板式精馏塔的设计
4.8.2精馏段气液流量的计算
4.8.2精馏段气液流量的计算R2.65??0.726R?12.65?1xD0.8386??0.2298R?12.65?1精馏段操作线方程RxDx??0.726x?0.2298R?1R?1L?RD?2.65?0.0159?0.04214kmol/sy?V?(R?1)D?(2.65?1)?0.0159?0.05804kmol/s由之前计算得ML1?29.70kg/kmolMV1?35.35kg/kmol???L1?803.86kg/m3?V1?1.22kg/m3质量流量：L1?M??L1L?29.70?0.04214?1.2516kg/sV1?MV1V?35.35?0.05804?2.0517kg/s体积流量：Ls1?Vs1?L1??1.2516?1.557?10-3m3/s803.862.0517?1.6817m3/s1.22?L1V1?V14.8.3提馏段气液流量的计算L/?L?qF?0.04214?0.057?0.09914kmol/sV/?V?(q?1)F?0.05804kmol/sL0.09914??1.7080.05804V/W?xW0.0411?0.001175??0.0008321/0.05804V提馏段操作线方程W?xWL/y?/x-?1.708x-0.0008321VV/由之前计算得ML2?19.53kg/kmolMV2?26.85kg/kmol??/
?L2?844.14kg/m3?V2?0.9259kg/m3质量流量：L2?ML2L/?19.53?0.09914?1.9362kg/sV2?MV2V/?26.85?0.05804?1.5584kg/s体积流量：Ls2?Vs2?L2??1.9362?2.294?10-3m3/s844.141.5584?1.6831m3/s0.9259???L2V2?V2-16错误！未指定书签。错误！未指定书签。-
板式精馏塔的设计
4.9理论板图解和逐板计算
(1)xD?0.8386,y1?xD?0.8386根据表1乙醇水相平衡数据，内插0.8491-0.83250.8386-0.8325?0.8387-0.8182x1-0.8182解得x1?0.8257（2）y2?0.726?0.8257?0.2298?0.8239根据表1乙醇水相平衡数据，内插0.8325-0.81830.8293-0.8183?0.8182-0.7982x2-0.7982解得x2?0.8137（3）y3?0.726?0.8137?0.2298?0.8205根据表1乙醇水相平衡数据，内插0.8325-0.81830.8205-0.8183?0.8182-0.7982x3-0.7982解得x3?0.8013（4）y4?0.726?0.8013?0.2298?0.8115根据表1乙醇水相平衡数据，内插0.8183-0.80420.8115-0.8042?0.7982-0.7788x4-0.7788解得x4?0.7888（5）y5?0.726?0.7888?0.2298?0.8025根据表1乙醇水相平衡数据，内插0.8042-0.79260.8025-0.7926?0.7788-0.7599x5-0.7599解得x5?0.7760（6）y6?0.726?0.7760?0.2298?0.7932根据表1乙醇水相平衡数据，内插0.8042-0.79260.7932-0.7926?0.7788-0.7599x6-0.7599解得x6?0.7609（7）y7?0.726?0.7609?0.2298?0.7822根据表1乙醇水相平衡数据，内插 0.7926-0.780.7822-0.78?0.7599-0.7415x7-0.7415解得x7?0.7447（8）y8?0.726?0.7447?0.2298?0.7705根据表1乙醇水相平衡数据，内插0.78-0.75820.7705-0.7582?0.7415-0.7063x8-0.7063解得x8?0.7262（9）y9?0.726?0.7262?0.2298?0.7570根据表1乙醇水相平衡数据，内插0.7582-0.73610.7570-0.7361?0.7063-0.6727x9-0.6727解得x9?0.7045（10）y10?0.726?0.7045?0.2298?0.7413根据表1乙醇水相平衡数据，内插0.7582-0.73610.7413-0.7361?0.7063-0.6727x10-0.6727解得x10?0.6806-17错误！未指定书签。错误！未指定书签。-
板式精馏塔的设计
