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an absorption refrigeration system, typically including a water-lithium bromide system, is limited to applications for heat sources with temperatures greater than 100°C. Therefore, the adsorption refrigeration system is selected for this chemical heat pump system. The adsorption refrigeration system comprises adsorption and desorption processes shown in Fig. 16. In the adsorption process, a water-vapor refrigerant is adsorbed in a silica gel adsorbent. The adsorption process is accompanied by evolution of heat; the adsorptive capacity increases with lowering temperature. Therefore, silica gel is cooled to 20°C using liquid CO2 supplied from the mechanical heat pump system described below. Water vapor that is adsorbed in silica gel is supplemented with water evaporation in the evaporator cell. The water temperature in the evaporator cell falls from effects of water evaporation; then, water in the circulation tubes of the cold-water supply system is chilled when cold water in the evaporator cell is sprayed on the outer surface of tubes. Chilled water of 7°C is silica gel using hot CO2 obtained from heat exchange in the pre-cooler. The desorbed water vapor is condensed in the condenser cell by cold CO2 supplied from the heat pump system. Finally, the condensed water is transferred to the evaporation cell. These adsorption and desorption processes repeat continuously. Hot heat is recovered from the pre-cooler and intercooler by the mechanical heat pump system, which will be used for a bioconversion system, described in the next section, and local heating. Its mechanism is described below. Carbon dioxide in the pre-cooler and the intercooler is cooled to the compressor inlet temperature of 35°C through boiling heat transfer using 20°C liquid CO2 as coolant. Pre-cooler and intercooler heat-exchanger sizes are minimized using efficient boiling heat transfer. The CO2 gas generated through boiling heat transfer in the pre-cooler and the intercooler is pressurized to 10 MPa by the compressor in the mechanical heat pump; its temperature is thereby raised to 93°C. Resultant CO2 at 93°C is used for heating water from 25°C to 85°C in the heat exchanger of the hot-water supply system; its temperature is thereby lowered to 30°C. Hot water of 85°C is delivered for bioconversion and local heating. The CO2 of 30°C is further cooled to 20°C by reducing pressure from 10 MPa to 5.7 MPa at the expander turbines. Liquid CO2 of 20°C and 5.7 MPa is used again for adsorption cooling processes in the refrigerator, pre- cooler, and intercooler. Net energy utilization to total thermal output generated in the core is estimated to be greater than 85% when considering energy recovered from waste heat as cold and hot water and compressor work required for the chemical and mechanical heat pump systems. The net energy utilization indicates 2.5-times-higher waste heat use for cooling and heating, in addition to supplied electricity, than in current LWRs with cycle efficiency of about 34%. This fact means that, compared to current LWRs, the cogeneration system can achieve 2.5 times more efficient natural resource utilization of uranium, and reduce greenhouse-gas emissions, while simultaneously mitigating long-half-life radioactive material accumulation. The cogeneration system is economically feasible because the hot water supply cost in the cogeneration system is expected to be lower beyond operation of about four years than those in conventional fossil-fired boilers. The energy produced by this system serves various commercial and residential sector needs.14 The usage fraction given in Fig. 17 shows that uses served only by electricity are limited to “power and others” ranging from 35.2% of the residential use sector to 40.0% of the commercial use sector. The remainder––60% of the energy used––can be supplied by hot and cold water, except for cooking use (6.7–8.0% in residential and commercial sector). The heat recovery system can provide energy sources for cities and bioconversion. Liquid G aseous CO2, CO2, 20°C 20°C C ooling CO2 S ilic a Gel Spray W ater W ater Water vapor 12°C Cold Water 7°C Liquid C O 2, 20°C CoolingCO2 G aseous C O 2, 20°C Gaseous Gaseous CO2, CO2, 105°C 55°C Heating C O 2 Cooling 2.2% Cooling 8.8% Hot Water 21.7% C ondenser A dsorber a) Adsorption Process Evaporator Pump S ilic a Gel Spray Water Condenser Adsorber Water V apor Water Evaporator Pump Power & Others 35.2% Cooking 6.7% 8 Heating 27.6% Hot Water 28.3% Power & Others 40.0% Cooking 8.0% Heating 21.5% b) Desorption Process Fig. 16 Adsorption refrigeration system a) Residential sector b) Commercial sector Fig. 17 Energy usage in Japan, 2000PDF Image | ADVANCED ENERGY SYSTEM WITH NUCLEAR REACTORS
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