抽凝机组原则性热力系统计算

1.汽轮机型式和技术数据,,,,,,,,

型号,,C15-8.83/0.98,,3.锅炉主要参数,,,,

额定功率(kW),P,15000,,主蒸汽出口压力（Mpa）,pb,9.8,,

蒸汽初参数,,,,汽包压力（Mpa）,pd,11.4,,

（1）压力(Mpa),p0,8.83,,过热蒸汽温度（℃）,tb,540,,

（2）温度（℃）,t0,535,,过热蒸汽焓(kj/kg),hb,3475,,

（3）焓值（kj/kg）,h0,3475,,锅炉给水温度（℃）,tfw,210.1,,

额定抽气量（t/h）,De,0,,锅炉给水焓(kj/kg),hfw,903.1,,

额定抽气压力（Mpa）,pe,0.98,,,,,,

额定抽气温度（℃）,te,296.9,,,,,,

凝结水回水焓值(kj/kg),hr,237,,,,,,

额定排气压力（kpa）,pc,4.6,,,,,,

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2.回热系统参数,,,,,,,,

项目,回热抽汽级数,,,,,,,

,一,二,三,四,,,,

加热器编号,GJ2,GJ1,LHE2,LHE1,,,,

抽汽压力（Mpa）,2.293,0.98,0.145,0.026,,,,

抽汽温度（℃）,385.9,296.9,132.9,65.8,,,,

4.计算选用数据,,,,,,,,

锅炉排污量,Dbl,0.05Db,0.05,,,,,

热电厂内汽水损失,Dlo,0.03Db,0.03,,,,,

锅炉出口过热蒸汽量,Db,Db,,,,,,

对外供热凝结水回水率,ψ,0,,,,,,

凝结水回水温度,th,80,,,,,,

锅炉效率,ηb,0.85,,,,,,

汽轮机机械效率,ηm,0.985,,,,,,

发电机效率,ηg,0.97,,,,,,

换热器效率,ηh,0.98,,,,,,

热电厂内管道效率,ηp,0.96,,,,,,

轴封用汽量,Dsg,0.01Do,,,,,,

汽轮机进汽量,Do,,,,,,,

5.汽轮机组汽水综合表,,,,,,,,

项目,各计算点,,,,,,备注,

,1,2,3,4,5,c,,

加热器编号,GJ2,GJ1,除氧器,LHE2,LHE1,,二级抽汽减压后用于除氧焓值不变,

抽汽压力pe(Mpa),2.29,0.98,,0.145,0.026,0.0046,,

抽汽温度te(℃),385.90,296.90,,132.90,65.80,,,

抽汽焓值he(kJ/kg),3205.60,3044.30,3044.3,2738.50,2519.50,2349.2,,

抽气压损△p（%）,8.00,8.00,,8.00,8.00,,,

加热器处汽压pj(Mpa),2.11,0.90,,0.13,0.02,,,

pj压力下饱和水温tj(℃),215.14,175.39,158,107.14,60.07,,,

pj压力下饱和水焓hj(kJ/kg),921.10,742.90,667.24,449.24,251.43,,,

抽气放热量qe=he-hj(kJ/kg),2284.50,2301.40,2377.06,2289.26,2268.07,,,

加热器端差δt(℃),5.00,5.00,,5.00,5.00,,,

加热器出口水温tw‘=tj-δt(℃),210.14,170.39,,102.14,55.07,,,

加热器出口水焓hw’(kJ/kg),903.10,727.70,,431.20,246.60,,,

加热器进口水温tw(℃),170.39,158.00,,55.07,31.44,31.44,,

加热器进口水焓hw(kJ/kg),727.70,667.24,,246.60,131.61,131.608,,

给水焓升△hw=hw'-hw(kJ/kg),175.40,60.46,,184.60,114.99,,,

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6.汽轮机耗气量近似计算,,,,,,,,

汽轮机功率,汽轮机进气初焓,汽轮机抽气焓,汽轮机实际终焓,汽轮机机械效率,发电机效率,调整抽气量,考虑非调整抽气回热用气量的系数,汽轮机汽耗量估算

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P（kW),ho（kj/kg),he（kj/kg),hc（kj/kg),ηm,ηg,De（kg/h）,αp,D（kg/h)

