EP2607635B1 - Cascaded Organic Rankine Cycle System - Google Patents
Cascaded Organic Rankine Cycle System Download PDFInfo
- Publication number
- EP2607635B1 EP2607635B1 EP12195287.3A EP12195287A EP2607635B1 EP 2607635 B1 EP2607635 B1 EP 2607635B1 EP 12195287 A EP12195287 A EP 12195287A EP 2607635 B1 EP2607635 B1 EP 2607635B1
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- fluid
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- 239000012530 fluid Substances 0.000 claims description 80
- 229920006395 saturated elastomer Polymers 0.000 claims description 14
- 210000003127 knee Anatomy 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 10
- 238000004891 communication Methods 0.000 claims description 8
- KPUWHANPEXNPJT-UHFFFAOYSA-N disiloxane Chemical class [SiH3]O[SiH3] KPUWHANPEXNPJT-UHFFFAOYSA-N 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 5
- MSSNHSVIGIHOJA-UHFFFAOYSA-N pentafluoropropane Chemical compound FC(F)CC(F)(F)F MSSNHSVIGIHOJA-UHFFFAOYSA-N 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 description 8
- 239000007788 liquid Substances 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
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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
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
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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
- F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
- F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
- F01K23/04—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled condensation heat from one cycle heating the fluid in another cycle
Definitions
- the present disclosure relates to a cascaded organic Rankine cycle.
- the Organic Rankine Cycle is a vapor power cycle with an organic fluid refrigerant instead of water/steam as the working fluid.
- the working fluid is heated in an "evaporator/boiler" by a source of waste or low quality heat.
- the fluid starts as a liquid and ends up as a vapor.
- the high-pressure refrigerant vapor expands in the turbine to produce power.
- the low-pressure vapor exhausted from the turbine is condensed then sent back to the pump to restart the cycle.
- the simple rankine cycle used for power generation follows the process order: 1) Adiabatic pressure rise through a pump; 2) Isobaric heat addition in a preheater, evaporator and superheater; 3) Adiabatic expansion in a turbine; and 4) Isobaric heat rejection in a condenser, although other cycle modifications are possible such as the addition of a vapor-to-liquid recuperator.
- thermodynamic irreversibility in organic Rankine cycles is caused by the large temperature difference in the evaporator between the temperature of the waste heat stream and the boiling refrigerant. The higher the waste heat stream temperature the greater this irreversibility becomes.
- One way to reduce this loss is to cascade two thermodynamic cycles together where a cycle operating at higher temperatures rejects heat to a cycle operating at lower temperatures.
- a cascaded Organic Rankine Cycle (ORC) system includes a bottoming cycle in thermal communication with a topping cycle through a condenser/evaporator in which a bottoming cycle working fluid is first evaporated and then superheated and a topping cycle working fluid is first desuperheated and then condensed such that a percentage of total heat transfer from the topping cycle fluid that occurs during a saturated condensation is equal to or less than a percentage of total heat transfer to the bottoming cycle fluid that occurs during a saturated evaporation, wherein only said bottoming cycle includes a recuperator.
- a method of operating a cascaded Organic Rankine Cycle (ORC) system in which a bottoming cycle is in thermal communication with a topping cycle which includes maintaining a percentage from a fluid in the topping cycle at equal or less than a percentage of total heat transfer to a fluid in the bottoming cycle, wherein only the working fluid in the bottoming cycle (24) is recuperated by use of a recuperator (24).
- ORC Organic Rankine Cycle
- FIG 1 schematically illustrates a cascaded Organic Rankine Cycle (ORC) system 20.
- the cascaded ORC system 20 includes at least two Rankine cycles, where a relatively hotter topping cycle 22 is cascaded with a relatively cooler bottoming cycle 24.
- the topping cycle 22 uses Siloxane MM as the working fluid while the bottoming cycle 24 uses R245fa. It should be appreciated, however, that additional cycles and other working fluids may additionally be utilized.
- the topping cycle 22 generally includes a power producing turbine 26 which is driven by the working fluid to drive a generator 28 that produces power.
- a refrigerant pump 30 increases the pressure of the working fluid from a condenser/evaporator 32.
- the heat exchanger group that transfers heat from the topping cycle 22 to the bottoming cycle 24 is referred to herein as the "condenser/evaporator" 32, although it should be understood that it may also include desuperheating and subcooling of the working fluid in the topping cycle 22, and preheating and superheating of the working fluid in the bottoming cycle 24.
