应化2006-2 太井超课程设计- 1 - - 1 -化学工程学院应化2006-2 太井超化工原理课程设计化工原理课程设计苯―甲苯双组分连续精馏筛板塔的设计学院、系：化学工程学院专业班级：应用化学0６级2班学生姓名：太井超（120063301005）指导教师：张泉泓赵振宁成绩：200９年６月２日应化2006-2 太井超课程设计- 2 - - 2 -化学工程学院应化2006-2 太井超化工原理课程设计目录序言 (3)第一部分工艺设计物料衡算 (4)塔顶温度、塔底温度及Rmin (4)确定最佳操作回流比及塔板层数 (7)第二部分结构设计塔顶实际气液相体积流量 (18)塔板间距HT的选择 (19)确定液泛的动能参数 (19)计算液泛速度UF （Umax） (19)空塔气速UG (19)确定溢流方式 (19)根据VG求D (20)计算圆整后实际气速 (20)确定溢流堰高度hw 及堰上液层高度how (20)板面筛孔位置设计 (21)水力学性能参数的计算、校核 (21)负荷性能图及操作性能评定 (25)筛板塔工艺设计计算结果总表 (27)第三部分结束语结束语………………………………………………………………… 28 应化2006-2 太井超课程设计- 3 -序言- 3 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 4 -苯—甲苯双组分连续精馏筛板塔的设计第一部分工艺设计一、物料衡算原料苯（78/Mkgkmol=）甲苯（92/Mkgkmol=）馏出液中低沸点组分的含量不低于0.97(质量分率)进料组成0.6780.63890.60.47892F x==+流出液组成0.97780.97440.970.037892D x==+14000/Fkgh= 将F换成/kmolh平均摩尔质量0.6389780.36119283.055/Mkgkmol=×+×=14000/168.563/83.055/kghFkmolhkgkmol==回收率0.98DAF DxFxη== 0.97440.98168.5630.6389D×=×流出液的流量0.98168.5630.6389108.314/0.9744Dk××==釜底流量168.563108.31460.249/WFDkmolh=−=−=易挥发组分（苯）物料衡算FD FxDxWx=+釜底组成168.5630.6389108.3140.974460.2490.03575FDw FxDxxW−×−×===二、塔顶温度、塔底温度及min R1、确定操作压力760PmmHg=顶- 4 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 5 -假设有25块板10076025943.82413.6PmmHg=+×=底2、计算塔顶温度（露点）tα设81.35o tC=αlg oAAAAa BPACt=−+据查表得：1211ln6.906220.8oAa Pt=−+代入数据得：1211lg6.9062.8987281.35220.8oA P=−=+790.782oA PmmHg=790.7821.0450760oAA PKP===顶1344ln6.9532.4817281.35219.4oBBBBa BPACt=−=−=++同理，304.91mm oB PH=304.910.401197760oBB PKP===顶AAA yxK= 其中AD yx=0.97440.936471.0405AAA yxK===BBB yxK= 其中1BA yy=−0.02560.0638090.401197BBB yxK===- 5 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 6 -110.936470.06380910.000280.0004iAB xxx−=−−=+−=<Σ所以确定塔顶温度83.15o tC=顶790.7822.593493304.91oAoB PPα∴===顶3、塔底温度tβ（泡点）设塔底温度116.77o tCβ=lg oAAAA BPACtβ=−+ lg oBBBB BPACtβ=−+查表得：1211lg6.906220.81344lg6.953219.4oAoB PtPtββ=−+=−+代入数据得：1211lg6.9063.318596220.8116.771344lg6.9532.95500219.4116.77oAoB PP=−=+=−=+2082.552oA PmmHg= 901.608oB PmmHg=2082.5520.078883943.824oAAw PyxP===底同理901.608(1)0.964250.9211306943.824oBBw PyxP=−=×=底110.0788830.921130610.000014(0.0004)AB yiyyε−=+−=+−=<Σ所以确定116.77o tC=底应化2006-2 太井超课程设计- 7 -B2082.5522.30979901.618oAo PPα===底所以 2.5934932.309792.44753ααα=×=×=顶底4.