15000,3475,3044.30,2349.2,0.985,0.97,0,1.15,57732.76944

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供热抽气量,汽轮机汽耗量,供热抽气占汽轮机汽耗量份额,,,,,,

De,D,αe,,,,,,

0,57732.76944,0,,,,,,

7.锅炉排污系统计算,,,,,,,,

汽轮机总汽耗量,D0',1.01D0,锅炉轴封用汽按0.01D0,,,,,

轴封用汽份额,αsg,0.01,,,,,,

汽轮机总汽耗量份额,α0',1.01,,,,,,

锅炉蒸发量,Db,1.04124D0,汽水损失锅炉蒸发量的0.03,,,,,

锅炉蒸发量份额,αb,1.04124,,,,,,

全厂厂内汽水损失份额,α10,0.03124,,,,,,

锅炉排污量,Dbl,0.05206D0,排污率按0.05,,,,,

锅炉排污量份额,αbl,0.052062,,,,,,

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锅炉汽包压力,饱和水焓,,,,,,,

Pd（Mpa）,hbl（kj/kg),,,,,,,

11.4,1466.2,,,,,,,

排污扩容器,,,,,,,,

扩容压力,扩容压力下饱和水焓值,排污扩容器二次蒸汽焓值,,,,,,

Pbl(Mpa),hbl'(Kj/kg),hf(Kj/kg),,,,,,

0.7,697.32,2763.29,,,,,,

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热平衡式,αblhblηh=αfhf+αbl'hbl',,,,,,,

物质平衡式,αbl'=αbl-αf,,二次蒸汽份额,排污水份额,,,,

αbl,hbl,ηh,αf,αbl',,,,

0.052062,1466.2,0.98,0.01864,0.03343,,,,

,,,0,,,,,

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对外供热凝结水损失占汽轮机耗气量的份额,,凝结水损失份额,凝结水回水量,,,,,

De,D,αow,αr,,,,,

0,57732.76944,0,0,,,,,

化学补充水量,,,,,,,,

排污水损失量,热电厂内汽水损失量,对外供热凝结水损失量,轴封用汽量,化学水补充水量,化学水补充份额,,,

Dbl'=αbl'*D0,D10=αlo*Db=αlo*αb*Do,Dow=αowDo,Dsg=0.01D0,Dma,αma,,,

0.03343,0.032525422,0,0,0.06595,0.06595,,,

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锅炉给水量,,,,,,,,

锅炉蒸发量份额,排污量份额,锅炉给水份额,,,,,,

αb,αbl,αfw,,,,,,

1.04124,0.052062,1.093302,,,,,,

排污水冷却器的计算,,,,,,,,

化学补充水温度,化学补充水焓值,排污水冷却器端差,冷却器加热后的给水温度,相应焓值,排污水焓值,排污水温度,故冷却器出水口温度,相应焓值

tma（℃）,hma（kj/kg）,℃,,kj/kg,"hbl""(kj/kg)",℃,tma'(℃),hma'(kj/kg)

75,314.025,7,"tbl""-7","hbl""-7*4.1868",460.8059014,87,80,334.94

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热平衡方程式,,,,,,,按汽机厂给的,

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整理得,,,,,,,,

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高压加热器,,,,,,,,

,GJ2,GJ1,,,,,,

抽气份额α1,0.085654955,0.02254055,,,,,,

抽气放热量qe,2284.50,2301.40,,,,,,

给水焓升△hw,175.40,60.46,,,,,,

给水份额αfw,1.093302,1.093302,,,,,,

换热器效率ηh,0.98,0.98,,,,,,

除氧器计算,,,,,,,,

物质平衡,αfw=αma+(α1+α2)+αf+(α3+α4+αc+αsg)+αd+αr,,,,,,,

给水份额αfw,1.093302,,,,,,,

给水份额αma,0.06595,0.90052,,,,,,

高加抽气冷却水份额α1+α2,0.108195506,,,,,,,

排污二次蒸汽份额αf,0.01864,,,,,,,

低加（含轴封）份额α3+α4+αc+αsg,0.52099-αd,,,,,,,

加热用蒸汽份额αd,0.0773,,,,,,,

冷却水回水份额αr,0,,,,,,,

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热平衡,αfwhd'=(αmahma'+(α1+α2)*h2'+αfhf+(α3+α4+αc+αsg)hw4+αdhd+αrhr)ηh,,,,,,,

