Fluid treatment plant

Abstract

To improve the thermal efficiency of a raw material fluid treatment plant.SOLUTION: A raw fluid processing plant includes a preheater for preheating a fluid. The preheater is a heat exchanger that heats the fluid by exchanging heat between the fluid and a second heating medium. The preheater includes a vaporizer that heats and vaporizes the fluid in a liquid state. The vaporizer is a heat exchanger configured to exchange heat between a second heating medium for vaporization, which is a kind of the second heating medium, and the liquid fluid to heat the liquid fluid.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present invention relates to a fluid treatment plant for heating a fluid. [Background technology]

[0002] To reduce CO2 emissions and protect 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 a fuel for gas turbines, hydrogen is not easy to transport or store. For this reason, the use of ammonia, which can be converted into hydrogen, as a fuel is being considered. Other fuels, such as methanol, are also being considered.

[0003] The following Patent Documents 1 and 2 disclose gas turbine plants. This gas turbine plant includes a raw material reaction facility that heats ammonia and thermally decomposes the ammonia into hydrogen and nitrogen. The raw material reaction facility has one heat exchanger. This heat exchanger has a gas frame through which exhaust gas from the gas turbine flows and a heat transfer tube disposed in the gas frame. In this heat exchanger, heat is exchanged between liquid ammonia flowing into the heat transfer tube and the exhaust gas flowing in the gas frame, heating the ammonia and causing a thermal decomposition reaction to produce a reaction gas containing hydrogen and nitrogen. This reaction gas is introduced into the combustor of the gas turbine. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Japanese Patent Application Publication No. 04-342829 [Patent Document 2] Japanese Patent Application Publication No. 2018-076794 Summary of the Invention [Problem to be solved by the invention]

[0005] In the technologies described in Patent Documents 1 and 2, a single heat exchanger exchanges heat between liquid ammonia and exhaust gas, heating the ammonia and causing the ammonia to undergo a thermal decomposition reaction, resulting in a large loss of thermal energy in the exhaust gas. Furthermore, in the technologies described in Patent Documents 1 and 2, the heat of the reaction gas after the reaction is not effectively utilized. Therefore, the technologies described in Patent Documents 1 and 2 result in a decrease in the thermal efficiency of the plant.

[0006] Therefore, an object of the present disclosure is to provide a technology that can reduce thermal energy loss from a heat source and improve the thermal efficiency of a plant when treating a fluid. [Means for solving the problem]

[0007] In order to achieve the above object, one aspect of the present invention relates to a raw material fluid processing plant, The raw material reaction facility includes a preheater that preheats the raw material fluid, a reactor that further heats the raw material fluid preheated in the preheater and reacts it to produce a reaction gas, a first heat medium line through which a first heat medium flows, and a second heat medium line through which a second heat medium different from the first heat medium flows. The reactor is a heat exchanger that exchanges heat between the raw material fluid and the first heat medium to heat and react the raw material fluid. The preheater is a heat exchanger that exchanges heat between the raw material fluid and the second heat medium to heat the raw material fluid. The first heat medium line guides the first heat medium to the reactor. The second heat medium line guides the second heat medium to the preheater.

[0008] In this embodiment, when the raw material fluid is heated and reacted, the raw material fluid is first preheated by heat exchange between the raw material fluid and a second heat medium different from the first heat medium. Then, in this embodiment, the preheated raw material fluid is heat exchanged between the first heat medium and the preheated raw material fluid to heat and react the raw material fluid. Therefore, in this embodiment, the amount of heat required to heat the first heat medium can be reduced compared to when the raw material fluid is preheated and reacted using a single heat medium. Therefore, in this embodiment, the thermal energy loss of the heat source, such as exhaust gas, used to heat the first heat medium can be reduced.

[0009] Here, in the raw material fluid processing plant according to the one aspect, the product of the constant pressure specific heat and the flow rate of the first heat medium flowing through the first heat medium line may be greater than the product of the constant pressure specific heat and the flow rate of the second heat medium flowing through the second heat medium line.

[0010] In this embodiment, a large amount of heat can be input to the temperature level of the reactor that requires a large amount of heat for the reaction of the raw material fluid, and a small amount of heat can be input to the temperature level of the preheater that requires a small amount of heat. Therefore, the amount of heat required for each temperature level can be input without excess or deficiency, and heat can be used effectively according to the temperature level.

[0011] The raw material fluid processing plant according to any of the above aspects may further include a waste heat utilization facility having a waste heat utilization heat cycle in which a heat cycle medium circulates, utilizing heat from a heat source to heat the heat cycle medium, and utilizing the heated heat cycle medium. In this case, the waste heat utilization facility utilizes heat from the heat source to heat the first heat medium. The first heat medium line introduces the first heat medium heated by the heat source to the reactor.

[0012] In this embodiment, the heat of the heat source that is not used to generate the reaction gas can be utilized in the heat cycle, thereby increasing the output and efficiency of the plant.

[0013] The raw material fluid processing plant of the above aspect equipped with the exhaust heat utilization equipment may further include an exhaust gas generation equipment that generates an exhaust gas. In this case, the heat source is the exhaust gas from the exhaust gas generation equipment. The exhaust heat utilization equipment heats the heat cycle medium by heat exchange with the exhaust gas. The exhaust heat utilization equipment includes a gas frame through which the exhaust gas flows, and a first heat medium heater provided in the gas frame that heats the first heat medium by heat exchange between the first heat medium and the exhaust gas. The first heat medium line is connected to the first heat medium heater of the exhaust heat utilization equipment, and introduces the first heat medium heated by the heat of the exhaust gas to the reactor.

[0014] In this embodiment, the heat of the exhaust gas from the exhaust gas generating facility is effectively utilized, thereby increasing the efficiency of the plant.

[0015] In the raw material fluid processing plant according to the above aspect, which is equipped with the exhaust gas generation facility, the exhaust gas generation facility may be a reaction gas utilization facility that utilizes the reaction gas as fuel.

[0016] In this embodiment, a reaction gas utilization facility can be provided separate from the exhaust heat utilization facility, and the exhaust heat generated after the reaction gas is utilized in the reaction gas utilization facility can be further utilized in the exhaust heat utilization facility. This allows the energy contained in the reaction gas to be repeatedly recovered, enabling highly efficient energy utilization.

[0017] In the raw material fluid processing plant of the above aspect having the first heat medium heater, the raw material reaction facility may have a first heat medium recovery line that returns the first heat medium after heat exchange with the raw material fluid from the reactor to the first heat medium heater.

[0018] In this embodiment, the first heat medium circulates between the reactor and the first heat medium heater. Therefore, in this embodiment, the temperature difference between the first heat medium flowing out of the first heat medium heater and the first heat medium flowing into the first heat medium heater can be minimized. Therefore, in this embodiment, the amount of heat required to heat the first heat medium can be reduced.

[0019] In the raw material fluid processing plant of the above aspect having the first heat medium recovery line, the reactor may be configured to prevent a phase change between the first heat medium before heat exchange with the raw material fluid and the first heat medium after heat exchange with the raw material fluid.

[0020] In this embodiment, the first heat medium does not undergo a phase change while circulating between the reactor and the first heat medium heater, and therefore, in this embodiment, the amount of heat required to heat the first heat medium can be reduced compared to when the first heat medium undergoes a phase change.

[0021] In any of the above-described aspects of the raw material fluid processing plant having the waste heat utilization heat cycle, at least one of the first heat medium and the second heat medium may be made of the same material as the heat cycle medium.

[0022] In this embodiment, since the first heat medium or the second heat medium is the same material as the heat cycle medium, the quality of the first heat medium or the second heat medium can be easily controlled.

[0023] In the raw material fluid processing plant of the above aspect, in which the first heat medium or the second heat medium is the same material as the thermal cycle medium, the pressure of one of the heat mediums may be lower than the maximum pressure of the thermal cycle medium in the waste heat utilization thermal cycle.

[0024] In this embodiment, the first heat medium can be easily supplied to the reactor or the second heat medium can be easily supplied to the preheater without providing a separate supply facility. In particular, the first heat medium can be easily supplied to the reactor or the second heat medium can be easily supplied to the preheater at the time of start-up or when the pressure of the first heat medium drops due to a seal leak, etc.

[0025] In any of the above-described aspects of the raw material fluid processing plant, the reactor may include a pre-reactor that further heats and reacts the raw material fluid preheated in the preheater to produce a reaction gas, and a post-reactor that further heats the gas from the pre-reactor to react the raw material fluid contained in the gas from the pre-reactor. In this case, the pre-reactor heats the raw material fluid by heat exchange between a first low-temperature heat medium, which is one type of the first heat medium, and the raw material fluid. The post-reactor heats the gas from the pre-reactor by heat exchange between a first high-temperature heat medium, which is one type of the first heat medium and different from the first low-temperature heat medium, and the gas from the pre-reactor. The first heat medium line includes a first low-temperature heat medium line through which the first low-temperature heat medium flows and a first high-temperature heat medium line through which the first high-temperature heat medium flows. The first low-temperature heat medium line is connected to the pre-reactor and introduces the first low-temperature heat medium to the pre-reactor. The first high-temperature heat transfer medium line is connected to the post-reactor and guides the first high-temperature heat transfer medium to the post-reactor.

[0026] In this embodiment, the reaction of the raw material fluid is carried out in two stages, a reaction in the pre-reactor and a reaction in the post-reactor, thereby reducing the concentration of residual raw materials contained in the reaction gas flowing out of the post-reactor. Furthermore, in this embodiment, the temperature of the first heat medium that exchanges heat with the reaction gas in the post-reactor is higher than the temperature of the first heat medium that exchanges heat with the raw material fluid in the pre-reactor, thereby enabling efficient use of heat for the reaction. Furthermore, by dividing the reactor into a pre-reactor and a post-reactor and supplying a heat medium to each, it is possible to input the exact amount of heat required for each temperature level, thereby enabling effective use of heat according to the temperature level.

[0027] In any of the above-described aspects of the raw material fluid processing plant, which is equipped with the waste heat utilization facility and the exhaust gas generation facility, the reactor may include a pre-reactor that further heats and reacts the raw material fluid preheated in the preheater to produce a reaction gas, and a post-reactor that further heats the gas from the pre-reactor to react the raw material fluid contained in the gas from the pre-reactor. In this case, the first heat medium heater includes a first low-temperature heat medium heater that heats the first low-temperature heat medium by heat exchange between the exhaust gas and a first low-temperature heat medium, which is one of the first heat mediums, and a first high-temperature heat medium heater that heats the first high-temperature heat medium by heat exchange between the exhaust gas and a first high-temperature heat medium, which is one of the first heat mediums. The first high-temperature heat medium heater is disposed upstream of the first low-temperature heat medium heater in the flow of the exhaust gas. The first heat medium line includes a first low-temperature heat medium line through which the first low-temperature heat medium flows and a first high-temperature heat medium line through which the first high-temperature heat medium flows. The first low-temperature heat medium line is connected to the first low-temperature heat medium heater and guides the first low-temperature heat medium heated by the exhaust gas to the pre-reactor, and the first high-temperature heat medium line is connected to the first high-temperature heat medium heater and guides the first high-temperature heat medium heated by the exhaust gas to the post-reactor.

[0028] In this embodiment, the reaction of the raw material fluid is carried out in two stages, a reaction in the pre-reactor and a reaction in the post-reactor, thereby reducing the concentration of residual raw materials contained in the reaction gas flowing out of the post-reactor. Furthermore, in this embodiment, the temperature of the first heat medium that exchanges heat with the reaction gas in the post-reactor is higher than the temperature of the first heat medium that exchanges heat with the raw material fluid in the pre-reactor, thereby enabling efficient use of heat for the reaction. Furthermore, by dividing the reactor into a pre-reactor and a post-reactor and supplying a heat medium to each, it is possible to input the exact amount of heat required for each temperature level, thereby enabling effective use of heat according to the temperature level.

[0029] In the raw material fluid processing plant of the above aspect having the pre-reactor and the post-reactor, the waste heat utilization equipment has a waste heat recovery boiler that uses heat of the exhaust gas to steam water, the waste heat recovery boiler has the gas frame, and both the first low-temperature heat medium and the first high-temperature heat medium may be water or steam.

[0030] In any of the above-described aspects of the raw material fluid processing plant having the pre-reactor and the post-reactor, the exhaust heat utilization equipment may include a burner that injects fuel into the exhaust gas flowing in the gas frame to combust the fuel. In this case, the burner is disposed in the gas frame upstream of the first high-temperature heat medium heater in the flow of the exhaust gas. The first high-temperature heat medium heater heats the first high-temperature heat medium by heat exchange between the first high-temperature heat medium and combustion gas generated by combustion of the fuel injected from the burner.

[0031] In this embodiment, a first heat medium having a higher temperature can be obtained than when the first heat medium is heated only by exhaust gas, thereby promoting the reaction of the raw material fluid and reducing the concentration of the raw material fluid contained in the reaction gas.

[0032] In any of the above-described aspects of the raw material fluid processing plant, the waste heat utilization equipment may include a burner that injects the fuel into the exhaust gas flowing through the gas frame to combust the fuel. In this case, the burner is disposed in the gas frame upstream of the first heat medium heater in the flow of the exhaust gas. The first heat medium heater heats the first heat medium by heat exchange between the first heat medium and combustion gas generated by combustion of the fuel injected from the burner.

[0033] In this embodiment, a first heat medium having a higher temperature can be obtained than when the first heat medium is heated only by exhaust gas, thereby promoting the reaction of the raw material fluid and reducing the concentration of the raw material fluid contained in the reaction gas.

[0034] In any of the above-described aspects of the raw material fluid processing plant having the first low-temperature heat transfer medium line and the first high-temperature heat transfer medium line, the product of the constant pressure specific heat and the flow rate of the first low-temperature heat transfer medium flowing through the first low-temperature heat transfer medium line may be greater than the product of the constant pressure specific heat and the flow rate of the first high-temperature heat transfer medium flowing through the first high-temperature heat transfer medium line.

[0035] In this embodiment, a large amount of heat can be input to the temperature level of the reactor that requires a large amount of heat for the reaction of the raw material fluid, and a small amount of heat can be input to the temperature level of the preheater that requires a small amount of heat. Therefore, the amount of heat required for each temperature level can be input without excess or deficiency, and heat can be used effectively according to the temperature level. In particular, when the reaction of most of the raw material fluid occurs in the pre-reactor, the required flow rate of the high-temperature first high-temperature heat transfer medium input to the post-reactor can be reduced, thereby saving high-temperature heat and improving heat utilization efficiency.

[0036] In any of the above-described aspects of the raw material fluid processing plant having the burner, the exhaust heat utilization equipment may have a partition member that divides an upstream side of the first heat medium heater in the gas frame in the flow of the exhaust gas into a first exhaust gas passage through which a portion of the exhaust gas flows and a second exhaust gas passage through which the remaining portion of the exhaust gas flows. In this case, the burner injects the fuel into the first exhaust gas passage.

[0037] In this embodiment, fuel is added to only a portion of the exhaust gas, burned, and used to heat the first heat medium, so the temperature of the first heat medium can be effectively increased with a small amount of reheating fuel, thereby saving reheating fuel and improving plant efficiency.

[0038] In any of the above-described aspects of the raw material fluid processing plant including the reaction gas utilization facility, the raw material reaction facility may include a reaction gas line through which the reaction gas generated in the reactor flows, and a residual raw material removal device that removes residual raw materials, which are raw material fluids contained in the reaction gas flowing through the reaction gas line, and discharges a treated reaction gas, which is a reaction gas from which the residual raw materials have been removed. In this case, the exhaust gas generation facility utilizes the treated reaction gas, which is a part of the reaction gas.

[0039] In this embodiment, it is possible to reduce the amount of raw material remaining in the reaction gas sent to the reaction gas utilization facility.

[0040] In the raw material fluid processing plant having the residual raw material removal device according to the above aspect, the second heat medium may be the reaction gas, and the second heat medium line may be the reaction gas line.

[0041] In this embodiment, heat exchange occurs between the raw material fluid and the reaction gas serving as the second heat transfer medium in the preheater, whereby the raw material fluid is heated while the reaction gas is cooled. Therefore, in this embodiment, a low-temperature reaction gas can be sent to the residual raw material removal unit. Furthermore, by effectively utilizing the waste heat from the reaction gas cooling, plant efficiency can be improved.

[0042] In any of the above-described aspects of the raw material fluid processing plant, the preheater may include a vaporizer that heats and vaporizes the liquid raw material fluid, and a gas heater that heats the gaseous raw material fluid from the vaporizer. In this case, the vaporizer is a heat exchanger that heats the liquid raw material fluid by exchanging heat between a second heat medium for vaporization, which is one type of the second heat medium, and the liquid raw material fluid. Also, the gas heater is a heat exchanger that heats the gaseous raw material fluid by exchanging heat between a second heat medium for gas heating, which is one type of the second heat medium and different from the second heat medium for vaporization, and the gaseous raw material fluid.

[0043] In this embodiment, different heat transfer media are used for vaporizing the raw material fluid, which requires a large amount of heat, and for heating with a gas, which requires a small amount of heat. In this embodiment, the amount of heat required for each temperature level for vaporizing the raw material fluid and heating with a gas can be input in just the right amount, and heat can be used effectively according to the temperature level.

[0044] In the raw material fluid processing plant of the above aspect having the vaporizer and the gas heater, the product of the constant pressure specific heat and the flow rate of the second heat medium for vaporization flowing through the vaporizer may be greater than the product of the constant pressure specific heat and the flow rate of the second heat medium for gas heating flowing through the gas heater.

[0045] In this embodiment, a large amount of heat can be input to the temperature level of the vaporizer, which requires a large amount of heat for vaporizing the raw material fluid, and a small amount of heat can be input to the temperature level of the gas heater, which is sufficient. Therefore, the amount of heat required for each temperature level can be input without excess or deficiency, and heat can be used effectively according to the temperature level, thereby improving heat utilization efficiency.

[0046] In the raw fluid processing plant of the above aspect having the vaporizer and the gas heater, the vaporizer may have the ability to receive the gaseous second heat medium for vaporization, perform heat exchange between the gaseous second heat medium for vaporization and the liquid raw fluid, and cool and condense the gaseous second heat medium for vaporization.

[0047] In this embodiment, the second heat medium for vaporization, which condenses at a constant temperature, is used as a heat source to vaporize the heat source medium at a constant temperature. Therefore, in this embodiment, heat at a relatively low constant temperature is effectively utilized to vaporize the raw material fluid, thereby improving heat utilization efficiency.

[0048] In the raw material fluid processing plant of the above aspect having the vaporizer and the gas heater, the vaporizer may include a liquid-phase preheater that raises the temperature of the liquid raw material fluid while it is still in liquid form, and a phase-change preheater that heats and vaporizes the liquid raw material fluid from the liquid-phase preheater. In this case, the liquid-phase preheater is a heat exchanger that heats the liquid raw material fluid by exchanging heat between the liquid-phase preheating second heat medium, which is one type of the vaporization second heat medium, and the liquid raw material fluid. The phase-change preheater is a heat exchanger that heats the liquid raw material fluid from the liquid-phase preheater by exchanging heat between the liquid-phase preheating second heat medium, which is one type of the vaporization second heat medium and different from the liquid-phase preheating second heat medium, and the liquid raw material fluid.

[0049] In this embodiment, the vaporizer is divided into a section for vaporizing the liquid-phase raw material fluid and a section for preheating the raw material fluid while it is in the liquid phase. Different heat transfer media are used for vaporizing the raw material fluid, which requires a large amount of heat, and for heating the raw material fluid while it is in the liquid phase, which requires a small amount of heat. Therefore, in this embodiment, the amount of heat required for each temperature level for vaporizing the raw material fluid and heating the raw material fluid while it is in the liquid phase can be input in just the right amount, and heat can be used effectively according to the temperature level.

[0050] In the raw material fluid processing plant of the above aspect having the liquid phase preheater and the phase change preheater, the product of the constant pressure specific heat and the flow rate of the second heat medium for phase change preheating flowing in the phase change preheater may be greater than the product of the constant pressure specific heat and the flow rate of the second heat medium for liquid phase preheating flowing in the liquid phase preheater.

[0051] In this embodiment, a large amount of heat can be input to the temperature level of the phase-change preheater, which requires a large amount of heat for vaporizing the raw material fluid, and a small amount of heat can be input to the temperature level of the liquid-phase preheater, which requires only a small amount of heat. Therefore, the amount of heat required for each temperature level can be input without excess or deficiency, and heat can be used effectively according to the temperature level, thereby improving heat utilization efficiency.

[0052] In the raw material fluid processing plant of the above aspect having the liquid phase preheater and the phase change preheater, the phase change preheater may have the ability to receive the gaseous phase change preheating second heat medium, perform heat exchange between the gaseous phase change preheating second heat medium and the liquid raw material fluid from the liquid phase preheater, and cool and condense the gaseous phase change preheating second heat medium.

[0053] In this embodiment, the raw material fluid can be vaporized at a constant temperature using the phase-change preheating second heat medium, which condenses at a constant temperature, as a heat source. Therefore, in this embodiment, the raw material fluid can be vaporized by effectively utilizing heat at a relatively low constant temperature, thereby improving heat utilization efficiency.

[0054] The raw material fluid processing plant according to any of the above aspects, which has a waste heat utilization thermal cycle, may include one or more thermal cycles. In this case, the one or more thermal cycles include the waste heat utilization thermal cycle through which the thermal cycle medium circulates. The raw material reaction facility has a second heat medium recovery line through which the second heat medium flows. The second heat medium is at least a part of the first heat cycle medium flowing in a first thermal cycle of the one or more thermal cycles. The second heat medium line guides the first heat cycle medium flowing in a first section of the first thermal cycle to the preheater as the second heat medium. The second heat medium recovery line guides the first heat cycle medium cooled by heat exchange with the raw material fluid to a second section through which the first heat cycle medium, which has a lower temperature than the first heat cycle medium flowing in the section in the first thermal cycle, flows.

[0055] In this embodiment, the first heat cycle medium flowing in the first heat cycle can be used to preheat the raw material fluid.

[0056] In the raw material fluid processing plant having the first heat cycle, the first heat cycle may be the waste heat utilization heat cycle, in which case the first heat cycle medium is water or steam as the heat cycle medium circulating in the waste heat utilization heat cycle.

[0057] In any of the above-described aspects of the raw material fluid processing plant, the raw material fluid processing plant may include a second heat medium heater located within the gas frame downstream of the first heat medium heater in the flow direction of the exhaust gas, and configured to heat at least a portion of the heat cycle medium by heat exchange between the first heat medium heater and the exhaust gas. In this case, the raw material reaction facility may include a second heat medium recovery line through which the second heat medium flows. The second heat medium line guides at least a portion of the heat cycle medium heated by the second heat medium heater to the preheater as the second heat medium. The second heat medium recovery line guides the heat cycle medium cooled by the preheater to a portion of the second heat medium heater in the exhaust heat utilization heat cycle where the heat cycle medium flows. The second heat medium recovery line guides the heat cycle medium, which has a temperature lower than that of the heat cycle medium, in the second heat medium heater.

