Gas turbine plant and method of fuel supply thereof

Abstract

A gas turbine device includes a gas turbine and a fuel supply device. The fuel supply device includes a liquid ammonia pipe, a hot water pipe through which hot water flows, a vaporizer that heats liquid ammonia from the liquid ammonia pipe by heat exchange with the hot water from the hot water pipe to vaporize the liquid ammonia, a heat exchanger that exchanges heat between the hot water in the hot water pipe and a medium, a heat exchange amount adjuster that adjusts the temperature of the hot water flowing into the vaporizer by adjusting the amount of heat exchange between the hot water and the medium, and a gaseous ammonia pipe that guides gaseous ammonia, which is ammonia vaporized by the vaporizer, to the gas turbine.

Description

Technical Field

[0001] This invention relates to a gas turbine device and a fuel supply method thereof.

[0002] This application claims priority based on Japanese Patent Application No. 2021-021755, filed on February 15, 2021, the contents of which are incorporated herein by reference. Background Technology

[0003] The gas turbine equipment includes a gas turbine and a fuel supply device for supplying fuel to the gas turbine.

[0004] In the gas turbine apparatus described in Patent Document 1 below, ammonia is supplied as fuel to the gas turbine. In addition to the fuel supply equipment that supplies ammonia as fuel to the gas turbine, the gas turbine apparatus also includes a waste heat recovery boiler that uses the heat from the exhaust gas from the gas turbine to generate steam.

[0005] The fuel supply equipment includes an ammonia tank for storing liquid ammonia, a liquid ammonia pipeline connected to the ammonia tank, a warm water pipeline for allowing warm water to flow, a vaporizer, a flow control valve for regulating the flow rate of warm water into the vaporizer, and a gaseous ammonia pipeline for guiding gaseous ammonia to the gas turbine. The vaporizer is connected to the end of the liquid ammonia pipeline. The vaporizer heats the liquid ammonia by exchanging heat between the warm water from the warm water pipeline and the liquid ammonia from the liquid ammonia pipeline, thereby vaporizing the liquid ammonia.

[0006] The vaporizer has heat transfer tubes for supplying ammonia flow and a vaporizer shell covering the heat transfer tubes and temporarily storing warm water. The warm water piping includes a warm water heater located within the waste heat recovery boiler, which heats the warm water by exchanging heat with the exhaust gas; a high-temperature water piping that guides the high-temperature water heated by the warm water heater to the vaporizer shell; and a low-temperature water piping connecting the vaporizer shell and the warm water heater. A flow control valve is located on the high-temperature water piping.

[0007] In this fuel supply device, the flow rate of warm water flowing into the vaporizer shell is regulated by a flow regulating valve to maintain the temperature of the warm water in the vaporizer shell within a target temperature range. Furthermore, the warm water in the vaporizer shell exchanges heat with liquid ammonia flowing within the heat transfer tubes.

[0008] Previous technical documents

[0009] Patent documents

[0010] Patent Document 1: Japanese Patent No. 6245404 Summary of the Invention

[0011] The technical problem to be solved by the invention

[0012] The temperature of the exhaust gas flowing within the waste heat recovery boiler varies depending on the operating conditions of the gas turbine. Therefore, in the technology described in Patent Document 1, even if the flow rate of warm water flowing into the gasifier housing is changed when the exhaust temperature varies, the amount of heat exchange between the liquid ammonia and the warm water is not proportional to the flow rate of the warm water, making it difficult to control this heat exchange. Therefore, it is considered that the technology described in Patent Document 1 has the problem of not being able to ensure the required amount of gaseous ammonia generated.

[0013] Therefore, the object of the present invention is to provide a technique that can easily obtain the amount of gaseous ammonia required for a gas turbine.

[0014] means for solving technical problems

[0015] As one method of achieving the aforementioned objective, a gas turbine device includes:

[0016] A gas turbine burns fuel and is driven by combustion gases generated from the combustion of said fuel; a waste heat recovery boiler utilizes heat from the exhaust gas from said gas turbine to generate steam; and a fuel supply device supplies ammonia, which is said fuel, to said gas turbine. The fuel supply device includes: a liquid ammonia pipeline connected to an ammonia tank capable of storing liquid ammonia; a warm water pipeline for flowing warm water; a vaporizer connected to one end of said liquid ammonia pipeline and capable of heating and vaporizing the liquid ammonia by heat exchange between the warm water from said warm water pipeline and said liquid ammonia; a heat exchanger for heat exchange between the warm water in said warm water pipeline and a medium; a heat exchange rate regulator for adjusting the amount of heat exchange between said warm water and said medium to adjust the temperature of the warm water flowing into said vaporizer; and a gaseous ammonia pipeline for guiding the ammonia vaporized by said vaporizer, i.e., gaseous ammonia, to said gas turbine. The vaporizer has an ammonia inlet, an ammonia outlet, a warm water inlet, and a warm water outlet. The liquid ammonia pipeline is connected to the ammonia inlet of the gasifier. The gaseous ammonia pipeline is connected to the ammonia outlet of the gasifier. The warm water pipeline includes a warm water heater disposed within the waste heat recovery boiler, which heats the warm water by exchanging heat with the exhaust gas, and a high-temperature water pipeline connecting the warm water heater to the warm water inlet of the gasifier. The heat exchanger is disposed within the high-temperature water pipeline.

[0017] In this method, heated water obtained through heat exchange between the water and exhaust gas in a water heater flows into a vaporizer after temperature regulation. In the vaporizer, the temperature-regulated water exchanges heat with liquid ammonia, causing the ammonia to vaporize. Since the exhaust gas temperature at the gas turbine outlet varies depending on the gas turbine's operating conditions, the inlet temperature of the water heater in the waste heat recovery boiler also varies depending on the gas turbine's operating conditions. Therefore, if the exhaust gas temperature changes, the temperature of the water heated by the water heater also changes. However, in this method, as mentioned above, the heated water flows into the vaporizer after temperature regulation. Therefore, in this method, even if the exhaust gas temperature changes, all liquid ammonia flowing into the vaporizer can be easily converted into gaseous ammonia.

[0018] Furthermore, the amount of gaseous ammonia required by the gas turbine also varies depending on the operating conditions of the gas turbine. In this method, even if the amount of gaseous ammonia required by the gas turbine changes, all liquid ammonia flowing into the gasifier can be easily converted into gaseous ammonia by changing the temperature of the warm water flowing into the gasifier.

[0019] Therefore, in this method, even if the operating conditions of the gas turbine change, the required amount of gaseous ammonia generated by the gas turbine can be easily obtained. Furthermore, this method improves the responsiveness of the amount of gaseous ammonia generated in response to changes in the operating conditions of the gas turbine.

[0020] As one method for achieving the aforementioned objective, a fuel supply method for a gas turbine includes a gas turbine that burns fuel and is driven by combustion gases generated from the combustion of the fuel, and a waste heat recovery boiler that utilizes heat from the exhaust gas from the gas turbine to generate steam. The fuel supply method for the gas turbine performs the following steps: a warm water heating step, in which warm water in a warm water heater disposed within the waste heat recovery boiler exchanges heat with the exhaust gas outside the warm water heater within the waste heat recovery boiler to heat the warm water. The process includes: a heat exchange process, in which the heated water obtained in the heated water process exchanges heat with a medium; a heat exchange rate adjustment process, in which the heat exchange rate between the heated water obtained in the heated water process and the medium is adjusted; a gasification process, in which the heated water, after the heat exchange rate with the medium has been adjusted by the heat exchange rate adjustment process, exchanges heat with the liquid ammonia from an ammonia tank containing liquid ammonia to gasify the liquid ammonia; and a fuel supply process, in which the ammonia gasified in the gasification process, i.e., gaseous ammonia, is supplied as fuel to the gas turbine.

[0021] In the heat exchange rate adjustment process, the temperature of the warm water flowing into the gasifier is adjusted by regulating the amount of heat exchange between the warm water and the medium in the heat exchange process.

[0022] In this method, similar to another method of the gas turbine equipment, the required amount of gaseous ammonia generated by the gas turbine can be easily obtained even if the operating conditions of the gas turbine change. Furthermore, this method also improves the responsiveness of the amount of gaseous ammonia generated in response to changes in the operating conditions of the gas turbine.

[0023] Invention Effects

[0024] In one aspect of the present invention, the amount of gaseous ammonia required for the gas turbine can be obtained. Attached Figure Description

[0025] Figure 1 This is a system diagram of the gas turbine device in the first embodiment of the present invention.

[0026] Figure 2 This is a functional block diagram of the control device in the first embodiment of the present invention.

[0027] Figure 3 This is a graph showing the relationship between fuel flow rate and target temperature in the first embodiment of the present invention.

[0028] Figure 4 This is a flowchart illustrating the steps of the fuel supply method in the first embodiment of the present invention.

[0029] Figure 5 This is a system diagram of the gas turbine device in the second embodiment of the present invention.

[0030] Figure 6 This is a flowchart illustrating the steps of the fuel supply method in the second embodiment of the present invention.

[0031] Figure 7 This is a functional block diagram of the control device in a modified embodiment of the present invention. Detailed Implementation

[0032] Hereinafter, various embodiments and modifications of the present invention will be described with reference to the accompanying drawings.

[0033] "First Embodiment"

[0034] The following uses Figures 1-4 A first embodiment of the gas turbine device according to the present invention will be described.

