BR112019017292A2 - device to convert thermal energy - Google Patents

Abstract

device to convert thermal energy. in a device to convert thermal energy from a heat source into mechanical energy by means of a thermodynamic cyclic system with an exchanger fluid, which flows in the cyclic system while being exposed to a variable pressure, in which each respective pressure is associated with a value of saturated vapor temperature of exchanger fluid, as well as an expansion device to expand the exchanger fluid from a high pressure to a reduced pressure, in which the exchanger fluid after expansion to the reduced pressure has an escape temperature, with prediction of the installation of an adjustment device to adjust the temperature of the exhaust vapor to a defined temperature of exhaust vapor, above the corresponding value of the saturated vapor temperature of the reduced pressure.

Description

DEVICE FOR CONVERTING THERMAL ENERGY BACKGROUND TO THE INVENTION

The invention relates to a device for converting thermal energy from a heat source into mechanical energy by means of a thermodynamic cycle with a heat exchanger fluid contained in a closed cycle and, subject to variable pressures, being at each index pressure associated with a corresponding saturation temperature value of the heat exchanger fluid and an expansion valve to expand the working fluid from a high pressure to a lower pressure, the working fluid having an exhaust temperature after expansion to the lowest pressure. In addition, the invention relates to a corresponding method for converting thermal energy to mechanical energy.

Generic devices and methods are used to generate electrical energy from thermal energy for the so-called heat conversion. As a thermodynamic cycle process, the Rankine cycle process is normally carried out, which in steam power plants uses water as a exchanger fluid. The water is heated to about 600 ° C using high temperature heat sources, such as coal, natural gas, oil and nuclear energy. If an organic working medium is used instead of water, this is called an ORC process (Organic-Rankine-CycleProcess). Organic heat exchanger fluids can have a boiling temperature well below the boiling water and reach the gaseous state at lower temperatures. Therefore, ORC processes are used to harness thermal energy from low temperature heat sources that have temperatures between 60 ° C and 200 ° C. These heat sources are solar thermal or geothermal sources as well as residual heat from engines, industrial production processes and

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2/37 biogas plants. They can only be used insufficiently in conventional devices and methods.

In a cyclical thermodynamic process, the exchanger fluid undergoes periodic changes in its thermodynamic state functions, such as temperature and pressure. Depending on the change in state of the thermodynamic functions, the exchanger fluid can absorb energy from the environment or release energy into the environment. In this case, the exchanger fluid is therefore exposed to a variable pressure. First it is placed under a higher pressure, remaining in a liquid state and then vaporized and overheated by transferring thermal energy from a heat source. The result is a compressed, energetic exchanger fluid vapor, which can again discharge its absorbed energy at an expansion of the increased pressure to a lower pressure by means of an expansion device. The energy thus obtained can feed a generator that in the form of mechanical energy will generate electrical energy.

After expansion, that is, the expansion process, the exchanger fluid presents vapor as exhaust vapor, usually in a proportion of liquid state. This proportion of fluid in the liquid state reduces the efficiency and service life of many expansion devices. An important reason for this is the need for most expansion devices, such as positive displacement machines and, in particular, the vane cell expander, typically require lubrication with a lubricating oil. Through the lubricating oil, a friction between the mobile components of the expansion devices can be kept low and the leakage cracks can be sealed in the area of passage of the exchanger fluid that leads to the expansion device. However, if, with the passage, the lubricating oil absorbs part of the exchanger fluid, the lubricating properties and the

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3/37 lubricant oil seal decreases. Lower lubricating properties increase wear on moving parts. Less sealing capacity leads to greater leakage of the exchanger fluid in the expansion devices and, therefore, less efficiency. In addition, additional heating energy is required for subsequent thermal expulsion of the liquid working fluid from a recirculated lubricating oil, which further reduces efficiency.

Core Task

The invention aims to provide an apparatus and a method for a thermodynamic cycle with a heat exchanger fluid for converting thermal energy. In this case, the thermodynamic cycle must be optimized, in particular in terms of the service life and efficiency of the expansion device and the expansion installation.

Solution presented by the objective invention according to the invention is a device for the conversion of thermal energy from a heat source into mechanical energy by a thermodynamic cycle with a exchanger fluid that circulates in the circuit and, thus, subjected to a pressure variable, so for each pressure, there is a saturated vapor temperature value of the associated exchanger fluid, as well as an expansion device to expand the exchanger fluid from an increased pressure to a lower pressure, where the exchanger fluid after expansion to the lower pressure has an exhaust vapor temperature. To resolve this, an adjustment device is provided to adjust the exhaust vapor temperature to a defined exhaust vapor temperature that is above the temperature corresponding to the lowest associated pressure value.

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By means of the device, object of the invention, the exchanger fluid that circulates in the circuit is subjected to a variable pressure, which, in particular, is subject to periodic changes. In this case, the exchanger fluid is subjected to variable pressure indices, which are specifically subject to periodic changes. In this way, each corresponding pressure of saturated steam to which the exchanger fluid is subjected will correspond to a value of saturated steam. The temperature value of the saturated vapor is the temperature value at which the exchanger fluid in the liquid state is in equilibrium with the exchanger fluid in the gaseous state. Depending on the respective pressure, which is indicated as the saturated steam pressure value. The dependence of the pressure value of the saturated steam and the temperature value of the saturated steam can be represented on a graphical vapor curve as a delimitation of the phase boundary between the exchanger fluid in the liquid state and in the gaseous state. The graphical vapor curve is specific for each exchanger fluid.

If the exchanger fluid has a temperature below the saturated vapor temperature value of the respective pressure to which it is currently exposed, then the exchanger fluid is in a liquid state. If the exchanger fluid is at a temperature above the saturated vapor temperature value of the respective pressure, then the exchanger fluid is in the gaseous state. when there is a cooling of the exchanger fluid that is in the gaseous state, the formation of condensation droplets of the exchanger fluid begins when the saturated vapor temperature value is reached.

By means of the expansion device, the exchanger fluid circulating in the circuit is expanded from a higher pressure to a lower pressure, that is, the pressure is released. During expansion, not only does the pressure of the exchanger fluid decrease to a lower pressure, but also the

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5/37 exchanger fluid temperature. The temperature that the exchanger fluid exhibits after expansion to the lowest pressure is called the exhaust vapor temperature.

