Efficient separation method for tert -butanol dehydration via extractive distillation

Lo, Ka-Man; Chien, I‐Lung

doi:10.1016/j.jtice.2016.07.040

Cited by 55 publications

(16 citation statements)

References 17 publications

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“…A variety of objective functions has been used in the literature. Minimizing TAC that incorporates both operational and capital costs, is a wide-spread choice (Kossack et al, 2008;Emhamed et al, 2008;Wang et al, 2012Wang et al, , 2015aMedina-Herrera et al, 2014;Brito et al, 2016;Lo and Chien, 2017;Ahmadian Behrooz, 2017). A similar measure, called economic potential was used by Langston et al (2005).…”

Section: Optimizationmentioning

confidence: 99%

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

Gerbaud

Rodríguez-Donis

Hégely

et al. 2019

Chemical Engineering Research and Design

200

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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: Optimizationmentioning

confidence: 99%

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

Gerbaud

Rodríguez-Donis

Hégely

et al. 2019

Chemical Engineering Research and Design

200

View full text Add to dashboard Cite

show abstract

“…The liquid–liquid extraction column consumes no energy, and all of the columns operate at atmospheric pressure, avoiding the high energy consumption caused by high‐pressure operation. The high‐purity IBE product can be directly used as gasoline additive without further separation 23 . A suitable solvent – 2‐EA or MTBE – which is applied in the extraction, combined with the extractive or azeotropic distillation process, is selected respectively through the COSMO‐SAC model and Aspen simulation.…”

Section: Introductionmentioning

confidence: 99%

A novel energy‐efficient extraction‐assisted distillation design for isopropanol–butanol–ethanol purification for use of gasoline additive

et al. 2021

J of Chemical Tech & Biotech

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BACKGROUND Biobutanol is considered to be a promising alternative biofuel in terms of sustainability and environmental friendliness because of its desirable properties. High purity isopropanol–butanol–ethanol (IBE) mixture can be directly used as gasoline additive. However, the purification process of IBE is hindered because of its low concentration and high energy consumption. In order to reduce energy consumption and improve the efficiency of the IBE purification process, two novel processes combining liquid–liquid extraction with extractive distillation or azeotropic distillation are proposed. Moreover, the heat integration designs of the processes are carried out to further reduce energy. These processes are compared with regard to energy, economic, environmental and exergy impact. RESULTS The results show that the energy consumption of these enhanced processes are effectively reduced compared with the original process in the literature. Among them, the thermal integrated process of liquid–liquid extraction combined with extractive distillation is the best design, which has a total annual cost of $32.656 × 105 and an energy consumption of 5936.94 kW. CONCLUSION Compared with the original process, this process can save 71.33% of energy consumption. © 2021 Society of Chemical Industry

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“…Extractive distillation (ED) has been widely applied to separate azeotropes, such as isopropanol dehydration, tert ‐butanol dehydration, propylene glycol methyl ether dehydration, ethyl acetate/ethanol separation, 2‐methoxyethanol/toluene separation and methylal/methanol separation . The azeotropic feed in plants usually contains impurities.…”

Section: Introductionmentioning

confidence: 99%

Control of extractive distillation processes with intermediate impurities removed as a side withdrawal from the extractive distillation column

Jiang

et al. 2020

J of Chemical Tech & Biotech

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BACKGROUND The design and control of extractive distillation (ED) for separating azeotropes has been widely investigated. However, most researches only deal with simple binary azeotropes without considering impurities. In fact, in industrial practices, intermediate impurities can be removed as a side withdrawal from the extractive distillation column. The dynamic control of such processes has not been investigated. Furthermore, there are many heat‐integrated alternatives of basic ED sequence. When considering impurities withdrawn, the dynamic control of these alternatives may face some difficulties. Thus, this article aims to establish the effective control structures of ED processes for separating azeotropes with intermediate impurities, including basic sequence and heat‐integrated alternatives. Ethanol dehydration is selected to be explored, including a basic sequence (BS), a heat‐integrated sequence (HIS) which combines the pre‐concentration column and the entrainer recovery column into one column and the thermodynamic equivalent sequence of the HIS (TEHIS). Overall assessment of the dynamic performances of these sequences is implemented. RESULTS For all the sequences, the dynamic performance with entrainer recycling stream being proportional to the extractive distillation column (EDC) feed is better than being proportional to the fresh feed. Meanwhile, large negative transient deviations in the water product purity and intensive fluctuations of sensitive‐stage temperatures can be observed for the HIS, but not for the TEHIS. CONCLUSIONS The TEHIS is the best sequence considering both economics and dynamics. These sequences and the analyses of their dynamic controllability are valuable in practice for multicompoent azeotropes purification. © 2020 Society of Chemical Industry

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Efficient separation method for tert -butanol dehydration via extractive distillation

Cited by 55 publications

References 17 publications

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

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

A novel energy‐efficient extraction‐assisted distillation design for isopropanol–butanol–ethanol purification for use of gasoline additive

Control of extractive distillation processes with intermediate impurities removed as a side withdrawal from the extractive distillation column

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