PROJECT REPORTON

DESIGN, SIMULATION AND EXERGY ANALYSIS OF SOLAR ASSISTED DOUBLE EFFECT ABSORPTION REFRIGERATION

SYSTEM

Department Of Mechanical Engineering

University College of Engineering

RAJASTHAN TECHNICAL UNIVERSITY, KOTA

Submitted By:- Guided By:-

1. Abbas Bohra (12/416) Dr. Shivlal2. Aditya Goyal (12/417) Associate Professor3. Akhil Chawla (12/419) Dept. of Mechanical Engg.4. Ankit Kumar Singh (12/424) UCE, RTU, KOTA5. Kapil Pareek (12/446)

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ACKNOWLEDGEMENT

We take this opportunity to express our profound sense of gratitude and respect to all those who helped us throughout the duration of this project till now .

We express our gratitude to Dr. Shivlal, Associate Professor, Mechanical Engineering Department, UCE, RTU, KOTA for giving us an opportunity to undertake this project.

We are also very grateful to all staff of Mechanical Engineering Department for encouragement, without which the satisfactory completion of the project stage -1st was not possible.

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CERTIFICATE

This is to certify that Abbas Bohra, Aditya Goyal, Akhil Chawla, Ankit Kumar Singh, Kapil Pareek students of B.Tech final year Mechanical Engineering have successfully completed project stage-1st. They have worked with full zeal and enthusiasm toward Design, Simulation and Exergy Analysis of Solar Assisted Double Effect Absorption Refrigeration System. Their conduct during the period of stage 1st is satisfactory.

Date:- Dr. Shivlal

Associate Professor

Dept. of Mechanical Engg.

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CONTENTS

Page No. Acknowledgement………………………………………………… 2 Certificate……………………………………………………………… 3 Contents……………………………………………………………….. 4 Introduction………………………………………………………….. 6 Literature Review………………………………………………….. 9 Description of Components………………………………….. 13 Methamatical Modeling………………………………………… 16 Nomenclature……………………………………………………….. 17 References…………………………………………………………….. 18

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INTRODUCTION

Energy supply to refrigeration and air-conditioning systems constitutes a significant role in the world. The International Institute of Refrigeration (IIR) has estimated that approximately 15% of all electricity produced worldwide is used for refrigeration and air-conditioning processes of various kinds. According to the statistics survey by JARN1 and JRAIA2, the demand for air conditioners worldwide has the fundamental tendency of steady increase (IIR, 2006). The global growth rate is about 17%.

The cooling load is generally high when solar radiation is high. Together with existing technologies, solar energy can be converted to both electricity and heat; either of which can be used to power refrigeration systems.

A solar-driven refrigerator was first recorded in Paris in 1872 by AlbelPifre (Thévenot, 1979). A solar boiler was used to supply heat to a crude absorption machine, producing a small amount of ice. Later, solar powered refrigeration systems have been installed worldwide in many countries e.g. Australia, Spain, and the USA. Most are thermally driven absorption systems, designed for air-conditioning purposes.

The International Energy Agency (IEA) inaugurated the ‘Solar Heating and Cooling’ program in 1976. This program is still on-going. Solar cooling is focused under task (No.25), “Solar Assisted Air Conditioning of Buildings” which was initiated on June 1, 1999 and ended on May 31, 2004. A new task (No.38) entitled ‘Solar Air-Conditioning and Refrigeration’ is inaugurated in October 2006.

Absorption cooling systems have become increasingly popular in recent years from the viewpoints of energy and environment. Despite a lower coefficient of performance (COP) as compared to the vapour compression cycle, absorption refrigeration systems are attractive for using inexpensive waste heat, solar, geothermal or biomass energy sources for which the cost of supply is negligible in many cases. In addition absorption refrigeration use natural substances, which do not cause ozone depletion and global warming as working fluids.

