WNS12-1.25-Q热力计算

序号名称符号单位计算公式及数据来源结果一设计规范1额定蒸发量Dt/h给定122额定蒸汽压力PMPa给定1.253额定饱和蒸汽温度tbq°C查表193.44给水温度tgs°C除氧器出水温度1045冷空气温度tlk°C给定30二燃料特性天然气1甲烷CH4%952氢气H2%13其它成分CmHn%2.44一氧化碳CO%0.15二氧化碳CO2%0.56氮气N2%17水分Wy%08应用基低位发热量QdwyKJ/Nm335588三燃烧产物计算1理论空气量V°Nm3/Nm³0.0476[0.5CO+0.5H2+∑(m+n/4)CmHn]9.41292氮气理论容积V°N2Nm3/Nm³0.79V0+0.01Ny7.4461913三原子气体容积VRO2Nm3/Nm³0.01(CO2+CO+∑mCmHn)1.0044水蒸气理论容积V°H2ONm3/Nm³0.01（H2+∑n/2CmHn）+0.0161Vy2.07788368四1平均过量空气系数αpj取定1.152实际水蒸汽容积VH20Nm3/m³V0H2O+0.0161(αpj-1)V02.100615833烟气总容积VyNm3/m³VRO2+V0N2+VH2O+(αpj-1)V011.96274184RO2气体容积份额rRO2VRO2/Vy0.083927255水蒸汽容积份额rH2OVHO2/Vy0.175596526三原子气体容积份额rqrRo2+rH2o0.267节能器漏风系数Δα取定0.18省煤器出口处过量空气系数αsαpj+Δα1.25各受热面烟道中烟气特性表9省煤器平均过量空气系数αs(αpj+αs)/21.210省煤器处实际水蒸汽容积VH20Nm3/m³VoH2O+0.0161(αs-1)Vo2.1081932111省煤器处烟气总容积VyNm3/m³VRO2+VoN2+VH2O+(αs-1)Vo12.440964212省煤器处RO2气体容积份额rRO2VRO2/Vy0.0807011413省煤器处水蒸汽容积份额rH2OVH2O/Vy0.16945577五IOy(KJ/Nm3)°C3+5+7(Cθ)KVO(Cθ)KI△I123456789101112100170170.68130968.00483151313.76043491452.44531321242.5031638.821200358359.4322601936.00966304631.67663722927.11832662503.8313302.6931663.872300559561.2363922918.90687463962.06014164442.2034033793.3995011.2131708.52400772775.0885273924.142666261300.7551815999.98585425101.7926765.2551754.042500996999.9846644944.270827951651.9175227596.17236846438.4248561.9361796.68160012231227.8928045986.737569672009.3135149223.94318307812.70710395.851833.91370014611466.8449467044.0966911472383.33257510894.2739809224.64212277.971882.1280017041710.81610938138.6867613362776.0525912625.555113010636.5814221.041943.07290019511958.80412439255.6154115243166.69472114381.114128112057.9216189.81968.761100022022210.808139410379.990317253584.3493416175.148143613516.9218202.692012.883110024582467.832154511504.365119264002.00395817974.201159515013.5820226.242023.551120000000013000000001400000000150035043518.016216516121.003527805776.51661725415.536224021084.928578.27160037683783.072232417304.947930026237.80679327325.827240322619.230718.712140.436170040364052.144248318488.892332286707.40850329248.445256724162.9132872.882154.175180043044321.216264219672.836634587185.32174831179.374273025697.2235033.962161.075190045724590.288280520886.565836897665.31287733142.167289727269.1737232.542198.585200048444863.376296422070.510139278159.84919235093.735306528850.5439421.322188.774210051165136.464312823291.685441628648.15185637076.301323230422.4941639.682218.35922000000000VRO2=1.598Nm3/kgVON2=8.822Nm3/kgVOH2O=1.677Nm3/kg(Cθ)N2(Cθ)H2OVOH2O×(Cθ)H2Oθ(Cθ)RO2VRO2×(Cθ)RO2VON2×(Cθ)N2焓温表IOK(KJ/Nm3)Iy=IOy+(