Embodiments disclosed herein relate generally to an Organic Flash Cycle (OFC), and more particularly to the use of an Organic Flash Cycle (OFC) as a vapor power cycle for thermal energy conversion.
As energy demands increase, the search for alternative energy sources to generate electricity, as well as improving existing methods to maximize efficiency, continues. In addition, greater attention to improving efficiency of all processes and reducing the amount of energy that is wasted or unused is needed. In many industries such as the ceramic, cement, metallurgical, paper and pulp, food and beverage, and oil refining industries, process heat containing significant amounts of energy is vented and lost to the environment.
High quality waste energy has the potential to be efficiently converted to electricity. Its recovery would reduce thermal pollution and overall plant operating costs as the electricity generated from the waste heat could be used to power the manufacturing plant itself or be sold back to the grid. In addition to industrial processes, energy from the exit stream of gas turbines in high temperature Brayton cycles could also be used to generate electricity. In fact, utilizing this energy is the premise in many combined cycle plants.
As disclosed herein, in a basic Organic Flash Cycle (OFC) system, organic working fluids are used and brought to sufficiently high pressures such that they retain their liquid state during a heat exchange process. The heated organic working fluid is sent through a throttling valve to an evaporator, where it flash evaporates to produce a two-phase mixture; the resulting saturated vapor is separated and then expanded in a turbine to produce power. The saturated liquid is brought to the same pressure as the expanded vapor, re-mixed, and subsequently cooled to condense back to a low pressure saturated liquid.
One innovative aspect of the subject matter described in this disclosure can be implemented a basic OFC system including a pump, a heat exchanger, a flash evaporator, a turbine, a throttling valve, a mixer, and a condenser. The heat exchanger is coupled to an outlet of the pump. The flash evaporator is coupled to an outlet of the heat exchanger. The turbine is coupled to a vapor outlet of the flash evaporator. The throttling valve is coupled to a liquid outlet of the flash evaporator. The mixer is coupled to an outlet of the turbine and to an outlet of the throttling valve. The condenser is coupled to an outlet of the mixer and to an inlet of the pump. The system configured to be operable with an organic liquid.
In some embodiments, the turbine is coupled to a generator. In some embodiments, the flash evaporator includes a pressure vessel and a second throttling valve.
Another innovative aspect of the subject matter described in this disclosure can be implemented a basic OFC method including: (a) compressing an organic fluid with a pump; (b) after operation (a), heating the organic fluid by passing the organic fluid through a heat exchanger; (c) after operation (b), flash evaporating the organic fluid in a flash evaporator to generate an organic vapor; (d) driving a turbine with the organic vapor and lowering a pressure of the organic vapor to a lower pressure; (e) reducing a pressure of the organic fluid in a liquid state after operation (c) to the lower pressure by passing the organic fluid through a throttling valve; (f) mixing the organic fluid after operation (e) and the organic vapor after operation (d) in a mixer to form a mixture; (g) after operation (f), condensing the mixture to a liquid state of the organic fluid with a condenser; and, (h) after operation (i), directing the organic fluid to the pump.
In some embodiments, the turbine is coupled to a generator, and operation (d) generates electricity. In some embodiments, the organic fluid is selected from the group consisting of toluene, ethylbenzene, butylbenzene, o-xylene, m-xylene, p-xylene, tetradecamethylhexasiloxane (MD4M), tetradecamethylhexasiloxane (MD4M), decamethylcyclopentasiloxane (D5), dodecamethylpentasiloxane (MD3M), and dodecamethylcyclohexasiloxane (D6).
In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is about 80° C. to 400° C. In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is below about 300° C.
In some embodiments, the organic fluid is in a subcooled liquid state after operation (a). In some embodiments, the organic fluid is heated isobarically in operation (b). In some embodiments, the organic fluid remains in a liquid state in operation (b). In some embodiments, the organic fluid is in a saturated liquid state after operation (b).
