热力系统计算模板

计算原始资料:汽轮机型式及参数机组型式：亚临界、一次中间再热、四缸四排汽、单轴、凝汽式汽轮机；额定功率：p600MWe=主蒸汽参数(主汽阀前)：p°=16.7MPa,t°=537°C；再热蒸汽参数(进汽阀前)：热段：p=3.23MPa,t=537Crhrh冷段：p"=3.56MPa,t"=315Crhrh(5)汽轮机排汽压力p=4.4/5.39MPa,排汽比焓：h=2333.8KJ/Kg。cc回热加热系统参数：项目单位H1H2H3H4H5项目单位H1H2H3H4H5H6H7H8抽汽压力p/j抽汽比焓h抽汽管道压Mpa5.893.591.60.740.3050.130.070.022KJ/Kg31333016331731082913275026502491损6pj水侧压力pw加热器上端%33333333Mpa20.120.1200.711.7241.7241.721.724差6°C-1.70002.82.82.82.8抽汽温度twj加热器下端°C380.9316429323223.213788.52.8差6C5.55.55.55.55.55.55.5表1-1 回热加热系统原始汽水参数t1(2)最终给水温度：t=274.1C；fw给水泵出口压力：p=20.13MPa,给水泵效率：n=0.83；pu pu除氧器至给水泵高差:H=21.6mpu小汽机排汽压力：p=6.27MPa；小汽机排汽焓：h.=2422.6KJ/Kge，xj c，xj锅炉型式及参数(1)锅炉型式：英国三井2027-17.3／541／541；额定蒸发量:D=2027t/h；b额定过热蒸汽压力p=20.13MPa;额定再热蒸汽压力p=20.13MPa；br额定过热气温t=541°C额定再热气温t=541°C；br汽包压力p=20.13MPa；du锅炉热效率：nb=92.5%。b其他数据汽轮机进汽节流损失5p=4%,中压缸进汽节流损失5p=2%12轴封加热器压力p=98KPa，疏水比焓：hd=415KJ/Kgsg d，sg机组各门杆漏汽、轴封漏汽等小汽流量及参数见表1-2锅炉暖风器耗汽、过热器减温水等全厂性汽水流量及参数见表1-3汽轮机机械效率n=0.985,n=0.99mg补充水温度t=20Cma厂用电率：£=0.07；(六)简化条件忽略加热器和抽汽管道的散热损失；忽略凝结水泵的介质比焓升。二、热系统计算汽水平衡计算全厂补水率ama全厂汽水平衡如图所示，各汽水流量见表1-3.将进出系统的各流量用相对量a表示。由于计算前汽轮机进汽量D0为未知，故预选D°=1848840Kg/h进行计算。全厂工质渗漏系数a=D/D=30000/1848840=0.01622LL0锅炉排污系数a=D/D=10000/1848840=0.005408blbl0其余各量经计算为厂用汽系数a尸0.01081pl减温水系数a=0.02974sp暖风器疏水系数af=0.01893nf由全厂物质平衡补水率a=a+a+a=0.01081+0.005408+0.01622=0.03244maplblL给水系数affw由图可知：1点物质平衡a=a+a=1+0.01622=1.01622b0L2点物质平衡a=a+a-a=1.01622+0.005408-0.02974=0.9919fwbblsp各小汽流量系数a ksg，k按预选的汽轮机进汽量D0和表1-2的原始数据，计算得到门杆漏汽、轴封漏汽等各小汽流量的流量系数，填于表1-2中。（二）汽轮机进汽参数计算主蒸汽参数由主汽门前压力p=16.7MPa,温度t=537°C，查水蒸气性质表，得主蒸汽00比焓值：h0=3394.4KJ/Kg。主汽门后压力p‘=(1-5p)p=(1-0.04)*16.7=16.032MPa010由p‘=16.032MPa,h'o=h0=3394.4KJ/Kg,查水蒸气性质表，得主汽门后000气温t‘=534.2C0再热蒸汽参数由中联门前压力P=3.234MPa,温度t=537C查水蒸气性质表，得再热蒸rhrh汽比焓值：hrh=3536.6KJ/Kg中联门后压力p‘二(1-5p)p=(1-0.02)*3.234=3.169MParh2rh由p‘=3.169MPa,h‘h=hh=3536.6KJ/Kg，查水蒸气性质表，得中联门后rh rhrh再热气温t‘=536.7Crh辅助计算轴封加热器计算以加权平均法计算轴封加热器的平均进汽比焓h。