Heat engine using liquid-vapor phase change material

Abstract

The present disclosure provides a solution for a system and method for converting heat to work. The solution uses a nozzle in which a pressurized heat transfer liquid (HTL) is mixed with a liquid-vapor phase change (LVPhC) working fluid at approximately the same pressure to form an LVPhC-HTL mixture. The mixture then evaporates as it flows through the nozzle, undergoing isothermal or quasi-isothermal expansion, resulting in the acceleration of the mixture. The accelerated mixture is then discharged, rotating a turbine and producing work from the generated kinetic energy. After the LVPhC is discharged from the nozzle, it is separated from the mixture, condensed, and its pressure is increased again to the working pressure within the nozzle. The solution utilizes the thermodynamic advantages of each phase of the LVPhC.

Description

[Technical Field]

[0001] TECHNICAL FIELD The present disclosure relates to the field of systems and methods for generating power from heat. [Background technology]

[0002] The following references are considered to be relevant as background to the presently disclosed subject matter. WO2022 / 049573 WO2022 / 234554 US9644615

[0003] Acknowledgment of the above references herein is not to be inferred as meaning that they are in any way relevant to the patentability of the presently disclosed subject matter. Summary of the Invention

[0004] The present disclosure provides a solution for a system and method for converting heat to work. The solution uses a nozzle in which a pressurized heat transfer liquid (HTL) is mixed with a liquid-vapor phase change (LVPhC) working fluid at approximately the same pressure to form an LVPhC-HTL mixture. The mixture then evaporates as it flows through the nozzle, undergoing isothermal or quasi-isothermal expansion, resulting in the acceleration of the mixture. The accelerated mixture is then discharged, rotating a turbine and producing work from the generated kinetic energy. After the LVPhC is discharged from the nozzle, it is separated from the mixture, condensed, and its pressure is increased again to the working pressure within the nozzle. The solution utilizes the thermodynamic advantages of each phase of the LVPhC.

[0005] Thus, a first method aspect of the present disclosure provides a method for converting heat to work. The method includes (i) vaporizing or transitioning a liquid-vapor phase change material (LVPhC) from a liquid phase to a vapor or supercritical phase at a temperature of about T1 and a pressure of about P1 and mixing it in a nozzle with a heat transfer liquid (HTL) having a temperature of about T1 and a pressure of about P1. It should be understood that (i) includes one of two things: (1) vaporizing the LVPhC at a temperature of about T1 and a pressure of about P1, or (2) transitioning the LVPhC to a supercritical phase at a temperature of about T1 and a pressure of about P1. The choice of (1) or (2) depends on the properties of the LVPhC at the desired operating values of T1 and P1. The LVPhC is in the liquid phase at a temperature below about T0 at a pressure of about P1, where T0 is lower than T1. The HTL and LVPhC are mixed at T1, and P1 causes vaporization and quasi-isothermal expansion, resulting in acceleration of the HTL / LVPhC mixture as the pressure is reduced to P0. Vapor expansion inherently reduces the vapor temperature, but the high heat capacity of the HTL and the high heat transfer rate within the mixture minimizes this temperature drop. Quasi-isothermal expansion requires that the vapor temperature along the nozzle maintain at least 95%, 75%, or 65% of its initial temperature, measured in degrees Kelvin. (ii) The accelerated HTL / LVPhC mixture is expelled from the nozzle, its kinetic energy converted into work, and the LVPhC and HTL are collected at a pressure of P0. This can be achieved with an impulse turbine, or preferably a reaction turbine. Following said collecting, the method further includes (iii) heating at least a portion of the HTL to a temperature of about T1 and increasing its pressure to a pressure of P1 to enable an additional cycle of said mixing. Because the HTL loses relatively little heat due to expansion, most of the HTL is sent to another cycle, and only a portion of the HTL needs to be reheated. Theoretically, the HTL can go through multiple cycles before needing to be reheated. The order of heating and pressure increase can be reversed, i.e., heating can occur before pressure increase, or pressure increase can occur before heating.

[0006] A second method aspect of the present disclosure provides a method for converting heat to work. The method includes (i) vaporizing or transitioning a liquid-vapor phase change material (LVPhC) from a liquid phase to a vapor or supercritical phase at a temperature of about T1 and a pressure of about P1 and mixing it in a nozzle with a heat transfer liquid (HTL) having a temperature of about T1 and a pressure of about P1. (i) is understood to include one of two steps: (1) vaporizing the LVPhC at a temperature of about T1 and a pressure of about P1, or (2) transitioning the LVPhC to a supercritical phase at a temperature of about T1 and a pressure of about P1. The choice of (1) or (2) depends on the properties of the LVPhC at the desired operating values of T1 and P1. The LVPhC is in the liquid phase at a pressure of about P1 and a temperature below about T0, where T0 is lower than T1, causing the mixture to vaporize and quasi-isothermal expansion to occur, resulting in acceleration of the HTL / LVPhC mixture. The quasi-isothermal expansion is such that the temperature of the vapor along the nozzle remains at least 95%, 75%, or 65% of the initial temperature, measured in Kelvin; and (ii) expelling the accelerated HTL / LVPhC mixture from the nozzle, converting its kinetic energy into work, and collecting the LVPhC and HTL at a pressure of P0. This can be accomplished with an impulse turbine, or preferably a reaction turbine. Following said collection, the method further includes (iii) increasing the pressure of the HTL to a pressure P1 to allow for an additional cycle of said mixing. The order of heating and pressure increase can be reversed, i.e., heating can occur before pressure increase, or pressure increase can occur before heating.

[0007] Theoretically, the HTL can go through the cycle multiple times before needing to be reheated or replaced. The second method embodiment differs from the first method embodiment by allowing the HTL to operate in an open-loop configuration. For example, the HTL can be seawater, and the HTL can be replaced after several cycles just before reaching a temperature at which it can no longer operate within the cycle, such as the freezing temperature of the HTL or the phase change temperature at P1 of the LVPhC working fluid. This configuration may be relevant to implementing the method when the LVPhC is liquefied natural gas (LNG), liquefied hydrogen, or any evaporation process of a liquefied LVPhC material.

[0008] It should be noted that for any aspect of the present disclosure, any combination of the described embodiments is applicable. In other words, any aspect of the present disclosure can be defined by any combination of the described embodiments. In particular, it should be noted that all of the following method embodiments are applicable to any of the above method aspects and in any combination thereof.

[0009] In some embodiments of the method, said collecting the LVPhC vapor comprises separating the LVPhC / HTL mixture.

[0010] In some embodiments, the evaporator is part of a nozzle in a reaction turbine and the LVPhC is injected as droplets into a mixing chamber.

[0011] In some embodiments, an additional pump is connected between the HTL drain and the turbine. Such a pump can change the overall pressure without changing the turbine's frequency (RPM). This is important for generating power at a fixed frequency while the HTL temperature and vapor pressure vary. For example, if the HTL temperature drops below nominal, the pump reduces the turbine's input pressure, reducing the pressure in the nozzle. This allows vaporization and work production at temperatures lower than nominal. Optionally, increasing the mass flow rate of the LVPhC maintains a constant void fraction (volume ratio of HTL to vapor) at HTL temperatures lower than nominal. This allows the nozzle to maintain maximum efficiency even in these off-design conditions. In this case, the nominal HTL temperature T nominal When is changed to another value T, the nominal mass flow rate

number

number

[0012] In some embodiments, the system does not have a pump between the HTL drain and the turbine. In this case, evaporation stops when the temperature drops below nominal, causing a drop in pressure in the nozzle. Evaporation returns at low pressure, changing the void fraction and resulting in reduced efficiency during off-design operation.

[0013] In some embodiments of the method, the liquefied LVPhC is liquefied natural gas (LNG), which is a mixture that may include methane, ethane, propane, and butane.

[0014] In some embodiments of the method, the mixing and vaporizing are performed simultaneously, i.e., LNG is mixed in the liquid phase with the HTL, the HTL heats and vaporizes the liquefied LVPhC, and then the vaporized LVPhC is quasi-isothermally expanded.

[0015] In some embodiments of the method, collecting includes directing the discharged natural gas to a natural gas pipe for flow to a natural gas consumer. That is, the pressure P of the natural gas after being discharged from the nozzle is equal to or greater than the pressure required to transport the gas in the natural gas pipe to the consumer. In some embodiments, when the pressure P falls below the pressure required to transport the gas in the natural gas pipe to the consumer, the method further includes recompressing the natural gas to the pressure required to transport the gas in the natural gas pipe to the consumer.

[0016] In some embodiments of the method, the method further comprises, following said collecting, cooling the LVPhC and increasing its pressure to obtain liquefied LVPhC at a pressure of about P1 and a temperature of about T0, allowing for an additional cycle of said mixing, i.e., passing it through a vaporization step again.

[0017] In some embodiments of the method, following the cooling and pressurizing, the method further includes heating the LVPhC with an LVPhC heat source from a temperature of about T0 to a temperature between T0 and T1, inclusive. That is, the LVPhC heat source is capable of heating the LVPhC to T1. The LVPhC heat source can be, for example, seawater or any external heat source.

[0018] In some embodiments of the method, the cooling comprises passing the vaporized LVPhC through a heat exchanger at a temperature of about T1 and a pressure of P0, optionally in heat exchange with liquefied LVPhC having an inlet temperature to the heat exchanger of about T0, resulting in the liquefied LVPhC being raised to a temperature of about T1.

[0019] In some embodiments of the method, the passing comprises maintaining a majority of the liquefied LVPhC in the liquid phase, which occurs at least in part due to latent heat.

[0020] In some embodiments of the method, the cooling and increasing the pressure includes condensing the vaporized LVPhC, or at least a majority of it, before increasing the pressure.

[0021] In some embodiments, the method further includes, following said collecting, condensing the liquid and then passing it through a heat exchanger to exchange heat with the collected vaporized LVPhC to obtain thermally liquefied LVPhC, and the method further includes increasing the pressure of the heated LVPhC to about P1.

