燃氣輪機部分計算,,,,,,,余熱鍋爐部分計算,,,,,,,,汽輪機部分,,,,除氧器部分,,,,冷凝器部分,,,,煙筒部分,,,,二號加熱器,

,,,,,,,,,,,,,,,汽機高壓進氣量D0ˊ(t/h),126,,,,,,,,,,,,,,,,

已知及選取值：,,,,,,,,,,,,t/h,,,汽機低壓進氣量D0〞(t/h),17.20202138,,,,,,,,,,,,,,,,

燃氣輪機軸功率Pgt（KW）,77100,,燃料熱值Hu（KJ/Kg),56263,,,輸入煙氣焓Qr(KJ/Kg）,1075.0079,,總煙氣利用能（KJ/s）,151509.4563,,,,汽機高壓蒸汽進氣壓力P0′(MPa),8,,,出水量,160.519623,,,排氣冷凝后溫度,30,,,煙筒中煙氣進氣溫度,130,,,進汽溫度,86

大氣溫度Ta（K）,288,,進氣道壓損率εc,0.01,,,排煙溫度tpy（℃）,130,,鍋爐高壓蒸汽最高流量（Kg/s）,43.04563868,154.9642993,,,汽機高壓蒸汽進氣溫度t0′(℃),550,,,出水壓力,0.12,,,排氣冷凝后焓值,125.6643,,,煙氣進氣焓,210,,,進汽壓力,0.06

大氣壓力Pa（Mpa）,0.1013,,燃燒室壓損率εb,0.03,,,排煙焓hpy（KJ/Kg）,210,,鍋爐低壓蒸汽最高流量（Kg/s）,51.30174933,184.6862976,,,汽機高壓蒸汽進氣焓h0′（KJ/Kg）,3519.74,,,出水溫度,104,,,冷卻水進入溫度,15,,,煙氣進氣流量(t/h),634.5,,,進汽焓,2434.9419

壓氣機內效率ηc,0.9,,排氣道壓損率εt,0.03,,,排煙損失q2,0.195347402,,取高壓蒸汽流量（Kg/s）,35,126,,,汽機低壓蒸汽進氣壓力P0″(MPa),0.72,,,出水焓,435.95,,,冷卻水進入焓,63.5142,,,煙氣排氣溫度,80,,,熱水進入溫度,44.64

透平內效率ηt,0.92,,煙氣泄露系數μc1,0.05,,,散熱損失q5,0.005,,低壓蒸汽流量（Kg/s）,9.588784174,34.51962303,,,汽機低壓蒸汽進氣溫度t0″(℃),250,,,除氧器加熱給水參數：,,,,冷卻水排出溫度,20,,,煙氣排氣焓,128.5,,,熱水進口焓,187.3783

燃燒室內效率ηb,0.98,,壓縮比π,17,,,灰渣損失q6,0,,,,,,,汽機低壓蒸汽進氣焓h0″（KJ/Kg）,2953.3,,,壓力,0.72,,,冷卻水排出焓,83.9548,,,煙氣排氣流量（t/h）,634.5,,,熱水出口溫度,60

整體效率ηm,0.99,,燃燒溫度T3﹡(K）,1623,,,化學未完全燃燒損失q3,0,,,,,,,高壓進氣處熵值S0′（KJ/(Kg.K)),6.8775,,,溫度,250,,,冷卻水量(t/h),6643.867328,,,換熱器換熱量(KW),14364.375,,,熱水出口焓,251.1591

Cpa[KJ/(Kg*K)],1.03,,ka,1.386,,,機械未完全燃燒損失q4,0,,,,,,,在1MPa進汽處：,,,,比焓,2953.3,,,冷卻水密度,1000,,,熱水進入溫度,20,,,熱水流量（t/h）,500

Cpg[KJ/(Kg*K)],1.2,,Kg,1.315,,,鍋爐總損失∑q,0.200347402,,,,,,,查P-S圖可知：,,,,0.06MPa抽汽加熱后參數：,,,,冷卻水流速（m/s),1.5,,,熱水進口焓,83.9548,,,換熱量(KW),8858.444444

燃料碳氫比x,3.72,,過量空氣系數α,1.1,,,鍋爐熱效率ηgl,0.799652598,,,,,,,抽汽溫度t1′(℃),238.93,,,壓力,0.06,,,所需流通截面,1.230345801,,,熱水流量（t/h）,500,,,蒸汽冷凝后出口溫度,70

計算部分：,,,,,,,鍋爐有效利用熱Q1（KJ/Kg）,859.6328605,,,,,,,抽汽焓h1′（KJ/Kg）,2918.1464,,,溫度,70,,,管徑（m),0.025,,,熱水出口焓,187.3783,,,蒸汽冷凝后出口焓,292.9962

⑴在壓縮機內,,,⑵在燃燒室中,,,,給水溫度tgs(℃),104,,,,,,,抽汽量D1（t/h),60,,,比焓,292.9962,,,管數,2506.442002,,,出口熱水溫度,44.64,,,蒸汽抽汽量(t/h）,14.88851935

