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1
Ceylan, Hatice. "Control And Simulation Studies For A Multicomponent Batch Packed Distillation Column." Master's thesis, METU, 2007. http://etd.lib.metu.edu.tr/upload/12608688/index.pdf.
Full textAbstract:
During the last decades, batch distillation is preferably used with an increasing demand over continuous one, to separate fine chemicals in chemical and petroleum industries, due to its advantages like, flexibility and high product purity. Consequently, packed distillation columns, with newly generated packing materials, are advantageous compared to plate columns because of their smaller holdups, resistivity to corrosive materials and their higher separation efficiencies. Also, in many industrial applications, mathematical models of distillation systems are frequently used in order to design effective control systems, to train operating personnel and to handle fault diagnostics. Thus, the main objective of this study is to develop a mathematical model for a multicomponent batch distillation column, which is used to separate mixtures at low operating pressures, packed with random packing materials. In multicomponent batch packed distillation, operation with optimum reflux ratio profile is important for efficiency to maximize the amount of the distillate with a specified concentration, for a given time. Therefore, it is also aimed to find the optimum reflux ratio profile for the multicomponent batch packed distillation column.
A simulation algorithm is written with the aid of MATLAB and FORTRAN programming languages by taking into account pressure drop and variation of physical properties. The selected incremental bed height, Δ
z, to be used in the simulation program has an effect on the accuracy of the results. This is analyzed and the optimal incremental height is found to be 3.5 cm for a 1.5m bed height. The change in distillate compositions with a given constant reflux ratio is found to be similar with those of previous studies. The simulation code is also used to obtain responses in distillate compositions for different reflux ratios, condenser holdups and reboiler duties and compared with similar studies found from literature and found to be adequate. Finally, experiments are conducted to verify simulation algorithm by using a lab-scale packed distillation column for the separation of a polar mixture of ethanol and water. It is observed that, there is a good agreement between the experimental and simulation results. After the verification of dynamic model, optimum operation policy to maximize product amount is investigated numerically by using capacity factor approach. The column is operated with and without recycling of the holdups of the slop cut tanks, in order to examine the effect of recycling on capacity factor, CAP. It is observed that, recycling of the molar holdups of the slop cut tanks is resulted in a 28% increase in the separation efficiency.
2
Yildiz, Ugur. "Multicomponent Batch Distillation Column Simulation And State Observer Design." Master's thesis, METU, 2002. http://etd.lib.metu.edu.tr/upload/12605551/index.pdf.
Full textAbstract:
In the control of batch and continuous distillation columns, one of the most
challenging problem is the difficulty in measuring compositions. This problem
can be handled by estimating the compositions from readily available online
temperature measurements using a state observer. The aim of this
study is to design a state observer that estimates the product composition
in a multicomponent batch distillation column (MBDC) from the temperature
measurements and to test this observer using a batch column simulation. To
achieve this, first a model for MBDC is prepared and compared with the data
from literature where a case column is utilized. After checking the validity of
the simulation package, it is used as a fictitious process for the performance
evaluations.
In the second phase of the study, an extended Kalman Filter (EKF) is designed
by utilizing a simplified model of MBDC and it is implemented for performance
investigation on the case column with 8 trays separating the mixture of cyclohexane,
n-heptane and toluene. The simplified model utilized in EKF results
in response, which have some deviation with rigorous model, mainly due to
the simplification of vapor-liquid equilibrium relationship. In the performance
evaluation, the tuning parameters of EKFthe diagonal terms of process noise covariance matrix and the diagonal terms of measurement model noise covariance matrix are changed in the range of 50¡
1x10¡
7 and 0:5¡
5x108 and the optimum values are found as 0:00001 and 5000, respectively. The effect of number of measurement points is also investigated with a result of number of component measurements. The effect of measurement period value is also studied and found that it has a major effect on the performance which has to be determined by the available computational facilities. The control of the column is done by utilizing the designed EKF estimator and the estimator is successfully used in controlling the product purities in MBDC under variable reflux-ratio operation.