α-1)IOk(KJ/Nm3)序号名称符号单位计算公式与数据来源结果六锅炉热平衡计算1排烟温度θpy℃假设1632排烟焓IpyKJ/Nm3查温焓表2687.0602483排烟处过量空气系数αpy取定1.154冷空气温度tlk℃设计给定305冷空气理论热焓IlkoKJ/Nm3查温焓表372.756机械不完全燃烧损失q4%取定07排烟热损失q2%（Ipy-αpj*I0lk）（100-q4）/Qydw6.3459529848散热损失q5%取定0.59化学不完全燃烧损失q3%取定0.510锅炉总热损失∑q%q2+q3+q4+q57.34595298411锅炉热效率η%1-∑q92.6540470212给水焓igsKJ/Kg查水、水蒸气表435.9513饱和水焓ibhKJ/Kg查水、水蒸气表822.4914饱和汽焓ibqKJ/Kg查水、水蒸气表2786.615锅炉排污率ρ%取定516蒸汽带水率w%取定417汽化潜热rKJ/Kgibq-ibh1964.1118保温系数φη/（η+q5）0.99463254719锅炉有效利用热Q1KJ/hD(ibq-igs-wr/100)+Dρ(ibh-igs)27496951.220燃料消耗量BNm3/h100Q1/(ηQydw)833.904980121计算燃料消耗量BjNm3/hB(1-q4)/100833.904980122炉膛容积热负荷qvMW/m3BQdw/(3600*1000Vf）0.745117593七炉膛计算a2燃烧器火焰直径dhmBj^0.31*(0.147-0.02*(1-EXP(-20*(apj-1)))1.0297733683炉胆直径dm结构设计1.44燃烧器火焰长度LhymBj^0.5*(0.182-0.02*(1-EXP(-16*(apj-1)))4.7305348985炉胆长度Lm按结构5.7096炉胆辐射受热面积Hf1m23.14*d*L25.0967647炉膛尾部长度L1m结构设计0.68炉膛尾部直径D1m结构设计2.29烟管外径dwm结构设计0.063510第一对流烟管数量n1假定144炉胆结构特性计算11检修孔直径djm结构设计0.412炉膛尾部辐射受热面Hf2m23.14*D1*L1+2*3.14*D1^2/4-3.14*d^2/4-n1*3.14*dw^2/4-3.14*dj^2/49.6235944613炉膛总辐射受热面积FLm2Hf1+Hf234.7203584614炉胆有效容积VL1m3L*3.14*d^2/48.783867415炉膛尾部容积VL2m3L1*3.14*D1^2/42.2796416炉膛总容积VLm3VL1+VL211.063507417炉膛有效辐射层厚度Sm3.6*VL/FL1.147126021b1空气带入燃烧室热量QkKJ/Nm3αpj*I0LK428.66252燃烧室每Nm³燃料输入热量QLKJ/Nm3Qydw*（100-q3）/100+QK35838.72253绝热燃烧温度θjr℃查焓温表1836.3196034绝热燃烧绝对温度TjrKθjr+2732109.3196035炉膛出口假定温度θlc℃先假定后校核11006炉膛出口烟气焓IcyKJ/Nm3查焓温表20226.237387烟气放热量QrpKJ/Nm3φ（Ql-Il）15528.685848出口绝对温度TlcKθlc+27313739受热面灰污系数ξ燃气按0.7-0.8选取0.7510有效辐射受热面Hfsm2ξ*Hf26.0402688511受热面平均热有效系数ψpjHfs/Hf0.7512三原子气体总分压力PqMPa0.1013*rq0.02628975813三原子气体辐射力m.MpaPq*S0.03015766514三原子气体辐射减弱系数Kp1/(m.Mpa)10.2*(0.78+1.6*RH2O)/(10.2PqS)^0.5-0.1)*(1-0.37*Tlc/1000)7.77070176115碳黑颗粒辐射减弱系数kj1/(m.Mpa)0.306*（2-αpj）*（1.6*Tlc/1000-0.5）*Cy/Hy1.27371338316火焰发光黑度afg1-e^(-(Kpr∑+Kth)*p*s)0.31774830917火焰不发光黑度aq1-e^(-Kp*rq*0.1013*s)0.20891212318系数m查《锅炉原理及计算》P2740.219火焰黑度ahmafg+（1-m）aq0.2306793620炉膛系统黑度aLah/（ah+（1-ah）*ψpj）0.28561096221火焰中心高度系数M0.53-0.6之间选取0.622烟气平均热容积V-cKJ/（Kg.℃）（QL-Icy）/（θjr-θlc）21.2034082323炉膛出口烟温tlc℃Tjr/（M*（5.7*10-11*aL*ψpj*Hf*Tjr^3/（φ*Bj*V-c））^0.6+1)-2731105.22305824计算与假设值差Δt℃θlc-tlc-5.223057575燃烧室热力计算25结论Δt允许范围-100＜Δt＜100合格八第一对流管束计算1烟管规格：外径dm锅炉结构0.06352厚度tm锅炉结构0.00353长度lm锅炉结构5.6754数量n锅炉结构1445螺纹高度em烟管结构0.0026螺纹节距sm0.047比值e/d0.0196~0.06820.035398238比值s/d0.324~0.920.7079646029烟管内径dimd-2t0.056510烟管受热面积Hm2πdiln144.97945211进口烟温θ'℃1105.22305812进口烟焓I'KJ/Nm3查温焓表20320.703713出口烟温θ℃假定32614出口烟焓IKJ/Nm3查温焓表5467.26368415烟气侧放热量QrpKJ/Nm3φ(I'-I)14773.7148716烟管流通截面积Fm2nπdi2/40.3608519417平均水温ts℃tbq193.418大温差△td℃θ'-ts911.823057