求最小回流比min R泡点进料q=10.6389PF xx==2.447530.63890.81241(1)11.447530.6389PPP xyxαα×===+−+×最小回流比min0.97440.81240.93370.81240.6389DDPP xyRyx−−===−−三、确定最佳操作回流比及塔板层数1、确定最佳操作回流及理论塔板数采用逐板法计算R=（1.1，1.2, 1.3，1.4, 1.5，1.6，1.7，1.8, 1.9, 2.0）min R 的理论塔板层数已知条件有0.6389F x=0.9744D x= 0.03575w x=168.563/Fkmo= 108.314/Dkmolh= 60.249/Wkmo =2.44753α= min0.9337R=(1) min1.11.10.93371.0271RR=×=×=相平衡方程1(1)2.447531.44753nnnnn yyxyyα==−−−精馏段：10.50690.480711Dnnn xRyxxRR+=+=+++Y 1=XD=0.9744 X1=0.9396 Y2=0.9570 X2=0.9009Y3=0.9374 X3=0.8595 Y4=0.9164 X4=0.8175Y5=0.8949 X5=0.7983 Y6=0.8854 X6=0.7594- 7 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 8 -Y 7 =0.8656 X 7 =0.7246 Y 8 =0.8480 X 8 =0.6951Y 9 =0.8330 X 9 =0.6708 Y 10 =0.8207 X 10=0.6516Y 11 =0.8110 X 11 =0.6368 X 11 =0.6368＜X F （0.6389）所以此操作回流比下精馏段理论塔板数为11（块） 提馏段：11.27440.00981mnn LFWyxLFWLFWx ++=−+−+−=− X 0=F x =0.6389Y 1=0.8044 X 1 =0.6269 Y 2 =0.7891 X 2=0.6045Y 3=0.7606 X 3 =0.5649 Y 4 =0.7101 X 4 =0.5002Y 5 =0.6276 X 5=0.4078 Y 6 =0.5099 X 6 =0.2083Y 7=0.3703 X 7=0.1937 Y 8 =0.2370 X 8 =0.1126Y 9 =0.1327 X 9 =0.05932 Y 10=0.06579 X 10 =0.02797X 10=0.02797＜X W （0.03575）此操作回流比下提馏段理论塔板数为10（块） 全塔理论塔板数N T =11+10-1=20（块）(2) min R=1.2R1.20.93371.12044=×=相平衡方程 1(1)2.447531.44753nnnnn yyxyy α==−−− 精馏段：10.52840.459511Dnnn xRyxxRR +=+=+++Y 1=X D =0.974 X 1 =0.9396 y 2=0.9560 X 2 =0.8988y 3 =0.9344 X 3 =0.8534 y 4 =0.9104 X 4 =0.8059- 8 -化学工程学院 应化 2006-2 太 井 超 化工原理课程设计应化 2006-2 太 井 超 课程设计 - 9 -y 5 =0.8853 X5=0.7592 y6 =0.8607 X6 =0.7163y7 =0.8380 X7=0.6908 y8 =0.8245 X8 =0.6575y9 =0.8069 X9=0.6306＜XF（0.6389）所以此操作回流比下精馏段理论塔板数为9（块）提馏段：11.26230.00938wmnn WxDRFyxDRFWDRFWx++=−+−+−=−X 0= XF=0.6389y 1=0.7971 X1=0.6161 y2 =0.7683 X2=0.5753y 3=0.7168 X3=0.5084 y4 =0.6324 X4=0.4128y 5=0.5117 X5=0.2998 y6 =0.3691 X6 =0.19296y 7 =0.2341 X7=0.1110 y8 =0.1307 X8 =0.05787y 9=0.000543 X9=0.000222＜XW（0.03575）此操作回流比下提馏段理论塔板数为9（块）全塔理论塔板数NT=9+9-1=17（块）(3) min1.31.30.93371.2138RR==×=相平衡方程1(1)2.447531.44753nnnnn yyxyyα==−−− 精馏段：10.54830.440111Dnnn xRyxxRR+=+=+++y=XD =0.9744 X1=0.9396 y2 =0.9553 X2 =0.8972y3 =0.9320 X3=0.8485 y4 =0.9053 X4 =0.7962y5 =0.8767 X5=0.7439 y6 =0.8480 X6 =0.6951y7=0.8212- 9 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 10 -X7=0.6524 y8 =0.7978 X8 =0.6172＜X F （0.6389）所以此操作回流比下精馏段理论塔板数为8（块）提馏段：11.25130.00898wmnn WxDRFyxDRFWDRFWx++=−+−+−=−X 0=XF=0.6389y 1 =0.7905 X1=0.6066 y2=0.7501 X2 =0.5508y 3 =0.6802 X3=0.4650 y4=0.5729 