International Journal of Applied Engineering Research, ISSN 0973-4562 Vol. 10 No.2 (2015) pp. 1673-1675 © Research India Publications; http://www.ripublication.com/ijaer.htm Economic Analysis of Solar Collector with Different Thermic Fluids of LiBr-Water Vapour Absorption Refrigeration System P.Rajkumar 1.a , R.Shankar 2, b* , T.Srinivas 3, c 1, Department of Mechanical Engineering, Dr. MGR Educational and Research Institute University, Chennai-600095 Tamil Nadu, India. 2, 3 Energy Division, School of Mechanical and Building Sciences, VIT University, Vellore, Tamilnadu, India-632014 rajkumar.mech@drmgrdu.ac.in a ,gentlewise26@yahoo.com b ,sri nivastpalli@yahoo.co.in Abstract: The therminol fluids are one of the effective parts in the solar thermal application. The amount of fluids consumed for various applications like solar thermal power plant, absorption refrigeration system, cooking etc. are high and it depends on the specific heat capacity. The cost of the thermic fluid is very high results increase in overall cost of the product. The cost analysis of the solar thermal vapor absorption refrigeration is made with different working fluids like therminol59, therminol66, therminol72, therminolD12 and therminolVP1. The area of the collector is reduced if the thermal capacity of the thermic fluid is high. Keywords—Thermic fluids, Heat transfer fluids, solar thermal, solar collector, cost analyses etc. INTRODUCTION The daily increasing rate of power consumption for both domestic and industrial usage is increasing enormously with growing population, calls for research on sustainable and efficient power generation methods to meet the needs. Renewable energy plays a role for the safe and continuous power and thus solar thermal power plant is referred [1]. Refrigeration accounts for majority of power used in industries as well as residential areas. The solar thermal energy used in many applications like solar thermal power station, Kalina Cycle[2], Goswami cycle[3], combined cycle[4], vapor absorption refrigeration cycle etc. Except to the solar thermal power system all cycle will run on low temperature [5-8], in which parabolic trough collectors will be used. The problem of solar thermal system is collector area cost and thermic fluid cost. The main objective is the investigation of total collector area required for the solar vapor absorption refrigeration system at various thermic fluids. The thermic fluids have high thermal heat carrying capacity their boiling point is high enough to with stand the temperature generated by the collector. The thermic fluid doesn’t get vaporized. It can with stand a temperature difference of -100˚C to 400˚C [9]. So the thermic fluid can transfer heat from collector to generator with negligible loss. Thus the thermic fluids capitalize the performance of the system without distortion with reasonable cost. Here we are considering the five thermic fluids specific heat capacity with respect collector area. So that the cost saving by the fluid to heat transfer is justified. The collector temperature respect to area of the collector proves utilization of which thermic fluids gives the higher performance with respect to each other. The property equation of the various thermic fluids like therminol59, therminol66, therminol72, therminolD12 and therminolVP1 are used from the industrial data [9]. WORKING CYCLE The double solar VAR is couple by using condenser heat recovery, helps in achieving the increased overall COP of system. The circuit in the left hand is Primary VAR system and the cycle which is running by the condenser heat load of the primary cycle is secondary VAR system. The primary cycle generator is couple directly to the solar parabolic trough collector and the condenser is coupled to the generator of the secondary cycle. The additional heat exchanger is provided in between the condenser and the evaporator in both the circuit to increase the cooling output. The strong solution concentration of the primary cycle is depends on the collector exit temperature and condensing pressure but the strong solution concentration for the secondary cycle is depends on the condenser exit temperature of the primary cycle. As same as the strong solutions concentration the weak solution also depends on the cooling pressure and temperature and it is fixed as 10 ⁰C for the analysis. The initial weak solution mass flow rate of 1 kg/s is assumed at the exit of the primary absorber is flow to the generator at the condensing pressure and high temperature. The total collector area required for running the above design is depends on the heat capacity of the thermic fluid, efficiency of the collector and beam radiation. The analyses for the proposed design are made at various thermic fluids with constant generator temperature, cooling load and beam radiation.