THERMAL TO MECHANICAL ENERGY CONVERSION METHOD USING A RANKINE CYCLE EQUIPPED WITH A HEAT PUMP

Abstract

The invention relates to a thermal to energy conversion method and system using a Rankine cycle equipped with a heat pump, wherein heat pump (2) is integrated in the Rankine cycle.

Description

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to the field of thermal to mechanical energy conversion and in particular for ocean thermal energy conversion (OTEC).

2. Description of the Prior Art

Conventional OTEC plants generally operate on a Rankine cycle. French Patent Application 2,981,129 describes the use of a Rankine cycle in the case of OTEC. FIG. 1 shows a block diagram of an OTEC plant operating with a Rankine cycle and comprising an exchanger 1 as the heat source SC (surface ocean water) and a secondary heat source 2. The secondary heat source allows the thermodynamic cycle to be improved. The system comprises an exchanger 5 as the cold source SF from cold seawater taken at depth. The circuit of the motive fluid, ammonia in the present example, comprises a pump 6 and a turbine 3 driving a generator 4 for conversion to electrical energy.

French Patent Application 2,981,129 also discloses a variant of this cycle with a heat pump as the secondary heat source for overheating the working fluid. Addition of a heat pump notably allows the net power generated by the system to be increased. A heat pump (PAC) is a thermodynamic device allowing transfer of heat from a cooler medium, or of the same temperature (and thus to cool it), to a warmer medium, or of the same temperature (and thus to heat it), whereas heat diffuses naturally from the warmest to the coolest medium until equality of temperature is reached. Therefore, for the Rankine cycle, several equipments are added to the pump which are a heat source-working fluid exchanger, a compressor, an exchanger between the working fluid of the heat pump and the working fluid of the Rankine cycle, and a valve. FIG. 2 illustrates an example of an OTEC plant operating on a Rankine cycle equipped with a heat pump. The circuit of the Rankine cycle is identical to the previous one and comprises an exchanger 1, a turbine 3, an exchanger 5 and a pump 6, secondary heat source 2 having of a heat pump. The heat pump comprises an exchanger 10 for heat exchange with the warm heat source, a compressor 7, an exchanger 8 for heat exchange with the working fluid of the Rankine cycle and a valve 9. Heat exchanger 10 undergoes corrosion and may get clogged up due to biofouling (incrustations on solid matter immersed in an aquatic environment from living species or developed by aquatic living species such as bacteria, protists, plants and animals. This equipment therefore requires significant maintenance.

SUMMARY OF THE INVENTION

The invention relates to a thermal to mechanical energy conversion method wherein a working fluid is circulated in a closed circuit comprising a circuit according to a Rankine cycle equipped with a heat pump for heating the working fluid vaporized in the Rankine cycle circuit. For the method, the working fluid of the Rankine cycle circuit is circulated in the circuit of the heat pump.

The invention relates to a thermal to mechanical energy conversion method and system using a Rankine cycle equipped with a heat pump, wherein the heat pump is integrated in the Rankine cycle. Thus, a single working fluid is used for the circuit of the Rankine cycle and the circuit of the heat pump, and the circuit of the heat pump requires no exchanger for heat exchange with the heat source.

A particular application of the present invention is to ocean thermal energy and the use of energy obtained from the temperature difference existing in tropical and subtropical regions between surface ocean waters and deep ocean waters, in particular at depths of the order of 1000 m. Surface waters are used for the heat source and deep waters for the cold source of a motive thermodynamic cycle. The temperature difference between the heat source and the cold source is low and the expected energy yields are also low.

According to the invention, the vaporized working fluid is separated into two portions with a first portion intended for conversion to mechanical energy by the Rankine cycle circuit and a second portion intended for the heat pump.

Advantageously, the first portion is mixed after the stage of conversion to mechanical energy in the Rankine cycle circuit with at least part of the second portion.

Preferably, the following stages are carried out:

• • a) vaporizing the working fluid by thermal exchange with a first heat source;
  • b) separating the vaporized working fluid into two portions;
  • c) heating a first portion by heat exchange with a previously compressed second portion;
  • d) converting part of the thermal energy contained in the first portion into mechanical energy;
  • e) re-forming at least part of the working fluid by mixing at least part of the first and second portions with the second portion being previously expanded;
  • f) condensing at least part of the re-formed working fluid by heat exchange with a second heat source; and
  • g) compressing the condensed working fluid.

