CN114575951B - Organic Rankine two-stage flash evaporation circulating system with gas-liquid injector - Google Patents
Organic Rankine two-stage flash evaporation circulating system with gas-liquid injector Download PDFInfo
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04F—PUMPING OF FLUID BY DIRECT CONTACT OF ANOTHER FLUID OR BY USING INERTIA OF FLUID TO BE PUMPED; SIPHONS
- F04F5/00—Jet pumps, i.e. devices in which flow is induced by pressure drop caused by velocity of another fluid flow
- F04F5/14—Jet pumps, i.e. devices in which flow is induced by pressure drop caused by velocity of another fluid flow the inducing fluid being elastic fluid
- F04F5/16—Jet pumps, i.e. devices in which flow is induced by pressure drop caused by velocity of another fluid flow the inducing fluid being elastic fluid displacing elastic fluids
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Abstract
The invention provides an organic Rankine double-stage flash evaporation circulating system with a gas-liquid ejector, which comprises an evaporator, a gas-liquid separator, a flash tank, a high-pressure expander, a low-pressure expander, a condenser, the gas-liquid ejector, a working medium pump, a first mixer, a second mixer, a first generator and a second generator. The invention realizes the full recovery and utilization of the medium-low grade heat energy; the aim of pressurizing the working medium is fulfilled under the condition of not consuming mechanical work, and a working medium pump at the outlet of the condenser is replaced, so that the power consumption of the working medium pump is effectively reduced; the expansion work amount sacrificed by injection is reduced to the greatest extent, so that the net output work amount of the system is increased.
Description
Technical Field
The invention relates to the technical field of organic Rankine flash evaporation cycle power generation, in particular to an organic Rankine double-stage flash evaporation cycle system with a gas-liquid injector.
Background
The distribution characteristics of clean energy in China are large total amount, multiple types and wide distribution, but most of clean energy is a medium-low temperature heat source, so that the development of a medium-low temperature resource utilization technology becomes urgent.
In order to efficiently utilize the low-temperature heat source, a low-grade primary energy or industrial waste heat, waste heat and the like are often converted into high-grade electric energy by combining a thermal power conversion technology. Among the thermal power conversion technologies, the organic Rankine cycle is one of the medium and low temperature resource utilization technologies with the most application prospect. However, as the power generation scale of the organic rankine cycle is reduced to adapt to local medium-low temperature resources, the size of each component of the system is reduced, the efficiency of a single machine is reduced, and the power consumption of a working medium pump is large, which can occupy more than half of the power output of an expander at most, so how to effectively reduce the power consumption of the working medium pump has become a key problem for improving the performance of the organic rankine cycle system. In the prior art, an organic Rankine two-stage flash evaporation circulation system which utilizes the boosting characteristic of a gas-liquid injector to reduce the power consumption of a working medium pump and improve the power generation performance of the system is needed.
Disclosure of Invention
In view of the above, the present invention aims to provide an organic rankine two-stage flash circulation system with a gas-liquid ejector.
The technical scheme for solving the technical problems is as follows:
an organic Rankine two-stage flash circulation system with a gas-liquid injector comprises an evaporator, a gas-liquid separator, a flash tank, a high-pressure expander, a low-pressure expander, a condenser, the gas-liquid injector, a working medium pump, a first mixer, a second mixer, a first generator and a second generator, wherein a working medium outlet of the evaporator is communicated with an inlet of the gas-liquid separator, a gaseous working medium outlet of the gas-liquid separator is communicated with an inlet of the high-pressure expander, and a liquid working medium outlet of the gas-liquid separator is communicated with an inlet of the flash tank; one part of the gaseous working medium outlet of the flash tank is communicated with the inlet of the low-pressure expander, the other part of the gaseous working medium outlet of the flash tank is communicated with the steam nozzle inlet of the gas-liquid injector, and the liquid working medium outlet of the flash tank is communicated with the inlet of the working medium pump; the high-pressure expander expands to do work to drive the first generator, and an outlet of the high-pressure expander is communicated with the first mixer; the expansion work of the low-pressure expansion machine drives the second generator, and the outlet of the low-pressure expansion machine is communicated with the first mixer; the first mixer is also communicated with a working medium inlet of the condenser; the working medium outlet of the condenser is communicated with the liquid nozzle inlet of the gas-liquid injector, and the cooling water inlet and the cooling water outlet of the condenser are connected with an external cooling water source; the outlet of the gas-liquid injector is communicated with the second mixer; the second mixer is also communicated with an outlet of the working medium pump; the second mixer is communicated with a working medium inlet of the evaporator; the heat source inlet of the evaporator is connected with the low-temperature heat source, and the heat source outlet of the evaporator is connected with the discharge position of the low-temperature heat source.
