Energy conversion system

Abstract

An energy extraction and / or conversion system comprising: a first sub-process utilizing a first compressor (A) to compress a first media used as an energy supply media, and a first heat exchanger (B) to transfer energy from the first media compressed by the first compressor (A) to a second media used as a cooling media in a second sub-process; the second sub-process utilizing the first heat exchanger (B) to transfer the energy from the compressed first media to the second media, a second compressor (G) to compress the second media from the first heat exchanger B, a second heat exchanger (D) configured to transfer energy from the compressed second media from the second compressor (G) to a third media used as a working media in a third sub-process, an expansion valve (E) configured to increase the volume and reduce pressure of the second media from the second heat exchanger (D), and a third heat exchanger (F) configured to transfer energy from the third media at an expanded state to the second media after the expansion valve (E); and a third sub-process utilizing the second heat exchanger (D) to transfer the energy from the compressed second media to the third media, an expander unit (H) configured to expand the third media from the second heat exchanger (D) into the expanded state, and the third heat exchanger (F) to transfer the energy from the third media at the expanded state to the second media, thus transferring thermal energy, and energy of the at least partial condensation, and facilitating at least partial condensation of the third medium.

Description

[0001] ENERGY CONVERSION SYSTEM

[0002] TECHNOLOGICAL FIELD

[0003] The present disclosure generally relates to energy transfer and conversion system and related processes.

[0004] BACKGROUND

[0005] While a four-stroke combustion-engine and a Diesel-engine look very similar and have also nearly all parts in common, they are significantly different. The higher pressure and temperature during the compression and then also the differences in adding the fuel to the air, lead with these two details to a rather different process. This disclosure is also based - as the Diesel-engine - on known components and still forms a process with large differences and a very different outcome, than the processes that share similar or the same components.

[0006] A process that can cool a medium, but without the need of external energy for the cooling-process, even maybe generating an energy-surplus, has been looked for since the beginning of cooling-processes. Already in patent GB 2064 (Sir Charles William Siemens from 1857) - there in Figure 2 - an expander - referred to as “air- engine” - is shown. This “air-engine” has the task to recover energy in form of mechanical-energy. Many other processes were thought of, invented, introduced, published, etc., but as we know today, obviously none of them were good enough to be realised, and or make it to the market. So, we still have to pay for the consumed external-energy of cooling-devices like air-condition-systems, refrigerators, etc.

[0007] In a vapour-compression-cooling-process external -energy is used to drive a compressor, which is used for increasing the temperature of the medium receiving the thermal-energy to be removed, and thus there is always more thermal -energy available at the end of a vapour-compression-cooling-process, than the thermal-energy, which has been removed by this cooling-process. A vapour-compression-cooling-process is converting thermal-energy with a specific temperature into more thermal-energy with higher temperature, which allows then easy dissipation of the thermal-energy into the environment, etc. Still, it is impossible with such cooling-processes to use this increased, warmer thermal-energy at the end, to sustain the process.

[0008] The most efficient possible recovery process among known and possible recovery -processes would be a Rankine-process or a process similar to it. In such a Rankine-process the largest amount of energy is (always) required for the necessary phase-change of the used medium of the Rankine-process from a liquid state of aggregate to a gaseous state of aggregate. Especially at lower temperature levels, this amount of energy needed for the phase-change in a Rankine-process, especially in an organic-Rankine-cycle, reaches easily significantly over 90% of the available introduced thermal-energy. These easily significantly over 90% of the available introduced energy cannot be used for the conversion into mechanical-energy in an expander-mechanism! Often this energy, required for the phase-change of the used medium, is also called “rejected heat” (even it is neither heat nor rejected!).

[0009] The term state of aggregate is used herein to refer to the physical state of matter either solid, liquid, gaseous, or super critical, etc.

[0010] To reach a meaningful conversion rate from generated thermal -energy into mechanical-energy at the end of a vapour-compression-cooling-process, especially at lower temperatures, it is necessary to recover at least a significant part of the energy of the phase-change.

[0011] Such a process that takes the energy of the phase change, the evaporationenthalpy, in the conversion from thermal energy to mechanical energy into consideration is described in WO 2019 053705 Al (Zettner).

[0012] This process described in WO 2019 053705 Al (Zettner) transfers the external thermal energy through a heat-exchanger. Thus, the temperature, with which the external thermal-energy is transferred to the expander, is at least slightly decreasing, thus lower, than at the beginning. To transfer a specific amount of thermal -energy at a lower temperature requires an increase of mass of the medium transferring that thermalenergy to reach the same amount of energy.

[0013] As a consequence, the relation between the energy for the phase change, from liquid to gas on one side, and the thermal-energy, available for the conversion to mechanical-energy, on the other side, is shifting - as more energy is required for the evaporation, as the mass is increasing. In turn, of the total energy the percentage of available energy for the conversion into mechanical energy is decreasing. While the process described in WO 2019 053705 Al (Zettner) is still able to get all of the external thermal-energy to the expander for the conversion to mechanical energy, the percentage of the energy needed at the same time for the phase-change is increasing, getting larger.

[0014] As the expander needs to process the total energy, which is used for the phasechange and also what is left for the conversion to mechanical energy, the total energy is higher, than just the part of the energy for the conversion to mechanical-energy - and so are then also the mechanical losses.

[0015] As described in WO 2019 053705 Al (Zettner) at a temperature of 200 degrees Centigrade the relation between the energy required for the phase change and the energy available for the conversion to mechanical-energy is around nine to one. If only ten per cent of the total energy can be converted to mechanical energy, this ten per cent need also to cover the mechanical losses, and the energy for the compressor and the two pumps. While with temperatures above 200 degrees Centigrade there might be enough energy left after the necessary phase-change, with temperatures at, or lower, than 200 degrees Centigrade, the process described in WO 2019 053705 Al (Zettner) will not be able to sustain itself.

[0016] At the end the mechanical losses of the used compressors, expanders, and pumps of such a system would consume more energy, than external energy has been supplied to the system. This is an inherent shortcoming of the process of WO 2019 053705 Al (Zettner).

[0017] GENERAL DESCRIPTION

[0018] There is a need in the art for improved energy extraction and or conversion techniques that can be operated with relatively low temperature energy sources (e.g., in the range of -80 to 250 degrees centigrade) and with relatively smaller amounts of intermediate energy transfer media (also referred to herein as sub-process 'Cooling Stream' or second media).

[0019] Today, known and used processes to cool a medium require external energy to extract thermal-energy from the medium that needs to be cooled. Those known and used processes to cool a medium convert with their process the extracted thermal energy into more thermal energy at a higher temperature-level. This more generated thermal-energy - at a higher temperature-level - needs at the end to be dissipated, what is then easier due to the reached higher temperature-difference to the ambient environment. This application discloses a new process configured to cool a medium without external energy!

[0020] This new process extracts thermal energy from a medium, and can be used to convert this extracted thermal energy into mechanical energy, which can then be used z.e., not changing into thermal-energy at a higher temperature level.

[0021] Because this new process generates mechanical energy out of the extraction of thermal-energy, it can be used either for cooling a medium, or for generating mechanical-energy from thermal-energy of a medium, as well for both at the same time.

[0022] In possible embodiments there is a combination of several, relatively simple, interconnected sub-processes, which together form a new, highly efficient process.

[0023] The process disclosed herein can especially use low-temperature heat-sources (e.g., between minus 80 to 150 degrees Centigrade) without the need of additional external energy, and thus able to generate mechanical-energy from a low-temperature medium used as the heat-source.

[0024] Embodiments hereof are significantly more energy efficient, than other known processes performing the same or a similar task.

[0025] This combination of several combined sub-processes can also be used in a repetitive layout, repeating steps. An example for such repetitive arrangements of the process would be a process for cooling a gas-stream containing carbon-dioxide to such a low temperature that allows extracting carbon-dioxide in liquid or solid form.

[0026] Furthermore, this new process is also, compared to many other known processes with a similar task, rather simple and not very complex. Also the new process disclosed herein can be varied in many ways, additional functions can easily be added, and thus this new process can be adjusted to many situations.

[0027] Embodiments disclosed herein are able to extract thermal-energy from a medium, with no additional external energy and convert it to mechanical energy. Thus, embodiments hereof could be used either as process with the primary aim of cooling, which would need no external energy - in contrast: nearly all used cooling process today (air-condition-system, refrigerator, freezer, etc.) require additional external energy. Optionally, embodiments hereof could be used with the primary aim to generate mechanical energy from a low-temperature medium - for example warm air of the surrounding - this generated mechanical energy in turn could then drive an electricpower-generator. Also, in possible embodiments a combination of cooling and power-generation is possible.

[0028] By using available thermal -energy as the energy-source (e.g., as exemplified hereinbelow) in general, and by using low-temperature thermal -energy in particular, otherwise unused natural and or renewable energy sources, etc., can be used as powersource, thus embodiments hereof have a significant positive environmental impact.

[0029] Embodiments disclosed herein utilize a combination of several sub-processes. One sub-process is based on a ‘vapour-compression-cooling-process’, while another sub-process is based on a ‘Rankine-cycle’ to generate mechanical-energy from thermalenergy. Other parts are necessary to complete this combination of sub-processes, which makes this process in itself a unique process or a unique combination of processes.

[0030] In one aspect there is provided an energy extraction and or conversion system comprising: a first sub-process utilizing a first compressor A to compress a first media used as an energy supply media, and a first heat exchanger B to transfer energy from the first media compressed by the first compressor A to a second media used as a cooling media in a second sub-process; the second sub-process utilizing the first heat exchanger B to transfer the energy from the compressed first media to the second media, a second compressor G to compress the second media from the first heat exchanger B, a second heat exchanger D configured to transfer energy from the compressed second media from the second compressor G to a third media used as a working media in a third subprocess, an expansion valve E configured to increase the volume and reduce pressure of the second media from the second heat exchanger D, and a third heat exchanger F configured to transfer energy from the third media at an expanded state to the second media after the expansion valve E; and the third sub-process utilizing the second heat exchanger D to transfer the energy from the compressed second media to the third media, an expander unit H configured to expand the third media from the second heat exchanger D into the expanded state, and the third heat exchanger F to transfer the energy from the third media at the expanded state to the second media, thus transferring thermal energy as well at least a part of the freed energy of the condensation of at least part the third media, and facilitating at least partial condensation of the third media.

[0031] The system comprises in some embodiments a pump I utilized in the third subprocess to pump and pressurize the third media through the third heat exchanger F into the second heat exchanger D. Optionally, but in some embodiments preferably, the system comprises first, second and third flow paths for flowing therein, the first, second and third media, being gas-containing media, of the first, second and third subprocesses, respectively.

[0032] The second flow path can be configured as a closed-loop flow path for circulating the second media therein to successively pass the second media through the first heat exchanger B, the second compressor G, the second heat exchanger D, the expansion-valve E, and the third heat exchanger F, to transfer the energy from the first media to the second media within the first heat exchanger B, compress the second media by the second compressor G, thus bringing the second media to its highest temperature, causing energy transfer from the second media to the third media within the second heat exchanger D, followed by further temperature drop of the second media by expansion when passing through the expansion valve E thus allowing energy transfer from the third media to the second media at the third heat exchanger F.

[0033] In embodiments wherein the system comprises the pump I to pump and pressurize the third media, the third flow path can be configured as a closed-loop flow path utilizing the pump I to circulate the third media therein to successively pass the third media through the third heat exchanger F, the pump I, the second heat exchanger D, and the expander unit H. The third closed-loop flow path can be configured for the energy transfer from the third media to the second media within the third heat exchanger F, at least partially condense the third media at heat exchanger F, pump and compress the third media by the pump I, transfer energy from the second media to the third media within the second heat exchanger D, and expansion of the third media by the expander unit H, thus at least partially converting thermal energy into mechanical energy.

[0034] The expander unit H can be coupled to an electrical generator selected from the following: an electro-motor, an electro-alternator, and a dynamo. The system can be configured to use the electrical generator to start-up the system. In possible embodiments the electrical generator is coupled to at least one of the first compressor A, the second compressor G, and the expander unit H.

[0035] The pump I can be located between the third heat exchanger F and the second heat exchanger D in the second closed-loop flow path, and the electrical generator can be coupled to at least one of the first compressor A, the second compressor G, the expander unit H and the pump I. In some embodiments at least two of the first compressor A, the second compressor G, the expander unit H, the pump I and the electrical generator are coupled to each other via a common drive-shaft. The system may utilize magnetic-couplings, or a system of magnetic-coupling, for the coupling.

