US3769789A - Rankine cycle engine - Google Patents

Rankine cycle engine Download PDF

Info

Publication number
US3769789A
US3769789A US00159804A US3769789DA US3769789A US 3769789 A US3769789 A US 3769789A US 00159804 A US00159804 A US 00159804A US 3769789D A US3769789D A US 3769789DA US 3769789 A US3769789 A US 3769789A
Authority
US
United States
Prior art keywords
feed liquid
heater
turbine
regenerator
vapor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US00159804A
Other languages
English (en)
Inventor
R Niggemann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sundstrand Corp
Original Assignee
Sundstrand Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sundstrand Corp filed Critical Sundstrand Corp
Application granted granted Critical
Publication of US3769789A publication Critical patent/US3769789A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
    • 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
    • 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
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
    • F01K3/20—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters with heating by combustion gases of main boiler
    • F01K3/22—Controlling, e.g. starting, stopping
    • 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
    • F01K9/00—Plants characterised by condensers arranged or modified to co-operate with the engines
    • F01K9/02—Arrangements or modifications of condensate or air pumps
    • F01K9/023—Control thereof

Definitions

  • CL 60/36 60/107 122/479 R toluene including a supercritical heater for vaporizing [51] Int 170" 25/00 the organic feed liquid, a turbine for expanding the [58] Field of Sear'ch 122/479 vapor and providing a mechanical output, a regenera- 122/256 tor for receiving superheated vapor from the turbine and preheating a portion of the feed liquid to the main [56] References Cited heater, and an economizer built around the main heater for preheating a portion of the feed liquid, cool- UNITED STATES PATENTS ing the exiting combustion gases in the economizer and 2,160,644 5/1939 Clarkson l22/250 R directing the preheated liquid to the main heater along 312 et 232 with feed liquid from the regenerator.
  • a supercritical heater for vaporizing [51] Int 170" 25/00 the organic feed liquid
  • a turbine for expanding the [58] Field of Sear'ch 122/479 vapor
  • organic fluids provide a wide range of freezing points, thermal stability, system pressure level and cost, that enable one or more fluids to be particularly useful in a given power conversion system.
  • the present invention has applicability to the generation of mechanical or electric power from thermal power. In some applications there is a low temperature start-up requirement that would render undesirable any fluid that is frozen, slushy, or even highly viscous at the start-up temperature. Because of the high temperature degradation with the resulting noncondensable gas production in organic fluids, it is desirable that the organic fluid have good thermal stability. 1
  • a power conversion system employing toluene as the working fluid.
  • Toluene is typical of the organic working fluids in that the vapor superheats upon expansion from a high to a low pressure. This results in a fairly low prime mover isentropic head and a relatively slow turbine tip speed so that a single stage turbine can be employed at its best efficiency safely within the turbine wheel stress limits.
  • the major components in the system are a supercritical heater-economizer, a single-stage turbine which may drive an alternator, a regenerator, a condenser and a feed pumprToluene is the working fluid because of its -1 39 FJfreezing point, its good thermal stability, its relatively high system pressure level which leads to compact heat transfer equipment, and its commercial availability.
  • the supercritical system cycle is selected so that the boiler becomes a liquid heater that precludes hydrodynamic instability, makes very high heat transfer rates possible without excessive wall temperatures, and results in a very small fluid inventory in the heater which minimizes fluid degradation and stored energy.
  • the heater-economizer may be a compact cylindrical unit with the burner surrounded by the heat exchanger.
  • combustion gases pass over the heat absorbing surfaces of the heater, heating the mixed flows from the regenerator liquid outlet and the economizer liquid outlet to the vapor outlet temperature in the heater.
  • the economizer feed liquid flow, preheated, is mixed with the other feed liquid (approximately 80 percent) of the system flow at the heater inlet.
