Method heat recovery exhaust gas in the converter of organic energy through an intermediate liquid cycle (variants) and a heat recovery system exhaust

 

Method heat recovery of exhaust gases of a gas turbine is carried out as follows. Heated intermediate fluid environment using exhaust gas into vapor organic liquid working fluid environment mentioned heated intermediate fluid medium in the evaporator for receiving the vaporous working fluid and the cooled intermediate fluid. Then expand referred vaporous working medium in the turbine running on vaporous organic working fluid, to generate energy and more vaporous working fluid. Condense mentioned the expanded vaporous working fluid medium to obtain a liquid organic working fluid coming out of the condensate. Transfer liquid organic working medium back to the said evaporator and before turning in pairs mentioned liquid organic working fluid environment pre-heat the cooled intermediate fluid medium. The invention can improve the regeneration cycle heat and use a heat recovery system in a climate with extreme temperatures. 3 C. and 16 h.p. f-crystals, 1 Il.

The present and the but it refers to the heat recovery system of a gas turbine and to a method of heat recovery of exhaust gases of the gas turbine.

Worldwide gas turbine in which fuel is burnt, used for energy generation. This energy can be used, for example, for fuel pump for gas compressors, for other equipment and to generate electricity. Often, these turbines are located in remote areas of the globe in extreme weather conditions, including freezing temperature. During operation of the gas turbine exhaust gases, which are usually extremely hot, and often these gases are simply released into the atmosphere instead of using them to generate additional energy.

For example, pipelines for the transmission of gas under high pressure is traditionally used to transport gas to consumers that are removed from the fields. Gas compressors supplying such pipelines, usually supplied with power using gas turbines, and additionally can be used cycle heat recovery to reduce the requirements for useful power by converting the heat of the exhaust gases of the NII as a reference. In General, this patent presents power plant with a gas turbine. In one of the embodiments of this invention presents turbine power plant with a lower supply of steam, while in another variant implementation, the power system with lower inlet steam and organic Rankine cycle uses the heat of exhaust gases of the gas turbine. Typically, the temperature of the exhaust gases is approximately 450oC. In accordance with known patent the temperature of the gases, the heat from which is transmitted to the power plant with the lower supply of steam is controlled by the use of ambient air added to the exhaust gases of the gas turbine system. When the weather is cold ambient temperatures can fall below freezing, causing freezing of the condensate of steam, thus adversely affecting the operation of the heat recovery system.

On the other hand, organic fluids, performing the function of the working fluid in such systems, having a relatively high temperature, can be unstable.

Therefore, the technical task of the present invention was the creation of an improved cycle regenerate temperatures and also has an improved cycle heat recovery.

The technical result of the present invention was the creation of a heat recovery system produced by such a heat source, such as a gas turbine. In the heat recovery system as the working fluid used organic fluid medium, so that an additional technical result was that the heat recovery system can be used in climates with extreme temperatures when temperatures drop below the freezing point of water. In addition, the technical result of the present invention was to increase the safety margin by using an intermediate fluid to transfer heat from the hot exhaust gases to the organic working fluid.

These technical results are achieved due to the fact that in the method of heat recovery of exhaust gases of a gas turbine according to the invention is heated intermediate fluid environment using exhaust gases; convert in pairs organic liquid working fluid environment mentioned heated intermediate fluid medium in the evaporator for receiving the vaporous working fluid and the cooled intermediate fluid; expanding mentioned vaporous working fluid medium in the turbine was shirenai vaporous working fluid; condense mentioned the expanded vaporous working fluid medium to obtain a liquid organic working fluid exiting the condenser; transferring liquid organic working fluid environment referred back to the evaporator, and before turning in pairs mentioned liquid organic working fluid environment pre-heat the cooled intermediate fluid medium.

Preferably optionally regulate the amount mentioned preheated liquid organic working fluid so that it was certain percentage of the total number mentioned intermediate fluid.

Preferably perform additional pre-heating of the liquid organic working fluid by heating the aforementioned liquid organic working fluid by using the expanded vaporous working fluid before mentioned liquid organic working fluid is pre-heated using the cooled intermediate fluid.