X4 =0.3540y 5 =0.4320 X5=0.2386 y6=0.2896 X6 =0.1176y 7 =0.1382 X7=0.06149 y8 =0.06796X 8=0.02893＜XW（0.03575）此操作回流比下提馏段理论塔板数为8（块）全塔理论塔板数NT=8+8-1=15（块）(4) min1.41.40.93371.3072RR==×=向平衡方程1(1)2.447531.44753nnnnn yyxyyα==−−− 精馏段：10.56660.422311Dnnn xRyxxRR+=+=+++y1=XD=0.9744 X1=0.9396 y2 =0.9547 X2 =0.8959y3 =0.9299 X3=0.8442 y4 =0.9006 X4 =0.7873y5 =0.8684 X5=0.7294 y6=0.8356 X6 =0.6750y7 =0.8048 X7=0.6275＜XF（0.6389）所以此操作回流比下精馏段理论塔板数为 7（块）提馏段：- 10 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 11 -11.24110.00862wmnn WxDRFyxDRFWDRFWx ++=−+−+−=−X 0 =X F =0.6389y 1 =0.7843 X 1=0.5977 y 2=0.7332 X2=0.5289 y 3 =0.6478 X 3=0.4291 y 4=0.5239 X4=0.3110 y 5 =0.3734 X 5=0.1958 y 6=0.2344 X6=0.1112y 7 =0.1294 X7=0.05725 y 8 =0.06243X 8=0.02649＜X W （0.03575）此操作回流比下提馏段理论塔板数为8（块） 全塔理论塔板数N T =7+8-1=14（块）(5) min 1.51.50.93371.4006RR ==×=向平衡方程 1(1)2.447531.44753nnnnn yyxyy α==−−− 精馏段：10.58340.405911Dnnn xRyxxRR +=+=+++y 1=XD=0.9744 X 1 =0.9396 y 2 =0.9541 X 2 =0.8947y 3 =0.9279 X 3=0.8402 y 4 =0.8961 X 4 =0.7789y 5 =0.8603 X5=0.7156 y 6=0.8234 X 6 =0.6558y 7 =0.7885 X7=0.6037＜X F （0.6389）所以此操作回流比下精馏段理论塔板数为 7（块） 提馏段：11.23170.00828wmnn WxDRFyxDRFWDRFWx ++=−+−+−=−应化 2006-2 太 井 超 课程设计 - 12 -X 0 =X F =0.6389y 1 =0.7786 X 1=0.5896 y 2=0.7179 X2=0.5097 y 3 =0.6195 X 3=0.3995 y 4=0.4838 X4=0.2769 y 5 =0.3328 X 5=0.1693 y 6=0.2002 X6=0.09278y 7 =0.1060 X7=0.04621 y 8 =0.04864X 8=0.02046＜X W （0.03575）此操作回流比下提馏段理论塔板数为8（块） 全塔理论塔板数N T =7+8-1=14（块）(6) min 1.61.60.93371.4939RR ==×=向平衡方程 1(1)2.447531.44753nnnnn yyxyy α==−−− 精馏段：10.59900.390711Dnnn xRyxxRR +=+=+++y 1=X D=0.9744 X1=0.9396 y 2=0.9535 X 2 =0.8934y 3 =0.9258 X 3=0.8360 y 4 =0.8915 X 4 =0.7705 y 5 =0.8522 X5=0.7020 y 6 =0.8112X 6 =0.6371 ＜X F （0.6389）所以此操作回流比下精馏段理论塔板数为 6（块） 提馏段：11.22300.00791wmnn WxDRFyxDRFWDRFWx ++=−+−+−=− X 0 =X F =0.6389y 1 =0.7735 X 1=0.5825 y 2 =0.7545 X 2=0.4934- 12 -化学工程学院 应化 2006-2 太 井 超 化工原理课程设计应化 2006-2 太 井 超 课程设计 - 13 -y 3=0.5955 X3=0.3756 y4 =0.4514 X4=0.2516y 5=0.2998 X5=0.1487 y6 =0.1740 X6 =0.07925y 7 =0.08901 X7=0.03839 y8 =0.03904X 8 =0.01633＜XW（0.03575）此操作回流比下提馏段理论塔板数为8（块）全塔理论塔板数NT=6+8-1=13（块）(7) min1.71.70.93371.5873RR=×=×=向平衡方程1(1)2.447531.44753nnnnn yyxyyα==−−− 精馏段：10.61350.376611Dnnn xRyxxRR+=+=+++y 1=XD=0.9744 X1=0.9396 y2=0.9530 X2 =0.8923y 3 =0.9240 X3=0.8324 y4 =0.8872 X4 =0.7627y 5 =0.8445 X5=0.6893 y6 =0.79995X 6 =0.6197＜XF（0.6389）所以此操作回流比下精馏段理论塔板数为 6（块）提馏段：11.21500.00769wmnn WxDRFyxDRFWDRFWx++=−+−+−=−X 0=XF=0.6389y 1=0.7686 X1=0.5757 y2 =0.6918 X2=0.4784y 3=0.5736 X3=0.3547 y4 =0.4233 X4=0.2307y 5=0.2726 X5=0.1328 y6 =0.1537 X6 =0.6908- 13 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 14 -y 7 =0.07624 X7=0.03262＜XW（0.03575）此操作回流比下提馏段理论塔板数为7（块）全塔理论塔板数NT=6+7-1=12（块）(8) min1.81.80.93371.6807RR==×=相平衡方程1(1)2.447531.44753nnnnn yyxyyα==−−− 精馏段：10.62700.363511Dnnn xRyxxRR+=+=+++y 1=0.9744 X1=0.9396 y2=0.9526 X2 =0.8914y 3 =0.9224 X3=0.8293 y4 =0.8835 X4 =0.7560y 5 =0.8375 X5=0.6780 y6 =0.7886X 6 =0.6038＜XF（0.6389）所以此操作回流比下精馏段理论塔板数为 8（块）提馏段：11.20750.00742wmnn WxDRFyxDRFWDRFWx++=−+−+−=−X 0=XF=0.6389y 1 =0.7641 X1=0.5696 y2 =0.6804 X2=0.4652y 3=0.5543 X3=0.3369 y4 =0.3994 X4=0.2137y 5=0.25061 X5=0.1202 y6 =0.1377 X6 =0.06125y 7 =0.06654 X7=0.02830＜XW（0.03575）此操作回流比下提馏段理论塔板数为7（块）全塔理论塔板数NT=6+7-1=12（块）(9) min1.91.90.93371.7740RR==×=- 14 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 15 -相平衡方程1(1)2.447531.44753nnnnn yyxyyα==−−− 精馏段：10.63950.359611Dnnn xRyxxRR+=+=+++y 1=XD=0.9744 X1=0.9396 y2=0.9605 X2 =0.9086y3 =0.9406 X3=0.8661 y4 =0.9135 X4 =0.8118y 5 =0.8787 X5=0.7475 y6 =0.8376 X6 =0.6752y7=0.2933 X7=0.6106 ＜XF（0.6389）所以此操作回流比下精馏段理论塔板数为 7（块）提馏段：11.20050.00717wmnn WxDRFyxDRFWDRFWx++=−+−+−=−X 0 =XF=0.6389y 1 =0.7598 X1=0.5638 y2 =0.6697 X2=0.4531y 3=0.5368 X3=0.3213 y4 =0.3786 X4=0.1993y 5=0.2321 X5=0.1099 y6 =0.1247 X6 =0.05501y 7 =0.05887 X7=0.02492＜XW（0.03575）此操作回流比下提馏段理论塔板数为7（块）全塔理论塔板数NT=7+7-1=13（块）(10) min2.02.00.93371.8674RR==×=相平衡方程1(1)2.447531.44753nnnnn yyxyyα==−−−精馏段：10.65130.339811Dnnn xRyxxRR+=+=+++- 15 -化学工程学院应化2006-2 太井超化工原理课程设计应化2006-2 太井超课程设计- 16 -y 1=0.9744 X1=0.9396 y2=0.9518 X2 =0.8897y 3 =0.9193 X3=0.8231 y4 =0.8677 X4 =0.7282y 5 =0.8141 X5=0.6415 y6 =0.7576X 6 =0.5608＜XF（0.6389）所以此操作回流比下精馏段理论塔板数为 6（块）提馏段：11.19400.00694wmnn WxDRFyxDRFWDRFWx++=−+−+=−X 0 =XF=0.6389y 1=0.6627 X1=0.4453 y2=0.5247 X2 =0.3108y 3 =0.3642 X3=0.1897 y4=0.2196 X4 =0.1031y 5 =0.1162 X5=0.05098 y6 =0.0539X 6 =0.02274＜XW（0.03575）此操作回流比下提馏段理论塔板数为6（块）全塔理论塔板数NT=6+6-1=11（块）回流比R为1.12.0倍:min R，步长为0.1min R时各塔段及全塔理论塔板数如下表： R为n倍min R 全塔理论塔板数NTR为n倍min R 全塔理论塔板数NT1.1 20 1.6 13 1.2 17 1.7 12 1.3 15 1.8 12 1.4 14 1.9 13 1.5 142.0 11。