[0058] In this embodiment, a part of the heat cycle medium circulating in the exhaust heat utilization heat cycle is heated by the exhaust gas EG, and this heat cycle medium is used as the second heat medium. Therefore, in this embodiment, it is easy to manage the quality of the second heat medium.

[0059] The feedstock fluid processing plant of any of the above aspects may include a Brayton cycle in which a gaseous working medium circulates. The Brayton cycle includes a medium compressor that compresses the working medium, a medium heater that heats the working medium compressed by the medium compressor, a medium turbine driven by the working medium heated by the medium heater, and a medium cooler that cools the working medium exhausted from the medium turbine. In this case, the feedstock reaction facility includes a second heat medium recovery line through which the second heat medium flows. The medium cooler constitutes at least a part of the preheater. The second heat medium line guides the working medium exhausted from the medium turbine to the medium cooler as the second heat medium. The second heat medium recovery line guides the working medium cooled by heat exchange with the feedstock fluid in the medium cooler to the medium compressor as the second heat medium.

[0060] In this embodiment, the working fluid is cooled by heat exchange between the feed fluid and the working fluid in the medium cooler that constitutes a part of the preheater. Therefore, in this embodiment, the heat of the feed fluid can be utilized to operate the Brayton cycle, thereby increasing the output of the plant.

[0061] In any of the above-described aspects of the raw material fluid processing plant including the exhaust heat utilization facility having the gas frame, the preheater may be a heat exchanger that is disposed in the gas frame downstream of the first heat medium heater in the flow of the exhaust gas and heats the raw material fluid by exchanging heat between the raw material fluid and the exhaust gas serving as the second heat medium. In this case, the second heat medium line is configured to include a part of the gas frame.

[0062] In this embodiment, the heat of the exhaust gas from which most of the heat has been removed, i.e., the low-temperature exhaust gas, is used to preheat the raw material fluid, and therefore, in this embodiment, the heat of the low-temperature exhaust gas can be effectively utilized.

[0063] In the raw material fluid processing plant of the above aspect, where the preheater is arranged in the gas frame, the exhaust heat utilization equipment may have one or more evaporators arranged in the gas frame and performing heat exchange between the liquid phase heat cycle medium and the exhaust gas to convert the liquid phase heat cycle medium into the gas phase heat cycle medium. In this case, the preheater is arranged in the gas frame downstream of the most downstream evaporator among the one or more evaporators. At least one of the one or more evaporators is arranged between the first heat medium heater and the preheater in the flow direction of the exhaust gas.

[0064] The raw material fluid processing plant of the above aspect having the residual material removal device may also include a thermal cycle through which a third heat medium flows and which utilizes the heated third heat medium. In this case, the raw material reaction facility includes a third heat medium line and a third heat medium recovery line connected to the thermal cycle, and a reaction gas cooler for cooling the reaction gas. The reaction gas cooler is provided in the reaction gas line and performs heat exchange between the reaction gas flowing through the reaction gas line and the third heat medium, thereby cooling the reaction gas and heating the third heat medium. The third heat medium line guides at least a portion of the third heat medium before being heated from the thermal cycle to the reaction gas cooler. The third heat medium recovery line guides the third heat medium after being heated in the reaction gas cooler to the thermal cycle. The residual material removal device removes the residual materials from the reaction gas cooled by the reaction gas cooler.

[0065] In this embodiment, the cooled reaction gas RG can be sent to the residual raw material removal device. Also, in this embodiment, the exhaust heat from the reaction gas cooling can be effectively utilized to send a heated third heat medium to the heat cycle, thereby improving the efficiency of the plant.

[0066] In the raw material fluid processing plant of the above aspect, which includes the thermal cycle using the third heat medium, the exhaust gas generation facility may include a gas turbine. The gas turbine includes an air compressor that compresses air to generate combustion air, a combustor that burns the treated reaction gas as fuel in the combustion air to generate combustion gas, and a turbine that is driven by the combustion gas and discharges the combustion gas as the exhaust gas. The thermal cycle is a gas turbine cycle configured with the gas turbine included in the exhaust gas generation facility. The third heat medium line guides the treated reaction gas from the residual material removal device to the reaction gas cooler as the third heat medium. The third heat medium recovery line guides the treated gas after being heated in the reaction gas cooler to the combustor.

[0067] In this embodiment, the reaction gas cooler exchanges heat between the reaction gas and the treated reaction gas as fuel, cooling the reaction gas while heating the fuel. Therefore, in this embodiment, cooled reaction gas can be sent to the residual raw material removal device, and preheated fuel can be sent to the combustor, thereby improving plant efficiency. Furthermore, by removing residual raw materials remaining in the reaction gas in the residual raw material removal device, the concentration of residual raw materials in the fuel sent to the combustor can be reduced, thereby reducing the generation of air pollutants caused by the residual raw materials in the fuel.

[0068] In the raw material fluid processing plant of the above aspect, which is equipped with the thermal cycle utilizing the third heat medium, the exhaust gas generation facility may include a gas turbine. The gas turbine includes an air compressor that compresses air to generate combustion air, a combustor that burns the treated reaction gas as fuel in the combustion air to generate combustion gas, and a turbine that is driven by the combustion gas and discharges the combustion gas as the exhaust gas. The thermal cycle is a gas turbine cycle configured with the gas turbine included in the exhaust gas generation facility. The third heat medium line guides the combustion air from the air compressor to the reaction gas cooler as the third heat medium. The third heat medium recovery line guides the combustion air after being heated in the reaction gas cooler to the combustor.

[0069] In this embodiment, the reaction gas cooler exchanges heat between the reaction gas and the combustion air, thereby cooling the reaction gas and heating the combustion air, thereby enabling cooled reaction gas to be sent to the residual raw material removal device and preheated combustion air to be sent to the combustor.

[0070] In the raw material fluid processing plant of the above aspect, which includes the thermal cycle that uses the third heat medium, the exhaust gas generation equipment may include a gas turbine driven by the treated reaction gas as fuel. The waste heat utilization equipment includes a heat recovery boiler that evaporates water by utilizing heat from the exhaust gas exhausted from the gas turbine, a steam turbine driven by steam from the heat recovery boiler, a condenser that converts the steam exhausted from the steam turbine back into water, and a feedwater pump that sends water in the condenser to the heat recovery boiler. The thermal cycle is a Rankine cycle that includes the heat recovery boiler, the steam turbine, the condenser, and the feedwater pump. The third heat medium line guides at least a portion of the water or steam flowing through a first section of the Rankine cycle to the reaction gas cooler as the third heat medium. The third heat medium recovery line guides the water or steam heated in the reaction gas cooler to a second section of the Rankine cycle, where water or steam flows at a temperature higher than that of the water or steam flowing through the first section.

[0071] In this embodiment, the reaction gas cooler exchanges heat between the reaction gas and water or steam flowing through the Rankine cycle, thereby cooling the reaction gas and heating the water or steam. Therefore, in this embodiment, the cooled reaction gas can be sent to the residual raw material removal device, and heated water or steam can be returned to the Rankine cycle, thereby improving the thermal efficiency of the Rankine cycle.

[0072] The feedstock fluid processing plant according to the above aspect, which includes the thermal cycle using the third heat medium, may also include a low-boiling-point medium Rankine cycle in which a low-boiling-point medium having a boiling point lower than that of water is circulated. The low-boiling-point medium Rankine cycle includes a medium booster that increases the pressure of the liquid-phase low-boiling-point medium, a medium heater that heats the liquid-phase low-boiling-point medium pressurized by the medium booster to convert it into a gas-phase low-boiling-point medium, a medium turbine driven by the gas-phase low-boiling-point medium from the medium heater, and a medium cooler that cools and condenses the gas-phase low-boiling-point medium exhausted from the medium turbine. The thermal cycle is the low-boiling-point medium Rankine cycle. The reaction gas cooler constitutes the medium heater. The third heat medium line leads the liquid-phase low-boiling-point medium pressurized by the medium booster as the third heat medium to the reaction gas cooler that constitutes the medium heater. The third heat medium recovery line guides the gas-phase low-boiling-point medium from the reaction gas cooler to the medium turbine.

[0073] In this embodiment, the reaction gas cooler, which serves as a medium heater for the low-boiling-point medium Rankine cycle, exchanges heat between the reaction gas and the low-boiling-point medium to cool the reaction gas while heating the low-boiling-point medium. Thus, in this embodiment, the heat of the reaction gas can be utilized to operate the low-boiling-point medium Rankine cycle, thereby increasing the output of the plant.

[0074] The feedstock fluid processing plant of the above aspect, which includes the thermal cycle utilizing the third heat medium, may also include a Brayton cycle in which a gaseous working medium circulates. The Brayton cycle includes a medium compressor that compresses the working medium, a medium heater that heats the working medium compressed by the medium compressor, a medium turbine driven by the working medium heated by the medium heater, and a medium cooler that cools the working medium exhausted from the medium turbine. The thermal cycle is the Brayton cycle. The reaction gas cooler constitutes the medium heater. The third heat medium line guides the working medium from the medium compressor as the third heat medium to the reaction gas cooler that constitutes the medium heater. The third heat medium recovery line guides the working medium from the reaction gas cooler to the medium turbine.

[0075] In this embodiment, the reaction gas cooler, which serves as a medium heater for the Brayton cycle, exchanges heat between the reaction gas and the working medium, thereby cooling the reaction gas and heating the working medium. Thus, in this embodiment, the heat of the reaction gas can be used to operate the Brayton cycle, thereby increasing the output of the plant.

[0076] In the raw material fluid processing plant according to any of the above aspects, the raw material reaction facility may include an oxidant introducing device that introduces an oxidant for causing an oxidation reaction of the raw material fluid into the raw material fluid after it has passed through the preheater.

[0077] In this embodiment, a part of the raw material fluid undergoes an oxidation reaction with the oxidant to generate heat, which increases the temperature of the raw material fluid, promoting the reaction of the raw material fluid and reducing the concentration of the raw material fluid in the reaction gas.

[0078] In the raw material fluid processing plant of the above aspect having the oxidant feeding device, the reactor may include a pre-reactor that further heats and reacts the raw material fluid preheated in the preheater to generate a reaction gas, and a post-reactor that further reacts the raw material fluid contained in the gas from the pre-reactor. In this case, the oxidant feeding device feeds the oxidant to at least one of the raw material fluid after passing through the pre-reactor but before flowing out from the pre-reactor, and the gas that has passed through the pre-reactor but before flowing out from the post-reactor.

[0079] In any of the above-described aspects of the raw material fluid processing plant having the oxidant introduction device, the oxidant introduction device may include a compressor that compresses air to generate compressed air. In this case, the oxidant introduction device introduces the compressed air as the oxidant into the raw material fluid after passing through the preheater.

[0080] The feedstock fluid processing plant of the above aspect, in which the oxidant injection device has the compressor, may further include a gas turbine. The gas turbine has an air compressor that compresses air to generate combustion air, a combustor that burns fuel in the combustion air to generate combustion gas, and a turbine that is driven by the combustion gas and discharges the combustion gas as exhaust gas. At least a part of the compressor of the oxidant injection device is the air compressor of the gas turbine. The oxidant injection device injects a part of the combustion air from the air compressor as the oxidant into the feedstock fluid after passing through the preheater.

[0081] In order to achieve the above object, a raw material fluid processing plant according to another aspect of the invention comprises: The system includes a raw material reaction facility that heats and reacts a raw material fluid to produce a reaction gas, and a thermal cycle through which a third heat medium flows and utilizes the heated third heat medium. The raw material reaction facility includes a reactor that heats and reacts the raw material fluid to produce a reaction gas, a reaction gas line through which the reaction gas produced in the reactor flows, a third heat medium line and a third heat medium recovery line connected to the thermal cycle, and a reaction gas cooler that cools the reaction gas. The reaction gas cooler is provided in the reaction gas line and exchanges heat between the reaction gas flowing through the reaction gas line and the third heat medium, thereby cooling the reaction gas and heating the third heat medium. The third heat medium line guides at least a portion of the third heat medium before being heated from the thermal cycle to the reaction gas cooler. The third heat medium recovery line guides the third heat medium after being heated in the reaction gas cooler to the thermal cycle.

[0082] According to this aspect, the third heat medium can be heated with the exhaust heat from the reaction gas cooler and used in the heat cycle, so that the exhaust heat can be effectively utilized and the efficiency of the plant can be improved.

[0083] In the raw material fluid processing plant of the other aspect, the reaction gas cooler may have a capacity to heat the third heat medium to a temperature higher than the temperature of the raw material fluid at the raw material fluid inlet of the reactor.

[0084] According to this aspect, even when a large amount of heat is required for the reaction in the reactor, the temperature of the medium in the thermal cycle can be increased to the temperature level of the reactor by utilizing the exhaust heat from the reaction gas cooler, thereby improving the efficiency of the thermal cycle and further increasing the efficiency of the plant.

[0085] The raw material fluid processing plant according to the other aspect may further include an exhaust gas generation facility that generates exhaust gas by combusting the reaction gas generated in the raw material reaction facility.

[0086] According to this aspect, the generated reaction gas is effectively utilized, and the efficiency of the plant is improved.

[0087] In any of the above-described aspects of the raw material fluid processing plant, the exhaust gas generation facility may include a gas turbine having an air compressor that compresses air to generate combustion air, a combustor that burns the reaction gas as fuel in the combustion air to generate combustion gas, and a turbine that is driven by the combustion gas and discharges the combustion gas as exhaust gas.

[0088] In the raw material fluid processing plant of any of the above aspects, the waste heat utilization equipment may include a heat recovery boiler that evaporates water by utilizing heat from exhaust gas as the heat source, a steam turbine that is driven by steam from the heat recovery boiler, a condenser that converts the steam exhausted from the steam turbine back into water, a feedwater line that introduces water in the condenser to the heat recovery boiler, and a feedwater pump provided in the feedwater line. The heat recovery boiler has the gas frame through which the exhaust gas flows.

[0089] In the raw material fluid processing plant of the above aspect having the feedwater line, the exhaust heat utilization equipment may have a feedwater preheater that heats the water by exchanging heat between the water flowing through the feedwater line and steam extracted from the steam turbine.

[0090] In this embodiment, the feedwater preheater can heat the water flowing through the feedwater line. Therefore, in this embodiment, the temperature of the feedwater flowing into the heat recovery boiler can be increased. When the temperature of the feedwater flowing into the heat recovery boiler is increased, the amount of heat exchange between the water or steam and the exhaust gas can be reduced in each economizer, evaporator, and heater in the heat recovery boiler. Therefore, this embodiment is preferably employed when the amount of heat required to heat the raw material fluid is small.

[0091] In any of the above aspects of the raw material fluid processing plant, the raw material fluid may be ammonia. In this case, the reactor heats the ammonia to cause a thermal decomposition reaction, thereby generating a reaction gas containing nitrogen and hydrogen.

[0092] In order to achieve the above object, one aspect of the present invention relates to a method for treating a raw material fluid, A raw material reaction process is carried out in which a raw material fluid is heated and reacted to generate a reaction gas. The raw material reaction process includes a raw material preheating process and a reaction execution process. In the raw material preheating process, a second heat medium and the raw material fluid are heat-exchanged to heat the raw material fluid. In the reaction execution process, the raw material fluid heated in the raw material preheating process is heat-exchanged with a first heat medium different from the second heat medium to further heat and react the raw material fluid to generate a reaction gas.

[0093] In order to achieve the above object, another aspect of the present invention relates to a method for treating a raw material fluid, The system includes a raw material reaction step of heating and reacting a raw material fluid to produce a reaction gas, and a thermal cycle execution step of flowing a third heat medium and utilizing the heated third heat medium. The raw material reaction step includes a reaction execution step of heating and reacting the raw material fluid to produce a reaction gas, and a reaction gas cooling step of cooling the reaction gas produced in the reaction execution step. In the reaction gas cooling step, heat is exchanged between at least a portion of the third heat medium before heating and the reaction gas, thereby cooling the reaction gas and heating the third heat medium. In the thermal cycle execution step, the third heat medium heated in the reaction gas cooling step is utilized. [Effects of the Invention]

[0094] According to one aspect of the present invention, when reacting raw material fluids, it is possible to suppress the loss of thermal energy from a heat source such as exhaust gas, thereby improving the thermal efficiency of the plant. [Brief explanation of the drawings]

[0095] [Figure 1] 1 is a system diagram of a raw material fluid processing plant in a first embodiment according to the present invention. [Figure 2] 3 is a flowchart showing an operation of the gas utilization plant in the first embodiment according to the present invention. [Figure 3] FIG. 1 is a TQ diagram of ammonia and a heat source in a reference example. [Figure 4] FIG. 2 is a TQ diagram of ammonia and a heat source in the first embodiment. [Figure 5] FIG. 4 is a system diagram of a raw material fluid processing plant in a second embodiment according to the present invention. [Figure 6] FIG. 10 is a system diagram of a raw material fluid processing plant in a third embodiment according to the present invention. [Figure 7] FIG. 10 is a TQ diagram of ammonia and a heat source in the third embodiment. [Figure 8] FIG. 11 is a TQ diagram of ammonia and a heat source in a modified example of the third embodiment. [Figure 9]FIG. 10 is a system diagram of a raw material fluid processing plant in a fourth embodiment according to the present invention. [Figure 10] FIG. 10 is a TQ diagram of ammonia and a heat source in the fourth embodiment. [Figure 11] FIG. 10 is a system diagram of a raw material fluid processing plant in a fifth embodiment according to the present invention. [Figure 12] FIG. 10 is a system diagram of a raw material fluid processing plant in a sixth embodiment according to the present invention. [Figure 13] FIG. 10 is a system diagram of a raw material fluid processing plant in a seventh embodiment according to the present invention. [Figure 14] FIG. 10 is a system diagram of a raw material fluid processing plant in an eighth embodiment according to the present invention. [Figure 15] FIG. 10 is a system diagram of a Brayton cycle, a heat cycle, and a low-boiling-point medium Rankine cycle in an eighth embodiment according to the present invention. [Figure 16] FIG. 13 is a system diagram of a raw material fluid processing plant in a ninth embodiment according to the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0096] Hereinafter, various embodiments and modifications of the raw material fluid processing plant according to the present invention will be described with reference to the drawings.

[0097] "First embodiment" A first embodiment of a raw material fluid processing plant will be described with reference to FIGS.

[0098] As shown in FIG. 1, the raw material fluid processing plant of this embodiment includes a raw material reaction facility 40 that reacts a raw material fluid NH to generate a reaction gas RG, a reaction gas utilization facility 10 that utilizes the reaction gas RG, and a waste heat utilization facility 20 that utilizes the heat of an exhaust gas EG from the reaction gas utilization facility 10.

[0099] The raw material fluid NH in this embodiment is ammonia. The raw material reaction equipment 40 thermally decomposes ammonia, which is the raw material fluid NH, to generate a reaction gas RG containing hydrogen and nitrogen. The reaction gas utilization equipment 10 is a gas turbine equipment including a gas turbine 11 that uses the reaction gas RG as fuel. Note that the reaction gas utilization equipment 10 in this embodiment and the reaction gas utilization equipment in each of the following embodiments are also exhaust gas generation equipment that generates exhaust gas EG. The exhaust heat utilization equipment 20 has a waste heat recovery boiler 21 that generates steam by utilizing the heat of the exhaust gas EG exhausted from the gas turbine 11, and steam turbines 31, 32, 33, etc. that are driven by this steam.

[0100] The raw material reaction equipment 40 includes a raw material reactor 41 and a residual raw material removal device 130. The raw material reactor 41 generates a reaction gas RG containing hydrogen, nitrogen, and residual ammonia by thermal decomposition of liquid ammonia NH, which is a raw material fluid. The residual raw material removal device 130 removes the residual raw material (residual ammonia) from the reaction gas RG, and discharges a treated reaction gas RGp, which is the reaction gas RG from which the residual raw material has been removed.

[0101] The raw material reactor 41 includes an ammonia supply line 42 through which liquid ammonia NH or gaseous ammonia NHg flows from an ammonia tank T, a raw material ammonia pump 43, preheaters 44a and 44b, a reactor 45, a reaction gas cooler 46, a reaction gas line 47, a first heat medium line 51, a first heat medium recovery line 52, and a first heat medium booster 53. Liquid ammonia NH is stored in the ammonia tank T. The liquid ammonia NH is produced using, for example, hydrogen as a raw material. This hydrogen is obtained by electrolyzing water using electricity generated by renewable energy sources such as wind power or solar power, or by steam reforming natural gas. Hydrogen is not as easy to transport or store as liquefied natural gas. Therefore, the hydrogen obtained as described above is used to produce liquid ammonia NH, which is easy to transport and store, and this liquid ammonia NH is stored in the ammonia tank T.

[0102] The ammonia supply line 42 has a first ammonia supply line 42a, a second ammonia supply line 42b, and a third ammonia supply line 42c. One end of the first ammonia supply line 42a is connected to the ammonia tank T. The preheaters 44a and 44b include a first preheater 44a and a second preheater 44b. The other end of the first ammonia supply line 42a is connected to an ammonia inlet of the first preheater 44a. The first preheater 44a is a heat exchanger. The first preheater 44a exchanges heat between liquid ammonia NH and a second heat medium, heating the liquid ammonia NH to gaseous ammonia NHg while cooling the second heat medium. One end of the second ammonia supply line 42b is connected to an ammonia outlet of the first preheater 44a, and the other end of the second ammonia supply line 42b is connected to an ammonia inlet of the second preheater 44b. The second preheater 44b is a heat exchanger. The second preheater 44b performs heat exchange between the gaseous ammonia NHg and the second heat medium to heat the gaseous ammonia NHg while cooling the second heat medium. One end of the third ammonia supply line 42c is connected to an ammonia outlet of the second preheater 44b, and the other end of the third ammonia supply line 42c is connected to an ammonia inlet of the reactor 45.

