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《化学工程》2021,(8)
针对丙烯酸与异丁烯酯化加成反应具有反应温度较低、精馏温度较高的特点,文中设计了加压较低温度反应-减压较高温度精馏集成的"背包式"反应精馏生产丙烯酸叔丁酯新工艺。以年度总成本(TAC)为目标,采用序贯优化法对过程工艺参数进行优化设计。规定新鲜丙烯酸进料量为10 kmol/h,塔顶产品中丙烯酸叔丁酯质量分数不低于98%,新鲜丙烯酸转化率达到99%,得到最佳过程配置参数和操作参数:侧反应器台数为2,进入侧反应器1(R1)的侧线采出量为10 kmol/h,进入侧反应器2(R2)的侧线采出量为5 kmol/h,以及催化剂总装填量为200 kg且分配比为0.7/0.3,总塔板数为28块(包括冷凝器和再沸器),精馏段塔板数为15块,侧反应器进出口间隔塔板数为5,回流比为0.64,此时TAC最小为1.439×10~6元/a。 相似文献
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乙酸乙酯和正己烷均为重要的有机溶剂,广泛应用于医药、橡胶、油漆等领域。由于乙酸乙酯和正己烷常压下形成共沸物,需采用特殊工艺对其进行分离。基于乙酸乙酯-正己烷二元共沸体系的压力敏感性,利用Aspen Plus软件,以年度总费用(TAC)最小为目标函数,模拟和优化了变压精馏稳态工艺,其中高压塔和低压塔的操作压力分别采用6 atm和1 atm,所得乙酸乙酯和正己烷产品纯度均大于99.9%。在此基础上,利用Aspen Dynamics软件考察了变压精馏工艺不同控制方案的有效性。结果表明:Q_R/F比例控制结构能够有效地应对进料流量扰动,且响应速度快,但在处理进料组分干扰时稍显不足。组分-温度串级控制能有效的改善进料组分扰动对产品纯度的影响。Q_R/F比例控制结构与组分-温度串级控制结构联用在变压精馏工艺中可实现稳健的控制,能够有效保证乙酸乙酯和正己烷产品纯度。 相似文献
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目前反应精馏法生产醋酸丁酯工艺发展迅速,但主要集中于对催化剂的探索与研究,在实际生产中仍缺乏较好的控制方法。利用Aspen Dynamics软件对醋酸丁酯反应精馏塔的操作进行了动态模拟,提出了两点温度控制法及温度浓度控制法两种控制方案,对系统进行了进料流量±10%,乙醇及醋酸进料浓度-5%,-10%的扰动测试。研究了不同扰动对产品组成的影响并比较了两种方案分别在面对不同扰动时的控制效果。实验结果表明:进料流量及醋酸进料组成对产品组成影响较大;两点温度控制法在面对不同扰动时均展现出了比温度组成控制法更好的控制效果,该控制方法具有响应速度快,产品组成偏差小的优点。 相似文献
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以磺酸阳离子树脂为催化剂,以对仲丁基苯酚和异丁烯为原料合成了2,6-二叔丁基对仲丁基苯酚。探讨了不同催化剂、反应温度、反应时间、物料配比和催化剂用量对反应的影响。最优的反应条件:催化剂的质量分数为3%~5%(以对仲丁基苯酚质量计,下同),n(对仲丁基苯酚)∶n(异丁烯)=1∶2,反应温度90~100℃,反应压力0.15~0.2 MPa,反应时间4 h,在该条件下,产物选择性达95%以上,精馏分离得到色谱纯度大于97.5%的2,6-二叔丁基对仲丁基苯酚,总收率达95%以上。 相似文献
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基于甲醇和苯共沸体系的压敏性,利用Aspen Plus和Aspen Dynamics软件对变压精馏分离该体系的稳态工艺进行了模拟和优化,研究了该工艺的动态特性,提出了控制产品纯度的3种控制结构:基础控制结构、比例控制结构和双比例与温度?组分联合控制结构,通过对控制结构添加±20%的组分和流量干扰测试控制结构的稳定性. 结果表明,基础控制结构基本能实现稳健控制,但不能解决组分干扰引起的产品纯度偏差过大等问题;比例控制结构可实现相对稳健的控制,但改进效果不显著;双比例与温度?组分联合控制结构在受到20%进料和组分干扰后,产品纯度能较快恢复至设定值的99.90%,实现稳健控制. 相似文献
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Qingrui Zhang Sen Yan Haiying Li Pengfei Xu 《Chemical Engineering Communications》2019,206(5):559-571
A conventional reactive distillation column will not be able to produce high purity isopropyl acetate (IPAc) due to the existence of a minimum boiling azeotrope in the system. In this work, a novel reactive and extractive distillation (RED) process was proposed and used for the synthesis of IPAc. Results showed that the purity of IPAc reached 99.5%. Then, the RED flowsheet was optimized with minimum total annual cost (TAC), and a number of key variables were determined with the assistance of program written in Visual Basic 6.0 (VB). After that, two control structures of the RED process were developed: a basic control structure with temperature/proportional cascade control and an improved control structure with composition/temperature cascade control. The integral of squared error (ISE) was introduced to evaluate the performance of control systems, it revealed that the improved control structure had better controllability. 相似文献
