= D0-∑
HDsg- Ddr2
==
D0?0.02D0?0.1545D0?2.294319
0.8255D0?2.294319
（3）由高压加热器H3热平衡计算D3
pupuhw.2?25.39?736.59kJ/kg 4?hw4??hw?711dddpu?D3(h3?hw3)?Ddr2(hw2?hw3)?n?Dfw(hw3?hw4)puddDfw(hw3?hw4)/?h?Ddr2(hw2?hw3)dh3?hw3??
D3?
(1.0101D0?15)(858.7?736.59)/0.99?(0.1545D0?2.294319)(876.1?743)3315?743 =
=
0.040445D0?0.600613
h3的疏水量Ddr3?Ddr2?D3?0.194945?2.894932
（4）由除氧器H4热平衡计算D4
'd[D4(h4?hw5)?Df(h\?h?Dfw(hw4?hw5)f?hw5)?Ddr3(hw3?hw5)]dDfw(hw4?hw5)/?h?Df(hf\?hw5)?Ddr3(hw3?hw5)
?D4'? =
h4?hw5
(1.0101D0?15)(711.2?559.8)/0.99?6?(2788.7?559.8)?(0.194945D0?2.894932)(743?559.8)3125.2?559.80.046293D0?4.525537 =
除氧器进水量
Dc4?Dfw?Ddr3?D4'?Df
==
1.0101D0?15?0.194945D0?2.894932?0.046293D0?4.525537?6 0.768862D0?10.630605
?D4?D4'?D1t?0.098293D0?4.525537
（5）由低压加热器
H5热平衡计算D5
d[D5(h5?hw?h?Dc4(hw5?hw6) 5)]?D5? =
Dc4(hw5?hw6)/?h(0.768862D0?10.630650)(559.8?434.6)/0.99?dh5?hw2930.6?456.85
0.039305D0?0.543454
?Ddr5?D5?0.039305?0.543454
H6热平衡计算D6
（6）由低压加热器
ddd[D6(h6?hw?h?Dc4(hw6?hw7) 6)?Ddr5(hw5?hw6)]ddDc4(hw6?hw7)/?h?Ddr5(hw5?hw6)?D6?dh6?hw6
=
(0.768862D0?10.630605)(434.6?351.4)/0.99?(0.039305D0?0.543454)(456.8?373.2)2754.5?373.2 =
0.025755D0?0.356094
Ddr6?D5?D6?0.06506D0?0.899548
（7）由低压加热器
H7热平衡计算D7
ddd[D7(h7?hw)?D(h?h?h?Dc4(hw7?hw8) 7dr6w6w7)]ddDc4(hw7?hw8)/?h?Ddr6(hw7?hw8)?D7?dh7?hw7
(0.768862D0?10.630605)(351.4?253.8)/0.99?(0.06506D0?0.899548)(373.2?275.5)2612.4?275.5=
=
0.029716D0?0.410861
Ddr7?Ddr6?D7?0.094776D0?1.310409
（8）由低压加热器
H8,轴封加热器SG和凝汽器热井构成一体的热平衡计算D8
dpuDc4(hw8?hc')=[D8(h8?hc')?Ddr7(hw7?hc')?Dsg(hsg?hc')?Dc4?hcw]?h
pudDc4(hw8?hc')/?h?Dc4?hcw?Ddr7(hw7?hc')?Dsg(hsg?hc')?D8? =
h8?hc'
0.007081D0?0.452804
Ddr8?Ddr7?D8?0.101857D0?1.763213
（9）由凝汽器热井物质热平衡计算Dc Dc=Dc4-
Ddr8- Dsg-Dma-D1t
=0.768862D0+10.630605-0.101857D0-1.763213-0.02D0-0.010101-9-0.0520D0 =0.584904 D0-0.132608 由汽轮机物质平衡校核：
D?D0??Dj?Dsg*c18
=
D0?0.395095D0?0.132608?0.02D0
=0.584905D0-0.132608 ?误差很小，符合工程要求； 计算结果汇总于表中： D(t/h) D0 Drh=0.8255D0—2.294319 D1=0.071596D0+1.063199 D2=0.082904D0+1.231120 D3=0.040445D0+0.600613 D4=0.098293D0-4.525537 D5=0.039305D0+0.543454 D6=0.025755D0+0.356094 D7=0.029716D0+0.410861 D8=0.007081D0+0.452804 h(kJ/kg) h0=3401.0 qrh=542.4 h1=3114.4 h2=3006.9 h3=3315 h4=3125.2 h5=2930.6 h6=2754.5 h7=2612.4 h8=2480.8 Dc hc=2310.8 Dsg=0.02D0 4.汽轮机汽耗计算及功率校核 （1）计算汽轮机内功率
hsg=3145.3
=[3401D0+(0.8255D0—2.294319)x542.4—(1194.849083D0—368.937787)— (0.584904D0—0.132608)x2310.8—0.02D0x3145.3]x103 =(1239.399954D0—569.0702726)x103 (kJ/h) (2)由功率方程式求D0 由
=654000/0.99/0.988x3600=2407066618 (kJ/h) =(1239.399954D0—569.0702726)x103 (kJ/h) 得：D0=1942.582 (t/h) （3）求各级抽汽量及功率校核
将D0数据代入各处汽水相对值和各抽汽及排汽内功率，如下表：
项目 数量（t/h） 项目 化学补充水量Dma=0.010101D0+9 数量（t/h） 汽轮机D0 1942.582 28.622021 锅炉蒸发量Db=1.0101D0 给水量Dfw=1.0101D0+15 全厂汽水损失Dl=0.01Db 项目 1962.202078 再热蒸汽量Drh 1977.202078 Drh=0.8255D0—2.294319 19.622021 1601.307122 抽汽量（t/h） 内功率Wj(kJ/h) 40165.3564x103 63954.1295x103 项目 一级抽汽D6 一级抽汽D7 抽汽量（t/h） 内功率Wj(kJ/h) 50.387293 58,136628 59905.4527x103 77379.8519x103 一级抽汽D1 140.1443 一级抽汽D2 162.278938 一级抽汽D3 79.168342 一级抽汽D4 186.416676 一级抽汽D5 76.896640 功率校核 49749.3861x103 一级抽汽D8 14.208227 20780.9528x103 152526.1243x103 汽轮机排汽77880.9170x103 Dc 1136.091374 1854782.777x103
5.热经济指标计算
（1）机组热耗Q0 、热耗率q ,绝对电效率
=(1942.582x3401+1601.307122x542.4+6x2788.7+28.622021x83.9609— 1977.202078x1197.7)x103 =5126310767 (kJ/h)
(2)锅炉热负荷Qb和管道效率
=5126310767/654000=7838.40 [kJ/(kw·h)]
根据锅炉蒸汽参数查得过热器出口焓hb=3401 (kJ/kg)
=(1962.202078x3401+1601.307122x542.4 —1977.202078x1197.7)x103 =5173903321 (kJ/h)
=Q0/Qb=5126310767/5173903321=0.9908
(3)全厂热经济指标 全厂热效率全厂热耗率：
= 8591.270 [kJ/(kw·h)]
发电标准煤耗率：
=0.9208x0.9908x0.4593=0.41903