设计说明书 - 图文

中国石油大学（华东）化工原理课程设计

3.3.3 理论塔板数NT与回流比R的确定

由吉利兰关联式：

??1?54.4X?(X?1)???11?117.2X?0.5?X? Y1?e?

Y?N?Nmin?N?1X

?R?Rmin?R?1

表3-9 数据表

R/Rmin R X (X-1)/X^0.5 1.125 1.2508 0.0617 -3.7759 1.25 1.3898 0.1163 -2.5912 1.375 1.5287 0.1649 -2.0567 1.5 1.6677 0.2084 -1.7341 1.625 1.8067 0.2476 -1.5122 1.75 1.9457 0.2831 -1.3475 1.875 2.0846 0.3154 -1.2191 2 2.2236 0.3449 -1.1155 2.125 2.3626 0.3720 -1.0297 2.25 2.5016 0.3969 -0.9573 2.375 2.6405 0.4199 -0.8952 2.5 2.7795 0.4412 -0.8412 2.75 3.0575 0.4795 -0.7516 2.875 3.1964 0.4968 -0.7140 3 3.3354 0.5129 -0.6802 3.125 3.4744 0.5280 -0.6495 3.25 3.6134 0.5422 -0.6216 3.375 3.7523 0.5556 -0.5961 3.5 3.8913 0.5683 -0.5727 3.75 4.1693 0.5915 -0.5312 由上表做出（R+1）N与R/Rmin关系图如下：

Y 0.5945 0.5374 0.4914 0.4533 0.4212 0.3936 0.3697 0.3486 0.3300 0.3134 0.2985 0.2849 0.2614 0.2510 0.2415 0.2327 0.2245 0.2169 0.2099 0.1970 N 18.2443 15.7459 14.1436 13.0184 12.1838 11.5389 11.0247 10.6046 10.2543 9.9576 9.7027 9.4813 9.1151 8.9618 8.8242 8.7000 8.5874 8.4846 8.3905 8.2243 N(R+1) 41.0638 37.6288 35.7653 34.7292 34.1958 33.9895 34.0071 34.1849 34.4809 34.8670 35.3230 35.8345 36.9840 37.6075 38.2566 38.9273 39.6165 40.3216 41.0406 42.5133 13

中国石油大学（华东）化工原理课程设计

图3-1 （R+1)N与R/Rmin关系图

在图中查得：

当[(R+1)*N]min=33.9895 R/Rmin=1.75

所以 R=1.75*1.1118=1.9457 所以理论塔板数NT=11.54

3.3.4 实际塔板数Np及进料位置的确定

N?NT?111.54?1??20.54 ET0,5131与所设N=21非常相近 所以实际塔板数Np=21 TD=85.1℃ Tw=132.35℃ 所以 αD=3.6332 αF=3.3048 αW=2.9430 由柯布铼德公式：

表3-10 塔顶、塔底相对挥发度数据表 A B 塔顶Pi/kPa 117.87 46.15 α 5.8062 2.2735 塔底Pi/kPa 399.13 180.78 α 4.3729 1.9806 C 20.30 1 91.28 1 14

中国石油大学（华东）化工原理课程设计

XAXBlog[()D()F]log?[W(*?F)0.5]NXBXA R?

XBNslog[XA0.5()F()W]log?[(D*?F)]XBXA0.99230.1987log[()D()F]log[(3.3048*2.9430)0.5]N0.00770.5166 R?

0.51660.4018Nslog[()F()W]log[(3.6332*3.3048)0.5]0.19870.0107 =0.7798

N R?0.7798

Ns

NR?Ns?21

所以Ns =11.8 NR =9.2 则进料位置为10块，与假设相同

3.4 验证清晰分割

log[(XXB)D(C)W]XCXB

log?mNmin ?1 ?0.00770.5875log[()D()W]XC0.40187.21 ?

log3.2415解得：XC?2.34*10?6?10?5 所以清晰分割验证成功

3.5 严格法计算

用化工过程模拟软件Aspen plus对物料衡算进行简捷法和严格法模拟，模拟的结果如下：

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中国石油大学（华东）化工原理课程设计

图3-2 简捷法模拟图

表3-11 物料衡算简捷法和模拟法模拟结果

C7-C8Stream IDTemperaturePressureVapor FracMole FlowMass FlowVolume FlowEnthalpyMass Flow C6H6 C7H8 C8H10-01Mass Frac C6H6 C7H8 C8H10-01Mole Flow C6H6 C7H8 C8H10-01Mole Frac C6H6 C7H8 C8H10-01 0.517 0.199 0.285kmol/hr 85.970 33.070 47.370 0.998 0.002 1 PPM 0.454 0.206 0.340 85.454 0.132 < 0.001 0.006 0.408 0.586kmol/hrkg/hrcum/hrGcal/hrkg/hr 6715.432 3047.090 5029.178 0.998 0.002 2 PPM 0.516 32.938 47.370 0.517 0.199 0.285Cbar01 110.0 1.600 0.000 166.410 14791.700 18.963 1.535 6675.139 12.188 0.012 0.005 0.374 0.621 85.970 33.070 47.370 0.992 0.008 21 PPM02 91.7 1.419 0.000 85.587 6687.339 8.343 1.202 40.293 3034.902 5029.166 0.454 0.206 0.340 85.110 0.661 0.002 0.011 0.402 0.58703 140.8 1.560 0.000 80.824 8104.360 10.773 0.397 6715.432 3047.090 5029.178 0.991 0.009 28 PPM 0.860 32.409 47.36804 104.4 1.219 0.200 166.410 14791.700 843.342 1.741 6648.278 60.943 0.189 0.008 0.369 0.62205 80.3 1.013 0.000 85.774 6709.411 8.241 1.167 67.154 2986.147 5028.98906 133.1 1.292 0.000 80.637 8082.289 10.628 0.367

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