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The performance of an ETBE reactive distillation column was evaluated by using dynamic simulations under open-loop operation and one-point control schemes for controlling the ETBE purity. In multiloop process control, the choice of the control scheme can have a profound effect on the disturbance rejection properties so that some standard control schemes, namely, LV, DV, LB and (L/D)V, were investigated. It is shown that open-loop operation is not acceptable because no correction can be made so that the process objectives could not be satisfied. The disturbance rejection properties could be increased with a one-point control scheme. The LV scheme has the 'best' disturbance rejection properties among the control schemes studied for feed disturbances. 相似文献
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The performance of an ETBE reactive distillation column was evaluated by using dynamic simulations under open-loop operation and one-point control schemes for controlling the ETBE purity. In multiloop process control, the choice of the control scheme can have a profound effect on the disturbance rejection properties so that some standard control schemes, namely, LV, DV, LB and (L/D)V, were investigated. It is shown that open-loop operation is not acceptable because no correction can be made so that the process objectives could not be satisfied. The disturbance rejection properties could be increased with a one-point control scheme. The LV scheme has the 'best' disturbance rejection properties among the control schemes studied for feed disturbances. 相似文献
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Dimethyl carbonate is an environmentally benign and biodegradable chemical. Based on integration of reactive distillation and pressure-swing distillation technologies, a novel process for synthesis of dimethyl carbonate through transesterification with propylene carbonate and methanol has been developed by Huang et al. In this work, the optimization of this process was performed by minimizing the total TAC. The results show that the op-timal design flowsheet can save energy consumption by 18.6%with the propylene carbonate conversion of 99.9%. Then, an effective plant-wide control structure for the process was developed. Dynamic simulation results dem-onstrate that the temperature/flow rate cascade control plus with simple temperature control can keep not only product purity but also the conversion of the reactant at their desired values in the face of the disturbance in re-actant feed flow rate and feed composition. 相似文献
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基于非平衡级和拟均相假设,建立了乳酸提纯反应精馏新工艺实验装置的动态机理模型.通过改进的数值计算方法提高了模型的求解效率,设计并实现了包含物性估算系统的模型仿真平台,以促进新工艺的工业化应用.利用仿真平台对新工艺装置进行了动态特性分析,在此基础上设计了两种单端质量控制方案:直接物料平衡和间接物料平衡方案.在不同类型和幅度的过程扰动下,分析比较了两种控制方案的调节性能.结果表明直接物料平衡方案控制品质优于间接物料平衡方案,可在不同扰动情况下满足过程的产品质量和转化率的联合控制要求.非平衡级动态机理模型能够反映反应精馏过程的动态特性,分析发现反应精馏过程有着独特的过程特性,基于机理模型的仿真平台是分析反应精馏特性的有效工具. 相似文献
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反应精馏技术是将反应和精馏两个单元操作耦合在一个设备中同时进行,其非线性给反应精馏过程的平稳操作和过程控制提出了更高的要求。目前,反应精馏过程控制研究都是针对特定反应体系进行的有针对性的研究,对于乙酸戊酯反应体系的控制研究少有报道。本文利用Aspen Plus和Aspen Dynamic 软件对乙酸戊酯的反应精馏过程进行动态模拟,针对塔釜产品组成要求提出温度控制和组成控制两种不同的控制方案,对两个控制系统分别进行±10%的进料流量扰动测试和酸醇比为1:1、1.2:1的进料组成扰动测试。研究了不同扰动对产品质量的影响并比较了两种方案在不同扰动干扰下的控制效果。结果表明:进料组成扰动会对两个控制方案造成较大影响;温度控制方案的控制稳定性要好于组成控制方案。 相似文献
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Kai-Luen Zeng 《Chemical engineering science》2006,61(13):4417-4431