Also preferably, as mentioned organic fluid using pentane, and as mentioned promejutke by that way heat recovery of exhaust gases of a gas turbine according to the invention serves the heated intermediate fluid medium heated by the exhaust heat; served pairs working organic fluid medium, which was obtained from the liquid using the hot intermediate fluid in the evaporator, in which receive the cooled intermediate fluid environment; receive electrical energy from the mentioned pair working organic fluid medium by means of an electrical generator driven by the turbine, fossil steam, which, in turn, is mentioned steam working organic fluid, which forms the expanded steam is the working fluid; get liquid organic working fluid medium in the condenser of the above-mentioned pair of working organic fluid after its use in the turbine running on a couple of organic working fluid; serves mentioned liquid organic working fluid medium in said evaporator and produce pre-heated liquid organic working fluid environment before mentioned liquid organic working fluid environment serves in the above-mentioned evaporator with onicescu the fluid.

Preferably additionally produce a preheated liquid organic working fluid environment mentioned advanced vapor of the working fluid before mentioned liquid organic working fluid medium is preheated using the cooled intermediate fluid.

Preferably mentioned liquid organic working fluid environment preheat mentioned the expanded vaporous working fluid medium.

Preferably as an intermediate fluid using water under pressure, and as a working fluid using pentane.

Technical results are also achieved due to the fact that the heat recovery system exhaust gas system of power generation according to the invention contains a source of energy production, which is served warm;
the exchanger with heat recovery, which takes the heat and in which the intermediate fluid is heated by heat;
system intermediate fluid containing intermediate the fluid and including a pump for intermediate fluid having input and output and line, connect the second fluid environment;
the evaporator, which receive vaporous organic working fluid medium from a liquid organic working fluid using heat contained in said intermediate fluid, and said line connecting the said heat exchanger heat recovery from the said evaporator and cooled intermediate fluid medium, which is produced from the specified evaporator;
turbine running on vaporous organic working fluid, which is driven vaporous organic working fluid medium and from which comes the expanded vaporous working fluid;
a condenser in which the specified extended vaporous organic working fluid condenses to form a liquid organic working fluid;
main pump for condensate, which is fed into the liquid organic working fluid from the above-mentioned capacitor, and which, in turn, delivers the liquid organic working fluid medium specified in the evaporator,
and the device is pre-heating, in which the aforementioned organic working fluid is heated cooled intermediate fluid medium before entering in upomanutoi intermediate fluid medium is water.

Also preferably mentioned intermediate fluid medium is water under pressure such that the water will not freeze at temperatures in areas of the planet with a cold climate.

Preferably, the system intermediate the fluid further includes a blower connected to the first line, located between the release of the above-mentioned pump intermediate fluid and said heat exchanger.

Preferably, the system intermediate the fluid further includes a storage tank having an inlet and outlet, and a charging pump for liquid connected to the line between the storage tank and the lines connecting the heat exchanger with heat recovery from the said evaporator.

Preferably the system further includes a storage tank having an inlet and outlet, and a pump connected to the line between the storage tank and the first line, located between the release of the above-mentioned pump for intermediate fluid and said heat exchanger;
moreover, the said supercharger includes a ventilation connection, which is associated with the specified storage tank.

Preferably the device is a bunch of environment, receiving heat, and referred to the pre-heater connected with said evaporator so as to receive from him referred to the cooled intermediate the fluid from the primary circuit and connected with said pump for condensate to take away the condensate from the secondary circuit and to provide an additional supply of the cooled intermediate fluid medium for the above-mentioned heat exchanger with heat recovery.

Preferably the heat exchanger with heat recovery includes the lower the first set of coils having entrance and exit, the upper second set of coils having an input and output, and line cross-connection connecting the output of the first set of coils to the input of the second set of coils, and in which the output of the above-mentioned pump for intermediate fluid connected with the said cross-line connection, and in which the pump for the intermediate fluid issuing through the valve to the specified line cross-connection.

Embodiments of the present invention will be described by example with reference to the attached drawing, which shows a block diagram of the system Regener the Klah intermediate fluid.