According to the invention, an adjustment device is provided with which this exhaust vapor temperature can be adjusted to an exhaust vapor temperature value defined above the saturated vapor temperature value associated with the lower pressure. With such an adjustment device, the exhaust vapor from the exchanger fluid can be adjusted specifically above the lowest pressure temperature corresponding to the saturated vapor temperature value. The exchanger fluid, which has an exhaust vapor temperature above the saturated vapor temperature, is in the gaseous state. Condensation of the exchanger fluid from its gaseous state to the aggregate liquid state during and after expansion can be safely avoided. Thus, inside the corresponding expansion equipment, a vapor exchange fluid is consistently free from condensation, with no associated liquid exchange fluid percentage. Inside and outside the expansion equipment, the existing and generally liquid lubricant, in particular a lubricating oil, cannot be contaminated with the exchanger fluid. The lubricant thus kept clean reliably prevents friction between the mobile components of the expansion device and reliably seals the expansion chamber against leakage of the changing fluid. In addition, subsequent heating is not necessary to expel a liquid exchanger fluid that would otherwise normally occur in the returned lubricant. Thus, both the efficiency and the service life of the expansion device, in accordance with the invention, compared to traditional generic devices, are significantly improved.

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The solution presented by the invention is initially surprising because additional components and additional energy consumption are required for the adjustment device. In addition, compared to traditional generic devices, a higher exhaust steam temperature value. Such a higher exhaust vapor temperature results in energy loss. Comparatively less energy can also be released during expansion, which would continue to be used as mechanical energy. In accordance with the invention, however, it has surprisingly been found that the advantage of consistently changing condenser-free vapor in the expansion device far outweighs the additional energy expenditure and the resulting energy loss.

In addition, the solution presented by the invention can prevent condensation of the gas exchange fluid after expansion regardless of the various external and internal conditions of the thermodynamic cycle. Regardless of the thermal energy that the heat source presents, regardless of the temperature and pressure that the exchanger fluid has when entering the expansion device, the exhaust vapor of the exchanger fluid will always be set above the lowest pressure associated with the steam temperature value. saturated. In this way, therefore, the exhaust steam temperature value will be defined as a function of the lower pressure, which can vary depending on the temperature and the inlet pressure of the exchanger fluid in the expansion device. In this way, the inlet temperature and pressure are often dependent on the thermal energy of the heat source. In addition, the exhaust steam temperature value is defined as a function associated with the lower pressure value corresponding to the saturated steam temperature. This temperature value of saturated steam is specific for each fluid

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7/37 exchanger, so that the condensation of the exchanger fluid in the gaseous state after expansion can always be safely avoided, regardless of the type of exchanger fluid.

In accordance with the invention, the set value of the exhaust steam temperature is preferably maintained in function of the lower pressure value corresponding to the saturated steam temperature. With the temperature value of the exhaust vapor kept constant in this way, expansion and condensation after expansion within the circuit can be carried out in a particularly uniform manner without major temperature fluctuations. In particular, there is only a small loss as a result of internal friction of the exchanger fluid and small external friction losses occur in relation to the piping that carries the exchanger fluid. Other types of energy losses can be saved.

In accordance with the invention, it will be favorable to set the exhaust vapor temperature between 2 K and 12 K, preferably between 4 K and 8 K and, more preferably, between 5 K and 6 K above the temperature of the lowest pressure value exhaust steam. It has been found that even a small margin of difference between the exhaust vapor temperature and the relevant saturated vapor temperature value is sufficient to safely avoid condensation in the vapor of the exchanger fluid on expansion to the lowest pressure. For a bigger difference, land that would set a higher value of exhaust steam temperature, which would cause an unnecessary loss of energy.

In addition, in accordance with the invention, it is advantageous to adjust, by means of a regulating device, an increase in the temperature of the exchanger fluid such that the temperature of the exhaust vapor has a defined value higher than the temperature corresponding to the temperature value

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8/37 saturated steam associated with the lowest pressure. This temperature rise is easy to do.

As is known, an exchange fluid inserted in a thermodynamic cycle process in its liquid state of aggregation from a lower pressure to a higher pressure. After that, the exchanger fluid placed under higher pressure is isobarically caused to evaporate and overheat. In this way the temperature of the exchanger fluid increases. When the compressed and superheated exchanger fluid vapor is expanded to the lowest pressure, the exchanger fluid vapor temperature drops to the exhaust vapor temperature.

In accordance with the invention, the temperature of the exchanger fluid circulating in the Thermodynamic cycle is then increased after evaporation and before or during expansion by means of the adjustment device such that the temperature of the exhaust vapor is now above the temperature value of saturated steam associated with the lower pressure.

In accordance with the invention, an increase in the temperature of the exchanger fluid within the expansion device should preferably be made by means of the adjustment device. Thus, the temperature can be increased during the expansion process, which is more energy efficient than increasing the temperature of the superheated exchanger fluid vapor before expansion. Mainly, the temperature of the exchanger fluid must be increased at the end of the expansion process. Upon completion of the expansion process, the temperature of the expanding exchanger fluid vapor is lower than at the beginning or in the middle of the expansion process. In this way the temperature of the exchanger fluid can be increased with energy savings compared from a low temperature to the required temperature value, with

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9/37 which must be reached after expansion, the set temperature of the exhaust vapor.

The regulating device according to the invention also advantageously includes a steam injector for injection of steam into the exchanger fluid, such that the steam will be especially superheated steam. The vapor-forming vapor molecules move quickly and transmit in their collision movement, with corresponding speed to the exchange fluid vapor molecules, which increases the temperature of the exchange fluid vapor in a corresponding way. In addition, depending on the temperature and the amount of steam injected, the temperature of the exchanger fluid vapor can be adjusted in a very targeted way to set the temperature of the exhaust vapor. If the steam is overheated, the temperature rise will be even faster.

Preferably, the steam injector should be adapted to inject the steam into the expansion device, in such a way that it is after the entry of steam from the thermodynamic cycle exchanger fluid into the expansion device. Thus, the temperature of the exchanger fluid vapor can be increased with energy savings during expansion. A steam addition, preferably at the end of the expansion process, in the expansion device, will be particularly energy saving according to the process described above.

In addition, the injection of steam into the expansion device has the advantage that the steam delivered can expand as additional steam. This results in an additional expansion of the additionally injected steam, which can be supplied in the form of additional mechanical energy to the expansion device. Greater performance and greater efficiency also associated with the expansion device will be achieved, which increases the efficiency of the entire device.

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In addition, in accordance with the invention, the advantage is that the steam is a fluid exchange vapor. Thus, despite the supply of additional steam, the exchange fluid remains pure exchange fluid, which is not contaminated with vapor from another exchange fluid. Preferably, the exchanger fluid vapor comes from the same thermal cycle as the exchanger fluid vapor itself, which must be injected into the expansion device at the beginning of the expansion. In this way there will be savings in energy and components due to the economy of having the need for only a single generation of steam, in which thermal energy can be transferred from a heat source.

