锅炉原理任务书指导书

PAGEPAGE1锅炉原理课程设计说明书课程设计题目：SZL10－10－16锅炉设计设计日期：姓名：学号：学院：专业：指导老师：目录一、设计目的·················································3二、原始资料·················································31、锅炉规范··············································32、燃料特性··············································3三、确定锅炉整体结构·········································3四、辅助计算·················································41、漏风系数和过量空气系数·································42、理论空气量、理论烟气量·································53、气体及灰分的比焓·······································54、烟气特性表·············································55、焓温表·················································66、热平衡计算表···········································6五、炉膛结构设计和传热计算···································71、炉膛结构设计···········································72、炉膛传热计算···········································9六、冷却室结构设计和传热计算································101、冷却室结构设计········································102、冷却室传热计算········································11七、对流管束结构设计及计算··································111、对流管束结构设计······································112、对流管束热力计算······································12八、铸铁省煤器热力计算······································131、省煤器结构设计········································132、省煤器热力计算········································13九、主要参考资料············································14SZL10－10－16锅炉设计一、设计目的用《锅炉原理》课程学习时所掌握的理论和技术知识解决实际工程问题，进一步提高设计计算、制图和使用参考资料能力，培养学生创造能力。通过课程设计，掌握锅炉本体的设计内容、程序和基本原则，巩固所学理论知识，并运用这些知识解决实际问题。二、原始资料：1、锅炉规范锅炉蒸发量D＝10t/h；额定出口蒸汽压力P＝1.6MPa（表压）；额定出口蒸汽温度t＝204℃（饱和）；给水压力Pgs＝1.8MPa（表压）；给水温度tgs＝105℃；排污率Ppw＝5％；冷空气温度tlk＝30℃。2、燃料特性收到基成份（%）CarHarOarNarSarAarMar58.24.36.31.10.828.11.2煤的灰熔点（℃）DTSTHTFT煤的可磨系数K1500137014001.46干燥无灰基挥发份Vdaf=24.0%收到基低位发热量Qnet,ar=22825KJ/Kg三、确定锅炉整体结构锅炉整体布置形式，本设计为纵置式低压锅炉，含2个锅筒，本体受热面布置采用M型，不设置空气预热器。水冷壁形式为光管水冷壁，管子类型为Φ60×3.5，水冷壁和对流管束用同规格的管子。对流管束上下两端的连接方式为········省煤器为铸铁省煤器。链条炉排的型式为轻型链带式。采用的空气温度为30℃。锅炉（包含对流受热面）的主视图和左视图的简图如下图所示：四、辅助计算1、漏风系数和过量空气系数：序号受热面名称入口α'漏风Δα出口α"1炉膛1.30.11.42冷却室1.401.43对流管束1.40.11.54省煤器1.50.11.552、理论空气量、理论烟气量计算：序号名称符号单位计算公式数值1理论空气量V0Nm3/kg0.0889（Car+0.375Sar）+0.265Har-0.0333Oar6.1302RO2容积VRO2Nm3/kgVCO2+VSO2=0.01866（Car+0.375Sar）1.0923理论N2体积V0N2Nm3/kg0.79V0+0.008*Nar4.8524理论H2O体积V0H2ONm3/kg0.111*Har+0.0124*Mar+0.0161*V00.5915理论烟气量V0yNm3/kgV0y=VRO2+V0N2+V0H2O6.5343、气体及灰分的比焓：t/℃hco2/(kJ/m3)hN2/(kJ/m3)ho2/(kJ/m3)hH2O/(kJ/m3)hk/(kJ/m3)hfh/(kJ/m3)VRO2(Nm/Kg)VN20(Nm/Kg)VH2O0(Nm/Kg)100170130132151132811.0924.8520.5912003572602673042661691.0924.8520.5913005593924074634032641.0924.8520.5914007725275516265423601.0924.8520.5915009946646997956844581.0924.8520.59160012258048509698305601.0924.8520.5917001462948100411499786621.0924.8520.591800170510941160133411297671.0924.8520.591900195212421318152612828751.0924.8520.5911000220413921478172314379841.0924.8520.59111002458154416381925159510971.0924.8520.59112002717169718012132175312061.0924.8520.59113002977185319642344191413611.0924.8520.59114003239200921282559207615831.0924.8520.59115003503216622942779223917581.0924.8520.59116003769232524603002240318761.0924.8520.59117004036248426293229256720641.0924.8520.59118004305264427973458273121861.0924.8520.5914、烟气特性表：序号名称符号单位计算公式炉膛出口对流管束省煤器1平均过量空气系数αpj－(α'+α")/21.41.451.5252实际水蒸汽体积VH2ONm3/kgV0H2O+0.0161(α-1)V00.6300.6350.6433实际烟气量VyNm3/kgV0y+1.0161(α-1)V09.0269.3379.8054RO2容积份额rRO2－VRO2/Vy0.1210.1170.1115水蒸汽容积份额rH2O－VH2O/Vy0.06980.06800.06566三原子气体容积份额rq－rRO2+rH2O0.1910.1850.1777无因次飞灰浓度μfh－1-Aar/100+1.306*αV011.92812.32812.9295、焓温表：t/℃h0y(KJ/Kg)h0k(KJ/Kg)α=1.4△hyα=1.45△hyα=1.55△hy1001078.9966.71465.61562.31610.62002181.81948.12961.11495.53155.91593.63253.31642.73003320.32951.44500.91539.84796.01640.24943.61690.34004493.53969.46081.31580.46478.21682.26676.71733.15005694.35009.37698.01616.78198.91720.78449.41772.76006927.76078.59359.11661.19966.91768.010270.91821.57008196.27162.411061.21702.111777.41810.512135.51864.78009487.68268.312794.91733.713621.71844.314035.11899.690010800.59388.814556.01761.115494.91873.215964.31929.2100012134.910523.916344.51788.517396.91902.017923.11958.8110013486.911681.018159.31814.819327.41930.519911.51988.4120014854.612838.219989.91830.621273.71946.321915.62004.1130016244.314017.221851.21861.323252.91979.223953.82038.2140017638.615203.723720.11868.925240.51987.526000.72046.9150019044.716397.425603.71883.627243.42002.928063.32062.6160020467.017598.427506.41902.729266.22022.830146.22082.9170021893.318799.529413.11906.731293.02026.832233.02086.8180023329.320000.631329.51916.433329.62036.634329.62096.66、热平衡计算表：序号名称符号单位计算公式或数据来源结果1收到基低位发热量Qnet,arKJ/Kg228252机械不完全燃烧热损失q4%《标准》P2545.53化学不完全燃烧热损失q3%查《标准》P254q3在0.5%-1%间0.84散热损失q5%查《锅炉》P155，图8-31.75灰渣焓(cϑ)hzKJ/Kg按照600℃。