[0036] The first sub-process comprises in some embodiments at least one of filter and or absorber units, located upstream from the first heat-exchanger B with respect to a direction of flow of the first media through the energy supply flow path. In some embodiments the system comprises in the first sub-process a separator, for separating compounds. The separator can be located downstream from the first heat exchanger B with respect to a direction of flow of the first media through the energy supply flow path.

[0037] Optionally, but in some embodiments preferably, the first media is (e.g., ambient) air or water. The energy supply flow path can be connected to an external fluid source to receive said first media therefrom.

[0038] The first sub-process is configured in some embodiments as an open-loop flow path. The system can further comprise a fourth heat exchanger C arranged in the third sub-process between the second heat exchanger D and the expander unit H, and in the first sub-process upstream from the first heat exchanger B. The fourth heat exchanger C can be adapted to transfer energy directly from the first media to the third media. The system can further comprise an additional flow path for passing a heating media therethrough. The additional flow path may comprise a fifth heat exchanger K located in the second sub-process between the second compressor G and the second heat exchanger D, such that the fifth heat exchanger K is adapted to transfer energy from the second media to the heating media.

[0039] The third sub-process is configured in some embodiments as a closed-loop flow path for circulating the first media therethrough. The first sub-process may have at least one segment thereof passing through a heating zone located upstream from the first heat-exchanger B with respect to a direction of flow of the first media along the energy supply flow path, thereby causing heating of the first media flowing, thus returning from the first heat exchanger B. The system may further comprise an additional closed loop flow path for flowing an additional heating media therethrough, and a fourth heat exchanger C arranged in the third sub-process between the second heat exchanger D and the expander unit H. The fourth heat exchanger C is adapted in possible embodiments to transfer energy from the additional heating media to the third media. In another aspect there is provided an energy extraction and or conversion system comprising a plurality of sub-systems, each one of the plurality of sub-systems configured according to any one of the embodiments disclosed herein, and the plurality of sub-systems are arranged in a cascade fashion for successive passage of at least some portion of the first media through their first sub-processes (e.g., the first heat exchangers 61,62,63, ... ) of the plurality of sub-systems to form a common energy supply flow path thereof. In yet another aspect there is provided an energy extraction and or conversion system comprising several sub-systems at least one of which configured to any of the embodiments disclosed herein, whereby at least one of the sub-systems is arranged in a parallel fashion for parallel passage of at least one of the first, second or third media.

[0040] Such systems can comprise an auxiliary heat-exchanger Ci in the first subsystem. This auxiliary heat-exchanger can be located upstream from the first heatexchangers 61 in the first sub-process of the first sub-system, and between the second heat-exchanger Di and the expander unit Hi in the third sub-process of said first subsystem, the auxiliary heat-exchanger Ci transferring energy from the first media to the third media. Additionally, or alternatively, the system comprises between the second heat-exchanger D and the expansion valve E of the second sub-process of each one of the plurality sub-systems an additional heat-exchanger for transferring energy from the second media to the first media backwardly, after passing through the last sub-system in the cascade. The system also comprise in some applications at least one centrifugal separator on the common energy supply flow path between two successive sub-systems.

[0041] The system of embodiments hereof can be configured to cool the first media and extract thermal-energy and or phase-change energy thereof, and convert the extracted energy into mechanical energy, and or for generating electricity from the surplus mechanical-energy of the process.

[0042] In yet another aspect there is provided a method of extraction and or conversion of energy. The method comprises a first sub-process of compressing a first media used as an energy supply media and transferring energy from the compressed first media to a second media used as a media of a second sub-process, the second sub-process comprises receiving firstly energy from the third media from the third sub-process, secondly receiving energy from the first media of the first sub-process, compressing the second media to a higher pressure and temperature level, followed by transferring energy from the compressed second media resulting from receiving the first and second energy in addition to the energy of the compression, to a third media used as a media of the third sub-process, passing the then cooler second media through an expansion valve, increasing volume, reducing pressure of the compressed second media, and receiving then, at lowest temperature and pressure point, energy of said second media, thereby closing the second sub-process, and a third sub-process that comprises the receiving of energy from the compressed second media to the third media, and expanding the third media to generate mechanical energy followed by transferring energy during at least partial condensation from the expanded third media to the second media.

[0043] The system comprises in some embodiments exploiting at least some portion of the mechanical energy for at least one of the following: the compressing of the second media; the compressing of the first media.

[0044] The method can further comprise pumping the expanded third media. Optionally, but in some embodiments preferably, the method comprises exploiting at least some portion of the mechanical energy for at least one of the following: the compressing of the second media; the compressing of the first media; the pumping of the third media.

[0045] In possible embodiments the method comprises filtering and or absorbing before compressing the first media. The method may comprise separating compounds from the first media after the transferring of energy thereof to the second media. The method can further comprise transferring energy from the first media to the third media after the transferring of the energy from the second media to the third media. In some embodiments the method comprises transferring energy from the second media to a fourth media as a heating media before transferring energy from the second media to the third media.

[0046] The method can comprise circulating the first media through a closed-loop flow path having a heating zone configured for thermal energy therein to said first media. In some embodiments the method comprises circulating an additional heating-media through closed loop flow path and transferring energy from the additional heating media to the third media after the transferring of the energy from the second media to the third media.

[0047] In yet another aspect there is provided a method of extraction and or conversion of energy, the method comprising streaming a first media through a plurality of subsystems arranged in a cascade fashion for serially communicating first media from one sub-system to the other and extracting and or converting energy from the first media by each one of the plurality of sub-systems disclosed herein. The method can comprise serially streaming at least some portion of the first media through the plurality of subsystems, and transferring energy in at least one of said plurality of sub-systems from the second media to the at least some portion of the first media. For example, the method may comprise streaming at least some portion of the first media, after it been forwardly streamed through the plurality of sub-systems, and then backwardly streaming at least some portion of the first media through at least one of the plurality of sub-systems for transferring energy from the second media to the at least some portion of the first media. The method can further comprise separating compounds from the first media passed between at least two successive sub-systems.

[0048] BRIEF DESCRIPTION OF THE DRAWINGS

[0049] In order to better understand the subject matter that is disclosed herein and to exemplify how it may be carried out in practice, embodiments will now be described, by way of non-limiting examples only, with reference to the accompanying drawings, in which:

[0050] Figure 1 shows a flowchart of a cooling-and-energy-conversion-process in its simplest and most basic form according to possible embodiments.

[0051] Figure 2 shows a flowchart of a conventional vapour-compression-cooling- process alongside the flowchart of Figure 1 in which the ‘Cooling- Stream’ of the new cooling-and-energy-conversion-process is emphasized.

[0052] Figure 3 shows a flowchart of a conventional ‘Rankine-cycle’ alongside the flowchart of Figure 1 in which the part ‘Work-Stream’ of the new cooling-and-energy- conversion-process is emphasized.

[0053] Figure 4 shows the flowchart of the new cooling-and-energy-conversion- process of embodiments hereof, where the part ‘Energy- Supply- Stream’ is emphasized.

[0054] Figure 5 shows a flowchart of a new cooling-and-energy-conversion-process of embodiments hereof, where the part ‘Energy-Supply-Stream’ is emphasized and an additional filter plus an additional expansion-valve are used in the ‘Energy-Supply- Stream’ sub-process. Figure 6 shows a flowchart of a cooling-and-energy-conversion-system of embodiments hereof, configured to extract energy from ambient humid air and thus cool this air.

[0055] Figure 7 shows a flowchart of a cooling-and-energy-conversion-system of embodiments hereof, that condenses the spent, exiting steam of a steam turbine and converts a large part of the energy of the condensation into mechanical energy.

[0056] Figure 8 shows a flowchart of a cooling-and-energy-conversion-process of embodiments hereof with several external heat- and or energy sources.

[0057] Figure 9 shows a flowchart of a cooling-and-energy-conversion-process of embodiments hereof with several external heat- and or energy sources plus one external energy-source directly connected to the sub-process ‘Work- Stream’.

[0058] Figure 10 shows a flowchart of a cooling-and-energy-conversion-process of embodiments hereof, configured for extracting energy from cold ambient air, thus cooling it more with an additional heat-exchanger extracting some thermal-energy after the compressor of the sub-process ‘Cooling- Stream’ for heating purposes.

[0059] Figure 11 schematically illustrates a cooling-and-energy-conversion-system for extracting energy from the hot exhaust gases of a power-station with the aim to separate compounds, especially carbon-dioxide, from the exhaust by cooling the exhaust in three steps (e.g., down to minus 80 degrees Centigrade), with additional heat-exchangers using the cooled compounds to cool further the sub-process ‘Cooling-Stream’ before the expansion-valve.

[0060] Figure 12 schematically illustrates a simplified combined power station such as shown in Figure 11, with six added parallel systems to cool the exhaust-gases in order to extract compounds e.g., carbon-dioxide, from the exhaust gas-stream, plus additional cooling streams for the air-intake of the power station and the condenser-cooling-units.

[0061] Figure 13 and Figure 14 each show a flowchart according to ISO 10628 with several indicators and controls all connected to a central PLC.

[0062] DETAILED DESCRIPTION OF EMBODIMENTS

[0063] The following disclosure is directed to a process and system, realized with a specific sequence of used devices. In this application the term ‘heat-exchanger’ is used for a part or a system, which is able to transfer energy from one medium to another medium. While the term ‘heat-exchanger’ might imply some kind of a limitation to thermal -energy, the transferred energy can also be the energy of the phase-change from liquid to gas and or from gas to liquid, as this is in ‘heat-exchangers’ in nearly all vapour-compression air- condition- systems the case. Also partly or complete evaporation or condensation is possible with such devices. The term ‘heat-exchanger’ refers generally today and specifically in this application to a system or part that can transfer, either directly or indirectly or in any other suitable form several kinds or forms of energy, especially thermal-energy and the energy of a phase-change, from one medium to another, and can also facilitate and enable either condensation, or evaporation of compounds.

[0064] The embodiments disclosed herein can be shown and be explained in the form of flowcharts, especially such flowcharts, which follow with their layout and symbols ISO 10628 (the international standard for such kind of flowcharts).

[0065] The complete process of embodiments hereof can be seen as the combination of three sub-processes, each sub-process with specific different tasks and specific features, and all three sub-processes connected directly and indirectly to each other enabling the complete process z.e., the sub-processes can be directly connected one to the other without requiring connecting lines / pipes.

[0066] Figure 1 shows this complete process in its simplest, thus most basic and minimal form.

[0067] There are many other ways, how the complete process and the sub-processes could be graphically displayed. In Figure 1 the sub-processes are arranged in a concentric way, in order to allow easy understanding and following.

[0068] The three sub-processes can be distinct easily by following the paths of the subprocess, which are shown as arrows (with several millimeters of width) marked mostly with sequential numbers. (Some numbers are missing in the basic applications - these numbers are then used in certain applications for additional features.)

[0069] The sub-process that is shown in Figure 1 as the innermost sub-process is marked with the sequential numbers 01 to 04. This sub-process is referred to hereinafter as the “Energy-Supply-Stream”. The sub-process that is shown in Figure 1 as the outermost sub-process is marked with the sequential numbers 11 to 16. This sub-process is referred to hereinafter as the “Work-Stream”.

[0070] The sub-process that is shown in Figure 1 between the other two sub-processes is marked with the sequential numbers 21 to 25. This sub-process is referred to hereinafter as the “Cooling-Stream”.

[0071] The sub-process ‘Cooling-Stream’

[0072] The sub-process ‘Cooling-Stream’ resembles the central part of a conventional vapour-compression-cooling-process. Figure 2 shows for comparison a conventional vapour-compression cooling-process on the left side and the sub-process ‘Cooling- Stream’ with the other streams just as silhouettes in white, on the right side.

[0073] The obvious main difference between both processes, the conventional vapour- compression-cooling-process and the sub-process ‘Cooling-Stream’, as can be seen in the flowcharts in Figure 2, is the additional heat-exchanger F in the sub-process ‘Cooling- Stream’ - a black arrow is pointing to this additional heat-exchanger. Between both processes, there are additionally more differences in their functions, as will be explained further below.

[0074] In a conventional vapour-compression cooling-process, the medium that needs to be cooled enters heat-exchanger B - in the left flowchart in Figure 2 as stream 01 from the right - and transfers energy in heat-exchanger B into the medium of the vapour-compression-cooling-process, thus raising the temperature of the medium of the cooling process. Stream 22 of the conventional vapour-compression-cooling-process has therefore a higher temperature, than stream 26 of the conventional vapourcompression cooling-process. Stream 26 has in the flowchart in Figure 2 - as usual in a conventional vapour-compression-cooling-process - the lowest temperature in that process.