According to an embodiment of the invention, the second portion is separated, upstream from the re-forming part of the working fluid, into a liquid phase and a gas phase with the gas phase of the second portion being mixed with the first portion during partially re-forming the working fluid, and the liquid phase of the second portion being mixed with the condensed working fluid.

In a variant, the partially re-formed working fluid is separated into a liquid phase and a gas phase with the gas phase of the working fluid being condensed during the condensation stage, and the liquid phase of the working fluid being mixed with the condensed working fluid.

According to the invention, the heat sources are seawater taken at different depths.

Advantageously, the working fluid comprises ammonia.

Furthermore, the invention relates to a thermal to mechanical energy conversion system comprising a closed circuit wherein a working fluid circulates, the closed circuit comprising a Rankine cycle circuit equipped with a heat pump for heating the vaporized working fluid in the Rankine cycle circuit. In the system, the working fluid of the Rankine cycle circuit circulates in the circuit of the heat pump.

According to the invention, the closed circuit comprises a first separator for separating the working fluid into two portions with a first portion being converted into mechanical energy by the Rankine cycle circuit and a second portion being for the circuit of the heat pump.

Advantageously, the closed circuit comprises, downstream from a means for conversion to mechanical energy in the Rankine cycle circuit, a first mixer for mixing the first portion with at least part of the second portion.

Preferably, the closed circuit comprises successively:

• • a first heat exchanger for vaporizing the working fluid with a first heat source;
  • a separator for separating the vaporized working fluid into two portions;
  • a second heat exchanger for heating a first portion with a second portion compressed by a compressor;
  • a turbine for converting part of the thermal energy contained in the first portion to mechanical energy;
  • a first mixer for mixing at least part of the first and second portions so as to re-form at least part of the working fluid and the second portion being expanded by an expansion means;
  • a third heat exchanger for condensing at least part of the working fluid by a second heat source; and
  • a pump for compressing the condensed working fluid.

Advantageously, the expansion means comprises a valve or a two-phase pump.

According to an embodiment of the invention, the closed circuit comprises, upstream from the first mixer, a second separator for separating the liquid and gas phases of the second portion and, downstream from the third exchanger, a second mixer for mixing the liquid phase with the working fluid at the third exchanger outlet, and the first mixer mixing the gas phase of the second portion with the first portion.

According to a variant embodiment of the invention, the closed circuit comprises, downstream from the first mixer, a third separator for separating the liquid and gas phases of the working fluid at an outlet of the first mixer and, downstream from the third exchanger, a second mixer for mixing the liquid phase with the working fluid at an outlet of the third exchanger with the third exchanger cooling the aqueous phase of the working fluid.

According to the invention, the working fluid comprises ammonia.

Furthermore, the heat sources can be seawater taken at different depths.

BRIEF DESCRIPTION OF THE DRAWINGS

Other features and advantages of the method according to the invention will be clear from reading the description hereafter of embodiments given by way of non limitative example, with reference to the accompanying figures wherein:

FIG. 1, which is already described, is a block diagram of an OTEC plant operating on a Rankine cycle according to the prior art;

FIG. 2, which is already described, is a diagram of an OTEC plant operating on a Rankine cycle equipped with a heat pump according to the prior art;

FIG. 3 is a diagram of a thermal energy conversion system operating on a Rankine cycle equipped with a heat pump according to a first embodiment of the invention;

FIG. 4 is a diagram of a thermal energy conversion system operating on a Rankine cycle equipped with a heat pump according to a second embodiment of the invention;

FIG. 5 is a diagram of a thermal energy conversion system operating on a Rankine cycle equipped with a heat pump according to a third embodiment of the invention;

FIG. 6 is a diagram of a thermal energy conversion system operating on a Rankine cycle equipped with a heat pump according to a fourth embodiment of the invention; and

FIG. 7 is a diagram of a thermal energy conversion system operating on a Rankine cycle equipped with a heat pump according to a variant of the first embodiment of the invention.