[0022] In some embodiments of the method, the vaporizing includes directing a portion of the collected HTL into heat exchange with the liquefied LVPhC at a temperature less than T1 and greater than T0, which is performed independently of the mixing, i.e., the HTL is operating in a closed loop, but the portion of the HTL used to vaporize the liquefied LVPhC is different from the portion of the HTL used to expand the liquefied LVPhC in the nozzle.

[0023] In some embodiments of the method, the induced step occurs before the heated step, i.e., the HTL induced to be heated first exchanges heat with liquefied LVPhC before receiving heat. This is accomplished by designing the method such that the end temperature of the HTL after heat exchange with liquefied LVPhC is above the boiling point of the liquefied LVPhC at P1.

[0024] In some embodiments of the method, the increasing of the HTL pressure occurs before the inducing and the heating occurs after the inducing.

[0025] In some embodiments of the method, the mixing and vaporizing are performed simultaneously, i.e., the LVPhC is mixed with the HTL in the liquid phase, the HTL heats the liquefied LVPhC to vaporize it, and then the vaporized LVPhC is subjected to a quasi-isothermal expansion.

[0026] In some embodiments of the method, the HTL is selected from the list consisting of molten salt, hot oil, water, brine, ethylene glycol, and water.

[0027] In some embodiments of the method, the HTL is ethylene glycol.

[0028] In some embodiments of the method, the LVPhC material is selected from the list consisting of water, pentane, isobutane, propane, R134a, R245fa, fluorocarbons, and toluene, or any steam used in organic Rankine cycle (ORC) technology.

[0029] In some embodiments of the method, the LVPhC is pentane.

[0030] In some embodiments of the method, the ejecting causes rotation of the nozzle, and the rotation of the nozzle produces work from kinetic energy.

[0031] In some embodiments of the method, the nozzle is part of, mounted on, or attached to a turbine, and the turbine is a reaction turbine.

[0032] In some embodiments of the method, the nozzle supports supersonic flow.

[0033] In some embodiments of the method, a jet exiting a nozzle is directed to form a film flow under centrifugal force.

[0034] In some embodiments of the method, the vaporizing or transferring comprises transferring the LVPhC to a supercritical phase, i.e., at P1 and T1, the LVPhC is in the supercritical phase and, after expansion in the nozzle, is in the gas phase at temperatures near P0 and T1.

[0035] Yet another aspect of the present disclosure provides a system for converting heat to work. The system includes an evaporator for receiving a liquefied vapor phase change material (LVPhC), i.e., LVPhC in the liquid phase, and vaporizing or transitioning the LVPhC to a vapor or supercritical phase at a pressure of about P1 and a temperature of about T1. It should be understood that the evaporator is configured to perform one of two operations: (1) vaporizing the LVPhC to a temperature of about T1 and a pressure of about P1, or (2) transitioning the LVPhC to a supercritical phase at a temperature of about T1 and a pressure of about P1. The choice of (1) or (2) typically depends on the properties of the LVPhC at the desired operating values of T1 and P1. The system further includes a heating volume for heating a heat transfer liquid (HTL) to a temperature of about T1. An HTL pump of the system is configured to increase the pressure of the HTL to about the pressure of P1. The system further includes a nozzle in fluid communication with the HTL pump and the evaporator, having an inlet portion for receiving the HTL and a mixing portion for (i) mixing the HTL with the LVPhC in the vapor phase at the temperature of about T1 and the pressure of about P1, and (ii) isothermal expansion of the mixture to a pressure of about P0, lower than the pressure P1, thereby causing acceleration of the mixture at the nozzle toward an outlet of the nozzle. The system further includes a turbine configured to rotate as a result of the acceleration of the mixture, thereby converting the kinetic energy of the mixture into work. The turbine may be an impulse turbine or, preferably, a reaction turbine. The system further includes a separation unit for separating the discharged HTL from the vaporized LVPhC. The separation unit includes a collection unit for collecting the discharged HTL and directing it to either a heating volume, an HTL pump, an evaporator, or any combination thereof, i.e., directing it to two or more components. For example, a portion of the HTL may be directed to the evaporator, and a portion of the HTL may be directed to the HTL pump.

[0036] In some embodiments of the system, the liquefied LVPhC is liquefied natural gas (LNG). LNG may be, for example, a mixture including at least one of methane, ethane, propane, and butane. Optionally, the LVPhC is hydrogen, water, CO2, or any LVPhC material.

[0037] In some embodiments of the system, the mixing section constitutes the vaporizer, i.e., LNG is mixed in the liquid phase with the HTL, the HTL heats and vaporizes the liquefied LVPhC, and the vaporized LVPhC is then quasi-isothermally expanded in a nozzle.

[0038] In some embodiments of the system, the separated vaporized natural gas is directed to a natural gas pipe to flow the natural gas to a natural gas consumer, i.e., the pressure P of the natural gas after it leaves the nozzle is equal to or greater than the pressure required to transport the gas in the natural gas pipe to the consumer.

[0039] In some embodiments, when the LVPhC is LNG, the system further comprises a heat exchanger in the form of a recuperator in fluid communication with: (1) a separation unit for receiving the discharged vaporized LNG into a heat rejection section of a heat exchanger; (2) a source of LNG at a pressure of about P1 for receiving LNG at about P1 into a heat receiving section of the heat exchanger; (3) a nozzle for flowing LNG from the heat receiving section to the nozzle; and (4) a natural gas line for flowing LNG from the heat rejection section to the natural gas line.

[0040] In some embodiments, the system further comprises a condenser for receiving the separated vaporized LVPhC and condensing it to a liquid state, and an LVPhC pump downstream of the condenser for increasing the pressure of the condensed LVPhC (received from the condenser).

[0041] In some embodiments, the system further comprises a heat exchanger in the form of a recuperator in fluid communication with the evaporator, (1) a separation unit for receiving the discharged vaporized LVPhC into a heat rejection section of the heat exchanger at a temperature of about T1 and a pressure of about P0; (2) a condenser for flowing the vaporized LVPhC discharged or exiting from the heat rejection section therethrough, wherein the vaporized LVPhC discharged from the heat rejection section is maintained substantially in a gas phase; (3) an LVPhC pump for receiving the liquefied LVPhC discharged from the LVPhC pump into a heat receiving section of the heat exchanger, wherein the liquefied LVPhC discharged from the LVPhC pump is at a pressure of about P1 and a temperature that may be less than T0; and (4) an evaporator for flowing the liquefied LVPhC discharged from the heat receiving section, wherein the liquefied LVPhC discharged from the heat receiving section is at a temperature of about T0 and a pressure of about P1. LVPhC is in the liquid phase at a pressure of about P1 and a temperature below about T0, where T0 is lower than T1.

[0042] In some embodiments, the system further comprises a heat exchanger in fluid communication with the LVPhC pump, (1) a separation unit for receiving the discharged vaporized LVPhC into a heat rejection section of the heat exchanger, (2) a condenser for flowing the vaporized LVPhC discharged from the heat rejection section thereto and receiving liquefied LVPhC therefrom into a heat receiving section of the heat exchanger, and (3) an LVPhC pump for flowing the liquefied LVPhC discharged from the heat receiving section to the LVPhC pump, wherein the evaporator is configured to receive the liquefied LVPhC from the LVPhC pump. This defines that the condensed LVPhC is first heated in the heat exchanger and then pressurized to about P1.

[0043] In some embodiments of the system, the liquefied LVPhC received at the heat receiving section is discharged from the heat receiving section in a manner that maintains at least a majority of it in the liquid phase, which occurs at least in part due to latent heat.

[0044] In some embodiments of the system, the condenser comprises or partly constitutes an LVPhC pump.

[0045] In some embodiments, the system further comprises an LVPhC heat source downstream of the condenser for heating the LVPhC to a temperature less than or approximately equal to the vaporization temperature of the LVPhC at a pressure of about P1, i.e., a temperature between T0 and T1, inclusive.

[0046] In some embodiments of the system, the vaporizer comprises or is part of the HTL pump.

[0047] In some embodiments of the system, an evaporator is in fluid communication with the collection unit for receiving at least a portion of the collected discharged HTL and exchanging heat with the liquefied LVPhC received in the evaporator, thereby vaporizing the liquefied LVPhC.

[0048] In some embodiments of the system, the evaporator is in fluid communication with a heated volume for flowing the HTL after heat exchange with the liquefied LVPhC in the evaporator.

[0049] In some embodiments of the system, the HTL pump is downstream of the nozzle and upstream of the vaporizer.

[0050] In some embodiments of the system, a portion of the HTL is flowed from the HTL pump to the vaporizer, and a portion of the HTL is flowed from the HTL to the nozzle.

[0051] In some embodiments of the system, at least a portion of the mixing section constitutes the evaporator.

[0052] In some embodiments of the system, the HTL is selected from the list consisting of molten salt, hot oil, water, brine, and ethylene glycol.

[0053] In some embodiments of the system, the HTL is ethylene glycol.

[0054] In some embodiments of the system, the LVPhC material is selected from the list consisting of water, pentane, isobutane, propane, R134a, R245fa, fluorocarbons, and toluene, or any steam used in Organic Rankine Cycle (ORC) technology.

[0055] In some embodiments of the system, the LVPhC is pentane.

[0056] In some embodiments of the system, the turbine is a reaction turbine and the nozzle is coupled to, mounted on, or part of the reaction turbine.

[0057] In some embodiments of the system, the collection unit defines a drain for accumulating the separated HTL, and as a result of the operation of the reaction turbine that constitutes the HTL pump, the HTL is sucked from the drain into the nozzle, whereby the HTL enters the nozzle at a pressure of about P1.

[0058] In some embodiments of the system, the separation unit comprises a curved or circular frame through which the mixture is discharged, and engagement of the mixture with the curved or circular frame results in a film flow on the surface of the curved or circular frame.

[0059] In some embodiments of the system, the evaporator is configured to receive a liquefied vapor phase change material (LVPhC) and transition it to a supercritical phase at a pressure of about P1 and a temperature of about T1, i.e., the LVPhC is a supercritical fluid at a pressure of about P1 and a temperature of about T1.