The simplest configuration is the single effectcycle. It is a common fact that the coefficient of performance (COP) of LiBr/H2O machines working with this cycle ranges from0.6 to 0.8. Besides, driving temperatures are between 80 and 100°C for water‐cooled systems, while for air‐cooled ones are about 20°C higher. This range of temperatures makes LiBr/H2O single‐effect cycles very appropriate for solar cooling.

By adding some extra components to the basic single‐effect configuration, the double effectcycle is able to use the input heat twice for generating a greater amount of refrigerant. Due to the higher working pressures achieved in this configuration, this cycle is not practical for refrigerants with low boiling temperatures such as ammonia. The COP obtained for LiBr/H2O double‐effect

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systems is typically between 1.1 and 1.3. In turn, the usual range of driving temperatures is 140‐170°C for water‐cooled machines and 160-190°C for air‐cooled ones, (Izquierdo et al., 2002). Those temperatures make more complicated the use of solar energy as driving source; however several technologies are available in the market to provide solar heat at such temperatures, (Mendes, 2007).

In this project, the exergy losses inherent in an absorption refrigeration system will be calculate. A design procedure has been applied to a lithium-bromide absorption cycle and an optimization procedure that consists of determining the enthalpy, temperature, mass flow rate, heat rate, exergy losses in each component, coefficient of performance and overall effciency has been performed. An availability analysis was carried out for each component in the system.

Exergy method

A second law analysis calculates the system performance based on exergy, which alwaysdecreases, owing to thermodynamic irreversibility. Exergy analysis is the combination of the first and second law of thermodynamics and is defined as the maximum amount of work potential of a material or a form of energy in relation to the surrounding environment. Therefore, in an exergy analysis the losses represent the real losses of work. The principle irreversibility in a process leading to these losses are due to :

. Dissipation (friction).

. Heat transfer under temperature difference.

. Unrestricted expansion.

Modeling of each component

Energy and mass balances were written around each of the components and combined with the state equations for the thermodynamic properties of the lithium-bromide and water to yield a set of equations describing the system. The state equations were evaluated by the thermodynamic properties of LiBr and water. The principle of the optimization lies in the identification and minimization of the sources of lost work within the refrigeration cycle. The operating characteristics of the system components including the heat exchangers and the temperature differences between the internal fluids and those between the external fluids are factors considered in the analysis.

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The computer simulation model

The computer program was based on heat and mass balances, heat transfer equations, andthermodynamic property reactions written in terms of the static point properties for each of the subunits and matched at the connecting points. The initial conditions read into the program included the ambient conditions, component temperature, mass fraction, and effectiveness, vapor and cold air flow rates. With the given parameters, the program calculated the thermodynamic properties of the mixture at all points in the cycle. The COP was also calculated, which is defined as the ratio of the generator load to the evaporator load. The computer program was written in Engineering Equation Solver(EES).