DETAILED DESCRIPTION OF THE INVENTION

The invention relates to a method and to a system for converting thermal energy from heat sources to mechanical energy. The heat sources can be for example seawater taken at different depths with the warm source (28° C. for example) taken at the sea surface, and the cold source (4° C. for example) taken at depths close to or greater than 1000 m.

The method and the system are based on the implementation of a thermodynamic cycle using a working fluid. For example, the working fluid can be ammonia (NH₃) indeed, ammonia can be vaporized through heat exchange with a warm source notably seawater because, within a reasonable pressure range, the temperature of the surface ocean water is high enough to allow ammonia vaporization. Similarly, the temperature of the cold source allows condensation thereof. Alternatively, the working fluid can be any organic fluid meeting the temperature/pressure criteria depending on the temperatures of the heat sources.

According to the invention, the thermodynamic cycle corresponds to a Rankine cycle equipped with a heat pump.

A Rankine cycle (FIG. 1) is a cycle wherein the working fluid is successively subjected to the following stages:

• • vaporization, for example by heat exchange with a warm source,
  • expansion, for example by a turbine that converts thermal energy to mechanical energy,
  • condensation, for example by frigories exchange with a cold source, and
  • compression, for example by a pump.

A heat pump (PAC) is a thermodynamic device allowing transfer heat of from a cooler medium, or of same temperature (and thus to cool it), to a warmer medium, or of same temperature (and thus to heat it), whereas heat diffuses naturally from the warmest to the coolest medium until equality of temperature. Therefore, a heat pump comprises several equipments (FIG. 2) which are an exchanger for heat exchange between a heat source and a working fluid, a compressor, an exchanger between the working fluid of the heat pump and the fluid to be heated, and a valve for expanding the working fluid of the heat pump. Adding a heat pump to the Rankine cycle allows overheating the vaporized working fluid before passing it into the turbine. Thus, the net power generated by this method (Rankine cycle+heat pump) is increased in relation to the power generated by the Rankine cycle alone. Net power is understood to be the power generated at the turbine minus the powers consumed by the pump or the compressor.

According to the invention, the heat pump is integrated into the Rankine cycle with the same working fluid being circulated in the components of the circuit corresponding to the Rankine cycle and in those corresponding to the heat pump. The working fluid is thus shared and unique for the thermodynamic cycle of the invention. Thus, the part of the circuit corresponding to the heat pump does not require using a heat exchanger with a warm source (subjected to corrosion and biofouling). Advantageously, the working fluid is separated into two portions with a first portion essentially intended for the thermodynamic stages of the Rankine cycle and a second portion essentially intended for the thermodynamic stages of the heat pump. A working fluid portion is understood to be a part of the working fluid that is used only in part of the thermodynamic circuit according to the invention. The working fluid is subsequently re-formed by means allowing implementation of the mixing and condensation stages, and optionally means allowing implementation of the liquid and gas phase separation stages.

According to a first embodiment of the invention, the fluid is separated into two portions after the stage of vaporization of the working fluid in the Rankine cycle with part of the gaseous working fluid stream being extracted at the evaporator outlet.

FIG. 3 illustrates this first embodiment of the invention. Elements identical or similar to the prior art embodiments of FIGS. 1 and 2 have the same reference signs.

The working fluid is vaporized in a first heat exchanger 1, also referred to as evaporator, through heat exchange with a warm source SC, notably surface ocean water. The vaporized working fluid is separated into two portions in a first separator or splitter 11.

The first working fluid portion (in gas form) is overheated in a second heat exchanger 8, also referred to as over heater, by means of the second portion. The thermal energy of the first working fluid portion is then converted to mechanical energy by turbine 3.

The second working fluid portion (in gas form) is compressed in a compressor 7 and subsequently used for heating the first portion by a second heat exchanger 8. At the outlet of second exchanger 8, the second portion is expanded, for example by a valve 9. The pressure at the outlet of valve 9 is adjusted at the pressure at the outlet of turbine 3 so that the two streams (portions) have the same pressure.

The first working fluid portion leaving turbine 3 and the second working fluid portion are then mixed together in mixer 12 to re-form the working fluid.

The re-formed working fluid is then condensed by a third heat exchanger 5, which is also referred to as condenser, by heat exchange with a cold source SF, notably seawater taken at depth. The condensed working fluid is then compressed for example in a pump 6 prior to being again vaporized in first heat exchanger 1.