Another innovative aspect of the subject matter described in this disclosure can be implemented a double flash OFC system including a pump, a heat exchanger, a first flash evaporator, a high pressure turbine, a second flash evaporator, a low pressure turbine, a throttling valve, a mixer, and a condenser. The heat exchanger is coupled to an outlet of the pump. The first flash evaporator is coupled to an outlet of the heat exchanger. The high pressure turbine is coupled to a vapor outlet of the first flash evaporator. The second flash evaporator is coupled to a liquid outlet of the first flash evaporator. The low pressure turbine is coupled to a vapor outlet of the second flash evaporator. The throttling valve is coupled to a liquid outlet of the second flash evaporator. The mixer is coupled to an outlet of the high pressure turbine, an outlet of the low pressure turbine, and an outlet of the throttling valve. The condenser is coupled to an outlet of the mixer and to an inlet of the pump. The system is configured to be operable with an organic fluid.
In some embodiments, the high pressure turbine and the low pressure turbine are coupled to a generator. In some embodiments, the first flash evaporator includes a first pressure vessel and a second throttling valve, and the second flash evaporator includes a second pressure vessel and a third throttling valve.
Another innovative aspect of the subject matter described in this disclosure can be implemented a double flash OFC method including (a) compressing an organic fluid with a pump; (b) after operation (a), heating the organic fluid by passing the organic fluid through a heat exchanger; (c) after operation (b), flash evaporating the organic fluid in a first flash evaporator to generate a high pressure organic vapor; (d) driving a high pressure turbine with the high pressure organic vapor and lowering a pressure of the high pressure organic vapor; (e) flash evaporating the organic fluid in a liquid state after operation (c) in a second flash evaporator to generate a low pressure organic vapor; (f) driving a low pressure turbine with the low pressure organic vapor and lowering a pressure of the low pressure organic vapor; (g) reducing a pressure of the organic fluid in a liquid state after operation (e) by passing the organic fluid through a throttling valve; (h) mixing the organic fluid after operation (g), the high pressure organic vapor after operation (d), and the low pressure organic vapor after operation (f) in a mixer to form an mixture; (i) condensing the mixture to a liquid state of the organic fluid with a condenser; and, (j) after operation (i), directing the organic fluid to the pump.
In some embodiments, the high pressure turbine and the low pressure turbine are coupled to a generator, and operations (d) and (f) generate electricity. In some embodiments, the organic fluid is selected from the group consisting of toluene, ethylbenzene, butylbenzene, o-xylene, m-xylene, p-xylene, tetradecamethylhexasiloxane (MD4M), tetradecamethylhexasiloxane (MD4M), decamethylcyclopentasiloxane (D5), dodecamethylpentasiloxane (MD3M), and dodecamethylcyclohexasiloxane (D6).
In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is about 80° C. to 400° C. In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is below about 300° C.
In some embodiments, the organic fluid is in a subcooled liquid state after operation (a). In some embodiments, the organic fluid is heated isobarically in operation (b). In some embodiments, the organic fluid remains in a liquid state in operation (b). In some embodiments, the organic fluid is in a saturated liquid state after operation (b).
Another innovative aspect of the subject matter described in this disclosure can be implemented a modified OFC system including a pump, a heat exchanger, a flash evaporator, a high pressure turbine, a throttling valve, a mixer, a low pressure turbine, and a condenser. The heat exchanger is coupled to an outlet of the pump. The flash evaporator is coupled to an outlet of the heat exchanger. The high pressure turbine is coupled to a vapor outlet of the flash evaporator. The throttling valve is coupled to a liquid outlet of the flash evaporator. The mixer is coupled to an outlet of the throttling valve and to an outlet of the high pressure turbine. The low pressure turbine is coupled to an outlet of the mixer. The condenser is coupled to an outlet of the low pressure turbine and to an inlet of the pump. The system is configured to be operable with an organic fluid.
In some embodiments, the high pressure turbine and the low pressure turbine are coupled to a generator. In some embodiments, the flash evaporator includes a pressure vessel and a second throttling value. In some embodiments, the organic fluid is selected from the group consisting of toluene, ethylbenzene, butylbenzene, o-xylene, m-xylene, p-xylene, tetradecamethylhexasiloxane (MD4M), tetradecamethylhexasiloxane (MD4M), decamethylcyclopentasiloxane (D5), dodecamethylpentasiloxane (MD3M), and dodecamethylcyclohexasiloxane (D6).
