加热炉热力计算-终版2

原始数据,,,,,,,

热负荷,Q,KW,600,燃料的低发热值,QL,KJ/kg或KJ/m3,35087

被加热介质比热容,Cp,KJ/（kg•K）,4.18,空气中水蒸汽含量,da,g/m3,0

介质运动粘度,νt1,mm2/s,0,送风机的风压,Pa,kPa,2.5

介质运动粘度,νt2,mm2/s,0,送风机的全压效率,ηa,%,100

原油含水率,Φ,,给定,送风机的机械效率,ηm,%,100

被加热介质的入口温度,ti,℃,40,送风机的电机效率,ηe,%,100

被加热介质的出口温度,to,℃,80,火嘴风压,Pbu,kPa,0

燃料气组成,CH4,%,100,火嘴机械效率,ηbu,%,100

,C2H6,%,0,转杯火嘴系数,ε,,1.1

,C3H8,%,0,排烟温度,tOU,℃,200

,CO,%,0,环境大气压,Pb,kPa,101.3

,H2S,%,0,,,,

,H2,%,0,,,,

,O2,%,0,,,,

,H2O,%,0,,,,

,CO2,%,0,,,,

,N2,%,0,,,,

燃烧计算（气体燃料),,,,,,,

燃料气密度,ρg,Kg/m3,0.7157,,,,

燃料气的折合分子量,M,,16,,,,

环境温度,ta,℃,40,,,,

燃料的初压力,Pf,kPa(绝压),,,,,

燃料中水蒸气的饱和压,Psf,kPa(绝压),7.375,,,,

燃料气中的饱和水含量,df,g/m3,0,,,,

应用基的低发热量,QLU,KJ/kg或KJ/m3,35087,,,,

理论空气量,Vath,m3/m3,9.5556,,,,

过剩空气系数,α,1.05～1.1,1.075,,,,

实际空气量,Va,m3/m3,10.27227,,,,

烟气中CO2容积,VCO2,m3/m3,1.003081681,,,,

烟气中SO2容积,VSO2,m3/m3,0,,,,

烟气中干三原子气体容积,VRO2,m3/m3,1.003081681,,,,

烟气中O2的容积,VO2,m3/m3,0.149999031,,,,

烟气中N2的容积,VN2,m3/m3,8.119202208,,,,

烟气中水蒸汽的容积,VH2O,m3/m3,2,,,,

实际烟气容积,Vsm,m3/m3,11.27228292,,,,

烟气的质量,msm,kg/m3,13.99774511,,,,

烟气的密度,ρsm,kg/m3,1.241784402,,,,

干三原子气体份额,rRO2,,0.08898656,,,,

水蒸汽份额,rH2O,,0.177426349,,,,

氮气份额,rN2,,0.720280201,,,,

氧气份额,rO2,,0.01330689,,,,

三原子气体份额,rt,,0.266412909,,,,

烟气的总压力,Psm,kPa(绝压),102,,,,

干三原子气体的分压力,PRO2,kPa,9.076629125,,,,

水蒸汽的分压力,PH2O,kPa,18.09748757,,,,

氮气的分压力,PN2,kPa,73.46858051,,,,

氧气的分压力,PO2,kPa,1.357302799,,,,

三原子气体的分压力,Pt,kPa,27.17411669,,,,

炉效及燃料用量,,,,,,,

燃料气的显热,Qf,KJ/m3,60,,,,

空气的显热,Qa,KJ/m3,533.7471492,,,,

送风机输入的热量,Qpa,KJ/m3,25.680675,,,,

引风机输入的热量,Qpb,KJ/m3,0,没有引风机,,,

转杯火嘴输入的热量,Qpd,KJ/m3,0,,,,

辅机输入的热量,Qp,KJ/m3,25.680675,,,,

加热炉系统输入的热量,Qis,KJ/m3,35706.42782,,,,

加热炉本体输入的热量,Qi,KJ/m3,35680.74715,,,,

系数A1,A1,,15.46582635,,,,

系数B1,B1,,0.001895806,,,,

排烟的焓,IOU,KJ/m3,3168.99751,可查表,,,

排烟热损失率,q2,%,7.380324835,,,,

气体不完全燃烧损失率,q3,%,0.5,,,,

固体不完全燃烧损失率,q4,%,0,,,,

散热损失率,q5,%,1,,,,

本体热效率,η,%,91.11967516,,,,

实际燃料用量,B,m3/s,0.018441349,,,,

实际每小时燃料用量,Bh,m3/h,66.38885585,,,,

