EP4306775A1 - Method and apparatus for converting low-temperature heat into technically usable mechanical energy - Google Patents

Abstract

In a two-stage process (Fig. 5), thermal energy from a low-temperature source with temperatures of maximum 200°C is first converted into potential energy in a first energy converter using a novel E-TLC process, and then the potential energy is converted into technically usable mechanical energy in a second energy converter.

Description

The invention relates to methods and devices for converting low-temperature heat with a temperature of less than 200 ° C into technically usable mechanical energy and subsequently electrical energy.

State of the art

Due to the small temperature difference between low-temperature heat sources and possible heat sinks such as water or ambient air and the resulting low theoretical efficiency, it is desirable to utilize the theoretically usable thermal energy as completely as possible. This is made possible by implementing a trilateral cycle (TLC) process according to Smith ( US4,557,112 ), which has the theoretically highest exergetic efficiency compared to other thermal power processes such as a steam power process or ORC process.

• Isochore Druckerhöhung (Pkt. 1 - Pkt. 2)
• Isobare Wärmezufuhr ohne Verdampfung des Arbeitsmittels (Pkt. 2 - Pkt. 3)
• Isentrope Entspannungsverdampfung bei kontinuierlicher Druckverringerung mit gleichzeitiger Volumenvergrößerung und Verrichten von Volumenarbeit (Pkt. 3 - Pkt. 5)
• Isobare Wärmeabfuhr und Kondensation des verdampften Anteils des Arbeitsmittels (Pkt. 5-Pkt. 1)

In the TLC process according to Smith (see Fig. 1 ), a work equipment goes through the steps:

• Isochoric pressure increase (point 1 - point 2)
• Isobaric heat supply without evaporation of the working fluid (point 2 - point 3)
• Isentropic flash evaporation with continuous pressure reduction with simultaneous increase in volume and performance of volume work (point 3 - point 5)
• Isobaric heat dissipation and condensation of the evaporated portion of the working fluid (point 5-point 1)

The basic structure of a device according to the prior art is in Fig.2 shown. Starting at point 1, a working fluid is put under working pressure by a pressure pump, external heat is supplied in a heat exchanger, and this is converted into a rotational movement by partial evaporation of the working fluid in a heat engine, which drives a generator. The resulting working medium vapor is condensed after it leaves the heat engine and the cycle begins again.

The technical challenge of the TLC process lies in the implementation of partial evaporation as forced flash evaporation with a vertically falling evaporation curve (see Fig. 1 , TS diagram, course from point 3 to point 5) through the wet steam area of the working fluid with a high proportion of liquid.

• Reduktion des Arbeitsdruckes zur Initiierung der Entspannungsverdampfung des Arbeitsmittels
• Volumenvergrößerung durch die Entspannungsverdampfung des Arbeitsmittels
• Verrichten von Expansionsarbeit durch den entstehenden Dampf des Arbeitsmittel
• im Nassdampfgebiet des Arbeitsmittels mit einem hohen Flüssigkeitsanteil

stellen hohe technische Anforderungen an die verwendete Vorrichtung.The continuous, simultaneous and spatial coexistence of:

• Reduction of the working pressure to initiate the flash evaporation of the working fluid
• Increase in volume through flash evaporation of the working fluid
• Carrying out expansion work through the resulting steam from the working medium
• in the wet steam area of the working fluid with a high liquid content

place high technical demands on the device used.

• US 3 169 375 A benennt Rotationsmaschinen
• US 4 557 112 A benennt Screw- und Vaneexpander
• US 7 093 503 B1 und DE 10 2007 041 457 A1 nennen Turbinensysteme
• WO 00 2007 115 769 A2 verweist auf Kolbenmaschinen

Various devices are known for implementing flash evaporation in a TLC process:

• US 3,169,375 A names rotary machines
• US 4,557,112 A names screw and vane expanders
• US 7,093,503 B1 and DE 10 2007 041 457 A1 call turbine systems
• WO 00 2007 115 769 A2 refers to piston engines

The specialist literature also names scroll expanders and other variants of rotary vane expanders as expansion machines.

• DE 34 20 293 A1 - ein Organic-Rankine-Cycle(ORC) System mit niedrigsiedenenden Arbeitsmittel bzw. -gemischen zur Gewinnung von Energie aus Niedertemperaturwärme
• US 2012 / 0 112 473 A1 - ein System zur Meerwasserentsalzung mit solarer Niedertemperaturwärme und Energiegewinnung in einem Dampfkraftprozess bzw. Wasserkraftwerk
• GB 280 926 A - ein System zur Gewinnung von Trockendampf durch eine Entspannungsverdampfung eines überhitzten Arbeitsmittels

Also known are:

• DE 34 20 293 A1 - an Organic Rankine Cycle (ORC) system with low-boiling working fluids or mixtures to generate energy from low-temperature heat
• US 2012 / 0 112 473 A1 - a system for seawater desalination with solar low-temperature heat and energy generation in a steam power process or hydroelectric power plant
• GB 280 926 A - a system for obtaining dry steam through flash evaporation of superheated working fluid

These devices were mostly developed as compression machines for the compression of gases or derived from machines for other thermal power processes and sometimes have unfavorable parameters for flash evaporation after the TLC process.

• Die p-V-Kennlinie der Vorrichtung entspricht nicht oder nur ungenügend der p-V-Verdampfungs-kennlinie des Arbeitsmittels, was zu Umwandlungsverlusten führt
• Ein zu geringes Expansionsverhältnis von Volumen und Druck und dadurch kein vollständiges Durchlaufen der Verdampfungskurve, was zu ungenutzter thermischer Energie führt
• hohe Spalt-Verluste an technisch bedingten Dichtflächen bei durch höhere Temperaturen bedingten höheren Arbeitsdrücken
• Schlechte Anpassung der Vorrichtung an Veränderungen der Eingangstemperatur bzw. der Kondensationstemperatur aufgrund mechanisch vorgegebener Arbeitspunkte
• Reibungsverluste
• Z.T. hohe Drehzahlen der Vorrichtung, die zusätzliche, verlustbehaftete Getriebe erfordern
• Aufwendig und teuer zu fertigende Spezialkomponenten (wie u.a. Turbinen, Screw-Expander)
• Bauteilschädigungen durch Tröpfchenerosion, ausgelöst durch eine schnelle, schlagartige Entspannungsverdampfung

This includes:

• The pV characteristic of the device does not correspond or only insufficiently corresponds to the pV evaporation characteristic of the working fluid, which leads to conversion losses
• An expansion ratio of volume and pressure that is too low and therefore does not complete the evaporation curve, which leads to unused thermal energy
• High gap losses on technically-related sealing surfaces at higher working pressures caused by higher temperatures
• Poor adaptation of the device to changes in the input temperature or the condensation temperature due to mechanically predetermined operating points
• Frictional losses
• Sometimes high speeds of the device, which require additional, lossy gears
• Special components that are complex and expensive to produce (such as turbines, screw expanders, among others)
• Damage to components caused by droplet erosion, triggered by rapid, sudden flash evaporation

Another point that is often emphasized in the scientific literature is the pumping power required to generate the required working pressure for the cold liquid working fluid at the beginning of the process, for which a significant proportion of the previously generated energy is required.

Task of the invention

The aim of the present invention is a technical solution for converting low-temperature heat into technically usable energy by implementing flash evaporation similar to the TLC process Fig. 1 while at the same time eliminating the disadvantages of the previously known devices.

• die p-V-Kennlinie der Vorrichtung entspricht der p-V-Verdampfungskennlinie des Arbeitsmittels
• Ein großes volumenbezogenes Expansionsverhältnis
• Ein großes druckbezogenes Expansionsverhältnis
• geringe Spaltverluste an technisch bedingten Dichtflächen
• Vermeidung einer schlagartigen Entspannungsverdampfung und dadurch ausgelöster Tröpfchenerosion
• Minimierung der zur Erzeugung des Arbeitsdruckes erforderlichen Pumpleistung
• Leichte Anpassung an Veränderungen der thermischen Umgebungsparameter wie Temperatur der Wärmequelle bzw. der Kondensationstemperatur
• Abdeckung eines großen Temperaturbereichs der Temperatur der NiedertemperaturWärmequelle und der Kondensationstemperatur

This means that the new technical solution should have the following properties:

• the pV characteristic of the device corresponds to the pV evaporation characteristic of the working medium
• A large volume expansion ratio
• A large pressure-related expansion ratio
• Low gap losses on technically required sealing surfaces
• Avoiding sudden flash evaporation and the resulting droplet erosion
• Minimization of the pumping power required to generate the working pressure
• Easy adaptation to changes in thermal environmental parameters such as the temperature of the heat source or the condensation temperature
• Covering a wide temperature range of low temperature heat source temperature and condensation temperature

Explanation of the solution approach

• Erste Wandlung: Umwandlung der thermischen Energie von Prozessmedien in potentielle Energie der Prozessmedien durch Anheben der Prozessmedien von einem unteren Niveau auf ein oberes Niveau unter Realisierung einer Entspannungsverdampfung nach dem Extended-TLC-Prozess
• Zweite Wandlung: Umwandlung der potentiellen Energie der Prozessmedien in technisch nutzbare Energie durch Rückführung der Prozessmedien vom oberen auf das untere Niveau und Umwandlung des statischen Druckes der Prozessmedien in mechanische Energie, z.B. in einem Hydraulikmotor / -turbine

The object is achieved according to the invention as defined in the claims by a novel "Extended TLC process", an energy conversion device and a method for converting thermal energy into potential energy as well as a device and method with two-fold energy conversion:

• First conversion: Conversion of the thermal energy of process media into potential energy of the process media by raising the process media from a lower level to an upper level while realizing flash evaporation according to the Extended TLC process
• Second conversion: Conversion of the potential energy of the process media into technically usable energy by returning the process media from the upper to the lower level and converting the static pressure of the process media into mechanical energy, e.g. in a hydraulic motor/turbine

• Der "Extended-TLC" Prozess
• Die erste Energiewandlungsvorrichtung und das Verfahren zur Wandlung von thermischer Energie in potentielle Energie unter Realisierung einer Entspannungsverdampfung nach dem Extended-TLC-Prozess
• Die Vorrichtung und das Verfahren der zweimaligen Wandlung unter Verwendung der neuartigen ersten Energiewandlungsvorrichtung

New are:

• The “Extended-TLC” process
• The first energy conversion device and the method for converting thermal energy into potential energy by realizing flash evaporation according to the extended TLC process
• The device and method of double conversion using the novel first energy conversion device

• Der "Extended-TLC" Prozess nachfolgend E-TLC Prozess genannt
• die erste Energiewandlungsvorrichtung zur Wandlung von thermischer Energie in potentielle Energie nachfolgend "Erster Energiewandler" genannt
• die Vorrichtung mit zweimaliger Energiewandlung nachfolgend als "Gesamtsystem" bezeichnet
• der im Gesamtsystem realisierte thermodynamische Prozess mit zweimaliger Energiewandlung wird aufgrund seiner Ähnlichkeit zum bekannten TLC-Prozess und zur besseren Unterscheidung zum neuartigen E-TLC-Prozess nachfolgend als "E-TLC2-Prozess" bezeichnet.

