Multicomponent homogeneous azeotropic distillation 3. Column sequence synthesis

Thong, Dennis Y.-C.; Jobson, Megan

doi:10.1016/s0009-2509(01)00057-4

Cited by 34 publications

(50 citation statements)

References 9 publications

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“…Product regions and feasible splits can be identified based on this test. Thong and Jobson further extend their approach toward an algorithmic procedure to generate column sequences [85,86]: first, all possible splits are identified, and then a superstructure covering (preferably all) recycling options is generated and reduced in complexity by applying a set of heuristic rules. The resulting superstructure is used to determine the compositions of product and recycle streams in an iterative procedure.…”

Section: Algorithmic Approaches For the Generation Of Distillation Prmentioning

confidence: 99%

Conceptual Design of Azeotropic Distillation Processes

2014

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Section: Algorithmic Approaches For the Generation Of Distillation Prmentioning

confidence: 99%

Conceptual Design of Azeotropic Distillation Processes

2014

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“…Hence, a recycle stream is not needed. Contrarily, a process alternative without recycle streams cannot be found, if a feasibility analysis based on SDB 27 is used. Using successive examination of residue curves, it can be determined that the balance line of column C‐1 intersects the SDB at x I = (0.0105, 0.1855, 0.4948, 0.3092).…”

Section: Additional Examplesmentioning

confidence: 99%

Conceptual design of distillation processes for mixtures with distillation boundaries. II. Optimization of recycle policies

Brüggermann

Marquardt

2011

AIChE Journal

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Geometric design methods for the conceptual design of azeotropic distillation processes are fast and efficient tools for the economic screening of different process alternatives. The second article of this two-part series presents a novel optimization-based conceptual design framework for azeotropic distillation processes, which allows a rapid screening of the different process alternatives with respect to feasibility and economic incentive. The design framework is based on the economic assessment of distillation columns by the rectification body method. The feasibility limits imposed by the azeotropes are incorporated using the split feasibility test introduced in the first part of this series. The application of the framework is highlighted with several ternary and quaternary process alternatives for the production of high-purity alcohols. Figure 6. Mass balances of the ternary pressure-swing process at the energetically optimal operating point.

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“…However, it is hard and complex to separate the specified mixture due to the presence of three binary azeotropes at atmospheric pressure. Many special techniques are available for the separation of azeotropes, such as azeotropic distillation, [1][2][3][4] extractive distillation, [5][6][7][8][9][10][11] pressure-swing distillation, 12-14 hybrid distillation-pervaporation, 15,16 salt distillation 17,18 and several other separation techniques. [19][20][21] Recently, a few pressure-swing distillation studies have been reported for separating multiazeotropic systems, [22][23][24] yet there have been no relevant studies on extractive distillation which is also a promising alternative method.…”

Section: Introductionmentioning

confidence: 99%

Comparison of extractive distillation separation sequences for acetonitrile/methanol/benzene multi‐azeotropic mixtures

Wang

Guang

et al. 2018

J of Chemical Tech & Biotech

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Background The extractive distillation‐based separation of a multi‐azeotropic mixture has several optional solvents and schemes. The screen of a suitable solvent was performed and diverse extractive distillation sequences were compared for separating the specified mixture of acetonitrile/methanol/benzene. Result As a solvent breaking all binary azeotropes, chlorobenzene was selected over aniline on the basis vapor–liquid equilibrium diagrams and infinite dilution factors. Four separation sequences were optimized by the sequential iterative procedure on the basis of minimal total annual cost (TAC), and CO2 emissions were calculated. Among four sequences, sequence III, composed of two extractive distillation columns and one solvent recovery column, is the best scheme from environmental and economic viewpoints. Simple partial heat integration was further implemented and can save 20.08% and 8.86% in terms of energy cost and TAC. Conclusion The results demonstrate that the separation of acetonitrile/methanol/benzene is fully achievable using common extractive distillation with chlorobenzene as solvent. Moreover, there is a trade‐off between heat transfer in the reboiler‐condenser and corresponding energy consumption variations due to pressure changes when considering heat integration. © 2018 Society of Chemical Industry

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Multicomponent homogeneous azeotropic distillation 3. Column sequence synthesis

Cited by 34 publications

References 9 publications

Conceptual Design of Azeotropic Distillation Processes

Conceptual Design of Azeotropic Distillation Processes

Conceptual design of distillation processes for mixtures with distillation boundaries. II. Optimization of recycle policies

Comparison of extractive distillation separation sequences for acetonitrile/methanol/benzene multi‐azeotropic mixtures

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