Effect of feed temperature on economics and controllability of pressure-swing distillation for separating binary azeotrope

Cao, Yujuan; Li, Min; Wang, Yong; Zhao, Tingran; Li, Xin; Zhu, Zhaoyou; Wang, Yinglong

doi:10.1016/j.cep.2016.10.011

Cited by 38 publications

(23 citation statements)

References 32 publications

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“…The operating pressure indeed affects the composition of the azeotrope, allowing a straightforward separation [8,9,13,[18][19][20]. For instance, pressure swing has been compared by Cao et al as for costs and control options, also adopting a variable diameter column [21] and different feed temperature [22], for the following azeotropic mixtures: acetone-chloroform, acetone-methanol, methanol-chloroform, benzene-cyclohexane and isopropyl alcohol-diisopropyl ether. A simulated annealing algorithm was used to optimize the operating pressure minimizing the total annual costs (TAC) in the case of the pressure swing separation of the acetone-methanol system [23].…”

Section: -Pressure Swing Feasibility Checkmentioning

confidence: 99%

“…A simulated annealing algorithm was used to optimize the operating pressure minimizing the total annual costs (TAC) in the case of the pressure swing separation of the acetone-methanol system [23]. The attention was often focused on the control options of pressure swing systems [9,12,14,21,22,[24][25][26], but only in some cases this strategy was adopted for the resolution of the acetonitrile/water system [9,11,13], and never as part of a fully integrated purification train as in the present case.…”

Section: -Pressure Swing Feasibility Checkmentioning

confidence: 99%

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Alternative integrated distillation strategies for the purification of acetonitrile from ethanol ammoxidation

Tripodi

Manzini

Compagnoni

et al. 2018

Journal of Industrial and Engineering Chemistry

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Acetonitrile is increasingly used as solvent for the fine chemicals and pharmaceutical industries. Ethanol ammoxidation has been proposed as an alternative way for its production starting from a renewable source. This process leads to a complex mixture of products, which needs an optimized separation train to maximize the recovery and purity of acetonitrile. Pressure swing distillation, operated at 7 and 10 bar, has been compared as for feasibility and economic impact with the extractive distillation using dichloromethane as entrainer. The pressure swing option led to higher CH3CN recovery (95.5%) with respect to extractive distillation (92.1%), irrespectively from the operating pressure. Furthermore, the pressure swing option allowed to tune more easily product purity by adding or removing trays in the stripping section of the high pressure column, leaving water as the only impurity. Similar results were obtained when operating the pressure swing between 1 and 7 bar or 1 and 10 bar, but the operation at 10 bar was characterised by lower installation and operating costs, thus it was considered as optimal. The same economical evaluation was carried out for the

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Section: -Pressure Swing Feasibility Checkmentioning

confidence: 99%

Section: -Pressure Swing Feasibility Checkmentioning

confidence: 99%

Alternative integrated distillation strategies for the purification of acetonitrile from ethanol ammoxidation

Tripodi

Manzini

Compagnoni

et al. 2018

Journal of Industrial and Engineering Chemistry

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“…where J i is the permeate flux of component i, mol h −1 m −2 ; Q i denotes the membrane specific permeance of component i, mol atm −1 h −1 m −2 ; Δp i is the driving force of pervaporation membrane of component i, atm; S w is a swelling coefficient for the polymeric membrane. Δp i and S w are expressed in Eqn (6) and Eqn (7), respectively.…”

Section: Mathematic Model Of Pv Modulementioning

confidence: 99%

“…Large amount of methyl acetate (MeAc) along with methanol (MeOH) are produced as byproducts in the polyvinyl alcohol (PVA) industry, which must be recovered and converted for more economic benefits and less environment impacts. 1 Currently, compared with direct methods of extractive distillation, [2][3][4] pressure-swing distillation, 5,6 and pervaporation (PV), 7-13 indirect methods such as hydrolysis [14][15][16][17][18] and transesterification [19][20][21][22][23][24][25][26] are gaining more popularity since MeAc is converted into a more economically valuable compound. Isopentyl acetate (iso-AmAc) is widely used as a flavor ester in the cosmetic and pharmaceutical industries.…”

Section: Introductionmentioning

confidence: 99%

Hybrid reactive distillation using polyoctylmethylsiloxane membrane for isopentyl acetate production from mixed PVA by products

Wang

Guang

et al. 2018

J of Chemical Tech & Biotech

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BACKGROUND The transesterification of methyl acetate and isoamyl alcohol catalyzed by ionic liquids is a new environment‐friendly method for isopentyl acetate (iso‐AmAc) production, and also appropriate for the recovery of polyvinyl alcohol (PVA) byproducts. Therefore, it is of great significance for iso‐AmAc production from PVA byproducts to explore alternative processes with the goal of improving the conversion of the chemical equilibrium reaction and energy efficiency, including reactive distillation (RD), dividing‐wall reactive distillation (RDWC) and pervaporation (PV)‐based hybrid reactive distillation. RESULT This article proposed four novel reactive hybrid processes with feedstock of mixed PVA byproducts and made a comparison with two conventional processes of RD and RDWC in terms of the minimum total annual cost (TAC) and CO2 emissions. The results revealed that the RDWC‐PV can give a 35.61% saving in TAC and a 40.27% reduction in CO2 emissions compared with the RD, and the other three RD‐PV hybrid processes have less CO2 emissions and equivalent TAC compared with the RDWC. CONCLUSION In summary, all hybrid processes proposed were more energy‐saving and economical than the conventional RD, especially the RDWC‐PV, due to synergistic advantages of various process intensification methods. © 2018 Society of Chemical Industry

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“…For the feed flow, the method to increase the liquid holdup in the feed plate through a middle vessel has been proposed [4]. The choice of the feed temperature should be considered from the perspectives of both the total annual cost and the dynamic control performance [5].…”

Section: Introductionmentioning

confidence: 99%

Development of the Feed Part Control System for Rectification Process

Dai¹,

An²

2019

JRNAL

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This paper completes the structure design of the feed process for the small rectification experimental unit. According to the process requirements, the overall scheme of the detection and control system and the main parameters are designed, and the type of the instrument is selected. The system hardware design is based on the CPU222 of Siemens s7-200 PLC (Programmable Logic Controller) and the corresponding input/output module. The lower computer adopts STEP 7-Micro/WIN programming software, and it completes the program design of parameter acquisition, scale transformation and PID (Proportion Integration Differentiation) operation through ladder diagram. The monitoring interface of the upper computer adopts Kingview monitoring software.

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Effect of feed temperature on economics and controllability of pressure-swing distillation for separating binary azeotrope

Cited by 38 publications

References 32 publications

Alternative integrated distillation strategies for the purification of acetonitrile from ethanol ammoxidation

Alternative integrated distillation strategies for the purification of acetonitrile from ethanol ammoxidation

Hybrid reactive distillation using polyoctylmethylsiloxane membrane for isopentyl acetate production from mixed PVA by products

Development of the Feed Part Control System for Rectification Process

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