• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
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    • 专利摘要:
    waste heat recovery system and method. the embodiments disclosed herein generally relate to the field of heat cycle systems for recovering waste heat (10), and more particularly, to a closed loop heat cycle system having a higher brayton cycle (12) and a lower rankine (14) to recover waste heat, and method for the same. the system comprises a Brayton cycle system (12) comprising a heater (16) configured to circulate carbon dioxide vapor in heat exchange relationship with a hot fluid to heat carbon dioxide vapour, a first turbine (18) ) coupled to the heater (16) and configured to expand the carbon dioxide vapor, a cooler (20) and a compressor (22) configured to compress the carbon dioxide vapor fed through the cooler (20) and a cycle system rankine (14) coupled to the brayton cycle system (12), wherein the rankine cycle system (14) comprises a first heat exchanger (28), a second heat exchanger (30), and a third heat exchanger ( 32), wherein carbon dioxide vapor from the first turbine (18) is circulated in heat exchange relationship with a sequentially vaporized working fluid through the first heat exchanger (28), the second heat exchanger (30) , and the third heat exchanger (32) pa To heat the working fluid in which a cooler (20) is configured to cool the carbon dioxide vapor fed through the first heat exchanger (28), the second heat exchanger (30), and the third heat exchanger ( 32), a fourth heat exchanger (34) configured to circulate the vaporized working fluid in heat exchange relationship with the carbon dioxide vapor fed from the compressor (22) to heat the working fluid; a second turbine (36) configured to expand the vaporized working fluid fed from the fourth heat exchanger (34) through the first heat exchanger (28) and a condenser (38) configured to condense the vaporized working fluid fed to from the second turbine (36) through the third heat exchanger (32).
    公开号:BR112012011468B1
    申请号:R112012011468-9
    申请日:2010-09-16
    公开日:2021-09-14
    发明作者:Matthew Alexander Lehar
    申请人:General Electric Company；
    IPC主号:
    专利说明:

    FIELD OF INVENTION
    [001] The present invention relates generally to the field of heat cycle systems for recovering waste heat, and more particularly, to a closed loop heat cycle system that has an upper Brayton cycle and a lower Rankine cycle for recover waste heat, and method for it. BACKGROUND OF THE INVENTION
    [002] Enormous amounts of waste heat are generated by a wide variety of industrial and commercial processes and operations. Examples of waste heat sources include heat sets from space heating, boilers, engines, and cooling systems. The term "waste heat" encompasses any supply of waste heat given off by a primary process that is not conventionally exploited as an energy source.
    [003] Some power generation systems provide improved safety and off-grid operation with alternative fuels such as biogas or landfill gases, with examples being gas turbines and combustion engines such as microturbines and reciprocating engines. Combustion engines can be generated to generate electricity using fuels such as gasoline, natural gas, biogas, vegetable oil, and diesel fuel. However, atmospheric pollutants such as nitrogen oxides and particulates can be emitted.
    [004] One method to generate electricity from the waste heat of a combustion engine without increasing emissions is to apply a lower Rankine steam cycle. A Rankine cycle typically includes a turbogenerator, an evaporator/boiler, a condenser, and a liquid pump. However, water-based Rankine steam cycles are not attractive in the low temperature waste heat regions mentioned above due to their high cost and low efficiency. The performance of an Organic Rankine Cycle (ORC) is limited by restrictions of the working fluid circulated within the ORC. Steam used as a working fluid may only be optimal for a specific range of cycling temperatures and pressures. This lower Rankine steam cycle requires condensing at relatively low pressure, which implies large turbines with low pressure and condenser volumes. Consequently the installation of a conventional lower Rankine steam cycle system is disproportionately voluminous, and complex considering the relatively small product derived from low temperature waste heat. The low pressure of steam condensation introduces other complexities, such as the need for special deaeration units to remove atmospheric air that leaks from the outside into subatmospheric pressure vessels.
    [005] It should be desirable to have a simple system and method that effectively recovers waste heat and is not limited by restrictions of a working fluid vapor circulated within a Rankine cycle system. DESCRIPTION OF THE INVENTION
    [006] According to an embodiment of the present invention, a waste heat recovery system is disclosed. The waste heat recovery system that includes a Brayton cycle system that has a heater configured to circulate carbon dioxide vapor in heat exchange relationship with a hot fluid to heat the carbon dioxide vapor. A Rankine cycle system is coupled to the Brayton cycle system and configured to circulate a working fluid in heat exchange relationship with carbon dioxide vapor to heat the working fluid.
    [007] According to another embodiment of the present invention, a method for operating the waste heat recovery system is disclosed.
