汽轮机课程设计计算

参数符号单位数值参数额定功率prMW25额定转速设计功率peMW20新蒸汽压力新蒸汽温度t0℃435排汽压力给水温度tfw℃160冷却水温度给水泵给压头pfpMPa6.3凝结水泵压头射汽抽汽器用汽量∆Dejkg/h500射汽抽汽器中凝结水温升∆tej℃3轴封漏气量∆D1kg/h1000第二高加中回收的轴封漏气量∆D'1kg/h700进汽机构节流损失∆P0MPa0.14排汽管中压力损失∆PcMPa0.00028调节级前的压力P0'MPa3.36末级动叶后压力PzMPa0.00728汽轮机相对内效率ηri0.84发电机效率ηg（全负荷）0.97机械效率ηax0.9870点h0kj/kg3303.612187v0m3/kg0.08977584s0kj/(kg·k)6.9592512371点s1kj/(kg·k)6.977373391v1m3/kg0.0935346t1℃434.10409113’点h3'kj/kg2166.8384t3'℃39.0009v3'm3/kg17.0745整机理想焓降∆htmackj/kg1136.773787整机有效焓降∆himackj/kg954.8899812h3''kj/kg2348.722206余速损失∆hc2kj/kg22.735475743点h3kj/kg2325.98673t3℃39.5264v3m3/kg17.6923s3kj/(kg·k)7.3805整机进汽量估计D0t/h98.44650119原始数据一、进汽量D0初步估算1确定主汽门、配汽机构及排汽管中的压力损失2选取机组的相对内效率、发电效率和机械效率3热力过程曲线初步拟定4整机进汽量估计tfw℃160Zfw5hfwkj/kg677.2613hckj/kg163.31每级中给水焓升∆hfwkj/kg102.79026高压加热器端差δt℃5低压加热器端差δt℃3除氧器端差℃0除氧器抽汽管道压损∆Pe=17%Pe0.17高低加抽气管道压损∆Pe=8%Pe0.08加热器号抽汽压力Pe抽汽比焓he抽汽管压损∆Pe/Pe加热器工作压力P'H10.76176127630050.080.700820374H20.31291796428100.080.287884527HD0.14216867526950.170.118H30.08987074626330.080.082681086H40.03617511325500.080.033281104H1Dfwt/h98.64650119加热器效率ηh0.98∆Delt/h6.134699101H2∆D'e2t/h4.519632222∆D'e1t/h0.386069464∆D''lt/h0.790351306∆De2t/h3.343211452HD∆Dcwt/h86.94532517∆Dgt/h1.523265463H3∆De3t/h3.803410006H4tw4℃42.0009hw4kj/kg175.9031003∆D'e4t/h4.406732345D'e3t/h0.162368699∆De4t/h4.244363646H1H2抽汽压力PeMPa0.7617612760.312917964加热器压力Pe'MPa0.7008203740.2878845276确定各级加热器的汽水参数8回热系统热平衡估算9计算结果表加热器号项目符号单位二、回热系统平衡初步估算1确定给水温度2确定抽汽级数3给水比焓升的分配4确定加热器端差5确定抽气管道压损抽汽比焓hekj/kg30052810压力pe’下饱和温度te℃165132.125压力pe’下饱和水比焓he'kj/kg697.3494977555.4670148每公斤蒸汽放热量∆hekj/kg2307.6505022254.532985被加热的给水量Dfwkg/h98.6465011998.64650119给水进口温度tw1℃127.125104.25给水进口比焓hw1kj/kg538.2727399437.0439421加热器端差δt℃55给水出口温度tw2℃160127.125给水出口比焓hw2kj/kg678.9123619538.2727399给水比焓升∆hfwkj/kg140.6396219101.2287978抽气量∆Dekg/h6134.6991013343.211452调节级型式双列复速级调节级理想焓降∆ht250平均直径dm1150反动度Ωb0.11Ωg0.02Ωb'0.03Ωm0.16喷嘴理想比焓降∆hn210喷嘴速度系数φ0.97喷嘴损失∆hnξ12.411h13106.023187p11.4v10.19εn0.416666667k1.3εcr0.545选α1º15喷嘴出口气流速度c1t648.0740698c1628.6318477喷嘴流量系数μn0.97G27.34625033喷嘴出口面积An82.65231202最小截面积（An）mincm270.41080136sin（α1+δ1）0.268963785δ1º0.6026153336喷嘴最小截面积及斜切部分偏转角7喷嘴出口高度和部分进气度5喷嘴出口面积4喷嘴出口气流速度2喷嘴理想比焓降3计算喷嘴出口气流状态并选择喷嘴型线1选取调节级的型式及相关参数三、调节级详细计算喷嘴出口高度lnem0.007530006取lnmm20e0.376500318um/s180.6415776β1º21.70240471w1m/s457.2355746∆hw1kj/kg104.53218539第一列动叶出口汽流相对速度动叶理想焓降∆hbkj/kg27.5动叶理想比焓降动叶滞止理想焓降∆h*bkj/kg132.0321853滞止理想焓降动叶出口气流相对速度w2tm/s513.8719399动叶出口理想相对速度Ψ0.922查得w2m/s473.7899286动叶出口实际相对速度∆hbξ19.79373709查hsp21.22查hsv20.21Ab121.2079916动叶出口截