余热锅炉 计算表(最新)

100一小时含尘量120000g0.1810.034水煤气温度每22.4立方米水煤气焓值kjH2CO1002815.22884.92005667.85804.93008520.48724.940011424.911646.250014348.614601.460017278.617612.770020215.120692.680023166.423845.990026141.927070.6水煤气理论焓值kj（每22.4立方米）水煤气理论焓值（不含灰的焓）kj/m32891.4508129.082635994.405267.607379097.3592406.1321112300.6398549.1357115602.6041696.5448319002.4709848.3245922499.36711004.43626091.70561164.808329776.58621329.3119本锅炉立式布置，烟气从锅炉顶部进入，依次通过过热器，蒸发器，省煤器，最后排出，由于水煤气温度低，炉口辐射热量忽略，采用全密封结构，，锅炉漏风系数很小，暂忽略漏风损失，烟气成分：H2%18.10.181CO2%17.50.175CH4%0.40.004N2%380.38H2O%22.60.226CO%3.40.034热平衡1进炉烟气量2入炉烟温3入炉烟焓4出炉烟温5出炉烟焓6烟气带入热功率kj/h7烟尘带入的热功率8入炉总热功率9漏风系数10烟气带走的热功率kj/h11烟尘带走的热功率水煤气成分H218.1%CO3.4%CH40.4%CO217.5%H2O22.6%N238%热值含尘量10g/m3经济型分析命题：余热回收利用煤化工水煤气余热去加热水蒸气800℃12000Nm3/h冷却到100℃另一工艺需水蒸气400℃1MPa设计换热器蒸汽流量？常规水20℃12散热损失kj/h13汽化吸热功率kj/h14给水温度15过热蒸汽焓kj/kg16给水焓kj/kg17排污率18饱和水焓kj/kg19产汽量t/h20给水压力Mpa21锅筒压力MPa22饱和温度23饱和蒸汽焓kj/kg24饱和水焓kj/kg25省煤器出口水温26省煤器出口焓kj/kg27过热器吸热量kj/h28省煤器吸热量kj/h29蒸发受热面吸热量kj/h0.0040.1750.2260.38CH4CO2H2ON23293.52470.83287.52882.36691.75951.86626.85803.110089.99432.89966.18723.913888.913366.71335711640.418225.317668.916830.214580.223151.422271.320405.917564.228659.12712024096.220606.634704.632172.627907.223715.241232.637395.931842.526891.8灰的焓kj/kg每m3灰的焓kj水煤气的理论焓值kj/m358.60.4688129.551425117.20.9376268.5449661175.81.4064407.5385071234.41.8752551.01090542932.344698.8888259351.62.8128851.1373938410.23.28161007.717631468.83.75041168.558686527.44.21921333.531084本锅炉立式布置，烟气从锅炉顶部进入，依次通过过热器，蒸发器，省煤器，最后排出，由于水煤气温度低，炉口辐射热量忽略，采用全密封结构，，锅炉漏风系数很小，暂忽略漏风损失，120008001168.559100129.551414022405.29298.938904814022704.2301554617.1566400水煤气成分H218.1%CO3.4%CH40.4%CO217.5%H2O22.6%N238%热值含尘量10g/m3经济型分析命题：余热回收利用煤化工水煤气余热去加热水蒸气800℃12000Nm3/h冷却到100℃另一工艺需水蒸气400℃1MPa设计换热器蒸汽流量？常规水20℃05001000150012345678914022.7042312454064.420.888135713203214.58502782.053.869570035无排污1.24481.18180.60722782.05794.8475170.60727181720965.0622519067.8328214031.531水煤气成分H218.1%CO3.4%CH40.4%CO217.5%H2O22.6%N238%热值含尘量10g/m3经济型分析命题：余热回收利用煤化工水煤气余热去加热水蒸气800℃12000Nm3/h冷却到100℃另一工艺需水蒸气400℃1MPa设计换热器蒸汽流量？常规水20℃9系列1锅炉额定蒸发量t/h给定3.869570035烟气温度℃给定800烟气热焓KJ/Nm³查表1168.559烟气流量Nm³/h给定12000排烟温度℃100排烟焓KJ/kg查表129.5514烟气放热量(KW)KWD(i``-i`)/360014022405.29有效热KW系数=0.9514022704.22给水温度℃给定20给水焓KJ/kg查表85省煤器出口饱和水温度℃P=1.18MPa170.6072省煤器出口饱和水热焓KJ/kg查表718蒸发器进口饱和水温度℃20饱和蒸汽的温度℃180.6072饱和蒸汽焓KJ/kg查表2782.05过热器进口饱和蒸汽温度℃180.6072过热器出口过热蒸汽温度℃400过热蒸汽焓KJ/kg查表3214.5省煤器吸收热量kj/h2519067.832蒸发器吸收热量kj/h8214031.531过热器吸收热量kj/h1720965.062总吸热量kj/h12454064.42烟气成分：H2%18.1CO2%17