[0035] like Figure 1As shown, the gas turbine equipment of this embodiment includes a gas turbine 10, a denitrification device 20 for decomposing NOx components contained in the exhaust gas from the gas turbine 10, a waste heat recovery boiler 21 for generating steam using the heat of the exhaust gas flowing out of the denitrification device 20, a chimney 22 for discharging the exhaust gas from the waste heat recovery boiler 21 to the outside, a steam turbine 23 driven by steam from the waste heat recovery boiler 21, a condenser 24 for converting steam from the steam turbine 23 back into water, a pump 25 for conveying water from the condenser 24 to the waste heat recovery boiler 21, a fuel supply device 40 for supplying fuel to the gas turbine 10, and a control device 60. Therefore, the gas turbine equipment of this embodiment is a combined cycle equipment.

[0036] The gas turbine 10 includes a compressor 14 for compressing air A, a combustor 15 for generating combustion gas by burning fuel F in the air compressed by the compressor 14, and a turbine 16 driven by the high-temperature and high-pressure combustion gas.

[0037] The compressor 14 has a compressor rotor 14r that rotates around a rotor axis Ar, a compressor housing 14c covering the compressor rotor 14r, and an intake air volume regulator (hereinafter referred to as IGV (inlet guide vane)) 14i provided at the intake of the compressor housing 14c. The IGV 14i regulates the flow rate of air drawn into the compressor housing 14c according to instructions from the control device 60. The turbine 16 has a turbine rotor 16r that rotates around a rotor axis Ar via combustion gases from the burner 15, and a turbine housing 16c covering the turbine rotor 16r. The turbine rotor 16r and the compressor rotor 14r are rotatably connected to each other around the same rotor axis Ar to form a gas turbine rotor 11. For example, a generator rotor is connected to this gas turbine rotor 11.

[0038] The gas turbine 10 also includes an intermediate housing 12. The intermediate housing 12 is disposed between the compressor housing 14c and the turbine housing 16c in the direction of the rotor axis Ar, and connects the compressor housing 14c and the turbine housing 16c. Compressed air ejected from the compressor 14 flows into the intermediate housing 12. Furthermore, a burner 15 is fixed in the intermediate housing 12.

[0039] Ammonia is supplied to the denitrification unit 20. The denitrification unit 20 uses the ammonia to decompose the NOx contained in the exhaust gas from the gas turbine 10 into nitrogen and water vapor.

[0040] The waste heat recovery boiler 21 comprises a boiler shell 21c from exhaust gas flowing from a denitrification unit 20, an economizer 21eco, an evaporator 21eva, and a superheater 21s. The economizer 21eco, evaporator 21eva, and superheater 21s are arranged in the order of economizer 21eco, evaporator 21eva, and superheater 21s, from downstream to upstream of the exhaust gas flowing within the boiler shell 21c. The economizer 21eco, evaporator 21eva, and superheater 21s have heat transfer tubes that allow heat exchange between the exhaust gas flowing within the boiler shell 21c and water or steam. The economizer 21eco heats the water to generate warm water through heat exchange between the exhaust gas flowing within the boiler shell 21c and water. The evaporator 21eva heats the warm water to generate steam through heat exchange between the exhaust gas flowing within the boiler shell 21c and the warm water from the economizer 21eco. The superheater 21s heats the steam to generate superheated steam by exchanging heat between the exhaust gas flowing in the boiler shell 21c and the steam from the evaporator 21eva.

[0041] The economizer 21eco of the waste heat recovery boiler 21 is connected to the condenser 24 via a water supply line 26. A pump 25 is installed in this water supply line 26 to transport water from the condenser 24 to the waste heat recovery boiler 21. The superheater 21s of the waste heat recovery boiler 21 is connected to the steam turbine 23 via a main steam line 27. Superheated steam from the waste heat recovery boiler 21 is transported to the steam turbine 23 via the main steam line 27. A generator rotor, for example, is connected to the rotor of the steam turbine 23. The steam discharged from the steam turbine 23 is converted back into water by the condenser 24.

[0042] The denitrification unit 20 is, for example, located within the boiler shell 21c around the evaporator 21eva. Ammonia is supplied to the denitrification unit 20. The denitrification unit 20 uses the ammonia to decompose NOx contained in the exhaust gas from the gas turbine 10 into nitrogen and water vapor.

[0043] The fuel supply equipment 40 includes an ammonia tank 41, a liquid ammonia pipeline 42, a liquid ammonia regulating valve 43a, a fuel regulating valve 43b, an ammonia pump 44, a vaporizer 45, a gaseous ammonia pipeline 46, a warm water pipeline 50, a warm water pump 54, a heat exchanger 55, a heat exchange capacity regulator 56, a medium pipeline 58i, a medium recovery pipeline 58o, and a medium flow regulator 59.

[0044] Liquid ammonia is stored in ammonia tank 41. One end of a liquid ammonia pipeline 42 is connected to the ammonia tank 41. An ammonia pump 44 is installed in the liquid ammonia pipeline 42 to pressurize the liquid ammonia from the ammonia tank 41, and a liquid ammonia regulating valve 43a is installed in the liquid ammonia pipeline 42 to regulate the flow rate of the liquid ammonia flowing in the liquid ammonia pipeline 42.

[0045] The vaporizer 45 is a heat exchanger that heats and vaporizes liquid ammonia by exchanging heat between warm water and liquid ammonia. The vaporizer 45 has a heat transfer tube 45p for supplying warm water and a vaporizer shell 45c covering the heat transfer tube 45p and temporarily storing liquid ammonia. One end of the heat transfer tube 45p forms a warm water inlet 45pi, and the other end forms a warm water outlet 45po. The vaporizer shell 45c has an ammonia inlet 45ci and an ammonia outlet 45co. The other end of the aforementioned liquid ammonia pipeline 42 is connected to the ammonia inlet 45ci of the vaporizer 45. One end of a gaseous ammonia pipeline 46 is connected to the ammonia outlet 45co of the vaporizer 45. The other end of the gaseous ammonia pipeline 46 is connected to the burner 15. A fuel regulating valve 43b is provided in the gaseous ammonia pipeline 46 to regulate the flow rate of gaseous ammonia as fuel flowing into the burner 15.

[0046] The warm water pipeline 50 includes a low-temperature water pipeline 51, a warm water heater 52, and a high-temperature water pipeline 53. The warm water heater 52 is located within the boiler shell 21c, downstream of the exhaust flow from the economizer 21rco. The low-temperature water pipeline 51 connects the warm water outlet 45po of the vaporizer 45 to the warm water heater 52. A warm water pump 54 is installed in the low-temperature water pipeline 51. The high-temperature water pipeline 53 includes a main high-temperature water pipeline 53x connecting the warm water heater 52 to the warm water inlet 45pi of the vaporizer 45, and a branch high-temperature water pipeline 53y branching from and connecting to the main high-temperature water pipeline 53x.

[0047] The warm water pipe 50 and the heat transfer tube 45p of the vaporizer 45 form a warm water circulation pipe for supplying warm water. The flow rate of the warm water circulating in this warm water circulation pipe is managed by the warm water pump 54 and is approximately constant.

[0048] Heat exchanger 55 facilitates heat exchange between a medium such as cooling water and warm water. The heat exchanger 55 includes heat transfer tubes 55p for medium flow and a heat exchanger shell 55c covering the heat transfer tubes 55p and temporarily storing warm water. One end of the heat transfer tubes 55p forms a medium inlet 55pi, and the other end forms a medium outlet 55po. A medium pipeline 58i is connected to the medium inlet 55pi. A medium flow regulator 59 is installed in the medium pipeline 58i to regulate the flow rate of the medium flowing therein. A medium recovery pipeline 58o is connected to the medium outlet 55po. The heat exchanger shell 55c is connected to a branch high-temperature water pipeline 53y. Therefore, high-temperature water from the branch high-temperature water pipeline 53y flows into the heat exchanger shell 55c. Furthermore, the medium flowing into the heat exchanger 55 can be a liquid such as river water, seawater, or industrial water, or a gas such as air.

[0049] The heat exchange capacity regulator 56 includes a three-way valve 57 that functions as a flow ratio regulator. This flow ratio regulator adjusts the ratio of the flow rate of warm water flowing in the main high-temperature water line 53x between the branch position and the connection position of the branch high-temperature water line 53y, to the flow rate of warm water flowing in the branch high-temperature water line 53y. The three-way valve 57 is located at the connection position between the main high-temperature water line 53x and the branch high-temperature water line 53y. Alternatively, the flow ratio regulator may not be a three-way valve 57, but may consist of a main high-temperature water regulating valve located in the main high-temperature water line 53x between the branch position and the connection position of the branch high-temperature water line 53y, and a branch high-temperature water regulating valve located in the branch high-temperature water line 53y.

[0050] In the main high-temperature water pipeline 53x, a thermometer 48 is installed between the three-way valve 57 and the vaporizer 45 to detect the temperature of the high-temperature water flowing between them. In the gaseous ammonia pipeline 46, a pressure gauge 49 is installed to detect the pressure of the gaseous ammonia flowing in the pipeline.

[0051] like Figure 2 As shown, the control device 60 includes a fuel flow calculation unit 61, a fuel valve control unit 62, an IGV control unit 63, a temperature control system 65, and a pressure control system 70.

[0052] The fuel flow calculation unit 61 receives a request output PWr from an external source for the gas turbine 10. The fuel flow calculation unit 61 calculates the fuel flow rate corresponding to the requested output PWr and outputs a fuel flow command Fro representing that fuel flow rate. The fuel flow rate calculated by the fuel flow calculation unit 61 is positively correlated with the requested output PWr. That is, if the requested output PWr increases, the fuel flow rate calculated by the fuel flow calculation unit 61 also increases.

