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ARTICLE IN PRESS 452 R.Z. Wang, R.G. Oliveira / Progress in Energy and Combustion Science 32 (2006) 424–458 the total energy received by each adsorber can be internally recovered [49]. Furthermore, the heat transfer fluid circuit can be very simple. It needs only a reversible pump, and control valves are not necessary. Tchernev and Emerson [112] developed a double bed zeolite–water adsorption air conditioner that employed the heat regeneration process to increase the COP and obtained experimental values between 1.6 and 1.0, according to the ambient temperature that ranged from 27 to 381C. The SCP was not sensitive to the ambient temperature and it was 36 W kg1. In the heat regenerative cycle, the flow rate and the type of heat transfer fluid have great influence on the performance of the adsorption system. High flow rates increase the SCP but decrease the COP [43], thus this variable must be chosen carefully to ensure that the machine will have the expected performance. The machine developed by Tchernev and Emerson [112] could achieve a SCP of 108 W kg1, but in this case, when the ambient temperature was 271C, the COP was reduced to 0.7, which is still relative high when compared to other adsorption machines. In the heat regenerative system developed by Miles and Shelton [113], the working pair used was activated carbon–ammonia, and the COP obtained varied between 1.19 and 0.42, for ambient tempera- tures from 20 to 35 1C. Another kind of heat regenerative cycle was suggested by Critoph [46], in which the refrigerant serves as heat transfer medium. A thermodynamic model presented by the author predicted a COP of 0.95 when the evaporation temperature is 0 1C and a condensation temperature is 42 1C. Wade et al. [40] simulated a regenerative adsorp- tion cycle with eight beds that could recover 76% of the waste energy from the adsorption process. During this cycle, the hot thermal fluid that left the hot adsorber (Adsorber 1 in Fig. 35) pre-heated the adsorbers 2–4, before be completely cooled by the heat sink. The cold heat transfer fluid flowed from the heat sink towards the adsorber at the adsorption phase (Adsorber 5). After remove the heat from the adsorber 5, the heat transfer fluid continued its path to pre-cool the adsorbers 6–8, and be pre-heated. Then, the thermal fluid was heated until the generation temperature by an external heat source, before it entered the adsorber 1. This fluid route was maintained during a specific period, before the adsorbers switch position. The previous work was the base for the design of a prototype with four beds that was used to produce cooling at 1361C [114]. The energy input neces- sary to produce 1 W of cooling in this prototype was 76.6 W, which was much lower than the 165 W required in the system without heat regeneration. Neveu and Castaing [41] proposed a heat recovery cycle between two adsorbers filled with different metallic salts. The adsorption chemical reaction inside the first adsorber releases the necessary heat to regenerate the salt placed in the second adsorber. Thus, only the salt in the first adsorber needs external heat supply. The use of MnCl2 in the first adsorber and NiCl2 in the second adsorber could produce a theoretical COP of 0.6 at evaporation temperature of 101C, while at this same evaporation temperature, the utilization of SrCl2 and FeCl2 would produce a COP of 0.7. In both cases, the assumed condensation temperature was 401C, and ammonia was the refrigerant desorbed and adsorbed. A different approach to improve the COP of sorption systems was followed by Satzger et al. [44]. The authors presented the theoretical results that can be expected when absorption and chemical Fig. 35. Scheme of the heating/cooling thermal fluid loop with eight adsorbers.PDF Image | Adsorption refrigeration
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