蒸汽管道压力降计算书

蒸汽管路计算说明1、输入参数过热蒸汽物料名称过热蒸汽质量流量WG 54000kg/h始端温度t1 315°C始端压力P] 3600kPa管路长度根据实际管路布置（如图1），大减温减压系统支路从试验厂房蒸汽入口到N3喷口按调节阀分为六段进行计算。图1管段轴测图A—BB—CC—DD—E项目ilz.日.[/ilz.日.[/ilz.日.[/当量长当量长当量长当量长数量（个）1丿度（m）数量（个）数量（个）度（m）数量（个）数量（个）度（m）数量（个） 度量长 数量（m）管道规格DN200DN200DN200DN250管道内径d（m）0.19410.19410.19410.248直管段l（m）5.958.724.1819.445弯头45°弯头90°15.823423.292211.646322.32标准三通（直通）13.88213.88229.92标准三通（分枝）111.65截止阀（全开）158.23止回阀二77?<l~t二？LII»截面积变化总长度L（m）70.0047.5419.7151.69按等温流动计算AfB段：设调节阀B阀前压力P2=3550kPa过热蒸汽密度*(0.461t+126.1)-0.0097+1.324x10-5tp=14.319kg；''m311p=14.105kgm214.319-14.105因此p=14.105+ =14.176kg-m3m 3查得过热蒸汽粘度卩=0.0204mPa.s雷诺数Re=354W^/d卩雷诺数Re=354W^/d卩=354x54000194.1x0.0204=4.83x106取s=0.2mm,贝Us/d=0.2/194.1=0.00103查《HG-T20570.7管道压力降计算》图124-1得，九=0.0205摩擦压力降APf九APf=6.26x103ggd5p0.0205x0.0205x70x540002194.15x14.176=6.26x103x9.81x=65.80kPaP2=P]-APf=3600-65.80=3534.20kPa与假设相符。计算结果P2=3534.20kPa,APf=65.80kPa设调节阀B阀后压力为P3,根据供货商资料:K=v12P；1-5.67(0.42-^—)式中：Kv为调节阀一定开度下的流量系数，此处按全开计算，下同；P和P

分别为阀前和阀后压力，Bar；w为流量，kg/h。对公式进行整理得：AP=P-P'= +0.2436P816.48PK2v带入P2，计算得△P=904.79kPa，P3=P2-△P=2629.41kPaB—C段：设调节阀C处阀前压力P4=2560kPa过热蒸汽密度l(0.461tl(0.461t+126.1)-0.0097+1.324x10-5tpp=10.240kg/m33p=9.955kg.;m34因此p=10.050kg」m3m查得过热蒸汽粘度卩=0.0207mPa.s雷诺数Re=354 /d卩雷诺数Re=354 /d卩=354x54000194.1x0.0207=4.75x106取s=0.2mm,贝Us/d=0.2/194.1=0.00103查《取s=0.2mm,贝Us/d=0.2/194.1=0.00103查《HG-T20570.7管道压力降计算》图124-1得，九=0.0206摩擦压力降APf九LW2=6.26x103g gd5pm=6.26x103x9.81x0.0206x47.54x540002194.15x10.05=63.34kPaP4=P3-△Pf=2629.41-63.34=2566.07kPa与假设相符。计算结果P4=2566.07kPa，APf=63.34kPa设调节阀C阀后压力为P5,根据供货商资料，整理的公式:W2AP=P-P'= +W2AP=P-P'= +0.2436P816.48PK2v带入P4，计算得△P=685.50kPa,P5=P4-AP=1880.57kPa—D段：设调节阀D处阀前压力P=1840kPa6过热蒸汽密度(0.461t+126.1)-0.0097+1.324x10-5tp=7.208kg『m35p=7.046kg;m36因此p=7.100kg」m3m查得过热蒸汽粘度卩=0.0207mPa.s雷诺数Re=354W^/d卩=354x54000194.1x0.0207=4.75x106取s=0.2mm,贝Us/d=0.2/194.1=0.00103查《HG-T20570.7管道压力降计算》图124-1得，九=0.0206摩擦压力降APf九APf=6.26x103g —0.0206x19.71x540000.0206x19.71x540002194.15x7.1=6.26x103x9.81x=37.17kPaP=P-△P=1880.57-37.17=1843.40kPa6 5f计算结果P=1843.40kPa,AP”=37.17kPa6f设调节阀D阀后压力为P7,根据供货商资料，整理的公式:AP=P-P'= +0.2436P816.48PK2v带入P，计算得厶P=533.14kPa,P=P-^P=1310.26kPa6 7 6

