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1、汽汽机机参参数数主给水温度汽机功率主蒸汽压力新蒸汽温度再热蒸汽温度进气阀前再热段再热冷段汽轮机排汽压力排汽比焓除氧器压力高高加加上上端端差差(高高入入低低出出）一级二级三级四至八级疏疏水水冷冷却却下下端端差差一级二级三级五级六级七级八级凝结水流程疏水流程汽动给水泵排汽扩容器工作压力减温水流量汽汽水水损损失失全场汽水损失厂用汽锅炉暖风用汽4级抽汽，疏水返回除氧器，疏水比焓各各漏漏气气表表1 1汽汽、水水代代号号汽汽水水流流量量（kg/hkg/h）汽汽水水比比焓焓（kj/kgkj/kg）漏漏气气系系数数sf,jsf,j汽汽水水流流量量（kg/hkg/h）汽汽水水比比焓焓（kj/kgkj/kg）漏漏
2、气气系系数数sf,jsf,j计计算算公公式式为为i=Dx/Doi=Dx/Do回回热热参参数数给给水水温温度度给给水水泵泵出出口口压压力力除除氧氧器器至至给给水水泵泵高高差差小小汽汽机机排排汽汽压压力力小小汽汽机机排排汽汽比比焓焓表表2 2项项目目单单位位抽抽汽汽管管道道压压损损PjPj%抽抽汽汽压压力力PjPjMpaMpa抽抽汽汽温温度度TjTj摄摄氏氏度度抽抽汽汽焓焓hjhjkj/kgkj/kg加加热热器器上上端端差差tjtj摄摄氏氏度度加加热热器器下下端端差差jj摄摄氏氏度度水水侧侧压压力力PwPwMPaMPa抽抽汽汽管管道道压压损损PjPj%再再热热后后的的进进汽汽损损失失后后Trh=5
3、34(532)Trh=534(532)锅炉参数额定蒸发量额定过热蒸汽压力额定过再热蒸汽压力额定过热汽温额定再热汽温汽包压力锅炉热效率其其他他数数据据汽机进气节流损失中压缸进汽节流损失轴封加热器压力汽机机械效率电机效率补充水温度厂用电率计计算算假设汽机进汽量为Do=1962700kg/h厂用水系数减温水系数全厂工质渗漏系数锅炉排污系数暖风机疏水系数全场物质平衡知补水率给水系数各各漏漏汽汽系系数数在在表表1-11-1内内（二二）汽汽机机进进汽汽参参数数计计算算1.1.主主蒸蒸汽汽参参数数主汽门前Po=16.5Mpa查表知比焓(kj/kg)主汽门后Po=(1-plpl)PoHo=Ho=3389.56
4、8610887kj/kgHo=Ho=3383.886643078kj/kg即门前压力门前温度门前比焓门后压力门后温度门后比焓全全厂厂汽汽水水进进出出系系统统有有关关数数据据名称汽水流量kg/h离开系统的介质比焓返回系统的介质比焓2.2.再再热热蒸蒸汽汽参参数数由中联门后压力温度查得比焓（热段)由中联门后压力温度查得比焓Hrh=HrhHrh=Hrh所以再再热热中中联联门门前前后后参参数数前压力PrhPrh前温度TrhTrh前比焓HrhHrh后压力PrhPrh后温度TrhTrh后比焓HrhHrh(二二）辅辅助助计计算算1.1.轴轴封封加加热热器器轴轴封封加加热热器器物物质质热热平平衡衡表表3 3项
5、目4汽水流量Gi,kg/h2908汽水系数i0.001473151汽水比焓hi3204.3总焓i*hi4.720417629平均比焓3334.8137442.2.均均压压箱箱平平均均蒸蒸汽汽比比焓焓表表4 4项目9汽水流量Gi，kg/h1551汽水系数i0.000785714汽水比焓hi3474总焓i*hi2.729571429平均比焓3156.859845回回热热加加热热系系统统汽汽水水参参数数表表5 5项目单位（汽汽侧侧）抽抽汽汽压压力力PjPjMpa（汽汽侧侧）抽抽汽汽比比焓焓HjHjkj/kg（汽汽侧侧）抽抽汽汽管管道道压压损损PjPj%（汽汽侧侧）加加热热器器汽汽侧侧压压力力PjPj
6、Mpa（汽汽侧侧）汽汽侧侧压压力力下下的的饱饱和和温温度度TsTs摄氏度（水水侧侧）加加热热器器上上端端差差tt摄氏度（水水侧侧）水水侧侧压压力力PwPwMpa（水水侧侧）出出水水温温度度TwjTwj摄氏度（水水侧侧）出出水水比比焓焓HwjHwjkj/kg（水水侧侧）进进水水温温度度TwjTwj摄氏度（水水侧侧）进进水水比比焓焓HwjHwjkj/kg（水水侧侧）加加热热器器下下端端差差jj摄氏度（水水侧侧）疏疏水水温温度度TdjTdj摄氏度（水水侧侧）疏疏水水比比焓焓HdjHdjkj/kg表表6 6做做工工和和抽抽汽汽量量的的计计算算按按结结果果Do=H11kg抽汽做工（kj/kg）253各抽
7、汽量(kg/h)143024.9407（抽汽量=i*Do）35493.85898抽抽汽汽总总量量总总内内功功a.ja.j=1*1+2*2+8*8=注意：总内功中H4为4*4,不是4*43。附加功sg.ksg.k=各小汽流量做功之和=sg.k=12(Ho-H12+Qrh)+(8+9+10)(Ho-H8)=此式中H，都来自表表1 14.汽轮机内功ii=c+a.j+sg.k=1234.9004421161.901003（十）汽机内效率，热经济性，汽水流量计算f2637.2622722774.742351汽机绝对内效率iii=i/Qo=0.4682509040.418741943汽机绝对电效率eee=
