Improved design and optimization for separating tetrahydrofuran–water azeotrope through extractive distillation with and without heat integration by varying pressure

Gu, Jinglian; You, Xinqiang; Tao, Changyuan; Li, Jun; Shen, Weifeng; Li, Jie

doi:10.1016/j.cherd.2018.03.015

Cited by 56 publications

(23 citation statements)

References 24 publications

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“…For TAC calculation, the tray efficiency was assumed to be 0.75 for estimating real trays. The payback period as set at 3 yr and the formulas for the calculations are summarized in Table . In the global economic optimization process, several key variables such as distillate flow, reflux ratios, side flow and location were adopted to meet the design requirements of recovery and purity of products and solvents.…”

Section: Design Basismentioning

confidence: 99%

Thermal coupled extractive distillation sequences with three entrainers for the separation of azeotrope isopropyl alcohol + diisopropyl ether

Zhang

Gao

et al. 2020

J of Chemical Tech & Biotech

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BACKGROUND During the synthesis of isopropyl alcohol (IPA) by hydration of propylene, diisopropyl ether (DIPE) is usually produced as a by‐product. Because IPA and DIPE can form a binary homogeneous azeotrope with the minimum boiling temperature at atmospheric pressure, it is difficult to separate the binary mixture by simple distillation. RESULT For separating the azeotrope IPA + DIPE, side‐stream extractive distillation column (SSED) and extractive dividing wall column (EDWC) processes with three entrainers [2‐methoxyethanol (2‐MEA), 2‐ethoxyethanol and propylene glycol ethyl ether (PGEE)] were simulated and optimized based on the minimal total annual cost (TAC). Moreover, CO2 emissions of the six sequences were calculated and the impact on the environment evaluated. CONCLUSIONS The sequence of SSED with PGEE as entrainer can reduce TAC by ≤34.48%, but EDWC with PGEE can offer TAC reduction of ≤52.46%. The results demonstrate that the EDWC sequence with PGEE as entrainer is favourable for separating the binary azeotrope IPA + DIPE. © 2020 Society of Chemical Industry

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Section: Design Basismentioning

confidence: 99%

Thermal coupled extractive distillation sequences with three entrainers for the separation of azeotrope isopropyl alcohol + diisopropyl ether

Zhang

Gao

et al. 2020

J of Chemical Tech & Biotech

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“…The cost formulas used in our previous study 41 are employed for the capital cost calculation, and a three-year payback period is used (see Table S1 in the Supporting Information). For the capital cost, only the major equipment like column shell, tray, condenser, reboiler, and heat exchanger (for cooling down the recycled entrainer stream) are considered while other costs such as the pumps, pipes, and valves are neglected.…”

Section: Tacmentioning

confidence: 99%

“…There are three possible conditions for the DEHI process: direct partial heat integration (DPHI), direct full heat integration (DFHI), and optimal heat integration (OHI). 41 The OHI process goes one step further than the DPHI and DFHI processes by optimizing the eight variables (N FE , N F1 , N F2 , N F3 , F E , RR 1 , RR 2 , RR 3 ) together via a two-step optimization procedure, but under the minimization of an improved full energy consumption (FEC2), as shown in eq 6. The meaning of the variables and the value of the factors are the same as in section 2.3.…”

Section: Double-effect Heat-integrated Extractive Distillationmentioning

confidence: 99%

Energy-Saving Reduced-Pressure Extractive Distillation with Heat Integration for Separating the Biazeotropic Ternary Mixture Tetrahydrofuran–Methanol–Water

You

Tao

et al. 2018

Ind. Eng. Chem. Res.

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There is rich literature on the separation of binary azeotropic mixtures, whereas few studies exist on the separation of biazeotropic ternary mixtures. In this work, we propose a systematic approach for energy-efficient extractive distillation processes for the separation of a biazeotropic mixture that involves thermodynamic insights via residue curve maps and the univolatility line to find the optimal entrainer and operating pressure, global optimization based on a proposed two-step optimization procedure, and double-effect heat integration to achieve further saving of energy consumption. An energy-saving reduced-pressure extractive distillation (RPED) with a heat integration flowsheet is then proposed to achieve the minimum total annual cost (TAC). The results show that the TAC, energy consumption, and exergy loss of the proposed RPED with heat integration are reduced by 75.2%, 80.5%, and 85.8% compared with literature designs.

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“…In the chemical industry are numerous combinations of organic solvent and water, which are waste products in various processes and, in many cases, form an azeotropic mixture. For the separation of those mixtures, several techniques are used, including membranes, pressure swing distillation, and extractive distillation, because conventional distillation is not sufficient for azeotropic mixtures [2][3][4][5][6]. However, the achievement of high purity at low cost and energy consumption is still a challenge.…”

Section: Introductionmentioning

confidence: 99%

Zero-Discharge Process for Recycling of Tetrahydrofuran–Water Mixtures

2021

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The sustainable design of separation and polymer synthesis processes is of great importance. Therefore, an energy-efficient process for the purification of tetrahydrofuran (THF)–water (H2O) solvent mixtures from an upstream polymer synthesis process in pilot scale was developed with the aim to obtain high purity separation products. The advantages and limitations of a hybrid process in the pilot scale were studied utilizing an Aspen Plus Dynamics® simulation at different pressures to prove the feasibility and energy efficiency. For the rough separation of the two components, distillation was chosen as the first process step. In this way, a separation of a water stream of sufficient quality for further precipitations after polymer synthesis could be achieved. In order to overcome the limitations of the distillation process posed by the azeotropic point of the mixture, a vapor permeation is used, which takes advantage of the heat of evaporation already used in the distillation column. For the purpose of achieving the required low water contents, an adsorption column is installed downstream for final THF purification. This leads to a novel hybrid separation process that is energy efficient and thus allows also the use of the solvents again for upstream polymer synthesis achieving the high purity requirements in a closed-loop process.

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Improved design and optimization for separating tetrahydrofuran–water azeotrope through extractive distillation with and without heat integration by varying pressure

Cited by 56 publications

References 24 publications

Thermal coupled extractive distillation sequences with three entrainers for the separation of azeotrope isopropyl alcohol + diisopropyl ether

Thermal coupled extractive distillation sequences with three entrainers for the separation of azeotrope isopropyl alcohol + diisopropyl ether

Energy-Saving Reduced-Pressure Extractive Distillation with Heat Integration for Separating the Biazeotropic Ternary Mixture Tetrahydrofuran–Methanol–Water

Zero-Discharge Process for Recycling of Tetrahydrofuran–Water Mixtures

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