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Chapter 3: Capture of CO2 Absorption processes in post-combustion capture make use of the reversible nature of the chemical reaction of an aqueous alkaline solvent, usually an amine, with an acid or sour gas. The process flow diagram of a commercial absorption system is presented in Figure 3.4. After cooling the flue gas, it is brought into contact with the solvent in the absorber. A blower is required to overcome the pressure drop through the absorber. At absorber temperatures typically between 40 and 60oC, CO2 is bound by the chemical solvent in the absorber. The flue gas then undergoes a water wash section to balance water in the system and to remove any solvent droplets or solvent vapour carried over, and then it leaves the absorber. It is possible to reduce CO2 concentration in the exit gas down to very low values, as a result of the chemical reaction in the solvent, but lower exit concentrations tend to increase the height of the absorption vessel. The ‘rich’ solvent, which contains the chemically bound CO2 is then pumped to the top of a stripper (or regeneration vessel), via a heat exchanger. The regeneration of the chemical solvent is carried out in the stripper at elevated temperatures (100oC–140oC) and pressures not very much higher than atmospheric pressure. Heat is supplied to the reboiler to maintain the regeneration conditions. This leads to a thermal energy penalty as a result of heating up the solvent, providing the required desorption heat for removing the chemically bound CO2 and for steam production which acts as a stripping gas. Steam is recovered in the condenser and fed back to the stripper, whereas the CO2 product gas leaves the stripper. The ‘lean’ solvent, containing far less CO2 is then pumped back to the absorber via the lean-rich heat exchanger and a cooler to bring it down to the absorber temperature level. Figure 3.4 also shows some additional equipment needed to maintain the solution quality as a result of the formation of 115 degradation products, corrosion products and the presence of particles. This is generally done using filters, carbon beds and a thermally operated reclaimer. Control of degradation and corrosion has in fact been an important aspect in the development of absorption processes over the past few decades. The key parameters determining the technical and economic operation of a CO2 absorption system are: • Flue gas flow rate - The flue gas flow rate will determine the size of the absorber and the absorber represents a sizeable contribution to the overall cost. • CO2 content in flue gas - Since flue gas is usually at atmospheric pressure, the partial pressure of CO2 will be as low as 3-15 kPa. Under these low CO2 partial pressure conditions, aqueous amines (chemical solvents) are the most suitable absorption solvents (Kohl and Nielsen, 1997). • CO2 removal - In practice, typical CO2 recoveries are between 80% and 95%. The exact recovery choice is an economic trade-off, a higher recovery will lead to a taller absorption column, higher energy penalties and hence increased costs. • Solvent flow rate - The solvent flow rate will determine the size of most equipment apart from the absorber. For a given solvent, the flow rate will be fixed by the previous parameters and also the chosen CO2 concentrations within the lean and the rich solutions. • Energy requirement - The energy consumption of the process is the sum of the thermal energy needed to regenerate the solvents and the electrical energy required to operate liquid pumps and the flue gas blower or fan. Energy is also required to compress the CO2 recovered to the final pressure required for transport and storage. Figure 3.4 Process flow diagram for CO2 recovery from flue gas by chemical absorption.PDF Image | CARBON DIOXIDE CAPTURE AND STORAGE
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