8、mgi=0.4566148690.408336205汽机热耗率qq q=3600/e=7884.1059428816.264519汽机汽耗率dd d=q/Qo=2.9895039353.177327262汽机进汽量DoDoDo=1000*d*Pe=1973072.5972097035.993Pe为660MW汽机而定功率校验汽机进汽量Do待校核的进汽量故在误差范围内，可用给水流量GfwGfwGfw=c4*Do=2026740凝结水泵流量GcpGcpGcp=c5*Do=1590812.6951685641.105凝汽量DcDcDc=c*Do=1185518.0361284796.968第1级抽汽量
9、D1 D1D1=Do*1=143024.9407第2级抽汽量D2 D2=Do*2=127722.7907第3级抽汽量D3 D3=Do*3=76642.34217第4级抽汽量D4 D4=Do*4=16593.23178第5级抽汽量D5 D5=Do*5=0.029137047第6级抽汽量D6 D6=Do*6=58882.00948第7级抽汽量D7 D7=Do*7=104249.9125第8级抽汽量D8 D8=Do*8=17603.38515(十一)全厂热经济性计算1.锅炉参数的计算额定过热蒸汽压力Pb=17.42MPaTb=537(535)查得过热蒸汽出口比焓Hb=3387.532519497（3
10、381.774497313）额定过热蒸汽温度537（535）摄氏度设计再热出口压力3.85MPa，高于汽机排汽压力Pr=3.16736,故按照汽机侧参数,确定Pr=3.16736Pr=3.16736来自再热计算中联门处。有Pr和额定再热温度537（535）查得再热蒸汽出口比焓Hr=3538.646767510（3534.129603936）再热器换热量Qrh=Hr-H2=511.5467675507.02960392.锅炉有效热量Q1Q1=(fw-bl)(Hb-Hfw)+bl(Hbl-Hfw)+sp(Hb-Hsp)+rh*Qrh=3.管道效率pp=Qo/Q1=0.9796618250.9828
11、02274.全厂效率cpcp=bep=0.4137785440.3712152195.全厂发电标准煤耗bs系数r=Q1/(Q1-b*Qnf)=1.0285225141.02716019其中Qnf暖风吸热量按下式计算Qnf=nf（Hnf-Hnf）=80.70666667相应的1kg标煤的输入热量QBSQBS=29300*r=30135.7096730095.79358发电标准煤耗bsbs=3600/(cp*QBS)=0.2887042060.3222336786.全厂热耗率QcpQcp=bs*29300=8459.0332289441.4467737.全场供电标准煤耗bnsbns=bs/(1-)
12、=0.310434630.346487826为全厂电率反平衡校核校核目标为i。计算中均以1kg工质1.锅炉输入热量Qr=Q1/b=2910.2842193052.2125882.锅炉损失qb=（1-b）Qr=218.2713164228.91594413.排污损失qbl=bl(Hbl-Hma)=16.7664.全厂工质渗漏ql=L（Hl-Hma）=55.265280735.全厂用汽损失qpl=pl*(Hpl-Hma)=33.70770016.凝汽流冷源损失Qc=c（Hc-Hc）=1269.5088891383.1865097.小机冷源损失qxj=xj(Hcxj-Hc)=79.814507838
13、0.24164898.化学补水冷源损失qma=ma(Hma-Hc)=-4.446812702-4.0183693359.低加H8疏水冷源qd8=d8(Hd8-Hc)=-4.986698577-3.55329299510.轴封加热器疏水冷源qdsg=dsg*(Hdsg-Hc)=11.W汽流冷源损失qsgw=sgw(Hsgw-Hc)=14.0688325414.12269465以上611项为凝汽器直接冷源损失12.暖风器损失qnf=nf(Hnf-hnf)=80.7066666713管道散热损失qp=b(Hb-Ho)+rh(Hrh-Hrh)=14.轴封漏气散热损失qsg=2H2+5H5+7H7+8H
14、8+9H9-均压箱平均比焓*jyx=此式中数据来自表一和表4损失之和qi=214之和=见例题=1686.1545691888.185031汽机内功率i=Qr-qi=1224.129651164.027557i=(i-i)/i=-0.0087219920.001830237Tfw=272摄氏度272272248摄氏度Pe=660MW660000000Po=16.5Mpa16.5To=534摄氏度534534Trh=534摄氏度534534Prh=3.232MPa3.232Prh=3.567MPa3.567Pc=4.4/5.38kpa44005380Hc=2315.6kj/kg0.9161MPa9
15、16100-1.7摄氏度-1.700-1.7摄氏度-1.72.8摄氏度2.85.5摄氏度5.55.5摄氏度5.55.5摄氏度5.55.5摄氏度5.55.5摄氏度5.55.5摄氏度5.55.5摄氏度5.5凝汽器-轴封加热器-4台低加-除氧器-给水泵加压-三台高加 1高加-2高加-3高加-除氧器 6.34KPa63401.55MPa155000066240kg/h6624033000kg/h3300022000kg/h2200065800kg/h65800汽汽水水损损失失1 1门门杆杆漏漏气气去去再再热热2 2门门杆杆漏漏气气去去均均压压箱箱3 3来来自自给给水水泵泵减减温温减减压压水水18243
