邻甲酚塔的参数优化和控制分析

精馏塔是石油化工和医药领域常见的生产过程设备,本文利用Aspen Pus软件分别采用简捷法和严格法对提酚装置中邻甲酚塔进行了设计计算。针对本项目研究的邻甲酚精馏塔,首先通过简捷法估算出精馏塔的回流比、塔板数以及进料位置。然后采用严格法的灵敏度分析得出回流比为6、塔板数为80块、进料位置为30。增加精馏塔回流比5%,分析回流比变化对塔板温度的影响,发现精馏段灵敏板的位置为26块,提馏段灵敏板的位置为43块。分别采用了精馏段温度控制方案和提馏段温度控制方案研究在进料流量、进料组成以及进料温度波动时,精馏塔的动态响应过程。研究表明:提馏段温度控制方案较精馏段温度控制方案具有明显的动态响应快,抗干扰能力强,建立平衡时间短等优点。     

离子液体催化反应精馏合成乙酸乙酯工艺模拟

为研究离子液体在反应精馏中的作用,采用离子液体1-丁基-3-甲基咪唑硫酸氢盐（[BMIM]HSO₄）作为催化剂,对乙酸和乙醇合成乙酸乙酯的反应精馏流程进行了计算模拟。在确定了参数的酯化反应动力学的基础上,用Aspen Plus软件建立了反应精馏流程,研究了催化剂用量、精馏段理论板数、反应段理论板数、乙醇进料位置、进料摩尔比、持液量及回流比等参数对反应精馏过程的影响。研究结果表明,塔顶乙酸乙酯的质量分数随催化剂用量、精馏段理论板数、反应段理论板数和持液量增大而增大,工艺流程存在最佳回流比以及最佳进料酸醇摩尔比。得到的优化条件如下：离子液体与乙酸摩尔比为1：2.5,进料酸醇摩尔比为4：1,理论塔板数为21块,乙酸和催化剂在第7块理论塔板进料,乙醇在第19块理论塔板进料,塔板持液量0.1L,回流比为4,塔顶乙酸乙酯的质量分数可以达到98.73%。     

催化精馏脱除乙醇-水共沸混合物中水的模拟研究

采用异丁烯(IB)水合生成叔丁醇(TBA)的方法和催化精馏工艺脱除乙醇中的水.选用Equilibrium模型描述催化精馏塔中反应段的反应过程.应用Aspen Plus系统的讨论了操作压力、塔顶采出率(D/F)、回流比、异丁烯/水摩尔进料比、进料位置、反应段位置、理论板数对脱水效果的影响.结果表明,在较少能量消耗下,异丁烯很容易水合生成叔丁醇,但是叔丁醇选择性较低,生成乙基叔丁基醚(ETBE)的反应占主导.当采用叔丁醇选择性高的催化剂,通过催化精馏,能够在较低的能耗和较少的IB消耗下实现乙醇的脱水.     

背包式酶催化反应精馏制备丁酸丁酯模拟优化

提出了背包式酶催化反应精馏合成丁酸丁酯的新工艺,将酶催化反应转移到塔外,优化了丁酸丁酯的生产过程。首先,进行丁酸乙酯与正丁醇的酯交换反应动力学实验,建立反应动力学模型,并验证该工艺流程中此模型计算结果的可靠性。然后,运用Aspen Plus对背包式反应精馏新工艺进行了流程模拟和优化设计,分别确定提馏段、精馏段的塔板数,回流比等主要参数。优化后的模拟操作条件为：精馏段塔板数5、提馏段塔板数7、回流比5、侧线循环总量6 kmol/h、侧反应器4个,此时正丁醇的反应转化率能达到99.85%,产品纯度为94.71%,有效减少了设备投资,为背包反应精馏的更优利用提供了理论依据和可行方案。     

CFC-113反应精馏合成CFC-113a的过程模拟与优化

将反应精馏技术应用于CFC-113转产CFC-113a的工艺,利用Aspen Plus软件对反应精馏制备CFC-113a的稳态工艺过程进行了研究。分别从操作压力、精馏段塔板数、反应段塔板数、提馏段塔板数和回流比等方面对该反应精馏系统进行了优化,该优化结果的获取旨在推动新工艺的工业化。     

乙酸甲酯的催化精馏水解实验研究

在自行设计的催化精馏塔中,以Amberlyst 35wet阳离子交换树脂为催化剂,全回流操作下,对乙酸甲酯催化精馏水解进行了研究。考察了空速、塔高度、回流进料比(体积比)以及进料中水酯物质的量比等操作条件对水解反应的影响。实验结果表明,在空速0.09 min-1,催化剂装填高度80 cm,提馏段7块塔板,回流进料比5∶1,进料中水酯物质的量比6.5∶1时,乙酸甲酯水解率达到83.5%。     

