塔板数

The following points are emphasized:The operation models of adiabatic and diabatic distillation have been set up and the operation block, thermodynamics model and mathematical model in the simulation have been determined as well;(2)Based on the simulation and exergy analysis with Aspen Plus program, shortcut distillation design—DSTWU model and rigorous distillation design—RADFRAC model, the author has determined the heat duty, exergy losses and the distribution of exergy losses along the adiabatic column, which will help the simulation and optimization of the diabatic distillation;(3)Diabatic distillation under various operation conditions has been simulated by using energy balance method and exergy analysis;(4)How the different mixture and the various degree of separation, number of trays and feed location influence exergy saving in diabatic distillation have also been discussed;(5)On the basis of the total exergy losses along the column, different schema of the heat transfer distribution along the column have been compared and analyzed;they can be classified in three categories: heat duty equipartition approach, empirical approach, separation degree matching approach. In conclusion, different heat transfer distribution along the column will have effect on total exergy losses. In particular, most satisfactory results have been obtained by using separation degree matching approach. In order to diminish the exergy losses, heat transfer distribution should meet the needs of the request of separation degree.And on this premise, the author makes his suggestion in increasing the proportion of heat supplied to the tray with minimum exergy losses and decreasing the proportion of heat supplied to the tray with the maximum exergy losses.

本文对透热精馏过程进行了模拟并对其节能效果的影响因素做了较为全面的分析和深入的研究，主要研究内容如下：(1)建立了常规精馏和透热精馏过程的模拟操作模块、热力学模型以及数学模型；(2)利用化工模拟软件Aspen Plus并分别采用DSTWU简捷模型和RADFRAC严格计算模型对常规精馏进行模拟计算和有效能分析，确定常规精馏塔的公用工程热负荷、有效能损失及有效能损失在塔内的分布，为透热精馏的模拟和优化提供数据参考；(3)对不同物系在不同分离度条件下进行透热精馏的模拟，分别采用能量衡算法和有效能分析法进行计算和分析；(4)探讨了各种因素如物系的选择、不同分离度、塔板数、进料位置对透热精馏节能效果的影响；(5)以全塔总有效能损失为比较基准，对热量在塔内的三种分布方案即热负荷平均分配法、经验法和分离度匹配法进行了对比分析并得出结论：塔内热量的不同分布方案对于全塔总有效能损失会产生影响，其中以分离度匹配法的节能效果最为理想，为减少有效能的损失，应使塔内的热量分布满足各塔板的分离度要求，并在此前提下，尽量减小有效能损失大的塔板的热负荷和增加有效能损失小的塔板的热负荷。

In addition, the auxiliary materials for fractionation is decided for different products by test.

同时，针对不同的产品，通过试验确定投入的分馏辅料及分馏塔板数。

This paper introduce an Excel-based graphic solution to the theoretical plate numbers of a rectification column and a VBA program.

介绍了用Excel图解法求精馏塔理论塔板数，并给出了VBA程序。

Finally, with the language of VB, the process of extractive rectification was simulated with the method of tri-opposite angles matrix and the effect was researched the ratio of raw and solvent, theory plate number and the feed position of raw and the solvent on the purity of mesitylene was studied.

编制VB程序，结合三对角矩阵法模拟萃取精馏过程，并考察了回流比、溶剂比、理论塔板数、溶剂及原料进料位置对萃取分离效果的影响，为下一步的小试提供了数据基础。

The unit of 1000t/a methylal synthesis by fluidized catalytic distillation was designed according to the results of equilibrium stage simulation, together with the consideration of the existence of plate efficiency and utilization ratio of catalyst.

在模拟过程中，探讨了塔板数、空时、回流比等对催化精馏效果的影响，分析了各因素对催化精馏的耦合影响关系，得到了较适宜的理论塔板数、空时和回流比，为本体系的工业性试验用催化精馏塔设计提供了依据。

Theoretical plates of propyl alcohol is 9.9×10^4 plates/m; resolution of ethanol and propyl alcohol is 4.66; RSD of correction factor of relative mass is 1.67% Good linearity with correlation coefficient 0.999 is observed over the range 45.0%~85.0% of ethanol in solvent. The method recovery for ethanol is 100.4% with RSD 1.69%; he RSD of accuracy is 1.74%.

结果：系统实用性实验测得正丙醇理论塔板数为99000，乙醇与正丙醇分离成4.66，相对质量校正因子的变异系数为1.67%；该方法在乙醇百分含量范围45.0%-85.0%内呈良好的线形关系，相关系数为0.999；平均回收率为100.4%， RSD为1.69%；精密度相对标准偏差为1.74%。

Theoretical plates of propyl alcohol is 9.9 ×104 plates/m; resolution of ethanol and propyl alcohol is 4.66; RSD of correction factor of relative mass is 1.67 % Good linearity with correlation coefficient 0.999 is observed over the range 45.0%-85.0%of ethanol in solvent.

结果：系统实用性实验测得正丙醇理论塔板数为99000，乙醇与正丙醇分离度为4.66，相对质量校正因子的变异系数为1.67％；该方法在乙醇百分含量范围45.0％-85.0％内呈良好的线形关系，相关系数为0.999；平均回收率为100.4％，RSD为1.69％；精密度相对标准偏差为1.74％。

Our company also supply SunTech column, the column theoretical plate number up to 80,000 / m and above, PH 2.0-9.2 around tailing factor 0.90-1.12, while the prices of imports of the same specification, only the other half of the column .

我公司另外还供应suntech 色谱柱，此色谱柱理论塔板数可达80000块/米以上，PH 2.0-9.2左右，拖尾因子0.90-1.12，而价格只有其他相同规格进口色谱柱一半。

The theoretical plate of analytical column is related with the flow rate of mobile phase, the type of sample and the injection quantity.

本实验发现DNB-Leucine CSP分析柱理论塔板数的测定与流动相的流量、标定物的种类和进样量有一定的关系。

A relational expression between column plate number and peak plate number was deduced.

在计算色谱柱塔板数时，应区分色谱柱塔板数和色谱峰塔板数(是由实际色谱峰形得到的，在色谱过程中实际发生的)，因色谱柱塔板数与色谱峰塔板数是不同的概念。

This one mode pays close attention to network credence foundation of the businessman very much.

这一模式非常关注商人的网络信用基础。

Cell morphology of bacterial ghost of Pasteurella multocida was observed by scanning electron microscopy and inactivation ratio was estimated by CFU analysi.

扫描电镜观察多杀性巴氏杆菌细菌幽灵和菌落形成单位评价遗传灭活率。