packed-bed thermal energy storage device

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packed-bed thermal energy storage device ( packed-bed-thermal-energy-storage-device )

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h is the heat transfer coefficient between air and ceramic balls, which can be calculated by the empirical correlation of Coutier[6]: h 700 G0.76d0.24 (4) 6(1) Where, d is diameter of ceramic balls, and G is the mass flow rate per unit cross section, which can be expressed as: G  m f ( 5 ) R2 Ss is the heat transfer surface area of ceramic balls per unit length of the tank, which can be calculated as Equation (4) based on assumption 2. 3 depending on the packing structure of ceramic balls. In this study, it is chosen to be 3. Uwall is the overall heat loss coefficient through the tank wall, which can be calculated by the method given by Hänchen[2]. Numerical Solution Equation (1) and (2) can be simplified by introducing the following dimensionless variables: T T f  f l (7) f  R 2 (1   ) Ss (6) s r Where, r is equivalent radius of ceramic balls, and fs is the surface shape factor, which may vary between 2 and T T hl  T T sl (8) zz z (9) s TT hl H tt  t (10) (H/U) Where, f is dimensionless fluid temperature, s is dimensionless solid temperature, zz is dimensionless packed height (while H is the actual total height of packed bed), and tt is dimensionless time. Thus, the dimensionless governing equations for both phases are as follows: Fluid: Solid: tt W Where, X, Y and W are the simplified coefficients, which are respectively expressed as: 1H hSs f f 1(sf)1(f) tt zz X Y (11) X U  c (1)R2 ff 1H 2Uwall Y U fcfR (13) (14) s  1 (  ) (12) fs 080027-5

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