计算详见表1-4sg均压箱计算以加权平均法计算均压箱内的平均蒸汽比焓h.。计算详见表1-5jy凝汽器平均压力计算由p=4.40KPa,查水蒸气性质表，得t=30.54Cs1 s1由p=5.39KPa,查水蒸气性质表，得t=34.24Cs2 s2凝汽器平均温度t=0.5*(t+t)=32.44Css1s2查水蒸气性质表,得凝汽器平均压力p=4.9KPas各加热器进、出水参数计算首先计算高压加热器H1加热器压力p1p=(1-Ap)p‘=(1-0.03)*5.894=5.717MPa111式中p‘——第一抽汽口压力1Ap——抽汽管道相对压损；1由p=5.717MPa，查水蒸气性质表，得1加热器饱和温度t=272.4°Cs1Hl出水温度t:w，1t=t-5t=272.4-(-1.7)=274.1Cw，1s1式中5t为加热器上端差。Hl疏水温度t：d，1t=t‘+5t=242.3+5.5=247.8Cd，1w，1 1式中5t——加热器下端差，5t=5.5C11t‘——进水温度，Cw，1已知加热器水侧压力p=20.13MPa,由t=274.1C,查得Hl出水比焓hTOC\o"1-5"\h\zw w，1 w，l=l202.lKJ/Kg由t‘=242.3C,p=20.13MPa,查得Hl进水比焓h =1050.9KJ/Kgw，1 w w，l由t=247.8C,p=5.717MPa,查得Hl疏水比焓h=1075.1KJ/Kgd，1 1 d，l至此，高压加热器Hl进、出口汽水参数已经全部计算出。按同样计算，可依次计算其余加热器H2〜H8的各进、出口汽水参数。将计算结果列于表l-6项目单位H1H2H3H4H5H6H7H8SG*抽汽压力p/j抽汽比焓h抽汽管道压Mpa5.893.591.60.740.3050.130.070.0222977KJ/Kg31333016331731082913275026502491损&P.加热器侧压%33333333力P.气侧压力下Mpa5.723.491.60.720.2960.1260.070.021饱和温度t°C272242200166132.6105.988.961.1水侧压力pw加热器上端Mpa20.120.1200.711.7241.7241.721.7241.72差6C-1.70002.82.82.82.8出水温度tw，j出水比焓hw，j进水温度t/C274242200166129.8103.186.158.332.8KJ/Kg12021051860699546.4433.3362246.7139进水比焓h，C242200166130103.186.158.332.7632.2KJ/Kg1051868727546433.3361.8245138.8136w,j加热器下端差6t1C5.55.55.55.55.55.55.55.5疏水温度td,jC248205175166108.691.663.838.2637.7疏水比焓hd,jKJ/Kg1075878726569455.5383.7268160.24151-6回热加热系统汽水参数计算1-6回热加热系统汽水参数计算高压加热器组抽汽系数计算由高压加热器Hl热平衡计算a1高压加热器H的抽汽系数a1；a=%(hw,i-hw,2)g=0.991^1202.1-10^^=0072931 h1-hd, 3132.9-1075.4咼压加热器的疏水系数ad1d，1a=a=0.07293d，1 1由高压加热器H2热平衡计算a、a。2rh高压加热器H2的抽汽系数aQfW(hw,2-hw,3)/6-勺,i(hd,1-hd,2)h2-hd,2二0.9919x(1050.9-860.1)/1.0-0.07289x(1075.4-877.5)=0081713016-877.5 •咼压加热器H2的疏水系数ad，2a=a+a=0.07271+0.08175=0.1546d，2 d，1 2再热器流量系数arha=1-a-a-a-a-a-a-a-a-a-arh 1 2 sg,B Jsg,L1 sg,N1 sg,L sg,M1 