In this study, the design and control of a reactive distillation column system for the production of butyl acrylate has been investigated. The proposed design is quite simple including only one reactive distillation column and an overhead decanter. The optimal design is selected based on the minimization of total annual cost (TAC) for the overall system. At this optimized flowsheet condition, output multiplicity was found with reboiler duty or feed ratio as the bifurcation parameter. The highest purity stable steady state was selected as the base case condition for the control study. The overall control of this system can be achieved with no on-line composition measurements. Simple single-point tray temperature control loop is designed to infer final product purity. From results of dynamic simulation, the proposed control strategy performs very well in rejecting various disturbances while maintaining butyl acrylate product at high purity. One of the important finding in this paper is that it is better to operate this reactive distillation column not at the exact feed stoichiometric balance point for better operability reason. The control performances of the proposed operating point and the operating condition right at the exact stoichiometric balance point will be compared. 相似文献
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基于变压精馏分离乙酸乙酯/正己烷共沸体系两塔的温差,利用Aspen Plus软件,以年度总成本最小为目标函数,对部分及完全热集成变压精馏工艺进行了稳态模拟及优化。在此基础上,利用Aspen Dynamics软件开发了多种控制结构,通过引入不同进料流量及组成的扰动测试控制结构的有效性。结果表明,完全热集成变压精馏工艺比部分热集成变压精馏工艺的经济性稍好。动态响应结果表明,部分热集成变压精馏工艺的压力?补偿温度控制结构可有效处理不同程度的干扰,能有效提高控制结构对干扰的响应速度,缩短达到新稳态的时间,保证乙酸乙酯和正己烷产品纯度在99.9wt%之上;而完全热集成变压精馏工艺的组分?温度串级控制结构仅能处理较小的组分和流量干扰,实现稳健控制,无法处理较大的干扰。综合比较两种工艺的经济性和可控性,认为部分热集成变压精馏工艺分离乙酸乙酯/正己烷共沸体系优于完全热集成变压精馏工艺。 相似文献
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M.V. Pavan Kumar 《Chemical engineering science》2008,63(1):228-243
Two-point and three-point temperature control structures are proposed for a kinetically controlled ideal reactive distillation (RD) column. The control structures maintain stable column operation for large throughput changes. However, large deviations in the final product purities are seen with three-point control giving comparatively lower deviations. The large product purity deviations are due to the kinetic regime so that two temperature set-points are adjusted in a cascade arrangement to maintain the distillate and bottoms purity. The proposed two-point and three-point structures with cascade compensation of the temperature set-points effectively maintain the distillate and bottoms purity for a large throughput decrease. However, the two-point structures fail for a large throughput increase. This is because in the kinetically controlled regime, maintaining the distillate purity requires an increase in the effective reflux ratio to internally recycle the escaping reactants back into the reactive zone. The two-point structures that use the fixed reflux ratio policy thus fail as an infeasible steady state is sought. The three-point structures effectively maintain the product purities as the reflux ratio is indirectly adjusted through the manipulation of the reflux rate. The work highlights the need for understanding the interaction between the reaction and separation sections for effective RD control system design. 相似文献