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LITERATURE REVIEW

Thevenot, in his history of refrigeration’s, touches on solar cooling several times. He quotes that, in Paris, Pifre produced some ice by using a solar boiler to regenerate the absorbing solution via steam as early as 1872! Some years later this was achieved in Catalania also. In the 20th century, the open 'Kathabar' system operating with LiC1 was realized before 1940. Solar cooling was experimented with at many locations during the 1950s. At Tashkent, USSR in 1953, a parabolic mirror was used for regenerating. Several machines were installed after 1956 by Trombe. A chiller activated by solar energy with H20/LiBr was realized in Brisbane, Australia in 1958. Later (1966) in Queensland, Australia, a solar house including a solar-assisted chiller was tested. Finally, in the USA around 1976, some 500 solar air conditioners were installed. They ran for about 75 to 80% of the time on solar energy. In the remaining period the chillers were operated with electricity or fuel oil. This is important to reconsider in the light of the energetic comparison made above: a single-effect chiller with a COP of 0.7 operated on electricity requires about five times the primary energy of a compression chiller with a COP of 3.5. Consequently, all of the energy saving made by solar operation will be compensated by a 20% share of electrical operation. We may conclude that a significant share of the above-mentioned installations resulted were no big energy savings. In the 1970s and 1980s, solar cooling grew to be an important issue. For instance, at an IIR conference held in 1982 at Jerusalem 9, around 200 people discussed 40 different papers. Today, there are several national and international R&D programmes with the aim of promoting the use of solar energy. One of the first collaboration projects of the International Energy Agency was the IEA Solar Heating and Cooling Programme which originated in 1977 and is still going on today t. The main focus of this programme, as deduced from the publications available, is on heating rather than cooling, although the energy demand for cooling is larger. Also, within the cooling topic, more interest is on the solar side than on the refrigeration equipment side. Today there is no specific task on cooling going on. One of the prominent national renewable energy programmes is the Japanese Sunshine project, which is sponsored by the Japanese Ministry of International Trade and Industry (MITI) via the New Energy Development Organization (NEDO). Only one solar cooling project using hydrides is known t i. The United States Department of Energy (DOE) supports solar cooling on a wider basis t2. Research on collectors, closed sorption and compression chillers as well as open systems is promoted. The situation is worse again in the European Union. In the Third Call for Proposals of the Joule' project 13 (area 3: renewable energies) as well as in the 'Thermie' project calls 14, "active and passive solar heating and cooling" is quoted as an objective. In the SESAME database of the Fachinformationszentrum Karlsruhe 15, however, only four projects concerning solar absorption could be traced down, two of them using solar collectors as an energy source (evaporator heat) in heat pumping and not for energizing absorption systems.One more theoretical project (market survey) was finished in 199616. However, there has been renewed interest during the last years with experimental projects still going on.

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Anand and Kumar (1987) carried out their reversibility analysis of single effect and series flow double effect systems for condenser and absorber temperatures 37.8 C, evaporator temperature 7.2 C and generator temperature87.8 C for single effect and 140.6 C for double effect systems. They did not attempt to find the optimum generator temperature for the operation of a series flow double effect system. Lee and Sherif (2001b) presented the second law analysis of various double effect lithium bromide–-water absorption chillers for a chilled water temperature 7.22 C and cooling water temperatures 29.4 C and 35 C, and computed COP and exergetic efficiency. In the studies of double effect systems, the effectiveness values of solution heat exchangers considered for analysis has not been specified. Moreover their results are only valid for water cooled systems.Ravikumar T.S, Suganthi L., AnandA.Samuel study in detail the exergy variation in the solar assisted absorption system. The influence of the cycle parameters are analysed on the basis of first law and second law effectiveness and the results indicated various ways of improving system performance by better design. Also a better quality of the evaporator has more effect on the system performance than the better quality of other components. It was shown that second law analysis quantitatively visualizes losses within a system and gives clear trends for optimization.B. Chaouachi and S. Gabsi: study was the design and the simulation of an absorption diffusion refrigerator using solar as source of energy, for domestic use. The design holds account about the climatic conditions and the unit cost due to technical constraints imposed by the technology of the various components of the installation such as the solar generator, the condenser, the absorber and the evaporator. Mass and energy conservation equations were developed for each component of the cycle and solved numerically. The obtained results showed, that the new designed mono pressure absorption cycle of ammonia was suitable well for the cold production by means of the solar energy and that with a simple plate collector we can reach a power, of the order of 900 watts sufficient for domestic use.S.C. Kaushik, AkhileshArora Presented the energy and exergy analysis of single effect and series flow double effect water–lithium bromide absorption systems. A computational model has been developed for the parametric investigation of these systems. Newly developed computationally efficient property equations of water–lithium bromide solution have been used in the computer code. The analysis involves the determination of effects of generator, absorber and evaporator temperatures on the energetic and exergetic performance of these systems. The effects of pressure drop between evaporator and absorber, and effectiveness of heat exchangers are also investigated. The performance parameters computed are coefficient of performance, exergy destruction, efficiency defects and exergetic efficiency. The results indicate that coefficient of performance of the single effect system lies in range of 0.6–0.75 and the corresponding value of coefficient of performance for the series flow double effect system lies in the range of 1–1.28. The effect of parameters such as temperature difference between heat source and generator and evaporator and cold room have also been investigated. Irreversibility is highest in the absorber in both systems when compared to other system components.

