MX2007000879A - Efficient conversion of heat to useful energy. - Google Patents

Abstract

A heat transfer system includes a power sub-system configured to receive a heatsource stream, and one or more heat exchangers configured to transfer heat fromthe heat source stream to a working stream. The working stream is ultimately heatedto a point where it can be passed through one or more turbines, to generate power,while the heat source stream is, cooled to a low temperature tail. A distillationcondensation sub-system cools the spent stream to generate an intermediatestream and a working stream. The working stream can be variably heated by the intermediatestream so that it is at a sufficient temperature to make efficient use of the lowtemperature tail. The working stream is. then heated by the low temperature tail,and subsequently passed on for use in the power sub-system.

Description

EFFICIENT CONVERSION OF HEAT TO USEFUL ENERGY 1. Field of the invention The present invention is related to systems, methods and apparatuses configured to implement a thermodynamic cycle by means of a heat interrupter exchange. In particular, the present invention is related to the generation of electricity obtained by heating a flow of multiple components with the flow of a heat source at one or more points in a thermodynamic cycle. 2. BACKGROUND OF THE INVENTION Some conventional heat transfer systems allow the heat that would be wasted to be transformed into useful energy. An example of a conventional heat transfer system is that which converts the source of wasted thermal energy from a heat source such as geothermal hot water for industrial use, converting it into electricity using heat exchange technology with a power cut. For example, the heat of the relative hot liquids in a geothermal vent (eg, "saline") can be used to heat a multi-component fluid in a closed system (a "fluid stream"), using one or more money changers of heat. The multi-component fluid heats up from a low-energy, low-temperature fluid to a relative high-pressure gas ("a working current"). The high pressure gas, or working current, can then pass through one or more turbines, causing this or these turbines to turn and generate electricity.

According to the previous, conventional heat transfer systems operate under the principles of heat exchange of a short-circuit to be able to heat the fluid of multiple components working through a range of different temperatures, from relatively cold to relatively hot. The conventional flow of a fluid for a system like this comprises different components of the fluid where each one has a different boiling point. Therefore, one component of the fluid flow can be converted into a gas at a certain temperature, while another component of the fluid flow can be maintained as a very hot liquid state at the same temperature. This can be useful to be able to separate the different components at different points of the closed system. However, all or almost all of the components of the fluid flow can be raised to a certain temperature necessary so that all components of the fluid flow collectively comprise a "working flow", or a high pressure gas.

In order to achieve the heating of the fluid between the flow of the fluid and the working flow, the heat transfer system comprises an apparatus configured primarily to bring the flow to work at a lower temperature, or to bring the flow of the fluid to a temperature more high. For example, the fluid stream passes through one or more heat exchangers that connect to the fluid stream to the fluid from the heat source while the flow stream progresses to a high temperature state, which subsequently passes to through one or more turbines. In contrast, the working current that has already passed through the turbines is normally sent as a current already used. The current already used in cooled when heat is transferred to the fluid stream in a heat exchanger, since the current used is relatively hotter than the fluid flow at one or more levels of the system.

In order to obtain the temperature required for expansion in the turbines, heat exchange systems with a short-circuit heat the fluid flow from low points of temperature to the highest points of temperature. This results in a number of system variables that conventional heat exchange systems will consider. For example, if the optimum temperature of expansion of the temperature of an environment with a multi-component current is already a working source of steam, the current of a very high temperature, a very hot heat source that is normally hotter than the desired temperature of the working current will be used. Alternatively, if the heat source is only slightly hotter than the last desired temperature of the multi-component stream, the flow stream will only need to be warmer than the ambient temperature, so that the multi-component fluid can be heated to the desired temperature for the current working.

At least in one part, due to the distinction of fluids from the stream at different temperatures at its boiling point, the temperatures of the heat source, the desired temperature of the working current, the efficiencies of the system, the saline solution of the Heat source is normally discarded at a hotter temperature than desired. For example, in certain illustrative systems such as conventional heat transfer systems pass the saline solution through one or more heat exchangers, the saline solution is then cooled from an average temperature of 600 ° F to an extreme temperature of more or minus 170-200 ° F. Although 200 ° F even at a relatively hot temperature to perform significant heat transfers in conventional flow streams, the conventional fluid flow is considered relatively cold, or lukewarm, at a temperature similar to 170- 200 ° F. In particular, the coldest point of a conventional fluid stream is usually too hot to be able to be heated efficiently by the low temperature portion (ie, the "low temperature tail") of the saline solution. Because of this, conventional heat systems tend to be more efficient when discarding saline at approximately 170-200 ° F.