[0060] In some embodiments of the system, the condenser and LVPhC pump are configured with a nozzle including a nozzle inlet for receiving a flow of a nozzle heat transfer liquid (HTL) into the nozzle (the nozzle HTL being different from the HTL of the system), an outlet, a suction compressible fluid inlet, and an arrangement of fluid handling sections arranged in cascade fluid communication and defining a flow path for said fluid, the arrangement including: a second fluid handling section having an expanding configuration in the direction of said flow path for receiving the nozzle HTL at a pressure lower than a pressure of a suction fluid, the suction fluid being the LVPhC at a pressure of about P0; the suction fluid inlet configured to enable suction fluid communication between the ambient or a suction fluid source and the second fluid handling section, allowing the suction fluid to be introduced into the second fluid handling section to mix with the nozzle HTL and thereby obtain a fluid mixture; the expanding configuration of the second fluid handling section designed to transition the two-phase mixture to supersonic velocity at least at a distal end thereof; and a second fluid handling section configured to expand the second fluid handling section to receive the nozzle HTL at a pressure lower than a pressure of a suction fluid, the suction fluid being the LVPhC at a pressure of about P0. a third fluid manipulation section having a constricting configuration in the direction of the flow path to decelerate a flow of the fluid mixture received from the third fluid manipulation section to sonic or subsonic speeds and increase the pressure of the two-phase fluid mixture flowing along the third fluid manipulation section; and a fourth fluid manipulation section having an expanding configuration in the direction of the flow path and configured to increase the pressure of the subsonic flow of the fluid mixture received from the third fluid manipulation section to a pressure higher than ambient pressure, wherein the outlet is downstream of or defined by a distal end of the fourth fluid manipulation section for discharging the fluid mixture received from the fourth fluid manipulation section, the fluid mixture discharged from the outlet comprising pressurized suction fluid.

[0061] In some embodiments of the system, the nozzle further comprises a first fluid handling section downstream of the nozzle inlet and upstream of the second fluid handling section, or whose proximal end constitutes the nozzle inlet, having a narrowing configuration in the direction of the flow path to reduce the pressure of the nozzle HTL flowing therethrough below ambient pressure or below the pressure of the suction fluid at the suction fluid source, thereby accelerating the flow of the nozzle HTL flow.

[0062] In some embodiments of the system, the nozzle HTL contains at least one of water, molten salt, hot oil, ethylene glycol, molten metal, bicarbonate liquid, anti-icing liquid, liquefied gas, or any combination thereof.

[0063] In some embodiments of the system, the suction fluid is a gas or vapor.

[0064] In some embodiments of the system, the fluid mixture is a two-phase mixture and the pressurized suction fluid discharged from the outlet of the nozzle comprises a compressed gas.

[0065] In some embodiments of the system, the fluid mixture emitted from the outlet is a liquid mixture, and the pressurized suction fluid emitted from the nozzle outlet comprises a pressurized liquid.

[0066] In some embodiments of the system, at least one of the fluid handling sections has a frustoconical longitudinal cross-sectional shape.

[0067] In some embodiments of the system, the nozzle further comprises at least one conduit extending from an exterior thereof into the second fluid handling section and configured to channel the suction fluid into a mixing unit that enables mixing of the suction fluid with the nozzle HTL flowing along it, reducing the speed of sound in the mixture below the flow velocity of the mixture, resulting in a supersonic flow.

[0068] In some embodiments of the system, at least one conduit is connectable to an external source of suction fluid.

[0069] In some embodiments of the system, the third fluid manipulation section is configured to decelerate the fluid mixture flowing therealong so that it reaches sonic or subsonic speeds at the end of the third section.

[0070] In some embodiments of the system, the discharged fluid mixture comprises a fluid having a discharge pressure value that is up to 1 bar lower than the initial pressure value of the nozzle HTL that is channeled to the first fluid handling section.

[0071] In some embodiments of the system, the initial pressure value is up to 30% greater than the discharge pressure value.

[0072] In some embodiments of the system, the suction fluid flowing into the first fluid-handling section has a subsonic velocity.

[0073] In some embodiments of the system, the nozzle inlet is configured to be in fluid communication with a nozzle HTL source for receiving the nozzle HTL at a pressure greater than ambient pressure.

[0074] In some embodiments of the system, the nozzles HTL and LVPhC are the same liquid or material.

[0075] In order to better understand the subject matter disclosed herein and to illustrate how it may be carried out in practice, embodiments will now be described, by way of non-limiting example only, with reference to the accompanying drawings, in which: [Brief explanation of the drawings]

[0076] [Figure 1] This is an example of a TS diagram for a quasi-isothermal two-phase cycle. [Figure 2A] 1A-1D are block diagrams of different non-limiting examples of system embodiments according to an aspect of the present disclosure. [Figure 2B] 1A-1D are block diagrams of different non-limiting examples of system embodiments according to an aspect of the present disclosure. [Figure 3]FIG. 1 is a schematic diagram illustrating the injection of LVPhC into a nozzle. [Figure 4] This is an example of a PV diagram for a thermodynamic cycle. [Figure 5] 1 is an example of a control volume calculation for a thermodynamic cycle using two-phase pentane and ethylene glycol as the HTL. [Figure 6] FIG. 1 is a diagram showing an example of a thermodynamic cycle employing supercritical conditions. [Figure 7] FIG. 1 illustrates an example of a thermodynamic cycle of the present disclosure when employing waste heat recovery from steam. [Figure 8] FIG. 2 is a schematic diagram of a condenser and compressor used in the system of the present disclosure. [Figure 9] FIG. 10 is a schematic diagram of a cross section of a nozzle for condensing and compressing a fluid, optionally used in the systems or methods of the present disclosure. [Figure 10] FIG. 2 is a schematic diagram of an evaporator for optional use in the system of the present disclosure. [Figure 11] FIG. 1 is a block diagram of a non-limiting example of an embodiment of a system for converting the vaporization energy of LNG into work. [Figure 12] 1 is a schematic diagram of a non-limiting example of an embodiment of a system according to an aspect of the present disclosure. [Figure 13] 1 is a schematic diagram of a non-limiting example of an embodiment of a system according to an aspect of the present disclosure. DETAILED DESCRIPTION OF THE INVENTION

[0077] The following figures are provided to illustrate inventive embodiments and implementations of the present disclosure.

[0078] The objective of this disclosure is to increase the energy density per volume by three orders of magnitude compared to other waste heat recovery (WHR) phase change cycles, thereby reducing the size of the heat engine and increasing its efficiency by inducing isothermal expansion of the working fluid. An optional added benefit is the replacement of expensive large condensers with an innovative compact compressor / condenser. Optionally, the innovative compressor / condenser also compresses the liquefied vapor.

[0079] The core component of this method and system is a nozzle that mixes compressed gas or vapor with a heat transfer liquid (HTL). The HTL maintains a liquid state within the nozzle. Optionally, the phase change material is vaporized from the liquid phase by mixing with the HTL within the nozzle. Optionally, vaporization occurs before reaching the nozzle. The vapor mixed with the HTL forms bubbles that expand within the nozzle while maintaining approximately the same temperature as the HTL due to the high heat capacity of the HTL and the excellent heat transfer coefficient between the vapor bubbles and the HTL. The thermal energy density is defined by the HTL and is orders of magnitude greater than the heat capacity of the vapor per volume. The expansion of the bubbles accelerates the mixture within the nozzle, generating thrust at the nozzle exit. Both the HTL and the vapor cool as they expand. This temperature drop is less than a few degrees, supporting quasi-isothermal expansion of the mixture. Optionally, the velocity of the mixture within the nozzle becomes supersonic. In the nozzle, the initial pressure and a portion of the thermal energy of the HTL are converted into kinetic energy under quasi-isothermal conditions. The kinetic energy generates thrust that rotates a turbine, producing electrical, mechanical, or other forms of work. In some embodiments, the turbine is a reaction turbine, and the accelerated mixture of HTL and phase change material is ejected from a nozzle, causing the nozzle to rotate and enabling the conversion of kinetic energy to work. Reaction turbines have an advantage over impulse turbines because the jet velocity in an inertial frame is non-zero. This non-zero velocity is used to separate the gas / vapor phase from the liquid phase by forcing the mixture over the turbine wall, creating a film flow. Optionally, the wall has a circular shape, creating a centrifugal force on the film, separating the gas from the liquid. The reaction turbine additionally increases the static pressure within the nozzle to approximately the stagnation pressure level, thereby enabling maximum work extraction and maximum efficiency. Figure 1 shows the temperature vs. entropy (TS) diagram for a quasi-isothermal two-phase process. Optionally, the LVPhC is superheated.

[0080] 2A-2B are schematic block diagrams illustrating non-limiting examples of systems according to one embodiment of the present disclosure that provide optional implementations of the thermodynamic cycle of FIG.

[0081] Referring first to FIG. 2A, FIG. 2A illustrates a system 200 for converting heat to work. The system 200 includes a heat source 202, or heated volume, configured to heat an HTL to a temperature T1. In this non-limiting example, the HTL is heated to a temperature T1 while at a low pressure P0. The high-temperature, low-pressure HTL is introduced into a turbine 204, where its pressure is increased to P1 by centrifugal force or by a dedicated pump, which may be external to the turbine. In the turbine 204, the HTL enters a nozzle (not explicitly shown in FIGS. 2A-2B but which is part of the turbine) at an inlet temperature T1 and pressure P1. At the nozzle exit, the temperature and pressure are P0 and T0, with P0 being lower than P1 and T0 being lower than T1. Note that for quasi-isothermal expansion, T0 after one cycle is optionally close to T1, but the HTL temperature after many cycles may be 5%, 10%, 20%, or any other value lower than T1, as measured in Kelvin. Also, note that P0 can be ambient pressure or any other selected operating low pressure. For example, if the system is integrated with a liquefied natural gas (LNG) supply, the low pressure P0 is the pressure at which the natural gas in its vapor phase is pumped, and therefore P0 will be higher than ambient pressure. In some other embodiments, P0 may be lower than ambient pressure, such as 0.7 bar.

