Design of multivariable control structure for crude oil distillation column: effect of capacity change

Document Type : Research paper

Abstract

This paper presents control structure design and dynamic modeling of atmospheric distillation column using relative gain array (RGA) and relative normalized gain array (RNGA). Nonsquare control structure selection for atmospheric distillation has not been addressed in the literature. The column has been modeled and simulated for 40,000 and 60,000 bbl/day capacities in order to examine the control performance of the column. Output performances of control structure were examined by ±5% step change in feed rate. Based on the results, the output responses for both RGA and RNGA methods show good control performance for 60,000 bbl/day capacity, while the output responses for 4,000 bbl/day capacity suggest change in control structure for both methods.

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References

[1] A. A. Kiss, (2014) "Distillation technology–still young and full of breakthrough opportunities", Journal of Chemical Technology and Biotechnology, 89, 479-498.
 
[2] V. Kariwala, S. Skogestad and J. F. Forbes, (2006) "Relative gain array for norm-bounded uncertain systems", Industrial &Engineering Chemistry Research, 45, 1751-1757.
 
[3] S. Motlaghi, F. Jalali and M. N. Ahmadabadi, (2008) "An expert system design for a crude oil distillation column with the neural networks model and the process optimization using genetic algorithm framework", Expert Systems with Applications, 35, 1540-1545.
 
[4] D. Jones, D. Bhattacharyya, R. Turton and S. E. Zitney, (2014) "Plant-wide control system design: Primary controlled variable selection", Computers & Chemical Engineering, 71, 220-234.
 
[5] A. Khaki-Sedigh and B. Moaveni, 2009 Control Configuration Selection for Multivariable Plants, Springer, Heidelberg.
 
[6] S. Skogestad, P. Lundström and E. W. Jacobsen, (1990) "Selecting the best distillation control configuration", AIChE Journal, 36, 753-764.
 
[7] E. Bristol, (1966) "On a new measure of interaction for multivariable process control", IEEE Transactions on Automatic Control, 11, 133-134.
 
[8] N. Chatrattanawet, S. Skogestad and A. Arpornwichanop, (2015) "Control structure design and dynamic modelling for a solid oxide fuel cell with direct internal reforming of methane", Chemical Engineering Research and Design, 98, 202-211.
 
[9] A. Mahabuba and M. A. Khan, (2008) "Optimal Location of Power System Stabilizers in a Multimachine Power System Using Relative Gain Array (RGA) and Genetic Algorithm", International Journal of Electrical and Power Engineering, 2, 19-27.
 
[10] F. Osuolale and J. Zhang, (2015) "Distillation Control Structure Selection for Energy‐Efficient Operations", Chemical Engineering & Technology, 38, 907-916.
 
[11] S. Hurowitz, J. Anderson, M. Duvall and J. B. Riggs, (2003) "Distillation control configuration selection", Journal of Process Control, 13, 357-362.
 
[12] V. C. Machado, D. Gabriel, J. Lafuente and J. A. Baeza, (2009) "Cost and effluent quality controllers design based on the relative gain array for a nutrient removal WWTP", Water Research, 43, 5129-5141.
 
[13] C. Bo, R. Zhang, C. Zhang, J. Tang, X. Qiao and F. Gao, (2014) "Comparison of Two Types of Control Structures for Benzene Chlorine Reactive Distillation Systems", Chinese Journal of Chemical Engineering, 22, 837-841.
 
[14] T. Mc Avoy, Y. Arkun, R. Chen, D. Robinson and P. D. Schnelle, (2003) "A new approach to defining a dynamic relative gain", Control Engineering Practice, 11, 907-914.
 
[15] Q. Xiong, W.-J. Cai and M.-J. He, (2005) "A practical loop pairing criterion for multivariable processes", Journal of Process Control, 15, 741-747.
 
[16] M.-J. He, W.-J. Cai, W. Ni and L.-H. Xie, (2009) "RNGA based control system configuration for multivariable processes", Journal of Process Control, 19, 1036-1042.
 
[17] J. F. Mulia-Soto and A. Flores-Tlacuahuac, (2011) "Modeling, simulation and control of an internally heat integrated pressure-swing distillation process for bioethanol separation", Computers & Chemical Engineering, 35, 1532-1546.
 
[18] C. D. Holland, 1981 Fundamentals of Multicomponent Distillation, McGraw-Hill, New York.
 
[19] L. Vanhorn, (1980) "Crude unit computer control... how good is it", Hydrocarbon Processing, 60, 145-148.
 [20] A. W. Drews, 1998 Manual on hydrocarbon analysis, ASTM International
 
[21] D. J. Dave, M. Z. Dabhiya, S. Satyadev, S. Ganguly and D. N. Saraf, (2003) "Online tuning of a steady state crude distillation unit model for real time applications", Journal of Process Control, 13, 267-282.
 
[22] V. Kumar, A. Sharma, I. R. Chowdhury, S. Ganguly and D. N. Saraf, (2001) "A crude distillation unit model suitable for online applications", Fuel Processing Technology, 73, 1-21.
 
[23] M. Van De Wal and B. De Jager, (2001) "A review of methods for input/output selection", Automatica, 37, 487-510.
 
[24] B. D. Tyreus and W. L. Luyben, (1992) "Tuning PI controllers for integrator/dead time processes", Industrial &Engineering Chemistry Research, 31, 2625-2628.
 
[25] W. L. Luyben, 2013 Distillation Design and Control Using Aspen Simulation, John Wiley & Sons, New Jersey, USA.
Journal of Separation Science and Engineering
Volume 8, Issue 2
January 0
Pages 1-12

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