  • the percent feed liquid flow passes from the feed pump outlet through the vapor-liquid regenerator. Because of the relatively high back pressure provided in the system through the useof toluene, the regenerator is quite small even though 20 percent of feed liquid bypasses the regenerator, requiring increased heat exchange capacity in place of unavailable liquid.
  • the passing of 20 percent of the feed flow through an economizer allows a significant reduction in flue gas stack loss and a commensurate increase in plant efficiency.
  • the high pressure hot fluid from the heater outlet passes through a suitable vapor flow control device to a single stage impulse turbine.
  • the turbine may be connected to drive either directly or through a gear box alternator and also a system pump.
  • the turbine exhaust is passed through the vapor side of the regenerator where it preheats the feed liquid on its way to the heater. From the exit of the regenerator, the vapor is ducted to a condenser where the waste heat is rejected to the condenser coolant.
  • this waste heat can be utilized for heating and/or for driving an adsorption air conditioner.
  • a device for separating the noncondensable gases that are present in the vapor in the condenser. This device confines the concentrated noncondensable gases in a separate container and prevents noncondensable gas accumulation. in the condenser. If these gases were allowed to accumulate in the condenser such that the noncondensable gas partial pressure approached 1 percent of the total condenser pressure, the resulting reduced condensing coefficient would increase condenser pressure and reduce cycle efficiency. From the condenser the condensate drains into a hotwell. A jet pump draws condensate from the hotwell and increases pressure to system inlet pressure. The system pump has two outlets providing high pressure primary flow to the system and also low pressure flow to the jet pump. This minimizes the system pumping power. The main system flow is'directed from the impeller pump to the regenerator and to the economizer. 1
  • Toluene was selected as the system working fluid for several reasons. It has a 1 39 F. freezing temperature which makes it desirable for cold. starts. The thermal stability of toluene is greater than most organic fluids. Toluene has a high back pressure in an air cooled Rankine cycle power system, i.e., 8 psi at 200 F. The high back pressure in a toluene system permits a small high speed turbine, and a low volume and low weight regenerator, even with 20 percent of the liquid feed bypassed to the economizer.
  • Toluene has thermal stability capabilities at temperatures well in excess of its critical temperature which allows the use of a compact, high heat flux, low fluid inventory supercritical vaporizer, where low inventory subcritical vaporizers (once-through boilers) are subject to hydrodynamic instability.
  • the net result is a minimization of component size which is desirable from a packaging standpoint, and a maximization of plant efficiency due to the incorporation of the economizer utilizing regenerator bypass liquid and also due to the ability to operate at high turbine inlet temperature which is allowed by the basic good thermal stability of toluene and also because of the very low fluid inventory in the heater as a result of the supercritical vaporizer.
  • FIG. 1 is a schematic illustration of a power conversion system according to the present invention.
  • FIG. 2 is a schematic illustration of a heatereconomizer according to the present invention.
  • a power conversion system is seen to include, generally, a heater-economizer 12 which delivers toluene vapor to a turbine 14, with exhaust vapor from the turbine passing through a regenerator 15 decreasing the vapor temperature and increasing the temperature of the feed liquid to the heater-economizer 12.
  • the vapor from the regenerator is condensed in condenser 16 and the condensate passes to hotwell 18 with the noncondensable gases being separated by separator 20.
  • a jet pump 22 withdraws condensate from hotwell 18 and conveys the same to a pump 25 which supplies feed liquid to the system.
  • a start tank 27 is provided for filling the system during start-up.
  • the jet pump 22 is provided to boost the pressure level of condensate in hotwell 18 up to a pressure which will prevent cavitation of the main system condensate pump 25.
  • Jet pump 22 delivers fluid to main system pump 25 which may be a stepped impeller pump having two outlet diffusers at different radii.
  • the inner diffuser provides fluidthrough line 30 to drive jet pump 25 and the outer diffuser provides fluid at 710 psi through line 31 to provide main system flow across check valve 32.
  • From line 32, about 80 percent of the organic feed liquid toluene is conveyed through line 35 to cooling tubing 37 associated with the alternator (not shown) for cooling the stator thereof.
  • the feed liquid exits the stator cooling device 37 in a typical system at about 212 F., since it takes up heat generated by machine losses. 1
  • the regenerator 15 may be a plate fin heat exchanger arranged in a folded counterflow configuration. Since the vapor is relatively dense and the flow rate is low, the heat exchanger requires a small vapor frontal area and long length in order to increase the heat transfer coefficient and at the same time maintain sufficient heat transfersurface.
  • the fins may be made of wavy nickel metal, while separator sheets, top and bottom plates, side channels and headers are all made of stainless steel, resulting in a unit having a small volume and low weight.
  • Flow leaving the regenerator 15 on the liquid side through line 38 is at approximately 488 F., in an exemplary installation.
  • the flow leaving the liquid side of the regenerator mixes at 40 with the preheated flow from economizer 42.
  • the economizer 42 is fed feed liquid through line 44, amounting to about percent of the total system feed liquid.
  • the heater-economizer is shown more clearly in FIG. 2 and is a supercritical once-through unit of compact design. High mass velocity through the heater insures high heat transfer thereby minimizing the hot spots.
  • the vaporizer-economizer 12 includes combustion gas inlets 49 and 50 which receive combustion gases, a central combustion gas chamber 52 at about 3,000 F., for example, an annular heater section 55 and an annular economizer section 42. In the heater section 55, a brazed sphere matrix 56 is provided on the flue gas side to provide a large gas side heat transfer area. Heater tubes 60 are provided packed with a sphere matrix 62 to increase mass velocity and heat transfer coefficient.
  • the economizer section 42 includes liquid feed tubes 63 surrounded by a brazed sphere matrix 55 through which the flue gases pass.
  • the feed liquid flowing through tubes 63 reduces the flue gas temperature from about 800 F. exiting from heater section 55 to approximately 400 F., thereby increasing cycle efficiency significantly.
  • the pressure of the liquid exiting economizer 42 is equal to the pressure at the regenerator outlet line 38 to maintain the proper flow split (i.e., about 80 percent-20 percent). This is accomplished by matching the hydraulic impedance of economizer 42 with that of regenerator 15.
  • the temperature of the liquid exiting the economizer in line 68 is approximately 490 F. This flow combines at 40 with the flow from regenerator line 38 and passes through line 70 to the heater tubes 60. Vapor leaving the super-critical heater section 55 exits the heater through line 72 somewhat above 700 F. and over 600 psia.
  • the high pressure, high temperature vapor in line 72 is controlled by a valve 75 decreasing the turbine inlet pressure somewhat, e.g., to 575 psia.
  • the valve 75 is a speed responsive control for maintaining the speed of turbine 14 constant.
  • a shut-down valve 78 is provided which responds upon a predetermined temperature in heatereconomizer 12 to open, permitting flow initiation to the turbine 14.
  • the turbine 14 is a single stage, supersonic, axial im pulse, partial admission turbine.
  • the organic working fluid toluene superheats upon expansion enabling high pressure ratios to be taken across the single stage of turbine 14 resulting in high cycle efficiencies.
  • the deleterious effect of moisture formation in the turbine nozzles and passages which would otherwise cause blade erosion and lack of flow control is not present.
  • the turbine 14 may, for example, run at 120,000 RPM.
  • the condenser 16 is a fin heat exchanger with the vapor condensing inside tubes and the cooling air flowing across the tubes and between the finned surfaces.
  • a fan (not shown) is provided for directing ambient air across the tubes in condenser 16.
  • the degradation of toluene results in the generation of noncondensable gases and high boiling compounds.
  • the noncondensable gas separator 20 is provided to prevent a decrease in the condenser heat transfer coefficients and to prevent an increase in the turbine back pressure which would otherwise reduce turbine power and cycle efficiency.
  • the condensed vapor flows through line 85 into the hotwell 18.
  • the start-up tank 27 includes a spring loaded valve (not shown) with a locking device for initiating flow from the start tank.
  • the burner air and fuel equipment (not shown) would be activated as would an igniter (not shown) delivering hot air to the heater-economizer 12.
  • an igniter (not shown) delivering hot air to the heater-economizer 12.
  • means are provided for releasing the locking device associated with start tank 27 and allowing the spring to force high pressure liquid to fill the high pressure lines 31, 35 and 44. This also initiates flow to the bearings as indicated in FIG. 1. While the heater metal and working fluid are coming up to temperature, the loop 30 from pump 25 to pump 22 is being filled by bleeding a small amount of high pressure fluid.
  • the shut-down valve 78 When the heater temperature reaches a certain level, the shut-down valve 78 is opened admitting flow to the turbine. The turbine then accelerates to 120,000 RPM in about to seconds. When the turbine is nearly up to speed, the system pump will put out more pressure than the start tank 27 and the check valve 32 will open supplying system flow. When the turbine is up to speed, the condenser fan (not shown) is activated and batteries associated with the burner are recharged. When the condensate in hotwell 18 reaches a temperature near its normal operating point, the unit is ready to supply fullload. This occurs rapidly since the system is relatively light and has a liquid inventory (toluene) of about 3 pounds. Start-up time can be further reduced if the alternator associated with turbine 14 is loaded in a programmed fashion to supply electric energy to heaters'wrapped around the hotwell.
  • a battery driven motor (not shown) is activated to reset the spring on start tank 27 to its prestart position.
  • a crank may also be provided to compress the start tank spring.
  • a power conversion system employing the Rankine cycle comprising: a source of organic fluid feed liquid, a combustion gas heater for heating the feed liquid to a high pressure-high temperature state, a turbine connected to receive the hot fluid from the heater, a regenerator connected to receive exhaust vapor from the turbine, said regenerator being constructed to pass at least a portion of said feed liquid in out-of-contact heat exchange relation with vapor from said turbine, and an economizer forming. a part of the combustion gas heater for passing at least another. portion of the feed liquid in out-of-contact heat exchange relation to the combustion gases from the heater to reduce the gas exit temperature.
  • Apower conversion system employing the Rankine cycle, comprising; a source of organic feed liquid including a first feed liquid, a combustion gas heater for the feed liquid to raise the temperature and pressure thereof, a turbine constructed to receive vapor from the heater to drive the turbine in expansion, means for receiving and condensing the vapor from the turbine, and an economizer associated with and forming a part .of the combustion gas heater for receiving at least another portion of the feed liquid in out-of-contact heat exchange relation with the hot combustion gases exiting the heater, and means for adding feed liquid from the economizer with said first feed liquid and directing the combined feed liquid to the combustion gas heater.
  • a power conversion system as defined in claim 4 including a regenerator for preheating at least a portion of the feed liquid, said regenerator receiving superheated vapor from the turbine and passing the same in out-of-contact heat exchange relation with the feed liquid in the regenerator.
  • An organic Rankine cycle power conversion system comprising, a hotwell for organic feed liquid, a pump for pumping'fluid from the hotwell, a regenerator for preheating feed liquid, conduit means for directing a major portion of the feed liquid to the regenerator, a combustion gas heater, means for conveying-feed liquid from the regenerator to the heater, an economizer forming part of the combustion gas heater including means for passing at least a portion of the feed liquid in out-of-contact heat exchange relation with exiting combustion gases to reduce the temperature of the gases, means to convey preheated liquid from the economizer to the heater, a turbine, means for conveying vapor from the heater to the turbine, means for conveying vapor from the turbine to the regenerator, a condenser, means for conveying vapor from the regenerator to the condenser, and means for conveying condensate from the condenser to the hotwell.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
US00159804A 1971-07-06 1971-07-06 Rankine cycle engine Expired - Lifetime US3769789A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US15980471A 1971-07-06 1971-07-06