In some embodiments, the system is operable to perform a method including: (a) compressing the organic fluid with the pump; (b) after operation (a), heating the organic fluid by passing the organic fluid through the heat exchanger; (c) after operation (b), flash evaporating the organic fluid in the flash evaporator to generate a high pressure organic vapor; (d) driving the high pressure turbine with the high pressure organic vapor and lowering a pressure of the high pressure organic vapor to an intermediate pressure; (e) reducing a pressure of the organic fluid in a liquid state after operation (c) to the intermediate pressure by passing the organic fluid through the throttling valve; (f) mixing the organic fluid after operation (e) and the high pressure organic vapor after operation (d) in the mixer to form a low pressure organic vapor; (g) driving the low pressure turbine with the low pressure organic vapor and lowering a pressure of the low pressure organic vapor; (h) after operation (g), condensing the low pressure organic vapor to a liquid state of the organic fluid with the condenser; and, (i) after operation (h), directing the organic fluid to the pump.
In some embodiments, the high pressure turbine and the low pressure turbine are coupled to a generator, and operations (d) and (g) generate electricity.
In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is about 80° C. to 400° C. In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is below about 300° C.
In some embodiments, the organic fluid is in a subcooled liquid state after operation (a). In some embodiments, the organic fluid is heated isobarically in operation (b). In some embodiments, the organic fluid remains in a liquid state in operation (b). In some embodiments, the organic fluid is in a saturated liquid state after operation (b).
In some embodiments, the high pressure organic vapor is a saturated vapor or a superheated vapor after operation (d). In some embodiments, the organic fluid comprises a liquid and vapor mixture after operation (e). In some embodiments, the low pressure organic vapor is a saturated vapor or a superheated vapor after operation (g).
Another innovative aspect of the subject matter described in this disclosure can be implemented a modified OFC method including: (a) compressing an organic fluid with a pump; (b) after operation (a), heating the organic fluid by passing the organic fluid through a heat exchanger; (c) after operation (b), flash evaporating the organic fluid in a flash evaporator to generate a high pressure organic vapor; (d) driving a high pressure turbine with the high pressure organic vapor and lowering a pressure of the high pressure organic vapor to an intermediate pressure; (e) reducing a pressure of the organic fluid in a liquid state after operation (c) to the intermediate pressure by passing the organic fluid through a throttling valve; (f) mixing the organic fluid after operation (e) and the high pressure organic vapor after operation (d) in a mixer to form a low pressure organic vapor; (g) driving a low pressure turbine with the low pressure organic vapor and lowering a pressure of the low pressure organic vapor; (h) after operation (g), condensing the low pressure organic vapor to a liquid state of the organic fluid with a condenser; and, (i) after operation (h), directing the organic fluid to the pump.
In some embodiments, the high pressure turbine and the low pressure turbine are coupled to a generator, and operations (d) and (g) generate electricity. In some embodiments, the organic fluid is selected from the group consisting of toluene, ethylbenzene, butylbenzene, o-xylene, m-xylene, p-xylene, tetradecamethylhexasiloxane (MD4M), tetradecamethylhexasiloxane (MD4M), decamethylcyclopentasiloxane (D5), dodecamethylpentasiloxane (MD3M), and dodecamethylcyclohexasiloxane (D6).
In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is about 80° C. to 400° C. In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is below about 300° C.
In some embodiments, the organic fluid is in a subcooled liquid state after operation (a). In some embodiments, the organic fluid is heated isobarically in operation (b). In some embodiments, the organic fluid remains in a liquid state in operation (b). In some embodiments, the organic fluid is in a saturated liquid state after operation (b).
In some embodiments, the high pressure organic vapor is a saturated vapor or a superheated vapor after operation (d). In some embodiments, the organic fluid comprises a liquid and vapor mixture after operation (e). In some embodiments, the low pressure organic vapor is a saturated vapor or a superheated vapor after operation (g).
