Formation of interfacial area at high rates of gas flow through submerged orifices

Abdelaal, Hesham; Stiles, Graham Bill; Holland, C. D.

doi:10.1002/aic.690120131

Cited by 15 publications

(6 citation statements)

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“…Similar agreement between the two injector types was found throughout the test range. It is notable that other phenomena involving gaseous injection into liquids have shown a similar lack of dependence on external injector geometry ( 9 ) .…”

Section: Resultsmentioning

confidence: 99%

“…X B = 0.7166B0. '689 ( Go/G,) 0.6446 (9) The multiple correlation coefficient for Equation (9) was 0.950 with an average absolute deviation between the measured and predicted values of penetration length of 11.7%. The standard deviations of the powers of B and the mass velocity ratio on the right-hand side of Equation ( 9 ) were 0.0342 and 0.0273, respectively.…”

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confidence: 94%

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Penetration characteristics of a submerged steam jet

1972

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The phenomena of a condensible gas jet discharging into a liquid bath has attracted attention from investigators representing a number of interests and disciplines. This process may involve condensation of a pure component (steam into water), dissolution of a gas into a bulk liquid phase (ammonia into water), or a more complicated reactive situation (oxidizing gas injected into a liquid metal bath). In each of these systems, it is of interest to know the size and chamcteristics of the submerged jet cavity as a function of the operating conditions. Since the steam jet condensing into water has experimental advantages due to its relative safety and good optical qualities, the present investigation was limited to this case.Although numerous studies, for example, (1 to 3 ) have been conducted on noncondensible gases discharging into water, there have been relatively few studies of the condensing jet. In one of the earliest studies, Boehm ( 4 ) observed the cavity formed by R steam jet issuing from a 3-mm. diameter injector into a water bath. He observed that the length of the cavity increased with increasing bath temperature. As the bath approached the saturation temperature, the cavity became unstable and broke up into numerous individual bubbles.Glikman ( 5 ) probed the velocity and temperature distribution in cavities formed from axisymmetric and two dimensional injectors. The data was limited and no attempt was made to correlate the results, however, Glikman concluded that condensation occurs in an irregular wavy interface. Unusually high turbulence levels were estimated in proximity to the interface. Binford et al. (6) observed cavities formed by steam jetsissuing from vertical tubes having inside diameters in the range 0.0109-0.0226m. at atmospheric pressure. Jet exit mass velocities were in the range 58-350 kg/m2 * s at a fixed bath temperature of 305°K. It was found that the ratio of cavity length to injector diameter varied logarithmically with jet exit mass velocity. A definite change in slope was observed for this correlation when the injector was choked. I n the choked flow regime, the growth of cavity length with increasing mass velocity was much more rapid than for unchoked flow.Correspondence concerning this paper should be addressed to G. M.Faeth. P. J. Kemey is with Lafayette College, Easton, Pennsylvania. Page 548May, 1972The goal of the present investigation was to extend the experimental range of these earlier investigations. Particular emphasis was placed on obtaining a correlation for cavity length as a function of operating conditions (bath temperature, injector mass velocity, diameter, etc.) . EXPERIMENTAL APPARATUS AND PROCEDUREA sketch of the overall test apparatus is shown in Figure 1. The water bath was contained within a rectangular steel tank equipped with windows for observation and photography of the steam cavities. The water bath was 0.76 m high, 0.76 m wide, and 1.52 in. long. The bath temperature was measured by seven thermocouples placed at various locations in the bath. The tempe...

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Section: Resultsmentioning

confidence: 99%

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confidence: 94%

Penetration characteristics of a submerged steam jet

1972

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“…Finally, in apparent contradiction to Equation ( 1) , Abdel-aal et al (1966) carried out experiments with bubbles in which they took care to exclude scattered light from the detector and they found a relationship of the form…”

Section: The Equation Which Applies Ismentioning

confidence: 96%

Light transmission through bubble swarms

Lockett

Safekourdi

1977

AIChE Journal

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In these calculations, we assumed the virial equation of 2 ' = 1 + BP, where B = ylB11 + y2B22 + tjly2812 state (18) (19) for the vapor phase, and UL = x 1 q L + x& for the liquid phase. The P-x data were correlated with polynomials or spline fits as shown in Table 1. I n each of the four cases, convergence was sensitive to the value of p k (the convergence parameter) and to the nature of the P-x equation chosen to fit the data. However, after several trials, each case was satisfactorily solved.The results for the chloroform-ethanol system are shown in Figure 1.

