Gas turbine plant and method for utilizing ammonia therein

Abstract

To enhance a utility value of ammonia while suppressing facility cost and running cost.SOLUTION: A gas turbine plant includes: an exhaust heat recovery boiler; an ammonia vaporizer that generates gas ammonia by exchanging heat between steam from the exhaust heat recovery boiler and liquid ammonia; an ammonia heater that exchanges heat between the steam from the exhaust heat recovery boiler and the gas ammonia and generates heated ammonia by heating the gas ammonia; a heated ammonia main line for guiding a part of the heated ammonia to a gas turbine as fuel; a heated ammonia branch line branched from the heated ammonia main line; an ammonia decomposition device that exchanges heat between the steam from the exhaust heat recovery boiler and the heated ammonia from the heated ammonia branch line and thermally decomposes the heated ammonia to generate decomposition gas; and a hydrogen purification facility that purifies hydrogen from at least a part of the decomposition gas.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present invention relates to a gas turbine plant equipped with a gas turbine and a heat recovery boiler, and a method for utilizing ammonia therein. [Background technology]

[0002] To reduce CO2 emissions from the perspective of protecting the global environment, the use of hydrogen as a fuel, which does not emit CO2 when burned, is a promising option. However, compared to fuels such as liquefied natural gas, which is widely used as fuel for gas turbines, hydrogen is not easy to transport or store. For this reason, the use of ammonia, which can be converted to hydrogen, as a fuel is being considered.

[0003] The following Patent Document 1 discloses a gas turbine plant that uses ammonia as fuel. This gas turbine plant includes a gas turbine and an ammonia tank. The gas turbine has an air compressor, a combustor, and a turbine. A portion of the ammonia from the ammonia tank is supplied as fuel to the upstream side of the combustor. Another portion of the ammonia from the ammonia tank is decomposed into hydrogen-rich gas. This hydrogen-rich gas is supplied as fuel to the downstream side of the combustor. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Special Publication No. 2018-535355 Summary of the Invention [Problem to be solved by the invention]

[0005] For gas turbine plants that use ammonia as fuel, it is desirable to increase the utility value of ammonia while keeping equipment costs and running costs low.

[0006] Therefore, an object of the present invention is to provide a gas turbine plant that can increase the utility value of ammonia while reducing equipment costs and running costs, and a method for utilizing ammonia therein. [Means for solving the problem]

[0007] In order to achieve the above object, a gas turbine plant according to one aspect of the invention comprises: an ammonia tank capable of storing liquid ammonia; a gas turbine capable of being driven by using ammonia as fuel; a heat recovery boiler capable of generating steam by utilizing the heat of exhaust gas from the gas turbine; an ammonia vaporizer capable of vaporizing the liquid ammonia by heat exchange between steam or hot water from the heat recovery boiler and liquid ammonia from the ammonia tank to generate gaseous ammonia; an ammonia heater capable of heat exchange between steam or hot water from the heat recovery boiler and the gaseous ammonia from the ammonia vaporizer to heat the gaseous ammonia; the ammonia decomposer capable of thermally decomposing the heated ammonia by heat exchange between steam from the heat recovery boiler and the heated ammonia from the heated ammonia branch line to generate a decomposition gas containing hydrogen; hydrogen purification equipment capable of purifying hydrogen from at least a portion of the decomposition gas; and a hydrogen line capable of guiding high-purity hydrogen, which is hydrogen purified by the hydrogen purification equipment, to a hydrogen tank.

[0008] In order to achieve the above object, one aspect of the present invention is to use ammonia in a method comprising the steps of: A method for utilizing ammonia in a gas turbine plant including a gas turbine and a heat recovery boiler capable of generating steam by utilizing the heat of exhaust gas from the gas turbine. This ammonia utilization method includes an ammonia vaporization process in which steam or hot water from the heat recovery boiler is heat exchanged with liquid ammonia to vaporize the liquid ammonia and produce gaseous ammonia; an ammonia heating process in which steam or hot water from the heat recovery boiler is heat exchanged with the gaseous ammonia produced in the ammonia vaporization process to heat the gaseous ammonia; a main fuel supply process in which a portion of the heated ammonia, that is, the gaseous ammonia heated in the ammonia heating process, is introduced as fuel to the gas turbine; an ammonia decomposition process in which steam from the heat recovery boiler is heat exchanged with another portion of the heated ammonia to thermally decompose the heated ammonia to produce a cracked gas containing hydrogen; and a hydrogen purification process in which hydrogen is purified from at least a portion of the cracked gas. [Effects of the Invention]

[0009] According to one aspect of the present invention, it is possible to increase the utility value of ammonia while reducing equipment costs and running costs. [Brief explanation of the drawings]

[0010] [Figure 1] 1 is a system diagram of a gas turbine plant in an embodiment according to the present invention. [Figure 2] 1 is a conceptual diagram showing a configuration of a combustor in an embodiment according to the present invention. [Figure 3] FIG. 1 is a system diagram of an ammonia decomposition facility in one embodiment according to the present invention. [Figure 4] 1 is a system diagram of a hydrogen purification facility according to an embodiment of the present invention. [Figure 5] 1 is a flowchart showing the steps of a method for utilizing ammonia in one embodiment according to the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0011] Various embodiments and modifications of a gas turbine plant equipped with an ammonia decomposition facility of the present invention will be described below with reference to the drawings.

[0012] "First embodiment" A first embodiment of a gas turbine plant will be described with reference to FIGS.

[0013] As shown in FIG. 1 , the gas turbine plant of this embodiment includes a gas turbine 10, a heat recovery boiler 20, a denitration device 29, a steam turbine facility 30, a power generator 39, an ammonia tank 50, an ammonia vaporizer 51, an ammonia heater 52, an ammonia decomposer 53, an ammonia recovery facility 60, an ammonia compressor 95 c, a hydrogen purification facility 70, an off-gas compressor 97 c, and a hydrogen tank 79.

[0014] The gas turbine 10 includes an air compressor 11 capable of compressing air to generate compressed air CA, a combustor 12 capable of burning fuel in the compressed air CA to generate combustion gas, and a turbine 13 that can be driven by the combustion gas from the combustor 12. The air compressor 11 includes a compressor rotor 11r and a compressor casing 11c that covers the compressor rotor 11r. The turbine 13 includes a turbine rotor 13r and a turbine casing 13c that covers the turbine rotor 13r. The compressor rotor 11r and the turbine rotor 13r are connected to each other to form a gas turbine rotor 14.

[0015] As shown in Fig. 2, the combustor 12 has a cylindrical combustion liner (or transition piece) 12p arranged around a cylinder axis Ac, and multiple burners 12b capable of injecting fuel into the combustion liner 12p. All of the multiple burners 12b extend in the same direction as the cylinder axis Ac. The multiple burners 12b include a central burner 12bc and multiple peripheral burners 12bp arranged around the central burner 12bc. The central burner 12bc is arranged on or near the cylinder axis Ac. The combustor 12 is configured so that compressed air CA is supplied from an air compressor 11 to the multiple burners 12b.

[0016] 1, the heat recovery steam generator 20 has a boiler frame 21 through which exhaust gas from the gas turbine 10 flows, a low-pressure steam generation system 22, an intermediate-pressure steam generation system 23, a high-pressure steam generation system 25, an intermediate-pressure pump 24, and a high-pressure pump 26. Here, the upstream side of the flow of exhaust gas within the boiler frame 21 is referred to as the boiler upstream side, and the opposite side is referred to as the boiler downstream side. A stack 28 that exhausts exhaust gas to the atmosphere is connected to the end of the boiler frame 21 that is furthest downstream from the boiler.