[0103] A first heat medium line 51 is connected to the medium inlet of the reactor 45. A first heat medium recovery line 52 is connected to the medium outlet of the reactor 45. A first heat medium booster 53 is provided on the first heat medium recovery line 52. The reactor 45 is a heat exchanger. A catalyst for promoting the thermal decomposition reaction of the raw material fluid is disposed in the region through which the raw material fluid passes in the reactor 45. As described above, the raw material fluid is ammonia. No catalyst is disposed in the preheaters 44a and 44b, but a catalyst is disposed in the reactor 45. That is, the catalyst is disposed only in the region where the temperature of the raw material fluid is high enough to actively promote the reaction, and is not disposed in the low-temperature region where the reaction does not proceed even if a catalyst is disposed. As a result, the reaction can be effectively promoted with a small amount of catalyst, thereby reducing the cost of the catalyst. Furthermore, the raw material fluid undergoes an endothermic reaction in the reactor 45. According to this embodiment, the heat required for the endothermic reaction can be efficiently supplied. The reactor 45 exchanges heat between the gaseous ammonia NHg heated in the second preheater 44b and the first heat medium from the first heat medium line 51 to further heat the gaseous ammonia NHg while cooling the first heat medium. The cooled first heat medium flows into the first heat medium recovery line 52. The gaseous ammonia NHg heated in the reactor 45 undergoes a thermal decomposition reaction to become a reaction gas RG containing hydrogen, nitrogen, and residual ammonia. The reaction gas line 47 includes a first reaction gas line 47a, a second reaction gas line 47b, and a third reaction gas line 47c. One end of the first reaction gas line 47a is connected to the reaction gas outlet of the reactor 45. The other end of the first reaction gas line 47a is connected to the second heat medium inlet of the second preheater 44b. One end of the second reaction gas line 47b is connected to the second heat medium outlet of the second preheater 44b, and the other end of the second reaction gas line 47b is connected to the second heat medium inlet of the first preheater 44a. One end of the third reactant gas line 47c is connected to the second heat medium outlet of the first preheater 44a, and the other end of the third reactant gas line 47c is connected to the residual raw material removal device 130. Therefore, in this embodiment, the reactant gas RG serves as the second heat medium. Also, in this embodiment, the second heat medium line that guides the reactant gas RG, which serves as the second heat medium, to the first preheater 44a and the second preheater 44b is the reactant gas line 47.The reaction gas cooler 46 is provided on the third reaction gas line 47c and cools the reaction gas RG flowing through the third reaction gas line 47c.

[0104] The residual raw material removal apparatus 130 includes an absorption tower 131, a regeneration tower 132, an ammonia water line 133, a water line 134, a water supply pump 135, a heat exchanger 136, a water circulation line 137, a condenser 138, a reboiler 139, a recovered ammonia line 140, and a recovered ammonia booster 141.

[0105] The other end of the reaction gas line 47 is connected to the lower part of the absorption tower 131. One end of the water line 134 is connected to the upper part of the absorption tower 131. Water is sprayed from the water line 134 into the absorption tower 131, and the reaction gas RG flows in from the reaction gas line 47. In the absorption tower 131, the water and the reaction gas RG come into contact with each other, and residual ammonia in the reaction gas RG dissolves in the water. As a result, ammonia water, which is water in which the residual ammonia has been dissolved, accumulates in the lower part of the absorption tower 131. Meanwhile, the treated reaction gas RGp, which is the reaction gas RG from which the residual ammonia has been removed, rises in the absorption tower 131. The concentration of gaseous ammonia NHg dissolved in water increases as the temperature in the absorption tower 131 decreases. For this reason, in this embodiment, the reaction gas RG flowing out from the reactor 45 is cooled sequentially in the second preheater 44b, the first preheater 44a, and the reaction gas cooler 46 before being introduced into the absorption tower 131.

[0106] An ammonia water line 133 connects the bottom of the absorption tower 131 and the top of the regeneration tower 132. The ammonia water accumulated in the absorption tower 131 is guided into the regeneration tower 132 via this ammonia water line 133. One end of a water circulation line 137 is connected to the bottom of the regeneration tower 132, and the other end of the water circulation line 137 is connected to the lower part (above the bottom) of the regeneration tower 132. A reboiler 139 is provided on this water circulation line 137. The reboiler 139 exchanges heat between steam from the exhaust heat utilization equipment 20 and water from the water circulation line 137, cooling and condensing the steam to produce heated water, while heating the water from the water circulation line 137 to produce steam. This steam flows into the regeneration tower 132 via the water circulation line 137. In the regeneration tower 132, the ammonia water is heated by the steam, and the ammonia in the ammonia water is separated and distilled as gaseous ammonia NHg. The water in the ammonia water accumulates in the regenerator 132. A portion of the water accumulated in the regenerator 132 flows into the regenerator 132 as steam via a water circulation line 137 and a reboiler 139. The other end of the water line 134 described above is connected to the water circulation line 137 or the reboiler 139. Therefore, the remainder of the water accumulated in the regenerator 132 is sent to the absorption tower 131 via the water line 134. A water supply pump 135 is provided on this water supply line. A heat exchanger 136 exchanges heat between the water flowing through the water line 134 and the ammonia water flowing through the ammonia water line 133, thereby cooling the water and heating the ammonia water.

[0107] One end of the recovered ammonia line 140 is connected to the top of the regeneration tower 132, and the other end of the recovered ammonia line 140 is connected to the second ammonia supply line 42b, through which gaseous ammonia NHg flows. The recovered ammonia line 140 is provided with a condenser 138 and a recovered ammonia booster 141. A gas containing gaseous ammonia NHg and moisture flows from the regeneration tower 132 into the condenser 138. The condenser 138 condenses moisture contained in the gas from the regeneration tower 132 and returns this moisture to the regeneration tower 132. The gas from which moisture has been removed in the condenser 138 and whose concentration of gaseous ammonia NHg has increased is pressurized by the recovered ammonia booster 141 and then flows into the second preheater 44b via the recovered ammonia line 140 and the second ammonia supply line 42b.

[0108] The reaction gas utilization facility 10 includes the gas turbine 11 described above, as well as a fuel line 12 and a fuel preheater 13 .

[0109] The gas turbine 11 includes an air compressor 11a that compresses air to generate combustion air, a combustor 11c that burns fuel in the combustion air to generate combustion gas, and a turbine 11d that is driven by the combustion gas. The air compressor 11a includes a compressor rotor and a compressor casing that covers the compressor rotor. The turbine 11d includes a turbine rotor and a turbine casing that covers the turbine rotor. The compressor rotor and turbine rotor are connected to each other to form a gas turbine rotor. A generator, for example, is connected to one end of the gas turbine rotor.

[0110] One end of the fuel line 12 is connected to the top of the absorption tower 131, and the other end of the fuel line 12 is connected to the combustor 11c. Thus, the treated reaction gas RGp generated in the absorption tower 131 is sent to the combustor 11c as fuel. A fuel preheater 13 is provided on the fuel line 12. The fuel preheater 13 heats the treated reaction gas RGp as fuel. The treated reaction gas RGp heated by the fuel preheater 13 flows into the combustor 11c.

[0111] The reaction gas utilization facility 10 described above has a gas turbine cycle, which is a type of thermal cycle. This gas turbine cycle is configured with a fuel line 12, a fuel preheater 13, and a gas turbine 11.

[0112] The waste heat utilization facility 20 includes the above-mentioned waste heat recovery boiler 21 and steam turbines 31, 32, and 33, as well as a condenser 34, a water supply line 35, a water supply pump 36, and a chimney 39.

[0113] The waste heat utilization equipment 20 of this embodiment includes steam turbines 31, 32, and 33: a low-pressure steam turbine 31, an intermediate-pressure steam turbine 32, and a high-pressure steam turbine 33. Each of the steam turbines 31, 32, and 33 includes a turbine rotor and a turbine casing that covers the turbine rotor. The turbine rotors of the steam turbines 31, 32, and 33 are connected to each other to form a single steam turbine rotor. A generator, for example, is connected to one end of the steam turbine rotor. A condenser 34 is connected to the low-pressure steam turbine 31. The condenser 34 converts steam exhausted from the low-pressure steam turbine 31 back into water. A feedwater line 35 connects the condenser 34 to the heat recovery steam generator 21. A feedwater pump 36 is provided in the feedwater line 35. The feedwater pump 36 sends water from the condenser 34 to the heat recovery steam generator 21 via the feedwater line 35.

[0114] The heat recovery boiler 21 has a gas frame 22, a first low-pressure economizer 23a, a second low-pressure economizer 23b, a low-pressure evaporator 23c, a low-pressure superheater 23f, a medium-pressure economizer 24a, a medium-pressure evaporator 24b, a first high-pressure economizer 25a, a second high-pressure economizer 25b, a high-pressure evaporator 25c, a high-pressure superheater 25d, a medium-pressure pump 24p, a high-pressure pump 25p, and a first heat medium heater 27.

[0115] Exhaust gas EG discharged from the gas turbine 11 flows inside the gas frame 22. This gas frame 22 has an inlet and an outlet. The inlet of the gas frame 22 is connected to the exhaust port of the turbine 11d. The outlet of the gas frame 22 is connected to a chimney 39. The exhaust gas EG flows inside the gas frame 22 from the inlet to the outlet. Here, the side where the inlet is located relative to the outlet is referred to as the upstream side, and the opposite side is referred to as the downstream side.

[0116] The first heat medium heater 27, the high-pressure superheater 25d, a part of the high-pressure evaporator 25c, the second high-pressure economizer 25b, the low-pressure superheater 23f, a part of the intermediate-pressure evaporator 24b, the intermediate-pressure economizer 24a and the first high-pressure economizer 25a, a part of the low-pressure evaporator 23c, the second low-pressure economizer 23b, and the first low-pressure economizer 23a are arranged in the above order from upstream to downstream in the gas frame 22. The intermediate-pressure economizer 24a is arranged at substantially the same position as the first high-pressure economizer 25a in the flow direction of the exhaust gas EG.

[0117] A water supply line 35 is connected to the first low-pressure economizer 23a. The first low-pressure economizer 23a heats the water from the water supply line 35 by exchanging heat with the exhaust gas EG. The second low-pressure economizer 23b further heats the water from the first low-pressure economizer 23a by exchanging heat with the exhaust gas EG, thereby producing low-pressure heated water. The low-pressure evaporator 23c heats the low-pressure heated water by exchanging heat with the exhaust gas EG, thereby heating the low-pressure heated water to produce steam. The low-pressure superheater 23f heats the steam from the low-pressure evaporator 23c by exchanging heat with the exhaust gas EG, thereby heating the steam to produce low-pressure steam. One end of a low-pressure steam line 88 is connected to an outlet of the low-pressure superheater 23f. The other end of the low-pressure steam line 88 is connected to an inlet of the low-pressure steam turbine 31.

[0118] The medium-pressure pump 24p pressurizes the low-pressure heating water. The medium-pressure economizer 24a exchanges heat between the heated water pressurized by the medium-pressure pump 24p and the exhaust gas EG, further heating the heated water to produce medium-pressure heated water. An outlet of the medium-pressure economizer 24a is connected to an inlet of the medium-pressure evaporator 24b and to a medium-pressure heating water line 77. This medium-pressure heating water line 77 is connected to a medium inlet of the fuel preheater 13 described above. The fuel preheater 13 exchanges heat between the medium-pressure heating water from the medium-pressure heating water line 77 and the treated reaction gas RGp used as fuel, heating the treated reaction gas RGp while cooling the medium-pressure heating water. A heated water recovery line 78 is connected to a medium outlet of the fuel preheater 13. This heated water recovery line 78 is connected to the water supply line 35.

[0119] The medium-pressure evaporator 24b exchanges heat between the medium-pressure heating water and the exhaust gas EG, heating the medium-pressure heating water to generate medium-pressure steam. A first reboiler medium line 71 is connected to the outlet of the medium-pressure evaporator 24b. This first reboiler medium line 71 is connected to the medium inlet of the reboiler 139 described above. A reboiler medium recovery line 73 is connected to the medium outlet of the reboiler 139. This reboiler medium recovery line 73 is connected to the inlet of the medium-pressure economizer 24a. A reboiler medium booster 74 is provided on this reboiler medium recovery line 73.

[0120] The high-pressure pump 25p pressurizes low-pressure heated water. The first high-pressure economizer 25a exchanges heat between the heated water pressurized by the high-pressure pump 25p and exhaust gas EG, further heating the heated water. The second high-pressure economizer 25b exchanges heat between the heated water heated by the first high-pressure economizer 25a and exhaust gas EG, further heating the heated water. The high-pressure evaporator 25c exchanges heat between the heated water heated by the second high-pressure economizer 25b and exhaust gas EG, heating the heated water to steam. The high-pressure superheater 25d exchanges heat between the steam and exhaust gas EG, further superheating the steam to high-pressure steam. One end of a high-pressure steam line 83 is connected to the outlet of the high-pressure superheater 25d. The other end of this high-pressure steam line 83 is connected to the inlet of the high-pressure steam turbine 33. One end of a high-pressure exhaust steam line 85 is connected to the outlet of the high-pressure steam turbine 33. The other end of this high-pressure exhaust steam line 85 is connected to the inlet of the intermediate-pressure steam turbine 32. A second reboiler medium line 72 is connected to this high-pressure exhaust steam line 85. This second reboiler medium line 72 is connected to the medium inlet of the reboiler 139 described above. Therefore, in addition to the first reboiler medium line 71 described above, the second reboiler medium line 72 is also connected to the medium inlet of the reboiler 139.

[0121] One end of an intermediate-pressure exhaust steam line 87 is connected to the outlet of the intermediate-pressure steam turbine 32. The other end of this intermediate-pressure exhaust steam line 87 is connected to the inlet of the low-pressure steam turbine 31. Therefore, this intermediate-pressure exhaust steam line 87 and the low-pressure steam line 88 are connected to the inlet of the low-pressure steam turbine 31.

[0122] A first heat medium recovery line 52 is connected to the medium inlet of the first heat medium heater 27. The first heat medium recovery line 52 and the high-pressure steam line 83 are connected by a heat medium replenishment line 55. Here, the first heat medium, the heat cycle medium, and the high-pressure steam serving as the working medium for the high-pressure steam turbine are all water vapor and are the same substance. The pressure of the first heat medium is lower than the maximum pressure of the heat cycle medium in the waste heat utilization heat cycle. Here, the pressure of the first heat medium is lower than the steam pressure at the inlet of the high-pressure steam turbine. This heat medium replenishment line 55 is provided with a heat medium replenishment valve 56. Normally, the heat medium replenishment valve 56 is closed, but when it is necessary to replenish the first heat medium, such as during startup or when the pressure of the first heat medium drops due to a leak of the first heat medium, the heat medium replenishment valve 56 is opened. In this case, high-pressure steam is supplied as the first heat medium from the high-pressure steam line 83 to the first heat medium recovery line 52 via the heat medium replenishment line 55 and the heat medium replenishment valve 56 as appropriate. A first heat medium line 51 is connected to the medium outlet of the first heat medium heater 27. The first heat medium heater 27 heats the first heat medium by heat exchange between the first heat medium from the first heat medium recovery line 52 and the exhaust gas EG. The first heat medium heated in the first heat medium heater 27 flows into the reactor 45 via the first heat medium line 51. As described above, the first heat medium is cooled in the reactor 45 by heat exchange with gaseous ammonia NHg. The cooled first heat medium returns to the first heat medium heater 27 via the first heat medium recovery line 52. During this process, the first heat medium is pressurized by the first heat medium booster 53. Note that, in the following embodiments, as in this embodiment, the first heat medium may be the same substance as the working medium of the high-pressure steam turbine, i.e., steam, and the pressure of the first heat medium may be lower than the inlet pressure of the high-pressure steam turbine. Furthermore, in the following embodiments, it is preferable to provide a heat medium replenishment line 55 and a heat medium replenishment valve 56 connecting the line that sends steam to the high-pressure steam turbine 33 and the first heat medium recovery line 52. In this way, also in the following embodiments, by providing the heat medium replenishment line 55 and the heat medium replenishment valve 56, the first heat medium can be replenished when necessary, such as at the time of start-up or when the first heat medium pressure drops, without providing any other equipment.

[0123] The above-described exhaust heat utilization equipment 20 has a Rankine cycle, which is a type of thermal cycle. This Rankine cycle is configured with an exhaust heat recovery boiler 21, steam turbines 31, 32, and 33, a condenser 34, and a feedwater pump 36. Note that this Rankine cycle is also a waste heat utilization thermal cycle because it utilizes the heat of the exhaust gas EG.

[0124] Next, the operation and function of the raw material fluid processing plant described above will be explained.

[0125] When the gas turbine 11 starts up, startup fuel is supplied to the combustor 11c through a startup fuel line (not shown). Examples of the startup fuel include hydrogen and natural gas. As described above, the air compressor 11a of the gas turbine 11 compresses air to generate combustion air. The combustor 11c burns the startup fuel in the combustion air to generate combustion gas. The pressure of the combustion air is, for example, approximately 2 MPa. Therefore, the pressure inside the combustor 11c into which the combustion air flows is also, for example, approximately 2 MPa. The combustion gas is supplied to the turbine 11d to drive the turbine 11d. The exhaust gas EG, which is the combustion gas that drives the turbine 11d, flows into the gas tank 22 of the heat recovery steam generator 21.

[0126] The first low-pressure economizer 23a exchanges heat between water from the water supply line 35 and exhaust gas EG to heat the water. The second low-pressure economizer 23b exchanges heat between the water from the first low-pressure economizer 23a and exhaust gas EG to further heat the water, converting it into low-pressure heated water. A portion of this low-pressure heated water is pressurized by a high-pressure pump 25p and then flows into the first high-pressure economizer 25a. The first high-pressure economizer 25a exchanges heat between the heated water pressurized by the high-pressure pump 25p and exhaust gas EG to further heat the heated water. The second high-pressure economizer 25b exchanges heat between the heated water heated in the first high-pressure economizer 25a and exhaust gas EG to further heat the heated water. The high-pressure evaporator 25c exchanges heat between the heated water heated in the second high-pressure economizer 25b and exhaust gas EG to heat the heated water and convert it into steam. The high-pressure superheater 25d exchanges heat between this steam and the exhaust gas EG, further superheating the steam to generate high-pressure steam. This high-pressure steam flows into the high-pressure steam turbine 33 via a high-pressure steam line 83. The high-pressure steam turbine 33 is driven by this high-pressure steam.

[0127] A portion of the high-pressure steam that has driven the high-pressure steam turbine 33 flows into the intermediate-pressure steam turbine 32 via a high-pressure exhaust steam line 85. Another portion of the high-pressure steam that has driven the high-pressure steam turbine 33 flows into the reboiler 139 via a second reboiler medium line 72. The intermediate-pressure steam turbine 32 is driven by steam from the high-pressure exhaust steam line 85. The steam that has driven the intermediate-pressure steam turbine 32 flows into the low-pressure steam turbine 31 via an intermediate-pressure exhaust steam line 87.

[0128] Another portion of the low-pressure heated water flows into the low-pressure evaporator 23c. The low-pressure evaporator 23c exchanges heat between the low-pressure heated water and the exhaust gas EG, heating the low-pressure heated water to form steam. The low-pressure superheater 23f exchanges heat between the steam from the low-pressure evaporator 23c and the exhaust gas EG, heating the steam to form low-pressure steam. This low-pressure steam flows into the low-pressure steam turbine 31 via the low-pressure steam line 88. In addition to the low-pressure steam flowing in from the low-pressure steam line 88, the steam that has driven the intermediate-pressure steam turbine 32, as described above, also flows into the low-pressure steam turbine 31. The low-pressure steam turbine 31 is driven by this steam.

[0129] The steam that drives the low-pressure steam turbine 31 flows into the condenser 34. The condenser 34 converts the steam from the low-pressure steam turbine 31 back into water. This water flows into the first low-pressure economizer 23a via a water supply line 35.

[0130] Another portion of the low-pressure heating water is pressurized by the medium-pressure pump 24p and then flows into the medium-pressure economizer 24a. The medium-pressure economizer 24a exchanges heat between the heated water pressurized by the medium-pressure pump 24p and the exhaust gas EG, further heating this heated water to form medium-pressure heated water. A portion of the medium-pressure heating water flows into the fuel preheater 13 via the medium-pressure heating water line 77. The heated water that flows into the fuel preheater 13 flows into the feedwater line 35 via the heated water recovery line 78. Another portion of the medium-pressure heating water flows into the medium-pressure evaporator 24b. The medium-pressure evaporator 24b exchanges heat between the medium-pressure heating water and the exhaust gas EG, heating the medium-pressure heating water to form medium-pressure steam. This medium-pressure steam flows into the reboiler 139 via the first reboiler medium line 71. That is, in addition to steam from the first reboiler medium line 71, as described above, steam also flows into the reboiler 139 from the second reboiler medium line 72. The steam that flows into the reboiler 139 becomes water and then flows into the medium pressure economizer 24a via the reboiler medium recovery line 73.

[0131] The first heat medium heater 27 exchanges heat between steam and the exhaust gas EG to raise the temperature of the steam. The heated steam flows into the reactor 45 via the first heat medium line 51. This steam flows into the first heat medium heater 27 via the first heat medium recovery line 52 without undergoing a phase change. This steam circulates as the first heat medium between the first heat medium heater 27 and the reactor 45 while the exhaust gas EG flows through the gas box 22. Because the first heat medium circulates between the first heat medium heater 27 and the reactor 45 without undergoing a phase change, there is no need to use a large amount of heat for evaporating the first heat medium, and heat can be effectively supplied to the reactor 45 with the limited heat of the exhaust gas EG.

[0132] In the Rankine cycle of the waste heat utilization equipment 20, in other words, in the waste heat utilization heat cycle, a heat cycle medium, which is water or steam, circulates. Furthermore, liquid ammonia NH in the ammonia tank T is supplied to the raw material reaction equipment 40. Below, the operation of the raw material fluid processing plant will be described according to the flowchart shown in Figure 2. Note that, as liquid ammonia NH is supplied to the raw material reaction equipment 40, steam as a first heat medium flows into the reactor 45. Furthermore, steam as a reboiler medium flows into the reboiler 139.

[0133] When liquid ammonia NH is supplied to the raw material reaction equipment 40, a raw material reaction step (S1) is carried out. In this raw material reaction step (S1), a reaction gas generation step (S2) and a residual raw material removal step (S6) are carried out. In the reaction gas generation step (S2), a raw material preheating step (S3), a reaction execution step (S4), and a reaction gas cooling step (S5) are carried out.

[0134] Liquid ammonia NH is stored in an ammonia tank T in a state cooled to a temperature below −33.4° C., which is its boiling point, and at approximately atmospheric pressure. The liquid ammonia NH in the ammonia tank T is pressurized by the raw ammonia pump 43, for example, to approximately 5 MPa, and then flows into the preheaters 44a and 44b, where it is preheated by heat exchange with a second heat medium (S3: raw material preheating step). The liquid ammonia NH pressurized by the raw ammonia pump 43 first flows into the first preheater 44a, where it is preheated. This preheating causes the liquid ammonia NH to vaporize and become gaseous ammonia NHg. When the liquid ammonia NH reaches 90° C. or higher under the pressure environment pressurized by the raw ammonia pump 43, it vaporizes and becomes gaseous ammonia NHg. For this reason, the first preheater 44a preheats the liquid ammonia NH so that the liquid ammonia NH reaches 90° C. or higher. Thus, the first preheater 44a functions as a vaporizer for the liquid ammonia NHg. The gaseous ammonia NHg flows into the second preheater 44b, where it is preheated to, for example, about 400° C. Thus, the second preheater 44b functions as a gas heater for the gaseous ammonia NHg.

