GB2114671A - Converting thermal energy into another energy form - Google Patents

Abstract

Liquid working fluid is pumped (and thereby pressurized) to a heater where it is heated without change of phase. Thereafter the heated pressurized liquid is supplied to an expansion machine wherein it flashes into its vapour phase and thereby operates the machine to provide the other energy form. The machine is capable of operating with wet working fluid and of progressively drying the fluid during expansion e.g. a rotary- vane or screw-type positive displacement machine, a two-phase turbine at a MHD device. Many examples of suitable working fluids are given.

Description

SPECIFICATION Converting thermal energy The present invention refers to a method of and apparatus for converting thermal energy into other forms of energy.

With the current and projected energy situation, efforts are increasingly being made to utilize sources of energy such as low-temperature industrial waste gases and liquids, geothermally heated water and the like, all of which sources were regarded as marginal and economically unfeasible for power generation as recently as ten years ago, when fossil fuel was still relatively inexpensive. Today, processes are being developed and apparatus devised which can definitely be regarded as profitable propositions.

Most of these processes are thermodynamically based on the well-known Rankine cycle and comprise a shaftpower-producing heat engine utilizing the expansive properties of gases or vapours. In all such engines an important feature of the work-producing process is that the vapour or gas should remain in the same phase throughout expansion and that the formation of liquid during expansion be avoided, because most mechanical expanders such as turbines and reciprocators do not operate well when liquid is present. Steam engines, which operate on a variety of modifications of the basic Rankine cycle to produce power, often generate a certain amount of moisture during the expansion process, either because the steam is initially wet or because, due to the thermodynamic properties of steam, the expanding vapour becomes wetter during the expansion process.In such cases, the engine is always made to minimise the moisture formation in the expander, either by superheating the steam, flashing it to a lower pressure before it enters the expander, or by separating off excess moisture at intermediate stages of the expansion princess. In recent years an important method of reducing the moisture content of expanding vapours in Rankine-cycle engines has been to use heavy molecular weight organic fluids in place of steam.Such engines, as manufactured for example, by Ormat in Israel, Thermoelectron, Sundstrand, GE, Aerojet and other companies in the U.S.A., IHI and Mitsui in Japan, Société Bertin in France, Dornier in Germany, and other companies in Italy, Sweden and the Soviet Union, all have the important feature in their cycle of operation that there is virtually no liquid phase formed in the expander. This permits higher turbine efficiencies than is possible with steam and constitutes a major reason for their good performance in low-temperature power systems used for the recovery of waste heat and geothermal energy.

However, Rankine-cycle-based processes still suffer from a number of drawbacks which impair their efficiency; thermal energy is consumed not only to raise the liquid temperature up to the boiling point, but also beyond that, along the entire evaporation portion of the cycle. Indeed, when organic working fluids are used, almost invariably they leave the expander in the superheated state and have to be desuperheated in an enlarged condenser. Although part of the abstracted desuperheat can be recycled to preheat the compressed liquid, this requires an additional heat exchanger known as a regenerator and while the above disadvantages can be circumvented to some degree by super-critical heating, such a step has to be paid for in greatly increased feed-pump work, which again reduced cycle efficiency.Also, the non-uniform rise of temperature of the working fluid during the heating process in the boiler makes it impossible to obtain a high cycle efficiency and to recover a high percentage of available heat simultaneously when the heat source is a single-phase fluid such as a hot gas or hot liquid stream.

Clearly, it is desirable to overcome the drawbacks and deficiencies of the Rankine-cycle prior art and to provide a method which requires heating of the working liquid only up to its boiling point, evaporation being effected by flashing during the expansion portion of the cycle. This dispenses with the need for a regenerator and permits a higher overall conversion of available heat to power from singlephase fluid streams. For low-temperature heat sources, which comprise the majority of industrial waste heat, solar ponds, geothermally-heated water and the like, this is substantially more cost-effective than the best Rankine-cycle base apparatus. Briefly, a solar pond is a shallow body of water with an upper layer of non-saline water and a lower layer of brine. The latter is heated to temperatures as high as 950 by the sun's radiation and heat can be abstracted from this brine.

