350MW机组原则性热力系统计算.doc
11、汽轮机型式及参数汽机型式为一次中间再热、亚临界、单轴、双缸、双排汽、冲动凝汽式汽轮机，额定功率为 352MW，额定主蒸汽参数：P0=17.46Mpa，t0=538；额定再热蒸汽参数：Prh=3.07Mpa，trh=538；额定排汽压力 Pc=0.0049Mpa； hc=2371kj/kg。2、锅炉型式及参数锅炉型式为露天布置、平衡通风，具有平行尾部通道的燃煤辐射锅炉；单汽包、单炉膛、具有一次中间再热的亚临界自然循环锅炉；额定蒸发量为1085.1t/h，额定饱和蒸汽压力 19.02Mpa，过热蒸汽压力 17.84Mpa，过热蒸汽温度 540.6，再热蒸汽温度 539，给水温度 282，锅炉效率为 93.7%。3、回热系统及参数机组采用八级回热（三高加四低加一除氧） 。额定工况下的抽汽参数：#1 高加#2 高加#3 高加除氧器#5 低加#6 低加#7 低加#8 低加抽汽1 2 3 4 5 6 7 8压力MPa6.773.351.830.850.410.190.0750.0309温度 40030245735726518598702除氧器滑压运行，凝泵出水压力为 2.15Mpa，采用汽轮给水泵，汽源与除氧器同为四抽蒸汽，额定蒸汽参数为：hDT=31774kj/kg，；MPapcDT005. 0kgkjhcDT/2440小汽机的耗汽量占给水流量的份额；小汽机排汽至冷凝器；给水泵出口压03376. 0DT力为 20.43 Mpa。、其它数据的选取主机、给泵汽机合用同一轴封汽系统；额定负荷时，由于系统采用自密封型式，高压缸前轴封漏汽通过一只汽动调阀回收到四抽；轴封母管过剩汽通过三通转换阀至#1低加汽侧回收；高压部分轴封漏汽经冷凝器冷却后供低压轴封；由轴加建立的微真空抽出汽缸轴封漏汽加热凝泵出口的凝水，由于轴封汽参数取用困难，因此在热力计算中省略了轴封漏汽部分计算，考虑到与系统实际运行可能出现计算偏差，在热力系统计算中考虑了轴封漏汽的加热量，根据实际运行数据，取#1 低加进口水温为 37.5。汽轮发电机组的机械效率 M=0.995发电效率 g=0.995管道效率 p=0.995、原始数据整理锅炉出口蒸汽参数 P0=17.84Mpa,t0=540.6，取新汽压损为 3%，故汽机进口蒸汽参数为 P0=17.3Mpa,t0=538；高压缸排汽口压力 3.35Mpa，再热蒸汽压损为10%，中压缸进汽参数 Prh=3.02Mpa,trh=538；中低压缸联通管压损取 2%，低压缸进汽压力 PL=0.83Mpa,在焓熵图上作该机组的汽态线：4200021002200230024002500260027002800290030003100320033003400350036003700380039004000410042005.05.56.06.57.07.58.08.59.05.05.56.06.57.07.58.08.59.020002100220023002400250026002700280029003000310032003300340035003600370038003900400041004200h KJ/kgKJ/kgKJ/kgKGE352MW机组的汽态线0.005pDTc2440hDTc2371hc0.0049pc70t8 80.0309p82627h82675h798t770.075p7185t6 60.19p62841h60.41p5265t5 5 2995h5357t4 440.83p20.85p43177h4457t333376h323540hrh540t0 538t017.84P017.3P03388h03168h12990h212400t1302t23.35p26.77p1100MP机组各计算点参数表：5抽汽口加热器汽侧加热器水侧计 算 点设备pj MPatjhj kj/kgPj MPatsj tdj hdj kj/kgqj kj/kgQj Pwj MPatwj hwjkj/kgj kj/kgj kj/kg017.435403388.6017.35383388.61H 86.644002115.46.64282.3243.11052.72115.40.320.432821241.3209.112H 73.33022104.33.3239.2207.4886.42104.31.220.432381031.6163116.323.025383540.53H 61.754572608.81.75205.8180.9767.52608.84.020.43201.8868.6115.5118.94 小 汽 机 除 氧 器0.85 3.57 3177.4 0.781702579.40.78171.9728.2130.25H 40.412652995.40.398143.4120.3505.12490.31.62.15141.8598115.4169.56H 30.191852841.10.182117.393.1390.124512.62.15108.7482.6113.81157H 20.075982675.80.07290.690.2377.822983.42.1587.2366.888.412.38H 10.0397026270.03569.638.9162.92464.13.52.1566.1278.4119.5CC0.04932.523712.1537.5158.9注：考虑给水泵焓升；#3 低加进口水焓取 368.8kj/kg；#1 低加进口水温考虑轴封漏汽加热取 37.5系统热经济性计算系统热经济性计算各加热器抽汽放热量 qj的计算6kgkjhhqd/8 .21077 .10525 .3160111kgkjhhqd/6 .21084 .8862995222kgkjhhqd/8 .26135 .7673 .3381333kgkjhhqw/7 .25779 .5976 .3175544kgkjhhqd/8 .24951 .5059 .3000555kgkjhhqd/5 .24281 .4116 .2839666kgkjhhqd/3 .23018 .3771 .2679777kgkjhhqd/9 .23909 .1628 .2553888a) 各加热器中水的焓升 j的计算kgkjhhww/7 .2096 .10313 .1241211kgkjhhww/1636 .8686 .1031322kgkjhhDTww/5 .1159 .242 .7286 .868433kgkjhhww/3 .1309 .5972 .728544kgkjhhww/4 .1365 .4619 .597655kgkjhhww/7 .948 .3665 .461766kgkjhhww/4 .884 .2788 .366877kgkjhhnw/5 .1199 .1584 .278' 88注：hw7取 hw7+2kj/kgb)各加热器中疏水放热量的计算jkgkjhhdd/3 .1664 .8867 .1052212kgkjhhdd/9 .1185 .7674 .8863237kgkjhhwd/6 .1699 .5975 .767534kgkjhhdd/941 .4111 .505656kgkjhhdd/3 .338 .3771 .411767c) 抽汽系数的计算（不考虑加热器散热损失）j09947. 08 .21077 .20911 1q069496. 06 .21083 .16609947. 01632212 2q036497. 08 .26139 .118)069496. 009947. 0(5 .115)(33213 3q036998. 07 .25776 .169)036497. 0069496. 009947. 0(3 .130)(443214 4q除氧器进口凝结水份额75754. 0036998. 0036497. 0069496. 009947. 01143214c041422. 08 .24957 .13675754. 055 45qc027316. 05 .242894041422. 07 .9475754. 066564 6qc8786658' 74 7)()(wwdwwc hhhhhh 024731. 04 .2781 .2679)4 .2781 .411()027316. 0041422. 0()4 .2788 .368(75754. 0列方程组：' 747765776547765776546658765477646655577657765466)()()()()()()()()(wcdwcdwcdwcwcdddwchhhhhhhhhhhhhhkgkjhhhcdwc w/15.36875754. 08 .377)024731. 0027316. 0041422. 0(8 .366)024731. 0027316. 004142. 075754. 0()()(4776577654' 78通过以上对 hw7的修正计算，hw7初取值为 368.8kj/kg，修正值与初始值偏差很小，则取 hw7=368.8kj/kg887654 8)( qc032176. 024645 .119)025378. 0033544. 0035089. 075767. 0(597128. 0033182. 0024731. 0027316. 0041422. 003376. 0036998. 0036497. 0069496. 009947. 01187654321DTc再热汽份额 831034. 0069496. 009947. 01121rhd) 正平衡计算1kg 再热蒸汽吸热量kgkjhhqrhrh/6 .54729956 .35422各段抽汽作功不足量计算：kgkjh/4 .3145 .316009947. 011kgkjh/1 .2082995069496. 022kgkjh/4 .1233 .3381036497. 033kgkjh/5 .1176 .3175036998. 044kgkjhDT/2 .1076 .317503376. 04kgkjh/3 .1249 .3000041422. 055kgkjh/6 .776 .2839027316. 066kgkjh/3 .661 .2679024731. 0779kgkjh/7 .848 .2553033182. 088kgkjhcc/4 .14176 .2373597132. 01kg 蒸汽循环净功 Wi：4810hhhqhWDTcc jjjrhrhi 35.120421.10735.1417271.111608.4551 .33906 .317503376. 06 .2373597132. 0271.11166 .547831038. 01 .3390 1kg 工质循环吸热量 q0：100wrhrhhqhqkgkj/9 .26033 .12416 .547831038. 01 .3390实际循环效率：i4529. 09 .260389.2438.12040qWDTi ie) 反平衡计算广义冷源损失：)()()(88nc DTDTndnccnhhhhhhqkgkj/75.141478.7789. 008.1336) 1 .1362440(03376. 0) 1 .1369 .162(0333182. 0) 1 .1366 .2373(597132. 0则实际循环效率4567. 09 .260375.14149 .260300qqqn i反平衡计算结果与正平衡计算结果相比较，实际循环效率偏差仅为 0.37%，小于 0.5%的计算偏差要求，表明热力系统计算基本正确。f) 热经济指标计算：(1) 机组热经济指标计算8汽耗量htNNDgmi/709.1084995. 0995. 0)9 .2438.1204(352000360036000汽耗率hkwkgNDdd/08. 335200010847090 0热耗量rhrhwqDhhDQ)(1000hkj/1082. 26 .5471084709831038. 0)3 .12411 .3390(10847099热耗率hkwkjNQqd/07.80243520001082. 29 0 0汽轮发电机组绝对电效率4487. 007.8024360036000qe(2)全厂热经济指标计算全厂热耗量hkjQQpbcp/1912. 399. 0%7 .931082. 299 0全厂热耗率 kgkjNQqdcp cp/64.88633520001012. 39 标准煤耗率：hkwgbgmipbs cp/56.293995. 0995. 04567. 099. 0937. 0123123标煤全厂热效率4162. 04487. 099. 0937. 0epbcp
