Gas turbine plant and fuel supply method therefor

Abstract

To obtain the amount of generation of gaseous ammonia required by a gas turbine.SOLUTION: A gas turbine plant comprises a gas turbine 10 and a fuel supply facility 40. The fuel supply facility comprises a liquid ammonia line 42, a hot water line 50 capable of passing hot water, a vaporizer 45 capable of exchanging heat between the hot water from the hot water line and liquid ammonia from the liquid ammonia line to heat and vaporize the liquid ammonia, a heat exchanger 55 capable of exchanging heat between the hot water in the hot water line and a medium, a heat exchange amount adjuster 56 capable of adjusting the amount of heat exchange between the hot water and the medium to adjust the temperature of the hot water flowing into the vaporizer, and a gaseous ammonia line 46 capable of guiding gaseous ammonia that is ammonia vaporized by the vaporizer, to the gas turbine.SELECTED DRAWING: Figure 1

Description

[Technical field]

[0001] The present disclosure relates to a gas turbine plant and a fuel supply method therefor. [Background technology]

[0002] A gas turbine plant includes a gas turbine and a fuel supply facility that supplies fuel to the gas turbine.

[0003] In a gas turbine plant described in the following Patent Document 1, ammonia is supplied as fuel to a gas turbine. This gas turbine plant is equipped with a fuel supply facility that supplies ammonia as fuel to the gas turbine, and also with a heat recovery boiler that generates steam by utilizing the heat of exhaust gas from the gas turbine.

[0004] The fuel supply facility includes an ammonia tank for storing liquid ammonia, a liquid ammonia line connected to the ammonia tank, a hot water line through which hot water can flow, a vaporizer, a flow rate control valve for controlling the flow rate of the hot water flowing into the vaporizer, and a gaseous ammonia line through which the gaseous ammonia is guided to the gas turbine. The vaporizer is connected to an end of the liquid ammonia line. The vaporizer exchanges heat between the hot water from the hot water line and the liquid ammonia from the liquid ammonia line to heat and vaporize the liquid ammonia.

[0005] The vaporizer has a heat transfer tube through which ammonia flows and a vaporizer casing that covers the heat transfer tube and temporarily stores hot water. The hot water line is disposed in the heat recovery boiler and has a hot water heater that exchanges heat between the hot water and the exhaust gas to heat the hot water, a high-temperature water line that introduces high-temperature water heated by the hot water heater into the vaporizer casing, and a low-temperature water line that connects the vaporizer casing and the hot water heater. The flow rate control valve is provided in the high-temperature water line.

[0006] In this fuel supply system, the flow rate of the hot water flowing into the vaporizer casing is adjusted by a flow control valve to maintain the temperature of the hot water in the vaporizer casing within a target temperature range. Heat is exchanged between the hot water in the vaporizer casing and the liquid ammonia flowing in the heat transfer tube. [Prior art documents] [Patent documents]

[0007] [Patent Document 1] Patent No. 6245404 Summary of the Invention [Problem to be solved by the invention]

[0008] The temperature of the exhaust gas flowing through the heat recovery boiler changes with changes in the operating conditions of the gas turbine. Therefore, in the technology described in Patent Document 1, even if the flow rate of the hot water flowing into the vaporizer casing is changed in an environment in which the temperature of the exhaust gas changes, the amount of heat exchanged between the liquid ammonia and the hot water is not proportional to the flow rate of the hot water, and it is difficult to control this amount of heat exchange. Therefore, it is considered that the technology described in Patent Document 1 may not be able to ensure the required amount of gaseous ammonia produced.

[0009] Therefore, an object of the present disclosure is to provide a technique that can easily produce the amount of gaseous ammonia required by a gas turbine. [Means for solving the problem]

[0010] A gas turbine plant as one embodiment for achieving the above object comprises: The present invention includes a gas turbine that burns a fuel and can be driven by a combustion gas generated by the combustion of the fuel, a heat recovery boiler that can generate steam by utilizing the heat of exhaust gas from the gas turbine, and a fuel supply facility that can supply ammonia as the fuel to the gas turbine. The fuel supply facility includes a liquid ammonia line connected to an ammonia tank that can store liquid ammonia, a hot water line through which hot water can flow, a vaporizer that is connected to an end of the liquid ammonia line and can heat exchange the hot water from the hot water line with the liquid ammonia to heat and vaporize the liquid ammonia, a heat exchanger that can exchange heat between the hot water in the hot water line and a medium, a heat exchange amount regulator that can adjust the amount of heat exchange between the hot water and the medium to adjust the temperature of the hot water flowing into the vaporizer, and a gaseous ammonia line that can guide gaseous ammonia, which is the ammonia vaporized in the vaporizer, to the gas turbine. The vaporizer has an ammonia inlet, an ammonia outlet, a hot water inlet, and a hot water outlet. The liquid ammonia line is connected to the ammonia inlet of the vaporizer. The gaseous ammonia line is connected to the ammonia outlet of the vaporizer. The hot water line is disposed in the heat recovery boiler and includes a hot water heater that heats hot water by exchanging heat between hot water and the exhaust gas, and a high-temperature water line that connects the hot water heater and the hot water inlet of the vaporizer. The heat exchanger is provided in the high-temperature water line.

[0011] In this aspect, the hot water heated by the heat exchange between the hot water and the exhaust gas in the hot water heater flows into the vaporizer after being temperature-adjusted. In this vaporizer, the temperature-adjusted hot water exchanges heat with liquid ammonia, and the ammonia vaporizes. However, since the exhaust gas temperature at the gas turbine outlet changes due to a change in the operating conditions of the gas turbine, the temperature at the hot water heater inlet in the heat recovery boiler changes depending on the operating conditions of the gas turbine. Therefore, when the temperature of the exhaust gas changes, the temperature of the hot water heated by the hot water heater also changes. However, in this aspect, as described above, the hot water heated by the hot water heater flows into the vaporizer after being temperature-adjusted. Therefore, in this aspect, even if the temperature of the exhaust gas changes, all of the liquid ammonia flowing into the vaporizer can be easily converted into gaseous ammonia.

[0012] In addition, the amount of gaseous ammonia required by the gas turbine also changes due to changes in the operating conditions of the gas turbine. In this aspect, even if the amount of gaseous ammonia required by the gas turbine changes, all of the liquid ammonia that has flowed into the vaporizer can be easily converted into gaseous ammonia by changing the temperature of the hot water that flows into the vaporizer.

[0013] Therefore, in this aspect, even if the operating conditions of the gas turbine change, the production amount of gaseous ammonia required by the gas turbine can be easily obtained. Also, in this aspect, the responsiveness of the production amount of gaseous ammonia to the change in the operating conditions of the gas turbine can be improved.

[0014] As one aspect of a fuel supply method for a gas turbine plant to achieve the above object, A fuel supply method for a gas turbine plant including a gas turbine that burns fuel and can be driven by combustion gas generated by the combustion of the fuel, and a heat recovery boiler that can generate steam by utilizing heat of exhaust gas from the gas turbine, the method includes the steps of: heating the hot water by heat exchange between hot water in a hot water heater arranged in the heat recovery boiler and the exhaust gas in the heat recovery boiler and outside the hot water heater; heat exchange process for heat exchange between the hot water heated in the hot water heating process and a medium; heat exchange amount adjustment process for adjusting an amount of heat exchange between the hot water heated in the hot water heating process and the medium; a vaporization process for vaporizing the liquid ammonia by heat exchange between the hot water after the amount of heat exchange with the medium has been adjusted in the heat exchange amount adjustment process in a vaporizer, and liquid ammonia from an ammonia tank that stores liquid ammonia; and a fuel supply process for supplying gaseous ammonia, which is the ammonia vaporized in the vaporization process, to the gas turbine as fuel. In the heat exchange amount adjusting step, the amount of heat exchanged between the hot water and the medium in the heat exchanging step is adjusted, thereby adjusting the temperature of the hot water flowing into the evaporator.

[0015] In this embodiment, similarly to the one embodiment of the gas turbine plan, even if the operating conditions of the gas turbine change, the production amount of gaseous ammonia required by the gas turbine can be easily obtained. Also in this embodiment, the responsiveness of the production amount of gaseous ammonia to the change in the operating conditions of the gas turbine can be improved. Effect of the Invention

[0016] In one aspect of the present disclosure, the production of gaseous ammonia required by a gas turbine can be obtained. [Brief description of the drawings]

[0017] [Figure 1] FIG. 1 is a system diagram of a gas turbine plant in a first embodiment according to the present disclosure. [Diagram 2] FIG. 2 is a functional block diagram of a control device in the first embodiment of the present disclosure. [Diagram 3]5 is a graph showing a relationship between a fuel flow rate and a target temperature in the first embodiment of the present disclosure. [Figure 4] 4 is a flowchart showing the procedure of a fuel supply method in the first embodiment according to the present disclosure. [Diagram 5] FIG. 4 is a system diagram of a gas turbine plant in a second embodiment according to the present disclosure. [Figure 6] 10 is a flowchart showing a procedure of a fuel supply method according to a second embodiment of the present disclosure. [Figure 7] FIG. 11 is a functional block diagram of a control device in a modified example according to the present disclosure. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0018] Hereinafter, various embodiments and modifications according to the present disclosure will be described with reference to the drawings.

