Theoretical Rankine power cycle efficiencies νR and the pressure (PR) have been presented for Rankine power cycles operating on R502. These values are listed in tabular form for temperature drops of 5–75°C and for boiler temperatures 35–80°C in 5°C increments. A composite graph showing the relationship between νR, TBO, (PR) and temperature drop (TBO - TCO illustrates the feasible operating range for R502 power cycle systems. The derived thermodynamic data can be used for the rapid preliminary design of Rankine power cycle systems operating on R502.

Theoretical Rankine power cycle efficiencies νR and the (PR) have been presented for Rankine power cycles operating on R142b. These values are listed in tabular form for temperature drops of 5–75°C and for boiler temperatures 25–125°C in 5°C increments. A composite graph showing the relationship between νR, TBO, (PR) and temperature drop (TBO − TCO) illustrates the feasible operating range for R142b power cycle systems. The derived thermodynamic data can be used for the rapid preliminary design of the Rankine power cycle systems operating on R142b.

Theoretical Rankine power cycle efficiencies νR and the pressure (PR) have been presented for rankine power cycles operating on R22. These values are listed in tabular form for temperature drops of 5–75°C and for boiler temperatures 40–85°C in 5°C increments. Composite graph showing the relationship between νR, TBO, (PR) and temperature drop (TBO - TCO) illustrates the feasible operating range for R22 power cycle systems. The derived thermodynamic data can be used for the rapid preliminary design of the Rankine power cycle systems operating on R22.

Theoretical Rankine coefficients of performance and the compression ratios have been presented for heat pump systems operating on R503. These values are listed in tabular form for temperature lifts of 5–75°C and condensing temperatures of 5–18°C in one degree increments. A composite plot has been drawn to illustrate the feasible operating range of R503 heat pump systems.

Theoretical Rankine coefficients of performance and the compression ratios have been presented for heat pump systems operating on R1270. These values are listed in tabular form for temperature lifts of 5–75°C and condensing temperatures of 12–90°C in one degree increments. A composite plot has been drawn to illustrate the feasible operating range of R1270 heat pump systems.

Theoretical Rankine coefficients of performance and the compression ratios have been presented for heat pump systems operating on R503. These values are listed in tabular form for temperature lifts of 10–55°C and condensing temperatures of 7–30°C in one degree increments. A composite plot has been drawn to illustrate the feasible operating range of R744 heat pump systems.

Theoretical Rankine coefficients of performance and the compression ratios have been presented for heat pump systems operating on R13. These values are listed in tabular form for temperature lifts of 5–75°C and condensing temperatures of 6–26°C in one degree increments. A composite plot has been drawn to illustrate the feasible operating range of R13 heat pump systems.

Theoretical Rankine coefficients of performance and the compression ratios have been presented for heat pump systems operating on R23. These values are listed in tabular form for temperature lifts of 5–75°C and condensing temperatures of 5–24°C in one degree increments. A composite plot has been drawn to illustrate the feasible operating range of R23 heat pump systems.

Theoretical Rankine coefficients of performance and the compression ratios have been presented for heat pump systems operating on R170. These values are listed in tabular form for temperature lifts of 5–75°C and condensing temperatures of 6–31°C in one degree increments. A composite plot has been drawn to illustrate the feasible operating range of R170 heat pump systems.

Presently out of the total energy consumption, a large share of energy is being used by refrigeration and air conditioning equipments. The present study is based on literature review on the refrigeration systems, currently used refrigerant–absorbent pairs and also on different sources of energy. The basis of this study is to know about the user friendly softwares used for the simulation techniques and also on the scope of different alternative forms of energy as a source to generator. The effects of operating temperature, effectiveness of heat exchangers and choice of working fluid on the systems were studied. It is evident from the studies that the cycle performance (COP) improves with increasing generator and evaporator temperatures, but reduces with increasing the absorber and condenser temperatures. The use of heat exchangers improves the overall performance of the system, especially solution heat exchanger (SHE). It is also evident that solar energy obtained in the range of about 100 °C is having good potential to supply sufficient energy to the generator for absorption–refrigeration cycles.