For better differentiation:

• The “Extended-TLC” process, hereinafter referred to as the E-TLC process
• the first energy conversion device for converting thermal energy into potential energy, hereinafter referred to as “first energy converter”.
• the device with double energy conversion is hereinafter referred to as the “overall system”.
• The thermodynamic process with double energy conversion implemented in the entire system is referred to below as the “E-TLC2 process” due to its similarity to the known TLC process and to better distinguish it from the new E-TLC process.

In the Fig.1 The reference symbols used for the TLC process are used identically in representations of the E-TLC and the E-TLC2 process.

The novel E-TLC process

• die Verwendung eines Wärmeträgermediums (nachfolgend vereinfacht Wärmemedium genannt) als interner Wärmespeicher
• die vollständige Verdampfung des Arbeitsmittels (vgl. TLC-Prozess: teilweise Verdampfung)
• die Verdampfung in einer polytropen Verdampfung (vgl. TLC-Prozess: isentrope Verdampfung)

Key features of the novel E-TLC process (see Fig.3 ) compared to the well-known TLC process Fig.1 are:

• the use of a heat transfer medium (hereinafter simply referred to as heat medium ) as an internal heat storage
• the complete evaporation of the working fluid (cf. TLC process: partial evaporation)
• the evaporation in a polytropic evaporation (cf. TLC process: isentropic evaporation)

As will be shown later, the use of a completely evaporating working medium and an additional heat medium results in completely new solutions for the technical implementation and control of a device for converting low-temperature heat into technically usable energy.

Complete system with double energy conversion (E-TLC2 process)

Core component of the overall system 11 Fig. 5 is the first energy converter 25.

In Fig. 4 the associated thermodynamic details of the two-stage E-TLC2 process for the entire system 11 as well as the associated TS and pV diagram are shown.

That at point 2 ( Fig.5 below) pressurized working medium 51 and the heat medium 55, which is also under pressure, are heated to the same temperature in a heat exchanger 31 by externally supplied thermal energy and fed to the first energy converter 25.

In the first energy converter 25 for converting thermal energy into potential energy, the step of flash evaporation (see Fig.4 , TS diagram) from working point 3 with the maximum temperature to working point 5 with the minimum temperature. This achieves a maximum in exergetic efficiency.

The working medium raised and completely evaporated by the first energy converter 25 is collected after exiting the first energy converter 25, the working medium vapor 54 condenses, collected and returned to the lower level in a second energy converter 34 while performing mechanical work.

The remaining liquid heat medium is also collected and returned to the lower level while performing mechanical work in the second energy converter 34. Deviating from the E-TLC process Fig. 3 In the two-stage E-TLC2 process, there is another point 7 between thermodynamic points 1 and 2, at which the cold working medium 51 and the cold heat medium 55 have a higher pressure than is required after the E-TLC process at point 2 . This pressure difference between points 7 and 2 of the E-TLC2 process is converted into technically usable energy in the second energy converter 34. At the same time, the pump required according to the state of the art to generate the necessary working pressure is no longer required.

The product of the pressure difference and the volume of the working medium and the heat medium corresponds to the thermal energy converted into potential energy in the first energy converter 25.

The first energy converter

The physical and technical basis for the first energy converter 25 (see Fig. 6a ) are work areas AB, each delimited by two pistons 170 and filled with warm working medium AM and warm heating medium WM.

A large number of these work areas, separated by pistons 170, are arranged one above the other in an upwardly directed tube (see Fig. 6b ).

Each work area is under a local working pressure pA, which is generated by the other work areas located in the pipe above the respective work area.

Depending on the number of additional work areas located above an individual work area and the local working pressure pA that prevails in an individual work area, the working fluid AM is in a flash evaporation - with a simultaneous increase in the volume of the work area - partially (lower and middle area) or completely (upper area ) evaporated and cooled. The thermal energy required for the complete evaporation of the working fluid is removed from the heat medium so that it is also cooled down (see Fig.4 and Fig. 6b ).

By adding new work areas (see Fig. 6b ) on the lower level of the upward pipe, the work areas above are raised to such an extent that the top work area emerges from the upward pipe at the upper level.

This reduces the local working pressure pA for all subsequent work areas.

This pressure reduction leads to small expansion evaporations in all work areas in the pipe and thus small volume increases in each individual work area and consequently a lifting of all work areas above.

The sum of these many small volume increases results in a large volume increase, which significantly raises the top work area (see Fig.6b - resulting change in path) and - after adding a new work area to the lower level - also exits to the upper level.

In order for this process to be repeated continuously, new work areas with warm working fluid and warm heating medium are constantly supplied at the lower level at a metering pressure pD.

In the Fig.6a and 6b The strict separation of heat medium and work equipment shown serves to provide an understandable representation of the processes within a work area during the movement from the lower to the upper level. In reality, within a working area AB, there is a mixing of heat medium and working fluid to form a working mixture AG (see Fig.6c ).

Due to the evaporation of the working fluid during the movement from the lower to the upper level, the working mixture is subject to a constant change in the mixing ratio until the working fluid has completely evaporated at the upper level and the heat medium remains solely as a liquid.

Optimization of the entire system

Considering the heat medium and working fluid as a working mixture suggests the possibility of an advantageous optimization of the in Fig.5 shown overall system 11 close.

In Fig.7 the optimized overall system 12 with a mixing chamber 33 for producing the working mixture AG is already shown outside the first energy converter.

The result of the optimization is only a one-piece second energy converter 34 and a one-piece heat exchanger 31 instead of a two-part second energy converter and heat exchanger Fig.5 necessary.

Further development of the first energy converter

This in Fig.6 The principle of the first energy converter outlined requires a greater height of the upward pipe - to build up the maximum working pressure pA, which increases with the temperature - the greater the temperature difference between the low-temperature heat source and the steam liquefaction temperature (given by the temperature of the heat sink).

This may require heights of several hundred meters to over 1000 meters. This can be done according to an advantageous further development of the first energy converter (see Fig. 10a-b ) can be avoided by inserting an additional weight area GB filled with a weight medium 60 between two work areas AB (see Fig. 10a ). The weight medium is - in contrast to the working medium and heat medium - not heated by the heat source.

The weight medium has the effect - with otherwise the same processes as before Fig 6 described - due to its own weight, an increase in the working pressure pA on each working area AB located in the upward pipe. This makes it possible - as will be shown - to significantly reduce the height required of the upward pipe to build up the working pressure pA.

In Fig. 11 the overall system 15 is shown with a further developed first energy converter 26, the structure of which is largely identical to the overall system 11 Fig. 5 is.

The in Fig. 12 The structure of the overall system 16 shown with a further developed first energy converter 26 and external production of a working mixture is largely identical to the overall system 12 Fig. 7 . What is new in both overall systems is the additional supply of weight medium 60 to the further developed first energy converter 26.

The thermodynamic processes of the E-TLC2 process Fig. 4 also apply to the overall systems 15 and 16 with the further developed first energy converter 26.

The reduced pressure difference between points 7 and 2 due to the lower height of the overall systems 15 and 16 is compensated for the second energy converter 34 by a larger volume of working medium, heat medium and weight medium (see Fig.11 +12, pV diagrams). Varying the amount of the working mixture (heat medium and working fluid) or the weight medium enables easy control of the entire system.

It is particularly advantageous that the further developed first energy converter can also be operated in an operating mode without a weight medium, thus extending the usable temperature range to lower temperatures.

Optimization of the further developed overall systems

As in Fig.11 and 12 shown, the use of a weight medium in the overall systems 15 and 16 requires the use of a two-part second energy converter 34.

This can be done by using working mixture as a weight medium as in Fig.13 shown can be avoided.

Further design variants of the overall system

By taking advantage of the different densities of the working medium and the heat or weight medium, various design variants of the overall system for converting thermal energy into technically usable energy are possible. Depending on the area of application (source of low-temperature heat, heat sink, temperature difference), technical advantages can be achieved.

So can, as in Fig.8 , 14 and 15 shown, the height of the entire system between the condensation device and the heat supply can be reduced to such an extent that the resulting liquid pressure of the working fluid or the working mixture corresponds to the working pressure required at point 2. The pressure difference between the - no longer present - points 7 and 2, which was previously used to generate energy, disappears. The loss of potential energy of the working medium or working mixture is compensated for by the larger usable volume of heat or weight medium. The total amount of technically usable energy remains the same. If the focus is on further reducing the height of the overall system, as in Fig.9 and 16 shown, the use of an additional pressure booster pump 35 is also possible.

However, this reduces the technically usable amount of energy to be released.

Increased performance through parallelization

The principle and the simple technology of the first energy converter 25 and the further developed first energy converter 26 for converting thermal energy into potential energy allow any number of upward pipes to be built in parallel for energy conversion (see Fig. 17 , exemplified using the example of the entire system 12).

This has the advantage that even with low temperature differences between the low-temperature source and the steam liquefaction temperature and the associated low efficiency, large amounts of heat can still be converted and technically usable energy can be obtained from it.

With parallelization, outputs well into the megawatt range can be achieved.

• Erfolgt durch das Prinzip der frei beweglichen Kolben eine selbsttätige Anpassung der p-V-Kennlinie der ersten Energiewandler an die p-V-Verdampfungskennlinie des Arbeitsmittels
• Ist eine stufenlose Volumenvergrößerung von mehr als 1:100 möglich (Ausgangsvolumen des flüssigen warmen Arbeitsmittels zu Endvolumen des verdampften gasförmigen Arbeitsmittels)
• ist eine stufenlose Druckentspannung von mehr als 1:10 möglich
  (maximaler Arbeitsdruck auf dem unteren Niveau zu minimalem Arbeitsdruck auf dem oberen Niveau)
• Wird durch einen sehr langsamen Druckabbau von mehreren Sekunden bis Minuten (Zeit zwischen Beginn und Ende der Entspannungsverdampfung des Arbeitsmittels) eine explosionsartige Verdampfung des Arbeitsmittels und nachfolgende Tröpfchenerosion, die zu Bauteilzerstörungen führen kann, vermieden
• Werden durch geringe Druckunterschiede von weit weniger als 0,001MPa (0,01bar) zwischen der Kolbenoberseite und der Kolbenunterseite die technischen Anforderungen an die Kolbendichtungen deutlich gesenkt und Spaltverluste weitestgehend reduziert
• Sind durch mehrere parallel arbeitende erste Energiewandler Leistungen bis weit in den Megawatt-Bereich möglich
• Ist durch Änderung der zugeführten Mengen des Arbeitsmittels, des Wärmemediums, des Gewichtsmediums oder der Betriebsweise im weiterentwickelten ersten Energiewandler eine einfache Anpassung an Veränderungen der externen Temperatur der Niedertemperaturwärmequelle und/oder der Temperatur der Dampfverflüssigung möglich
• können bereits geringe Temperaturdifferenzen von 10°K zur Energiegewinnung ausgenutzt werden
• ist ein flexibler Tag/Nacht-Betrieb sowie ein flexibler Sommer/Winter-Betrieb mit Anpassung an die sich verändernden Temperaturen der Niedertemperaturwärmequelle oder der Dampfverflüssigungstemperatur möglich