含盐乙腈废水的分离模拟与优化

利用Aspen Plus模拟软件对含盐乙腈废水采用双塔精馏流程进行分离模拟和优化。进料为100 kg/h,选择ENRTL-RK方程,模拟结果为:对于1#塔,理论塔板数为15块,进料位置为第7块,回流比2,操作压力0.140×10~5~0.148×10~5 Pa;对于2#塔,理论塔板数8块,进料位置为第5块,回流比2,操作压力0.135×10~5~0.145×10~5 Pa。利用灵敏度分析分析了回流比、进料位置、采出量对塔进行了优化,对于1#塔,进料位置第7块,回流比1.5,采出量25 kg/h;对于2#塔,进料位置第4块,回流比1.5,采出量10 kg/h。     

叔丁醇催化精馏脱水制高纯度异丁烯中试研究

采用大颗粒阳离子树脂催化剂,在Φ100 mm×4 100 mm的催化精馏中试装置上对叔丁醇脱水制异丁烯进行研究,考察操作压力、回流比、叔丁醇进料量和催化剂填装量对叔丁醇转化率的影响。结果表明,在操作压力0.39 MPa、回流比1.5、叔丁醇进料量4.32 L/h、催化剂填装量6 kg的条件下,叔丁醇转化率达98.12%,经分离后可以得到纯度为99.83%的异丁烯。     

氯乙烯精馏过程的模拟与优化

利用Aspen Plus模拟软件对某厂电石法生产的氯乙烯精馏过程进行了建模与模拟,进料规模为20 m~3/h。选择NRTL物性方法,对低沸塔和高沸塔进行了模拟,模拟结果如下:低沸塔的塔板数为29块,进料位置第3块,回流比为5,操作压力为0.52~0.53 MPa,高沸塔的塔板数为41块,进料位置12块,回流比为0.6,操作压力0.26~0.28 MPa;利用灵敏度分析工具研究了进料位置、采出率、回流比三个因素对精馏过程的影响,对氯乙烯精馏过程进行了优化,结果表明:对于低沸塔,进料位置为3,塔板数为29,B/F为0.99,回流比为6;对于高沸塔,进料位置为12,塔板数为41,D/F为0.99,回流比为0.2。     

反应精馏制备乙酸乙酯的工艺分析

为揭示反应精馏法制备乙酸乙酯的特性及得到较高纯度的产品,并为反应精馏工艺过程的深入研究及工业化提供理论依据,应用Aspen Plus软件模拟分析反应精馏过程。结果表明：给定回流比的情况下,理论塔板数、精馏段塔板数及进料位置、进料比、催化剂用量等参数均对产品纯度及分离效果产生影响。     

反应精馏生产甲缩醛工艺的研究

对合成甲缩醛反应精馏过程进行了模拟和实验,分析了过程操作参数回流比、进料位置、醇醛进料摩尔比的变化结果的影响,模拟结果表明,当精馏段级数为11,反应段级数为26,提馏段为5,回流比为3,甲醇和甲醛的进料位置分别为第37级和第12级,甲醇/甲醛(摩尔比)=2.1时,塔顶可得到质量分数大于99.5%的高纯度甲缩醛。并通过反应精馏实验对模拟结果进行验证,实验结果与模拟结果吻合较好。     

反应精馏合成醋酸正丁酯的模拟和优化

利用Aspen Plus模拟了合成醋酸正丁酯的反应精馏过程,并分析各工艺参数对产品纯度和再沸器热负荷影响。通过优化得出最佳工艺参数为:理论塔板数为16;精馏段、反应段和提馏段塔板数分别为5、7和4;醋酸和正丁醇的进料塔板数分别为5和7;酸醇进料比为1:1;回流比为1。在此条件下产品醋酸正丁酯的纯度达99.55%;乙酸的转化率达99.71%,再沸器的能耗较低。     

乙酸甲酯与甲醇共沸物催化精馏水解工艺

以乙酸甲酯与甲醇共沸物为原料,采用阳离子交换树脂为催化剂,研究了乙酸甲酯催化精馏水解工艺。在实验中以捆扎包作为催化剂的装填方式,系统地研究了催化精馏段和提馏段的高度、进料位置、进料中含甲醇、水酯物质的量比、回流进料比和空速等对酯分解率的影响,获得了最佳的工艺条件。分析了传统的水解分离工艺,提出了可行的新工艺。在最佳工艺条件下,新工艺系统的能耗比传统的固定床工艺降低39.99%。     

Simulation studies on reactive distillation for synthesis oftert-amyl ethyl ether

In this work, a reactive distillation column in which chemical reactions and separations occur simultaneously is applied for the synthesis of tert-amyl ethyl ether (TAEE) from ethanol (EtOH) and tert-amyl alcohol (TAA). A rate-based kinetic model for liquid-phase etherification and an equilibrium stage model for separation are employed to study the reactive distillation. The calculation is carried out using the commercial software package, Aspen Plus. Simulations are performed to examine the effects of design variables, i.e., a number of rectifying, reaction and stripping stages on the performance of reactive distillation column. It has been found that an optimal column configuration for the TAEE production under the study is designed with no rectifying, 4 reaction and 8 stripping stages. With such an appropriate specification of the reactive distillation column, the effects of various operating variables on the TAA conversion and TAEE selectivity are further investigated and the results have shown that the reflux ratio and operating pressure are the most important factors to the operation of the reactive distillation.     