[0017] The low-pressure steam generation system 22 has an economizer 22a, an evaporator 22b, and a superheater 22c. The economizer 22a exchanges heat between water and exhaust gas to heat the water and turn it into hot water. The evaporator 22b exchanges heat between a portion of the hot water from the economizer 22a and exhaust gas to heat the water and turn it into steam. The superheater 22c exchanges heat between the steam from the evaporator 22b and exhaust gas to superheat the steam. The economizer 22a, at least a portion of the evaporator 22b, and the superheater 22c are all arranged within the boiler frame 21. The economizer 22a, at least a portion of the evaporator 22b, and the superheater 22c are arranged in this order from the downstream side of the boiler to the upstream side of the boiler.

[0018] Although not shown, the intermediate-pressure steam generation system 23 and the high-pressure steam generation system 25 each have an economizer, an evaporator, and a superheater, similar to the low-pressure steam generation system 22. The intermediate-pressure pump 24 pressurizes a portion of the hot water from the economizer 22a of the low-pressure steam generation system 22 and then sends it to the economizer of the intermediate-pressure steam generation system 23. The high-pressure pump 26 pressurizes another portion of the hot water from the economizer 22a of the low-pressure steam generation system 22 and then sends it to the economizer of the high-pressure steam generation system 25.

[0019] Of the superheaters of the steam generation systems 22, 23, and 25, the superheater of the high-pressure steam generation system 25 is disposed upstream of the other superheaters within the boiler frame 21. The superheater of the intermediate-pressure steam generation system 23 is disposed downstream of the superheater of the high-pressure steam generation system 25 and upstream of the superheater 22c of the low-pressure steam generation system 22 within the boiler frame 21. The denitration device 29 is disposed, for example, between the high-pressure steam generation system 25 and the intermediate-pressure steam generation system 23 within the boiler frame 21. The denitration device 29 uses ammonia water and, through the action of a catalyst, decomposes NOx contained in the exhaust gas from the gas turbine 10 into nitrogen and water vapor.

[0020] The steam turbine facility 30 includes a low-pressure steam turbine 31, an intermediate-pressure steam turbine 32, a high-pressure steam turbine 33, a condenser 35, a feedwater line 36, and a feedwater pump 37. The low-pressure steam turbine 31 includes a low-pressure steam turbine rotor 31r and a casing 31c that covers the low-pressure steam turbine rotor 31r. The intermediate-pressure steam turbine 32 includes an intermediate-pressure steam turbine rotor 32r and a casing 32c that covers the intermediate-pressure steam turbine rotor 32r. The high-pressure steam turbine 33 includes a high-pressure steam turbine rotor 33r and a casing 33c that covers the high-pressure steam turbine rotor 33r. The low-pressure steam turbine rotor 31r, the intermediate-pressure steam turbine rotor 32r, and the high-pressure steam turbine rotor 33r are connected to one another to form a single steam turbine rotor 34. The gas turbine rotor 14 described above is connected to one end of the steam turbine rotor 34. A generator 39 is connected to the other end of the steam turbine rotor 34.

[0021] In this embodiment, the steam turbine rotor 34 and the gas turbine rotor 14 are connected to each other, and a generator 39 is connected to an end of the rotors. However, the steam turbine rotor 34 and the gas turbine rotor 14 may not be connected to each other, and a generator may be connected to an end of the steam turbine rotor 34, and a generator may also be connected to an end of the gas turbine rotor 14.

[0022] The superheater of the high-pressure steam generation system 25 and the steam inlet of the high-pressure steam turbine 33 are connected by a high-pressure steam line 43. The superheater of the intermediate-pressure steam generation system 23 and the steam inlet of the intermediate-pressure steam turbine 32 are connected by an intermediate-pressure steam line 42. The steam inlet of the intermediate-pressure steam turbine 32 is further connected to the steam outlet of the high-pressure steam turbine 33 by a high-pressure exhaust steam line 44. The superheater 22c of the low-pressure steam generation system 22 and the steam inlet of the low-pressure steam turbine 31 are connected by a low-pressure steam line 41. The steam inlet of the low-pressure steam turbine 31 is further connected to the steam outlet of the intermediate-pressure steam turbine 32 by an intermediate-pressure exhaust steam line 45. The aforementioned condenser 35 is connected to the steam outlet of the low-pressure steam turbine 31. This condenser 35 converts steam exhausted from the low-pressure steam turbine 31 back into liquid water. The condenser 35 and the economizer of the low-pressure steam generation system 22 are connected by a feedwater line 36. A water supply pump 37 is provided on the water supply line 36 .

[0023] The ammonia tank 50 is a tank capable of storing liquid ammonia NHL.

[0024] The ammonia vaporizer 51 is a heat exchanger that exchanges heat between steam and liquid ammonia NHL to vaporize the liquid ammonia NHL and generate gaseous ammonia NHG. An ammonia inlet of the ammonia vaporizer 51 and an ammonia outlet of the ammonia tank 50 are connected by a liquid ammonia line 80. An ammonia pump 81 is provided on the liquid ammonia line 80. A steam inlet of the ammonia vaporizer 51 and the low-pressure steam line 41 are connected by a low-pressure steam branch line 83. A steam outlet of the ammonia vaporizer 51 is connected to the condenser 35, for example, by a low-pressure steam recovery line 84. Thus, the ammonia vaporizer 51 exchanges heat between the liquid ammonia NHL from the ammonia tank 50 and the low-pressure steam LS from the low-pressure steam generation system 22. The temperature of the low-pressure steam LS is, for example, 130 to 180°C. In the ammonia vaporizer 51, for example, heat exchange may be performed between the liquid ammonia NHL from the ammonia tank 50 and hot water heated by the economizer of the intermediate pressure steam generation system 23.

[0025] The ammonia heater 52 is a heat exchanger capable of heating the gaseous ammonia NHG by exchanging heat between steam and the gaseous ammonia NHG. An ammonia inlet of the ammonia heater 52 and an ammonia outlet of the ammonia vaporizer 51 are connected by a gaseous ammonia line 82. A steam inlet of the ammonia heater 52 and the medium-pressure steam line 42 are connected by a first medium-pressure steam branch line 85. A steam outlet of the ammonia heater 52 is connected to the condenser 35, for example, by a first medium-pressure steam recovery line 86. Thus, the ammonia heater 52 exchanges heat between the gaseous ammonia NHG from the ammonia vaporizer 51 and the medium-pressure steam IS from the medium-pressure steam generation system 23. The temperature of the medium-pressure steam IS is, for example, 250 to 350°C. Note that the ammonia heater 52 may also exchange heat between the gaseous ammonia NHG from the ammonia vaporizer 51 and hot water from the economizer of the high-pressure steam generation system 25 or hot water from the economizer of the medium-pressure steam generation system 23, for example. Furthermore, depending on the temperature of the low-pressure steam LS described above, in the ammonia heater 52, heat exchange may be performed between the gaseous ammonia NHG from the ammonia vaporizer 51 and the low-pressure steam LS from the low-pressure steam generation system 22. The ammonia outlet of the ammonia heater 52 and the plurality of peripheral burners 12bp (see FIG. 2) of the combustor 12 are connected by a heated ammonia main line 87. Therefore, heated ammonia NHH, which is gaseous ammonia NHG heated by the ammonia heater 52, is sent as fuel to the plurality of peripheral burners 12bp of the combustor 12 via the heated ammonia main line 87. The heated ammonia main line 87 is provided with a main fuel valve 88 that can adjust the flow rate of the heated ammonia NHH sent to the combustor 12.

[0026] The ammonia decomposer 53 is a heat exchanger that exchanges heat between steam and heated ammonia (NHH) to thermally decompose the heated ammonia (NHH) and generate decomposition gas (DG). This decomposition gas (DG) contains residual ammonia as well as hydrogen and nitrogen obtained by the thermal decomposition of ammonia. The interior of the ammonia decomposer 53 is divided by a heat transfer wall formed of a heat transfer tube or the like into a target gas space through which ammonia or decomposition gas (DG) flows and a steam space through which steam flows. The heat transfer wall is formed of, for example, Ni steel. The target gas space is filled with a catalyst for promoting the thermal decomposition of ammonia. This catalyst includes a catalytic component that activates the decomposition reaction and a carrier that supports the catalytic component. Examples of the catalytic component include particles of a noble metal such as Ru, and metal particles containing a transition metal such as Ni, Co, or Fe. Examples of the carrier include metal oxides such as Al2O3, ZrO2, Pr2O3, La2O3, and MgO. The catalyst is not limited to the catalysts exemplified above, as long as it activates the ammonia decomposition reaction.