面积动叶进口高度查得动叶出口高度顶部盖度∆tmm1.5根部盖度∆rmm0.5∆mm2lbimm22对于短叶片lbmm22即β2º23.89349345α2º37.23037072c2m/s317.1835917∆hg5∆hg*55.30271541理想速度c1t’332.5739479查得Ψg0.908实际速度c1'301.9771447∆hgξkj/kg9.707617453查hsp1'MPa1.2v1'm3/kg0.22轮轴功率导叶出口截面积Agcm2199.2261725导叶进口高度lgi2430部分进汽损失与叶轮摩擦损失16导叶内损失29轮周有效比焓降17计算导叶出口截面积及进口高度15导叶出口速度28计算叶高损失26轮周有效焓降(不计叶高损失)14导叶的理想比焓降27轮周效率的计算及校核13第一列动叶抽口汽流速度和出汽角25余速损失为23第二列动叶出口汽流角24第二列动叶出口汽流绝对速度方向与大小11第一列动叶出口面积22计算第二列动叶相关参数12第一列动叶出口高度和汽流出口角10第一列动叶损失21第二列动叶损失为20计算第二列动叶出口汽流相对速度8第一列动叶进口气流角和相对速度α'1º34.96821428β1'68.88915973w1'185.5208763∆hi153.41875内功率Pi4195.427543ηi0.613675喷嘴：TC-2B第一列动叶：bnmm49.6tn平均mm0.72Bnmm30.2tnmm35.712Zn38.08894012取整Zn38反算tn35.79558499取整tn平均0.721685181反算查得安装角βxº38查得安装角导叶：TP-3Aα2º37.23037072第二列动叶：bnmm32.5tn平均mm0.6Bnmm32.1tnmm19.5Zn69.75549896取整Zn70取整反算tnmm19.431889反算tn平均mm0.597904277查得安装角βxº78查得安装角Dm1mm1040Dmzmm1720Dm1:Dmz0.604651163级数1234直径1040106010901160速度比0.4780.4820.4860.491级数78910直径1310137014401520速度比0.5020.5080.5170.5282凝汽式汽轮机末级平均直径的估取3凝汽式汽轮机级数及焓降的确定四、压力级焓降分配和级数确定1第一非调节级平均直径的估计33调节级叶栅几何参数选择31级的有效比焓降32级效率18导叶出汽角19第二列动叶进口相对速度w1'(∆ht)1kj/kg58.40104843h1(∆ht)2kj/kg59.66606714h2(∆ht)3kj/kg62.05691983h3(∆ht)4kj/kg68.85932364h4(∆ht)5kj/kg72.50398091h5(∆ht)6kj/kg77.7268556h6(∆ht)7kj/kg84.0126948h7(∆ht)8kj/kg89.72706625h8(∆ht)9kj/kg95.70919345h9(∆ht)10kj/kg102.2419418h10(∆ht)11kj/kg104.9502204h11(∆ht)12kj/kg107.7508446h12Σ(∆ht)kj/kg983.6061569∆ht平均kj/kg81.96717974由hs得h2'3101s2'7.134Pc'0.00728查得h2219.1833∆htp881.8167初估重热系数α0.06Z11.40365821取整得Z12取k0.16ηrit'0.8178α0.056239842比焓降分配∆H-48.8804549∆H/12kj/kg-4.07337124级号1234平均直径1040106010901160速度比0.4780.4820.4860.491试算比焓降58.4010484359.6660671462.0569198368.85932364最后确定的比焓降54.327677255.592695957.9835485964.7859524级号78910平均直径1310137014401520速度比0.5020.5080.5170.528试算比焓降84.012694889.7270662595.70919345102.2419418最后确定的比焓降79.9393235685.6536950291.6358222198.16857059确定非调节级各级理想比焓降各点焓值级数的确定重热系数的校核需改变数值符号单位数值序号ner/min3000标题p0MPa3.5符号pcMPa0.007待处理问题tw1℃27固定(经验）数值pcpMPa1.2重要数据查表数值主汽门和调节阀中节流损失0.04m1.2∆D/D00.04原始数据一、进汽量D0初步估算除氧器压力0.118除氧器饱和水温度104.25饱和水温度te'饱和水比焓he'出口端差δt给水出口温度t'w给水出口比焓h'w165697.34949775160678.9123619132.125555.46701485127.125538.2727399104.25437.04379150104.25437.043942194.375395.3856661391.375383.622255471.5299.3027336368.5287.6958391HDH3H40.1421686750.0898707460.0361751130.1180.0826810860.0332811049计算结果表加热器号二、回热系统平衡初步估算269526332550104.2594.37571.5437.0437915395.3856661299.30273362257.9562092237.6143342250.69726698.6465011986.9453251786.9453251791.37568.542.0009383.6222554287.6958391175.9031003