[0075] Compressor G, following heat-exchanger B, has in a conventional vapourcompression cooling-process the task to increase the temperature of the used cooling medium so the energy, which has been received at heat-exchanger B can be dissipated at heat-exchanger D at a higher temperature-level. In most cases the energy at a higher temperature-level is dissipated with heat-exchanger D into the surrounding, ambient air, or a body of water, etc. In a conventional vapour-compression cooling-process it is the compressor, independent of the kind of compressor, which is used to increase the temperature and or the pressure of the gaseous and or supercritical compounds of the compressed medium, which consumes nearly all of the required energy for the cooling-process to perform. The energy consumption of this compressor is therefore usually kept as low as possible to fulfil this task!

[0076] In the complete process of embodiments hereof, the sub-process ‘Cooling- Stream’ - in Figure 2 on the right side - is used for three main purposes: the first of the three main purposes is to cool the used medium of the subprocess ‘Cooling Stream’ and create thus for the complete-process an artificial heatsink, located directly after the expansion valve E, where the Joule-Thompson-effect leads to a reduction in temperature, similar to the expansion valve E in a conventional vapour-compression-cooling-process; this artificial heat-sink is also referred to as coldreservoir; the second of the three main purposes is to extract energy from an external medium, realised with heat-exchanger B, where energy is extracted from the ‘Energy- Supply- Stream’; the third main purpose is to transfer the energy:

[0077] • at heat-exchanger B from the ‘Energy -Supply -Stream’ 01, used as energy source of the system,

[0078] • together with extracted and captured energy from heat-exchanger F, which is at least a large part of the condensation-enthalpy (energy of the condensation) of the ‘Work-Stream’ after expander H, and

[0079] • the introduced energy from, or through compressor G, whereby all energy being transferred then through heat-exchanger D - right after compressor G - into the ‘Work-Stream’;

[0080] By adding the additional heat-exchanger F into the sub-process ‘Cooling- Stream’ the otherwise lost energy of the condensation-enthalpy of the condensation of the medium of the sub-process ‘Work-Stream’ is, at least to a great part, saved and kept inside the complete-process. This additionally transferred energy needs also to be transformed to a higher temperature-level by the compressor G in the sub-process ‘Cooling- Stream’

[0081] The medium of the sub-process ‘Cooling-Stream’ also extracts and thus receives with heat-exchanger B at least a large part of the external energy for the complete-process into the sub-process ‘Cooling-Stream’ - instead, for example, of introducing the external energy exclusively into the sub-process ‘Work- Stream’.

[0082] Compressor G of the sub-process ‘Cooling- Stream’ requires thus with two sources of transferred energy - at heat-exchangers B and F - significantly more energy to increase the temperature-level of the medium used in the sub-process ‘Cooling- Stream’, - from stream 22 to stream 23 - as the compressor in a conventional vapourcompression cooling-process would need for increasing the temperature of just one single source of energy at heat exchanger B. This specific constellation of the present disclosure runs contrary to usual attempts to keep the energy-consumption of the compressor in a conventional vapour-compression cooling-process as low as possible.

[0083] By adding the additional heat-exchanger F into the sub-process ‘Cooling- Stream’ before heat-exchanger B, which receives the energy from the sub-process ‘Energy-Supply-Stream’, the external -energy from the sub-process ‘Energy-Supply- Stream’ is not transferred into the sub-process ‘Cooling- Stream’ at the lowest temperature of the medium of the sub-process ‘Cooling- Stream’. Only after some increase of the temperature of the medium of the sub-process ‘Cooling- Stream’ occurs at heat-exchanger F, the energy is transferred at heat-exchanger B.

[0084] To transfer the energy into the already at least partly heated medium of the sub- process ‘Cooling- Stream’ after heat-exchanger F, requires, at least in most cases, an additional second compressor or pump A in the sub-process ‘Energy-Supply-Stream’ which in turn further increases the energy consumption of the complete system and also of the sub-process ‘Cooling- Stream’, because the medium from the sub-process ‘Energy-Supply-Stream’ enters heat-exchanger B at a higher temperature level - due to compressor or pump A. Also, this step runs contrary to usual attempts to keep the energy-consumption of the compressor in a conventional vapour-compression-cooling- process as low as possible.

[0085] The sub-process ‘Work-Stream’ is transferring energy at heat-exchanger F to the sub-process ‘Cooling-Stream’. Heat-exchanger F is situated in the sub-process ‘Cooling- Stream’ following, thus right after, the expansion valve E, where the Joule- Thompson-effect happens. As the lowest temperature in the sub-process ‘Cooling- Stream’ and the lowest temperature in the complete process are reached at the expansion valve E with the Joule-Thompson-effect, the temperature of the medium of the sub-process ‘Work-Stream’ after the Heat-exchanger F is thus also the lowest temperature of this sub-process ‘Work- Stream’.

[0086] This is an important detail, because it leads then, at heat-exchanger D, to a higher temperature-difference in the medium of the sub-process ‘Work-Stream’ what in turn is one of several points, which are essential for embodiments hereof.

[0087] With compressor G the medium in the sub-process ‘Cooling- Stream’ is compressed and as a consequence the pressure and also the temperature of the medium increase.

[0088] While in a flowchart it looks for the new process the same, as in a conventional vapour-compression cooling-process, the higher temperature of the medium in the subprocess ‘Cooling- Stream’ entering compressor G, caused by two times introducing energy into the medium of the sub-process ‘Cooling- Stream’ - at heat-exchanger F and at heat-exchanger B - causes a significant difference: when the medium is compressed it will reach with the same compression-ratio and the same input of energy at the driveshaft of the compressor, a different, higher temperature-level, than in the conventional vapour-compression cooling-process - due to the higher temperature at the beginning of the compression. This has then substantial consequences on the energy -transfer at heatexchanger D. These substantial consequences are explained with more details further below.

[0089] After compressor G, the now compressed medium - in most cases a refrigerant - of the sub-process ‘Cooling- Stream’ is passing through another heat-exchanger, D, which is similar in conventional vapour-compression-cooling-process. In a conventional vapour-compression-cooling-process the heat-exchanger following the compressor is commonly referred to as “condenser”. In the flowcharts in Figure 1 and Figure 2 this heat-exchanger is referred to as D.

[0090] In the process of the present disclosure the transferred energy at heat-exchanger D is significantly higher, or more, than at heat-exchanger D of a conventional vapour- compression-cooling-process with the same masses and same pressure-range (e.g., by a factor of about 2, as explained in the examples below) of the 'Work- Stream'. This higher or more transferred energy is due to lower temperature of the medium of the subprocess ‘Work- Stream’, entering heat-exchanger D from the other side (coming from pump I as stream 11) and also due to the higher temperature reached at compressor G, thus increasing the reachable temperature-difference at heat-exchanger D. In a conventional vapour-compression cooling-process the cooling counterstream to the medium or refrigerant in heat-exchanger D is in most cases ambient air with ambient temperature, thus offering only a relatively small temperature-difference, compared to heat-exchanger D in the process of embodiments hereof.

[0091] After passing through heat-exchanger D, both, the refrigerant of a conventional vapour-compression cooling-process, as well of the sub-process ‘Cooling- Stream’, are each passing the expansion valve E, also referred to as reduction valve or throttle. There at E, due to an increase of the cross-section of the duct, thus an increase of the volume and a reduction of the pressure, the temperature of the refrigerant drops, is significantly reduced - referred commonly to as the Joule-Thomson-effect.

[0092] In the sub-process ‘Cooling- Stream’ of embodiments hereof, the higher pressure at compressor G, compared to the pressure-range of the conventional vapourcompression cooling-process (e.g., GB 2064 Charles Williams Siemens 1857), together with the lower temperature-range of the cooling counter-stream medium of the “work- Stream” at the entrance of heat-exchanger D, leads in the sub-process ‘Cooling-Stream’, among other effects, to a significant lower temperature-range before reaching the expansion-valve E, than in a conventional vapour-compression-cooling-process. Consequently the temperature-range of the medium of the sub-process ‘Cooling- Stream’ reaches a significantly lower temperature-range after the reduction-valve E, than the reached temperature-range of the medium of a conventional vapour- compression-cooling-process at the same point, at the exit of E.

[0093] With the lower temperature-range, than in a conventional vapour-compression cooling-process, the medium of the sub-process ‘Cooling- Stream’ reaches heatexchanger F.

[0094] Due to the low temperature the medium of the sub-process ‘Work-Stream’ coming from expander H condenses at least partially. This follows in principle patent GB 913 A (from James Watt from 1763 about the external condenser). At heatexchanger F at least a large part of the energy of the condensation of the medium of the sub-process ‘Work-Stream’ together with some thermal-energy is transferred from the medium of the sub-process ‘Work-Stream’ to the medium of the sub-process ‘Cooling-

[0095] Stream’.

[0096] From here the sub-process ‘Cooling-Stream’ is then repeating. Due to the higher temperature-range and higher pressure-range in the subprocess ‘Cooling- Stream’, compared to a conventional vapour-compression-cooling- process, the mass of the used medium in the sub-process ‘Cooling- Stream’ can be kept smaller, than in a conventional vapour-compression cooling-process, while at the same time the temperature-range and thus the energy transferred at heat-exchanger D increases.

[0097] The sub-process ‘Work-Stream’

[0098] The sub-process ‘Work-Stream’ resembles the central part of a conventional ‘Rankine-cycle’.

[0099] Figure 3 shows for comparison a conventional ‘Rankine-cycle’ on the left side and the sub-process ‘Work-Stream’ on the right side, with the other streams just as silhouettes, in white.

[0100] Similar to a Rankine-cycle the task of the sub-process ‘Work-Stream’ is to convert thermal-energy entering the sub-process ‘Work-Stream’ at heat-exchanger D into mechanical-energy with an ‘expander’ also referred to a “heat-machine”, shown in Figure 3 as expander H.

[0101] A Rankine-cycle receives thermal -energy at heat-exchanger D - heat-exchanger D usually functioning as a boiler-system. Different to the Rankine-cycle, in the present disclosure the sub-process ‘Work-Stream’ receives through heat-exchanger D thermalenergy from the sub-process ‘Cooling-Stream’ - which is not directly external-energy, but indirectly, as the external -energy passes first through the sub-process ‘Cooling- Stream’.

[0102] While both systems, the Rankine-Cycle and the sub-process ‘Work-Stream’ look very similar, there are some important differences, especially in their functions, which are explained further below.

[0103] What can also in Figure 3 is some sort of buffer, buffer-tank or reservoir R, used in some embodiments for the at least mostly condensed medium of the sub-process ‘Work-Stream’ as it is usually used before a pump (at the right side in the bottom corner).

[0104] The sub-process ‘Energy-Supply-Stream’

[0105] In Figure 4 the third sub-process ‘Energy- Supply- Stream’ is shown, with the other sub-processes just as silhouettes, in white. The main task of the sub-process ‘Energy-Supply-Stream’ is to provide the complete process with energy from outside. All energy that the complete process requires and receives enters through this sub-process ‘Energy-Supply-Stream’.

[0106] By delivering energy to the complete process, the temperature of the medium of the sub-process ‘energy-Supply-Stream’ is lowered, thus the medium is cooled and then at the end of the sub-process ‘Energy-Supply-Stream’ released at a lower temperaturerange, than at the entrance to the sub-process ‘Energy-Transfer- Stream’. This can be seen as cooling.

[0107] The medium enters the sub-process ‘Energy-Supply-Stream’ before compressor or pump A - this can be seen in Figure 4. Compressor or pump A receives or in some cases sucks in the medium of the sub-process ‘Energy-Supply-Stream - in Figure 4 this would be from the left side - and either pumps, moves, or releases the compressed medium of the sub-process ‘Energy-Supply-Stream’ to heat-exchanger B. The temperature-range and pressure-range of the pumped or compressed medium of the subprocess ‘Energy- Supply- Stream’ increases due to the compression or pumping (A), and the medium of the sub-process energy supply stream then enters in this state the heatexchanger B. At or in heat-exchanger B, the medium of the sub-process ‘Energy- Supply- Stream’ is transferring energy into the significantly colder medium of the subprocess ’Cooling- Stream’. This transferred energy is not limited to thermal-energy, but can also be energy of the phase-change from the gaseous state of aggregate to the liquid state of aggregate, for example if moisture is in the otherwise gaseous medium of the sub-process ‘Energy-Supply-Stream’, which would either partly or completely condense due to the lowered temperature, thus lowered dew-point, at the exit of heat-exchanger B.

