A power generation system and method

Abstract

The application discloses a power generation system and method, and relates to the technical field of waste heat power generation. The power generation system comprises a mixing device, the mixing device is used for pretreating superheated fluid to obtain first state fluid; wherein the temperature of the first state fluid is lower than that of the superheated fluid; and a power generation module, the power generation module is used for heating working fluid by using the first state fluid to obtain steam, and generating power by using the steam. In this way, after the superheated fluid is pretreated, the superheat degree of the superheated fluid is reduced, so that the heat exchange efficiency is improved, and the problem that the heat exchange efficiency of the heat exchange technology in the prior art is low and the energy utilization efficiency is insufficient is solved. The power generation method adopts the above power generation system, and comprises the following steps: pretreating superheated fluid to obtain first state fluid; wherein the temperature of the first state fluid is lower than that of the superheated fluid; heating working fluid by using the first state fluid to obtain steam, and generating power by using the steam. In this way, the heat exchange efficiency and the energy utilization efficiency are improved.

Description

Technical Field

[0001] This application relates to the field of waste heat power generation technology, specifically to a power generation system and method. Background Technology

[0002] Waste heat is excess heat energy released during the production process. Most of the fluids that generate waste heat exist in a superheated state, meaning their current temperature is higher than the saturation temperature corresponding to the current pressure. The energy wasted in waste heat is enormous, and recovering and reusing it can save a significant amount of energy. Therefore, it is crucial to efficiently utilize waste heat resources to improve energy efficiency.

[0003] Currently, the most common technology for waste heat recovery and utilization is heat exchange technology. However, existing heat exchange technologies have low heat exchange efficiency, resulting in insufficient energy utilization efficiency. Summary of the Invention

[0004] This application provides a power generation system that reduces the superheat of a superheated fluid by pre-treating it with a mixing device, thereby improving heat exchange efficiency and solving the problem of low heat exchange efficiency in existing heat exchange technologies, which leads to insufficient energy utilization efficiency. This application also provides a power generation method that uses the above-mentioned power generation system to improve heat exchange efficiency and energy utilization efficiency.

[0005] This application provides a power generation system, including:

[0006] A mixing device for pre-treating a superheated fluid to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid.

[0007] A power generation module is used to heat a working fluid with the first-state fluid to obtain steam, and to generate electricity using the steam.

[0008] In some embodiments, the mixing device includes:

[0009] A first mixing inlet is used to input the superheated fluid;

[0010] The second mixing inlet is used to input the fluid in the second state.

[0011] A mixing outlet, wherein the mixing outlet is used to output the fluid in the first state;

[0012] The temperature of the second state fluid is lower than that of the superheated fluid, and the second state fluid and the superheated fluid are mixed in the mixing device to obtain the first state fluid.

[0013] In some embodiments, the mixing device is an ejector, and the pressure of the superheated fluid is greater than the pressure of the fluid in the second state.

[0014] In some embodiments, the power generation module includes an evaporator, an expansion device, a condenser, a generator, and a booster pump;

[0015] The evaporation device is connected to the mixing device, and the first state fluid heats the working fluid in the evaporation device to obtain the vapor;

[0016] The expansion device is connected to the evaporation device, and the steam is pressurized in the expansion device;

[0017] The generator is connected to the expansion device to drive power generation through the pressurized steam;

[0018] The condensing device is connected to the expansion device and the evaporating device to condense the vapor to obtain the working fluid, and to deliver the working fluid to the evaporating device.

[0019] The pressurizing pump is connected to the condensing device and the evaporating device, and is used to pressurize the working fluid.

[0020] In some embodiments, the power generation module includes:

[0021] The evaporation device includes a first evaporation inlet, a second evaporation inlet, and a second evaporation outlet; the first evaporation inlet is connected to the mixing outlet, the second evaporation inlet is connected to the pressurizing pump, and the second evaporation outlet is connected to the expansion device.

[0022] In some embodiments, the evaporation apparatus further includes a first evaporation outlet, which is in communication with the second mixing inlet.

[0023] In some embodiments, the power generation system further includes a booster device connected to the mixing device for outputting a second-state fluid to the mixing device;

[0024] The temperature of the second state fluid is lower than that of the superheated fluid, and the second state fluid and the superheated fluid are mixed in the mixing device to obtain the first state fluid.

[0025] In some embodiments, the pressurization device is connected to the evaporation device to allow the first-state fluid to flow through the evaporation device to form a third-state fluid;

[0026] The pressurizing device is connected to the evaporating device, and the third-state fluid forms the second-state fluid after passing through the pressurizing device.

[0027] In some embodiments, the power generation system further includes:

[0028] A separation device is disposed between the evaporation device and the pressurization device, the separation device being used to input at least a portion of the third-state fluid into the pressurization device.

[0029] In some embodiments, the superheated fluid is one or more of steam, nitrogen, carbon dioxide, hydrogen, carbon monoxide, oxygen, methanol, crude coal gas, and natural gas.

[0030] In some embodiments, the working fluid is one or more of R410a, R152a, R132, R290, R134a, R600a, R600, R601a, R123, R245fa, R1234yf, R1234ze, and ammonia.

[0031] Accordingly, this application also provides a power generation method, employing a power generation system as described in any of the above embodiments; comprising the following steps:

[0032] The superheated fluid is pretreated to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid.

[0033] The working fluid is heated by the fluid in the first state to obtain steam, and the steam is used to generate electricity.

[0034] In some embodiments, the step of pretreating the superheated fluid to obtain a first-state fluid includes:

[0035] A second-state fluid is obtained, the temperature of which is lower than the temperature of the superheated fluid;

[0036] The second-state fluid and the superheated fluid are mixed to obtain the first-state fluid.

[0037] In some embodiments, the step of heating the working fluid with the first-state fluid to obtain steam, and using the steam to generate electricity, includes:

[0038] The working fluid is heated using the fluid in the first state to obtain the vapor;

[0039] The pressurized steam is used to drive power generation;

[0040] The working fluid is obtained by condensing the vapor;

[0041] The working fluid is pressurized, and the steps of heating the working fluid using the first-state fluid to obtain the vapor are repeated.

[0042] In some embodiments, it also includes:

[0043] After the first-state fluid heats the working fluid, a third-state fluid is formed.

[0044] At least a portion of the third-state fluid is used as a reflux fluid, and the reflux fluid is pressurized to obtain the second-state fluid; the reflux flow rate of the reflux fluid is determined according to the following formula:

[0045]

[0046]

[0047]

[0048] Where Q1 is the heat load of the superheated fluid in the superheated section, c p1 t1 is the specific heat of the superheated fluid under superheated conditions, t2 is the flow rate of the superheated fluid, t3 is the temperature of the superheated fluid before cooling, t4 is the saturation temperature of the superheated fluid at the current pressure, t5 is the heat load of the superheated fluid in the mixing cooling section, t6 is the temperature of the superheated fluid after cooling, t7 is the return flow rate of the fluid in the third state, and q2 is the latent heat of vaporization of the fluid in the third state. The superheated section is the stage where the temperature of the superheated fluid is higher than the saturation temperature, and the mixing cooling section is the stage where the superheated fluid undergoes heat exchange and cooling.

[0049] Compared with the prior art, a power generation system according to an embodiment of this application includes: a mixing device for pre-treating a superheated fluid to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid; and a power generation module for heating a working fluid with the first-state fluid to obtain steam, and using the steam to generate electricity. Thus, by pre-treating the superheated fluid, the superheat of the superheated fluid is reduced, thereby improving heat exchange efficiency and solving the problem of low heat exchange efficiency in existing heat exchange technologies, leading to insufficient energy utilization efficiency.

[0050] Compared with the prior art, a power generation method according to an embodiment of this application, employing the aforementioned power generation system, includes: pre-treating a superheated fluid to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid; using the first-state fluid to heat a working fluid to obtain steam, and using the steam to generate electricity. This improves heat exchange efficiency and energy utilization efficiency. Attached Figure Description

[0051] To more clearly illustrate the technical solutions in the embodiments of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0052] Figure 1 A schematic diagram of a power generation system provided in this application embodiment. Figure 1 ;

[0053] Figure 2 A schematic diagram of a power generation system provided in this application embodiment. Figure 2 ;

[0054] Figure 3 A schematic diagram of a power generation system provided in this application embodiment. Figure 3 ;

[0055] Figure 4 A schematic diagram of a power generation system provided in this application embodiment. Figure 4 ;

[0056] Figure 5 Temperature entropy of a power generation system provided in this application embodiment Figure 1 ;

[0057] Figure 6 Temperature entropy of a power generation system provided in this application embodiment Figure 2 .

[0058] Reference numerals: 100-mixing device; 110-first mixing inlet; 120-second mixing inlet; 130-mixing outlet; 140-ejector; 200-power generation module; 210-evaporation device; 211-first evaporation inlet; 212-first evaporation outlet; 213-second evaporation inlet; 214-second evaporation outlet; 220-expansion device; 230-condensation device; 240-generator; 250-pressurization pump; 300-pressurization device; 400-separation device. Detailed Implementation

[0059] The technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of this application without creative effort are within the scope of protection of this application.

[0060] The applicant discovered that the superheated fluid used in existing heat exchange technologies is in a gaseous state. However, the heat transfer coefficient of gas is very low during the cooling process, resulting in excessively low heat exchange efficiency.

[0061] Therefore, the first embodiment of this application provides a power generation system, see [link to relevant documentation]. Figure 1 A schematic diagram of a power generation system provided in this application embodiment. Figure 1 ,Depend on Figure 1 It is known that the power generation system includes a mixing device 100 and a power generation module 200.

[0062] Specifically, the mixing device 100 is used to pre-treat the superheated fluid to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid; the power generation module 200 is used to heat the working fluid with the first-state fluid to obtain steam, and to generate electricity using the steam.

[0063] Specifically, superheated fluid refers to a fluid in a superheated state, characterized by its large volume due to its high temperature. The inventors of this application found in practical operation that directly using superheated fluid for heat exchange resulted in very low heat exchange efficiency due to its excessive volume. Therefore, by pre-processing the superheated fluid to reduce its volume, the temperature of the obtained first-state fluid is at or near its saturation temperature. Since the temperature of the first-state fluid is lower than that of the superheated fluid, its volume is correspondingly smaller, thus improving the heat exchange efficiency.

[0064] Specifically, the saturation temperature range of the superheated fluid is 50~500℃, and can be 50℃, 52℃, 54℃, 60℃, 70℃, 80℃, 100℃, 140℃, 200℃, 250℃, 300℃, 400℃, 490℃, 500℃, etc. The superheat range of the superheated fluid is 1~200℃, and can be 1℃, 3℃, 5℃, 7℃, 10℃, 15℃, 20℃, 30℃, 50℃, 100℃, 200℃, etc.

[0065] In one possible implementation, the mixing device 100 includes a first mixing inlet 110, a second mixing inlet 120, and a mixing outlet 130.

[0066] Specifically, the first mixing inlet 110 is used to input superheated fluid; the second mixing inlet 120 is used to input second-state fluid; and the mixing outlet 130 is used to output first-state fluid. The temperature of the second-state fluid is lower than that of the superheated fluid. The second-state fluid and the superheated fluid are mixed in the mixing device 100 to obtain the first-state fluid.

[0067] Thus, this application cools the superheated fluid by mixing the second-state fluid with the superheated fluid, thereby reducing the volume of the superheated fluid and improving the heat exchange efficiency of the first-state fluid.

[0068] Specifically, the fluid in the second state can have the same or different composition as the superheated fluid. When the composition is different from that of the superheated fluid, the cryogenic fluid does not react chemically with the original superheated fluid and does not affect the operation of the original device.

[0069] See Figure 2 A schematic diagram of a power generation system provided in this application embodiment. Figure 2 ,Depend on Figure 2 It is understood that, in one possible implementation, the mixing device 100 is an ejector 140, and the pressure of the superheated fluid is greater than the pressure of the fluid in the second state.

[0070] Specifically, due to the characteristics of the ejector, it can drive the flow of low-pressure fluid through high-pressure fluid, thereby enabling the flow of superheated fluid to drive the flow of fluid in the second state.

[0071] In one possible implementation, the power generation module 200 includes an evaporator 210, an expansion device 220, a condenser 230, a generator 240, and a pressure pump 250.

[0072] Specifically, the evaporator 210 is connected to the mixing device 100, and the first state fluid heats the working fluid in the evaporator 210 to obtain steam; the expansion device 220 is connected to the evaporator 210, and the steam is pressurized in the expansion device 220; the generator 240 is connected to the expansion device 220 to drive the generation of electricity through the pressurized steam; the condenser 230 is connected to the expansion device 220 and the evaporator 210 to condense the steam to obtain the working fluid, and to transport the working fluid to the evaporator 210; the pressurization pump 250 is connected to the condenser 230 and the evaporator 210 to pressurize the working fluid.

[0073] Specifically, the power generation module 200 undergoes heat exchange through the evaporation device 210, specifically, the working fluid exchanges heat with the first-state fluid. At this time, since the volume of the first-state fluid is significantly reduced compared to the volume of the superheated fluid, the heat exchange efficiency in the evaporation device 210 is greatly improved. The steam expands and pressurizes in the expansion device 220, then generates electricity using the generator 240, and subsequently condenses into a liquid working fluid through the condensation device 230. Finally, it is pressurized by the booster pump 250 and recirculated back into the evaporation device 210.

[0074] Specifically, the expansion device 220 is an axial flow turbine expander, a centrifugal turbine expander, a screw expander, a scroll expander, or a piston expander.

[0075] In one possible implementation, the evaporation device 210 includes a first evaporation inlet 211, a second evaporation inlet 213, and a second evaporation outlet 214; the first evaporation inlet 211 is connected to the mixing outlet 130, the second evaporation inlet 213 is connected to the pressurization pump 250, and the second evaporation outlet 214 is connected to the expansion device 220.

[0076] Specifically, the first state fluid enters the evaporation device 210 through the first evaporation inlet 211, the working fluid enters the evaporation device 210 through the second evaporation inlet 213, and is output from the second evaporation outlet 214 after heat exchange is completed.

[0077] In one possible implementation, the evaporation device 210 further includes a first evaporation outlet 212, which is connected to a second mixing inlet 120.

[0078] Specifically, after heat exchange, the temperature of the fluid in the first state is further reduced, and it can enter the second mixing inlet 120 through the first evaporation outlet 212, thereby exchanging heat with the superheated fluid again.

[0079] See Figure 3 A schematic diagram of a power generation system provided in this application embodiment. Figure 3 ;Depend on Figure 3 It is understood that, in one possible implementation, the power generation system further includes a booster device 300, which is connected to the mixing device 100 to output a second-state fluid to the mixing device 100; wherein, the temperature of the second-state fluid is lower than the temperature of the superheated fluid, and the second-state fluid and the superheated fluid are mixed in the mixing device 100 to obtain a first-state fluid.

[0080] Specifically, the pressurizing device 300 can pressurize the fluid in the second state before it enters the mixing device 100, thereby improving the mixing efficiency with the superheated fluid.

[0081] In one possible implementation, the pressurizing device 300 is connected to the evaporating device 210 to allow the first state fluid to flow through the evaporating device 210 and form a third state fluid; the pressurizing device 300 is connected to the evaporating device 210, and the third state fluid forms a second state fluid after passing through the pressurizing device 300.

[0082] Specifically, recycling at least a portion of the fluid from the third state after pressurization can improve mixing efficiency with superheated fluids and further enhance energy utilization.