[0019] "First embodiment" Hereinafter, a first embodiment of a gas turbine plant according to the present disclosure will be described with reference to FIGS. 1 to 4. FIG.

[0020] 1, the gas turbine plant of this embodiment includes a gas turbine 10, a denitration device 20 that decomposes NOx contained in exhaust gas from the gas turbine 10, a heat recovery boiler 21 that generates steam by utilizing heat of the exhaust gas flowing out from the denitration device 20, a chimney 22 that exhausts exhaust gas from the heat recovery boiler 21 to the outside, a steam turbine 23 that is driven by steam from the heat recovery boiler 21, a condenser 24 that converts the steam from the steam turbine 23 back into water, a pump 25 that sends the water in the condenser 24 to the heat recovery boiler 21, a fuel supply facility 40 that supplies fuel to the gas turbine 10, and a control device 60. Thus, the gas turbine plant of this embodiment is a combined cycle plant.

[0021] The gas turbine 10 includes a compressor 14 that compresses air A, a combustor 15 that burns fuel in the air compressed by the compressor 14 to generate combustion gas, and a turbine 16 that is driven by the high-temperature, high-pressure combustion gas.

[0022] The compressor 14 has a compressor rotor 14r rotating about a rotor axis Ar, a compressor casing 14c covering the compressor rotor 14r, and an intake air regulator (hereinafter, referred to as an inlet guide vane (IGV)) 14i provided at the intake port of the compressor casing 14c. The IGV 14i adjusts the flow rate of air sucked into the compressor casing 14c according to an instruction from a control device 60. The turbine 16 has a turbine rotor 16r rotating about a rotor axis Ar by combustion gas from the combustor 15, and a turbine casing 16c covering the turbine rotor 16r. The turbine rotor 16r and the compressor rotor 14r are connected to each other so as to be rotatable about the same rotor axis Ar, forming a gas turbine rotor 11. For example, a rotor of a generator is connected to the gas turbine rotor 11.

[0023] The gas turbine 10 further includes an intermediate casing 12. The intermediate casing 12 is disposed between the compressor casing 14c and the turbine casing 16c in the direction in which the rotor axis Ar extends, and connects the compressor casing 14c and the turbine casing 16c. Compressed air discharged from the compressor 14 flows into the intermediate casing 12. A combustor 15 is fixed to the intermediate casing 12.

[0024] Ammonia is supplied to the denitration device 20. The denitration device 20 uses the ammonia to decompose NOx contained in the exhaust gas from the gas turbine 10 into nitrogen and water vapor.

[0025] The exhaust heat recovery boiler 21 has a boiler casing 21c through which the exhaust gas from the denitrification device 20 flows, an economizer 21eco, an evaporator 21eva, and a superheater 21s. The economizer 21eco, the evaporator 21eva, and the superheater 21s are arranged in this order from downstream to upstream in the flow of the exhaust gas flowing in the boiler casing 21c. The economizer 21eco, the evaporator 21eva, and the superheater 21s have heat transfer tubes that exchange heat between the exhaust gas flowing in the boiler casing 21c and water or steam. The economizer 21eco exchanges heat between the exhaust gas flowing in the boiler casing 21c and water, heating the water and generating hot water. The evaporator 21eva exchanges heat between the exhaust gas flowing in the boiler casing 21c and the hot water from the economizer 21eco to heat the hot water and generate steam. The superheater 21s exchanges heat between the exhaust gas flowing in the boiler casing 21c and the steam from the evaporator 21eva to heat the steam and generate superheated steam.

[0026] The economizer 21eco of the heat recovery boiler 21 and the condenser 24 are connected by a water supply line 26. A pump 25 is provided on this water supply line 26 to send water in the condenser 24 to the heat recovery boiler 21. The superheater 21s of the heat recovery boiler 21 and the steam turbine 23 are connected by a main steam line 27. Superheated steam from the heat recovery boiler 21 is sent to the steam turbine 23 via the main steam line 27. A rotor of a generator, for example, is connected to the rotor of the steam turbine 23. Steam exhausted from the steam turbine 23 is returned to water by the condenser 24.

[0027] The denitration device 20 is disposed, for example, in a position around the evaporator 21eva in the boiler casing 21c. Ammonia is supplied to the denitration device 20. The denitration device 20 uses the ammonia to decompose NOx contained in the exhaust gas from the gas turbine 10 into nitrogen and water vapor.

[0028] The fuel supply equipment 40 includes an ammonia tank 41, a liquid ammonia line 42, a liquid ammonia control valve 43a, a fuel control valve 43b, an ammonia pump 44, a vaporizer 45, a gaseous ammonia line 46, a hot water line 50, a hot water pump 54, a heat exchanger 55, a heat exchange amount regulator 56, a medium line 58i, a medium recovery line 58o, and a medium flow rate regulator 59.

[0029] Liquid ammonia is stored in the ammonia tank 41. One end of a liquid ammonia line 42 is connected to this ammonia tank 41. This liquid ammonia line 42 is provided with an ammonia pump 44 that pressurizes the liquid ammonia from the ammonia tank 41, and a liquid ammonia control valve 43a that controls the flow rate of the liquid ammonia flowing through the liquid ammonia line 42.

[0030] The vaporizer 45 is a heat exchanger that exchanges heat between hot water and liquid ammonia to heat and vaporize the liquid ammonia. The vaporizer 45 has a heat transfer tube 45p through which the hot water flows, and a vaporizer casing 45c that covers the heat transfer tube 45p and temporarily stores the liquid ammonia. One end of the heat transfer tube 45p forms a hot water inlet 45pi, and the other end of the heat transfer tube 45p forms a hot water outlet 45po. The vaporizer casing 45c has an ammonia inlet 45ci and an ammonia outlet 45co. The other end of the liquid ammonia line 42 is connected to the ammonia inlet 45ci of the vaporizer 45. One end of a gaseous ammonia line 46 is connected to the ammonia outlet 45co of the vaporizer 45. The other end of the gaseous ammonia line 46 is connected to the combustor 15. This gaseous ammonia line 46 is provided with a fuel regulating valve 43b that regulates the flow rate of gaseous ammonia as fuel flowing into the combustor 15.

[0031] The hot water line 50 includes a low-temperature water line 51, a hot water heater 52, and a high-temperature water line 53. The hot water heater 52 is disposed in the boiler casing 21c at a position downstream of the exhaust gas flow from the economizer 21eco. The low-temperature water line 51 connects the hot water outlet 45po of the vaporizer 45 to the hot water heater 52. A hot water pump 54 is provided in the low-temperature water line 51. The high-temperature water line 53 includes a main high-temperature water line 53x that connects the hot water heater 52 to the hot water inlet 45pi of the vaporizer 45, and a branch high-temperature water line 53y that branches off from the main high-temperature water line 53x and is then connected to the main high-temperature water line 53x.

[0032] The hot water line 50 and the heat transfer tube 45p of the vaporizer 45 form a hot water circulation line through which hot water circulates. The flow rate of the hot water circulating in this hot water circulation line is controlled by a hot water pump 54 and is kept approximately constant.

[0033] The heat exchanger 55 exchanges heat between a medium such as cooling water and hot water. The heat exchanger 55 has a heat transfer tube 55p through which the medium flows, and a heat exchanger casing 55c that covers the heat transfer tube 55p and temporarily stores the hot water. One end of the heat transfer tube 55p forms a medium inlet 55pi, and the other end of the heat transfer tube 55p forms a medium outlet 55po. A medium line 58i is connected to the medium inlet 55pi. A medium flow rate regulator 59 that regulates the flow rate of the medium flowing through the medium line 58i is provided on the medium line 58i. A medium recovery line 58o is connected to the medium outlet 55po. The heat exchanger casing 55c is provided on the branch high-temperature water line 53y. Therefore, high-temperature water from the branch high-temperature water line 53y flows into the heat exchanger casing 55c. The medium that flows into the heat exchanger 55 may be a liquid such as river water, seawater, or industrial water, or a gas such as air.

[0034] The heat exchange amount adjuster 56 has a three-way valve 57 as a flow rate ratio adjuster that adjusts the ratio between the flow rate of hot water flowing in the main high-temperature water line 53x between the branch position of the branch high-temperature water line 53y and the connection position of the branch high-temperature water line 53y, and the flow rate of hot water flowing in the branch high-temperature water line 53y. This three-way valve 57 is provided at the connection position of the main high-temperature water line 53x and the branch high-temperature water line 53y. Note that the flow rate ratio adjuster may be composed of a main high-temperature water control valve provided in the main high-temperature water line 53x between the branch position of the branch high-temperature water line 53y and the connection position of the branch high-temperature water line 53y, and a branch high-temperature water control valve provided in the branch high-temperature water line 53y, instead of the three-way valve 57.