As seen in the drawing, the position of the 10 designated system of a gas turbine in accordance with the present invention. Site gas turbine leads Energostroy or mechanical Energostroy, such as an electric generator 14 to produce electrical energy or gas compressor. The exhaust gases leaving the gas turbine 13, served on a system 20 of the regeneration exhaust gas.

The system 20 of the regeneration exhaust gas includes heating coils 36 and 40, located in the housing 24 of the heat exchanger 22 for transferring the heat contained in the exhaust gases, the system 60 of the intermediate fluid. When heat is transferred to the system 60 of the intermediate fluid, the exhaust gases of the gas turbine on line 18 is fed to the input 26 of the system 20 of the heat recovery of exhaust gases and further to the coils 36 and 40 of the opening valve 32 and closing the valve 30. After that, the exhaust gases with low enthalpy out of the heat exchanger 22 through the outlet 52 and into the atmosphere through the pipe 56. If required, the path of the exhaust gases can be changed in accordance with a particular site. If for any reason the heat exchanger 22 should be bypassed, the exhaust gases are carried into the atmosphere by closing klepatelnii water, arriving in system 60 of the intermediate fluid, which is a closed system of water supply under pressure, receives heat from the exhaust gases flowing in the heat exchanger 22. Fluid transferring heat flowing in the system 60 intermediate the fluid leaves the heat exchanger 22 at point 48 and transmits heat to the organic fluid present in the system 90 with an organic working fluid, operating on the Rankine cycle, by using the evaporator 62. Part of the cooled heat transfer fluid leaving the evaporator 62, is supplied by means of pump 64 and the heat exchanger 22 at point 44, while the other portion of the cooled heat transfer fluid is supplied to the heater 68 for pre-heating the organic working fluid in the system 90 with organic working fluid medium, operating on the Rankine cycle. In the preferred construction, the pump 64 actually consists of two centrifugal pumps connected in parallel, each pump is able to perform 100% of the requirements for the pump, which at full load and stable mode is about 130 kilograms per second (kg/sec). The ratio of the volume flow Pere, supplied to the device 68 pre-heating is determined by the valve 66. Typically, this ratio is 70%, which enter the heat exchanger 22 at point 44, and 30% of that received by the device 68 pre-heating, and preferably from 72,5% to 27.5%. Next, the cooled fluid that transfers the heat that comes out of the device 68 pre-heating is supplied to the heat exchanger 22 to the input 42 of the coil 36 to transfer more heat from the exhaust gases. In a preferred embodiment, the heat exchanger 22 has the ability to send (i.e. recycling) approximately 33,000 kilowatt (kW) of energy.

When using water pressure of the water or fluid that transfers heat entering the system 60 of the intermediate fluid, is supported through the blower 76. The bottom of the liquid highways blower 76 is connected by line 70 in the system 60 of the intermediate fluid through the line 78 and the pump or pumps 80, together with the valve 82. The valve 82 takes the pressure of the fluid that transfers heat flowing in line 63, to maintain the required pressure. Usually this pressure is maintained approximately at the level of 3500 kPa in the range from 3000 to 4000 kPa to provide such services is atoy fluid medium, transfers heat from which optionally serves fresh portions of the fluid. Fresh portion of the fluid to transfer heat supplied to the system 60 of the intermediate fluid in accordance with the liquid level in the pressurizer 76, which is determined by the level sensor 84. The sensor 84 is also connected to the controller 86 for controlling the operation of the pump 74. If necessary, transferring heat to the fluid present in the system 60 of the intermediate fluid may be transferred to the storage tank 72. Such work may reduce the risk of freezing heat transfer fluid. System 90 with organic working fluid medium, operating on the Rankine cycle includes an evaporator 62 for receiving a pair of organic working fluid, which is supplied to the turbine 92, which operates on the vapor of the organic working fluid. Preferably the organic working fluid is a pentane. Turbine to work on vaporous organic working fluid preferably includes a module 94 of the turbine with high pressure, which takes pairs of organic working fluid from the evaporator 62, module 96 of the turbine to work on vaporous organic RA, coming out of the module 96 turbine with high pressure. As the module 94 of the turbine with high pressure and module 96 of the turbine low pressure produces energy and preferably rotate an electrical generator 98, which may be located between the modules of the turbine. Next, the expanded steam is organic working fluid exiting the module 96 low-pressure turbine is supplied to the capacitor 102 through the heat exchanger 100, where the liquid organic working fluid exiting the condenser 102, cools more advanced pairs organic working fluid. Each turbine 92 and 94 may be a turbine of 3.75 MW, rotating at 1800 rpm.