[0083] See Figure 4 A schematic diagram of a power generation system provided in this application embodiment. Figure 4 ;Depend on Figure 4It is understood that, in one possible implementation, the power generation system further includes a separation device 400. The separation device 400 is disposed between the evaporation device 210 and the pressurization device 300, and the separation device 400 is used to input at least a portion of the third-state fluid into the pressurization device 300.

[0084] Specifically, the use of the separation device 400 can further control the volume of the refluxed third-state fluid. The superheat of the superheated fluid, the heat load of the superheated section, and the working fluid need to be determined first based on the pressure, temperature, and flow rate of the superheated fluid. The reflux flow rate of the third-state fluid is determined based on the superheat of the superheated fluid, the heat load of the superheated section, and the state of the third-state fluid, wherein the superheated section is the stage where the temperature of the superheated fluid is higher than the saturation temperature.

[0085] Specifically, the heat load of the superheated section is determined using the following formula:

[0086]

[0087] Where Q1 is the heat load of the superheated fluid in the superheated section, c p1 t1 is the specific heat of the superheated fluid under superheated conditions, m1 is the flow rate of the superheated fluid, t1 is the temperature of the superheated fluid before cooling, and t0 is the saturation temperature of the superheated fluid at the current pressure.

[0088] Specifically, the heat load for mixed cooling is determined using the following formula:

[0089]

[0090] Where Q2 is the heat load of the superheated fluid in the mixing and cooling section, c p1 t1 is the specific heat of the superheated fluid under superheated conditions, m1 is the flow rate of the superheated fluid, t1 is the temperature of the superheated fluid before cooling, t3 is the temperature of the superheated fluid after cooling, and t0 is the saturation temperature of the superheated fluid at the current pressure.

[0091] Specifically, the return flow rate of the fluid in the third state is determined according to the following formula:

[0092]

[0093] Where m2 is the return flow rate of the fluid in the third state, Q2 is the heat load of the superheated fluid in the mixing and cooling section, and q2 is the latent heat of vaporization of the fluid in the third state.

[0094] It is understandable that t1 in formula (1) is much higher than t0, and t3 in formula (2) is equal to or higher than t0. Only in this way can we ensure that the final Q2 is lower than or equal to Q1, that is, the waste heat medium is in a saturated temperature state or a slightly superheated state when it enters the evaporation device 210. It should be noted that t3 is a set temperature value, and preferably t3 is higher than t0 in the range of [0, 3].

[0095] In one possible implementation, the superheated fluid is one or more of steam, nitrogen, carbon dioxide, hydrogen, carbon monoxide, oxygen, methanol, crude coal gas, and natural gas.

[0096] In one possible implementation, the working fluid is one or more of R410a, R152a, R132, R290, R134a, R600a, R600, R601a, R123, R245fa, R1234yf, R1234ze, and ammonia.

[0097] Compared with existing technologies, a power generation system according to an embodiment of this application includes: a mixing device for pre-treating a superheated fluid to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid; and a power generation module for heating a working fluid with the first-state fluid to obtain steam, and using the steam to generate electricity. Thus, by pre-treating the superheated fluid, its volume is reduced, thereby improving heat exchange efficiency and solving the problem of low heat exchange efficiency in existing heat exchange technologies, leading to insufficient energy utilization efficiency.

[0098] Accordingly, the second embodiment of this application provides a power generation method, which employs a power generation system as described in any of the above-described possible embodiments;

[0099] The power generation method includes the following steps:

[0100] Step 101: Pre-treat the superheated fluid to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid.

[0101] Step 102: Use the first-state fluid to heat the working fluid to obtain steam, and use the steam to generate electricity.

[0102] In one possible implementation, step 101 includes:

[0103] Obtain the second-state fluid, whose temperature is lower than that of the superheated fluid;

[0104] The second-state fluid and the superheated fluid are mixed to obtain the first-state fluid.

[0105] In one possible implementation, step 102 includes:

[0106] Steam is obtained by heating the working fluid with a fluid in its first state.