    [008] According to an embodiment of the present invention, a waste heat recovery system is disclosed. The waste heat recovery system that includes a Brayton cycle system that has a heater configured to circulate carbon dioxide vapor in heat exchange relationship with a hot fluid from a heat source to heat carbon dioxide vapor. A Rankine cycle system is coupled to the Brayton cycle system and configured to circulate a working fluid in heat exchange relationship with the carbon dioxide vapor and hot fluid to heat the working fluid. BRIEF DESCRIPTION OF THE DRAWINGS
    [009] These and other features, aspects and advantages of the present invention will be better understood when the following detailed description is read with reference to the attached figures in which similar characters represent similar parts throughout the drawings, in which:- Figure 1 is a diagrammatic representation of a waste heat recovery system that has a Brayton cycle system and a Rankine cycle system according to an embodiment of the present invention;- Figure 2 is a flowchart illustrating steps involved in the method of system operation of waste heat recovery in accordance with an embodiment of the present invention; e- Figure 3 is a diagrammatic representation of a waste heat recovery system having a Brayton cycle system and a Rankine cycle system in accordance with an embodiment of the present invention. DESCRIPTION OF ACHIEVEMENTS OF THE INVENTION
    [0010] In accordance with the embodiment discussed in this document, a waste heat recovery system is disclosed. The system includes a Brayton cycle system (upper cycle) that has a heater configured to circulate carbon dioxide vapor in heat exchange relationship with a hot fluid to heat carbon dioxide vapor. A Rankine cycle system (lower cycle) is coupled to the Brayton cycle system and configured to circulate a working fluid in heat exchange relationship with carbon dioxide vapor to heat the working fluid. In accordance with the embodiment of the present invention, the waste heat recovery system is integrated with heat sources to enable high efficiency waste heat recovery for electricity generation. Heat sources can include combustion engine, gas turbine, geothermal, solar thermal, industrial and residential heat sources, and so on.
    [0011] Referring to Figure 1, a waste heat recovery system 10 is illustrated in accordance with an embodiment of the present invention. The system 10 which includes a Brayton cycle system (upper cycle) 12 coupled to a Rankine cycle system (lower cycle) 14. In the illustrated embodiment, the Brayton cycle system 12 which includes a heater 16, a first turbine 18, a refrigerator 20, and a compressor 22. Carbon dioxide vapor is circulated through the Brayton 12 cycle system.
    [0012] The heater 16 is coupled to a heat source 24, eg an exhaust unit of a heat generating system (eg an engine). The heater 16 receives heat from a hot fluid, for example an exhaust gas generated from the heat source, and heats carbon dioxide to heat carbon dioxide vapor. In a specific embodiment, the carbon dioxide vapor from heater 16 can be at a temperature of approximately 490°C and a pressure of approximately 20,000 kPa (200 bar). Carbon dioxide vapor is passed through the first turbine 18 to expand the carbon dioxide vapor and to drive a first generator 26 configured to generate electrical energy. In a specific embodiment, the carbon dioxide vapor from the first turbine 18 can be at a temperature of approximately 320°C and a pressure of approximately 4,000 kPa (40 bar).
    [0013] In the illustrated embodiment, the use of carbon dioxide as the working fluid has the advantage of being non-flammable, non-corrosive, non-toxic, and capable of withstanding high cycle temperatures (eg, above 400°C) . In an embodiment as described above, carbon dioxide can be super critically heated to high temperatures without risk of chemical decomposition.
    [0014] In the illustrated embodiment, the Rankine cycle system 14 which includes a first heat exchanger 28, a second heat exchanger 30, a third heat exchanger 32, and a fourth heat exchanger 34. A working fluid, per For example, a hydrocarbon fluid is circulated through the Rankine 14 cycle system. In a more specific embodiment, the working fluid may include an organic working fluid. The organic working fluid can include propane, butane, pentafluoro-propane, pentafluoro-butane, pentafluoro-polyether, oil, or combinations thereof. It should be noted in this document that this list of organic working fluids is not inclusive and other organic working fluids applicable to organic Rankine cycles are also provided. Carbon dioxide vapor from the first turbine 18 is circulated in heat exchange relationship with the vaporized working fluid sequentially through the first heat exchanger 28, the second heat exchanger 30, and the third heat exchanger 32 to heat the fluid. of work. In a specific embodiment, the carbon dioxide vapor at the outlet of the third heat exchanger 32 is at a temperature of 85°C and a pressure of 4,000 kPa (40 bar). Carbon dioxide from the third heat exchanger 32 is fed through the cooler 20 to cool the carbon dioxide vapor. The refrigerated carbon dioxide vapor is then compressed to a substantially greater pressure through compressor 22. In one embodiment, carbon dioxide vapor from compressor 22 is at a temperature of approximately 210°C and a pressure of approximately 20,000 kPa (200 bar). In one embodiment, compressor 22 can be a multi-stage compressor with an intercooler disposed between each compressor stage.