The control method of the organic Rankine two-stage flash evaporation circulation system comprises the following steps:
starting a medium-low temperature heat source, enabling the medium-low temperature heat source to enter a heat source inlet of an evaporator, exchanging heat with a liquid organic working medium in the evaporator, and enabling the working medium to undergo an incomplete evaporation process in the evaporator, wherein the liquid organic working medium is changed into a gas-liquid two-phase organic working medium; the medium-low temperature heat source after heat exchange flows out from a heat source outlet of the evaporator 1;
the gas-liquid two-phase organic working medium flows out from a working medium outlet of the evaporator and enters a gas-liquid separator to realize gas-liquid separation; the separated gaseous organic working medium flows out from a gaseous working medium outlet of the gas-liquid separator, enters a high-pressure expander to expand and apply work, and drives a first generator to generate electricity; the separated liquid organic working medium flows out from a liquid working medium outlet of the gas-liquid separator and enters a flash tank for flash evaporation;
after the liquid organic working medium obtained by separation in the gas-liquid separator is subjected to gas-liquid separation in the flash tank, the obtained gaseous organic working medium is divided into two parts, one part enters a low-pressure expansion machine to expand and do work so as to drive a second generator to generate power, and the other part enters a steam nozzle of a gas-liquid ejector; meanwhile, after the liquid organic working medium obtained by separation in the gas-liquid separator is subjected to gas-liquid separation in the flash tank, the obtained liquid working medium enters a working medium pump; the exhaust steam of the high-pressure expander and the exhaust steam of the low-pressure expander enter a first mixer to be mixed, and a gaseous organic working medium obtained by mixing in the first mixer enters a condenser;
the gaseous organic working medium flowing out of the high-pressure expander and the low-pressure expander exchanges heat with cooling water entering the condenser from the outside, the low-temperature cooling water after heat exchange is changed into high-temperature cooling water, and the high-temperature cooling water flows out of a cooling water outlet of the condenser; condensing the gaseous organic working medium after heat exchange into a saturated liquid organic working medium, flowing out from a working medium outlet of a condenser, and entering a liquid nozzle of a gas-liquid injector;
in the gas-liquid injector, the gaseous organic working medium obtained after gas-liquid separation in the flash tank is used as working fluid and passes through the steam nozzle at high speed, and meanwhile, the low-temperature low-pressure liquid flowing out from the working medium outlet of the condenser is used as injection fluid and is subjected to acceleration and depressurization through the liquid nozzle; the working fluid and the injection fluid are mixed in a mixing chamber of the gas-liquid injector through a steam nozzle outlet and a liquid nozzle outlet respectively; the obtained mixed fluid is diffused in a diffusion chamber of the gas-liquid injector and then enters the second mixer; simultaneously, the organic working medium pressurized to the evaporating pressure by the working medium pump enters the second mixer;
the two parts of fluid are mixed in the second mixer and then enter the evaporator to complete circulation.