Publications (1)

Publication Number Publication Date
US3769789A true US3769789A (en) 1973-11-06

Family

ID=22574102

Family Applications (1)

Application Number Title Priority Date Filing Date
US00159804A Expired - Lifetime US3769789A (en) 1971-07-06 1971-07-06 Rankine cycle engine

Country Status (4)

Country Link
US (1) US3769789A (enExample)
DE (1) DE2233327A1 (enExample)
FR (1) FR2145251A5 (enExample)
GB (1) GB1381126A (enExample)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4241869A (en) * 1979-01-11 1980-12-30 Standard Oil Company (Indiana) Furnace fuel optimizer
AP289A (en) * 1990-12-31 1993-11-08 Ormat Turbines 1965 Ltd Rankine cycle power plant utilizing an organic fluid and method for using the same.
WO1995002115A1 (en) * 1993-07-05 1995-01-19 Loeytty Ari Veli Olavi Method for exploitation of waste thermal energy in power plants
US5560210A (en) * 1990-12-31 1996-10-01 Ormat Turbines (1965) Ltd. Rankine cycle power plant utilizing an organ fluid and method for using the same
US6199382B1 (en) * 1998-11-25 2001-03-13 Penn State Research Foundation Dynamic condensate system
WO2007077293A1 (en) * 2005-12-30 2007-07-12 Wärtsilä Biopower Oy Method of heating and/or evaporating an organic medium and a heat exchanger unit for recovering heat from a hot gas flow
US20090235664A1 (en) * 2008-03-24 2009-09-24 Total Separation Solutions, Llc Cavitation evaporator system for oil well fluids integrated with a Rankine cycle
US20090284011A1 (en) * 2008-05-16 2009-11-19 Mcbride Thomas S Continuos-Absorption Turbine
US20110094227A1 (en) * 2009-10-27 2011-04-28 General Electric Company Waste Heat Recovery System
US20120085097A1 (en) * 2010-10-06 2012-04-12 Chevron U.S.A. Inc. Utilization of process heat by-product
US20120151924A1 (en) * 2009-08-24 2012-06-21 Ogilvy Renault Llp/S.E.N.C.R.L., S.R.L. Method and system for generating high pressure steam
CN103038457A (zh) * 2009-11-24 2013-04-10 通用电气公司 直接蒸发器设备和能量回收系统
US8613189B1 (en) * 2009-11-30 2013-12-24 Florida Turbine Technologies, Inc. Centrifugal impeller for a rocket engine having high and low pressure outlets
US20150345482A1 (en) * 2014-05-30 2015-12-03 Balcke-Dürr GmbH Geothermal power plant facility, method for operating a geothermal power plant facility, and method for increasing the efficiency of a geothermal power plant facility
US10941706B2 (en) 2018-02-13 2021-03-09 General Electric Company Closed cycle heat engine for a gas turbine engine
US11015534B2 (en) 2018-11-28 2021-05-25 General Electric Company Thermal management system

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1535154A (en) * 1977-05-26 1978-12-06 Stewart R Power generating device
DE19914287A1 (de) * 1999-03-30 2000-10-12 Friedrich Roth Dampferzeuger

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2160644A (en) * 1936-09-08 1939-05-30 Clarkson Alick Steam generating system
US2790429A (en) * 1951-11-06 1957-04-30 Bailey Meter Co Control systems
US3016712A (en) * 1960-07-14 1962-01-16 Foster Wheeler Corp Method and apparatus for preheating boiler feed water for steam power plants
US3040528A (en) * 1959-03-22 1962-06-26 Tabor Harry Zvi Vapor turbines
CA644925A (en) * 1962-07-17 C.A. Parsons And Company Limited Thermal power plants

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA644925A (en) * 1962-07-17 C.A. Parsons And Company Limited Thermal power plants
US2160644A (en) * 1936-09-08 1939-05-30 Clarkson Alick Steam generating system
US2790429A (en) * 1951-11-06 1957-04-30 Bailey Meter Co Control systems
US3040528A (en) * 1959-03-22 1962-06-26 Tabor Harry Zvi Vapor turbines
US3016712A (en) * 1960-07-14 1962-01-16 Foster Wheeler Corp Method and apparatus for preheating boiler feed water for steam power plants