With the use of the novel E-TLC process, the first energy converter according to the invention, the further developed first energy converter according to the invention and the parallelization of the first and the further developed first energy converter:

• The principle of freely movable pistons automatically adapts the pV characteristic curve of the first energy converter to the pV evaporation characteristic curve of the working medium
• Is a continuous volume increase of more than 1:100 possible (initial volume of the liquid warm working fluid to final volume of the evaporated gaseous working fluid)
• A continuous pressure relief of more than 1:10 is possible
  (maximum working pressure at the lower level to minimum working pressure at the upper level)
• A very slow pressure reduction of several seconds to minutes (time between the start and end of the flash evaporation of the working fluid) avoids explosive evaporation of the working fluid and subsequent droplet erosion, which can lead to component destruction
• Through small pressure differences of far less than 0.001 MPa (0.01 bar) between the top of the piston and the bottom of the piston, the technical requirements for the piston seals are significantly reduced and gap losses are largely reduced
• With several first energy converters working in parallel, outputs well into the megawatt range are possible
• Is it possible to easily adapt to changes in the external temperature of the low-temperature heat source and/or the temperature of the steam liquefaction by changing the supplied quantities of the working medium, the heat medium, the weight medium or the operating mode in the further developed first energy converter
• Even small temperature differences of 10°K can be used to generate energy
• Flexible day/night operation and flexible summer/winter operation are possible with adaptation to the changing temperatures of the low-temperature heat source or the steam liquefaction temperature

• die thermodynamisch anspruchsvollen Vorgänge der Wandlung der thermischen Energie nach dem E-TLC-Prozess in eine andere Energieform werden von der Wandlung in technisch nutzbare mechanische Energie entkoppelt (vergleichbar der Trennung von Dampferzeugung und Turbine in klassischen Wärmekraftwerken)
• die technische Komplexität einer Vorrichtung zur Umwandlung thermischer Energie in technisch nutzbare Energie wird im Vergleich zum Stand der Technik deutlich reduziert, da jede der beiden Energiewandlungsstufen für ihre jeweilige Aufgabe optimiert werden kann
• Der zu Prozessbeginn erforderliche Arbeitsdruck für das Arbeitsmittel, das Wärmemedium und ggf. das Gewichtsmedium wird verfahrens- und vorrichtungsintern ohne die nach dem Stand der Technik erforderliche Druckpumpe erzeugt
• dies senkt die technisch bedingten Verluste, erhöht den technischen Wirkungsgrad und bringt ökonomische Vorteile
• je nach Einsatzfall kann aus verschiedenen Bauweisen des Gesamtsystems die optimale Bauform zur Realisierung eines E-TLC2-Prozesses ausgewählt werden

The advantages of the two-stage E-TLC2 process according to the invention for converting thermal energy into technically usable energy according to the E-TLC2 process are:

• The thermodynamically demanding processes of converting thermal energy into another form of energy according to the E-TLC process are decoupled from the conversion into technically usable mechanical energy (comparable to the separation of steam generation and turbine in classic thermal power plants)
• The technical complexity of a device for converting thermal energy into technically usable energy is significantly reduced compared to the prior art, since each of the two energy conversion stages can be optimized for its respective task
• The working pressure required at the start of the process for the working fluid, the heat medium and, if applicable, the weight medium is generated within the process and device without the pressure pump required according to the prior art
• This reduces technical losses, increases technical efficiency and brings economic advantages
• Depending on the application, the optimal design for implementing an E-TLC2 process can be selected from various designs of the entire system

List of illustrations

Fig. 1 -

Thermodynamics of the TLC process according to the state of the art

Fig. 2 -

Principle structure of a system for using the TLC process according to the state of the art

Fig. 3 -

Thermodynamics of the novel E-TLC process

Fig. 4 -

Thermodynamics of the novel E-TLC2 process

Fig. 5 -

Representation of the entire system 11 according to the E-TLC2 process

Fig. 6 -

Functional principle of the first energy converter 25

Fig. 7 -

Representation of optimized overall system 12 with mixing chamber 33

Fig. 8 -

Representation of the entire system 13 with the first energy converter 25 at a reduced height

Fig. 9 -

Representation of the entire system 14 with reduced height and pressure booster pump 35

Fig. 10 -

Functional principle of further developed first energy converter 26

Fig. 11 -

Representation of the entire system 15 with further developed first energy converter 26

Fig. 12 -

Representation of the entire system 16 with a further developed first energy converter 26 and mixing chamber 33

Fig. 13 -

Representation of the entire system 17 with a further developed first energy converter 26 and working mixture as a weight medium

Fig. 14 -

Representation of the entire system 18 with a further developed first energy converter 26 at a reduced height

Fig. 15 -

Representation of the entire system 19 with a further developed first energy converter 26 and mixing chamber 33 at a reduced height

Fig. 16 -

Representation of the entire system 20 with a further developed first energy converter 26 and pressure booster pump 35 at a reduced height

Fig. 17 -

Representation of the entire system 12 with several parallel first energy converters 25

Fig. 18 -

Thermodynamics of the modified mE-TLC2 process

Fig. 19 -

Representation of the entire system 211 according to the mE-TLC2 process with the first energy converter 25

Fig. 20 -

Representation of the entire system 212 according to the mE-TLC2 process with the first energy converter 25 and working mixture

Fig. 21 -

Representation of the entire system 216 according to the mE-TLC2 process with the first energy converter 26 and working mixture

Fig. 22 -

Representation of the entire system 219 according to the mE-TLC2 process with the first energy converter 26 and working mixture at reduced height

Fig. 23 -

Representation of the first energy converter 25

Fig. 24 -

Representation of the first energy converter 25 with supply of working mixture

Fig. 25 -

Representation of further developed first energy converters 26

Fig. 26 -

Representation of further developed first energy converter 26 with supply of working mixture

Fig. 27 -

Representation of the variation of possible operating states of the first energy converters 25 and 26 in the T-S diagram

Fig. 28 -

Representation of possible design variants of the pipe system on the lower and upper levels

List of reference symbols and numbering used Reference symbols

• AB - work area
• AG - working mixture of heat medium and working fluid, generally used
• AM - work equipment, commonly used
• GB - weight range
• H - height of fall
• WM - heat medium, commonly used
• pA - working pressure
• pD - dosing pressure
• pK - pressure piston stack

Numbers 1 - 7 --- Points for specific thermodynamic states in T-S and p-V diagrams

• Number without addition indicates status point for the work equipment
• The addition "..wm" indicates the status point for the heat medium
• The addition "..gm" indicates the status point for the weight medium
• The addition "..ag" indicates the status point for the working mixture of heat medium and working fluid

Numbers 10 - 99 --- Components of the entire system

• 11 - Overall system with first energy converter 25 and internal generation of a working mixture
• 12 - Overall system with first energy converter 25 and external generation of a working mixture
• 13 - Overall system with first energy converter 25, external generation of a working mixture at reduced height
• 14 - Overall system with first energy converter 25, external generation of a working mixture at reduced altitude and additional pressure booster pump 35
• 15 - Overall system with further developed first energy converter 26, internal generation of a working mixture and heat medium as a weight medium
• 16 - Overall system with further developed first energy converter 26, external generation of a working mixture and heat medium as a weight medium
• 17 - Overall system with further developed first energy converter 26, external generation of a working mixture and working mixture as a weight medium
• 18 - Overall system with further developed first energy converter 26, external generation of a working mixture with pressure build-up through working fluid and heat medium as a weight medium at a reduced height
• 19 - Overall system with further developed first energy converter 26, external generation of a working mixture with pressure build-up through working mixture and heat medium as a weight medium at reduced height
• 20 - Overall system with a further developed first energy converter 26, external generation of a working mixture, heat medium as a weight medium and additional pressure booster pump 35 for the working medium at a reduced height
• 25 - First energy converter thermal to potential energy
• 26 - Further developed first energy converter thermal to potential energy
• 31 - Heat exchanger for absorbing thermal energy
• 32 - Steam condenser for working medium steam
• 33 - mixing chamber for working medium and heating medium
• 34 - Second energy converter, potential to technically usable energy
• 35 - booster pump
• 40 - Feeders, general
• 41 - Feed weight medium
• 51 - Working fluid, liquid, cold
• 52 - Working fluid, liquid, warm
• 53 - Working fluid, vaporous, warm
• 54 - Working fluid, vaporous, cold
• 55 - heat medium, liquid, cold
• 56 - heat medium, liquid, warm
• 58 - Working mixture of heat medium and working medium, cold
• 59 - Working mixture of heat medium and working medium, warm
• 60 - Weight medium, liquid

Numbers 100-199 --- First and further developed first energy converter

• 110 - pipe bend, lower level
• 120 - Insertion device, general
• 121 - Introduction device for working fluid and heat medium or working mixture
• 122 - Introduction device for working fluid and heat medium or working mixture and weight medium
• 125 - piston stop device
• 126 - dosing device
• 130 - rise pipe
• 140 - Pipe elbow, upper level
• 150 - Separation device for separating liquids and working medium vapor
• 160 - descent pipe
• 170 - single piston
• 171 - piston stack

Detailed description of the E-TLC process

Essential feature of the novel E-TLC process Fig.3 compared to the well-known TLC process Fig.1 is the use of a heat medium and the complete evaporation of the working fluid into a polytropic evaporation curve.

The TLC process according to Smith ( Fig.1 ) uses the thermal energy absorbed by the working fluid to evaporate. Since the amount of energy required for evaporation is greater than the amount of energy absorbed, this always leads to only partial evaporation of the working fluid.

In the E-TLC process, a significant portion of the thermal energy required for complete evaporation is supplied to the working medium through the heated thermal medium during the flash evaporation phase (see Fig.3 , TS diagram). The heat medium never turns into vapor and always remains in its liquid state.

The working fluid thus undergoes polytropic flash evaporation (cf. Fig.1 , TLC process: isentropic flash evaporation). If you look at the sum of the amount of heat contained in the heated working fluid and heated heating medium - without taking into account the different heat capacities - this corresponds to the amount of energy converted into evaporation of the working fluid. This means that in a direct comparison of the TLC and E-TLC process, with the same amount of thermal energy absorbed, the same amount of thermal energy is converted through the evaporation of working fluid.

However, the use of a separate heat medium with different, advantageous physical and chemical properties (e.g. density, heat capacity) as well as the targeted mixing of working medium and heat medium to form a working mixture AM results in completely new approaches for the technical implementation of a device for converting low-temperature heat into a technically usable form of energy that would not be possible using pure work equipment according to the TLC process.

Detailed description of the E-TLC2 process and the overall systems for converting thermal energy into technically usable energy

The following description presents the operation of the overall system 11 ( Fig.5 ) and the further developed overall system 15 ( Fig.11 ) together.

Differences are discussed in the text. The description of the thermodynamic steps follows the course of the E-TLC2 process Fig.4 .

The overall systems 12 ( Fig.7 ) and 16 ( Fig.12 ) are variations of the overall systems 11 and 15 using a working mixture AG consisting of working medium AM and heating medium WM. Their operation corresponds to overall systems 11 and 15, respectively.

