苯和甲苯常压连续筛板精馏塔设计

409832Р0.541010Р8Р0.42987Р0.241048Р0.328192Р0.429870Р9Р0.311238Р0.160623Р0.241048Р0.311238Р10Р0.201752Р0.096579Р0.160623Р0.201752Р11Р0.114567Р0.05129Р0.096579Р0.114567Р12Р0.052912Р0.021849Р0.051290Р0.052912Р(注:X-Y是指位于气液相平衡的点,x-y是指位于操作线方程的点)。Р表1.3.3-2每层理论板气液平衡数据Р理论板数Рx(液相)Рy(气相)Р1Р0.9659Р2Р0.9160Р0.9301Р3Р0.8375Р0.8738Р4Р0.7296Р0.7965Р5Р0.6079Р0.7092Р6Р0.4957Р0.6288Р7Р0.4098Р0.5410Р8Р0.3282Р0.4299Р9Р0.2410Р0.3112Р10Р0.1606Р0.2018Р11Р0.0966Р0.1146Р12Р0.0513Р0.0529Р0.0218Р1.3.4实际板层数的确定Р根据塔板效率公式:РET=NTNPР精馏段的实际理论板数:РNP=NTET=50.5=10Р提馏段的实际理论板数:РNP'=NTET=60.5=12Р总理论板数:РNPall=NP+NP'=10+12=22Р总实际塔板层数22块,进料位置11块板。Р1.4精馏塔的工艺条件及有关的物性数据的计算Р1.4.1操作压力计算Р精馏塔操作在常压下进行,则:Р塔顶操作压力 PD=4kPa表压=105.325kPa(绝压Р每层塔板压降取∆P=0.7kPaР则进料板的压力PF=105.325+10×0.7=112.325kPa(绝压)Р塔釜操作压力PW=105.325+22×0.7=120.725kPa(绝压)Р精馏段平均操作压强: