Systems and methods for heat utilization in nature

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Systems and methods for utilizing heat in nature – We welcome guidance and corrections from everyone. Title: Systems and Methods for Utilizing Heat in Nature. Abstract: Nature is abundant with unlimited sources of ambient temperature energy, such as air, seawater, and geothermal heat, all of which hold great potential for exploitation. The present invention provides a system and method for utilizing heat from nature. The said device includes a drive unit and heat exchange equipment, wherein the drive unit comprises a compressor, an expander, and valves for controlling the pressure of the compressor and the expander ； The heat exchange equipment mentioned includes heat exchangers for process heat exchange, as well as heat exchangers for absorbing heat from the environment. The method involves: the compressor raising the pressure of the gas working medium; during this pressure increase, the temperature of the gas working medium rises as well. The gas with the increased temperature passes through a heat exchanger, where it transfers heat to a third-party liquid working medium, thereby enabling the vaporization and superheating of that liquid medium, resulting in superheated gas from the third-party medium. The cooled gas working medium then passes through a second expansion machine, where it does work and its pressure decreases while its temperature also drops. The temperature of the gas at the exit of the second expansion machine is kept below the temperature of the natural heat source used for heat extraction, thus allowing for the utilization of heat from that natural heat source. The gas exiting the second expansion machine then returns to the compressor, completing the cycle of the working medium ； The vaporized and superheated third-party gas medium enters the first expansion machine to perform work through expansion. The third-party medium at the exit of the first expansion machine is condensed into a liquid, forming a third-party liquid medium. This liquid medium is then pressurized using a pump, and it exchanges heat with the medium at the exit of the compressor, thereby being vaporized and superheated, thus completing the cycle of the third-party medium. Complete the absorption and utilization of heat from nature. The compressor and the expander form a drive unit that generates mechanical energy, which is used to power machinery. It is suitable for driving generators to produce electricity, enabling ships to navigate, vehicles to move, and airplanes to fly. The core of this invention lies in making use of the heat from natural sources such as air, seawater, or geothermal energy; it is also applicable to the recovery and utilization of low-temperature waste heat from factories, thereby enabling the clean use of energy. If applied to factory cooling processes and urban central air conditioning systems, its benefits will be significantly enhanced. Technical Field: The present invention belongs to the field of energy utilization, and relates to methods for utilizing heat from nature. In particular, it concerns the use of heat from natural sources such as air, seawater, or geothermal energy, and it is also applicable to the recovery and utilization of low-temperature waste heat from factories. Background Technology: The resources available to humanity in the field of energy utilization include solar energy, wind energy, ocean tidal energy, and hydroelectric power from rivers; fossil fuels such as oil, natural gas, and coal; as well as nuclear energy derived from nuclear fission and nuclear fusion. Although solar energy, wind energy, ocean tidal energy, and river hydroelectric power are clean sources, they are ultimately limited, and they can disrupt the natural state of the environment ； Fossil fuels such as oil, natural gas, and coal all contribute to rising global temperatures, air pollution, and an increase in the level of carbon dioxide, a greenhouse gas, in the atmosphere ； The energy from nuclear fission and nuclear fusion will cause the Earth’s temperature to rise. Summary of the invention: The objective of this invention is to provide a system and method for utilizing heat from nature, offering humanity a new way of harnessing energy. The technical concept of this invention is that mediums such as air, seawater, or geothermal heat in nature are extremely abundant and all possess a certain temperature; the energy that can be released during their cooling process is enormous. If utilized effectively, it will surely replace the current methods of energy use, and it will also help to lower rather than raise the Earth’s temperature. (1) A