[0107] Pressurized steam;

[0108] Power generation is driven by pressurized steam;

[0109] The process involves condensing the vapor to obtain the working fluid, and then reusing the first-state fluid to heat the working fluid to obtain vapor.

[0110] In one possible implementation, the power generation method further includes:

[0111] After the first-state fluid is heated by the working fluid, it forms a third-state fluid.

[0112] At least a portion of the fluid in the third state is used as the reflux fluid, and the reflux fluid is pressurized to obtain the fluid in the second state; the reflux flow rate of the reflux fluid is determined according to the following formula:

[0113]

[0114]

[0115]

[0116] Where Q1 is the heat load of the superheated fluid in the superheated section, c p1 t1 is the specific heat of the superheated fluid in its superheated state, t2 is the flow rate of the superheated fluid, t3 is the temperature of the superheated fluid before cooling, and t4 is the saturation temperature of the superheated fluid at the current pressure. Q2 is the heat load of the superheated fluid in the mixing and cooling section, t5 is the temperature of the superheated fluid after cooling, m2 is the return flow rate of the fluid in the third state, and q2 is the latent heat of vaporization of the fluid in the third state. The superheated section is the stage where the temperature of the superheated fluid is higher than the saturation temperature, and the mixing and cooling section is the stage where the superheated fluid undergoes heat exchange and cooling.

[0117] Specifically, see Figure 5 Temperature entropy of a power generation system provided in this application embodiment Figure 1 The superheated fluid enters the system from state H0, first mixing with a portion of the fluid from state H3 (now pressurized to state H4) until saturation, then releasing heat according to the process from state H1 to H2 to H3. The working fluid, after endothermic evaporation (processes 1-2-3), becomes vapor; after expansion and work (processes 3-4), its pressure decreases; after cooling and condensation (processes 4-5-6), it becomes liquid; and after pressurization (process 6-1), it reabsorbs heat from the saturated superheated fluid. See also... Figure 6 Temperature entropy of a power generation system provided in this application embodiment Figure 2 ,and Figure 5 The difference is that the superheated fluid is a single fluid in this case.

[0118] Compared with the prior art, a power generation method according to an embodiment of this application, employing the aforementioned power generation system, includes: pre-treating a superheated fluid to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid; using the first-state fluid to heat a working fluid to obtain steam, and using the steam to generate electricity. This improves heat exchange efficiency and energy utilization efficiency.

[0119] The above provides a detailed description of a power generation system and method provided in the embodiments of this application. Specific examples have been used to illustrate the principles and implementation methods of this application. The description of the above embodiments is only for the purpose of helping to understand the technical solutions and core ideas of this application. Those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. These modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this application.

Claims

1. A power generation system, characterized in that, include: A mixing device (100), which is an ejector (140), is used to pre-treat superheated fluid to obtain a first-state fluid. The ejector (140) includes a first mixing inlet (110), a second mixing inlet (120), and a mixing outlet (130). The first mixing inlet (110) is used to input the superheated fluid, the second mixing inlet (120) is used to input a second-state fluid, and the mixing outlet (130) is used to output the first-state fluid. The temperature of the second-state fluid is lower than the temperature of the superheated fluid. The second-state fluid and the superheated fluid are mixed in the ejector (140) to obtain the first-state fluid, wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid. A power generation module (200) is used to heat a working fluid with a first state fluid to obtain steam, and to generate electricity with the steam. The power generation module (200) includes an evaporation device (210) which is connected to the ejector (140). The first state fluid heats the working fluid in the evaporation device (210) to obtain the steam. The evaporation device (210) includes a first evaporation inlet (211) and a first evaporation outlet (212). The first evaporation inlet (211) is connected to the mixing outlet (130), and the first evaporation outlet (212) is connected to the second mixing inlet (120). The power generation system further includes a booster device (300), which is connected to the ejector (140) to output a second state fluid to the ejector (140). The booster device (300) is also connected to the evaporator (210) to allow the first state fluid to flow through the evaporator (210) to form a third state fluid. After passing through the booster device (300), the third state fluid forms the second state fluid.