- An evaporator 34 such as a boiler receives a significant heat input from, for example, an oil circuit 36 to vaporize the Siloxane MM working fluid with the vapor thereof passed through to the turbine 26 to provide motive power.
- the relatively lower pressure working fluid vapor passes to the condenser/evaporator 32 and is condensed by way of a heat exchange relationship with the bottoming cycle 24 such that the condenser/evaporator 32 operates as a condenser in the topping cycle 22 as well as an evaporator in the bottoming cycle 24.
- the turbine 26 is a radial inflow turbine that expands the topping cycle working fluid vapor down to a lower pressure and generates power by the extraction of work from this expansion process.
- the vapor is still superheated so that its heat potential is utilized in the condenser/evaporator 32.
- the condenser/evaporator 32 actually de-superheats the working fluid and ultimately condenses the working fluid back to liquid for communication through the pump 30.
- the condensed working fluid is then circulated to the evaporator 34 by the pump 30 to complete the topping cycle 22.
- the bottoming cycle 24 generally includes a power producing turbine 36 which is driven by the working fluid in the bottoming cycle and in turn drives a generator 38 that produces power.
- a refrigerant pump 40 increases the pressure of the working fluid from a recuperator 40.
- the bottom cycle working fluid is in thermal communication with a cooling system such as a water circuit 42 through a water cooled condenser 44.
- the vapor entering and leaving turbine 36 is highly superheated.
- the energy potential of the superheated vapor at the turbine exit is not wasted, but is fed into a recuperator 46.
- the recuperator 46 transfers heat from the low-pressure hot vapor from the turbine exit to the high pressure liquid at the pump exit.
- the recuperator 46 uses this superheat to preheat the liquid working fluid downstream of the pump 40. That is, if a cycle is driven to high turbine inlet superheat, then turbine outlet superheat will be high. The availability of this heat is thereby captured to maintain cycle efficiency as the recuperator 46 is an internal heat exchanger. When the low pressure side of the topping cycle 22 is de-superheated, it is essentially recuperated into the bottoming cycle 24 which is where high superheat is achieved. Matching of the working fluids and the pressures thereof facilitates this interaction.
- the recuperator 46 is only in the bottoming cycle 24. As the topping cycle 22 is not recuperated, its waste heat is captured by the condenser/evaporator 32. Both cycles are highly superheated yet avoid heat-exchanger pinches to minimize the heat-transfer temperature difference and minimize process irreversibility
- Figure 2 shows a TS diagram for the bottoming cycle 24.
- the condenser/evaporator 32 receives nearly saturated liquid (a temperature that is close to boiling) from the recuperator 46.
- the condenser/evaporator 32 boils then heats the refrigerant from state 6 to 1.
- the state 1 condition is highly superheated.
- the exit state from the turbine 36, state 2, is also highly superheated.
- the recuperator 46 uses this heat (state 2 to 3) to heat the high pressure working fluid (state 5 to 6). Sizing of the recuperator 46 affects state 6.
- recuperator 46 results in less heat transferred and therefore a cooler more subcooled state at 6 which results in more heat transfer required from the condenser/evaporator 32, and a larger percentage of that heat in the preheating and evaporating regimes.
- Figure 3 shows a TS diagram for the topping cycle 22.
- the exit state of the topping cycle turbine 26 is highly superheated, but a recuperator is not used. Instead, the low pressure working fluid vapor is de-superheated as the bottoming cycle high-pressure working fluid is superheated.
- the choice of a heavy molecule such as Siloxane for the topping cycle 22 results in the highly angled saturation dome. As a result, the inlet state to turbine 26 is only slightly superheated.
- Figure 4 represents an idealized counter-flow heat exchanger.
- the x-axis is normalized enthalpy change of each fluid, and the y-axis is temperature.
- m is the mass flow rate
- h is the enthalpy of the fluid.
- the warmer fluid (A) is shown to travel from right to left, and the colder fluid (B) to travel from left to right through the heat exchanger.
- the above equation must be true. For example, the first 10% reduction in enthalpy of Fluid A must equal the last 10% increase of enthalpy of fluid B. If the fluids were simple fluids with constant specific heat, then each temperature profile would be a straight line. When the fluids are refrigerants, the temperature profiles have various non-linear shapes. When a fluid is saturated there is no change in temperature with change in enthalpy.
- the change in temperature with enthalpy is generally different for a fluid as a liquid than as a vapor; therefore, the choice of fluid and operational temperatures affect the shape of these curves. Furthermore, the choice of other system components will affect their shape. Specifically the choice of and the size of the recuperator 46 in the proposed cycle affects the starting enthalpy (and therefore temperature) of stream B.
