Structured packing scale

Figure 9-21H. Updated generalized pressure-drop correlation rearranged version of earlier Eckert and Leva, using linear scale for the ordinate and use of capacity factor, Cg. Used by permission of Strigle, R. F., Jr., Packed Tower Design and Applications Random and Structured Packings, 2nd ed. Gulf Publishing Co. p. 21 (1994). Note G = gas, Ib/ft -hr, L = liquid, Ib/ft -hr.

This latter type appears similar to some previously discussed, closely spaced structural packing, but is specifically designed for this application. Beyers [148] recommends film fill as the best choice if the water conditions of Table 9-49 are appropriate. For scaling or plugging water conditions, select splash fill. 

Hufton, J. R, J. L. Bravo, andj. R. Fair, Scale-up of Laboratory Data for Distillation Columns Containing Corrugated Metal-type Structured Packing, Ind. and Eng. Chem. Res., American Chem. Soc., V. 27, No. 11 (1988) p. 2096. 

From the very beginning, continuous reactor concepts, an alternative to the truly microfabricated reactors, were used, for example, static meso-scaled mixers or HPLCs and other smart tubing (see Iwasaki et al. 2006 for an example). This completed functionality by filling niches not yet covered by microfabricated reactors or even by replacing the latter as a more robust, more easily accessed or more inexpensive processing tool. Further innovative equipment, coming from related developments in the process intensification field, is another source e.g., structured packings such as fleeces, foams, or monoliths. 

Use of HTU and K a Data In estimating the size of a commercial gas absorber or liquid stripper it is desirable to have data on the overall mass-transfer coefficients (or heights of transfer units) for the system of interest, and at the desired conditions of temperature, pressure, solute concentration, and fluid velocities. Such data should best be obtained in an apparatus of pilot-plant or semiworks size to avoid the abnormalities of scale-up. Within the packing category, there are both random and ordered (structured) packing elements. Physical characteristics of these devices will be described later. 

The potential of structured packings as catalyst carriers for reactive stripping, film-flow-monoliths, Sulzer DX -packings, both coated with zeolite BEA, and katapak-S , filled with BEA-particles, was explored in cold-flow experiments and under reactive stripping conditions in a pilot-scale plant. 

The separation operation called distillation utilizes vapor and liquid phases at essentially the same temperature and pressure for the coexisting zones. Various kinds of devices such as random or structured packings and plates or trays are used to bring the two phases into intimate contact. Trays are stacked one above the other and enclosed in a cylindrical shell to form a column. Packings are also generally contained in a cylindrical shell between hold-down and support plates. The column may be operated continuously or in batch mode depending on a number of factors such as scale and flexibility of operations and solids content of feed. A typical tray-type continuous distillation column plus major external accessories is shown schematically in Fig. 13-1. 

Parkinson and Ondrey report that structured packing is becoming more frequently used in air separations. They also report that structured packings are being favored because they have a higher capacity than dumped packing, and the scale up is more predicable. 

Simulations of an industrial scale column with structured packing have been reported by Taylor et al. (1992). They modeled a packed C4 splitter that had an internal diameter of about 2.5 m and five beds of structured packing with a total height of approximately 37 m as shown in Figure 14.33. The feed, which contains predominantly isobutane and n-butane... 

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