[0027] The ammonia inlet of the ammonia decomposer 53 and the heated ammonia main line 87 are connected by a heated ammonia branch line 89. That is, the heated ammonia branch line 89 is a line branched from the heated ammonia main line 87 through which heated ammonia NHH flows. A branch valve 89v is provided on the heated ammonia branch line 89. The steam inlet of the ammonia decomposer 53 and the high-pressure steam line 43 are connected by a high-pressure steam branch line 91. The steam outlet of the ammonia decomposer 53 is connected to the intermediate-pressure steam generation system 23 or the condenser 35, for example, by a high-pressure steam recovery line 92. Therefore, the ammonia decomposer 53 exchanges heat between the heated ammonia NHH from the ammonia heater 52 and the high-pressure steam HS from the high-pressure steam generation system 25. The temperature of the high-pressure steam HS is, for example, 450 to 550°C. One end of a cracked gas line 90 is connected to the cracked gas outlet of the ammonia decomposer 53.

[0028] The ammonia recovery facility 60 is a facility that recovers ammonia from the decomposition gas DG from the ammonia decomposer 53. As shown in Fig. 3 , the ammonia recovery facility 60 includes an absorption tower 61, a water line 62, an ammonia water line 63, an ammonia water heater 64, a separation tower 65, a water circulation line 66, a reboiler 67, a water condenser 68, and a water recovery line 69.

[0029] In the absorption tower 61, a packing 61a is arranged in a vertically intermediate region of the absorption tower 61. The other end of the cracked gas line 90 is connected to a portion of the absorption tower 61 below the intermediate region. The water line 62 is connected to a portion of the absorption tower 61 above the intermediate region. One end of a treated gas line 96 is connected to the top of the absorption tower 61. One end of an ammonia water line 63 is connected to the bottom of the absorption tower 61.

[0030] The decomposition gas DG from the ammonia decomposer 53 flows into the absorption tower 61 from below the intermediate region of the absorption tower 61 via the decomposition gas line 90. Furthermore, water is sprayed into the absorption tower 61 from above the intermediate region of the absorption tower 61 via the water line 62. The decomposition gas DG that flows into the absorption tower 61 rises within the absorption tower 61. Meanwhile, the water sprayed into the absorption tower 61 descends within the absorption tower 61. As the water descends within the absorption tower 61, it comes into contact with the fillers 61a. The water that comes into contact with the fillers 61a forms a water film that covers the surfaces of the fillers 61a. As the decomposition gas DG rises within the absorption tower 61, it comes into contact with the water film that covers the surfaces of the fillers 61a. During this process, residual ammonia contained in the decomposition gas DG dissolves in water. Ammonia water, which is water in which residual ammonia has been dissolved, accumulates in the lower part of the absorption tower 61 and flows into the ammonia water line 63. The treated gas PG, which is the cracked gas DG from which the residual ammonia has been removed, rises inside the absorption tower 61 and flows into the treated gas line 96.

[0031] Within the separation tower 65, a tray 65a is arranged in a vertically intermediate region of the separation tower 65. The multiple stages constituting the tray 65a are aligned vertically. Each of the multiple stages constituting the tray 65a is composed of a plate having a large number of holes formed therein. The other end of the ammonia water line 63 is connected to a middle stage among the multiple stages constituting the tray 65a. One end of a water circulation line 66 is connected to the bottom of the separation tower 65, and the other end of the water circulation line 66 is connected to a position in the separation tower 65 above the bottom and below the intermediate region. A reboiler 67 is provided on the water circulation line 66. The reboiler 67 is a heat exchanger that exchanges heat between water flowing through the water circulation line 66 and steam. A steam inlet of the reboiler 67 and the intermediate-pressure steam line 42 are connected by a second intermediate-pressure steam branch line 93. A steam outlet of the reboiler 67 is connected to the condenser 35, for example, by a second intermediate-pressure steam recovery line 94. Therefore, the reboiler 67 heats water by heat exchange between the water and the intermediate-pressure steam IS, converting the water into steam. This steam flows into the separation column 65 via a water circulation line 66. Note that the reboiler 67 may exchange heat between the water and, for example, the high-pressure steam HS from the superheater of the high-pressure steam generation system 25, the hot water from the economizer of the high-pressure steam generation system 25, or the hot water from the economizer of the intermediate-pressure steam generation system 23.

[0032] Steam flows into the separation tower 65 from below the intermediate region of the separation tower 65. Furthermore, ammonia water from the ammonia water line 63 is sprayed into the separation tower 65 from the intermediate trays 65a. The steam flowing into the separation tower 65 rises within the separation tower 65. The ammonia water sprayed from the intermediate trays 65a forms a liquid layer on each tray 65a and gradually flows down to the lower trays. The steam rises through numerous holes provided on each tray 65a while coming into gas-liquid contact with the ammonia water, heating the ammonia water. Ammonia, which evaporates more easily than water, is heated by the steam, which is gas-phase water, and transitions from the liquid phase to the gas phase, while water transitions from the gas phase to the liquid phase. The gas-phase ammonia rises within the separation tower 65. Furthermore, liquid-phase water, more specifically, water with a low ammonia concentration, accumulates in the lower part of the separation tower 65. A part of this water passes through the water circulation line 66 and the reboiler 67 and flows into the separation column 65 again as steam.

[0033] The other end of the water line 62 is connected to the water circulation line 66. Therefore, part of the water accumulated in the lower part of the separation tower 65 returns to the separation tower 65 via the water circulation line 66, and another part of the water accumulated in the lower part of the separation tower 65 flows into the absorption tower 61 via the water circulation line 66 and the water line 62.

[0034] The ammonia water heater 64 is provided in the ammonia water line 63. This ammonia water heater 64 is a heat exchanger that exchanges heat between the ammonia water flowing through the ammonia water line 63 and the water flowing through the water line 62. The ammonia water heater 64 heats the ammonia water by heat exchange between the ammonia water and the water. The heated ammonia water is sprayed into the separation tower 65 as described above. On the other hand, the water cooled by heat exchange with the ammonia water is sprayed into the absorption tower 61 via the water line 62.

[0035] One end of an ammonia recovery line 95 is connected to the top of the separation tower 65. The other end of the ammonia recovery line 95 is connected to the ammonia inlet of the ammonia heater 52. The ammonia recovery line 95 is provided with a water condenser 68 and an ammonia compressor 95c. The water condenser 68 cools the gas containing ammonia in a gaseous phase flowing through the ammonia recovery line 95, condensing part of the water and ammonia in this gas. The water condensed in the water condenser 68 passes through a water recovery line 69 and returns to the space above the tray 65a in the separation tower 65. The gas mainly containing ammonia that passes through the water condenser 68 flows into the ammonia heater 52 via the ammonia recovery line 95. Thus, in the ammonia heater 52, the gaseous ammonia NHG from the ammonia vaporizer 51 and the gas mainly containing ammonia from the ammonia recovery facility 60 are heated with steam.

[0036] When an ammonia condenser is provided downstream of the water condenser 68, the liquid ammonia NHL from the ammonia condenser may be returned to the ammonia tank 50 or the ammonia vaporizer 51.