Another innovative aspect of the subject matter described in this disclosure can be implemented a two-phase OFC system including a pump, a heat exchanger, a two phase expander, a separator, a turbine, a throttling valve, a mixer, and a condenser. The heat exchanger is coupled to an outlet of the pump. The two phase expander is coupled to an outlet of the heat exchanger. The separator is coupled to an outlet of the two phase expander. The turbine is coupled to a vapor outlet of the separator. The throttling valve is coupled to a liquid outlet of the separator. The mixer is coupled to an outlet of the turbine and an outlet of the throttling valve. The condenser is coupled to an outlet of the mixer and to an inlet of the pump, the system configured to be operable with an organic liquid.
In some embodiments, the turbine is coupled to a generator.
Details of one or more embodiments of the subject matter described in this specification are set forth in the accompanying drawings and the description below. Other features, aspects, and advantages will become apparent from the description, the drawings, and the claims. Note that the relative dimensions of the following figures may not be drawn to scale.
Reference will now be made in detail to some specific examples of the invention including the best modes contemplated by the inventors for carrying out the invention. Examples of these specific embodiments are illustrated in the accompanying drawings. While the invention is described in conjunction with these specific embodiments, it will be understood that it is not intended to limit the invention to the described embodiments. On the contrary, it is intended to cover alternatives, modifications, and equivalents as may be included within the spirit and scope of the invention as defined by the appended claims.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. Particular example embodiments of the present invention may be implemented without some or all of these specific details. In other instances, well known process operations have not been described in detail in order not to unnecessarily obscure the present invention.
Various techniques and mechanisms of the present invention will sometimes be described in singular form for clarity. However, it should be noted that some embodiments include multiple iterations of a technique or multiple instantiations of a mechanism unless noted otherwise.
Introduction
As worldwide energy consumption continues to increase, the need for greater efficiency in energy production and usage becomes more critical. Maximizing the efficient conversion of heat to power in industries such as biomass, geothermal, solar thermal, and industrial processes is one avenue that can be pursued to better address this growing demand for energy.
Large power plants that operate under high temperatures typically use a Rankine Cycle to convert heat to electricity. A Rankine Cycle is a closed cycle where water absorbs heat from an external heat source and is transformed to vapor. The water vapor is then expanded in a turbine to produce electricity.
A major disadvantage of the water/steam flash cycle is that the steam, after expansion, contains a significant amount of moisture because water is a “wet” fluid. Wet fluids exhibit a saturated vapor curve on a temperature-entropy (T-S) diagram that is negatively sloped. Isentropic expansion of a “wet” fluid from its saturated vapor state will always produce a two-phase mixture with liquid droplets forming. Although large steam turbines often have isentropic efficiencies of 80% to 90%, saturated steam cycles in both geothermal and nuclear power industries still use special wet steam turbines. Wet steam turbines are constructed with expensive reinforcing materials to protect the blades from erosion and damage caused by the liquid droplets.
At low temperatures, organic fluids are more widely used to enhance performance. Organic fluids are “dry” fluids, meaning that there is no risk, after expansion in a turbine, of formation of liquid droplets that could damage turbine blades and lower the system efficiency. “Dry” and “isentropic” fluids exhibit a positively or infinitely sloped saturated vapor curve, respectively, on a temperature-entropy (T-S) diagram. Unlike “wet” fluids like water that have a negatively sloped saturated vapor curve, isentropic expansion from a saturated vapor state for “dry” and “isentropic” fluids will always result in a saturated vapor or a superheated vapor.
The Organic Rankine Cycle (ORC) is a Rankine Cycle that uses an organic fluid in place of water. ORC technology has been utilized for decades; it has been commercialized by a number of companies and is used in heat-to-power applications in the industrial, geothermal, and biomass sectors. ORC technology is generally used for low temperature and low flow thermal sources where the use of an organic fluid, in place of water, increases or maximizes performance. Some organic fluids, however, are flammable and their use may be limited to low temperature thermal sources. Typically, the ORC works well for temperatures between about 50° C. and 350° C. Above about 350° C., the use of water does not present performance disadvantages and is the preferred working fluid with higher temperature thermal sources given its economic, safety, and efficiency benefits.
Generally, in the ORC the organic fluid is pumped to increase its pressure and is then vaporized inside a heater. Within an ORC system, the heater or heat exchanger may include three separate components: a preheater, a boiler, and a superheater. In the heater, the organic liquid is heated by an external heat source, such as heat from industrial processes, geothermal energy, biomass energy, or solar applications. Through the heater, the organic liquid is vaporized into a high-pressure gas and goes through a turbine to generate electricity. After the gas expands, the fluid is condensed back into its liquid form and the closed cycle is completed.
