水动力计算

烟气成分质量分数单位取值分子质量气体分压飞灰含量20-100g/Nm360二氧化硫“1-4%2.5641145.77313Pa二氧化碳20左右%174411332.7378Pa氮气70左右%692872281.916Pa氧气5左右%4.5324124.78325Pa水蒸气”4-12%71811406.808Pa100292.018Pa烟气进口温度196℃469K烟气出口温度140℃413K烟气平均温度168℃441K烟气初始压力1atm101325Pa烟气实际密度0.8kg/m3烟气实际粘度2.25E-05Pa*s烟气实际导热系数0.0339W/mK烟气实际比热1.039kJ/kgK1.3507kJ/Nm3K烟气Pr数6.90E-01烟气流量10353Nm3/h实际流量16724.08m3/h2.87583333Nm3/s4.645577m3/s烟道厚1.3m1300mm烟道宽1.6m1600mm相变换热器下段高度1.1m1100mm相变换热器上段高度0.7m700mm烟道截面积1.808m2烟气速度假设7m/s烟气流通截面积0.66365385m2先计算下段，假设管排水平，且为翅片管，错列排布，管轴向为烟道厚方向灰的比热cp0.85484468kJ/kgKat168℃灰流量0.17255kg/sQ灰8.26019316kW假设没有漏风和热损失烟气放热量+灰225.785926kW核算烟气极限流速（避免烟气灰分磨损）烟气速度w假设为7m/s飞灰含量μθ37.1428571g/m3每平方米飞灰量G0.26kg/m2sk0.037143灰粒的密度ρ假设2000kg/m3灰粒的直径δ假设60μm6.00E-05m无因次数K7.14E+00yita0.2C1.00E-05s2/m2Jmax1.15E+01deltamax1.46E-03m1.46E+00mm磨损量貌似有点大，对于10m/s的速度来说，还需继续验证相变换热器下段管外径32mm0.032m管壁厚3mm0.003m管长1130mm1.13m翅片高16mm0.016m翅片厚1.2mm0.0012m翅片中心间距10mm0.01m下段烟道收窄，使长1000mm1m则烟道面积1.3换热器迎风面上流速2.21217949Nm/s3.573521m/s若要使最窄截面上的流速达到7m/s，则阻断系数φ0.48949704翅片外径64mm0.064m热管横向中心距s173.2180115mm0.073218ms1取值74mm0.074m第一排管子数(列数）21.6216216取值22阻断面积0.8909824m2实际阻断系数0.4928实际流速w7.045585m/s4.361553Nm/s烟气在管束中的流动Re8.02E+03Prf6.90E-01at441K168℃Prw0.7at398K125℃假设值s264mm0.064m假设值s2/ds1/s21.15625Nuf5.31E+01α5.62E+01W/m2KFb0.09996799m2Ff0.57254395m2Fw0.11359999m2Q235钢导热系数45W/mKAL0.00001992H`0.0166x5.36E-01r2`0.0646r2`/r1yitaf0.8查图（传热学）αa276.242682W/m2K翅片接触热阻忽略污垢热阻0.258m2K/kW0.000258m2K/W蒸发热阻0.258m2K/kW0.000258m2K/W蒸发段传热系数Ka241.779182W/m2K传热面积21.7174839m2总管数191.175051取值194排数9相变换热器上段管长640mm0.64m管外径32mm0.032m翅片高16mm0.016m翅片厚1.2mm0.0012m翅片中心间距3mm0.003m管壁厚2mm0.002m翅片外径64mm0.064m空气进口温度16℃289K空气出口温度83℃356K空气平均温度49.5℃322.5K空气物性322.5Kcp1.005kJ/kgK导热系数0.0283W/mK粘度1.96E-05Pa*sPr0.698密度1.039kg/m3空气流量9424Nm3/h11132.75m3/h2.61777778Nm3/s3.09243m3/s空气换热量208.22876kW1/2换热量104.1144kW假设空气流速为7m/s空气流通面积为0.44177568m2取一半0.220888m2中间烟气孔的面积为0.66365385m2假设采取侧开孔的方法,将1600mm那段截出一部分让烟气流过，则截出的长度0.51050296m510mm那么空气部分为1090mm1.09m考虑隔板厚度取1050mm1.05m取一半500上段迎风面积0.32m2阻断系数0.30972549横向中心距s1144.644213mm0.144644ms1取值145mm0.145m第一排管数3.44827586取值4阻断面积0.114688m2实际阻断系数0.3584实际空气流速7.5310498m/sRe1.28E+04管壁温度125℃Prw0.686s2假设125mm0.125ms2/d3.90625s1/s21.16b/d0.09375h/d0.5Nuf5.86E+01α5.18E+01Fb0.03860389m2Ff1.08090893m2Fw0.06433982m2yitaf0.8同下段αa727.953155W/m2K冷凝热阻rc0.215m2K/kW0.000215m2K/WKa629.439607W/m2K传热面积4.38167028m2取一半则2.190835m2需要管数68.1020005根取值70大概有10排纵向长度1250mm1300mm是满足的阻力计算侧开口后的烟气侧阻力烟气侧肋化系数5.92肋化系数5.92σ1=s1/d2.3125σ1=s1/d3σ2=s2/d2σ2=s2/d2.59375Re8.02E+03Re6.98E+03Eu7.34E-01Eu5.78E-