[0035] A thermometer 48 for detecting the temperature of the high-temperature water flowing between the three-way valve 57 and the vaporizer 45 in the main high-temperature water line 53x is provided. A pressure gauge 49 for detecting the pressure of the gaseous ammonia flowing through this line is provided in the gaseous ammonia line 46.

[0036] As shown in FIG. 2, the control device 60 has a fuel flow rate calculation unit 61, a fuel valve control unit 62, an IGV control unit 63, a temperature control system 65, and a pressure control system .

[0037] The fuel flow rate calculation unit 61 receives a required output PWr for the gas turbine 10 from the outside. The fuel flow rate calculation unit 61 calculates a fuel flow rate according to the required output PWr, and outputs a fuel flow rate command Fro indicating this fuel flow rate. The fuel flow rate calculated by the fuel flow rate calculation unit 61 has a positive correlation with the required output PWr. That is, as the required output PWr increases, the fuel flow rate calculated by the fuel flow rate calculation unit 61 also increases.

[0038] The fuel valve control unit 62 controls the opening degree of the fuel regulating valve 43b in response to the fuel flow command Fro. The IGV control unit 63 controls the opening degree of the IGV 14i in response to the fuel flow command Fro. Specifically, the IGV control unit 63 controls the IGV opening degree so that the IGV opening degree has a positive correlation with the fuel flow rate indicated by the fuel flow command Fro. The liquid ammonia regulating valve 43a changes its valve opening degree in response to the amount of liquid ammonia in the vaporizer casing 45c. Specifically, when the amount of liquid ammonia in the vaporizer casing 45c decreases, the liquid ammonia regulating valve 43a opens to replenish the liquid ammonia.

[0039] The temperature control system 65 has a target temperature calculator 66 , a temperature deviation calculator 67 , and a PI controller 68 .

[0040] As shown in Fig. 3, the target temperature calculator 66 has a function F1 that indicates the relationship between the fuel flow rate indicated by the fuel flow rate command Fro and the target temperature of the hot water. This function F1 indicates a relationship in which the target temperature increases as the fuel flow rate increases. The target temperature calculator 66 uses this function F1 to find the target temperature of the hot water for the fuel flow rate indicated by the fuel flow rate command Fro.

[0041] Temperature deviation calculator 67 calculates deviation ΔT between the target temperature and the temperature detected by thermometer 48. Specifically, temperature deviation calculator 67 subtracts the temperature detected by thermometer 48 from the target temperature, and outputs this value as temperature deviation ΔT. PI controller 68 calculates an opening correction amount for proportional and integral action corresponding to the temperature deviation ΔT, and outputs a valve command corresponding to this opening correction amount to three-way valve 57.

[0042] 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 judger 74a, an upper limit deviation judger 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 the PI controller 68. The functions of the above elements of the pressure control system 70 will be described in the process of describing the operation of the pressure control system 70.

[0043] The control device 60 described above is a computer. In terms of hardware, the control device 60 has a CPU (Central Processing Unit) that performs various calculations, a main storage device such as a memory that serves as a work area for the CPU, an auxiliary storage device such as a hard disk drive device, an input device such as a keyboard or a mouse, and a display device. Each functional unit in the control device 60, such as the fuel flow rate calculation unit 61, the fuel valve control unit 62, the IGV control unit 63, the temperature control system 65, and the pressure control system 70, functions by, for example, the CPU executing a control program stored in the auxiliary storage device.

[0044] Next, the fuel supply method for the gas turbine plant described above will be described with reference to the flowchart shown in FIG.

[0045] The fuel supply method of this embodiment executes a hot water heating step S1, a heat exchange amount adjustment step S2, a heat exchange step S3, a temperature control step S4, a vaporization step S6, a low-temperature water recovery step S7, and a fuel supply step S8. In addition, this fuel supply method also executes a pressure control step S5 in response to a request from an operator.

[0046] In the hot water heating step S1, hot water in the hot water heater 52 arranged in the boiler casing 21c is heat exchanged with exhaust gas in the boiler casing 21c and outside the hot water heater 52, thereby heating the hot water. In this hot water heating step S1, for example, hot water (low temperature water) of about 60°C is heated to hot water (high temperature water) of about 90°C. This high temperature water flows from the hot water heater 52 into the main high temperature water line 53x.

[0047] In the heat exchange amount adjustment process S2, 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 is adjusted to adjust the temperature of the high-temperature water flowing into the vaporizer 45. This heat exchange amount adjustment process S2 includes a flow division process S2a and a flow rate ratio adjustment process S2b. In the flow division process S2a of the heat exchange amount adjustment process S2, a part of the high-temperature water flowing through the main high-temperature water line 53x is caused to flow into the branch high-temperature water line 53y, while the remaining high-temperature water is caused to flow in the main high-temperature water line 53x downstream of the branch position with the branch high-temperature water line 53y. That is, in this flow division process S2a, the high-temperature water flowing through the main high-temperature water line 53x is divided into the branch high-temperature water flowing through the branch high-temperature water line 53y and the main high-temperature water flowing through the main high-temperature water line 53x. The flow rate ratio adjustment process S2b of the heat exchange amount adjustment process S2 will be described later.

[0048] In the heat exchange step S3, the heat exchanger 55 provided in the branch high-temperature water line 53y exchanges heat between the branch high-temperature water and a medium flowing into the heat exchanger 55. Here, when the medium flowing into the heat exchanger 55 is cooling water as described above, the temperature of the branch high-temperature water decreases.

[0049] In the temperature control step S4, a required output PWr of the gas turbine 10 is received, and the heat exchange amount in the heat exchange amount adjustment step S2 is controlled according to the required output PWr. The temperature control system 65 of the control device 60 executes this temperature control step S4.

[0050] Here, the operation of the control device 60 will be described with reference to FIG.

[0051] As described above, the fuel flow rate calculation unit 61 of the control device 60 receives the required output PWr for the gas turbine 10 from the outside. The fuel flow rate calculation unit 61 calculates a fuel flow rate according to the required output PWr, and outputs a fuel flow rate command Fro indicating this fuel flow rate. Note that the flow rate here is a mass flow rate.

[0052] The fuel valve control unit 62 controls the opening degree of the fuel regulating valve 43b so that the mass flow rate of the fuel passing through the fuel regulating valve 43b becomes the fuel flow rate indicated by the fuel flow rate command Fro. As a result, the mass flow rate of ammonia as fuel flowing from the gaseous ammonia line 46 into the combustor 15 becomes the fuel flow rate indicated by the fuel flow rate command Fro. The IGV control unit 63 controls the IGV opening degree so that the flow rate of air flowing into the compressor casing 14c becomes the flow rate corresponding to the fuel flow rate indicated by the fuel flow rate command Fro.

[0053] As described above, the target temperature calculator 66 of the temperature control system 65 uses the function F1 to obtain the target temperature of the hot water for the fuel flow rate indicated by the fuel flow rate 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 this value as the temperature deviation ΔT.

[0054] The PI controller 68 of the temperature control system 65 calculates an opening correction amount for the proportional and integral action corresponding to the temperature deviation ΔT, and outputs an action amount corresponding to this opening correction amount to the three-way valve 57 as a valve command.

[0055] The operation of the three-way valve 57 is controlled by the operation of the temperature control system 65 described above, and the amount of heat exchange in the heat exchange amount adjustment step S2 is thereby adjusted.

[0056] As described above, the pressure control step S5 is executed when an operator or the like desires to correct the pressure. The pressure control system 70 of the control device 60 executes this pressure control step S5.

[0057] The pressure correction mode button 71 of the pressure control system 70 accepts whether or not the operator, etc., desires pressure correction. When the operator, etc. desires pressure correction and presses the pressure correction mode button 71, the pressure correction mode button 71 outputs an ON signal, and the control device 60 enters the pressure correction mode.

[0058] The lower limit value memory 72a stores a pressure lower limit value Pa of the fuel (gaseous ammonia) flowing into the combustor 15. The upper limit value memory 72b stores a pressure upper limit value Pb of the fuel (gaseous ammonia) flowing into the combustor 15.

[0059] The lower limit deviation calculator 73a of the pressure control system 70 calculates a deviation ΔPat between the pressure lower 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 pressure lower 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 a deviation ΔPbt between the pressure upper 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 pressure upper limit value Pb, and outputs this value as the upper limit deviation ΔPbt.