[0108] The medium of the sub -process ‘Energy-Transfer- Stream’ is after heatexchanger B at its coldest temperature-range and is then either released or circulated. If the medium used was ambient air or a hot exhaust-stream, the medium would be released. If the medium is used for indirect heat-transfer, for example from a coolingliquid of a different exothermic process, then it might be useful to circulate the medium. For the complete process there is no difference, whether the medium of the sub-process ‘Energy-Supply-Stream’ is circulated, thus reused, or continuously or intermittently replaced. Depending on what kind of medium is used for the sub -process ‘Energy- Transfer- Stream’, other possible process-steps might be useful or required before the medium is entering compressor A. Those other possible process-steps, like an air-filter, an absorber or similar, could lead to additional drag, gas-friction, or other energyconsuming effects, which could also be balanced or covered by compressor A. Otherwise those other possible process steps would make no difference to the subprocess ‘Energy-Transfer-Stream’ and thus to the complete process, other than eventually increase the energy-consumption of compressor A.

[0109] Depending on what kind of medium is used for the sub -process ‘Energy- Transfer- Stream’, other possible process-steps might be useful or required after the medium is leaving heat-exchanger B. In case that a condensation of parts of the used medium occurs, a step allowing the separation of the different phases, or states of aggregate, would be or might be useful. If for example steam is part of the medium used in the sub-process ‘Energy-Transfer-Stream’ then an additional step separating the condensed water - after the temperature has been lowered at heat-exchanger B - from the other remaining parts of the used medium might be useful.

[0110] Those other possible process-steps might require a specific pressure drop, which in turn needs to be enabled by a specific increase of the pressure. This can also be done and facilitated at compressor A. The energy for this additional task of compressor A has to be provided to compressor A by the complete process through the expander H. Otherwise those other possible process steps make no difference to the sub-process ‘Energy-Transfer-Stream’ and thus the complete process, other than eventually increase the energy-consumption of compressor A.

[0111] Figure 5 shows nearly the same process shown in Figure 4, with the differences of an additional filter T before compressor A and an additional separator S after heatexchanger B - also all Streams are shown in grey colour - not just as silhouettes in white. This process of Figure 5 is then also the first of the six example-applications, shown and explained further below.

[0112] The Complete Process

[0113] The complete process consists of the three sub-processes, which were already described in the previous chapters.

[0114] The connections between these three sub-processes are heat-exchangers and the common drive-shaft, which is mechanically connecting the expander H, the two compressors A and G, and the pump I. These connections between the three subprocesses are used to transfer different kinds of mechanical energy between the different sub-processes. This connectivity can be further used to transfer mechanical energy between the different sub-processes and an electrical generator 90, which can be used to start-up the system and or generate electricity from surplus energy.

[0115] By transferring different forms of energy in a certain specific way between the sub-processes and compressing and expanding the streams in a particular sequence, the complete process is enabled.

[0116] Different and Novel Entry-Point of Thermal Energy

[0117] One of the most important points or aspects, if not the most crucial point or aspect, is the introduction of the external-energy of the process into the sub-process ‘Cooling- Stream’ before compressor G.

[0118] By introducing the external -energy into the sub-process ‘Cooling-Stream’ specifically before the compressor G, this introduced, thus added external -energy is then in turn also introduced at heat-exchanger D into the sub-process ‘Work-Stream’ at a higher, elevated temperature-level, higher, than the external-energy had at the beginning.

[0119] The compression at G leads to an increase of temperature of the compressed medium - thus also to an increase of the temperature-range of the part of the energy, which originates from the introduced external energy.

[0120] In turn, this higher temperature-range or -level enables to transfer the energy from the medium of the sub-process ‘Cooling- Stream’ at heat-exchanger D into the subprocess ‘Work-Stream’ with a lower required mass of the sub-process ‘Work- Stream’. If the temperature of the medium of the sub-process ‘Cooling-Stream’ is lower, then according to the laws of physics, the mass of the medium of the sub-process ‘Work- Stream’ has to be higher to receive and absorb the exact same amount of thermalenergy.)

[0121] The following example illustrates this: if the energy of lOOkJ (a number randomly chosen just for this specific and non-limiting example) needs to be transferred at a heat-exchanger, then the formula that describes (among others) the relation between the mass and the temperature difference is:

[0122] E = m • AT • Cp where E stands for the energy (in kJ), m stands for the mass (in kg), Cpstands for the specific heat capacity (in kJ / kg K), AT stands for the temperature difference (in °C or K) at the entrance and the exit of the heat-exchanger, in our example, heat-exchanger D

[0123] - in either degrees Centigrade or Kelvin, as both provide the same value for AT, thus they are here interchangeable. The specific heat capacity Cpis a pressure and temperature depending specific property of the chosen medium, with which the energy is transferred. In this example we take 2kJ / kgK, which is an even number and close to the real value of most conventional refrigerants, which could be the medium of the subprocess ‘Cooling- Stream’.

[0124] If the energy is given - in this specific and non-limiting example we chose lOOkJ as the energy to be transferred from and out of the sub-process ‘Cooling- Stream’

[0125] - then the temperature difference determines the necessary mass required to transfer the specific amount of energy. If the temperature-difference were 50°C (this equals a AT of 50K), then the mass needs to be 1kg - inserted into the formula: lOOkJ = 1kg • 50K • 2kJ / kgK

[0126] If the temperature-difference is 100°C (this equals a AT of 100K), then the mass needs only to be 0.5kg - inserted into the formula: lOOkJ = 0.5kg • 100K • 2kJ / kgK

[0127] The lower mass of the medium of the sub-process ‘Work- Stream’, receiving the energy from heat-exchanger D, leads consequently to a lower amount of the energy required for the phase-change from liquid state of aggregate to the gaseous state of aggregate of the medium of the sub-process ‘Work- Stream’- this change of the state of aggregate from a liquid state to a at least partially gaseous state of aggregate is a (absolutely) necessary precondition to generate - with the expansion of the gaseous part of the medium - mechanical energy in form of physical work inside the expander H.

[0128] The medium of the sub-process ‘Work-Stream’ is at least to a large part condensed at heat-exchanger F and pumped, thus pressurized by pump I, following heat-exchanger F, as a liquid or at least to a large part as a liquid. This at least to a large part pressurized liquid is the medium of the sub-process ‘Work- Stream’, and receives thus thermal-energy as a liquid and not as a gas at heat-exchanger D from the medium of the sub-process ‘Cooling- Stream’. In order to generate mechanical energy at expander H, the medium of the subprocess ‘Work-Stream’ needs to be in a gaseous state, or at least a large part of the medium has to be in a gaseous state of aggregate. When the gas or the gaseous part of the medium expands inside expander H, then this expansion is converted into mechanical-energy, thus enabling the expander e.g., to move or turn a drive shaft. (According to the laws of physics, only a gas can expand!). Because the medium of the sub-process ‘Work-Stream’ is at least to a large part in a liquid state before reaching heat-exchanger D and needs to be at least to a large part in a gaseous state in expander H, it is necessary to evaporate at least a large part of the medium.

[0129] The energy for this necessary evaporation of at least a large part of the medium of the sub-process ‘Work-stream’ is supplied to the medium of the sub-process ‘Work- Stream’ at heat-exchanger D. After a part of the energy, which has been transferred from the sub-process ‘Cooling-Stream’ to the sub-process ‘Work-Stream’ at heatexchanger D, has been used to evaporate at least a large part of the medium of the subprocess ‘Work- Stream’, this energy is then not any more available as thermal -energy to generate mechanical-energy in expander H as it has been used for the change of the state of aggregate from a liquid to a gaseous state.

[0130] In the example above lOOkJ of energy are provided to the medium of the subprocess ‘Work-Stream’ at heat-exchanger D.

[0131] If for the evaporation of the used medium of the sub-process 87kJ / kg were necessary at the given pressure and temperature range at heat-exchanger D, then the remaining energy from the lOOkJ can be calculated by using the above equation e.g., in case the mass of the medium is 1kg:

[0132] 87kJ / kg • 1kg = 87kJ for the evaporation 87kJ of the available energy is used for the evaporation the remaining energy from the lOOkJ, which is available for expansion is 13kJ; and in case the mass of the medium is 0.5kg:

[0133] 87kJ / kg • 0.5kg = 43.5kJ for the evaporation 43.5kJ of the available energy is used for the evaporation the remaining energy from the lOOkJ, which is available for expansion is 56,5kJ. This lower mass and consequently the lower amount of energy required for the change of the state of aggregate in turn leaves thus a larger part of the available energy - after the evaporation as thermal energy, which can then be transformed in expander H into mechanical energy. By elevating the temperature of the received external -energy - first with compressor A and second with compressor G - the necessary mass of the medium of the sub-process ‘Work-Stream’ can be kept and is kept (indirectly) smaller.

[0134] As the energy for the phase-change - the evaporation enthalpy - at expander H is depending directly on the used mass of the sub-process ‘Work- Stream’, and as the energy for the phase-change of the medium of the sub-process ‘Work-Stream’ is the largest amount of energy in such a process - as it is also the case with every Rankine- cycle - this is a decisive point of the complete process.

[0135] Additional Positive Effect on Mechanical Losses

[0136] This effect of the lower mass, as a consequence of the different point and thus also temperature of introduction of the external energy in this new cooling-and-energy- conversion-process, has also another important consequence: the mechanical losses of the used expander H are relative to the mass, which is processed in the expander, thus reducing the mass of the medium of the sub-process ‘Work-Stream’ also reduces the mechanical losses of the used expander.

[0137] Keeping at least a large part of the Energy of the Condensation inside the Process

[0138] Furthermore, an important point or aspect is about: keeping at least a large part of the energy used for the evaporation of at least a large part of the medium of the sub-process ‘Work-Stream’ inside the process. The medium of the sub-process ‘Work-Stream’ is at least to a large part condensed at heat-exchanger F and pumped, thus pressurized by pump I, following heat-exchanger F, as a liquid or at least to a large part as a liquid. This pressurized liquid is thus at least to a large part the medium of the sub-process ‘Work- Stream’, and receives thus thermalenergy at heat-exchanger D from the medium of the sub-process ‘Cooling- Stream’.

[0139] In order to generate mechanical energy at expander H, the medium of the subprocess ‘Work-Stream’ needs to be in expander H in a gaseous state or at least a large part of the medium has to be in a gaseous state of aggregate. When the gas or the gaseous part of the medium expands inside expander H, then this expansion is converted into mechanical -energy, thus enabling the expander e.g. to move or turn a drive shaft. (According to the laws of physics, only a gas can expand!) Because the medium of the sub-process ‘Work-Stream’ is at least to a large part in a liquid state before reaching heat-exchanger D and needs to be at least to a large part in a gaseous state in expander H, it is necessary to evaporate at least this large liquid part of the medium.

[0140] The energy for this necessary evaporation of at least a large part of the medium of the sub-process ‘Work-stream’ is supplied to the medium of the sub-process ‘Work- Stream’ at heat-exchanger D.

[0141] After a part of the energy, which has been transferred from the sub-process ‘Cooling- Stream’ to the sub-process ‘Work-Stream’ at heat-exchanger D, has been used to evaporate at least a large part of the medium of the sub-process ‘Work- Stream’, this energy is then not any more available as thermal-energy to generate mechanical-energy in expander H as it has been used for the change of the state of aggregate from a liquid to a gaseous state.

[0142] As it is usual in all Rankine-Cycles, the energy for the evaporation of the liquid medium, as part of the energy introduced at heat-exchanger D (usually configured as a boiler), is the largest part of the energy. Or in other words: the part of the thermal energy that can be converted with an expander (e.g., turbine) or expander H, is always significantly smaller, than the part of the energy necessary for the phase-change. Even in a Rankine-cycle using a steam-turbine and steam with over 600 degrees Centigrade this part of the energy used for the phase change from water to overheated steam is around 60 per cent of the primary energy entering the Rankine-cycle, and only 40 per cent of this primary energy is available as thermal energy, which can be used to generate mechanical energy in the expander (e.g., turbine). Usually the energy of the phase-change is lost in a Rankine-cycle (and dissipated with the condenser into the environment).