In accordance with the invention, it is advantageous that the expansion device has been designed as a positive displacement machine in the passage of the exchanger fluid that is transformed into at least one expansion space or increased volume space. For this purpose, there is an inlet to inject high-pressure exchanger fluid vapor into the expansion space. The injected exchanger fluid vapor then displaces a space-limiting component of the expansion chamber. As a result, the expansion space is increased and, at the same time, displaces the mechanical work execution component. Expansion of the expansion chamber causes the exchange fluid vapor to expand from an increased pressure to a lower pressure.

In such a positive displacement machine, the exchange fluid vapor can be injected through an inlet and the additional steam injected into an additional inlet in a position between the inlet of the steam supply and the outlet to the expansion chamber. Thus, the vapor of exchanger fluid can expand in the passage through the expansion chamber and during the enlargement of the chamber it can be reheated through the injected steam. Concomitantly with the steam supplied, the

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11/37 reheated fluid exchange steam can continue to expand towards the exhaust valve.

Specifically targeted, the injection of steam into the positive displacement machine can be designed so that there are two or more expansion chambers. The steam injection can, in this case, be designed so that additional steam is injected specifically into the expansion chamber, when the expansion chamber has reached a desired size. Correspondingly with this dimension, there will then be vapor from the exchanger fluid which will be expanded and cooled, and which must then undergo directed heating. The heated exchanger fluid vapor can then continue to expand in the expanding space of the expansion chamber, until the expansion chamber can reach an outlet, whereby the exchanger fluid vapor and the additional vapor can escape. In this case, at least, the inlet for the exchanger fluid vapor must be located sufficiently distant from the steam injection installation, so that the expansion chamber for the inlet is located spatially well separated from the expansion chamber for steam injection. Preferably the exhaust will be spatially far enough from the steam supply so that an exhaust expansion chamber is located spatially separate from the expansion chamber where the steam injection is located. This will allow for a particularly targeted increase in temperature during expansion to a defined expansion zone. The defined expansion zone will then correspond to the size of the steam injection expansion chamber.

In addition, in accordance with the invention to advantageously generate, by means of the adjustment equipment, a return pressure on the exchanger fluid so that the exhaust vapor has the vapor temperature

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12/37 exhaust above the minimum pressure temperature value of the associated saturated steam. Structuring such a back pressure is particularly efficient for saving energy.

With this back pressure, the lower pressure is not initially reached during expansion, but a reduced, increased pressure, corresponding to the increase in back pressure. This reduced pressure, increased, will be associated with a corresponding saturated vapor temperature value of the exchanger fluid. By means of the back pressure, the exchanger fluid vapor will initially be maintained at a higher reduced pressure and thus has an exhaust temperature, which will correspond to this increased saturated vapor temperature value. After further expansion, the increased reduced pressure corresponding to the back pressure is then relaxed or expanded to the lowest pressure. After the remaining pressure is relaxed, the exchanger fluid vapor will have an exhaust temperature that corresponds to the set exhaust temperature value, above the exhaust temperature value of the reduced saturated steam pressure. In this way the condensation of the exchange fluid vapor is safely avoided during the entire expansion process.

For this purpose, an expansion device is preferably provided to expand the exchanger fluid from a higher pressure to a lower pressure, in which the lowest pressure can be achieved by means of a two-stage expansion process. The highest pressure is achieved in a first expansion stage by generating or increasing the back pressure pressure, for a reduced first pressure. Then, the first reduced pressure is expanded in a second expansion phase to a second reduced pressure, where the second reduced pressure

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13/37 will correspond to the reduced pressure mentioned above, after expansion.

In this process, the first and second expansion stages can occur on a single expansion device. In a particularly preferred manner, the execution must be of the first expansion stage on a first expansion device and the second expansion stage carried out separately on a second expansion device. The first expansion device is designed in particular with a positive displacement machine and the second structurally simple expansion device as a conductive element within the duct that carries the exchanger fluid. The first and second expansion means then represent the total expansion device.

In addition, the adjustment device, in accordance with the invention, advantageously comprises a locking element for the generation of back pressure on the exchanger fluid, which is designed particularly with a valve to selectively open and close the duct that conducts exchanger fluid. By means of the blocking element, a stream of exchanger fluid or exchanger fluid flow of the exchanger fluid contained in the cyclical process can be switched off by its particularly simple and quick construction. After this shutdown, the desired back pressure builds up in the exchanger fluid. The back pressure can be released again with a short reaction speed, if necessary, by placing a valve on the locking element that can be easily reopened.

Preferably, the locking element is arranged in the expansion device between the first and the second expansion device, thus enabling the expansion process in two stages as described.

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Furthermore, according to the invention, advantageously, the exchanger fluid is guided in a circulatory direction and in that circulatory direction downstream of the expansion device, a condensing device is provided for condensing the expanded exchanger fluid, in which the adjustment device includes, a temperature measuring element for measuring the temperature of the exchanger fluid in the direction of circulation after expansion and before condensation and / or a pressure measuring element for measuring the pressure of the exchanger fluid in the direction of circulation after expansion and before expansion condensation. Using a temperature measuring element and / or pressure measuring element, a control device is possible, with which the regulating device is regulated according to the measured temperature and / or the measured pressure. With such regulation, the adjustment device can be used to adjust the exhaust vapor temperature adapted to the need and reliably to the defined exhaust vapor temperature value.

In this case, the temperature measuring element in particular measures the temperature of the exhaust vapor of the exchanger fluid after expansion. The temperature of the exhaust steam also depends on the inlet temperature of the exchanger fluid vapor at the injection into the expansion device. In addition, the temperature of the exchanger fluid before condensation or condensation temperature can be determined. The value of the condensing temperature corresponds, in particular, to the value of the temperature of the saturated steam associated with the lowest pressure. With the pressure measuring element, a current saturated vapor pressure value or valid condensing pressure value of the exchanger fluid can be measured, just before condensation, which depends on the cooling capacity of the condensing device.

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In addition, the invention is intended to be a method of converting thermal energy from a heat source into mechanical energy by means of a thermodynamic cycle, by means of a exchanger fluid, in which each pressure, a saturation temperature value of the associated exchanger fluid medium circulating in a cyclical process and, thus, exposed to alternating pressures, where each pressure index corresponds to a temperature value of the saturated vapor exchanger fluid, as well as an expansion stage of the exchanger fluid of a higher pressure to lower pressure, where the exchanger fluid after expanding to reduced pressure has an exhaust vapor temperature. Where the exhaust vapor temperature is adjusted to an exhaust vapor temperature level set above the reduced pressure associated with the vapor saturation temperature.