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Rabah Gomri , Riad Hakimi presented exergy analysis of double effect lithium bromide/water absorption refrigeration system is presented. The system consists of a second effect generator between the generator and condenser of the single effect absorption refrigeration system, including two solution heat exchangers between the absorber and the two generators. In order to simulate the refrigeration system by using a computer, a new set of computationally efficient formulations of thermodynamic properties of lithium bromide/water solution developed is used. The exergy analysis is carried out for each component of the system. All exergy losses that exist in double effect lithium bromide/water absorption system are calculated. In addition to the coefficient of performance and the exergetic efficiency of the system, the number of exergy of each component of the system is also estimated. This study suggests the component of the absorption refrigeration system that should be developed. The results show that the performance of the system increases with increasing low pressure generator (LPG) temperature, but decreases with increasing high pressure generator (HPG) temperature. The highest exergy loss occurs in the absorber and in the HPG, which therefore makes the absorber and HPG the most important components of the double effect refrigeration system.Omer Kaynakli and Recep Yamankaradeniz study, the first and second law thermodynamic analysis of a single-stage absorption refrigeration cycle with water/lithium bromide as working fluid pair is performed. Thermodynamic properties of each point in the cycle are calculated using related equations of state. Heat transfer rate of each component in the cycle and some performance parameters are calculated from the first law analysis. From the second law analysis, the entropy generation of each component and the total entropy generation of all the system components are obtained. Variation of the performance and entropy generation of the system are examined at various operating conditions. The results show that high coefficient of performance (COP) value is obtained at high generator and evaporator temperatures, and also at low condenser and absorber temperatures. With increasing generator temperature, total entropy generation of the system decreases. Whereas maximum entropy generation occurs in the generator at various operating conditions, entropy generation in the refrigerant heat exchanger, expansion valve and solution pump is negligibly small.

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WORKING PRINCIPLE

An absorption refrigeration system is a heat operated device based on two factors which produce a refrigeration effect; these are

1. A primary fluid will boil at low temperatures.2. A secondary fluid will absorb the primary fluid which has been vaporized in the

evaporator.When the system utilizes a mechanical pump to circulate the absorbent refrigerant solution, a small amount of work input will be required. The heat source may be steam or an another hot fluid. There are two main types of absorption systems: the aqueous lithium bromide system and the aqua ammonia system.

Description of LiBr/H2O double effect cycle

The double-effect technology permits to take advantage of the higher availability associated with a higher temperature heat input (exergy). As a result, the double-effect cycles present a higher COP, approximately twice of single-effect cycles.The double-effect absorption cycle has two generator, namely the high-pressuregenerator (HG) and the low-pressure generator (LG). Vapor is generated in the HG by supplying external heat (QHG). This vapor flows then to the LG, where it changes phase by rejectingheat at sufficiently high temperature that it can be used to separate vapor from thesolution flowing through the LG. Thus, the input heat is used twice, which the term “double-effect” refers to.There are two basic configurations for the double-effect cycle depending upon thedistribution of the solution through the components, namely series or parallel flow. In theformer case, the whole solution from the absorber goes through the two generators in series,while in the latter case part of the solution flows to the HG and the rest goes to the LG.The parallel flow configuration offers a higher COP than theseries flow. Furthermore, parallel flow distribution reducespressure drops in the solution flow. What is more, reported thatparallel flow provides for better control of refrigerant generation.In Figure, a schematic representation of a parallel flow double-effect LiBr/H2Oabsorption cycle is shown. In the present configuration, the weak solution leaving the absorber is split into two circuits flowing in parallel. One part of the solution flows to the HGby passing through the high-temperature solution heat exchanger, and the other one goesinto the LG after passing through the low-temperature heat exchanger. The two solutionheat exchangers have a similar role as described for the single-effect cycle. The vapor generated in the LG is driven directly to the condenser. However, the refrigerant separated in the HG (and condensed in the LG) passes through a condensor to restore its thermodynamic conditions before entering the evaporator.