sg,Msg,N=1-0.07298-0.08175-0.0001444-0.01636-0.001637-0.00004814-0.0003050-0.001859-0.00005463-0.0003456=0.8246由高压加热器H3热平衡计算a3a二Qfw(hw,3-hpu)/Hh-勺,2(hd,2-hd,3)—Usg,k(hsg,k一hd,3)h3-hd,3二0.9919x(860.1-724.7)/1.0-0.1546x(877.5-740.1)-0.004008x(3536.6-740.1)3317.7-740.1=0.03848a=a+a+a=0.1546+0.03848+0.004008=0.1971d，3 d，2 3 sg，k除氧器抽汽系数计算除氧器出水流量ac，4a=a+a=0.9919+0.02974=1.0216c，4 fw sp抽汽系数a4除氧器的物质平衡和热平衡见图，由于除氧器为汇集式加热器，进水流量a为未知c，5a=[a(h-h)/n-a,(h-h)-a(h-h)-a(h-h)c,4w,4w,5 hd3d，3 w,3 sg,L1sg,L1w,5 sg,Lsg,Lw,5-a(h-h)]/(h-h)nfnfw,54w,5二[1.0216X(726.6-546.4)/1.0-0.1981X(740.1-546.4)-0.001637X(3328.1-546.4)-0.001859X(3016-546.4)-0.01893X(687-546.4)]/(3108.2-546.4)=0.04242(七)低压加热器组抽汽系数计算由低压加热器H5热平衡计算a5a=a-a-a-a-a-ac，5 c，4 d，3 4sg,L1sg,Lnf=1.0216-0.1981-0.04242-0.001637-0.001859-0.01893=0.7597低压加热器H5抽汽系数a5a二他,5(hw,5-hw,6)/5二07488X(546・4一433・3)/1.0=0.03496h5- 2912.9-455.55 d,5低压加热器H5疏水系数ad，5a=a=0.03496d，5 5由低压加热器H6热平衡计算a6低压加热器H6抽汽系数a6a二d(hw,6一hw,7)/出一勺,5(hd,5一hd,6)h6-hd,6二0.7488x(433.3-361.8)/1.0-0.03446x(455.5-383.7)2749.5-383.7=0.0219低压加热器H6疏水系数ad，6a=a+a=0.0219+0.03496=0.05686.由低压加热器H7热平衡计算ad，6 6 d，5 7

a二叫5(hw,7一hw,8)/叫一勺,6(hd,6一hd,7)7 h7-hd,7二0.7488x(361.8-245.4)/1.0-0.05604x(383.7-267.0)2649.5-267.0=0.03396低压加热器H7疏水系数ad，7ad，7=a7+ad，6=0.03396+0.05604=0.090825d，7 7 d，6由低压加热器H8热平衡计算a8a二叫5(hw,8一hw,sg)/6一姿,7(hd,7一hd,8)8 h-h8-d,8二0.7488x(245.4-138.72)/1.0-0.08988x(267-160.2)2491.1-160.2=0.030991低压加热器H7疏水系数ad，7ad，8=a8+ad，7=0.030991+0.08988=0.121816d，8 8 d，7（八）凝气系数a计算c2.由凝汽器的质量平衡计算a2.由凝汽器的质量平衡计算aa”ta —c,xpuxjh-h.4c，xj1.0216x25.43108.2-2422.60.03785xjca=a-a-Za-a-a-ac c，5 d，8 sgxjwma=0.7488-0.1200-0.0007069-0.03785-0.0003716-0.03244=0.566478由汽轮机汽侧平衡校核acH4抽汽口抽汽系数a‘4a‘=a+a+a+a=0.05227+0.03785+0.01893+0.01082=0.110014 4xjnfpf各加热器抽汽系数和ZaZa=a+a+a+a+a+a+a+a‘j12356784=0.07289+0.08175+0.03951+0.1199+0.03446+0.02158+0.03384+0.03015=0.424949轴圭寸漏气系数和Zasg，kZa=a+a+a+a+a+a+a+a+a+a+asg，ksg,k+sg,Bsg,L1sg,N1sg,M1sg,Lsg,Nsg,Msg,Psg,R-asg,Tsg,S=0.004008+0.0001444++0.001637+0.0000481+0.000305+0.001859+0.0000546+0.0003456+0.0004846+0.0001027+0.000357-0.0007637=0.008582凝气系数aca=1-Za-Za =1-0.424949-0.008582=0.566468cj sg，k该值与由凝汽器质量平衡计算得到的a相等，凝气系数计算正确。