[0060] A lower limit deviation determiner 74a of the pressure control system 70 determines whether the lower limit deviation ΔPat is a positive value or not, in other words, whether the pressure detected by the pressure gauge 49 is smaller than the pressure lower limit value Pa or not, and outputs a result to that effect. An upper limit deviation determiner 74b of the pressure control system 70 determines whether the upper limit deviation ΔPbt is a negative value or not, in other words, whether the pressure detected by the pressure gauge 49 is larger than the pressure upper limit value Pb or not, and outputs a result to that effect.

[0061] When the lower limit deviation ΔPat is a positive value and the lower limit correction indicator 75a of the pressure control system 70 receives an ON signal from the pressure correction mode button 71, it outputs an ONa signal indicating that temperature correction based on the pressure lower limit value Pa is to be performed. On the other hand, when the lower limit deviation ΔPat is not a positive value or the lower limit correction indicator 75a does not receive an ON signal from the pressure correction mode button 71, it outputs an OFFa signal indicating that temperature correction based on the pressure lower limit value Pa is not to be performed. When the upper limit deviation ΔPbt is a negative value and the upper limit correction indicator 75b of the pressure control system 70 receives an ON signal from the pressure correction mode button 71, it outputs an ONb signal indicating that temperature correction based on the pressure upper limit value Pb is to be performed. On the other hand, when the upper limit deviation ΔPbt is not a negative value or the upper limit correction indicator 75b does not receive an ON signal from the pressure correction mode button 71, it outputs an OFFb signal indicating that temperature correction based on the pressure upper limit value Pb is not to be performed.

[0062] The fuel flow command Fro and the lower limit deviation ΔPat are input to a 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 determine a lower limit correction value Ca according to the fuel flow Fr indicated 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 pressure lower limit value Pa. In addition, this lower limit correction value Ca is a positive value. Fa:Ca=k×ΔPat / Fr In the above formula, k is a correction coefficient.

[0063] 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 determine the upper limit correction value Cb according to the fuel flow Fr indicated 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. Moreover, this upper limit correction value Cb is a negative value. Fb:Cb=k×ΔPbt / Fr In the above formula, k is a correction coefficient.

[0064] When the first switch 78a of the pressure control system 70 receives an 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. On the other hand, when the first switch 78a does not receive an 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 an 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. On the other hand, when the second switch 78b does not receive an ONb signal from the upper limit correction indicator 75b, it outputs 0 as the upper limit correction value.

[0065] 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.

[0066] The PI controller 68 of the pressure control system 70 calculates an opening correction amount for the proportional and integral action corresponding to (temperature deviation ΔT + lower limit correction value Ca) or (temperature deviation ΔT + upper limit correction value Cb), and outputs a valve command corresponding to this opening correction amount to the three-way valve 57.

[0067] The operation of the three-way valve 57 is controlled by the operation of the temperature control system 65 described above, and the heat exchange amount in the heat exchange amount adjustment process S2 is controlled so that the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within a predetermined pressure range.

[0068] The flow rate ratio adjustment step S2b of the heat exchange amount adjustment step S2 is performed by the three-way valve 57, which is the heat exchange amount adjuster 56. The three-way valve 57 adjusts the flow rate ratio between the main high temperature water and the branch high temperature water after heat exchange in the heat exchange step S3 in response to an instruction from the temperature control system 65, and merges the main high temperature water and the branch high temperature water after heat exchange in the heat exchange step S3. As a result, the high temperature water after the merging is adjusted to a temperature sufficient for vaporizing the 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 hot water flowing into the vaporizer 45 is adjusted to about 90°C to 60°C.

[0069] Furthermore, when the three-way valve 57 receives an instruction from the pressure control system 70, it also adjusts the flow rate ratio between the main high temperature water and the branch high temperature water after heat exchange in the heat exchange process S3 in response to this instruction to merge the main high temperature water and the branch high temperature water after heat exchange in the heat exchange process S3. As a result, the high temperature water after the merging is at a temperature sufficient to vaporize the liquid ammonia in the vaporizer 45, and is adjusted so that the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within a predetermined pressure range.

[0070] In the vaporization step S6, the liquid ammonia is vaporized by heat exchange between the hot water, the amount of heat exchange with the medium of which has been adjusted in the heat exchange amount adjustment step S2, and the liquid ammonia in the vaporizer 45.

[0071] In the low-temperature water recovery step S7, the hot water cooled by heat exchange with liquid ammonia in the vaporizer 45 is returned to the hot water heater 52 via the low-temperature water line 51. The hot water returned to the hot water heater 52 is heated by the exhaust gas here. That is, in this hot water heater 52, the above-mentioned hot water heating step S1 is executed.

[0072] In the fuel supply step S8, gaseous ammonia, which is the ammonia vaporized in the vaporizer 45, is supplied to the combustor 15 of the gas turbine 10 via a gaseous ammonia line 46.

[0073] As described above, in this embodiment, the hot water heated by the heat exchange between the hot water and the exhaust gas in the hot water heater 52 flows into the vaporizer 45 after being temperature-adjusted. In this vaporizer 45, the temperature-adjusted hot water exchanges heat with liquid ammonia, and the ammonia vaporizes. Incidentally, the temperature of the exhaust gas flowing through the exhaust heat recovery boiler 21 changes due to changes in the operating conditions of the gas turbine 10. Therefore, when the temperature of the exhaust gas changes, the temperature of the hot water heated by the hot water heater 52 also changes. However, in this embodiment, as described above, the hot water heated by the hot water heater 52 flows into the vaporizer 45 after being temperature-adjusted. Therefore, in this embodiment, even if the temperature of the exhaust gas changes, all of the liquid ammonia flowing into the vaporizer 45 can be easily and reliably converted into gaseous ammonia.

[0074] Furthermore, the amount of gaseous ammonia required by the gas turbine 10 also changes due to changes in 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, by changing the temperature of the hot water flowing into the vaporizer 45, all of the liquid ammonia flowing into the vaporizer 45 can be easily and reliably converted into gaseous ammonia.

[0075] Therefore, in this embodiment, even if the operating conditions of the gas turbine 10 change, it is possible to easily and reliably obtain the production amount of gaseous ammonia required by the gas turbine 10. Also, in this embodiment, it is possible to improve the responsiveness of the production amount of gaseous ammonia to changes in the operating conditions of the gas turbine 10.

[0076] As described above, the flow rate of the fuel supplied to the gas turbine 10 changes according to the change in the required output PWr of the gas turbine 10. In this case, the amount of heat exchange between the fuel and the hot water in the vaporizer 45 changes with the change in the fuel flow rate. If the temperature of the hot water is adjusted according to the result of the change in the amount of heat exchange, it takes time from when the required output PWr changes to when the amount of gaseous ammonia is ensured. In this embodiment, the operation amount of the heat exchange amount regulator 56 is determined according to the required output PWr, so that it is possible to shorten the time from when the required output PWr changes to when the amount of gaseous ammonia is ensured. Therefore, in this embodiment, from the above viewpoint, it is possible to improve the responsiveness of the amount of gaseous ammonia produced to the change in the required output PWr.

[0077] Unless the pressure of the gaseous ammonia flowing into the gas turbine 10 is within a predetermined pressure range, the gaseous ammonia cannot be stably burned in the gas turbine 10. In this embodiment, the pressure control system 70 controls the pressure of the gaseous ammonia flowing into the gas turbine 10 to fall within the predetermined pressure range. Therefore, in this embodiment, the gaseous ammonia can be stably burned in the gas turbine 10.

[0078] Here, consider the case where liquid ammonia flows into heat transfer tube 45p of vaporizer 45, and hot water flows into vaporizer casing 45c covering heat transfer tube 45p. In this case, liquid ammonia becomes gaseous ammonia in heat transfer tube 45p, and gaseous ammonia accumulates in a part of heat transfer tube 45p. Therefore, the heat transfer area effective for heat exchange between liquid ammonia and hot water becomes smaller than the total heat transfer area of ​​heat transfer tube 45p. Moreover, in this case, the heat transfer area effective for heat exchange between liquid ammonia and hot water also changes with the change in the amount of gaseous ammonia produced. Therefore, in this case, it is difficult to control the amount of heat exchange between liquid ammonia and hot water, and it may not be possible to ensure the required amount of gaseous ammonia produced.

[0079] On the other hand, in this embodiment, hot water flows into the heat transfer tube 45p of the vaporizer 45, and liquid ammonia flows into the vaporizer casing 45c that covers the heat transfer tube 45p. Therefore, in this embodiment, the liquid ammonia in contact with the outer surface of the heat transfer tube 45p can be separated from the outer surface of the heat transfer tube 45p when vaporized. Therefore, in this embodiment, the heat transfer area effective for heat exchange between the liquid ammonia and the hot water can be made larger than the previous case with respect to the total heat transfer area of ​​the heat transfer tube 45p. Moreover, in this embodiment, the heat transfer area effective for heat exchange between the liquid ammonia and the hot water does not substantially change with respect to the change in the amount of gaseous ammonia produced. Therefore, in this embodiment, from this viewpoint, it is easy to control the amount of heat exchange between the liquid ammonia and the hot water, and the required amount of gaseous ammonia produced can be easily and reliably obtained.