[0053] The fuel valve control unit 62 controls the opening of the fuel regulating valve 43b according to the fuel flow command Fro. The IGV control unit 63 controls the opening of the IGV 14i according to the fuel flow command Fro. Specifically, the IGV control unit 63 controls the IGV opening so that the fuel flow represented by the fuel flow command Fro is positively correlated with the IGV opening. In addition, the opening of the liquid ammonia regulating valve 43a changes according to the amount of liquid ammonia in the vaporizer housing 45c. Specifically, if the amount of liquid ammonia in the vaporizer housing 45c decreases, the liquid ammonia regulating valve 43a is opened to replenish the liquid ammonia.

[0054] The temperature control system 65 has a target temperature calculator 66, a temperature deviation calculator 67, and a PI controller 68.

[0055] like Figure 3As shown, the target temperature calculator 66 has a function F1 that represents the relationship between the fuel flow rate indicated by the fuel flow rate command Fro and the target temperature of the warm water. This function F1 indicates that if the fuel flow rate increases, the target temperature increases. The target temperature calculator 66 uses this function F1 to calculate the target temperature of the warm water relative to the fuel flow rate indicated by the fuel flow rate command Fro.

[0056] The temperature deviation calculator 67 calculates the deviation ΔT between the target temperature and the temperature detected by the thermometer 48. Specifically, the temperature deviation calculator 67 subtracts the temperature detected by the thermometer 48 from the target temperature and outputs this value as the temperature deviation ΔT. The PI controller 68 calculates the opening correction amount of the proportional / integral action corresponding to the temperature deviation ΔT and outputs the valve command corresponding to the opening correction amount to the three-way valve 57.

[0057] The pressure control system 70 includes a pressure correction mode button 71, a lower limit value memory 72a, an upper limit value memory 72b, a lower limit deviation calculator 73a, an upper limit deviation calculator 73b, a lower limit deviation judge 74a, an upper limit deviation judge 74b, a lower limit correction indicator 75a, an upper limit correction indicator 75b, a lower limit correction value calculator 77a, an upper limit correction value calculator 77b, a first switch 78a, a second switch 78b, a first adder 79a, a second adder 79b, and a PI controller 68. The pressure control system 70 and the temperature control system 65 share this PI controller 68. Furthermore, the functions of the above-mentioned components of the pressure control system 70 will be explained during the description of the operation of the pressure control system 70.

[0058] The control device 60 described above is a computer. In terms of hardware, the control device 60 includes a CPU (Central Processing Unit) for performing various calculations, a main storage device such as memory serving as the CPU's working area, an auxiliary storage device such as a hard disk drive, an input device such as a keyboard or mouse, and a display device. The functional units within the control device 60, such as the fuel flow calculation unit 61, fuel valve control unit 62, IGV control unit 63, temperature control system 65, and pressure control system 70, function, for example, by the CPU executing control programs stored in the auxiliary storage device.

[0059] Next, according to Figure 4 The flowchart shown illustrates the fuel supply method for the gas turbine equipment described above.

[0060] In the fuel supply method of this embodiment, the following steps are performed: warm water heating step S1, heat exchange quantity adjustment step S2, heat exchange step S3, temperature control step S4, gasification step S6, low temperature water recovery step S7, and fuel supply step S8. Furthermore, in this fuel supply method, a pressure control step S5 is also performed based on a request from the operator.

[0061] In the warm water heating process S1, warm water inside the warm water heater 52 located inside the boiler shell 21c is heated by heat exchange with exhaust gas outside the warm water heater 52 inside the boiler shell 21c. In this warm water heating process S1, for example, warm water (low temperature water) at about 60°C is heated to warm water (high temperature water) at about 90°C. This high temperature water flows from the warm water heater 52 into the main high temperature water pipe 53x.

[0062] In the heat exchange rate adjustment step S2, the temperature of the high-temperature water flowing into the vaporizer 45 is adjusted by regulating the amount of heat exchange between the high-temperature water from the hot water heater 52 and the medium flowing into the heat exchanger 55. This heat exchange rate adjustment step S2 includes a diversion step S2a and a flow ratio adjustment step S2b. In the diversion step S2a of the heat exchange rate adjustment step S2, a portion of the high-temperature water flowing from the main high-temperature water pipe 53x is diverted to the branch high-temperature water pipe 53y, while the remaining high-temperature water flows downstream of the branch in the main high-temperature water pipe 53x. That is, in this diversion step S2a, the high-temperature water flowing from the main high-temperature water pipe 53x is divided into branch high-temperature water flowing in the branch high-temperature water pipe 53y and main high-temperature water flowing in the main high-temperature water pipe 53x. The flow ratio adjustment step S2b of the heat exchange rate adjustment step S2 will be described later.

[0063] In the heat exchange process S3, the branch high-temperature water exchanges heat with the medium flowing into the heat exchanger 55 through the heat exchanger 55 installed in the branch high-temperature water pipeline 53y. Here, as mentioned above, when the medium flowing into the heat exchanger 55 is cooling water, the temperature of the branch high-temperature water decreases.

[0064] In the temperature control step S4, the request output PWr from the gas turbine 10 is received, and the heat exchange quantity in the heat exchange quantity adjustment step S2 is controlled according to the request output PWr. The temperature control system 65 of the control device 60 executes this temperature control step S4.

[0065] Here, for reference Figure 2 The operation of the control device 60 will be explained.

[0066] As mentioned above, the fuel flow calculation unit 61 of the control device 60 receives a request output PWr from an external source for the gas turbine 10. The fuel flow calculation unit 61 calculates the fuel flow rate corresponding to the request output PWr and outputs a fuel flow command Fro representing the fuel flow rate. Furthermore, the flow rate here is a mass flow rate.

[0067] The fuel valve control unit 62 controls the opening of the fuel regulating valve 43b so that the mass flow rate of fuel passing through the fuel regulating valve 43b becomes the fuel flow rate indicated by the fuel flow command Fro. As a result, the mass flow rate of ammonia as fuel flowing from the gaseous ammonia line 46 into the burner 15 becomes the fuel flow rate indicated by the fuel flow command Fro. The IGV control unit 63 controls the opening of the IGV so that the flow rate of air flowing into the compressor housing 14c becomes the flow rate corresponding to the fuel flow rate indicated by the fuel flow command Fro.

[0068] As mentioned above, the target temperature calculator 66 of the temperature control system 65 uses function F1 to calculate the target temperature of the warm water relative to the fuel flow rate represented by the fuel flow command Fro. The temperature deviation calculator 67 of the temperature control system 65 subtracts the temperature detected by the thermometer 48 from the target temperature and outputs the value as the temperature deviation ΔT.

[0069] The PI controller 68 of the temperature control system 65 calculates the opening correction amount of the proportional / integral action corresponding to the temperature deviation ΔT, and outputs the action amount corresponding to the opening correction amount as a valve command to the three-way valve 57.

[0070] The operation of the temperature control system 65 described above controls the operation of the three-way valve 57, thereby regulating the heat exchange quantity in the heat exchange quantity regulation process S2.

[0071] As mentioned above, when operators or others wish to adjust the pressure, pressure control step S5 is executed. The pressure control system 70 of the control device 60 executes this pressure control step S5.

[0072] The pressure calibration mode button 71 of the pressure control system 70 receives information from the operator or other personnel regarding whether they wish to calibrate the pressure. If the operator or other personnel press the pressure calibration mode button 71 to calibrate the pressure, the pressure calibration mode button 71 outputs an ON signal, and the control device 60 enters the pressure calibration mode.

[0073] The lower limit memory 72a stores the lower limit value Pa of the pressure of the fuel (gaseous ammonia) flowing into the burner 15. The upper limit memory 72b stores the upper limit value Pb of the pressure of the fuel (gaseous ammonia) flowing into the burner 15.

[0074] The lower limit deviation calculator 73a of the pressure control system 70 calculates the deviation ΔPat between the lower pressure limit value Pa and the pressure detected by the pressure gauge 49. Specifically, the lower limit deviation calculator 73a subtracts the pressure detected by the pressure gauge 49 from the lower pressure limit value Pa and outputs this value as the lower limit deviation ΔPat. The upper limit deviation calculator 73b of the pressure control system 70 calculates the deviation ΔPbt between the upper pressure limit value Pb and the pressure detected by the pressure gauge 49. Specifically, the upper limit deviation calculator 73b subtracts the pressure detected by the pressure gauge 49 from the upper pressure limit value Pb and outputs this value as the upper limit deviation ΔPbt.

[0075] The lower limit deviation detector 74a of the pressure control system 70 determines whether the lower limit deviation ΔPat is positive; in other words, it determines whether the pressure detected by the pressure gauge 49 is less than the lower pressure limit value Pa, and outputs the result. The upper limit deviation detector 74b of the pressure control system 70 determines whether the upper limit deviation ΔPbt is negative; in other words, it determines whether the pressure detected by the pressure gauge 49 is greater than the upper pressure limit value Pb, and outputs the result.