The advantages of such a method in accordance with the invention will become apparent from the advantages already described in the description of the device in accordance with the invention.

BRIEF DESCRIPTION OF THE DRAWINGS

In the following, examples of implementing the solution in accordance with the invention are explained in greater detail from the accompanying schematic drawings. It is shown below:

Figure 1 is a simplified scheme of the process for a device for converting thermal energy according to technology,

Figure 2 shows a schematic pressure enthalpy diagram (log) of the thermodynamic cyclical process according to Figure 1,

Figure 3 shows the vapor curve of exchanger fluid contained in a cyclic process,

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Figure 4 shows detail IV in accordance with Figure 1 of a first example of making an exhaust device in accordance with the invention,

Figure 5 is a schematic pressure enthalpy diagram (log) of the thermodynamic cyclical process in accordance with Figure 4,

Figure 6 shows a cross section of a positive displacement machine of the device in accordance with Figure 4,

Figure 7 shows detail IV in accordance with Figure 1 of a second example of how a device is made and

Figure 8 is a schematic pressure enthalpy diagram (log) of the cyclical thermodynamic process Figure 7.

DETAILED DESCRIPTION OF THE PERFORMANCE

In the Figures, a device 10 and a corresponding procedure 12 are shown, for converting thermal energy from a heat source 14. Device 10 forms a closed system of a process installation in which a thermodynamic cycle 16 which by means of a cyclical process 16 in which is exchanged fluid that flows through it.

The detailed thermodynamic cyclical process 16 is a modified Organic Rankine Cycle (ORC) process in which the exchanger fluid is an organic exchanger fluid. The one available is using ammonia as a exchanger fluid, preferably with anhydrous ammonia (NH3, R 717) in a concentration of more than 99.6 percent by weight. With an almost pure ammonia, the physical and thermodynamic properties of ammonia can be exploited without interfering with other substances. Thus, liquid ammonia has a high enthalpy of vaporization, with which a relatively high amount of energy must be used to convert ammonia from its liquid state to the gaseous aggregate state. Consequently, a

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17/37 corresponding amount of energy can be stored in the gaseous ammonia and then converted into mechanical energy in the expansion.

As a heat source 14, low temperature heat sources are used. In this case, the project may provide for use in the heat source 14 a single heat source 14 or with two different heat sources 14 and 17. In the detailed embodiments, two different heat sources are used, one of which, the heat source. heat 14 has a lower temperature than the heat source 17. In this case, the heat source 14 is the residual heat from an engine and the heat source 17 is the heat from the exhaust gases of an internal combustion engine. a cogeneration thermal power plant.

Belonging to a cyclical process 16 there are collection containers 18 for the provision of exchanger fluid in the form of liquefied gas under pressure. In this case, the exchanger fluid is under a pressure that represents a reduced pressure 20 at a lower pressure level than that of the thermodynamic cyclical process 16. Starting from the collection container 18, a duct 22 conducts the exchanger fluid in a direction of circulation 24 for a pressure increasing device 26. With the pressure increasing device 26, the pressure to which the exchanger fluid is exposed is increased from the reduced pressure 20 to an elevated pressure 28 which represents an upper pressure level of cycle 16 .

Subsequently, in the direction of circulation 24, the liquid exchanger fluid is pumped from the pressure increase device 26 through the duct 22 to a heat transfer device 30. The heat transfer device 30 comprises a first heat exchanger 32 and connected in series, a second heat exchanger 34. The first heat exchanger 32 is a heat exchanger by means of a heat exchanger fluid through a duct connection 36

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18/37 with the heat source 14. Consequently, the second heat exchanger 34 is connected via a duct connection 38 in which a heat exchanger fluid circulates, with the heat source 17.

Between the two heat exchangers 32 and 34, a separator 40 is arranged having a portion of the lower area 42 and a portion of the upper area 44. In the upper area 44, the liquid exchanger fluid is injected through the pipe 22. Liquid exchanger fluid it separates from the possibly existing gaseous exchanger fluid and flows into the lower area zone 42. From there, a pipe 46 conducts the liquid exchanger fluid medium thus separated into the first heat exchanger 32, which serves for the preheating and vaporization. There, the exchanger liquid is preheated by transferring thermal energy from the first heat source 14 and vaporized for the most part. A vapor exchange fluid thus produced is a wet vapor. This means that there are still small drops and finely distributed exchanger fluid liquid is present as part of the condensate in the exchanger fluid in a gaseous state. This wet steam flows out of the first heat exchanger 32 through a pipe 48 to the upper area 44 of the separator 40. In this operation, the condensed part flows into the lower area 42 and joins there as a liquid exchanger in the liquid state, while in the upper area 44 only exchanger fluid remains in the gaseous state. Therefore, a particularly dry gas exchange fluid can be generated. The liquid exchanger in the liquid state flows from the lower area 42 through the tubing 46 back to the first heat exchanger 32 for reheating.

With the separator 40, having pipe 22 and 48 located in its upper area portion 44 as well as leaving the lower area portion 42, pipe 46, vaporization is possible according to the thermosiphon principle.

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This principle is based on the fact that during evaporation in the first heat exchanger 32, the density of the exchanger fluid located there is reduced due to the wet vapor formed. Thus, the wet steam forced through the pipe 48 to the separator 40. In addition, the same amount of liquid exchanger fluid necessary for vaporization always flows back through the pipe 46 to the first heat exchanger 32. In the separator 40 , a level controller not shown, with which the pressure increase device 26 can be adjusted, so that only the amount of exchanger fluid is pumped into the first heat exchanger 32, which can also be evaporated.

From separator 40, the gaseous exchanger fluid in the upper area 44 flows through a duct 50 to the second heat exchanger 34. The second heat exchanger 34 serves as a superheater, with which the gaseous exchanger fluid it must be overheated by transferring thermal energy from the heat source 17. The superheated exchanger fluid vapor is then passed from the second heat exchanger 34 through a pipe 52 through an inlet valve 54 to an expansion device 56.

By means of the expansion device 56, the steam fluid exchanger overheated and expanded from the high pressure 28 to the reduced pressure 20, at the same time as the temperature of the exchanger fluid decreases. The energy released in this way is transmitted as mechanical energy to the expansion device 58, which serves as a motor unit for driving a generator coupled to the expansion device 56 to generate electrical energy.