T1＊（K）,288,,T3＊（K),1623,,,給水壓力Pgs（Mpa）,0.12,,,,,,,抽汽后蒸汽流量D1′,66,,,流量,14.8,,,取管數,2507,,,查得換熱器換熱系數,116,,,換熱器換熱系數,3000

T2s＊（K）,633.9742588,,qb(KJ/Kg),1255.011682,,,給水焓hgs（KJ/Kg）,435.95,,,,,,,在0.72MPa進氣處：,,,,排氣冷卻后參數：,,,,傳熱系數K（W/(m2℃),3000,,,逆流時的對數平均溫差,71.93651879,,,逆流時的對數平均溫差,25.67867077

△Tcs（K）,345.9742588,,燃料空氣比f,0.022761391,,,高壓過熱蒸汽壓力Pgy(MPa),8,,,,,,,查P-S圖可知：,,,,壓力,0.005,,,熱損失系數,0.98,,,溫差修正系數,0.97,,,溫差修正系數,0.97

△Tc（K）,384.4158431,,f在0.02~0.03之間，0.0227614符合要求,,,,高壓過熱蒸汽溫度tgy(℃),550,,,,,,,原高壓蒸汽焓h2′（KJ/Kg）,2846.327,,,溫度,30,,,傳熱量（KW）,36969.03939,,,修正溫差,69.77842323,,,有效平均溫差,24.90831064

T2＊（K）,672.4158431,,,,,,高壓過熱蒸汽焓hgy(KJ/Kg),3519.74,,,,,,,兩股蒸汽匯合后總蒸汽焓h2（KJ/Kg）,2868.443672,,,比焓,125.6643,,,逆流時的對數平均溫差,13.923616,,,熱損失系數,0.95,,,需要傳熱面積,118.5473739

壓氣機壓縮功ωc,395.9483184,,,,,,低壓過熱蒸汽壓力Pdy（MPa）,0.72,,,,,,,查P-h圖可知：,,,,補水參數：,,,,溫差損失系數,0.97,,,換熱量（KW),13646.15625,,,選取管子直徑（m）,0.025

,,,,,,,低壓過熱蒸汽溫度tdy（℃）,250,,,,,,,匯合后蒸汽溫度t2(℃),211.2,,,壓力,0.1013,,,有效平均溫差,13.50590752,,,需要的傳熱面積（m2),1635.320697,,,管厚,0.0025

⑶在透平內,,,⑷整體性能,,,,低壓過熱蒸汽焓hdy（KJ/Kg）,2953.3,,,,,,,匯合后蒸汽熵S2（KJ/(Kg.K)),6.9236,,,溫度,30,,,需要傳熱面積,912.4165197,,,翅化率,23.4,,,熱水流速（m/s),1.5

πt,15.835347,,比功ωn（KJ/Kg),466.5935406,,,高壓蒸汽流量Dgy(t/h),126,,,,,,,匯合后蒸汽流量D2(t/h),83.20202138,,,比焓,138.287,,,每根管長,4.63392412,,,,,,,流通截面積(m2),0.092592593

T4s﹡（K),837.4430027,,空氣流量qm(Kg/s),165.2401786,,,低壓蒸汽流量Ddy(t/h),34.51962303,,,,,,,在0.06MPa抽汽處：,,,,加熱除氧器用汽量,17.31760165,,,取標準長,5,,,,,,,需要管子數,188.6280807

△Tts(K),785.5569973,,燃料流量qmf（Kg/s),3.761096383,,,總蒸汽流量D（t/h）,160.519623,,,,,,,查P-S圖可知：,,,,補給水流量(t/h),42.68239835,,,校正傳熱面積,984.4965978,,,,,,,取整數,190

△Tt(K),722.7124375,,循環效率ηgt,0.364348537,,,鍋爐額定容量Dc（t/h）,165,,,,,,,抽汽溫度t3′(℃),86,,,汽機排氣量（t/h),68.40202138,,,超出范圍,0.078999094,,,,,,,管子長度,3.972084325

排氣溫度T4﹡（K),900.2875625,,煙氣流量qmgs（Kg/s),176.2490282,,,,,,,,,,,抽汽焓h3′（KJ/Kg）,2434.9419,,,,,,,0.1到0.2之間,符合要求,,,,,,,取標準長度,4

透平膨脹功ωt（KJ/Kg),867.254925,,煙氣焓hmgs（KJ/Kg),1075.0079,,,,,,,,,,,抽汽量D3（t/h),14.88851935,,,,,,,,,,,,,,,,

,,,,,,,,,,,,,,,排氣壓力Dpq(Mpa),0.005,,,,,,,,,,,,,,,,

,,,,,,,,,,,,,,,排氣溫度tpq（℃）,33,,,,,,,,,,,,,,,,

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