Compared with the prior art, the invention has the beneficial effects that:
1. the device is provided with a gas-liquid separator and a flash tank, and vapor obtained by incomplete evaporation of the evaporator is subjected to a gas-liquid separation process and a flash evaporation process in sequence, so that vapor capable of acting is obtained, and full recovery and utilization of medium-low grade heat energy are realized.
2. The device is provided with a gas-liquid injector, part of high-temperature high-pressure gaseous working medium at the gaseous working medium outlet of the flash tank enters a steam nozzle of the gas-liquid injector, a low-pressure zone is formed at supersonic speed at the outlet of the steam nozzle, so that the low-temperature low-pressure liquid working medium at the working medium outlet of the condenser is ejected to enter the liquid nozzle of the gas-liquid injector, and the two parts of fluid sequentially undergo a mixing process, a condensation shock wave process and a diffusion process, so that the pressure of the mixed fluid at the outlet of the gas-liquid injector is increased to exceed the pressure of the gas from the flash tank, the aim of pressurizing the working medium is fulfilled under the condition of not consuming mechanical work, and a working medium pump at the outlet of the condenser is replaced, thereby effectively reducing the work consumption of the working medium pump.
3. The gaseous working medium outlet of the flash tank is split, steam necessary for normal operation of the gas-liquid ejector is sent to the steam nozzle by controlling the flow ratio, and the residual steam is sent to the low-pressure expander for expansion work, so that the expansion work amount sacrificed by injection is reduced to the greatest extent, and the net output work amount of the system is increased.
Drawings
FIG. 1 is a schematic diagram of a system according to an embodiment of the present invention.
The figure shows: 1-an evaporator; 2-a gas-liquid separator; 3-a flash tank; 4-a high pressure expander; 5-a low pressure expander; 6-a first mixer; 7-a condenser; 8-gas-liquid ejector; 9-working medium pump; 10-a second mixer; 11-a first generator; 12-a second generator.
Detailed Description
The invention will be further described with reference to examples and figures. The specific examples are provided only for further elaboration of the invention and do not limit the scope of the claims of the present application.
The organic Rankine double-stage flash evaporation circulation system with the gas-liquid ejector as shown in fig. 1 comprises an evaporator 1, a gas-liquid separator 2, a flash tank 3, a high-pressure expander 4, a low-pressure expander 5, a first mixer 6, a condenser 7, the gas-liquid ejector 8, a working medium pump 9, a second mixer 10, a first generator 11 and a second generator 12.
The working medium outlet of the evaporator 1 is communicated with the inlet of the gas-liquid separator 2, the gaseous working medium outlet of the gas-liquid separator 2 is communicated with the inlet of the high-pressure expander 4, and the liquid working medium outlet of the gas-liquid separator 2 is communicated with the inlet of the flash tank 3; a part of the gaseous working medium outlet of the flash tank 3 is communicated with the inlet of the low-pressure expander 5, the other part of the gaseous working medium outlet of the flash tank 3 is communicated with the steam nozzle inlet of the gas-liquid injector 8, and the liquid working medium outlet of the flash tank 3 is communicated with the inlet of the working medium pump 9; the high-pressure expander 4 expands and does work to drive the first generator 11, and the outlet of the high-pressure expander 4 is communicated with the first mixer 6; the expansion work driving of the low-pressure expander 5 is the second generator 12, and the outlet of the low-pressure expander 5 is communicated with the first mixer 6; the first mixer 6 is also communicated with a working medium inlet of the condenser 7; the working medium outlet of the condenser 7 is communicated with the liquid nozzle inlet of the gas-liquid injector 8, and the cooling water inlet and the cooling water outlet of the condenser 7 are connected with an external cooling water source; the outlet of the gas-liquid injector 8 communicates with the second mixer 10; the second mixer 10 is also communicated with the outlet of the working medium pump 9; the second mixer 10 is communicated with a working medium inlet of the evaporator 1; the heat source inlet of the evaporator 1 is connected with a low temperature heat source, and the heat source outlet of the evaporator 1 is connected with the discharge position of the low temperature heat source.