    [0015] Compressed carbon dioxide vapor from compressor 22 is circulated in heat exchange relationship with the working fluid through the fourth heat exchanger 34 to heat the vaporized working fluid to reduce the temperature of the carbon dioxide vapor. carbon enough, to absorb calluses at temperatures as low as, for example, 120°C from the waste heat source 24. This facilitates maximum extraction of heat from the waste heat source 24. In a specific embodiment, the vaporized working fluid a from the fourth heat exchanger 34 it can be at a temperature of approximately 170°C and a pressure of approximately 6,000 kPa (60 bar). In other words, the vaporized working fluid is in a supercritical state. The cycle is repeated in the Brayton cycle system 12. The working fluid vaporized from the fourth heat exchanger 34 is then fed through the first heat exchanger 28 in heat exchange relationship with the carbon dioxide vapor to heat additionally the vaporized working fluid. In one embodiment, the working fluid vaporized at the outlet of the first heat exchanger 28 has a temperature of approximately 205°C and a pressure of approximately 6,000 kPa (60 bar).
    [0016] The Rankine cycle system 14 additionally includes a second turbine 36, a condenser 38, a pump 40, and a flow divider device 42. The vaporized working fluid is passed through the second turbine 36 to expand the working fluid vaporized and to drive a second generator 44 configured to generate electrical energy. In a specific embodiment, the second turbine working fluid is at a temperature of approximately 105°C and a pressure of approximately 500 kPa (5 bar). The second turbine 36 may be an axial type expander, impulse type expander, or high temperature screw type expander, radial inlet flow expander type turbine. In other words, the vaporized working fluid is in a subcritical state. The expanded vaporized working fluid from the second turbine 36 is fed through the third heat exchanger 32 in heat exchange relationship with the carbon dioxide vapor. In one embodiment, the working fluid vaporized from the third heat exchanger 32 has a temperature of approximately 65°C and a pressure of approximately 500 kPa (5 bar).
    [0017] After passing through the second turbine 36, the vaporized working fluid is passed through the third heat exchanger 32 to the condenser 38. The vaporized working fluid is condensed into a liquid to generate a condensed working fluid. In a specific embodiment, the condensed working fluid has a temperature of approximately 50°C and a pressure of approximately 500 kPa (5 bar). The condensed working fluid is then pumped at a relatively higher pressure using a pump 40 through the third heat exchanger 32 to the flow divider device 42. Pressurizing and reheating the working fluid results in gradual phase change of state liquid to the vapor state. In a specific embodiment, the working fluid at the outlet of the third heat exchanger is at a temperature of approximately 100°C and a pressure of approximately 6,000 kPa (60 bar).
    [0018] In the illustrated embodiment, the flow divider device 42 divides the flow of working fluid from the third heat exchanger 32 into two parts. The flow divider device 42 is configured to feed a portion of the vaporized working fluid from the third heat exchanger 32 to the fourth heat exchanger 34 and another portion of the vaporized working fluid from the third heat exchanger 32 to a point 46 upstream of the first heat exchanger 28. The other part of the vaporized working fluid from the third heat exchanger 32 is mixed with the vaporized working fluid fed from the fourth heat exchanger 34 to the first heat exchanger 28. The cycle is repeated in the Rankine 14 cycle system.
    [0019] In the illustrated embodiment, there are a plurality of heat exchanger instances (may also be referred to as "intra-cycle" heat transfer) between carbon dioxide vapor and the vaporized working fluid. This heat exchange between the carbon dioxide vapor and the working fluid is vaporized through heat exchangers 28, 30, 32, and 34. This heat exchange serves to boil (if the working fluid is at subcritical temperature) or otherwise increase the enthalpy (if the working fluid is at supercritical temperature) of the working fluid in the Rankine 14 cycle system.
    [0020] According to the embodiment discussed in this document, in the Brayton 12 cycle system, carbon dioxide is heated directly (without transferring heat through an intermediate fluid) by a source of waste heat. Carbon dioxide vapor is expanded to produce electrical energy. The heat from the carbon dioxide vapor is transferred to the hydrocarbon fluid circulated in the Rankine 14 cycle system through the series of heat exchangers 28, 30, 32, and 34. The carbon dioxide is circulated in the vapor state in the system. Brayton 12 cycle, while in the Rankine 14 cycle system; the hydrocarbon fluid is cooled and condensed to a liquid phase prior to re-pressurization and heating.