[0082] The liquid-vapor phase change (LVPhC) material is the working fluid in the system and is optionally maintained at a temperature T close to the operating temperature T1 and pressure P1. HTL_cold It is in the vapor phase at T cold and P1 into the liquid phase, where T HTL_cold is the temperature of the HTL after heat exchange with LVPhC in the evaporator to evaporate the LVPhC, and T cold is the temperature of the LVPhC after discharge from the nozzle and subsequent application of heat by a counter-flow heat exchanger, which are further described below. In some embodiments, T coldis at or near ambient temperature. The LVPhC can either enter the nozzle as a vapor at pressure P1 or as a liquid and evaporate within the nozzle; in the latter embodiment, the evaporator is constituted by a portion of the nozzle. Note that the term LVPhC is interchangeable with the term LGPhC shown in the figures.

[0083] The HTL and LVPhC are mixed in a mixing chamber or volume within the nozzle, forming a two-phase mixture within the nozzle. The LVPhC is injected as a liquid into the HTL, vaporizing it to form a two-phase mixture. This two-phase mixture is at temperature T1 and pressure P1 when mixed. The nozzle is then designed to reduce static pressure along its flow, resulting in the expansion of the LVPhC vapor within the nozzle, which accelerates the LVPhC / HTL mixture and generates thrust at the nozzle exit. This thrust rotates the nozzle, which is part of a reaction turbine, and generates work. The LVPhC / HTL mixture cools to temperature T0 along its flow within the nozzle due to the heat transfer to the LVPhC as it expands and, optionally, vaporizes. In practice, this expansion is quasi-isothermal, since the volumetric heat capacity of the HTL is approximately 1,000 times that of a gas or vapor. Quasi-isothermal means that the temperature of the steam, measured in Kelvin, remains the same with the flow through the nozzle within 95%, 75%, or at least 65%. In some embodiments, the flow through the nozzle is supersonic, allowing for a higher LVPhC / HTL mass ratio than subsonic flow. After the LVPhC exits the nozzle, it is separated from the HTL by gravity, and the HTL is collected in the turbine. Note that the HTL collected in the turbine 204 may participate in multiple cycles of HTL flowing through the nozzle before the HTL temperature drops to T_HTL-cold, requiring reheating by the heat source 202. Thus, most of the HTL collected in the turbine drain is pumped back to the nozzle at pressure P1. In some embodiments, if the LVPhC is vaporized before entering the nozzle, some or all of the HTL in the turbine flows from the turbine housing into the evaporator 206, which transfers heat to the LVPhC and vaporizes it.

[0084] The LVPhC steam after the turbine flows into a counter-flow heat exchanger (recuperator) 208, where T _coldThe LVPhC is then cooled to P1. The LVPhC then flows into condenser 210 and pressure increase unit 212, where it is condensed and its pressure is increased to P1. Condenser 210 and pressure increase unit 212 may be two separate units, or a single unit that performs both condensation and pressure increase. Note that condenser 210 and pressure increase unit 212 may be positioned along the flow path in any desired order; i.e., condenser 210 may be upstream of pressure increase unit 212, or pressure increase unit 212 may be upstream of condenser 210. Pressure increase unit 212 may be either a compressor that compresses the LVPhC in its vapor phase, or a pump that increases the pressure of the LVPhC in its liquid phase.

[0085] The pressurized LVPhC liquid at pressure P1 returns to the counter-flow heat exchanger (recuperator) 208 for reheating. Optionally, due to the high latent heat, the LVPhC liquid is partially vaporized in the heat exchanger. The pressurized LVPhC liquid then reaches the evaporator 206, which vaporizes the pressurized LVPhC at high pressure P1. Due to the latent heat required for evaporation, the temperature of the evaporator 206 is increased to T HTL_cold The pressurized LVPhC steam then returns to the turbine nozzle to produce work, and the HTL flows from the evaporator 206 to the heat source 202 to raise the temperature to T1.

[0086] Optionally, the evaporator may be in the form of a rotating drum, in which case the pressure of the HTL increases due to centrifugal force as it flows away from the axis of rotation of the drum (described in more detail below). LVPhC liquid is injected at high pressure, mixes with the HTL and vaporizes, and then the pressure of the HTL is reduced by flowing past the axis of rotation.

[0087] Optionally, the evaporator is a mixing section that is part of the nozzle. In this case, the LVPhC liquid from the recuperator is injected directly into the nozzle. To maintain the HTL at T1, a portion of the HTL flows from the turbine 204 to the heat source heat exchanger 202 and back to the turbine 204.

[0088] Optionally, an HTL pump (not shown) is connected between the HTL drain and the turbine to increase the input pressure to the turbine, decoupling the nozzle pressure from the turbine rotational frequency (revolutions per minute - RPM). In this case, if the HTL temperature drops below nominal, the pump reduces the input pressure, and the turbine maintains a constant RPM. This reduces the nozzle pressure, allowing the LVPhC to be vaporized at a lower temperature while still producing power at a constant frequency. Additionally, the mass flow rate of the LVPhC may be varied to compensate for temperature changes. The nominal HTL temperature, T nominal When is changed to another value T, the LVPhC nominal mass flow rate

number

number

[0089] Referring now to FIG. 2B, FIG. 2B differs from FIG. 2A by including an HTL pump 214 configured to increase the pressure of the HTL from P0 to P1. The HTL pump 214 can be located anywhere in the flow path between the turbine's collection drain, where the HTL is collected after being discharged from the nozzle, and the nozzle's inlet. For example, as shown in FIG. 2B, the HTL pump 214 is located downstream of the turbine, i.e., immediately after the collection drain, and the pressurized HTL discharged from the HTL pump 214 is either directed to the evaporator 206 or returned to the turbine 204, i.e., a portion is directed to undergo another cycle within the turbine; thus, the turbine is designed for a small pressure increase, and a portion is directed to transfer heat to the LVPhC in the evaporator 206 to vaporize it, and then directed to the heat source 202 to be reheated to T1. In this case, the evaporator 206 is simply a mixing tank in which both the HTL and LVPhC liquids are mixed at P1. Optionally, the HTL and LVPhC liquids flow through the mixing tank as the mixture vaporizes while cooling the HTL. At the outlet of the mixing tank, the HTL temperature is at a temperature T higher than the evaporation temperature of the LVPhC at pressure P1. HTL_cold Optionally, an additional pump (not shown) is added after the heat source to compensate for the head losses in the evaporator and heat exchanger. This ensures that the two streams of HTL meet at approximately the same pressure.

[0090] The term "about" is to be interpreted as a ±20% deviation of the nominal value. For example, a value of about 10 should be understood to be in the range of 8-12.

[0091] Optionally, the temperature change of the HTL is small, less than one degree or a few degrees, with each pass through the nozzle. In this case, most of the HTL returns to the nozzle through the bypass without passing through the evaporator and reheating. In this way, the temperature of the HTL decreases with each iteration. This defines the ratio of bypass to evaporator flow. The advantage is that the number of iterations, N, allows the LVPhC vapor expansion to be maintained at a high temperature, leading to high efficiency, while the HTL reaches the heat source at its lowest temperature, which is the liquid-vapor phase change temperature at P1, extracting maximum heat from the heat source, thereby increasing efficiency.

[0092] At a specific mass ratio, nozzle ΔT expansion Also, assume that the mass ratio is ΔT latent Then, after N cycles in the turbine, the outlet temperature is T0=T1-N*ΔT expansion The temperature change in the evaporator is T HTL_cold =T0-N*ΔT latent This defines N, which results in the minimum desired HTL temperature, which defines the average operating temperature within the nozzle, which in turn defines the efficiency.

[0093] For example, ethylene glycol is an HTL material and pentane is an LVPhC material. At a mass ratio of 0.01 and an operating pressure of 14.5 bar, the temperature change due to expansion is about 0.3 degrees Celsius, and the temperature change due to latent heat and mass ratio is about 1.4 degrees Celsius. Also, if the high temperature T1 is 155°C and the low temperature woT HTL_cold = 100°C. The value N≈32 then defines the number of cycles the HTL passes through the nozzle before flowing to the evaporator. This is also the ratio between the amount of HTL flowing to the evaporator and the amount recycled to the turbine. The average expansion temperature is 155-N / 2*0.3=150°C, which is almost the maximum temperature, and the outlet temperature from the evaporator is 155-44(0.3+1.4)≈100°C, which is the minimum temperature required to evaporate the pentane at P1.

[0094] Optionally, the mass ratio of LVPhC / HTL is 10% to 0.1% (small proportion of LVPhC in HTL).

[0095] Optionally, the LVPhC enters the nozzle as a liquid, where evaporation occurs. This requires an insulated liquid LVPhC pipe to reach the mixing chamber, which may be the case when using natural gas as the LVPhC. Figure 3 shows an optional nozzle where the liquid LVPhC flows through an insulated pipe and is injected into the mixing chamber as a liquid. Note that while Figure 3 illustrates the injection of LNG, this can be achieved with any suitable LVPhC.

[0096] Optionally, the sound velocity in the mixture is reduced due to the bubbly medium, and the velocity of the LVPhC / HTL mixture becomes supersonic. In such an option, a DeLaval-type two-phase nozzle design is applied (see the reference on supersonic two-phase flow in “Thrust Enhancement Through Bubble Injection into an Expanding-Contracting Nozzle With a Throat Sowmitra Singh”, Tiffany Fourmeau, Jin-Keun Choi, Georges and L. Chahine, DOI: 10.1115 / 1.4026855).

