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Distillation design and operation

One of the challenging aspects of distillation column control is the many limitations imposed on the operation of the column. There are hydraulic constraints, separation constraints, heat-transfer constraints, pressure constraints, and temperature constraints. We recommend the excellent books by Kister (1992 and 1990) on distillation design and operation. [Pg.199]

I. M. Mujtaba, 2004, Batch Distillation Design and Operation, Imperial College Press, London. I.M. Mujtaba and S. Macchietto, 1993, Optimal operation of multicomponent batch distillation-... [Pg.258]

I.M. Mutjaba, Batch Distillation Design and Operation, World Scientific Publ Co, 2004. ISBN 9781860944376. [Pg.52]

Matab, I. M., Batch Distillation. Design and Operation, Imperial College Press, London, 2004. [Pg.371]

Distillation columns can be used to separate chemical components when there are differences in the concentrations of these components in the liquid and vapor phases. These concentration differences are analyzed and quantified using basic thermodynamic principles covering phase equilibrium. Vapor-liquid equilibrium (VLE) data and analysis are vital components of distillation design and operation. [Pg.30]

The point efficiency is an essential information in distillation design and operation. The tray efficiency can be calculated by the CMT models presented in this chapter it shows that the tray efficiency is in connection with the tray structure, flow pattern, and operating conditions, and thus, it is only referred to a specific distillation column under specific condition. On the other hand, the point efficiency, which depends on only the local condition of vapor-liquid contact and the physical properties of the system, is the better way to evaluate the feasibility of using distillation tray column for the separation. [Pg.111]

Design and Operation of Azeotropie Distillation Columns Simulation and design of azeotropic distiUation columns is a difficult computational problem, but one tnat is readily handled, in most cases, by widely available commercial computer process simulation packages [Glasscock and Hale, Chem. Eng., 101(11), 82 (1994)]. Most simida-... [Pg.1313]

Precondensers are recommended for any ejector system when the pressure conditions and coolant temperature will allow condensation of vapors, thus reducing the required design and operating load on the ejectors. This is usually the situation when operating a distillation column under vacuum. The overhead vapors are condensed in a unit designed to operate at top column pressure, with only the non-condensables and vapors remaining after condensation passing to the ejector system. [Pg.346]

This chapter contains examples of optimization techniques applied to the design and operation of two of the most common staged and continuous processes, namely, distillation and extraction. We also illustrate the use of parameter estimation for fitting a function to thermodynamic data. [Pg.443]

EXAMPLE 12.1 OPTIMAL DESIGN AND OPERATION OF A CONVENTIONAL STAGED-DISTILLATION COLUMN... [Pg.443]

Example 12.1 Optimal Design and Operation of a Conventional Staged-Distillation Column... [Pg.659]

Logsdon, J. S., Diwekar, U. M., and Biegler, L. T., On jhe simultaneous optimal design and operation of batch distillation columns, Trans. IChE 68A, 1134 (1990). [Pg.255]

Many azeotropic combinations exist among hydrocarbons themselves. Aromatic hydrocarbons, for example, are almost always found in petroleum fractions distilling below the true boiling point of the aromatics. Marschner and Cropper (41) accurately delineated the limits of azeotropy for benzene and toluene with saturated hydrocarbons, and Denyer et al. (11) did the same for the thiols. Consideration of such data is desirable in the design and operation of equipment for the distillation of gasoline fractions to produce specialized products. [Pg.207]

The literature on extractive distillation is rather sparse. In addition to that on the design and operation of the commercial units, the bench scale work of Griswold and coworkers (21) at the University of Texas and that of Dicks and Carlson (12) at the University of Pennsylvania are noteworthy. Pertinent thermodynamic data on extractive distillation systems have been presented by Wohl (59), and Colburn and coworkers (20, 43) have published vapor-liquid equilibria for several systems. Scheibel (48) has presented an approximate method for design of extractive distillation units. [Pg.208]

The qualities of the styrene product and toluene by-product depend primarily on three factors the impurities in the ethylbenzene feed-stock, the catalyst used, and the design and operation of the dehydrogenation and distillation units. Other than benzene and toluene, the presence of which is usually inconsequential, possible impurities in ethylbenzene are Cj-Cm nonaromatics and C Cm aromatics. The condensed reactor effluent is separated in the settling drum into vent gas (mostly hydrogen), process water, and organic phase. The organic phase with polymerization inhibitor added is pumped to file distillation train. [Pg.1555]

Design and Operating Principles in Solar Distillation Basins... [Pg.159]

Fixed-bed catalytic reactors and reactive distillation columns are widely used in many industrial processes. Recently, structured packing (e.g., monoliths, katapak, mella-pak etc.) has been suggested for various chemical processes [1-4,14].One of the major challenges in the design and operation of reactors with structured packing is the prevention of liquid flow maldistribution, which could cause portions of the bed to be incompletely wetted. Such maldistribution, when it occurs, causes severe under-performance of reactors or catalytic distillation columns. It also can lead to hot spot formation, reactor runaway in exothermic reactions, decreased selectivity to desired products, in addition to the general underutilization of the catalyst bed. [Pg.59]

Describing the behavior of undefined mixtures, whether from natural or synthetic sources, often begins with the separation of these complex systems into effective pseudocomponents by distillation (1 ). Each pseudocomponent is then characterized as if it were a pure compound, and its characterization data are used in appropriate correlations. The presence of nonvolatile residuum poses a serious limitation to such methodology. For coal-derived liquids, heavy crude oils, tar sands, and shale oil, more than 50 percent of the fluid may not be distillable (JL). Since this nonvolatile residue cannot be separated using conventional techniques, new methods of separation and characterization must be developed to provide the necessary information for design and operation of plants utilizing the fossil fuels mentioned above (2). [Pg.229]

Distillation is the most mature separation method in industry and its design and operation procedures are well established. Only when vapour-liquid equilibrium or other data are uncertain, are laboratory and/or pilot plant studies necessary prior to the design of a commercial unit. [Pg.156]

Stichlmair and Fair11 and Rose8 are textbooks devoted entirely to design and operation of distillation columns, Ruthven12 considers absorption and Astarita et alP absorption with chemical reaction. Ho14 is a handbook for membrane separations and Guiochon15 considers chromatographic separations. [Pg.169]

Since the reactor feed may contain inert species (e.g., nitrogen and solvents) and since there may be unconverted feed and by-products in the reactor effluent, a number of unit operations (distillation, filtration, etc.) may be required to produce the desired product(s). In practice, the flow of mass and energy through the process is captured by a process flow sheet. The flow sheet may require recycle (of unconverted feed, solvents, etc.) and purging that may affect reaction chemistry. Reactor design and operation influence the process and vice versa. [Pg.4]

Low, K.H., Optimal Configuration, Design and Operation of Batch Distillation Processes, PhD Thesis, (University of London, 2003). [Pg.10]

For single separation duty, Al-Tuwaim and Luyben (1991) proposed a shortcut method to design and operate multicomponent batch distillation columns. Their method, however, required a great number of simulations, which must be computationally very expensive, before they could arrive at an optimum design and find an optimum reflux ratio. Further details are in Chapter 7. [Pg.154]

Bemot, C., Doherty, M.F. and Malone, M.F., Design and operating policies for multicomponent batch distillation. AIChE Annual Meeting, Los Angeles, USA (1991). [Pg.191]


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