[0143] As the energy of the phase-change is not thermal-energy, this energy of the phase-change can generally not be used for an expander, and particularly not in this cooling-and-energy-conversion-process at expander H, to generate mechanical energy. However, instead of being dissipated at a condenser, this energy of the phase-change is transferred at least to a significantly large part in heat-exchanger F, which is used as an external-condenser, and then used to increase the temperature-level of the medium of the sub-process ‘Cooling- Stream’. By condensing at least a large part of the gaseous part of the medium of the subprocess ‘Cooling- Stream’ after the expander H, entering heat-exchanger F, the energy that is freed with the condensation, is transferred to the medium of the sub-process ‘Cooling- Stream’ and thus kept inside the complete-process, and thus the system does not lose this energy or at least can keep a large part of this recovered energy of the condensation.

[0144] Using an Artificial heat-Sink

[0145] What is of course also an important point or aspect of this new process is the artificial heat-sink in this process (at the expansion valve E) as it allows the process to function independently from outside temperatures. A process that uses the ambient air or an ambient water, just as two examples, as the heat-sink or the cold reservoir for the used process, has to increase the temperature of the warmest or hottest point in such a specific process according to the ambient temperature, in order to generate a useful temperature-difference that would then in turn allow for a reasonable efficiency of such a process. In contrast: using an artificial heat-sink (at E), eliminates the need to determine the temperature-difference as part of the process, such that any thermalenergy above the temperature-range of the artificial heat-sink will be able to generate mechanical energy.

[0146] High Adjustability of this New Process

[0147] This new process of embodiments hereof is highly adjustable.

[0148] With the compressor for the sub-process ‘Energy-Supply-Stream’ - shown as compressor or pump A in the different Figures - it is possible to adjust the temperature, with which the medium of the sub-process ‘Energy-Supply-Stream’ enters the heatexchanger of the sub-process ‘Cooling- Stream’ - shown in the different Figures as heatexchanger B. Thus, it is possible to transfer an optimal amount of energy from the subprocess ‘Energy- Supply- Stream’ into the sub-process ‘Cooling-Stream’ by adjusting the performance of compressor or pump A.

[0149] With the compressor for the sub-process ‘Energy-Supply-Stream’ - shown as compressor or pump A in the different Figures - it is possible to adjust the pressure of the medium of the sub-process ‘Energy-Supply-Stream’ so that additional steps can be added to the sub-process ‘Energy-Supply-Stream’, either before or after the compressor or pump - shown as compressor or pump A in the different Figures. For example: a filter, an additional expansion-valve at the end, after heat- exchanger B, for a separation of compounds, like moisture in air, or nitrogen-dioxide, or carbon-dioxide in exhauststreams and or similar units can be embedded to regulate the ‘Energy-Supply-Stream’.

[0150] With the compressor in the sub -process ‘Cooling- Stream’ - shown in the different Figures as compressor G - it is possible to adjust the pressure and temperature, with which the medium of the sub-process ‘Cooling- Stream’ enters the heat-exchanger, where the energy from the sub-process ‘Cooling-Stream’ is transferred to the medium of the sub-process ‘Work-Stream’ - shown in the different Figures as heat-exchanger D. Thus it is possible to adjust the amount or mass of the medium of the sub-process ‘Work- Stream’ accordingly by increasing or decreasing the temperature-difference at heat-exchanger D, following the compressor G of the sub-process ‘Cooling-Stream’.

[0151] With the compressor in the sub -process ‘Cooling- Stream’ - shown in the different Figures as compressor G - it is possible to adjust the pressure, with which the medium of the sub-process ‘Cooling- Stream’ passes through the following heatexchanger - shown in the different Figures a D - and reaches the expansion-valve E, where the chosen pressure has an influence on the possible and reached temperaturedrop at the expansion-valve E in the sub-process ‘Work- Stream’, thus influencing and or adjusting the temperature that can be reached after the expansion-valve - shown in the different Figures as expansion-vale E.

[0152] With the pump in the sub-process ‘Work-Stream’ - shown in the different Figures as pump I - it is possible to adjust the pressure of the medium of the subprocess ‘Work-Stream’ (stream 15) thus allowing to adjust the evaporation-temperature of the medium of the sub-process ‘Work- Stream’. With the right pressure a supercritical or trans-critical state of the medium of the sub-process ‘Work-Stream’ can be reached, and or a lower pressure for a different thermodynamic performance of the expander.

[0153] It is also possible to use the process not just as a process with one single step, but in several sequential steps as will be described further below. Accordingly, in possible embodiments the medium of the sub-process ‘Energy-Supply-Stream’ pass through a number of units of the processes in steps. Each step would lead to further cooling and thus lower temperatures of the medium of the sub-process ‘Energy- Supply- Stream’.

[0154] Adding other functional Devices or Systems It is also possible to add additional functional devices to the cooling-and-energy- conversion-process without changing the basic intended function of the cooling-and- energy-conversion-process of the disclosed embodiments.

[0155] Here are some examples for such functional devices:

[0156] As an example, it is possible to add additional heat-exchangers in the process, especially in the sub-process ‘Cooling-Stream’ additional heat-exchangers could be inserted, which further cool the medium of the sub-process ‘Cooling-Stream’ before the expansion-valve E, to reach thus a lower temperature at the exit of expansi on-valve E. This additional heat-exchanger could be from a different process or a different processstep, as for example described further below in the sixth example application, where a very cold stream at the end of a number of sequential cooling-steps, realized with a number of sequential processes of the present disclosure, leads to a very low temperature (minus 70 to minus 80 degrees Centigrade in that example further below) and is then used to cool previous processes and process-steps. This is similar to the basic ideas of patent publication No. DE 88824 (Carl Linde from 1895), where at the end of the cooling-process at least a part of the then very cold medium (for example after a separation of compounds) is used to enhance the cooling-steps, which are located sequentially before the step, where the cooling-process reaches the lowest temperature, by leading the very cold medium backwards as a counter- stream in one heat-exchanger, or sequentially several heat-exchangers, in several process-steps, against the medium in locations in the process where this medium is still less cold.

[0157] In case the temperature of the medium of the sub-process ‘Energy- Supply- Stream’ before the compressor or pump in the sub-process ‘Energy-Supply-Stream’ - in the different Figures shown as compressor A - is sufficiently above the temperature of the medium of the sub-process ‘Work-Stream’ before the expander H in sub-process ‘Work-Stream’ - shown in the different Figures as expander H - an additional heatexchanger could be added. A part of the thermal energy of the medium of the subprocess ‘Energy- Supply- Stream’, which has to be above the temperature-range of the medium of the sub-process ‘Work-Stream’ at this point, could be transferred to the medium of the sub-process ‘Work-Stream’ and increase the yield of the following expander - shown in the different Figures as expander H. This is described further below in the second example application. Adding an additional expansion-valve, in the sub-process ‘Energy- Supply- Stream, after the medium of the sub-process ‘Energy-Supply-Stream’ leaves the heatexchanger - shown in the Figures as heat-exchanger B - would allow an additional function of separating compounds. If the medium of the sub-process ‘Energy-Supply- Stream’ contains different compounds, for example gases with different condensationtemperatures or dew-points, then this additional expansion-valve would lead to a further drop of the temperature of the medium of the sub-process ‘Energy-Supply-Stream’ and certain specific components would condense or deposit at this additional expansionvalve, while other components would remain in a gaseous state. The pressure drop can be adjusted with the compressor or pump in the sub-process ‘Energy-Supply-Stream’ - this compressor is shown in the different Figures as compressor A.

[0158] Further below the sixth example application of the cooling-and-energy- conversion-process of this disclosure describes a cooling-process that separates in three consecutive processes as cooling-steps, first water, then in the second cooling-step compounds like nitrogen-dioxide and compounds with a condensation-temperature in the same temperature range, and in the third cooling-step carbon-dioxide. Usual devices can then be added, like centrifuges or a simple spray -tower for the carbon-dioxide, following the streams of separated compounds, while the not separated, remaining compounds in the first two cooling-steps continue each to the next cooling-step.

[0159] It is also possible to use instead of one compressor, or one pump, or one heatexchanger in the different sub-processes, as it has been described above, several expanders, and or compressors, and or pumps, and or heat-exchangers, even with intercoolers between the compressors and or compressor- steps. This could be seen as dividing one, or several of the single steps - compressor, expander, pump, heatexchanger, connecting duct - into several sequential and or parallel steps, whereby the separated steps even do not need to be identical.

[0160] In a similar way it is also possible to split the process of the present disclosure or sub-processes thereof into several parts and connect them either straight, or as one cross-over, or several cross-overs, where in a cross-over, a specific stream of a first part would change with the same specific stream of another, second part, and the first part would continue with the medium of the other, second part, while the second part continues with the medium of the first part. There are many possibilities to vary, split and connect parts of this process. Further below, in the sixth example application the cooling-and-energy-conversion- process is split into several parallel processes, which is shown in Figure 12.

[0161] These resulting possible modified processes would still all be based on the cooling-and-energy-conversion-process of the present disclosure, where the sequence of different transfer of different energies between the sub-processes leads to the results and the number of sequential or parallel or crossing devices or ducts, to realize this process, is of lesser importance.

[0162] Control System

[0163] Systems or devices, used to realize processes can be operated, managed, monitored, surveyed, and controlled today by using indicators, controllers, controllable parts and systems, and programmable logic controllers. The same can be done with the process and all of the different possible embodiments of this disclosure.

[0164] The process of this disclosure can be fitted at least partly with indicators and or control means, like valves, controllable valves, indicators, sensor units, controllers, controllable parts and systems, and programmable logic controllers etc.

[0165] Either single functions, or parts, or sub-systems, up to all parts and functions of the process of this disclosure can be fitted for either single or selected functions, up to the complete system, and also with programmable logical control system (PLC) for at least one function, sub-system, or device.

[0166] Figure 13 shows the adjusted flowchart of the first example application - shown in Figure 5 - with a number of added temperature indicators (usually abbreviated as TIC), pressure indicators (usually abbreviated as PIC), flow indicators (usually abbreviated as FIC), and a control-valve at E, all connected to a central programmable logic controller (PLC).

[0167] For the graphic display in Figure 13 the symbols of ISO 10628 (the international standard for such kind of flowcharts) have been used. As usual in such flow-charts the different indicators and or controllers have an address-number, which is also shown in Figure 13. There are of course many different ways how to control such a process, and this example here shown as just one possible option.

[0168] Figure 14 shows the adjusted flowchart of the forth example application - shown in Figure 8 - with a number of added temperature indicators (usually abbreviated as TIC), pressure indicators (usually abbreviated as PIC), flow indicators (usually abbreviated as FIC), and several control -valves, all connected to a central programmable logic controller (PLC).

[0169] For the graphic display in Figure 14 the symbols of ISO 10628 (the international standard for such kind of flowcharts) have been used. As usual in such flow-charts the different indicators and or controllers have an address-number, which is also shown in Figure 14. There are many different ways how to control such a process, and this example here shows just one possible option.

[0170] Six Possible Basic Embodiments as Examples

[0171] Below are examples that describe six different possible embodiments, realisations, or applications of the cooling-and-energy-conversion-process, also at least partly with such additional steps and or additional features as described above. These examples themselves illustrate some basic ways of using and or utilizing the new cooling-and-energy-conversion-process of the present disclosure and in them, with several possible variations.

[0172] These six example applications only illustrate the wide variety of possible uses. There are more possible combinations of the different sub-process, features, devices, etc., and there are also many more possibilities to use the cooling-and-energy- conversi on-process of the present disclosure, than these six example applications. All the different possibilities and features, which are in these six example applications, can be also used in different ways, can be combined with other features, or in different ways.

[0173] Cooling-and-Energy-Conversion-System used as an Air-Condition-System with Air-Filter and Dust-Absorber

[0174] In this first example application the practical implementation of the cooling-and- energy-conversion-process of the present disclosure is illustrated on basis of a conventional air-condition-system, where the new cooling-and-energy-conversion- process replaces the conventional cooling-process of a vapour-compression-process.

[0175] Figure 5 shows the flowchart of such a cooling-and-energy-conversion-system that cools ambient humid air. The warm and humid ambient air enters the process as Stream 01 through an air- and dust-filter T. The air- and dust-filter T is, are added as non-essential systems to the cooling-and-energy-conversion-process. While in this first example-application the additional air- and dust-filter T is located in flow-direction before the compressor A, it can also be located in flow-direction after compressor A. When this filtered ambient air leaves the process as Stream 04 the cooling-and-energy- conversion-process has reduced the temperature of the air, thus has also removed a large part of the moisture.

[0176] Here is a thermodynamical calculation provided as an example for better understanding:

[0177] If the ambient, outside temperature is 25 (twenty five) degrees Centigrade with 50 per cent relative humidity (this equals about 9.98 gram of water in each kilogram of air), then compressor A would suck in this 25 degrees Centigrade warm, humid air, Stream 01, passing with some friction losses e.g., through the air-filter and dust-filter (T) and compress it sufficiently to a pressure of 0.129MPa (an increase of around 200mbar) to move through the heat-exchanger B - following compressor A - and beyond as Stream 04.