    [0021] As discussed above, the use of carbon dioxide as a working fluid in the Brayton 12 cycle system has the advantage that carbon dioxide must remain inert even at substantially higher temperatures, eg in the range of 300 to 600°C. Also, carbon dioxide does not undergo significant chemical decomposition at higher temperatures which facilitate greater system efficiency. System 10 operates at significantly higher pressures, for example 7,000 to 20,000 kPa (70 to 200 bar). Consequently system 10 is compact and simple. The cycle fluid remains pure and does not require the deaeration units typical of steam installations. The combination of a Brayton cycle system operating on carbon dioxide as a process fluid and a Rankine cycle system effectively extracts heat from a high temperature heat source and at the same time efficiently converts low temperature waste heat to electrical energy .
    [0022] Referring to Figure 2, a flowchart is disclosed illustrating steps involved in the method of operation of the waste heat recovery system 10. The method involves circulating carbon dioxide vapor in heat exchange relationship with a hot fluid through of heater 16 of the Brayton cycle system 12 as represented by step 48. Heater 16 receives heat from a hot fluid, e.g., an exhaust gas generated from the heat source, and heats carbon dioxide to heat carbon dioxide vapor. carbon. Carbon dioxide vapor is passed through the first turbine 18 to expand the carbon dioxide vapor as represented by step 50. In other words, the carbon dioxide vapor is passed through the first turbine 18 to expand the dioxide vapor of carbon and to drive the first generator 26 configured to generate electrical energy.
    [0023] The carbon dioxide vapor from the first turbine 18 is circulated in heat exchange relationship with the vaporized working fluid sequentially through the first heat exchanger 28, the second heat exchanger 30, and the third heat exchanger 32 of the Rankine cycle system 14 to heat the working fluid as represented by step 52. Carbon dioxide from the third heat exchanger 32 is fed through cooler 20 to cool the carbon dioxide vapor as represented by step 54. The refrigerated carbon dioxide vapor is then compressed to a substantially greater pressure through compressor 22 as represented by step 56. Compressed carbon dioxide vapor from compressor 22 is then circulated in heat exchange relationship with the vaporized working fluid through the fourth heat exchanger 34 to heat the vaporized working fluid as represented by step 58. The cycle is repeated at Brayton 12 cycle system.
    [0024] The vaporized working fluid from the fourth heat exchanger 34 is then fed through the first heat exchanger 28 in heat exchange relationship with the carbon dioxide vapor to further heat the vaporized working fluid. The vaporized working fluid is passed through the second turbine 36 of the Rankine cycle system 14 to expand the vaporized working fluid and to drive the second generator 44 configured to generate electrical energy as represented by step 60. second turbine 36 is fed through third heat exchanger 32 in heat exchange relationship with carbon dioxide vapor.
    [0025] After passing through the second turbine 36, the vaporized working fluid is passed through the third heat exchanger 32 to the condenser 38 as represented by step 62. The vaporized working fluid is condensed into a liquid, to generate a fluid of condensed work. The condensed working fluid is then pumped at a relatively higher pressure using a pump 40 through the third heat exchanger 32 to the flow divider device 42 as represented by step 64. Pressurizing and reheating the working fluid results in shifting phase gradient from liquid to vapor state.
    [0026] In the illustrated embodiment, the flow divider device 42 divides the flow of working fluid from the third heat exchanger 32 into two parts. The method includes feeding a portion of the vaporized working fluid from the third heat exchanger 32 to the fourth heat exchanger 34 as represented by step 66. The method further includes feeding another portion of the vaporized working fluid from the third heat exchanger. heat 32 to a point 46 upstream of the first heat exchanger 28 as represented by step 68. The other portion of the vaporized working fluid from the third heat exchanger 32 is mixed with the vaporized working fluid fed from the fourth heat exchanger 34 to the first heat exchanger 28 as represented by step 70. The cycle is repeated in the Rankine 14 cycle system.
    [0027] With reference to Figure 3, a waste heat recovery system 72 is illustrated in accordance with an embodiment of the present invention. The system 72 which includes a Brayton cycle system (upper cycle) 74 coupled to a Rankine cycle system (lower cycle) 76. In the illustrated embodiment, the Brayton cycle system 74 which includes a heater 77, a turbine 78, a cooler 80, a first compressor stage 82, a second compressor stage 84, and an intercooler 86 disposed between the first compressor stage 82 and the second compressor stage 84. The carbon dioxide vapor is circulated through the loop system. Brayton 74.
    [0028] Heater 77 is coupled to a heat source 88, eg an exhaust unit of a heat generating system (eg an engine). Heater 77 receives heat from a hot fluid, for example an exhaust gas generated from the heat source, and heats carbon dioxide to heat carbon dioxide vapor. Carbon dioxide steam is passed through turbine 78 to expand the carbon dioxide steam and to drive a generator 90 configured to generate electrical power.
