600MW火电厂原则性热力系统计算

123加热器编号H1H2H3抽汽压力5.8943.5931.612抽汽温度380.9316.9429.1上端差-1.700下端差5.55.5/抽汽焓3132.930163317.7抽汽管道压损0.030.030.03漏汽点代码ABKL1漏汽量62026774103027漏汽系数0.0004769230.0002053850.00570.002328462漏汽点比焓3394.43394.43536.63328.1项目名称BN1NT漏汽量26789101660漏汽系数0.0002053856.84615E-057.76923E-050.000507692漏汽比焓3394.43328.130162716.2总焓0.6971575380.2278468460.234321.378993846平均比焓项目名称符号单位数值项目名称主蒸汽压力P0Mp16.7锅炉连续排污量主蒸汽温度t0℃537全厂汽水损失prhMp3.234全厂工质渗漏trh℃537暖风器prh'Mp3.56过热器减温trh'℃315厂用电率0.0053化学补充水温度0.0044除氧器至给水泵高差给水泵出口压力20.13小汽轮机排汽压力1.927835332/0.000647671=2976.565953pc其他原始数据整理Mp再热蒸汽参数（热段）再热蒸汽参数（冷段）排汽压力回热抽汽参数门杆漏汽、轴封漏汽数据轴封加热器物质热平衡计算单位项目给水温度274.1小汽机排汽给水泵效率0.83汽轮机进汽节流损失锅炉连续蒸发量Dbt/h2027中压缸进汽节流损失额定过热蒸汽压力pbMp17.3新汽焓额定过热蒸汽温度tb℃541轴封加热器压力PT额定再热蒸汽压力3.734汽轮机机械效率额定再热蒸汽温度541发电机效率锅炉效率0.925排汽比焓汽包压力18.44再热器吸热项目名称符号单位数值化学补充水焓hmat/h83.7汽轮机总进汽量（预估）D0kg/h13000002018000给水量Dfwkg/h132626045678H4H5H6H7H80.74470.3050.130.06970.022323.6223.2137.888.561/2.82.82.82.85.55.55.55.55.53108.22912.92749.52649.52491.10.050.050.050.050.05N1M1LNM8956434371016396.84615E-050.0004338460.0026438467.76923E-050.0004915383328.13328.1301630163016R和项目名称p1901307漏汽量8960.0001461540.001005385漏汽系数0.0006892313108.2漏汽比焓3108.20.4542753852.992593615总焓2.142267077平均比焓符号单位数值Dblkg/h10000Dlkg/h30000kg/h30000kg/h35000550000.0720m21.66.272976.5659533.2652/0.001040139=其他原始数据整理项目汽侧水侧回热抽汽参数门杆漏汽、轴封漏汽数据轴封加热器物质热平衡计算均压箱平均蒸汽比焓计算2422.60.040.02h0kJ/kg3394.4KPA980.9850.99hc2333.8qrh520.61284181.818水侧RPTSJW1908966601412302456870.0001461540.0006892310.0005076920.0010861540.0232653850.0005284623108.23108.22716.22716.23016.152337.8MM1和63956420990.0004915380.0004338460.00161461530163328.11.482481.4438833855.068630462单位H1H2H3H4抽汽压力5.8943.5931.6120.7447抽汽比焓3132.930163317.73108.2抽汽管道压损0.030.030.030.05加热器侧压力5.717183.485211.563640.707465汽侧压力下饱和温度272.4242.35200.302165.409水侧压力20.1320.1320.130.7074加热器上端差-1.700/出水温度274.1242.35200.302165.409出水比焓1201.6541381050.732756861.7536376699.7914635进水温度242.35200.302165.409129.5733.2652/0.001040139=3139.218485回热加热系统汽水参数计算项目门杆漏汽、轴封漏汽数据均压箱平均蒸汽比焓计算进水比焓1050.732756861.7536376699.7914635545.5463624加热器下端差5.55.5/5.5疏水温度247.85205.802165.409135.073疏水比焓1076.247036886.0217056710.4659529568.3640444H5H6H7H8SG0.3050.130.06970.0222912.92749.52649.52491.12976.50.050.050.050.050.289750.12350.0662150.02090.098132.373105.62588