The gas-liquid separator 2 is used for separating gas from liquid of the working medium which is not completely evaporated due to low grade heat source.
The flash tank 3 has the function of flash evaporating the liquid working medium from the gas-liquid separator 2 through pressure reduction and capacity expansion to obtain available gaseous working medium.
The gas-liquid injector 8 is used for injecting low-temperature and low-pressure liquid from the working medium 7 by utilizing the steam from the flash evaporation of the high-temperature and high-pressure steam from the flash evaporation 3, condensing the gas in the mixing chamber of the gas-liquid injector 8 through direct contact heat exchange, generating strong condensation shock waves at the tail end of the mixing chamber, rapidly increasing the pressure of the mixed fluid, and finally further increasing the pressure of the mixed fluid through a diffusion process, thereby achieving the purpose of high-efficiency pressurization.
Preferably, the present system selects either dry working medium or isentropic working medium to avoid vapor droplet formation during expansion of the nozzle of the gas-liquid injector 8 affecting acceleration and increasing flow losses.
The working principle and the working flow of the invention are as follows:
taking medium-low temperature heat source water as an example, the medium-low temperature heat source water enters a heat source inlet of the evaporator 1 and exchanges heat with liquid organic working media in the evaporator 1, so that the working media undergo an incomplete evaporation process, and the liquid organic working media are changed into gas-liquid two-phase organic working media; the medium-low temperature heat source after heat exchange flows out from a heat source outlet of the evaporator 1; the gas-liquid two-phase organic working medium flows out from a working medium outlet of the evaporator 1 and enters the gas-liquid separator 2 to realize gas-liquid separation; the separated gaseous organic working medium flows out from a gaseous working medium outlet of the gas-liquid separator 2, enters the high-pressure expander 4 to expand and do work, and drives the first generator 11 to generate power; the separated liquid organic working medium flows out from a liquid working medium outlet of the gas-liquid separator 2 and enters a flash tank 3 for flash evaporation; the gaseous organic working medium obtained by the gas-liquid separation of the flash tank 3 is divided into two parts, and one part enters the low-pressure expander 5 to expand and do work so as to drive the second generator 12 to generate power; another part enters a steam nozzle of the gas-liquid injector; the liquid working medium separated from the flash tank 3 enters a working medium pump 9; the exhaust steam of the high-pressure expander 4 and the exhaust steam of the low-pressure expander 5 enter a first mixer 6 to be mixed, and the mixed gaseous organic working medium enters a condenser 7; the gaseous organic working medium exchanges heat with the cooling water entering the condenser 7 from the outside, the low-temperature cooling water after heat exchange becomes high-temperature cooling water, and the high-temperature cooling water flows out from a cooling water outlet of the condenser 7; condensing the gaseous organic working medium after heat exchange into a saturated liquid organic working medium, flowing out from a working medium outlet of the condenser 7, and entering a liquid nozzle of the gas-liquid injector;
in the gas-liquid injector 8, the gaseous organic working fluid obtained after gas-liquid separation in the flash tank 3 is used as working fluid and passes through a steam nozzle at high speed, and meanwhile, low-temperature low-pressure liquid flowing out from a working medium outlet of the condenser 7 is used as injection fluid and is subjected to acceleration and depressurization through a liquid nozzle; the working fluid and the injection fluid are mixed in the mixing chamber of the gas-liquid injector 8 through the steam nozzle outlet and the liquid nozzle outlet respectively; the resulting mixed fluid is diffused again in the diffusion chamber of the gas-liquid ejector 8 and then enters the second mixer 10; simultaneously, the organic working medium pressurized to the evaporating pressure by the working medium pump 9 enters the second mixer 10;