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DESCRIPTION OF THE MAIN COMPONENTS

Flat Plate Solar Collectors

A flat plate solar collector is, often the most economical choice for low temperature applications such as solar water heating systems. Absorbers can be made of a plastic or a metallic plate such as copper. A tracking system is not necessary for this type of collector. The maintenance routines and structure are simpler than other types of solar collectors The optical efficiency of a flat plate solar collector can be written as a product of the transmissivity (τ) of the glass cover and absorptivity (α) of the absorber.

Generators

As earlier mentioned, one of the requirements for the prototype was to achieve a compact design. On account of this, plate heat exchangers (PHE) were used in every generator of the absorption machine. It is well known that this kind of devices presents a high ratio of heat transfer rates to volume and, consequently, may reduce the final size of absorption machines.The high‐pressure generator is indirectly fired; that is, an intermediate fluid previously heated by an external source like waste heat or fuel combustion flows through one of the sides of the PHE. In the other side of the PHE, the LiBr/H2O solution pumped from the absorber flows and, as a result of the heat transfer taking place, part of the refrigerant boils off the solution. Regarding the low‐pressure generator, it consists of a PHE with similar characteristics to the previous one, except for the heat transfer capacity, which is lower. In this case, LiBr/H2O solution from the absorber flows through one side of the PHE, while in the other side the refrigerant previously separated in the high‐generator is condensed.

Solution heat exchangers

In the same manner as for the generators, the three solution heat exchangers in the prototype are plate heat exchangers. The main function of this kind of devices is to reduce the temperature of the solution coming from the generators before entering the absorber. At the same time, the solution flowing to the generators is preheated and, as a result, the input energy needed to boil the solution is lower.

Condenser

The condenser of the prototype is a finned heat exchanger where coolant separated in both the low‐generator and the single‐effect generator is directly condensed by the outdoor air. Refrigerant flows inside a cooper tube while air circulates through the aluminum fins in a cross

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flow configuration. As well know, the heat transfer coefficients of the air are quite low, thus the importance of increasing the air‐side surface by means of the fins.Thesubcooler is a heat exchanger similar to the condenser but with a considerably lower heat transfer capacity. The function of this device is to reduce the temperature of the refrigerant condensed in the low‐generator, ensuring besides that no vapor flows to the expansion valve. The condenser and the subcooler are horizontally placed just below the fan. They are installed in such a way that the air coming from the heat exchanger of the adiabatic absorber firstly passes through the condenser and then through the subcooler.

Evaporator absorber assembly

In this prototype, the evaporator and the absorber are assembled together in the same chamber. In this way, the water vapor generated in the evaporator is directly absorbed by the solution in the absorber. The lack of piping between these two components significantly reduces the pressure drop and consequently improves the absorption process. The evaporator basically consists of a falling film heat exchanger where the chilled water circulates inside a cooper coil and the refrigerant drops on its outer surface. With the purpose of improving the heat transfer from the chilled water to the refrigerant, both inner and outer surfaces of the tube coil tube are enhanced surfaces. In this sense, while the inner surface presents helical fins, the outer of the tubes is a micro‐structured surface.

Expansion devices:-

Two expansion valves where installed in the prototype: the first at the outlet of the condenser and the second at the exit of the sub-cooler. They consist of two flow restrictor devices generating a pressure drop in the refrigerant entering the evaporator chamber. As seen in Fig, they are hand controlled valves.

Piping materials:-

In this prototype, the tubes and surfaces in contact with the LiBr/H2O solution are made of stainless steel, while those ones exclusively contacting water are made of copper. Even though the aqueous LiBr solution is known to be highly aggressive to these metals (and to many others) in the presence of dissolved oxygen, the hermetic environment inside an absorption machine strongly reduces the amount of oxygen and, consequently, the corrosion rates are much slower.