    [0029] In the illustrated embodiment, the Rankine cycle system 76 includes a plurality of heat exchangers 92, 94, 96. A working fluid, e.g., a hydrocarbon fluid, is circulated through the Rankine cycle system 76. Carbon dioxide from turbine 78 is circulated in heat exchange relationship with the vaporized working fluid sequentially through heat exchangers 92, 94, 96 to heat the working fluid. Carbon dioxide from heat exchanger 96 is fed through cooler 80 to cool the carbon dioxide vapor. The cooled carbon dioxide vapor is then compressed to substantially higher pressures through the first stage compressor 82 and the second stage compressor 84. The carbon dioxide vapor from the first stage compressor 82 is cooled through the intercooler 86 and then fed to the second compressor stage 84.
    [0030] Compressed carbon dioxide vapor from the second stage of compressor 84 is circulated in heat exchange relationship with hot fluid from heat source 88 through heater 77 to heat the carbon dioxide vapor. The heat transmitted to the carbon dioxide vapor stream by each compression stage can be removed through refrigeration or by the vaporized working fluid or by ambient air, in order to reduce the energy investment required to drive the compressor. The cycle is repeated on the Brayton 12 cycle system.
    [0031] In the illustrated embodiment, the vaporized working fluid from the Rankine cycle system 76 is also circulated in heat exchange relationship with the hot fluid from the heat source 88 through heater 77 to heat the vaporized working fluid. In other words, heat from heat source 88 is used to heat both the carbon dioxide vapor and working fluid vaporized through heater 77. To be more specific, heat from heat source 88 is used first to heat carbon dioxide vapor and then heat the vaporized working fluid.
    [0032] The Rankine cycle system 76 additionally includes a turbine 98, a condenser 100, a pump 102, and a flow divider device 104. The vaporized working fluid is passed through the turbine 98 to expand the vaporized working fluid and to drive a generator 106 configured to generate electrical energy. The expanded vaporized working fluid from turbine 98 is fed through heat exchanger 96 in heat exchange relationship with the return flow of condensed working fluid from pump 102.
    [0033] After passing through the turbine 98, the vaporized working fluid is passed through the heat exchanger 96 to the condenser 100. The vaporized working fluid is condensed into a liquid, to generate a condensed working fluid. The condensed working fluid is then pumped at a relatively higher pressure using the pump 102 through the third heat exchanger 96 to the flow divider device 104. The pressurized liquid working fluid from the pump 102 is heated within the heat exchanger 96, first by the expanded working fluid vapor flow entering the heat exchanger 96 of the turbine 98, and then by the carbon dioxide vapor flow also passing through the heat exchanger 96. The pressurization and reheating of the fluid result in gradual phase change from liquid to vapor state.
    [0034] In the illustrated embodiment, the flow divider device 104 divides the flow of working fluid from the third heat exchanger 96 into two parts. The flow divider device 104 is configured to feed a portion of the vaporized working fluid from the third heat exchanger 96 to the heater 77 and another portion of the vaporized working fluid from the heat exchanger 96 fed through the heat exchanger 94, is supplied to a point 108 upstream of the heat exchanger 92. The working fluid is further heated by the carbon dioxide vapor stream. The last portion of the vaporized working fluid from heat exchanger 96 is mixed at point 108 with the vaporized working fluid fed from heater 77 to heat exchanger 92. The cycle is repeated in the Rankine cycle system 76.
    [0035] Although only certain features of the invention have been illustrated and described in this document, many modifications and changes will occur for those skilled in the art. Therefore it is to be understood that the appended claims are intended to cover all such modifications and changes as being within the scope of the invention.
    权利要求:
    Claims (12)
    [0001]
    1. RESIDUAL HEAT RECOVERY SYSTEM, comprising: a Brayton cycle system (12) comprising: a heater (16) configured to circulate carbon dioxide steam in heat exchange relationship with a hot fluid to heat the steam of carbon dioxide; a first turbine (18) coupled to the heater (16) and configured to expand the carbon dioxide vapor; a cooler (20) configured to cool the carbon dioxide vapor; and a compressor (22) configured to compress carbon dioxide vapor fed through the cooler (20); and a Rankine cycle system (14) coupled to the Brayton cycle system (12) and configured to circulate a working fluid in heat exchange relationship with carbon dioxide vapor to heat the working fluid, in which the Rankine cycle (14) comprises: a first heat exchanger (28), a second heat exchanger (30), and a third heat exchanger (32), wherein the carbon dioxide vapor from the first turbine (18) is circulated in heat exchange relationship with a vaporized working fluid sequentially through the first heat exchanger (28), the second heat exchanger (30), and the third heat exchanger (32) to heat the working fluid; wherein a cooler (20) is configured to cool carbon dioxide vapor fed through the first heat exchanger (28), the second heat exchanger (30) and the third heat exchanger (32); a fourth heat exchanger heat (34) configured to circulate the vaporized working fluid in heat exchange relationship with the carbon dioxide vapor fed from the compressor (22) to heat the working fluid; a second turbine (36) configured to expand the vaporized working fluid fed from the fourth heat exchanger (34) through the first heat exchanger (28); and the system being characterized by further comprising: a condenser (38) configured to condense the vaporized working fluid fed from the second turbine (36) through the third heat exchanger (32); a pump (40) configured to pressurize and supply the vaporized working fluid from the condenser (38) to the third heat exchanger (32) to vaporize the condensed working fluid, and a flow divider device (42) configured to feed a portion of the vaporized working fluid from the pump (40) through the third heat exchanger (32) to the fourth heat exchanger (34) and another portion of the vaporized working fluid from the pump (40) through the third heat exchanger (32) to a point (46) upstream of the first heat exchanger (28), wherein the other portion of the vaporized working fluid from the pump (40) through the third heat exchanger (32) is mixed with the vaporized working fluid fed from the fourth heat exchanger (34) to the first heat exchanger (28).