(11)y11?0.726?0.6806?0.2298?0.7239根据表1乙醇水相平衡数据，内插0.7361-0.71100.7239-0.7110?0.6727-0.6252x11-0.6252解得x11?0.6496（12）y12?0.726?0.6496?0.2298?0.7014根据表1乙醇水相平衡数据，内插0.7110-0.68760.7014-0.6876?0.6252-0.5811x12-0.5811解得x12?0.6071(13)y13?0.726?0.6071?0.2298?0.6912根据表1乙醇水相平衡数据，内插0.7110-0.68760.6912-0.6876?0.6252-0.5811x13-0.5811解得x13?0.5879(14)y14?0.726?0.5879?0.2298?0.6566根据表1乙醇水相平衡数据，内插0.6876-0.64700.6566-0.6470?0.5811-0.4892x14-0.4892解得x14?0.5112(15)y15?0.726?0.5112?0.2298?0.6009根据表1乙醇水相平衡数据，内插0.6144-0.59100.6009-0.5910?0.4000-0.3416x15-0.3416解得x15?0.3663(16)y16?0.726?0.3663?0.2298?0.4957根据表1乙醇水相平衡数据，内插0.5127-0.48680.4957-0.4868?0.1677-0.1377x16-0.1377解得x16?0.1480 板式精馏塔的设计 4.10实际板数的计算 4.10.1精馏段的计算由之前的计算可知：?1?2.633，?1?0.4112mPa?s查《化工工业设计手册》（上版）第2-163页ET1?0.49(?1?1)?0.245?0.49?(2.633?0.4112)?0.245?0.4996NP1?NT115??30.02块，取31块。ET10.4996 4.10.2提馏段的计算由之前的计算可知：?2?8.046，?2?0.3171mPa?s查《化工工业设计手册》（上版）第2-163页ET2?0.49(?2?2)?0.245?0.49?(8.046?0.3171)?0.245?0.3895NP2?NT22??5.135块，取6块。ET20.3895 5、主体设备设计 5.1精馏塔的塔体工艺尺寸计算 5.1.1塔径的计算 5.1.1.1精馏段的计算 由《板式塔设计设计》第27页得史密斯关联图 图6 史密斯关联图 由化工原理可知： ????L??VC?C20?L? u??安全系数??umax umax?C20? ??V0.2-19错误！未指定书签。错误！未指定书签。- 板式精馏塔的设计 ?V1?1.22kg/m3,?L1?803.86kg/m3Ls1?1.734?10?3m3/s,Vs1?1.789m3/s?L1?20.931.734?10????0.024881.7891.22??取板间距HT?0.40m，板上层液高度hL?0.05m横坐标K1?（?所以HT-hL?0.40-0.05?0.35m查图6得C20?0.07083Ls1?）（Vs1?V11L12）?31?803.86?2??20.93?所以C1?C20(L1)0.2?0.07083???2020??umax1?C10.2?0.07148?L1??V1803.86?1.22?0.07148??1.8334m/s?V11.22本设计中安全系数暂取0.78u1?0.78umax1?0.78?1.8334?1.430m/sD1?4VS14?1.789??1.262m,圆整后取D1?1.4m?u13.14?1.430?23.14D1??1.42?1.5444V1.789实际空塔气速为u1?S1??1.1617AT11.545.1.1.2提馏段的计算塔截面积为AT1??V2?0.9259kg/m3,?L2?844.14kg/m3Ls2?2.512?10?3m3/s,Vs2?1.626m3/s?L2?59.762.512?10?????0.04665 1.626?0.9259?取板间距HT?0.40m，板上层液高度hL?0.05m横坐标K2?（?所以HT-hL?0.40-0.05?0.35m查图6得C20?0.0750Ls2?）（Vs2?V21L22）?31844.14?2??59.76?所以C2?C20(L2)0.2?0.0750???2020??umax2?C20.2?0.09335?L2??V2844.14?0.9259?0.09335??2.8171m/s?V20.9259本设计中安全系数暂取0.78u2?0.78umax2?0.78?2.8171?2.1973m/sD2?4VS24?1.626??0.9709m,圆整后取D2?1.4m?u23.14?2.1973?23.14D2??1.42?1.5444V1.626实际空塔气速为u2?S2??1.0558AT21.54-20错误！未指定书签。错误！未指定书签。- 塔截面积为AT2?