Performance data have been obtained on a small glass absorption heat-pump operating with water as a working fluid in combination with both single- and double-salt solutions as the absorbent. The salts were lithium chloride, lithium bromide, lithium iodide and mixtures of lithium chloride and lithium bromide, and lithium chloride and lithium iodide. The experiments were carried out with a delivery temperature of 70°C and an initial generator temperature of about 100°C.

An experimental study has been carried out on a continuously operated pilot fractional distillation column equipped with an external heat pump. The distillation column was a 153 mm diameter stainless steel unit containing fourty-four sieve plates. An ethanol-water mixture was fed to the column and the heat pump working fluid was R114. The actual coefficient of performance (COP)A of the heat pump increased with an increase in the mass flow rate of the working fluid. A maximum value of 4.5 was obtained with a gross temperature lift of 45°C. The performance of two reciprocating compressors was compared. A heat pump effectiveness factor of 0.8 was achieved. A maximum relative contribution of the heat pump of 65 per cent was obtained with minimum temporary insulation. With good insulation it is estimated that the relative contribution of the heat pump should exceed 80 per cent at the design feed rate. No control problems were encountered in the experiments.

Derived thermodynamic design data including Carnot coefficients of performance, enthalpy based coefficients of performance and flow ratios for possible combinations of operating temperatures for absorption heat pump systems operating on water-lithium chloride for heating are presented. The variations of the derived data with operating temperatures are illustrated graphically. The data obtained for the water-LiCl pair are compared with published data for the water-LiBr pair for identical conditions of temperatures.

Absorption heat pumps and coolers can be satisfactorily operated using the water—lithium bromide—ethylene glycol ternary system with an ethylene glycol to water mole ratio of 1/15. This gives a high coefficient of performance and a lower risk of crystallization.

Derived thermodynamic design data, including Carnot coefficients of performance, enthalpy based coefficients of performance and flow ratios for possible combinations of operating temperatures, are presented for absorption heat transformers operating on water-lithium chloride. The variations of the derived data with operating temperatures are graphically illustrated. The data obtained for the water-LiCl pair are compared with published data for the water-LiBr and water-CaCl2 pairs for identical temperature conditions.

Theoretical Rankine coefficients of performance and the compression ratios have been presented for heat pump systems operating on R504. These values are listed in tabular form for temperature lifts of 10–75°C and condensing temperatures of 15–50°C in 5°C increments. A composite plot has been drawn to illustrate the feasible operating range of R504 heat pump systems.

Theoretical Rankine coeffiecients of performance and compression ratios have been presented for heat pumps systems operating on R40. These values are listed in tabular form for temperature lifts of 10–75°C and condensing temperatures of 10–75°C in 5°C increments. A composite plot has been drawn to illustrate the feasible operating range of R40 heat pump systems.

The problems in matching a heat driven absorption heat pump to a distillation process in heat pump assisted distillation are discussed. The performance of an absorption system is a function of the temperatures in the evaporator, the condenser, the absorber and the generator and the ratio of the mass flow rate in the secondary circuit to the mass flow rate in the primary circuit. In absorption systems design choices are limited by the Gibbs phase rule. Plots are given of the coefficient of performance against the temperatures of the top and bottom products and also against the energy saved.

The operating efficiency of an absorption heat pump is critically dependent on the chemical, thermophysical and thermodynamic properties of the working fluid, the absorbent and their solution. The desirable properties are discussed in the light of the operating parameters and the thermodynamic limits. Deviations from ideality are considered with specific reference to water/salt systems. Plots of the heat of hydration and heat of solution against the effective ionic radius, the lowering of vapour pressure against the heat of solution and the solubility against the melting point have been made for aqueous alkali metal halide solutions. It is demonstrated that an optimisation procedure is necessary to select suitable working fluid-absorbent combinations from the hundreds of possible combinations based on the operating conditions and the field of application.