2. The power generation system as described in claim 1, characterized in that, The pressure of the superheated fluid is greater than the pressure of the fluid in the second state.

3. The power generation system as described in claim 1, characterized in that, The power generation module (200) also includes an expansion device (220), a condensation device (230), a generator (240), and a pressure pump (250). The expansion device (220) is connected to the evaporation device (210), and the steam is pressurized in the expansion device (220); The generator (240) is connected to the expansion device (220) to drive the generation of electricity through the pressurized steam; The condensing device (230) is connected to the expansion device (220) and the evaporating device (210) to condense the vapor to obtain the working fluid and to deliver the working fluid to the evaporating device (210). The pressurizing pump (250) is connected to the condensing device (230) and the evaporating device (210) to pressurize the working fluid.

4. The power generation system as described in claim 3, characterized in that, The evaporation device (210) includes a second evaporation inlet (213) and a second evaporation outlet (214); the second evaporation inlet (213) is connected to the pressurization pump (250), and the second evaporation outlet (214) is connected to the expansion device (220).

5. The power generation system as described in claim 1, characterized in that, The power generation system also includes: A separation device (400) is disposed between the evaporation device (210) and the pressurization device (300), the separation device (400) being used to input at least a portion of the third-state fluid into the pressurization device (300).

6. The power generation system as described in claim 1, characterized in that, The superheated fluid is one or more of the following: steam, nitrogen, carbon dioxide, hydrogen, carbon monoxide, oxygen, methanol, crude coal gas, and natural gas.

7. The power generation system as described in claim 1, characterized in that, The working fluid is one or more of R410a, R152a, R132, R290, R134a, R600a, R600, R601a, R123, R245fa, R1234yf, R1234ze, and ammonia.

8. A method for generating electricity, characterized in that, The power generation system as described in any one of claims 1-7 is adopted; The power generation method includes the following steps: The superheated fluid is pretreated to obtain a first-state fluid; wherein the temperature of the first-state fluid is lower than the temperature of the superheated fluid. The working fluid is heated by the fluid in the first state to obtain steam, and the steam is used to generate electricity.

9. The power generation method as described in claim 8, characterized in that, The step of pretreating the superheated fluid to obtain the first-state fluid includes: A second-state fluid is obtained, the temperature of which is lower than the temperature of the superheated fluid; The second-state fluid and the superheated fluid are mixed to obtain the first-state fluid.

10. The power generation method as described in claim 9, characterized in that, The step of heating the working fluid with the first-state fluid to obtain steam, and then using the steam to generate electricity, includes: The working fluid is heated using the fluid in the first state to obtain the vapor; The pressurized steam is used to drive power generation; The working fluid is obtained by condensing the vapor; The working fluid is pressurized, and the steps of heating the working fluid using the first-state fluid to obtain the vapor are repeated.

11. The power generation method as described in claim 10, characterized in that, Also includes: After the first-state fluid heats the working fluid, a third-state fluid is formed. At least a portion of the third-state fluid is used as a reflux fluid, and the reflux fluid is pressurized to obtain the second-state fluid; the reflux flow rate of the reflux fluid is determined according to the following formula: Wherein, Q1 is the heat load of the superheated fluid in the superheated section, cp1 is the specific heat of the superheated fluid in the superheated state, m1 is the flow rate of the superheated fluid, t1 is the temperature of the superheated fluid before cooling, and t0 is the saturation temperature of the superheated fluid at the current pressure; Q2 is the heat load of the superheated fluid in the mixing cooling section, t3 is the temperature of the superheated fluid after cooling, m2 is the return flow rate of the fluid in the third state, and q2 is the latent heat of vaporization of the fluid in the third state; the superheated section is the stage where the temperature of the superheated fluid is higher than the saturation temperature, and the mixing cooling section is the stage where the superheated fluid undergoes heat exchange and cooling.

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