According to the present invention there is provided a method of converting thermal energy into another energy form, comprising the steps of providing a liquid working fluid with said thermal energy, substantially adiabatically compressing the working fluid, substantially adiabatically expanding the hot compressed working fluid by flashing to yield said other energy form in an expansion machine capable of operating with wet working fluid and of progressively drying said fluid during expansion, and condensing the exhaust working fluid from the expansion machine.

Further according to the present invention there is provided apparatus for converting thermal energy into another energy form comprising means for supplying a liquid working fluid with said thermal energy, pump means for substantially adiabatically compressing the working fluid, expander means for substantially adiabatically expanding the hot working fluid by flashing to yield said other energy form, said expander means being capable of operating with wet working fluid and of progressively drying said working fluid during expansion and condensing the exhaust working fluid from the expansion machine.

The invention will now be described, by way of example, in connection with reference to the accompanying diagrammatic drawings, in which: Fig. 1 is a T-s (Temperature-Entropy) diagram of a Rankine cycle using steam; Fig. 2 is a T-s diagram of a Rankine cycle using an organic fluid; Fig. 3 is a block diagram of the mechanical components using to produce the cycle indicated in Fig. 2; Fig. 4 is a T-s diagram similar to that of Fig. 2, but with rejected desuperheat used to preheat the compressed liquid; Fig. 5 is a block diagram showing the use of a regenerator; Fig. 6 is a T-s diagram of the ideal Carnot cycle; Fig. 7 illustrates the cooling of a steam of hot liquid or gas going to waste; Fig. 8 shows how this cooling line is matched to the heating portion of the cycle in Figs. 1,2 and 4; Fig. 9 is similar to Fig. 8, but indicates a more desirable matching than that of Fig. 8;; Fig. 10 shows how this cycle can be conceived as a series of infinitesimal Carnot cycles; Figs. 12 and 1 3 illustrate previous attempts to improve the Rankine cycle for recovering power from constant phase heat streams; Figs. 14 and 15 are T-s diagrams including the saturation envelope, explaining the "wet-vapour" cycle in accordance with the invention in greater detail; Fig. 1 6 is a block diagram of the mechanical components operable on a T-s diagram as in Fig. 14; Fig. 1 7 is a T-s diagram of the cycle in accordance with the invention when used in conjunction with a compound liquid-metal/volatile-liquid working fluid as in MHD applications; Fig. 1 8 is a T-s diagram of a more practical form of the "wet-vapour" cycle; and Fig. 19 is a block diagram of the mechanical components used to produce a T-s diagram as in Fig.

18.

The method according to the present invention, which is suitable for constant-phase sources of thermal energy, i.e., sources that, upon transferring their thermal energy to the working fluid, do not change phase, is best understood by a detailed comparison with the well-known Rankine cycle from which it differs in essential points, although the mechanical components with which these two different cycles can be realized, may be similar.

The basic Rankine cycle is illustrated in T-s diagrams in Fig. 1 for steam and in Fig. 2 for an organic working fluid, such as is used, e.g., in the Ormat system.

The sequence of operations in Fig. 1 is liquid compression (1It2), heating and evaporation (2 < 3), expansion (3o4) and condensation (4e1). It should be noted that in this case the steam leaves the expander in the wet state. As to Fig. 2, the properties of organic fluids are such that in most cases the fluid leaves the expander in the superheated state at point 4, so that the vapour has to be desuperheated (4It5) as shown in Fig. 2. Desuperheating can be achieved within an enlarged condenser.

The mechanical components which match this cycle are shown in Fig. 3 and include a feed pump 20, a boiler 22, and expander 24 (turbine, reciprocator or the like), and a desuperheater-condenser 26.