[0076] The lower limit correction indicator 75a of the pressure control system 70 outputs an ONa signal indicating that temperature correction based on the lower pressure limit value Pa is performed when the lower limit deviation ΔPat is positive and an ON signal is received from the pressure correction mode button 71. Conversely, when the lower limit deviation ΔPat is not positive or an ON signal is not received from the pressure correction mode button 71, the lower limit correction indicator 75a outputs an OFFa signal indicating that temperature correction based on the lower pressure limit value Pa is not performed. The upper limit correction indicator 75b of the pressure control system 70 outputs an ONb signal indicating that temperature correction based on the upper pressure limit value Pb is performed when the upper limit deviation ΔPbt is negative and an ON signal is received from the pressure correction mode button 71. Conversely, when the upper limit deviation ΔPbt is not negative or an ON signal is not received from the pressure correction mode button 71, the upper limit correction indicator 75b outputs an OFFb signal indicating that temperature correction based on the upper pressure limit value Pb is not performed.

[0077] The fuel flow command Fro and the lower limit deviation ΔPat are input to the lower limit correction value calculator 77a of the pressure control system 70. The lower limit correction value calculator 77a uses the function Fa shown below to calculate the lower limit correction value Ca corresponding to the fuel flow Fr represented by the fuel flow command Fro and the lower limit deviation ΔPat (>0). This lower limit correction value Ca is a temperature correction value based on the lower pressure limit value Pa. Furthermore, this lower limit correction value Ca is a positive value.

[0078] Fa:Ca=k×ΔPat / Fr

[0079] Additionally, in the above formula, k is the correction coefficient.

[0080] The fuel flow command Fro and the upper limit deviation ΔPbt are input to the upper limit correction value calculator 77b of the pressure control system 70. The upper limit correction value calculator 77b uses the function Fb shown below to calculate the upper limit correction value Cb corresponding to the fuel flow rate Fr represented by the fuel flow command Fro and the upper limit deviation ΔPbt (<0). This upper limit correction value Cb is a temperature correction value based on the pressure upper limit value Pb. Furthermore, this upper limit correction value Cb is negative.

[0081] Fb:Cb=k×ΔPbt / Fr

[0082] Additionally, in the above formula, k is the correction coefficient.

[0083] When the first switch 78a of the pressure control system 70 receives the ONa signal from the lower limit correction indicator 75a, it outputs the lower limit correction value Ca calculated by the lower limit correction value calculator 77a. Conversely, when the first switch 78a does not receive the ONa signal from the lower limit correction indicator 75a, it outputs 0 as the lower limit correction value. When the second switch 78b of the pressure control system 70 receives the ONb signal from the upper limit correction indicator 75b, it outputs the upper limit correction value Cb calculated by the upper limit correction value calculator 77b. Conversely, when the second switch 78b does not receive the ONb signal from the upper limit correction indicator 75b, it outputs 0 as the upper limit correction value.

[0084] The first adder 79a of the pressure control system 70 adds the lower limit correction value Ca to the temperature deviation ΔT calculated by the temperature deviation calculator 67. The second adder 79b of the pressure control system 70 adds the upper limit correction value Cb to the temperature deviation ΔT calculated by the temperature deviation calculator 67.

[0085] The PI controller 68 of the pressure control system 70 calculates the opening correction amount corresponding to (temperature deviation ΔT + lower limit correction value Ca) or (temperature deviation ΔT + upper limit correction value Cb) of the proportional / integral action quantity, and outputs the valve command corresponding to the opening correction amount to the three-way valve 57.

[0086] The operation of the three-way valve 57 is controlled by the operation of the temperature control system 65 described above, thereby controlling the amount of heat exchange in the heat exchange regulation process S2 so that the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within the preset pressure range.

[0087] The flow ratio adjustment step S2b of the heat exchange quantity adjustment step S2 is executed by the heat exchange quantity regulator 56, i.e., the three-way valve 57. The three-way valve 57 adjusts the ratio of the flow rate of the main high-temperature water to the flow rate of the branch high-temperature water after heat exchange in the heat exchange step S3, based on an instruction from the temperature control system 65, and merges the main high-temperature water with the branch high-temperature water after heat exchange in the heat exchange step S3. As a result, the merged high-temperature water is adjusted to a temperature sufficient to vaporize liquid ammonia in the vaporizer 45. In this embodiment, the boiling point of the liquid ammonia pressurized by the ammonia pump 44 is less than 60°C. Therefore, in this embodiment, the temperature of the warm water flowing into the vaporizer 45 is adjusted to approximately 60°C to 90°C.

[0088] Furthermore, upon receiving an instruction from the pressure control system 70, the three-way valve 57 adjusts the ratio of the flow rate of the main high-temperature water to the flow rate of the branch high-temperature water after heat exchange in the heat exchange process S3, thereby merging the main high-temperature water with the branch high-temperature water after heat exchange in the heat exchange process S3. As a result, the merged high-temperature water is adjusted to a temperature sufficient to vaporize liquid ammonia in the vaporizer 45, and the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within a preset pressure range.

[0089] In the gasification process S6, within the gasifier 45, warm water, whose heat exchange with the medium has been adjusted through the heat exchange rate adjustment process S2, exchanges heat with liquid ammonia to vaporize the liquid ammonia.

[0090] In the low-temperature water recovery process S7, in the vaporizer 45, warm water cooled by heat exchange with liquid ammonia is returned to the warm water heater 52 via the low-temperature water pipeline 51. The warm water returned to the warm water heater 52 is heated by exhaust gas. That is, the aforementioned warm water heating process S1 is performed by the warm water heater 52.

[0091] In the fuel supply process S8, ammonia vaporized by the gasifier 45, i.e. gaseous ammonia, is supplied to the burner 15 of the gas turbine 10 via the gaseous ammonia pipeline 46.

[0092] As described above, in this embodiment, the warm water heated in the warm water heater 52 through heat exchange with the exhaust gas is conditioned before flowing into the vaporizer 45. In the vaporizer 45, the conditioned warm water exchanges heat with liquid ammonia, causing the ammonia to vaporize. The temperature of the exhaust gas flowing within the waste heat recovery boiler 21 varies depending on the operating conditions of the gas turbine 10. Therefore, if the exhaust gas temperature changes, the temperature of the warm water heated by the warm water heater 52 also changes. However, in this embodiment, as mentioned earlier, the warm water heated by the warm water heater 52 flows into the vaporizer 45 after temperature conditioning. Therefore, in this embodiment, even if the exhaust gas temperature changes, all liquid ammonia flowing into the vaporizer 45 can be easily and reliably converted into gaseous ammonia.

[0093] Furthermore, the amount of gaseous ammonia required by the gas turbine 10 also varies depending on the operating conditions of the gas turbine 10. In this embodiment, even if the amount of gaseous ammonia required by the gas turbine 10 changes, all liquid ammonia flowing into the vaporizer 45 can be easily and reliably converted into gaseous ammonia by changing the temperature of the warm water flowing into the vaporizer 45.

[0094] Therefore, in this embodiment, even if the operating conditions of the gas turbine 10 change, the required amount of gaseous ammonia generated by the gas turbine 10 can be easily and reliably obtained. Furthermore, in this embodiment, the responsiveness of the amount of gaseous ammonia generated in response to changes in the operating conditions of the gas turbine 10 can be improved.

[0095] As mentioned above, the flow rate of fuel supplied to the gas turbine 10 changes according to the change in the requested output PWr of the gas turbine 10. In this case, the amount of heat exchange between the fuel and warm water in the vaporizer 45 changes along with the change in fuel flow rate. If the temperature of the warm water is adjusted according to the result of this change in heat exchange, it would take time from the time the requested output PWr changes until the amount of gaseous ammonia generated is ensured. In this embodiment, the operating amount of the heat exchange regulator 56 is set according to the requested output PWr, thus shortening the time from the time the requested output PWr changes until the amount of gaseous ammonia generated is ensured. Therefore, in this embodiment, from the above viewpoint, the responsiveness of the amount of gaseous ammonia generated to changes in the requested output PWr can also be improved.

[0096] If the pressure of gaseous ammonia flowing into the gas turbine 10 is not within a preset pressure range, stable combustion of the gaseous ammonia cannot be achieved within the gas turbine 10. In this embodiment, the pressure is controlled by the pressure control system 70 to ensure that the pressure of gaseous ammonia flowing into the gas turbine 10 falls within a preset pressure range. Therefore, in this embodiment, stable combustion of gaseous ammonia can be achieved within the gas turbine 10.

[0097] Here, we investigate the case where liquid ammonia flows into the heat transfer tube 45p of the vaporizer 45, and warm water flows into the vaporizer shell 45c covering the heat transfer tube 45p. In this case, the liquid ammonia in the heat transfer tube 45p becomes gaseous ammonia, and a portion of the gaseous ammonia remains within the heat transfer tube 45p. Therefore, the effective heat transfer area for heat exchange between the liquid ammonia and the warm water decreases relative to the total heat transfer area of ​​the heat transfer tube 45p. Moreover, in this case, the effective heat transfer area for heat exchange between the liquid ammonia and the warm water also changes relative to the change in the amount of gaseous ammonia generated. Therefore, in this case, it is sometimes difficult to control the amount of heat exchange between the liquid ammonia and the warm water, and it is impossible to ensure the required amount of gaseous ammonia generated.