16、89662403397.23397.2773.36641260.0009240120.0001970620.0335562319 9中中漏漏去去均均压压1010中中漏漏去去除除氧氧1111厂厂用用汽汽15512785220003474347431690.0007857140.0014108410.0111448834级抽汽，疏水返回除氧器，疏水比焓各各漏漏气气表表1 1272272248248Ppu=21.47MPa21.47给水泵效率pu0.83Hpu=22.4m22.4Pc,xj=6.27KPa6270Hc，xj=2422.6kj/kgH1H1H2H2H3H33335.69895.6989
17、（3.84883.8488）3.6681.776384.5315384.5315（369.3963369.3963）320.5152445.95893144.23027.13352.2-1.70-1.75.55.55.521.4721.4721.47333Prh=0.98*Prh=3.167p2=0.02Hrh=3531.874868270Db=2208t/h2208Pb=17.42MPa17.42Pr=3.85MPa3.85Tb=541摄氏度541Tr=541摄氏度541Pdu=18.28MPa18.28n=92.5%0.925plpl=4%0.04p2p2=2%0.02PsgPsg=102
18、kpa102000疏水比焓 Hd，sg=415kj/kgmm=0.9850.985gg=0.990.99TmaTma=20摄氏度20=0.070.07待待校校核核19740001974000plpl=厂用汽/Do0.011144883spsp=减温水流量/Do0.033556231L L=DL/Do0.016717325blbl=Dbl/Do0.01Dbl=Do*0.01nfnf=暖风用汽/Do0.033333333mama=L+bl+pl0.037862209bb=o+L (o=1)1.016717325fwfw=b+bl-sp0.993161094表表2 2To=534摄氏度To=532摄
19、氏度3389.5686113383.886643Po=(1-0.04)*16.515.84查表的主汽门后To=531.296350529531.2963505查表的主汽门后To=529.277898889529.277898916.516.55345323389.5686113383.88664315.8415.84531.2963505529.27789893389.5686113383.886643全厂工质渗漏14锅炉排污厂用汽1133000197490220003389.5686111760.33108.283.783.783.7PrhPrh=3.232 HrhHrh=3531.2330
20、823526.712605PrhPrh=(1-p2)Prh(1-0.02)*3.2323.16736温度为3.2323.2325345323531.2330823526.7126053.167363.16736533.7203577531.71827843531.2330823526.712605197400019740005672099323625720.0010633230.0016393110.0013029383204.33204.33204.33.4072065355.2528443774.175004863875全全厂厂汽汽水水进进出出系系统统有有关关数数据据轴轴封封加加热热器器物
21、物质质热热平平衡衡表表3 33334.813744表表4 42785257220990.0014108410.0013029380.00106332331693024.33024.34.4709549143.9404759883.21580835930.6192671534.1856165832.402441874.8686查表得加热器饱和温度Ts，1=270.3所以H1出水温度查表得加热器饱和温度Ts，1=246.3所以H1出水温度245.3521237查表得加热器饱和温度Ts，2=513.002123673k 所以H2出水温度239.8521237212.1630068查表得加热器饱和温度
22、Ts,3=478.113006761k所以H3出水温度204.9630068185.3633627查表得加热器饱和温度Ts,4=449.248790145k所以H4出水温度3156.859845回回热热加加热热系系统统汽汽水水参参数数表表5 5表表6 6sg.k=12(Ho-H12+Qrh)+(8+9+10)(Ho-H8)=其中gm分别为0.99,0.98535493.85898127727.292881710.8368524222.9066960945.0936962391.96848110464.25426960.532942692.0129032823.296644Tb=537(535)
23、查得过热蒸汽出口比焓Hb=3387.532519497（3381.774497313）设计再热出口压力3.85MPa，高于汽机排汽压力Pr=3.16736,故按照汽机侧参数,确定Pr=3.16736有Pr和额定再热温度537（535）查得再热蒸汽出口比焓Hr=3538.646767510（3534.129603936）其中b为锅炉效率0.925Hma为化学补水比焓Hc=排汽比焓=23152315Hc=sg进水比焓凝汽器出水比焓Hcxj=小机排汽焓=2315.61.927274686其中dsg来自表三的漏气系数之和2.029254984sgw,Hsgw来自表四-3.489532681其中Hrh=