In the present case, it is a provision for connecting expansion devices in parallel to the

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20/37 expansion 56, in which the vapor of compressed and overheated exchanger fluid is injected by means of an associated additional inlet valve. For a better overview, the additional expansion device with its associated components is designated by the same reference design as the expansion device 56. With such a parallel connection of the expansion devices 56, a particularly uniform expansion is possible over the over time, steam from the superheated exchanger fluid without great pulsations. In addition, if necessary, a greater amount of vapor from the exchange fluid can be expanded. In this way, a uniform and high performance of the thermodynamic cycle 16 can be achieved. To improve this effect, more than two expansion devices 56 connected in parallel can be provided.

The vapor of expanded exchanger fluid is expelled outwardly in the direction of circulation 24 after the expansion device 56 through a pipe, that is, exhaust duct 60 exiting the expansion device 56 and passing through a condenser device 62. With the condenser device 62, the expanded exchanger fluid vapor is cooled and condensed. The condensed exchanger fluid is passed to the collection container 18, which is arranged in the duct

22 in the direction gives circulation 24 after the device in condensation 62. With condensation o thermodynamic cycle 16 it's done and can be repeated how many times for required. Beyond of this , the device 10 have a circuit in

oil supply 64, each with an oil supply pipe 66, through which an oil must be injected via a corresponding oil inlet valve 68 into expansion device 56. The oil serves to seal and lubricate the components expansion device

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56. During expansion of the exchanger fluid vapor, the oil in the expansion device 56 can enter the exchanger fluid vapor. For this reason, the steam exchange fluid expanded with the oil in each expansion device 56, must be vented through the associated exhaust steam duct 60 to an associated oil separator 70. With the oil separator 70, the oil in the expanded exchanger fluid vapor must be separated. For this purpose in the oil separator 70 described above, a separating element 71 has been designed as a mechanical separator. The separating element 71 separates the oil from the vapor of the exchanger fluid expanded as a gas as a liquid, mechanically and due to the different densities of liquid and gas.

The steam of expanded exchanger fluid thus purified is passed from the oil separator 70 through the exhaust duct 60 in continuity of the cyclical process 16 to the condensing device 62.

The separated oil is directed from each oil separator 70 through an associated oil discharge pipe 72, to an oil collection vessel 74. In this case, the separated oil may contain a portion of liquid changer fluid, which formed during expanding the vapor from the exchanger fluid medium in a conventional manner. To remove this part of the liquid exchange fluid in the oil collection vessel 74, an oil heater 76 is provided. With the oil heater 7 6, the separated oil is heated for so long and until the proportion of liquid exchange fluid has been almost completely evaporated or expelled from the oil. The exchange fluid vapor resulting from the process is guided through a steam circulation duct 78 out of the oil collection container 74 in the direction of circulation 24 between the oil separator 70 and the condenser device 62

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22/37 back to the exhaust steam duct 60 and thus to the cyclical process 16.

An oil pump 80 is also arranged in the supply line 66, with which the oil separated from the exchanger fluid in a liquid state thus purified, passes through an oil supply line 66 again returning to the expansion device 56. In addition In addition, the oil heater 76 comprises a heating source driven by a heating circuit pipe 82 which is coupled to the second heat source 17 for heat transmission.

Figure 2 shows a schematic diagram of enthalpy of pressure (log) of the thermodynamic cycle 16 of method 12, which by means of device 10 can be performed according to Figure 1. In this case, it is drawn on the axis of the logarithmic pressure ordinates 83 and on the abscissa axis, enthalpy 84. The arcuate curve drawn represents the phase limit curve 85 of the exchanger fluid. While the phase limit curve 85 is increasing, this curve represents the boil in which a transition from the saturated liquid exchanger fluid to wet steam occurs. If the phase boundary curve 85 is descending, it represents the dew point, which defines the transition from wet vapor to saturated exchanger fluid vapor. In the transition of this type, steam is also referred to as saturated steam. An area bounded by the phase boundary curve 85 and the abscissa axis, is wet vapor 86 of the exchanger fluid, in which the vapor of the exchanger fluid as a gas phase and liquid exchanger fluid as the liquid phase are present at the same time.

Starting from the exchanger liquid that is under reduced pressure 18, a process step is made, that is, a step of increasing the pressure 88 of the exchanger fluid through the pressure increasing device 26, placing the fluid under the

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23/37 high pressure 28. Ammonia is subjected to a reduced pressure 18 of about 8.4 bar, at a temperature of about 23 ° C to a high pressure 28. of about 37 bar and a temperature of about 30 ° C.

All pressure values given here must be understood as absolute pressure values.

With the first heat exchanger 32, in a preheating step 90, the heat exchanger fluid under high pressure 28 is heated by isobaric transformation to an evaporation temperature value associated with high pressure 28. For ammonia, this value is around 76 ° C. Subsequently, in a vaporization step 92, the still liquid, preheated to the evaporation temperature, the exchanger fluid is vaporized by isobaric transformation. During step 92, the main part of thermal energy is supplied to the exchanger fluid. During vaporization, the temperature of the exchanger fluid remains constant. Subsequently, by means of the second heat exchanger 34, in an overheating step 94, the vapor of the exchange fluid produced in step 92 is superheated by isobaric transformation to a final temperature. The final temperature for ammonia is about 120 ° C.

The steam exchange fluid superheated in this way as ammonia gas is in an expansion step 96 by means of the two expansion devices 56 connected in parallel, expanded by an adiabatic system. Adiabatic or isolated means that there is no heat exchange with the environment during expansion. During the expansion the real conversion of thermal energy into mechanical energy takes place. In this case, when entering the expansion device 56, the exchanger fluid has high pressure 28 as the injection pressure and the temperature of the superheated exchanger fluid in the form of steam as the inlet temperature. The exchanger fluid that comes out

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24/37 of the expansion device 56 then has the reduced pressure 20 as being, exhaust vapor and exhaust temperature which is below the inlet temperature. The ammonia inlet has a high pressure 28 of about 37 bar and the inlet temperature of about 120 ° C and the ammonia outlet has a reduced pressure 20 of about 8.4 bar and an exhaust temperature of about 23 ° Ç. In this case, the vapor of the exchanger fluid contains a liquid fraction in the exhaust vapor, since both the inlet temperature and the exhaust temperature are subject to certain tolerances. With a slightly lower inlet temperature, condensate forms in the exhaust vapor. The then reached escape temperature, that is, the end point of expansion step 96, is in the context of wet steam 86.

Subsequently, the expanded exchanger fluid leaving the expansion device 56 is in the condensation step 98, by means of the condensation device 62 it is condensed by isobaric transformation and thus reaches its initial state in the cyclic process 16 again.