[0098] On the other hand, in this embodiment, warm water flows into the heat transfer tube 45p of the vaporizer 45, and liquid ammonia flows into the vaporizer shell 45c covering the heat transfer tube 45p. Therefore, in this embodiment, if the liquid ammonia in contact with the outer surface of the heat transfer tube 45p is vaporized, it can be separated from the outer surface of the heat transfer tube 45p. Therefore, in this embodiment, compared with the previous case, the effective heat transfer area for heat exchange between liquid ammonia and warm water can be increased relative to the total heat transfer area of ​​the heat transfer tube 45p. Moreover, in this embodiment, the effective heat transfer area for heat exchange between liquid ammonia and warm water does not actually change relative to changes in the amount of gaseous ammonia generated. Therefore, from this point of view, in this embodiment, the amount of heat exchange between liquid ammonia and warm water can be easily controlled, and the desired amount of gaseous ammonia generated can be easily and reliably obtained.

[0099] Within the boiler shell 21c, the temperature of the exhaust gas decreases as it flows downstream. In this embodiment, the hot water heater 52 is positioned further downstream than the most downstream heat transfer tube (economizer 21eco) among the plurality of heat transfer tubes within the boiler shell 21c. Therefore, in this embodiment, the heat from the cooled exhaust gas can be effectively utilized in the hot water heater 52.

[0100] "Second Implementation Method"

[0101] Next, using Figure 5 and Figure 6 A second embodiment of the gas turbine device according to the present invention will be described.

[0102] Similar to the gas turbine device of the first embodiment, such as Figure 5 As shown, the gas turbine equipment of this embodiment also includes a gas turbine 10, a denitrification device 20, a waste heat recovery boiler 21, a chimney 22, a steam turbine 23, a condenser 24, a pump 25, and a control device 60. Furthermore, the gas turbine equipment of this embodiment includes a fuel supply device 40a, which is different from the fuel supply device 40 of the first embodiment.

[0103] Similar to the fuel supply device 40 of the first embodiment, the fuel supply device 40a of this embodiment includes an ammonia tank 41, a liquid ammonia pipeline 42, a liquid ammonia regulating valve 43a, a fuel regulating valve 43b, an ammonia pump 44, a vaporizer 45, a gaseous ammonia pipeline 46, a warm water pump 54, a heat exchanger 55, a medium pipeline 58i, a medium recovery pipeline 58o, and a medium flow regulator 59. Furthermore, the fuel supply device 40a of this embodiment has a warm water pipeline 50a, which is different from the warm water pipeline 50 of the first embodiment, and a heat exchange quantity regulator 56a, which is different from the heat exchange quantity regulator 56 of the first embodiment.

[0104] Similar to the warm water pipe 50 of the first embodiment, the warm water pipe 50a of this embodiment includes a low-temperature water pipe 51 and a warm water heater 52. Furthermore, the warm water pipe 50a of this embodiment includes a high-temperature water pipe 53a, which differs from the high-temperature water pipe 53 of the first embodiment. The high-temperature water pipe 53 of the first embodiment has a branch high-temperature water pipe 53y, but the high-temperature water pipe 53a of this embodiment does not have this branch high-temperature water pipe 53y.

[0105] In this embodiment, the heat exchanger 55 is installed in the high-temperature water pipe 53a. Therefore, all high-temperature water from the warm water heater 52 flows into the heat exchanger 55 via the high-temperature water pipe 53a. Similar to the first embodiment, a medium flow regulator 59 is installed in the medium pipe 58i connected to the heat exchanger 55. The heat exchange capacity regulator 56a in this embodiment includes the medium flow regulator 59.

[0106] In this embodiment, the control device 60 controls the operation of the medium flow regulator 59 when adjusting the temperature of the warm water.

[0107] Next, according to Figure 6 The flowchart shown illustrates the fuel supply method for the gas turbine equipment in this embodiment.

[0108] Similar to the fuel supply method of the first embodiment, the fuel supply method of this embodiment performs the following steps: warm water heating step S1, heat exchange step S3, pressure control step S5, temperature control step S4, gasification step S6, low-temperature water recovery step S7, and fuel supply step S8. Furthermore, similar to the fuel supply method of the first embodiment, the fuel supply method of this embodiment also performs the pressure control step S5 based on a request from the operator. Moreover, the fuel supply method of this embodiment performs a heat exchange quantity adjustment step S2X, which is different from the heat exchange quantity adjustment step S2 of the first embodiment.

[0109] Similar to the heat exchange rate adjustment step S2 in the first embodiment, in the heat exchange rate adjustment step S2X of this embodiment, the temperature of the high-temperature water flowing into the vaporizer 45 is also adjusted by regulating the amount of heat exchange between the high-temperature water from the warm water heater 52 and the medium flowing into the heat exchanger 55. However, the method for adjusting the amount of heat exchange in the heat exchange rate adjustment step S2X of this embodiment differs from the method for adjusting the amount of heat exchange in the heat exchange rate adjustment step S2 in the first embodiment. The heat exchange rate adjustment step S2X of this embodiment includes a medium flow rate adjustment step S2c.

[0110] In the medium flow rate regulation step S2c, the medium flow rate regulator 59, which acts as a heat exchange quantity regulator 56a, operates according to the instruction from the temperature control system 65 or the pressure control system 70 of the control device 60. As a result, the flow rate of the medium flowing into the heat exchanger 55 is regulated. Consequently, the amount of heat exchange between the medium in the heat exchanger 55 and the high-temperature water is regulated, and the temperature of the high-temperature water flowing into the vaporizer 45 is regulated.

[0111] Furthermore, in this embodiment, the PI controller 68 of the temperature control system 65 calculates the opening correction amount of the proportional / integral action corresponding to the temperature deviation ΔT, and outputs the action amount corresponding to the opening correction amount to the medium flow regulator 59. Also, in this embodiment, the PI controller 68 of the pressure control system 70 calculates the opening correction amount of the proportional / integral action corresponding to (temperature deviation ΔT + lower limit correction value Ca) or (temperature deviation ΔT + upper limit correction value Cb), and outputs the action amount corresponding to the opening correction amount to the medium flow regulator 59.

[0112] Thus, the operation of the medium flow regulator 59 is controlled by the operation of the temperature control system 65 or the pressure control system 70, thereby controlling the heat exchange quantity in the heat exchange quantity regulation process S2X.

[0113] As described above, in this embodiment, the warm water heated by the warm water heater 52 flows into the vaporizer 45 after temperature regulation, so even if the operating conditions of the gas turbine 10 change, the required amount of gaseous ammonia generated by the gas turbine 10 can be easily obtained. Furthermore, in this embodiment, the responsiveness of the amount of gaseous ammonia generated in response to changes in the operating conditions of the gas turbine 10 can be improved.

[0114] Furthermore, the high-temperature water pipe 53a of this embodiment does not have a branch high-temperature water pipe 53y, thus simplifying the pipe structure compared to the gas turbine equipment of the first embodiment, thereby reducing equipment costs.

[0115] In addition, similar to this embodiment, the heat exchange quantity regulator 56 of the first embodiment may also have a medium flow regulator 59 in addition to the three-way valve 57.

[0116] "Modifications of the control device"

[0117] Next, using Figure 7 A variation of the control device described above will be explained. In the control device 60 of each of the above embodiments, it can be set to a pressure correction mode. In the control device 60a of this variation, in addition to the pressure correction mode, it can also be set to a lower pressure limit control mode and a higher pressure limit control mode.

[0118] Similar to the control device 60 in the above embodiments, the control device 60a in this modified example includes a fuel flow calculation unit 61, a fuel valve control unit 62, and an IGV control unit 63. Furthermore, the control device 60a in this modified example includes a temperature control system 65a, which is different from the temperature control system 65 in the above embodiments, and a pressure control system 70a, which is different from the pressure control system 70 in the above embodiments.

[0119] Similar to the temperature control system 65 in the above embodiments, the temperature control system 65a of this modified example has a target temperature calculator 66 and a temperature deviation calculator 67. Furthermore, the temperature control system 65a of this modified example includes a PT controller / switcher 68a having the same functions as the PI controller 68 in the above embodiments.

[0120] Similar to the temperature control system 65 in the above embodiments, the temperature control system 65a of this modified example calculates the opening correction amount of the proportional / integral action quantity corresponding to the temperature deviation ΔT between the target temperature and the temperature detected by the thermometer 48, and outputs the action quantity corresponding to the opening correction amount to the three-way valve 57 or the medium flow regulator 59, which are heat exchange quantity regulators 56 and 56a.

[0121] Similar to the pressure control system 70 in the above embodiments, the pressure control system 70a of this modified example includes a pressure correction mode button 71, a lower limit value memory 72a, an upper limit value memory 72b, a lower limit deviation calculator 73a, an upper limit deviation calculator 73b, a lower limit deviation judge 74a, an upper limit deviation judge 74b, a lower limit correction indicator 75a, an upper limit correction indicator 75b, a lower limit correction value calculator 77a, an upper limit correction value calculator 77b, a first switch 78a, a second switch 78b, a first adder 79a, and a second adder 79b. The pressure control system 70a of this modified example also includes a PI control / switcher 68a. The pressure control system 70a and the temperature control system 65a share this PI control / switcher 68a.

[0122] The pressure control system 70a of this modified example also has a lower limit control mode button 71a, an upper limit control mode button 71b, a lower limit control indicator 76a, and an upper limit control indicator 76b.

[0123] The lower limit control mode button 71a receives information from the operator regarding whether they wish to control the lower pressure limit. If the operator presses the lower limit control mode button 71a, it outputs an ON signal, and the control device 60a enters the lower pressure limit control mode. The upper limit control mode button 71b receives information from the operator regarding whether they wish to control the upper pressure limit. If the operator presses the upper limit control mode button 71b, it outputs an ON signal, and the control device 60a enters the upper pressure limit control mode.

