Feasibility and synthesis of hybrid reactive distillation systems

Chadda, Nitin; Malone, Michael F.; Doherty, Michael F.

doi:10.1002/aic.690481206

Cited by 15 publications

(11 citation statements)

References 30 publications

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“…3. Chadda et al [12] also studied the effect of increasing pressure on the feasible products which lowers the methyl acetate purity. Fig.…”

Section: Production Of Methyl Acetatementioning

confidence: 99%

Conceptual Design of Double‐Feed Reactive Distillation Columns

Avami

2012

Chem Eng & Technol

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The feasibility and feasible range of operating parameters for double-feed reactive distillation columns are evaluated, based on the combination of pinch point map analysis for the middle-section in the compositional space and the feed angle method as an efficient shortcut design method. Limiting bounds for operating parameters are determined where the properties of singular points change. The existence and values of such bounds may vary in double-feed reactive distillation columns depending on the nature of the system under study. The methodology is illustrated by production of methyl acetate and ethyl acetate. An efficient method is described to identify the most promising candidates of double-feed reactive distillation columns and to study the design flexibility in terms of operating parameters.

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“…3. Chadda et al [12] also studied the effect of increasing pressure on the feasible products which lowers the methyl acetate purity. Fig.…”

Section: Production Of Methyl Acetatementioning

confidence: 99%

Conceptual Design of Double‐Feed Reactive Distillation Columns

Avami

2012

Chem Eng & Technol

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“…However, representation of compositions by such transformations alone is not sufficient for kinetically‐controlled reaction regimes, and a three‐dimensional (3‐D) representation is necessary. Chadda et al (2002) found a convenient set of coordinates to represent the liquid‐phase compositions using two reaction invariants given by together with one reference component mole fraction. X 1 , X 2 are the reaction invariants (same as liquid‐phase transformed mole fractions) (Ung and Doherty,1995a), and x IPOAc is the mole fraction of a reference component, isopropyl acetate.…”

Section: Modelmentioning

confidence: 99%

Experimental study of feasibility in kinetically‐controlled reactive distillation

et al. 2005

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Bifurcation studies predict limited ranges of feasibility for products in certain reactive distillations. These are closely related to the bifurcations in the singular points of dynamic models for simple reactive distillation (isobaric open evaporation with liquid phase reaction). A new dynamic model is described with constant vapor rate together with an experimental study for the reactive distillation of acetic acid with isopropanol to produce isopropyl acetate, catalyzed by Amberlyst-15 ion-exchange resin. An experimental apparatus with real-time measurement of liquid compositions based on Fourier transform infrared (FTIR) spectroscopy is described, and used to follow the composition dynamics at several initial conditions and Damköhler numbers (Da). The experimental results match model predictions that show four regions of behavior. For Da Keywords: kinetically-controlled reactive distillation, feasibility, isopropyl acetate reaction, infrared spectroscopy IntroductionReactive distillation is a process alternative that combines reaction and distillation into a single device. Examples of successful reactive distillations are the methyl acetate process, invented by the Eastman Chemical Company (Agreda and Partin, 1984;Agreda et al., 1990) and the diphenyl carbonate process at GE plastics (Oyevaar et al., 2000). However, combining reaction and distillation is not always advantageous, and in some cases may not even be feasible. For example, temperatures for reaction and phase equilibrium may have a large mismatch, some systems may have large energy requirements and costs, for example, ethylene glycol reactive distillation (Okasinski and Doherty, 1997), or interactions of phase behavior and reactions may make separations difficult . Thus, it is necessary to decide whether reactive distillation is a good alternative and a general set of rules is necessary to decide feasibility and incentives for reactive distillation (Xu et al., 1985;Bessling et al., 1998). The feasible product compositions from a reactive distillation are deterCorrespondence concerning this article should be addressed to M. F. Doherty at this current address: Dept. of Chemical Engineering, UCSB, Santa Barbara, CA 93106; e-mail: mfd@engineering.ucsb.edu.This article includes Supplementary Material available from the authors upon request or via the Internet at http://interscience.wiley.com/jpages/0001-1541/suppmat. © 2005 American Institute of Chemical Engineers 464AIChE Journal February 2005 Vol. 51, No. 2 mined for a given feed, column pressure and a rate of reaction, which can be varied parametrically to enlarge the design space ). To design a reactive distillation column, it is necessary to know the product composition specifications that generate a feasible column design and how they depend on operating conditions. Thus, once the basic process chemistry and phase equilibrium are known, feasible product compositions can be obtained from theory (Chadda et al., 2001) and be used in design. However, the validity of this new feasibility theory needs t...

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“…Such generalized reactors involve simultaneous reaction and separation in order to capture beneficial effects such as Le Chatelier's principle, selectivity improvement, avoiding or eliminating difficult separations, and reducing energy usage . Examples of simultaneous reaction‐separation systems include reactive distillation, reactions with membrane separation, and reactive crystallization . Geometric AR methods have been developed for simultaneous reaction and separation, but like the traditional AR methods this approach is limited to a small number of components (typically three or four) …”

Section: Introductionmentioning

confidence: 99%

Target bounds on reaction selectivity via Feinberg's CFSTR equivalence principle

Frumkin

Doherty

2017

AIChE Journal

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In this work, we show that the continuous flow stirred tank reactor (CFSTR) equivalence principle, developed by Feinberg and Ellison, can be used to obtain practical upper bounds on reaction selectivity for any chemistry of interest. The CFSTR equivalence principle allows one to explore the attainable reaction region by decomposing any arbitrary, steady‐state reactor‐mixer‐separator system with total reaction volume V > 0 into a new system comprising R+1 CFSTRs (where scriptR is the number of linearly independent chemical reactions) with the same total reaction volume and a perfect separator system. This work further refines the allowable selectivities by incorporating capacity constraints into the CFSTR equivalence principle to prevent arbitrarily large recycle streams between the CFSTRs and the separators and infinitesimally small CFSTR conversions. These constraints provide practical upper bounds on reaction selectivities of chemistries completely independent of reactor design. We present the methodology and the results for a selection of realistic chemistries. © 2017 American Institute of Chemical Engineers AIChE J, 64: 926–939, 2018

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Feasibility and synthesis of hybrid reactive distillation systems

Cited by 15 publications

References 30 publications

Conceptual Design of Double‐Feed Reactive Distillation Columns

Conceptual Design of Double‐Feed Reactive Distillation Columns

Experimental study of feasibility in kinetically‐controlled reactive distillation

Target bounds on reaction selectivity via Feinberg's CFSTR equivalence principle

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