in the process of spraying by the gas-liquid sprayer 8, the flow ratio of the gas outlet of the flash tank 4 needs to be controlled, and the gaseous organic working fluid obtained after gas-liquid separation in the flash tank 3 is used as working fluid, and the high-temperature high-pressure steam which is necessary for the normal operation of the gas-liquid sprayer 8 is used as injection fluid, and the low-temperature low-pressure liquid flowing out from the working fluid outlet of the condenser 7 is used as injection fluid. The working fluid is sent into the steam nozzle of the gas-liquid injector 8, the working fluid converts heat energy into kinetic energy and passes through the steam nozzle at a high speed, and meanwhile, pressure difference is formed to inject injection fluid, and acceleration and depressurization are carried out through the liquid nozzle; the working fluid and the injection fluid respectively pass through a steam nozzle outlet and a liquid nozzle outlet, gas is condensed in a mixing chamber through direct contact heat exchange, and uniform two-phase flow is gradually formed through intense mass, momentum and heat exchange; the two-phase flow generates strong condensed shock waves at the tail end of the mixing chamber under the influence of back pressure, so that the pressure of the mixed fluid is rapidly increased; the mixed fluid is subjected to a diffusion process in the diffusion chamber, so that the pressure is further increased to exceed the pressure of the working fluid, and the evaporation pressure of the evaporator is reached;
the mixed fluid of the gas-liquid ejector 8 enters the second mixer 10; at the same time, the organic working medium pressurized to the evaporating pressure by the working medium pump 9 enters the second mixer 10 as well.
The two fluids are mixed in the second mixer 10 and then enter the evaporator 1 to complete the cycle.
For example, in the system, the temperature is 110 ℃, and the heat source water with the mass flow rate of 1kg/s enters the evaporator 1 to provide heat for the system; cooling water with the temperature of 20 ℃ and the mass flow rate of 2kg/s enters a condenser 7; the condensing temperature is 35 ℃; the injection ratio is 8; the mechanical friction efficiency is 95%; the power generation efficiency is 95%; the organic working medium R245fa flows into the evaporator 1 at 0.92kg/s, and expands and works in the high-pressure expander 4 and the low-pressure expander 5 respectively to provide about 8.34kW expansion work; the power consumption of the working medium pump is about 0.86kW; the net output work of the finally obtained system is 6.67kW; compared with an organic Rankine flash evaporation circulating system without a gas-liquid injector under the same working condition, the output work of the expander is reduced by 0.58kW, but the power consumption of a working medium pump is saved by 1.22kW, the net output work of the system is improved by 0.7kW, and the net output work of the system is relatively improved by 11.73%.
The present invention is not limited to the above-described embodiments, and it is apparent to those skilled in the art that various modifications and improvements can be made without departing from the spirit of the invention.
Claims (2)
1. An organic Rankine two-stage flash evaporation circulating system with a gas-liquid injector is characterized by comprising an evaporator (1), a gas-liquid separator (2), a flash tank (3), a high-pressure expander (4), a low-pressure expander (5), a condenser (7), the gas-liquid injector (8), a working medium pump (9), a first mixer (6), a second mixer (10), a first generator (11) and a second generator (12), wherein a working medium outlet of the evaporator (1) is communicated with an inlet of the gas-liquid separator (2), a gaseous working medium outlet of the gas-liquid separator (2) is communicated with an inlet of the high-pressure expander (4), and a liquid working medium outlet of the gas-liquid separator (2) is communicated with an inlet of the flash tank (3); one part of a gaseous working medium outlet of the flash tank (3) is communicated with an inlet of the low-pressure expander (5), the other part of the gaseous working medium outlet of the flash tank is communicated with a steam nozzle inlet of the gas-liquid injector (8), and a liquid working medium outlet of the flash tank (3) is communicated with an inlet of the working medium pump (9); the high-pressure expander (4) expands to do work to drive the first generator (11), and an outlet of the high-pressure expander (4) is communicated with the first mixer (6); the expansion work driving of the low-pressure expander (5) is the second generator (12), and the outlet of the low-pressure expander (5) is communicated with the first mixer (6); the first mixer (6) is also communicated with a working medium inlet of the condenser (7); the working medium outlet of the condenser (7) is communicated with the liquid nozzle inlet of the gas-liquid injector (8), and the cooling water inlet and the cooling water outlet of the condenser (7) are connected with an external cooling water source; the outlet of the gas-liquid injector (8) is in communication with the second mixer (10); the second mixer (10) is also communicated with the outlet of the working medium pump (9); the second mixer (10) is communicated with a working medium inlet of the evaporator (1); the heat source inlet of the evaporator (1) is connected with the low-temperature heat source, and the heat source outlet of the evaporator (1) is connected with the discharge position of the low-temperature heat source.