One possible solution could be to cool the fluid stream to a lower temperature than 190-200 ° F, so that the fluid stream can be efficiently heated using the low temperature tail heat. In principle, this may involve the use of a distillation and condensation subsystem ("DCSS") in conjunction with the heat transfer system described above. Unfortunately, while the use of a DCSS could efficiently cool an already used current, the temperature at which a conventional DCSS could cool a commonly used current would be too low to be used efficiently. That is, a conventional DCSS could cool the current already used at such a low temperature that it could not be efficiently raised to the point where it can become part of the working current.

According to the aforementioned, an advantage in this technique can be realized with systems and apparatuses that allow the efficiency of the use of a low temperature . In particular, an advantage in this technique can be noted with heat transfer systems that can efficiently use a DCSS, so that a fluid stream can still be raised to a temperature sufficient to become a working current.

BRIEF DESCRIPTION OF THE INVENTION The present invention solves one or more of the problems that may arise in the prior art with systems and apparatuses configured to efficiently utilize all of the wasteful heat possible in previous heat transfer systems. In particular, the present invention is provided for the use of a "low temperature queue" of the heat source of a saline solution in a heat transfer system, at least in part by efficiently incorporating a DCSS together with an apparatus additional heat exchange.

For example, in one of the embodiments of the present invention, a DCSS is connected to the short-circuit of a heat exchange system. The DCSS is used at least in part to cool a current used after the current working has passed through one or more turbines. Due to the relatively low temperature of the fluid stream provided by the DCSS, however, one or more heat exchange apparatuses are added to increase the temperature of the fluid stream to a useful range of temperature. In this temperature range, the fluid stream can subsequently join a low temperature tail as low as 150-200 ° F by means of an additional heat exchanger, and even ultimately reach a temperature to be part of the current working.

Related to the above, a heat transfer system according to the present invention can convert a large amount of heat from the heat source into useful energy, and can do so with a more significant energy efficiency than heat transfer systems previous Other features and advantages of the exemplary embodiments are found in the following description, and will be partly obvious in the description, or may be learned from the practice of said example modalities. The characteristics and advantages of said modalities may be noted and obtained by means of the instruments and combinations particularly pointed out in the appended claims. This and other features will be more apparent in the following description and appended claims, or may be learned through the practice of such exemplary implementations found herein below.

BRIEF DESCRIPTION OF THE DRAWINGS In order to describe the manner in which the aforementioned and other advantages and features of the invention can be obtained, a more detailed description of the invention will be described below with reference to specific embodiments which are illustrated in the accompanying drawings. In order to understand these drawings which represent the typical embodiments of the invention and are therefore not to be considered as limiting the scope of the invention, this invention will be described and explained with additional specifications and details through the use of the drawings that the accompany where: Figure 1 illustrates a heat transfer system according to the embodiment of the present invention, wherein two turbines are used; Y Figure 2 illustrates a heat transfer system according to another embodiment of the present invention, wherein a turbine is used.

DETAILED DESCRIPTION OF THE PREFERRED MODALITIES The present invention extends to systems and apparatuses configured to efficiently utilize the waste heat that is possible in previous heat transfer systems. In particular, the present invention is provided due to the use of a "low temperature queue" of a heating source of a saline solution in a heat transfer system, at least in part to incorporate as an efficiency agent into a DCSS together with other heat exchange devices.

For example, Figure 1 illustrates an embodiment of the present invention wherein a heat transfer system 100 comprises a power subsystem 101 that is connected to a cooling system, such as a distillation and condensation subsystem ("DCSS"). The power subsystem 101 can be thought of as being so general as to heat the stream of multiple components to a point where the stream of the multi-component stream becomes at least partially a working steam stream. In contrast, the DCSS 103 may be thought to generally cool an expansion of a current used to a cold fluid stream, in the same manner, to heat the fluid stream where appropriate to be used subsequently as a multi-component stream in the subsystem of 101 Figure 1 also shows the direction of a multi-component stream (both for the fluid stream and for the heat source stream) through the heat transfer system 100, while the fluid is condensed and heated in heat exchangers in the system.

