Relevant bibliographies by topics / Multicomponent Batch Distillation System

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  1. Journal articles
  2. Dissertations / Theses
  3. Book chapters
  4. Conference papers

Academic literature on the topic 'Multicomponent Batch Distillation System'

Author: Grafiati
Published: 4 June 2021
Last updated: 13 February 2022

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Journal articles on the topic "Multicomponent Batch Distillation System"

1

Luyben, William L. "Multicomponent batch distillation. 1. Ternary systems with slop recycle." Industrial & Engineering Chemistry Research 27, no. 4 (April 1988): 642–47. http://dx.doi.org/10.1021/ie00076a019.

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Barolo, M., and G. B. Guarise. "Batch Distillation of Multicomponent Systems with Constant Relative Volatilities." Chemical Engineering Research and Design 74, no. 8 (November 1996): 863–71. http://dx.doi.org/10.1205/026387696523166.

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Reuter, E., G. Wozny, and L. Jeromin. "Modeling of multicomponent batch distillation processes with chemical reaction and their control systems." Computers & Chemical Engineering 13, no. 4-5 (April 1989): 499–510. http://dx.doi.org/10.1016/0098-1354(89)85032-x.

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Al-Tuwaim, Mohammad S., and William L. Luyben. "Multicomponent batch distillation. 3. Shortcut design of batch distillation columns." Industrial & Engineering Chemistry Research 30, no. 3 (March 1991): 507–16. http://dx.doi.org/10.1021/ie00051a011.

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Diwekar, Urmila M., and K. P. Madhavan. "Multicomponent batch distillation column design." Industrial & Engineering Chemistry Research 30, no. 4 (April 1991): 713–21. http://dx.doi.org/10.1021/ie00052a014.

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Ahmad, Berit S., and Paul I. Barton. "Homogeneous multicomponent azeotropic batch distillation." AIChE Journal 42, no. 12 (December 1996): 3419–33. http://dx.doi.org/10.1002/aic.690421212.

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Diwekar, Urmilla, K. P. Madhavan, and R. E. Swaney. "Optimization of multicomponent batch distillation columns." Industrial & Engineering Chemistry Research 28, no. 7 (July 1989): 1011–17. http://dx.doi.org/10.1021/ie00091a019.

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CHIOTTI, OMAR J., HECTOR E. SALOMONE, and OSCAR A. IRIBARREN. "SELECTION OF MULTICOMPONENT BATCH DISTILLATION SEQUENCES." Chemical Engineering Communications 119, no. 1 (January 1993): 1–21. http://dx.doi.org/10.1080/00986449308936104.

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Galindez, H., and Aa Fredenslund. "Simulation of multicomponent batch distillation processes." Computers & Chemical Engineering 12, no. 4 (April 1988): 281–88. http://dx.doi.org/10.1016/0098-1354(88)85039-7.

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Kim, Jeung Kun, and Dong Pyo Ju. "Multicomponent batch distillation with distillate receiver." Korean Journal of Chemical Engineering 20, no. 3 (May 2003): 522–27. http://dx.doi.org/10.1007/bf02705559.

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Dissertations / Theses on the topic "Multicomponent Batch Distillation System"

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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.

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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, &
#916
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.
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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.

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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 EKF
the 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.
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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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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.

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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
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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.

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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.
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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.

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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.
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Bernot, Christine. "Design and synthesis of multicomponent batch distillation." 1990. https://scholarworks.umass.edu/dissertations/AAI9110105.

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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.
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"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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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.

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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™”.
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Huang, Cheng Yuan, and 黃正淵. "Operation and control of batch distillation system." Thesis, 2004. http://ndltd.ncl.edu.tw/handle/43163995424164635492.

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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.
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Book chapters on the topic "Multicomponent Batch Distillation System"

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Floudas, Christodoulos A. "Mixed-Integer Linear Optimization." In Nonlinear and Mixed-Integer Optimization. Oxford University Press, 1995. http://dx.doi.org/10.1093/oso/9780195100563.003.0010.