2. A control method of an organic rankine two-stage flash cycle system according to claim 1, comprising the steps of:
starting a medium-low temperature heat source, enabling the medium-low temperature heat source to enter a heat source inlet of an evaporator (1), exchanging heat with a liquid organic working medium in the evaporator (1), and enabling the working medium to undergo an incomplete evaporation process in the evaporator (1), wherein the liquid organic working medium is changed into a gas-liquid two-phase organic working medium; the medium-low temperature heat source after heat exchange flows out from a heat source outlet of the evaporator (1);
the gas-liquid two-phase organic working medium flows out from a working medium outlet of the evaporator (1) and enters a gas-liquid separator (2) to realize gas-liquid separation; the gaseous organic working medium obtained through separation flows out from a gaseous working medium outlet of the gas-liquid separator (2), enters a high-pressure expander (4) to expand and apply work, and drives a first generator (11) to generate power; the separated liquid organic working medium flows out from a liquid working medium outlet of the gas-liquid separator (2) and enters a flash tank (3) for flash evaporation;
the liquid organic working medium obtained by separation in the gas-liquid separator (2) enters a flash tank (3) for flash evaporation, the gaseous organic working medium obtained after flash evaporation is divided into two parts, one part enters a low-pressure expander (5) for expansion work to drive a second generator (12) to generate power, and the other part enters a steam nozzle of a gas-liquid ejector (8); meanwhile, the liquid working medium obtained after flash evaporation enters a working medium pump (9); the exhaust steam of the high-pressure expander (4) and the exhaust steam of the low-pressure expander (5) enter a first mixer (6) to be mixed, and gaseous organic working medium obtained by mixing in the first mixer (6) enters a condenser (7);
the gaseous organic working medium flowing out of the high-pressure expander (4) and the low-pressure expander (5) exchanges heat with cooling water entering the condenser (7) from the outside, the low-temperature cooling water after heat exchange becomes high-temperature cooling water, and the high-temperature cooling water flows out of a cooling water outlet of the condenser (7); condensing the gaseous organic working medium after heat exchange into a saturated liquid organic working medium, flowing out from a working medium outlet of a condenser (7), and entering a liquid nozzle of a gas-liquid injector (8);
in the gas-liquid ejector (8), the gaseous organic working medium obtained after gas-liquid separation in the flash tank (3) is used as working fluid and passes through the steam nozzle at high speed, and meanwhile, low-temperature low-pressure liquid flowing out from the working medium outlet of the condenser (7) is used as injection fluid and is subjected to acceleration and depressurization through the liquid nozzle; the working fluid and the injection fluid are mixed in a mixing chamber of the gas-liquid injector (8) through a steam nozzle outlet and a liquid nozzle outlet respectively; the obtained mixed fluid is diffused again in the diffusion chamber of the gas-liquid ejector (8) and then enters the second mixer (10); simultaneously, the organic working medium pressurized to the evaporating pressure by the working medium pump (9) enters the second mixer (10);
the two fluids enter the evaporator (1) after being mixed in the second mixer (10), and the circulation is completed.