[0080] In the boiler casing 21c, the temperature of the exhaust gas decreases toward the downstream side of the exhaust gas flow. In this embodiment, the hot water heater 52 is disposed downstream of the economizer 21eco, which is the most downstream heat transfer tube among the multiple heat transfer tubes, in the boiler casing 21c. Therefore, in this embodiment, the heat of the exhaust gas whose temperature has been reduced can be effectively utilized by the hot water heater 52.

[0081] Second Embodiment Next, a second embodiment of a gas turbine plant according to the present disclosure will be described with reference to FIGS.

[0082] 5, the gas turbine plant of this embodiment includes a gas turbine 10, a denitration device 20, a heat recovery steam generator 21, a chimney 22, a steam turbine 23, a condenser 24, a pump 25, and a control device 60, similar to the gas turbine plant of the first embodiment. Furthermore, the gas turbine plant of this embodiment includes a fuel supply facility 40a different from the fuel supply facility 40 of the first embodiment.

[0083] The fuel supply equipment 40a of this embodiment, like the fuel supply equipment 40 of the first embodiment, includes an ammonia tank 41, a liquid ammonia line 42, a liquid ammonia control valve 43a, a fuel control valve 43b, an ammonia pump 44, a vaporizer 45, a gaseous ammonia line 46, a hot water pump 54, a heat exchanger 55, a medium line 58i, a medium recovery line 58o, and a medium flow rate regulator 59. Furthermore, the fuel supply equipment 40a of this embodiment includes a hot water line 50a different from the hot water line 50 of the first embodiment, and a heat exchange amount regulator 56a different from the heat exchange amount regulator 56 of the first embodiment.

[0084] The hot water line 50a of this embodiment has a low-temperature water line 51 and a hot water heater 52, similar to the hot water line 50 of the first embodiment. Furthermore, the hot water line 50a of this embodiment has a high-temperature water line 53a different from the high-temperature water line 53 of the first embodiment. The high-temperature water line 53 of the first embodiment has a branch high-temperature water line 53y, but the high-temperature water line 53a of this embodiment does not have this branch high-temperature water line 53y.

[0085] The heat exchanger 55 of this embodiment is provided in this high-temperature water line 53a. Therefore, all of the high-temperature water from the hot water heater 52 flows into the heat exchanger 55 via the high-temperature water line 53a. A medium flow rate regulator 59 is provided in the medium line 58i connected to this heat exchanger 55, as in the first embodiment. The heat exchange amount regulator 56a of this embodiment has this medium flow rate regulator 59.

[0086] The control device 60 of the present embodiment controls the operation of this medium flow rate regulator 59 when regulating the temperature of the hot water.

[0087] Next, a fuel supply method for the gas turbine plant in this embodiment will be described with reference to the flowchart shown in FIG.

[0088] In the fuel supply method of this embodiment, similar to the fuel supply method of the first embodiment, a hot water heating step S1, a heat exchange step S3, a pressure control step S5, a temperature control step S4, a vaporization step S6, a low-temperature water recovery step S7, and a fuel supply step S8 are executed. Also, in the fuel supply method of this embodiment, similar to the fuel supply method of the first embodiment, a pressure control step S5 is also executed in response to a request from an operator. Furthermore, in the fuel supply method of this embodiment, a heat exchange amount adjustment step S2X different from the heat exchange amount adjustment step S2 of the first embodiment is executed.

[0089] In the heat exchange amount adjusting step S2X of this embodiment, similarly to the heat exchange amount adjusting step S2 of the first embodiment, the heat exchange amount between the high-temperature water from the hot water heater 52 and the medium flowing into the heat exchanger 55 is adjusted to adjust the temperature of the high-temperature water flowing into the evaporator 45. However, the method of adjusting the heat exchange amount in the heat exchange amount adjusting step S2X of this embodiment is different from the method of adjusting the heat exchange amount in the heat exchange amount adjusting step S2 of the first embodiment. The heat exchange amount adjusting step S2X of this embodiment includes a medium flow rate adjusting step S2c.

[0090] In the medium flow rate adjustment step S2c, the medium flow rate adjuster 59 serving as the heat exchange amount adjuster 56a operates based on an 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 adjusted. As a result, the amount of heat exchange between the medium and the high-temperature water in the heat exchanger 55 is adjusted, and the temperature of the high-temperature water flowing into the vaporizer 45 is adjusted.

[0091] The PI controller 68 of the temperature control system 65 in this embodiment determines an opening correction amount for proportional and integral action corresponding to the temperature deviation ΔT, and outputs an operation amount corresponding to this opening correction amount to the medium flow regulator 59. The PI controller 68 of the pressure control system 70 in this embodiment determines an opening correction amount for proportional and integral action corresponding to (temperature deviation ΔT+lower limit correction value Ca) or (temperature deviation ΔT+upper limit correction value Cb), and outputs an operation amount corresponding to this opening correction amount to the medium flow regulator 59.

[0092] In this manner, the operation of the medium flow rate regulator 59 is controlled by the operation of the temperature control system 65 or the pressure control system 70, whereby the amount of heat exchange in the heat exchange amount adjusting step S2X is controlled.

[0093] As described above, in this embodiment as well, the hot water heated by the hot water heater 52 flows into the vaporizer 45 after being temperature-adjusted, so that it is possible to easily obtain the amount of gaseous ammonia produced that the gas turbine 10 requires, even if the operating conditions of the gas turbine 10 change. Furthermore, in this embodiment, it is possible to improve the responsiveness of the amount of gaseous ammonia produced to changes in the operating conditions of the gas turbine 10.

[0094] Furthermore, since the high-temperature water line 53a of this embodiment does not have the branch high-temperature water line 53y, the line configuration is simpler than that of the gas turbine plant of the first embodiment, and the equipment costs can be reduced.

[0095] The heat exchange amount adjuster 56 of the first embodiment may have a medium flow rate adjuster 59 in addition to the three-way valve 57, similarly to the present embodiment.

[0096] "Modification of the control device" Next, a modified example of the control device described above will be described with reference to Fig. 7. The control device 60 of each of the above embodiments can be set to a pressure correction mode. The control device 60a of this modified example can also be set to a pressure lower limit control mode and a pressure upper limit control mode in addition to the pressure correction mode.

[0097] Like the control device 60 of each of the above embodiments, the control device 60a of this modification has a fuel flow rate calculation unit 61, a fuel valve control unit 62, and an IGV control unit 63. Furthermore, the control device 60a of this modification has a temperature control system 65a different from the temperature control system 65 of each of the above embodiments, and a pressure control system 70a different from the pressure control system 70 of each of the above embodiments.

[0098] Similar to the temperature control system 65 of each of 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 has a PI control / switcher 68a having the same function as the PI controller 68 of each of the above embodiments.

[0099] Similar to the temperature control system 65 of each of the above-described embodiments, the temperature control system 65a of this modified example calculates an opening correction amount for proportional and integral action corresponding to the deviation temperature ΔT between the target temperature and the temperature detected by the thermometer 48, and outputs the opening correction amount to the three-way valve 57 or medium flow rate regulator 59 as the heat exchange amount regulator 56, 56a according to the opening correction amount.

[0100] The pressure control system 70a of this modification has 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 judger 74a, an upper limit deviation judger 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, like the pressure control system 70 of each of the above embodiments. The pressure control system 70a of this modification further has a PI control / switch 68a. The pressure control system 70a and the temperature control system 65a share this PI control / switch 68a.

[0101] The pressure control system 70a of this modified example further 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.

[0102] The lower limit control mode button 71a accepts whether or not the operator, etc. desires lower limit pressure control. When the operator, etc. desires lower limit pressure control and presses the lower limit control mode button 71a, the lower limit control mode button 71a outputs an ON signal, and the control device 60a enters the lower limit pressure control mode. The upper limit control mode button 71b accepts whether or not the operator, etc. desires upper limit pressure control. When the operator, etc. desires upper limit pressure control and presses the upper limit control mode button 71b, the upper limit control mode button 71b outputs an ON signal, and the control device 60a enters the upper limit pressure control mode.

[0103] When the lower limit deviation ΔPat calculated by the lower limit deviation calculator 73a is a positive value and the lower limit control indicator 76a receives an ON signal from the lower limit control mode button 71a, the lower limit control indicator 76a outputs an ONac signal indicating that temperature control based on the pressure lower limit value Pa is to be executed. On the other hand, when the lower limit deviation ΔPat is not a positive value or the lower limit control indicator 76a does not receive an ON signal 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 pressure lower limit value Pa is not to be executed. When the upper limit deviation ΔPbt calculated by the upper limit deviation calculator 73b is a negative value and the upper limit control indicator 76b receives an ON signal 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 pressure upper limit value Pb is to be executed. On the other hand, when the upper limit deviation ΔPbt is not a negative value or the upper limit control indicator 76b does not receive an ON signal 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 pressure upper limit value Pb is not to be executed.

