计算-管道压力降3.5表格文件下载.xls

计算-管道压力降3.5表格文件下载.xls

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摩擦系数查表压压力力降降P100kPa/100m#DIV/0!

直管长度Lm管件当量长度Lem总总长长度度L0m0.00000摩摩擦擦压压力力降降PfMpa#DIV/0!

管端标高m管末标高m异径1位差Hm0.00000异径2管管道道垂垂直直压压力力降降PhMpa0.00000异径3总总压压力力降降PMPa#DIV/0!

起始压力P1Mpa末末端端压压力力P2Mpa#DIV/0!

起起始始压压力力P1Mpa#DIV/0!

末端压力P2Mpa扬扬程程计计算算压力，Mpa（A）比重，kg/m3扬程，m液柱#DIV/0!

压压力力计计算算扬程，m液柱比重，kg/m3压力，Mpa（A）0管管道道当当量量长长度度Le计计算算管管道道公公称称直直径径dmm管管件件名名称称系系数数数数量量当当量量长长度度Le闸阀130截止阀3400角阀1600蝶阀全开DN200450蝶阀全开DN250350350蝶阀全开DN400600250球阀全孔径30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20090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900虾米弯30（每节）80虾米弯45（每节）150由容器入管口200000合合计计当当量量长长度度Le0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管管道道总总长长度度L0m0.00000起点介质密度0kg/m3管管道道内内径径dmm管内介质流速um/s#DIV/0!

介质粘度mPas雷诺数Re#DIV/0!

管道绝对粗糙度mm0.30000相对粗糙度/d#DIV/0!

摩擦系数查表压压力力降降PkPa#DIV/0!

终点压力P1MPa#DIV/0!

介介质质终终点点密密度度1kg/m3介质平均密度avkg/m30.00000管内介质流速uavm/s#DIV/0!

雷诺数Re#DIV/0!

摩擦系数查表压压力力降降PkPa#DIV/0!

终终点点压压力力P1Mpa#DIV/0!

压力降幅度#DIV/0!

是是否否合合格格#DIV/0!

介质体积流量Qm3/h介质密度kg/m3介介质质质质量量流流量量WGkg/h0.00000管道外径D0mm管道壁厚mm管管道道内内径径Dmm0.00000气气体体管管道道-Babcock公公式式（蒸蒸汽汽）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mm00管道内径dmm000气体平均密度kg/m3#DIV/0!

#DIV/0!

流流速速um/s#DIV/0!

压力降PkPa#DIV/0!

Mpa#DIV/0!

105Ps#DIV/0!

1起点压力P0MPa#DIV/0!

105Pa0#DIV/0!

终点压力PeMPa#DIV/0!

105Pa#DIV/0!

平均压力P-MPa#DIV/0!

气体平均密度kg/m3#DIV/0!

2终点压力PeMPa#DIV/0!

百百米米压压力力降降kPa/100m#DIV/0!

Mpa/100m#DIV/0!

105Pa/100m#DIV/0!

异异径径的的当当量量长长度度管管径径以以大大管管端端为为基基准准以以小小管管端端为为基基准准mm变大缩小变大缩小设设备备名名称称25200.30.30.150.15管壳式换热器251510.064.570.30.340252.441.220.30.3402016.467.320.30.3板式换热器4015116.1648.780.30.3螺旋板换热器50400.920.610.30.3空冷器502524.0910.760.30.3在线过滤器（液体）502010040.550.610.3在线过滤器（气体）5015601.83239.020.30.3集尘器/布袋过滤器80506.713.960.920.61气体干燥器804038.1118.290.920.61在线混合器8025271.04113.410.920.3塔的部件8020952.74339.940.610.3100803.052.130.610.611005053.6626.831.520.6110040223.1799.091.220.61固定床反应器100251345.12534.150.920.3加热炉15010015.248.541.830.921508091.4643.62.441.2215050650.3257.622.130.92150402286.58864.021.520.612001507.315.181.521.22200100130.7969.933.351.52仪表20080542252.443.051.522005032661405.882.440.922502004.273.661.521.2225015057.3230.794.272.13250100500.3221.654.271.83250801855.18759.153.661.523002503.353.351.221.2230020036.5921.654.572.74300150210.9898.175.792.743001001500.91652.444.572.133503001.831.830.920.9235025020.7313.115.662.13350200116.4657.936.713.35350150540.55233.236.713.054003501.521.520.610.6140030013.419.453.352.1340025076.2239.336.713.35400200281.4125.618.233.664001501167.68483.847.623.054504001.221.220.610.6145035010.377.932.752.1345030054.2730.186.713.66450250191.1688.118.543.065004500.610.610.30.35004005.184.571.521.2250035026.8316.164.272.44500300102.4449.097.323.66500250355.79146.049.453.966005004.574.571.831.8360045021.0414.944.883.6660040070.4339.028.544.88600350190.8592.9911.895.796506000.610.610.30.365050014.6310.983.662.7465045047.5628.057.013.967006500.610.610.30.37006003.363.351.521.5270050033.94256.714.27700450107.3256.110.675.717507000.610.610.30.37506503.353.351.521.5275060011.289.453.252.7475050089.0249.3910.676.19007508.238.233.353.3590065057.6236.8911.287.32900600125.369.5115.248.54常常见见设设备备压压力力降降压压力力降降壳侧70kPa管侧100kPa70100kPa35kPa50kPa105kPa（结垢）15kPa（结垢）25kPa35kPa105kPa塔板150mmH2O喷淋喷嘴105kPa管分布器28kPa150350kPa常压塔及减压塔加热炉550850kPa延迟焦化加热炉15001750kPa裂解炉150kPa气体重整炉250500kPa其他形式的加热炉350450kPa流量测量15kPaCoriolis质量流量计100kPa容积式流量计70kPa设设备备名名称称管壳式换热器板式换热器螺旋板换热器空冷器在线过滤器（液体）在线过滤器（气体）集尘器/布袋过滤器气体干燥器在线混合器塔的部件固定床反应器加热炉序序号号管管道道类类别别绝绝对对粗粗糙糙度度，mm1无缝黄铜管、铜管及铅管0.010.052金新的无缝钢管或镀锌铁管0.10.23新的铸铁管0.250.424属具有轻度腐蚀的无缝钢管0.20.35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0.00150.019非橡皮软管0.010.0310金木管道0.251.2511属陶土排水管0.450.612管接头平整的水泥管0.3313石棉水泥管0.030.8烟烟囱囱计计算算烟气流量Vm3/h烟囱出口处烟气速度m/s烟烟囱囱出出口口内内径径Dim#DIV/0!

由烟气总阻力决定的烟囱高度在0760mmHg下烟气的重度ykg/m3烟气总阻力PmmH2O烟囱内烟气的平均温度ty烟烟囱囱高高度度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H2S0.00烟烟气气排排出出SO2含含量量Gkg/h0.000.00烟烟囱囱高高度度Hm0.00最最终终烟烟囱囱高高度度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摩摩擦擦损损失失PfmmH2O烟气出口温度、烟气出口速度m/s动动能能损损失失PmmmH2OP463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有有效效抽抽力力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mm0.00烟囱外径D0m#DIV/0!

烟烟囱囱自自振振周周期期Ts#DIV/0!

临临界界风风速速cm/s#DIV/0!

摘自化学工业炉设计手册烟烟气气出出口口速速度度负荷情况单位自然通风机械通风最大负荷时出口速度m/s101820正常运行时m/s681215最小负荷时出口速度m/s2.5345重度kg/m3#DIV/0!

容积m3#DIV/0!

重量kg0