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This chapter provides an introduction to the basic notions in Mixed-Integer Linear Optimization. Sections 5.1 and 5.2 present the motivation, formulation, and outline of methods. Section 5.3 discusses the key ideas in a branch and bound framework for mixed-integer linear programming problems. A large number of optimization models have continuous and integer variables which appear linearly, and hence separably, in the objective function and constraints. These mathematical models are denoted as Mixed-Integer Linear Programming MILP problems. In many applications of MILP models the integer variables are 0 — 1 variables (i.e., binary variables), and in this chapter we will focus on this sub-class of MILP problems. A wide range of applications can be modeled as mixed-integer linear programming MILP problems. These applications have attracted a lot of attention in the field of Operations Research and include facility location and allocation problems, scheduling problems, and fixed-charge network problems. The excellent books of Nemhauser and Wolsey (1988), and Parker and Rardin (1988) provide not only an exposition to such applications but also very thorough presentation of the theory of discrete optimization. Applications of MILP models in Chemical Engineering have also received significant attention particularly in the areas of Process Synthesis, Design, and Control. These applications include (i) the minimum number of matches in heat exchanger synthesis (Papoulias and Grossmann, 1983; see also chapter 8) (ii) heat integration of sharp distillation sequences (Andrecovich and Westerberg, 1985); (iii) multicomponent multiproduct distillation column synthesis (Floudas and Anastasiadis, 1988); (iv) multiperiod heat exchanger network, and distillation system synthesis (Floudas and Grossmann, 1986; Paules and Floudas, 1988); flexibility analysis of chemical processes (Grossmann and Floudas, 1987); (v) structural properties of control systems (Georgiou and Floudas, 1989, 1990); (vi) scheduling of batch processes (e.g., Rich and Prokapakis, 1986, 1986; Kondili et al., 1993; Shah et al, 1993; Voudouris and Grossmann, 1992, 1993); and (vii) planning and scheduling of batch processes (Shah and Pantelides, 1991, Sahinidis et al, 1989, Sahinidis and Grossmann, 1991). In addition to the above applications, MILP models are employed as subproblems in the mixed-integer nonlinear optimization approaches which we will discuss in the next chapter. In this section, we will present the formulation of Mixed-Integer Linear Programming MILP problems, discuss the complexity issues, and provide a brief overview of the solution methodologies proposed for MILP models.
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Narváez-García, A., J. C. Zavala-Loría, A. Ruiz-Marín, and Y. Canedo-López. "Short-Cut Methods for Multicomponent Batch Distillation." In Distillation - Innovative Applications and Modeling. InTech, 2017. http://dx.doi.org/10.5772/66830.

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Basualdo, Marta S., Carlos A. Ruiz, and Nicolás J. Scenna. "SIMULATION OF MULTICOMPONENT BATCH DISTILLATION WITH CHEMICAL REACTIONS PROCESSES." In Dynamics and Control of Chemical Reactors, Distillation Columns and Batch Processes (Dycord'95), 191–96. Elsevier, 1995. http://dx.doi.org/10.1016/b978-0-08-042368-5.50036-8.

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Zumoffen, D., L. Garyulo, M. Basualdo, and L. Jiménez. "Predictive functional control applied to multicomponent batch distillation column." In Computer Aided Chemical Engineering, 1465–70. Elsevier, 2005. http://dx.doi.org/10.1016/s1570-7946(05)80086-0.

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Sébastien, Pommier, Massebeuf Silvère, Gerbaud Vincent, Baudouin Olivier, Baudet Philippe, and Joulia Xavier. "Heterogeneous batch distillation processes: Real system optimisation." In Computer Aided Chemical Engineering, 1081–86. Elsevier, 2005. http://dx.doi.org/10.1016/s1570-7946(05)80022-7.

