Separation of azeotropes in batch extractive stripper with intermediate entrainer

Varga, V.; Frits, Erika R.; Gerbaud, Vincent; Fonyó, Z.; Joulia, Xavier; Lelkes, Z.; Rév, Endre

doi:10.1016/s1570-7946(06)80142-2

Cited by 7 publications

(12 citation statements)

References 4 publications

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“…Comparison of all processes leads to recommend the use of BED-I with a heavy entrainer. With a light entrainer the BES-I column configuration was recommended (Lang et al, 1999;Varga, 2006;Shen et al, 2015c) but a batch rectifier configuration is also possible (Stéger et al, 2005;Varga et al, 2006aVarga et al, , 2006b. Table 6 summarizes the configurations recommended when using batch extractive distillation process for the separation of minimum or maximum boiling azeotrope or low relative volatility mixtures with a heavy, light or intermediate boiling entrainer (Varga, 2006) With a heavy entrainer, the main load F AB is initially in the still, the batch column is a rectifier with an extractive and a rectifying section (Fig.…”

Section: Batch Operating Modementioning

confidence: 99%

Review of extractive distillation. Process design, operation, optimization and control

Gerbaud

Rodríguez-Donis

Hégely

et al. 2019

Chemical Engineering Research and Design

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190

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Operation and control Extractive distillation processes enable the separation of non-ideal mixtures, including minimum or maximum boiling azeotropes and low relative volatility mixtures. Unlike azeotropic distillation, the entrainer fed at another location than the main mixture induces an extractive section within the column. A general feasibility criterion shows that intermediate and light entrainers and heterogeneous entrainers are suitable along common heavy entrainers. Entrainer selection rules rely upon selectivity ratios and residue curve map (rcm) topology including univolatility curves. For each type of entrainer, we define extractive separation classes that summarize feasibility regions, achievable products and entrainer-feed flow rate ratio limits. Case studies are listed as Supplementary materials. Depending on the separation class, a direct or an indirect split column configuration will allow to obtain a distillate product or a bottom product, which is usually a saddle point of rcm. Batch and continuous process operations differ mainly by the feasible ranges for the entrainer-feed flow rate ratio and reflux ratio. The batch process is feasible under total reflux and can orient the still path by changing the reflux policy. Optimisation of the extractive process must systematically consider the extractive column along with the entrainer regeneration column that requires energy and may limit the product purity in the extractive column through recycle. For the sake of reducing the energy cost and the total cost, pressure change can be beneficial as it affects volatility, or new process structures can be devised, namely heat integrated extractive distillation, extractive divided wall column or processes with preconcentrator.

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Section: Batch Operating Modementioning

confidence: 99%

Review of extractive distillation. Process design, operation, optimization and control

Gerbaud

Rodríguez-Donis

Hégely

et al. 2019

Chemical Engineering Research and Design

Self Cite

190

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“…Batch extractive distillation columns can be divided into three different zones: rectifying or stripping section, extractive section, and still vessel [10][11][12]. The rectifying section is located below the distillate and the stripping section above the bottom product.…”

Section: Single-reaction Systemsmentioning

confidence: 99%

“…proposed by Stéger et al [2], where "a i " can be any liquid, vapor, feed, or product component flow rate, the reactive profiles are brought to the same form used for the nonreactive sections by Lelkes et al [10] and Varga et al [12] ( Table 1).…”

Section: Single-reaction Systemsmentioning

confidence: 99%

“…where ν i is stoichiometric coefficient of component i in the reaction, ν T is the sum (total) of all the stoichiometric coefficients in the reaction, and the index ref refers to a reference component. Using this transformation together with the transformation shown in (1), proposed by Stéger et al [2], the vessel path equation is brought to a form similar to that used for the nonreactive vessel by Lelkes et al [10] and Varga et al [12]. The equations have the same form if the total change of moles in the reaction is zero.…”

Section: Section Nonreactive Reactivementioning

confidence: 99%

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Feasibility of Batch Reactive Distillation with Equilibrium‐Limited Consecutive Reactions in Rectifier, Stripper, or Middle‐Vessel Column