3
Afvander, Åsa. "Development of a working method for the study of a distillation process : Distillation of a multicomponent system." Thesis, Umeå universitet, Kemiska institutionen, 2015. http://urn.kb.se/resolve?urn=urn:nbn:se:umu:diva-109140.
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4
Edreder, E. A. "Modelling and optimisation of batch distillation involving esterification and hydrolysis reaction systems. Modelling and optimisation of conventional and unconventional batch distillation process: Application to esterification of methanol and ethanol using acetic acid and hydrolysis of methyl lactate system." Thesis, University of Bradford, 2010. http://hdl.handle.net/10454/4296.
Full textAbstract:
Batch distillation with chemical reaction when takes place in the same unit is referred to
as batch reactive distillation process. The combination reduces the capital and operating
costs considerably. Among many different types of batch reactive distillation column
configurations, (a) conventional (b) inverted (c) semi-batch columns are considered
here.
Three reaction schemes such as (a) esterification of methanol (b) esterification of
ethanol (c) hydrolysis of methyl lactate are studied here. Four different types of
dynamic optimisation problems such as (a) maximum conversion (b) maximum
productivity (c) maximum profit and (d) minimum time are formulated in this work.
Optimal design and or operation policies are obtained for all the reaction schemes.
A detailed rigorous dynamic model consisting of mass, energy balances, chemical
reaction and thermodynamic properties is considered for the process. The model was
incorporated within the dynamic optimisation problems. Control Vector
Parameterisation (CVP) technique was used to convert the dynamic optimisation
problem into a nonlinear programming problem which was solved using efficient SQP
(Successive Quadratic Programming) method available within the gPROMS (general
PROcess Modelling System) software.
It is observed that multi-reflux ratio or linear reflux operation always led to better
performance in terms of conversion, productivity for all reaction schemes compared to
that obtained using single reflux operation.
Feed dilution (in the case of ethanol esterification) led to more profit even though
productivity was found to be lower. This was due to reduction in feed price because of
feed dilution. Semi-batch reactive distillation opertation (for ethanol esterification) led
to better conversion compared to conventional batch distillation, however, the total
amount of acetic acid (reactant) was greater in semi-batch operation. Optimisation of
design and operation (for ethanol esterification) clearly showed that a single cloumn
will not lead to profitable operation for all possible product demand profile. Also
change in feed and /or product price may lead to adjust the production target to
maximise the profitability.
In batch distillation, total reflux operation is recommended or observed at the begining
of the operation (as is the case for methnaol or ethanol esterification). However, in the
case of hydrolysis, total reflux operation was obseved at the end of the operation. This
was due to lactic acid (being the heaviest) was withrawn as the final bottom product.Libyan Petroleum Institute
5
Edreder, Elmahboub A. "Modelling and optimisation of batch distillation involving esterification and hydrolysis reaction systems : modelling and optimisation of conventional and unconventional batch distillation process : application to esterification of methanol and ethanol using acetic acid and hydrolysis of methyl lactate system." Thesis, University of Bradford, 2010. http://hdl.handle.net/10454/4296.