Therefore, the following description summarizes the current of the heat source stream (eg, "saline solution") while running through the heat transfer system 100 (and system 200), and subsequently the streams, the used and the intermediate fluid, which are different and separated from the heat source current through the power subsystem 101 and the DCSS 103. With reference to the current of the heat source, it will be understood that various types of heat source streams may have been implemented with the present invention. For example, a stream of the heat source found to be used by the present invention may comprise any available hot liquid or vapor, or a mixture thereof, such as liquids, vapors, oils and other synthetically produced agents. or natural Therefore, implementations of the systems described herein can be particularly useful for converting heat from geothermal fluids, such as "saline", into electrical power, as well as converting other synthetic fluids of heat waste into the environment. of a factory in electrical power.

Referring again to figure 1, the current from the power source enters the heat transfer system 100 at point 50 (anywhere between 2500F to 8000F), where the heat source is divided into two streams 51 and 151, They are used to add heat to a working current just before the working current passes to a turbine or other expansion component. For example, current 51 passes through a heat exchanger 304, which transfers the heat to the current working at point 30 just before entering the first turbine 501. As described herein, the division of the currents can be carried out by any available means, as is a conventional division component that divides the stream of multiple components into two separate streams.

After the working current passes through the first turbine, the working current is cooled until it reaches a point 32. Therefore, current 151 heats the current working from point 32 to point 35 where it passes through the heat exchanger 305, which is adjacent to a second turbine 502, so that the working current can be heated just before it passes to the second turbine 502. As used herein, a "heat exchanger" can be any conventional type. of heat exchangers, such as a conventional pipe or frame, or heat exchangers of the plate type, or variations or combinations. Therefore, the current of the power source at point 151 is cooled to parameters at point 150, having transferred an amount of its first heating in heat exchanger 305.

The currents 50 (original stream 151) and 152 (original stream 51) are then combined at point 153 before entering heat exchanger 303, where the combined current at a point 153 is a somewhat cooler quantity than at point 50. Any mixture or combination of any fluid stream, working, intermediate, used or otherwise can be carried out by any mixing device available to combine the currents and thus form a single stream.

Having passed the heat exchangers at point 153.1a the combined current of the heat source is still at a relatively high temperature, so it still has a significant amount of heat that can be transferred to the working current. Therefore, the combined current at point 153 passes through a heat exchanger 303, where it transfers heat from the current of the heat source to the working current, causing the working current to be heated from a point 66 to one. 67. The current of the heat source, having certain cooling parameters at point 53, still has a certain relative high temperature, so it passes through a heat exchanger 301. This heats the current from point 161 to 61 , and cool the current of the heat source beyond point 53 to point 54.

In one embodiment, at point 54, these parameters of the heat source current are associated with a temperature range around 170-200 ° F, depending in part on other operating conditions of the relevant heat source and of system 101. In another embodiment, the parameters of the heat source current at point 54 are associated with temperature ranges around 130-250 ° F. In point 54, the current of the heat source is now in parameters of the conventional "low temperature tail", and can usually be discarded. As will be better understood and fully understood in the following description, however, the system 100 can efficiently utilize this low temperature queue, just as the heat source current passes from the point 54 through a heat exchanger 405 to a point 55. From the moment the heat exchanger 405 transfers the heat from the low temperature queue, the heat exchanger 405 can be called a "residual heat exchanger".

Having already described the flow path of the heat source, the following description illustrates the path and changes to the fluid flow of the system 100, while heating and cooling in several stages through the power subsystem 101 of the point 60- to point 36, and then the way it travels through DCSS 103 from point 38 to point 29 \? In an embodiment, the fluid stream may be comprised of a mixture of water with ammonia having a boiling point of 338 ° F. As will be understood in the present description, therefore, the fluid stream is either ce approaches its boiling point at point 60, at or near its point of spray at point 30, I near liquid forms at points from 18, and 102. These differences between the boiling point, the point of spray, and the liquid form occur since the working fluid is formed by a mixture of components rather than a pure substance.

