Optimization of multi-stage membrane systems for CO 2 capture from flue gas

Arias, Ana Marisa; Mussati, Miguel C.; Mores, Patricia Liliana; Scenna, Nicolás J.; Caballero, José A.; Mussati, Sergio F.

doi:10.1016/j.ijggc.2016.08.005

Cited by 86 publications

(44 citation statements)

References 57 publications

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“…The countercurrent flow hollow fiber membrane modeled in this work has been provided in Fig. (a), whereby major assumptions are as follows: Essentially no back mixing is assumed with ‘plugs’ of gas passing through the hollow fiber membrane . Therefore, hollow fiber membrane can be divided into predefined number of states, whereby mass balance can be performed independently. All hollow fibers within the membrane are similar .…”

Section: Methodsmentioning

confidence: 99%

“…Ideal behavior of gas mixture on both sides of the membrane attributed to low operating pressure close to ambient condition Isothermal operation within the hollow fiber membrane module due to negligible Joule Thomson temperature drop that has been contributed by low trans‐membrane pressure. Resistance of the porous supporting layer against the flow is negligible Deformation of the hollow fibers under pressure is negligible …”

Section: Methodsmentioning

confidence: 99%

“…Essentially no back mixing is assumed with 'plugs' of gas passing through the hollow fiber membrane. 11,21,27,63,[80][81][82][83][84][85][86][87] Therefore, hollow fiber membrane can be divided into predefined number of states, whereby mass balance can be performed independently. ii.…”

Section: Succession Of States For Separation Mechanism Of Hollow Fibementioning

confidence: 99%

“…These assumptions have been adapted since they are frequently used in hollow fiber membrane modeling, which persist till recent simulation works. [85][86][87]90,94,[96][97][98][99] As presented in Table 2, these assumptions merely limit the accuracy of simulation model at very high pressures and for asymmetric membranes with very high selectivity and permeances, which is not pertinent to the present scope of study. Therefore, a mathematical model based on these assumptions is still sufficiently accurate for design of membrane process in the present work.…”

Section: Succession Of States For Separation Mechanism Of Hollow Fibementioning

confidence: 99%

See 3 more Smart Citations

Process simulation and optimization of oxygen enriched combustion using thin polymeric membranes: effect of thickness and temperature dependent physical aging

Lock

Lau

Shariff

et al. 2019

J of Chemical Tech & Biotech

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BACKGROUND Limited work has been available to model thickness and temperature dependent physical aging encountered in polymeric membranes for gas separation to provide physically intuitive interpretation underlying the process. The Tait equation of states has been integrated within conventional dual mode mathematical model to characterize the physical aging mechanism, whereby the model requires merely temperature dependent parameters. Subsequently, the Tait‐dual mode mechanism model has been incorporated within a succession of states methodology that quantifies transport mechanism in a countercurrent hollow fiber membrane. Finally, the developed mathematical model has been implemented in Aspen HYSYS to constitute an oxygen enrichment plant. RESULTS The simulation model has been validated with experimental observation with an acceptable error of < 6.5%. The process simulation tool has been used to evaluate the separation performance of oxygen enrichment plant using polymeric membrane with consideration of operating temperature (35–55 °C) and thickness dependent (400–1000 nm) physical aging. It is found that the optimal membrane design that generates highest profitability with physical aging consideration is at film thickness of ∼400 nm and operating temperature of 55 °C. Under such operating condition, the deviation between ideal and non‐ideal simulation model is also the smallest at ∼6%, which implies that physical aging has the least impact to the operability of the plant. CONCLUSION The developed simulation model has the potential to be applied for complex membrane system design (multiple membranes or hybrid system), scale up and optimization study that is essentially required for industrial scale application. © 2019 Society of Chemical Industry

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Section: Methodsmentioning

confidence: 99%

Section: Methodsmentioning

confidence: 99%

Section: Succession Of States For Separation Mechanism Of Hollow Fibementioning

confidence: 99%

Section: Succession Of States For Separation Mechanism Of Hollow Fibementioning

confidence: 99%

See 2 more Smart Citations

Process simulation and optimization of oxygen enriched combustion using thin polymeric membranes: effect of thickness and temperature dependent physical aging