[0037] Here, the moisture condenser 68 is disposed outside the separation tower 65. However, the moisture condenser 68 may also be disposed in the upper space of the separation tower 65. Also, here, the reboiler 67 is disposed outside the separation tower 65. However, the reboiler 67 may also be disposed inside the separation tower 65. Also, here, a packing type is adopted as the gas-liquid contacting method in the absorption tower 61. Also, a tray type is adopted as the gas-liquid contacting method in the separation tower 65. However, since there are other types of gas-liquid contacting methods, other types may also be adopted as the gas-liquid contacting methods in the absorption tower 61 and the separation tower 65. Each of the multiple methods for realizing the gas-liquid contacting method has advantages and disadvantages in terms of equipment size, equipment installation costs, equipment maintenance costs, equipment pressure loss, required power, and equipment durability. Therefore, from the multiple methods for realizing the liquid contacting method, an optimal method may be selected depending on the plant specifications, location conditions, and the like.

[0038] The ammonia recovery facility 60 described above is a known facility. This ammonia recovery facility may be a facility with a different configuration as long as it is a facility that can recover ammonia from the cracked gas DG.

[0039] The hydrogen purification system 70 of this embodiment uses pressure swing adsorption to adsorb and separate ammonia from a gas containing ammonia and hydrogen, thereby purifying hydrogen. As shown in FIG. 4 , the hydrogen purification system 70 includes a first adsorption tower 71a, a second adsorption tower 71b, a first treated gas line 72a, a second treated gas line 72b, a first treated gas valve 73a, a second treated gas valve 73b, a first off-gas line 74a, a second off-gas line 74b, a first off-gas valve 75a, a second off-gas valve 75b, a vacuum pump 76, a first hydrogen line 77a, a second hydrogen line 77b, a first hydrogen valve 78a, a second hydrogen valve 78b, and a hydrogen compressor 77c. Although the hydrogen purification system 70 of this embodiment includes two adsorption towers 71a and 71b, it may include three or more adsorption towers.

[0040] The first adsorption tower 71a and the second adsorption tower 71b are each provided with an ammonia adsorbent Ab capable of adsorbing ammonia under high pressure and releasing ammonia under low pressure. One end of a first treated gas line 72a and one end of a second treated gas line 72b are connected to the other end of the treated gas line 96. The other end of the first treated gas line 72a is connected to the treated gas inlet of the first adsorption tower 71a. The other end of the second treated gas line 72b is connected to the treated gas inlet of the second adsorption tower 71b. Thus, the treated gas PG from the ammonia recovery system 60, i.e., the cracked gas DG from which ammonia has been recovered in the ammonia recovery system 60, can flow into the first adsorption tower 71a and the second adsorption tower 71b. A first treated gas valve 73a is provided on the first treated gas line 72a, and a second treated gas valve 73b is provided on the second treated gas line 72b.

[0041] One end of a first offgas line 74a is connected to the first treated gas line 72a at a position closer to the first adsorption tower 71a than the first treated gas valve 73a. A first offgas valve 75a is provided on the first offgas line 74a. One end of a second offgas line 74b is connected to the second treated gas line 72b at a position closer to the second adsorption tower 71b than the second treated gas valve 73b. A second offgas valve 75b is provided on the second offgas line 74b. One end of an offgas line 97 is connected to the other end of the first offgas line 74a and the other end of the second offgas line 74b. The other end of the offgas line 97 is connected to the central burner 12bc of the combustor 12 (see FIG. 2). The offgas line 97 is provided with a vacuum pump 76, an offgas compressor 97c, and an auxiliary fuel valve 98.

[0042] One end of the first hydrogen line 77a is connected to the outlet of the first adsorption tower 71a. A first hydrogen valve 78a is provided on this first hydrogen line 77a. One end of the second hydrogen line 77b is connected to the outlet of the second adsorption tower 71b. A second hydrogen valve 78b is provided on this second hydrogen line 77b. One end of a hydrogen line 99 is connected to the other end of the first hydrogen line 77a and the other end of the second hydrogen line 77b. A hydrogen compressor 77c is provided on this hydrogen line 99.

[0043] Suppose the ammonia adsorption capacity of the ammonia adsorbent Ab in the first adsorption tower 71a is extremely low, while the ammonia adsorption capacity of the ammonia adsorbent Ab in the second adsorption tower 71b is high. In this case, the first treated gas valve 73a, the first hydrogen valve 78a, and the second off-gas valve 75b are opened, and the second treated gas valve 73b, the second hydrogen valve 78b, and the first off-gas valve 75a are closed. Treated gas PG from the ammonia recovery system 60 flows into the first adsorption tower 71a via the first treated gas line 72a and the first treated gas valve 73a. As the treated gas PG flows into the first adsorption tower 71a and passes through the ammonia adsorbent Ab, much of the undecomposed ammonia contained in the treated gas PG is adsorbed by the ammonia adsorbent Ab, and much of the hydrogen contained in the treated gas PG is discharged from the first adsorption tower 71a as high-purity hydrogen. This high-purity hydrogen is sent to the hydrogen tank 79 via the first hydrogen line 77a, the first hydrogen valve 78a, the hydrogen line 99, and the hydrogen compressor 77c. Meanwhile, the ammonia adsorbed to the ammonia adsorbent Ab in the second adsorption tower 71b is released from the ammonia adsorbent Ab by vacuum suctioning the second adsorption tower 71b with the vacuum pump 76. Then, from the second adsorption tower 71b, an off-gas OG containing this ammonia and hydrogen remaining in the second adsorption tower 71b is sent to the combustor 12 via the second off-gas line 74b, the second off-gas valve 75b, the off-gas line 97, the vacuum pump 76, the off-gas compressor 97c, and the auxiliary fuel valve 98.

[0044] When the ammonia adsorption amount of the ammonia adsorbent Ab in the first adsorption tower 71a increases and the ammonia adsorption amount of the ammonia adsorbent Ab in the second adsorption tower 71b becomes extremely small, the first treated gas valve 73a, the first hydrogen valve 78a, and the second off-gas valve 75b are closed, and the second treated gas valve 73b, the second hydrogen valve 78b, and the first off-gas valve 75a are opened. Treated gas PG from the ammonia recovery system 60 flows into the second adsorption tower 71b via the second treated gas line 72b and the second treated gas valve 73b. As the treated gas PG flows into the second adsorption tower 71b and passes through the ammonia adsorbent Ab, much of the undecomposed ammonia contained in the treated gas PG is adsorbed by the ammonia adsorbent Ab, and much of the hydrogen contained in the treated gas PG is discharged from the second adsorption tower 71b as high-purity hydrogen. This high-purity hydrogen is sent to the hydrogen tank 79 via the second hydrogen line 77b, the second hydrogen valve 78b, the hydrogen line 99, and the hydrogen compressor 77c. Meanwhile, the ammonia adsorbed to the ammonia adsorbent Ab in the first adsorption tower 71a is released from the ammonia adsorbent Ab by vacuum suctioning the first adsorption tower 71a with the vacuum pump 76. Then, the off-gas OG containing the ammonia and hydrogen remaining in the first adsorption tower 71a is sent from the first adsorption tower 71a to the combustor 12 via the first off-gas line 74a, the first off-gas valve 75a, the off-gas line 97, the vacuum pump 76, the off-gas compressor 97c, and the auxiliary fuel valve 98.

[0045] As described above, in the hydrogen purification system 70 of this embodiment, while ammonia is being adsorbed onto the ammonia adsorbent Ab in the first adsorption tower 71a, ammonia is released from the ammonia adsorbent Ab in the second adsorption tower 71b. Furthermore, in the hydrogen purification system 70 of this embodiment, while ammonia is being released from the ammonia adsorbent Ab in the first adsorption tower 71a, ammonia is adsorbed onto the ammonia adsorbent Ab in the second adsorption tower 71b. Therefore, the hydrogen purification system 70 of this embodiment can continuously receive the treated gas PG from the ammonia recovery system 60, remove most of the undecomposed ammonia, and continuously discharge high-purity hydrogen, while also continuously discharge the off-gas OG containing residual ammonia and residual hydrogen.

