600MW热力发电厂课程设计

一、课程设计目的通过设计加深巩固热力发电厂所学理论知识，了解热力发电厂计算的一般步骤，掌握热力系统的能量平衡式、质量平衡式和热经济性指标的计算，并考虑不同辅助成分引入回热系统对机组热经济性影响，一期达到通过课程设计进一步了解发电厂系统和设备的目的。具体要求是按给定的设计条件及有关参数，求出给出的热力系统额定工况时各部分的汽水流量和各项热经济性指标。二、设计目的及已知条件1、600MW机组的原则性热力系统计算2、原则性热力系统图3、汽机形式和参数机组形式：国产N125—135/550/550型超高压中间再热凝汽式汽轮机额定参数：600000千瓦，处参数：0135P绝对大气压，00550tC再热参数：热段压力23.4绝对大气压，温度：0550C排气参数：00.05P绝对大气压0.942nX4、回热系统参数该机组有7组不调节抽气，额定工况时，其抽气参数如表1，给水泵的压力为170绝对大气压，凝结水泵的出口压力为12绝对大气压。表1N125—135/550/550型机组回热抽气参数项目单位回热抽气级数ⅠⅡⅢⅣⅤⅥⅦ抽汽压力ata37.12267.854.672.50.7270.16抽汽温度℃375.14331394326255135X=0.975加热器端差℃0101333疏水出口端差℃885、门杆漏气和轴封系统漏气表2门杆漏气量和轴封系统漏气量地点1234567891011121314(17)15(16)符号1m2m3m4m5l6l7l8l9l10l11l12l13l14l15l数值41025433565178282274909711106、锅炉型式和参数锅炉形式：国产SG400/140型汽包式自然循环锅炉额定蒸发量：400吨/时过热蒸汽参数：141grP绝对大气压,0555Cgrt,156bP绝对大气压给水温度：0240Cgst锅炉效率：0.911gl7、其他已知及数据汽机进汽节流损失00.05P中间联合汽门节流损失0.05sP均压缸压力1.5绝对大气压轴封加热器压力0.97绝对大气压锅炉排污量：0.01PWglDD全厂汽水损失：0.015lglDD化学补充水压力为6绝对大气压温度为20℃该热发电机组的电机效率mg0.980.985排污水冷却器效率b0.98排污水冷却器端差8℃除氧器水箱水位标示20m三、计算过程1、汽态曲线（N125-135/550/550型机组的蒸汽膨胀过程曲线）2、根据已知数据计算或查出有关的汽水参数如表3项目单位抽汽级数12345678抽汽压力jpMPa3.7492.6260.7920.4730.2540.0740.0160.005抽汽温度jt0C375.15331394.2326255135X=0.975X=94.2抽汽比焓jh/kJkg3163.623081.263261.373117.822983.122749.532541.142421.043、锅炉排污利用系统计算表4有关热汽量及排污利用系统的比焓值计算项目单位计算公式及数据来源数值绝对量相对量进入汽轮机做功的蒸汽D0kg/hD01抽管压损系数p%7.97.87.97.97.87.67.88加热器压力'jpMPa3.4532.4210.730.4350.2330.06750.015加热器饱和温度sgt0C241.3221.1166.6146.51258953加热器饱和水比焓jh/kJkg1045.84954.03704.73618526.61372.67225.93加热器端差θ0C0101333加热器出口水温wjt0C241.3221.1166.6145.51228650加热器出口水比焓wjh/kJkg1043.22946.87710.28612.4511.11359214.69疏水冷却器进口端差θ0C88疏水冷却器疏水温度cjt0C229.1193.9疏水冷却器疏水比焓hcj/kJkg987.23826.81汽轮机总进汽量D'0kg/h0912lmmDDDD1.0311D01.0311锅炉蒸发量Dglkg/h0lDD1.0468D01.0468锅炉连续排污量Dpwkg/h0.01glD0.01047D00.01047锅炉给水量Dfwkg/hglpwDD1.05727D01.05727锅炉排污水比焓h'pw/kJkg由汽包压力查水蒸气表1208.07排污扩容器的扩容蒸汽比焓h''f/kJkg取s=0.98，由扩容器压力取0.663MPa及s查表4718.31排污水比焓h'f/kJkg0.663PWPMpa678.1扩容蒸汽系数αf()pwpwfffpwffhhhh0.002561扩容排污水系数α'pwpwf0.007909补充水量DmaLPWDD0.026172D00.026172补充水比焓Dmahw/kJkgP=0.606MPa,t=20℃84.42排污冷却器出口补充水比焓cwmah/kJkg()()cpwfwcmawwhhhmahma锅炉连续排污利用系统4、各级抽汽量计算给水泵中的比焓升ph，除氧器水箱标示20m，则给水泵进口压力为363109.820/100.792fppghp＝0.958MPa除氧器压力下的饱和温度0174.5pftC，查表732.723/fphKJKg，2.134/fpfpSSKJKg，给