[0124] When the lower limit control indicator 76a receives an ONac signal indicating that temperature control based on the lower pressure limit value Pa is executed, and the lower limit deviation ΔPat calculated by the lower limit deviation calculator 73a is positive and an ON signal is received from the lower limit control mode button 71a, the lower limit control indicator 76a outputs an OFFac signal indicating that temperature control based on the lower pressure limit value Pa is not executed. When the upper limit control indicator 76b receives an ON signal indicating that the upper limit deviation ΔPbt calculated by the upper limit deviation calculator 73b is negative and an ON signal is received from the upper limit control mode button 71b, the upper limit control indicator 76b outputs an ONbc signal indicating that temperature control based on the upper pressure limit value Pb is executed. Conversely, when the upper limit deviation ΔPbt is not negative and an ON signal is not received from the upper limit control mode button 71b, the upper limit control indicator 76b outputs an OFFbc signal indicating that temperature control based on the upper pressure limit value Pb is not executed.

[0125] When the PI controller / switcher 68a receives the ONac signal from the lower limit control indicator 76a, it calculates the action amount based on the lower limit deviation ΔPat calculated by the lower limit deviation calculator 73a, and outputs this action amount to the three-way valve 57 or the medium flow regulator 59, which acts as heat exchange quantity regulators 56, 56a. The action amount of the three-way valve 57 or the medium flow regulator 59 at this time differs from the action amount when temperature correction based on the lower pressure limit value Pa is performed in pressure correction mode. Therefore, the action amount of the three-way valve 57 or the medium flow regulator 59 changes depending on whether the operator selects the pressure correction mode or the lower pressure limit control mode.

[0126] Furthermore, when the PI controller / switcher 68a receives the ONbc signal from the upper limit control indicator 76b, it calculates the action amount based on the upper limit deviation ΔPbt calculated by the upper limit deviation calculator 73b, and outputs this action amount to the three-way valve 57 or the medium flow regulator 59, which acts as heat exchange quantity regulators 56 and 56a. At this time, the action amount of the three-way valve 57 or the medium flow regulator 59 differs from the action amount when temperature correction based on the pressure upper limit value Pb is performed in pressure correction mode. Therefore, the action amount of the three-way valve 57 or the medium flow regulator 59 changes depending on whether the operator selects the pressure correction mode or the pressure condition value control mode.

[0127] Furthermore, the buttons of the control device 60 in the above embodiments and the control device 60a in this modified example can be physically existing buttons or virtually existing buttons in the display, etc.

[0128] Other variations

[0129] The above example uses cooling water as the medium for heat exchange with warm water. However, any medium other than cooling water can be used as long as there is a certain temperature difference between the medium and the warm water.

[0130] In the above embodiments and modifications, after the warm water is heated to approximately 90°C by the warm water heater 52, the warm water is subjected to heat exchange with a medium such as cooling water, thereby cooling the warm water and setting its temperature to 90°C to 60°C. However, the temperature of the warm water can also be adjusted by further heating the heated water using the warm water heater 52. In this case, the warm water is heated to approximately 50°C in the warm water heater 52, for example. Then, the heated warm water is further heated by heat exchange with a medium of approximately 100°C to 70°C, for example, to set its temperature to 90°C to 60°C.

[0131] In the above embodiments and modifications, the hot water heater 52 is disposed within the boiler shell 21c at a position further downstream than the downstream heat transfer tube, i.e., the economizer 21eco, among the plurality of heat transfer tubes. However, the hot water heater 52 may also be disposed within the boiler shell 21c at a position overlapping the downstream heat transfer tube in the direction of exhaust flow.

[0132] The gas turbine 10 in the above embodiments and modifications are all so-called single-shaft gas turbines. However, the gas turbine can also be a dual-shaft gas turbine. That is, the gas turbine can also have a compressor, a burner, a high-pressure turbine, and a low-pressure turbine. In this case, the compressor rotor and the high-pressure turbine rotor are connected to each other to form a first gas turbine rotor. Furthermore, the low-pressure turbine rotor forms a second gas turbine rotor and is not mechanically connected to the first gas turbine rotor.

[0133] The gas turbine equipment described in the above embodiments and modifications is a combined cycle unit comprising a gas turbine 10, a waste heat recovery boiler 21, and a steam turbine 23. However, the gas turbine equipment may also be a cogeneration unit comprising a gas turbine 10 and a waste heat recovery boiler 21 but without a steam turbine. In this case, the steam generated in the waste heat recovery boiler 21 is utilized, for example, within the plant.

[0134] The gas turbine equipment in the above embodiments and modifications includes a denitrification device 20. However, when the NOx concentration in the exhaust gas discharged from the gas turbine 10 meets environmental standards, the gas turbine equipment may also be an equipment without a denitrification device.

[0135] The embodiments and modifications of the present invention have been described in detail above, but the present invention is not limited to the above embodiments and modifications. Various additions, modifications, substitutions, and partial deletions can be made without departing from the conceptual idea and spirit of the present invention derived from the content specified in the technical solutions and their equivalents.

[0136] Postscript

[0137] For example, the gas turbine device in the above embodiments can be understood as follows.

[0138] (1) The gas turbine equipment in the first method has:

[0139] A gas turbine 10 burns fuel and is driven by combustion gases generated from the combustion of said fuel; a waste heat recovery boiler 21 is able to generate steam using heat from the exhaust gas from said gas turbine 10; and fuel supply devices 40, 40a are able to supply ammonia, which is said fuel, to said gas turbine 10. The fuel supply devices 40 and 40a include: a liquid ammonia pipeline 42 connected to an ammonia tank 41 capable of storing liquid ammonia; warm water pipelines 50 and 50a for flowing warm water; a vaporizer 45 connected to the end of the liquid ammonia pipeline 42, capable of exchanging heat between the warm water from the warm water pipelines 50 and 50a and the liquid ammonia to heat and vaporize the liquid ammonia; a heat exchanger 55 for exchanging heat between the warm water in the warm water pipelines 50 and 50a and a medium; heat exchange rate regulators 56 and 56a for adjusting the amount of heat exchange between the warm water and the medium to adjust the temperature of the warm water flowing into the vaporizer 45; and a gaseous ammonia pipeline 46 for guiding the ammonia vaporized by the vaporizer 45, i.e., gaseous ammonia, to the gas turbine 10. The vaporizer 45 has an ammonia inlet 45ci, an ammonia outlet 45co, a warm water inlet 45pi, and a warm water outlet 45po. The liquid ammonia pipeline 42 is connected to the ammonia inlet 45ci of the vaporizer 45. The gaseous ammonia pipeline 46 is connected to the ammonia outlet 45co of the vaporizer 45. The warm water pipelines 50 and 50a have a warm water heater 52 disposed in the waste heat recovery boiler 21 to heat the warm water by exchanging heat with the exhaust gas, and high-temperature water pipelines 53 and 53a connecting the warm water heater 52 to the warm water inlet 45pi of the vaporizer 45. The heat exchanger 55 is disposed in the high-temperature water pipelines 53 and 53a.

[0140] In this method, the heated water obtained through heat exchange between the water heater 52 and the exhaust gas flows into the vaporizer 45 after temperature regulation. In the vaporizer 45, the temperature-regulated water exchanges heat with liquid ammonia, causing the ammonia to vaporize. The temperature of the exhaust gas flowing within the waste heat recovery boiler 21 varies depending on the operating conditions of the gas turbine 10. Therefore, if the exhaust gas temperature changes, the temperature of the heated water from the water heater 52 also changes. However, in this method, as mentioned above, the heated water from the water heater 52 flows into the vaporizer 45 after temperature regulation. Therefore, in this method, even if the exhaust gas temperature changes, all the liquid ammonia flowing into the vaporizer 45 can be easily converted into gaseous ammonia.

[0141] Furthermore, the amount of gaseous ammonia required by the gas turbine 10 also varies depending on the operating conditions of the gas turbine 10. In this method, even if the amount of gaseous ammonia required by the gas turbine 10 changes, all liquid ammonia flowing into the gasifier 45 can be easily converted into gaseous ammonia by changing the temperature of the warm water flowing into the gasifier 45.

[0142] Therefore, in this method, even if the operating conditions of the gas turbine 10 change, the required amount of gaseous ammonia generated by the gas turbine 10 can be easily obtained. Furthermore, this method improves the responsiveness of the amount of gaseous ammonia generated in response to changes in the operating conditions of the gas turbine 10.

[0143] (2) The gas turbine device in the second embodiment is the same as the gas turbine device in the first embodiment.

[0144] The high-temperature water pipeline 53 has a main high-temperature water pipeline 53x connecting the warm water inlet 45pi of the vaporizer 45 to the warm water heater 52, and a branch high-temperature water pipeline 53y connecting to the main high-temperature water pipeline 53x after branching off from it. The heat exchanger 55 is disposed in the branch high-temperature water pipeline 53y. The heat exchange capacity regulator 56 has a flow ratio regulator that adjusts the ratio of the flow rate of warm water flowing in the main high-temperature water pipeline 53x between the branch position and the connection position of the branch high-temperature water pipeline 53y to the flow rate of warm water flowing in the branch high-temperature water pipeline 53y.

[0145] In this method, the amount of heat exchange between the warm water and the medium can be adjusted by adjusting the ratio of the flow rate of the warm water flowing between the branch position of the branch high-temperature water pipe 53y and the connection position of the branch high-temperature water pipe 53y in the main high-temperature water pipe 53x and the flow rate of the warm water flowing in the branch high-temperature water pipe 53y.

