1981
DOI: 10.1021/i200012a017
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Maximum heat transfer coefficient between a horizontal tube and a gas-solid fluidized bed

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Cited by 53 publications
(13 citation statements)
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“…4 is applicable to both large and small particles. This approach is in agreement with that of Grewal and Saxena,11 who suggested that the bed‐to‐surface heat transfer is dependent on particle residence time at the tube surface and particle concentration near the surface. Shorter particle residence time and higher dense phase fraction near the surface both contribute to higher values of local heat‐transfer coefficient 12.…”
Section: Bed‐to‐surface Heat Transfer In Fluidized Bedssupporting
confidence: 90%
See 1 more Smart Citation
“…4 is applicable to both large and small particles. This approach is in agreement with that of Grewal and Saxena,11 who suggested that the bed‐to‐surface heat transfer is dependent on particle residence time at the tube surface and particle concentration near the surface. Shorter particle residence time and higher dense phase fraction near the surface both contribute to higher values of local heat‐transfer coefficient 12.…”
Section: Bed‐to‐surface Heat Transfer In Fluidized Bedssupporting
confidence: 90%
“…Following Mickey and Fairbanks1 and Gelperin and Einstein,9 the overall particle convective component can be expressed as Shorter particle residence time (so that particles are frequently replaced) and higher average solids concentration will contribute to higher values of the local heat‐transfer coefficient 11, 12. In this case, the local average solids concentration can be estimated from the “occupancy” * values derived from the PEPT measurements.…”
Section: Resultsmentioning
confidence: 99%
“…The coefficients, h avg increase with increasing pressure at the given fluidizing number (U g /U mf ) as reported in previous studies [5,16]. Heat transfer rate between the tube and fluidized bed is a function of soild holdup and particle residence time at the tube surface [16] which indicates high h avg can be obtained at short contact time of particle or packet or high solids holdup at the tube surface. With increasing gas velocity, packet residence time at the surface becomes short by vigorous bubbling behavior, and consequent increae in h avg .…”
Section: Heat Transfer Characterisitics At the Tube Surfacesupporting
confidence: 73%
“…However, all the heat flux values given in Fig. 7 are lower than those reported for PC boilers (see for example (Seltzer et al, 2007;Xu et al, 2000;Butler and Webb, 1991)) and within the ranges reported in the literature for oxy-fuel conditions (Seddighi Khavidak et al, 2015) and air-fired conditions (Seddighi Khavidak et al, 2015;II'chenko et al, 1968;Grewal, 1981;Huilin et al, 2000;Xie et al, 2003aXie et al, , 2003b in CFB boilers. One should note that the detailed description of the role and share of convective and radiative heat transfer in the air-and oxy-fired CFB furnace is given in detail in Seddighi Khavidak et al (2015) where it is shown that the radiative heat extraction is more than 70% of total heat extraction in the furnace while the solids radiation dominates the gas radiation in conditions relevant for CFB combustion.…”
Section: Resultssupporting
confidence: 81%