The heated liquid organic working fluid comprising a heat exchanger 100, preferably is supplied to the device 68 preheating for receiving heat transferred from the fluid heat transfer occurring in the system 60 of the intermediate fluid. Further, the heated liquid organic working fluid released from the device 68 pre-heating is supplied to the evaporator 62, thus completing the cycle of organic working fluid.

In the above-described system degeneracies, and the gas temperature is reduced from approximately 463oWith up to about 92oC. This recycled heat allows you to get a generator 98 network capacity, approximately 5.8 MW with a total capacity of approximately 6.5 MW, and this difference is the power required for operation of the system components.

In the above-described embodiment, the regeneration cycle of the heat is used to generate electricity. However, the useful power produced by the turbines 94 and 96, operating on gaseous organic working fluid, can alternatively be used for direct connection of equipment such as gas compressors, or for the production mechanisms without converting it to useful power into electricity.

Moreover, while in the above description of the defined gas turbine, can also be used with other heat sources, such as industrial heat, internal combustion engines such as diesel engines, gas reciprocating engines, etc., In addition to this, while in the above description illustrates a single cycle heat recovery with organic working fluid medium, the present invention also vkluchenie nodes, turbine or turbine with higher pressure, can use water as a working fluid medium in a closed loop.

Moreover, while in the above description illustrates the power plant using organic working fluid by a simple closed cycle or Rankine cycles with air cooled condenser, air can be added to the exhaust gases of the gas turbine to control the temperature of the gases from which heat is given during the regeneration cycle heat. When used for heat recovery power plant with a closed Rankine cycle, not steam turbine design, operation and maintenance of the entire system is simplified, allowing for reliable and independent work systems for a long time and at a long distance.

The advantages and improved results afforded by the method and device, which are the subject of the present invention, is obvious based on the above descriptions of preferred options for performing the present invention. Various changes and modifications can be made within the scope and essence of the present invention, as represented in the claims.

2. The method according to p. 1, which further regulate the amount mentioned preheated liquid organic working fluid so that it was certain percentage of the total number mentioned intermediate fluid.

3. The method according to p. 1, wherein implementing the additional pre-heating of the liquid organizatisonniy expanded vaporous working fluid before as mentioned liquid organic working fluid is pre-heated using the cooled intermediate fluid.

4. The method according to p. 1, which as mentioned organic fluid using pentane.

5. The method according to p. 1, which as mentioned organic fluid using water under pressure.

6. Method heat recovery exhaust gas turbine, which serves the heated intermediate fluid heated by the exhaust gases; served pairs working organic fluid medium, which was obtained from the liquid using the hot intermediate fluid in the evaporator, in which receive the cooled intermediate fluid environment; receive electrical energy from the mentioned pair working organic fluid medium by means of an electrical generator driven by the turbine, Rabochaya organic pair, which, in turn, is mentioned steam working organic fluid, which forms the expanded steam is the working fluid; get liquid organic working medium in the condenser of the above-mentioned pair of working organic fluid liquid organic working fluid in said evaporator, produce pre-heated liquid organic working fluid environment before mentioned liquid organic working fluid environment served in the said evaporator with said cooled intermediate fluid medium after the intermediate fluid has evaporated the organic fluid environment.

7. The method according to p. 6, which additionally produce a preheated liquid organic working fluid environment mentioned advanced vapor of the working fluid before mentioned liquid organic working fluid medium is preheated using the cooled intermediate fluid.

8. The method according to p. 6, in which the aforementioned liquid organic working fluid environment preheat mentioned the expanded vaporous working fluid medium.