compressor is used to increase the pressure of the gas medium; as the pressure of the gas medium rises, its temperature also increases accordingly ； (2) The high-temperature gas working fluid exchanges heat with a third-party liquid working fluid through a heat exchanger, resulting in superheated gas of the third-party liquid working fluid, while its own temperature is reduced ； (3) The cooled high-pressure gas refrigerant enters the second expander to expand and do work; as its pressure decreases, its temperature also drops, with its temperature being kept below that of the natural heat source material used for heat extraction ； (4) The fluid at the exit of the first expansion machine undergoes heat exchange with a natural heat source selected for heat utilization through a heat exchanger; this process lowers the temperature of the natural heat source while raising the temperature of the fluid itself ； (5) After absorbing heat and its temperature rising, the gas refrigerant enters the compressor, completing the cycle of the refrigerant ； (6) The gas obtained after vaporization and superheating of the third-party liquid working fluid enters the first expander to expand and perform work ； (7) The third-party working fluid at the exit of the first expansion machine exchanges heat with the working fluid at that exit, and condenses into a liquid of the third working fluid ； (8) The condensed third-party liquid working medium enters the liquid storage tank ； (9) The third-party liquid fluid at the outlet of the liquid storage tank is pumped to an elevated pressure and sent to the evaporation heat exchanger and the superheating heat exchanger, where it exchanges heat with the fluid at the compressor outlet, resulting in a superheated gas of the third-party fluid, thus completing the circulation of this fluid ； Key to control: The temperature of the gas refrigerant at the compressor outlet must meet the requirements for the vaporization and superheating of the third-party liquid refrigerant ； The working fluid at the outlet of the first expander is near the critical state, in order to reduce the heat consumption during the condensation process and to increase the utilization of heat from natural heat sources ； The temperature at the outlet of the second expander must be lower than the temperature of the natural heat source material selected. During this process, the heat from natural heat sources is used to generate the power required for the expansion of the expander. The compressor and the expander together form a drive unit that produces mechanical energy, which can be used to power various machinery. This energy can be utilized to operate generators for electricity production, as well as to propel ships, vehicles, and aircraft. The use of this energy in generating electricity is also suitable for cooling processes in factories and urban central air conditioning systems, thereby enhancing overall efficiency. The technical solution of this invention is as follows (see Figure 1): The gas working medium has its pressure increased by a compressor, which raises its temperature; the temperature is then controlled to meet the requirements for superheating during the vaporization of the third-party working medium ； The high-pressure, high-temperature working fluid supplies heat to a third-party liquid fluid, which is used for the vaporization and superheating of that liquid fluid ； The high-pressure working fluid expands through the second expansion machine to perform work, and its temperature is controlled to be lower than that of the selected natural heat source material ； The superheated third-party gas working fluid expands through the first expander to perform work ； The fluid at the outlet of the second expander is heated by the heat source from nature and by the third fluid coming from the outlet of the first expander, as a result of which its temperature rises; meanwhile, the temperature of the heat source from nature decreases and the third fluid condenses into a liquid ； The heated working fluid is fed into the compressor inlet to complete the cycle ； The liquid of the third-party working fluid enters the storage tank; the third-party liquid working fluid output from the tank is pressurized by a pump, vaporized, and superheated to complete the circulation of this working fluid ； Complete the absorption and utilization of heat from natural heat sources. a. The gas working fluid (01) is pressurized by the compressor (J1); the pressure is controlled via valve (F1), thereby indirectly regulating its temperature to meet the requirements for the vaporization and superheating of the third-party working fluid, resulting in gas working fluid (02) ； b. The gas medium (03) passing through valve (F1) is cooled by heat exchangers (E1), (E2) to form gas medium (05); c. The third-party liquid medium (13) is vaporized into saturated steam (14) by heat exchanger (E2) and heated to become superheated steam (15) by (E1), resulting in the third-party gas medium (15). The flow rate of the third-party liquid working medium (13) DE is controlled by valve (F4), thereby regulating the temperature of the third-party gas working medium (15); the pressure of the third-party gas working medium (15) is controlled by valve (F5), which in turn indirectly brings the working medium at the outlet of the first expander (J2) to a subcritical state close to the critical condition (with temperatures and pressures close to, but below, the critical point) ； d. The cooled gas fluid (05) enters the second expander (J3); the pressure of fluid (06) is controlled via valve (F2), thereby indirectly ensuring that the temperature of fluid (06) remains below the temperature of the selected natural heat source material ； e. The fluid (06) at the outlet of the second expander (J3) has its flow rate controlled (07) by valve (F3); it passes through heat exchanger (E3) to supply cooling energy to the third fluid (17) at the outlet of the first expander (J2), thereby condensing the third liquid fluid to produce liquid form of that fluid (18) ； Part (08) is heated by a selected natural heat source material through the heat exchanger (E4), raising the temperature of the working fluid at the outlet of the second expander (J3). The heated working fluid at the exits of heat exchangers (E3) and (E4) merges to form gas fluid (11), which is then fed into the inlet of compressor (J1), completing the circulation of the working fluid ； f. The third-party liquid working fluid enters tank (V); the third-party liquid working fluid discharged from the bottom of tank (V) is pumped by pump (P) to be pressurized and sent to heat exchanger (E2) for vaporization, as well as to heat exchanger (E1) for superheating, thus completing the circulation of the third-party working fluid ； g. The pressure of the working fluid at the compressor inlet (01) is controlled by the supply or discharge through valve (F6) ； h. The compressor (J1), the first expander (J2), and the second expander (J3) together form a drive unit that generates mechanical energy to power the machinery (E) in operation ； I. The heat exchanger (E4) absorbs heat from natural heat sources. To make the most of the heat from natural heat source materials, the key to control is to keep the working fluid at the exit of the expander (J2) in a subcritical state (with temperature and pressure close to, but below, the critical point). Description of the drawings: The following examples are provided to illustrate the present invention, but are not intended to limit its scope of application. 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present invention, which should not be construed as a limitation of the present invention. The relevant equipment names in Figure 1 are defined as follows to make the description clearer.: Device name: J1: Compressor J2: First expander J3: Second expander E1: Heat exchanger E2: Evaporator E3: Condenser E4: Heat exchanger F1: Compressor outlet pressure control valve F2: Second expander outlet pressure control valve F3: Flow control valve F4: Flow control valve F5: Pressure control valve F6: Compressor inlet pressure control valve V: Third-party liquid process Quality storage tank P: Third-party liquid working medium pressure lift pump E: Driven machinery Specific embodiments The present invention will be further described below in conjunction with the drawings and examples. The key is to select a substance with critical low temperature and low pressure as the third-party working medium. In this embodiment, carbon dioxide is selected as the working medium and the third-party working medium. The inaccuracy of the data in the embodiment does not constitute a limitation on the present invention. 