[0135] The gaseous ammonia NHg from the second preheater 44b flows into the reactor 45. Also, steam, which is a first heat medium heated by the first heat medium heater 27 of the heat recovery boiler 21, flows into this reactor 45 via a first heat medium line 51. This steam has a temperature of, for example, approximately 620°C. In this reactor 45, the gaseous ammonia NHg is further heated by heat exchange between the gaseous ammonia NHg and the first heat medium, while the first heat medium is cooled. The cooled first heat medium returns to the first heat medium recovery line 52 via a first heat medium recovery line 52. This first heat medium circulates between the reactor 45 and the first heat medium heater 27. The first heat medium does not change phase during the process of circulating between the reactor 45 and the first heat medium heater 27. The gaseous ammonia NHg heated in this reactor 45 is decomposed into hydrogen and nitrogen by the thermal decomposition reaction shown in the following formula (S4: reaction execution step). NH3 → 3 / 2H2 + 1 / 2N2

[0136] However, in this reaction execution step (S4), a portion of the gaseous ammonia NHg flowing into the reactor 45 remains as residual ammonia (residual raw material). Therefore, in addition to hydrogen and nitrogen, residual ammonia remains in the reaction gas RG obtained by executing this reaction execution step (S4). This reaction gas RG has a temperature of about 600°C.

[0137] The reaction gas RG flows sequentially into the second preheater 44b, the first preheater 44a, and the reaction gas cooler 46, and is sequentially cooled as it passes through these (S5: reaction gas cooling step). The reaction gas RG from the reactor 45 flows into the second preheater 44b as a second heat medium through the reaction gas line 47, which also serves as the second heat medium line. In this second preheater 44b, the gaseous ammonia NHg is preheated as described above by heat exchange between the gaseous ammonia NHg and the reaction gas RG, while the reaction gas RG is cooled. The reaction gas RG cooled in the first preheater 44a flows into the first preheater 44a as a second heat medium through the reaction gas line 47, which also serves as the second heat medium line. In this first preheater 44a, the liquid ammonia NH is preheated and vaporized as described above by heat exchange between the liquid ammonia NH and the reaction gas RG, while the reaction gas RG is further cooled. The reaction gas RG cooled by the first preheater 44a flows into the reaction gas cooler 46 and is further cooled. The temperature of this reaction gas RG is, for example, about 30 to 50°C. As described above, the second preheater 44b and the first preheater 44a of this embodiment function as preheaters that preheat ammonia NH, and also function as reaction gas coolers that cool the reaction gas RG. In addition, the reaction gas RG here is a second heat medium that preheats ammonia NH, and the ammonia NH is a third heat medium that cools the reaction gas RG.

[0138] This completes the reaction gas generation step (S2). After the reaction gas generation step (S2) is completed, the residual raw material removal step (S6) is carried out.

[0139] In the residual raw material removal step (S6), a residual raw material absorption step (S7) and a residual raw material separation step (S8) are carried out.

[0140] The residual raw material absorption step (S7) is performed in the absorption tower 131. The reaction gas RG from the raw material reactor 41 flows into the absorption tower 131. Furthermore, water at approximately 30°C is sprayed into the absorption tower 131 from a water line 134. Inside the absorption tower 131, the reaction gas RG comes into contact with the water, and residual ammonia in the reaction gas RG dissolves in the water. Ammonia water, which is the water in which the residual ammonia has been dissolved, accumulates in the lower part of the absorption tower 131. Meanwhile, the treated reaction gas RGp, which is the reaction gas RG from which the residual ammonia has been removed, is sent to the gas turbine 11 via the fuel line 12.

[0141] In the residual raw material separation step (S8), a raw material water heating step (S9), a raw material separation execution step (S10), and a water heating step (S11) are carried out.

[0142] The ammonia water (raw water) accumulated in the lower part of the absorption tower 131 is sent to the regeneration tower 132 via the ammonia water line 133. In this process, the ammonia water is heated in the heat exchanger 136 (S9: raw water heating step). In addition to the ammonia water heated in the heat exchanger 136, steam from the reboiler 139 also flows into the regeneration tower 132. The ammonia water is heated by this steam, and the ammonia in the ammonia water is separated and distilled as gaseous ammonia NHg (S10: raw material separation execution step). Meanwhile, the steam transitions to liquid water and accumulates in the lower part of the regeneration tower 132. A portion of this water flows into the reboiler 139 via the water circulation line 137. Medium-pressure steam from the medium-pressure evaporator 24b flows into the reboiler 139 via the first reboiler medium line 71, and steam exhausted from the high-pressure steam turbine 33 flows into the reboiler 139 via the second reboiler medium line 72. In the reboiler 139, the water flowing in from the water circulation line 137 is heated by heat exchange with the steam to become steam (S11: water heating step). This steam is sent to the regenerator 132. Meanwhile, the steam that has exchanged heat with the water flowing in from the water circulation line 137 is cooled and converted into heated water, which flows into the medium-pressure coal economizer 24a via the reboiler medium recovery line 73.

[0143] The gas containing gaseous ammonia NHg in the regenerator 132 flows into the condenser 138 via the recovered ammonia line 140. In the condenser 138, the gas is cooled, and the moisture contained in the gas is condensed to form liquid water. This water returns to the regenerator 132. On the other hand, the gas from which the moisture has been removed, i.e., the gas with a high concentration of gaseous ammonia, is pressurized by the recovered ammonia booster 141 provided in the recovered ammonia line 140, and then flows into the second preheater 44b via the recovered ammonia line 140 and the second ammonia supply line 42b (S12: raw material recovery step). As described above, in this embodiment, the residual ammonia removed from the reaction gas RG in the residual raw material removal device 130 returns to the second preheater 44b, thereby minimizing the amount of ammonia wasted as raw material.

[0144] As described above, the treated reaction gas RGp is ​​sent to the gas turbine 11 via the fuel line 12. During this process, the treated reaction gas RGp is ​​preheated by the fuel preheater 13. The gas turbine 11 is driven by burning the treated reaction gas RGp as fuel (S13: reaction gas utilization step). The exhaust gas EG from the gas turbine 11 flows into the heat recovery boiler 21 of the waste heat utilization facility 20.

[0145] The exhaust heat utilization equipment 20 utilizes the heat of the exhaust gas EG to heat a heat cycle medium flowing in the exhaust heat utilization heat cycle, and utilizes the heated heat cycle medium (S14: exhaust heat utilization step). That is, in the exhaust heat utilization equipment 20, water is heated by the exhaust gas EG to become steam, and this steam is utilized to drive steam turbines (medium utilization equipment) 31, 32, 33. In this exhaust heat utilization step (S14), a first heat medium heating step (S15), a heat cycle medium heating step (S16), and a heat cycle medium utilization step (S17) are performed.

[0146] As described above, the exhaust gas EG that has flowed into the gas frame 22 exchanges heat with steam, which is the first heat medium, in the first heat medium heater 27 to heat the first heat medium (S14: first heat medium heating step). The steam heated in the first heat medium heater 27 is sent to the reactor 45. As described above, in the reactor 45, heat exchange occurs between the gaseous ammonia NHg that has flowed into the reactor 45 at this time and the steam, which is the first heat medium, and the gaseous ammonia NHg is heated. The gaseous ammonia NHg heated in the reactor 45 becomes a reaction gas RG through a thermal decomposition reaction (S4: reaction execution step).

[0147] As described above, the exhaust gas EG that has flowed into the heat recovery boiler 21 exchanges heat with the heat cycle medium, which is steam or water, to heat the heat cycle medium and turn it into steam that can be used by each of the steam turbines 31, 32, and 33 (S16: heat cycle medium heating step). This steam is sent to each of the steam turbines 31, 32, and 33 to drive each of the steam turbines 31, 32, and 33 (S17: heat cycle medium utilization step).

[0148] This completes the series of operations in the raw fluid processing plant.

[0149] Next, the main effects of this embodiment will be described with reference to Fig. 3 and Fig. 4. Fig. 3 and Fig. 4 are TQ diagrams relating to ammonia (solid line) and a heat source for heating the ammonia (dashed line). Therefore, in Fig. 3 and Fig. 4, the horizontal axis represents the amount of heat, and the vertical axis represents the temperature. Furthermore, Fig. 3 is a TQ diagram relating to ammonia and a heat source up to the thermal decomposition reaction of liquid ammonia in one heat exchanger, similar to Patent Documents 1 and 2 described above. Meanwhile, Fig. 4 is a TQ diagram relating to ammonia and a heat source up to the thermal decomposition reaction of liquid ammonia in this embodiment.

[0150] As shown in Figures 3 and 4, the temperature of liquid ammonia increases as the amount of heat increases due to preheating. When the temperature of this liquid ammonia reaches the saturation temperature, the liquid ammonia gradually vaporizes. During this vaporization process, even if the amount of heat of ammonia increases, this heat is used as heat of vaporization (latent heat), and the temperature of the ammonia does not change. When all the liquid ammonia has vaporized and turned into gaseous ammonia, the amount of heat increases due to preheating, and the temperature increases. When the temperature of the gaseous ammonia has risen to a certain level, a thermal decomposition reaction begins. Because this thermal decomposition reaction is an endothermic reaction, the amount of temperature increase relative to the amount of heat increase is smaller than in the process of preheating gaseous ammonia. However, as the thermal decomposition reaction progresses and the concentration of ammonia decreases, the amount of temperature increase relative to the amount of heat increase gradually becomes larger.

[0151] In one heat exchanger, the only heat source for the thermal decomposition reaction of liquid ammonia is the exhaust gas passing through the gas frame of the heat exchanger. In this case, as shown in Figure 3, the exhaust gas as a heat source gradually decreases in heat quantity and temperature as it moves from the inlet (in) to the outlet (out) of the gas frame due to heat exchange with ammonia. At this time, the amount of temperature decrease relative to the amount of heat decrease for the exhaust gas as a heat source is approximately constant, whether ammonia is undergoing a thermal decomposition reaction or liquid ammonia is vaporized. For this reason, for example, the temperature difference ΔT1 between the ammonia when vaporizing and the exhaust gas exchanging heat with this ammonia becomes large, and the heat of the high-temperature exhaust gas is recovered by the low-temperature ammonia, resulting in low thermal utilization efficiency of the exhaust gas.

[0152] On the other hand, in this embodiment, the heat sources for the thermal decomposition reaction of liquid ammonia are a first heat medium heated by exhaust gas EG and a second heat medium which is reaction gas RG. The system through which this second heat medium flows is different from the system through which the first heat medium flows. The heat of the first heat medium, which is part of the heat source, is used to cause the thermal decomposition reaction of ammonia. During this thermal decomposition reaction, the first heat medium loses heat and its temperature drops due to heat exchange with ammonia, as shown in Figure 4. At this time, the amount of temperature decrease relative to the amount of heat decrease for the first heat medium as a heat source is approximately constant.

[0153] In this embodiment, the heat of the second heat medium, which is another part of the heat source, is used to preheat ammonia. During this preheating, the second heat medium loses heat quantity and drops in temperature due to heat exchange with ammonia. However, by using a second heat medium at a suitable flow rate and temperature for preheating ammonia, the TQ line showing the change in temperature relative to the change in heat quantity of the second heat medium as a heat source follows the TQ line showing the change in temperature relative to the change in heat quantity of the ammonia. Therefore, the temperature difference ΔT2 between the ammonia and the second heat medium during preheating becomes small, and the ammonia recovers the heat of the second heat medium, which is close to the temperature of the ammonia, thereby increasing the heat utilization efficiency of the second heat medium.

[0154] Furthermore, in this embodiment, when ammonia is subjected to a thermal decomposition reaction, first, ammonia is preheated by heat exchange between the reaction gas RG as the second heat medium and ammonia up to just before the reaction zone including the temperature at which the slope becomes minimum P on the ammonia TQ line. Then, in this embodiment, ammonia is subjected to a thermal decomposition reaction in the reaction zone using heat from steam as the first heat medium. Therefore, in this embodiment, the amount of heat required to heat the first heat medium can be reduced compared to when ammonia is preheated and subjected to a thermal decomposition reaction using a single heat medium. Therefore, in this embodiment, the thermal energy loss of the exhaust gas EG required to heat the first heat medium can be reduced.

[0155] In the reactor 45, a large portion of the applied heat is utilized for the ammonia decomposition reaction, which is an endothermic reaction, so the slope of the TQ line for ammonia is small, as mentioned above. On the other hand, in the preheating process, no endothermic reaction occurs, so the slope of the TQ line is large on average. Therefore, the first heat medium is circulated so that the product of the constant-pressure specific heat and flow rate of the steam, which is the first heat medium and the heat source of the reactor 45, is greater than the product of the constant-pressure specific heat and flow rate of the reaction gas RG, which is the second heat medium and the heat source of the preheater 44, which is composed of the second preheater 44b and the first preheater 44a. Here, for example, if the constant-pressure specific heat is expressed in kJ / kgK and the flow rate is expressed in kg / s, the product of the constant-pressure specific heat and flow rate, i.e., the heat capacity of the heat medium per unit time, can be expressed in kW / K. The units of the constant pressure specific heat and the flow rate may be any as long as the same units are used for the first and second heat media. For example, the constant pressure specific heat may be expressed in kcal / molK and the flow rate in mol / h, and the product of the constant pressure specific heat and the flow rate may be calculated in kcal / hK for comparison. Unless a reaction or phase change occurs, the slope of the TQ line is inversely proportional to the product of the constant pressure specific heat and the flow rate. The larger the product of the constant pressure specific heat and the flow rate, the smaller the slope of the TQ line. Therefore, the first heat medium is circulated so that the product of the constant pressure specific heat and the flow rate of the steam, which is the first heat medium, is greater than the product of the constant pressure specific heat and the flow rate of the second heat medium, which is the heat source of the preheater 44, i.e., the reaction gas RG. As a result, the slopes of the TQ lines of the first heat medium and the second heat medium can be made closer to the slope of the TQ line of ammonia, the temperature difference ΔT2 between the ammonia and the second heat medium during preheating can be reduced, the heat of the second heat medium can be recovered to ammonia at a similar temperature, and the amount of heat required for each temperature level can be input without excess or deficiency. Therefore, heat can be used effectively according to the temperature level, and the heat utilization efficiency of the second heat medium is increased.

[0156] The above effects are obtained by using different media for the first and second heat transfer media for the reaction and preheating, respectively, in response to the difference in the slope of the TQ line of the raw material fluid, i.e., ammonia, between the reaction and preheating, as shown in a) and b) below. a) The heat capacities per unit time of the first heat medium and the second heat medium, i.e., the slopes of the TQ lines, are made different, and the slopes of the TQ lines of the first heat medium and the second heat medium are made to approach the slopes of the TQ lines of ammonia in the reactor and the preheater, respectively. b) The first and second heat transfer media used had temperatures close to the temperatures of the ammonia in the reactor and preheater, respectively.

[0157] Therefore, to achieve the above effects, the first heat medium and the second heat medium must be different from each other. In this embodiment, the first heat medium is steam, and the second heat medium is a reaction gas. Although the two are different substances, the types of heat medium substances do not necessarily need to be different. The same substance may have different heat capacities per unit time or temperatures due to differences in phase, flow rate, pressure, etc. Different heat capacities per unit time can change the slope of the heat medium's TQ line, making it possible to approximate the slope of the TQ line of the feed fluid in each reactor and preheater. Furthermore, different temperatures can be used to supply heat mediums at temperatures close to those of the feed fluids in each reactor and preheater, enabling the reaction and preheating of the feed fluids with a lower temperature heat medium.

[0158] Furthermore, in the present embodiment, the first heat medium circulates between the reactor 45 and the first heat medium heater 27. This makes it possible to minimize the temperature difference between the temperature of the first heat medium flowing out of the first heat medium heater 27 and the temperature of the first heat medium flowing into the first heat medium heater 27. Moreover, as described above, the first heat medium of the present embodiment does not undergo a phase change while circulating between the reactor 45 and the first heat medium heater 27. Therefore, in the present embodiment, from this viewpoint as well, the amount of heat required to heat the first heat medium can be reduced.

[0159] The temperature of the exhaust gas EG for heating the first heat medium is higher than the temperature of the exhaust gas EG for generating steam to be sent to the steam turbines 31, 32, and 33. Therefore, as described above, if the amount of heat required to heat the first heat medium can be reduced, the thermal energy loss of the high-temperature exhaust gas EG can be suppressed.

[0160] As described above, in this embodiment, when liquid ammonia NH is converted into the reaction gas RG, the loss of thermal energy of the exhaust gas EG can be suppressed. Therefore, in this embodiment, more thermal energy can be used to drive the steam turbines 31, 32, and 33 out of the thermal energy of the exhaust gas EG, and the thermal efficiency of the plant can be improved.

[0161] In this embodiment, the heat cycle medium flowing in the exhaust heat utilization heat cycle and the first heat medium are the same substance, that is, water, so that the quality of the first heat medium, that is, water, can be easily managed.

[0162] In this embodiment, the pressure of the steam serving as the first heat medium is lower than the maximum pressure of the heat cycle medium in the waste heat cycle. Therefore, without requiring additional equipment, part of the heat cycle medium from the waste heat cycle can be easily supplied to the first heat medium system as the first heat medium to replenish the first heat medium upon startup or when the pressure of the first heat medium drops. Specifically, as described above, high-pressure steam is supplied as the first heat medium from the high-pressure steam line 83, which constitutes part of the waste heat cycle, to the first heat medium recovery line 52 via the heat medium replenishment line 55 and the heat medium replenishment valve 56. During normal operation, the heat medium replenishment valve 56 is closed. Here, the pressure of the steam serving as the first heat medium is lower than the pressure of the high-pressure steam serving as the heat cycle medium in the waste heat cycle. Only when it is necessary to replenish the first heat medium, such as during startup or when the pressure of the first heat medium drops due to a seal leak or the like, the heat medium replenishment valve 56 is opened, and part of the high-pressure steam flowing through the high-pressure steam line 83 is directed to the first heat medium recovery line 52, thereby replenishing the first heat medium to the first heat medium recovery line 52, etc. In this embodiment, no separate equipment is required, and the first heat medium can be easily replenished during startup or when the pressure of the first heat medium drops.

[0163] As described above, in this embodiment, the heat cycle medium and the first heat medium flowing through the exhaust heat cycle are made of the same material, and the pressure of the first heat medium, steam, is set lower than the maximum pressure of the heat cycle medium in the exhaust heat cycle. This allows the first heat medium to be easily replenished from the exhaust heat cycle. Therefore, similar to the first heat medium, the second heat medium is also made of the same material as the heat cycle medium flowing through the exhaust heat cycle, and the pressure of the second heat medium is set lower than the maximum pressure of the heat cycle medium in the exhaust heat cycle. In particular, even in a closed loop consisting of heat exchange elements, piping, and pressure-boosting elements, without a component for extracting work by the expansion of at least one of the first and second heat mediums and without a medium inlet for receiving a medium from the outside during normal operation, the same effect as above can be achieved by making the heat medium flowing through the closed loop the same material as the heat cycle medium and setting the pressure of the heat medium lower than the maximum pressure of the heat cycle medium in the exhaust heat cycle. That is, even when the heat medium is in a closed loop, no separate equipment is required, and the first heat medium can be easily replenished at the time of start-up or when the pressure of the first heat medium drops.

[0164] Furthermore, the raw material reaction equipment 40 of this embodiment includes, in addition to the raw material reactor 41 that thermally decomposes ammonia NH, a residual raw material removal unit 130 that removes residual ammonia contained in the reaction gas RG from the raw material reactor 41. Therefore, in this embodiment, the concentration of residual ammonia contained in the gas sent to the reaction gas utilization equipment 10 can be suppressed.

[0165] Incidentally, when fuel containing ammonia is burned, the ammonia in the fuel is converted to NOx by the combustion, and the exhaust gas contains NOx. As described above, the raw material reaction equipment 40 of this embodiment can reduce the concentration of residual ammonia contained in the gas sent to the reaction gas utilization equipment 10. The reaction gas utilization equipment 10 of this embodiment is a gas turbine equipment that burns the gas from the raw material reaction equipment 40 as fuel. Therefore, in this embodiment, the NOx concentration in the exhaust gas EG generated by the combustion of the fuel can be reduced. Furthermore, in this embodiment, the CO2 concentration in the exhaust gas EG generated by the combustion of the fuel can also be reduced.

[0166] Second Embodiment A second embodiment of the raw fluid processing plant will now be described with reference to FIG.

[0167] The raw material fluid processing plant of this embodiment is a plant in which the heat source for preheating ammonia NH and the heat source for cooling the reactant gas RG are changed from those of the raw material fluid processing plant of the first embodiment. Therefore, the raw material preheating step of the series of operations in the raw material fluid processing plant of this embodiment is different from the raw material preheating step (S3) of the first embodiment. Furthermore, the reactant gas cooling step of the series of operations in the raw material fluid processing plant of this embodiment is different from the reactant gas cooling step (S5) of the first embodiment.

[0168] Similar to the first embodiment, the raw material fluid processing plant of this embodiment also includes a raw material reaction facility 40a, a reaction gas utilization facility 10, and a waste heat utilization facility 20a.

[0169] Like the raw material reaction equipment 40 of the first embodiment, the raw material reaction equipment 40a of the present embodiment includes a raw material reaction apparatus 41a and a residual raw material removal apparatus 130. The raw material reaction apparatus 41a of the present embodiment is different from the raw material reaction apparatus 41 of the first embodiment. On the other hand, the residual raw material removal apparatus 130 of the present embodiment is the same as the residual raw material removal apparatus 130 of the first embodiment.

[0170] The reaction gas utilization equipment 10 of this embodiment is basically the same as the reaction gas utilization equipment 10 of the first embodiment. The individual devices constituting the exhaust heat utilization equipment 20a of this embodiment are the same as the individual devices constituting the exhaust heat utilization equipment 20 of the first embodiment. However, the line configuration connecting the individual devices in this embodiment is different from the line configuration connecting the individual devices in the first embodiment.

[0171] Similar to the raw material reactor 41 of the first embodiment, the raw material reactor 41a of the present embodiment includes an ammonia supply line 42, a raw material ammonia pump 43, preheaters 44c and 44d, a reactor 45, a reaction gas cooler 46, and a reaction gas line 47. Similar to the first embodiment, the preheaters 44c and 44d include a first preheater 44c and a second preheater 44d. Furthermore, the reaction gas coolers 46a and 46b include a first reaction gas cooler 46a and a second reaction gas cooler 46b.