Full textAbstract:
Batch distillation with chemical reaction when takes place in the same unit is referred to as batch reactive distillation process. The combination reduces the capital and operating costs considerably. Among many different types of batch reactive distillation column configurations, (a) conventional (b) inverted (c) semi-batch columns are considered here. Three reaction schemes such as (a) esterification of methanol (b) esterification of ethanol (c) hydrolysis of methyl lactate are studied here. Four different types of dynamic optimisation problems such as (a) maximum conversion (b) maximum productivity (c) maximum profit and (d) minimum time are formulated in this work. Optimal design and or operation policies are obtained for all the reaction schemes. A detailed rigorous dynamic model consisting of mass, energy balances, chemical reaction and thermodynamic properties is considered for the process. The model was incorporated within the dynamic optimisation problems. Control Vector Parameterisation (CVP) technique was used to convert the dynamic optimisation problem into a nonlinear programming problem which was solved using efficient SQP (Successive Quadratic Programming) method available within the gPROMS (general PROcess Modelling System) software. It is observed that multi-reflux ratio or linear reflux operation always led to better performance in terms of conversion, productivity for all reaction schemes compared to that obtained using single reflux operation. Feed dilution (in the case of ethanol esterification) led to more profit even though productivity was found to be lower. This was due to reduction in feed price because of feed dilution. Semi-batch reactive distillation opertation (for ethanol esterification) led to better conversion compared to conventional batch distillation, however, the total amount of acetic acid (reactant) was greater in semi-batch operation. Optimisation of design and operation (for ethanol esterification) clearly showed that a single cloumn will not lead to profitable operation for all possible product demand profile. Also change in feed and /or product price may lead to adjust the production target to maximise the profitability. In batch distillation, total reflux operation is recommended or observed at the begining of the operation (as is the case for methnaol or ethanol esterification). However, in the case of hydrolysis, total reflux operation was obseved at the end of the operation. This was due to lactic acid (being the heaviest) was withrawn as the final bottom product.
6
BHANDARI, SHASHANK. "Design of a solvent recovery system in a pharmaceutical manufacturing plant." Thesis, KTH, Skolan för kemivetenskap (CHE), 2016. http://urn.kb.se/resolve?urn=urn:nbn:se:kth:diva-190901.
Full textAbstract:
Solvents play a crucial role in the Active Pharmaceutical Ingredient (API) manufacturing and are used in large quantities. Most of the industries incinerate the waste solvents or send it to waste management companies for destruction to avoid waste handling and cross-contamination. It is not a cost effective method and also hazardous to the environment. This study has been performed at AstraZeneca’s API manufacturing plant at Sodertalje, Sweden. In order to find a solution, a solvent recovery system is modeled and simulated using ASPEN plus and ASPEN batch modeler. The waste streams were selected based on the quantity and cost of the solvents present in them. The solvent mixture in the first waste stream was toluene-methanol in which toluene was the key-solvent whereas in the second waste stream, isooctane-ethyl acetate was the solvent mixture in which isooctane was the key-solvent. The solvents in the waste stream were making an azeotrope and hence it was difficult to separate them using conventional distillation techniques. Liquid-Liquid Extraction with water as a solvent followed by batch distillation was used for the first waste stream and Pressure Swing Distillation was used for the second waste stream. The design was optimized based on cost analysis and was successful to deliver 96.1% toluene recovery with 99.5% purity and 83.6% isooctane recovery with 99% purity. The purity of the solvents was decided based on the quality conventions used at AstraZeneca so that it can be recovered and recycled in the same system. The results were favorable with a benefit of €335,000 per year and preventing nearly one ton per year carbon dioxide emissions to the environment. A theoretical study for the recovery system of toluene-methanol mixture was performed. The proposed design was an integration of pervaporation to the batch distillation. A blend of polyurethane / poly(dimethylsiloxane) (PU / PDMS) membrane was selected for the separation of methanol and toluene mixture. The results of preliminary calculations show 91.4% toluene recovery and 72% methanol recovery with desired purity.
7
Bernot, Christine. "Design and synthesis of multicomponent batch distillation." 1990. https://scholarworks.umass.edu/dissertations/AAI9110105.