With reference to Figure 1 at point 60, the heat transfer system 100 divides the current by working on two multiple component currents at points 161 and 162. The current working at point 161 is heated, by the current at the source of heat to parameters up to point 61 in heat exchanger 301, while the current working at point 162 is heated to parameters of point 62 by the current used 36 in the heat exchanger 302. After passing through the relevant heat exchangers, the currents working at points 61 and 62 are combined in a working current that has parameters at point 66. Since they are part of the current working at point 60 it is heated by the current of the heat source, while another part of the working current is heated by the current used, the power subsystem 101 can make effective use of a potential number of heat sources.

The current working at point 66 is heated by the current of the heat source from point 153 to parameters to point 67 by means of a heat exchanger 303. In one of the modes, at point 67 the working current starts to become in a super heated steam. Then, the working current is heated by the current of the heat source at point 51, so that the working current is heated from point 67 to point 30 by means of a heat exchanger 304. This optimizes the current working conventional so that it can pass through the turbine 501 in a desired state of high energy. In one of the embodiments, the desired high energy state is superheated heat.

As the working current passes through the turbine 501, from points 30 to 32, the working current becomes part of a "used current", so that it loses an amount of energy in the form of pressure loss and temperature. The current partially used at point 32 is heated through a heat exchanger 305 to obtain parameters from point 35. After this, it can then be seen that the system 100 will then be able to find an additional increase in energy, obtained from the continuous separation of the heat source current at point 50 to further heat up subsequent iterations of a partially used stream through various numbers of heat exchangers and turbines and so on. For all this, the use of one or two turbines of the present description are merely by way of example of one of the available modalities.

After the working current passes through one or more turbines 501, 502, the now used current at point 36 passes through a heat exchanger 302. This cools the current used up to the parameters of point 38, while that at the same time a part of the current is heated working from point 162 to 62. (At least in some cases, the current spent at point 36 can occur at a lower pressure than at the current working at high high pressure at points 162 and 62, although the current working at point 36 is hotter.) In conventional systems, the current used at point 38 ordinarily must pass to point 60 for a recuperative reheat. In the present system 100, however, the current used at point 38 is subsequently cooled using a DCSS 103.

For example, the current used at point 38 passes through a heat exchanger 401, just as the current used is cooled from point 38 to parameters at points 16 and then 17. This cooling of the current used from point 38 at point 17 in the heat exchanger 401 transfers the heat to the relatively cold intermediate current "support current" from point 102 to point 5. The support current goes from relatively cold parameters from point 102 to relatively hot parameters in point 3 (typically, the boiling point), and finally to parameters at point 5. In general, a "support stream" refers to a fluid stream that has a component with a boiling point lower than a component with a higher boiling point (eg Ammonia versus water), while a "rich stream" refers to a fluid stream that has a component with a boiling point lower than a component with a pu higher boiling. In addition, a "thin-intermediate" stream has more than one component with a low boiling point (eg, ammonia, in an ammonia water) than a "thin" or "very thin" stream (ie, less ammonia in a ammonia water), but with a component with a lower boiling point than a "rich" stream.

The current already used at point 17 is then combined with a very thin current having parameters from point 12, to produce a combined stream of fluid (or a "thin intermediate" current) having point parameters 18. The thin intermediate current The combined heat exchanger is then cooled in the heat exchanger 402, which transfers heat from the thin intermediate stream at point 18 to a medium cold. Apparatus 402 and 404 can counter some heat exchange condensers, such as water changers or air cooling.

The median cooling may have any amount or a combination of means sufficient to condense the median thin stream from point 18 to point 1 by means of the heat exchanger 402. Said medium may include air, water, a chemical cooler, or any other agent , and are found in a simple manner in an inward and outward cycle of the system 100, as appropriate. Therefore, the medium cooling is introduced to the relatively cold system 100, such as that of point 23, heated by heat exchangers 402 and 404 to points 59 and 58, and then in the outward cycle of the system 100 relatively hot at point 24. Since the medium cooling is inside the cycle in and out of the system, the medium cooling maintains a constant relative cold temperature that can absorb the heat of the multi component current.