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P/i62KKAMjw9b3cUV9LeWptXubx5liZ1YhSFAyVJHateiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAo oooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAoo ooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooo oAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigAooooAKKKKACiiigD/9k= Figure 2 The gas carbon dioxide (01) at 1000Kmol/hour, 15℃, 0.51795Mpa enters the compressor (J1). The valve (F1) controls the pressure of the carbon dioxide (02) at the outlet of the compressor (J1) to be 5.39Mpa. During the process, the temperature of the gas carbon dioxide at the compressor outlet increases to 228 ℃ ； Through valve (F1), carbon dioxide (03) passes through heat exchangers E1 and E2 for heat exchange; due to flow resistance, its pressure and temperature decrease, resulting in carbon dioxide gas (05) with a pressure of 5.35 Mpa and a temperature of 45°C ； Gas carbon dioxide (05) at a flow rate of 1000 Kmol/h, at a temperature of 45°C and a pressure of 5.35 Mpa enters the second expander (J3) to perform work through expansion. The pressure of carbon dioxide (06) at the outlet of the expander (J3) is controlled by valve (F2) and is 0.53795 Mpa; the corresponding equivalent temperature is calculated to be -111°C. In reality, this carbon dioxide is in a saturated state with both gas and liquid phases present, and the actual temperature corresponds to the saturation temperature of carbon dioxide at 0.53795 Mpa, which is -55.75°C. The proportion of liquid carbon dioxide is 11.63%, and this liquid content is determined by the temperature and pressure of carbon dioxide at the inlet of the second expander (J3) ； The carbon dioxide (06) at the outlet of the second expander (J3) is divided into two streams; one stream (07) passes through the heat exchanger (E3), with its flow rate controlled by valve (F3), thereby keeping the carbon dioxide (17) at the outlet of the first expander in a subcritical state of 31°C and 7.06 Mpa (temperature and pressure close to, but below, the critical values) ； Along the way, it passes through heat exchanger (E4), where it is heated by natural heat sources; the carbon dioxide gas that has passed through heat exchanger (E3) (09) merges with the carbon dioxide gas that has passed through heat exchanger (E4) (10) at point (11). At a temperature of 30°C from the natural heat sources, the temperature of carbon dioxide gas (11) is 15°C, with a pressure of 0.51795 Mpa. The heated carbon dioxide gas (11) is regulated through the supply or discharge control via valve (F6), thereby controlling the pressure (01) of the carbon dioxide gas entering compressor (J1), which in turn completes the cycle ； The heat from the heat exchangers (E1) and (E2) during this process is equivalent to the vaporization and superheating of 1212 Kmol of liquid carbon dioxide ； The liquid carbon dioxide (18) at 31°C and 7.06 Mpa, which is condensed in the heat exchanger (E3), enters the liquid carbon dioxide storage tank (V); the liquid carbon dioxide (19) discharged from the tank (V) is pressurized to 26.2 Mpa using a pump ； The liquid carbon dioxide (12) after being pumped to a higher pressure has its flow rate controlled by valve (F4) at 1212 Kmol/h; it is vaporized in heat exchanger (E1) and then superheated in heat exchanger (E2). The pressure of the superheated carbon dioxide gas (15) is controlled by valve (F5) at 25.8 Mpa, while its temperature is controlled by valve (F4) at 165℃ ； The superheated carbon dioxide gas (16) passes through valve (F5) and enters the first expander to do work through expansion ； The carbon dioxide (17) at 1212 Kmol/hour, 7.06 Mpa, and 31°C exiting the expander (J2) is condensed to liquid carbon dioxide (18) at 7.06 Mpa and 31°C through the heat exchanger (E3), and then enters the liquid carbon dioxide storage tank (V), thus completing the cycle ； Carbon dioxide (08) at 0.53795 Mpa, -55.75°C, and containing 11.63% liquid at the exit of the expander (J3) passes through the heat exchanger (E4), where it is heated by a natural heat source at 30°C, absorbing 3195668 KJ per hour of heat ； During the process, the expander (J1) requires 7,489,360 KJ/hour of energy input; the first expander outputs 6,441,161 KJ/hour of energy, while the second expander outputs 4,419,105 KJ/hour of energy. The pump (P) needs 82,213 KJ/hour of energy input. Theoretically, the drive unit composed of the compressor (J1), the first expander (J2), and the second expander (J3) can deliver 3,195,668 KJ/hour of energy, which corresponds to a power output of 887 KW. The key to control: Keep the carbon dioxide at the outlet of the first expander (J2) in a subcritical state (with temperature and pressure close to, but below, the critical point), thereby reducing the heat released during its condensation into a liquid. This allows the heat exchanger (E4) to absorb more heat from natural heat sources. The heat absorbed by the heat exchanger (E4) from the natural environment is converted into mechanical energy output by the expander (J2), which can be used to drive machinery. It is suitable for powering generators to produce electricity, enabling ships to navigate, vehicles to move, and airplanes to fly. The process of using this energy to drive generators is applicable to factory cooling systems and urban central air conditioning systems, thereby expanding its benefits.