Vacuum system:-

From the design requirements, it can be drawn that the needed evaporation temperatures are between 8°C and 14°C, which implies vapor pressures around 1 kPa (or 10 mbar). Although

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these pressure levels are not particularly low, the sensibility of LiBr/H2O absorption technology to leaks is very high, not only because of performance considerations, but also because of corrosion problems. This fact makes indispensable to control the vacuum inside the prototype in a very effective way. In the construction of the prototype, special care was taken into sealing all the joints.Besides, in order to ensure no vacuum loses occur through the solution pumps, magnetically driven gear pumps were utilized. Additionally, a vacuum pump and a vacuum meter were installed in the prototype, Figure. This vacuum system permits to pump out the air from the absorption machine before introducing the solution for the first time. What is more, this system enables to recover the low pressures in case of maintenance

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MATHEMATICAL MODELING

Fig: Schematic diagram of a series flow double effect absorption refrigeration system

High-pressure generator (HG)

Assuming the refrigerant flow rate separated in this generator is mr , 1Hthe energy and mass balances can be written as

QHG=mr , 1H h1H+m12h12−m11h11

m11=mr ,1H+m12

X11m11=X12m12

m12

mr ,1 H=

X12

X12−X11

mr , 1H=QHG

X12

X12−X11(h12−h11 )+ (h1H−h12 )

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Low-pressure generator (LG)

As above mentioned, the heat source for this desorber is the refrigerant vapor separatedin the HG, which transfers its latent heat to the solution (QLG). The input power canbe therefore written as

QLG=mr ,1H (h1 H−h1 ,CH )

If ṁr,1 is the refrigerant separated in the low‐generator, the energy and mass balancesfor this component can be expressed as

QLG=mr ,1h1+m9h9−m8h8

m8=mr ,1+m9

X 9m9=X8 m8

m8

mr ,1=

X 9

X9−X8

mr , 1=mr ,1 H(h1H−h1 ,CH )X9

X 9−X8(h9−h8 )+(h1−h9)

Absorber

Energy and mass balances in the absorber (assumed as adiabatic) are given by

Qa=m14 h14+m16 h16+ m4h4−m5h5

m16+m14=m8+m11−mr

Where ṁr represents the total refrigerant mass flow

mr=mr ,1+mr , 1H

Condenser

The latent heat rejected in the condenser by the vapor produced in the LG is given as

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Qcond=mr ,1 (h1−h2 )

Sub-cooler

In this component, an energy balance is expressed as

Q¿=mr ,1 H (h1 ,CH−h2 )

Evaporator

An energy balance in the evaporator yields

Qe=mr (h3−h4 )

High-temperature solution heat exchanger

The effectiveness of this heat exchanger, which has the purpose of cooling down theconcentrated solution leaving the HG, is given by

ηHshx=h12−h13

h12−h10

The heat recovered in this component can be calculated as

QHshx=m12 (h12−h13 )=m12 cp , s(T 12−T13)

As well, it can be expressed as

QHshx=m11 (h11−h10 )=m11 cp , s(T 11−T 10)

Low-temperature solution heat exchanger

Similarly to the high‐temperature solution heat exchanger, the effectiveness of thiscomponent is given by

ηLshx=h9−h15

h9−h7

The heat recovered in this component can be calculated as

QLshx=m9 (h9−h15 )=m9c p , s(T 9−T 15)

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QLshx=m7 (h8−h7 )=m7 cp , s(T 8−T 7)