Figure 3 shows its saturation vapor pressure curve or vapor pressure line or vapor curve 100 of the exchanger fluid contained in the cyclic process 16, in the case

present, the steam curve 100 of ammonia. In case The temperature is represented at the ordinate axis and The pressure on abscissa axis . THE curved line represents The

vapor curve 100 of the exchanger fluid and is the boundary line of the phase between the liquid and gaseous exchanger fluid. Therefore, it can be read on the steam curve 100 to which the saturated steam temperature value is associated with a respective pressure of the exchanger fluid, in which the gas exchanger fluid begins to condense. For the reduced pressure 20, the saturated steam temperature 102 corresponds,

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25/37 which for ammonia is 23 ° C at a reduced pressure 20 of 8.4 bar.

Figures 4 and 7 show a section of the device 10, in which, in contrast to the device 12 according to Figure 1, a regulating device 104 is provided to adjust the escape temperature of the exchanger fluid after the expansion step 96. By means of regulation device 104, the exhaust temperature is adjusted to a defined value of exhaust temperature 106 above the reduced pressure 20 corresponding to the value of the saturated vapor temperature 102. The value of the defined saturated vapor temperature 106 is between 4 K and 8 K above the reduced pressure 20 corresponding to the saturated steam temperature value 102.

In accordance with Figure 4, the regulating device 104 comprises a connection for the supply of steam 108 for injection of steam during expansion step 96 for each expansion device 56. Such steam supply is also referred to as intermediate injection. With this type of steam supply 108, the temperature of the exchanger fluid vapor can be increased during expansion, such that the escape temperature of the exchanger fluid after step 96 already has the set exhaust vapor temperature 106.

For this purpose, the steam supply 108 is designed with a steam supply duct 110 containing an additional inlet valve 112 arranged therein, which leads, in the direction of circulation 24, after the inlet valve 54 to the expansion device 56 corresponding. With such a connection, it can be conducted via the second heat exchanger 34 vapor of superheated exchanger fluid from the duct 52 through the additional intake valve 112 into the expansion device 56. In this

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In this case, the superheated exchanger fluid vapor is passed, at a more advanced stage, in particular at the end of the expansion step 96, into the expansion device 56.

In addition, the regulating device 104 according to Figure 4 comprises one in each expansion device 56, corresponding temperature measurement element 114, which is arranged in the direction of circulation 24 after expansion just after each oil separator 70. In this way, the temperature of the exchanger fluid can be determined by means of the temperature measuring element 114. In addition, a temperature measuring element 116 and shortly before a pressure measuring element 118 are placed in the direction of circulation 24 and shortly before the condensing device 62.

Corresponding to the condensing device 62 a pressure measuring element 118 and the temperature measuring element 116 are correspondingly to the expansion device 56 coupled to the temperature measuring element 114. In addition, the measured values in one for each expansion device 56, transmitted to the control device 120. The control device 120 then opens and closes the additional inlet valve 112 for injecting steam into the expansion device 56 depending on the measurement result.

Concomitantly, the current valid pressure value of the reduced pressure 20 immediately before the condensing device 62 is measured using the pressure measuring element 118. The reduced pressure 20 can vary depending on the value of the inlet pressure of the high pressure 28 in the expansion device 56 and depending on the condensing temperature of the condensing device 62.

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Corresponding to the value of the measured pressure of reduced pressure 20, the corresponding valid temperature of saturated steam 102 is obtained in the control device 120, vapor curve 100. Depending on the valid value of the saturated steam temperature 102, by means of inlet control device 120 the additional intake valve 112 will be kept open for as long or with such an opening until with the temperature measuring element 114 the defined temperature of the exhaust vapor 106 is measured. Depending on the duration and from the opening of the intake valve 112, in this way a corresponding amount of additional steam is supplied until the temperature of the defined exhaust steam 106 is reached mainly is kept constant.

Alternatively or additionally, with the temperature measuring element 116, the temperature value of the exchanger upstream of the condensing device 62 can be determined. This measured temperature value corresponds to a valid current saturated steam temperature value 102, which will depend on the cooling capacity of the condensing device 62. The cooling capacity may vary according to the temperature of the refrigerant. In particular, when the refrigerant is structurally removed, especially simplified and inexpensive air from the environment, the cooling capacity is directly dependent on the prevailing outdoor temperature. Depending on the currently valid measured value of the saturated steam temperature 102, by means of the control device 120 the additional intake valve 112 is opened for so long and / or opened until the temperature reading element 114 is able to read the temperature exhaust steam 106.

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28/37

Conditional on the measured value of the saturated steam temperature, currently valid 102, according to the steam curve 100 the corresponding saturated steam value can be determined. This pressure value of the saturated steam corresponds to the reduced pressure 20.

In Figure 5, in contrast to the diagram in accordance with Figure 2, lines corresponding to the isotherms are additionally inserted, that is, curves of the same temperature, thus 122 represents the isotherm122 of 20 ° C, and 124 the isotherm- 124 ° C at 30 ° C. In addition, it can be identified during step 96, how the temperature of the exchanger fluid increases when receiving superheated exchanger fluid vapor at the end of the expansion process through the steam supply 108. Upon reaching the reduced pressure 20, the exchanger fluid has the exhaust vapor temperature set 106 above the reduced pressure 20 to the saturated vapor temperature value 102. Thus, the end of step 96 will be relatively far from the wet vapor area 86, in such a way that condensed parts exhaust steam is reliably avoided. In the case of ammonia, the set value of the exhaust steam temperature 106 corresponds to about 28 ° C and is thus about 5 K above the value of the saturated steam temperature 102 of about 23 ° C with the reduced lower pressure 20 of about 8.4 bar.

Figure 6 shows the expansion device 56 used in device 10 in accordance with Figure 4 and equipped with a rotary sliding machine as a displacement machine. The rotary sliding machine is a rotary piston expander that is placed previously to a rotary piston compressor and in the present case is a vane cell expander.

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29/37

Such a vane cell expander has a cylindrical ring 126 with an inlet 128 and an exhaust 130. The inlet 128 serves to allow injection at high pressure 28 of the exchanger fluid vapor and the exhaust 130 to discharge the expanded exchanger fluid vapor. . In this case, for each direction of the flow of steam from the exchanger fluid there is an indication of a flow arrow. The cylindrical ring 126 is formed by a hollow cylinder whose surface of the inner sleeve forms an inner wall of the ring 132. In the cylindrical ring 126 eccentrically to the axis of the hollow cylinder one, rotary piston 134 is centrally mounted around a rotational axis 136. The rotary piston 134 contains along its longitudinal deflection eight grooves 138, in each of which there is a corresponding slide 140 mounted radially and being able to be displaced to both sides.