[0172] As in the first embodiment, the ammonia supply line 42 has a first ammonia supply line 42a, a second ammonia supply line 42b, and a third ammonia supply line 42c. One end of the first ammonia supply line 42a is connected to the ammonia tank T, and the other end of the first ammonia supply line 42a is connected to an ammonia inlet of a first preheater 44c. The first preheater 44c is a heat exchanger. This first preheater 44c exchanges heat between liquid ammonia NH and a second heat medium, heating the liquid ammonia NH to gaseous ammonia NHg while cooling the second heat medium. One end of the second ammonia supply line 42b is connected to an ammonia outlet of the first preheater 44c, and the other end of the second ammonia supply line 42b is connected to an ammonia inlet of a second preheater 44d. The second preheater 44d is a heat exchanger. This second preheater 44d exchanges heat between the gaseous ammonia NHg and the second heat medium, heating the gaseous ammonia NHg while cooling the second heat medium. One end of the third ammonia supply line 42c is connected to the ammonia outlet of the second preheater 44d, and the other end of the third ammonia supply line 42c is connected to the ammonia inlet of the reactor 45.

[0173] A first heat medium line 51 is connected to a medium inlet of the reactor 45. A first heat medium recovery line 52 is connected to a medium outlet of the reactor 45. A first heat medium booster 53 is provided on the first heat medium recovery line 52. The reactor 45 is a heat exchanger. Similar to the reactor 45 of the first embodiment, the reactor 45 exchanges heat between the gaseous ammonia NHg heated in the second preheater 44d and the first heat medium from the first heat medium line 51 to further heat the gaseous ammonia NHg while cooling the first heat medium. The cooled first heat medium flows into the first heat medium recovery line 52. Similar to the first embodiment, the first heat medium line 51 and the first heat medium recovery line 52 are both connected to the first heat medium heater 27 of the exhaust heat recovery boiler 21.

[0174] The reactant gas line 47 includes a first reactant gas line 47a and a second reactant gas line 47b. One end of the first reactant gas line 47a is connected to the reactant gas outlet of the reactor 45. The other end of the first reactant gas line 47a is connected to the second heat medium inlet of the second preheater 44d. Therefore, in this embodiment, the reactant gas RG is a type of second heat medium. A first reactant gas cooler 46a is provided on the first reactant gas line 47a. One end of the second reactant gas line 47b is connected to the second heat medium outlet of the second preheater 44d, and the other end of the second reactant gas line 47b is connected to the residual raw material removal device 130. A second reactant gas cooler 46b is provided on the second reactant gas line 47b.

[0175] The high-pressure steam line connecting the high-pressure superheater 25d of the heat recovery boiler 21 and the high-pressure steam turbine 33 includes a first high-pressure steam line 83a and a second high-pressure steam line 83b. One end of the first high-pressure steam line 83a is connected to the outlet of the high-pressure superheater 25d, and the other end of the first high-pressure steam line 83a is connected to the third heat medium inlet of the first reactant gas cooler 46a. One end of the second high-pressure steam line 83b is connected to the third heat medium outlet of the first reactant gas cooler 46a, and the other end of the second high-pressure steam line 83b is connected to the inlet of the high-pressure steam turbine 33. Thus, in this embodiment, the high-pressure steam from the high-pressure superheater 25d is a type of third heat medium. The first high-pressure steam line 83a is a type of third heat medium line. The second high-pressure steam line 83b is a type of third heat medium recovery line.

[0176] One end of a high-pressure heating water line 81 is connected to the outlet of the second high-pressure economizer 25b in the heat recovery boiler 21. The other end of this high-pressure heating water line 81 is connected to the medium inlet of the fuel preheater 13. One end of a high-pressure heating water recovery line 82 is connected to the medium outlet of the fuel preheater 13. The other end of this high-pressure heating water recovery line 82 is connected to the feedwater line 35. Thus, the fuel preheater 13 of this embodiment exchanges heat between the high-pressure heating water from the second high-pressure economizer 25b and the fuel, thereby heating the fuel.

[0177] A branch water supply line 91 branched from the water supply line 35 is connected to a third heat medium inlet of the second reactant gas cooler 46b. One end of a connecting water supply line 92 is connected to a third heat medium outlet of the second reactant gas cooler 46b. The other end of the connecting water supply line 92 is connected to a second heat medium inlet of the first preheater 44c. Therefore, in this embodiment, the feedwater flowing through the water supply line 35 is a type of third heat medium that exchanges heat with the reactant gas RG. The branch water supply line 91 is a type of third heat medium line. The connecting water supply line 92 is a type of third heat medium recovery line for the second reactant gas cooler 46b. In this embodiment, the feedwater flowing from the connecting water supply line 92 to the first preheater 44c is a type of second heat medium. The connecting water supply line 92 is a type of second heat medium line for the first preheater 44c. One end of a heated water recovery line 78 is connected to a second heat medium outlet of the first preheater 44c. The other end of the heated water recovery line 78 is connected to the inlet of the second low-pressure economizer 23b of the heat recovery boiler 21. Therefore, the heated water recovery line 78 is a type of second heat medium recovery line for the first preheater 44c, and also a type of third heat medium recovery line for the second reaction gas cooler 46b.

[0178] The low-pressure heating water line 76 connects the second low-pressure economizer 23b and the first preheater 44c of the heat recovery boiler 21. Specifically, one end of the low-pressure heating water line 76 is connected to the outlet of the second low-pressure economizer 23b, and the other end of this low-pressure heating water line 76 is connected to the second heat medium inlet of the first preheater 44c. A portion of the low-pressure heating water from the second low-pressure economizer 23b flows into the first preheater 44c via the low-pressure heating water line 76 as a type of second heat medium. Therefore, this low-pressure heating water line 76 is a type of second heat medium line.

[0179] In the raw material preheating step of the present embodiment, similarly to the first embodiment, liquid ammonia NH is pressurized by the raw material ammonia pump 43, flows into the preheaters 44c, 44d, and is preheated in the preheaters 44c, 44d by heat exchange with the second heat medium.

[0180] The liquid ammonia NH pressurized by the raw ammonia pump 43 first flows into the first preheater 44c, where it is preheated by heat exchange with the second heat medium. As a result, the liquid ammonia NH vaporizes to become gaseous ammonia NHg. Therefore, the first preheater 44c functions as a vaporizer for the liquid ammonia NH. The second heat medium flowing into the first preheater 44c includes feedwater flowing into the first preheater 44c from the second reaction gas cooler 46b via a connecting feedwater line 92, and low-pressure heating water flowing into the first preheater 44c from the second low-pressure economizer 23b via a low-pressure heating water line 76. The second heat medium cooled by heat exchange with the liquid ammonia NH in the first preheater 44c flows into the second low-pressure economizer 23b via a heating water recovery line 78, which is a type of second heat medium recovery line and a type of third heat medium recovery line.

[0181] The heat recovery steam generator 21, steam turbines 31, 32, and 33, condenser 34, feedwater pump 36, and various piping connecting these components constitute a Rankine cycle, which is a type of first heat cycle. A connecting water supply line 92, which is a type of second heat medium line, guides a portion of the water (first heat cycle medium) flowing through the outlet of the second low-pressure economizer 23b (the first section of the first heat cycle) to the first preheater 44c via the low-pressure heated water line 76 as a type of second heat medium. A heated water recovery line 78, which is a type of second heat medium recovery line, guides water cooled by heat exchange with the feed fluid (ammonia) to the second section, where water at a lower temperature than the first section flows, i.e., the inlet of the second low-pressure economizer 23b. This configuration allows heat at an appropriate temperature to be supplied to the preheater from the Rankine cycle (first heat cycle) in just the right amount, and this heat can be used to preheat the feed fluid. Therefore, this embodiment improves heat utilization efficiency.

[0182] Furthermore, a branch water supply line 91, which is a type of third heat medium line, guides water from a water supply line 35 (a first portion in the Rankine cycle), which is one of the components of the Rankine cycle, to the second reactant gas cooler 46b. A heated water recovery line 78, which is a type of third heat medium recovery line, receives water heated by heat exchange with the reactant gas in the second reactant gas cooler 46b, via a connecting water supply line 92 and the first preheater 44c. The heated water recovery line 78 then guides the water to a second portion, through which water at a higher temperature than that in the water supply line 35 (first portion), flows, i.e., to the inlet of the second low-pressure economizer 23b. With this configuration, the waste heat of the reactant gas cooler is recovered as an appropriate amount of water, and the water is recovered at a location of an appropriate temperature in the Rankine cycle, thereby improving heat utilization efficiency.

[0183] The gaseous ammonia NHg from the first preheater 44c flows into the second preheater 44d, where it is further preheated by heat exchange with the second heat medium. Thus, the second preheater 44d functions as a gas heater for the gaseous ammonia NHg. This completes the raw material preheating step of this embodiment. The second heat medium flowing into the second preheater 44d is the reaction gas RG that flows into the second preheater 44d from the first reaction gas cooler 46a via the first reaction gas line 47a. This reaction gas RG is cooled by heat exchange with the gaseous ammonia NHg in the second preheater 44d.

[0184] The gaseous ammonia NHg from the second preheater 44d flows into the reactor 45, and similarly to the first embodiment, is decomposed into hydrogen and nitrogen by a thermal decomposition reaction to generate a reaction gas RG (reaction carrying out step).

[0185] In the reaction gas cooling step, the reaction gas RG is cooled by heat exchange between the reaction gas RG and the third heat medium. The reaction gas RG from the reactor 45 flows into the first reaction gas cooler 46a, the second preheater 44d, and the second reaction gas cooler 46b in this order, and is cooled sequentially as it passes through these coolers.

[0186] In the first reactant gas cooler 46a, heat is exchanged between the reactant gas RG from the reactor 45 and high-pressure steam from the high-pressure superheater 25d of the heat recovery boiler 21, which serves as a third heat medium, thereby cooling the reactant gas RG and superheating the high-pressure steam. The superheated high-pressure steam flows into the high-pressure steam turbine 33 via the second high-pressure steam line 83b and drives the high-pressure steam turbine 33. As described above, in this embodiment, high-pressure steam at a higher temperature than in the first embodiment flows into the high-pressure steam turbine 33, and therefore the output of the high-pressure steam turbine 33 can be increased compared to the first embodiment.

[0187] In this embodiment, the first high-pressure steam line 83a, which is a type of third heat medium line, guides all of the steam flowing out from the outlet of the high-pressure superheater 25d to the first reactant gas cooler 46a. The outlet of the high-pressure superheater 25d is a type of first section in the Rankine cycle. The second high-pressure steam line 83b, which is a type of third heat medium recovery line, guides steam that has been superheated by heat exchange with the reactant gas in the first reactant gas cooler 46a to a second section that flows steam at a higher temperature than the outlet (first section) of the high-pressure superheater 25d, i.e., the inlet of the high-pressure steam turbine 33. With this configuration, the waste heat of the reactant gas cooler is recovered as an appropriate amount of steam, and the steam is recovered at a location of an appropriate temperature in the Rankine cycle, thereby improving heat utilization efficiency.

[0188] In a plant using heat to react a raw material fluid to produce a reaction gas, as in the present embodiment, the reaction of the raw material fluid consumes a large amount of high-temperature heat, which may prevent the temperature of the heat cycle medium from being sufficiently increased. Specifically, to supply heat high enough to react with the raw material fluid, the first heat medium heater 27 is disposed in the gas chamber 22 of the heat recovery boiler 21 at the most upstream and highest temperature position relative to the flow of the exhaust gas EG. As described above, the reaction of the raw material fluid requires a large amount of heat, so the first heat medium heater 27 requires a large amount of heat from the first heat medium, which serves as a heat source for the reaction. In this case, the heat exchange rate in the first heat medium heater 27 is large, and the temperature of the exhaust gas EG in the first heat medium heater 27 drops significantly. As a result, the temperature of the exhaust gas EG available as a heat source in the high-pressure superheater 25d, which is disposed downstream of the first heat medium heater 27 in terms of the flow of the exhaust gas EG, becomes low, which may prevent the high-pressure superheater 25d from heating the high-pressure steam to a sufficiently high temperature. When steam from the outlet of the high-pressure superheater 25d is directly supplied to the high-pressure steam turbine 33 as in the first embodiment, the inlet temperature of the high-pressure steam turbine 33 is low. Furthermore, in order to suppress erosion of turbine blades due to moisture near the outlet of the low-pressure steam turbine 31, the wetness at the outlet of the low-pressure steam turbine 31 must be kept low, and therefore the enthalpy at the outlet of the low-pressure steam turbine 31 must be kept at a certain level or higher. When the inlet temperature of the high-pressure steam turbine 33 is low, in order to keep the enthalpy at the outlet of the low-pressure steam turbine 31 at a certain level or higher, the heat drop from the inlet of the high-pressure steam turbine 33 to the outlet of the low-pressure steam turbine 31 must be kept small. In other words, the pressure ratio from the inlet of the high-pressure steam turbine 33 to the outlet of the low-pressure steam turbine 31 must be small. Therefore, in the first embodiment, the inlet steam pressure of the high-pressure steam turbine 33 cannot be increased.

[0189] In this embodiment, steam at the outlet of the high-pressure superheater 25d is supplied as a third heat medium to the first reaction gas cooler 46a, which cools the reaction gas, and the exhaust heat of the reaction gas cooler 46a is recovered before being supplied to the high-pressure steam turbine 33. Therefore, in this embodiment, the steam temperature at the inlet of the high-pressure steam turbine 33 can be increased, and the entropy of the low-pressure steam turbine 31 can be made equal to or greater than a certain level. Therefore, in this embodiment, the inlet steam pressure and temperature of the high-pressure steam turbine 33 can be increased while suppressing the occurrence of erosion at the outlet of the low-pressure steam turbine 31. As described above, in this embodiment, even when a large amount of high-temperature heat is required for the reaction in the reactor 45 or for heating the first heat medium in the first heat medium heater 27, the output of the steam turbine can be increased and plant efficiency can be improved.

[0190] In the first embodiment and the present embodiment, the first heat medium circulates between the reactor 45 and the first heat medium heater 27. The reactor 45 exchanges heat between the first heat medium and the raw material fluid, so the difference between the first heat medium outlet temperature of the reactor 45 and the raw material fluid inlet temperature can be reduced to the minimum temperature difference achievable with a reasonable heat exchange area. Furthermore, the first heat medium leaving the reactor 45 enters the first heat medium heater 27 only after being pressurized by the amount of pressure loss in the system, so the difference between the first heat medium inlet temperature of the first heat medium heater 27 and the first heat medium outlet temperature of the reactor 45 is small. Furthermore, the first heat medium heater 27 exchanges heat between the exhaust gas EG and the first heat medium, so the difference between the exhaust gas outlet temperature of the first heat medium heater 27 and the first heat medium inlet temperature of the first heat medium heater 27 can be reduced to the minimum temperature difference achievable with a reasonable heat exchange area. Furthermore, the exhaust gas outlet temperature of the first heat medium heater 27 and the exhaust gas inlet temperature of the high-pressure superheater 25d are substantially equal. Therefore, when the heat exchange temperature difference is sufficiently reduced to increase the heat utilization efficiency of the reactor 45 and the first heat medium heater 27, the temperature difference between the exhaust gas inlet temperature of the high-pressure superheater 25d and the raw material fluid inlet temperature of the reactor 45 becomes small. When the steam to be supplied to the high-pressure steam turbine 33 is superheated using only the heat of the exhaust gas as in the first embodiment, it is difficult to increase the steam temperature at the inlet of the high-pressure steam turbine 33 above the raw material fluid inlet temperature of the reactor 45.

[0191] In this embodiment, the temperature of the high-pressure steam is increased by utilizing the exhaust heat of the reaction gas cooler 46a. In the first heat medium heater 27, the difference between the exhaust gas inlet temperature and the first heat medium outlet temperature (i.e., the first heat medium inlet temperature of the reactor 45) can be reduced to the minimum temperature difference achievable with a reasonable heat exchange area. In the reactor 45, the difference between the first heat medium inlet temperature of the reactor 45 and the reaction gas outlet temperature can be reduced to the minimum temperature difference achievable with a reasonable heat exchange area. Furthermore, in the reaction gas cooler 46a, heat is exchanged between the steam supplied to the high-pressure steam turbine 33, which serves as the third heat medium, and the reaction gas at the outlet of the reactor 45. Therefore, the difference between the reaction gas temperature at the outlet of the reactor 45 and the inlet steam temperature of the high-pressure steam turbine 33 can be reduced to the minimum temperature difference achievable with a reasonable heat exchange area. Therefore, in this embodiment, the inlet steam temperature of the high-pressure steam turbine 33 can be increased to a temperature close to the exhaust gas inlet temperature of the first heat medium heater 27. Because heat is exchanged between the exhaust gas EG at the exhaust gas outlet of the first heat medium heater 27 and the raw material fluid at the raw material fluid inlet of the reactor 45 via the first heat medium heater 27, the first heat medium, and the reactor 45, the raw material fluid inlet temperature of the reactor 45 is lower than the temperature at the exhaust gas outlet of the first heat medium heater 27. As described above, considering that the exhaust gas temperature is significantly reduced in the first heat medium heater 27, the exhaust gas inlet temperature of the first heat medium heater 27 is significantly higher than the raw material fluid inlet temperature of the reactor 45. For this reason, in the second embodiment, by utilizing exhaust heat from a reaction gas cooler that cools the reaction gas, it is possible to relatively easily heat the third heat medium (inlet steam of the high-pressure steam turbine 33) to a temperature higher than the temperature of the raw material fluid at the reactor inlet.

[0192] Furthermore, in the reactor 45, heat is imparted from the first heat medium at the first heat medium outlet of the reactor 45 to the raw fluid at the raw fluid inlet of the reactor 45. For this reason, the first heat medium outlet temperature of the reactor 45 is higher than the raw fluid inlet temperature of the reactor 45. Therefore, it is even more difficult to supply the high-pressure steam turbine 33 with a third heat medium (steam at the inlet of the high-pressure steam turbine 33) having a higher temperature than the first heat medium outlet temperature of the reactor 45 without using the exhaust heat from cooling the reaction gas. However, as described above, by using the configuration of this embodiment, steam at such a high temperature can be supplied to the high-pressure steam turbine 33 relatively easily.

[0193] In this embodiment, as described above, the third heat medium is heated to a temperature higher than the outlet temperature of the first heat medium of the reactor 45 using the exhaust heat from the reaction gas cooling, and then this third medium is supplied to the heat cycle, thereby particularly enhancing the effect of increasing the output of the heat cycle (here, the steam turbine) and the effect of improving the plant efficiency.

[0194] As described above, in the second preheater 44d, the reaction gas RG cooled in the first reaction gas cooler 46a is further cooled by heat exchange with gaseous ammonia NHg, while the gaseous ammonia NHg is preheated. Therefore, the second preheater 44d functions as a preheater that preheats gaseous ammonia NHg, and also functions as a reaction gas cooler that cools the reaction gas RG. In addition, the reaction gas RG here is a second heat medium that preheats gaseous ammonia NHg, and the gaseous ammonia NHg is a third heat medium that cools the reaction gas RG.

[0195] In the second reactant gas cooler 46b, heat exchange occurs between the reactant gas RG cooled in the second preheater 44d and feedwater as a third heat medium, thereby cooling the reactant gas RG and heating the feedwater. The heated feedwater flows into the first preheater 44c as a second heat medium. As described above, low-pressure heated water also flows into this first preheater 44c as a second heat medium.

[0196] This completes the reaction gas cooling process. The reaction gas RG cooled in the second reaction gas cooler 46b flows into the residual raw material removal device 130, where residual ammonia contained in the reaction gas RG is removed, similar to the first embodiment.

[0197] As described above, the second heat medium that preheats ammonia NH by heat exchange with the ammonia NH may be the reaction gas RG, or may be water or steam as a heat cycle medium flowing in the exhaust heat utilization heat cycle. Also, the third heat medium that cools the reaction gas RG by heat exchange with the reaction gas RG may be ammonia NH or may be water or steam as a heat cycle medium flowing in the exhaust heat utilization heat cycle.

[0198] In this embodiment, a liquid-phase raw material fluid, i.e., liquid ammonia, is vaporized in a first preheater (vaporizer) 44c and then sent to a second preheater (gas heater) 44d. Feedwater and heated water are supplied to the first preheater (vaporizer) 44c as a second heat medium for vaporization, and a reaction gas is supplied to the second preheater (gas heater) 44d as a second heat medium for gas heating. In particular, a large amount of water is supplied to the first preheater (vaporizer) 44c as a second heat medium for vaporization, the water being a mixture of feedwater flowing into the first preheater 44c from the second reaction gas cooler 46b via a connecting water supply line 92 and low-pressure heated water flowing into the first preheater 44c from the second low-pressure economizer 23b via a low-pressure heated water line 76. Therefore, in this embodiment, the product of the constant-pressure specific heat and flow rate of the second vaporization heat medium flowing through the first preheater (vaporizer) 44c is greater than the product of the constant-pressure specific heat and flow rate of the second gas-heating heat medium flowing through the second preheater (gas heater) 44d. That is, in this embodiment, a large amount of heat is supplied to the first preheater (vaporizer) 44c, which requires a large amount of heat for vaporizing the raw material fluid, at the temperature level required by the first preheater 44c. A small amount of heat is supplied to the second preheater (gas heater) 44d, which requires a small amount of heat, at the temperature level required by the second preheater 44c. Therefore, in this embodiment, the amount of heat required for each temperature level can be input without excess or deficiency, heat can be used effectively according to the temperature level, and heat utilization efficiency can be improved. As in the first embodiment, any units for the constant-pressure specific heat and flow rate can be used as long as the same units are used for comparison between the second vaporization heat medium and the second gas-heating heat medium.

[0199] In this embodiment, the effect of improving the heat utilization efficiency in the preheater is achieved by supplying different media to the second heat medium for vaporization and the second heat medium for gas heating. In this embodiment, water is used as the second heat medium for vaporization and a reaction gas is used as the second heat medium for gas heating, and the two are different substances. However, the two do not need to be different substances; they may be the same substance, but may have different heat capacities per unit time or different temperatures due to differences in phase, flow rate, pressure, etc. When the heat capacities per unit time of the two heat mediums are different, it is possible to supply a larger amount of heat than the temperature rise of the feed fluid gas to a temperature level for vaporization that requires a larger amount of heat. Furthermore, when the temperatures of the second heat medium for vaporization and the second heat medium for gas heating are different, it is possible to supply heat mediums with temperatures close to that of the feed fluid to each of the feed fluid vaporizer and the feed fluid gas heater. This enables the vaporization and heating of the feed fluid to be achieved with a heat medium of a relatively low temperature, and also makes it possible to supply the heat required for preheating according to the temperature level of the feed fluid, thereby improving heat utilization efficiency and improving plant efficiency.