[0097] Optionally, upon reaching the nozzle, the vapor LVPhC is heated to T1. Optionally, this heating is isochoric (constant volume). This is achieved when the velocity of the HTL is high enough to carry the LVPhC through a cross-sectional area where the pressure increases while heating the LVPhC. Optionally, for subsonic flow, this occurs at an diverging cross-section. Optionally, heating is at constant pressure (isobaric) or any combination between isochoric and isobaric. For isobaric heating, to account for the additional volume, the mixing chamber optionally has an diverging cross-section. Optionally, the diverging cross-section of the mixing chamber is sized appropriately for the additional volume change of the LVPhC vapor. After heating, the LVPhC vapor expands isothermally or quasi-isothermally, with heat transfer from the HTL to the LVPhC vapor. Optionally, the vapor temperature upon exiting the nozzle is similar to the HTL temperature. Optionally, the LVPhC temperature is 1%, 10%, or 20% lower than the HTL temperature, measured in Kelvin.

[0098] The method is optionally described in terms of engine cycle stages.

[0099] 1->2: The liquefied LVPhC is pumped out of the condenser and pressurized to a pressure P1 equal to or close to the pressure in the mixing chamber in the nozzle.

[0100] 2->3: The liquefied LVPhC exchanges heat with the steam leaving the turbine, raising its temperature without a phase change (due to its high latent heat, the liquefied LVPhC remains liquid). Optionally, some of the LVPhC is evaporated.

[0101] Optionally, stages 1->2 and 2->3 are interchanged and the LVPhC liquid is first heated in a recuperator and then the pressure is increased to P1.

[0102] 3->4: The compressed liquid (optionally partly vapor) LVPhC is injected into an evaporator where it is vaporized. Optionally, this stage takes place in a nozzle.

[0103] 4->5: The compressed vapor LVPhC mixes with the HTL in a mixing chamber in the nozzle, where the HTL flows. The drop in static pressure and temperature along the flow in the nozzle causes quasi-isothermal expansion, accelerating the LVPhC / HTL mixture and generating thrust at the nozzle exit that spins a turbine, producing electrical, mechanical, or other forms of work. Optionally, the mixture's velocity can become supersonic in parts of the nozzle.

[0104] 5->6: The hot steam LVPhC vapor leaves the nozzle, is separated from the HTL, and flows into a heat exchanger (recuperator) where it exchanges heat with the liquid LVPhC coming from the condenser, but there is no phase change (the vapor remains vapor). Optionally, some of the vapor is condensed.

[0105] 6->1: The vapor is cooled in the condenser until it condenses and is compressed into a liquid.

[0106] Figure 4 shows the PV diagram of the thermodynamic cycle.

[0107] The method is optionally implemented to convert low temperature to work using an organic LVPhC, similar to an organic Rankine cycle (ORC), but using isothermal expansion, which is more efficient than adiabatic expansion. Examples of LVPhC materials include the traditional ORC materials pentane, isobutane, propane, R134a, R245fa, fluorocarbons, and antifreeze materials such as toluene.

[0108] Figure 5 and the list below show an example of a control volume calculation for a thermodynamic cycle using biphasic pentane and ethylene glycol as the HTL.

[0109] Consider 1 kg of pentane. The values in the TS diagram are P0 = 1 bar, P1 = 14.5 bar, T1 = 155 °C, T HTL_cold = 35°C, which is a different thermodynamic state.

[0110] 6->1: Condensation: 342KJ / Kg

[0111] 1->2: Isentropic compression up to P1 with LVPhC liquid pump: 4KJ / Kg

[0112] 2->3a: LVPhC liquid heat exchange with LVPhC vapor assuming a 30 degree gap: 146KJ / Kg

[0113] 3a->3: With additional heat from HTL, the liquid-vapor equilibrium point at P1 is reached: 144KJ / Kg

[0114] 3->4: Evaporation of LVPhC liquid and heating of vapor to 155°C: 246KJ / Kg

[0115] 4->5: LVPhC steam expands in the nozzle and performs isothermal work: 133KJ / Kg

[0116] 5->6: Steam cooling in heat exchange: 146KJ / Kg

[0117] This calculation is

number

[0118] Assuming an ideal heat exchanger (temperature difference of 0°C), the efficiency reaches the Carnot efficiency, which is twice as high as the efficiency of conventional ORC under similar conditions.

[0119] Optionally, the condenser operates above the expansion end pressure P0. This eliminates the need for a condenser to compress the vapor before or during condensation. This allows the condensation temperature to be maintained high, reducing the cooling (5-6 in the diagram) and heating (3-4 in the diagram) stages and optionally eliminating the need for heat exchangers before or after the condenser. Therefore, the temperatures of stages 6 and 1 are optionally higher than ambient temperature (dotted line and points 1b and 6b in the diagram). Optionally, condensation occurs at temperatures higher than 50°C, 75°C, or 100°C. For example, the vapor pressure of pentane at 120°C is 9 bar. Optionally, the turbine operates at 120°C and 9 bar by injecting pentane into the nozzle at 9 bar and reducing the pressure to 1 bar. The vapor is then cooled to 100°C, compressed at 100°C and 9 bar, condensed, and the liquid pentane is reinjected into the nozzle. High-temperature condensation reduces the size and cost of the condenser. The high condensing pressure allows operation at elevated ambient temperatures. Optionally, the condensing pressure can be increased as the ambient temperature increases, allowing continuous operation under all environmental conditions. High temperature condensation eliminates the need for a heat exchanger between the turbine and the condenser, resulting in cost savings. However, cycle efficiency is defined by the high temperature T1 and the low temperature T_cold, which should be as low as possible.

[0120] Another option is to eliminate the recuperator heat exchanger between the turbine and the condenser. In this case, the hot vapor is cooled when it mixes with the HTL in the condenser (more on this later), and this heat is removed by a blower or other means, keeping the condenser temperature, T_cold, as low as possible. Heating of the pressurized liquid LVPhC after the condenser is optionally achieved by a heat source, lowering its temperature to T_low. By eliminating the recuperator (gas / liquid) heat exchanger and replacing it with a liquid / liquid heat exchanger between the heat source and the liquid LVPhC, costs are significantly reduced.

[0121] In another example, supercritical conditions are used for energy conversion. Figure 6 shows such a thermodynamic cycle using pentane. The cycle with the closed black solid line is the supercritical cycle. Pentane, a non-limiting example of an LVPhC, is heated beyond its phase transition curve, e.g., to 280 °C at 50 bar pressure. At this supercritical temperature and pressure, pentane is in a liquid-gas mixture. As it expands, the pressure drops and the gas phase becomes dominant (upper black horizontal solid line at 280 °C in Figure 6). Because the nozzle contains a gaseous medium, the mixture does not affect operation and does not cause potential damage to the gas turbine. The advantage is the amount of work extracted. As seen in the conventional cycle (horizontal dashed line at 140 °C in Figure 6), as it heats up, much of the enthalpy is lost in the phase change without producing work. The total work that can be extracted (H5-H4 in Figure 6) is approximately 43 kJ / kg. On the other hand, in a supercritical isothermal expansion, the available work (H5*** to H3*** in Figure 6) is about 84 kJ / Kg, which is almost twice that of a conventional cycle. Work at supercritical conditions is limited by the durability of materials or by engineering limits on operating pressure and temperature.

[0122] Another example is waste heat recovery from steam. Assume steam at 135°C and 2.4 bar. The following cycle, or a similar one, is possible: Steam is injected into a water tank at 2.3 bar pressure. The water is heated to a temperature slightly below its evaporation temperature (~130°C). A heat exchanger between the water and ethylene glycol raises the temperature of the ethylene glycol to 120°C, which flows into the nozzle of a turbine operating at 9 bar. Pentane liquid at 9 bar is injected into the nozzle, vaporizes, and accelerates the HTL / pentane mixture, generating thrust and electricity. In some embodiments, the nozzle is part of a reaction turbine, and the HTL / pentane mixture exiting it causes the turbine to rotate. In some embodiments, a non-zero velocity jet from the nozzle forms a film flow on the wall of the reaction turbine. This film flow optionally has centrifugal forces that separate the vapor phase from the liquid phase. The pentane vapor is cooled in a heat exchanger, condensed into a liquid, pressurized, and returned to the heat exchanger for heating and return to the nozzle. Optionally, condensation is performed at a temperature above ambient. Optionally, the heat exchanger is removed and the condenser is cooled to 50°C. Optionally, heating of pressurized pentane liquid from 50°C to 135°C is performed by reducing the temperature from 120°C to 50°C using residual heat from a heat source.

[0123] The same thermodynamic cycle proposed can be run at higher temperatures, as in the Ranking cycle, but twice the efficiency is supported by the quasi-isothermal expansion in the nozzle. For example, use water as the LVPhC and hot oil or molten salt as the HTL. When mixed with the molten salt, water evaporates. Therefore, the molten salt must be selected so that it does not react chemically with the water vapor and cause damage to the operation (causing toxicity, corrosion, erosion, etc.). Some typical parameters are: T1 = 530°C, P1 = 50 bar, P0 = 0.06 bar, T0 = 40°C (see Figure 7).

[0124] The advantages of this method are at least the following: (1) The thermal density of the HTL is three orders of magnitude higher than that of any gas or vapor, allowing for a reduction in device size; (2) It induces quasi-isothermal expansion, which is nearly as efficient as the Carnot-Ericsson and Stirling cycles, and is much more efficient than conventional adiabatic expansion (such as ORC). This is achieved by mixing vapor bubbles within the HTL.

[0125] Traditionally, ORCs use large, expensive condensers, followed by pumps to increase the pressure of the organic liquid. To achieve the same goal in a much smaller, less expensive way, we describe the condenser / compressor described below. Optionally, the organic vapor and HTL in the condenser / compressor are at approximately the same pressure. In this case, the vapor is bubbled into the heat transfer liquid (HTL) in the chamber at a temperature below the phase transition, where it liquefies due to the large surface area of the vapor bubbles and the high heat capacity of the HTL. Optionally, the HTL is heavier than the liquid LVPhC, so counterflow is designed by injecting the vapor from the bottom and collecting the liquid LVPhC at the top. The inlet of the HTL is at the top and the outlet is at the bottom.