- Figure 4 shows how each temperature profile relates to the other at each physical location along the heat exchanger.
- Fluid A In order for heat to flow from Fluid A to Fluid B, Fluid A must always be warmer than Fluid B. If A gets too close to B this is referred to as a temperature "pinch" condition. This is undesirable because a large heat exchange area is required to exchange the enthalpy in this region. In fact, the entire size of a heat exchanger may be defined by a "pinch” condition. Where the temperature difference is large, the thermodynamic cycle will be less efficient since more entropy is generated by heat exchange through larger temperature differences. An ideal arrangement is when the temperature difference throughout the heat exchanger remains relatively constant.
- the condenser/evaporator 32 heat exchanger has two major regions. The first (on the left in Figure 4 ) is saturated for both fluids and the temperature profiles are flat. This section covers about 40 percent of the total heat transfer in the disclosed non-limiting embodiment. The second (on the right in Figure 4 ) is superheated and temperature increases with enthalpy. That is, a percent saturation for a fluid in the topping cycle 22 is maintained at 38 percent saturation compared to a 40 percent saturation for the working fluid in the bottoming cycle 24.
- the "knee" of fluid A must lie equal to or slightly to the left of the "knee” of fluid B in the normalized enthalpy plot. If the "knee" lies far to the left then the saturated section may have a good heat transfer difference (typically 5 to 15F; 3 to 8C), but the heat transfer difference of the vapor section will be too large. If the "knee" lies too far to the right then a "pinch” condition will be created between the two fluids. Practically the temperature difference will increase and the saturated temperature difference will be too high.
- the effect of the recuperator 46 on the condenser/evaporator 32 in the proposed cycle is to change the inlet enthalpy, and therefore temperature, of the colder fluid, B.
- the enthalpy of the inlet of B increases by recovering heat from the turbine exit. This results in a smaller percentage of the total heat transfer for Fluid B occurring to the left of the knee, shifts the knee of B to the left and results in a pinch condition.
- the recuperator heat exchange is reduced or eliminated, this shifts knee of B to the right and therefore increases the temperature difference in the vapor section.
- a percentage of total heat transfer from the working fluid in the topping cycle 22 that occurs during a saturated condensation is equal to or slightly less (within 10%) than a percentage of total heat transfer to the working fluid in the bottoming cycle 24 that occurs during a saturated evaporation.
Description
- The present disclosure relates to a cascaded organic Rankine cycle.
- The Organic Rankine Cycle (ORC) is a vapor power cycle with an organic fluid refrigerant instead of water/steam as the working fluid. The working fluid is heated in an "evaporator/boiler" by a source of waste or low quality heat. The fluid starts as a liquid and ends up as a vapor. The high-pressure refrigerant vapor expands in the turbine to produce power. The low-pressure vapor exhausted from the turbine is condensed then sent back to the pump to restart the cycle.
- The simple rankine cycle used for power generation follows the process order: 1) Adiabatic pressure rise through a pump; 2) Isobaric heat addition in a preheater, evaporator and superheater; 3) Adiabatic expansion in a turbine; and 4) Isobaric heat rejection in a condenser, although other cycle modifications are possible such as the addition of a vapor-to-liquid recuperator.
- A main thermodynamic irreversibility in organic Rankine cycles is caused by the large temperature difference in the evaporator between the temperature of the waste heat stream and the boiling refrigerant. The higher the waste heat stream temperature the greater this irreversibility becomes. One way to reduce this loss is to cascade two thermodynamic cycles together where a cycle operating at higher temperatures rejects heat to a cycle operating at lower temperatures.
- Cascaded Organic Rankine Cycle (ORC) systems are known from
US 2010/319346 A1 ,WO 2006/104490 A1 ,WO 2009/045196 A1 andDE 199 07 512 A1 . - A cascaded Organic Rankine Cycle (ORC) system according to an exemplary aspect of the present invention includes a bottoming cycle in thermal communication with a topping cycle through a condenser/evaporator in which a bottoming cycle working fluid is first evaporated and then superheated and a topping cycle working fluid is first desuperheated and then condensed such that a percentage of total heat transfer from the topping cycle fluid that occurs during a saturated condensation is equal to or less than a percentage of total heat transfer to the bottoming cycle fluid that occurs during a saturated evaporation, wherein only said bottoming cycle includes a recuperator.