[0046] Next, the overall operation of the gas turbine plant described above will be described. First, the operations of the gas turbine 10, the heat recovery steam generator 20, and the steam turbine facility 30 will be described.

[0047] The air compressor 11 of the gas turbine 10 compresses air to generate compressed air CA. The combustor 12 burns fuel in the compressed air CA to generate combustion gas. This combustion gas is supplied to and drives the turbine 13. The exhaust gas, which is the combustion gas that drives the turbine 13, flows into the boiler frame 21 of the heat recovery steam generator 20.

[0048] In each steam generation system 22, 23, 25 of the heat recovery boiler 20, heat is exchanged between the exhaust gas flowing inside the boiler frame 21 and water, converting liquid water into steam. Water is supplied to the economizer 22a of the low-pressure steam generation system 22 from a feedwater pump 37. In the economizer 22a, heat is exchanged between this water and the exhaust gas, heating the water to convert it into hot water. A portion of this hot water is pressurized by the high-pressure pump 26 and then sent to the high-pressure steam generation system 25. The hot water sent to the high-pressure steam generation system 25 exchanges heat with the exhaust gas to become high-pressure steam HS. This high-pressure steam HS is supplied to the high-pressure steam turbine 33 via a high-pressure steam line 43. The high-pressure steam turbine 33 is driven by this high-pressure steam HS.

[0049] Another portion of the hot water from the economizer 22a of the low-pressure steam generating system 22 is pressurized by the intermediate-pressure pump 24 and then sent to the intermediate-pressure steam generating system 23. The hot water sent to the intermediate-pressure steam generating system 23 exchanges heat with the exhaust gas to become medium-pressure steam IS. This medium-pressure steam IS is supplied to the intermediate-pressure steam turbine 32 via an intermediate-pressure steam line 42. In addition, steam exhausted from the high-pressure steam turbine 33 is supplied to the intermediate-pressure steam turbine 32 via a high-pressure exhaust steam line 44. That is, the intermediate-pressure steam turbine 32 is supplied with the medium-pressure steam IS from the intermediate-pressure steam generating system 23 and the steam exhausted from the high-pressure steam turbine 33. The intermediate-pressure steam turbine 32 is driven by the steam supplied to the intermediate-pressure steam turbine 32.

[0050] Another portion of the hot water from the economizer 22a of the low-pressure steam generating system 22 is heated by exhaust gas in the evaporator 22b of the low-pressure steam generating system 22 to become steam. This steam is superheated by exhaust gas in the superheater 22c of the low-pressure steam generating system 22 to become low-pressure steam LS. This low-pressure steam LS is supplied to the low-pressure steam turbine 31 via a low-pressure steam line 41. Furthermore, steam exhausted from the intermediate-pressure steam turbine 32 is supplied to the low-pressure steam turbine 31 via an intermediate-pressure exhaust steam line 45. That is, the low-pressure steam turbine 31 is supplied with the low-pressure steam LS from the low-pressure steam generating system 22 and the steam exhausted from the intermediate-pressure steam turbine 32. The low-pressure steam turbine 31 is driven by the steam supplied to the low-pressure steam turbine 31.

[0051] The steam exhausted from the low-pressure steam turbine 31 is returned to water in a condenser 35. The water in the condenser 35 is sent to the economizer 22a of the low-pressure steam generating system 22 via a feedwater line 36 and a feedwater pump 37.

[0052] Next, the operations of the ammonia vaporizer 51, the ammonia heater 52, the ammonia decomposer 53, the ammonia recovery facility 60, and the hydrogen purification facility 70 will be described with reference to the flowchart shown in FIG.

[0053] The liquid ammonia NHL in the ammonia tank 50 is pressurized by an ammonia pump 81 and then flows into the ammonia vaporizer 51.

[0054] In the ammonia vaporizer 51, heat is exchanged between the low-pressure steam LS from the low-pressure steam generation system 22 of the exhaust heat recovery boiler 20 and the liquid ammonia NHL to vaporize the liquid ammonia NHL and generate gaseous ammonia NHG (ammonia vaporization step S1). In this ammonia vaporization step S1, the low-pressure steam LS cooled by heat exchange with the liquid ammonia NHL is sent to, for example, the condenser 35. Note that, as described above, the medium for heating the liquid ammonia NHL in the ammonia vaporizer 51 does not have to be the low-pressure steam LS, and may be, for example, hot water from the economizer of the medium-pressure steam generation system 23.

[0055] The gaseous ammonia NHG flows into the ammonia heater 52. In the ammonia heater 52, the gaseous ammonia NHG is heated by heat exchange between the medium-pressure steam IS from the medium-pressure steam generation system 23 of the exhaust heat recovery boiler 20 and the gaseous ammonia NHG (ammonia heating step S2). Note that, as described above, the medium for heating the gaseous ammonia NHG in the ammonia heater 52 does not have to be the medium-pressure steam IS, and may be, for example, hot water from the economizer of the high-pressure steam generation system 25, hot water from the economizer of the medium-pressure steam generation system 23, or low-pressure steam LS from the low-pressure steam generation system 22.

[0056] A part of the heated ammonia NHH, which is gaseous ammonia NHG heated by the ammonia heater 52, is supplied as fuel to the peripheral burner 12bp of the combustor 12 via the heated ammonia main line 87 (main fuel supply step S3).

[0057] Another portion of the heated ammonia NHH flows into the ammonia decomposer 53 via the heated ammonia branch line 89. In the ammonia decomposer 53, heat exchange occurs between the high-pressure steam HS from the high-pressure steam generation system 25 of the heat recovery boiler 20 and the heated ammonia NHH in a catalytic environment, and the heated ammonia NHH is thermally decomposed to produce a decomposed gas DG (ammonia decomposition step S4). This decomposed gas DG contains residual ammonia as well as hydrogen and nitrogen obtained by the thermal decomposition of the heated ammonia NHH.

[0058] The cracked gas DG flows into the absorption tower 61 of the ammonia recovery system 60. In the absorption tower 61, the cracked gas DG is brought into contact with water, and residual ammonia in the cracked gas DG is dissolved in the water. As a result, ammonia water is produced in the absorption tower 61. The absorber 61 also discharges treated gas PG, which is the cracked gas DG from which most of the residual ammonia has been removed. The ammonia water flows into the separation tower 65 of the ammonia recovery system 60 via an ammonia water line 63. Steam generated by heat exchange between water and medium-pressure steam IS from the medium-pressure steam generation system 23 of the heat recovery boiler 20 also flows into the separation tower 65 from the reboiler 67. As mentioned above, the medium for heating the water in the reboiler 67 does not have to be the medium-pressure steam IS. For example, the medium may be high-pressure steam HS from the superheater of the high-pressure steam generation system 25, hot water from the economizer of the high-pressure steam generation system 25, or hot water from the economizer of the medium-pressure steam generation system 23. The ammonia water that has flowed into the separation tower 65 is heated by the steam that has flowed into the separation tower 65, and the ammonia in the ammonia water transitions from the liquid phase to the gas phase, and is discharged from the separation tower 65. The gas phase ammonia discharged from the separation tower 65, i.e., gaseous ammonia NHG, is pressurized by the ammonia compressor 95c and sent to the ammonia heater 52 via the ammonia recovery line 95 (ammonia recovery step S5).

[0059] Therefore, in the ammonia heater 52 in this embodiment, the gaseous ammonia NHG from the ammonia vaporizer 51 as well as the gaseous ammonia NHG from the ammonia recovery facility 60 are heated with steam.

[0060] As described above, when an ammonia condenser is provided downstream of the water condenser 68 in the ammonia recovery facility 60, the liquid ammonia NHL from the ammonia condenser may be returned to the ammonia tank 50 or the ammonia vaporizer 51. In this case, in the ammonia vaporizer 51, the liquid ammonia NHL from the ammonia recovery facility 60 is also heated with steam and vaporized.