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Denes, Ferenc, Peter Lang, and Xavier Joulia. "New generalised double-column system for batch heteroazeotropic distillation." In Computer Aided Chemical Engineering, 366–70. Elsevier, 2011. http://dx.doi.org/10.1016/b978-0-444-53711-9.50074-2.

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MUJTABA, I. M., and S. MACCHIETTO. "OPTIMAL OPERATION OF MULTICOMPONENT BATCH DISTILLATION - A COMPARATIVE STUDY USING CONVENTIONAL AND UNCONVENTIONAL COLUMNS." In Advanced Control of Chemical Processes 1994, 401–6. Elsevier, 1994. http://dx.doi.org/10.1016/b978-0-08-042229-9.50067-7.

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HASEBE, Shinji, Taketoshi KUROOKA, and Iori HASHIMOTO. "COMPARISON OF THE SEPARATION PERFORMANCES OF A MULTI-EFFECT BATCH DISTILLATION SYSTEM AND A CONTINUOUS DISTILLATION SYSTEM." In Dynamics and Control of Chemical Reactors, Distillation Columns and Batch Processes (Dycord'95), 249–54. Elsevier, 1995. http://dx.doi.org/10.1016/b978-0-08-042368-5.50043-5.

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Rao, Ming, and J. Corbin. "INTELLIGENT OPERATION SUPPORT SYSTEM FOR A BATCH SULPHITE PULPING DIGESTER." In Dynamics and Control of Chemical Reactors, Distillation Columns and Batch Processes, 315–19. Elsevier, 1993. http://dx.doi.org/10.1016/b978-0-08-041711-0.50052-0.

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Averbukh, E. A., and A. V. Brodsky. "ELECTROVACUUM GLASS QUALITY CONTROL SYSTEM TRANSFERRING." In Dynamics and Control of Chemical Reactors, Distillation Columns and Batch Processes, 363–66. Elsevier, 1993. http://dx.doi.org/10.1016/b978-0-08-041711-0.50060-x.

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Conference papers on the topic "Multicomponent Batch Distillation System"

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King, Michael S. A., and Ian G. Foulds. "Sensing System for Direct Monitoring of Small Batch Alcohol Distillation." In 2019 IEEE SENSORS. IEEE, 2019. http://dx.doi.org/10.1109/sensors43011.2019.8956511.

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Mardyaningsih, Wedar Panji, Pranoto Hidaya Rusmin, and Budi Rahardjo. "Anomaly Detection and Data Recovery on Mini Batch Distillation Column based Cyber Physical System." In 2019 6th International Conference on Electrical Engineering, Computer Science and Informatics (EECSI). IEEE, 2019. http://dx.doi.org/10.23919/eecsi48112.2019.8977070.

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Susanti, Novita Dwi, Arief Syaichu Rohman, Pranoto Hidaya Rusmin, and Eko Joni Pristianto. "Design of Ethanol Concentration Measurement System Using Specific Gravity Approach for Batch Distillation Column Automation." In 2019 International Conference on Radar, Antenna, Microwave, Electronics, and Telecommunications (ICRAMET). IEEE, 2019. http://dx.doi.org/10.1109/icramet47453.2019.8980445.

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Murkute, Chandrashekhar, and S. D. Agashe. "Development of Comprehensive Decision Support System for the Binary Batch Distillation Column Pilot Plant using PHYTHON." In 2019 3rd International Conference on Trends in Electronics and Informatics (ICOEI). IEEE, 2019. http://dx.doi.org/10.1109/icoei.2019.8862545.

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Budiawan, Irvan, Hidayah R. Pranoto, Egi M. I. Hidayat, and Syaichu R. Arief. "Design and Implementation of Cyber-Physical System-Based Automation on Plant Chemical Process: Study Case Mini Batch Distillation Column." In 2018 6th International Conference on Information and Communication Technology (ICoICT). IEEE, 2018. http://dx.doi.org/10.1109/icoict.2018.8528798.