Fig. 4 indicates how the rejected desuperheat (4e5 in Fig. 2) can be utilized to improve cycle efficiency by using at least part of it to preheat the compressed liquid (2It7), thereby reducing the amount of external heat required. Physically, this is achieved by the inclusion in the circuit, of an additional heat-exchanger 28, known as a regenerator, as shown in Fig. 5.

In T-s diagrams such as those used throughout this specification, the area delimited by the lines joining the state points in a cycle represents the work done.

Now, it is a well-known consequence of the laws of thermodynamics that, when heat is obtained from a constant temperature or infinite heat source, the ideal heat-engine cycle is the Carnot cycle shown in Fig. 6.

Examining Figs. 1, 2 and 4, it is seen that the Rankine cycle comes close to the ideal Carnot cycle largely because of the large amount of heat supplied at constant temperature during the evaporation process indicated in Fig. 1. This process takes place in the boiler and, in nearly all cases, the amount of heat supplied, is much larger than that necessary to raise the temperature of the working fluid to its boiling point. It follows that evaporation of the fluid is a key feature of the sequence of processes involved in an Ormat-type system and, indeed, any Rankine cycle. However, when heat is not supplied from an infinite or constant-temperature heat source, the Carnot cycle is not necessarily the ideal model. Consider a flow of hot liquid or gas going to waste. If this flow is cooled, the heat transferred from it is dependent on its temperature drop as shown in the cooling curve on temperature vs. heattransferred coordinates in Fig. 7.

Matching of the cooling of a constant-phase fluid flow to the boiler heating process 22 in Figs. 1 and 2, and 73 in Fig. 4, is shown in Fig. 8. In this case, it can be seen that the large amount of heat required to evaporate the working fluid in the Rankine-cycle boiler limits the maximum temperature which the working fluid can attain to a value far less than the maximum temperature of the fluid flow being cooled.

A much more desirable conversion of heat to mechanical power could be attained if the working fluid heated in the boiler followed a temperature versus heat-transferred path which exactly matches that of the cooling fluid flow which heats it. The ideal case for this is shown in Fig. 9, which would result in an ideal heat-engine cycle shown on T-s coordinates in Fig. 10. At first sight, this appears to be contrary to the concept of a Carnot cycle as the ideal. However, it must be appreciated that the Carnot cycle is only ideal for a constant-temperature or infinite heat source, whereas here the heating-source temperature changes throughout the heat-transfer process. Another way of visualizing the cycle shown in Fig. 10 is to consider it as a series of infinitesimal Carnot cycles, each receiving heat at a slightly different, but constant, temperature, as shown in Fig. 11.

For such a cycle, the large evaporative heat required in an Ormat-type (Rankine) cycle is no advantage. Improvements have, therefore, been proposed to the latter, such as superheating the vapour after evaporation is complete, to obtain the cycle shown in Fig. 12, or to raise the feed-pump exit pressure to the super-critical level, to obtain the cycle shown in Fig. 13, as both these effects bring the Rankine cycle shape nearer the ideal. However, both these cycles usually require a large amount of desuperheat, which means a large regenerator if efficiences are to be maintained, and this means a more expensive system. Both these cycles normally expand the working fluid as dry vapour, although some have been suggested where the vapour may become slightly wet during the expansion process.It is not so well known that the supercritical cycle usually requires a very large amount of feed-pump work, especially if there is little desuperheat in the vapour leaving the expander, and this reduces the cycle efficiency.

The cycle according to the present invention is that shown on temperature-entropy coordinates in Figs. 14 and 15, and is seen to consist of liquid compression adiabatically in the cold, saturated, state (1It2) as in the Rankine cycle, heating in the liquid phase only by heat transfer from the thermal source at approximately constant pressure substantially to the boiling point (2 < 3), expansion (3It4) by phase change from liquid to vapour again, substantially adiabatically, down to the approximate pressure thereof when introduced to the pump as already described and, possibly, condensation back to state point 1. It can be seen from Fig. 1 5 that, for some organic fluids, expansion leads to completely dry vapour at the expander exit.The components needed for the cycles of Fig. 14 and Fig. 1 5 are shown in Fig. 16.