[0061] The treated gas PG discharged from the absorption tower 61 flows into the hydrogen purification equipment 70 via a treated gas line 96. In the hydrogen purification equipment 70, hydrogen is purified from the treated gas PG, and an off-gas OG containing hydrogen is generated (hydrogen purification step S6). The high-purity hydrogen purified from the treated gas PG is sent to the hydrogen tank 79 via a hydrogen line 99. In addition, the off-gas OG obtained in the hydrogen purification process is supplied as fuel to the central burner 12bc of the combustor 12 via an off-gas line 97 (secondary fuel supply step S7).

[0062] The off-gas OG containing hydrogen sent to the central burner 12bc is ejected from the central burner 12bc into the combustion liner 12p and combusted in the compressed air. Meanwhile, the heated ammonia NHH sent to the peripheral burners 12bp is ejected from the peripheral burners 12bp into the combustion liner 12p and combusted in the compressed air. The combustion gas generated by the combustion of the off-gas OG and the heated ammonia NHH flows into the turbine 13 and drives the turbine 13. The combustion gas that drives the turbine 13 flows into the boiler frame 21 of the heat recovery steam generator 20 as exhaust gas.

[0063] Hydrogen has a faster combustion speed than ammonia. Therefore, when a fuel containing hydrogen is burned, localized high temperatures are likely to occur within the combustion tube 12p, which may increase the NOx concentration in the combustion gas. Therefore, in this embodiment, off-gas OG containing hydrogen is injected into the combustion tube 12p from the central burner 12bc, and the jet of this off-gas OG is surrounded by jets of ammonia from the multiple peripheral burners 12bp. Therefore, in this embodiment, even when off-gas OG containing hydrogen is burned, the generation of localized high temperatures within the combustion tube 12p is suppressed, and the NOx concentration in the combustion gas can be suppressed.

[0064] As described above, in this embodiment, gaseous ammonia NHG is heated from liquid ammonia NHL to produce heated ammonia NHH. Then, in this embodiment, a portion of this heated ammonia NHH is supplied to the gas turbine 10 as fuel. Furthermore, in this embodiment, another portion of this heated ammonia NHH is thermally decomposed to produce a cracked gas DG containing hydrogen, and then hydrogen is purified from at least a portion of this cracked gas DG, and the high-purity hydrogen is led to the hydrogen tank 79. Therefore, in this embodiment, the utility value of the liquid ammonia NHL can be increased compared to when all of the liquid ammonia NHL is simply used as fuel for the gas turbine 10.

[0065] Furthermore, in this embodiment, the ammonia vaporizer 51 and the ammonia heater 52, which are necessary for producing heated ammonia NHH from liquid ammonia NHL to be supplied as fuel to the gas turbine 10, are also used for purifying high-purity hydrogen, thereby making it possible to reduce equipment costs and running costs. Furthermore, in this embodiment, steam or hot water from the heat recovery boiler 20 is used as a heat source for heating the liquid ammonia NHL in the ammonia vaporizer 51, for heating the gaseous ammonia NHG in the ammonia heater 52, and for thermally decomposing the gaseous ammonia NHG in the ammonia decomposer 53. Therefore, in this embodiment, it is possible to reduce running costs from this perspective as well.

[0066] As described above, in this embodiment, it is possible to increase the utility value of ammonia while suppressing equipment costs and running costs.

[0067] In this embodiment, ammonia is recovered from the cracked gas DG from the ammonia decomposer 53, and the cracked gas DG from which the ammonia has been recovered is sent to the hydrogen purification equipment 70, while the ammonia recovered in the ammonia recovery equipment 60 can be returned to any one of the ammonia tank 50, the ammonia vaporizer 51, or the ammonia heater 52. Therefore, in this embodiment, most of the ammonia in the ammonia tank 50 can be effectively utilized.

[0068] In this embodiment, the off-gas OG containing hydrogen generated in the process of refining hydrogen in the hydrogen refining equipment 70 is sent to the gas turbine 10 as fuel, so that the hydrogen in the off-gas OG can also be effectively utilized.

[0069] "Variations" In the hydrogen purification equipment 70 in the above embodiment, an ammonia adsorbent Ab capable of adsorbing ammonia is used. However, a hydrogen adsorbent capable of adsorbing hydrogen may also be used. In this case, the hydrogen purification equipment has a hydrogen adsorbent capable of adsorbing hydrogen under high pressure and releasing hydrogen under low pressure, and hydrogen can be purified from at least a portion of the decomposition gas by a pressure swing adsorption method. When a hydrogen adsorbent is used in this manner, during the process of adsorbing hydrogen with the hydrogen adsorbent, a gas containing hydrogen and undecomposed ammonia that has passed through the hydrogen adsorbent is supplied to the combustor 12 as off-gas, and hydrogen released from the hydrogen adsorbent under low pressure is supplied to the hydrogen tank 79.

[0070] The heat recovery steam generator 20 in the above embodiment has three types of steam generation systems 22, 23, and 25 that have different steam pressures and temperatures. However, the heat recovery steam generator 20 may have one or two types of steam generation systems as long as it can supply steam or hot water at appropriate temperatures to the ammonia vaporizer 51, the ammonia heater 52, the ammonia decomposer 53, and the ammonia recovery facility 60, respectively.

[0071] The steam turbine facility 30 in the above embodiment has three types of steam turbines 31, 32, and 33 with different inflow steam pressures. However, the steam turbine facility 30 may have only one type of steam turbine. Also, the steam from the heat recovery steam generator 20 may not be used for the steam turbine, but may be used as a heat source for a factory, for example. In this case, the steam generation system of the heat recovery steam generator 20 may have only one type of steam generation system as a steam generation system that generates steam for driving the steam turbine.

[0072] In the above embodiment, the ammonia vaporizer 51 and the ammonia heater 52 are separate devices. However, the ammonia vaporizer 51 and the ammonia heater 52 may be integrated. That is, in one heat exchanger, heat is exchanged between steam or hot water and liquid ammonia NHL to heat the liquid ammonia NHL and convert the liquid ammonia NHL into gaseous ammonia NHG, and then the gaseous ammonia NHG may be further heated to convert it into heated ammonia NHH.

[0073] Although the embodiments of the present disclosure have been described in detail above, the present disclosure is not limited to the above embodiments. Various additions, modifications, substitutions, partial deletions, etc. are possible within the scope of the conceptual idea and spirit of the present invention derived from the content defined in the claims and their equivalents.

[0074] "Addendum" The gas turbine plants in the above-described embodiments and modifications can be understood, for example, as follows.

[0075] (1) A gas turbine plant according to a first aspect includes: an ammonia tank 50 capable of storing liquid ammonia NHL; a gas turbine 10 capable of being driven by ammonia as fuel; a heat recovery boiler 20 capable of generating steam by utilizing the heat of exhaust gas from the gas turbine 10; an ammonia vaporizer 51 capable of performing heat exchange between steam or hot water from the heat recovery boiler 20 and the liquid ammonia NHL from the ammonia tank 50 to vaporize the liquid ammonia NHL and generate gaseous ammonia NHG; an ammonia heater 52 capable of performing heat exchange between steam or hot water from the heat recovery boiler 20 and the gaseous ammonia NHG from the ammonia vaporizer 51 to heat the gaseous ammonia NHG; The system includes a heated ammonia main line 87 capable of guiding a portion of the heated ammonia NHH, which is gaseous ammonia NHG, to the gas turbine 10 as fuel, a heated ammonia branch line 89 branching off from the heated ammonia main line 87, an ammonia decomposer 53 capable of heat exchanging steam from the exhaust heat recovery boiler 20 with the heated ammonia NHH from the heated ammonia branch line 89 to thermally decompose the heated ammonia NHH and generate a cracked gas DG containing hydrogen, a hydrogen purification facility 70 capable of purifying hydrogen from at least a portion of the cracked gas DG, and a hydrogen line 99 capable of guiding high-purity hydrogen, which is hydrogen purified in the hydrogen purification facility 70, to a hydrogen tank 79.