[0200] In this embodiment, steam may be supplied to the first preheater (vaporizer) 44c from the low-pressure evaporator 23c or an intermediate stage of the low-pressure steam turbine 31, and the liquid-phase raw material fluid, i.e., liquid ammonia, may be evaporated in the first preheater 44c using heat generated by condensation of the steam. The heat of vaporization or condensation of a fluid, i.e., latent heat, is generally greater than the heat associated with a temperature change, i.e., sensible heat. Therefore, with this configuration, the heat of vaporization, which requires a large amount of heat, can be supplied using condensation heat, which can be easily obtained. In this case, the heat source medium can be vaporized at a constant temperature using a second heat medium for vaporization, which condenses at a constant temperature, as a heat source. The raw material fluid can be vaporized by effectively utilizing heat at a relatively low, constant temperature, thereby improving heat utilization efficiency.

[0201] "Third embodiment" A third embodiment of the raw material fluid processing plant will be described with reference to FIGS.

[0202] The raw material fluid processing plant of this embodiment is also a plant in which the heat source for preheating ammonia NH and the heat source for cooling the reactant gas RG are changed compared to the raw material fluid processing plant of the first embodiment. Therefore, the raw material preheating step in the series of operations in the raw material fluid processing plant of this embodiment is different from the raw material preheating step (S3) in the first embodiment. Furthermore, the reactant gas cooling step in the series of operations in the raw material fluid processing plant of this embodiment is different from the reactant gas cooling step (S5) in the first embodiment.

[0203] As shown in FIG. 6, the raw material fluid processing plant of this embodiment also includes a raw material reaction facility 40b, a reaction gas utilization facility 10, and a waste heat utilization facility 20b, similar to the above embodiments.

[0204] Similar to the raw material reaction equipment of the above embodiments, raw material reaction equipment 40b of this embodiment includes a raw material reaction apparatus 41b and a residual raw material removal apparatus 130. The raw material reaction apparatus 41b of this embodiment is different from the raw material reaction apparatus of the above embodiments. On the other hand, the residual raw material removal apparatus 130 of this embodiment is the same as the residual raw material removal apparatus 130 of the first embodiment.

[0205] The reaction gas utilization facility 10 of this embodiment is basically the same as the reaction gas utilization facility 10 of the above-described embodiments. Furthermore, the exhaust heat utilization facility 20b of this embodiment is different from the exhaust heat utilization facilities of the above-described embodiments.

[0206] The waste heat utilization equipment 20b of this embodiment, like the above embodiments, has a waste heat recovery boiler 21b, a low-pressure steam turbine 31, an intermediate-pressure steam turbine 32, a high-pressure steam turbine 33, a condenser 34, a water supply line 35, a water supply pump 36, and a chimney 39.

[0207] Similar to the above-described embodiments, the heat recovery steam generator 21b includes a gas frame 22, a first low-pressure economizer 23a, a second low-pressure economizer 23b, a low-pressure evaporator 23c, a low-pressure superheater 23f, a medium-pressure evaporator 24b, a first high-pressure economizer 25a, a medium-pressure economizer 24a, a second high-pressure economizer 25b, a high-pressure evaporator 25c, a first high-pressure superheater 25d, a high-pressure pump 25p, and a first heat medium heater 27. The heat recovery steam generator 21 of this embodiment further includes a second high-pressure superheater 25e, a first high-pressure reheater 26a, and a second high-pressure reheater 26b.

[0208] The first heat medium heater 27, the second high-pressure reheater 26b, the second high-pressure superheater 25e, the first high-pressure superheater 25d, the first high-pressure reheater 26a, part of the high-pressure evaporator 25c, the second high-pressure economizer 25b, the low-pressure superheater 23f, part of the intermediate-pressure evaporator 24b, the intermediate-pressure economizer 24a, the first high-pressure economizer 25a, part of the low-pressure evaporator 23c, the second low-pressure economizer 23b, and the first low-pressure economizer 23a are arranged in the gas frame 22 in this order from upstream to downstream. The first high-pressure reheater 26a is arranged at substantially the same position as the first high-pressure superheater 25d in the flow direction of the exhaust gas EG. The second high-pressure reheater 26b further superheats the steam superheated by the first high-pressure reheater 26a. An outlet of the second high-pressure reheater 26b is connected to an inlet of the high-pressure steam turbine 33 by a high-pressure reheat steam line 84.

[0209] The raw material reaction apparatus 41b of this embodiment includes an ammonia supply line 42, a raw material ammonia pump 43, preheaters 44e to 44i, a reactor 45, reaction gas coolers 46c and 46d, and a reaction gas line 47. The preheaters 44e to 44i of this embodiment include a first preheater 44e, a second preheater 44f, a third preheater 44g, a fourth preheater 44h, and a fifth preheater 44i. The reaction gas coolers 46c and 46d of this embodiment include a first reaction gas cooler 46c and a second reaction gas cooler 46d.

[0210] The ammonia supply line 42 includes a first ammonia supply line 42a, a second ammonia supply line 42b, a third ammonia supply line 42c, a fourth ammonia supply line 42d, a fifth ammonia supply line 42e, and a sixth ammonia supply line 42f.

[0211] One end of the first ammonia supply line 42a is connected to the ammonia tank T, and the other end of the first ammonia supply line 42a is connected to an ammonia inlet of a first preheater 44e. The first preheater 44e is a heat exchanger. The first preheater 44e exchanges heat between liquid ammonia NH and a second heat medium to heat the liquid ammonia NH while cooling the second heat medium. One end of the second ammonia supply line 42b is connected to an ammonia outlet of the first preheater 44e, and the other end of the second ammonia supply line 42b is connected to an ammonia inlet of a second preheater 44f. The second preheater 44f is a heat exchanger. The second preheater 44f exchanges heat between the liquid ammonia NH heated in the first preheater 44e and the second heat medium to heat the liquid ammonia NH to gaseous ammonia NHg while cooling the second heat medium. One end of the third ammonia supply line 42c is connected to the ammonia outlet of the second preheater 44f, and the other end of the third ammonia supply line 42c is connected to the ammonia inlet of the third preheater 44g. The recovered ammonia line 140 is connected to the third ammonia supply line 42c. The third preheater 44g is a heat exchanger. The third preheater 44g exchanges heat between the gaseous ammonia NHg and the second heat medium to heat the gaseous ammonia NHg while cooling the second heat medium. One end of the fourth ammonia supply line 42d is connected to the ammonia outlet of the third preheater 44g, and the other end of the fourth ammonia supply line 42d is connected to the ammonia inlet of the fourth preheater 44h. The fourth preheater 44h is a heat exchanger. The fourth preheater 44h exchanges heat between the gaseous ammonia NHg and the second heat medium to heat the gaseous ammonia NHg while cooling the second heat medium. One end of the fifth ammonia supply line 42e is connected to the ammonia outlet of the fourth preheater 44h, and the other end of the fifth ammonia supply line 42e is connected to the ammonia inlet of the fifth preheater 44i. The fifth preheater 44i is a heat exchanger. The fifth preheater 44i exchanges heat between the gaseous ammonia NHg and the second heat medium to heat the gaseous ammonia NHg and cool the second heat medium.One end of the sixth ammonia supply line 42f is connected to the ammonia outlet of the fifth preheater 44i, and the other end of the sixth ammonia supply line 42f is connected to the ammonia inlet of the reactor 45.

[0212] As in the above-described embodiments, a first heat medium line 51 is connected to a medium inlet of the reactor 45. A first heat medium recovery line 52 is connected to a medium outlet of the reactor 45. A first heat medium booster 53 is provided on the first heat medium recovery line 52. The reactor 45 is a heat exchanger. The reactor 45 exchanges heat between the gaseous ammonia NHg heated in the fifth preheater 44i and the first heat medium from the first heat medium line 51, thereby further heating the gaseous ammonia NHg and cooling the first heat medium. The cooled first heat medium flows into the first heat medium recovery line 52. As in the first embodiment, the first heat medium line 51 and the first heat medium recovery line 52 are both connected to the first heat medium heater 27 of the exhaust heat recovery boiler 21b.

[0213] One end of the reaction gas line 47 is connected to the reaction gas outlet of the reactor 45, and the other end of the reaction gas line 47 is connected to the residual raw material removal device 130. A first reaction gas cooler 46c and a second reaction gas cooler 46d are provided on this reaction gas line 47.

[0214] One end of a low-pressure heating water line 76 is connected to the second heat medium inlet of the second preheater 44f. The other end of this low-pressure heating water line 76 is connected to the outlet of the second low-pressure economizer 23b in the heat recovery boiler 21b. Therefore, this low-pressure heating water line 76 is a type of second heat medium line. One end of a first connected heating water line 78e is connected to the second heat medium outlet of the second preheater 44f. The other end of this first connected heating water line 78e is connected to the second heat medium inlet of the first preheater 44e. Therefore, this first connected heating water line 78e is a type of second heat medium recovery line for the second preheater 44f and a type of second heat medium line for the first preheater 44e. One end of a second heated water recovery line 78b is further connected to the second heat medium outlet of the second preheater 44f. The other end of this second heated water recovery line 78b is connected to the inlet of the second low-pressure economizer 23b. Therefore, the second heated water recovery line 78b is a type of second heat medium recovery line for the second preheater 44f. One end of a first heated water recovery line 78a is connected to the second heat medium outlet of the first preheater 44e. The other end of the first heated water recovery line 78a is connected to the water supply line 35. Therefore, the first heated water recovery line 78a is a type of second heat medium recovery line.

[0215] One end of a high-pressure heating water line 81 is connected to the second heat medium inlet of the fourth preheater 44h. The other end of this high-pressure heating water line 81 is connected to the outlet of the second high-pressure economizer 25b of the heat recovery boiler 21b. Therefore, this high-pressure heating water line 81 is a type of second heat medium line. One end of a second connected heating water line 78f is connected to the second heat medium outlet of the fourth preheater 44h. The other end of this second connected heating water line 78f is connected to the second heat medium inlet of the third preheater 44g. Therefore, this second connected heating water line 78f is a type of second heat medium recovery line for the fourth preheater 44h and a type of second heat medium line for the third preheater 44g. One end of a medium-pressure heating water line 77 is further connected to the second heat medium inlet of the third preheater 44g. The other end of this medium-pressure heating water line 77 is connected to the outlet of the medium-pressure economizer 24a. Therefore, the medium-pressure heated water line 77 is a type of second heat medium line for the third preheater 44g. One end of a third heated water recovery line 78c is connected to the second heat medium outlet of the third preheater 44g. The other end of the third heated water recovery line 78c is connected to the inlet of the second low-pressure economizer 23b. Therefore, the third heated water recovery line 78c is a type of second heat medium recovery line.

[0216] One end of a high-pressure steam line 83 is connected to the second heat medium inlet of the fifth preheater 44i. The other end of this high-pressure steam line 83 is connected to the outlet of the second high-pressure superheater 25e. Therefore, this high-pressure steam line 83 is a type of second heat medium line. One end of a high-pressure steam recovery line 86 is connected to the second heat medium outlet of the fifth preheater 44i. The other end of this high-pressure steam recovery line 86 is connected to the inlet of the first high-pressure reheater 26a. Therefore, this high-pressure steam recovery line 86 is a type of second heat medium recovery line.

[0217] The fuel line 12 includes a first fuel line 12a and a second fuel line 12b. One end of the first fuel line 12a is connected to a third heat medium inlet of the first reactant gas cooler 46c. The other end of the first fuel line 12a is connected to the residual raw material removal unit 130. The treated reactant gas RGp generated in the residual raw material removal unit 130 flows through the first fuel line 12a. The first reactant gas cooler 46c is a heat exchanger. The first reactant gas cooler 46c exchanges heat between the reactant gas RG flowing through the reactant gas line 47 and the treated reactant gas RGp as fuel flowing through the first fuel line 12a, thereby cooling the reactant gas RG and heating the treated reactant gas RGp. Therefore, the first reactant gas cooler 46c of this embodiment functions not only as a reactant gas cooler that cools the reactant gas RG, but also as a fuel preheater that preheats the treated reactant gas RGp, which is fuel for the gas turbine 11. Therefore, the first reaction gas cooler 46c, which also functions as a fuel preheater, is a component of the raw material reaction apparatus 41b and also a component of the reaction gas utilization facility 10.

[0218] The treated reactant gas RGp is ​​a type of third heat medium that cools the reactant gas RG in the first reactant gas cooler 46c. Therefore, the first fuel line 12a through which the treated reactant gas RGp flows is a type of third heat medium line. One end of a second fuel line 12b is connected to a third heat medium outlet of the first reactant gas cooler 46c. The other end of this second fuel line 12b is connected to the combustor 11c.

[0219] One end of a branched water supply line 91 is connected to a third heat medium inlet of the second reactant gas cooler 46d. The other end of the branched water supply line 91 is connected to the water supply line 35. Therefore, the supply water is a type of third heat medium for the second reactant gas cooler 46d. The branched water supply line 91 is a type of third heat medium line. The second reactant gas cooler 46d is a heat exchanger. This second reactant gas cooler 46d cools the reactant gas RG by exchanging heat between the reactant gas RG flowing through the reactant gas line 47 and the supply water flowing through the branched water supply line 91. One end of a supply water recovery line 75 is connected to a third heat medium outlet of the second reactant gas cooler 46d. The other end of this supply water recovery line 75 is connected to the water supply line 35. Therefore, this supply water recovery line 75 is a type of third heat medium recovery line.

[0220] In the raw material preheating step of this embodiment, similarly to the above-described embodiments, liquid ammonia NH is pressurized by the raw material ammonia pump 43, flows into the preheaters 44e to 44i, and is preheated in these preheaters 44e to 44i by heat exchange with the second heat medium.

[0221] Liquid ammonia NH pressurized by the raw ammonia pump 43 first flows into the first preheater 44e, where it is preheated by heat exchange with a second heat medium. The second heat medium flowing into the first preheater 44e is heated water that flows into the first preheater 44e from the second preheater 44f via a first connected heated water line 78e. The heated water cooled by heat exchange with liquid ammonia NH in the first preheater 44e flows into the water supply line 35 via a first heated water recovery line 78a.

[0222] The liquid ammonia NH preheated in the first preheater 44e flows into the second preheater 44f, where it is further preheated by heat exchange with the second heat medium to become gaseous ammonia NHg. Thus, in this embodiment, the first preheater 44e and the second preheater 44d function as vaporizers for the liquid ammonia NH. The first preheater 44e functions as a liquid-phase preheater for the liquid ammonia NH, and the second preheater 44d functions as a phase-change preheater for the liquid ammonia NH. The second heat medium flowing into the second preheater 44f is low-pressure heated water that flows into the second preheater 44f from the second low-pressure economizer 23b via the low-pressure heated water line 76. As described above, a portion of the heated water cooled by heat exchange with the liquid ammonia NH in the second preheater 44f flows into the first preheater 44e via the first connected heated water line 78e. Another portion of this heated water flows into the second low-pressure economizer 23b via the second heated water recovery line 78b.

[0223] The gaseous ammonia NHg produced in the second preheater 44f flows into the third preheater 44g, where it is further preheated by heat exchange with the second heat medium. The second heat medium flowing into the third preheater 44g is the heated water flowing into the third preheater 44g from the fourth preheater 44h via the second connected heated water line 78f, and the medium-pressure heated water flowing into the third preheater 44g from the medium-pressure economizer 24a via the medium-pressure heated water line 77. The heated water cooled by heat exchange with the gaseous ammonia NHg in the third preheater 44g flows into the second low-pressure economizer 23b via the third heated water recovery line 78c.

[0224] The gaseous ammonia NHg preheated in the third preheater 44g flows into the fourth preheater 44h, where it is further preheated by heat exchange with the second heat medium. The second heat medium flowing into the fourth preheater 44h is high-pressure heated water that flows into the fourth preheater 44h from the second high-pressure economizer 25b via the high-pressure heated water line 81. The heated water cooled by heat exchange with the gaseous ammonia NHg in the fourth preheater 44h flows into the third preheater 44g via the second connected heated water line 78f, as described above.

[0225] The gaseous ammonia NHg preheated in the fourth preheater 44h flows into the fifth preheater 44i, where it is further preheated by heat exchange with the second heat medium. Thus, in this embodiment, the third preheater 44g, the fourth preheater 44h, and the fifth preheater 44i function as gas heaters for the gaseous ammonia NHg. This completes the raw material preheating process of this embodiment. The second heat medium flowing into the fifth preheater 44i is the high-pressure steam flowing into the fifth preheater 44i from the second high-pressure superheater 25e via the high-pressure steam line 83. The steam cooled by heat exchange with the gaseous ammonia NHg in the fifth preheater 44i flows into the first high-pressure reheater 26a via the high-pressure steam recovery line 86. The first high-pressure reheater 26a superheats the steam from the fifth preheater 44i by heat exchange with the exhaust gas EG. The second high-pressure reheater 26b exchanges heat between the steam from the first high-pressure reheater 26a and the exhaust gas EG, heating the steam to generate high-pressure reheat steam. As described above, this high-pressure reheat steam flows into the high-pressure steam turbine 33 via the high-pressure reheat steam line 84. The high-pressure steam turbine 33 is driven by this high-pressure reheat steam. As described above, a portion of the steam exhausted from the high-pressure steam turbine 33 flows into the intermediate-pressure steam turbine 32 via the high-pressure exhaust steam line 85. The other portion of the steam exhausted from the high-pressure steam turbine 33 flows into the reboiler 139 via the second high-pressure exhaust steam line 85b.

[0226] The gaseous ammonia NHg from the fifth preheater 44i flows into the reactor 45, and similarly to the above embodiment, is decomposed into hydrogen and nitrogen by a thermal decomposition reaction to generate a reaction gas RG (reaction carrying out step).

[0227] In the reaction gas cooling step, the reaction gas RG is cooled by heat exchange between the reaction gas RG and the third heat medium. The reaction gas RG from the reactor 45 flows into the first reaction gas cooler 46c and the second reaction gas cooler 46d in this order, and is sequentially cooled as it passes through them.

[0228] In the first reactant gas cooler 46c, the reactant gas RG from the reactor 45 is cooled and the treated reactant gas RGp is ​​heated by heat exchange between the reactant gas RG and the treated reactant gas RGp from the residual raw material removal device 130, which serves as a third heat medium. The treated reactant gas RGp heated in the first reactant gas cooler 46c flows into the combustor 11c as fuel. Therefore, the first reactant gas cooler 46c also functions as a fuel preheater, as described above.

[0229] The reactant gas RG cooled in the first reactant gas cooler 46c flows into the second reactant gas cooler 46d. In the second reactant gas cooler 46d, the reactant gas RG is cooled and the feedwater is heated by heat exchange between the reactant gas RG and the feedwater from the branch feedwater line 91. The feedwater heated in the second reactant gas cooler 46d flows into the feedwater line 35 via the feedwater recovery line 75.

[0230] This completes the reaction gas cooling process. The reaction gas RG cooled in the second reaction gas cooler 46d flows into the residual raw material removal device 130, where residual ammonia contained in the reaction gas RG is removed in the same manner as in the above embodiment.

[0231] As described above, the second heat medium that preheats ammonia NH by heat exchange with the ammonia NH may be water or steam as a heat cycle medium flowing in the exhaust heat utilization heat cycle. Also, the third heat medium that cools the reactant gas RG by heat exchange with the reactant gas RG may be water as a heat cycle medium flowing in the exhaust heat utilization heat cycle. Also, the third heat medium may be the treated reactant gas RGp as fuel.

[0232] In this embodiment, the first heat medium from the first heat medium heater 27 is used in the reactor 45, the second heat medium (high-pressure steam) from the second high-pressure superheater 25e is used in the fifth preheater 44i, the second heat medium (high-pressure heating water) from the second high-pressure economizer 25b is used in the fourth preheater 44h, the second heat medium (medium-pressure heating water) from the medium-pressure economizer 24a is used in the third preheater 44g, and the second heat medium (low-pressure heating water) from the second low-pressure economizer 23b is used in the second preheater 44f.

[0233] The required temperature relationships of the heat transfer media are as follows: Required temperature of the first heat transfer medium used in reactor 45 > Required temperature of the second heat medium used in the fifth preheater 44i > Required temperature of the second heat medium used in the fourth preheater 44h > Required temperature of the second heat medium used in the third preheater 44g > Required temperature of the second heat medium used in the second preheater 44f

[0234] As described above, in this embodiment, the raw ammonia NH is heated using a plurality of heat exchangers to convert the raw ammonia NH into the reaction gas RG. Moreover, a heat medium having a temperature necessary and sufficient for heating the ammonia NH is supplied to each of the plurality of heat exchangers. Therefore, in this embodiment, heat can be effectively used to convert the raw ammonia NH into the reaction gas RG. Therefore, in this embodiment, heat at the lowest possible temperature can be effectively used to convert the raw ammonia NH into the reaction gas RG.

[0235] Furthermore, in this embodiment, even when a large amount of relatively high-temperature heat is consumed in the reaction of the raw material fluid, i.e., ammonia NH, the treated reactant gas RGp, which is a type of third heat medium and is the fuel input to the gas turbine 11, can be heated to a high temperature by using the high-temperature exhaust heat from the first reactant gas cooler 46c. Therefore, in this embodiment, the required fuel flow rate of the gas turbine 11 can be reduced, and the efficiency of the plant can be improved. Furthermore, in this embodiment, as a result of the above, when liquid ammonia NH is converted into the reactant gas RG, the heat utilization efficiency of the exhaust gas EG is improved, and from this viewpoint as well, the efficiency of the plant can be improved.

[0236] The heating of the raw material fluid in this embodiment will be described with reference to Fig. 7. Similar to Fig. 4, Fig. 7 is a TQ diagram for ammonia (solid line) and a heat source for heating the ammonia (dashed line). In Fig. 7, the horizontal axis represents the amount of heat, and the vertical axis represents the temperature.

[0237] In the first preheater (liquid-phase preheater) 44e, as described above, heat exchange occurs between the liquid ammonia NH and the second heat medium for liquid-phase preheating, and the liquid ammonia NH is heated while still in liquid form. In the second preheater (phase-change preheater) 44f, as described above, heat exchange occurs between the liquid ammonia NH from the first preheater (liquid-phase preheater) 44e and the second heat medium for phase-change preheating, and the liquid ammonia NH is heated and vaporized to form gaseous ammonia NHg. This gaseous ammonia NHg is sequentially heated in the third preheater (gas heater) 44g, the fourth preheater (gas heater) 44h, and the fifth preheater (gas heater) 44i. In Figure 7, the temperature change relative to the change in heat quantity during the heating (preheating) process of this gaseous ammonia NHg is simplified and depicted as a straight line.