While these components are similar to those used in the basic Rankine cycle, (except for the smaller condenser 30), the wet-vapour differs radially from the Rankine cycle in that, unlike in the latter, the liquid heater should operate with minimal or preferably no evaporation, and the function of the expander differs from that in the Rankine system as already described. If compared with the supercritical Rankine cycle shown in Fig. 13 where heating is equally carried out in one phase only, the cycle according to the invention still differs in that it is only in this novel cycle that the fluid is heated at subcritical pressures, which is an altogether different process, and the expander differs from the Rankine-cycle expander as already described.Should this cycle be used with a compound liquidmetal/volatile-liquid working fluid, as in MHD (magneto-hydrodynamic) applications, then, on temperature-entropy coordinates, the expansion line will slope more to the right as shown on Fig. 1 7 due to the large heat capacity of the liquid metal. The volatile fluid will thus be much drier at the expander exit.

The cycle according to the invention confers a number of advantages over the Rankine cycle even in such an extremely modified form of the latter as in the supercritical system of figure 13. These advantages are: 1) It requires little or no desuperheat and hence no regenerator; 2) It requires less feed-pump work than a super-critical Rankine cycle such as indicated in Fig. 13; 3) It permits higher cycle efficiencies in the case of constant-phase heat flows; and 4) It enables more heat to be transferred to the working fluid from constant-phase flows where there are no limits to the temperature to which the constant-phase flow can be cooled, than is possible with Rankine cycles.

The basic "wet-vapour" cycle in accordance with the invention so far described can be further improved if the following points are taken into account: 1) The basic cycle requires a volume expansion ratio in passing from saturated liquid to the final vapour state of the order of 10 times the expansion ratio required in a Rankine cycle operating between the same temperature limits. This may lead to difficulties in the mechanical design of certain types of expander.

2) Flashing from the purely liquid condition is relatively slow in its initial stages before sufficient vapour has formed to permit a large surface of contact between the liquid and vapour phases. Thus the cycle and components as described with reference to Figs. 14 to 1 7 could be inefficient due to incompleteness of the flashing process in the expander leading to a large loss of recoverable energy from the expander through the fliud leaving it as a mixture of superheated liquid and low pressure vapour.

Both of these points can be met by carrying out an initial stage of the expansion in a flashing chamber prior to the production of work in the expander as indicated in process 3-4 on the T-s diagram in Fig. 18 and in item 32 in the block diagram of components shown in Fig. 1 9. By this means the first part of the expansion is not required to take place at a rate dictated by the required speed of rotation of the expander and sufficient time can be allowed for this process in the flashing chamber in order to achieve a well mixed liquid/vapour combination at equilibrium conditions before any further expansion begins. In addition, the volume expansion ratio of the expander is thereby substantially reduced making the task of designing it much easier.

Superficially it would appear that such a modification of the basic "wet-vapour" cycle may lead to such a loss of available energy as to eliminate its theoretical advantage over the Rankine cycle. Closer examination of the expansion process shows however that the penalty in lost power imposed by such a modification is quite small, being of the order of only a few percent although the exact amount depends on the working fluid and the temperature range through which it is expanded in the flashing chamber.

The reason for this is that the initial liquid voluine is small relative to the final volume attained by the vapour. Since flow work is equal to the integrated product of pressure drop times volume, an expansion ratio of 3 or more in the initial stages is responsible for only a fraction of the work accounted for by a similar expansion ratio in the final stage of expansion. This has been verified by exact calculation.

