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Therefore, the actual capital cost of absorber in this case may be estimated as equipments installed (Z10) in order to get the total cost of installation for that process area (10). Similarly, in case of other process areas some physical quantity can be identified (e.g., flue gas flow rate, solvent flow rate, CO2 product flow rate, CO2 compression energy requirement, steam flow rate, makeup MEA flow rate etc.) that may be used for scaling of the capital cost. The direct capital cost (process facilities) of CO2 capture and separation system consists of the following cost items Direct contact cooler: In case of coal-fired power plant applications that have a wet FGD (flue gas desulfurization) unit upstream of the amine system, the wet scrubber helps in substantial cooling of the flue gases, and additional cooler may not be required. In case of gas-fired power plants or majority of coal-fired power plants that do not have wet scrubbers for SO2 removal, a direct contact cooler has to be installed to bring down the temperature of the flue gas stream to acceptable levels. A direct contact cooler is essentially a large vessel where the incoming hot flue gas is made to contact with the cooling water. The size of this unit is mainly a function of the volumetric flow rate of the flue gas, which in turn depends upon the temperature and pressure conditions of the flue gas stream. The actual cost of the unit is estimated on the basis of the cost information available for a particular reference case study using 0.6 power law for scaling purposes. X 0.6 C10 =C10,ref 10 X10, ref Once the cost of a particular equipment is calculated (C10), it needs to be multiplied by the total number of V T0.6 Cdcc = Cdcc, ref fg fg Vfg,ref Tfg,ref Flue gas blower: The cooled flue gas is pressurized using a blower before it enters the absorber. The size (and the cost) of the blower is again a function of the volumetric flow rate of the flue gas as it enters the blower. So, the cost maybe estimated using as above V T0.6 Cblower = Cblower, ref fg,1 fg,1 Vfg,1,ref Tfg,1,ref Absorber: This is the vessel where the flue gas is made to contact with the MEA-based solvent, and some of the CO2 from the flue gas gets dissolved in the solvent. Again, the size of this unit is mainly a function of the volumetric flow rate of the flue gas, which in turn depends upon the temperature and pressure conditions of the flue gas stream, as it enters this vessel. The actual cost of the unit is estimated on the basis of the cost information available for a particular reference case study using 0.6 power law for scaling purposes. V T0.6 Cabsorber = Cabsorber, ref fg,in fg,in Vfg,in,ref Tfg,in,ref Rich/lean cross heat exchanger: The rich (CO2-loaded) and lean (regenerated) solvent streams are passed through this cross heat exchanger, where the rich solvent gets heated and the lean solvent gets cooled. So, the size (and cost) of this unit is mainly a function of the volumetric solvent flow rate in the absorber. It is assumed that this volumetric flow rate is fairly constant in the range of temperature and Integrated Environmental Control Model - Technical Documentation • 30PDF Image | Amine Based CO2 Capture
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