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10.3  Flue Gas Desulfurization                                  295

                                   CaO þ H 2 O ! Ca OHÞ                 ð10:19Þ
                                                  ð
                                                      2
              Consequently, the desulfurization reaction becomes

                               Ca OHÞ þSO 2 ! CaSO 3 þ H 2 O            ð10:20Þ
                                  ð
                                      2
              The reaction would be even faster before complete water evaporation due to the
            ions in liquid phase.
              A potential problem associated with the semi-dry FGD is the corrosion of duct
            under humidified environment. Typically these systems are operated with a Ca/S
            ratio near 2, with typical SO 2 concentrations of a few 1000 ppmv from coal
            combustion.
              Another important parameter is the approach temperature, which is defined as
            how far the gas temperature is above the saturation temperature for the water in the
            gas. The lower the approach temperature, the longer it takes for water to be
            vaporized completely, and consequently, a higher sulfur uptake by the sorbent.



            10.4 NO x Reduction Using SCR and SNCR


            NO x control from the flue gas can be completed by dry and wet approaches too. Dry
            approaches include (SCR), selective noncatalytic reduction (SNCR), and adsorp-
            tion, whereas wet approaches are, similar to wet FGD, by wet scrubbers. This
            section focuses on dry approach of SCR/SNCR.



            10.4.1 Selective Catalytic Reduction

            SCR is one of the most successful technologies for NO x removal from flue gases
            [7, 24, 34]. Typical catalysts include V 2 O 5 or WO 3 on a TiO 2 support. SCR
            operates at temperatures of 350–400 °C. For a power plant the location is right
            before the air pre-heater, where ammonia is injected into the furnace and reacts with
            NO to form water and nitrogen as products:

                                   NH 3 þ NO ! N 2 þ H 2 O              ð10:21Þ

              Typical NO x reduction efficiency is in the range of 90–95 % when SCR is
            operated at an ammonia injection molar ratio of NH 3 /NO of about 0.8. The NH 3
            concentration after removal is below 5 ppm. It was reported that commercial SCR
            units reduce NO x emissions by 40–70 %, depending on upstream NO x concentra-
            tions and the local allowable NO x emissions [32].
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