[0146] (3) The gas turbine equipment in the third method is in the gas turbine equipment in the first method or the second method.

[0147] The heat exchange capacity regulator 56a has a medium flow regulator 59 for regulating the flow rate of the medium flowing into the heat exchanger 55.

[0148] In this method, the amount of heat exchange between the warm water and the medium can be adjusted by regulating the flow rate of the medium flowing into the heat exchanger 55.

[0149] (4) The gas turbine equipment in the fourth embodiment is the same as the gas turbine equipment in any one of the first to third embodiments.

[0150] The vaporizer 45 has a heat transfer tube 45p and a vaporizer shell 45c. The heat transfer tube 45p has a warm water inlet 45pi and a warm water outlet 45po, and warm water can flow through it. The vaporizer shell 45c covers the heat transfer tube 45p and can temporarily store the liquid ammonia. The vaporizer shell 45c has an ammonia inlet 45ci and an ammonia outlet 45co. A liquid ammonia pipeline 42 is connected to the ammonia inlet 45ci of the vaporizer shell 45c, and a gaseous ammonia pipeline 46 is connected to the ammonia outlet 45co of the vaporizer shell 45c.

[0151] When liquid ammonia flows into heat transfer tube 45p and warm water flows into the vaporizer shell 45c covering heat transfer tube 45p, the liquid ammonia in heat transfer tube 45p becomes gaseous ammonia, and a portion of the gaseous ammonia remains in heat transfer tube 45p. Therefore, the effective heat transfer area for heat exchange between liquid ammonia and warm water decreases relative to the total heat transfer area of ​​heat transfer tube 45p. Furthermore, in this case, the effective heat transfer area for heat exchange between liquid ammonia and warm water also changes relative to the amount of gaseous ammonia generated. Therefore, in this situation, it is sometimes difficult to control the amount of heat exchange between liquid ammonia and warm water, and it is impossible to ensure the required amount of gaseous ammonia generated.

[0152] On the other hand, in this method, warm water flows into the heat transfer tube 45p, and liquid ammonia flows into the vaporizer shell 45c covering the heat transfer tube 45p. Therefore, in this method, if the liquid ammonia in contact with the outer surface of the heat transfer tube 45p is vaporized, it can be separated from the outer surface of the heat transfer tube 45p. Therefore, in this method, compared with the previous case, the effective heat transfer area for heat exchange between liquid ammonia and warm water can be increased relative to the total heat transfer area of ​​the heat transfer tube 45p. Moreover, in this method, the effective heat transfer area for heat exchange between liquid ammonia and warm water does not actually change relative to changes in the amount of gaseous ammonia generated. Therefore, in this method, the amount of heat exchange between liquid ammonia and warm water can be easily controlled, and the desired amount of gaseous ammonia generated can be easily obtained.

[0153] (5) The gas turbine device in the fifth embodiment is the same as the gas turbine device in any one of the first to fourth embodiments.

[0154] The waste heat recovery boiler 21 has a boiler shell 21c from the exhaust flow of the gas turbine 10 and a plurality of heat transfer tubes disposed within the boiler shell 21c and into which water or steam flows. The plurality of heat transfer tubes are arranged within the boiler shell 21c along the flow direction of the exhaust. The hot water heater 52 is disposed within the boiler shell 21c at an overlapping position or further downstream of the downstream heat transfer tube in the flow direction of the exhaust, relative to the downstreammost heat transfer tube among the plurality of heat transfer tubes.

[0155] Within the boiler shell 21c, the temperature of the exhaust gas decreases as it flows downstream. In this configuration, the heat from the cooled exhaust gas can be effectively utilized in the hot water heater 52.

[0156] (6) The gas turbine device in the sixth embodiment further comprises:

[0157] Control devices 60 and 60a control the operation of the heat exchange quantity regulators 56 and 56a. The control devices 60 and 60a have a temperature control system 65 and 65a that sets the operation amount of the heat exchange quantity regulators 56 and 56a based on an external request output PWr to the gas turbine 10 and instructs the heat exchange quantity regulators 56 and 56a to operate at that amount.

[0158] The flow rate of fuel supplied to the gas turbine 10 changes according to the change in the requested output PWr of the gas turbine 10. In this case, the amount of heat exchange between the fuel and warm water in the vaporizer 45 changes along with the change in fuel flow rate. If the temperature of the warm water is adjusted based on this change in heat exchange, it would require a time from the time the requested output PWr changes until the amount of gaseous ammonia generated is ensured. In this method, the operating amount of the heat exchange regulators 56 and 56a is set according to the requested output PWr, thus shortening the time from the time the requested output PWr changes until the amount of gaseous ammonia generated is ensured. In other words, in this method, the responsiveness of gaseous ammonia generation to changes in the requested output PWr can be improved.

[0159] (7) The gas turbine device in the seventh embodiment is the same as the gas turbine device in the sixth embodiment.

[0160] The control devices 60 and 60a also have pressure control systems 70 and 70a, which control the actuation amount of the heat exchange quantity regulators 56 and 56a and instruct the heat exchange quantity regulators 56 and 56a to ensure that the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within a preset pressure range.

[0161] If the pressure of gaseous ammonia flowing into the gas turbine 10 is not within a preset pressure range, stable combustion of the gaseous ammonia cannot be achieved within the gas turbine 10. In this method, pressure control systems 70 and 70a are used to ensure that the pressure of gaseous ammonia flowing into the gas turbine 10 falls within a preset pressure range. Therefore, in this method, stable combustion of gaseous ammonia can be achieved within the gas turbine 10.

[0162] For example, the fuel supply methods of the gas turbine equipment in the above embodiments and modifications can be understood as follows.

[0163] (8) The fuel supply method for the gas turbine equipment in the eighth embodiment is a fuel supply method for the gas turbine equipment, wherein the gas turbine equipment includes a gas turbine 10 that burns fuel and is driven by combustion gases generated from the combustion of the fuel, and a waste heat recovery boiler 21 that can generate steam using heat from the exhaust gas from the gas turbine 10. The fuel supply method for the gas turbine equipment performs the following steps: a warm water heating step S1, wherein the warm water in the warm water heater 52 disposed in the waste heat recovery boiler 21 is heated by exchanging heat with the exhaust gas outside the warm water heater 52 in the waste heat recovery boiler 21; The heat exchange process S3 involves exchanging heat between the heated water obtained in the heating process S1 and the medium; the heat exchange amount adjustment processes S2 and S2X adjust the amount of heat exchange between the heated water obtained in the heating process S1 and the medium; the gasification process S6 involves, within the gasifier 45, exchanging heat between the heated water, after the heat exchange amount adjustment processes S2 and S2X, and the liquid ammonia from the ammonia tank 41 containing liquid ammonia, thereby gasifying the liquid ammonia; and the fuel supply process S8 supplies the gasified ammonia, i.e., gaseous ammonia, obtained in the gasification process S6, to the gas turbine 10 as fuel.

[0164] In the heat exchange rate adjustment processes S2 and S2X, the temperature of the warm water flowing into the vaporizer 45 is adjusted by regulating the amount of heat exchange between the warm water and the medium in the heat exchange process S3.

[0165] In this method, similar to the gas turbine device of the first method, the required amount of gaseous ammonia generated by the gas turbine 10 can be easily obtained even if the operating conditions of the gas turbine 10 change. Moreover, in this method, the responsiveness of the amount of gaseous ammonia generated in response to changes in the operating conditions of the gas turbine 10 can also be improved.

[0166] (9) The fuel supply method for the gas turbine equipment in the ninth embodiment is described in the fuel supply method for the gas turbine equipment in the eighth embodiment.

[0167] The heat exchange rate adjustment process S2 includes a diversion process S2a, which separates the heated water obtained in the warm water heating process S1 into main high-temperature water and branch high-temperature water, and a flow ratio adjustment process S2b. In the heat exchange process S3, the branch high-temperature water exchanges heat with the medium. In the flow ratio adjustment process S2b, the ratio of the flow rate of the main high-temperature water to the flow rate of the branch high-temperature water after heat exchange in the heat exchange process S3 is adjusted, and the main high-temperature water and the branch high-temperature water after heat exchange in the heat exchange process S3 are combined.

[0168] In this method, similar to the gas turbine device as the second method, the amount of heat exchange between the warm water and the medium can be adjusted.

[0169] (10) The fuel supply method for the gas turbine equipment in the 10th embodiment is in the fuel supply method for the gas turbine equipment in the 8th or 9th embodiment.

[0170] The heat exchange quantity adjustment process S2X includes a medium flow rate adjustment process S2c that adjusts the flow rate of the medium that exchanges heat with the warm water in the heat exchange process S3.

[0171] In this method, similar to the gas turbine device as the third method, the amount of heat exchange between the warm water and the medium can be adjusted.

[0172] (11) The fuel supply method for the gas turbine equipment in the 11th embodiment further comprises, in any one of the 8th to 10th embodiments, the fuel supply method for the gas turbine equipment:

[0173] Temperature control step S4 outputs PWr based on external requests to the gas turbine 10, and controls the adjustment of heat exchange quantity in heat exchange quantity adjustment steps S2 and S2X.

[0174] In this method, similar to the gas turbine device as the sixth method, the responsiveness of gaseous ammonia generation to changes in the requested output PWr can be improved.

[0175] (12) The fuel supply method for the gas turbine in the 12th embodiment further includes, in addition to, the fuel supply method for the gas turbine in the 11th embodiment:

[0176] Pressure control step S5 controls the adjustment of heat exchange quantity in the heat exchange quantity adjustment steps S2 and S2X so that the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within a preset pressure range.