水泵出口压力17.029fpPMPa，749.94/fphKJkg，故749.94732.723()/21.52/0.8pfpfpgphhhhKJKg高压加热器和除氧器计算系统＃1加热器平均为1112()()znf1211()1.05727(1043.22946.67)0.04786()(3163.62987.23)0.98f＃2加热器平均为22211223()()()zzznf，2(3081.26826.81)0.04786(987.23826.61)0.981.05727(946.67710.28)20.1047486120.1047460.047860.1526086＃3除氧器物质平衡为87123123()()llmmcffw433[(7851)254]100.1521470.0025611.05727c330.897162c热平衡为872102333412123()llmmrncwfffwhhhhhhhhnh化学补充化学补充30.02784，30.84945C＃4加热器热平衡444345()()ncwwhhhh4(3117.82618)0.980.84945(612.21511.11)40.033955＃5加热器热平衡55545356()4()()ncwwhhhhhh56(2983.11526.61)0.03509(618526.610.980.84945(511.11)wzh560.1751930.00034674wzh混合点m的物质平衡为3456766()cccc5．汽机各级段通流量计算（1）调节级第1-6级通流量：161（2）第7-8级通流量：1781691010.0080.04786LL0.95294（3）再热蒸汽通流量：82780.952940.00780.10474860.84039rhL（4）中压缸第9-14级通流量：341011914rhmmLL0.847390.00030.00030.02740.0090.86628（5）中压缸第15-16级通流量：31115169140.866280.027850.0090.83754L（6）中压缸第17-18级通流量：4171815160.83750.035060.80248（7）低压缸第19-21级通流量:512192117180.802480.065840.00090.73574（8）低压缸第22-23级通流量：6222319210.735740.020850.71526（9）低压缸第24级通流量：24722230.715160.021540.69362（10）排入凝汽器流量:'2415160.693620.0010.0010.69162n甲凝汽器物质平衡验算:670.751970.0261720.021540.00410.69016nmasg误差：'0.691620.690016100%100%0.23%0.690016nnnn允许。6.汽机汽耗量与各项汽水流量计算表6做功不足系数计算jY的计算式jYjjjY11/ccrhiYhhqh0.810980.047860.03881422/ccrhiYhhqh0.756880.10474860.07928233/cciYhhh0.551560.027840.01535544/cciYhhh0.457290.035060.01663355/cciYhhh0.368860.0658240.0242966/cciYhhh0.215580.020580.0044477/cciYhhh0.078850.021540.00168971jjjY0.17991223574.323081.19rhrhqhh493.13/kjkg03451.632421.04493.13cicrhhhhq1523.72/kjkg汽轮机组汽耗量：07136001ecimgjjjpDhY33600125101523.720.980.98510.179912373043/kgh表7各项汽水流量项目符号xxD0g/xDkh汽机总进汽量'01.0311384645再热蒸汽量rh0.84039313502排汽量0.69106257795一级抽汽10.0478617854二级抽汽20.104748639076三级抽汽30.027410385四级抽汽40.0350613078五级抽汽50.0658424561六级抽汽60.020587677七级抽汽70.021547662锅炉给水fw1.05727394407锅炉蒸发量b1.0468390501化学补水ma0.0261729763锅炉连续排污pw0.010413883连续扩容蒸汽f0.0025619554排污后排污水'pw0.0079092950入除氧器轴封汽1sg0.0026969入#6加热器轴封汽2sg0.00572126入轴封加热器sg0.004115297.功率计算表8功率核算符号计算公式数值1p101/3600mgDhh1378.862p202/3600mgDhh3881.43p303/3600rhmgDhhq1902.954p404/3600rhmgDhhq2899.855p505/3600rhmgDhhq6333.196p606/3600rhmgDhhq2460.47p707/3600rhmgDhhq