To limit the cylindrical ring 126 in the axial direction, two opposing retaining surfaces are provided, but are not shown. The two containment surfaces delimit, with the rotary plunger 134, the inner wall of the ring 132 and the eight slides 140 of the eight cells 142 the corresponding variable volume 144.

The individual variable volume 144 is formed by the movement in which the respective slide 140 during rotation, through the centrifugal force is pressed against the inner wall of the ring 132 making a seal. Because the rotary piston 134 is eccentrically mounted on the cylindrical ring 126, the distance between the rotary piston 134 and the inner wall of the ring 132 varies during the rotation movement. For this reason, the respective slide 140 during rotation is pushed into the groove 138 associated back and forth. When the distance is extended, the slide 140 is pushed out of the associated slot 138, up to the maximum distance and thus also the maximized volume of the volume 144

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30/37 is reached. Subsequently, the distance is reduced again and the slide 140 sliding along the inner wall of the 132, is, as it were, driven by the inner wall of the ring 132 into the associated groove 138, until the minimum distance and thus the minimum volume of the volume 144 is reached.

The variable volume 144 during the rotating movement grows from the intake 128 to the exhaust 130, so that in the passage of the exchanger fluid vapor under high pressure 28, this exchanger fluid vapor is expanded. During expansion, the exchanger fluid vapor presses in the orbital direction against a slide 140 respectively, in such a way that the rotation movement starts and is maintained. In this way the axis 136 is driven which in turn drives the generator 58 to generate the electric current.

The variable volume 144 of each cell 142 is in its capacity, depending on the rotation angle corresponding to the rotation movement, which can be divided into successive individual rotation angle zones. Thus, volume 144 in a rotational angle zone 146 has its minimum volume. At inlet 128, volume 144 increases in a rotating angle zone 148 slowly during the injection of steam from the compressed exchanger fluid and is expanded in the rotating angle zone 150 to its maximum volume. In the contraction, the temperature of the vapor of the exchanger fluid decreases. Before reaching the maximum volume, through the steam supply duct 110 of exchanger fluid through supply 108, the superheated vapor of exchanger fluid is introduced by intermediate injection into each cell 142 Thanks to the intermediate injected exchanger fluid vapor, the the temperature of the expanding exchanger fluid vapor is increased to such an extent that the exhaust vapor in the exhaust 130 of the exchanger fluid vapor has the value of the temperature set for steam

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31/37 exhaust 10 6. The exchanger fluid vapor with this intermediate and expanded heating at its maximum volume then flows into a rotating angle zone 152, except for a small residual volume from the exhaust 130. The exchanger fluid vapor that leaves through the exhaust 130 of each cell 142 it is in this case the exchanger fluid vapor admitted through the inlet 128 with the intermediate injected exchanger fluid vapor. The residual volume remains in the respective cell 142 and in the rotating angle zone 146 it is compressed through until inlet 128 again exchanger fluid vapor is injected. This process is repeated periodically.

The expansion ratio, that is, the ratio between volume 144 at intake 128 and volume 144 at exhaust 130 is set to 1 to 3 through 1 to 4 and thus specially adapted for the ammonia as an exchange fluid.

In order to seal and lubricate the respective groove 138 and the corresponding slide 140, the radial and axial cracks that occur, there is provision for an oil supply pipe 66 to supply oil (Figure 4). With this oil, the slide surface of slide 140 along the inner wall of ring 132 is specially sealed and lubricated. The oil mixes with the vapor of the exchanger fluid when it expands, as already described and is discharged through the exhaust steam duct 60 through the oil separator 70 leaving the expansion device 56. In the oil separator 70, the oil separates again from the exchange fluid vapor. Due to the fact that the oil separated by means of equipment 10 in accordance with Figure 4 and Figure 7, a significant part of liquid exchanger fluid is reliably avoided, oil heater 76 can normally be required in accordance with Figure 1 be discarded with the respective energy savings.

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In the device 10 of Figure 7 it is through the installation of a regulating valve 104 that a return pressure is achieved on the exchanger fluid, such that the vapor escaping from the expanded exchanger fluid will have the set temperature value of the exhaust vapor 106 above the reduced pressure 20 corresponding to the saturated steam temperature value 102. For this purpose, a control valve is provided, that is, a steam exhaust control valve 154 as a locking element 156, with which the steam pipe of the duct exhaust 60 can be blocked. With this block, a reduction in the pressure of the exchanger fluid in the direction of circulation 24 is avoided. The exchanger fluid is dammed in the exhaust steam duct 60 in the opposite direction of circulation 24, that is, damped in the flow direction, so the desired back pressure can be generated. With an opening of the exhaust control valve 154, the back pressure can be reduced again when necessary.

For the regulation of the exhaust valve control register 154, the configuration of the regulating equipment 104 of the device 10 in accordance with Figure 7 the temperature measurement element 114 of the expansion in the direction of circulation 24, just before the control valve exhaust valve 154. After the exhaust control valve 154 and just before the condenser device 62, the temperature measuring element 116 is placed with which the temperature value of the saturated vapor 102, of the exchanger fluid, as described for Figure 4, can be determined. In addition, the pressure measuring element 118 is provided in the direction of circulation 24 after the exhaust control valve 154 and immediately before the condensing device 62. With the pressure measuring element 118, a pressure value in the cyclical process 16 currently valid for reduced pressure

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33/37 can be measured just before the condensing device 62 in accordance with the executions related to Figure 4.

The temperature measuring elements 114 and 116 as well as the pressure measuring element 118 are coupled to transmit data to the control device 120, which closes or opens the exhaust control valve 154 depending on the measurement result. Corresponding to the measured pressure value of the reduced pressure 20, and thus the currently valid saturated steam pressure results stored in the control device 120 in accordance with the steam curve 100 corresponding to the valid temperature value for the saturated steam 102. Depending on of the valid temperature value of the saturated steam 102 by means of the control device 120, the exhaust regulating valve 154 is kept as long and / or so open, until the temperature value 114 or 116 is set with the temperature value exhaust steam 106 is measured.

In Figure 8 it can be seen that through the exhaust control valve 154 the exhaust pressure can be raised to a first reduced pressure 158, which will be slightly higher than the reduced pressure 20. In this way the superheated exchanger fluid vapor by means of the expansion device 56 it initially goes on a first expansion stage 160 for the first reduced pressure 158. For ammonia, this first reduced pressure 158 is about 12 bar. For this first reduced pressure 158 in accordance with the steam curve 100, a saturated steam temperature of about 33 ° C corresponds.

