计算管道压力降

管道编号和类别自至物料名称设计温度T℃设计压力PMpa密度ρkg/m31,113.00000粘度μmPa·s21.00000质量流量Wkg/h###########流量Qm3/hr134.77089管道公称直径Dmm150.00000管道外径D0mm159.00000管道壁厚δmm4.50000管道内径dmm150.00000绝对粗糙度εmm0.10000相对粗糙度ε/d0.00067流速um/s2.50000雷诺数Re19,875.00000摩擦系数λ查表0.02700压力降ΔP100kPa/100m45.00000直管长度Lm5,000.00000管件当量长度Lem1,035.00000总长度L0m6,035.00000摩擦压力降ΔPfMpa3.77829管端标高m管末标高m异径1位差ΔHm0.00000异径2管道垂直压力降ΔPhMpa0.00000异径3总压力降ΔPMPa3.77829起始压力P1Mpa末端压力P2Mpa-3.77829起始压力P1Mpa3.77829末端压力P2Mpa压力，Mpa（A）比重，kg/m3扬程，m液柱#DIV/0!扬程计算扬程，m液柱比重，kg/m3压力，Mpa（A）0压力计算管道当量长度Le计算管道公称直径dmm150管件名称系数数量当量长度Le闸阀130截止阀3409459角阀1600蝶阀全开DN≤200450蝶阀全开DN250～350350蝶阀全开DN400～600250球阀全孔径33113.95旋启式止回阀1350升降式止回阀6000带有滤水器的底阀（全开）4200盘式流量计（水表）4000文式流量计120转子流量计250090°长半径弯头2015646890°短变径弯头30090°方形弯头600180°弯头75045°弯头100三通主＋支→主600三通支→主＋主600三通主→支←主90794.5虾米弯30°（每节）80虾米弯45°（每节）150由容器入管口200000合计当量长度Le1035.45介质名称设计温度T℃设计起点压力P0MPa质量流量WGkg/h管道直管长度Lm管件当量长度Lem管道总长度L0m0.00000起点介质密度ρ0kg/m3管道内径dmm管内介质流速um/s#DIV/0!介质粘度μmPa·s雷诺数Re#DIV/0!管道绝对粗糙度εmm0.30000相对粗糙度ε/d#DIV/0!摩擦系数λ查表压力降ΔPkPa#DIV/0!终点压力P1MPa#DIV/0!介质终点密度ρ1kg/m3介质平均密度ρavkg/m30.00000管内介质流速uavm/s#DIV/0!雷诺数Re'#DIV/0!摩擦系数λ'查表压力降ΔP'kPa#DIV/0!终点压力P1'Mpa#DIV/0!压力降幅度#DIV/0!是否合格#DIV/0!介质体积流量Qm3/h介质密度ρkg/m3介质质量流量WGkg/h0.00000管道外径D0mm管道壁厚δmm管道内径Dmm0.00000气体管道-Babcock公式（蒸汽）气体的质量流量WGkg/hr00管道长度Lzm当量长度Lem管道总长度Lm000管道外径D0mm00管道壁厚δmm00管道内径dmm000气体平均密度ρkg/m3#DIV/0!#DIV/0!#DIV/0!流速um/s#DIV/0!#DIV/0!#DIV/0!压力降ΔPkPa#DIV/0!#DIV/0!#DIV/0!Mpa#DIV/0!#DIV/0!#DIV/0!105Ps#DIV/0!#DIV/0!#DIV/0!1起点压力P0MPa#DIV/0!#DIV/0!105Pa0#DIV/0!#DIV/0!终点压力PeMPa#DIV/0!#DIV/0!#DIV/0!105Pa#DIV/0!#DIV/0!#DIV/0!平均压力P-MPa#DIV/0!#DIV/0!#DIV/0!105Pa#DIV/0!#DIV/0!#DIV/0!气体平均密度ρkg/m3#DIV/0!#DIV/0!#DIV/0!压力降ΔPkPa#DIV/0!#DIV/0!#DIV/0!Mpa#DIV/0!#DIV/0!#DIV/0!105Pa#DIV/0!#DIV/0!#DIV/0!2终点压力PeMPa#DIV/0!#DIV/0!#DIV/0!105Pa#DIV/0!#DIV/0!#DIV/0!平均压力P-MPa#DIV/0!#DIV/0!#DIV/0!105Pa#DIV/0!#DIV/0!#DIV/0!百米压力降kPa/100m#DIV/0!#DIV/0!#DIV/0!Mpa/100m#DIV/0!#DIV/0!#DIV/0!105Pa/100m#DIV/0!#DIV/0!#DIV/0!异径的当量长度管径以大管端为基准以小管端为基准mm变大缩小变大缩小设备名称25×200.30.30.150.15管壳式换热器25×1510.064.570.30.340×252.441.220.30.340×2016.467.320.30.3板式换热器40×15116.1648.780.30.3螺旋板换热器50×400.920.610.30.3空冷器50×2524.0910.760.30.3在线过滤器（液体）50×2010040.550.610.3在线过滤器（气体）50×15601.83239.020.30.3集尘器/布袋过滤器80×506.713.960.920.61气体干燥器80×4038.1118.290.920.61在线混合器80×25271.04113.410.920.3塔的部件80×20952.74339.940.610.3100×803.052.130.610.61100×5053.6626.831.520.61100×40223.1799.091.220.61固定床反应器100×251345.12534.150.920.3加热