Carbonate looping process simulation using a 1D fluidized bed model for the carbonator

A new model of the carbonator reactor in the calcium looping technology for post-combustion CO2 capture

“…Despite that Equation (2) cannot reflect the effect of calcination under high CO 2 pressure as would be the case in the CaL technology, it has been routinely used in theoretical studies as representative of the sorbent behavior in order to model the carbonator reactor [15][16][17][18].…”

“…As mentioned in the introduction, in order to predict the CO 2 capture efficiency of the CaL technology, many authors [15][16][17][18] propose to simplify the CaO conversion behavior by assuming that it reaches a maximum value, X N , at a constant rate (proportional to the free surface available of CaO and the thickness of the CaCO 3 layer formed) in a 5 time t lim , after which the reaction rate drops to zero (solid lines in Fig. 4a).…”

“…In order to predict the efficiency of CO 2 capture by integrating the CaL technology on existing power plants, a number of models have being proposed in the literature [15][16][17][18]. Besides, several pilot-medium scale plants (up to 1.7 MWth) demonstrate a high CO 2 capture efficiency, which raises hopes on a successful scale-up of the technology [13,14,[19][20][21].…”

Thermochemical energy storage of concentrated solar power by integration of the calcium looping process and a CO2 power cycle

“…Under these conditions, limestone derived CaO exhibits a severe drop of conversion in only a few cycles converging towards a residual value of just about 0.07, which makes it necessary to periodically purge the poorly active sorbent and replace it by a makeup flow of fresh limestone. The efficiency of the calciner reactor and the energy penalty efficiency caused by the CaL integration [32,33] into coal fired power plants (CFPP) have been also important subjects of analysis [25,[34][35][36]. Pilot plants (of size on the order of 1-2 MWth) demonstrate the achievement of CO 2 capture efficiencies around 90% [37,38] whereas model simulations predict an efficiency penalty on power generation around 5-6% when scaling up the technology to a commercial level [39].…”

The impact of calcium sulfate and inert solids accumulation in post-combustion calcium looping systems

“…In the calciner coal burns under oxy-fired conditions [10] to attain the temperatures required to convert both the CaCO 3 from the carbonator and the fresh sorbent back to CaO (around 900ºC). Although the heat demand in this reactor (coal and O 2 ) is high [10][11], the overall energy penalty of the CaL process is low [10,[12][13][14][15][16][17][18][19], since energy can be recovered from high-quality heat sources (the solids streams between reactors, the carbonator and the high temperature gases abandoning the reactors). As a consequence of the nature of the CaL process, these systems have a continuous input of inert solids, mainly due to the coal fed into the circulating fluidized bed calciner but also because of the SO 2 in the flue gas entering the circulating fluidized bed carbonator.…”