Improved ODE integrator and mass transfer approach for simulating a cyclic adsorption process

Todd, Richard S.; Ferraris, G. Buzzi; Manca, Davide; Webley, Paul A.

doi:10.1016/s0098-1354(03)00003-6

Cited by 19 publications

(10 citation statements)

References 48 publications

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“…For this reason there is a need for a reliable, validated numerical model to evaluate and estimate the performance of various PSA cycle designs, adsorbent materials, and process conditions of temperature and pressure on plant performance, as measured by parameters such as product purity, recovery and power consumption. Our numerical model (MINSA) was built on the basis of mass and energy balances using a variety of adsorption isotherm models, kinetic models and heat transfer models as described earlier He 2000 andTodd et al 2003). The kinetic model contains a discrete pellet version implementing the Dusty Gas Model to describe mass transfer within porous materials.…”

Section: Introductionmentioning

confidence: 99%

Capture of CO2 from flue gas streams with zeolite 13X by vacuum-pressure swing adsorption

et al. 2008

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Vacuum swing adsorption (VSA) capture of CO 2 from flue gas streams is a promising technology for greenhouse gas mitigation. In this study we use a detailed, validated numerical model of the CO2VSA process to study the effect of a range of operating and design parameters on the system performance. The adsorbent used is 13X and a feed stream of 12% CO 2 and dry air is used to mimic flue gas. Feed pressures of 1.2 bar are used to minimize flue gas compression. A 9-step cycle with two equalisations and a 12-step cycle including product purge were both used to understand the impact of several cycle changes on performance. The ultimate vacuum level used is one of the most important parameters in dictating CO 2 purity, recovery and power consumption. For vacuum levels of 4 kPa and lower, CO 2 purities of >90% are achievable with a recovery of greater than 70%. Both purity and recovery drop quickly as the vacuum level is raised to 10 kPa. Total power consumption decreases as the vacuum pressure is raised, as expected, but the recovery decreases even quicker leading to a net increase in the specific power. The specific power appears to minimize at a vacuum pressure of approximately 4 kPa for the operating conditions used in our study. In addition to the ultimate vacuum level, vacuum time and feed time are found to impact the results for differing reasons. Longer evacuation times (to the same pressure level) imply lower flow rates and less pressure drop providing improved performance. Longer feed times led to partial breakthrough of the CO 2 front and reduced recovery but improved purity. The starting pressure of evacuation (which is not necessarily equal to the feed pressure) was also found to be important since the gas phase was enriched in CO 2 prior to removal by vacuum leading to improved CO 2 purity. A 12-step cycle including product purge was able to produce high purity CO 2 (>95%) with minimal impact on recovery. Finally, it was found that for 13X, the optimal feed temperature was around 67°C to maximize system purity. This is a consequence of the temperature dependence of the working selectivity and working capacity of 13X. In summary, our numerical model indicates that there is considerable scope for improvement and use of the VSA process for CO 2 capture from flue gas streams.

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Section: Introductionmentioning

confidence: 99%

Capture of CO2 from flue gas streams with zeolite 13X by vacuum-pressure swing adsorption

et al. 2008

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“…To predict the performance of the different investigated adsorbents in a pressure swing adsorption unit, the numerical adsorption simulator MINSA developed by Webley, He and Todd was used. 46,47 The equations for the conservation of mass and energy were reported by Todd et al 47 Mass transfer from the gas to the adsorbed phase is described via the so-called Partial pressure form of the LDF model, 47 where the LDF coefficients obtained from the breakthrough simulations (vide supra) are used as input parameters. Pressure drop calculations are performed via the Ergun equation (eqn (9)).…”

Section: Adsorption At Industrial Scale (Psa Modeling With Minsa)mentioning

confidence: 99%

Biogas upgrading through kinetic separation of carbon dioxide and methane over Rb- and Cs-ZK-5 zeolites

et al. 2014

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“…The adsorption process simulator that has been developed and verified in our research group uses conservation of mass and energy for the interpellet gas phase with discretised pellet models (DPMs) to represent the intrapellet region (Webley and He, 2000;Todd et al, 2003).…”

Section: Simulation and Intrapellet Flux Equationsmentioning

confidence: 99%

Macropore diffusion dusty-gas coefficient for pelletised zeolites from breakthrough experiments in the O2/N2 system

Todd

Webley

2005

Chemical Engineering Science

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Improved ODE integrator and mass transfer approach for simulating a cyclic adsorption process

Cited by 19 publications

References 48 publications

Capture of CO2 from flue gas streams with zeolite 13X by vacuum-pressure swing adsorption

Capture of CO2 from flue gas streams with zeolite 13X by vacuum-pressure swing adsorption

Biogas upgrading through kinetic separation of carbon dioxide and methane over Rb- and Cs-ZK-5 zeolites

Macropore diffusion dusty-gas coefficient for pelletised zeolites from breakthrough experiments in the O2/N2 system

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