【已应助】丙烯精馏塔过程模拟

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2010/12/11

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论文学科】化学工程论文
【论文级别】硕士论文,硕士毕业论文,硕士研究生论文
【中文关键词】丙烯精馏塔论文; Aspen Plus论文; Aspen Dynamics论文; 稳态模拟论文; 动态模拟论文; 优化论文
【中文题名】丙烯精馏塔过程模拟
【英文题名】Process Simulation for Propylene Rectification Tower
【所属分类】工程科技I,有机化工,基本有机化学工业
【英文关键词】propylene rectification tower; Aspen Plus; Aspen Dynamics; stable-state simulation; dynamics simulation; optimization

【中文摘要】利用Aspen Plus及Aspen Dynamics模拟软件对丙烯精馏塔的操作进行了稳态及动态模拟,通过模拟结果与实际操作结果的对比,验证了DJ型塔板具有高效率和大通量的优点,利用模拟结果与设计数据的对比关系,对液泛系数模拟值进行了76%的合理修正,开辟了以普通塔板代替DJ型塔板进行过程模拟的新方法,得出该塔的理论板数为128块,多于改造设计的估算值118块,表明改造设计对理论塔板数估算偏少导致实际塔板数不足是第一次改造不成功的主要原因。确立了合理的模拟优化步骤:确定模拟输入初值→最佳进料位置→最佳回流比→最佳产出量范围→其他优化参数。总结出了丙烯精馏塔的优化调整规律:在相同进料组成下,当进料量增加时,最佳回流比及最佳进料位置固定不变,塔釜产出量增大,产出量的可调整范围也相应扩大,塔顶冷却器负荷、塔釜再沸器负荷增大,塔釜温度基本不变,液泛系数增大;在相同进料量下,当进料组成中丙烷含量增加(来源:Aad2dBC论文网www.abclunwen.com)时,最佳进料位置板数增大,最佳回流比增大,塔釜产出量增大,产出量的可调整范围也相应扩大,塔顶冷却器负荷、塔釜再沸器负荷增大,塔釜温度降低,液泛系数增大。操作优化后,塔顶丙烯浓度在99.63%~99.65%,塔釜丙烯浓度在5.43%~7.92%。两塔位置对换,有利于大加工量下的操作。动态特性表明,无论是进料量、进料组成还是回流量扰动,均对操作产生了较大影响,主要体现在406塔釜温度、冷却器负荷、再沸器负荷、塔顶丙烯浓度、塔釜丙烯浓度、塔顶产出量、塔釜产出量的波动上,尤其是塔顶产出量和塔釜产出量不仅波动大,而且响应迅速,塔顶丙烯浓度及塔釜丙烯浓度的响应速度缓慢,波动持续时间均超过3h,动态特性要求操作人员必须采取比较平稳且循序渐进的方式进行操作调整。仪表调节规律对动态特性具有重要的影响。(来源:ABabC论文0808网www.abclunwen.com)

【英文摘要】 The process of propylene rectification tower was simulated in stable-state and dynamic simulation with Aspen Plus and Aspen Dynamics.The high efficiency and large throughput of DJ type plates were verified by comparing the simulateion results with practical operating results.The simulation value of flooding modulus was modified reasonably by 76% using the contrast results between simulation results and design data.A new way of process simulation with common plates instead of DJ type was created accordingly.It was found that the number of theoretical plates was 128,more than designed number of 118 for reconstruction,which indicated that the main reason failed the reconstruction for the first time was the lack of plates due to estimated less of designed theoretical number of plates.Reasonable optimum simulation process were:confirmation of simulation input initial value―best feed inlet―best reflux ratio― best yield range― other optimized parameters.The optimized adjusting rules for propylene rectification tower were summarized as following:with the same composition but increased amount of feed, the best reflux ratio and feed inlet kept unchanged, and the yield of column went up, the adjusting range of yield expanded respectively,the load of overhead condenser and column reboiler raised,the temperature of column stabilized and the flooding modulus added too;with the same amount of feed but increased content of propane,the number of plates in the best feed inlet,the best reflux ratio and the yield of column increased respectively,and the adjusting range of yield expanded,load of overhead condenser and column reboiler raised,column temperature down and flooding modulus up.Followed with optimized process,the concentration of propylene overhead kept at 99.63% to 99.65%,and the concentration in column pot lied from 5.43% to 7.92%.Exchanging the two towers position was beneficial to process under large amount.Dynamics properties showed that the amount or composition of feed,or quantity of reflux disturbance all had relatively great impact on the process,which mainly reflected on the fluctuation of 406 tower pot temperature,condenser and reboiler load,concentration of propylene over and in the column,the yield over and in the column which not only fluctuated greatly,but responded rapidly.The concentration of propylene over and in the column responded slowly and the fluctuating period exceeded 3 hours.These dynamic properties required steady and gradual operation and adjustment.The adjusting rules for instruments impacted the dynamics properties greatly.

中文摘要	3-4
ABSTRACT	4
前言	7-8
第一章化工过程模拟技术的发展与应用	8-15
1.1 国内外化工过程模拟技术的发展	8-12
1.1.1 稳态模拟技术	8-10
1.1.2 动态模拟技术	10-12
1.2 模拟软件在精馏过程中的应用	12-15
第二章丙烯精馏塔改造情况	15-17
2.1 丙烯精馏塔改造经过	15
2.2 DJ-3 和DJ-5 型塔板介绍	15-17
第三章 406 单塔稳态模拟	17-24
3.1 406 单塔操作流程	17
3.2 计算模型的选取	17
3.3 406 单塔设计核算	17-19
3.4 406 单塔实际操作模拟	19-21
3.5 406 单塔理论板数核定	21-24
第四章双塔稳态模拟	24-45
4.1 双塔操作流程	24
4.2 双塔设计核算	24-28
4.3 双塔操作优化	28-43
4.3.1 模拟步骤的确立	29
4.3.2 模拟输入初值的确定	29-30
4.3.3 不同进料量下的操作优化	30-35
4.3.4 不同进料组成下的操作优化	35-39
4.3.5 不同工况下的操作优化	39-43
4.4 双塔位置对换对操作的影响	43-45
第五章双塔操作动态模拟	45-59
5.1 双塔动态模拟流程的建立	45-48
5.2 动态模拟初始化	48-51
5.3 进料量扰动下的动态模拟	51-52
5.4 进料组成扰动下的动态模拟	52-54
5.5 回流量扰动下的动态模拟	54-57
5.6 仪表调节规律对动态特性的影响	57-59
第六章结论	59-61
参考文献	61-64
发表论文和科研情况说明	64-65
致谢	65

yilai1002 2010/12/11

丙烯精馏塔过程模拟