In
Basic OFC
As disclosed herein, the Organic Flash Cycle (OFC) may result in better efficiency utilization of thermal resources. One difference between the ORC and the OFC is that the OFC uses a throttling valve that manages passage of the fluid within the system. With a throttling valve, vapor is produced from a saturated liquid instead of using an evaporation process through the heater.
In embodiments of the OFC, the working fluid is always in a liquid phase as it passes through the heater. Once the liquid is hot, it may be subsequently throttled in a flash evaporator, which separates it into vapor and liquid. The separated vapor is transferred to the turbine, and the separated liquid may be throttled again to lower pressure, where it is mixed with vapor exhaust from the turbine.
One potential advantage of the OFC is that it can reduce inefficiencies in the heating process. In the ORC, the fluid in the heater goes through a phase change from liquid to vapor, and because of this phase change the heat transfer process is not as efficient as the temperature profiles of the working fluid and the heat source are more likely to mismatch. In addition, less efficient heat transfer occurs while the working fluid is in the vapor phase due to lower heat transfer coefficients. Since the heat addition in the OFC is completely in the liquid phase, the process will have higher heat transfer coefficients and more efficient heat transfer. Also, as there is no phase change in the heater of the OFC, inefficiencies of the process are primarily due to the throttling valve of the flash evaporator. The OFC also can be modified beyond its basic design to yield greater efficiency than the basic ORC.
The sizes and specifications of the components of the OFC systems disclosed herein depend upon the size of the system (e.g., the volumes of the system components) and the operating conditions (e.g., temperatures and pressures) for which the OFC system is designed. Further, each of the OFC systems disclosed herein are closed systems in which an organic fluid circulates through the system with the temperature, the pressure, and the state (e.g., gaseous state or liquid state) of the organic fluid changing depending on where it is in the system.
Generally, a heat exchanger is a piece of equipment designed for efficient heat transfer from one medium to another. The heat exchanger 305 is used to heat an organic fluid. The OFC does not use an evaporator, as the cycle keeps the organic fluid in the liquid phase during the entire heat addition process. In some embodiments, a basic OFC system 300 may use a larger preheater and condenser compared to a similarly sized ORC. In some embodiments, the heat exchanger 305 is a countercurrent heat exchanger. In a countercurrent heat exchanger, two fluids flow is opposite directions to one another. An increased or maximum amount of heat can be transferred in a countercurrent heat exchanger (e.g., as compared to a co-current (parallel) heat exchanger) because the countercurrent flow maintains a slowly declining temperature difference or gradient between the fluids flowing through the heat exchanger.
Generally, a flash evaporator is operable to generate a saturated vapor and a saturated liquid when a saturated liquid undergoes a reduction in pressure by passing through a throttling device, such as a throttling valve, for example. The flash evaporator 310 includes a throttling valve 312 and a pressure vessel 314.
Generally, a turbine is a rotary mechanical device that extracts energy from a fluid flow to rotate a shaft. The shaft of the turbine may be coupled or connected to a generator to convert the mechanical energy of the shaft to electrical energy. As shown in
The throttling valve 320 is operable to reduce the pressure of the saturated liquid from the flash evaporator 310. Generally, a mixer is a device operable to mix fluids. The mixer 325 mixes liquid from the throttling valve 320 and vapor from the turbine 315.
Generally, a condenser is a device operable to condense a substance from its gaseous to its liquid state. Typically, a condenser condenses a substance from its gaseous to its liquid state by cooling it. The condenser 330 condenses the mixture from the mixer 325 to a liquid.
Generally, a pump is a device operable to move or transport fluids (i.e., liquids or gases) by mechanical action. A pump may also be operable to pressurize (i.e., to increase the pressure of) a fluid. The pump 325 is operable to pressurize a fluid and to transport the fluid from the condenser 320 to the heat exchanger 305.