The second embodiment of the invention differs from the first one in that only the gas phase of the second working fluid portion is mixed with the first working fluid portion at the turbine outlet. Indeed, the second portion at the valve outlet is made up of a liquid and gaseous combination. It is therefore not necessary to cool the liquid phase in the condenser. The liquid and gas phases of the second portion are therefore separated upstream from the mixture. The collected liquid is mixed with the liquid working fluid at the condenser outlet.

FIG. 4 illustrates this second embodiment of the invention. Elements similar to the first embodiment are not described.

The second working fluid portion at the outlet of valve 9 is separated into a liquid phase and a gas phase in a second separator 13 which may be a flash drum for example. The gas phase of the second portion at the outlet of separator 13 is mixed with the first portion at the outlet of turbine 3 in mixer 12. The working fluid which is re-formed is condensed in a third heat exchanger 5. The liquid phase of the second portion at the outlet of separator 13 is mixed in a second mixer 14 with the condensed working fluid at the outlet of third heat exchanger 5. Thus, all of the working fluid circulates in liquid form at the outlet of second mixer 14.

The third embodiment of the invention differs from the first in that only the gas phase of the re-formed working fluid is condensed. Indeed, the proportion of liquid at the turbine outlet can be significant. It is not necessary for the liquid phase to be condensed and it may therefore be judicious to use a flash drum after mixing the two streams.

FIG. 5 illustrates this third embodiment of the invention. Elements similar to the first two embodiments are not described.

The re-formed working fluid at the outlet of first mixer 12 is separated into a liquid phase and a gas phase by means of a third separator 15, notably a flash drum. The gas phase of the working fluid at the outlet of third separator 15 is condensed in third heat exchanger 5. The liquid phase of the working fluid at the outlet of third separator 15 is mixed in a second mixer 14 with the condensed working fluid at the outlet of third heat exchanger 5. Thus, all of the working fluid circulates in liquid form at the outlet of second mixer 14.

The fourth embodiment of the invention combines the second and third embodiments. Only the gas phase of the second working fluid portion is mixed with the first working fluid portion at the turbine outlet and only the gas phase of the re-formed working fluid is condensed.

FIG. 6 illustrates the fourth embodiment of the invention. Elements similar to the first three embodiments are not described.

The second working fluid portion at the outlet of valve 9 is separated into a liquid phase and a gas phase in a second separator 13 which may be a flash drum for example. The gas phase of the second portion at the outlet of separator 13 is mixed with the first portion at the outlet of turbine 3 in mixer 12.

The partially re-formed working fluid at the outlet of first mixer 12 is separated into a liquid phase and a gas phase by a third separator 15 which may be a flash drum for example. The gas phase of the working fluid at the outlet of third separator 15 is condensed in third heat exchanger 5.

The liquid phase of the second portion at the outlet of separator 13 is mixed in a second mixer 14 with the liquid phase of the partially re-formed working fluid in first mixer 12 and with the condensed working fluid at the outlet of third heat exchanger 5. Thus, all of the working fluid circulates in liquid form at the outlet of second mixer 14.

According to a variant embodiment of the invention compatible with all the embodiments described above, expansion of the second portion in the circuit relative to the heat pump can be performed by means of a two-phase pump. The two-phase pump allows increasing the net power generated by the thermodynamic cycle according to the invention. FIG. 7 illustrates this variant for the first embodiment. Elements similar to the four embodiments are not described.

In this circuit, valve 9 of the heat pump is replaced by a two-phase pump 16.

The method and the system according to the invention are particularly suited for use as an OTEC plant with the warm source being seawater taken at the surface and the cold source being seawater taken at depth ( 1000 m for example).

APPLICATION EXAMPLES

In order to show the use of the method and of the system according to the invention, simulations were performed for various embodiments of the invention and for two embodiments of the prior art.

To study and compare the different methods, the working fluid is considered to be ammonia (NH3) and we set the following parameters are set:

• • Warm water (warm source SC)
    • Temperature 28° C.
  • Cold water (cold source SF)
    • Temperature 4° C.
  • Rankine cycle without heat pump (prior art of FIG. 1)
    • NH 3 flow rate in turbine 3: 100 kg/s
  • Heat pump 2
    • NH 3 flow rate: 4 kg/s.