《燃烧》P685606灰渣物理热损失q6%Q6=（1-afh）（Cϑ）hzAar/Qnet,ar0.5527排烟温度ϑpy℃工业锅炉在150℃-200℃间1708排烟焓hpyKJ/Kg查焓温表2107.009冷空气温度tlk℃锅炉规范已知3010冷空气焓h0lkKJ/Kg查焓温表376.211排烟热损失q2%(Ipy-αpyI0lk)(100-q4)/Qnet,ar6.3112反平衡热效率η％100-(q2+q3+q4+q5+q6)85.13913干饱和蒸汽焓h"KJ/Kg1.7Mpa,204℃《水和水蒸气热力性质图表》2794.9114蒸汽湿度W％≤3%215汽化潜热rKJ/Kg1925.9316给水焓hgsKJ/Kg1.9Mpa,105℃439.6117排污焓hpwKJ/Kg1.7Mpa,饱和水867.518锅炉有效吸热量QKJ/hD（h"-hgs-rw/100）+Dρ（hpw-hgs）2.34E+0719燃煤量BKg/hQ/ηQnet,ar=2520/(0.768×2.4720)1203.220计算燃煤量BjKg/hB(1-q4/100)1137.021保热系数ϕ—η/(η+q5)0.980五、炉膛结构设计和传热计算1、炉膛结构设计：序号名称符号单位公式或数据来源结果1前墙总面积Fqm2炉膛宽度×前墙延伸高度12.82前墙曝光水冷壁面积Fq1m25.83管径dmm604管子根数根175管子节距smm1526前墙水冷壁角系数xq1s/d＝0.71e/d＝0.50.71《锅炉》P1747前墙覆盖耐火涂料的水冷壁面积Fq2m27.008炉顶总面积Fdm28.519炉顶曝光水冷壁面积Fd1m26.5610管径dmm6011管子根数根3412管子节距smm72.6013炉顶水冷壁角系数xd1s/d＝0.97e/d＝0.50.97《锅炉》P17414侧墙总面积Fcm29.5715侧墙曝光水冷壁面积Fc1m25.3716管径dmm0.9717管子根数根3418管子节距smm72.6019侧墙水冷壁角系数xc1s/d＝0.97e/d＝0.50.97《标准》P293线算图120侧墙覆盖耐火涂料的水冷壁面积Fc2m24.521后墙总面积Fhm2炉膛宽度×后墙延伸高度19.5422后墙曝光水冷壁面积Fh1m2023后墙水冷壁角系数xh1s/d＝0e/d＝无0《标准》P293线算图124后墙覆盖耐火砖的水冷壁面积Fh3m2025炉膛出口烟窗面积Fckm2出口烟窗高度×出口烟窗宽度0.6326炉排面积Rm2长12宽2.412此处核对炉排面积热负荷(《锅炉课件》第四章有具体要求)qR对1类烟煤范围是550-800KW/m2，II类是700-1050KW/m2qR=BQar,net/3600/R635.7227炉膛容积Vlm330.62此处核对炉膛容积热负荷(《锅炉课件》第四章有具体要求)对抛煤机链条炉qV范围是290-470KW/m2qv=BQar,net/3600/V1249.142859.99Flm2Fq＋Fd＋2×Fc＋Fh59.992937.53Hfm2ΣFixi＝(Fq1xq1＋Fq2)＋Fd1xd1＋2(Fc1xc1＋Fc2)＋(Fh1xh1＋Fh3)＋Fck37.53300.6ζ1《标准》P38表6-20.6310.2ζ2《标准》P38表6-20.2320.1ζ3《标准》P38表6-20.13316.12ψFlm2ΣFixiζi＝(Fq1xq1ζ1＋Fq2ζ2)＋Fd1xd1ζ1＋2(Fc1xc1ζ1＋Fc2ζ2)＋(Fh1xh1ζ1＋Fh3ζ3)＋Fckζ116.12340.269ψ(ΣFixiζi)/Fl0.269351.531sm3.6×Vl/(Fl＋R)1.531360.200ρR/Fl0.2002、炉膛传热计算：序号名称符号单位公式或数据来源结果1燃料输入热QrKJ/Kg近似等于燃料收到基低位发热量228252空气带入炉内的热量QkKJ/Kg(α"-△αl)h0rk+△αlh0lk=α"lh0lk526.683炉膛有效放热量QlKJ/KgQr*(100-q3-q4-q6)/(100-q4)+Qk23025.24理论燃烧温度ϑa℃按Ql查焓温表1600.05理论燃烧温度TaKϑa＋273＝1873.06炉膛出口烟温ϑ”l℃先假设，再校核10007炉膛出口烟温T”lKϑ”l＋273＝12738炉膛出口烟气焓h”lKJ/Kg按ϑ”l查焓温表17849.79烟气平均热容量VCpKJ/KgK(Ql－h”l)/(Ta－T”l)＝8.6310三原子气体辐射减弱系数kqrq1/(mMPa)10((0.78+1.6*rH20)/sqrt(10*p*rq*s)-0.1)(1-0.37*T”l/1000)rq1.56411灰粒辐射减弱系数khμh1/(mMPa)10*4300*1.3*μh/power（（T”l2*dh2），1/3）0.30412焦炭粒子辐射减弱系数10C1C21/(mMPa)烟煤Ⅰ类C10.15层燃炉C20.030.1513火焰辐射减弱系数k1/(mMPa)kqrq＋khμh＋10C1C2＝2.01814炉膛绝对压力pMPa0.115火焰黑度ahy1－e－kps＝0.26616炉膛黑度al(ahy+(1-ahy)*ρ)/(1-(1-ahy)*(1-ψ)(1-ρ))0.72317炉膛出口烟温ϑ”l℃Ta/(M*power(2.041*0.0000001*al*ψFl*ta3/ϕ/Bj/VCp,0.6)+1)-273831.2718炉膛出口烟气焓h”lKJ/Kg按ϑ”l查焓温表11168.6919炉膛辐射换热量QfKJ/Kgϕ(Ql-hl")11624.44六、冷却室结构设计和传热计算1、冷却室结构设计：序号名称符号单位公式或数据来源结果1冷却室前墙面积Fqm25.242冷却室顶棚面积Fdm21.963冷却室侧墙面积Fcm21.544冷却室侧墙包墙管面积Fc1m2Fc1=Fc1.545管径dmm606管子根数根107管子节距smm70.008冷却室侧墙包墙管角系数xc1s/d＝0.95e/d＝0.50.95《标准》P293线算图19冷却室后墙面积Fhm26.2610冷却室后墙包墙管面积Fh1m26.2611管径dmm6012管子根数根3713管子节距smm70.2714冷却室后墙包墙管角系数xh1s/d＝0.95e/d＝0.50.56《标准》P293线算图115冷却室下平面面积Fxm24.3216冷却室容积Vlqm34.86617冷却室墙总面积Flqm2Fq＋Fd＋2×Fc＋Fh＋Fx20.8618冷却室辐射受热面积Hfm2ΣFixi＝2Fc1xc1＋Fh1xh18.8719有效辐射层厚度sm3.6×Vlq/Flq0.8402、冷却室传热计算：序号名称符号单位公式或数据来源结果1冷却室进口烟温ϑ'℃炉膛出口烟温831.272冷却室进口烟焓h'KJ/Kg炉膛出口烟焓11168.693冷却室出口烟温ϑ"℃先假设，再校核7504冷却室出口烟焓h"KJ/Kg查焓温表9999.255烟气侧放热量QrpKJ/Kgϕ*(h'y-h"y+△αhk0)1146.556管内工质温度t℃锅炉出口压力对应的饱和水温度2037对数平均温差Δt℃(ϑ'-ϑ")/㏑((ϑ'-t)/(ϑ"-t))586.708平均烟温ϑ℃t＋Δt789.709管壁灰层表面温度tb℃t＋8028310不含灰气体辐射减弱系数k1/(mMPa)10((0.78+1.6*rH20)/sqrt(10*p*rq*s)-0.1)(1-0.37*(ϑ+273)/1000)rq2.41911烟气黑度ay1－e－kps0.18412辐射放热系数αfKW/(m2℃)《标准》P314线算图19，αHayCr158.4013冷却室传热量QcrKJ/Kgαf(ϑ－tb)Hf/Bj1096.0714相对误差Δ％abs(Qrp－Qcr)/Qrp×100％（要求不超过5％）0.04七、对流管束结构设计及计算1、对流管束结构设计：序号名称符号单位公式或数据来源结果1管径dmm选定管径602平均管长mm选定18003横向管束根数n1'根154纵向管束根数n2'根325横向节距S1mm146.66666676纵向节距S2mm78.1257横向相对节距σ1S1/d2.448纵向相对节距σ2S2/d1.309区段I受热面积H1m2n1*n2'*π*d*l86.8610区段II受热面积H2m2n2*n2'*π*d*l76.0011管束总对流受热面积Hzsm2H1+H2162.8612区段I流通断面积F1m2(S1-d)*l*(n1-1)1.09213区段II流通断面积F2m2(S1-d)*l*(n2-1)0.93614烟气流通截面积Fym(H1+H2)/(H1/F1+H2/F2)1.01315烟气容积Vym36.85016辐射层厚度Sm0.9*d*(4*S1*S2/π*d2-1)0.1652、对流管束热力计算：序号名称符号单位公式或数据来源结果1进口烟温ϑ'℃冷却室出口烟温7502进口烟气焓h'KJ/Kg冷却室出口烟焓9999.253出口烟温ϑ”℃先假定，在校核4004出口烟气焓h"KJ/Kg查焓温表5430.85烟气侧放热量QrpKJ/Kgϕ*(h'y-h"y+△αhk0)4515.906管内工质温度t℃p=1.6MPa的饱和温度2037对数平均温度差Δt℃(ϑ'-ϑ")/㏑((ϑ'-t)/(ϑ"-t))342.728平均烟温ϑpj℃t＋Δt545.729烟气流速wym/sBj*Vy*(ϑpj+273)/Fy/273/36006.4010基准对流放热系数αHw/(m2*℃)《标准》P3045011节距修正系数Cs《标准》P3040.90管排修正系数Cz《标准》P3050.96烟气物性修正系数Cφ《标准》P3050.9712对流放热系数αdw/(m2*℃)α0*Cs*Cz*Ccp41.9013管子灰壁温度thb℃t+6026314基准辐射放热系数αHw/(m2*℃)《标准》P31465.61715修正系数Crw/(m2*℃)《标准》P3140.9516三原子气体总分压力pq1/m.Mpap*rq0.01817三原子气体辐射减弱系数kq1/m.Mpa((7.8+16*rH2O)/3.16/sqrt(pq*s)-1)*(1-0.37*(ϑpj+273)/1000)34.8118烟气的辐射总厚度kpskq*rq*p*s0.10619烟气黑度ay1-exp(-kps)0.100720管间辐射放热系数αf'w/(m2*℃)αH*Cr*ay6.2821利用系数ξ《标准》P660.8522烟气侧放热系数α1w/(m2*℃)ξ*(αf'+αd)40.9523热有效系数ψ《标准》