    [0002]
    2. SYSTEM according to claim 1, characterized in that the Brayton cycle system (12) system comprises a first generator (26) coupled to the first turbine (18) and configured to generate energy.
    [0003]
    3. SYSTEM according to claim 1, characterized in that the Rankine cycle system (14) comprises a second generator (44) coupled to the second turbine (36) and configured to generate energy.
    [0004]
    4. SYSTEM according to claim 1, characterized in that the Rankine cycle system (14) comprises a pump (40) configured to pressurize and feed the condensed working fluid from the condenser (38) to the third heat exchanger ( 32) to vaporize the condensed working fluid.
    [0005]
    5. SYSTEM according to claim 4, characterized in that the Rankine cycle system (14) comprises a flow divider device (42) configured to feed a portion of the vaporized working fluid from the third heat exchanger (32) to the fourth heat exchanger (34) and another part of the working fluid vaporized from the third heat exchanger (32) to a point upstream of the first heat exchanger (28), wherein the other part of the working fluid vaporized the from the third heat exchanger (32) is mixed with the vaporized working fluid fed from the fourth heat exchanger (34) to the first heat exchanger (28).
    [0006]
    6. SYSTEM according to claim 1, characterized in that the working fluid comprises a hydrocarbon.
    [0007]
    7. METHOD OF RESIDUAL HEAT RECOVERY, which comprises: circulating carbon dioxide vapor in heat exchange relationship with a hot fluid to heat the carbon dioxide vapor through a heater (16) of a Brayton cycle system ( 12), in which the Brayton cycle system (12) is coupled to a Rankine cycle system (14); expanding the carbon dioxide vapor through a first turbine (26) coupled to the heater (16) of the cycle system Brayton (12); circulating carbon dioxide vapor from the first turbine (26) in heat exchange relationship with a sequentially vaporized working fluid through a first heat exchanger (28), a second heat exchanger ( 30), and a third heat exchanger (32) of the Rankine cycle system (14) for heating the vaporized working fluid; cooling carbon dioxide vapor fed through the first heat exchanger (28), the second heat exchanger (30) and the third heat exchanger (32) through a cooler (20) of the Brayton cycle system (12) ; compress the carbon dioxide vapor fed through the cooler (20) through a compressor (22) of the Brayton cycle system (12); circulate the vaporized working fluid in heat exchange relationship with the carbon dioxide vapor fed from the compressor (22) to heat the vaporized working fluid through a fourth heat exchanger (34) of the Rankine cycle system (14); expand the vaporized working fluid fed through the fourth heat exchanger (34) , from the first heat exchanger (28) through a second turbine (36) of the Rankine cycle system (14); the method being characterized by condensing the vaporized working fluid fed from the second turbine (36) through the third heat exchanger. heat (32), using a condenser (38) of the Rankine cycle system (14); pressurizing and feeding (64) the vaporized working fluid from the condenser (38) to the third heat exchanger (32) by means of a pump (40) of the system of Rankine cycle (14), feeding (66, 68) a part of the vaporized working fluid from the pump (40) through the third heat exchanger (32) to the fourth heat exchanger (34) and another part of the working fluid vaporized from the pump (40) through the third heat exchanger (32) to a point (46) upstream of the first heat exchanger (28) by means of a flow divider device (44) of the Rankine cycle system (14) , mixing (70) the other portion of the vaporized working fluid from the pump (40) through the third heat exchanger (32) with the vaporized working fluid fed from the fourth heat exchanger (34) to the first heat exchanger (28 ).
    [0008]
    8. METHOD according to claim 7, characterized in that the method further comprises generating energy through a first generator (26) coupled to the first turbine (18) of the Brayton cycle system (12).