[0126] Optionally, the HTL is water, other organic liquids such as ethylene glycol, the same organic substance as an organic vapor in liquid phase, or any other liquid that has a liquid phase at the operating temperature. Optionally, the inlet temperature of the HTL is between -200°C and 140°C. A cryogenic HTL is optionally used to liquefy air, nitrogen, hydrogen, CO2, or any other gas.

[0127] An optional method and system for condensing and compressing gases or vapors is shown in Figure 8. This system is designed to increase the surface area between the condensed liquid and the condensed vapor, thereby reducing the size and cost of the compressor. The closed-loop flow of the HTL is driven by a pump at a pressure higher than ambient. The nozzle is designed to reduce the pressure below the incoming vapor pressure. This draws the vapor or other gas into the HTL flow. The gas enters from the surrounding envelope or through a designated pipe. The vapor and HTL mix, and the HTL's temperature and its high heat capacity relative to the vapor per volume cause the vapor to liquefy. The nozzle geometry is designed so that the pressure at the nozzle outlet is higher than ambient pressure. Optionally, all vapor is liquefied in a mixing section with the liquid, and the nozzle is expanded to recover the high pressure. In such cases, the nozzle is diverging (pressure reduced below ambient pressure) followed by a mixing chamber, which optionally diverges to allow the vapor to enter the liquid, followed by a diverging outlet to increase the liquid's pressure. Optionally, the length of the mixing section is long enough to allow >10%, >30%, or >90% of the vapor to liquefy. Optionally, a portion of the organic material remains in the vapor phase and is compressed as a gas. Optionally, the vapor / HTL mixture reduces the sonic velocity below the mixture's flow velocity, resulting in supersonic flow within the nozzle. In this case, an inverse De Laval nozzle is designed. Optionally, the compression is isothermal or quasi-isothermal. Optionally, if the HTL is a liquid different from the organic material, after the nozzle, the mixture is separated by gravity, centrifugal action, or any other separation method. The organic liquid is collected (at the top if its density is lower than that of the HTL), and the HTL reaches the pump to continue circulation. The HTL heats up as it condenses and compresses. The hot HTL is replaced by cooled HTL (not shown) for continuous operation of the compressor. Optionally, the HTL can be cooled by heat transfer to the surroundings through the flow surface without replacement. Optionally, the compressor suction pressure is lower than ambient pressure, e.g., 0.7 bar.This allows the turbine to operate between the maximum compression pressure and the minimum inlet pressure, 0.7 bar in this example. The large surface area allows for faster condensation, and compressing the fluid creates an additional pressure gap, improving energy efficiency. In Figure 5, point 5C represents the additional power generated by the turbine due to the reduced end pressure, while the dotted line represents the condensation and compression process reaching point 6. Under steady-state conditions, the HTL can evaporate below ambient pressure in the low-pressure region. In this case, the flow time in the low-pressure region is much shorter than the heat exchange rate. Therefore, the HTL does not have enough time to absorb the heat of evaporation from the environment and remains liquid, making the HTL and LVPhC the same material. For example, liquid pentane can be used as the HTL working fluid flowing through the condenser / compressor to condense the pentane vapor. In the low-pressure region, conditions may support the vapor phase, but as long as the flow in the low-pressure region is faster than the speed of sound, no phase change occurs. Also, if the HTL temperature is below the evaporation point, no phase change occurs as long as the flow in the low-pressure region is faster than the heat transfer rate. Instead, the liquid sucks in the pentane vapor arriving from the turbine, condenses it, and compresses it, the advantage being that there is no separation between the two liquids after condensation.

[0128] The ability to operate at pressures lower than ambient allows for conversion at lower temperatures. For example, the phase change of pentane at 100°C is approximately 7 bar, and as the pressure is reduced to ambient pressure of 1 bar by expansion, a small amount of work is generated in the turbine. The ability to operate the turbine from 7 bar to 0.46 bar effectively generates work as if the operating pressure were between 15 bar and 1 bar, typically at 155°C. Optionally, the steam condenser / compressor inlet pressure can be designed to be less than 1 bar, less than 0.5 bar, or even less than 0.1 bar. Because the steam can be condensed and compressed faster than the heat transfer rate, the process can be completed at higher temperatures. For example, high-speed compression up to 10 bar allows condensation even at temperatures above 90°C. That is, in Figure 5, condensation optionally ends at point 3 or between points 2 and 3. A larger temperature difference between the compressor and ambient increases the cooling rate, reducing the compressor size accordingly. Optionally, the HTL in the compressor is maintained at a temperature 30°C, 50°C, 70°C, or 90°C above ambient. Optionally, the high-pressure condenser operates at the turbine exit temperature T0, eliminating the need for a (costly) heat exchanger between the turbine and condenser. Increasing T_cold may reduce engine cost $ / kW, even at the expense of cycle efficiency. For high efficiency, it is preferable to reduce the HTL temperature before increasing the pressure, allowing the steam in the mixing chamber to cool. Optionally, the steam temperature, measured in Kelvin, reaches the HTL temperature within 5%, 10%, or 20% before increasing the pressure.

[0129] Figure 9 shows an example of a reverse De Laval nozzle for supersonic continuous isothermal compression of gases or vapors (not to scale). The nozzle may comprise the following sections, in order: 1. Converging inlet section for reducing pressure above ambient pressure, consisting of HTL only. 2. Diffusion two-phase section: The pressure is constant and steam is drawn into the HTL from the surroundings through holes or gaps in the outer wall of the nozzle. The cross section marked with "-" is where the drawing begins, and the cross section marked with "+" is where the drawing ends. Optionally, this section is long enough to allow the steam temperature to reach the HTL temperature as soon as possible. The mixture reduces the sonic velocity below the velocity of the mixture. At the end of the "diffusion two-phase section" (marked with "+"), the flow becomes supersonic. 3. In the converging two-phase section, the pressure increases and the Mach number (ratio of flow velocity to the speed of sound) decreases. At the end of this section, marked with an "*", Mach = 1. Optionally, Mach 1 can be reached earlier in the converging two-phase section. 4. At the diffusive two-phase outlet, the pressure increases and the Mach number decreases.

[0130] An efficient way to vaporize the LVPhC is to use an HTL at the lower temperature T0 after it leaves the turbine, optionally after several cycles in the nozzle. In this way, the expansion takes place in the hot HTL, maximizing efficiency. The remaining low-temperature thermal energy in the HTL is used to vaporize the liquid LVPhC at high pressure.

[0131] Optionally, if the HTL and liquid LVPhC are at similar pressures, a chamber can be used to mix the HTL and liquid LVPhC, allowing evaporation to occur and the vapor to be collected at the top of the chamber. Optionally, a direct contact counterflow heat exchanger can be configured by injecting the HTL into the top of the chamber with an outlet at the bottom and the liquid LVPhC being injected into the bottom of the chamber.

[0132] To mix the low-pressure HTL (exiting the turbine) with the high-temperature liquid LVPhC, a direct-contact evaporator, as described above, is optionally used. This consists of a rotating drum with a high-temperature HTL inlet channel and a low-temperature outlet HTL channel, both located near the axis of rotation to reduce centrifugal pressure. The HTL flows along the drum boundary, where the centrifugal pressure is close to that of the liquid LVPhC. The liquid LVPhC is injected into the HTL in the high-pressure region and evaporated by cooling the HTL. The vapor reaches the center of the drum by centrifugal force and is discharged at high pressure through the vapor LVPhC outlet channel. The cold HTL exits the drum near the shaft. Such devices operate continuously with very little mechanical input because the HTL enters and exits near the shaft at pressures close to ambient. Figure 10 shows an example of such an evaporator, with a rotating drum and an HTL inlet and outlet adjacent to the axis of rotation at low pressure. The liquid LVPhC is injected into the high-centrifugal-pressure region of the HTL, where it mixes with the HTL and evaporates while cooling the HTL. The steam flows to the center of the drum and is discharged at high pressure.

[0133] Also, as mentioned above, the solutions provided in this disclosure can utilize the LNG regasification process.

[0134] Conventional technologies for recovering the energy extracted in the regasification process include direct expansion technologies, such as the open organic Rankine cycle (ORC), in which natural gas is used as the organic working fluid. In this concept, LNG (as a liquid) is compressed to the required supply pipe pressure. After heating with seawater, the pressure is increased by gasification and converted to work using an organic turbine. The gas expands adiabatically, decreasing in temperature as it expands, necessitating a second heat exchanger (also using seawater) to reach room temperature. Conventional pipe pressures range from 70 bar to 150 bar. The isentropic (adiabatic) efficiency of conventional expansion is 80%, with the two heat exchangers being the major energy loss. Another method is to use LNG as a cold source in an ocean thermal energy conversion (OTEC) Rankine cycle. This Rankine cycle can extract energy from the temperature difference between the pre-gasification seawater and the LNG, which can then be added to the direct expansion technology. Together, the overall efficiency is around 8%.

[0135] This disclosure provides a solution that uses expansion to accelerate the HTL gasification and generate power. In this scenario, LNG, liquefied hydrogen, ammonia, or other liquefied gas is mixed with the HTL gas, such as room-temperature water, in a mixing chamber. The LNG is isochorically heated and vaporizes as bubbles, increasing its pressure to near its vapor pressure or evaporation pressure at the temperature of the HTL. Optionally, the pressure of the LNG before evaporation is increased to 300 bar, 140 bar, 70 bar, or any other value, thereby increasing power extraction and improving efficiency. Optionally, the liquefied gas is isobarically heated or heated at a level between isochoric and isobaric heating. This pressure is converted to kinetic energy at the nozzle exit as the gas expands isothermally due to thermal contact with the HTL gas. The natural gas, hydrogen, ammonia, or any other regasified gas is separated from the HTL gas by gravity, collected, and transported to a gas pipe for distribution to consumers. Optionally, the gas pipe is at 140 bar, 70 bar, or any other value. In that case, the nozzle outlet pressure is optionally at that pressure.