After the median thin stream has been condensed into parameters at point 1, pump 504 raises the pressure of the current, causing the intermediate thin stream to rise to parameters of point 2.? Next, the high pressure of the intermediate thin stream is divided into two parts. A part, which will be discussed in greater detail later, has parameters of point 8, and is mixed with a rich current with parameters of point 6. The other part of the medium pressure thin stream, having parameters of point 102, is heated in the apparatus 401 by the current already used from point 6, so that the intermediate thin current gains parameters from point 5.

In point 5, the intermediate thin stream is separated in the apparatus 503 into primary components of vapor and liquid, as the vapor component has parameters of point 7, and the liquid component has parameters of point 9. One may appreciate, however , that neither of the two components, neither the vapor nor the liquid are a pure component or another. However, the steam flow will be richer in the low-boiling component (i.e., a "rich" stream); while the flow of the liquid has a large number of components with a high boiling point (i.e., a "thin" current). The apparatus 503 may contain some separator or distiller device which is within the description, such as a gravity separator (E, a conventional flash tank).

In one embodiment, the vapor and liquid components of the streams at points 7 and 9 are separated so that they can be selective upon mixing (or not mixing) to heat (or maintain) the amount of temperature provided in an intermediate heat exchanger 403 For example, a portion of the steam at point 7 can selectively be divided into a current at point 6, and in another stream at point 15. If the liquid component at point 9 is not hot enough to set the current From multiple components from point 21 to point 29 in the heat exchanger 403, a larger portion of the stream with a hotter vapor component from point 15 can be added to the liquid component stream at point 9, to produce a current hotter having parameters in point 10. As an alternative mode, if the liquid component in point 9 is hot enough for what is needed in the heat exchanger 403, and Now it is not necessary to mix with the steam at point 15. This mixture is therefore optional and depends on the relevant operational conditions.

Whether or not said mixing is carried out, the current at point 10 is generally a "very thin" stream or a stream with a very low amount of low boiling components. This very thin current at point 10 passes through the intermediate heat exchanger 403, heats the fluid stream from point 21, and cools the very thin current from point 10 to point 1. In some cases, if necessary, the current fluid at point 11 can subsequently be subjected to a lower pressure. However, the fluid stream at point 11 goes to parameters of point 12, and then mixes with the current already used at point 17 before passing through the heat exchanger 402. Referring again to the point current 5, the vapor component at point 7 which is divided apart from the liquid component of point 9, differs from the vapor components at points 6 and 15 primarily with respect to the current cup. In practice, however, the vapor components of points 6, 7, and 15 may also have slightly different pressures. Without taking this into account, the vapor component (ie, the component of point 7, or the components of streams 6, or 15), is a "rich" stream, having a relatively high amount of components with a low point of boiling. This "rich" current at point 6 as subsequently mixed with the portion of the intermediate thin stream at point 8, to produce the multi-component stream at point 13. The intermediate stream at point 13 is approximately the same portion of components with high and low boiling points (eg, proportion of ammonia in water) that the current working subsequently used in the process of heat transfer, such as that of points 60 and above.

This intermediate stream at point 13 is condensed in the heat exchanger 404 by the aforementioned cooling medium and converted into a condensed stream. Due to this, this fluid stream at point 13 is cooled from parameters of point 13 to parameters of point 14. The fluid stream at point 14 is then pumped by pump 505, so that the fluid stream becomes in a working high pressure stream having parameters of point 21. The current working at point 21 is then heated to point 29 through heat exchanger 403, causing the intermediate current to cool from point 10 to point 11. In point 29, the working current is heated by the "low temperature tail" of the source current in the heat exchanger 405, so that the current of the heat source is cooled from points 54 to 55.

In the following, it will be appreciated that the current worked in point 29 must be at an appropriate temperature so that its use can be effective (i.e., to be heated by) in the tail of the low temperature in the heat exchanger 405. This can help to ensure that the current working at point 30 passes through the turbine 501 at the highest available point of energy of the system 100 According to this, although the current working at point 30 reaches its most efficient energy output may depend in part on the temperature of the intermediate current at point 10. For example, if the current working at point 29 is at a very high temperature, there is very little or no added efficiency transferring heat from the low temperature tail at points 54 to 55. In contrast, if the current working at point 29 is very cold after having passed through the DCSS 103 , the low temperature tail of points 54-55 can not heat the current working from point 29 to the desired temperature at point 60.