For better understanding, Figures 5, 7, 11 and 12 show the TS diagrams and the pV diagrams of the respective overall process, separated by work medium (without index), heat medium (index "wm"), weight medium (index "gm") or working mixture (index "ag").

The hatched area in the p-V diagrams corresponds to the thermal energy of the respective medium converted into technically usable work. The sum of the converted thermal energy is the same for all overall systems with the same input parameters (amount of thermal energy absorbed).

The overall systems 13,14 ( Fig.8,9 ) and 17-20 ( Fig.13-16 ) represent further advantageous variations of the overall systems 11 and 15. Their basic operation corresponds to the overall systems 11 and 15. Differences are discussed in the text.

• Einem Wärmetauscher 31 zur Erwärmung des unter Druck stehenden Arbeitsmittels 52, des Wärmemediums 55 bzw. des Arbeitsgemisches 58 durch eine Niedertemperaturwärmequelle ohne Verdampfung des Arbeitsmittels
• Einem ersten Energiewandler 25 zur Wandlung der aufgenommenen thermischen Energie in potentielle Energie
• Einer Dampfverflüssigungsvorrichtung 32
• Einem zweiten Energiewandler 34 zur Wandlung der potentiellen Energie des Arbeitsmittels 51, des Wärmemediums 55 bzw. des Arbeitsgemisches 58 in eine technisch nutzbare Energieform
• Zuführungen 40 zur Verbindung der einzelnen Bestandteile
• Zusätzlich weisen die Gesamtsysteme 12-14 eine Mischkammer 33 zur Herstellung eines Arbeitsgemisches 58 auf

The overall systems 11-14 according to the invention ( Fig.5 , 7-9 ) for the conversion of thermal energy into technically usable energy consist at least of the following components:

• A heat exchanger 31 for heating the pressurized working fluid 52, the heat medium 55 or the working mixture 58 by a low-temperature heat source without evaporation of the working fluid
• A first energy converter 25 for converting the absorbed thermal energy into potential energy
• A vapor liquefaction device 32
• A second energy converter 34 for converting the potential energy of the working fluid 51, the heat medium 55 or the working mixture 58 into a technically usable form of energy
• Feeds 40 for connecting the individual components
• In addition, the overall systems 12-14 have a mixing chamber 33 for producing a working mixture 58

• Einem Wärmetauscher 31 zur Erwärmung des unter Druck stehenden Arbeitsmittels 51, des Wärmemediums 55 bzw. des Arbeitsgemisches 58 durch eine Niedertemperaturwärmequelle ohne Verdampfung
• Einem weiterentwickelten ersten Energiewandler 26 zur Wandlung der aufgenommenen thermischen Energie in potentielle Energie
• Einer Dampfverflüssigungsvorrichtung 32
• Einem zweiten Energiewandler 34 zur Wandlung der potentiellen Energie des Wärmemediums, des Arbeitsmittels, des Gewichtsmediums bzw. des Arbeitsgemisches in eine technisch nutzbare Energieform
• Zuführungen 40 zur Verbindung der einzelnen Bestandteile
• Einer Zuführung 41 zur Zuführung von Gewichtsmedium 60 zum weiterentwickelten ersten Energiewandler 26
• Zusätzlich weisen die Gesamtsysteme 16-20 eine Mischkammer 33 zur Herstellung eines Arbeitsgemisches 58 auf

The further developed overall systems 15-20 according to the invention ( Fig.10-16 ) consist at least of the following components:

• A heat exchanger 31 for heating the pressurized working medium 51, the heating medium 55 or the working mixture 58 by a low-temperature heat source without evaporation
• A further developed first energy converter 26 for converting the absorbed thermal energy into potential energy
• A vapor liquefaction device 32
• A second energy converter 34 for converting the potential energy of the heat medium, the working medium, the weight medium or the working mixture into a technically usable form of energy
• Feeds 40 for connecting the individual components
• A feed 41 for feeding weight medium 60 to the further developed first energy converter 26
• In addition, the overall systems 16-20 have a mixing chamber 33 for producing a working mixture 58

Various auxiliary systems are not shown in the illustrations, as their position and function can be solved in many different ways.

• Absaugung von nicht kondensierbaren Gasen
• Filtersysteme zur Reinigung des Arbeitsmittels und des Wärmemediums von Fremdstoffen
• Austreiber zur vollständigen Trennung von Arbeitsmittel und Wärmemedium
• Meßsensoren sowie Prozess-Steuerungs- und Regeltechnik
• Vorratsbehälter
• Wärmespeicher

Auxiliary systems can be, for example:

• Extraction of non-condensable gases
• Filter systems for cleaning the working fluid and the heat medium from foreign substances
• Expeller for complete separation of working fluid and heat medium
• Measuring sensors as well as process control and regulation technology
• storage container
• Heat storage

• Schritt a: Isobares Erwärmen (Fig.4: Pkt.2 - Pkt.3) des unter Dosierdruck (pD) stehenden flüssigen Arbeitsmittels und des unter Dosierdruck (pD) stehenden flüssigen Wärmemedium (55) - die auch als Arbeitsgemisch (58) vorliegen können - aus einer Niedertemperaturwärmequelle ohne Verdampfung des Arbeitsmittels
• Schritt b: Polytrope Umwandlung (Fig.4: Pkt.3 - Pkt.5) der aufgenommenen thermischen Energie in mindestens einem ersten Energiewandler 25 oder 26 in potentielle Energie
• Schritt c: Isobares Kondensieren (Fig.4: Pkt.5 - Pkt.1) des vollständig verdampften Arbeitsmittels
• Schritt d: Isochore Umwandlung (Fig.4: Pkt.1 - Pkt.7) der gewonnenen potentiellen Energie über die Fallhöhe H in statischen Druck
• Schritt e: Isochore Umwandlung (Fig.4: Pkt.7 - Pkt.2) eines Teils des statischen Druckes im zweiten Energiewandler 34 in technisch nutzbare mechanische Energie

In all overall systems 11-20, the thermal energy is converted into technically usable energy using the E-TLC2 process (see Fig. 4 ) in the procedural steps:

• Step a: Isobaric heating ( Fig.4 : Point 2 - Point 3) of the liquid working fluid under metering pressure (pD) and the liquid heat medium (55) under metering pressure (pD) - which can also be present as a working mixture (58) - from a low-temperature heat source without evaporation of the working fluid
• Step b: Polytropic conversion ( Fig.4 : Point 3 - Point 5) of the thermal energy absorbed in at least one first energy converter 25 or 26 into potential energy
• Step c: Isobaric condensation ( Fig.4 : Point 5 - Point 1) of the completely evaporated working fluid
• Step d: Isochoric conversion ( Fig.4 : Point 1 - Point 7) of the potential energy gained over the fall height H in static pressure
• Step e: Isochoric conversion ( Fig.4 : Point 7 - Point 2) part of the static pressure in the second energy converter 34 into technically usable mechanical energy

Thermodynamic point 2

The starting point of the energy conversion process is point 2 of the E-TLC2 process (see Fig.4 , TS and pV diagram) in the lower area of the overall systems 11-20 ( Fig.5 , 7-9 , 11-16 ).

The cold liquid working fluid 51 and the cold heat medium 55 (overall system 11, 15) or the cold working mixture (overall system 12-14, 16-20) are under pressure and are fed through feeds 40 to the heat exchanger 31 to absorb thermal energy from the low-temperature heat source and heated therein without evaporation of the working fluid.

In addition to geothermal heat, ocean heat, solar heat, waste heat from technical processes (e.g. steel and plastics industries), heat from cooling processes (e.g. cold storages, data centers), heat from combustion processes (e.g. waste incineration, biogas) or residual heat from other processes (e.g. chemical industry) can be used as low-temperature heat sources. be used.

Depending on the temperature level and the temperature difference between the low-temperature heat source used and the available condensation temperature, all organic and inorganic substances and mixtures of substances can be used as working materials Cover the temperature range from the maximum temperature of the low-temperature heat source to the minimum temperature of vapor liquefaction as a liquid without thermal decomposition and without freezing.

When selecting the work equipment, it is important to ensure that chemical reactions between the work equipment and individual components of the overall system are avoided.

The preferred heating medium is water due to its heat capacity. However, other temperature-stable substances that remain liquid in the intended temperature range, do not decompose or freeze and do not enter into a chemical reaction or other interaction with the work equipment can also be used. In addition, there should be no chemical reactions between the heat medium and individual components of the overall system.

Thermodynamic point 3

The working fluid 52 and heat medium 56 (overall system 11, 15) emerging from the heat exchanger 31 and heated to the same temperature or the heated working mixture (overall system 12-14, 16-20) then flow through thermally insulated feeds 40 to the first energy converter 25 (overall system 11-14) or the further developed first energy converter 26 (overall system 15-20).

In the further developed overall systems 15-20 ( Fig.11-16 ) additionally cold weight medium 60 flows through feeds 41 to the first energy converter 26.

The preferred weight medium is the heat medium, preferably water, due to its high density. However, cold working mixture (see overall system 17), pure working fluid or an additional liquid can also be used as a weight medium.

The latter variants are mentioned here as technically possible solutions, but are not explained further.

Thermodynamic points 4' and 4"

In the first energy converter 25 (overall system 11-14) or the further developed first energy converter 26 (overall system 15-20), the absorbed thermal energy of the warm working medium 52 and the warm heating medium 56 or the resulting warm working mixture 59 is converted in accordance with the E-TLC or E-TLC2 process ( Fig.3 , 4 Points 4' and 4") are converted into potential energy by a flash evaporation of the working fluid while performing volume change work in the form of lifting work. The heat medium cools down by releasing heat to the working fluid.

The working medium and the heat medium or the weight medium (the latter only complete systems 15-20) are raised from the lower to the upper area.

Thermodynamic point 5

In the upper area of the first energy converters 25,26 the working medium is in accordance with the E-TLC or E-TLC2 process ( Fig.3 , 4 Point 5) completely evaporated and cooled.

The remaining liquid heat medium 55 has also cooled down.

The evaporated and cooled working medium 54 and the liquid, cold heat medium 55 leave the first energy converter 25 (overall system 11-14) or the further developed first energy converter 26 (overall system 15-20) at the upper level.

In the further developed overall systems 15-20, the cold weight medium 60 mixes with the cold heat medium 55 and increases the volume of the heat medium 55.

Thermodynamic point 6

After leaving the first energy converter 25 or 26, the evaporated working fluid 54 flows to the vapor liquefaction device 32 and is here reduced in entropy ( Fig.3 , 4 TS diagram point 6) liquefied again.

Any non-condensable gases that may arise are sucked out here.

Thermodynamic point 1

With the exit of the heat medium or the weight medium from the first energy converters 25 and 26 and the exit of the liquefied working medium from the vapor liquefaction device 32 at the upper level of the overall system, point 1 of the E-TLC or E-TLC2 process ( Fig.3 , 4 Point 1) reached.

The cold working medium 51 and the cold heating medium 55 (including weight medium 60) are now cooled down and under low pressure, the previously absorbed thermal energy is converted into potential energy.