Lock

Lau

Shariff

et al. 2019

J of Chemical Tech & Biotech

View full text Add to dashboard Cite

show abstract

“…The number of trade-offs rises along with the number of stages. Therefore, a process-level analysis is highly suggested by several authors [19][20][21]. Thus, the application of the aforementioned process simulators and sequential methods to optimize multi-stage processes may be computationally expensive (time-consuming and large number of iterations) due to the presence of recycle streams [14].…”

Section: Introductionmentioning

confidence: 99%

Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes

Arias¹,

Scenna

et al. 2018

Processes

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This paper fits into the process system engineering field by addressing the optimization of a two-stage membrane system for H 2 separation in refinery processes. To this end, a nonlinear mathematical programming (NLP) model is developed to simultaneously optimize the size of each membrane stage (membrane area, heat transfer area, and installed power for compressors and vacuum pumps) and operating conditions (flow rates, pressures, temperatures, and compositions) to achieve desired target levels of H 2 product purity and H 2 recovery at a minimum total annual cost. Optimal configuration and process design are obtained from a model which embeds different operating modes and process configurations. For instance, the following candidate ways to create the driving force across the membrane are embedded: (a) compression of both feed and/or permeate streams, or (b) vacuum application in permeate streams, or (c) a combination of (a) and (b). In addition, the potential selection of an expansion turbine to recover energy from the retentate stream (energy recovery system) is also embedded. For a H 2 product purity of 0.90 and H 2 recovery of 90%, a minimum total annual cost of 1.764 M$·year −1 was obtained for treating 100 kmol·h −1 with 0.18, 0.16, 0.62, and 0.04 mole fraction of H 2 , CO, N 2 , CO 2 , respectively. The optimal solution selected a combination of compression and vacuum to create the driving force and removed the expansion turbine. Afterwards, this optimal solution was compared in terms of costs, process-unit sizes, and operating conditions to the following two sub-optimal solutions: (i) no vacuum in permeate stream is applied, and (ii) the expansion turbine is included into the process. The comparison showed that the latter (ii) has the highest total annual cost (TAC) value, which is around 7% higher than the former (i) and 24% higher than the found optimal solution. Finally, a sensitivity analysis to investigate the influence of the desired H 2 product purity and H 2 recovery is presented. Opposite cost-based trade-offs between total membrane area and total electric power were observed with the variations of these two model parameters. This paper contributes a valuable decision-support tool in the process system engineering field for designing, simulating, and optimizing membrane-based systems for H 2 separation in a particular industrial case; and the presented optimization results provide useful guidelines to assist in selecting the optimal configuration and operating mode.

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Energetic Optimization of the Three‐Stage Gas Permeation Process for the Upgrading of Biogas

Kube¹

2019

Chem Eng & Technol

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The mass balances of countercurrent gas permeation modules for the separation of multicomponent gas mixtures are formulated as a boundary value problem, using the ideal gas law and isobaric isothermal stages. The balances are extended for the common three‐stage gas permeation process for the upgrading of biogas. The solution is calculated with MATLAB's BVP4C boundary value solver. The process is optimized by means of the FMINCON SQP‐algorithm towards lowest power consumption. Parameter variations are conducted, highlighting the impact of product and lean‐gas quality setpoints, biogas composition, membrane surface and selectivity, permeate compression, and choice of compressor model on the energetic optimum.

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Optimization of multi-stage membrane systems for CO 2 capture from flue gas

Cited by 86 publications

References 57 publications

Process simulation and optimization of oxygen enriched combustion using thin polymeric membranes: effect of thickness and temperature dependent physical aging

Process simulation and optimization of oxygen enriched combustion using thin polymeric membranes: effect of thickness and temperature dependent physical aging

Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes

Energetic Optimization of the Three‐Stage Gas Permeation Process for the Upgrading of Biogas

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