1982
DOI: 10.1002/cjce.5450600410
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Mass transfer modelling for GS heavy water plants: Part 1: Point efficiency on GS sieve trays

Abstract: A model that takes into account the gas‐phase and liquid‐phase resistance to mass transfer has been developed, where the overall mass transfer coefficient (KOGa) is expressed as a function of the equivalent Sauter‐mean bubble diameter. This parameter was back calculated from mass transfer measurements made at a pilot plant on single pass sieve trays of 0.311 m diameter. Hydraulic parameters were measured for these trays as well. Mean bubble diameters were then correlated as a function of active area F‐factor a… Show more

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Cited by 14 publications
(19 citation statements)
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“…Point efficiencies, which for the present trays are assumed equivalent to measured tray efficiencies, are also shown in the diagram. Tray efficiencies at GS pilot plant which at similar conditions operated with froth heights between 15 cm and 25 cm, have ranged between 35% and 55% for similar hole F-factors (Neuburg and Chuang, 1982). It can be seen that for the single-hole bubble column trays, the major part of mass transfer takes place in the region where the gas contacts the liquid at the top of the froth.…”
Section: Discussionmentioning
confidence: 94%
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“…Point efficiencies, which for the present trays are assumed equivalent to measured tray efficiencies, are also shown in the diagram. Tray efficiencies at GS pilot plant which at similar conditions operated with froth heights between 15 cm and 25 cm, have ranged between 35% and 55% for similar hole F-factors (Neuburg and Chuang, 1982). It can be seen that for the single-hole bubble column trays, the major part of mass transfer takes place in the region where the gas contacts the liquid at the top of the froth.…”
Section: Discussionmentioning
confidence: 94%
“…Derivation of the equation for KO, in a bubble as a function of gas and liquid mass transfer resistances is given elsewhere (Neuburg and Chuang, 1982) as:…”
Section: Approach To Equilibrium In Bubble Formation Regionmentioning
confidence: 99%
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“…The model of Neuburg and Chuang (1982a) was used to calculate equivalent Sauter-mean bubble diameters (dB) from efficiency and hydraulic data. As illustrated in Figure 8, packing reduced dB by 5 to 25% resulting in a corresponding increase of up to 2.5 times in interfacial area.…”
Section: Resultsmentioning
confidence: 99%
“…However, 6 G and 6L have not been determined by experiments. Consequently, a rather arbitrary assumption of 6 G = OL has been made by many investigators (Calderbank and Pereira, 1977;Lockett and Uddin, 1980;Neuburg and Chuang, 1982;Stichlmair, 1978;Dribika and Biddulph, 1986). If 8G = OL, eq 20 becomes for a typical distillation system, eq 21 would give LPR = 0.17 and GPR = 0.83, which might indicate that distillation is a gas-phase-controlled operation.…”
Section: Theorymentioning
confidence: 96%