计算燃料用量,Bc,m3/s,0.018441349,,,,

实际烟气流量,Qsm,m3/s,0.207876102,,,,

保热系数,Φ,,0.989144556,,,,

火筒的热力计算,,,,,,,

输入火筒的热量,Qfi,KJ/m3,35505.31215,,,,

火筒内径,Dfi,m,0.5,0.3582375,,,

火筒长度,Lf,m,4.5,,,,

火筒受热面积,Af,m2,7.06858335,,,,

火筒的辐射系数,C,KW/(m2•k4),0.0044,,,,

被加热介质的平均温度,ts,℃,151.84,,,,

壁面的温度增值,△t,℃,0,,,,

火筒烟气侧壁面温度,Tw,K,424.99,可取火筒外侧介质温度,,,

火筒出口的烟气温度,tp,℃,800,,,,

火筒出口的烟气温度,Tp,K,1073.15,,,,

火筒的传热量,Qft,KJ/m3,21818.17449,,,,

火筒出口烟气的焓,Isp,KJ/m3,13585.97692,可查表,,,

火筒内烟气的输出热量,Qfb,KJ/m3,21919.33523,,,,

火筒传热量与输出热量的校核,δf,,0.004615137,,,,

校核结果,,,合格,,,,

火筒长度的计算,Lf,m,4.57047899,,,,

火筒的热流量,QfL,KW,404.2221074,,,,

火筒的热流密度,qf,KW/m2,57.1857312,,,,

火筒容积热流密度,qv,KW/m3,733.0832579,,,,

火筒截面积热流密度,qs,KW/m2,3350.541628,,,,

火筒的有效输出热量,Qfe,KJ/m3,21681.3911,,,,

烟管的热力计算,,,,,,,

烟气的对数平均温差,△tm,℃,230.8039598,,,,

烟管的内径,dsi,m,0.05,,,,

烟管的内截面积,Sti,m2,0.0019635,,,,

烟管的根数,N,,10,,,,

烟管内烟气的平均温度,tms,℃,382.6439598,,,,

烟管内烟气的平均开氏温度,Tms,K,655.7939598,,,,

实际烟气平均流速,Ws,m/s,25.24347499,,,,

烟管长度,Ls,m,4.7,,,,

烟气在tms下的运动粘度,νst,m2/s,5.77823E-05,可查表,,,

烟气在tms下的密度,ρst,Kg/m3,0.520799693,可查表,,,

烟气在Tms下的导热率,λst,W/(m•k),0.055481529,可查表,,,

烟气在tms下的普朗特数,Pr,,0.641735604,,,,

烟气在烟管内的雷诺数,Re,,21843.60796,热管的管径,d,m,0.032

层流时烟管内的对流换热系数,αc,W/(m2•k),10.76375343,热管传热方程计算的传热量,Qsf,KJ/m3,33029.32379

过滤流时的换热系数,αc,W/(m2•k),53.4054517,热管的面积,As,m2,5.2

紊流是的换热系数,αc,W/(m2•k),59.00975305,热管的传热系数,κ,W/(m2•k),507.5113584

对流换热系数,αc,W/(m2•k),123,热管的对流换热系数,αd,W/(m2•k),534.2224826

烟管的有效辐射层厚度,l,m,0.045,饱和水的压力,Ps,bar（绝压）,5

烟管内灰污壁面开氏温度,Tws,K,449.99,水的临界压力,Pk,bar（绝压）,220.5

烟气的辐射减弱系数,Kg,1/(m•MPa),0.413953101,临界热流密度,qcr,W/m2,21.81089549

烟气的黑度,αsa,,0.397216054,临界换热系数,acr,W/(m2•k),34.47158764

烟气的辐射换热系数,αr,W/(m2•k),0.013513688,临界过热度,△tct,℃,0.632720944

烟管内侧的换热系数,α1,W/(m2•k),123.0135137,过热度,△tr,℃,0.61

烟管受热面的传热系数,κ,W/(m2•k),113.1724326,烟管外侧的换热系数,a2,W/(m2•k),3.180651097

烟管内径,dsi,m,0.05,,,,

烟管受热面面积,As,,7.38274261,,,,

传热方程计算的传热量,Qsf,KJ/m3,10457.04437,,,,

热平衡方程计算的传热量,Qc,KJ/m3,10416.97941,,,,