.5CH4%0.4N2%38H2O%22.6CO%3.4序号名称符号单位1管子规格d×δmm×mm2横向节距S1mm3纵向节距S2mm4布置方式5横向排数N16纵向排数N27管束直段长度lzmm8管束弯段长度lwmm9管束长度lmm10受热面积H1m211炉膛宽度amm12炉膛深度bmm13烟气流通截面积Fsh214蒸汽流通截面积fm215蒸汽流量Dt/h16蒸汽进口温度t′℃17蒸汽进口焓i′kJ/kg18蒸汽出口温度t``℃19蒸汽出口焓i``kJ/kg20蒸汽平均温度tav℃21进口烟温T`℃22进口烟焓I`kJ/m323平均烟温Tav℃24烟气标况流量Vy25烟气工况流量Vy'26蒸汽吸热量QxiKW27烟气放热量Qh.bKW28出口烟焓I``kJ/Nm329出口烟温T``℃30烟气平均速度Wym/s31管壁温度tb32边界层平均温度tb133管排修正系数C34管子排列系数n2hm/3hNm/335烟气导热率b136传热系数α0kW/m2.℃37实际传热系数38对数平均温差Δtm℃39对流吸热功率kj/h40积灰系数41总吸热功率kj/h42应吸热功率kj/h43误差%dt0.1810.1750.0040.380.2260.034当排烟温度为100℃时计算公式或来源数值32*3.532100总图75错列304总图2750总图75lz+lw2825nπdl/1000/100034.0790总图2740.00总图1300.000.8500nπdn^2/40.0147给定3.87p=1.18MPa180.61查焓温表(P=2.5)2782.05给定400.00查焓温表(P=2.55)3214.50tav=(t’+t”)/2290.30给定800.001168.5590(T`+T``)/2450.0012000.0031780.22D(i``-i`)516.541.1Qxi542.36I`-Qy/φ1023.70712.00Vy'/3600/Fsh210.39180.6072+212023260.140.690.040.07410.0296462.591681559.55选取0.401681559.551720965.06(2.29)11bwCdnnw)ln(tTtTtm序号名称符号单位1管子规格d×δmm×mm2横向节距S1mm3纵向节距S2mm4布置方式5横向排数N16纵向排数N2管束与水平面的夹角°9管束长度lmm10受热面积H1m211炉膛在管中心线平面的宽度amm12炉膛深度bmm13烟气流通截面积Fsh214蒸汽流通截面积fm216饱和水进口温度t′℃17饱和水进口焓i′kJ/kg循环倍率18出口饱和蒸汽温度t``℃19饱和蒸汽出口焓i``kJ/kg20介质平均温度tav℃21进口烟温T`℃22进口烟焓I`kJ/Nm325平均烟温Tav℃26烟气标况流量VyNm³/h27烟气工况流量Vy'm³/h28蒸汽吸热量QxiKW烟气放热量Qh.bKW23出口烟焓I``kJ/Nm324出口烟温T``℃36烟气平均速度Wym/s37管壁温度tb38边界层平均温度tb139管排修正系数C40管子排列系数n41烟气导热率b142传热系数α0kW/m2.℃43实际传热系数44对数平均温差Δtm℃45对流吸热功率kj/h46积灰系数47总吸热功率kj/h48应吸热功率kj/h49误差%505152535455565758596061d2626364当排烟温度为100℃时计算公式或来源数值42*3.542选定100总图90错列2518102540nπdl/1000/1000150.81总图2780总图13000.95nπdn^2/40.14p=1.18MPa180.6072查焓温表(P=1.18)2782.05选取40给定201.6072查焓温表(P=2.55)3214.5tav=(t’+t”)/2191.1072给定7121023.70(T`+T``)/2481.521200033165.49D(i``-i`)8214031.531.1Qxi8297001.55I`-Qy/φ339.47251.039.73180.6072+21201.6072341.560.150.690.0390.080.06213.176954024.79选取0.66954024.798214031.53(15.34)11bwCdnnw)ln(tTtTtm63CO2的辐射传热功64SO2的辐射传热功65H2O的辐射传热功67QCO2W·m-2查表########QSO2W·m-2查表10.0000QH2OW·m-2查表########序号名称符号1管子规格d×δ2横向节距S13纵向节距S24布置方式5横向排数N16纵向排数N27管束长度l8受热面积H19炉膛宽度a10炉膛深度b11烟气流通截面积Fsh212蒸汽流通截面积f13给水流量D14给水温度t′15给水焓i′16饱和水出口温度t``17水平均温度t18饱和水出口焓i``19进口烟温T`20进口烟焓I`21平均烟温Tav22烟气标况流量Vy23烟气工况流量Vy'24水吸热量Qxi25烟气放热量Qh.b26出口烟焓I``27排烟温度T``28烟气平均速度Wy29管壁温度tb30边界层平均温度tb131管排修正系数C32管子排列系数n33烟气导热率b134传热系数α035对数平均温差Δtm36总吸热功率37应吸热功率38误差2626364当排烟温度为100℃时单位计算公式或来源数值mm×mm32*3.532mm选定88mm总图60错列3618mm2540m2nπdl/1000/1000165.47mm总图2740mm总图13000.64m2nπdn^2/40.018t/h给定3.869570035℃给定20kJ/kg查焓温表85℃给定170.6072℃(t`+t``)/295.3036kJ/kg718℃251.03kJ/Nm3339.47℃(T`+T``)/2175.52Nm³/h