Calculations using a computer programme have been completed on a study of power recovery from Geothermal hot water at 1 000C. These were compared with a Rankine cycle system. Assumptions for both were identical except that the Rankine turbine efficiency was assumed to be 85% and that of a suitable screw expander 80%. No allowance was made for circulating the geothermally heated water but this would be almost the same for both with the power loss for the Rankine cycle possibly slightly larger than for the wet vapour system. Hot water flow rate = 75 kg/s.In all cases refrigerant R1 14 was chosen as the working fluid and all analyses were optim-ised: Power from Rankine system = 717 kWe Wet Vapour System

Flashing Volumetric Ratio 1.0 2.0 3.0 9.57 Expander Volumetric Ration 32.8 16.5 11.0 3.5 Power Output kWe 1138 1105 1059 700 Percentage Improvement over Rankine System 59% 54% 48% -2.4% Percentage Power Loss due to flashing 0.0 2.9 6.9 38.0 In these cases the expander volumetric ratio is so low that doubling the fluid volume in flashing makes the entire expansion feasible in a single stage screw expander for a loss of less than 3% of the power. By trebling the volume in flashing the expansion could be achieved even in a single stage vane expander if one could be built for this output.

For higher overall volumetric ratios the power loss penalty would be even less. It will be noted that even the figures for the last column where the expander volumetric ratio is extremely modest, the deterioration in relation to the Rankine system is very slight.

To assess the possible advantages of such a cycle over Rankine alternatives, a highly detailed study of recoverable power from hot-rock, geothermally-heated, water was carried out, assuming a water flow rate of 75 kg/sec. Many working fluids were considered and for each of these, all systems were fully optimized, using a computer programme developed over a period of 10 years, which programme includes a detailed account of all internal losses and inefficiencies. The results of this study are summarized in the following table.

Power Output Estimated Cost Per Attainable, kWe Unit Output, /kWe Geothermally Best Best Heated Water, Rankine Wet Vapour Rankine Wet Vapour Inlet Temp. "C. Cycle Cycle Cycle Cycle 150 2600 3500 380 350 170 4070 4780 330 290 190 5470 6160 290 250 210 6920 7420 280 230 It is clearly seen that the new "wet-vapour" cycle offers prospects of significantly greater power recovery at a tower cost per unit output than any Rankine cycle system.

Further studies were carried out on very low-temperature systems as used for power recovery from solar ponds and collectors and here outputs nearly three times as great as those from Rankine Cycle systems were shown to be possible.

A further advantage of the "wet-vapour" cycle according to the invention will be explained in the following: Many industrial processes, particularly in chemical plants, terminate with large quantities of hot liquids which have to be cooled. In such plants, large heat-exchangers are required to remove the heat and these can, of course, form boilers for power plants in accordance with the invention as hereinbefore described. An alternative way of using this process heat is to dispense with the boiler and use the hot liquid itself as the working fluid so that it enters the expander either directly or through a flashing chamber and produces work while expanding and cooling.The final heat extraction still requires a pump to recompress the liquid and a condenser after the expansion stage, but such a process "wet-vapour" expander system will be cheaper than an installed heat engine, in that it requires no boiler or liquid heat and it will be more efficient in that no temperature drop is required to transfer the heat from one fluid to the other in the boiler or heater.

This principle may also be used with a wet-vapour expander in recovering power from hot-rock geothermal or other thermal sources, when the circulating fluid need not be limited to water.

As already mentioned, one of the fundamental differences between the "wet-vapour" cycle of the present invention and the Rankine cycle resides in the fact that, with the former, the change of phase during the expansion process is a most essential feature, whereas in the latter it is to be avoided as far as possible. Moreover, when moisture does form in a Rankine-cycle system, the vapour becomes progressively wetter during the expansion process, while in the "wet-vapour" cycle according to the invention, the vapour becomes drier as expansion proceeds.