Full textAbstract:
Interest in batch processes has increased with the growing importance of specialty chemicals, characterized by high-value, low-capacity, short-term production and strongly nonideal mixtures. While separation is an important step in these processes, few publications deal with the feasibility and design aspects of batch distillation for azeotropic mixtures. In this dissertation, a simple dynamic model is developed to describe composition changes in batch distillation by decoupling the variations in flows and compositions through a dimensionless warped time. The model is based on constant molar overflow and quasi-steady state assumptions in the column and on a differential model for the batch tank. Two types of batch distillation columns are presented: the batch rectifier, where products are withdrawn at the distillate, and the batch stripper, where products are withdrawn at the bottom. Composition changes for azeotropic mixtures are complex because the sequence of cuts collected depends on the relative amount of each component in the feed. However, in the limiting case of large number of stages and large reflux or reboil ratio, a method is presented to predict the variation of the batch and product compositions as a function of time. As a result, the composition space is divided into regions leading to the same set of fractions. The method is geometrical and requires little or no computation. A systematic procedure to devise a feasible sequence is proposed. This procedure includes determining suitable entrainers to break binary azeotropes. It is shown that the use of a batch stripper is essential in breaking minimum boiling binary azeotropes. The techniques developed are illustrated on the separation of methyl acetate from a quaternary azeotropic feed coming from a transesterification reactor. A simple, tractable, design method is presented to estimate flows, equipment sizes, utility loads and costs for any batch column. This method provides a rapid estimate of the design targets for a variable reflux (or reboil) policy without the need of integrating the column model numerically. This policy, which approximates the constant distillate (or bottom) composition policy, shows significant cost savings over the constant reflux (or reboil) policy.
8
"MULTICOMPONENT BATCH DISTILLATION COLUMN SIMULATION AND STATE OBSERVER DESIGN." Master's thesis, METU, 2002. http://etd.lib.metu.edu.tr/upload/12605551/index.pdf.
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9
Yau, Chun-yang, and 姚君揚. "Operation and Control of Batch Extractive Distillation SystemOperation and Control of Batch Extractive Distillation SystemOperation and Control of Batch Extractive Distillation System." Thesis, 2005. http://ndltd.ncl.edu.tw/handle/87946904107531864666.
Full textAbstract:
碩士國立臺灣科技大學
化學工程系
93
In order to separate mixtures containing azeotrope, usually an entrainer is added into the system. There are two ways to add entrainer, including batch extractive distillation (BED) and solvent enhance distillation (SED). According to the boiling points of the mixture and the entrainer, we can distinguish azeotropes and entrainer into six types, but only 4 types are worthy of study. This research completely analyse and simulate operation steps of these four different systems. An important operation step is developed to save entrainer and operation time. This research also compares different separate methods and control strategies. The influence of the operational parameters on the process is studied by computer simulation. Calculations were carried out with a rigorous simulation software “Aspen plus®”and “Aspen dynamics™”.
10
Huang, Cheng Yuan, and 黃正淵. "Operation and control of batch distillation system." Thesis, 2004. http://ndltd.ncl.edu.tw/handle/43163995424164635492.
Full textAbstract:
碩士國立臺灣科技大學
化學工程系
92
The batch distillation can be categorized into four types, as shown in the following: regular column, inverted column, middle vessel column and multivessel column, each has its characteristic and advantage. This research compares different operation and control methods via batch distillation simulation. We will discuss how process dynamic response would be influenced if feed composition changes. These includes fixing reflux ratio strategy, fixing composition strategy and total reflux operation strategy within batch distillation columns that are used for the separation of binary system, ternary system and quaternary nonideal system. Simulation results demonstrate fixing composition strategy in temperature control within regular column is suitable for binary system separation. Fixing composition strategy in temperature control and total reflux strategy in temperature control within middle vessel column is suitable for ternary system separation. Finally, total reflux strategy in temperature control within multivessel column is suitable for quaternary system separation.
11
Lin, Sheng-yu, and 林聖育. "The Optimal Operation of Batch Extractive Distillation System." Thesis, 2006. http://ndltd.ncl.edu.tw/handle/s4u3p3.
