Alternative extractive distillation system for CO2–ethane azeotrope separation in enhanced oil recovery processes

Ebrahimzadeh, Edris; Matagi, Jacob; Fazlollahi, Farhad; Baxter, Larry

doi:10.1016/j.applthermaleng.2015.11.082

Cited by 40 publications

(28 citation statements)

References 36 publications

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“…Apart from the entrainer selection, and whatever the solving methods or the continuous or batch operating mode, the following variables should be optimized for extractive distillation. These are the numbers of trays of columns, feed locations, reflux ratios (boilup ratio), distillate flow rates (bottom flow rates) and entrainer flow rate (Mujtaba, 1999;Milani, 1999;Munoz et al, 2006;Arifin and Chien 2008;Kossack et al, 2008;Lek-Utaiwan et al, 2011;García-Herreros et al, 2011;Wang et al, 2012;Li and Bai 2012;Duc Long and Lee 2013;Luo et al, 2014;Han et al, 2015;Shen et al, 2015a;Brito et al, 2016;Ebrahimzadeh et al, 2016;Aniya et al, 2016;Zhao et al, 2017b;Li et al, 2017 and others).…”

Section: Solving Strategiesmentioning

confidence: 99%

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

Gerbaud

Rodríguez-Donis

Hégely

et al. 2019

Chemical Engineering Research and Design

190

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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: Solving Strategiesmentioning

confidence: 99%

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

Gerbaud

Rodríguez-Donis

Hégely

et al. 2019

Chemical Engineering Research and Design

190

View full text Add to dashboard Cite

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“…The equipment and utilities investments were calculated using the formulas provided by Luyben . In this paper, TAC is calculated as:

italicTAC = \frac{italiccaptical \cos t}{italiclife italicof italicthe plant} + italicoperating \cos t

where a plant life of 30 years is considered based on the report of Ebrahimzadeh et al . The Aspen Process Economic Analyzer provides relative costs by taking into account capital and operating costs together with technical and process parameters.…”

Section: Process Evaluationmentioning

confidence: 99%

“…where a plant life of 30 years is considered based on the report of Ebrahimzadeh et al 5 The Aspen Process Economic Analyzer provides relative costs by taking into account capital and operating costs together with technical and process parameters. Table 6 shows the TAC of the ionic liquid extractive distillation process.…”

Section: Total Annual Costmentioning

confidence: 99%

“…Luyben 4 first reported the separation of CO 2 and C 2 H 6 in enhanced oil recovery processes using extractive distillation with hydrocarbons as the solvent. Ebrahimzadeh et al 5 proposed a useful, less expensive alternative extractive distillation process for CO 2 -C 2 H 6 separation. Lastari et al 6 demonstrated extractive distillation for the separation of the CO 2 -ethane azeotrope using hydrocarbon solvents.…”

Section: Introductionmentioning

confidence: 99%

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Process design of carbon dioxide and ethane separation using ionic liquid by extractive distillation

Zhu

Geng

et al. 2017

J of Chemical Tech & Biotech

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BACKGROUND Carbon dioxide and ethane easily form a binary azeotrope under liquefied conditions. An extractive distillation process for the separation of carbon dioxide and ethane using the ionic liquids [bmim][Tf2N], [emim][Tf2N] and [emim][EtSO4] as solvents was explored. The thermodynamic and physical property parameters of each ionic liquid and their thermo‐physical properties that correlated with the experimental data were used to create the ionic liquid components and conduct the process simulation. RESULT Based on the analysis of its physical properties and relative volatilities, [emim][Tf2N] is the best option as a solvent for extractive distillation separation compared with other ionic liquids. Based on the sensitivity analysis optimization procedure, the minimum total annual cost, carbon dioxide emissions and thermodynamic efficiency were calculated. Compared with traditional extraction distillation, the total annual cost and carbon dioxide emissions of the process using [emim][Tf2N] as a solvent decreased by 62% and 31%, respectively. The thermodynamic efficiency (η) of the electricity generated from hydropower increase by 0.7%. CONCLUSION The results show that an ionic liquid extractive distillation process using an ionic liquid as the entrainer performs better than a process using traditional organic solvents in terms of economics. Due to the non‐volatility of ionic liquids, a flash tank was used instead of a solvent recovery column to efficiently realize solvent recovery. © 2017 Society of Chemical Industry

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“…In oxyfuel technologies, pure oxygen is used to combust the fuel [24,25]. Cryogenic technologies have also been considered for carbon dioxide removal, and they have several forms such as an inertial carbon extraction system, a thermal swing process, and cryogenic carbon capture with an external cooling loop (CCCECL) [26,27]. In this investigation, the latter category of cryogenic capture process is considered for removing CO 2 from the flue gas of power plants.…”

Section: Introductionmentioning

confidence: 99%

Dynamic optimization of a hybrid system of energy-storing cryogenic carbon capture and a baseline power generation unit

2016

Self Cite

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Recently promulgated regulations of the US Environmental Protection Agency (EPA) aggressively limit CO 2 emissions from the US power industry. Carbon capture and increased utilization of renewable energy sources are viable approaches to reduce CO 2 emissions from the power industry. Cryogenic carbon capture considered in this study is a post-combustion CO 2 removal system that separates CO 2 from the flue gas by desublimation. In this investigation, a hybrid system of cryogenic carbon capture and a baseline fossil-fueled power generation unit are optimized with a framework to mathematically represent this hybrid system. Optimization of this hybrid system results in meeting the electricity demand through a combination of coal, gas, and wind power sources with a priority given to wind power for utilization. A comparison of the cost associated with operating the steam turbine as a baseline or load-following unit is also made. A significant decrease in the cycling cost associated with load-following of the coal-fired power plant is observed when it operates as a baseline unit. The decrease in the cycling costs is 82% and 85%, respectively, for when wind power is utilized in meeting the electricity demand and when it is not. The saving in the cycling costs is attributed to the energy storage of cryogenic carbon capture.

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Alternative extractive distillation system for CO2–ethane azeotrope separation in enhanced oil recovery processes

Cited by 40 publications

References 36 publications

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

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

Process design of carbon dioxide and ethane separation using ionic liquid by extractive distillation

Dynamic optimization of a hybrid system of energy-storing cryogenic carbon capture and a baseline power generation unit

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