烟管传热校核,δf,,0.00384612,,,,

校核结果,,,合格,10303.89847,,,

烟管的热流密度,qc,KW/m2,26.02056735,,,,

盘管的热力计算,,,,,,,

对数平均温差,△tm,℃,90.3693692,,,,

液体介质成过渡流或紊流的平均温度,tf,℃,56,,,,

气体介质或层流状态下的液体平均温度,tf,℃,60,,,,

介质的平均开氏温度,Tf,K,329.15,,,,

加热含水原油,,,含水原油,,,,

估取传热系数,κ,W/(m2•k),145,,,,

设计盘管传热面积,Ac,m2,45.7890884,,,,

盘管内径,Di,m,0.147,,,,

盘管外径,Do,m,0.159,,,,

盘管长度,La,m,12.39380932,可以自定,,,

介质平均温度下的密度,ρt,Kg/m3,962,,,,

介质平均温度下的运动粘度,νt,mm2/s,8,,,,

介质平均温度下的动力粘度,μt,Pa•s,0.0077,,,,

介质平均温度下的热导率,λt,W/(m•k),0.55,,,,

介质平均温度下的比热容,Cpt,KJ/（kg•K）,3.8,,,,

介质平均温度下的普朗特数,Pr,,53.17236364,,,,

估取盘管内壁面温度,twi,℃,128,125.5983357,参考值,,

估取盘管外壁面温度,two,℃,144,141.7207786,参考值,,

介质盘管内壁面温度下的密度,ρw,Kg/m3,960,,,,

介质盘管内壁面温度下的的运动粘度,νw,mm2/s,7.8,,,,

介质盘管内壁面温度下的的动力粘度,μw,Pa•s,0.0075,,,,

介质盘管内壁面温度下的下的热导率,λw,W/(m•k),0.54,,,,

介质盘管内壁面温度下的下的比热容,Cpw,KJ/（kg•K）,3.78,,,,

介质盘管内壁面温度下的下的普朗特数,Prw,,52.416,,,,

估取盘管内介质流速,W,m/s,0.157,0.241780264,参考值,,

雷诺数,Re,,2884.875,,,,

盘管内液体或气体呈层流,αi,W/(m2•k),83.16370622,,,,

盘管内液体呈过渡流,αi,W/(m2•k),172.3760733,,,,

盘管内气体呈过渡流,αi,W/(m2•k),180.308245,,,,

盘管内液体呈紊流,αi,W/(m2•k),197.5401674,,,,

盘管内气体呈紊流,αi,W/(m2•k),214.9751697,,,,

盘管内水成紊流,αi,W/(m2•k),879.6709868,,,,

盘管内壁的换热系数,αi,W/(m2•k),172.3760733,,,,

管外蒸汽凝结膜的平均温度,tf,℃,147.92,,,,

管外蒸汽凝结液的动力粘度,μL,Pa•s,0.000205,,,,

介质在平均温度下的密度,ρL,Kg/m3,929.7,,,,

介质在平均温度下的导热系数,λL,W/(m•k),0.685,盘管外膜的换热系数（按加热炉设计统一规定所得）,,,

盘管外壁水蒸汽凝结的汽化潜热,r,kJ/kg,2110,定性温度,tn,℃,147.92

盘管外壁水蒸汽凝结流量,qms,kg/s,0.28436019,tn下饱和水的密度,ρL,Kg/m3,929.7

盘管外壁水蒸汽凝结液雷诺数,Re,,153.7826117,tn下饱和水的热导率,λL,W/(m•k),0.685

盘管通道管子根数,Nc,,8,tn下饱和水的动力粘度,μL,Pa•s,0.000205

管子当量排数,Ne,,2.9111386,tn下饱和水的汽化潜热,r,J/kg,2154000

管子排数,Nt,,2,外膜的初算换热系数,ao1,W/(m2•k),8923.362424

盘管外壁水蒸汽凝结膜呈层流换热系数,αo,W/(m2•k),10000,外膜的热流密度,qo,W/m2,80000

盘管内污垢热阻,ri,(m2•k)/W,0.00017,按热流密度计算的外膜换热系数,ao2,W/(m2•k),8533.171439

盘管外污垢热阻,ro,(m2•k)/W,0.00009,外膜换热系数校核,δso,,0.045726374

盘管壁厚,δ,m,0.008,校核结果,,,合格

盘管壁的导热系数,λe,W/(m•k),40,盘管外膜的换热系数,ao,W/(m2•k),10204.08163

盘管加热紊流状态下水传热系数,κ,W/(m•k),589.3485884,盘管的传热系数,,,637.034766