[0178] In this specific and non-limiting example the compressed air reaches then after compressor A, in Stream 03, with the increase of pressure from ambient pressure of 0.101355MP (ambient pressure) to an increased pressure of 0.129MPa at a temperature of 46 degrees Centigrade.

[0179] In heat-exchanger B the slightly compressed and warmer humid air transfers thermal energy and the energy of the condensation of a part of the containing moisture to the medium of the sub-process ‘Cooling-Stream’.

[0180] In this non-limiting example the air, when passing through heat-exchanger B, is cooled down to plus four degrees Centigrade in Stream 04. While the air is cooled, the dew-point of the moisture, contained in the air, is changed and around six gram of water per kilogram of air is condensed at heat-exchanger B.

[0181] From the 25 degrees Centigrade warm air at the beginning, with an usable energy (pressure and temperature - usually referred to as enthalpy) of 323.4kJ / kg before compressor A, and with an usable energy (pressure and temperature - usually referred to as enthalpy) of 288.1kJ / kg after heat-exchanger B the process has extracted 35.3kJ / kg of thermal energy from the air, which are now available for the process of this disclosure.

[0182] From the 50 per cent relative moisture in the 25 degrees Centigrade warm air with 9.98 gram gaseous water per kilo at the entrance, in Stream 01, to 4.31 gram gaseous water per kilogram at the exit, in Stream 04, 5.67 gram of moisture per kilogram of air have been condensed, changed from gas or steam to liquid. This condensation of 5.67 gram of moisture per kilogram of air frees 12.7kJ per kilogram of air, which is then also transferred at heat-exchanger B into the colder medium of the sub-process ‘Cooling-Stream’, (each 1kg of gaseous water, moisture or steam free in this pressure range about 2,245kJ when condensing).

[0183] With the energy of the cooling of air - 35.3kJ / kg - and the energy of the condensation of the moisture - 12.7kJ / kg - the process of this disclosure receives in this example 48kJ per kilogram of air.

[0184] Different temperatures, pressures and moisture contents, than in this nonlimiting example would then also lead to different results.

[0185] The now much dryer and colder air is used for cooling by releasing it (fairly dust-free) into the room or space that needs cooling.

[0186] This sample process can sustain itself already with low temperatures around 20 degrees Centigrade, and adjusted in the right way also below 20 degrees Centigrade. The energy, which can be used to sustain the cooling-and-energy-conversi on-process, is gained from the medium of the sub-process ‘Energy-Supply-Stream’, in this case ambient humid air. How much of energy can be extracted from the medium of the subprocess, depends on the temperature-difference between the incoming stream of air, shown as Stream 01 in Figure 5, and the temperature of the medium of the sub-process ‘Cooling- Stream’ entering heat-exchanger F as Stream 26. The medium of the subprocess ‘Cooling- Stream’ has at the entrance of heat-exchanger F, which follows the expansion valve E, its lowest temperature. This temperature of Stream 26 can be adjusted! This Stream 26 functions also as the artificial heat-sink of the complete cooling-and-energy-conversion-process by adjusting the temperature at heat exchanger F also consequently the temperature at heat exchange B is determined and thus, in turn, the amount of energy that can be extracted from the media of the sub-process energy transfer stream.

[0187] In a conventional air-condition-system based on the vapour-compression- process, the heat sink is the ambient-outside temperature, which cannot be adjusted. In a conventional vapour-compression-cooling-process, as shown in Figure 2 on the left side the compressor G is increasing the temperature of the used medium to a temperature, which is sufficiently above the ambient, outside temperature, so that the removed thermal-energy can be dissipated into the ambient air. The warmer or hotter the ambient, outside air is, the higher needs to be the temperature of the used medium of the conventional cooling-process of a vapour-compression-process after the compressor, in order to enable heat-dissipation. Thus, the compressor of a conventional vapour- compression-cooling-process needs to increase its performance with the increase of the ambient, outside temperature. In the new cooling-and-energy-conversion-process, the increase of the ambient, outside temperature would lead to more extracted thermalenergy from the incoming air at heat-exchanger B and thus would increase the efficiency of the new cooling-and-energy-conversion-process and in turn allow more, or additional generation of mechanical -energy at expander H.

[0188] A conventional vapour-compression-cooling-process transforms the removed thermal-energy into thermal-energy with a higher temperature. The new cooling-and- energy-conversion-process transforms the removed thermal -energy and or eventually the energy of the condensation of the moisture in the air into mechanical-energy at the expander H.

[0189] Condensation of the Spent, Exiting Steam of a Steam-Turbine with a Closed Sub-Process ‘Energy-Supply-Stream’

[0190] In this second example application the practical implementation of the cooling- and-energy-conversion-process of the present disclosure is illustrated on basis of a cooling-and-energy-conversion-system to condense spent, exiting steam from a steamturbine and generate electricity from the energy of the condensation. The spent, exiting steam has in this example at the entrance of the cooling-and-energy-conversion-process, at Stream 01, a temperature-range of 120 degrees Centigrade to 150 degrees Centigrade. Figure 6 shows a flowchart for this cooling-and-energy-conversion-process, with the spent, exiting steam from the turbine entering the cooling-and-energy-conversion- process as Stream 01 from the left side and the cooled, condensed water leaving the cooling-and-energy-conversion-process as Stream 04 towards the left side, going back to the turbine-process. The parts of the process of the steam-turbine are not changed and also not shown in Figure 6.

[0191] Compressor A regulates and controls the stream of the spent steam, leaving the steam-turbine, to ensure that no backwards-disturbances or backlash can occur. The spent steam is condensed at heat-exchanger B as described above. Different to the previous example, the main source of energy for this process is the condensationenthalpy of the steam and only to a rather small amount the thermal-energy of the spent steam. As the condensation of the spent steam can extract large amounts of energy, in form of the condensation-enthalpy of the spent steam, also a large amount of energysurplus can be generated with this process.

[0192] In this second example application of a cooling-and-energy-conversion-system, the cooling and condensation of the steam might be the main objective in order to enable the process of the connected steam-turbine. However, the energy, released by this cooling-and-energy-conversion-process, is able to generate more mechanical energy, than the steam-turbine itself.

[0193] In the first example application above, the sub-process ‘Energy-Supply-Stream’ is an open sub-process, where the air enters at one point and exits at another point. Here in the second example application, the sub-process ‘Energy- Supply- Stream’ is a closed sub-process, even if it is not immediately visible in Figure 6 due to the parts of the steam-turbine-process, which are not shown. Either the spent steam that needs to be condensed is circulating directly in this sub-process, or another substance in contact with the spent steam, is circulating as the medium in this sub-process.

[0194] Also, in this example process the hot medium, either the spent steam or said another substance in contact with the spent steam, is passing through an additional heatexchanger, shown in Figure 6 as heat-exchanger C. At this additional heat-exchanger C only a part of thermal-energy of the steam is transferred, which is the part with a temperature sufficiently above the temperature-range of the medium of the sub-process ‘Work- Stream’ after heat-exchanger D. In this way a part of the thermal -energy of the spent steam is going directly into the sub-process ‘Work- Stream’, thus some mechanical energy for the compressor G of the sub-process ‘Cooling-Stream’ is saved.

[0195] While in this example there is only a single heat-exchanger C transferring some of the energy directly to the sub-process ‘Work-Stream’ there could also be more, than just one such heat-exchanger, either arranged sequentially and or parallel, for transfer of energy.

[0196] It would also be possible, instead of just one single Stream 12 and or 13 of the sub-process ‘Work- Stream’, to split either one or both streams into several parallel streams, which even do not need to be identical, and then add heat-exchangers to at least one partial stream. This would make especially sense, if a steam-turbine power-plant were to be retrofitted and the new cooling-and-energy-conversion-process were connected directly to a number of already existing condensation-units. There are many ways how to vary and modify this specific example process.

[0197] The basic of all those possible variations and modifications would be the same cooling- and-energy-conversion-process.

[0198] Cooling-and-Energy-Conversion-Process with Several External Heat- and Energy- Sources and thus Cooled Systems

[0199] In this third example application the practical implementation of the cooling- and-energy-conversion-process of the present disclosure is illustrated on basis of a cooling-and-energy-conversion-system with several parallel arranged external -energysources in a closed, circulating sub-process ‘Energy-Supply-Stream’.

[0200] Figure 7 shows a flowchart for such an example-process.

[0201] This example could be the cooling-and-energy-conversion-system for a computersystem. Several central-processing-units (CPUs) with integrated liquid-cooling, as they are usual today, additionally a graphic-card, with its own processor(s) and also with integrated liquid-cooling, are arranged in a parallel layout and connected to the subprocess ‘Energy- Supply- Stream’. In Figure 7 the two central processing units are shown with the symbol of heat exchangers in the Streams 05 and 06, the processor(s) of the graphic-card is shown with the symbol of a heat-exchanger in Stream 07.

[0202] This connection, between the used cooling-liquid of the central-processing-units and the medium of the sub-process ‘Energy-Transfer-Stream’, as well for the coolingliquid of the processor(s) of the graphic-card, with and to the medium of the sub-process ‘Energy-Transfer-Stream’, could be easily realized by using and circulating the same cooling-liquid as the medium of the sub-process ‘Energy- Supply- Stream’ and as the cooling medium for the central-processing-units and the processor(s) of the graphiccard. Of course, there are other options for the transfer of thermal -energy from those central-processing-units and or the processor(s) of the graphic card to the medium of the sub-process ‘Energy-Transfer-Stream’, which are known to the person skilled in the arts, and for this cooling-and-energy-conversion-process not from great importance.

[0203] Optionally, a forth heat-exchanger shown in Figure 7 in Stream 08 is receiving thermal-energy from the ambient surrounding of the computer, thus this heat-exchanger would probably best be integrated into one of the outside-walls of the housing of the computer-system. In case of a server-farm, having a great number of computers, there would be a separate circulating medium, supplying those servers with ambient external - energy. In possible embodiments, such as server-farms, where a graphic-card is not necessarily required for each computer, the heat-exchanger in Stream 07 can be removed. Of course, additional such cooling heat-exchangers may be added, according to the number of processors in each computer machine.

[0204] The medium of the sub -process ‘Energy-Transfer- Stream’ is pumped and thus circulated by pump A.

[0205] During the time the computer-system is working and thus the centralprocessing-units and the processor(s) graphic-card are consuming electricity, which is then during their performance turned into thermal-energy, the medium of the subprocess ‘Energy-Transfer-Stream’ is receiving this thermal -energy as external-energy. With expander H the cooling-and-energy-conversion-process can convert this thermalenergy at least partly to mechanical -energy. This mechanical -energy can in turn generate electricity, which can charge a battery-system, like an uninterruptible-powersupply-system providing electricity for the computer-system.

[0206] During the time the computer-system is not working and the central-processingunits and the graphic-card are not generating thermal-energy, the forth source of external-heat, through the heat-exchanger in Stream 08 in the sub-process ‘Energy- Supply- Stream’ can continue to supply external -energy, which in turn is then leading to a continued generation mechanical -energy at expander H, which in turn can be used for the generation of electricity charging the battery-system of the computer-system. In this way the (unavoidable) mechanical-losses and other losses of the cooling-and-energy- conversion-process would be balanced over time with this additional source of externalenergy and thus the computer-system can operate continuously without the need of external electricity.

[0207] The cooling-and-energy-conversion-process has, as described above, its own artificial heat-sink. Thus, the temperatures used for cooling the central -processing-units and the graphic-card can be chosen to be - just as an example - in the range of minus 20 degrees Centigrade. At this low temperature range electronic components require less electricity to function, also their processing speed significantly increases. The cooling- and-energy-conversion-process would thus not only lead to better cooling, saving of electric-energy, but also to a significantly improved performance of the computersystem. Cooling-and-Energy-Conversion-Process with Several Heat-Sources and thus Cooled Systems plus an Additional Energy-Transfer at the Sub-Process ‘Work- Stream’

[0208] In this forth example application the practical implementation of the cooling- and-energy-conversion-process of the present disclosure is illustrated on basis of a cooling-and-energy-conversion-system with several parallel arranged external -energysources in a closed, circulating sub-process ‘Energy-Supply-Stream’, as described in the third example before, plus an additional external -energy-source directly connected to the sub-process ‘Work- Stream’.