[0238] The second preheater (phase change preheater) 44f is supplied with low-pressure heating water flowing into the second preheater 44f from the second low-pressure economizer 23b via the low-pressure heating water line 76 as a phase-change preheating second heat medium. Furthermore, a portion of the phase-change preheating second heat medium flowing out of the second preheater (phase change preheater) 44f is supplied to the first preheater (liquid-phase preheater) 44e as a liquid-phase preheating second heat medium. Therefore, the flow rate of the phase-change preheating second heat medium differs from the flow rate of the liquid-phase preheating second heat medium. Furthermore, the temperature of the phase-change preheating second heat medium at the inlet of the second preheater (phase change preheater) 44f differs from the temperature of the liquid-phase preheating second heat medium at the inlet of the first preheater (liquid-phase preheater) 44e. Therefore, the phase-change preheating second heat medium and the liquid-phase preheating second heat medium are both water but are different second heat media.

[0239] Here, the flow rate of the second phase-change preheating heat medium is greater than the flow rate of the second liquid-phase preheating heat medium. The constant-pressure specific heat of the second phase-change preheating heat medium is equal to that of the second liquid-phase preheating heat medium. Therefore, the product of the constant-pressure specific heat of the second phase-change preheating heat medium and the flow rate is greater than the product of the constant-pressure specific heat of the second liquid-phase preheating heat medium and the flow rate. The slope of the TQ line for a medium that does not involve a phase change or chemical reaction is inversely proportional to the product of the constant-pressure specific heat and the flow rate, i.e., the heat capacity per unit time. Therefore, in Figure 7, the slope of the TQ line for the second phase-change preheating heat medium is smaller than the slope of the TQ line for the second liquid-phase preheating heat medium. When ammonia vaporizes, it absorbs heat and evaporates at a constant temperature. Therefore, the TQ line of ammonia is parallel to the horizontal axis, and heat exchange occurs between the second phase-change preheating heat medium and ammonia while maintaining a small, nearly constant temperature difference. On the other hand, in the first preheater (liquid-phase preheater) 44e, liquid ammonia is preheated while still in liquid form, so the TQ line of this ammonia has a slope. Also, as described above, the product of the constant pressure specific heat and the flow rate, i.e., the heat capacity per unit time, of the second heat medium for liquid-phase preheating is small, so the slope of the TQ line of this second heat medium for liquid-phase preheating is large.

[0240] The flow rate of the liquid-phase preheating second heat medium can be adjusted by adjusting the flow rate of water returned to the second low-pressure economizer 23b via the second heated water recovery line 78b. Therefore, the heat capacity per unit time of the liquid-phase preheating second heat medium, i.e., the product of the constant-pressure specific heat and the flow rate, can be made equal to the heat capacity per unit time of liquid ammonia, i.e., the product of the constant-pressure specific heat and the flow rate, thereby making the slopes of the TQ lines of liquid ammonia and liquid-phase preheating second heat medium equal. Therefore, in this embodiment, by adjusting the flow rate of the liquid-phase preheating second heat medium, the slopes of the TQ lines of liquid ammonia and liquid-phase preheating second heat medium are made equal, and heat is exchanged between the liquid ammonia and the liquid-phase preheating second heat medium while maintaining a constant temperature difference between them. As a result, in this embodiment, liquid ammonia can be preheated with a minimum flow rate of the liquid-phase preheating second heat medium, allowing heat to be used effectively.

[0241] In addition, in this embodiment, as described above, the product of the constant pressure specific heat and the flow rate of the phase-change preheating second heat medium is larger than the product of the constant pressure specific heat and the flow rate of the liquid-phase preheating second heat medium. Therefore, in this embodiment, a large amount of heat can be supplied to liquid ammonia for vaporization, which requires a large amount of heat, and a small amount of heat can be supplied to preheating gaseous ammonia, which does not require a sufficient phase change and requires a small amount of heat.

[0242] From the above, in this embodiment, the TQ line of the second heat medium can be aligned with the TQ line of the ammonia (feedstock fluid). Therefore, in this embodiment, the temperature difference between the second heat medium and the ammonia (feedstock fluid) can be reduced, the amount of heat required for each temperature level can be supplied without excess or deficiency, and the heat utilization efficiency can be improved, thereby improving the plant efficiency.

[0243] Although the second heat medium for phase change preheating and the second heat medium for liquid phase preheating must be different media, they do not need to be different substances; they only need to have different heat capacities or temperatures, i.e., the product of the specific heat at constant pressure and the flow rate.

[0244] Alternatively, a gaseous phase heat medium may be supplied to the second preheater (phase change preheater) 44f as the phase-change preheating second heat medium, and the phase-change preheating second heat medium may be condensed in the second preheater (phase change preheater) 44f. Condensing the gaseous phase-change preheating second heat medium in the second preheater (phase change preheater) 44f and vaporizing the liquid ammonia (feedstock fluid) using the heat of condensation results in heat exchange between the phase-change preheating second heat medium and the feedstock fluid, while maintaining constant temperatures and reducing the temperature difference ΔT2 between them, as shown in FIG. 8 . Supplying the gaseous phase-change preheating second heat medium to the second preheater (phase change preheater) 44f and condensing the phase-change preheating second heat medium therein improves heat utilization efficiency and plant efficiency. Examples of such a gas-phase second heat medium for second vaporization include steam evaporated in the low-pressure evaporator 23d and steam extracted from the intermediate stage of the low-pressure steam turbine 31, as will be described later in the sixth embodiment.

[0245] "Fourth Embodiment" A fourth embodiment of the raw fluid processing plant will be described with reference to FIGS.

[0246] The raw material fluid processing plant of this embodiment is a modified example of the raw material fluid processing plant of the third embodiment. The raw material fluid processing plant of this embodiment promotes the thermal decomposition reaction of ammonia NH more than the raw material fluid processing plant of the third embodiment. Therefore, the reaction execution step of the series of operations in the raw material fluid processing plant of this embodiment is different from the reaction execution step of the third embodiment.

[0247] As in the above embodiments, the raw material fluid processing plant of this embodiment also includes a raw material reaction facility 40c, a reaction gas utilization facility 10, and a waste heat utilization facility 20c, as shown in FIG.

[0248] The heat recovery boiler 21c of the waste heat utilization equipment 20c, like the heat recovery boiler 21b of the third embodiment, includes a gas frame 22, a first low-pressure economizer 23a, a second low-pressure economizer 23b, a low-pressure evaporator 23c, a low-pressure superheater 23f, an intermediate-pressure economizer 24a, an intermediate-pressure evaporator 24b, a first high-pressure economizer 25a, a second high-pressure economizer 25b, a high-pressure evaporator 25c, a first high-pressure superheater 25d, a second high-pressure superheater 25e, a first high-pressure reheater 26a, a second high-pressure reheater 26b, a high-pressure pump 25p, and first heat medium heaters 27a and 27b. The heat recovery boiler 21c of this embodiment further includes a third high-pressure reheater 26c and a burner 28. The first heat medium heaters 27a, 27b of this embodiment include a first low-temperature heat medium heater 27a and a first high-temperature heat medium heater 27b.

[0249] The burner 28, the first high-temperature heat medium heater 27b, the third high-pressure reheater 26c, and the first low-temperature heat medium heater 27a are arranged upstream of the second high-pressure reheater 26b within the gas frame 22. The heat recovery boiler 21c has a partition member 29 that divides the upstream side of the exhaust gas EG flow from the first high-temperature heat medium heater 27b within the gas frame 22 into a first exhaust gas flow path 29a through which a portion of the exhaust gas EG flows and a second exhaust gas flow path 29b through which the remaining portion of the exhaust gas EG flows. The burner 28, the first high-temperature heat medium heater 27b, and the third high-pressure reheater 26c are arranged in this order from upstream to downstream within the first exhaust gas flow path 29a. A branch fuel line 12c branching from the fuel line 12 is connected to the burner 28. The burner 28 injects the treated reaction gas RGp as fuel from the branch fuel line 12c into the exhaust gas EG flowing through the first exhaust gas flow path 29a. The fuel injected into the gas frame 22 is combusted. As a result, combustion gas is generated, and high-temperature gas flows in the first exhaust gas passage 29a. In the gas frame 22, downstream of the partition member 29, the combustion gas flowing in the first exhaust gas passage 29a and the exhaust gas EG flowing in the second exhaust gas passage 29b merge. In the gas frame 22, downstream of the partition member 29, a first low-temperature heat medium heater 27a and a second high-pressure reheater 26b are arranged in this order.

[0250] The reactors 45a, 45b of the raw material reaction device 41c in the raw material reaction facility 40c include a pre-reactor 45a and a post-reactor 45b.

[0251] One end of a first low-temperature heat medium line 51a is connected to the first heat medium inlet of the pre-reactor 45a. The other end of this first low-temperature heat medium line 51a is connected to the outlet of the first low-temperature heat medium heater 27a. One end of a first low-temperature heat medium recovery line 52a is connected to the first heat medium outlet of the pre-reactor 45a. The other end of this first low-temperature heat medium recovery line 52a is connected to the inlet of the first low-temperature heat medium heater 27a. The outlet of the second high-pressure reheater 26b is also connected to the inlet of the first low-temperature heat medium heater 27a. A first heat medium booster 53 is provided on the first low-temperature heat medium recovery line 52a.

[0252] The outlet of the first low-temperature heat medium heater 27a is further connected to the inlet of a third high-pressure reheater 26c. The outlet of the third high-pressure reheater 26c is connected to one end of a high-pressure reheat steam line 84. The other end of the high-pressure reheat steam line 84 is connected to the inlet of the high-pressure steam turbine 33.

[0253] The outlet of the first low-temperature heat medium heater 27a is further connected to the inlet of a first high-temperature heat medium heater 27b. One end of a first high-temperature heat medium line 51b is connected to the outlet of the first high-temperature heat medium heater 27b. The other end of the first high-temperature heat medium line 51b is connected to the first heat medium inlet of the post-reactor 45b. One end of a first high-temperature heat medium recovery line 52b is connected to the first heat medium outlet of the post-reactor 45b. The other end of the first high-temperature heat medium recovery line 52b is connected to the first heat medium inlet of the pre-reactor 45a.

[0254] The first low-temperature heat medium heater 27a receives the steam superheated in the second high-pressure reheater 26b and the steam from the first low-temperature heat medium recovery line 52a. The first low-temperature heat medium heater 27a exchanges heat between the steam and the exhaust gas EG, thereby superheating the steam.

[0255] A portion of the steam superheated in the first low-temperature heat medium heater 27a flows into the pre-reactor 45a via the first low-temperature heat medium line 51a as the first low-temperature heat medium. Another portion of the steam superheated in the first low-temperature heat medium heater 27a flows into the third high-pressure reheater 26c. The third high-pressure reheater 26c comes into contact with high-temperature combustion gas. Fuel from the burner 28 is injected into the exhaust gas EG from the gas turbine 11, and this fuel is combusted to generate high-temperature combustion gas. The third high-pressure reheater 26c comes into contact with this high-temperature combustion gas. The third high-pressure reheater 26c exchanges heat between the high-temperature combustion gas and steam, superheating the steam. The steam flows into the high-pressure steam turbine 33 via the high-pressure reheat steam line 84 and drives the high-pressure steam turbine 33. Therefore, the temperature of the steam flowing into the high-pressure steam turbine 33 in this embodiment is higher than the temperature of the steam flowing into the high-pressure steam turbine 33 in the third embodiment. Therefore, in this embodiment, the output of the high-pressure steam turbine 33 can be increased.

[0256] The remainder of the steam superheated in the first low-temperature heat medium heater 27a flows into the first high-temperature heat medium heater 27b. The first high-temperature heat medium heater 27b superheats the steam by heat exchange between the high-temperature mixed gas and the steam. This steam flows into the post-reactor 45b as the first high-temperature heat medium via the first high-temperature heat medium line 51b. The temperature of this first high-temperature heat medium is higher than the temperature of the first low-temperature heat medium.

[0257] In the reaction performing step of this embodiment, similarly to the above embodiments, heat is exchanged between gaseous ammonia NH and the first heat medium, and the gaseous ammonia NH is heated to cause a thermal decomposition reaction, thereby generating a reaction gas RG.

[0258] The gaseous ammonia NHg preheated in the fifth preheater 44i flows into the pre-reactor 45a. Steam flows into this pre-reactor 45a from the post-reactor 45b via the first high-temperature heat medium recovery line 52b as the first low-temperature heat medium. Furthermore, steam flows into this pre-reactor 45a from the first low-temperature heat medium heater 27a via the first low-temperature heat medium line 51a as the first low-temperature heat medium. The pre-reactor 45a exchanges heat between the gaseous ammonia NHg and the first low-temperature heat medium, heating the gaseous ammonia NHg and cooling the first low-temperature heat medium. The cooled steam, which is the first low-temperature heat medium, flows into the first low-temperature heat medium heater 27a via the first low-temperature heat medium recovery line 52a. Furthermore, a portion of the heated gaseous ammonia NHg undergoes a thermal decomposition reaction to become a reaction gas RG containing hydrogen, oxygen, and ammonia.

[0259] The reaction gas RG generated in the pre-reactor 45a flows into the post-reactor 45b. Steam superheated in the first high-temperature heat medium heater 27b flows into this post-reactor 45b as a first high-temperature heat medium. The post-reactor 45b exchanges heat between the reaction gas RG from the pre-reactor 45a and the first high-temperature heat medium, heating the reaction gas RG while cooling the first high-temperature heat medium. The cooled steam, which is the first high-temperature heat medium, flows into the pre-reactor 45a as a first low-temperature heat medium via the first high-temperature heat medium line 51b. A portion of the gaseous ammonia NHg contained in the heated reaction gas RG undergoes a thermal decomposition reaction to become a reaction gas RG containing hydrogen, oxygen, and ammonia NH.

[0260] Heating of the raw material fluid in this embodiment will be described with reference to Fig. 10. Similar to Fig. 4 etc., Fig. 10 is a TQ diagram for ammonia (solid line) and a heat source for heating the ammonia (dashed line). In Fig. 10, the horizontal axis represents the amount of heat, and the vertical axis represents the temperature.

[0261] The thermal decomposition reaction of ammonia is promoted as the temperature of the reaction environment increases. Furthermore, as shown in FIG. 10, as the ammonia concentration decreases during the thermal decomposition reaction, the rate of temperature increase relative to the increase in heat gradually increases. In this embodiment, as described above, gaseous ammonia NHg is first introduced into the pre-reactor 45a and heat-exchanged with a first low-temperature heat medium to produce a reaction gas RG containing hydrogen, oxygen, and ammonia. In this embodiment, the reaction gas RG is then introduced into the post-reactor 45b and heat-exchanged with a first high-temperature heat medium, which is hotter than the first low-temperature heat medium, to thermally decompose the ammonia contained in the reaction gas RG. Therefore, in this embodiment, the concentration of residual ammonia contained in the reaction gas RG flowing out from the post-reactor 45b can be made lower than the concentration of residual ammonia contained in the reaction gas RG flowing out from the reactor 45 in the above-described embodiments.

[0262] In the first, second, and third embodiments, only the exhaust gas EG from the gas turbine 11 is used as a heat source to generate a first heat medium used in the thermal decomposition reaction of ammonia (feedstock fluid). Therefore, in the first, second, and third embodiments, a first heat medium having a temperature higher than the temperature of the exhaust gas EG at the outlet of the gas turbine 11 is obtained, and the feedstock fluid cannot be reacted at a temperature higher than the temperature of the exhaust gas EG at the outlet of the gas turbine 11. On the other hand, in the present embodiment, fuel is added to the exhaust gas EG and reheated. Therefore, a first heat medium having a temperature higher than the temperature of the exhaust gas EG at the outlet of the gas turbine 11, which is the reactive gas utilization facility (exhaust gas generation facility), is obtained, and the feedstock fluid can be reacted at a temperature higher than the temperature of the exhaust gas EG at the outlet of the gas turbine 11, which is the reactive gas utilization facility (exhaust gas generation facility). Furthermore, in the present embodiment, the exhaust gas EG from the gas turbine 11 is diverted, and additional fuel is added to and combusted in only a portion of the diverted gas. Therefore, the temperature of the exhaust gas can be increased with a small amount of additional fuel. This improves plant efficiency.

[0263] In this embodiment, the first high-temperature heat medium used in the post-reactor 45b plus steam supplied from the first low-temperature heat medium heater 27a is supplied to the pre-reactor 45a as the first low-temperature heat medium. Therefore, in this embodiment, the flow rate of the first low-temperature heat medium, which is the heat source of the pre-reactor 45a, is greater than that of the first high-temperature heat medium. Because the first low-temperature heat medium and the first high-temperature heat medium have the same pressure and constant-pressure specific heat, the product of the constant-pressure specific heat and flow rate of the first low-temperature heat medium, i.e., the heat capacity per unit time, is greater than the product of the constant-pressure specific heat and flow rate of the first high-temperature heat medium. For a medium that does not involve a phase change or chemical reaction, the slope of the TQ line is inversely proportional to the product of the constant-pressure specific heat and flow rate, i.e., the heat capacity per unit time. Therefore, as shown in FIG. 10, the slope of the TQ line of the first low-temperature heat medium in the pre-reactor 45a is smaller than the slope of the TQ line of the first high-temperature heat medium in the post-reactor 45b.

[0264] The temperature level of the pre-reactor 45a is near the temperature at which the reaction of ammonia (raw material fluid) proceeds most actively, and a large amount of heat is required for the reaction, so the slope of the TQ line of ammonia in the pre-reactor 45a is small. On the other hand, in the post-reactor 45b, the amount of remaining ammonia decreases, the reaction amount decreases, and the amount of heat required for the reaction also decreases, so the temperature rises with a small amount of heat. Therefore, the slope of the TQ line of ammonia in the post-reactor 45b is large.

[0265] By adjusting the flow rate of steam supplied from the first low-temperature heat medium heater 27a to the pre-reactor 45a via the first low-temperature heat medium line 51a without passing through the post-reactor 45b, the heat capacities of the first low-temperature heat medium and the first high-temperature heat medium can be adjusted independently. Therefore, by adjusting the heat capacity of the first low-temperature heat medium, the slope of the TQ line of this first low-temperature heat medium can be made closer to the slope of the TQ line of the ammonia and reactant gas in the pre-reactor 45a. Furthermore, by adjusting the heat capacity of the first high-temperature heat medium, the slope of the TQ line of this first high-temperature heat medium can be made closer to the slope of the TQ line of the ammonia and reactant gas in the post-reactor 45b.

[0266] In this embodiment, as described above, the product of the constant pressure specific heat and the flow rate of the first low-temperature heat transfer medium is larger than the product of the constant pressure specific heat and the flow rate of the first high-temperature heat transfer medium, so that the reaction proceeds vigorously and a large amount of heat can be supplied to the pre-reactor 45a, which requires a large amount of heat, and a small amount of heat can be supplied to the post-reactor 45b, which requires a small amount of heat.

[0267] From the above, in this embodiment, the TQ lines of the first low-temperature heat transfer medium and the first high-temperature heat transfer medium can be aligned with the TQ lines of the ammonia and the reactant gas in the pre-reactor 45a and the post-reactor 45b, respectively. Therefore, in this embodiment, the temperature difference between the first heat transfer medium and the ammonia (raw material fluid) and the reactant gas is reduced, the amount of heat required for each temperature level is supplied without excess or deficiency, and the heat utilization efficiency and plant efficiency can be improved.

[0268] Although the first low-temperature heat medium and the first high-temperature heat medium need to be different media, they do not need to be different substances, as long as they have different product of constant pressure specific heat and flow rate, i.e., different heat capacities, or different temperatures.

[0269] Furthermore, in this embodiment, as described above, the concentration of residual ammonia contained in the reactive gas RG can be reduced, so that the energy consumption in the residual raw material removal unit 130 can be reduced.

[0270] In this embodiment, the temperature of the reaction gas is further increased in the post-reactor 45b using a high-temperature first high-temperature heat medium, so the temperature of the reaction gas RG at the inlet of the first reaction gas cooler 46c is higher than in the third embodiment. Therefore, in the first reaction gas cooler 46c, the treated reaction gas RGp, which serves as fuel, can be preheated to a temperature higher than in the third embodiment and then input into the combustor 11c of the gas turbine 11. Therefore, in this embodiment, the fuel consumption of the gas turbine 11 can be reduced and plant efficiency can be further improved. The gas turbine 11 is a type of thermal cycle, and the treated reaction gas RGp is ​​a type of third heat medium used in the thermal cycle. Therefore, the high-temperature third heat medium can be used in the thermal cycle, which improves plant efficiency as described above. In this embodiment, the reaction in the post-reactor 45b can be realized at a temperature higher than the temperature of the exhaust gas EG at the outlet of the gas turbine 11, which is a type of reaction gas utilization equipment (exhaust gas generation equipment). Therefore, the temperature of the third heat medium can be increased to a temperature higher than the temperature of the exhaust gas EG at the outlet of the gas turbine 11, which is a type of reaction gas utilization equipment (exhaust gas generation equipment). Therefore, in this embodiment, by configuring in this way, it is possible to further improve the plant efficiency.

[0271] In this embodiment, the reactor includes a pre-reactor 45a and a post-reactor 45b, and the first heat medium heater includes a first low-temperature heat medium heater 27a and a first high-temperature heat medium heater 27b. However, similar to the above embodiments, there may be only one reactor and one first heat medium heater.

[0272] In this embodiment, the gas frame 22 is divided into two exhaust gas flow paths 29a, 29b. However, the gas frame 22 does not have to be divided into two exhaust gas flow paths. In this case, one first heat medium heater heats the first heat medium by exchanging heat between the first heat medium and combustion gas formed by combustion of fuel injected from the burner 28 into the exhaust gas EG from the gas turbine 11. The first heat medium heated by one first heat medium heater flows into one reactor 45, where it heats gaseous ammonia NHg and causes the gaseous ammonia NHg to undergo a thermal decomposition reaction.

[0273] Furthermore, a natural gas line 15 through which natural gas NG flows may be connected to the fuel line 12 through which the treated reactant gas RGp flows. This natural gas line 15 is connected, for example, to the upstream side of the fuel preheater (first reactant gas cooler 46c) in the fuel line 12. As described above, by connecting the natural gas line 15 to the fuel line 12, it is possible to operate the turbine using only natural gas NG, for example, when the gas turbine exhaust gas cannot be obtained at a temperature required for generating the reactant gas during startup or low load. Note that, in other embodiments, the natural gas line 15 through which natural gas NG flows may also be connected to the fuel line 12. Although not shown, natural gas may be supplied to the burner 28 instead of the treated reactant gas RG. This facilitates temperature control of the combustion gas at the outlet of the burner 28. Note that, in other embodiments, when a burner is added, either the treated reactant gas RG or natural gas may be supplied to the burner. Furthermore, only a fuel other than the reactant gas RG or the treated reactant gas RGp, such as natural gas, may be supplied to the fuel line 12. In this case, the gas turbine 11 is an exhaust gas generating facility, but is not a reactive gas utilizing facility.