Depending on the design of the overall system 11-20, the working medium 51 and the heat medium 55 (including weight medium 60) flow back to the lower level of the overall system in different ways, building up static pressure.

In the overall systems 12 and 17, a complete mixing of working fluid and heat medium into a working mixture takes place in a mixing chamber 33, and in the overall systems 16 and 19, a partial mixing takes place.

Thermodynamic point 7

To convert the potential energy - in the form of hydrostatic pressure - into technically usable energy, the heat medium 55, the working fluid 51 or the working mixture 58 flow to a second energy converter 34. Here the liquid columns generate high pressure (pV diagram points 7, 7 _wm , 7 _gm , 7 _ag ). This pressure is partially converted into mechanical movement in the second energy converter 34, which is subsequently converted into electrical energy, for example in a generator, but can also be used as mechanical energy to drive machines.

In the overall systems 11, 15 and 16 ( Fig.5 , 11 , 12 ) the resulting pressure varies due to the different densities of the two liquids. This requires a two-part second energy converter 34.

In the overall systems 12-14 ( Fig. 7-9 ) and 17-20 ( Fig.13-16 ), only a one-piece second energy converter 34 is required.

The overall systems 13, 18 and 19 represent a special feature.

These systems are characterized by a reduced height between the vapor liquefaction device 32 and the heat exchanger 31, which means that the resulting liquid pressure of the working fluid 51 or the working mixture 58 at the lower level of the overall system corresponds to the working pressure required at point 2. This design reduces technical effort and costs. The pressure difference between the - no longer present - points 7 and 2, which was previously used to generate energy, disappears. The - apparent - loss of potential energy is compensated for by the larger volume of the weight medium required to build up the working pressure pA in the first energy converter 25 or 26. This means that the sum of the technically usable amount of energy remains the same - with the same input conditions.

Thermodynamic point 2

After exiting the second energy converter 34, the cold working medium 51, the cold heating medium 55 (including cold weight medium 60) or the cold working mixture 58 is under an equally high remaining residual pressure (point 2 of the E-TLC2 process).

This residual pressure is so high that the working fluid 51 does not begin to evaporate when thermal energy is subsequently absorbed in the heat exchanger 31.

The overall systems 14 and 20 are an exception. Here the height of the overall system was reduced to such an extent that the necessary working pressure at point 2 is not reached. An additional pressure boosting pump 35 is therefore required to achieve the required working pressure. This solution can be useful for various reasons, but it worsens the overall technical efficiency.

This means that the starting point of the E-TLC2 process has been reached for all overall systems 11-20 and the cycle is closed.

Comparison of the overall systems 11 and 15

When comparing the pV diagrams of the entire system 11 ( Fig. 5 ) with the first energy converter 25 and the overall system 15 ( Fig. 11 ) with the further developed first energy converter 26 it can be seen that in the overall system 15 the larger part of the technically usable energy is obtained from the larger volume of the heat medium 55 or weight medium 60 with a significantly reduced pressure difference between points 7 and 2. This arises from the volume of the weight medium 60 used and the resulting reduced height of the first energy converter 26, which is represented as the pressure difference between points 2 and 7 of the pV diagram.

However, with the same amount of thermal energy supplied, the same amount of technically usable energy is always generated in the overall systems 11 and 15.

performance increase

To increase the performance of the overall systems 11 to 20, several first energy converters 25 (see example Fig. 17 ) or further developed first energy converters 26 can be used in parallel. The number of energy converters 25,26 can be increased as desired.

A corresponding adjustment of the performance of the shared components heat exchanger 31, steam condenser 32, mixing chamber 33 and second energy converter 34 is assumed.

By switching off individual first energy converters 25 or 26 by stopping the supply of working fluid, heat medium or working mixture, it is possible to easily adapt the performance of the first energy converters 25 or 26 to the amount of available thermal energy. An additional use of several energy converters 34 that can be switched off individually is advantageous.

Usable temperature range

The operation of the overall systems 11 to 20 is based only on the pressure difference between the vapor pressure at maximum working temperature and the vapor pressure at vapor liquefaction temperature.

The overall systems 11-14 are particularly advantageous for small temperature differences, the overall systems 15-20 for higher temperature differences.

In particular, because the further developed overall system 15 can be operated like an overall system 11 through appropriate control of the further developed first energy converter 26, the area of application of the overall system 15 is significantly expanded.

Further use of the condensation heat

Due to the wide usable and variable temperature range, further use of the condensation heat is possible at a corresponding temperature of the low-temperature heat source.

For example, at a maximum working temperature of 150°C and a condensation temperature of 70°C, the condensation heat can heat heating water.

The amount of energy generated by the entire system decreases accordingly. The exergetic efficiency of the entire system changes according to the degree of use of the condensation heat.

Description of the mE-TLC2 process and the overall systems 211, 212, 216 and 219 for using the mE-TLC2 process as special versions of the overall systems 11, 12, 16 and 19

Depending on the type of low-temperature heat source and the location where the low-temperature heat is provided, further special designs of the overall systems 11 to 20 are possible. In Fig. 19 to 22 Preferred arrangements for using low-temperature heat from solar thermal heating, but also from flue gases or coolant vapors are shown.

The overall systems are modified further developments of the previously explained overall systems 11, 12, 16 and 19.

A common feature of the modified overall systems 211, 212, 216 and 219 is that the heat exchanger 31 for introducing the low-temperature heat is arranged between the lower and upper levels of the overall system and extends partially or completely over the head H.

In the overall system 211 and 212, the working medium 51, heating medium 55 or working mixture 58 to be heated pass through the vertically arranged heat exchanger 31 while pressure builds up at the same time and are fed to the second energy converter 34 as already heated liquids.

After the warm working fluid or working mixture exits the second energy converter 34, there is no evaporation due to the remaining high metering pressure pD. The heated working fluid, heat medium or working mixture is then fed directly to the first energy converter 25.

In the overall system 216 and 219, only the working mixture 58 passes through the heat exchanger 31. The weight medium 60 runs directly to the second energy converter 34 without heating.

In the overall system 216, the working mixture continues to the second energy converter 34 to convert potential energy into technically usable energy. After the working mixture exits the second energy converter 34, there is no evaporation of the working fluid due to the remaining high metering pressure pD.

In the overall system 219 with a reduced height, the heated working mixture is fed directly to the first energy converter 26 while building up the metering pressure pD.

In Fig.18 is the one on the in Fig.3 E-TLC process shown and used in the overall systems 211, 212, 216 and 219 modified two-stage extended tri-lateral cycle process (hereinafter referred to as mE-TLC2 ).

• Schritt a: Polytrope Umwandlung (Fig.3: Pkt. 4' und 4") der thermischen Energie des erwärmten Arbeitsmittels und des erwärmten Wärmemediums in einem ersten Energiewandler 25 oder 26 in potentielle Energie
• Schritt b: Isobares Kondensieren (Fig.3: Pkt.5 - Pkt.1) des vollständig verdampften Arbeitsmittels
• Schritt c: Isochores Erwärmen (Fig.3: Pkt.1 - Pkt.7) des flüssigen Arbeitsmittels und des flüssigen Wärmemediums bzw. des Arbeitsgemisches aus einer Niedertemperaturwärmequelle bei gleichzeitigem Aufbau von statischem Druck über die Fallhöhe H ohne Verdampfung des Arbeitsmittels
• Schritt d: Isotherme Umwandlung (Fig.3: Pkt.7 - Pkt.3) eines Teils des statischen Druckes im zweiten Energiewandler 34 in technisch nutzbare mechanische Energie

The conversion of thermal energy into technically usable energy takes place in the mE-TLC2 process in the following steps:

• Step a: Polytropic conversion ( Fig.3 : Points 4' and 4") of the thermal energy of the heated working fluid and the heated thermal medium in a first energy converter 25 or 26 into potential energy
• Step b: Isobaric condensation ( Fig.3 : Point 5 - Point 1) of the completely evaporated working fluid
• Step c: Isochoric heating ( Fig.3 : Point 1 - Point 7) of the liquid working medium and the liquid heat medium or the working mixture from a low-temperature heat source with simultaneous build-up of static pressure above the head H without evaporation of the working medium
• Step d: Isothermal conversion ( Fig.3 : Point 7 - Point 3) part of the static pressure in the second energy converter 34 into technically usable mechanical energy

Point 2 of the original E-TLC2 process Fig. 4 is omitted and point 7 has a changed position in the new mE-TLC2 process (see Fig.18 ).

The thermodynamic sequence of the mE-TLC2 process is compared to the E-TLC2 process Fig.4 Visually similar in the pV diagram, there are few changes in the curve. This is different in the TS diagram, where the missing point 2 and the changed position of point 7 represent the new arrangement of the heat exchanger and the resulting changed thermodynamic course.

Compared to the E-TLC2 process, the thermal energy converted into technically usable work in the mE-TLC2 process is the same with the same input parameters (amount of thermal energy absorbed).

The main distinguishing feature of the mE-TLC2 process is the changed position of the heat exchanger in the overall system and thus the changed application requirements for the heat exchanger 31 and the second energy converter 34.

Detailed description of the function of the first energy converter 25 or the further developed first energy converter 26 for converting thermal energy into potential energy

The following description presents the operation of the first energy converter 25 ( Fig.23 and 24 ) and the further developed first energy converter 26 ( Fig.25 and 26 ) together. Differences are discussed in the text. The description follows the course of the E-TLC or E-TLC2 process Fig.3 and 4 between points 3 and 5.

• Einem geschlossenen, aufwärts gerichteten Rohrsystem mit einem Aufstiegsrohr 130 und einem Abstiegsrohr 160 verbunden durch einen unteren Rohrbogen 110 und einen oberen Rohrbogen 140
• Einer großen Anzahl von, in dem Rohrsystem frei umlaufenden, nicht kippenden Kolben 170
• Einbringöffnungen und einer Einbringvorrichtung 121 im unteren Bereich des Rohrsystems zum Einbringen von Wärmemedium 56 und Arbeitsmittel 52 (Fig. 23) bzw. Arbeitsgemisch 59 (Fig.24)
• Auslassöffnungen und einer Separierungsvorrichtung 150 auf dem oberen Niveau des Rohrsystems zum Auslassen des abgekühlten, flüssigen Wärmemediums 55 und des verdampften Arbeitsmittels 54

The first energy converter 25 according to the invention ( Fig.23 , 24 ) for converting thermal energy into potential energy consists at least of the following components:

• A closed, upward pipe system with an ascent pipe 130 and a descent pipe 160 connected by a lower pipe bend 110 and an upper pipe bend 140
• A large number of non-tilting pistons 170 rotating freely in the pipe system
• Introduction openings and an introduction device 121 in the lower region of the pipe system for introducing heat medium 56 and working fluid 52 ( Fig. 23 ) or working mixture 59 ( Fig.24 )
• Outlet openings and a separation device 150 on the upper level of the pipe system for exhausting the cooled, liquid heat medium 55 and the evaporated working fluid 54

• einer erweiterten Einbringvorrichtung 122 auf dem unteren Niveau des Rohrsystems zum zusätzlichen Einbringen eines Gewichtsmedium 60

The further developed first energy converter 26 ( Fig.25 and 26 ) consists of at least the same components as the energy converter 25 and differently:

• an extended introduction device 122 on the lower level of the pipe system for the additional introduction of a weight medium 60

Various auxiliary and additional systems are not shown in the illustrations, as their position and function can be solved in a variety of ways.