    [0009]
    9. METHOD, according to claim 7, characterized in that the method further comprises generating energy through a second generator (44) coupled to the second turbine (36) of the Rankine cycle system (14).
    [0010]
    10. METHOD according to claim 7, characterized in that the method further comprises pressurizing and feeding the condensed working fluid from the condenser (38) to the third heat exchanger (32) through a pump (40) of the heat system. Rankine cycle (14).
    [0011]
    11. METHOD according to claim 10, characterized in that the method further comprises feeding a part of the vaporized working fluid from the third heat exchanger (32) to the fourth heat exchanger (34) and another part of the working fluid vaporized from the third heat exchanger (32) to a point upstream of the first heat exchanger (28) via a flow divider device (42) of the Rankine cycle system (14).
    [0012]
    12. METHOD according to claim 11, characterized in that the method further comprises mixing the other part of the vaporized working fluid from the third heat exchanger (32) with the vaporized working fluid fed from the fourth heat exchanger ( 34) for the first heat exchanger (28).
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    同族专利:
    公开号 | 公开日
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    GB1105521A|1963-10-18|1968-03-06|Lancelot Walter Bamford|Improvements in or relating to closed-cycle gas turbine plant|
    US3466871A|1967-04-07|1969-09-16|Gen Motors Corp|Turbine power plant|
    US3913315A|1971-05-17|1975-10-21|Foster Wheeler Energy Corp|Sulfur recovery from fluidized bed which heats gas in a closed circuit gas turbine|
    US4358930A|1980-06-23|1982-11-16|The United States Of America As Represented By The United States Department Of Energy|Method of optimizing performance of Rankine cycle power plants|
    US4573321A|1984-11-06|1986-03-04|Ecoenergy I, Ltd.|Power generating cycle|
    JPS62502209A|1985-03-15|1987-08-27|
    US5317904A|1989-11-27|1994-06-07|4E Co.|Method of and apparatus for conditioning air|
    SU1795128A1|1990-01-30|1993-02-15|Andrej V Polupan|Power-generating unit|
    US5431016A|1993-08-16|1995-07-11|Loral Vought Systems Corp.|High efficiency power generation|
    US5799490A|1994-03-03|1998-09-01|Ormat Industries Ltd.|Externally fired combined cycle gas turbine|
    DE4409567A1|1994-03-21|1995-09-28|Abb Management Ag|Process for cooling thermally loaded components of a gas turbine group|
    US6170264B1|1997-09-22|2001-01-09|Clean Energy Systems, Inc.|Hydrocarbon combustion power generation system with CO2 sequestration|
    GB2307277A|1995-11-17|1997-05-21|Branko Stankovic|Combined cycle powerplant with gas turbine cooling|
    US6960839B2|2000-07-17|2005-11-01|Ormat Technologies, Inc.|Method of and apparatus for producing power from a heat source|
    US20040265651A1|2003-06-27|2004-12-30|Meyer Steinberg|Combined-Cycle Energy, Carbon and Hydrogen Production Process|
    AU2005318868A1|2004-12-24|2006-06-29|Renewable Energy Systems Limited|Methods and apparatus for power generation|
    US7961835B2|2005-08-26|2011-06-14|Keller Michael F|Hybrid integrated energy production process|
    US20070163261A1|2005-11-08|2007-07-19|Mev Technology, Inc.|Dual thermodynamic cycle cryogenically fueled systems|
    JP4724848B2|2006-04-21|2011-07-13|独立行政法人日本原子力研究開発機構|Combined Brayton cycle power generation system using nuclear heat|
    US7685820B2|2006-12-08|2010-03-30|United Technologies Corporation|Supercritical CO2 turbine for use in solar power plants|US20100212316A1|2009-02-20|2010-08-26|Robert Waterstripe|Thermodynamic power generation system|
    US8522552B2|2009-02-20|2013-09-03|American Thermal Power, Llc|Thermodynamic power generation system|
    US8459029B2|2009-09-28|2013-06-11|General Electric Company|Dual reheat rankine cycle system and method thereof|
    US8887503B2|2011-12-13|2014-11-18|Aerojet Rocketdyne of DE, Inc|Recuperative supercritical carbon dioxide cycle|
    US9540999B2|2012-01-17|2017-01-10|Peregrine Turbine Technologies, Llc|System and method for generating power using a supercritical fluid|
    CN104662262B|2012-08-22|2017-09-08|海埃芙实用救援有限责任公司|High efficiency electricity generation system and system upgrade|
    US10260415B2|2012-08-22|2019-04-16|Hi Eff Utility Rescue LLC|High efficiency power generation system and system upgrades|
    US9540959B2|2012-10-25|2017-01-10|General Electric Company|System and method for generating electric power|