盘管加热液体传热系数,κ,W/(m•k),157.2013341,,,,

按传热方程计算紊流状态下水的热功率,Qtc,KW,2438.683814,,,,

按传热方程计算的热功率,Qtc,KW,650.4882789,,,,

加热紊流状态下水的热功率校核,δf,,3.064473023,,,,

热功率校核,δf,,0.084147132,,,,

加热紊流状态下水的校核结果,,,不合格,,,,

校核结果,,,合格,,,,

盘管的压力损失计算,,,,,,,

层流状态时的摩阻系数,f,,0.02218467,,,,

过渡流时的摩阻系数,f,,0.043172254,,,,

紊流时的摩阻系数,f,,0.100753858,,,,

摩阻系数,f,,0.043172254,输入k值,,,

当量长度,Le,m,145.4554746,,,,

盘管压力损失,△Pc,Pa,506.4794663,,,,

烟囱计算,,,,,,,

烟气在烟囱中的流速,Wch,m/s,3,,,,

烟囱直径计算值,Dch,m,0.390904779,,,,

烟囱直径圆整值,Dch,m,0.317,,,,

烟气在烟囱中的实际流速,Wch,m/s,4.562091449,,,,

火筒入口处的烟气温度,tsi,℃,1838.990014,,,,

烟气在火筒中的平均温度,tml,℃,1319.495007,,,,

烟气的平均流速,Wsl,m/s,6.172521941,,,,

烟气在平均温度tml下的运动粘度,υsl,m2/s,0.000250631,可查表,,,

雷诺数,Rel,,12313.95365,,,,

层流状态时的摩阻系数,fsl,,0.005197356,,,,

过渡流时的摩阻系数,fsl,,0.030035654,,,,

紊流时的摩阻系数,fsl,,0.10421064,输入k值,,,

摩阻系数,fsl,,0.10421064,,,,

烟气在tml下的密度,ρsl,Kg/m3,0.212974899,,,,

烟气流通的直段长度,Lsl,m,4,,,,

烟气在火筒中的沿程阻力,△P1,Pa,3.382406183,,,,

烟管中烟气层流状态时的摩阻系数,fs2,,0.002929919,,,,

烟管中烟气过渡流状态时的摩阻系数,fs2,,0.026025878,,,,

烟管中烟气紊流状态时的摩阻系数,fs2,,0.130863656,输入k值,,,

摩阻系数,fs2,,0.130863656,,,,

烟管中的沿程阻力,△P2,,2041.201625,,,,

估取烟囱高度,Hcb,m,5,,,,

烟囱出口的烟气温度,tso,℃,188.5,,,,

烟气的平均温度,tm3,℃,194.25,,,,

烟气的平均流速,Ws3,m/s,4.506650203,,,,

烟气tm3下的运动粘度,υs3,m2/s,0.00003188,,,,

雷诺数,Re3,,44812.05586,,,,

层流状态时的摩阻系数,fs3,,0.001428187,,,,

过渡流时的摩阻系数,fs3,,0.021746419,,,,

紊流时的摩阻系数,fs3,,0.116620086,,,,

摩阻系数,fs3,,0.116620086,,,,

烟气在tm3下的密度,ρs3,Kg/m3,0.725702631,,,,

烟囱的沿程阻力,△P3,Pa,13.55565483,,,,

火筒出口与烟管之间的拐弯处局部阻力系数,ζ1,,2.66,,,,

烟气密度,ρp1,Kg/m3,0.348552032,不同的火筒要调,,,

弯头处弯管内径,Di,m,0.303,,,,

烟气流速,Wp1,m/s,10.27018334,不同的火筒要调,,,

火筒出口弯头局部阻力,△P4,Pa,48.89626122,,,,

烟管入口处的局部阻力系数,ζ2,,0.5,,,,

烟气流速,Wp2,m/s,37.71831128,,,,

烟管入口处局部阻力,△P5,Pa,123.9687173,,,,

烟管出口处的局部阻力系数,ζ3,,0.5,,,,

烟气密度,ρp3,Kg/m3,0.716883461,,,,

烟气流速,Wp3,m/s,18.3388162,,,,

烟管出口处的局部阻力,△P6,Pa,60.27415978,,,,

烟箱出口处的局部阻力系数,ζ4,,0.1,,,,

烟气流速,Wp4,m/s,4.562091449,,,,

烟箱出口处的局部阻力,△P7,Pa