Heat Transfer in Bubble Bed

Yoshitome, Hiroshi; Mannami, Yoshitaka; Mukai, Kazuhiro; Kanazawa, Takaki; Yoshikoshi, Narimitsu

doi:10.1252/kakoronbunshu1953.29.19

Cited by 7 publications

(5 citation statements)

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“…It is also seen that the effects of the location of the heat transfer section Zh and the aerated liquid height Za on the hv value can be neglected. Similar observations have been reported by previous workers (Fair et al, 1962; Yoshitome et al, 1965).…”

Section: Resultssupporting

confidence: 93%

“…In Figure 6 the present hw data for the air-water system at 25 °C are compared with the previous data heat transfer from the column wall or the immersed heating element of various geometries into water. In view of the previous results (Kast, 1962;Yoshitome et al, 1965), the effect of the geometry of the heating elements may be considered to be negligible. The present data are roughly in agreement with the data of Nishikawa et al (1977) and Yoshitome et al (1965) within 13%.…”

Section: Resultsmentioning

confidence: 89%

“…In view of the previous results (Kast, 1962;Yoshitome et al, 1965), the effect of the geometry of the heating elements may be considered to be negligible. The present data are roughly in agreement with the data of Nishikawa et al (1977) and Yoshitome et al (1965) within 13%.…”

Section: Resultsmentioning

confidence: 89%

“…Thus, information on heat transfer coefficients hv between the cooling or heating surface and the gas-liquid dispersed bed is required in designing the bubble columns. Such heat transfer coefficients have been measured by numerous investigators (Kólbel et al, 1958(Kólbel et al, , 1960Fair et al, 1962;Kast, 1962Kast, ,1963; Yoshitome et al, 1965;Ruckenstein and Smigelschi, 1965;Burkel, 1972;Hart, 1976; Nishikawa et al, 1977;Steiff and Weinspach, 1978) for various geometries of heating elements. However, most of the previous data were obtained at relatively low gas velocities and the effect of the physical properties of the gas and liquid on the heat transfer coefficient has not been studied very extensively.…”

Section: Introductionmentioning

confidence: 92%

“…Various empirical correlations for the heat transfer coefficient in the bubble columns have been proposed by a number of investigators (Kólbel et al, 1958(Kólbel et al, ,1960; Kast, 1962Kast, , 1963; Yoshitome et al, 1965;Burkel, 1972;Hart, 1976;Nishikawa et al, 1977;Steiff and Weinspach, 1978). A summary of the previous correlations was presented by Steiff and Weinspach (1978).…”

Section: Previous Correlationsmentioning

confidence: 99%

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Heat transfer coefficient in bubble columns

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Section: Resultssupporting

confidence: 93%

Section: Resultsmentioning

confidence: 89%

Section: Resultsmentioning

confidence: 89%

Section: Introductionmentioning

confidence: 92%

Section: Previous Correlationsmentioning

confidence: 99%

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Heat transfer coefficient in bubble columns

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Kikukawa³

et al. 1981

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Men

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Heat transfer in three‐phase fluidization and bubble‐columns with high gas holdups

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Bubble column and three-phase fluidized bed reactors have wide applications in biotechnological and petroleum processes (Deckwer, 1985;Fan, 1989). In such biotechnological processes as fermentation and waste water treatment, small bubbles of oxygen and/or nitrogen are introduced in the column to enhance oxygen transfer and to ensure the stability of immobilized cell particles. In addition, tiny bubbles are formed by such gases as C02, H2, and CHI, which are produced during the biological process due to the production of surface active compounds. The presence of these small bubbles causes an increase in the gas holdup of the system. High gas holdups are also characteristics of industrial processes such as coal liquefaction and hydrotreating of residual oils. Tarmy et al. (1984) studied high gas holdup behavior in pilot-and large-scale coal liquefaction reactors and reported gas holdup as high as 50 ~0 1 % .Such high gas holdups were attributed to the formation of small rigid bubbles with noncoalescing tendencies due to high-pressure and high-temperature operations. Blum and Toman (1977) reported a maximum gas holdup of 0.5 in a hightemperature (100 to 350"C, 6.9 MPa) three-phase fluidized bed methanator. Thus, good understanding of the transport properties of three-phase fluidized beds with high gas holdups is essential to the design, control and optimum operations of the commercial reactors employed in the above-mentioned processes.High gas holdups in laboratory scale under ambient conditions can be obtained by the addition of surfactants in airwater and air-water-solid systems. Such high gas holdups in the presence of a surfactant simulate the conditions commonly encountered in coal liquefaction and petroleum resids hydrotreating operations. Levich (1962) reported that the presence of surfactants induces a noncoalescing tendency in the gasliquid flow and reduces the bubble rise velocity significantly by creating surface tension gradients that cause tangential stresses along the bubble surface. The addition of surfactants to pure water systems, however, increases the system complexity by altering the average bubble size, gas holdup, and bubble-particle interactions. This causes the flow regime transition which affects the heat-transfer behavior of the system. In addition to the dependence on liquid properties, operating

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Heat Transfer in Bubble Bed

Cited by 7 publications

References 0 publications

Heat transfer coefficient in bubble columns

Heat transfer coefficient in bubble columns

Fischer–tropsch Processes and Reactors

Heat transfer in three‐phase fluidization and bubble‐columns with high gas holdups

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