• Startvorrichtung zur initialen Inbetriebsetzung des Prozesses
• Serviceeinrichtungen zum Befüllen der Energiewandler mit Kolben und Arbeitsmittel, Austausch defekter Kolben oder Reinigung des Arbeitsmittels (z.B. von Abrieb)
• Austreiber zur vollständigen Trennung von Arbeitsmittel und Wärmemedium
• Meßsensoren sowie Prozess-Steuerungs- und Regeltechnik
• Wärmespeicher

Auxiliary and additional systems can be, for example:

• Starting device for initial startup of the process
• Service facilities for filling the energy converters with pistons and working fluid, replacing defective pistons or cleaning the working fluid (e.g. from abrasion)
• Expeller for complete separation of working fluid and heat medium
• Measuring sensors as well as process control and regulation technology
• Heat storage

Step 1 - Bring in the media

The starting point for the conversion of thermal energy into potential energy is in the lower area of the pipe system - shown as an example in the lower pipe bend 110.

From the descent pipe 160, pistons 170, which are under the pressure pK (generated by the weight of the subsequent piston stack 171), are introduced into the introduction devices 121 ( Fig.23 , 24 ) or 122 ( Fig.25 , 26 ) pushed. The pressure pK is greater than the maximum working pressure pA generated by the areas in the riser pipe 130.

The introduction device 121 or 122 is supplied from the outside with the heated working medium 52, the heated heating medium 56 or the heated working mixture 59, which is under a metering pressure pD - which is also greater than the maximum working pressure pA.

In the introduction device 121 or 122, the heated working fluid 52 and the heated thermal medium 56 ( Fig.23 , 25 ) or the heated working mixture 59 ( Fig.24 , 26 ) between two pistons 170 introduced. This area thus becomes a work area.

For the overall systems Fig.23 and 25 With separate introduction of the heated working medium 52 and the heated heating medium 56, the two media are mixed after introduction with the internal formation of a working mixture 59.

In addition, in the insertion device 122 ( Fig.25 , 26 ) of the further developed first energy converter 26 unheated weight medium can be introduced between two work areas. An area filled with weight medium 60 thus becomes a weight area GB.

The amount of media supplied and the time of introduction are controlled by metering devices 126. To safely introduce the working medium or the weight medium, individual pistons 170 can be briefly stopped in the introduction devices 121 and 122 by a piston stop device 125. After the stopped pistons 170 are released, the introduced areas are pushed into the riser pipe 130 by the piston pressure pK of the subsequent pistons or the next introduced areas.

The pistons 170 create a spatial and thermally insulated boundary for the heated working medium or the weight medium from the preceding or following areas.

The targeted control of the introduction allows the further developed first energy converter 26 to also be operated in an operating mode without a weight medium and thus the usable temperature range is extended to lower temperature differences.

In principle, it is not necessary for the further developed first energy converter 26 ( Fig. 24 , 25 ) to give the areas between two pistons a specific assignment to the working area or weight range. Any area between two pistons can be a working area or a weight area. From a technical point of view, however, it can make sense to design the pistons differently and thus explicitly assign the pistons to the working or weight range.

• Leichteres und sichereres Einbringen der Medien
• Bessere Steuerungsmöglichkeiten des Energiewandlers
• Messtechnische Aufgaben

Possible reasons include:

• Easier and safer introduction of media
• Better control options for the energy converter
• Measurement tasks

Step 2 - Conversion of thermal energy into potential energy

After the work areas AB or weight areas GB (the latter only in the further developed first energy converter 26) enter the rise pipe 130, as in connection with Fig. 6 and 10 explains, a slow reduction in the working pressure pA on the upper piston. The preferred embodiment of the riser pipe 130 according to the invention is vertical without a change in direction. The general basic principle of pressure build-up also allows an oblique, helical or other upward design of the rise pipe 130.

After falling below a working pressure pA, which is dependent on the temperature and the vapor pressure curve of the working fluid used, the warm working fluid 52 contained in the working mixture 59 begins to evaporate in a flash evaporation, so that warm working fluid vapor 53 is created. This results in an increase in the volume of the working area while at the same time cooling down the remaining working mixture. Due to this increase in volume, all work and weight areas located above this work area (the latter only in the further developed energy converter 26) are raised in the riser pipe. With a sufficiently large increase in volume, this leads to an escape of cold working medium vapor 54, cold heat medium 55 and, in the further developed energy converter 26, weight medium 60 in the upper region of the pipe system - shown as an example in the upper pipe bend 140 - into the separation device 150.

As the media exits the separation device 150, the remaining working pressure pA, which is placed on the work and weight areas remaining in the riser pipe 130 (the latter only in the further developed first energy converter 26), is reduced. In the work areas AB that are still in the riser pipe 130, this leads to further expansion evaporation of the working mixture 59, an expansion of the already warm, pressurized working medium vapor 53, an associated increase in volume of the work areas and the lifting of all areas located above an individual work area.

• Austritt von Medien im oberen Bereich des Rohrsystems
• eine dadurch initiierten Druckverringerung im Aufstiegsrohr 130
• einer nachfolgenden Entspannungsverdampfung von Arbeitsmittel aus dem Arbeitsgemisch
• Anheben der Bereiche im Aufstiegsrohr 130

wiederholt sich stetig durch Zuführung neuer Bereiche in den Einbringvorrichtungen 121 bzw. 122. Dadurch unterliegt das warme Arbeitsgemisch 59 während des Aufstiegs im Aufstiegsrohr 130 einer kontinuierlichen Entspannungsverdampfung des Arbeitsmittels bei gleichzeitiger Abkühlung des Arbeitsgemisches 59 und des bereits entstandenen Arbeitsmitteldampf 53.The described process of

• Media leakage in the upper area of the pipe system
• a pressure reduction initiated thereby in the riser pipe 130
• a subsequent flash evaporation of working fluid from the working mixture
• Raising the areas in the riser pipe 130

is repeated continuously by supplying new areas in the introduction devices 121 and 122. As a result, the warm working mixture 59 is subject to continuous flash evaporation of the working fluid during the rise in the riser pipe 130, with simultaneous cooling of the working mixture 59 and the already formed working fluid vapor 53.

At the end of the ascent, the working medium 52 has completely evaporated from the working mixture 59 and only the heating medium 55 remains liquid. The heat medium has cooled down to the condensation temperature, the resulting working medium vapor 54 is expanded with an increase in volume and cooling down to the condensation pressure.

Due to the principle of the freely movable pistons 170, there is no mechanically predetermined p-V characteristic curve of the first (25) and the further developed first energy converter (26). This means that the p-V characteristic of the first energy converters is variable and, due to the self-regulating working pressure pA of each individual work area and the resulting forced expansion evaporation of the work fluid, automatically adapts to the p-V evaporation characteristic of the work fluid used in the temperature range used.

Something comparable is not possible with devices according to the state of the art.

• eine stufenlose Volumenvergrößerung von mehr als 1:100 - bezogen auf das Ausgangsvolumen des flüssigen warmen Arbeitsmittels 52 zum Endvolumen des vollständig verdampften kalten Arbeitsmittels 54 - sowie
• eine stufenlose Druckentspannung von weit mehr als 1:10 - bezogen auf den maximalen Arbeitsdruck pA auf dem unteren Niveau des ersten Energiewandlers zum minimalem Arbeitsdruck (Kondensationsdruck) auf dem oberen Niveau des ersten Energiewandlers - möglich

The same is with it

• a continuous volume increase of more than 1:100 - based on the initial volume of the liquid warm working fluid 52 to the final volume of the completely evaporated cold working fluid 54 - as well
• a continuous pressure relief of well over 1:10 - based on the maximum working pressure pA at the lower level of the first energy converter to the minimum working pressure (condensation pressure) at the upper level of the first energy converter - is possible

Step 3 - Separation and removal of media

After the working medium vapor 54, the cooled, liquid-remaining heat medium 55 or weight medium 60 (the latter only in the further developed first energy converter 26) emerges from the pipe system at the upper level - shown as an example, the upper pipe bend 140 - the media are separated in the separation device 150 .

The remaining liquid heat medium 55 is captured and collected. In the further developed energy converter 26, the remaining liquid heat medium 55 is collected together with the weight medium 60. The collected cold heat medium 55 - also the weight medium in the further developed first energy converter 26 - leaves the first energy converter 25 or 26 via feeds 40 and, depending on the design of the overall system, flows into the mixing chamber 33, the second energy converter 34 or - in the case of overall systems using the mE- TLC process - the heat exchanger 31.

The working medium vapor 54 is supplied to the vapor liquefaction device 32 through feeds 40. Any droplets of the heat medium that may have been entrained by the working medium vapor 54 are separated in the separation device 150 and fed to the collected heat medium.

Step 4 - Return the Pistons

The pistons 170, which are inoperative after the media exits the upper pipe bend 140, are guided further to the descent pipe 160. There, due to the weight of the pistons, the remaining working medium vapor 54 is pressed out of the pipe system into the separation device 150 through outlet openings provided for this purpose.

The pistons 170 are brought together as a piston stack 171 and, due to their own weight, generate the piston pressure pK required in the insertion devices 121 and 122.

Further considerations

The inventive structure of the first energy converters 25 and 26 as a closed pipe system with free-running pistons opens up the possibility of energy conversion from thermal to potential energy with a very large and variable working range in terms of the possible increase in volume and the working pressure to be reduced.

The stepless and variable flash evaporation of a working medium, which can be achieved using the principle of individual small working areas, can only be compared with a very finely stepped turbine.

The particular advantage of the large number of individual work areas is the associated long time (compared to the state of the art) from the start of the flash evaporation of the work fluid until it exits at the upper level (see Fig.4 ff., points 3-5 of the TS diagram).

With a maximum of 5 new working areas per second (ideally less than one working area per second) and a minimum of 10 working areas required to build up pressure in the pipe, this results in a relatively long flash evaporation time of 2-10 seconds (at higher temperatures of the warm working fluid and the heating medium up to a few minutes due to the larger number of work areas), which cannot be achieved with devices according to the prior art.

This long period of flash evaporation avoids the formation of explosive vapor bubbles, which poses a great danger in devices according to the prior art due to droplet erosion.

As a further advantage, the flash evaporation curve of the E-TLC or E-TLC2 process can be seen in the TS diagram according to Fig. 34 and Fig. 4 from point 3 to point 5 pass through safely and completely and the thermal energy previously absorbed can be completely converted.