In the direction of circulation 24 after the exhaust control valve 154, the first reduced pressure 158 is residually expanded to a second expansion stage 162 of the reduced pressure corresponding to the reduced pressure 20. The reduced pressure 20 is the condensing pressure of the fluid

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34/37 exchanger, that is, the pressure at which the exchanger fluid is condensed in the condensing device 62. In Figure 8, it can be seen that the temperature of the exchanger fluid after expansion to reduced pressure 20 has the set value of exhaust steam 106 above that of the reduced pressure 20 corresponding to the saturated steam temperature value 102. The end point of step 96 is thus located outside the wet steam region 86, whereby condensation of the exchanger fluid vapor is prevented.

In another form not shown, for example, the pressure increase device 26 is designed with a steam pump. The steam pump serves to increase the pressure in the exchanger fluid by the action of steam on the exchanger fluid. For this purpose, the steam pump is a heat transmitter by means of the heat transfer device 30 and a steam transmitter connected to the heat source 14. heat transfer device 30 which forms steam from exchanger fluid must be partially transferred from the steam transmitter to the steam pump. In this way, the thermal energy from the heat source 14 can be particularly well used and also electrical energy would otherwise be required for the pressure booster 26 can be saved. Overall, efficiency can be increased again.

In addition, through the solution according to the invention, there can also be optimization in a drying process to dry a substance. In addition, the energy released in the condensation step 98 of the exchanger fluid can be connected with energy transmission for the drying process. In addition, residual engine heat as well as residual exhaust gas heat will be used for drying the substance as additional heat sources 14 and 17

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35/37 of some process of burning flammable material mainly biogas.

LIST OF REFERENCE NUMBERS

Device for converting thermal energy procedures heat source thermodynamic cyclical process heat source collection containers reduced pressure duct, pipe direction of circulation, circuit high pressure increase device heat transfer device first heat exchanger second heat exchanger duct, duct pipe, separator pipe lower area upper duct area, duct pipe, duct pipe, duct pipe, inlet valve expansion device generator exhaust steam duct or exhaust duct condensing device oil supply circuit supply pipe of oil or feed

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36/37 oil inlet valve oil separator separation element oil discharge pipe oil collection container

Oil heater steam circulation ducts

Oil pump heating circuit pipe logarithmic pressure enthalpy

85 Curve in phase limit 86 area < wet steam 88 stage in increased pressure 90 stage in preheating 92 stage in vaporization 94 stage in overheating 96 stage in expansion 98 stage in condensation

100 Steam curve

102 value of saturated steam temperature

104 regulating device

106 set exhaust steam temperature

108 steam supply

110 steam supply duct

112 inlet valve

114 temperature measuring element

116 temperature measuring element

118 pressure measuring element

120 control device

122 isothermal at 20 ° C

124 isothermal at 30 ° C

126 Cylindrical ring

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37/37 inlet exhaust inner wall of the ring rotary pistons shaft slide slide cells volume

zone in angle rotary zone in angle rotary zone in angle rotary zone in angle rotary

valves or exhaust control valve blocking element first reduced pressure first expansion stage second expansion stage

Claims (10)

1. Device (10) for converting thermal energy from a heat source (14, 17) into mechanical energy by means of a thermodynamic cyclical process (16) with - an exchange fluid, which circulates in a cyclical process (16) and thus exposed to a variable pressure, where for each respective pressure it is associated with a saturated vapor temperature value of the exchange fluid, as well as - an expansion device (56) for expanding the exchanger fluid from a high pressure (28) to a reduced pressure (20), wherein the exchanger fluid after expanding to the reduced pressure (20) has an exhaust temperature, characterized in that a regulating device (104) is provided to adjust the exhaust steam temperature to a defined exhaust steam temperature (106) above the reduced pressure value (20) corresponding to the saturated steam temperature value (102) . Equipment according to claim 1, characterized in that the value of the exhaust vapor temperature (106) is between 2 K and 12 K, preferably between 4 K and 8 K as well as particularly preferably between 5 K and 6 K above the reduced pressure (20) corresponding to the saturated steam temperature value (102). 3. Equipment, according to claim 1 or 2, characterized by the fact that, by means of the regulating device (104), it is possible to increase the temperature of the exchanger fluid in such a way that the temperature of the exhaust vapor will present the set exhaust steam temperature value (106), above that of the reduced pressure (20) corresponding to the saturated steam temperature value (102). 4. Equipment, according to claim 3, characterized by the fact that, by means of the Petition 870190080769, of 20/08/2019, p. 66/68 2/3 setting (104), the temperature of the exchanger fluid inside the expansion device (56) can be increased. Equipment according to one of claims 1 to 4, characterized in that the means of the regulating device (104) comprises a supply of steam (108) to supply steam to the exchanger fluid, the steam being especially superheated steam. 6. Equipment according to claim 5, characterized by the fact that the vapor is an exchange fluid vapor. 7. Equipment according to one of claims 1 to 6, characterized by the fact that, by means of the regulating device (104), it is possible to generate such a counter pressure on the exchanger fluid, that the exhaust vapor has the value set exhaust temperature (106) above the reduced pressure (20) corresponding to the saturated steam temperature value (102). 8. Equipment according to claim 7, characterized in that the means of the regulating device (104), in order to generate the back pressure on the exchanger fluid, comprises a locking element (156) which is specially designed with a valve exhaust control (154) to selectively open and close a pipe that conducts the changing fluid (60). 9. Equipment according to one of claims 1 to 8, characterized in that the exchanger fluid circulates in the direction of the circuit (24) and in this direction of the circuit (24) after the expansion device (56), a device is provided condensing device (62) for condensing the expanded exchanger fluid, where the regulating device (104) includes a temperature measuring element (114, 116) for measuring the temperature of the exchanging fluid in the direction of the circuit (24) after expansion and before condensation and / or a Petition 870190080769, of 20/08/2019, p. 67/68 3/3 pressure measuring element (118) for measuring the pressure of the exchanger fluid in the direction of the circuit (24) after expansion and before condensation. 10. Procedure (12) for converting thermal energy from a heat source (14, 17) into mechanical energy by means of a thermodynamic cyclic system (16) with an exchanger fluid, which flows in the cyclic system (16) and exposed to a variable pressure, and where each respective pressure is associated with a temperature value of the saturated vapor of the exchanger fluid, as well as a step (96) of expansion of the exchanger fluid from a high pressure (28) to a reduced pressure (20), where the exchanger fluid after expansion to reduced pressure (20) has an exhaust temperature, characterized by the fact that the exhaust temperature is at a defined exhaust vapor temperature (106), set above the corresponding reduced pressure (20) to the temperature value of the saturated steam (102).