,,,,取整数,190

△Tt(K),722.7124375,,循环效率ηgt,0.364348537,,,锅炉额定容量Dc（t/h）,165,,,,,,,抽汽温度t3′(℃),86,,,汽机排气量（t/h),68.40202138,,,超出范围,0.078999094,,,,,,,管子长度,3.972084325

排气温度T4﹡（K),900.2875625,,烟气流量qmgs（Kg/s),176.2490282,,,,,,,,,,,抽汽焓h3′（KJ/Kg）,2434.9419,,,,,,,0.1到0.2之间,符合要求,,,,,,,取标准长度,4

透平膨胀功ωt（KJ/Kg),867.254925,,烟气焓hmgs（KJ/Kg),1075.0079,,,,,,,,,,,抽汽量D3（t/h),14.88851935,,,,,,,,,,,,,,,,

,,,,,,,,,,,,,,,排气压力Dpq(Mpa),0.005,,,,,,,,,,,,,,,,

,,,,,,,,,,,,,,,排气温度tpq（℃）,33,,,,,,,,,,,,,,,,

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