    US9410451B2|2012-12-04|2016-08-09|General Electric Company|Gas turbine engine with integrated bottoming cycle system|
    EP2954175A4|2013-01-24|2016-11-30|Hinders Edward|Combined brayton/rankine cycle gas and steam turbine generating system operated in two closed loops|
    CN103161607A|2013-03-04|2013-06-19|西安交通大学|Combined power generating system based on waste-heat utilization of combustion motor|
    US9145795B2|2013-05-30|2015-09-29|General Electric Company|System and method of waste heat recovery|
    US9260982B2|2013-05-30|2016-02-16|General Electric Company|System and method of waste heat recovery|
    US9593597B2|2013-05-30|2017-03-14|General Electric Company|System and method of waste heat recovery|
    US9587520B2|2013-05-30|2017-03-07|General Electric Company|System and method of waste heat recovery|
    US9702270B2|2013-06-07|2017-07-11|Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources|Hybrid Rankine cycle|
    US9453433B2|2013-06-21|2016-09-27|Sankar K. Mohan|Systems and methods for reducing parasitic losses in closed loop systems|
    ES2848307T3|2014-09-08|2021-08-06|Siemens Ag|System and method of recovery of residual thermal energy|
    US9644502B2|2015-04-09|2017-05-09|General Electric Company|Regenerative thermodynamic power generation cycle systems, and methods for operating thereof|
    CN105953454B|2015-04-13|2021-04-20|李华玉|Bidirectional thermodynamic cycle and first-class thermally-driven compression heat pump|
    US9976448B2|2015-05-29|2018-05-22|General Electric Company|Regenerative thermodynamic power generation cycle systems, and methods for operating thereof|
    CN106246265A|2015-06-08|2016-12-21|淮安信息职业技术学院|A kind of use Boulez pause circulation device for generating power by waste heat of tail gas of automobile|
    CN106246406A|2015-06-08|2016-12-21|淮安信息职业技术学院|A kind of use enclosed Boulez pause circulation device for generating power by waste heat of tail gas of automobile|
    EP3106645B1|2015-06-15|2018-08-15|Rolls-Royce Corporation|Gas turbine engine driven by sco2 cycle with advanced heat rejection|
    EP3109433B1|2015-06-19|2018-08-15|Rolls-Royce Corporation|Engine driven by sc02 cycle with independent shafts for combustion cycle elements and propulsion elements|
    EP3121409B1|2015-07-20|2020-03-18|Rolls-Royce Corporation|Sectioned gas turbine engine driven by sco2 cycle|
    EP3147219B1|2015-09-23|2021-03-17|Rolls-Royce Corporation|Propulsion system using supercritical co2 power transfer|
    US9510486B1|2016-07-13|2016-11-29|Matteo B. Gravina|Data center cooling system having electrical power generation|
    CN106089337B|2016-08-10|2017-07-07|西安热工研究院有限公司|For the supercritical CO of waste heat recovery2With organic Rankine association circulating power generation system|
    BR112019005434A2|2016-09-22|2019-06-18|Gas Technology Inst|power cycle systems and methods|
    US9907213B1|2016-12-12|2018-02-27|Matteo B. Gravina|Data center cooling system having electrical power generation|
    US10020436B1|2017-06-15|2018-07-10|Matteo B. Gravina|Thermal energy accumulator for power generation and high performance computing center|
    WO2019035896A1|2017-08-15|2019-02-21|Enhanced Energy Group, Llc|Improved method and system of carbon sequestration and carbon negative power system|
    US11204190B2|2017-10-03|2021-12-21|Enviro Power, Inc.|Evaporator with integrated heat recovery|
    CN110905611B|2019-11-28|2021-08-17|中南大学|Combined supply system based on organic Rankine cycle and supercritical carbon dioxide cycle|
    CN110863961B|2019-11-28|2021-08-31|西安石油大学|Supercritical CO2Recompression brayton and LNG combined cycle power generation system|
    法律状态:
    2020-09-08| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2020-10-20| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2021-07-06| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2021-09-14| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 16/09/2010, OBSERVADAS AS CONDICOES LEGAIS. PATENTE CONCEDIDA CONFORME ADI 5.529/DF, QUE DETERMINA A ALTERACAO DO PRAZO DE CONCESSAO. |
    优先权:
    申请号 | 申请日 | 专利标题
    US12/618,958|US8490397B2|2009-11-16|2009-11-16|Compound closed-loop heat cycle system for recovering waste heat and method thereof|
    US12/618,958|2009-11-16|
    PCT/US2010/049080|WO2011059563A2|2009-11-16|2010-09-16|Compound closed-loop heat cycle system for recovering waste heat and method thereof|
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