Thermodynamic tuning in separation process simulation and design

Urlic, L.E.; Bottini, Susana B.; Brignole, Esteban A.; Romagnoli, José A.

doi:10.1016/0098-1354(91)85026-q

Cited by 10 publications

(7 citation statements)

References 11 publications

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“…A plot of the K-value AAD % against k ij indicates an optimum k ij value of about 0.0157 for the SRK data model when default R formulations are used. The value of 0.0152 quoted by Urlic et al 6 is consistent with a value of 0.0153 obtained by Kamphausen, 12 if the original acentric factor formulation of Soave 19 is used for the R term. These values for k ij are in contrast to the PRO/II default value of 0.0112 and a value of 0.0178 obtained from REGRESS in automatic regression mode.…”

Section: K-value Data-model Tuning Resultssupporting

confidence: 85%

“…Therefore, the dominant thermodynamic separation variable in the deethyleniser column as a whole is the relative volatility between the key components ethylene and ethane. This is in agreement with the conclusion reached by Urlic et al in their sensitivity analysis of distillation processes as applied to the modeling of a splitter.…”

Section: Thermodynamic Data Modelssupporting

confidence: 92%

“…There is also a low relative volatility between the key components. These criteria, according to Urlic et al, 6 identify the deethyleniser as a process critical separation unit that requires fine-tuning of the simulation model fitting parameters.…”

Section: Parametrization Strategymentioning

confidence: 99%

“…The process of tuning appropriate equation of state (EOS) data models and using these EOSs in simulation studies in both their tuned and untuned form, together with classic quadratic mixing rules, has received considerable attention. Studies by Hernandez et al on industrial superfractionators and Urlic et al on the fractionation train of an industrial ethylene plant are among the most relevant to this investigation.…”

Section: Introductionmentioning

confidence: 99%

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Plant−Model Mismatch Analysis in Deethyleniser Simulation. 2. Application to Data-Model Selection and Tuning

Kamphausen

O'Donnell

2004

Ind. Eng. Chem. Res.

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The focus of this investigation into difficulties associated with the simulation of a commercial deethyleniser is on the use of K-value data models based on equations of state as provided in PRO/II (Simulation Sciences, Inc.). For various K-value data-model definitions, the value of the temperature-independent form of the binary interaction coefficient, k ij = α ij , of the dominant ethylene/ethane binary has been varied. All other thermodynamic data-model definitions were kept the same. The values of the optimized average equilibrium tray efficiency parameter, , can vary markedly with the choice of the K-value data model and the k ij values used and ranged from about 0.84 to about 1.01. The associated minimum total error objective function values are, however, remarkably similar, leading to the concept of “Equivalent” simulation models. For all three equation of state K-value data models examined, a quadratic relation was found to exist between a defined k ij and the corresponding optimized average equilibrium tray efficiency.

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Section: K-value Data-model Tuning Resultssupporting

confidence: 85%

Section: Thermodynamic Data Modelssupporting

confidence: 92%

Section: Parametrization Strategymentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

See 2 more Smart Citations

Plant−Model Mismatch Analysis in Deethyleniser Simulation. 2. Application to Data-Model Selection and Tuning

Kamphausen

O'Donnell

2004

Ind. Eng. Chem. Res.

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“…Urlic et al [55] recommended the use of the SRK equation of state with a binary interaction parameter (BIP) of 0.0152. Using this value, the tray efficiency as assessed by UOP can be reproduced ( Figure 5.7).…”

Section: Ethylene-ethane Splittermentioning

confidence: 99%