Coalescence bubble

In [568] the use of Co catalyzed sulfite oxidation is recommended for determining a. Depending upon the catalyst concentration, the rate of reaction at pH = 8 and T = 15-25°C could be varied between 50 and 10000 s . The activation energy was r 50000 kj/kmol. 

This should only give modest deviations, because the height dependence of d is low.) 

The term coalescence generally describes the prcxiess in which the primary produced, mostly very small gas bubbles or drops merge together into larger, stable ones. In fact, in fluid G/1 and L/L material systems, dispersion and merging together (coalescence) of the dispersed phase takes place constantly and the so-called stable bubble (droplet) size, under turbulent flow conditions, merely represents the the steady-state situation. 

In this section only those coalescence phenomena are discussed, which occur in G/L systems. They are also much more strongly pronounced in this material system than in Lf L systems and have a significant effect particularly on the interfacial area and thus on mass transfer. 

Calderbank [64] already mentioned that even very small quantities of the solute (often as little as 0.05%) were sufficient, to increase the interfacial area in the G/L system many times over. This also includes substances which are so weakly surface active, that the surface tension is hardly measurably affected, but nevertheless they exercise a large influence on the rate with which the gas bubbles coalesce. 

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It sometimes happens that two or more bubbles coalesce to form one that hardly rises at all in the narrow part of the nitrometer tube this may be driven up to the rest of the collected gas at the top of the tube by gently squeezing the rubber pressure tubing connecting the movable reservoir J with the nitrometer proper. 

Classical bubbles do not exist in the vigorously bubbling, or turbulent fluidization regimes. Rather, bubbles coalesce constantly, and the bed can be treated as a pseudohomogenous reactor. Small bubble size improves heat transfer and conversion, as shown in Figure 5b. Increasing fines levels beyond 30—40% tends to lower heat transfer and conversion as the powder moves into Group C. 

This empirical equation attempts to account for complex bubble coalescence, spHtting, irregular shapes, etc. Apparent bubble rise velocity in vigorously bubbling beds of Group A particles is lower than equation 16 predicts. 

Film Rupture. Another general mechanism by which foams evolve is the coalescence of neighboring bubbles via film mpture. This occurs if the nature of the surface-active components is such that the repulsive interactions and Marangoni flows are not sufficient to keep neighboring bubbles apart. Bubble coalescence can become more frequent as the foam drains and there is less Hquid to separate neighbors. Long-Hved foams can be easHy... 

This equation has been experimentally verified in liquids, and Figure 2 shows that it applies equally well for fluidized solids, provided that G is taken as the flow rate in excess of minimum fluidization requirements. In most practical fluidized beds, bubbles coalesce or break up after formation, but this equation nevertheless gives a useful starting point estimate of bubble size. 

Measurements in large fluidized beds of fine particles indicate that bubble coalescence often ceases within a short distance above the gas distributor plate. Indications from density measurements or single bubble velocities are that bubble velocity Ug and diameter often reach maximum stable values, which are invariant with height or fluidizing gas velocity. 

In a gas and liquid system, when gas is introduced into a culture medium, bubbles are formed. The bubbles rise rapidly through the medium and dispersion of the bubbles occurs at surface, forming froth. The froth collapses by coalescence, but in most cases the fermentation broth is viscous so this coalescence may be reduced to form stable froth. Any compounds in the broth, such as proteins, that reduce the surface tension may influence foam formation. The stability of preventing bubbles coalescing depends on the film elasticity, which is increased by the presence of peptides, proteins and soaps. On the other hand, the presence of alcohols and fatty acids will make the foam unstable. 

The two models commonly used for the analysis of processes in which axial mixing is of importance are (1) the series of perfectly mixed stages and (2) the axial-dispersion model. The latter, which will be used in the following, is based on the assumption that a diffusion process in the flow direction is superimposed upon the net flow. This model has been widely used for the analysis of single-phase flow systems, and its use for a continuous phase in a two-phase system appears justified. For a dispersed phase (for example, a bubble phase) in a two-phase system, as discussed by Miyauchi and Vermeulen, the model is applicable if all of the dispersed phase at a given level in a column is at the same concentration. Such will be the case if the bubbles coalesce and break up rapidly. However, the model is probably a useful approximation even if this condition is not fulfilled. It is assumed in the following that the model is applicable for a continuous as well as for a dispersed phase in gas-liquid-particle operations. 

Bubble coalescence may considerably influence holdup, residence-time distribution, and other properties of bubble-columns. Reference is made to the review by Jackson and to a recent study by Calderbank et al. (Cl). 