It can be noted that, under such conditions, the ammonia is dry at the turbine outlet. For the cycles with integrated heat pump according to the invention, splitter 11 is so adjusted that the ammonia flow rate in the turbine is the same as for the Rankine cycle with or without a heat pump, i.e. 100 kg/s.

For all the cycles, the warm or cold water flow rates are so adjusted so that the pinch is slightly above 2° C. For overheater 8, the pressure at the compressor outlet is adjusted so as to have the same 2° C. pinch.

The various methods simulated are:

• • the Rankine cycle alone, denoted by Cycle 1, as illustrated in FIG. 1 (prior art)
  • the thermodynamic cycle of FIG. 2 with a Rankine cycle and a heat pump, denoted by Cycle 2 (prior art)
  • the first, second and third embodiments of the invention, as illustrated in FIGS. 3 to 5 and denoted by Cycles 3, 4 and 5 respectively.

Table 1 summarizes the powers consumed and generated in the various methods and their comparison in relation to the Rankine cycle.

TABLE 1
Comparison of the consumed and generated powers
Powers	Cycle 1	Cycle 2	Cycle 3	Cycle 4	Cycle 5
Pump SC	431	464	464	464	464
(kW)
Pump SF (kW)	319	557	574	560	570
Pump 6 (kW)	54	65	67	67	67
Compressor 7		578	578	578	578
(kW)
Pump PAC		0.8
(kW)
Turbine 3	4046	5406	5406	5406	5406
(kW)
Net power	3242	3741	3726	3736	3726
(kW)
Gain/Cycle		15.4	14.8	15.2	14.9
1 (%)

It can be observed that addition of a heat pump allows generation around 500 kW more in relation to the Rankine cycle, that is a power gain of around 15%.

Integration of the heat pump PAC according to the invention (Cycles 3, 4 and 5 ) in the Rankine cycle causes a slight reduction in the gain obtained in Cycle 2 (according to the prior art) due to the increase in power of the cold water pump. However, the second embodiment of the invention allows to practically get back to the same generated power as the Rankine cycle with heat pump PAC of Cycle 2.

On the other hand, integration of the heat pump PAC according to the invention in the cycle has little effect on the sizing of the exchanger with the cold source (condenser) and has no impact on the vaporizer and the overheater.

A second series of simulations was carried out by replacing valve 9 by a two-phase pump. Table 2 shows the results of these simulations:

TABLE 2
Comparison of the consumed and generated powers
with a two-phase turbine
Powers	Cycle 1	Cycle 2	Cycle 3	Cycle 4	Cycle 5
Pump SC	431	464.31	464.31	464.31	464.31
(kW)
Pump SF (kW)	319	557.23	570.26	560.48	570.26
Pump 6 (kW)	54	64.52	67.10	67.0	67.10
Compressor 7		578.18	578.15	578.15	578.15
(kW)
Pump PAC		0.80
(kW)
Multiphase		5.26	6.85	6.85	6.85
turbine (kW)
Turbine 3	4046	5405.68	5405.66	5405.66	5405.66
(kW)
Net power	3242	3745.91	3732.69	3742.46	3732.69
(kW)
Gain 1 (%)		15.5	15.1	15.4	15.1

With the two-phase turbine, the shaft power generated in this example is 6.85 kW.

Table 3 allows assessment of the generated power gain:

TABLE 3
Comparison of the gains with a two-phase pump in relation to the same
cycles provided with a valve
		Cycle 2	Cycle 3	Cycle 4	Cycle 5
	Net power	5.26	10.11	6.85	6.85
	gain (kW)
	Gain (%)	0.2	0.3	0.2	0.2

This gain is low but revealing. Furthermore, addition of a two-phase turbine provides no particular change in the parameters dimensioning the exchangers. This conclusion derives from the fact that, given the conditions under which it operates in this example, the two-phase turbine has little effect on the thermodynamic conditions of the working fluid at the outlet.

Several variants of the method according to the invention, were studied involving overheating of a Rankine cycle with a heat pump. These variants allow without the seawater-heat pump, a working fluid exchanger. Indeed, although this exchanger is small in size in relation to the main exchangers of the Rankine cycle, it has corrosion and biofouling problems.