In some embodiments, the basic OFC system 300 is configured to operate with an organic fluid as the working fluid. In some embodiments, the organic fluid may comprise toluene, ethylbenzene, butylbenzene, o-xylene, m-xylene, p-xylene, tetradecamethylhexasiloxane (MD4M), tetradecamethylhexasiloxane (MD4M), decamethylcyclopentasiloxane (D5), dodecamethylpentasiloxane (MD3M), or dodecamethylcyclohexasiloxane (D6). Further, all of the OFC systems disclosed herein may operate with any of the organic fluids listed above.
As shown in
It should be noted that energy in the saturated liquid (i.e., at state 6) can be further utilized by using an internal heat exchanger (IHE) as is often done in ORCs. The flashing process could also be performed in two steps to extract more work; this is sometimes done in higher temperature geothermal plants to boost power output.
Enhancements to the Basic OFC
A major source of irreversibilities and exergy destruction in the basic OFC results from the flash evaporation process (state 2 to state 3 in
The Double Flash OFC.
The motivation of the double flash OFC is similar to that of the double flash steam cycle in geothermal energy. By splitting the flash evaporation process into two steps instead of one, more of the fluid is vaporized and consequently, more of the fluid can be expanded for power production.
The first flash evaporator 410 includes a throttling valve 412 and a pressure vessel 414. The second flash evaporator 440 includes a throttling valve 442 and a pressure vessel 444. The high pressure turbine 415 and the low pressure turbine 416 may be coupled to a generator 417 for power/electricity production. In some embodiments, the high pressure turbine 415 and the low pressure turbine 416 are coupled to a single shaft that is coupled to the generator 417. In some embodiments, the high pressure turbine 415 and the low pressure turbine 416 may be single-stage turbines.
As shown in
In operation, the double flash OFC system 400 brings a saturated organic liquid at a low pressure at state 13 to a high pressure at state 1 using the pump 435. In some embodiments, the organic liquid at state 13 may be slightly sub-cooled to prevent pump cavitation. Next, from state 1 to state 2, the high pressure organic liquid absorbs heat while passing though the heat exchanger 405 (e.g., from a finite thermal source). The organic liquid is then flash evaporated in the flash evaporator 410 to a lower pressure liquid-vapor mixture at state 3. The liquid-vapor mixture is separated into its saturated vapor and saturated liquid components at states 4 and 6, respectively. From state 4 to state 5, the saturated vapor is expanded to the condensing pressure and work is extracted with the high pressure turbine 415. The saturated liquid is flash evaporated a second time in the flash evaporator 440. The liquid-vapor mixture is separated into its saturated vapor and saturated liquid components at states 8 and 10, respectively. From state 8 to state 9, the saturated vapor is expanded to the condensing pressure and work is extracted with the low pressure turbine 416. The saturated liquid from the flash evaporator 440 is brought to a condenser pressure using the throttling valve 420 from state 10 to state 11. The liquid and vapor are then recombined in the mixer 425 and subsequently condensed back to a low pressure saturated liquid in the condenser 430 from state 12 to state 13.
The Modified OFC.
It was found that the “drying” nature of the organic working fluids causes a substantial degree of superheat at the turbine exit, particularly for siloxanes. Siloxanes are molecularly complex, and have been shown to result in less positively sloped saturated vapor curves on a T-S diagram and correspondingly more superheat after expansion from a saturated vapor state. The modified OFC is designed with this observation in mind.
In some embodiments of a modified OFC, turbine expansion is performed in two stages. After the fluid is separated into liquid and vapor in the flash evaporator, the vapor goes through a first turbine. After expansion in the first turbine, the vapor exhaust is mixed with the liquid from the flash evaporator in a mixer. In the mixer, the superheated vapor and saturated liquid produce a saturated vapor that can be used again in a second turbine. The liquid is condensed in the condenser once it exits the second turbine and the cycle is completed.
The flash evaporator 510 includes a throttling valve 512 and a pressure vessel 514. The high pressure turbine 515 and the low pressure turbine 516 may be coupled to a generator 517 for power/electricity production. In some embodiments, the high pressure turbine 515 and the low pressure turbine 516 are coupled to a single shaft that is coupled to the generator 517. In some embodiments, the high pressure turbine 515 and the low pressure turbine 516 may be single-stage turbines.