A complicating factor in this process is the formation of finely divided carbon, which causes an increase of liquid viscosity and promotes bubble coalescence whereby the gas-liquid interfacial area is reduced. Also observed was a effect of reactor height, which may be attributed to bubble coalescence. 

The absorption rate increased with increasing nominal liquid velocity for all particle sizes and decreased with increasing particle size for all liquid velocities. The absorption rates were lower than those measured in an equivalent gas-liquid system with no solid particles present. The difference is explained as being due to a higher rate of bubble coalescence and, consequently, a lower gas-liquid interfacial area in the gas-liquid fluidized bed. 

The results of Massimilla et al., 0stergaard, and Adlington and Thompson are in substantial agreement on the fact that gas-liquid fluidized beds are characterized by higher rates of bubble coalescence and, as a consequence, lower gas-liquid interfacial areas than those observed in equivalent gas-liquid systems with no solid particles present. This supports the observations of gas absorption rate by Massimilla et al. It may be assumed that the absorption rate depends upon the interfacial area, the gas residence-time, and a mass-transfer coefficient. The last of these factors is probably higher in a gas-liquid fluidized bed because the bubble Reynolds number is higher, but the interfacial area is lower and the gas residence-time is also lower, as will be further discussed in Section V,E,3. 

Figure 15.2 Bubble coalescence measured in a stirred tank reactor at 1000 Hz with a single 10-bit monochrome camera (From [8]).

Andersson, B. (2003) Important factors in bubble coalescence modeling in stirred tank reactors. 6th International Conference on Gas liquid and Gas-Liquid -Solid Reactor Engineering, 2003, Vancouver. 

Reversal (both selective and nonselective) of matter from the froth to the pulp through froth subduction, bubble coalescence and liquid drainage. 

Point C in Figure 15.14 is termed the critical heat flux or maximum boiling flux or peak boiling flux as bubbles coalesce on the surface creating a vapor blanket. Critical heat flux occurs because insufficient liquid is able to reach the heat transfer surface due to the rate at which vapor is leaving. Beyond Point D, the surface is dry and entirely blanketed by vapor and heat is transferred by conduction and radiation. 

The primary factor controlling how much gas is in the form of discontinuous bubbles is the lamellae stability. As lamellae rupture, the bubble size or texture increases. Indeed, if bubble coalescence is very rapid, then most all of the gas phase will be continuous and the effectiveness of foam as a mobility-control fluid will be lost. This paper addresses the fundamental mechanisms underlying foam stability in oil-free porous media. 

Oolman TO, Blanch HW (1986) Bubble coalescence in stagnant liquids. Chem Engnrg Commun 43 237-261... 

Abstract Sonoluminescence from alkali-metal salt solutions reveals excited state alkali - metal atom emission which exhibits asymmetrically-broadened lines. The location of the emission site is of interest as well as how nonvolatile ions are reduced and electronically excited. This chapter reviews sonoluminescence studies on alkali-metal atom emission in various environments. We focus on the emission mechanism does the emission occur in the gas phase within bubbles or in heated fluid at the bubble/liquid interface Many studies support the gas phase origin. The transfer of nonvolatile ions into bubbles is suggested to occur by means of liquid droplets, which are injected into bubbles during nonspherical bubble oscillation, bubble coalescence and/or bubble fragmentation. The line width of the alkali-metal atom emission may provide the relative density of gas at bubble collapse under the assumption of the gas phase origin. 

An issue as interesting as it is contentious is that of electrolyte inhibition of bubble coalescence. Recently, a number of studies have reported the ion-specific nature of electrolyte inhibition of bubble coalescence, albeit in static (non-acoustic) fields [43 -9]. Some electrolytes appear to be highly efficacious whereas others almost completely ineffectual in inhibiting coalescence and ion combination rules have been devised to predict the behavior of various ion pairs. Various explanations have been proposed, most implying a gas-liquid interfacial mechanism. Christenson and Yaminsky [44] have reported a correlation between the inverse Marangoni factor, (dy/ dc]) 2, and coalescence inhibition ability for several different... 

Fig. 14.7 (a) Normalised extent of bubble coalescence (AVr) as a function of bulk electrolyte concentration, (b) Absolute AFT as a function of dissolved gas concentration. Solutions were argon-saturated and sonicated at 355 kHz (figures adapted from reference [41])... 

Whereas the amount of gas in the system influences the extent of bubble-bubble coalescence and, in turn, the bubble radius, the composition of the gas atmosphere within the bubble plays a crucial role in determining the conditions of collapse. 

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