[0177] In this method, similar to the gas turbine device as the seventh method, gaseous ammonia can be stably burned within the gas turbine 10.

[0178] Industrial availability

[0179] According to one aspect of the present invention, the amount of gaseous ammonia required for the gas turbine can be easily obtained.

[0180] Symbol Explanation

[0181] 10-Gas turbine, 11-Gas turbine rotor, 12-Intermediate casing, 14-Compressor, 14r-Compressor rotor, 14c-Compressor casing, 14i-Intake volume regulator (or IGV), 15-Burner, 16-Turbine, 16r-Turbine rotor, 16c-Turbine casing, 20-Denitrification unit, 21-Waste heat recovery boiler, 21c-Boiler casing, 21eco-Economizer, 21eva-Evaporator, 21s-Superheater, 22-Chimney, 23-Steam turbine, 24-Condenser, 25-Pump, 26-Water supply line, 27-Main steam line, 40, 40a-Fuel supply equipment, 41 42-Ammonia tank, 43a-Liquid ammonia pipeline, 43b-Fuel regulating valve, 44-Ammonia pump, 45-Vaporizer, 45c-Vaporizer shell, 45ci-Ammonia inlet, 45co-Ammonia outlet, 45p-Heat transfer tube, 45pi-Warm water inlet, 45po-Warm water outlet, 46-Gaseous ammonia pipeline, 48-Thermometer, 49-Pressure gauge, 50, 50a-Warm water pipeline, 51-Low temperature water pipeline, 52-Warm water heater, 53, 53a-High temperature water pipeline, 53x-Main high temperature water pipeline, 53y-Branch high temperature water pipeline, 54-Warm water pump, 55-Heat exchanger, 55c-Heat exchanger Shell, 55p - heat transfer tube, 55pi - medium inlet, 55po - medium outlet, 56, 56a - heat exchange capacity regulator, 57 - three-way valve (or flow ratio regulator), 58i - medium pipeline, 58o - medium recovery pipeline, 59 - medium flow regulator, 60, 60a - control device, 61 - fuel flow calculation unit, 62 - fuel valve control unit, 63 - IGV control unit, 65, 65a - temperature control system, 66 - target temperature calculator, 67 - temperature deviation calculator, 68 - PI controller, 68a - PI controller / switcher, 70, 70a - pressure control system, 71 - pressure correction Mode buttons: 71a - Lower limit control mode button, 71b - Upper limit control mode button, 72a - Lower limit value memory, 72b - Upper limit value memory, 73a - Lower limit deviation calculator, 73b - Upper limit deviation calculator, 74a - Lower limit deviation judge, 74b - Upper limit deviation judge, 75a - Lower limit correction indicator, 75b - Upper limit correction indicator, 76a - Lower limit control indicator, 76b - Upper limit control indicator, 77a - Lower limit correction value calculator, 77b - Upper limit correction value calculator, 78a - First switcher, 78b - Second switcher, 79a - First adder, 79b - Second adder.

Claims

1. A gas turbine device, comprising: A gas turbine that burns fuel and is driven by the combustion gases generated from the combustion of said fuel; A waste heat recovery boiler is capable of generating steam using heat from the exhaust gas of the gas turbine; and A fuel supply device capable of supplying ammonia, the fuel, to the gas turbine. The fuel supply equipment has: Liquid ammonia pipeline, connected to an ammonia tank capable of storing liquid ammonia; Warm water pipes enable the flow of warm water; A vaporizer is connected to one end of the liquid ammonia pipeline and enables the warm water from the warm water pipeline to exchange heat with the liquid ammonia to heat the liquid ammonia and vaporize it. A heat exchanger enables the warm water in the warm water pipeline to exchange heat with the medium. A heat exchange regulator is used to adjust the amount of heat exchange between the warm water and the medium to adjust the temperature of the warm water flowing into the vaporizer. and The gaseous ammonia pipeline guides the ammonia vaporized by the vaporizer, i.e., gaseous ammonia, to the gas turbine. The vaporizer has an ammonia inlet, an ammonia outlet, a warm water inlet, and a warm water outlet. The liquid ammonia pipeline is connected to the ammonia inlet of the vaporizer. The gaseous ammonia pipeline is connected to the ammonia outlet of the vaporizer. The warm water pipeline includes a warm water heater disposed within the waste heat recovery boiler, which heats the warm water by exchanging heat with the exhaust gas, and a high-temperature water pipeline connecting the warm water heater to the warm water inlet of the gasifier. The heat exchanger is installed in the high-temperature water pipeline. The high-temperature water pipeline has a main high-temperature water pipeline connecting the warm water inlet of the vaporizer to the warm water heater, and a branch high-temperature water pipeline that branches off from the main high-temperature water pipeline and connects to the main high-temperature water pipeline. The heat exchanger is installed in the branch high-temperature water pipeline. The heat exchange capacity regulator has a flow ratio regulator, which adjusts the ratio of the flow rate of warm water flowing in the main high-temperature water pipeline between the branch position of the branch high-temperature water pipeline and the connection position of the branch high-temperature water pipeline to the flow rate of warm water flowing in the branch high-temperature water pipeline.

2. The gas turbine device according to claim 1, wherein, The heat exchange capacity regulator has a medium flow regulator for regulating the flow rate of the medium flowing into the heat exchanger.

3. The gas turbine device according to claim 1 or 2, wherein, The vaporizer has heat transfer tubes and a vaporizer shell. The heat transfer tubes have a warm water inlet and a warm water outlet, and the warm water can flow through them. The vaporizer shell covers the heat transfer tubes and can temporarily store the liquid ammonia. The vaporizer housing has the ammonia inlet and the ammonia outlet. The liquid ammonia pipeline is connected to the ammonia inlet of the vaporizer housing, and the gaseous ammonia pipeline is connected to the ammonia outlet of the vaporizer housing.

4. The gas turbine device according to claim 1 or 2, wherein, The waste heat recovery boiler has a boiler shell for the flow of exhaust gas from the gas turbine and multiple heat transfer tubes disposed within the boiler shell for the flow of water or steam. The plurality of heat transfer tubes are arranged within the boiler shell along the flow direction of the exhaust gas. The hot water heater is located within the boiler shell at a position overlapping or further downstream of the downstream heat transfer tube in the direction of exhaust flow, relative to the downstream heat transfer tube among the plurality of heat transfer tubes.

5. The gas turbine equipment according to claim 1 or 2, further comprising: The control device controls the operation of the heat exchange regulator. The control device has a temperature control system that sets the operating amount of the heat exchange quantity regulator based on an external request output to the gas turbine and instructs the operating amount of the heat exchange quantity regulator.

6. The gas turbine device according to claim 5, wherein, The control device also includes a pressure control system that sets the actuation amount of the heat exchange quantity regulator and instructs the heat exchange quantity regulator to actuate the actuation amount so that the pressure of the gaseous ammonia flowing into the gas turbine falls within a preset pressure range.

7. A fuel supply method for a gas turbine device, the gas turbine device comprising a gas turbine that burns fuel and is driven by combustion gases generated from the combustion of the fuel, and a waste heat recovery boiler that utilizes heat from exhaust gas from the gas turbine to generate steam, wherein the fuel supply method for the gas turbine device comprises the following steps: The warm water heating process involves exchanging heat between the warm water in the warm water heater located inside the waste heat recovery boiler and the exhaust gas outside the warm water heater inside the waste heat recovery boiler to heat the warm water. The heat exchange process involves exchanging heat between the heated water obtained in the warm water heating process and the medium. The heat exchange rate adjustment process adjusts the heat exchange rate between the heated water obtained in the heated water heating process and the medium. In the vaporization process, within the vaporizer, the warm water, after its heat exchange with the medium has been adjusted through the heat exchange rate adjustment process, exchanges heat with the liquid ammonia from an ammonia tank containing liquid ammonia to vaporize the liquid ammonia; and In the fuel supply process, the ammonia vaporized in the gasification process, i.e., gaseous ammonia, is supplied as fuel to the gas turbine. In the heat exchange rate adjustment process, the temperature of the warm water flowing into the vaporizer is adjusted by regulating the heat exchange rate between the warm water and the medium in the heat exchange process. The heat exchange rate adjustment process includes a process of dividing the heated water obtained in the heating process into a main high-temperature water and a branch high-temperature water, and a flow ratio adjustment process. In the heat exchange process, the branched high-temperature water exchanges heat with the medium. In the flow ratio adjustment process, the ratio of the flow rate of the main high-temperature water to the flow rate of the branch high-temperature water after heat exchange in the heat exchange process is adjusted, and the main high-temperature water and the branch high-temperature water after heat exchange in the heat exchange process are merged.

8. The fuel supply method for the gas turbine equipment according to claim 7, wherein, The heat exchange quantity adjustment process includes a medium flow rate adjustment process for adjusting the flow rate of the medium that exchanges heat with the warm water in the heat exchange process.

9. The fuel supply method for the gas turbine equipment according to claim 7 or 8, further comprising: The temperature control process controls the adjustment of the heat exchange quantity in the heat exchange quantity adjustment process based on the external request output to the gas turbine.

10. The fuel supply method for the gas turbine equipment according to claim 9, further comprising: The pressure control process controls the heat exchange rate in the heat exchange rate regulation process so that the pressure of the gaseous ammonia flowing into the gas turbine falls within a preset pressure range.

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