- A method of operating a cascaded Organic Rankine Cycle (ORC) system in which a bottoming cycle is in thermal communication with a topping cycle according to an exemplary aspect of the present invention which includes maintaining a percentage from a fluid in the topping cycle at equal or less than a percentage of total heat transfer to a fluid in the bottoming cycle, wherein only the working fluid in the bottoming cycle (24) is recuperated by use of a recuperator (24).
- Various features will become apparent to those skilled in the art from the following detailed description of the disclosed non-limiting embodiment. The drawings that accompany the detailed description can be briefly described as follows:
-
Figure 1 is a schematic diagram of a cascaded organic rankine cycle with a topping cycle and a bottoming cycle; -
Figure 2 is a TS-diagram for the bottoming cycle; -
Figure 3 is a TS-diagram for the topping cycle; and -
Figure 4 is a plot of temperature profiles in the counter-flow heat exchangers of the desuperheating and then condensing topping fluid (Siloxane MM), and the evaporating and then superheating bottoming fluid (R245fa). -
Figure 1 schematically illustrates a cascaded Organic Rankine Cycle (ORC)system 20. Thecascaded ORC system 20 includes at least two Rankine cycles, where a relativelyhotter topping cycle 22 is cascaded with a relativelycooler bottoming cycle 24. In the disclosed non-limiting embodiment, thetopping cycle 22 uses Siloxane MM as the working fluid while thebottoming cycle 24 uses R245fa. It should be appreciated, however, that additional cycles and other working fluids may additionally be utilized. - The
topping cycle 22 generally includes apower producing turbine 26 which is driven by the working fluid to drive agenerator 28 that produces power. Arefrigerant pump 30 increases the pressure of the working fluid from a condenser/evaporator 32. The heat exchanger group that transfers heat from thetopping cycle 22 to thebottoming cycle 24 is referred to herein as the "condenser/evaporator" 32, although it should be understood that it may also include desuperheating and subcooling of the working fluid in thetopping cycle 22, and preheating and superheating of the working fluid in thebottoming cycle 24. - An
evaporator 34 such as a boiler receives a significant heat input from, for example, anoil circuit 36 to vaporize the Siloxane MM working fluid with the vapor thereof passed through to theturbine 26 to provide motive power. Upon leaving theturbine 26, the relatively lower pressure working fluid vapor passes to the condenser/evaporator 32 and is condensed by way of a heat exchange relationship with thebottoming cycle 24 such that the condenser/evaporator 32 operates as a condenser in thetopping cycle 22 as well as an evaporator in thebottoming cycle 24. - In the disclosed non-limiting embodiment, the
turbine 26 is a radial inflow turbine that expands the topping cycle working fluid vapor down to a lower pressure and generates power by the extraction of work from this expansion process. The vapor is still superheated so that its heat potential is utilized in the condenser/evaporator 32. The condenser/evaporator 32 actually de-superheats the working fluid and ultimately condenses the working fluid back to liquid for communication through thepump 30. The condensed working fluid is then circulated to theevaporator 34 by thepump 30 to complete thetopping cycle 22. - The
bottoming cycle 24 generally includes apower producing turbine 36 which is driven by the working fluid in the bottoming cycle and in turn drives agenerator 38 that produces power. Arefrigerant pump 40 increases the pressure of the working fluid from arecuperator 40. The bottom cycle working fluid is in thermal communication with a cooling system such as awater circuit 42 through a water cooledcondenser 44. - By the nature of the proposed cycle, the vapor entering and leaving
turbine 36 is highly superheated. The energy potential of the superheated vapor at the turbine exit is not wasted, but is fed into arecuperator 46. Therecuperator 46 transfers heat from the low-pressure hot vapor from the turbine exit to the high pressure liquid at the pump exit. - The
recuperator 46 uses this superheat to preheat the liquid working fluid downstream of thepump 40. That is, if a cycle is driven to high turbine inlet superheat, then turbine outlet superheat will be high. The availability of this heat is thereby captured to maintain cycle efficiency as therecuperator 46 is an internal heat exchanger. When the low pressure side of thetopping cycle 22 is de-superheated, it is essentially recuperated into thebottoming cycle 24 which is where high superheat is achieved. Matching of the working fluids and the pressures thereof facilitates this interaction. - The
recuperator 46 is only in thebottoming cycle 24. As thetopping cycle 22 is not recuperated, its waste heat is captured by the condenser/evaporator 32. Both cycles are highly superheated yet avoid heat-exchanger pinches to minimize the heat-transfer temperature difference and minimize process irreversibility -