01阻力1.31E+02Pa阻力69.6606732Pa空气侧肋化系数17.4σ1=s1/d4.53125σ2=s2/d3.90625Re1.28E+04Eu5.53E-01阻力1.41E+02换热器下段的结构方案（第二种，侧孔）烟道迎风面积1.243m2烟气流通面积0.66365385m2阻断系数0.46608701m2s176.8955135mm0.076896ms1取值96mm管子数11.4583333取12实际阻断面积0.4859904m2实际阻断系数0.39098182实际流速6.1367477m/sRe6.98E+03Prf6.90E-01at441K168℃Prw0.7at398K125℃s2假设83mm0.083ms1/s21.15662651Nuf3.85E+01α4.08E+01W/m2Kαa2.00E+02W/m2K污垢热阻0.258m2K/kW0.000258m2K/W蒸发热阻0.258m2K/kW0.000258m2K/WKa1.82E+02W/m2K传热面积28.9097654m2管子总数254.487393取值91约共8排664热管气化潜热2263073J/kg蒸发量0.09976962kg/s99.76962g/s下段的热流密度10.2451151kW/m2Lair/Lsmoke0.56637168Toperating89.3559322℃KyFy/KaFa1.90385842Top127.192225℃Kaout241.779182W/m2KTy163℃Twout120.626149℃nanda45W/mKrout32mm0.032mrin26mm0.026mTwin119.11341℃hi2000W/m2Kqin12609.3725W/m2Tvapor112.808723℃m22约正三角形排布2.01875mm0.5m正三角形分布名称符号值单位值单位备注烟气物性比热Cpy1.039kJ/kgK1.3507kJ/Nm3K168℃下粘度μy2.25E-05Pa*s168℃下密度ρy0.8kg/m3168℃下导热系数ky0.0339W/mK168℃下PrPry0.69168℃下Pry_w0.7125℃下灰的物性比热Cph0.8548kJ/kgK168℃下比热Cph0.8833kJ/kgK253℃下空气物性密度ρa1.039kg/m349.5℃下比热Cpa1.005kJ/kgK49.5℃下粘度μa1.96E-05Pa*s49.5℃下导热系数ka0.0283W/mK49.5℃下PrPra0.69849.5℃下边界条件烟气流量Vy10353Nm3/h2.875833Nm3/s空气流量Va9424Nm3/h2.617778Nm3/s灰流量Vh621180g/h0.17255kg/s烟气进口温度Tyin310℃583K烟气出口温度Tyout140℃413K空气进口温度Tain15.7℃288.7K空气出口温度Taout249℃522K需要假设的温度项烟气通过管式空预器后的温度Ty_mid196℃469K空气进入管式空预器的温度Ta_mid83℃356K尺寸总共高度Htotal4.5m4500mm烟道宽度L11.6m1600mm烟道厚度L21.3m1300mm尺寸的假设项管式空预器高度Ha2.7m2700mm相变换热器上段高度Hup0.7m700mm相变换热器下段高度Hdown1.1m1100mmPart1计算管式空预器方案：圆形翅片管，空气管内，烟气管外，冲刷翅片管，叉排烟气流速uy7m/s暂定管束参数管外径do0.032m32mm管壁厚δ_pipe0.003m3mm管长Lpipe1.3m1300mm长度方向为烟道厚方向翅片高h0.01m10mm翅片厚δ_fin0.0012m1.2mm翅片中心间距b0.008m8mm翅片外径dfin0.052m52mm烟气平均温度Ty_aver253℃526K烟气物性比热Cpy1.079kJ/kgK1.4027kJ/Nm3K253℃下粘度μy2.65E-05Pa*s253℃下密度ρy0.674714829kg/m3253℃下导热系数ky0.0439W/mK253℃下PrPry0.66253℃下烟道截面积S2.08m2烟气初始流速uyin1.382612179Nm/s2.663934m/s阻断系数φ0.619437987阻断面积Sφ1.288431013m2横向节距s10.056502831m56.50283mm取值为横向管数n127.5862069取值为实际阻断面积Sφ`1.274m2实际阻断系数φ`0.6125实际烟气流速uy`6.874668618m/s雷诺数Re5.60E+03s1/doσ11.8125纵向节距s248mm最小值为s2/doσ21.5σ1/σ2σ1/σ21.208333333b/dob/d0.25h/doh/d0.3125空气平均温度Ta_aver166℃439K管壁温度Tw209.5℃482.5KPrwPrw0.67209.5℃下努赛尔数Nu4.28E+01对流换热系数α5.88E+01W/m2KFbFb0.180515914m2FfFf0.460683147m2翅片效率r2`D/2+δ/20.0266mH`h+δ/20.0106mALH`*δ0.00001272m2H`3/2[h/(λAL)]1/20.349705077管壁（钢）导热系数λ45W/mKr2`/r1r2`/(do/2)1.6625翅片效率ηf0.9查图（传热学，P65)光面面积Fw0.130690254m2光面面积下的换热系数αa267.6425062W/m2K灰污系数的计算基本值ε00.0032m2K/W查图管径修正系数Cd1.1飞灰改正系数Csf1灰污系数ε0.00352m2K/W换热系数Ka137.8107629W/m2K烟气放热量Qy459.8681815kW灰放热量Qh17.37512931kW总放热量Q477.2433108kW烟气辐射放热系数的计算三原子气