[0136] The HTL cools as the gas evaporates and expands isothermally. For example, the latent heat of natural gas (methane) is ~510 Kj / K, and the phase diagram for water and methane shows a pressure of >30 MPa (300 bar) at 300 K, with a temperature of 22.5 cm 3 / mol. Similarly, hydrogen has a latent heat of ~450 Kj / Kg, and its phase diagram shows pressures of >250 MPa (250 bar) at 300 K. The amount of heat extracted from the HTL is enthalpy energy (1.45 MJ / Kg), which includes the latent heat and the specific heat times the temperature difference. Calculate the work W that can be produced at a terminal pressure of 70 bar:

[0137] The density of methane at 1 bar is ρ = 0.657 kg / m 3 Let's say.

[0138] For isothermal expansion from 300 bar,

number

[0139] The HTL is optionally seawater and is constantly replaced before freezing. Optionally, the HTL is tap water or another liquid flowing in a closed loop and passing through a heat exchanger for reheating. Optionally, the closed-loop HTL is a liquid with a low freezing point, such as alcohol, methanol, or other organic substance with a liquid phase in the LNG temperature and pressure operating range. Optionally, after cooling in the nozzle, the HTL is used to run a heat engine (cold side). For example, the cooled alcohol exiting the nozzle is optionally used to isothermally compress air for the heat engine. The cold HTL is optionally used for refrigeration or air conditioning. Optionally, seawater is used to heat the HTL through a heat exchanger. Optionally, the HTL is heated by burning a small portion of the gas.

[0140] Figure 11 illustrates a method for operating a HTL / LNG mixed turbine. LNG or other liquefied gas enters the LNG heat exchanger, where it vaporizes and undergoes isobaric expansion. It enters the turbine as a gas, mixes with the HTL in the nozzle, and expands isothermally at approximately the temperature of the HTL. The expansion of the combined HTL and gas accelerates the HTL, generating thrust, rotating the turbine, and producing work. The exhaust gas is approximately at the temperature of the HTL and at ambient pressure. Optionally, the terminal pressure is not ambient pressure but the pressure required for the pipe transporting the gas, which may be 6 bar, 40 bar, 70 bar, 140 bar, or any other value. The vaporized natural gas exhausted from the turbine returns through the heat exchanger, vaporizing the LNG isobarically. Optionally, the gas does not return to the LNG heat exchanger; instead, the LNG heat exchanger uses an external heat source, such as seawater, to vaporize the LNG. In this option, the LNG heat exchanger is a pipe immersed in seawater. Optionally, the LNG can be vaporized using other heat sources, such as by burning a small portion of the gas.

[0141] Optionally, there is no LNG heat exchanger, and the LNG (as a liquid) enters the turbine directly, mixing with the HTL in the nozzle and vaporizing, where it vaporizes and expands isothermally. The vaporized gas is optionally isochorically heated by injecting the LNG into a narrow section of the nozzle where the HTL velocity is high and static pressure is low. This forces the LNG to leave the mixing chamber as a liquid before heating, and heating occurs in the wider section where pressure is higher. Isochoric heating of the LNG is induced by matching the cross-sectional area expansion rate and the rate of pressure rise in the nozzle to the heating rate. Optionally, the heating is quasi-isochoric, and the pressure rise in the nozzle is lower than the liquid-vapor phase change pressure at the HTL temperature. Optionally, the pressure rise is 10%, 20%, or 50% higher than the liquid-vapor phase change pressure at the HTL temperature.

[0142] The HTL is cooled by latent heat and isothermal expansion. After one or several cycles in the turbine, the HTL temperature drops and the HTL needs to be reheated. Optionally, the HTL is reheated with seawater in a heat exchanger (HTL heat exchanger in the diagram). Optionally, tap water or other liquids can also be used to heat the HTL. Optionally, the cold HTL leaves the HTL heat exchanger at a lower temperature and is used for refrigeration or air conditioning.

[0143] In the nozzle, LNG, liquefied hydrogen, ammonia, or other gases are optionally injected into the nozzle as a liquid. This requires an insulated LNG pipe to reach the mixing chamber as a liquid. This is illustrated in Figure 3 and described above. The liquefied gas flows through the insulated pipe and is injected into a narrow mixing chamber. The velocity of the HTL is optionally high enough to carry the LNG into an expanding cross-sectional area where pressure increases before the LNG vaporizes. In that section, the expanding cross-sectional area increases the pressure of the HTL. The LNG mixed with the HTL vaporizes and expands isothermally or quasi-isothermally. Optionally, the gas temperature upon exiting the nozzle is similar to the HTL temperature. Optionally, the LNG temperature, measured in Kelvin, is 1%, 10%, or 20% lower than the HTL temperature.

[0144] Optionally, the LNG is vaporized before being mixed with the HTL. Optionally, the LNG (in the liquid phase) is pre-compressed to the level of the LNG vapor pressure at the HTL temperature. Optionally, the LNG is pre-compressed to the pressure level of the gas in the existing pipe from the turbine. Optionally, this pressure is the desired gas pressure in the pipe, which can be 140 bar, 70 bar, 6 bar, or another value. Optionally, the gas is expanded isochorically or quasi-isochorically in the nozzle. Optionally, the pressure in the nozzle exceeds 10% of the vaporization pressure of the liquefied gas at the HTL temperature. Optionally, this value exceeds 20%, 50%, or 90%. Optionally, the nozzle does not have an expanding cross section after the mixing chamber.

[0145] Optionally, the desired gas pressure in the pipe is 140 bar, 70 bar, 40 bar, 6 bar, or any other value. Optionally, the difference between the LNG vapor pressure and the pipe pressure is converted to work by the isothermal expansion of the vaporized LNG in the nozzle. For this reason, the HTL turbine is optionally maintained at a pressure equal to or greater than the operating pressure of the pipe.

[0146] Figure 12 shows an impulse HTL gas turbine, including an HTL reservoir and an HTL pump that delivers HTL to the nozzle. Liquefied gas, such as hydrogen, flows as a liquid into the nozzle, where it mixes with the HTL, vaporizes, and expands isothermally. This accelerates the HTL, which then rotates the turbine and generates electricity.

[0147] Figure 13 shows a reaction turbine configuration in which LNG is fed into a rotating nozzle. The thrust produced by the nozzle drives an electric motor, generating electricity. The HTL returns to the drain and is sucked back into the turbine by centrifugal force. The level of HTL in the drain is lower than that of the nozzle to avoid collisions between the HTL and the turbine, but high enough to avoid discontinuities in the flow of HTL to the turbine.

[0148] Note that due to some insulation issues, some of the LNG will boil off as part of the transport and storage. This boil off gas (BOG) can be several percent of the total LNG volume. This BOG optionally enters the nozzle, mixes with the HTL, and expands isothermally within the nozzle.

Claims

1. 1. A method for converting heat to work, comprising: vaporizing or transitioning a liquid vapor phase change material (LVPhC) from a liquid phase to a vapor or supercritical phase at a temperature of about T1 and a pressure of about P1, and mixing in a nozzle with a heat transfer liquid (HTL) having a temperature of about T1 and a pressure of about P1, wherein the LVPhC is in the liquid phase at a temperature less than about T0 at a pressure of about P1, where T0 is less than T1, thereby causing a quasi-isothermal expansion, reducing the pressure to P0, and causing an acceleration of the HTL / LVPhC mixture; expelling the accelerated HTL / LVPhC mixture through a nozzle, converting its kinetic energy into work, and collecting the LVPhC and the HTL at a pressure of P0; The method further comprises, following the collecting, heating at least a portion of said HTL to a temperature of about T1 and increasing its pressure to a pressure of P1 to allow for an additional cycle of said mixing; further comprising: method.

2. 10. The method of claim 1, wherein said collecting said LVPhC vapor comprises separating said LVPhC / HTL mixture.

3. 3. The method of claim 1 or 2, wherein the liquefied LVPhC is liquefied natural gas (LNG).

4. The method of any one of claims 1 to 3, wherein the mixing and the vaporizing are performed simultaneously.

5. 5. The method of claim 3 or 4, wherein said collecting comprises directing the vented natural gas to a natural gas line for flow to a natural gas consumer.

6. 3. The method of claim 1 or 2, wherein the method further comprises, following the collecting, cooling the LVPhC and increasing its pressure to obtain liquefied LVPhC at a pressure of about P1 and a temperature of about T0 to allow for additional cycles of the mixing.

7. 7. The method of claim 6, wherein the cooling comprises passing the vaporized LVPhC through a heat exchanger to exchange heat with the liquefied LVPhC, the liquefied LVPhC entering the heat exchanger at an inlet temperature of about T0.

8. 8. The method of claim 7, wherein the passing comprises maintaining a majority of the liquefied LVPhC in a liquid phase.

9. 9. The method of any one of claims 6 to 8, wherein the cooling and increasing pressure comprises condensing the vaporized LVPhC before increasing its pressure.

10. 2. The method of claim 1, wherein the method further comprises, following the collecting, condensing the liquid and then passing it through a heat exchanger to exchange heat with the collected vaporized LVPhC to obtain thermally liquefied LVPhC, and the method further comprises increasing the pressure of the heated LVPhC to about P1.

11. The method of any one of claims 1 to 10, wherein the vaporizing comprises directing a portion of the collected HTL into heat exchange with the liquefied LVPhC.

12. The method of claim 11 , wherein the inducing occurs before the heating.

13. 13. The method of claim 11 or 12, wherein the increasing of the HTL pressure occurs before the inducing and the heating occurs after the inducing.

14. 10. The method of any one of claims 6 to 9, wherein following the cooling and pressurizing, the method further comprises heating the LVPhC from a temperature of about T0 to a temperature between T0 and T1 with an LVPhC heat source.

15. The method of any one of claims 1 to 14, wherein the mixing and vaporizing are performed simultaneously.

16. The method of any one of claims 1 to 15, wherein the HTL is selected from the list consisting of molten salt, hot oil, water, brine, ethylene glycol.

17. The method of any one of claims 1 to 16, wherein the HTL is ethylene glycol.

18. 18. The method of any one of claims 1 to 17, wherein the LVPhC material is selected from the list consisting of water, pentane, isobutane, propane, R134a, R245fa, fluorocarbons, and toluene.