Full textAbstract:
碩士國立臺灣科技大學
化學工程系
94
This research studied the optimal operation of batch extractive distillation system for Acetone-Methanol-Water system and Methyl acetate-Carbon tetrachloride- Cyclohexane system. By changing reboiler duty, flow rate of entrainer, reflux ratio, and with different object functions, study on the optimal operation of batch extractive distillation was carried out. The first part of this work studied the case when reboiler duty can be changed at each stage, and comparison was made with that of Yau(2005). The next part studied the optimization under constant reboiler duty policy at each stage but the value of this reboiler duty can be varied. In the final part of this study, operation of batch extractive distillation with middle vessel was investigated and applied to Acetone-Methanol-Water system. It was hope that this kind of operation with a middle vessel can overcome the problems of low yield and long operation time for the regular batch extractive distillation. The comparison was made on these two kinds of operations. The operating results in this work were obtained from computer simulation. Calculations were carried out with rigorous simulation software “Aspen plus®”and “Aspen dynamics™”.
12
Huang, Han jie, and 黃漢傑. "Operation and control of heteroazeotropic batch distillation system." Thesis, 2007. http://ndltd.ncl.edu.tw/handle/92v2c5.
Full textAbstract:
碩士國立臺灣科技大學
化學工程系
95
This research studied the operation and control of the heteroazeotropic batch distillation system. The first part uses regular column to separate the minimum boiling temperature mixture. The next part uses regular column to separate the close-boiling mixture. In this study, we make the operation and control of heteroazeotropic batch distillation system to approach actual condition. For the close-boiling mixture, we compare three kinds of the entrainer and the case without entrainer. We also study and compare three operation and control strategies. The discussion will include effects of the simulation results by changing reboiler duty, the setpoint of the controller, and the content of the entrainer. We also discuss the result of recycling the entrainer and the comparison among different kind of entrainers. In the final part of this study, operation of heteroazeotropic batch distillation with middle vessel was inestigated. It was hope that this kind of operation with a middle vessel can improve the rate of recovery and operating time. We discuss the simulation results of using different entrainers, changing the setpoint of the controller, content of the entrainer, and compare the regular column and middle vessel column. The operating results in this work were obtained from computer simulation. Calculations were carried out with rigorous simulation software “Aspen plus®”and “Aspen dynamics™”.
13
Weerachaipichasgul, W., P. Kittisupakorn, and Iqbal M. Mujtaba. "Improvement of multicomponent batch reactive distillation under parameter uncertainty by inferential state with model predictive control." 2013. http://hdl.handle.net/10454/9752.
Full textAbstract:
yesBatch reactive distillation is aimed at achieving a high purity product, therefore, there is a great deal to find an optimal operating condition and effective control strategy to obtain maximum of the high purity product. An off-line dynamic optimization is first performed with an objective function to provide optimal product composition for the batch reactive distillation: maximum productivity. An inferential state estimator (an extended Kalman filter, EKF) based on simplified mathematical models and on-line temperature measurements, is incorporated to estimate the compositions in the reflux drum and the reboiler. Model Predictive Control (MPC) has been implemented to provide tracking of the desired product compositions subject to simplified model equations. Simulation results demonstrate that the inferential state estimation can provide good estimates of compositions. Therefore, the control performance of the MPC with the inferential state is better than that of PID. In addition, in the presence of unknown/uncertain parameters (forward reaction rate constant), the estimator is still able to provide accurate concentrations. As a result, the MPC with the inferential state is still robust and applicable in real plants.
14
Edreder, E. A., Iqbal M. Mujtaba, and M. Emtir. "Optimal Operation of Batch Reactive Distillation Process Involving Esterification Reaction System." 2015. http://hdl.handle.net/10454/9141.
Full textAbstract:
NoThe performance of batch reactive distillation process involving the esterification of acetic acid with methanol to produce methyl acetate and water is considered in this work. Two cases studies with varying amount of the reactants are considered. The reflux ratio (single time interval) is selected as the control variable to be optimised (treated as piecewise constant) for different but fixed batch time ranging from 5 to 15 h, so as to maximise the conversion of methanol subject to product purity of methyl acetate. The dynamic optimisation problem is converted to a nonlinear programming problem by Control Vector Parameterization (CVP) technique and is solved by using efficient SQP method. The optimisation results show that as the methanol and methyl acetate are wide boiling, the separation of methyl acetate is easier without losing much of methanol reactant. The conversion improves by 6.4 % due to sufficient amount of acetic acid being reacted with methanol. Moreover an excess of acetic acid leads to high operation temperature and therefore high reflux operation (to reduce loss of methanol from the top of the column) to maximise the conversion.
