Mass transfer structured packings

S. Mass-transfer structured packing and static mixers. Liquid with or without fluidized particles. Electrochemical... 

Boston inside-out method. 172-177, 198 Bravo, et al. rfructured packing pressure drop, 447, 499, 500 Bravo Fair et al. mass transfer random packing, 528-530 structured packings, 474, 529, 531, 532 Brown-Martin method, 109 Bryoden method, 161, 162, 175, 176. 179... 

The macroporous structure of monoliths allows the overcoming of some of the disadvantages of conventional affinity chromatographyt . Monoliths have lower mass transfer resistance and pressure drop than conventional random packed beds, and mass transfer within monolith channel rates can be substantially larger than mass transfer in packed beds used in conventional chromatography. 

Figure 9-6MM. Nutter BHS structured packing with expanded metal texture, which maintains high mass transfer efficiency across all operating conditions. Nutter Engineering designs and manufactures BSH in North America under exclusive license from Julius Montz GmbH of Germany. Used by permission of Nutter Engineering, Harsco Corp.

Structured packings maintain mass-transfer performance with minimum penalty for pressure drop [108]. Two models are presented for calculating pressure drop (1) Bravo-Rocha-Fair [111] and (2) Stichlmair-Bravo-Fair [112]. Each method is qmte involved with rather complex equations to calculate the factor to ultimately calculate a pressure drop. The authors [108] recommend for design using... 

The three principal catalyst bed configurations are the pellet bed, the monolith, and the metallic wire meshes. An open structure with large openings is needed to fulfill the requirement of a low pressure drop even at the very high space velocities of 200,000 hr-1. On the other hand, packings with small diameters would provide more external surface area to fulfill the requirement for rapid mass transfer from the g .s stream to the solid surface. The compromise between these two ideals results in a rather narrow range of dimensions pellets are from to 1 in. in diameter, monoliths have 6 to 20 channels/in., and metallic meshes have diameters of about 0.004 to 0.03 in. 

Experimental results for fixed packed beds are very sensitive to the structure of the bed which may be strongly influenced by its method of formation. GUPTA and Thodos157 have studied both heat transfer and mass transfer in fixed beds and have shown that the results for both processes may be correlated by similar equations based on. / -factors (see Section 10.8.1). Re-arrangement of the terms in the mass transfer equation, permits the results for the Sherwood number (Sh1) to be expressed as a function of the Reynolds (Re,) and Schmidt numbers (Sc) ... 

This is the first reactor reported where the aim was to form micro-channel-like conduits not by employing microfabrication, but rather using the void space of structured packing from smart, precise-sized conventional materials such as filaments (Figure 3.25). In this way, a structured catalytic packing was made from filaments of 3-10 pm size [8]. The inner diameter of the void space between such filaments lies in the range of typical micro channels, so ensuring laminar flow, a narrow residence time distribution and efficient mass transfer. 

The large porous particles are the oldest of these materials, and are no longer used in analytical hplc, although because of their high sample capacity they are still useful in preparative work. Columns packed with the large particles have relatively low efficiencies because of the long time it takes for solute species to diffuse into and out of the porous structure (slow mass transfer). 

Dispersion in packed tubes with wall effects was part of the CFD study by Magnico (2003), for N — 5.96 and N — 7.8, so the author was able to focus on mass transfer mechanisms near the tube wall. After establishing a steady-state flow, a Lagrangian approach was used in which particles were followed along the trajectories, with molecular diffusion suppressed, to single out the connection between flow and radial mass transport. The results showed the ratio of longitudinal to transverse dispersion coefficients to be smaller than in the literature, which may have been connected to the wall effects. The flow structure near the wall was probed by the tracer technique, and it was observed that there was a boundary layer near the wall of width about Jp/4 (at Ret — 7) in which there was no radial velocity component, so that mass transfer across the layer... 

Completely solid packings produce no mass transfer effects related to solute movement into and out of tortuous pore structures. The principal limitation of solid packings is low total surface area and consequent limited sample capacity. Even with very small particles, the overall surface area generated per unit length of the column is still low compared to the porous materials with mean pore sizes in the 60 to 300 A range. Figures 13.5 A and B show a comparison of surface areas of... 

The necessity of forming zeolite powders into larger particles or other structures stems from a combination of pressure drop, reactor/adsorber design and mass transfer considerahons. For an adsorption or catalytic process to be productive, the molecules of interest need to diffuse to adsorption/catalytic sites as quickly as possible, while some trade-off may be necessary in cases of shape- or size-selective reactions. A schematic diagram of the principal resistances to mass transfer in a packed-bed zeolite adsorbent or catalyst system is shown in Figure 3.1 [69]. 

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