DtE段：设调节阀E处阀前压力P8=1280kPa,t8=197°C（根据供货商资料，减温器进出口压损可忽略。出口温度为过热5C）过热蒸汽密度*(0.461t*(0.461t+126.1)-0.0097+1.324x10-5tP=6.311kg'm37p=6.159kg：'m38因此p=6.209kg;m3m查得过热蒸汽粘度卩=0.0157mPa.s54000雷诺数Re=354W/d卩=354x =4.91x106248x0.0157取s=0.2mm,贝Us/d=0.2/248=0.000806查《HG-T20570.7管道压力降计算》图124-1得，九=0.0194摩擦压力降APf九APf0.0194x51.69x5400022485x6.209=0.0194x51.69x5400022485x6.209=6.26x103x9.81x=30.83kPaP=P-^P=1310.26-30.83=1279.43kPa与假设相符。8 7f计算结果P=1279.43kPa,APf=30.83kPa8f设调节阀E阀后压力为P9,根据供货商资料，整理的公式:AP=P—P'= +0.2436P816.48PK2v带入P，计算得厶P=432.82kPa,P=P-^P=846.61kPa8 9 8EtF段：设调节阀F处阀前压力P10=780kPa过热蒸汽密度卜0.461卜0.461t+126.1)-0.0097+1.324x10-5tpp=4.014kg」m39p=3.690kg加310因此p=3.798kg;'m3m查得过热蒸汽粘度卩=0.0158mPa.s雷诺数Re=354 /dp雷诺数Re=354 /dp=354x54000248x0.0158二4.88x106取s=0.2mm,贝U取s=0.2mm,贝Us/d=0.2/248=0.000806查《HG-T20570.7管道压力降计算》图124-1得，九=0.0195摩擦压力降AP二f九LW26.26x103g g-d5pm6.26x103x9.81x0.0195x66.3x5400022485x3.798二64.98kPaPio=P9-△Pf=846.61-64.98=781.63kPa计算结果P10=781.63kPa，APf=64.98kPa设调节阀F阀后压力为P11，根据供货商资料，整理的公式:W2AP=P—P'= +0.2436P816.48PK2v带入P10，计算得△P=388.72kPa，Pn=P10-AP=392.91kPaF—G段：设管道出口G处压力P12=320kPa过热蒸汽密度卜0.461卜0.461t+126.1)-0.0097+1.324x10-5tP=1.835kg;'m311'p=1.491kg；'m312因此p=1.606kg''m3m查得过热蒸汽粘度卩=0.0160mPa.s雷诺数Re=354^/d卩雷诺数Re=354^/d卩=354x54000248x0.016=4.82x106取s=0.2mm,贝Us/d=0.2/248=0.000806查《HG-T20570.7管道压力降计算》图124-1得，九=0.0195摩擦压力降AP=f九LW26.26x103g jd5pm0.0195x31.85x540002=6.26x103x9.81x2485x1.606=73.84kPaPi2=Pii-APf=392.91-73.84=319.07kPa计算结果P12=319.07kPa，APf=73.84kPa计算结果过热蒸汽54000kg/h过热蒸汽54000kg/h315°C3600