Liquid-vapor exchange

The latent heat transport accounts for only 2% of the total heat flux in this case. However, it was observed by several investigators that the total heat transfer rate is proportional to this value, <7, lenl, because it is proportional to the bubble volume and the number of bubbles that cause intense agitation of the liquid layer close to the surface. This agitation, termed microconvection, together with the liquid-vapor exchange, were considered to be the key to excellent characteristics of boiling heat transfer (Forster and Greif, 1959). 

Heat transfer by liquid-vapor exchange caused by bubble agitation of the boundary layer, q Bl. (microconvection)... 

Figure 5.15 Liquid-vapor exchange effect on CHF (circular tubes). (From Tong, 1975. Copyright 1975 by American Society of Mechanical Engineers, New York. Reprinted with permission.)...

The spacer grid in a rod bundle is also a turbulence promoter that enhances liquid-vapor exchange and bubble condensation. The local intensity of such turbulence is a function of the grid pressure loss coefficient, K, and the distance from the grid, t D. Thus an empirical spacer factor, Fs, can be defined as... 

Because liquid-vapor exchange reaction is the resultant of vapor-phase exchange reaction and the vaporization equilibrium reaction... 

The reactor effluent might require cooling by direct heat transfer because the reaction needs to be stopped quickly, or a conventional exchanger would foul, or the reactor products are too hot or corrosive to pass to a conventional heat exchanger. The reactor product is mixed with a liquid that can be recycled, cooled product, or an inert material such as water. The liquid vaporizes partially or totally and cools the reactor effluent. Here, the reactor Teed is a cold stream, and the vapor and any liquid from the quench are hot streams. 

The shell-and-tube exchanger is by far the most common type of heat exchanger used in production operations. It can be applied to liquid/liquid, liquid/vapor, or vapor/vapor heat transfer services. The TEMA standards dcTine the design requirements for virtually all ranges of temperature and pressure that would be encountered in an oil or gas production facility. 

Figure 1-6. The MCR process for liquefying natural gas (1) coolers, (2) heat exchangers, (3,4) two stage compressors, (5) liquid-vapor phase separator.

B is a powerful neutron absorber and has been employed in reactor control rods, neutron detectors, and other applications. Cascades based on exchange distillation of boron-ether complexes have usefully large a s and were used for 10B/UB isotope separation by the US DOE. Exchange distillation takes advantage of the fact that condensed phase/vapor phase separation factors can be enhanced (as compared to liquid/vapor a s) by association/dissociation equilibria in one or the other phase. At the normal boiling point (173 K) the VPIE for... 

The factors 4 and 4 accormt for the heterogeneity of the interface. The interfacial flux conditions. Equations (6.56) and (6.57), can be straightforwardly applied at plain interfaces of the PEM with adjacent homogeneous phases of water (either vapor or liquid). However, in PEFCs with ionomer-impregnated catalyst layers, the ionomer interfaces with vapor and liquid water are randomly dispersed inside the porous composite media. This leads to a highly distributed heterogeneous interface. An attempt to incorporate vaporization exchange into models of catalyst layer operation has been made and will be described in Section 6.9.4. 

Tanks are used in innumerable ways in the chemical process industry, not only to store every conceivable liquid, vapor, or solid, but also in a number of processing applications. For example, as well as reactors, tanks have served as the vessels for various unit operations such as settling, mixing, crystallization (qv), phase separation, and heat exchange. Herein the main focus is on the use of tanks as liquid storage vessels. The principles outlined, however, can generally be applied to tanks in other applications as well as to other pressure-containing equipment. 

Figure 1 Flowsheet of the RCH/RP hydroformylation process 38 1 Continuous flow stirred tank reactor,424 2 Phase separator, 3 Stripping column, 4 Distillation column, 5 Heat exchanger, 6 Falling film evaporator, 7 Liquid vapor separator.

Fig. 4. Flow diagram of the Ruhrchemie/Rhone-Poulenc process (137) 1, continuous-flow, stirred tank reactor 2, phase separator 3, stripping column 4, distillation column 5, heat exchanger 6, falling film evaporator 7, liquid-vapor separator.

By analogy to the liquid-vapor equilibrium the system is said to be condensed for 2 > 0. The critical temperature is expressed in terms of a Heisenberg exchange parameter... 

D2O-DT exchange can be used for transferring tritium from heavy water to deuterium. Further enrichment is achieved by cryogenic distillation. Because of the similarity between deuterium and tritium, platinum on charcoal is the catalyst for vapor phase exchange, whereas hydrophobic catalyst is used for liquid-gas exchange. 

The miscibility of water and hquid carbon dioxide is very poor and an intermediate solvent has to be used to allow the replacement of water by carbon dioxide. In a procedure initially developed to prepare representative samples for electron microscopy, water is replaced by ethanol through exchanges with alcoholic solutions of increasing concentration. The alcogel prepared by a final exchange with absolute ethanol (Fig. 3c) is introduced in a pressure vessel in which liquid CO2 is admitted and replaces ethanol in the gel. The C02-impregnated gel is compressed and heated above the critical point of CO2 (31.05°C, 73.8 bar). Release of pressure above the critical temperature allows CO2 to be extracted without the formation of any liquid-vapor interface and a dried aerogel is formed (Fig. 3d). 

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