炉150×10015.248.541.830.92150×8091.4643.62.441.22150×50650.3257.622.130.92150×402286.58864.021.520.61200×1507.315.181.521.22200×100130.7969.933.351.52仪表200×80542252.443.051.52200×5032661405.882.440.92250×2004.273.661.521.22250×15057.3230.794.272.13250×100500.3221.654.271.83250×801855.18759.153.661.52300×2503.353.351.221.22300×20036.5921.654.572.74300×150210.9898.175.792.74300×1001500.91652.444.572.13350×3001.831.830.920.92350×25020.7313.115.662.13350×200116.4657.936.713.35350×150540.55233.236.713.05400×3501.521.520.610.61400×30013.419.453.352.13400×25076.2239.336.713.35400×200281.4125.618.233.66400×1501167.68483.847.623.05450×4001.221.220.610.61450×35010.377.932.752.13450×30054.2730.186.713.66450×250191.1688.118.543.06500×4500.610.610.30.3500×4005.184.571.521.22500×35026.8316.164.272.44500×300102.4449.097.323.66500×250355.79146.049.453.96600×5004.574.571.831.83600×45021.0414.944.883.66600×40070.4339.028.544.88600×350190.8592.9911.895.79650×6000.610.610.30.3650×50014.6310.983.662.74650×45047.5628.057.013.96700×6500.610.610.30.3700×6003.363.351.521.52700×50033.94256.714.27700×450107.3256.110.675.71750×7000.610.610.30.3750×6503.353.351.521.52750×60011.289.453.252.74750×50089.0249.3910.676.1900×7508.238.233.353.35900×65057.6236.8911.287.32900×600125.369.5115.248.54常见设备压力降设备名称压力降管壳式换热器壳侧70kPa管侧100kPa板式换热器70～100kPa螺旋板换热器35kPa空冷器50kPa在线过滤器（液体）105kPa（结垢）在线过滤器（气体）15kPa（结垢）集尘器/布袋过滤器25kPa气体干燥器35kPa在线混合器105kPa塔的部件塔板150mmH2O喷淋喷嘴105kPa管分布器2～8kPa固定床反应器150～350kPa加热炉常压塔及减压塔加热炉550～850kPa延迟焦化加热炉1500～1750kPa裂解炉150kPa气体重整炉250～500kPa其他形式的加热炉350～450kPa流量测量15kPaCoriolis质量流量计100kPa容积式流量计70kPa序号管道类别绝对粗糙度ε，mm1无缝黄铜管、铜管及铅管0.01~0.052金新的无缝钢管或镀锌铁管0.1~0.23新的铸铁管0.25~0.424属具有轻度腐蚀的无缝钢管0.2~0.35具有显著腐蚀的无缝钢管0.5以上6管旧的铸铁管0.85以上7钢板制管0.338干净玻璃管0.0015~0.019非橡皮软管0.01~0.0310金木管道0.25~1.2511属陶土排水管0.45~0.612管接头平整的水泥管0.3313石棉水泥管0.03~0.8烟囱计算烟气流量Vm3/h烟囱出口处烟气速度ωm/s烟囱出口内径Dim#DIV/0!由烟气总阻力决定的烟囱高度在0℃760mmHg下烟气的重度γykg/m3烟气总阻力ΔPmmH2O烟囱内烟气的平均温度ty℃烟囱高度Hm0.00★一般烟气总阻力不宜超过30mmH2O，否则就要设置引风机由烟气污染标准决定的烟囱高度燃料耗量Bkg/h固、液体燃料中硫含量S％气体燃料中H2S含量H2S％0.00烟气排出SO2含量Gkg/h0.000.00烟囱高度Hm0.00最终烟囱高度Hm0.00P459图7-21烟气出口温度℃、烟气平均速度m/s→烟囱平均直径m→烟囱高度m→摩擦损失ΔPfmmH2O烟气出口温度℃、烟气出口速度m/s→动能损失ΔPmmmH2OP463图7-24烟囱高度m→烟气平均温度℃→理论抽力mmH2O烟囱高度m→大气温度℃→校正值mmH2O有效抽力mmH2O0.00临界风速计算单位高度重量mkg/m烟囱高度Hm0.00烟囱壁厚smm壁厚δmm0.00烟囱外径D0m#DIV/0!烟囱自振周期Ts#DIV/0!临界风速ωcm/s#DIV/0!☆摘自《化学工业炉设计手册》烟气出口速度ω负荷情况单位自然通风机械通风最大负荷时出口速度≤m/s1018~20正常运行时m/s6~812~15最小负荷时出口速度≥m/s2.5~34~5重度kg/m3#DIV/0!容积m3#DIV/0!重量kg0