IECM 14.0 beta User Manual > Modules Included with the IECM > Low-Carbon Hydrogen Production & Transport > SET PARAMETERS > Flue Gas CO2 Capture > MEA >

Adjustment Factors

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Inputs for the capital costs of modifications to process areas of the MEA CO2 capture system itself are entered on the Adjustment Factors parameter screen. The MEA CO2 capture system has the following capital cost process areas:

•Flue Gas Water Condenser: This area includes the flue gas water condenser used to reduce the temperature and condensed water vapors in the flue gas before it enters the absorber vessel.

•Flue Gas Blower: The flue gas enters the bottom of the absorber column and flows upward, countercurrent to the sorbent flow. Blowers are required to overcome the substantial pressure drop as they pass through a very tall absorber column. The cost is a function of the volumetric flow rate of flue gas.

•CO2 Absorber Vessel: The capital cost of the absorber will go down with higher MEA concentration and higher CO2 loading level of the solvent, and lower CO2 content in the lean solvent. Therefore, a power law relationship based on flue gas flow rate is used. This is based on cost and flow rate data from Fluor Daniel, Inc. The cost assumes one absorber vessel per train. The cost is a function of the volumetric flow rate of flue gas and the flue gas temperature.

•Intercooler (Absorber): This area includes the intercooler used for the CO2 absorber.

•Wash Column: Each wash column consists of a condenser and a knock-out (KO) drum. The capital cost of the wash columns is the summation of the condenser and the KO drum. The capital cost of the condenser is a function of cooling duty. The capital cost of the KO drum is a function of the mass flow rate of the inlet gas.

•Lean/Rich Heat Exchanger: The CO2-loaded sorbent must be heated to strip off CO2 and regenerate the sorbent. In addition, the regenerated sorbent must be cooled down before it can be recirculated back to the absorber column. Heat exchangers are used to accomplish these two tasks. This area is a function of the sorbent flow rate.

•Circulation Pumps: Circulation pumps are required to take the sorbent, introduced at atmospheric pressure, and lift it to the top of the absorber column. This area is a function of the sorbent flow rate.

•Solvent Regenerator: The regenerator (or stripper) is a column where the weak intermediate compound (carbamate) is broken down by the application of heat. The result is the release of CO2 (in concentrated form) and the return of the recovered sorbent to the absorber.

•Reboiler: The regenerator is connected to a reboiler, which is a heat exchanger that utilizes low-pressure steam to heat the loaded sorbent. The reboiler is part of the sorbent regeneration cycle. The cost is a function of the sorbent and steam flow rates.

•Solvent Reclaimer: A portion of the sorbent stream is distilled in the reclaimer to avoid accumulation of heat-stable salts in the sorbent stream. Caustic is added to recover some of the MEA in this vessel. The reclaimer cost is a function of the sorbent makeup flow rate.

•Solvent Processing: The sorbent processing area primarily consists of a sorbent cooler, an MEA storage tank, and a mixer. The regenerated sorbent is further cooled with the sorbent cooler, and MEA is added to make up for sorbent losses. This area is a function of the sorbent makeup flow rate.

•CO2 Drying & Compression Unit: The product CO2 must be separated from the water vapor (dried) and compressed to liquid form to transport it over long distances.