Figure 2 shows a TS diagram for thebottoming cycle 24. The condenser/evaporator 32 receives nearly saturated liquid (a temperature that is close to boiling) from therecuperator 46. The condenser/evaporator 32 boils then heats the refrigerant from state 6 to 1. Thestate 1 condition is highly superheated. The exit state from theturbine 36,state 2, is also highly superheated. Therecuperator 46 uses this heat (state 2 to 3) to heat the high pressure working fluid (state 5 to 6). Sizing of therecuperator 46 affects state 6. Asmaller recuperator 46, for example, results in less heat transferred and therefore a cooler more subcooled state at 6 which results in more heat transfer required from the condenser/evaporator 32, and a larger percentage of that heat in the preheating and evaporating regimes. -
Figure 3 shows a TS diagram for thetopping cycle 22. The exit state of thetopping cycle turbine 26 is highly superheated, but a recuperator is not used. Instead, the low pressure working fluid vapor is de-superheated as the bottoming cycle high-pressure working fluid is superheated. The choice of a heavy molecule such as Siloxane for thetopping cycle 22 results in the highly angled saturation dome. As a result, the inlet state toturbine 26 is only slightly superheated. -
- Where the subscripts A and B refer to streams A and B respectively, m is the mass flow rate, and h is the enthalpy of the fluid.
- In
Figure 4 , the warmer fluid (A) is shown to travel from right to left, and the colder fluid (B) to travel from left to right through the heat exchanger. Heat transfers from fluid A to fluid B; therefore, fluid A's enthalpy decreases while fluid B's enthalpy increases. For each section of the heat exchanger the above equation must be true. For example, the first 10% reduction in enthalpy of Fluid A must equal the last 10% increase of enthalpy of fluid B. If the fluids were simple fluids with constant specific heat, then each temperature profile would be a straight line. When the fluids are refrigerants, the temperature profiles have various non-linear shapes. When a fluid is saturated there is no change in temperature with change in enthalpy. The change in temperature with enthalpy is generally different for a fluid as a liquid than as a vapor; therefore, the choice of fluid and operational temperatures affect the shape of these curves. Furthermore, the choice of other system components will affect their shape. Specifically the choice of and the size of therecuperator 46 in the proposed cycle affects the starting enthalpy (and therefore temperature) of stream B. -
Figure 4 shows how each temperature profile relates to the other at each physical location along the heat exchanger. In order for heat to flow from Fluid A to Fluid B, Fluid A must always be warmer than Fluid B. If A gets too close to B this is referred to as a temperature "pinch" condition. This is undesirable because a large heat exchange area is required to exchange the enthalpy in this region. In fact, the entire size of a heat exchanger may be defined by a "pinch" condition. Where the temperature difference is large, the thermodynamic cycle will be less efficient since more entropy is generated by heat exchange through larger temperature differences. An ideal arrangement is when the temperature difference throughout the heat exchanger remains relatively constant. Since vapor heat exchange usually has a lower heat transfer rate than saturated, it may be desirable to maintain a somewhat higher temperature difference in this region, typically up to or equal to 1 to 2 times. For theORC system 20, the condenser/evaporator 32 heat exchanger has two major regions. The first (on the left inFigure 4 ) is saturated for both fluids and the temperature profiles are flat. This section covers about 40 percent of the total heat transfer in the disclosed non-limiting embodiment. The second (on the right inFigure 4 ) is superheated and temperature increases with enthalpy. That is, a percent saturation for a fluid in the toppingcycle 22 is maintained at 38 percent saturation compared to a 40 percent saturation for the working fluid in the bottomingcycle 24. - The point where the temperature profile transitions from flat (saturated) to increasing (vapor) will be identified herein as the "knee." For the above goals to be achieved, the "knee" of fluid A must lie equal to or slightly to the left of the "knee" of fluid B in the normalized enthalpy plot. If the "knee" lies far to the left then the saturated section may have a good heat transfer difference (typically 5 to 15F; 3 to 8C), but the heat transfer difference of the vapor section will be too large. If the "knee" lies too far to the right then a "pinch" condition will be created between the two fluids. Practically the temperature difference will increase and the saturated temperature difference will be too high.