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Arau´jo, Ofe´lia Q. F., Jose´ L. de Medeiros, and Hellen P. M. Carvalho. "A Maxwell-Stefan Approach for Predicting Mixing Effects in Contiguous Batches of Multi-Product Pipelines." In 2002 4th International Pipeline Conference. ASMEDC, 2002. http://dx.doi.org/10.1115/ipc2002-27179.

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Transient phenomena in the liquid batch interfacial zone are addressed based on: (i) a reliable compositional description; and (ii) mass transfer modeling. In phase (i), compositional models are proposed for transported fluids, with parameters estimated by maximum likelihood procedures to match known characterizing data, like distillation curve, density, viscosity and heteroatom weight fractions. In phase (ii), the transient mixing problem is posed on the continua of axial position in the duct, and described by Maxwell-Stefan formalism for multicomponent mass transfer between two contiguous semi-infinite fluids. Turbulent effects are considered on calculation of mass transfer coefficients, and rigorous thermodynamic driving forces are accounted for through component fugacities predicted by equations of state. The model was solved by the finite element method and the resulting set of ordinary differential equations in time was numerically integrated enabling determination of the mixing zone, calculation of property profiles and monitoring loss of product specifications.
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Mathew, Anil, Mitch Crook, Keith Chaney, and Andrea Humphries. "Bioethanol Production From Canola Straw Using a Continuous Flow Immobilized Cell System." In ASME 2012 6th International Conference on Energy Sustainability collocated with the ASME 2012 10th International Conference on Fuel Cell Science, Engineering and Technology. American Society of Mechanical Engineers, 2012. http://dx.doi.org/10.1115/es2012-91061.

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Abstract:
Global cultivation of canola increased by approximately 22% between 2000 and 2009, due to increased demand for canola oil for biodiesel production and as an edible oil. In 2009 over 290,000 km2 of canola was cultivated globally. In contrast to oilseed, the commercial market for canola straw is minimal and it is generally ploughed back into the field. The high carbohydrate content (greater than 50 % by dry weight) of canola straw suggests it would be a good feedstock for second-generation bioethanol production. There are four major steps involved in bioethanol production from lignocellulosic materials: (i) pretreatment, (ii) hydrolysis, (iii) fermentation, and (iv) further purification to fuel grade bioethanol through distillation and dehydration. Previous research demonstrated a glucose yield of (440.6 ± 14.9) g kg−1 when canola straw was treated using alkaline pretreatment followed by enzymatic hydrolysis. Whilst bioethanol can be produced using cells free in solution, cell immobilization provides the opportunity to reduce bioethanol production costs by minimizing the extent to which down-stream processing is required, and increasing cellular stability against shear forces. Furthermore, the immobilization process can reduce substrate and product inhibition, which enhances the yield and volumetric productivity of bioethanol production during fermentation, improves operational stability and increases cell viability ensuring cells can be used for several cycles of operation. Previous research used cells of Saccharomyces cerevisiae immobilized in Lentikat® discs to convert glucose extracted from canola straw to bioethanol. In batch mode a yield of (165.1 ± 0.1) g bioethanol kg−1 canola straw was achieved. Continuous fermentation is advantageous in comparison to batch fermentation. The amount of unproductive time (e.g. due to filling, emptying and cleaning) is reduced leading to increased volumetric productivity. The higher volumetric productivity of continuous fermentation means that smaller reactor vessels can be used to produce the same amount of product. This reduces the capital costs associated with a fermentation plant. Research demonstrated a higher bioethanol yield was attained (224.7 g bioethanol kg−1 canola straw) when glucose was converted to bioethanol using immobilized cells in packed-bed continuous flow columns. On an energy generation basis, conversion of 1 kg of canola straw to bioethanol resulted in an energy generation of 6 MJ, representing approximately 35% energy recovery from canola straw. The amount of energy recovered from canola straw could be improved by increasing the amount of energy recovered as bioethanol and by utilising the process by-products in a biorefinery concept.
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