Comparative study of conventional, reactive-distillation and pervaporation integrated hybrid process for ethyl tert-butyl ether production

Norkobilov, Adham; Gorri, Daniel; Ortiz, Inmaculada

doi:10.1016/j.cep.2017.07.003

Cited by 33 publications

(9 citation statements)

References 39 publications

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“…The vaporous permeate leaving the membrane module is condensed in an external heat exchanger. The vacuum pump is only used for the removal of the inert gases, but has no other function in the process . The continuous removal of the vaporous permeate creates a concentration gradient across both sides of the pervaporation membrane.…”

Section: Introductionmentioning

confidence: 99%

Alcohol and Alkane Organic Extraction Using Pervaporation Process

Hamouni

Arous²,

Abdessemed

et al. 2019

Macromolecular Symposia

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In this work, different feed mixtures are investigated for the separation of alcohol‐water, toluene‐water, alcohol‐toluene, and alkane‐toluene mixtures by pervaporation using a poly (dimethylsiloxane) membrane (PDMS). The polymeric membrane is characterized by Fourier transform infrared spectrometry (FTIR), scanning electron microscopy (SEM), and thermogravimetric analysis (TGA). The total flux and membrane selectivity for hexane‐toluene mixtures are found to be greater than those obtained for heptane‐toluene, alcohol‐toluene, toluene‐water, and alcohol‐water mixtures. Moreover, the total flux and selectivity for the alkane‐toluene mixtures are found to be higher than those obtained for the alcohol‐toluene mixtures. The feed concentration and the temperature for hexane‐toluene mixture have the same effect on the membrane total flux. Overall, the pervaporation separation index (PSI) decreases with increasing feed concentration. The highest PSI value of 20 359 g m−2 h−1 is found at a hexane feed concentration of 10 wt%, a temperature of 40 °C, a permeation flux equal to 717 g m−2 h and a selectivity of 29.

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Section: Introductionmentioning

confidence: 99%

Alcohol and Alkane Organic Extraction Using Pervaporation Process

Hamouni

Arous²,

Abdessemed

et al. 2019

Macromolecular Symposia

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“…[7][8][9][10] In a conventional HDPS, the pervaporation unit is externally connected to the distillation column (externally connected distillation-pervaporation, ECDP). [11] As a result, the main pervaporation and distillation limitations are introduced to an ECDP system. Specifically, concentration and temperature polarization occur inside the pervaporation module, decreasing the mass and energy transport across the membrane.…”

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confidence: 99%

Analysis of a hybrid distillation‐pervaporation column in a single unit: Intermediate membrane section in the rectifying and stripping section

León

Fontalvo

2020

Can J Chem Eng

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Distillation‐pervaporation in a single unit (DPSU) column can perform separations that are not possible in conventional distillation by overcoming distillation boundaries. Unlike conventional hybrid distillation‐pervaporation columns, in a DPSU system the pervaporation membrane is located inside the column. The separation by distillation and pervaporation is carried out simultaneously inside the same column section. In a previous work, a simplified model was used to design and analyze distillation‐pervaporation in a single unit (DPSU) systems with a hybrid rectifying‐pervaporation section, where the membrane constitutes the whole section. In this study, this simplified model is applied to DPSU columns where the membrane partially constitutes the rectifying or the stripping sections, including the model derivation of the stripping section and the operation leaves. The simplified model is applied for the separation of two mixtures with different Serafimov's topology classifications: acetone‐isopropanol‐water (topology type 1.0‐2) and ethyl acetate‐ethanol‐methanol (topology type 2.0‐2b). Thermodynamic limitations are identified for the separation of the ethyl acetate‐ethanol‐methanol mixture. Multiple operation leaves are produced depending on the liquid composition at the beginning of the membrane section, hindering the conditions that help to overcome the distillation boundary through a DPSU column. For some conditions, a section that is partially constituted by a membrane performs better than if the membrane constitutes the whole section.

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“…In order to improve the conversion, process intensification techniques have been used. Instead of using a reactor and a couple of distillation columns, a reactive distillation tower has been evaluated − and optimized. , Recent studies have compared the traditional and the integrated method resulting in the fact that although the reactive distillation column increases the conversion, the energy consumption is higher . However, other studies highlight not only the high conversions but also the low operating costs. ,, However, typically the feed of i -butene contains a number of other chemicals.…”

Section: Introductionmentioning

confidence: 99%

Integrated Renewable Production of ETBE from Switchgrass

Galán

Martı́n

Grossmann

2019

ACS Sustainable Chem. Eng.

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In this work, we propose the optimization of a flowsheet for the conceptual design of an integrated renewable production of ETBE from ethanol and i-butene from switchgrass. A superstructure embedding a number of alternatives is proposed. Two technologies are considered for switchgrass pretreatment, dilute acid and a novel ammonia fiber explosion (AFEX), so that the structure of the grass is broken down. Only glucose is fermented to produce i-butene, while xylose is fermented to ethanol. Ethanol is purified using a multieffect column followed by molecular sieves and a PSA-membrane system is used to upgrade the i-butene. The problem is formulated as an MINLP, and solved for each pretreatment as an NLP. Finally, an economic evaluation is performed including a sensitivity analysis. Biomass composition determines the byproduct obtained. Dilute acid is the selected pretreatment due to the largest yield to sugars and the possibility of adjusting the production of both i-butene and ethanol for the needs to ETBE. For a facility that produces 90 kt/yr of ETBE, the investment adds up to 160 M€ for a production cost of 0.61€/kg, which is above market price. Even though the results look promising, further experimental and scale up studies are required for validation.

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Comparative study of conventional, reactive-distillation and pervaporation integrated hybrid process for ethyl tert-butyl ether production

Abstract: Comparative study of conventional, reactive-distillation and pervaporation integrated hybrid process for ethyl tert-butyl ether production, Chemical Engineering and

Cited by 33 publications

References 39 publications

Alcohol and Alkane Organic Extraction Using Pervaporation Process

Alcohol and Alkane Organic Extraction Using Pervaporation Process

Analysis of a hybrid distillation‐pervaporation column in a single unit: Intermediate membrane section in the rectifying and stripping section

Integrated Renewable Production of ETBE from Switchgrass

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