According to one of the embodiments of the present invention, the DCSS 103 can help to ensure the appropriate temperature of the current working at point 29 allowing the variable addition of heat to the intermediate current at point 10. As previously described , this can be achieved by variablely adding (or not adding) a vapor component 15 with a liquid component 9. In other words, the more vapor 15 is added to stream 9, the hotter the fluid mixing stream will be at the point 10, and the more heat is added to the current working at point 21. Therefore, the provisions for separating and mixing in the fluid stream in the DCSS 103 allows the system 100 to achieve efficient use in the tail of low temperature (ie, points 54-55) in the working current. Even, the implementations of the present invention make effective the use of the low heat source current to obtain additional power in the turbines 501 and 502, and so on.

Figure 2 shows an alternative in the heat transfer system 200, which implements only one turbine 502. In particular, the system 100 can be modified, as shown in Figure 2, so that the streams 32, 150, and 151, and the heat exchanger 305 are omitted. This results only in the current working at point 30 passing through turbine 502 to produce an already worn current 36, which is subsequently processed in a heat exchanger 302, as described above. As we also mentioned, however, the number of turbines that can be used to increase the energy gain may vary within the context of the present invention.

In alternate embodiments of the present invention, where the heat exchanger 303 of the system 100 or 200 may be supplied by a heat exchanger 304. In another embodiment, the heat exchanger 302 may be replaced by a heat exchanger. 301 The present invention can be modified in specific ways, without departing from its spirit or essential characteristics. The described modalities are to be considered in all their aspects only by way of illustration but not restricted. The scope of the invention is, therefore, indicated in the appended claims rather than in the present description. All the changes that are within the explained and in the equivalence range of the claims are to be taken into account within their scope.

Claims (21)

1. An apparatus for implementing a thermodynamic cycle comprising: An expansion mandrel which is connected to receive a working current of multiple gaseous components and which is adapted to transform the energy of the working current of multiple gaseous components into a useful form and produce a precondensed current; a condensation distillation subsystem configured to receive the precondensed stream, wherein the precondensed stream has a parameter of the first temperature, the distillation condenser subsystem including: at least a first capacitor configured to condense the precondensed stream to produce a condensed stream; a current separator configured to separate the condensed current into a rich current and a light current to be used in forming a working liquid stream, and a pump configured to pressurize the liquid stream working, where the temperature parameter of the pressurized working current has a low temperature parameter compared to the temperature parameter of the precondensed stream entering the condensation distillation subsystem; and a first heat exchanger configured to heat the current by working pressurized using a stream of the condensation distillation subsystem; and a residual heat exchanger that receives the pressurized working current from the first heat exchanger, the residual heat exchanger configured to heat the current working by using a low temperature end of the current from an external heat source where the temperature parameter of the pressurized working current that is entering the residual heat exchanger is lower than the temperature parameter of the precondensed stream entering the condensation distillation subsystem.

2. The heat transfer system as recited in claim 1, wherein the working stream comprises a mixture of components where each has a different boiling point as a mixture that includes one or more members such as water and ammonia.

3. the heat transfer system as recited in claim 1 wherein the stream of the heat source is a fluid material comprising one or more Saline solutions arising from a geothermal wind or

4. The heat transfer system "" as recited in claim 1, wherein the condensation distillation subsystem also comprises a separator configured to substantially separate a vapor component in an intermediate stream from a liquid component.

5. The heat transfer system as recited in claim 4, wherein the condensation distillation subsystem is configured to optionally combine the vapor component with the liquid component in order to obtain the appropriate temperature for the intermediate stream.

6. The heat transfer system as recited in claim 5, wherein the condensation distillation subsystem also comprises a heat exchanger that transfers heat from the intermediate current to the working current after the intermediate current has passed the separator, so that the intermediate current heats the current working at the appropriate temperature to be used with the low temperature glue.

7. The heat transfer system as recited in claim 1, wherein the expansion mandrel comprises a plurality of turbines configured to generate electricity from the working current.

8. The heat transfer system as recited in claim 7, wherein the power subsystem comprises a plurality of corresponding heat exchangers, positioned adjacent each to the plurality of turbines, so that at least a portion of the Current from the heat source pass through each of the different and corresponding heat exchangers to heat the working current.