[0104] When the PI control / switch 68a receives an ONac signal from the lower limit control indicator 76a, it calculates an operation amount based on the lower limit deviation ΔPat calculated by the lower limit deviation calculator 73a, and outputs this operation amount to the three-way valve 57 or the medium flow rate regulator 59 serving as the heat exchange amount regulator 56, 56a. The operation amount of the three-way valve 57 or the medium flow rate regulator 59 at this time is different from the operation amount when temperature correction is performed based on the pressure lower limit value Pa in the pressure correction mode. Therefore, the operation amount of the three-way valve 57 or the medium flow rate regulator 59 changes depending on whether the pressure correction mode or the pressure lower limit value control mode is selected by the operator, etc.

[0105] Furthermore, when the PI control / switch 68a receives an ONbc signal from the upper limit control indicator 76b, it calculates an operating amount based on the upper limit deviation ΔPbt calculated by the upper limit deviation calculator 73b, and outputs this operating amount to the three-way valve 57 or the medium flow rate regulator 59 serving as the heat exchange amount regulator 56, 56a. The operating amount of the three-way valve 57 or the medium flow rate regulator 59 at this time is different from the operating amount when temperature correction is performed based on the pressure upper limit value Pb in the pressure correction mode. Therefore, the operating amount of the three-way valve 57 or the medium flow rate regulator 59 changes depending on whether the pressure correction mode or the pressure condition value control mode is selected by the operator, etc.

[0106] The buttons of the control device 60 in each of the above embodiments and the control device 60a in this modification may be physically present buttons, or may be virtually present buttons on a display or the like.

[0107] "Other Modifications" In the above, cooling water is exemplified as the medium to be subjected to heat exchange with the hot water. However, a medium other than cooling water may be used as long as there is a certain temperature difference between the cooling water and the hot water.

[0108] In each of the above embodiments and modifications, the hot water is heated to about 90°C by the hot water heater 52, and then the hot water is cooled by exchanging heat with a medium such as cooling water to a temperature of 90°C to 60°C. However, the hot water may be further heated by the hot water heater 52 to adjust the temperature of the hot water. In this case, the hot water heater 52 heats the hot water to, for example, about 50°C. Then, the heated hot water is further heated by exchanging heat with a medium of, for example, about 100°C to 70°C to a temperature of 90°C to 60°C.

[0109] In each of the above-described embodiments and modifications, the hot water heater 52 is disposed downstream of the economizer 21eco, which is the most downstream heat transfer tube among the plurality of heat transfer tubes, in the boiler casing 21c. However, the hot water heater 52 may be disposed at a position overlapping with the most downstream heat transfer tube in the flow direction of the exhaust gas in the boiler casing 21c.

[0110] The gas turbines 10 in the above-described embodiments and modified examples are all so-called single-shaft gas turbines. However, the gas turbine may be a two-shaft gas turbine. That is, the gas turbine may have a compressor, a combustor, 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.

[0111] The gas turbine plants of the above-described embodiments and modifications are combined cycle plants including a gas turbine 10, a heat recovery steam generator 20, and a steam turbine 23. However, the gas turbine plant may be a cogeneration plant including the gas turbine 10 and the heat recovery steam generator 20, but not including a steam turbine. In this case, the steam generated in the heat recovery steam generator 20 is used, for example, in a factory.

[0112] The gas turbine plants of the above-described embodiments and modified examples include a denitration device 20. However, when the NOx concentration in the exhaust gas discharged from the gas turbine 10 satisfies the environmental standard, the gas turbine plant may not include a denitration device.

[0113] "Additional Notes" The gas turbine plant in the above embodiment can be understood, for example, as follows.

[0114] (1) A gas turbine plant according to a first aspect, The system includes a gas turbine 10 that burns fuel and can be driven by combustion gas produced by the combustion of the fuel, a heat recovery boiler 21 that can generate steam by utilizing heat of exhaust gas from the gas turbine 10, and fuel supply equipment 40, 40a that can supply ammonia as the fuel to the gas turbine 10. The fuel supply equipment 40, 40a includes a liquid ammonia line 42 connected to an ammonia tank 41 capable of storing liquid ammonia, hot water lines 50, 50a through which hot water can flow, a vaporizer 45 connected to an end of the liquid ammonia line 42 and capable of heating and vaporizing the liquid ammonia by heat exchange between the hot water from the hot water line 50, 50a and the liquid ammonia, a heat exchanger 55 capable of heat exchange between the hot water in the hot water line 50, 50a and a medium, a heat exchange amount regulator 56, 56a capable of adjusting the amount of heat exchange between the hot water and the medium to adjust the temperature of the hot water flowing into the vaporizer 45, and a gaseous ammonia line 46 capable of guiding gaseous ammonia, which is the ammonia vaporized in the vaporizer 45, to the gas turbine 10. The vaporizer 45 has an ammonia inlet 45ci, an ammonia outlet 45co, a hot water inlet 45pi, and a hot water outlet 45po. The liquid ammonia line 42 is connected to the ammonia inlet 45ci of the vaporizer 45. The gaseous ammonia line 46 is connected to the ammonia outlet 45co of the vaporizer 45. The hot water lines 50, 50a are disposed in the heat recovery boiler 21 and include a hot water heater 52 that heats the hot water by heat exchange between the hot water and the exhaust gas, and high-temperature water lines 53, 53a that connect the hot water heater 52 and the hot water inlet 45pi of the vaporizer 45. The heat exchanger 55 is provided in the high-temperature water lines 53, 53a.

[0115] In this embodiment, the hot water heated by the heat exchange between the hot water and the exhaust gas in the hot water heater 52 flows into the vaporizer 45 after being temperature-adjusted. In this vaporizer 45, the temperature-adjusted hot water exchanges heat with liquid ammonia, and the ammonia vaporizes. Meanwhile, the temperature of the exhaust gas flowing through the exhaust heat recovery boiler 21 changes due to changes in the operating conditions of the gas turbine 10. Therefore, when the temperature of the exhaust gas changes, the temperature of the hot water heated by the hot water heater 52 also changes. However, in this embodiment, as described above, the hot water heated by the hot water heater 52 flows into the vaporizer 45 after being temperature-adjusted. Therefore, in this embodiment, even if the temperature of the exhaust gas changes, all of the liquid ammonia flowing into the vaporizer 45 can be easily converted into gaseous ammonia.

[0116] Furthermore, the amount of gaseous ammonia required by the gas turbine 10 also changes due to changes in 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 of the liquid ammonia that has flowed into the vaporizer 45 can be easily converted into gaseous ammonia by changing the temperature of the hot water that flows into the vaporizer 45.

[0117] Therefore, in this embodiment, even if the operating conditions of the gas turbine 10 change, it is possible to easily obtain the production amount of gaseous ammonia required by the gas turbine 10. Also, in this embodiment, it is possible to improve the responsiveness of the production amount of gaseous ammonia to changes in the operating conditions of the gas turbine 10.

[0118] (2) A gas turbine plant according to a second aspect of the present invention comprises: In the gas turbine plant according to the first embodiment, the high-temperature water line 53 includes a main high-temperature water line 53x that connects the hot-water inlet 45pi of the vaporizer 45 and the hot-water heater 52, and a branch high-temperature water line 53y that branches off from the main high-temperature water line 53x and is then connected to the main high-temperature water line 53x. The heat exchanger 55 is provided in the branch high-temperature water line 53y. The heat exchange amount adjuster 56 includes a flow rate ratio adjuster that adjusts the ratio between the flow rate of hot water flowing in the main high-temperature water line 53x between the branch position of the branch high-temperature water line 53y and the connection position of the branch high-temperature water line 53y, and the flow rate of hot water flowing in the branch high-temperature water line 53y.

[0119] In this embodiment, the amount of heat exchange between the warm water and the medium can be adjusted by adjusting the ratio between the flow rate of the warm water flowing in the main high-temperature water line 53x between the branching position of the branch high-temperature water line 53y and the connection position of the branch high-temperature water line 53y and the flow rate of the warm water flowing in the branch high-temperature water line 53y.

[0120] (3) A gas turbine plant according to a third aspect, In the gas turbine plant according to the first or second aspect, the heat exchange amount adjuster 56 a has a medium flow rate adjuster 59 that adjusts the flow rate of the medium flowing into the heat exchanger 55 .

[0121] In this embodiment, by adjusting the flow rate of the medium flowing into the heat exchanger 55, the amount of heat exchanged between the hot water and the medium can be adjusted.

