The power station will abstract 5.34 million m3 per day of seawater with both units operating at base load. This is used for cooling purposes and to operate the seawater washing flue gas desulfurization (FGD) system. This water will be drawn in from the harbor at low velocity (0.3 m/s) to avoid interference with shipping and to allow fish to escape from the intake current.
A bar screen will be installed to remove large debris from the intake water. A traveling screen will provide a finer screening of the water to remove small fish and other smaller aquatic life. These screens will protect the cooling water intake pumps and the rest of the cooling system from blockage. Debris collected on the bar screen will be removed and disposed of as a waste.

The traveling screens will be back-washed to remove debris. If the organisms in the wash water are found to be generally viable they will be returned to the sea by gravity in a channel or pipe. The velocity of flow in this will be such as to minimize damage to fish and other marine life. If only dead debris is being collected, this will be removed and disposed of off-site as waste.

The cooling water system will require intermittent dosing with chlorine to control biological fouling of the system. If uncontrolled, fouling would result in decreased heat transfer efficiency in the condensers and hence loss of generating effluent standard of 1.0 mg/1. In fact, any residual active chlorine in the water leaving the condensers will be reduced on contact with the FGD process water containing unoxidized SO2 or sulfite. As no further biofouling control will be required downstream of the aeration lagoon, the residual oxidant levels in the discharge will be negligible.

The water will pass through the condensers in the power station to cool the steam leaving the turbines. A portion of this flow is then routed to the FGD absorber where it is sprayed through the flue gas after it has passed through the electrostatic precipitators. The natural bicarbonate alkalinity in the seawater absorbs SO2 from the gas, with a resultant fall in pH as it does so. The system is designed for an efficiency of 70% removal of the SO2 from the flue gas.

The low pH seawater is then passed to a water treatment plant where it is mixed with the remainder of the cooling water flow and aerated to strip off the free CO2 produced from the bicarbonates. This removal of CO2 increases the pH of the water again, such that the discharge from the aeration lagoons has a pH value 7.0. The aeration also oxidizes sulfite in the water to sulfate, resulting in a well-oxygenated discharge with a low chemical oxygen demand. Heat is transferred into the water both in the condensers and the FGD absorber. The system is designed not to exceed a maximum temperature of 40 °C at the discharge.

The discharge will be via a channel placed at the southern shoreline of the site with a velocity of 1.5 m/s.