[0076] In this embodiment, gaseous ammonia NHG is heated from liquid ammonia NHL to produce heated ammonia NHH. Then, in this embodiment, a portion of this heated ammonia NHH is supplied to the gas turbine 10 as fuel. Furthermore, in this embodiment, another portion of this heated ammonia NHH is thermally decomposed to produce a cracked gas DG containing hydrogen, and then hydrogen is purified from at least a portion of this cracked gas DG, and the high-purity hydrogen is led to the hydrogen tank 79. Therefore, in this embodiment, the utility value of the liquid ammonia NHL can be increased compared to when all of the liquid ammonia NHL is simply used as fuel for the gas turbine 10.

[0077] In addition, in this embodiment, the ammonia vaporizer 51 and the ammonia heater 52, which are necessary for producing heated ammonia NHH from liquid ammonia NHL to be supplied as fuel to the gas turbine 10, are also used for purifying high-purity hydrogen, thereby reducing equipment costs and running costs. Furthermore, in this embodiment, steam or hot water from the heat recovery boiler 20 is used as a heat source for heating the liquid ammonia NHL in the ammonia vaporizer 51, for heating the gaseous ammonia NHG in the ammonia heater 52, and for thermally decomposing the gaseous ammonia NHG in the ammonia decomposer 53. Therefore, in this embodiment, running costs can be reduced from this perspective as well.

[0078] (2) A gas turbine plant according to a second aspect of the present invention comprises: In the gas turbine plant of the first aspect, the hydrogen purification equipment 70 has an ammonia adsorbent Ab that can adsorb ammonia under high pressure and release ammonia under low pressure, and can purify hydrogen by removing undecomposed ammonia from at least a portion of the decomposition gas DG using a pressure swing adsorption method.

[0079] (3) A gas turbine plant according to a third aspect includes: The gas turbine plant in the second aspect is provided with an off-gas line 97 that can guide hydrogen-containing off-gas OG, which is generated in the process of refining hydrogen in the hydrogen purification equipment 70, to the gas turbine 10 as fuel.

[0080] In this embodiment, the off-gas OG containing hydrogen generated in the process of refining hydrogen in the hydrogen refining equipment 70 is sent to the gas turbine 10 as fuel, so that the hydrogen in the off-gas OG can also be effectively utilized.

[0081] (4) A gas turbine plant according to a fourth aspect includes: In the gas turbine plant of the third aspect, the gas turbine 10 includes an air compressor 11 capable of compressing air to generate compressed air, a combustor 12 capable of burning fuel in the compressed air to generate combustion gas, and a turbine 13 capable of being driven by the combustion gas from the combustor 12. The combustor 12 includes a cylindrical cylinder 12p around a cylinder axis Ac in which the fuel can be burned, and a plurality of burners 12b capable of injecting fuel into the cylinder 12p. The plurality of burners 12b includes a central burner 12bc and a plurality of peripheral burners 12bp arranged around the central burner 12bc. The off-gas line 97 is connected to the central burner 12bc. The heated ammonia main line 87 is connected to the plurality of peripheral burners 12bp.

[0082] Hydrogen has a faster combustion speed than ammonia. Therefore, when hydrogen is burned as fuel, localized high temperatures are likely to occur within the combustion tube 12p, which may increase the NOx concentration in the combustion gas. Therefore, in this embodiment, off-gas OG containing hydrogen is injected into the tube 12p from the central burner 12bc, and the jet of this off-gas OG is surrounded by jets of ammonia from the multiple peripheral burners 12bp. Therefore, in this embodiment, even when off-gas OG containing hydrogen is burned, the generation of localized high temperatures within the tube 12p is suppressed, and the NOx concentration in the combustion gas can be suppressed.

[0083] (5) A gas turbine plant according to a fifth aspect includes: The gas turbine plant according to any one of the first to fourth aspects includes an ammonia recovery system (60) that recovers ammonia from the cracked gas (DG) from the ammonia decomposer (53) and sends the cracked gas (DG) from which ammonia has been recovered to the hydrogen purification system (70), and an ammonia recovery line (95) that can guide the ammonia recovered in the ammonia recovery system (60) to any one of the ammonia tank (50), the ammonia vaporizer (51), and the ammonia heater (52).

[0084] In this embodiment, ammonia is recovered from the cracked gas DG from the ammonia decomposer 53, and the cracked gas DG from which the ammonia has been recovered is sent to the hydrogen purification equipment 70, while the ammonia recovered in the ammonia recovery equipment 60 can be returned to any one of the ammonia tank 50, the ammonia vaporizer 51, and the ammonia heater 52. Therefore, in this embodiment, most of the ammonia in the ammonia tank 50 can be effectively utilized.

[0085] The method of utilizing ammonia in the gas turbine plant in the above-described embodiment and modified example can be understood as follows, for example.

[0086] (6) The method for utilizing ammonia in the sixth aspect is as follows: The present invention relates to a method for utilizing ammonia in a gas turbine plant including a gas turbine 10 and a heat recovery boiler 20 capable of generating steam by utilizing the heat of exhaust gas from the gas turbine 10. This utilization method includes an ammonia vaporization step S1 in which steam or hot water from the heat recovery boiler 20 is heat-exchanged with liquid ammonia NHL to vaporize the liquid ammonia NHL and produce gaseous ammonia NHG; an ammonia heating step S2 in which steam or hot water from the heat recovery boiler 20 is heat-exchanged with the gaseous ammonia NHG produced in the ammonia vaporization step S1 to heat the gaseous ammonia NHG; a main fuel supply step S3 in which a portion of the heated ammonia NHH, which is the gaseous ammonia NHG heated in the ammonia heating step S2, is introduced as fuel to the gas turbine 10; an ammonia decomposition step S4 in which steam from the heat recovery boiler 20 is heat-exchanged with another portion of the heated ammonia NHH to thermally decompose the heated ammonia NHH to produce a cracked gas DG containing hydrogen; and a hydrogen purification step S6 in which hydrogen is purified from at least a portion of the cracked gas DG.

[0087] In this aspect, similar to the gas turbine plant in the first aspect, it is possible to increase the utility value of ammonia while suppressing equipment costs and running costs.

[0088] (7) The seventh aspect of the ammonia utilization method is In the ammonia utilization method according to the sixth aspect, in the hydrogen purification step S6, an ammonia adsorbent Ab capable of adsorbing ammonia under high pressure and releasing ammonia under low pressure is used to remove undecomposed ammonia from at least a portion of the decomposition gas DG by a pressure swing adsorption method, thereby purifying hydrogen.

[0089] (8) In the eighth aspect, the method for utilizing ammonia is In the ammonia utilization method of the seventh aspect, a secondary fuel supply step S7 is carried out in which hydrogen-containing off-gas OG, which is generated in the hydrogen purification step S6 during the process of refining hydrogen, is introduced as fuel into the gas turbine 10.

[0090] In this embodiment, similar to the gas turbine plant in the third embodiment, it is possible to effectively utilize hydrogen in the off-gas generated in the process of refining hydrogen in the hydrogen refining step S6.

[0091] (9) In the ninth aspect, the method for utilizing ammonia comprises: In the method for utilizing ammonia according to any one of the sixth to eighth aspects, an ammonia recovery step S5 is carried out in which ammonia is recovered from the cracked gas DG. In the hydrogen purification step S6, hydrogen is purified from the cracked gas DG from which ammonia has been recovered in the ammonia recovery step S5. In either the ammonia vaporization step S1 or the ammonia heating step S2, heat exchange is carried out between the ammonia recovered in the ammonia recovery step S5 and steam or hot water from the heat recovery boiler 20.

