This paper proposes and designs two novels Fault Ride Through (FRT) controllers for maintaining Fixed Speed Wind Generation system (FSWGs) stability during fault events. The first technique has been implemented by increasing the wind turbine blade pitch angle with maximum possible rate to reduce the mechanical extracted wind power and consequently suppress wind generation system acceleration. The second FRT technique has been verified by adapting gear ratio of wind generation system to run far from optimum maximum power point and help FRT process. Effectiveness of the two proposed FRT techniques has been proven by accurate simulation of the most severe disturbance conditions. Also, Results indicated that second technique gives faster response than the first one. Without employing any FRT technique, FSWGs cannot keep its stability and the standalone Micro-Grid (MG) transfers to the blackout mode. Implementation the two FRT techniques requires no additional hardware. Only, control algorithms need little modification to deal with fault event and help FRT process. This fact makes the two proposed FRT techniques are simple, practical and highly economical attractive.

The influence of spinning cup and disk atomizer configurations on droplet size and ejection velocity characteristics has been experimentally investigated. The Phase Doppler Particle Analyzer (PDPA) was used to measure spray characteristics in the downstream tangential distance along the spray trajectory. Four groups of both rotating disks and cups with different configurations have been experimentally studied. The first group comprises spinning disks serrated with different numbers of teeth ranging from 0 to 240. The second group includes spinning disks with different upper and lower edge angles in the range of 15° to 60°. The third set consists of spinning conical cups with different half cone angles ranging from 15° to 60° and different base diameters in the range of 0.002 to 0.06 m (2–60 mm). The last set includes spinning cylindrical cups with different heights in the range of 0.005 to 0.045 m (5–45 mm). The outer diameter of all cups and disks in all sets is 0.07 m. All experimental tests have been performed at a rotating speed of 1257 rad/s (12,000 rpm), and supply water flow rate of 2.22×10−6 m3/s (8 L/h). Measurements of Sauter mean diameter and average droplet velocity for droplets produced by studied cups and disks are compared with those of droplets produced by a regular flat disk atomizer. Comparisons indicate that all values of Sauter mean diameters and average droplet velocities for different configurations are statistically within 95% confidence level intervals around the mean of those produced by a regular flat disk. Numerically, the mean of Sauter mean diameters produced by different configurations of spinning disk and cup atomizers varied between −8% and 12% around the mean of Sauter mean diameter produced by a regular flat disk. In addition, the virtual slip ratio ranged between 18% and 41% for all atomizer configurations, while for a regular flat disk, it was 33%. The developed correlation predicting Sauter mean diameter produced by spinning regular flat disks can be satisfactorily used to predict those produced by rotating cup and disk atomizers with different configurations. In addition, the values of drag coefficient and drag force for droplets of a regular flat disk are slightly different from those calculated for investigated disk and cup atomizers.

The influence of spinning cup and disk atomizer configurations on droplet size and ejection velocity characteristics has been experimentally investigated. The Phase Doppler Particle Analyzer (PDPA) was used to measure spray characteristics in the downstream tangential distance along the spray trajectory. Four groups of both rotating disks and cups with different configurations have been experimentally studied. The first group comprises spinning disks serrated with different numbers of teeth ranging from 0 to 240. The second group includes spinning disks with different upper and lower edge angles in the range of 15° to 60°. The third set consists of spinning conical cups with different half cone angles ranging from 15° to 60° and different base diameters in the range of 0.002 to 0.06 m (2–60 mm). The last set includes spinning cylindrical cups with different heights in the range of 0.005 to 0.045 m (5–45 mm). The outer diameter of all cups and disks in all sets is 0.07 m. All experimental tests have been performed at a rotating speed of 1257 rad/s (12,000 rpm), and supply water flow rate of 2.22×10−6 m3/s (8 L/h). Measurements of Sauter mean diameter and average droplet velocity for droplets produced by studied cups and disks are compared with those of droplets produced by a regular flat disk atomizer. Comparisons indicate that all values of Sauter mean diameters and average droplet velocities for different configurations are statistically within 95% confidence level intervals around the mean of those produced by a regular flat disk. Numerically, the mean of Sauter mean diameters produced by different configurations of spinning disk and cup atomizers varied between −8% and 12% around the mean of Sauter mean diameter produced by a regular flat disk. In addition, the virtual slip ratio ranged between 18% and 41% for all atomizer configurations, while for a regular flat disk, it was 33%. The developed correlation predicting Sauter mean diameter produced by spinning regular flat disks can be satisfactorily used to predict those produced by rotating cup and disk atomizers with different configurations. In addition, the values of drag coefficient and drag force for droplets of a regular flat disk are slightly different from those calculated for investigated disk and cup atomizers.