24、Hr(表中C列452行),且Hrh=Hrh-8.9328174379.74781159114.轴封漏气散热损失qsg=2H2+5H5+7H7+8H8+9H9-均压箱平均比焓*jyx=jyx=i/4248248532532532532Trh=534Trh=534Trh=532Trh=532Trh=315Trh=3155低加-6低加-7低加-8低加-疏水泵-主凝结水混合 120800120800697kj/kg697排污损失1%4 4高高漏漏去去除除氧氧器器5 5高高漏漏去去均均压压箱箱6 6高高漏漏去去除除氧氧器器7 7高高漏漏去去均均压压箱箱29082099323625723024.33024
25、.33024.33024.30.0014731510.0010633230.0016393110.0013029381212暖暖风风器器13131414全全场场汽汽水水损损失失1515均均压压去去轴轴封封加加热热6580074740330001270316984.13397.23334.8137440.0333333330.0378622090.0378622090.0167173250.000643364来自均压箱平均比焓0.83H4H4除除氧氧器器H5H5H6H6H7H753330.9640.4160.2260.109354.772257.0419190.8571120.152331692
26、978.528512716-2.82.82.8-5.55.55.50.9162.7582.7582.75853333527.35888319740疏水比焓 Hd，sg=415kj/kgpl=0.04pl=0.04p2=0.02p2=0.02暖风器12过热器减温水365800662403108.2724.7687724.789101513691551278512700.0006935160.0007857140.0014108410.0006433643169374737473217.72.1977512662.9440714295.2864209732.07015146923334.81374
27、438993960.0001970620.0047598783397.20.66945835915.02626905Tw，1=Ts，1-t1=272Tw，1=Ts，1-t1=248t1=-1.7Tw，2=Ts,2-t2=239.8521237t2=0Tw，3=Ts,3-t3=206.6630068t3=-1.7Tw，4=Ts,4-t4=176.0987901t4=0（因为除氧器为混合式）Tw，5=Ts,5-t5=141.1286585t5=2.8Tw，6=Ts,6-t6=120.3371236t5=2.8Tw，7=Ts,7-t7=98.37099573t7=2.8Tw，8=Ts,8-t8=56
28、.9323254t8=2.8H4H5H6H70.9640.4160.2260.10931692978.52851271653330.91580.403520.219220.10573176.0987901143.9286585123.1371236101.1709957-2.82.82.80.9162.7582.7582.758176.0987901141.1286585120.337123698.37099573746.0100677595.5864002507.0143303414.2376606141.1286585120.337123698.3709957356.9323254745.
29、9850932507.0143303414.2376606240.6417033-5.55.55.5176.0987901125.8371236103.870995762.4323254745.9849892528.7421466435.5185133261.40146530.0084058920.012270976H5H6H7H8922.8330821050.3330821185.3330821445.533082918.31260491045.8126051180.8126051441.01260557516.5309258882.00948104249.912517603.3851560
30、945.0936962391.96848110464.25426960.532948 8中中漏漏去去均均压压136931690.0006935161616均均压压去去7 7低低加加58213334.8137440.002948835来自均压箱平均比焓H8H830.019759.73232455.82.8-2.7583177900.00901215826697.930.05386854H8SG0.01972455.82976.530.0191090.0010259.73232547.2584054882.82.7582.75856.932325447.4304060740.65639608240.6417033201.1472608189.831403132.6524418732.15244187139.3221615-5.552.9304060746.15639608159.830715415