Mass transfer modelling for GS heavy water plants: Part 1: Point efficiency on GS sieve trays

Neuburg, Heinz J.; Chuang, Karl T.

doi:10.1002/cjce.5450600410

Cited by 14 publications

(19 citation statements)

References 10 publications

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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%

“…Information obtained from these experiments has been valuable in the development of a mass transfer model to predict tray efficiency for large industrial sieve trays (Neuburg and Chuang, 1982).…”

mentioning

confidence: 99%

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Mass transfer in a single‐hole tray column

Neuburg

Chuang

1986

Can J Chem Eng

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A theoretical model for deuterium exchange in the H2S/H20 system was derived to describe mass transfer in the bubble formation, bubble displacement and bubble breakup regions above a single-hole tray in an 8 cm diameter transparent column. The model was applied to data measured at 31°C in the pressure range of 790 to 2000 kPa and in a wide range of gas and liquid flows. High speed cinematography was used to measure bubble diameters, bubble formation times and bubble contact times in the liquid, all of which are parameters in the mass transfer models.Results show that for single-hole trays and the major part of mass transfer occurs in the upper surface of the froth where bubbles disengage from the liquid. However, when the same model is applied to pilot plant sieve trays, it is shown that the bulk of mass transfer takes place in the region where bubbles are ascending in the froth. The tray efficiencies predicted by the model agree well with measured values.

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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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Mass transfer in a single‐hole tray column

Neuburg

Chuang

1986

Can J Chem Eng

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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%

Improving sieve tray performance with knitted mesh packing

Spagnolo¹,

Chuang²

1984

Ind. Eng. Chem. Proc. Des. Dev.

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Wadsworth, M. E.; roves, R. D. Trans. Soc. Min. Eng. A I M Perry, R. H.; Chllton, C. H. "Chemlcai Englneers' Handbook", 5th ed.; Szekeiy, J.; Themeiis. N. J. Wiley: New York, 1971; Chapter 17. Vlzsolyi, E. et al.Sieve trays have become popular contacting devices for mass and heat transfer applications because of their relative simplicity and low cost. As a result, much has been published in recent years on their hydraulic and mass transfer performance. However, little has appeared on improving contact performance by adding a shallow bed of packing on the trays. The hydraulic and mass transfer performance of sieve trays containing a 25-mm bed of a knitted mesh packing was studied for the Glrdier-Sulfide (GS) heavy water production process operating at 32 OC and 2.17 MPa. With packing, tray pressure drops increased, tray-to-tray entrainment decreased, and efficiency increased by 3 to 20 percentage points. The greatest efficiency gains occurred in the low gas flow range where the tray operated in the bubble regime.

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“…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%

Liquid-Phase Resistance to Mass Transfer on Distillation Trays

Chen¹,

Chuang²

1995

Ind. Eng. Chem. Res.

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The liquid-phase resistance to mass transfer was determined for the distillation of six binary mixtures. It was found that the liquid-phase resistance to mass transfer is significant, ranging from 20 to 55% of the total mass-transfer resistance. The results also indicated that the traditional assumption of & = OL is not valid for distillation systems. If this assumption is applied, the fraction of liquid-phase resistance to mass transfer will be significantly underestimated. Tray efficiency models developed from data obtained from absorption and stripping systems (e.g., the AIChE method) were suggested to greatly overpredict the number of liquidphase mass-transfer units for distillation systems. Thus, careful examination of the use of various efficiency models for tray design is required.

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Mass transfer modelling for GS heavy water plants: Part 1: Point efficiency on GS sieve trays

Cited by 14 publications

References 10 publications

Mass transfer in a single‐hole tray column

Mass transfer in a single‐hole tray column

Improving sieve tray performance with knitted mesh packing

Liquid-Phase Resistance to Mass Transfer on Distillation Trays

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