换热管破裂时泄放量的计算(待续)

k(绝热指数)P1（MPaA）Pc（MPaA）P1为高压侧操作压力Pc=P1*（2/（κ+1））κ/（κ-1）RV-10311.42.91.532017184RV-10511.45.93.116862548RV-10411.44.32.271611687温度取较小值用于计算κP1（MPaA）P2（MPaA）d(管内径m)M(分子量)A(压缩度)Z(压缩因子)T(高压侧流体温度K)W(kg/h)管两头总流量RV-10311.42.91.5320.021281.120.867393459353.1511474.21094RV-10511.45.93.1170.015281.1270.98430305313.1511873.20113RV-10411.44.32.2720.015281.1260.983429666313.158657.191497P1(psia)1bf/in2P2(psia)dP(psia)di(管内径in)C(为定值)ρv(气体密度kg/m3)ρv(气体密度1b/ft3)W(b/h)W(kg/h)压差管两头总流量RV-1031420.6073222.196684198.4106160.826770.631.3941.95980184426012.756811799.38648RV-1051855.7183452.080329403.6379710.590550.664.9734.05600449827232.764312352.78189RV-1041623.6591329.524064294.1350360.590550.646.842.9240338419738.853768953.5440672、破裂时泄放量计算P2(MPaA)为安全阀排放时换热器低压侧的压力。设备允许超压10%，P2=低压侧正常操作绝对压力(G)*1.1+0.1MPaA若P2〉Pc，则计算中P2=P2；若P2〈Pc，则计算中P2=Pc一、管内为气相且无相变管壳式换热器换热管断裂时泄放量计算(计算结果为两截面的总流量)1、临界压力计算（方法一、中文文献）（方法二、外文文献）算压缩因子通过查低温图表中的压缩度得到密度应用较低温度对应密度（较大值）κ1κ12κ212127)1-κκ(10129.6PPPPZTMPdWVidPCdPdPW21)317.01(18912P1（MPaA）P2（MPaA）=P2d(管内径m)ρv(液相密度kg/m3)W(kg/h)RV-10001.1690.9250.02592.726937.69275三、管内为气液两相(见资料)二、管内为液相且无相变liPPdW)(106.52126