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4241869A (en) * 1979-01-11 1980-12-30 Standard Oil Company (Indiana) Furnace fuel optimizer
AP289A (en) * 1990-12-31 1993-11-08 Ormat Turbines 1965 Ltd Rankine cycle power plant utilizing an organic fluid and method for using the same.
US5560210A (en) * 1990-12-31 1996-10-01 Ormat Turbines (1965) Ltd. Rankine cycle power plant utilizing an organ fluid and method for using the same
WO1995002115A1 (en) * 1993-07-05 1995-01-19 Loeytty Ari Veli Olavi Method for exploitation of waste thermal energy in power plants
US6199382B1 (en) * 1998-11-25 2001-03-13 Penn State Research Foundation Dynamic condensate system
RU2403522C2 (ru) * 2005-12-30 2010-11-10 Мв Биопауэр Ой Способ нагрева и/или испарения органической среды и теплообменный блок для извлечения теплоты от потока горячего газа
WO2007077293A1 (en) * 2005-12-30 2007-07-12 Wärtsilä Biopower Oy Method of heating and/or evaporating an organic medium and a heat exchanger unit for recovering heat from a hot gas flow
US20090235664A1 (en) * 2008-03-24 2009-09-24 Total Separation Solutions, Llc Cavitation evaporator system for oil well fluids integrated with a Rankine cycle
US20090284011A1 (en) * 2008-05-16 2009-11-19 Mcbride Thomas S Continuos-Absorption Turbine
US20120151924A1 (en) * 2009-08-24 2012-06-21 Ogilvy Renault Llp/S.E.N.C.R.L., S.R.L. Method and system for generating high pressure steam
US20110094227A1 (en) * 2009-10-27 2011-04-28 General Electric Company Waste Heat Recovery System
CN103038457A (zh) * 2009-11-24 2013-04-10 通用电气公司 直接蒸发器设备和能量回收系统
CN103038457B (zh) * 2009-11-24 2016-01-20 通用电气公司 直接蒸发器设备和能量回收系统
US8613189B1 (en) * 2009-11-30 2013-12-24 Florida Turbine Technologies, Inc. Centrifugal impeller for a rocket engine having high and low pressure outlets
US20120085097A1 (en) * 2010-10-06 2012-04-12 Chevron U.S.A. Inc. Utilization of process heat by-product
US20150345482A1 (en) * 2014-05-30 2015-12-03 Balcke-Dürr GmbH Geothermal power plant facility, method for operating a geothermal power plant facility, and method for increasing the efficiency of a geothermal power plant facility
US10941706B2 (en) 2018-02-13 2021-03-09 General Electric Company Closed cycle heat engine for a gas turbine engine
US11015534B2 (en) 2018-11-28 2021-05-25 General Electric Company Thermal management system
US11506131B2 (en) 2018-11-28 2022-11-22 General Electric Company Thermal management system

Also Published As

Publication number Publication date
GB1381126A (en) 1975-01-22
FR2145251A5 (enExample) 1973-02-16
DE2233327A1 (de) 1973-01-18

Similar Documents

Publication Publication Date Title
US3769789A (en) Rankine cycle engine
US6076355A (en) Vapor force engine
US7665304B2 (en) Rankine cycle device having multiple turbo-generators
US3830062A (en) Rankine cycle bottoming plant
JP2675732B2 (ja) 燃焼装置
CA2589781C (en) Method and apparatus for power generation using waste heat
US20110247335A1 (en) Waste heat steam generator and method for improved operation of a waste heat steam generator
EP0379880A1 (en) A system and method for cooling in a gas turbine
US2568787A (en) Steam power plant using exhaust from auxiliary gas turbine for condensing steam
WO2006060252A1 (en) Method and apparatus for decreasing marine vessel power plant exhaust temperature
JPS6213485B2 (enExample)
JP2004526900A (ja) ガスタービン用冷却材の冷却装置とガス・蒸気複合タービン設備
US3756023A (en) Heat recovery steam generator employing means for preventing economizer steaming
US11719156B2 (en) Combined power generation system with feedwater fuel preheating arrangement
US4166361A (en) Components and arrangement thereof for Brayton-Rankine turbine
US3611718A (en) Waste heat steam generating cycle
US4023367A (en) Steam engine for a motor vehicle
RU2514570C1 (ru) Устройство для регенеративного охлаждения сверхзвуковой части сопла жидкостного ракетного двигателя
RU2029119C1 (ru) Газотурбинная установка
US1994009A (en) Heat exchanger
JPH0242102A (ja) 熱エネルギ回収方法、及び熱エネルギ回収装置
US3466871A (en) Turbine power plant
KR102481490B1 (ko) 복합 발전 시스템 및 복합 발전 시스템의 구동 방법
KR20220136294A (ko) 복합 발전 시스템 및 복합 발전 시스템의 구동 방법
US2202298A (en) Power generating, transmitting, and delivering apparatus