9. The method according to p. 6, in which an intermediate fluid using water under pressure.

10. The method according to p. 6, in which the working fluid using pentane.

11. The heat recovery system exhaust gas system of power generation, containing the source of energy production, which is served warm; the heat exchanger with PE is using heat; system intermediate fluid containing intermediate the fluid and including a pump for intermediate fluid having input and output and the line connected to the input and production of the pump, and said line contain and serves the mentioned intermediate the fluid; an evaporator, in which receive the vaporous organic working fluid medium from a liquid organic working fluid using heat contained in said intermediate fluid, and said line connecting the said heat exchanger heat recovery from the said evaporator and cooled intermediate fluid medium, which is produced from the specified evaporator; a turbine, rabochuyu on vaporous organic working body, which is driven using vaporous organic working fluid and from which comes the expanded vaporous working fluid; a condenser in which the specified extended vaporous organic working fluid condenses to form a liquid organic working fluid; a main pump for condensate, which is fed into the liquid organic working fluid of the above-mentioned Conde device that preheats, in which the aforementioned organic working fluid is heated cooled intermediate fluid medium prior to entry into the said evaporator.

12. System on p. 11, in which the aforementioned organic working fluid environment is pentane.

13. System on p. 11, in which the mentioned intermediate fluid medium is water.

14. System on p. 11, in which the mentioned intermediate fluid medium is water under pressure such that the water will not freeze at temperatures in areas of the planet with a cold climate.

15. System on p. 11, in which said system intermediate the fluid further includes a blower connected to the first line, located to the honey production of the pump intermediate fluid and said heat exchanger.

16. System on p. 14, in which said system intermediate the fluid further includes a storage tank having an inlet and outlet, and a charging pump for liquid connected to the channels between the storage tank and the lines connecting the heat exchanger with heat recovery from the said evaporator.

17. The system under item 15, further comprising a reservoir for storing the than necessary, between the release of the above-mentioned pump for intermediate fluid and said heat exchanger, moreover, the said supercharger includes a ventilation connection, which is associated with the specified storage tank.

18. System on p. 11, which mentions the pre-heater has a primary circuit with a fluid medium, heat transfer and secondary circuit with a fluid medium receiving heat, and referred to the pre-heater connected with said evaporator so as to receive from him referred to the cooled intermediate the fluid from the primary circuit and connected with said pump for condensate to take away the condensate from the secondary circuit and to provide an additional supply of the cooled intermediate fluid medium for the above-mentioned heat exchanger with heat recovery.

19. System on p. 11, in which the said heat exchanger with heat recovery includes the lower the first set of coils having entrance and exit, the upper second set of coils having an input and output, and line cross-connection connecting the output of the first set of coils to the input of the second set of coils, the output of the above-mentioned pump for intermediate fluid connected with the said cross-line suetnogo connection.

 

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FIELD: electric power and chemical industries; methods of production of the electric power and liquid synthetic fuel.

SUBSTANCE: the invention presents a combined method of production of the electric power and liquid synthetic fuel with use of the gas turbine and steam-gaseous installations and is dealt with the field of electric power and chemical industries. The method provides for the partial oxidation of hydrocarbon fuel in a stream of the compressed air taken from the high-pressure compressor of the gas turbine installation with its consequent additional compression, production of a synthesis gas, its cooling and ecological purification, feeding of the produced synthesis gas in a single-pass reactor of a synthesis of a liquid synthetic fuel with the partial transformation of the synthesis gas into a liquid fuel. The power gas left in the reactor of synthesis of liquid synthetic fuel is removed into the combustion chamber of the gas-turbine installation. At that the degree of conversion of the synthesis gas is chosen from the condition of maintenance of the working medium temperature at the inlet of the gas turbine depending on the type of the gas-turbine installation used for production of the electric power, and the consequent additional compression of the air taken from the high-pressure compressor of the gas-turbine installation is realized with the help of the gas-expansion machine powered by a power gas heated at the expense of the synthesis gas cooling before the reactor of synthesis. The invention allows simultaneously produce electric power and synthetic liquid fuels.

EFFECT: the invention ensures simultaneous production of electric power and synthetic liquid fuels.

2 cl, 2 dwg

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