Study on the Synthesis of n‐Butyl Acetate by Catalytic Rectification

With Hβ zeolite as the catalyst and θ rings as the fillings, the technological process of synthesizing n‐butyl acetate with acetic acid and n‐butanol in a Φ 30 mm and 2 m tall catalytic rectifying column was studied. The influence of factors such as catalyst loading height, material feed site, reflux ratio and feed rate on the esterification reaction and the rectification effect was investigated. The study results suggested that the appropriate conditions of n‐butyl acetate synthesis by catalytic rectification include: The height ratio of the rectifying section, the reaction section and the stripping section is 1:1:1; acetic acid and n‐butanol are fed in upside and downside of the reaction section, respectively; the reflux ratio is 2.5; the liquid hourly space velocity of n‐butanol is 0.64 h^–1. Under these conditions, the mass fraction of n‐butyl acetate in the column bottom is 98.64 %, and the total yield of n‐butyl acetate is 91.5 %.     

Mutual separation of two monovalent metal ions by multistage electrodialysis

A multistage electrodialyzer having an enriching section and a stripping one has been developed to separate monovalent cation species in the aqueous solution. A feed solution containing LiCl and KCl is supplied to the middle stage of the dialyzer, and a solution of HCl is supplied to the cathode stage. Stages from cathode to feed are the enriching section and those from feed to anode are stripping section. Aqueous solution flows from the cathode stage toward the anode stage as a reflux flow. The ratio K⁺/Li⁺ in the enriching product increased with the increase in reflux flow rate and decreased with the increase in current density, while the ratio Li⁺/K⁺ in the stripping product increased with the current density and decreased with the reflux flow rate. Simulation by a stage to stage calculation was carried out by use of the operating equation based on mass balance and the relation of permselectivities alternatively. The calculated results were in good agreement with the experimental ones, and indicated that a large yield of product as well as a large concentration ratio can be achieved by increasing stage number.     

催化精馏塔内甲酸甲酯水解制甲酸的研究

在催化精馏塔内以压制的强酸性阳离子交换树脂为催化剂填料对甲酸甲酯水解制甲酸进行了实验研究.在全回流操作条件下,通过改变操作参数获得了高于90%的水解转化率.考虑到反应过程中水的阻碍作用,根据实验结果提出了可用于催化精馏过程的动力学方程并建立了基于平衡级理论的反应与分离耦合的数学模型.通过设定进料水酯摩尔比、回流与进料比、反应段与分离段理论级数等参数获得了水解过程的仿真结果,并提出了较佳的工艺操作条件.研究表明:仿真结果与实测数据相吻合;通过改变操作条件可调整反应段内水与甲酸甲酯的浓度,提高水解速度;增加反应段的高度比增加分离段的高度更有利;产品甲醇和甲酸在催化精馏塔内能够完全分离,反应段两端反应速度高于中间段的反应速度.     

Reactive distillation for synthesis of glycerol carbonate via glycerolysis of urea

This study developed a new process for synthesis of glycerol carbonate via glycerolysis of urea by reactive distillation. Missing thermodynamic parameters were estimated by various group contribution methods. The results of Gibbs free energy showed that Gani's method provided the lowest deviation. Equilibrium and kinetic model parameters of the glycerolysis obtained from batch experiments were employed for the simulation of the reactive distillation using Aspen Plus^® software. High conversion of glycerol was achieved by reducing reactant loss in distillate through an increase in the number of stripping and reaction stages and a decrease in the number of rectifying stages. Moreover, glycerol and urea in distillate were recycled to the reactive section by increasing reflux ratio to a reasonable value. The suitable design and operating parameters were achieved at 3 stripping stages, 3 reactive stages, no rectifying stage, reboiler heat duty of 15 kW and reflux ratio of 2. This offered 93.6% conversion of glycerol, and 90.0% yield of glycerol carbonate with 100% purity in the final product. Compared with conventional in vacuo process, reactive distillation promoted glycerol conversion by 29.1% and saved in energy consumption by 37.1%.     

丙酮缩合制备异丙叉丙酮的催化精馏模拟

利用Aspen Plus研究了丙酮脱水缩合生成异丙叉丙酮的反应精馏工艺流程,首先对丙酮脱水缩合生成二丙酮醇和异丙叉丙酮的动力学进行实验研究,考察了反应温度对丙酮反应速率的影响,根据经验反应动力学模型,通过Matlab回归得到了动力学参数。将得到的动力学方程用Fortran语言编写并嵌入到Aspen Plus。分析了反应段理论板数、进料板位置、精馏段理论板数、提馏段理论板数等因素对丙酮转化率和异丙叉丙酮选择性的影响。优化后的催化反应精馏塔工艺,丙酮转化率达到99%,异丙叉丙酮选择性达到93%。