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| CN116558140B (en) * | 2023-05-12 | 2023-12-15 | 广东海洋大学 | Combined cooling and power system |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108005743A (en) * | 2017-11-13 | 2018-05-08 | 中国科学院广州能源研究所 | A kind of cold synergy of contraction with pressure without pump organic Rankine cycle power generation system |
| CN108167040A (en) * | 2017-11-17 | 2018-06-15 | 昆明理工大学 | A kind of double compression swelling Organic Rankine Cycle recycling middle and low temperature waste heat power generation systems |
| CN109083705A (en) * | 2018-07-03 | 2018-12-25 | 广东工业大学 | Change component multiple pressure with injector evaporates non-azeotropic working medium Rankine cycle system |
| CN109812309A (en) * | 2019-01-17 | 2019-05-28 | 江苏大学 | A kind of organic rankine cycle system of overcritical double expansion two-stage backheats |
| CN110578566A (en) * | 2019-09-01 | 2019-12-17 | 天津大学 | organic Rankine cycle power generation system combining flash evaporation and injection pump and control method thereof |
| CN111022137A (en) * | 2019-11-27 | 2020-04-17 | 西安交通大学 | Waste heat recovery system and method based on organic Rankine cycle and organic flash cycle |
| CN111306830A (en) * | 2019-11-20 | 2020-06-19 | 中国科学院广州能源研究所 | Jet organic Rankine flash evaporation combined cooling and power system |
| CN111456822A (en) * | 2020-04-20 | 2020-07-28 | 高冠怡 | Dual-working-medium organic Rankine cycle power generation system and control method thereof |
| WO2021171312A1 (en) * | 2020-02-26 | 2021-09-02 | INDIAN INSTITUTE OF TECHNOLOGY MADRAS (IIT Madras) | Two stage regenerative organic rankine cycle (orc) heat recovery based power generation system |
-
2022
- 2022-03-11 CN CN202210242925.1A patent/CN114575951B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108005743A (en) * | 2017-11-13 | 2018-05-08 | 中国科学院广州能源研究所 | A kind of cold synergy of contraction with pressure without pump organic Rankine cycle power generation system |
| CN108167040A (en) * | 2017-11-17 | 2018-06-15 | 昆明理工大学 | A kind of double compression swelling Organic Rankine Cycle recycling middle and low temperature waste heat power generation systems |
| CN109083705A (en) * | 2018-07-03 | 2018-12-25 | 广东工业大学 | Change component multiple pressure with injector evaporates non-azeotropic working medium Rankine cycle system |
| CN109812309A (en) * | 2019-01-17 | 2019-05-28 | 江苏大学 | A kind of organic rankine cycle system of overcritical double expansion two-stage backheats |
| CN110578566A (en) * | 2019-09-01 | 2019-12-17 | 天津大学 | organic Rankine cycle power generation system combining flash evaporation and injection pump and control method thereof |
| CN111306830A (en) * | 2019-11-20 | 2020-06-19 | 中国科学院广州能源研究所 | Jet organic Rankine flash evaporation combined cooling and power system |
| CN111022137A (en) * | 2019-11-27 | 2020-04-17 | 西安交通大学 | Waste heat recovery system and method based on organic Rankine cycle and organic flash cycle |
| WO2021171312A1 (en) * | 2020-02-26 | 2021-09-02 | INDIAN INSTITUTE OF TECHNOLOGY MADRAS (IIT Madras) | Two stage regenerative organic rankine cycle (orc) heat recovery based power generation system |
| CN111456822A (en) * | 2020-04-20 | 2020-07-28 | 高冠怡 | Dual-working-medium organic Rankine cycle power generation system and control method thereof |
Non-Patent Citations (1)
| Title |
|---|
| 跨临界有机朗肯循环工质选择及系统参数优化;薄华宇;朱家玲;李太禄;;太阳能学报(第11期);全文 * |
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