[0209] Figure 8 shows a flowchart for such an example-process.

[0210] This forth example application could be the cooling-and-energy-conversion-system for an electric vehicle with electro-motors, a battery with its battery-charging-system, and disc-break-systems on all four wheels. In this example the electro-motors (cooled by streams 05, 06, and 07) and the battery-charging-system are fitted with a cooling-system using a cooling-liquid, which is also the medium of the sub-process ‘Energy-Transfer- Stream’ of the cooling-and-energy-conversion-process.

[0211] Also, as in the previous third example application, an additional heat-exchanger shown in Figure 8 in Stream 08 is connected to ambient air. During the time the electric- vehicle is not operating and the electro-motors and the battery-charging-system are not generating thermal-energy, the additional source of external-heat, through the heat-exchanger in Stream 08 in the sub-process ‘Energy-Supply-Stream’ can continue to supply external-energy, which in turn is then leading to a continued generation of electricity and gradually charging of the battery-system. In this way the (unavoidable) mechanical-losses and other losses of the cooling-and-energy-conversion-process would be balanced over time with this additional source of external -energy and thus the electric- vehicle can operate either continuously, without the need of external electricity, or at least with significantly less need of external charging of the battery.

[0212] Until here the forth example application of a practical implementation of the cooling- and-energy-conversion-process is besides the amounts of energy of the different heatsources quite similar to the previous third example application above.

[0213] Different, than in the previous examples, there is in this forth example an additional source of external -energy directly connected through an additional heatexchanger C to the sub-process ‘Work- Stream’. This additional heat-exchanger C is positioned in the sub-process ‘Work-Stream’ after heat-exchanger D and before the medium of the sub-process ‘Work-Stream’ reaches the expander H. This is similar to the second example above.

[0214] In this forth example application, an additional, secondary energy source is added and connected to the cooling-and-energy-conversion-system. In this forth example application this additional, secondary energy-source is the disc-break-systems of the four wheels, with liquid-cooled break-disks, where the cooling-liquid is in a closed system, which is directly connected to the additional heat-exchanger C in the sub-process ‘Work- Stream’. In Figure 8 this additional closed system with the coolingliquid for the breaks is shown as 30, the four breaks are shown just as heat-exchangers in the additional Streams 31, 32, 33, and 34.

[0215] It is also possible to have of the four breaks being connected each to a separate heat-exchanger in the sub-process ‘Work- Stream’, which could then either be mounted sequentially and or parallel with four parallel Streams of the medium of the sub-process ‘Work-Stream’ between heat-exchanger D and expander H.

[0216] The specific way, in which the external-energy is transferred into the subprocess ‘Work-Stream’ is for the function of the cooling-and-energy-conversion- process not of particular importance and many variations are possible. Important in this specific example is the possibility to have at least one additional extemal-heat-source, which is connected directly to the sub-process ‘Work-Stream’ as described above.

[0217] Energy-Conversion-Process with one External-Energy-Sources plus an Additional Energy-Transfer out at the Sub-Process ‘Cooling-Stream’

[0218] In this fifth example application the practical implementation of the cooling- and-energy-conversion-process of the present disclosure is illustrated on basis of a cooling-and-energy-conversion-system with ambient air, or an ambient water-carrier as the source of external-energy, plus an additional outlet of thermal energy in the subprocess ‘Cooling- Stream’, which is not in the other five example-applications.

[0219] Figure 9 shows a flowchart for such an example-process.

[0220] With the exception of the additional energy-outlet (K) in the sub-process ‘Cooling- Stream’ this fifth example application has the same structure and sub-systems as the first example application shown in Figure 5.

[0221] This fifth example application could be a heat-pump-system. For this fifth example-application the heat-pump-system has the same purpose as commercially available heat-pump-systems for heating houses, living-spaces, etc., which comprise among other parts and subsystems an out-door-unit that receives cold air, or groundwater, or other water-sources, etc. and also a usually fluid medium, which forwards the gained thermal-energy into the space that is supposed to be warmed or heated, referred to hereinafter as ‘Heating -Medium’.

[0222] In the new cooling-and-energy-conversion-process the sub-process ‘Energy- Transfer- Stream’ is connected through Stream 01 to a source of water or air (not shown). This could be ground-water, or just ambient air with e.g., minus 30 degrees Centigrade or any other temperature or a similar source for thermal-energy.

[0223] Because the cooling-and-energy-conversion-process is not depending on an external heat-sink or external cold-reservoir, the lowest temperature in the sub-process ‘Cooling- Stream’, at the expansion-valve E, could be adjusted to be low enough, for example minus 50 degrees Centigrade, to facilitate a sufficiently great temperature difference, to the external heat-source, which in turn would enable this process to be self-sustainable at such low temperatures or even lower temperatures.

[0224] In such a heat-pump-system the desired outcome is usually a warm or hot ‘Heating-Medium’ for heating. In this fifth example application an additional heatexchanger K is placed to this end to receive a ‘Heated-Medium’ in the sub-process ‘Cooling- Stream’ after the compressor G. This could then either be before heatexchanger D or after heat-exchanger D. In the flowchart in Figure 9 this is shown as heat-exchanger K, placed before heat-exchanger D. The ‘Heated-Medium’ in the connected sub-process is entering the process in Figure 9 as stream 41 and leaves as stream 42 receiving a part of the thermal-energy of the sub-process ‘Cooling- Stream’ for heating purposes and the remaining thermal -energy of the sub-process ‘Cooling- Stream’ is transferred at heat-exchanger D to the medium of the sub-process ‘Work- Stream’. In this fifth example application, the amount of energy that the expander H receives is smaller, than it would be in the cooling-and-energy-conversion-process of the first example application, due to the diversion of some of the energy at heatexchanger K. The process in this fifth example application can be adjusted in order to let sufficient energy pass through heat-exchanger D to the sub-process ‘Work-Stream’ to allow expander H to generate enough mechanical -energy to sustain the complete cooling-and-energy-conversion-process. Whether an additional pump or natural convection or any other suitable mean is circulating the ‘Heating-Medium’ in the additional sub-process is for the complete process not of particular importance. Important is to see that in this example the energy extracted from cold air, in this example at minus 30 degrees Centigrade, and then released with much lower temperature, in our example at minus 45 degrees Centigrade, as shown in Figure 9, is sufficient to sustain the cooling-and-energy-conversion- process. To extract a certain amount of thermal -energy at heat-exchanger K before it is converted to mechanical energy, saves energy that would otherwise be lost with, or in the mechanical losses of the mechanical system of the process, the expander, compressor, and pump, as well losses to convert at a later stage the gained surplus energy back from mechanical -energy to thermal-energy for the heating-purpose.

[0225] This example shows the same basic cooling-and-energy-conversion-process, as in the first example, just added with a different second mean to extract energy and in a different temperature-range.

[0226] Energy-Conversion-Process with one External-Energy-Source in three Consecutive Steps plus Additional Cooling at the Sub-Process ‘Cooling- Stream’

[0227] In this sixth example application the practical implementation of the cooling- and-energy-conversion-process of the present disclosure is illustrated on basis of a carbon-capture-system, which is cooling the hot exhaust-gas-stream of a power-station in three consecutive steps, in order to reach the condensation-temperature of carbondioxide, with the hot exhaust-stream of the power-station as the source of externalenergy.

[0228] Different to the previous example applications of the cooling-and-energy-conversion- process, there are in this sixth example-application three of the cooling-and-energy- conversion-process connected consecutively, in a row, in steps. The cooled exhaust-gas stream is cooled successively and at the end the remaining cooled compounds are used to further cool the previous process-steps.

[0229] Also, the complete process for the exhaust gas of a power-station is additionally split into six parallel processes, as will be described below.

[0230] Figure 10 shows a flowchart for only one of the six parallel partial processes as the sixth example application. The other five parallel process-steps would be similar. Figure 10 shows the hot exhaust gas from the power station entering the process as Stream 01. This hot exhaust gas has a temperature in a usual range, assumed in this sixth example application to be in the range of 110 degrees Centigrade to 180 degrees Centigrade. Through the additional (also referred to herein as auxiliary) heat-exchanger Ci in the sub-process ‘Work-Stream’ a part of the thermal -energy is transferred directly to the medium of the sub-process ‘Work- Stream’. This is analogue to the function of the additional heat-exchanger C (in Figure 8) in the second example-application described above.

[0231] In this example-application the additional heat-exchanger Ci in the sub-process ‘Work-Stream’ is only in the first, of the three consecutive process-steps.

[0232] In Figure 10 it can also be seen that after the cooled exhaust-gas leaves heat-exchanger Bi, at the end of the first of the three consecutive steps of the process, an additional expansion-valve with a centrifugal -separator, shown in Figure 10 with the symbol of a centrifugal-separator 56i, facilitates the separation of the condensed water. In the exhaust-gas of a power-station, based on the combustion of fossil-fuel, there is a significant amount of water in form of steam, as a product of the combustion, in the exhaust-gas-stream. The separated water leaves the first of the three consecutive processes as Stream 57.

[0233] The remaining exhaust-gas-stream enters then the second step of the three consecutive partial processes or process-steps. This can be seen in Figure 10 in the middle. In the second step of the three consecutive process-steps after heat-exchanger B2, another additional expansion-valve with a centrifugal-separator 562, shown in Figure 10 with the symbol of a centrifugal -separator, facilitates with a centrifugalseparator the separation of nitrogen-dioxide and other compounds of the exhaust-gas- stream, which have a similar range of the condensation-temperature. These separated compounds leave the second of the three consecutive processes as Stream 58.

[0234] The remaining compounds of the exhaust-gas-stream enter then the third consecutive process-step, where the remaining compounds are further cooled. After heat-exchanger B3 an additional expansion-valve with a centrifugal-separator, shown in Figure 10 with the symbol of a centrifugal-separator, facilitates the separation of either liquid or solid carbon-dioxide from the remaining compounds.

[0235] The separated carbon-dioxide is leaving the process, through a separator 563, as Stream 59. The remaining compounds - after separator 563 - have then the lowest temperature of the complete cooling-and-energy-conversion-process, which would be in the range of minus 70 degrees Centigrade to minus 80 degrees Centigrade. The remaining compounds are mainly nitrogen and oxygen (together with other natural compounds of air).

[0236] These remaining compounds are then passing as Stream 60 through the three additional heat-exchangers L3, L2 and Li. Each of these additional heat-exchangers L3, L2, and Li are situated in each of the three sub-processes ‘Cooling- Stream’ before the respective expansion-valves E3, E2, and Ei, and further cool down the media of the subprocess, before the medium in each of the three steps reaches the respective expansionvalve, E3, E2, and Ei.

[0237] This arrangement of additional heat-exchangers, to use the cool gases at the lowest temperature, in order to further cool down the previous process-steps, is in so far different from the basic idea of DE 88824 (Carl Linde from 1895) as not the gases that need to be cooled - in this sixth example application the exhaust-gases from a power- station - are the counter- stream in the heat-exchangers L3, L2, and Li, but the media used in the sub-processes ‘Cooling-Stream’. By cooling the medium of each of the subprocesses ‘Cooling-Stream’ of the three consecutive process-steps further, thus reaching before the expansion-valves Ei, E2, and E3, a lower temperature, means that less pressure at the compressors Gi, G2, and G3 is required to reach a very low temperature at the respective expansi on-valve, Ei, E2, and E3. Thus, less from the generated mechanical-energy of the expanders Hi, H2, and H3 has to be diverted to the compressors, and additionally also less consequent mechanical losses occur at the compressors Gi, G2, and G3, as they need to perform less, than without this additional cooling.

[0238] An additional compressor or blower can help the remaining, cooled compounds of the exhaust-gas-stream stream through the heat-exchangers L3, L2, and Li. In the flowchart in Figure 10 this additional compressor or blower is placed at the exit of the exhaust-stream as compressor or blower G4 (quite at the top of the flowchart). After heat-exchanger Li the temperature is not as low as before heat-exchanger L3, thus this specific advantageous location has been chosen for the compressor or blower G4.

[0239] The exiting, still relatively cold exhaust-stream can be used for cooling an additional medium, which in turn can cool the incoming air of the power station. In Figure 10 this is shown in the flowchart on the top at the left side as Stream 50. In Figure 12 this additional cooling sub-process is shown also as Stream 50 leading to the existing cooling-system 51 of the air-intake.

