Abstract. This paper presents the hydrodynamics of chopped oil palm fronds (OPF) from cold Row experiments carried out in a swirling fluidized bed dryer (SFBD). The chopped OPF was 10 -15 m m in size and falls in between Geldart type B and D. The OPF which consisted of leaves and petiole (stem) were fnst separated before studied individually due to their different physical characteristics. 2 bed loadings of 120g and 140g were investigated for bed pressure drop, (APb), minimum fluidization velocity (U,,,f) and minimum swirling velocity ( U , , ) while regimes of operation were closely observed. The experiments yield that the OPF leaves and petiole have distinct hydrodynamic behavior due to their different bulk densities and voidage, hence suggesting drying should also be conducted separately unlike the current industrial practice. The leaves have lower Umf and U,, compared to the petiole and thus swirling motion was initiated earlier in SFBD when operating with leaves. Both samples however, have limited operating velocities due to elutriation. In conclusion, the SFBD was found to fluidize the chopped OPF well while providing good solid-gas contact whieh is highly desired for drying.

The wall-tekd heat transfer coefficients were measued by fixing a thin constaztan foil heater on the bed wall. Thermocouples located at diffemt heigh~s on the foil show a decrease in the wall heat transfer coefficient with bed height It was seen that only a discrete particle model which accounts for the conduction between the particle and the heat transfer s h c e and the gaxonvective augmentation can adequately represent the mechanism ofheat transfer in the swuline, fluidized bed. As the jet of gas enters the bed at a certain small angle, 8, to the horizantal plane, the jet will have two componentF ofvelocity. The vatical component of the jet yelocity, wlich is given by V sin 8, will mate fluididon ofmticles, while the h h t a l c o m m a V cos 8, will cmte s\v%kg [4]. The dish7iitor used in this bed ~i~. 1. ~~~i~ ofa swirling fluidized bed, consists of overlapping blades that are truncated sectors of a circle forming an mular region for gas flow The wne in the centn. of the bed avoiak a dead zone while graduaUy inueasing the 8oss-Many of the early works on wall-bed heat k f e r in fluidized sectional area of gas flow to the fRe nubx abve the bed beds held tha[ theprhcipal resiskce to heathsfer is a fluid film and that moving fluid&d pahcles acting as ttnin~lence promoters ' To whom corresnandence should be addressed.sw1u the 6lm to reduce the resistrmce. Ihe solid particle-surface

The present study aims to provide insight on energy profiling of a residential college in public university. The study involves electrical energy monitoring for six months from the month of March until August 2017. The data utilized to derive the average monthly consumption for both semester period and semester break. The consumption during semester break has been recorded to increase as much as 88% from the consumption during the semester break. The building energy index of the residential college has been recorded to be at 22.90 kWh/m2/year meanwhile the energy intensity was recorded to be at 1,932.08 kWh/occupant/year.

Abstraet--Geldart Type-D particles are often associated with poor fluidization characteristics due ro rneu large sizes ana nigner aensmes. lnls paper reports the hydrodynamics of various Geldart Type-D particles when fluidized in a swirling fluidized bed (SFB). Four different sizes of particles rancine from 3.85 mm to 9.84 mm with resnective densities ranging kom 840 kg/m3 to 1200 kgIm3 were used as bed material to study the effect of various bed weights (500 gam to 2000 gram) and centre bodies (cone and cylinder) for superficial velocities up to 6 mls. The performance of the SFB was assessed in terms of pressure drop values, minimum fluidization velociiy, UmEand iiuidizailun q o a i i~ by ui~vsicai observation on regimes of operation. The swirling fluidized bed showed excellent capability in fluidizing Geldart TypeD particles in contrast to the conventional fluidized beds. The bed pressure drop of increased with superficial velocity after minimum fluidization as a result of increasing centrifugal bed weight. It was also found that the particle size and centre body strongly influence the bed hydrodynamics.