• Fig. 27a - Verlauf unter Basis-Betriebsbedingungen (siehe gestrichelte Linien) definiert durch die Temperatur der Wärmequelle und der Dampfverflüssigungstemperatur
• Fig. 27b - Verlauf mit gegenüber den Basis-Betriebsbedingungen (siehe gestrichelte Linien) erhöhter Temperatur der Wärmequelle
  • (Bsp.: Nutzung von Solarthermie als Wärmequelle im Sommer)
  • Der Ausgangspunkt der Entspannungsverdampfung (Punkt 3) ist nach oben verschoben.
  • Es wird mehr thermische Energie als unter Basis-Betriebsbedingungen umgesetzt.
• Fig. 27c - Verlauf mit gegenüber den Basis-Betriebsbedingungen (siehe gestrichelte Linien) erhöhter Dampfverflüssigungstemperatur
  • (Bsp.: Nutzung von Erdwärme als Wärmequelle und Kühlung durch Umgebungsluft im Sommer)
  • Die Kondensationslinie von Punkt 5 zu Punkt 1 ist nach oben verschoben.
  • Die Entspannungskurve von Punkt 3 zu Punkt 5 ist verkürzt.
  • Es wird weniger Energie als unter Basis-Betriebsbedingungen umgesetzt.
• Fig. 27d - Verlauf mit gegenüber den Basis-Betriebsbedingungen (siehe gestrichelte Linien) erhöhter Temperatur der Wärmequelle und erhöhter Dampfverflüssigungstemperatur
  • (Bsp.: Nutzung von Solarthermie als Wärmequelle und Kühlung durch Umgebungsluft im Sommer)
  • Je nach Temperaturdifferenz zwischen Punkt 2 und 3 kann mehr oder auch weniger thermische Energie als unter Basis-Betriebsbedingungen umgesetzt werden.

In addition, various scenarios are shown in Fig. 27 as a TS diagram of the work equipment in the E-TLC process.

• Fig. 27a - Course under basic operating conditions (see dashed lines) defined by the temperature of the heat source and the vapor liquefaction temperature
• Fig. 27b - Course with the temperature of the heat source increased compared to the basic operating conditions (see dashed lines).
  • (Ex.: Use of solar thermal energy as a heat source in summer)
  • The starting point of flash evaporation (point 3) is shifted upwards.
  • More thermal energy is converted than under basic operating conditions.
• Fig. 27c - Course with increased vapor liquefaction temperature compared to the basic operating conditions (see dashed lines).
  • (Ex.: Use of geothermal energy as a heat source and cooling by ambient air in summer)
  • The condensation line from point 5 to point 1 is shifted upward.
  • The relaxation curve from point 3 to point 5 is shortened.
  • Less energy is converted than under basic operating conditions.
• Fig. 27d - Course with increased temperature of the heat source and increased vapor liquefaction temperature compared to the basic operating conditions (see dashed lines).
  • (Ex.: Use of solar thermal energy as a heat source and cooling using ambient air in summer)
  • Depending on the temperature difference between points 2 and 3, more or less thermal energy can be converted than under basic operating conditions.

Another important point is the design of the surrounding pipe system and the pistons. The tubes for guiding the pistons are provided with a well-sliding thermal internal insulation such as PTFE or polyamide (PA).

The pistons themselves are provided on the sealing surfaces with a sealing and sliding material that matches the material of the inner insulation of the pipe, which ensures both sealing of the areas and thermal insulation.

Within a working area, the contact of the media with the pipe wall and the stripping of the media from the pipe wall by the piston leads to turbulence and intensive mixing of the media. This promotes heat distribution and thus the evaporation of the working fluid. This turbulence can be promoted through a suitable design of the piston and the piston seal.

The pistons also preferably have a roughened, porous surface, which promotes the formation of bubbles when the working fluid evaporates (comparable to the effect of boiling stones).

Since, due to the design of the first energy converters according to the invention, only very small pressure differences of less than 0.001 MPa (0.01 bar) occur on the pistons (pressure difference = piston weight/area), the main task of the piston seal is to provide a support function to prevent the pistons from tipping in the pipe system to prevent. This is possible through a suitable piston design. Corresponding piston designs are known in the professional world.

The pipe cross section supports the piston design. In addition to a circular cross section, non-circular pipe cross sections (e.g. ellipse or oval) have advantages, for example in the design of the insertion device or the outlet openings and other tasks.

Designing the lower and upper sections of the circumferential pipe system as a horizontal zone with constant pressure (for examples see Fig. 27) in combination with a non-circular pipe cross section also facilitates the technical design of the introduction devices 120 and 121 or the separation device 150.

Process examples

As listed in Table 1 as an example, the overall system is 11 or 15 ( Fig.5 , 11 ) even small temperature differences of 10°K can be used.

The small pressure difference of only 0.033 MPa (0.33 bar), which is thermodynamically given due to the temperature difference, between the maximum working pressure and the steam liquefaction pressure in the first energy converter 25 or 26 according to the invention is converted into one - through the second Energy converter 34 technically usable - pressure difference of at least 0.25 MPa (2.5 bar) for the working medium or at least 0.4 MPa (4.0 bar) for the heat medium is implemented. Something comparable cannot be achieved with devices according to the state of the art.

With such small temperature differences, the entire system should preferably be 17 Fig. 13 with a cold working mixture 58 as weight medium 60 are used. This has a further reduced height compared to the overall system 15 and only requires a one-piece second energy converter 34 or one-piece heat exchanger 31.

The use of the further developed energy converter 26 according to the invention Fig.25 or 26 with additional weight ranges significantly reduces the technically necessary height to build up the maximum working pressure pA between the lower and upper levels at higher inlet temperatures, as already explained in the explanation Fig. 10 to 12 explained.

Table 2 shows an example of a comparison of the overall systems 11 (without weight medium) and 15 (with weight medium) with otherwise identical input parameters. The use of the further developed first energy converter 26 with a weight medium reduces the overall height of the entire system by approximately 85%.

As can be seen from the values for the entire system 15, when using a weight medium, the minimum required differential pressure (see Fig.11 pV diagram: Difference between points 7 and 2) of the working fluid for the second energy converter 34 to the limiting factor for the height of the first energy converter (0.25 MPa in the example).

The use of an overall system 17 ( Fig.13 ) with working mixture significantly reduces the overall height of the entire system by approx. 20%.

Table 3 shows examples of the working parameters of an overall system 18 with a further developed first energy converter 26 at different working temperatures. The temperature scenario shown (increase in the maximum working temperature from 40 to 100 °C) corresponds to the daily course of an energy converter with solar thermal heat supply and liquefaction of the working fluid vapor by ambient air as the ambient temperature increases (increase in the condensation temperature from 20 to 40 °C).

The changing operating parameters depending on the change in the maximum working temperature and the condensation temperature are clearly visible.

The last column shows an example of the influence of the condensation temperature on the achievable performance. The lower the condensation temperature, the higher the theoretical efficiency and thus the achievable performance.

Assuming the number of new work areas added per second, the number of total work areas in the riser tube corresponds to the number of seconds that a work area requires to pass from the lower to the upper level of the overall system.

Also listed are the number of work areas in which the work fluid passes through the flash evaporation curve from thermodynamic point 3 to point 5 of the E-TLC2 process. The influence of the condensation temperature is also clearly visible here. Table 1: Example values for the implementation of the E-TLC process with devices 11, 12 and 17 at a temperature difference of 10° between the inlet and condensation temperatures Input parameters Unit Device 11 Device 15 Device 17 Max. working temperature °C 40 condensation temperature °C 30 Mean Efficiency according to Carnot % 1.62 Pipe diameter m 0.1 Work equipment/density - / kg/ ^m2 N - Pentane / 605.76 Max. working pressure MPa 0.115 Condensation pressure MPa 0.082 Amount of work equipment kg 0.10 Starting height of work equipment m 0.021 Heat medium/density - / kg/ ^m2 Water / 998 Amount of heat medium kg 0.82 Amount of weight medium kg 0 0.6 1.6 Result parameters Height of working fluid vapor m 5.23 Relaxation ratio AM 1:249 Necessary pipe height m 74 48 32 Number of work areas - 30 19 13 Usable differential pressure between points 7 and 2 of the pV diagram Work equipment MPa 0.41 0.253 --- Heat/weight medium MPa 0.687 0.433 --- Working mixture MPa --- --- 0.26 Work performed per work area kWs -0.6 Area performance kW/ ^m2 -75 Example values for reducing the overall height of the entire system by using weight medium at an inlet temperature of 100°C and a condensation temperature of 40°C Input parameters Unit Overall system 11 Overall system 15 Overall system 17 Design of the first energy converter - 25 26 Max. working temperature °C 100 condensation temperature °C 40 Average efficiency according to Carnot % 8.74 Pipe diameter m 0.1 Work equipment/density - / kg/ ^m2 n - pentane / 605.76 Max. working pressure MPa 0.59 Condensation pressure MPa 0.115 Amount of work equipment kg 0.1 Starting height of work equipment m 0.024 Heat medium/density - / kg/ ^m2 Water / 998 Amount of heat medium kg 0.081 Weight Medium/Density - / kg/ ^m2 Water / 998 Amount of weight medium kg 0 4.5 9 Result parameters Height of working fluid vapor m 3.8 relaxation ratio - 1:158 Necessary pipe height m 880 124 100 Number of work areas - 915 79 40 Differential pressure of work equipment between points 7 and 2 MPa 4.7 0.25 --- Differential pressure of heat/weight medium between points 7 and 2 MPa 8.1 0.72 --- Differential pressure working mixture between points 7 and 2 --- --- 0.26 Work performed per work area kWs -3.1 Area performance in a working area / sec kW/ ^m2 395 Example spread of working parameters for solar thermal heating and cooling by ambient air Input parameters Unit Overall system 18 First energy converter operating mode - Energy converter 26 Max. working temperature °C 40 60 80 100 100 condensation temperature °C 20 30 40 20 Average efficiency according to Carnot % 3.3 4.7 6 8.74 12.0 Pipe height m 90 Pipe diameter m 0.1 Working medium / density @20°C - / kg/ ^m2 N - Pentane / 625.76 Max. working pressure MPa 0.115 0.214 0.368 0.59 Condensation pressure MPa 0.056 0.082 0.115 0.056 Amount of warm work equipment kg 0.1 Starting height of work equipment m 0.0210 0.0215 0.227 0.24 0.24 Heat medium / density @20°C - / kg/ ^m2 Water / 998 Amount of heat medium kg 0.39 0.155 0.081 0.052 Height of heat medium m 0.05 0.02 0.0106 0.0067 Weight medium / density @20°C - / kg/ ^m2 Water / 998 Amount of cold weight medium kg 1.4 2.2 3.5 8.7 15.8 Height weight medium m 0.18 0.28 0.45 1.12 2.0 Result parameters Height of working fluid vapor m 7.37 5.23 3.78 3.78 7.37 relaxation ratio - 1:350 1:243 1:166 1:157 1:307 Total number of work areas / work areas with evaporation - 180/20 126/36 93/49 43 / 41 28/27 Work performed per work area kWs 1.2 1.71 2.13 3.1 4.4 Area performance in a working area / sec kW/ ^m2 155 218 270 395 566

Claims (20)