[0122] (4) A gas turbine plant according to a fourth aspect comprises: In the gas turbine plant according to any one of the first to third aspects, the vaporizer 45 includes a heat transfer tube 45p having the hot water inlet 45pi and the hot water outlet 45po, through which hot water can flow, and a vaporizer casing 45c that covers the heat transfer tube 45p and can temporarily store the liquid ammonia. The vaporizer casing 45c includes the ammonia inlet 45ci and the ammonia outlet 45co. The liquid ammonia line 42 is connected to the ammonia inlet 45ci of the vaporizer casing 45c, and the gaseous ammonia line 46 is connected to the ammonia outlet 45co of the vaporizer casing 45c.

[0123] When liquid ammonia flows into the heat transfer tube 45p and hot water flows into the vaporizer casing 45c that covers the heat transfer tube 45p, the liquid ammonia becomes gaseous ammonia in the heat transfer tube 45p, and the gaseous ammonia accumulates in a part of the heat transfer tube 45p. Therefore, the heat transfer area effective for heat exchange between the liquid ammonia and the hot water becomes smaller than the total heat transfer area of ​​the heat transfer tube 45p. Moreover, in this case, the heat transfer area effective for heat exchange between the liquid ammonia and the hot water also changes with the change in the amount of gaseous ammonia produced. Therefore, in this case, it is difficult to control the amount of heat exchange between the liquid ammonia and the hot water, and it may not be possible to ensure the required amount of gaseous ammonia produced.

[0124] On the other hand, in this embodiment, hot water flows into the heat transfer tube 45p, and liquid ammonia flows into the vaporizer casing 45c that covers the heat transfer tube 45p. Therefore, in this embodiment, the liquid ammonia in contact with the outer surface of the heat transfer tube 45p can be separated from the outer surface of the heat transfer tube 45p when vaporized. Therefore, in this embodiment, the heat transfer area effective for heat exchange between the liquid ammonia and the hot water can be made larger than the previous case with respect to the total heat transfer area of ​​the heat transfer tube 45p. Moreover, in this embodiment, the heat transfer area effective for heat exchange between the liquid ammonia and the hot water does not substantially change with respect to the change in the amount of gaseous ammonia produced. Therefore, in this embodiment, the amount of heat exchange between the liquid ammonia and the hot water can be easily controlled, and the required amount of gaseous ammonia produced can be easily obtained.

[0125] (5) A gas turbine plant according to a fifth aspect comprises: In the gas turbine plant according to any one of the first to fourth aspects, the heat recovery boiler 21 includes a boiler casing 21c through which exhaust gas from a gas turbine 10 flows, and a plurality of heat transfer tubes arranged in the boiler casing 21c and through which water or steam flows. The plurality of heat transfer tubes are aligned in the flow direction of the exhaust gas within the boiler casing 21c. The hot water heater 52 is arranged in the boiler casing 21c at a position overlapping, in the flow direction of the exhaust gas, a heat transfer tube that is most downstream in the flow direction of the exhaust gas among the plurality of heat transfer tubes, or at a position further downstream of the heat transfer tube.

[0126] In the boiler casing 21c, the temperature of the exhaust gas decreases toward the downstream side of the exhaust gas flow. In this embodiment, the heat of the exhaust gas whose temperature has been reduced can be effectively utilized by the hot water heater 52.

[0127] (6) A gas turbine plant according to a sixth aspect, The gas turbine plant according to any one of the first to fifth aspects further includes a control device 60, 60a for controlling an operation of the heat exchange amount adjuster 56, 56a. The control device 60, 60a has a temperature control system 65, 65a for determining an operation amount of the heat exchange amount adjuster 56, 56a according to a required output PWr for the gas turbine 10 from the outside and for instructing the operation amount to the heat exchange amount adjuster 56, 56a.

[0128] The flow rate of fuel supplied to the gas turbine 10 changes according to the change in the required output PWr of the gas turbine 10. In this case, the amount of heat exchange between the fuel and the hot water in the vaporizer 45 changes with the change in the fuel flow rate. If the temperature of the hot water is adjusted according to the result of the change in the amount of heat exchange, it takes time from when the required output PWr changes to when the amount of gaseous ammonia generated is ensured. In this embodiment, the operation amount of the heat exchange amount regulators 56, 56a is determined according to the required output PWr, so that it is possible to shorten the time from when the required output PWr changes to when the amount of gaseous ammonia generated is ensured. In other words, in this embodiment, it is possible to improve the responsiveness of the amount of gaseous ammonia generated to the change in the required output PWr.

[0129] (7) A gas turbine plant according to a seventh aspect comprises: In the gas turbine plant in the sixth aspect, the control device 60, 60a further includes a pressure control system 70, 70a which determines an operating amount of the heat exchange amount adjuster 56, 56a so that the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within a predetermined pressure range, and instructs the operating amount to the heat exchange amount adjuster 56, 56a.

[0130] If the pressure of the gaseous ammonia flowing into the gas turbine 10 is not within a predetermined pressure range, the gaseous ammonia cannot be stably burned in the gas turbine 10. In this embodiment, the pressure control systems 70, 70a control the pressure of the gaseous ammonia flowing into the gas turbine 10 to be within the predetermined pressure range. Therefore, in this embodiment, the gaseous ammonia can be stably burned in the gas turbine 10.

[0131] The fuel supply method for a gas turbine plant in each of the above-described embodiments and modifications can be understood, for example, as follows. (8) In an eighth aspect, a fuel supply method for a gas turbine plant includes the steps of: A fuel supply method for a gas turbine plant including a gas turbine 10 capable of burning fuel and being driven by combustion gas generated by the combustion of the fuel, and a heat recovery boiler 21 capable of generating steam by utilizing heat of exhaust gas from the gas turbine 10, the method comprising the steps of: a hot water heating step S1 for exchanging heat between hot water in a hot water heater 52 disposed in the heat recovery boiler 21 and the exhaust gas in the heat recovery boiler 21 and outside the hot water heater 52 to heat the hot water; and a heat exchange step for exchanging heat between the hot water heated in the hot water heating step S1 and a medium. S3, heat exchange amount adjustment steps S2 and S2X for adjusting the amount of heat exchange between the hot water heated in the hot water heating step S1 and the medium, a vaporization step S6 for vaporizing the liquid ammonia by heat exchange between the hot water after the amount of heat exchange with the medium is adjusted in the heat exchange amount adjustment steps S2 and S2X and the liquid ammonia from the ammonia tank 41 storing the liquid ammonia in the vaporizer 45, and a fuel supply step S8 for supplying gaseous ammonia, which is the ammonia vaporized in the vaporization step S6, to the gas turbine 10 as fuel. In the heat exchange amount adjustment steps S2 and S2X, the amount of heat exchange between the hot water and the medium in the heat exchange step S3 is adjusted to adjust the temperature of the hot water flowing into the vaporizer 45.

[0132] In this embodiment, similarly to the gas turbine plant of the first embodiment, even if the operating conditions of the gas turbine 10 change, it is possible to easily obtain the production amount of gaseous ammonia required by the gas turbine 10. Furthermore, also in this embodiment, it is possible to improve the responsiveness of the production amount of gaseous ammonia to the change in the operating conditions of the gas turbine 10.

[0133] (9) A fuel supply method for a gas turbine plant according to a ninth aspect, In the fuel supply method for a gas turbine plant according to the eighth aspect, the heat exchange amount adjustment step S2 includes a division step S2a of dividing the hot water heated in the hot water heating step S1 into main high temperature water and branch high temperature water, and a flow rate ratio adjustment step S2b. In the heat exchange step S3, the branch high temperature water is heat exchanged with the medium. In the flow rate ratio adjustment step S2b, a flow rate ratio between the main high temperature water and the branch high temperature water after heat exchange in the heat exchange step S3 is adjusted, and the main high temperature water and the branch high temperature water after heat exchange in the heat exchange step S3 are merged.

[0134] In this embodiment, like the gas turbine plant of the second embodiment, the amount of heat exchanged between the hot water and the medium can be adjusted.

[0135] (10) A fuel supply method for a gas turbine plant according to a tenth aspect, comprising: In the fuel supply method for a gas turbine plant according to the eighth or ninth aspect, the heat exchange amount adjusting step S2X includes a medium flow rate adjusting step S2c of adjusting a flow rate of the medium performing heat exchange with the hot water in the heat exchanging step S3.

[0136] In this aspect, like the gas turbine plant of the third aspect, the amount of heat exchanged between the hot water and the medium can be adjusted.

[0137] (11) In an eleventh aspect, a fuel supply method for a gas turbine plant includes the steps of: In the fuel supply method for a gas turbine plant in any one of the eighth to tenth embodiments, a temperature control step S4 is further executed to control the adjustment of the heat exchange amount in the heat exchange amount adjustment steps S2, S2X in accordance with a required output PWr for the gas turbine 10 from the outside.