Split valve

Energy and mass balances in the valve that divides up the solution flow yield

m5=m8−m11

h6=h7=h10

Expansion valves

Isenthalpic process is assumed to occur in the expansion devices located at the outletof both the condenser and the sub‐cooler. Thus, it is obtained that

h2=h3

Throttle valves

In these flow restrictors, it is considered that an isenthalpic pressure reductiontakes place. Hence, the following expressions can be written

h13=h14

h15=h16

Solution pump

The pump driving the solution must be able to exceed the pressure drops in all thecomponents, maintaining a constant pressure in both generators. The work performed bythe pump is calculated as follows:

W p=m5(P6−P5)ρ5∗ηp

Coefficient of performance

The thermal coefficient of performance is defined by

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COPth=QeQHG

NomenclatureA area, m2COP coefficient of performanceη Efficiencyρ Density Kg/m3

cp isobaric specific heat, kJ/kgKDE double-effectHG high-pressure generatorh specific enthalpy, kJ/kg / heat transfer coefficient, W/m2Kk conductivity, W/mKL length, mLG low-pressure generatorm mass flow rate, kg/sQ heat transfer rate, kWq specific heat transfer rate, kW/kgR solar radiation, kWSE single‐effectSF solar fractionSHX solution heat exchangerSP solution pumpT temperature, °Ct time, sU global heat transfer coefficient, v specific volume, m3/kgW power consumption, kWw specific work, kW/kgrX concentration of LiBr in the solution (%)

References1. Thevenot, R., A History of Refrigeration Throughout the World. Int. Inst. Refrigeration.

Paris, 1979.2. S.C. Kaushik, Akhilesh Arora,(2009) Energy and exergy analysis of single effect and

series flow double effect water–lithium bromide absorption refrigeration systems. 3 2 ( 2 0 0 9 ) 1 2 4 7 – 1 2 5 8

3. Rabah Gomri, Riad Hakimi,(2008)Second law analysis of double effect vapour absorption cooler system 49 (2008) 3343–3348.

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4. Lee FS, Sherif SA. Thermodynamic analysis of a lithium bromide/water absorption system for cooling and heating applications. Int J Energy Res2001;25:1019–31.

5. Ravikumar T.S., Suganthi L. and Anand A.Samuel Exergy Analysis Of Solar Assisted Double Effect Absorption Refrigeration System Renewable Energy, Vol. 14, Nos. 1-4, pp. 55-59, 1998

6. M.M. Talbi, B. Agnew Exergy analysis: an absorption refrigerator using lithium bromide and water as the working fuids. Applied Thermal Engineering 20 (2000) 619±630

7. B. Chaouachi and S. Gabsi Design and Simulation of an Absorption Diffusion Solar Refrigeration Unit. American Journal of Applied Sciences 4 (2): 85-88, 2007 ISSN 1546-9239

8. Sushil Kumar Singh, L .P. Singh, Vijendra K.Kushwaha & Vivek Kumar Analytical Study Of A Solar Absorption Refrigeration System. Engineering Research And Development (Ijmperd) Issn(P): 2249-6890; ISSN(E): 2249-8001.

9. R Shankar And T Srinivas Development and analysis of a new integrated powerand cooling plant using LiBr–H2Omixture. Vol. 39, Part 6, December 2014, pp. 1547–1562. Indian Academy of Sciences.

10. Dillip Kumar Mohanty Abhijit Padhiary Thermodynamic Performance Analysis of a Solar Vapour Absorption Refrigeration System. International Journal of Enhanced Research in Science Technology & Engineering, ISSN: 2319-7463 Vol. 4 Issue 4, April-2015, pp: (45-54), Impact Factor: 1.252, Available online at: www.erpublications.com.

11. Subhash Kumar, Dr.R.R Arakerimath Comparative Study on Performance Analysis of Vapour Absorption Refrigeration System Usingvarious Refrigerants. IPASJ WebSite: http://www.ipasj.org/IIJME/IIJME.htm Email: editoriijme@ipasj.org ISSN 2321-6441

12. R. Fathi et S. Ouaskit Performance of a Solar LiBr - Water Absorption Refrigerating Systems. Rev. Energ. Ren. : Journées de Thermique (2001) 73-78 73

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