[0240] The remaining part of the treated exhaust-stream at the end of the completed cooling-and-energy-conversion-process is shown as Stream 53 and is released into the ambient air exactly below the condenser-coolers. In Figures 11 and 12, the condensercoolers 52 are shown in the background, on the right side. As this exhaust-stream, after the cooling-and-energy-conversion-process, has a stable temperature-range, independent from the weather-depending ambient air-temperature, it would be suitable and helpful for the condenser-coolers to be cooled by this stream and not by ambient air.

[0241] The complete cooling-and-energy-conversion-process can sustain itself, thus does not need any other external -energy input, except maybe for a start-up-procedure, and can most likely in most cases even generate additional electric -energy.

[0242] Figure 11 shows a view in light grey -tones of a simplified combined-cycle power-station with the air in-let on the right side and the steam-turbine on the left side. The chimney has in Figure 11 an open maintenance-opening of the chimney 54. Figure 12 shows the same view in light grey-tones of the simplified combined-cycle power-station, but this time with the cooling-and-energy-conversion-system installed and shown in contrast in distinct darker grey-tones.

[0243] As can be seen in Figure 12 the complete cooling-and-energy-conversion- system of embodiments hereof is retrofitted. The exhaust-gas from the chimney is sucked in through the maintenance opening of the chimney 54, the additional coolingcycle 50, for the air-intake, is mounted on the right side on the existing cooling-system for the air-intake 51. An additional duct 53 leads the exiting exhaust-gas stream, after the cooling-and-energy-conversion-process, underneath the condenser-cooler units 52. The separated and liquid or solid carbon-dioxide can be extracted from underneath the six parallel units, these spaces are marked each with 55.

[0244] These six example-applications of the cooling-and-energy-conversion-process show how versatile this new process is.

[0245] Common Shaft and Magnetic-Coupling

[0246] In the different Figures it can be seen that expander H, compressor G, compressor A, and pump I, thus all the mechanical devices, are mechanically coupled to the same starter-motor-generator or dynamo (located at the bottom of the different flowcharts) e.g., they are all mounted on, or connected to the same common shaft.

[0247] When and if the different mechanical -devices have a direct contact, the transfer of mechanical-energy between the mechanical-devices has the lowest mechanical loss. If the mechanical devices are driven by electro-motors, then the losses of the different devices would significantly add to the losses of the complete system. Compressors and expanders, which usually work with pressure, are often encapsulated together with the driving electro-motor in a pressure-proof housing. In case of this cooling-and-energy- conversion-process different pressures of the different devices and also the possible difference of the used media in the different sub-process would make this kind of encapsulation difficult. A relatively simple solution would be to have the different mechanical devices in several pressure-proof encapsulated housing and connected to the common shaft with or through a magnetic coupling or a magnetic coupling-system. Thus, both advantages are reached.

[0248] This solution is also possible, when several process-steps are following each other, as in the last example above, where all the expanders, Hi, H2, and H3 together with all compressors, Gi, G2, G3, G4, Ai, A2, and A3, together with all pumps Ii, I2, and I3, are all mechanically coupled to the same common shaft, as can be seen in Figure 10.

Claims

1. CLAIMS:

1. An energy extraction and or conversion system comprising: a first sub-process utilizing a first compressor A to compress a first media used as an energy supply media, and a first heat exchanger B to transfer energy from the first media compressed by said first compressor A to a second media used as a cooling media in a second sub-process; the second sub-process utilizing said first heat exchanger B to transfer the energy from the compressed first media to said second media, a second compressor G to compress the second media from said first heat exchanger B, a second heat exchanger D configured to transfer energy from the compressed second media from said second compressor G to a third media used as a working media in a third sub-process, an expansion valve E configured to increase the volume and reduce pressure of said second media from said second heat exchanger D, and a third heat exchanger F configured to transfer energy from the third media at an expanded state to said second media after said expansion valve E; and a third sub-process utilizing said second heat exchanger D to transfer the energy from the compressed second media to said third media, an expander unit H configured to expand the third media from said second heat exchanger D into said expanded state, and said third heat exchanger F to transfer the energy from the third media at said expanded state to said second media, thus transferring thermal energy, and energy of the at least partial condensation, and facilitating at least partial condensation of said third medium.

2. The system of claim 1 comprising a pump I utilized in the third sub-process to pump and pressurize the third media through the third heat exchanger F into the second heat exchanger D.

3. The system of claim 1 or 2 comprising first, second and third flow paths for flowing therein, the first, second and third media, being gas-containing media, of the first, second and third sub-processes, respectively.

4. The system of any one of the preceding claims wherein the second flow path is configured as a closed-loop flow path for circulating the second media therein to successively pass the second media through the first heat exchanger B, the second compressor G, the second heat exchanger D, the expansion-valve E, and the third heatexchanger F, to transfer the energy from the first media to the second media within the first heat exchanger B, compress the second media by the second compressor G, thus bringing the second media to its highest temperature, causing energy transfer from the second media to the third media within the second heat exchanger D, followed by further temperature drop of the second media by expansion when passing through the expansion valve E thus allowing energy transfer from the third media to the second media at the third heat exchanger F.

5. The system of any one of the preceding claims comprising a pump I to pump and pressurize the third media, and wherein the third flow path is configured as a closed-loop flow path utilizing said pump I to circulate the third media therein to successively pass the third media through the third heat exchanger F, said pump I, the second heat exchanger D, and the expander unit H, said third closed-loop flow path configured for the energy transfer from the third media to the second media within the third heat exchanger F, thus at least partially condensing the third media at heat exchanger F, pumping and compression of the third media by said pump I, energy transfer from the second media to the third media within the second heat exchanger D, and expansion of the third media by the expander unit H, thus at least partially converting thermal energy into mechanical energy.

6. The system of any one of the preceding claims, wherein the expander unit H is coupled to an electrical generator selected from the following: an electro-motor, an electro-alternator, and a dynamo.

7. The system of claim 6, configured to use the electrical generator to start-up the system.

8. The system of claim 6 or 7, wherein the electrical generator is coupled to at least one of the first compressor A, the second compressor G, and the expander unit H.

9. The system of claim 6 or 7, further comprising a pump I located between the third heat exchanger F and the second heat exchanger D in the second closed-loop flow path, wherein the electrical generator is coupled to at least one of the first compressor A, the second compressor G, the expander unit H and the pump I.

10. The system of claim 8 or 9, wherein at least two of the first compressor A, the second compressor G, the expander unit H, the pump I and the electrical generator are coupled to each other via a common drive-shaft.

11. The system of claim 10, comprising magnetic-couplings, or a system of magnetic-coupling, for the coupling.

12. The system of any one of the preceding claims, wherein the first sub-process comprises at least one of filter and or absorber elements, located upstream from the first heat-exchanger B with respect to a direction of flow of the first media through the energy supply flow path.

13. The system of any one of the preceding claims, comprising in the first subprocess a separator, for separating compounds, said separator located downstream from the first heat exchanger B with respect to a direction of flow of the first media through the energy supply flow path.

14. The system of any one of the preceding claims, wherein the first media is air or water.

15. The system of claim 14, wherein the energy supply flow path is connected to an external fluid source to receive said first media therefrom.

16. The system of any one of the preceding claims, wherein the first sub-process is configured as an open-loop flow path.

17. The system of claim 16, further comprising a fourth heat exchanger C arranged in the third sub-process between the second heat exchanger D and the expander unit H, and in the first sub-process upstream from the first heat exchanger B, said fourth heat exchanger C being adapted to transfer energy directly from the first media to the third media.

18. The system of claim 16 or 17, further comprising an additional flow path for passing a heating media therethrough, said additional flow path comprising a fifth heat exchanger K located in the second sub-process between the second compressor G and the second heat exchanger D, such that the fifth heat exchanger K is adapted to transfer energy from the second media to the heating media.

19. The system of any one of the preceding claims, wherein the third sub-process is configured as a closed-loop flow path for circulating said first media therethrough.

20. The system of claim 19, wherein the first sub-process comprises at least one segment thereof passing through a heating zone located upstream from the first heatexchanger B with respect to a direction of flow of the first media along the energy supply flow path, thereby causing heating of the first media flowing, thus returning from the first heat exchanger B.

21. The system of claim 19 or 20, further comprising an additional closed loop flow path for flowing an additional heating media therethrough, and a fourth heat exchanger C arranged in the third sub-process between the second heat exchanger D and the expander unit H, said fourth heat exchanger C being adapted to transfer energy from said additional heating media to the third media.

22. An energy extraction and or conversion system comprising a plurality of subsystems, each one of said plurality of sub-systems configured according to any one of the preceding claims, said plurality of sub-systems arranged in a cascade fashion for successive passage of at least some portion of the first media through their first subprocesses (first heat exchangers Bi, 62,63,. . .) of said plurality of sub-systems to form a common energy supply flow path thereof.

23. An energy extraction and or conversion system comprising several sub-systems at least one of which configured to any one of the preceding claims, whereby at least one of said sub-systems is arranged in a parallel fashion for parallel passage of at least one of the first, second or third media.

24. The system of claim 22 or 23, comprising an auxiliary heat-exchanger Ci in the first sub-system, said auxiliary heat-exchanger is located upstream from the first heatexchanger Bi in the first sub-process of said first sub-system, and between the second heat-exchanger Di and the expander unit Hi in the third sub-process of said first subsystem, said auxiliary heat-exchanger Ci transferring energy from the first media to the third media.

25. The system of claim 23 or 24, comprising between the second heat-exchanger D and the expansion valve E of the second sub-process of each one of the plurality subsystems an additional heat-exchanger for transferring energy from the second media to the first media backwardly, after passing through the last sub-system in the cascade.

26. The system of any one of claims 23 to 25, comprising at least one centrifugal separator on the common energy supply flow path between two successive sub-systems.

27. The system of any one of the preceding claims configured to cool the first media and extract thermal-energy and or phase-change energy thereof, and convert said extracted energy into mechanical energy, and or for generating electricity from the surplus mechanical -energy of the process.

28. A method of extraction and or conversion of energy, the method comprising:a first sub-process of compressing a first media used as an energy supply media and transferring energy from the compressed first media to a second media used as a media of a second sub-process, the second sub-process comprising receiving firstly energy from the third media from the third sub-process, secondly receiving energy from the first media of the first sub-process, compressing said second media to a higher pressure and temperature level, followed by transferring energy from the compressed second media resulting from receiving said first and second energy in addition the energy of the compression, to a third media used as a media of the third sub-process, passing the then cooler second media through an expansion valve, increasing volume, reducing pressure of the compressed second media, and receiving at lowest temperature and pressure point energy of said second media, thereby closing said second sub-process, and a third sub-process comprising the receiving energy from the compressed second media to the third media, and expanding said third media to generate mechanical energy followed by transferring energy during at least partial condensation from the expanded third media to said second media.

29. The method of claim 28 comprising exploiting at least some portion of the mechanical energy for at least one of the following: the compressing of the second media; the compressing of the first media.

30. The method of claim 28 or 29 comprising pumping the expanded third media.

31. The method of claim 30 comprising exploiting at least some portion of the mechanical energy for at least one of the following: the compressing of the second media; the compressing of the first media; the pumping of the third media.

32. The method of any one of claims 28 to 31, comprising filtering and or absorbing before compressing the first media.

33. The method of any one of claims 28 to 32, comprising separating compounds from the first media after the transferring of energy thereof to the second media.

34. The method of any one of claims 28 to 33, comprising transferring energy from the first media to the third media after the transferring of the energy from the second media to the third media.

35. The method of any one of claims 28 to 34, comprising transferring energy from the second media to a fourth media as a heating media before the transferring energy from the second media to the third media.

36. The method of any one of claims 28 to 34, comprising circulating the first media through a closed-loop flow path having a heating zone configured for thermal energy therein to said first media.

37. The method of claim 36, comprising circulating an additional heating-media through closed loop flow path and transferring energy from said additional heating media to the third media after the transferring of the energy from the second media to the third media.

38. A method of extraction and or conversion of energy, the method comprising streaming a first media through a plurality of sub-systems arranged in a cascade fashion for serially communicating first media from one sub-system to the other and extracting and or converting energy from said first media by each one of said plurality of subsystems as defined in any one of claims 28 to 37.

39. The method of claim 38 comprising serially streaming at least some portion of the first media through the plurality of sub-systems, and transferring energy in at least one of said plurality of sub-systems from the second media to said at least some portion of the first media.

40. The method of claim 39 comprising streaming at least some portion of the first media after forwardly streaming it through said plurality of sub-systems, and then backwardly streaming said at least some portion of the first media through at least one of the plurality of sub-systems for transferring energy from the second media to said at least some portion of the first media.

41. The method of claim 40 comprising separating compounds from the first media passed between at least two successive sub-systems.

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