[0138] In this aspect, similarly to the gas turbine plant of the sixth aspect, the responsiveness of the amount of gaseous ammonia produced to a change in the required output PWr can be improved.

[0139] (12) A fuel supply method for a gas turbine plant according to a twelfth aspect, comprising: The fuel supply method for a gas turbine plant in the eleventh aspect further includes a pressure control step S5 for controlling adjustment of the heat exchange amount in the heat exchange amount adjustment steps S2, S2X so that the pressure of the gaseous ammonia flowing into the gas turbine 10 falls within a predetermined pressure range.

[0140] In this embodiment, similarly to the gas turbine plant of the seventh embodiment, gaseous ammonia can be stably combusted in the gas turbine 10. [Explanation of symbols]

[0141] 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: Combustor 16: Turbine 16r: Turbine rotor 16c: Turbine casing 20:Denitration equipment 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: Ammonia tank 42: Liquid ammonia line 43a: Liquid ammonia control valve 43b: Fuel control valve 44: Ammonia pump 45: Carburetor 45c: Carburetor casing 45ci: Ammonia inlet 45co: Ammonia outlet 45p: Heat transfer tube 45pi: Hot water inlet 45po: Hot water outlet 46: Gaseous ammonia line 48: Thermometer 49: Pressure gauge 50,50a: Hot water line 51: Low temperature water line 52:Hot water heater 53, 53a: Hot water line 53x: Main hot water line 53y: Branch hot water line 54: Hot water pump 55: Heat exchanger 55c: Heat exchanger casing 55p: Heat transfer tube 55pi: Media inlet 55po: Media outlet 56,56a: Heat exchange amount regulator 57: Three-way valve (or flow ratio regulator) 58i: Media Line 58o: Media collection line 59:Media flow regulator 60, 60a: Control device 61:Fuel flow rate calculation section 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 control / switch 70, 70a: Pressure control system 71: Pressure compensation mode button 71a: Lower limit control mode button 71b: Upper limit control mode button 72a: Lower limit memory 72b: Upper limit memory 73a: Lower limit deviation calculator 73b: Upper limit deviation calculator 74a: Lower limit deviation judger 74b: Upper limit deviation judger 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 changer 78b: Second switch 79a: First adder 79b: Second adder

Claims

1. A gas turbine that burns fuel and is capable of being driven by combustion gas generated by the combustion of the fuel; a heat recovery boiler capable of generating steam by utilizing heat of exhaust gas from the gas turbine; A fuel supply facility capable of supplying ammonia as the fuel to the gas turbine; Equipped with The fuel supply equipment includes: a liquid ammonia line connected to an ammonia tank capable of storing liquid ammonia; A hot water line that can run hot water; A vaporizer connected to an end of the liquid ammonia line, capable of exchanging heat between the hot water from the hot water line and the liquid ammonia to heat and vaporize the liquid ammonia; a heat exchanger capable of exchanging heat between the hot water in the hot water line and a medium; a heat exchange amount adjuster that adjusts the amount of heat exchange between the hot water and the medium to adjust the temperature of the hot water flowing into the vaporizer; a gaseous ammonia line capable of guiding gaseous ammonia, which is the ammonia vaporized in the vaporizer, to the gas turbine; having The vaporizer has an ammonia inlet, an ammonia outlet, a hot water inlet, and a hot water outlet, the liquid ammonia line is connected to an ammonia inlet of the vaporizer; the gaseous ammonia line is connected to the ammonia outlet of the vaporizer; The hot water line includes a hot water heater that is disposed in the heat recovery boiler and heats hot water by exchanging heat between hot water and the exhaust gas, and a high-temperature water line that connects the hot water heater and the hot water inlet of the vaporizer, The heat exchanger is provided in the high-temperature water line. Gas turbine plant.

2. 2. The gas turbine plant according to claim 1, The high-temperature water line includes a main high-temperature water line that connects the hot water inlet of the evaporator and the hot water heater, and a branch high-temperature water line that branches off from the main high-temperature water line and is then connected to the main high-temperature water line, The heat exchanger is provided in the branch high-temperature water line, the heat exchange amount adjuster has a flow rate ratio adjuster that adjusts a ratio between a flow rate of hot water flowing in the main high temperature water line between a branch position of the branch high temperature water line and a connection position of the branch high temperature water line and a flow rate of hot water flowing in the branch high temperature water line, Gas turbine plant.

3. The gas turbine plant according to claim 1 or 2, The heat exchange amount regulator has a medium flow rate regulator that regulates the flow rate of the medium flowing into the heat exchanger. Gas turbine plant.

4. In the gas turbine plant according to any one of claims 1 to 3, The vaporizer has the hot water inlet and the hot water outlet, and includes a heat transfer tube through which hot water can flow, and a vaporizer casing that covers the heat transfer tube and is capable of temporarily storing the liquid ammonia, The vaporizer casing has the ammonia inlet and the ammonia outlet, The liquid ammonia line is connected to the ammonia inlet of the vaporizer casing, and the gaseous ammonia line is connected to the ammonia outlet of the vaporizer casing. Gas turbine plant.

5. In the gas turbine plant according to any one of claims 1 to 4, The heat recovery boiler includes a boiler casing through which exhaust gas from a gas turbine flows, and a plurality of heat transfer tubes arranged in the boiler casing and through which water or steam flows, The plurality of heat transfer tubes are arranged in the boiler casing in a flow direction of the exhaust gas, The hot water heater is disposed in the boiler casing at a position overlapping with a heat transfer tube that is the most downstream in the flow direction of the exhaust gas among the plurality of heat transfer tubes, or at a position further downstream of the heat transfer tube. Gas turbine plant.

6. In the gas turbine plant according to any one of claims 1 to 5, Further, a control device for controlling the operation of the heat exchange amount regulator is provided, the control device has a temperature control system that determines an operation amount of the heat exchange amount regulator in response to an output required for the gas turbine from an outside and instructs the operation amount to the heat exchange amount regulator. Gas turbine plant.

7. 7. The gas turbine plant according to claim 6, The control device further includes a pressure control system that determines an operation amount of the heat exchange amount regulator so that the pressure of the gaseous ammonia flowing into the gas turbine falls within a predetermined pressure range, and instructs the heat exchange amount regulator on the operation amount. Gas turbine plant.

8. A fuel supply method for a gas turbine plant including a gas turbine capable of burning fuel and being driven by combustion gas produced by the combustion of the fuel, and a heat recovery boiler capable of generating steam by utilizing heat of exhaust gas from the gas turbine, comprising the steps of: a hot water heating process of exchanging heat between hot water in a hot water heater disposed in the heat recovery boiler and the exhaust gas outside the hot water heater in the heat recovery boiler to heat the hot water; a heat exchange step of exchanging heat between the hot water heated in the hot water heating step and a medium; a heat exchange amount adjusting step of adjusting an amount of heat exchange between the hot water heated in the hot water heating step and the medium; a vaporization step of vaporizing the liquid ammonia by heat exchange between the hot water after the heat exchange amount with the medium is adjusted by the heat exchange amount adjustment step and the liquid ammonia from an ammonia tank storing the liquid ammonia in a vaporizer; a fuel supplying step of supplying gaseous ammonia, which is the ammonia vaporized in the vaporization step, to the gas turbine as fuel; Run In the heat exchange amount adjustment step, the amount of heat exchange between the hot water and the medium in the heat exchange step is adjusted to adjust the temperature of the hot water flowing into the evaporator. A fuel supply method for a gas turbine plant.

9. 9. The fuel supply method for a gas turbine plant according to claim 8, The heat exchange amount adjustment step includes a flow dividing step of dividing the hot water heated in the hot water heating step into main high temperature water and branch high temperature water, and a flow rate ratio adjustment step. In the heat exchange step, the branched high-temperature water is heat exchanged with the medium, In the flow rate ratio adjustment step, a flow rate ratio between the main high temperature water and the branch high temperature water after heat exchange in the heat exchange step is adjusted, and the main high temperature water and the branch high temperature water after heat exchange in the heat exchange step are merged. A fuel supply method for a gas turbine plant.

10. The fuel supply method for a gas turbine plant according to claim 8 or 9, The heat exchange amount adjusting step includes a medium flow rate adjusting step of adjusting a flow rate of the medium that exchanges heat with the hot water in the heat exchange step. A fuel supply method for a gas turbine plant.

11. The fuel supply method for a gas turbine plant according to any one of claims 8 to 10, and further executing a temperature control step of controlling the adjustment of the heat exchange amount in the heat exchange amount adjustment step in response to an output required for the gas turbine from an outside. A fuel supply method for a gas turbine plant.

12. 12. The fuel supply method for a gas turbine plant according to claim 11, Furthermore, a pressure control step is performed to control a heat exchange amount in the heat exchange amount adjustment step so that a pressure of the gaseous ammonia flowing into the gas turbine falls within a predetermined pressure range. A fuel supply method for a gas turbine plant.

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