- The effect of the
recuperator 46 on the condenser/evaporator 32 in the proposed cycle is to change the inlet enthalpy, and therefore temperature, of the colder fluid, B. By increasing the size of therecuperator 46, the enthalpy of the inlet of B increases by recovering heat from the turbine exit. This results in a smaller percentage of the total heat transfer for Fluid B occurring to the left of the knee, shifts the knee of B to the left and results in a pinch condition. Conversely, if the recuperator heat exchange is reduced or eliminated, this shifts knee of B to the right and therefore increases the temperature difference in the vapor section. That is, a percentage of total heat transfer from the working fluid in the toppingcycle 22 that occurs during a saturated condensation is equal to or slightly less (within 10%) than a percentage of total heat transfer to the working fluid in the bottomingcycle 24 that occurs during a saturated evaporation. - The selection of a high superheat cascaded cycle with a condenser/evaporator heat exchanger transferring heat from the topping cycle to the bottoming cycle, and the selection of refrigerants for the topping and bottoming cycles and recuperator in the bottoming cycle allows for optimized heat exchanger temperature profiles.
Claims (12)
- A cascaded Organic Rankine Cycle (ORC) system (20) comprising:a topping cycle (22); anda bottoming cycle (24) in thermal communication with said topping cycle (22) through a condenser/evaporator (32) in which a bottoming cycle (24) working fluid is first evaporated and then superheated and a topping cycle working fluid is first desuperheated and then condensed such that a percentage of total heat transfer from said topping cycle fluid that occurs during a saturated condensation is equal to or less than a percentage of total heat transfer to said bottoming cycle fluid that occurs during a saturated evaporation,characterized in that only said bottoming cycle (24) includes a recuperator (46).
- The system (20) as recited in claim 1, wherein said working fluid for said topping cycle (22) is Siloxane MM.
- The system (20) as recited in claim 1 or 2, wherein said working fluid for said bottoming cycle (24) is R245fa.
- The system (20) as recited in any preceding claim, wherein both said bottoming cycle fluid and said topping cycle fluid in the condenser/evaporator (32) are saturated over approximately 40% of said total heat transfer.
- The system (20) as recited in any preceding claim, further comprising a hot oil circuit (36) in thermal communication with said topping cycle (22) through an evaporator (34).
- The system (20) as recited in any preceding claim, further comprising a cooling circuit (42) in thermal communication with said bottoming cycle (24) through a condenser (44).
- A method of operating a cascaded Organic Rankine Cycle (ORC) system (20) in which a bottoming cycle (24) is in thermal communication with a topping cycle (24) comprising maintaining a percentage of total heart transfer from a working fluid in the topping cycle (22) at equal to or less than a percentage of total heart transfer to a working fluid in the bottoming cycle (24),
characterized in that only the working fluid in the bottoming cycle (24) is recuperated by use of a recuperator (46). - The method as recited in claim 7, further comprising:utilizing Siloxane MM as the working fluid in the topping cycle (22); and/orutilizing R245fa as the working fluid in the bottoming cycle (24).
- The method as recited in claim 7 or 8, further comprising utilizing a condenser/evaporator (32) as the thermal interface between the bottoming cycle (24) and the topping cycle (22).
- The method as recited in any of claims 7 to 9, further comprising operating a condenser/evaporator (32) as a condenser for the topping cycle (22) and as an evaporator for the bottoming cycle (24).
- The method as recited in any of claims 7 to 10, wherein a "knee" of the working fluid in the topping cycle (22) flowing right to left lies to the left of the "knee" of the working fluid of the bottoming cycle (24) flowing left to right in a normalized enthalpy plot.
- The method as recited in any of claims 7 to 11, wherein the working fluid in the topping cycle (22) and the working fluid in the bottoming cycle (24) are saturated over approximately 40 % of said total heat transfer.
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US13/334,994 US20130160449A1 (en) | 2011-12-22 | 2011-12-22 | Cascaded organic rankine cycle system |
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EP2607635A2 EP2607635A2 (en) | 2013-06-26 |
EP2607635A3 EP2607635A3 (en) | 2017-03-29 |
EP2607635B1 true EP2607635B1 (en) | 2021-01-20 |
EP2607635B8 EP2607635B8 (en) | 2021-03-24 |
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CN103925022A (en) * | 2014-03-21 | 2014-07-16 | 成信绿集成股份有限公司 | Two-stage power generation system and method using low and medium pressure steam |
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CA2798770A1 (en) | 2013-06-22 |
EP2607635A2 (en) | 2013-06-26 |
CN103174475B (en) | 2016-08-03 |
EP2607635B8 (en) | 2021-03-24 |
US20130160449A1 (en) | 2013-06-27 |
SG191468A1 (en) | 2013-07-31 |
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