19. 19. The method of any one of claims 1 to 18, wherein the LVPhC is pentane.

20. 20. The method of any one of claims 1 to 19, wherein the ejecting causes rotation of the nozzle, and the rotation of the nozzle causes the production of work from the kinetic energy.

21. The method of any one of claims 1 to 20, wherein the nozzle supports supersonic flow.

22. A method according to any preceding claim, wherein the turbine is a reaction turbine and the nozzle is connected to or is part of the reaction turbine.

23. 23. The method according to any one of claims 1 to 22, wherein the jet discharged from the nozzle is subjected to centrifugal force and directed to form a film flow.

24. 24. The method of any one of claims 1 to 23, wherein the vaporizing or transferring comprises transferring the LVPhC to a supercritical phase.

25. an evaporator for receiving a liquefied vapor phase change material (LVPhC) and vaporizing or transitioning the LVPhC to a vapor or supercritical phase at a pressure of about P1 and a temperature of about T1; a heating volume for heating a heat transfer liquid (HTL) to a temperature of about T1; a HTL pump for increasing the pressure of the HTL to about the P1 pressure; a nozzle having an inlet portion in fluid communication with the HTL pump and the evaporator for receiving the HTL, and a mixing portion for (i) allowing the HTL to mix with the LVPhC in a vapor phase at the temperature of about T1 and the pressure of about P1, and (ii) allowing the mixture to undergo isothermal expansion to a pressure of about P0, which is lower than the pressure P1, thereby causing acceleration of the mixture at the nozzle toward an outlet of the nozzle; a turbine configured to rotate as a result of the acceleration of the mixture, thereby converting the kinetic energy of the mixture into work; a separation unit for separating the exhausted HTL and the vaporized LVPhC, the separation unit comprising a collection unit capable of collecting the exhausted HTL and directing it to either the heated volume, the HTL pump, the nozzle, the evaporator, or any combination thereof; 1. A system for converting heat into work, comprising:

26. 26. The system of claim 25, wherein the liquefied LVPhC is liquefied natural gas (LNG).

27. 27. The system of claim 26, wherein the mixing section comprises the evaporator.

28. 28. The system of claim 26 or 27, wherein the separated vaporized natural gas is directed to a natural gas line for flowing the natural gas to a natural gas consumer.

29. 29. The system of any one of claims 25 to 28, comprising: (1) the separation unit for receiving the discharged vaporized LNG into a heat rejection section of a heat exchanger; (2) a source of LNG at a pressure of about P1 for receiving LNG at about P1 into a heat reception section of the heat exchanger; (3) the nozzle for flowing the LNG from the heat reception section to the nozzle; and (4) the heat exchanger in fluid communication with a natural gas pipe for flowing the LNG from the heat rejection section to the natural gas pipe.

30. a condenser for receiving the separated vaporized LVPhC and condensing it to a liquid state; an LVPhC pump downstream of the condenser for increasing the pressure of the condensed LVPhC; 26. The system of claim 25, further comprising:

31. 31. The system of claim 30, comprising: (1) the separation unit for receiving the discharged vaporized LVPhC into a heat rejection section of the heat exchanger; (2) a condenser for flowing the vaporized LVPhC discharged from the heat rejection section thereto; (3) the LVPhC pump for receiving the liquefied LVPhC discharged from the LVPhC pump into a heat receiving section of the heat exchanger; and (4) the heat exchanger in fluid communication with the evaporator for flowing the liquefied LVPhC discharged from the heat receiving section.

32. 31. The system of claim 30, comprising: (1) the separation unit for receiving the discharged vaporized LVPhC into a heat rejection section of the heat exchanger; (2) a condenser for flowing the vaporized LVPhC discharged from the heat rejection section thereto and receiving the liquefied LVPhC therefrom into a heat receiving section of the heat exchanger; and (3) an LVPhC pump for flowing the liquefied LVPhC discharged from the heat receiving section to the LVPhC pump, wherein the evaporator is configured to receive the liquefied LVPhC from the LVPhC pump, the heat exchanger being in fluid communication with the LVPhC pump.

33. The system of any one of claims 30 to 32, wherein the liquefied LVPhC received in the heat receiving section is discharged from the heat receiving section so that at least a majority of it is maintained in a liquid phase.

34. A system according to any one of claims 30 to 33, wherein the condenser comprises or part of the LVPhC pump.

35. 35. The system of claim 30, further comprising an LVPhC heat source downstream of the condenser for heating the LVPhC to a temperature less than or approximately equal to the vaporization temperature of the LVPhC at a pressure of about P1.

36. 36. The system of any one of claims 30 to 35, wherein the evaporator is in fluid communication with the collection unit for receiving at least a portion of the collected discharged HTL and exchanging heat with the liquefied LVPhC received at the evaporator, thereby vaporizing the liquefied LVPhC.

37. 37. The system of claim 36, wherein the evaporator is in fluid communication with the heated volume for flowing the HTL after heat exchange with the liquefied LVPhC in the evaporator.

38. 38. The system of claim 36 or 37, wherein the HTL pump is downstream of the nozzle and upstream of the evaporator.

39. 39. The system of claim 38, wherein a portion of the HTL is channeled from the HTL pump to the vaporizer and a portion of the HTL is channeled from the HTL to the nozzle.

40. The system according to any one of claims 30 to 39, wherein at least a part of the mixing section constitutes the evaporator.

41. The system of any one of claims 30 to 40, wherein the HTL is selected from the list consisting of molten salt, hot oil, water, brine, ethylene glycol.

42. The system of any one of claims 30 to 41, wherein the HTL is ethylene glycol.

43. 43. The system of any one of claims 30 to 42, wherein the LVPhC material is selected from the list consisting of water, pentane, isobutane, propane, R134a, R245fa, fluorocarbons, and toluene.

44. The system of any one of claims 30 to 43, wherein the LVPhC is pentane.

45. The condenser and the LVPhC pump a nozzle inlet for receiving a flow of a nozzle heat transfer liquid (HTL) into said nozzle, an outlet, and a fluid handling section disposed in cascade fluid communication with a suction compressible fluid inlet, said fluid handling section defining a flow path for said fluid; The arrangement is a first fluid-handling section downstream of the nozzle inlet and upstream of the second fluid-handling section, or a proximal end thereof constituting the nozzle inlet, the first fluid-handling section having a narrowing configuration in the direction of the flow path for reducing the pressure of the nozzle HTL flowing therethrough below the pressure of the suction fluid of the suction fluid source and accelerating the flow of the nozzle HTL, the first fluid-handling section being the LVPhC in a gas or vapor phase at a pressure of about P0; a second fluid-handling section having an expanding configuration in the direction of the flow path for receiving the nozzle HTL at a pressure lower than the pressure of the suction fluid, the suction fluid inlet configured to allow suction fluid communication between the surroundings or the suction fluid source and the second fluid-handling section, and to allow suction fluid to be introduced into the second fluid-handling section to mix with the nozzle HTL, thereby obtaining a fluid mixture, the expanding configuration of the second fluid-handling section designed to transition the two-phase mixture to supersonic velocity, at least at a distal end thereof; a third fluid manipulation section having a narrowing configuration in the direction of the flow path to decelerate the flow of the fluid mixture received from the second fluid manipulation section to sonic or subsonic speeds and to increase the pressure of the two-phase fluid mixture flowing along the third fluid manipulation section; a fourth fluid manipulation section configured to expand in the direction of the flow path and configured to increase the pressure of the subsonic flow of the fluid mixture received from the third fluid manipulation section to a pressure greater than ambient pressure; and a nozzle comprising a fluid handling section arrangement comprising: the outlet is downstream of or defined by a distal end of the fourth fluid-handling section and is for discharging the fluid mixture received from the fourth fluid-handling section, the fluid mixture discharged from the outlet comprising pressurized suction fluid; A system according to any one of claims 30 to 44.

46. 46. The system of claim 45, wherein the nozzle HTL contains at least one of water, molten salt, hot oil, ethylene glycol, molten metal, bicarbonate liquid, anti-icing liquid, liquefied gas, or any combination thereof.

47. 47. The system of claim 45 or 46, wherein the fluid mixture is a two-phase mixture and the pressurized suction fluid discharged from the outlet of the nozzle comprises compressed gas.

48. 48. The system of any one of claims 45 to 47, wherein the nozzle further comprises at least one conduit extending from an exterior thereof into the second fluid handling section and configured to channel the suction fluid into the mixing unit that enables mixing of the suction fluid with the HTL flowing therealong, reducing the speed of sound in the mixture below a flow velocity of the mixture, resulting in a supersonic flow.

49. 49. The system of any one of claims 45 to 48, wherein the third fluid handling section is configured to decelerate the fluid mixture flowing therealong so that it reaches the sonic or subsonic speed at an end of the third section.

50. The system of any one of claims 45 to 49, wherein the HTL and the suction fluid are the same material.

51. A system according to any one of claims 25 to 50, wherein the turbine is a reaction turbine.

52. 52. The system of claim 51, wherein the nozzle is coupled to or is part of the reaction turbine.

53. 53. The system of claim 51 or 52, wherein the collection unit defines a drain for accumulating the separated HTL, and wherein operation of the reaction turbine results in HTL being suctioned from the drain into the nozzle, thereby forming the HTL pump, and wherein the suction causes the HTL to flow into the nozzle at a pressure of about P1.

54. 54. The system of claim 53, comprising a second HTL pump disposed between the drain and the turbine so as to be capable of pressurizing the HTL independently of the HTL pump constituted by the reaction turbine.

55. 55. The system of any one of claims 25 to 54, wherein the separation unit comprises a curved or circular frame into which the mixture is discharged, and wherein engagement of the mixture with the curved or circular frame results in a film flow on a surface of the curved or circular frame.

56. 56. The system of any one of claims 25 to 55, wherein the evaporator is configured to receive a liquefied vapor phase change material (LVPhC) and transition it to a supercritical phase at a pressure of about P1 and a temperature of about T1.

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