c（九）汽轮机内功计算1.凝气流做功wcw=(a-a+a)(h-h+q)-aq-a(h-h)ccsg,Ssg,T0Crhjrhsg,A02=(0.55736+0.0007637+0.000357)(3394.4-2333.8+520.6)-0.01636X520.6-0.0003353X(3394.4-3016)=886.4126847抽气流做功£wa，j1KgH1抽汽做功wa，1w=h-h=3394.4-3132.9=261.5KJ/Kga，1011KgH2抽汽做功wa，2w=h-h=3394.4-3016=378.4KJ/Kga，202lKgH3抽汽做功wa，3w=h-h+q=3394.4-3317.7+520.6=597.3KJ/Kga，3 0 3rhlKgH4抽汽做功wa，4w=h-h+q=3394.4-3108.2+520.6=806.8KJ/Kga，4 0 4rhlKgH5抽汽做功wa，5w=h-h+q=3394.4-2912.9+520.6=1002.1KJ/Kga，5 0 5rhlKgH6抽汽做功wa，6w=h-h+q=3394.4-2749.5+520.6=1165.5KJ/Kga，606rhlKgH7抽汽做功wa，7w=h-h+q=3394.4-2649.5+520.6=1265.5KJ/Kga，7 0 7rh1KgH8抽汽做功wa，8w=h-h+q=3394.4-2491.1+520.6=1423.9KJ/Kga，808rh列于表1-7抽汽流总内功£wa，jXw=aw+aw+aw+a"w+aw+awa，j 1a,1 2a,2 3a,3 4a,4 5a,5 6a,6+aw+aw7 a,7 8 a,8=0.072891X261.5+0.081753X378.4+0.0395122X597.3+0.119861X806.8+0.0344619X1002.1+0.0215839X1165.5+0.033837X1265.5+0.030152X1423.9=309.386KJ/Kg附加功量£wsg，k附加功量£w是指各小汽流量做功之和：sg，k£w二asg,k(h-h+q)+(a+a+a)(h-h)+(a+a+sg，k 0sg,krh sg,L1sg,N1sg,M10sg,L1 sg,Lsg,Na)(h-h )+(a+a)(h-h+q)sg,M0sg,L sg,Psg,R0sg,Prh=0.004008X(3394.4-3536.6+520.6)+(0.001637+0.00004814+0.000305)X(3394.4-3328.1)+(0.001859+0.00005463+0.0003456)X(3394.4-3016)+(0.000485+0.000103)X(3394.4-3108.2+520.6)=2.9773KJ/Kg汽轮机内功wiw=w+£w+£w=872.016766+315.7462+2.9773=1184.38KJ/Kgic a，j sg，k(十)汽轮机内效率、热经济性指标、汽水流量计算汽轮机比热耗q0q=h-h+aq=3394.4-1202.1+0.8235X520.6=2621.588KJ/Kg0 0frhrh汽轮机绝对内效率nin=wq=1190.740274／2621.0141=0.45178ii／0汽轮机绝对电效率nen=nnn=0.985X0.99X0.4543052=0.440553e m・g・i *汽轮机热耗率qq=3600／ne=3600／0.440553=8171.551KJ/(kwh)e汽轮机汽耗率dd=q／q0=8171.551／2621.0141=3.117706Kg/(kwh)汽轮机进汽量D：0D0=l00°•d•Pe=l00°X3.1177O6X6OO=i87O623Kg/h0e给水流量GfwwGf=a4D0=1.