The simulations of these various methods show that the integration according to the invention improves substantially the Rankine cycle by the simple addition of a heat pump to the Rankine cycle.

Furthermore, addition of a two-phase turbine in these methods allows improvement of the efficiency by several percentage points without requiring any particular change in the design of the main exchangers.

Claims

1-17. (canceled)

18. A thermal to mechanical energy conversion method comprising circulating a working fluid in a closed Rankine cycle circuit equipped with a heat pump for heating the working fluid vaporized in the Rankine cycle circuit, and circulating the working fluid of the Rankine cycle circuit in a circuit of the heat pump.

19. A method as claimed in claim 18, wherein the vaporized working fluid is separated into two portions with a first portion being converted into mechanical energy by the Rankine cycle circuit and a second portion being circulated in the circuit of the heat pump.

20. A method as claimed in claim 19, wherein the first portion is mixed after conversion into mechanical energy in the Rankine cycle circuit with at least part of the second portion.

21. A method as claimed in claim 18, comprising: a) vaporizing the working fluid by thermal exchange with a first heat source;b) separating the vaporized working fluid into two portions;c) heating a first portion by heat exchange with a previously compressed second portion;d) converting part of thermal energy contained in the first portion into mechanical energy;e) re-forming at least part of the working fluid by mixing at least part of the first and second portions with the second portion which was previously expanded;f) condensing at least part of the re-formed working fluid by heat exchange with a second heat source; andg) compressing the condensed working fluid.

22. A method as claimed in claim 19, comprising: a) vaporizing the working fluid by thermal exchange with a first heat source;b) separating the vaporized working fluid into two portions;c) heating a first portion by heat exchange with a previously compressed second portion;d) converting part of thermal energy contained in the first portion into mechanical energy;e) re-forming at least part of the working fluid by mixing at least part of the first and second portions with the second portion which was previously expanded;f) condensing at least part of the re-formed working fluid by heat exchange with a second heat source; andg) compressing the condensed working fluid.

23. A method as claimed in claim 20, comprising: a) vaporizing the working fluid by thermal exchange with a first heat source;b) separating the vaporized working fluid into two portions;c) heating a first portion by heat exchange with a previously compressed second portion;d) converting part of thermal energy contained in the first portion into mechanical energy;e) re-forming at least part of the working fluid by mixing at least part of the first and second portions with the second portion which was previously expanded;f) condensing at least part of the re-formed working fluid by heat exchange with a second heat source; andg) compressing the condensed working fluid.

24. A method as claimed in claim 21, compromising separating the second portion, upstream from re-forming part of the working fluid into a liquid phase and a gas phase, mixing with the gas phase of the second portion with the first portion during partially re-forming the working fluid, and mixing the liquid phase of the second portion is mixed with the condensed working fluid.

25. A method as claimed in claim 22, compromising separating the second portion, upstream from re-forming part of the working fluid into a liquid phase and a gas phase, mixing with the gas phase of the second portion with the first portion during partially re-forming the working fluid, and mixing the liquid phase of the second portion is mixed with the condensed working fluid.

26. A method as claimed in claim 23, compromising separating the second portion, upstream from re-forming part of the working fluid into a liquid phase and a gas phase, mixing with the gas phase of the second portion with the first portion during partially re-forming the working fluid, and mixing the liquid phase of the second portion is mixed with the condensed working fluid.

27. A method as claimed in claim 21, comprising separating the partially re-formed working fluid into a liquid phase and a gas phase with the the gas phase of the working fluid being condensed during the condensation stage and the liquid phase of the working fluid being mixed with the condensed working fluid.

28. A method as claimed in claim 24, comprising separating the partially re-formed working fluid into a liquid phase and a gas phase with the the gas phase of the working fluid being condensed during the condensation stage and the liquid phase of the working fluid being mixed with the condensed working fluid.