As a consequence of the above, conventional turbines and reciprocators are not suitable for the expansion phase of the "wet-vapour" cycle according to the invention, since liquid droplets erode turbine blades and reduce the aerodynamic efficiency of the turbine, while washing the lubricating oil off the cylinder walls of reciprocating expanders, thus promoting wear and seizure of the mechanism.

Alternative machines exist which can be used for this purpose; the following are examples: 1) Positive-displacement machines such as rotary-vane and screw expanders. The pressure of liquid in these should promote lubrication and reduce leakage. Small machines of the vane type with very high efficiencies are available; 2) Two-phase turbines; and 3) MHD (Magnetohydrodynamic) ducts through which the working fluid flows. In this case, the fluid comprises a mixture of a volatile liquid which changes its phase and a non-volatile liquid such as a liquid metal or other conducting fluid, which is propelled through a rectangular section duct by the expanding volatile liquid. If two opposite walls of the duct generate a magnetic field between them and the other pair of opposite walls contain electrical conductors, direct generation of electricity by this means is possible.

A variety of working fluids have been examined for use in the proposed "wet-vapour" cycle and "wet-vapour" process expansion systems, including Refrigerants 11, 12, 21, 30, 113, 114, 115, toluene, thiophene, n-pentane, pyridene hexafluorobenzene, FC 75, monochlorobenzene and water. The main disadvantage of water is the very high volume ratios required in the expander, but R 11, R 12 and most of the other refrigerants as well as n-pentane give much more desirable volume ratios which can be attained in one, two, three or four stages of expansion, dependent on the temperature limits of operation.

In order to increase system efficiency, the system may advantageously include features to accelerate the flashing process both in the expander and in the flashing chamber, if fitted. These features, per se known, include turbulence promoters to impart swirl to the fluid before it enters the expander; seeding agents to promote nucleation points for vapour bubbles to form in the fluid; wetting agents to reduce the surface tension of the working fluid and thereby accelerate the rate of bubble growth in the initial stages of flashing, and combinations of all or selected ones of these features.

In addition, mechanical expander efficiencies can be improved by the addition of a suitable lubricant to the working fluid to reduce friction between the contacting surfaces of the moving working parts.

It will be appreciated that although the working fluid is preferably organic, suitable inorganic fluids can also be used. The thermal source, although generally liquid from the point of view of keeping the size of heat exchangers within reasonable limits, can also be a vapour or a gas.

It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments and that the present invention may be embodied in other specific forms without departing from the essential attributes thereof, and it is, therefore, desired that the present embodiments be considered in all respects as illustrative and not restrictive, reference being made to the appended claims, rather than to the foregoing description, and all changes which come with the meaning and range of equivalency of the claims are, therefore, intended to be embraced therein.

Claims (25)

1. A method of converting thermal energy into another energy form, comprising the steps of providing a liquid working fluid with said thermal energy, substantially adiabatically compressing the working fluid, substantially adiabatically expanding the hot compressed working fluid by flashing to yield said other energy form in an expansion machine capable of operating with wet working fluid and of progressively drying said fluid during expansion, and condensing the exhaust working fluid from the expansion machine.

2. A method according to claim 1 wherein flashing is initiated prior to admission to the expansion machine.

3. A method according to claim 1 or claim 2, wherein the condensate is recirculated for recompression.

4. A method according to claim 3 wherein the working fluid is adiabatically compressed from the cold saturated state and heated by heat transfer from a source of thermal energy.

5. A method according to any one of the preceding claims wherein the expansion machine is a rotary vane machine.

6. A method according to any of claims 1 to 4 wherein the expansion machine is a screw expander.

7. A method according to any one of claim s 3 to 6 wherein the working fluid is an organic or suitable inorganic fluid.

8. A method according to claim 7, wherein said organic working fluid is selected from the group including refrigerants 1 12,21, 30, 1 113, 114, 115, toluene, thiophene, n-pentane, pyridene, hexafluorobenzene, FC 75, monochlorobenzene and water.