As shown in
After operation 562, in operation 564, the organic fluid is heated by passing the organic fluid through a heat exchanger (state 1 to state 2). In some embodiments, a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is about 80° C. to 400° C. or below about 300° C. In some embodiments, the organic fluid is heated isobarically (i.e., at a constant pressure) in operation 564. In some embodiments, the organic fluid remains in a liquid state in operation 564. In some embodiments, the organic fluid is in a saturated liquid state after operation 564. A saturated liquid is a liquid which is at its saturation pressure and saturation temperature; i.e., a liquid which is at its boiling point for any given pressure.
After operation 564, in operation 566, the organic fluid is flash evaporated in a flash evaporator. Flash evaporating the organic fluid produces a high pressure organic vapor and an organic liquid (state 2 to state 3). The high pressure organic vapor and the organic liquid are saturated fluids. In some embodiments, gravity separates the organic liquid and the high pressure organic vapor, with the denser liquid (state 4) flowing out of a bottom of the flash evaporator and the less dense vapor (state 5) flowing out of the top of the flash evaporator.
In operation 568, a high pressure turbine is driven with the high pressure organic vapor (state 4 to state 5). The high pressure turbine is driven with the high pressure organic vapor by expanding the high pressure organic vapor through the high pressure turbine. Operation 568 also lowers the pressure of the high pressure organic vapor to an intermediate pressure. In some embodiments, the high pressure organic vapor is a saturated vapor or a superheated vapor after operation 568. A saturated vapor is a vapor which is at its saturation pressure and saturation temperature. A superheated vapor is a vapor at a temperature that is higher than its vaporization (boiling) point at the absolute pressure where the temperature measurement is taken; therefore, the vapor can cool (i.e., lose internal energy) by some amount, resulting in a lowering of its temperature without changing state (i.e., condensing) from a gas to a mixture of saturated vapor and liquid.
In operation 570, a pressure of the organic fluid in a liquid state from the flash evaporator is reduced to an intermediate pressure by passing the organic fluid through a throttling valve (state 6 to state 7). In some embodiments, the organic fluid comprises a liquid and vapor mixture after operation 570.
In operation 572, the organic fluid after operation 570 and the high pressure organic vapor after operation 568 are mixed in a mixer to form a low pressure organic vapor (states 5 and 7 to state 8). In some embodiments, the mixing process is an isobaric mixing process.
In operation 574, a low pressure turbine is driven with the low pressure organic vapor (state 8 to state 9). The low pressure turbine is driven with the low pressure organic vapor by expanding the low pressure organic vapor through the low pressure turbine. Operation 574 also lowers a pressure of the low pressure organic vapor. In some embodiments, the low pressure organic vapor is a saturated vapor or a superheated vapor after operation 574.
After operation 574, in operation 576, the low pressure organic vapor is condensed to a liquid state of the organic fluid with a condenser (state 9 to state 10). In the condensation process, the low pressure organic vapor releases heat or energy. In some embodiments, the organic fluid is a saturated liquid after operation 576.
After operation 576, in operation 578, the organic fluid is directed to the pump. The organic fluid can then flow through the method 560 again, starting with operation 562 in which the organic fluid is compressed with the pump. In some embodiments, the high pressure turbine and the low pressure turbine are coupled to a generator, with operations 568 and 574 generating electricity.
One advantage of a modified OFC system is that more of the organic fluid goes through the expansion process to produce work. In the basic OFC shown in
Another advantage of the modified OFC system is that the organic vapor is less superheated at the low pressure turbine exit. This can be seen more clearly in the T-S diagram of
Yet another advantage of the modified OFC system is that the organic fluid is flashed to a lower quality which results in the liquid being at a higher temperature and pressure prior to the high pressure turbine. This also results in reduced exergy destruction in the flash evaporation process since the separated liquid can still be used to produce power in the low pressure turbine.
The Two-Phase OFC.
In some embodiments of a two-phase OFC, the flash expander in the basic OFC (state 2 to state 3 in
In some embodiments, the separator 614 may comprise a pressure vessel. The turbine 615 may be coupled to a generator 617 for power/electricity production. The two-phase expander 610 may be coupled to a second generator (not shown) for power/electricity production.