Lukacs

Stéger

Rév

et al. 2011

International Journal of Chemical Engineering

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A general overall feasibility methodology of batch reactive distillation of multireaction systems is developed to study all the possible configurations of batch reactive distillation. The general model equations are derived for multireaction system with any number of chemical equilibrium-limited reactions and for any number of components. The present methodology is demonstrated with the detailed study of the transesterification of dimethyl carbonate in two reversible cascade reactions in batch reactive distillation process. Pure methanol is produced as distillate, and pure diethyl carbonate is produced at the bottom simultaneously in middle-vessel column; in each section, continuous feeding of ethanol is necessary. The results of feasibility study are successfully validated by rigorous simulations.

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“…The model equations can be constructed from a submodel related to batch rectifiers and a separate submodel related to batch strippers. Our research group has already published the model equations for nonreactive batch extractive distillation performed in batch rectifier4 and in batch stripper 18. Table 1 summarizes all the model equations for nonreactive column profiles.…”

Section: Generic Feasibility Studymentioning

confidence: 99%

A generic feasibility study of batch reactive distillation in hybrid configurations

Stéger¹,

Lukacs²,

Rév³

et al. 2009

AIChE Journal

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A new graphical feasibility method is developed to investigate batch reactive distillation processes in middle vessel column. The suggested methodology can deal with fully reactive, nonreactive, and complex column configuration. A new formulation is suggested to describe the composition profiles in the reactive sections. Its application has made possible to develop a generic feasibility methodology containing the same model equations independently of the presence or absence of reaction. By combining the reactive and nonreactive models, not only the fully reactive and fully nonreactive but also hybrid configurations can be studied. Feasibility criteria related to the hybrid configurations are also presented. Application of the new methodology is demonstrated on the production of ethyl acetate in batch reactive distillation. Five configurations are found feasible; pure EtOAc is produced as distillate, and pure H 2 O is produced at the bottom. In each case, continuous feeding of AcOH is necessary. V V C 2009 American Institute of Chemical Engineers AIChE J, 55: 1185AIChE J, 55: -1199AIChE J, 55: , 2009 Keywords: separation, reactive distillation, design, feasibility study, hybrid column IntroductionApplying reactive distillation is one of the most important options for process intensification. 1,2 In traditional processes, the reaction itself and the separation of the reaction products are carried out in subsequent operations, and in separate devices. Total conversion cannot be reached if the reaction is equilibrium limited, and the nonreacted components must be recycled to the reactor. This recycling increases the investment and the energy demand, as well. In addition, transportation of the compounds between the equipment units makes the production more hazardous.In reactive distillation, on the other hand, the reaction and the separation are carried out in one operation, in the same unit ( Figure 1). The investment costs are decreased because of the decreasing number of operation units. The operation costs, the hazards related to the process, and the amount of by-products are also decreased because no external recycling is applied.In spite of the numerous advantages, the number of industrial applications is yet small. One of the reasons of this reluctance may be the lack of well-known design and control Correspondence concerning this article should be addressed to C. Stéger at stegercsaba@googlemail.com. methodology. Hence, the thorough investigation and deep understanding of this integrated process is a really important task.Preliminary design methodologies are normally applied to find a feasible configuration accompanied by a suggested value or range of the most important operation parameters. These methods usually rely on some simplified model with thermodynamic approach, 3 namely they neglect such technical parameters such as the hold-up, the pressure drop, the height and the diameter of the column, and so forth. Most of the preliminary methods work in graphical mode; this eases their understanding but, at t...

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Separation of azeotropes in batch extractive stripper with intermediate entrainer

Cited by 7 publications

References 4 publications

Review of extractive distillation. Process design, operation, optimization and control

Review of extractive distillation. Process design, operation, optimization and control

Feasibility of Batch Reactive Distillation with Equilibrium‐Limited Consecutive Reactions in Rectifier, Stripper, or Middle‐Vessel Column

A generic feasibility study of batch reactive distillation in hybrid configurations

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