9. A method according to claim 3, or claim 4 wherein said working fluid is a mixture of a liquid, electrically-conducting substance and a volatile liquid and said working fluid is adiabatically expanded in a magneto-hydrodynamic duct.

10. A method according to any one of the preceding claims further comprising the step of accelerating said flashing process by inducing turbulence in said working fluid upstream of the inlet of said expansion machine.

11. A method according to any one of preceding claims further comprising adding seeding agents to promote nucleation points for vapour bubbles to form in the fluid upstream of the inlet of the expansion machine.

1 2. A method according to any one of the preceding claims further comprising adding wetting agents to reduce the surface tension of the working fluid and thereby accelerate the rate of flashing.

13. A method according to any one of the preceding claims comprising adding lubricants to the working fluid to improve the efficiency of the expansion machine.

14. A method of converting thermal energy into another energy form, comprising substantially adiabatically compressing an organic working fluid in a cold, saturated, state, heating the working fluid by heat transfer from the source of said thermal energy, initially flashing the working fluid and continuing flashing of the wet working fluid in a screw expander wherein the wetness fraction is decreased and whereby shaft power is produced, condensing the exhaust from the screw or other positive displacement expander and returning the condensate to the compression stage.

1 5. A method of converting thermal energy into another form of energy, comprising the steps of providing a liquid working fluid to be exposed to the source of said thermal energy, substantially adiabatically compressing said working fluid in the cold, saturated, state thereof, heating the working fluid by heat transfer from said source at approximately constant pressure substantially to the boiling point of said working fluid, substantially adiabatically expanding the heated working fluid down to the approximate pressure thereof immediately prior to said compression, said working fluid being thereby flashed from the liquid phase to the vapour phase, yielding energy, condensing said working fluid from the vapour phase to the liquid phase thereof and recirculating the condensed working fluid to the commencement of the compression stage.

1 6. Apparatus for converting thermal energy into another energy form comprising means for supplying a liquid working fluid with said thermal energy, pump means for substantially adiabatically compressing the working fluid, expander means for substantially adiabatically expanding the hot working fluid by flashing to yield said other energy form, said expander means being capable of operating with wet working fluid and of progressively drying said working fluid during expansion, and condensing the exhaust working fluid from the expansion machine.

1 7. Apparatus according to claim 16, comprising means for initiating said flashing upstream of the expander means.

1 8. Apparatus according to claim 16 or claim 1 7, comprising means for recirculating the condensate to the inlet of the pump means.

1 9. Apparatus according to claim 1 8, comprising heat-exchange means for transferring said thermal energy from a source to the working fluid as a cold, saturated, state.

20. Apparatus according to any one of claims 1 6 to 1 9 wherein the expander means is a rotary vane machine.

21. Apparatus according to any one of claims 16 to 19 wherein the expander means is a screw expander.

22. Apparatus according to claim 18 or claim 1 9 wherein the expander is a magnetohydrodynamic duct.

23. Apparatus for converting thermal energy into electrical power comprising pump means for adiabatically compressing a cold, saturated, organic working fluid and delivering the compressed working fluid to a heat-exchanger, the hot pass of which receives a flow of geothermally or otherwise heated liquid, vapour or gas, a flashing chamber wherein the heated working fluid is flashed to a degree such that a minor proportion of the overall expansion ratio is expended therein, an expander machine in which the flashing is substantially completed by adiabatic expansion of the working fluid, said expander machine being operable with the working fluid in an at least initially wet state, a condenser for condensing the exhaust from the expander machine and means for returning the condensate to the inlet of the pump means.

24. A method of converting thermal energy to another energy form substantially as hereinbefore described with reference to any one of Figs. 1 3 to 1 9 of the accompanying drawings.

25. Apparatus for converting thermal energy to another energy form substantially as hereinbefore described with reference to any one of Figs. 1 3 to 19 of the accompanying drawings.