15
Lin, Yu-Sheng, and 林昱昇. "Windows Programming of Batch Extractive Distillation Column for Acetone-Methanol-Water System." Thesis, 2010. http://ndltd.ncl.edu.tw/handle/qt339t.
Full textAbstract:
碩士國立臺北科技大學
化學工程研究所
98
Entrainer was added to a distillation column to increase the relative volatility of mixtures, and then the mixtures can be separated by normal distillation. This research developed a windows simulation program of batch extract distillation column which water was used as the entertainer to separate acetone and methanol. By changing reboiler duty, flow rate of entrainer, reflux ratio, learner can study the optimal operation of batch extractive distillation. This research was to develop program with solving the mass balance, energy balance and phase equilibrium equations of the different operation units and then construct them to be a series of subroutine models. Visual Basic was used to develop the operating interface. By virtue of this simulation results, the steady state value of simulation program is similar by calculated. The dynamic response is also reasonable, therefore this simulation program can be provided for further studies and research of control strategy.
16
Wei, Min-jhong, and 魏民忠. "The operation and control of various batch distillation system with middle vessel." Thesis, 2008. http://ndltd.ncl.edu.tw/handle/46121715733142843815.
Full textAbstract:
碩士國立臺灣科技大學
化學工程系
96
This research mainly studied the operation and control of two kinds of batch distillation system which used middle vessel. These two kinds of system are batch extractive distillation and heteroazeotropic batch distillation. First, we studied batch extractive distillation and heteroazeotropic batch distillation with regular column. Then, we studied these two systems with middle vessel and compared the result vs the regular column. In regular batch extractive distillation, we used two kinds of operative strategy and discussed which strategy is better. These two strategies are “Fix column stage 1 temperature＂ and “Fix reflux ratio＂. As operating each strategy, we discussed the effect of changing each operating variables. Then we discussed the batch extractive distillation with middle vessel. As with the regular column, we also used two operative strategies and compared which one is better. As operating each strategy, we discussed the effect of changing each operating variables. Finally, we discussed the result of recovery percentage, recovered product purity and batch operating time in regular column and middle vessel, respectively. In regular heteroazeotropic batch distillation system, we discussed the result of using two operating strategies. As operating each strategy, we discussed the effect of changing each operating variable . Then we discussed the effect of changing variables in heteroazeotropic batch distillation system with middle vessel. Finally, we discussed the result of recovery percentage, recovered product and batch operating time in regular column and middle vessel operation ,respectively.
17
Edreder, E. A., M. Emtir, and Iqbal M. Mujtaba. "Energy saving in conventional and uncoventional batch reactive distillation: application to hydrolysis of methyl lactate system." 2014. http://hdl.handle.net/10454/10623.
Full textAbstract:
NoIn this work, energy consumption in a middle vessel batch reactive distillation (MVBRD) column is considered for the production of lactic acid via hydrolysis of methyl lactate. A dynamic optimization problem incorporating a process model is formulated to minimize the batch time which consequently minimizes the total energy consumption. The problem is subject to constraints on the amount and purity of lactic acid. The optimisation variables are reflux ratio and/or reboil ratio which are treated as piecewise constant. The earlier work of the authors on energy consumption in conventional batch reactive distillation column (CBRD) for the same reaction system is used for comparative analysis with the energy consumption in MVBRD. As an example, for a given separation task, the optimization results show that MVBRD is capable of saving over 23 % energy compared to energy consumption in CBRD column for the same task.