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“…Additionally, experiments measuring the change in mass transfer parameters due to increases in viscosity yield differing results depending upon whether the viscosity increase is caused by the addition of solids or by the addition of a high-viscosity fluid. Sharma and Mashelkar (1968) and Abdel-aal et al (1966) demonstrated an increase in a with increased viscosity for a glycerol and water mixture in a bubble column. Godbole et al (1 983) and Gollakota and Guin (1984), however, reported that a decreased with increased viscosity caused by increased solids loading.…”

Section: Discussionmentioning

confidence: 96%

Effects of finely divided solids on mass transfer between a gas and an organic liquid

Bartoš

Satterfield

1986

AIChE Journal

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Global gas-liquid mass transfer parameters, k,a and a were determined in an organic liquid in which finely divided solid particles were suspended in a mechanically stirred vessel. The product kLa and a both decreased linearly with solids loading; both were independent of particle size and particle density. Gas holdup was independent of solids loading. SCOPEThree-phase slurry reactors, in which a gas, a liquid, and a finely-divided solid are contacted, are widely used in industry. Gas-liquid mass transfer often presents a major resistance to the rate of reaction and it can affect product selectivity. If present, this resistance is usually much more important than that of mass transfer from liquid to the outside surface of solid particles. The prediction of gas-liquid mass transfer in these systems is still highly uncertain, partly because most laboratory or pilot plant studies have been conducted with water. Water is safe and cheap, and aqueous systems are of intrinsic interest for some applications. However, aqueous systems often behave substantially differently than organic systems. The latter are of primary interest in the chemical and petroleum industry and much less is known about them.Interfacial area, a, was determined here by the socalled chemical method (unsteady state absorption with simultaneous chemical reaction in the fast-reaction regime) using the reaction of COP with cyclohexylamine (CHA) in a solution of 90% toluene and 10% isopropanol. The overall mass transfer coefficient, kLa, was determined by the unsteady state desorption of helium from the same liquid into a nitrogen purge stream. The solid properties investigated were particle concentration (0-45 vol.%), size (35-200 pm), density (0.7-4.5 g / mL), and composition (glass, polytetrafluoroethylene, polypropylene). The effect of gas phase mixing upon the calculation of these parameters was also evaluated. Studies were made in a 1 L aerated and mechanically agitated reactor. CONCLUSIONS AND SIGNIFICANCEThe overall mass transfer coefficient and the interfacial area decreased linearly with inert solids loading. The decrease in kLa can be attributed to the decrease in a: kL was independent of solids loading for the conditions of this study. Gas holdup did not vary with inert solids loading, indicating that the decrease in a was due to bubble coalescence.Correspondence concerning this paper should be addressed to C.N. Satterfield Both kLa and a were independent of particle size for particle sizes below 200 pm. Both were also independent of particle density. Stirring speed was shown to be an appropriate basis for comparison of mass transfer parameters. At high solids loadings kLa and a were lower when the solids were relatively nonwetting. A mechanism for enhanced bubble coalescence was postulated.The use of an apparent viscosity for prediction of AIChE JournalMay 1986 Vol. 32, No. 5 773 mass transfer can be misleading because results differ depending upon whether a viscosity increase is caused by addition of solids or, e.g., by addition of a high-vi...

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Formation of interfacial area at high rates of gas flow through submerged orifices

Abstract: The interfacial area produced was correlated as a function of the physical properties of the fluids, the diameter and number of orifices per plate, and the gas flow rate.

Cited by 15 publications

References 11 publications

Penetration characteristics of a submerged steam jet

Penetration characteristics of a submerged steam jet

Light transmission through bubble swarms

Effects of finely divided solids on mass transfer between a gas and an organic liquid

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