29. A method as claimed in claim 18, wherein the heat sources are seawater taken at different depths.

30. A method as claimed in claim 19, wherein the heat sources are seawater taken at different depths.

31. A method as claimed in claim 20, wherein the heat sources are seawater taken at different depths.

32. A method as claimed in claim 21, wherein the heat sources are seawater taken at different depths.

33. A method as claimed in claim 24, wherein the heat sources are seawater taken at different depths.

34. A method as claimed in claim 27, wherein the heat sources are seawater taken at different depths.

35. A method as claimed in claim 18, wherein the working fluid comprises ammonia.

36. A method as claimed in claim 19, wherein the working fluid comprises ammonia.

37. A method as claimed in claim 20, wherein the working fluid comprises ammonia.

38. A method as claimed in claim 21, wherein the working fluid comprises ammonia.

39. A method as claimed in claim 24, wherein the working fluid comprises ammonia.

40. A method as claimed in claim 27, wherein the working fluid comprises ammonia.

41. A thermal to mechanical energy conversion system comprising: a closed circuit which circulates a working fluid comprising a Rankine cycle circuit equipped with a heat pump for heating the vaporized working fluid in the Rankine cycle circuit, with the working fluid of the Rankine cycle circuit circulating in the circuit of the heat pump.

42. A system as claimed in claim 41, wherein: the closed circuit which circulates a first separator for separating the working fluid into two portions with a first portion being converted into mechanical energy by the Rankine cycle circuit and a second portion circulating the circuit of the heat pump.

43. A system as claimed in claim 41, wherein the closed circuit comprises: a first mixer for mixing the first portion with at least part of the second portion which is downstream from means for conversion of energy in the Rankine cycle circuit into mechanical energy.

44. A system as claimed in claim 41, wherein the closed circuit comprises in succession: a first heat exchanger for vaporizing the working fluid with a first heat source;a separator for separating the vaporized working fluid into two portions;a second heat exchanger for heating a first portion with a second portion compressed by a compressor;a turbine for converting part of the thermal energy contained in the first portion to mechanical energy;a first mixer for mixing at least part of the first and second portions to re-form at least part of the working fluid with the second portion being expanded by an expansion means;a third heat exchanger for condensing at least part of the working fluid by a second heat source; andpump for compressing the condensed working fluid.

45. A system as claimed in claim 42, wherein the closed circuit comprises in succession: a first heat exchanger for vaporizing the working fluid with a first heat source;a separator for separating the vaporized working fluid into two portions;a second heat exchanger for heating a first portion with a second portion compressed by a compressor;a turbine for converting part of the thermal energy contained in the first portion to mechanical energy;a first mixer for mixing at least part of the first and second portions to re-form at least part of the working fluid with the second portion being expanded by an expansion means;a third heat exchanger for condensing at least part of the working fluid by a second heat source; andpump for compressing the condensed working fluid.

46. A system as claimed in claim 43, wherein the closed circuit comprises in succession: a first heat exchanger for vaporizing the working fluid with a first heat source;a separator for separating the vaporized working fluid into two portions;a second heat exchanger for heating a first portion with a second portion compressed by a compressor;a turbine for converting part of the thermal energy contained in the first portion to mechanical energy;a first mixer for mixing at least part of the first and second portions to re-form at least part of the working fluid with the second portion being expanded by an expansion means;a third heat exchanger for condensing at least part of the working fluid by a second heat source; andpump for compressing the condensed working fluid.

47. A system as claimed in claim 44, wherein the expansion means comprises a two-phase pump.

48. A system as claimed in claim 44, wherein the closed circuit comprises: a second separator upstream from the first mixer, for separating the liquid and gas phases of the second portion, and a second mixer downstream from the third mixer for mixing the liquid phase with the working fluid at an outlet of third exchanger with the first mixer mixing the gas phase of the second portion with the first portion.

49. A system as claimed in claim 47, wherein the closed circuit comprises: a second separator upstream from the first mixer, for separating the liquid and gas phases of the second portion, and a second mixer downstream from the third mixer for mixing the liquid phase with the working fluid at an outlet of third exchanger with the first mixer mixing the gas phase of the second portion with the first portion.

50. A system as claimed in claim 44, wherein the closed circuit comprises: a third separator downstream from the first mixer for separating the liquid and gas phases of the working fluid at an outlet of the first mixer and a second mixer downstream from the third exchanger for mixing the liquid phase with the working fluid at the outlet of the third exchanger and the third exchanger cooling the aqueous phase of the working fluid.

51. A system as claimed in claim 41, wherein the working fluid comprises ammonia.

52. A system as claimed in claim 41, wherein the heat sources are seawater taken at different depths.