Traditionally, the task of designing a reliable and efficient two-phase turbine has been challenging because it requires the turbine to be able to handle a fluid with both liquid and vapor behaviors. Tailoring the turbine specifically to one phase or the other is thus not appropriate in this case, which has made it difficult to achieve a suitable design. In a sense, two-phase expanders are similar to throttling valves, except they have the ability to recover some of the energy dissipated by the throttling process (capturing energy associated with the rapid expansion of the vapor after flashing from a liquid as the fluid drops to a lower pressure). Presently, radial inflow turbine manufacturers have reported that isentropic efficiencies of about 70% can be achieved reliably in the two-phase regime. Significant advances have also been achieved recently for screw-type and scroll-type expanders.
As shown in
The Modified Two-Phase OFC.
Combining the embodiments described with respect to
In some embodiments, the separator 714 may comprise a pressure vessel. The high pressure turbine 715 and the low pressure turbine 716 may be coupled to a generator 717 for power/electricity production. The two-phase expander 710 may be coupled to a second generator (not shown) for power/electricity production.
In some embodiments, the modified two-phase OFC system 700 includes operations as described above with respect to the modified OFC (
Results and Discussion
A combination of modern equations of state was used to calculate working fluid thermodynamic properties of the various embodiments, as described in the papers “Comparison of the Organic Flash Cycle (OFC) to other advanced vapor cycles for intermediate and high temperature waste heat reclamation and solar thermal energy,” Ho, Tony, et al., Energy 42 (2012) 213-223, and “Increased power production through enhancements to the Organic Flash Cycle (OFC),” Ho, Tony, et al., Energy 45 (2012), 686-695. Both papers are herein incorporated by reference.
Results showed that in some embodiments the modified OFC can produce more power than the double flash OFC. The modified OFC also may be more attractive than the double flash OFC in terms of system simplicity because a second flash evaporator is not used. In some embodiments, the modified OFC configuration can produce more power because all the flow is expanded through the low pressure turbine. In addition, less energy may be lost in the condenser because the fluid is less superheated at the low pressure turbine exit and energy from the separated saturated liquid after flash evaporation is also utilized to produce power.
Combining the advantages of the modified OFC and the two-phase OFC, the modified two-phase OFC showed the greatest potential for increased power output. For aromatic hydrocarbon working fluids, the modified two-phase OFC produced approximately 76% of the theoretically available power initially in the finite thermal energy source. For the same finite thermal energy source, the modified two-phase OFC produced approximately 20% more power than the optimized conventional ORC. Although this cycle can generate substantially more power, this embodiment needs to be evaluated with respect to the additional complexity and equipment costs.
The modified OFC may be an attractive compromise between high power output and additional equipment costs. By adding an additional low pressure turbine to the basic OFC, a 10% to 12% increase in power output compared to the optimized ORC may be achieved for aromatic hydrocarbons. The heat exchangers for the modified OFC could also be less expensive than for the basic OFC because more power is being produced, which reduces the total heat rejection rate in the condenser and subsequently decreases the necessary heat transfer area for the condenser.
Several different embodiments of an Organic Flash Cycle (OFC) disclosed herein may improve power output from a specific flow rate of a given finite thermal energy reservoir. Some of the sources of inefficiency in the basic OFC configuration, including irreversibilities generated by the flash evaporation process and the high superheat at the turbine exit, may be reduced with enhancements to the basic OFC configuration disclosed herein.
In the foregoing specification, the invention has been described with reference to specific embodiments. However, one of ordinary skill in the art appreciates that various modifications and changes can be made without departing from the scope of the invention as set forth in the claims below. Accordingly, the specification and figures are to be regarded in an illustrative rather than a restrictive sense, and all such modifications are intended to be included within the scope of invention.
This application claims priority to U.S. Provisional Patent Application No. 61/664,697, filed Jun. 26, 2012, which is herein incorporated by reference.
This invention was made with government support under Contract No. DE-AC02-05CH11231 awarded by the U.S. Department of Energy. The government has certain rights in this invention.
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Number | Date | Country | |
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20130341929 A1 | Dec 2013 | US |
Number | Date | Country | |
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61664697 | Jun 2012 | US |