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1、目录第一部分 工艺设计 物料衡算2塔顶温度、塔底温度及R 2min 确定最佳操作回流比及塔板层数4第二部分 结构设计 塔顶实际气液相体积流量12塔板间距H的选择 13T确定液泛的动能参数 13计算液泛速度U(U ) 14F max空塔气速U 14G 确定溢流方式14根据V求D 14G计算圆整后实际气速 14确定溢流堰高度h及堰上液层高度h 15w ow板面筛孔位置设计 15水力学性能参数的计算、校核 16负荷性能图及操作性能评定 17筛板塔工艺设计计算结果总表 18第三部分 结束语结束语19甲苯二甲苯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 甲苯 (M=92kg/kmol) 二甲
2、苯 (M=106kg/kmol)F=12500kg/h 将 F 换成 kmol/hF=12500X0.45/92+12500X (l-0.45)/106=126.00kmol/h馏出液中低沸点组分的含量不低于0.952XF = 0.45/(0.45/92+0.55/106)=0.485XD =0.952/920.952/92+(1-0.952)/106=0.9581D XD/F XF=0.962DFD =0.962 X 126.00 X 0.4852/0.9581=61.38kmol/hW =FD =126.0061.38=64.62F XF = D XD+WXWFD WXW =(F XD X
3、)/W=(126.00X0.485261.38X0.9581)/64.62=0.036WFD二、塔顶温度、塔底温度及Rmin1、确定操作压力P 顶=760mmHgP 底=760+28X 100/13.6=965.882 mmHg2、计算塔顶温度td (露点)设 td =112=A.-B./(C.+1)A i i i dAA=6.953 BA=1344 CA=219,4AB=7,000 BB=1463 CB=214.7BBBlgp0A =AA-BA/(CA+td)= 6.953-1344/(112+219.4)P0A =789.73mmHgKA = PoA/P 顶=789.73/760=1.03
4、9lgP0B =ABBB/(CB+td)= 7.0001463/(112+214.7)同理，PoB = 332.57mmHgKB=0.4376Bx =y / k 其中 y 二 xA A A A DxA=yA/ KA =0.9581/1.039=0.9221XB = yB/ KB 其中 yB=1 yA =1 0.9581=0.0419BBBB AxB = yB/ KB =0.0419/0.4376=0.0957BBBI SXi 1 I = |XA+ XB1 I=I 0.9221+0.0957 1 I =0.0178e(0.0004) 设 td =112.7rlgP0A =AABA/(CA+td)
5、= 6.9531344/(112.7+219.4)P0A =805.43mmHgKA = p0A/P 顶丸060lgP0B =ABBB/(CB+td)= 7.0001463/(112.7+214.7)同理，P0B = 339.99mmHgKB=0.4473x =y / k 其中 y 二 xA A A A DxA=yA/ KA =0.9039XB = yB/ KB 其中 yB=1 yA =1 0.9581=0.0419BBBB AxB = yB/ KB =0.0937BBBI SXi 1 I = IXA+ XB1 I=I 0.9039+0.0937 1 I =0.024e(0.0004)设 td
6、 =112.6tlgP0A =AABA/(CA+td)= 6.9531344/(112.6+219.4)P0A =803.12mmHgKa = P0a/P 顶=1.057lgP0B =ABBB/(CB+td)= 7.0001463/(112.6+214.7)同理，PoB = 338.92mmHgKB=0.4459x =y / k 其中 y 二 xA A AA DxA=yA/ KA =0.9064XB =yB/KB其中 yB=1 yA=1 0.9581=0.0419BBBBAxB =yB/KB=0.09396BBBI SXi 1 I = |XA+ XB1 I=I 0.9064+0.09396 1
7、 I =0.00036(0.0004)设 tb =149rP0A =2017.4mmHgKA =2.0886同理，P0B =949.41KB=0.9829BByA = 0.075 yB = 0.9475I 2yi 1 I = IyA+ yB1 I=I 0.075+0.9475 1 I =0.0225e(0.00004)设 tb =148rbP0A =1971.79mmHgKA =2.0414同理，P0B =925.47KB=0.9582BByA = 0.073 yB = 0.9236I 2yi 1 I = IyA+ yB1 I=I 0.073+0.92361 I =0.0033e(0.0004
8、)设 tb =148.1cbP0A =1976.32mmHgKA =2.0461同理，P0B =927.84KB=0.9606BByA = 0.0737yB = 0.9260I 2yi 1 I = IyA+ yB1 I=| 0.0737+0.9260 1 I =0.00026V（0.0004） a 底二 P0A /PB =1976.32/927.84=2.1300= 148.1ca =（ a 顶 X a 底）1/2=（2.3696 X 2.1030） 1/2 =2.2474.求Rminq=1Xe= XF =0.4852ye =aXe/1+（a1）Xe =2.247X0.4852/1+（2.24
9、71）X0.4852=0.6793Rmin=X ye） / （yeXe） = （0.95810.6793） / （0.67930.4852） =1.4364 D三、确定最佳操作回流比及塔板层数R=（1.1, 1.3, 1.5, 1.7, 1.9） Rmin采用逐板法计算（1.2, 1.4, 1.6, 1.8, 2.0） Rmin采用捷算法计算 逐板法计算R= R=1.1Rmin =1.1X1.4364=1.580精馏段：Xn =yn/a（a1）yn = yn /2.2472.2471）XynnYn+1 n=XnR/（R+1）+ XD/（R+1）=0.6124 X+0.3713X1=0.9150
10、y2=0.9289X2=0.85326y3 =0.8938X3=0.3793y4=0.7236X4=0.7124y5 =0.8144X5=0.66137y6=0.7763X6=0.6070y7 =0.7430X7=0.5627y8=0.7159X8=0.5286y9 =0.6950X9=0.503510 =0.6797X10 =0.4856y11=0.6687X11 =0.4732VXf （0.4852）所以此操作回流比下精馏段理论塔板数为10（块）提馏段：Ym+1= (R+qXF/D) Xn/ (R+l)(l q)XF/D(F/D 1)、/ (R+l) (1 q)XF/D=1.4081 人一
11、0.01469y12 =0.6516X12=0.4543y14 =0.5849X14=0.3854y16 =0.4534X16=0.26961616y18 =0.2721X18=0.14261818y20 =0.1154X20=0.0548y13 =0.6249X13 =0.4258y15 =0.5280X15 =0.332415 15y17 =0.3649 X17 =0.2036y19 =0.1861X19 =0.09241919y21 =0.0625X21VXW (0.036)2121W此操作回流比下提馏段理论塔板数为10（块）全塔理论塔板数叫=20 （块） R=1.3Rminmin精馏段：X1 =0.9105X3 =0.7786X5 =0.62815X7 = 0.51038提馏段：Y9 =0.6305y11 =0.5031y13 =0.3113y15 =0.135915时，y2 =0.9217y4 =0.8412y6 =0.74326y8 =0.66658X9 =0.4316X11 =0.3106X13 =0.1674X15 =0.065415 R=1.5Rmin 时， min精馏段：X1 =0.9105y2 =0.9256X2 =0.8499y3 =0.8877X4 =0.7022y5 = 0.795145X6