.48761.0311.7241.7241.7241.7241.7242.82.82.82.8129.573102.82585.68758.23132.76545.5463624432.2032344360.1220642245.1963015138.7102.82585.68758.23132.7632.19432.2032344360.1220642245.1963015138.7136.35.55.55.55.55.5108.32591.18763.73138.26455.4107704383.2106572268.1857995161.7554195415设计工况420（一）汽水平衡计算1、全厂工质渗漏系数αLDL/DO0.023076923锅炉排污率αblDbl/DO0.007692308厂用汽系数αpl0.0078减温水系数αsp0.0287暖风器疏水系数αnf0.01893补水率αmaαpl+αbl+αl0.0385692312、给水系数1点物质平衡αb1.0230769232点物质平衡αfw1.0020692313、各小汽流量系数（二）汽轮机进汽参数（四）各加热器进出口参数计算（五）高加抽汽系数计算1、H1的抽汽系数α10.07353388H1的疏水系数αd,10.073533883、泵入口静压P,pu0.913788给水泵内介质平均压力Ppj10.521894给水泵平均比焓hpj699.3给水泵介质平均比容vpu0.001103给水泵介质焓升τpu25.5367251（六）除氧器抽汽系统计算4、除氧器出水系数αc,41.030769231除氧器抽汽系数α40.043208138（七）低加抽汽系数计算5、H5出水系数αc，50.766136307H5的抽汽系数α50.035335368H5疏水系数αd,50.0353353687、H7的抽汽系数α70.034192859H7的疏水系数αd,70.091787881(三）辅助计算（八）凝汽系数1、小汽机抽汽系数αxj0.0383933352、凝汽器的质量平衡αc0.565018592校核误差（九）汽轮机内功计算1、凝汽流做功ωc880.20030691KG抽汽做功2、抽汽流做功ωa,1各级抽汽量抽汽流总内功∑ωa,j307.78849413、附加功量∑ωsg,k4.2343766154、汽轮机内功ωi1192.223178（十）汽轮机比热耗q02616.832675汽轮机绝对内效率ηi0.455597788汽轮机绝对电效率ηe0.444276183汽轮机热耗率q8103.06773汽轮机汽耗率d3.096517331汽轮机的进汽量D01300537.279给水流量Gfw1340553.811凝结水泵流量Gcp996388.8278凝汽量Dc734827.7419第一级抽汽量D195633.5528（十一）全厂热经济指标1、锅炉参数计算q'rh527hb3399.22、锅炉有效热量q12695.5446453、管道效率ηp0.9707992334、全厂效率ηcp0.3989552545、全厂发电标准煤耗系数r1.01597826相当于一千克标准煤29768.16301发电标准煤耗bs0.3031281556、全厂热耗率qcp8881.6549487、全厂供电标准煤耗bns0.325944253（十二）反平衡校核1、锅炉输入热量qr2914.1023192、锅炉损失Δqb218.55767393、排污损失Δqbl12.896923084、全厂工质渗漏损失ΔqL76.400769235、厂用汽损失23.59116、凝汽流冷源损失1241.6283557、小汽机冷源损失87.778681868、化学补水冷源损失-2.0287415389、低加H8疏水冷源损失3.12137671210.轴封加疏水冷源损失0.28020069211.w汽流冷源损失1.16340807712、暖风器损失45.83331613、管道散热损失32.9334091714、轴封汽散热损失1.058123692损失之和1719.623496汽轮机内功1194.478823正反平衡相对误差0.0018883932、H2的抽汽系数α2H2的疏水系数αd,2再热器流量系数αrh给水泵出口比焓hpuH3的抽汽系数α3H3的疏水系数αd,36、H6的抽汽系数α6H6的疏水系数αd,68、轴封加热器出水焓hw,sg139.6614893疏水温度td,838.26H8的抽汽系数α80.030833422H8de疏水系数αd,80.1226213033、H4抽汽口抽汽系数和α'40.108331473各种加热器抽汽系数和∑αj0.422775254轴封漏汽系数和∑αsg,k0.012206154凝汽系数αc0.5650185920H1H2H3H4H5261.5378.4597.3806.81002.195633.5528107086.08146752.6501656193.794345954.96295校核误差0.0004131210.0823398780.1558737590.814611626724.83672510.035948720.1975224780.0222596550.057595022出水温度tw,sg32.76H8疏水焓hd,8161.9H6H7H81165.51265.51423.928949.5109144469.087540100.01454