[0092] In this embodiment, similar to the gas turbine plant in the fifth embodiment, most of the ammonia in the ammonia tank 50 can be effectively utilized. [Explanation of symbols]

[0093] 10: Gas turbine 11: Air compressor 11r: Compressor rotor 11c: Compressor casing 12: Combustor 12p: Combustion tube 12b: Burner 12bc: Center burner 12bp: Peripheral burner 13: Turbine 13r: Turbine rotor 13c: Turbine casing 14: Gas turbine rotor 20: Waste heat recovery boiler 21: Boiler frame 22: Low pressure steam generation system 22a: Economizer 22b: Evaporator 22c: Superheater 23: Medium pressure steam generation system 24: Medium pressure pump 25: High-pressure steam generation system 26: High pressure pump 28: Stack 29: Denitration equipment 30: Steam turbine equipment 31: Low-pressure steam turbine 32: Medium pressure steam turbine 33: High-pressure steam turbine 34: Steam turbine rotor 35: Condenser 36: Water supply line 37: Water supply pump 39: Generator 41: Low pressure steam line 42: Medium pressure steam line 43: High-pressure steam line 44: High pressure exhaust steam line 45: Medium pressure exhaust steam line 50: Ammonia tank 51: Ammonia vaporizer 52: Ammonia heater 53: Ammonia decomposer 60: Ammonia recovery facility 61: Absorption tower 61a: Filling 62: Water line 63: Ammonia water line 64: Ammonia water heater 65: Separation tower 65a: Shelf 66: Water circulation line 67: Reboiler 68: Moisture condenser 69: Water recovery line 70: Hydrogen purification equipment 71a:First adsorption tower 71b:Second adsorption tower 72a: First treated gas line 72b: Second treated gas line 73a: First treated gas valve 73b: Second treated gas valve 74a: First off-gas line 74b: Second off-gas line 75a: First off-gas valve 75b: Second off-gas valve 76: Vacuum pump 77a: First Hydrogen Line 77b: Second hydrogen line 78a: First hydrogen valve 78b: Second hydrogen valve 77c: Hydrogen compressor 79: Hydrogen tank 80: Liquid ammonia line 81: Ammonia pump 82: Gaseous ammonia line 83: Low pressure steam branch line 84: Low pressure steam recovery line 85: First medium pressure steam branch line 86: First medium pressure steam recovery line 87: Heated ammonia main line 88: Main fuel valve 89: Heated ammonia branch line 89v: Branch valve 90: Decomposition gas line 91: High pressure steam branch line 92: High-pressure steam recovery line 93: Second medium pressure steam branch line 94: Second medium pressure steam recovery line 95: Ammonia recovery line 95c: Ammonia compressor 96: Treated gas line 97: Offgas line 97c: Offgas compressor 98: Sub fuel valve 99: Hydrogen Line Ab: Ammonia adsorbent Ac: Cylinder axis CA: Compressed air LS: Low pressure steam IS: Medium pressure steam HS: High pressure steam NHL: Liquid ammonia NHG: Gaseous ammonia NHH: heated ammonia DG: Decomposition gas PG: Treated gas OG: Offgassing

Claims

1. an ammonia tank capable of storing liquid ammonia; a gas turbine that can be driven using ammonia as fuel; a heat recovery boiler capable of generating steam by utilizing heat of exhaust gas from the gas turbine; an ammonia vaporizer capable of performing heat exchange between steam or hot water from the heat recovery boiler and liquid ammonia from the ammonia tank to vaporize the liquid ammonia and generate gaseous ammonia; an ammonia heater capable of heating the gaseous ammonia by heat exchange between steam or hot water from the heat recovery boiler and the gaseous ammonia from the ammonia vaporizer; a heated ammonia main line capable of guiding a portion of the heated ammonia, which is gaseous ammonia heated by the ammonia heater, to the gas turbine as fuel; a heated ammonia branch line branching from the heated ammonia main line; an ammonia decomposer that performs heat exchange between steam or hot water from the heat recovery boiler and the heated ammonia from the heated ammonia branch line, thereby thermally decomposing the heated ammonia to generate a cracked gas containing hydrogen; A gas turbine plant comprising:

2. In the gas turbine plant according to claim 1, a hydrogen purification facility capable of purifying hydrogen from at least a portion of the cracked gas; a hydrogen line capable of guiding hydrogen purified by the hydrogen purification facility to a hydrogen tank; A gas turbine plant comprising:

3. In the gas turbine plant according to claim 2, The hydrogen purification facility has an ammonia adsorbent that can adsorb ammonia under high pressure and release ammonia under low pressure, and is capable of purifying hydrogen by removing undecomposed ammonia from at least a portion of the decomposition gas by a pressure swing adsorption method. Gas turbine plant.

4. In the gas turbine plant according to claim 3, an off-gas line capable of guiding hydrogen-containing off-gas generated in the process of purifying hydrogen in the hydrogen purification facility to the gas turbine as fuel; Gas turbine plant.

5. In the gas turbine plant according to claim 4, The gas turbine comprises: an air compressor capable of compressing air to generate compressed air; a combustor capable of combusting the fuel in the compressed air to generate combustion gases; a turbine that can be driven by the combustion gas from the combustor; and The combustor includes: a cylinder having a cylindrical shape around a cylinder axis, the cylinder having a fuel combustable therein; a plurality of burners capable of injecting the fuel into the cylinder; and The plurality of burners include a central burner and a plurality of peripheral burners arranged around the central burner, The off-gas line is connected to the central burner, The heated ammonia main line is connected to the plurality of peripheral burners. Gas turbine plant.

6. A gas turbine plant according to any one of claims 2 to 5, an ammonia recovery facility that recovers ammonia from the cracked gas from the ammonia decomposer and sends the cracked gas from which ammonia has been recovered to the hydrogen purification facility; an ammonia recovery line capable of guiding the ammonia recovered in the ammonia recovery facility to any one of the ammonia tank, the ammonia vaporizer, and the ammonia heater; A gas turbine plant comprising:

7. A method for utilizing ammonia in a gas turbine plant including a gas turbine and a heat recovery boiler capable of generating steam by utilizing heat of exhaust gas from the gas turbine, comprising: an ammonia vaporization step of exchanging heat between the steam or hot water from the heat recovery boiler and liquid ammonia to vaporize the liquid ammonia and generate gaseous ammonia; an ammonia heating step of exchanging heat between steam or hot water from the heat recovery boiler and the gaseous ammonia generated in the ammonia vaporization step to heat the gaseous ammonia; a main fuel supply step of introducing a part of the heated ammonia, which is the gaseous ammonia heated in the ammonia heating step, as fuel to the gas turbine; an ammonia decomposition step of exchanging heat between the steam or hot water from the heat recovery boiler and another part of the heated ammonia to thermally decompose the heated ammonia and generate a cracked gas containing hydrogen; a hydrogen purification step of purifying hydrogen from at least a portion of the cracked gas; A method of using ammonia to perform the above.

8. The method for utilizing ammonia according to claim 7, a hydrogen purification step of purifying hydrogen from at least a portion of the cracked gas; A method of using ammonia to perform the above.

9. The method for utilizing ammonia according to claim 8, In the hydrogen purification step, undecomposed ammonia is removed from at least a portion of the cracked gas by a pressure swing adsorption method using an ammonia adsorbent capable of adsorbing ammonia under high pressure and releasing ammonia under low pressure, thereby purifying hydrogen. Ammonia use.

10. The method for utilizing ammonia according to claim 9, a secondary fuel supply step of supplying hydrogen-containing off-gas, which is generated during the hydrogen purification step, to the gas turbine as fuel; Ammonia use.

11. The method for utilizing ammonia according to any one of claims 8 to 10, carrying out an ammonia recovery step of recovering ammonia from the cracked gas; In the hydrogen purification step, hydrogen is purified from the cracked gas from which ammonia has been recovered in the ammonia recovery step, In any one of the ammonia vaporization step and the ammonia heating step, the ammonia recovered in the ammonia recovery step is heat exchanged with steam or hot water from the heat recovery boiler. Ammonia use.

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