Dynamic simulation of a batch extractive distillation process

Yatim, H.; Morand, Pierre; Otterbein, M.; Lang, P. T.

doi:10.1016/0098-1354(93)80209-6

Cited by 37 publications

(31 citation statements)

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“…In both regions hexylamine is the high boiling component. In addition, the existence of the curve ␣ s1 adds et al 1993, Lang et al 1994, and Lelkes et al 1998 , for a batch extractive homogeneous rectifying column. The only difference with the homogeneous entrainer process is the immiscibility gap defined by the presence of the binary heteroazeotrope.…”

Section: A B a E B Ementioning

confidence: 95%

Heterogeneous batch‐extractive distillation of minimum boiling azeotropic mixtures

et al. 2003

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Section: A B a E B Ementioning

confidence: 95%

Heterogeneous batch‐extractive distillation of minimum boiling azeotropic mixtures

et al. 2003

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“…On the other hand, for the heterogeneous process, top entrainer feeding is possible and discussed in Sections 3.1.1 and 3.1. 2. The continuous process for a direct split was studied early in the twentieth century (Schneibel, 1923) and later suggested for the indirect split (Hunek et al, 1989) while batch extractive distillation was studied since the 90's (Lang et al, 1999 for the indirect split; Yatim et al, 1993 for the direct split). For the batch process many different column configurations, depending on the entrainer feed location, were investigated extensively, which results were summarized in Stéger et al (2005) for the direct split configuration and Varga (2006) for the indirect split configuration (see Table 6 later).…”

Section: Column Configuration and Operation 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

192

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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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“…The batch extractive distillation with the application of a heavy solvent in a batch rectifier was studied among others by Yatim et al [13], Lelkes et al [14], and in a middle vessel column by Safrit et al [15], Warter and Stichlmair [16], Cui et al [17], Low and Sorensen [18], Warter et al [19]. Hua et al, [20] proposed a tworeboiler batch rectifier configuration for batch extractive distillation.…”

Section: Introductionmentioning

confidence: 99%

Generalised model for heteroazeotropic batch distillation with variable decanter hold-up

Hégely

Gerbaud

Lang

2013

Separation and Purification Technology

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OATAO is an open access repository that collects the work of Toulouse researchers and makes it freely available over the web where possible. This is an author-deposited version published in : http://oatao. hold-up. (2013) Separation and Purification Technology, vol. 115. pp. 9-19. ISSN 1383-5866 Any correspondance concerning this service should be sent to the repository administrator: staff-oatao@listes-diff.inp-toulouse.fr t r a c tA general model of batch heteroazeotropic distillation is proposed. Both liquid phases present in the decanter can be refluxed or withdrawn as distillate, their hold-up can be increased, decreased or kept constant, as well. By assuming maximal separation, that is, that the composition of the condensate always equals to that of the heteroazeotrope, the still path equation was derived. The still path directions are determined for all the 16 possible operational policies. It is possible to steer the still path in a desired direction by changing the operational parameters, which allows the recovery of a pure component in the still. The still path directions are validated by rigorous simulations for three policies not published yet using the mixture water -formaldehyde -propyl formate. From the 16 operational policies, 11 can be considered as useful in practice. To demonstrate the advantage of using a non-traditional policy, the separation of the mixture aniline -ethylene glycol -water was investigated, as well. By using a non-traditional operational policy with hold-up reduction in the decanter a higher purity of ethylene glycol was obtained in the still.

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Dynamic simulation of a batch extractive distillation process

Cited by 37 publications

References 1 publication

Heterogeneous batch‐extractive distillation of minimum boiling azeotropic mixtures

Heterogeneous batch‐extractive distillation of minimum boiling azeotropic mixtures

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

Generalised model for heteroazeotropic batch distillation with variable decanter hold-up

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