Method for converting thermal energy from a low-temperature heat source with temperatures of a maximum of 200 ° C in a triangular process, hereinafter referred to as "Extended Trilateral Cycle" (E-TLC), into volume change work and subsequently technically usable energy that goes through the following states or steps: • A first process state (1) with a liquid working mixture (58) under a first pressure at a first temperature • An increase in the pressure and an increase in the temperature of the working mixture to a second pressure and a second temperature without evaporation of the working mixture, the second pressure and the second temperature being higher than the first pressure and the first temperature • A second process state (3) with a liquid working mixture (59) under the second pressure and heated to the second temperature. • A flash evaporation of the working mixture initiated by external pressure reduction with partial evaporation of the working mixture while at the same time volume change work is carried out by the resulting steam or volume increase of the already existing steam • A third process state (5) with the working mixture (58) which is again under the first pressure, partially evaporated and cooled to the first temperature. • A condensation of the evaporated portion of the working mixture at the first temperature with the removal of entropy to a liquid and subsequent mixing with the remaining liquid portion, which restores the first process state characterized by that : • The working mixture consists of a working medium and a heat medium that is not chemically identical to the working medium, whereby the heating medium has a higher evaporation temperature than the working medium at the same pressure • During flash evaporation, only the working medium evaporates and the heating medium remains in a liquid state at all times • The working fluid completely evaporates from the working mixture and only the heating medium remains liquid • The flash evaporation of the working fluid is polytropic • The additional thermal energy required for the polytropic flash evaporation of the working medium is transferred from the heating medium (56) to the evaporating working medium (52), thereby cooling the heating medium. Energy converter (25) for converting thermal energy into potential energy to realize polytropic flash evaporation of a working medium according to claim 1 , characterized by at least the components: • A closed, thermally insulated, upward pipe system with an ascent pipe (130) and a descent pipe (160), connected by pipe bends (110, 140) • A number of at least 10 pistons (170) rotating freely in the closed pipe system, which have a roughened, porous surface on the front, which promotes the formation of bubbles in the working fluid • Introduction openings and an introduction device (121) on the lower level of the pipe system for introducing a working medium (52) heated by contact with a heat source and a heated heating medium (56), which can also be present as a working mixture (59), into a work area (AB ) between two pistons (170) • Outlet openings in the jacket of the pipe at the upper level for exhausting the completely evaporated working fluid (54) and the cooled heat medium (55) that has remained liquid from the pipe system • A separation device (150) for separating the evaporated working fluid (54) and the cold heat medium (55) that remains liquid. Energy converter (26) according to claim 2, characterized by at least the components: • Additional introduction openings and an introduction device (122) on the lower level of the pipe system for introducing a weight medium (60) into a weight area (GB) between two work areas (AB), whereby the weight medium (60) has not been heated by the heat source • Outlet openings on the upper level for jointly exhausting the completely evaporated working medium (54), the remaining liquid heat medium (55) and the weight medium (60) from the pipe system • A separation device (150) for separating the evaporated working fluid (54) from the cold heat medium (55) that remains liquid and the liquid weight medium (60). Energy converter (26) according to claim 3, characterized in that an operating mode without a weight medium according to claim 2 is possible by appropriate control. Energy converter according to one of the preceding claims 2-4, characterized in that : • At least 10, preferably more than 20, independent, individual work areas (AB) are provided in the riser pipe (130) of the energy converter to convert the thermal energy of the heated working fluid (52) and the warm heat medium (56) into potential energy • the working pressure (pA) of the work areas (AB) is released continuously • The volume of the work areas (AB) can be increased continuously • the movement of an individual work area (AB) from introduction to the lower level to reaching the upper level takes at least 2 seconds, preferably more than 10 seconds • There are pressure differences of less than 0.001 MPa on the seal of the pistons (170) between the individual working areas (AB) or working areas (AB) and weight areas (GB). Device for converting the thermal energy of a low-temperature heat source with temperatures of a maximum of 200 ° C in two steps into technically usable mechanical energy, characterized by • at least one first energy converter according to one of the preceding claims 2-5, which has a working medium (AM) and a heat medium (WM) using thermal energy from a low-temperature heat source with a temperature of a maximum of 200 ° C by implementing the E-TLC process Claim 1 raises from a lower level to an upper level and converts the thermal energy absorbed by the working fluid (AM) and the thermal medium (WM) into potential energy of the working fluid (AM) and the thermal medium (WM). • a second energy converter (34), which releases the obtained potential energy as technically usable mechanical energy by returning the working medium (AM) and the heat medium (WM) from the upper to the lower level. Device (11) according to claim 6, characterized in that it comprises at least the following components: • A heat exchanger (31) for transferring the thermal energy of a low-temperature heat source with temperatures of a maximum of 200 ° C to a liquid working fluid (51) under metering pressure (pD) and to a liquid heat medium under metering pressure (pD) without evaporation of the working fluid or of the heat medium • Thermally insulated feeds (40) in order to supply the working fluid (52) heated in the heat exchanger (31) and the heated thermal medium (56) to a first energy converter (25) according to one of claims 2-9 • At least one first energy converter (25) according to one of claims 2-5 for converting the thermal energy of the working fluid (52) and the heat medium (56) into potential energy • Feeds (40) to feed the working medium (54) which has completely evaporated in the first energy converter (25) to a steam liquefaction device (32). • A vapor liquefaction device (32) for liquefying the evaporated working fluid (54) • Feeds to supply the liquid, cold heat medium (55) and the condensed liquid working medium (51) to a second energy converter (34). • A two-part second energy converter (34) for converting the potential energy of the working medium (51) and the heat medium (55) into technically usable energy • Feeds to feed the working medium (51) still under metering pressure (pD) and the heat medium (55) still under metering pressure (pD) from the second energy converter back to the heat exchanger (31). Device (2xx) according to claims 6-7, characterized in that the transfer of the thermal energy from a low-temperature heat source with temperatures of a maximum of 200 ° C to the working fluid (51) and the heat medium (55) without evaporation of the working fluid or the heat medium in one vertically arranged heat exchanger (31) while simultaneously building up a high static pressure Device (12-14, 16-20, 212, 216, 219) according to claim 7 or 8, characterized in that the working medium (AM) and the heat medium (WM) are in one before being fed to the first energy converter (25, 26). Mixing chamber (33) are combined in a process-specific ratio to form a working mixture (AG). Device (15-20, 216,219) according to one of claims 6 to 9, characterized in that in addition to the working medium (52) and the heat medium (56), a weight medium (60) is raised from the lower to the upper level. Device according to claim 10, characterized in that the weight medium (60) • unheated heat medium or • unheated work equipment or • is a mixture of unheated working fluid and unheated heating medium. Device (11-20, 211,212,216,219) according to one of claims 6-11, characterized in that: • Several of the first energy converters (25,26) according to one of claims 2 to 5 are arranged in parallel, which share the other listed components • The first several energy converters (25,26) can be switched on or off individually. Device (11-20, 211, 212, 216, 219) according to claims 6-12, characterized in that it has a control and regulation system which: • controls the number of first energy converters (25,26) switched on or off and adapts them to changes in the temperature of the low-temperature heat source, the condensation temperature or the available amount of energy of the low-temperature heat source • It has a control and regulation system which regulates the amount of heated working fluid (52), the heated heat medium (56) and the weight medium (60) fed in and adapts it to changes in the temperature of the low-temperature heat source, the condensation temperature or the available amount of energy of the low-temperature heat source . Method according to claim 1 for converting the thermal energy of a working medium (52) heated by the thermal energy of a low-temperature heat source with a temperature of a maximum of 200 ° C and a heat medium (56) heated to the same temperature by the thermal energy of the low-temperature heat source into potential energy the working fluid and the heat medium comprising the steps • The warm, liquid working medium (52) and the warm, liquid heat medium (56) are introduced into an energy converter (25,26) according to one of claims 2-5 • The warm, liquid working medium and the warm, liquid heating medium are conducted as a working mixture (AG) in the first energy converter (25,26) in a working area (AB) spatially delimited by pistons (170). • The working areas (AB) with the warm working mixture (59) are raised from a lower level to an upper level in the first energy converter (25,26), with the working mixture being raised to the upper level by polytropic conversion of the thermal energy of the working medium ( 52) and the heat medium (56) in lifting work by complete flash evaporation of the working medium (52) according to the E-TLC process according to claim 1. Method according to claim 14, characterized in that • In addition to the heated working medium (52) and heating medium (56), an unheated weight medium (60) is lifted from the lower to the upper level • the weight medium (60) is transported to the upper level in a thermally isolated manner from the heated working medium (52) and the heated heat medium (56) in weight areas (GB) spatially delimited by pistons (170). Method according to one of the aforementioned claims 14-15, characterized in that the conversion of the thermal energy of the working medium (52) and the heat medium (56) into potential energy in the first energy converter (25,26) • takes place in at least 10, preferably more than 20, independent, individual work areas (AB). • runs continuously and steplessly • The pV characteristic curve of the first energy converter (25,26) according to claims 2-5 is automatically adapted to the pV evaporation characteristic curve of the working fluid used. Method for converting the thermal energy of a low-temperature heat source with a temperature of a maximum of 200 ° C in a closed circuit into technically usable mechanical energy, characterized in that the conversion takes place in at least the following steps: • The thermal energy of the low-temperature heat source is converted into potential energy in a first step in a method according to claims 14-16 • In a second step, the potential energy is converted into technically usable mechanical energy Method (E-TLC2 process) according to claim 17 with at least the following method steps: • Step a: Isobaric heating of a liquid working fluid (51) under metering pressure (pD) and a liquid heat medium (55) under metering pressure (pD) - which can also be present as a working mixture (58) - from a low-temperature heat source without evaporation of the working fluid • Step b: Polytropic conversion of the absorbed thermal energy according to claim 1 in at least one, preferably several first energy converters (25, 26) according to claims 2-5 into potential energy of the working medium and the heat medium • Step c: Isobaric condensation of the evaporated working fluid (54) • Step d: Isothermal conversion of part of the obtained potential energy of the working medium and the heat medium - which can also be present as a working mixture (58) - in at least a second energy conversion device (34) into technically usable mechanical energy Method (mE-TLC2 process) according to claim 17 with at least the following method steps: • Step a: Polytropic conversion of the thermal energy of a heated working medium (52) under metering pressure and a heated heating medium (56) under metering pressure - which can also be present as a working mixture (58) - according to claim 1 in at least one, preferably several first energy converters (25,26) according to claims 2-5 in potential energy of the working fluid and the heat medium • Step b: Isobaric condensation of the evaporated working fluid (54) • Step c: Isochoric heating of the liquid working fluid (51) and the liquid heat medium (55) - which can also be present as a working mixture (58) - with simultaneous pressure increase from a low-temperature heat source (31) without evaporation of the working fluid • Step d: Isothermal conversion of part of the obtained potential energy of the working fluid (52) and the heat medium (56) in at least one second energy converter (34) into technically usable mechanical energy without evaporation of the working fluid. Method according to one of the aforementioned claims 17-19, characterized in that a continuous adjustment is achieved by varying the amount of the heated working medium (52), the heated heating medium (56) and, if necessary, the weight medium (60). • due to changes in the temperature of the low-temperature heat source • due to changes in the condensation temperature • due to changes in the amount of energy available from the low-temperature heat source.

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