给水焓值hd'（kj/kg),667.24,,,,,,,

补水焓值hma'（kj/kg),334.94,,,,,,,

高加冷凝水h2'（kj/kg),742.90,,,,,,,

二次蒸汽焓值hf（kj/kg),2763.29,,,,,,,

低加出水焓值hw4（kj/kg),246.60,,,,,,,

加热蒸汽焓值hd（kj/kg),3044.30,,,,,,,

凝结水焓值hr（kj/kg),0,,,,,,,

求得αd,0.0773,,,,,,,

α3+α4+αsg+αc,0.82317,,,,,,,

低压加热器组,,,,,,,,

热平衡式一（包括二级低加）,(α3+α4+αsg+αc)*hc'-αchc-(α3+α4)h4'-αsghsg'=(（α3（h3-h3')+α4(h4-h4')+αsg(h0-hsg'))ηh,,,,,,,

热平衡式一（不包括二级低加）,"(α3+α4+αsg+αc)*hc""-αchc-(α3+α4)h4'-αsghsg'=(α4(h4-h4')+αsg(h0-hsg'))ηh",,,,,,,

二级低加出水焓值hc',431.20,,,,,,,

"一级低加出水焓值hc""",246.60,,求得α3,0.0664,,,,

冷却水焓值hc,131.61,,α4,0.0233,,,,

二级低加抽汽焓值h3,2738.50,,αc,0.72349,,,,

二级低加冷凝水焓值h3',449.24,,各份额相加,1.00871,0.87%,,,

一级低加抽汽焓值h4,2519.50,,,,,,,

一级低加冷凝水焓值h4',251.43,,,,,,,

轴封抽气焓值h0,3405.5,,,,,,,

轴封凝结水焓值hsg',251.09,,轴封冷凝水温度取60，对应焓值为251.09kj/kg,,,,,

汽轮机汽耗量及各项汽水流量计算,,,,,,,,

（1）做功不足系数计算,,,,,,,,

GJ2抽气系数Y1,0.7607035,,,,,,,

GJ1抽气系数Y2,0.617427607,,,,,,,

LHE2抽气系数Y3,0.345798543,,,,,,,

LHE1抽气系数Y4,0.151270208,,,,,,,

各级抽气份额及做功不足系数乘积,,,,,,,,

α1Y1,0.065158024,,,,,,,

（α2+αd+αe)Y2,0.061672561,,,,,,,

α3Y3,0.022953611,,,,,,,

α4Y4,0.003525612,,,,,,,

(2)汽轮机纯凝工况时的汽耗量,,,,,,,,

Dco,50202.40821,,,,,,,

(3)有回热抽气汽轮机汽耗量D0,,,,,,,,

D0,59292.53544,,,,,,,

核算汽轮机耗气量误差,2.63%,,,,,,,

各项抽汽和汽水流量计算,,,kg/h,,,,,

锅炉排污αbl,0.052062,锅炉排污Dbl（kg/h),3086.9,,,,,

排污扩容蒸汽αf,0.01864,排污扩容蒸汽Df（kg/h),1105.0,,,,,

排污水αbl',0.03343,排污水Dbl'（kg/h),1981.9,,,,,

厂内汽水损失α10,0.03124,厂内汽水损失D10（kg/h),1852.1,,,,,

轴封用汽量αsg,0.01,轴封用汽量Dsg（kg/h),592.9,,,,,

化学补充水量αma,0.06595,化学补充水量Dma（kg/h),3910.4,,,,,

锅炉给水量αfw,1.093302,锅炉给水量Dfw（kg/h),64824.6,,,,,

汽轮机总汽耗量α0',1.01,汽轮机总汽耗量D0'（kg/h),59885.5,,,,,

锅炉蒸发量αb,1.04124,锅炉蒸发量Db（kg/h),61737.8,,,,,

一级抽汽量α1,0.085654955,一级抽汽量D1（kg/h),5078.7,,,,,

二级抽汽量α2+αd+αe,0.0999,二级抽汽量D2（kg/h),5922.5,,,,,

三级抽汽量α3,0.0664,三级抽汽量D3（kg/h),3935.8,,,,,

四级抽汽量α4,0.0233,四级抽汽量D4（kg/h),1381.9,,,,,

凝汽器凝结水量αc,0.72349,凝汽器凝结水量Dc（kg/h),42897.4,,,,,

汽轮机功率核算,,