Process design computers

Ng, K. M. (2004) MOPSD a framework linking business decision-making to product and process design, Computers and Chemical Engineering, 29, 51. 

In practical combustion systems, such as CO boilers, the flue gas experiences spatial and temporal variations. Constituent concentration, streamline residence time, and temperature are critical to determining an efficient process design. Computational fluid dynamics (CFD) modeling and chemical kinetic modeling are used to achieve accurate design assessments and NO, reduction predictions based on these parameters. The critical parameters affecting SNCR and eSNCR design are listed in Table 17.4. 

Chemical Process Design Computer-Aided Case Studies. Alexandre C. Dimian and Costin Sorin Bildea Copyright 2008 WILEY-VCH Verlag GmbH Co. KGaA, Weinheim ISBN 978-3-527-31403-4... 

Chemical Process Design Computer-Aided Case Studies. Alexandre C. Dimian and Costin Sorin Bildea... 

Umeda, T. and Kuriyama, T. (1980). Interactive solution to multiple criteria problems in chemical process design, Computers Chemical Engineering 4, pp. 157-165. 

Adjiman C.S., Androulakis I.P., Maranas C.D. and Floudas C.A. 1996. A global optimization method, aBB, for process design, Comput. Chem. Eng., 20(Suppl.), S419-S424. 

Ryoo H.S. and Sahinidis N.V. 1995. Global optimization of nonconvex NLPs and MINLPs with applications in process design, Comput. Chem. Eng., 19(5), 551-566. 

Wayburn T.L. and Seader J.D. (1987). Homotopy continuation methods for computer-aided process design. Computers and Chemical Engineering 11 (1), 7-25. 7.2.3... 

Ouattara A, Pibouleau L, Azzaro-Pantel C, Domenecha S, Baudetb P, Yaoc B. Economic and environmental strategies for process design. Comput Chem Eng 2012 36 174-88. 

Mizsey, P. and Fonyo, Z., 1991 Assessing plant operability during process design. Computer-Oriented Process Engineering, Elsevier, 411-416. 

Most distillation and equilibrium parts of process-design computer programs (e.g.. Aspen, ChemCad, ProMax) report A, values for each species in the VLE data for mixtures, and some distillation programs report a. It must be clear from their definitions that they are made up from values of the y, and Xi. The computer programs mostly first compute the y and Xi, by the methods shown in the rest of this chapter and the next, and then compute and report the A, and a values for the convenience of users who prefer that formulation the, x, and y are the basic values. The common hand-calculation methods of estimating VLE are presented in terms of the A values in Section 8.9. 

If we must perform an 5 or V specified flash, the procedure is the same as for an adiabatic (H specified) flash. We guess a final T and P, solve for V/F and then the mol fractions, and compare the computed 5 or V with the specification. If the specification is not met, we adjust the guessed T and P and repeat the calculation until agreement is reached. This is seldom done by hand, but is offered as an option in some process-design computer programs. 

The most widely used method of this type is that of Chao and Seader [7]. This estimation method (and several variants of it proposed by other authors, particularly Grayson and Streed [8]) is offered as a calculation method in many current process-design computer packages and is widely recommended as being very good with hydrocarbon systems at high pressure (like Figure 10.1). 

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