9. A method to implement a thermodynamic cycle comprises: expanding a current working with multiple gaseous components transforming its energy to a useful form and producing a current already used; cooling the current already used in a heat exchanger using an intermediate current to produce a precondensed stream; condensing the current already used in a condensation distillation subsystem to produce a condensed current, where the temperature of the current already used after cooling and before condensing has a first temperature parameter; Separate the condensed current into a rich current and a light current to produce a liquid current working; pressurize the liquid stream by working and producing a pressurized working current; heat the pressurized working current in a first heat exchanger using a condensation distillation subsystem current, and heat the pressurized working flow of the first heat exchanger to a residual heat exchanger using a low temperature tail of a heat source current external where the parameter of the temperature of the pressurized working current that is entering the residual heat exchanger is lower than the parameter temperature of the precondensed current that is entering the condensation distillation subsystem.

10. The method as mentioned in claim 9, also comprises the possibility of dividing the current of the heat source at the moment it is received so that the current of the heat source is used to heat the current working at the moment in which it directly passes through a plurality of heat exchangers adjacent to a plurality of corresponding turbines.

11. The method as recited in claim 9, wherein the intermediate stream comprises a vapor component and a liquid component.

12. The method as recited in claim 11, also comprises the possibility of dividing the intermediate heated stream into a substantially vapor component and a substantially liquid component, such that at least a portion of the intermediate stream comprises the substantially liquid component.

13. The method as recited in claim 12, also optionally comprises modifying the temperature of at least a portion of the intermediate stream with the substantially vapor component, so that the working stream is heated to an appropriate temperature to be able to be heated by the low temperature tail.

14. A method to implement a thermodynamic cycle comprises: Expanding the current by working with multiple gaseous components transforming their energy in some usable way and producing a current already used; Condensing the current used in a condensation distillation system and producing a condensed current where the temperature of the current used before entering the condensation distillation subsystem has a first temperature parameter; Pressurize the condensed current and produce a stream of multiple components; Heat the stream of multiple components with fluid from the condensation distillation subsystem; and Subsequent to the heating of the multi-component stream with condensation distillation subsystem fluid, heat the current by working with the low temperature tail of a stream from a heat source in a residual heat exchanger where the temperature parameter of the working current that is entering the residual heat exchanger is lower than the temperature parameter of the current used entering the condensation distillation subsystem.

15. The power subsystem mentioned in claim 14, wherein subsequent to the heating of the current working with the low temperature tail of a current from a heat source, it divides the current by working in a first and in a second current.

16. The power subsystem mentioned in claim 15, wherein the first current is heated with the current from the heat source.

17. The power subsystem mentioned in claim 15, wherein the second current is heated with the current already used.

18. A condensation distillation subsystem configured to transmit heat from a stream from a heat source, such as a low temperature tail of a stream from a heat source can be used efficiently comprising: One or more heat exchangers configured to transfer heat from an already used stream to an intermediate stream in a condensation distillation subsystem, such that the current already used is cooled, and the intermediate stream is heated to form a substantially vapor component and a substantially liquid component; an intermediate heat exchanger operatively joining a power subsystem to the condensation distillation subsystem, where the intermediate heat exchanger transfers the heat from the intermediate current in the condensation distillation subsystem to a current working in the power subsystem; and a heat exchanger using the low-temperature tail of the heat source current to a multi-component stream where the condensation distillation subsystem cools to the current working so that the heating of the working current is cooled to the current of A source of heat at a temperature parameter such that the current of the heat sources leaves the system at a lower temperature parameter than in the absence of cooling provided by the condensation distillation subsystem.

The condensation distillation subsystem as claimed in claim 18 also comprises a separator configured to separate the substantially vapor component from the substantially liquid component so that the intermediate stream comprises the substantially liquid component.

20. The condensation distillation subsystem as recited in claim 18, wherein the separator is configured to optionally heat the intermediate stream with the vapor component, so that the working current can be brought to the appropriate temperature.

21. The condensation distillation subsystem as recited in claim 18, wherein the heat exchanger using the low temperature queue of the heat source current for heating the multi component stream comprises a residual heat exchanger.