°2164Xi870623=1911104Kg/hfwc,4 0凝结水泵流量GcpG=a5D0=0.748777284X1870623=1421043Kg/hcpc,5 0凝气量DcD二aD0=0.557363859X1870623=1059648Kg/hcc0第一级抽汽量D1D1=a1•D0=O.O72891995X1870623=136424.6Kg/h(十一)全厂性热经济指标计算锅炉有效热量q1q=(a-a)(h-h)+a (h-h)+a(h-h)+aq"1 fwbl bfw blblfw spbsp rhrh=(O.9919-O.OO54O8)(3399.2-12O2.1)+O.OO54O8(176O.3-12O2.1+O.O2974(3399.2-724.7)+O.8246O1O5X527=2684.54573KJ/Kg管道效率npnp=qO／q1=2621.O141／2684.54573=0.976334p O／1全厂效率ncpncp=nbnpne=O.925X0.976334XO.443O157=0.397955cpbpe全厂发电标准煤耗率r=q= 2684.5447 =r= 1 = =1.016045q1-耳b•qnf2684.5447-0.925x45.831Kg标准煤的输入热量QsbQs=293OOXr=293OOX1.016045=2977O.112KJ/Kgb发电标准煤耗bbs=3600bs=3600“cp・Qb36000.40009x29770.112全厂热耗率qcpq=29300bs=29300X0.30387=8903.391cp全厂供电标准煤耗bsnbs=bsbs=bsn1-£0.3022471-0.07=0.326742抽汽压损为5%时的计算方法同上：计算结果如以下表格：回热加热系统汽水参数计算项目单位H1H2H3H4H5H6H7H8SG*抽汽压力p/j抽汽比焓h抽汽管道压Mpa5.893.591.60.740.3050.130.070.0222977KJ/Kg31333016###31082913275026502491损&P.加热器侧压%55555555力P.气侧压力下Mpa5.63.411.50.710.290.1240.070.021饱和温度t°C271241199165132.4105.788.561水侧压力pw加热器上端Mpa20.120.1200.711.7241.7241.721.7241.72差6C-1.70002.82.82.82.8出水温度tw，j出水比焓hw，j进水温度t/C273241199165129.6102.985.758.232.8KJ/Kg11961045857699545.7432.5361245.1139进水比焓h，C241199165130102.985.758.232.7632.2KJ/Kg1045857725546432.5360.5245138.7136w,j加热器下端差6t1C5.55.55.55.55.55.55.55.5疏水温度td,jC247205174165108.491.263.738.2637.7疏水比焓hKJ/Kg1071875738699454.7382267160.2415

抽汽压损为8%时回热加热系统汽水参数计算项目单位H1H2H3H4H5H6H7H8SG*抽汽压力p/j抽汽比焓h抽汽管道压Mpa5.893.591.60.740.3050.130.070.0222977KJ/Kg31333016###31082913275026502491损&P.加热器侧压%88888888力P.气侧压力下Mpa5.423.311.50.660.2810.120.060.02饱和温度t°C268239197164130.9104.587.460水侧压力pw加热器上端Mpa20.120.1200.711.7241.7241.721.7241.72差6C-1.70002.82.82.82.8出水温度tw，j出水比焓hw，j进水温度t/C271239197164128.1101.784.657.232.8KJ/Kg11861037849693539.2427.4356240.8139进水比焓h，C