[0274] Fifth Embodiment A fifth embodiment of the raw fluid processing plant will be described with reference to FIG.

[0275] The raw material fluid processing plant of this embodiment is a modified example of the raw material fluid processing plant of Embodiment 2. In the raw material fluid processing plant of this embodiment, part of ammonia is subjected to an autothermal decomposition reaction.

[0276] Similar to the above-described embodiments, the raw material fluid processing plant of this embodiment also includes a raw material reaction facility 40d, a reaction gas utilization facility 10d, and a waste heat utilization facility 20d.

[0277] Like the raw material reaction equipment of the above embodiments, raw material reaction equipment 40d of this embodiment includes a raw material reaction apparatus 41d and a residual raw material removal apparatus 130. Raw material reaction apparatus 41d of this embodiment differs from raw material reaction apparatus 41a of the second embodiment. On the other hand, residual raw material removal apparatus 130 of this embodiment is the same as the residual raw material removal apparatus 130 of the above embodiments.

[0278] The reaction gas utilization equipment 10d of this embodiment is basically the same as the reaction gas utilization equipment 10 of the above-described embodiments. However, the fuel preheaters in the reaction gas utilization equipment 10d include a first fuel preheater 13a and a second fuel preheater 13b. Furthermore, the exhaust heat utilization equipment 20d of this embodiment is different from the exhaust heat utilization equipment of the above-described embodiments.

[0279] Similar to the above-described embodiments, the waste heat utilization equipment 20d of this embodiment includes a waste heat recovery steam generator 21, a low-pressure steam turbine 31, an intermediate-pressure steam turbine 32, a high-pressure steam turbine 33, a condenser 34, a feedwater line 35, a feedwater pump 36, and a chimney 39. The waste heat utilization equipment 20d of this embodiment further includes a feedwater preheater 37 that preheats feedwater. The feedwater preheater 37 is provided on the feedwater line 35. One end of an extracted steam line 95 is connected to a medium inlet of the feedwater preheater 37. The other end of the extracted steam line 95 is connected to a casing of the low-pressure steam turbine 31. One end of an extracted steam recovery line 94 is connected to a medium outlet of the feedwater preheater 37. The other end of the extracted steam recovery line 94 is connected to a position in the feedwater line 35 closer to the condenser 34 than the feedwater preheater 37. The heat recovery steam generator 21 is the same as the heat recovery steam generator 21 of the second embodiment. Note that one end of a high-pressure steam line 83 is connected to an outlet of the high-pressure superheater 25d of the heat recovery steam generator 21 of the present embodiment. The other end of this high-pressure steam line 83 is connected to an inlet of the high-pressure steam turbine 33. Therefore, in the present embodiment, similarly to the first embodiment, high-pressure steam from the high-pressure superheater 25d flows into the high-pressure steam turbine 33 via the high-pressure steam line 83.

[0280] Similar to the raw material reactor 41a of the second embodiment, the raw material reactor 41d of this embodiment includes an ammonia supply line 42, a raw material ammonia pump 43, a first preheater 44c, a second preheater 44d, reactors 45a and 45b, a first reactant gas cooler 46a, a second reactant gas cooler 46b, and a reactant gas line 47. However, the reactors 45a and 45b of this embodiment include a pre-reactor 45a and a post-reactor 45b. The raw material reactor 41d of this embodiment further includes an oxidant introducing device 60 that introduces an oxidant into ammonia NH, which is the raw material fluid NH.

[0281] The oxidant in this embodiment is air. The oxidant introduction device 60 includes an oxidant receiving line 61 through which the gaseous oxidant flows, an oxidant cooler 62 that cools the oxidant from the oxidant receiving line 61, an oxidant compressor 63 that compresses the oxidant cooled in the oxidant cooler 62, an oxidant heater 64 that heats the oxidant compressed in the oxidant compressor 63, and an oxidant introduction line 65 that introduces the oxidant heated in the oxidant heater 64 to the reactor 45.

[0282] The gas turbine 11 has a combustion air passage 11b that connects the discharge port of the air compressor 11a and the compressed air inlet of the combustor 11c. Combustion air from the air compressor 11a flows through the combustion air passage 11b. One end of an oxidant receiving line 61 is connected to the combustion air passage 11b. The other end of the oxidant receiving line 61 is connected to the inlet of the oxidant compressor 63. An oxidant cooler 62 is provided on the oxidant receiving line 61. The oxidant cooler 62 is a heat exchanger. One end of a high-pressure feedwater line 79 is connected to a medium inlet of the oxidant cooler 62. The other end of the high-pressure feedwater line 79 is connected to the discharge port of the high-pressure pump 25p in the heat recovery boiler 21. One end of a high-pressure feedwater recovery line 80 is connected to a medium outlet of the oxidant cooler 62. The other end of the high-pressure feedwater recovery line 80 is connected to the inlet of the high-pressure evaporator 25c in the heat recovery boiler 21. The oxidant compressor 63 pressurizes the oxidant cooled in the oxidant cooler 62 to a pressure at which the oxidant can be introduced into the reactors 45a, 45b. The oxidant heater 64 is a heat exchanger. One end of a second high-pressure heated water line 81a is connected to a medium inlet of the oxidant heater 64. The other end of the second high-pressure heated water line 81a is connected to an outlet of the second high-pressure economizer 25b in the heat recovery boiler 21. One end of a second high-pressure heated water recovery line 82a is connected to the medium outlet of the oxidant heater 64. The other end of the second high-pressure heated water recovery line 82a is connected to the inlet of the medium-pressure economizer 24a in the heat recovery boiler 21. The oxidant introduction line 65 has a first oxidant introduction line 65b and a second oxidant introduction line 65c. One end of the first oxidant introduction line 65b and one end of the second oxidant introduction line 65c are both connected to the oxidant outlet of the oxidant heater 64. The other end of the first oxidant introduction line 65b is connected to the pre-reactor 45a. The other end of the second oxidant introduction line 65c is connected to the post-reactor 45b.

[0283] In addition to the oxidant from the oxidant supply device 60, gaseous ammonia NHg from the second preheater 44d flows into the pre-reactor 45a. One end of a first heat medium line 51 is connected to a medium inlet of the pre-reactor 45a. The other end of the first heat medium line 51 is connected to an outlet of the first heat medium heater 27. One end of a first heat medium recovery line 52 is connected to a medium outlet of the pre-reactor 45a. The other end of the first heat medium recovery line 52 is connected to an inlet of the second heat medium heater. In addition to the oxidant from the oxidant supply device 60, the reaction gas RG from the pre-reactor 45a flows into the post-reactor 45b.

[0284] A first reactant gas line 47a is connected to the post-reactor 45b. Similar to the second embodiment, the first reactant gas line 47a is provided with a first reactant gas cooler 46a. Similarly to the second embodiment, the second reactant gas line 47b is provided with a second reactant gas cooler 46b.

[0285] The treated reactant gas RGp from the residual raw material removal device 130 flows into the first fuel preheater 13a in the reactant gas utilization facility 10d. One end of a high-pressure heated water line 81 is connected to a medium inlet of the first fuel preheater 13a, similar to the fuel preheater 13 of the second embodiment. One end of a high-pressure heated water recovery line 82 is connected to a medium outlet of the first fuel preheater 13a, similar to the fuel preheater 13 of the second embodiment. The treated reactant gas RGp preheated in the first fuel preheater 13a flows into the second fuel preheater 13b, which further preheats the treated reactant gas RGp. The treated reactant gas RGp preheated in the second fuel preheater 13b flows into the combustor 11c.

[0286] One end of a first high-pressure exhaust steam line 85a is connected to the third heat medium inlet of the first reaction gas cooler 46a. The other end of the first high-pressure exhaust steam line 85a is connected to the outlet of the high-pressure steam turbine 33. One end of a second high-pressure exhaust steam line 85b is connected to the third heat medium outlet of the first reaction gas cooler 46a. The other end of the second high-pressure exhaust steam line 85b is connected to the medium inlet of the second fuel preheater 13b. One end of a third high-pressure exhaust steam line 85c is connected to the medium outlet of the second fuel preheater 13b. The other end of the third high-pressure exhaust steam line 85c is connected to the inlet of the intermediate-pressure steam turbine 32.

[0287] A portion of the combustion air from the air compressor 11a of the gas turbine 11 flows as an oxidant into the oxidant cooler 62 via an oxidant receiving line 61. High-pressure feedwater from the high-pressure pump 25p of the heat recovery boiler 21 flows into the oxidant cooler 62 via a high-pressure feedwater line 79. The temperature of the combustion air from the air compressor 11a is, for example, approximately 450°C, and the pressure of this combustion air is, for example, approximately 2 MPa. The oxidant cooler 62 exchanges heat between the combustion air as an oxidant and the high-pressure feedwater, cooling the combustion air while heating the high-pressure feedwater. The heated high-pressure feedwater flows into the high-pressure evaporator 25c of the heat recovery boiler 21 via a high-pressure feedwater recovery line 80.

[0288] The oxidant compressor 63 compresses and pressurizes the combustion air cooled by the oxidant cooler 62. The pressure of the liquid ammonia NH flowing into the first preheater 44c is increased by the raw ammonia pump 43 to about 5 MPa as described above. Therefore, the pressure inside the pre-reactor 45a and the post-reactor 45b is also about 5 MPa. The oxidant compressor 63 increases the pressure of the oxidant to a pressure at which the oxidant can be introduced into the pre-reactor 45a and the post-reactor 45b. The oxidant cooler 62 cools the oxidant before it flows into the oxidant compressor 63 in order to reduce the compression power in the oxidant compressor 63.

[0289] The combustion air compressed by the oxidant compressor 63 flows into the oxidant heater 64. High-pressure heated water from the second high-pressure economizer 25b flows into this oxidant heater 64 via a second high-pressure heated water line 81a. The oxidant heater 64 exchanges heat between the combustion air as an oxidant and the high-pressure heated water, heating the combustion air while cooling the high-pressure heated water. The high-pressure heated water cooled in the oxidant heater 64 flows into the medium-pressure economizer 24a via a second high-pressure heated water recovery line 82a. The oxidant heater 64 supplies heat to the pre-reactor 45a and post-reactor 45b together with the combustion air as an oxidant, thereby increasing the temperature in the pre-reactor 45a and post-reactor 45b and activating the reaction in the pre-reactor 45a and post-reactor 45b even with a small amount of oxidant and a small oxidation reaction amount of the gas to be oxidized. Specifically, the oxidant heater 64 raises the temperature of the combustion air serving as the oxidant to a temperature close to or higher than the temperature of the gas to be oxidized flowing into each of the reactors 45a, 45b.

[0290] Gaseous ammonia NHg from the second preheater 44d and combustion air from the oxidant supply device 60 flow into the prereactor 45a. In the prereactor 45a, a portion of the gaseous ammonia NHg undergoes an oxidation reaction (combustion) with the combustion air. The heat generated by this oxidation reaction heats the gaseous ammonia NHg. Furthermore, the gaseous ammonia NHg is heated in the first heat medium heater 27 and then heated by heat exchange with the first heat medium. Therefore, in the prereactor 45a, the gaseous ammonia NHg is heated to a higher temperature than in the reactor 45 of the second embodiment, and the thermal decomposition reaction of the gaseous ammonia NHg is promoted.

[0291] The post-reactor 45b receives the reaction gas RG from the pre-reactor 45a and the combustion air from the oxidant supply device 60. In the post-reactor 45b, a portion of the gaseous ammonia NHg contained in the reaction gas RG from the pre-reactor 45a and a portion of the hydrogen generated by the thermal decomposition reaction in the pre-reactor 45a undergo an oxidation reaction (combustion) with the combustion air. The heat generated by this oxidation reaction heats the gaseous ammonia NHg. Therefore, in the post-reactor 45b, the gaseous ammonia NHg contained in the reaction gas RG from the pre-reactor 45a is heated, further accelerating the thermal decomposition reaction of this gaseous ammonia NHg.

[0292] As described above, in this embodiment, by introducing an oxidizing agent into each of the reactors 45 a, 45 b, a part of the gaseous ammonia NHg in each of the reactors 45 a, 45 b undergoes an oxidation reaction, thereby making it possible to increase the environmental temperature of the thermal decomposition reaction in each of the reactors 45 a, 45 b. Therefore, in this embodiment, it is possible to reduce the ammonia concentration in the reaction gas RG flowing out from each of the reactors 45 a, 45 b.

[0293] In this embodiment, combustion air from the air compressor 11a of the gas turbine 11 is used as the oxidant. This combustion air is air that has already been compressed by the air compressor 11a, and therefore has a higher pressure than atmospheric air. The oxidant compressor 63 increases the pressure of this combustion air to a pressure that allows it to be introduced into the pre-reactor 45a and post-reactor 45b. Therefore, in this embodiment, the driving force of the oxidant compressor 63 can be reduced compared to when the oxidant compressor 63 increases the pressure of atmospheric air to a pressure that allows it to be introduced into the pre-reactor 45a and post-reactor 45b.

[0294] The reaction gas RG from the post-reactor 45b flows into the first reaction gas cooler 46a via a reaction gas line 47. High-pressure steam exhausted from the high-pressure steam turbine 33 flows into the first reaction gas cooler 46a via a first high-pressure exhaust steam line 85a as a third heat medium. In the first reaction gas cooler 46a, heat exchange occurs between the reaction gas RG from the post-reactor 45b and the high-pressure steam exhausted from the high-pressure steam turbine 33, whereby the reaction gas RG is cooled and the high-pressure steam is superheated.

[0295] In the second preheater 44d, as in the second embodiment, the reaction gas RG cooled in the first reaction gas cooler 46a is further cooled by heat exchange with the gaseous ammonia NHg, while the gaseous ammonia NHg is preheated.

[0296] As in the second embodiment, the second reactant gas cooler 46b cools the reactant gas RG while heating the feedwater by heat exchange between the reactant gas RG cooled in the second preheater 44d and the feedwater as a third heat medium. The heated feedwater flows into the first preheater 44c as a second heat medium.

[0297] The reaction gas RG cooled by the second reaction gas cooler 46b flows into the residual raw material removal device 130, where residual ammonia contained in the reaction gas RG is removed, similar to the second embodiment.

[0298] The treated reactant gas RGp from the residual raw material removal unit 130 flows into the combustor 11c as fuel via the fuel line 12. During this process, the treated reactant gas RGp is ​​preheated sequentially by the first fuel preheater 13a and the second fuel preheater 13b. Similar to the fuel preheater 13 of the second embodiment, the first fuel preheater 13a heats the treated reactant gas RGp by exchanging heat between the treated reactant gas RGp and high-pressure heating water from the second high-pressure economizer 25b. The treated reactant gas RGp heated by the first fuel preheater 13a flows into the second fuel preheater 13b. Steam superheated in the first reactant gas cooler 46a also flows into the second fuel preheater 13b via the second high-pressure exhaust steam line 85b. In the second fuel preheater 13b, the treated reactant gas RGp heated in the first fuel preheater 13a is heated and the steam from the first reactant gas cooler 46a is cooled by heat exchange between the treated reactant gas RGp and the steam. The steam cooled in the second fuel preheater 13b flows into the intermediate-pressure steam turbine 32 via the third high-pressure exhaust steam line 85c and drives the intermediate-pressure steam turbine 32. The treated reactant gas RGp heated in the second fuel preheater 13b flows into the combustor 11c.

[0299] As described above, in this embodiment, an oxidizing agent for ammonia NH is introduced into each reactor 45, and part of this ammonia NH is burned to raise the environmental temperature of the thermal decomposition reaction in each reactor 45, thereby making it possible to lower the ammonia concentration in the reaction gas RG flowing through the reaction gas line 47. Therefore, in this embodiment as well, as in the fourth embodiment, it is possible to reduce energy consumption in the residual raw material removal apparatus 130.

[0300] In this embodiment, the oxidizing agent is introduced into both the pre-reactor 45a and the post-reactor 45b. However, the oxidizing agent may be introduced into either the pre-reactor 45a or the post-reactor 45b. When the oxidizing agent is introduced only into the pre-reactor 45a, the post-reactor 45b is not necessary.

[0301] In this embodiment, high-temperature exhaust heat in the first reactant gas cooler 46a is recovered by the high-pressure steam exhausted from the high-pressure steam turbine 33. Then, the heat of this high-pressure steam is utilized in the second fuel preheater 13b, and then this high-pressure steam is caused to flow into the intermediate-pressure steam turbine 32. Therefore, in this embodiment, the treated reactant gas RGp heated to a high temperature in the second fuel preheater 13b can be supplied to the gas turbine 11, thereby improving the efficiency of the gas turbine 11, and high-temperature steam can also be supplied to the inlet of the intermediate-pressure steam turbine 32, thereby increasing the output of the steam turbine and improving the efficiency of the plant.

[0302] When ammonia NH is decomposed using only the exhaust gas EG from the gas turbine 11 as a heat source to preheat the fuel input to the gas turbine 11 and drive the steam turbine, the reaction temperature of ammonia, the temperature of the fuel input to the gas turbine 11, and the steam temperature at the inlet of the steam turbine are all lower than the temperature of the exhaust gas EG at the outlet of the gas turbine 11. However, in this embodiment, the ammonia and a portion of the reaction gas are oxidized by an oxidizer in each of the reactors 45a and 45b, thereby raising the temperature of these gases. Therefore, the reaction temperature of the raw material fluid (ammonia in this case) can be made higher than the temperature of the exhaust gas EG at the outlet of the reaction gas utilization facility (or the exhaust gas generation facility (gas turbine 11 in this case)). Therefore, the concentration of the remaining raw material (ammonia in this case) in the reaction gas (ammonia decomposition gas in this case) at the outlet of the reactor 45 can be reduced. Furthermore, in this embodiment, the exhaust heat used to cool the reaction gas, which is hotter than the exhaust gas EG at the outlet of the gas turbine 11, can be used to raise the temperature of the fuel input to the gas turbine and the steam at the inlet of the steam turbine. For this reason, in this embodiment, it is possible to raise the gas turbine input fuel temperature and the steam turbine inlet steam temperature higher than the temperature of the exhaust gas EG at the outlet of the gas turbine 11, and in such a case, particularly high plant efficiency can be obtained. In other words, it is possible to raise the temperature of the third heat medium (here, the high-pressure steam exhausted from the high-pressure steam turbine 33) to a temperature higher than the temperature of the exhaust gas EG at the outlet of the reaction gas utilization facility (or the exhaust gas generation facility, here the gas turbine 11). Therefore, in this embodiment, by configuring in this way, it is possible to further improve plant efficiency.

[0303] In this embodiment, combustion air is used as the oxidant for the raw material fluid NH. However, the oxidant is not limited to combustion air, and may be any gas that can cause an oxidation reaction of the raw material fluid NH, such as air or oxygen.

[0304] In this embodiment, the feedwater from the condenser 34 is heated by the feedwater preheater 37 through heat exchange with steam extracted from the low-pressure steam turbine 31. The steam extracted from the low-pressure steam turbine 31 condenses into water through heat exchange with the feedwater. This water flows into the feedwater. Therefore, in this embodiment, the temperature of the feedwater flowing into the heat recovery steam generator 21 can be increased. When the temperature of the feedwater flowing into the heat recovery steam generator 21 increases, the water temperatures at the inlets and outlets of the low-pressure economizers 23a, 23b in the heat recovery steam generator 21 increase, and the temperature of the water supplied to the first preheater 44c via the low-pressure heating water line 76 also increases. Therefore, when the amount of heat required to heat ammonia in the preheater is small, providing the feedwater preheater 37 as in this embodiment makes it possible to supply a sufficient amount of heat to the preheater. Therefore, when the amount of heat required to heat ammonia in the preheater is small, as in this embodiment, providing the feedwater preheater 37 is preferable.

[0305] "Sixth Embodiment" A sixth embodiment of the raw fluid processing plant will be described with reference to FIG.

[0306] The raw material fluid processing plant of this embodiment is a modified example of the raw material fluid processing plant of the third embodiment. In the raw material fluid processing plant of this embodiment, part of ammonia NH is subjected to an autothermal decomposition reaction, as in the fifth embodiment.

[0307] Similar to the above-described embodiments, the raw material fluid processing plant of this embodiment also includes a raw material reaction facility 40e, a reaction gas utilization facility 10, and a waste heat utilization facility 20e.

[0308] Like the raw material reaction equipment of the above embodiments, raw material reaction equipment 40e of this embodiment includes a raw material reaction apparatus 41e and a residual raw material removal apparatus 130. Raw material reaction apparatus 41e of this embodiment differs from raw material reaction apparatus 41b of the third embodiment. On the other hand, residual raw material removal apparatus 130 of this embodiment is the same as the residual raw material removal apparatus 130 of the above embodiments.

[0309] The reaction gas utilization equipment 10 of this embodiment is the same as the reaction gas utilization equipment 10 of the third embodiment. In addition, the exhaust heat utilization equipment 20e of this embodiment is basically the same as the exhaust heat utilization equipment 20b of the third embodiment. However, since the raw material reaction apparatus 41e is different from that of the third embodiment, the line configuration connected to each device constituting the exhaust heat utilization equipment 20e is different from that of the third embodiment. In addition, the configuration of the exhaust heat recovery boiler 21e is also different from that of the third embodiment.

[0310] The heat recovery steam generator 21e of this embodiment is basically the same as the heat recovery steam generator 21b of the third embodiment. However, the heat recovery steam generator 21e of this embodiment has a first low-pressure evaporator 23d and a second low-pressure evaporator 23e as low-pressure evaporators. The first low-pressure evaporator 23d is disposed between the first low-pressure economizer 23a and the second low-pressure economizer 23b. The second low-pressure evaporator 23e is disposed between the second low-pressure economizer 23b and the first high-pressure economizer 25a. The first low-pressure evaporator 23d heats the water by exchanging heat between a portion of the water from the first low-pressure economizer 23a and the exhaust gas EG. The second low-pressure economizer 23b heats the water by exchanging heat between another portion of the water from the first low-pressure economizer 23a and the exhaust gas EG. The second low-pressure evaporator 23e exchanges heat between the heated water from the second low-pressure economizer 23b and the exhaust gas EG, heating the heated water to generate steam. The steam is further superheated in the low-pressure superheater 23f to generate low-pressure steam.

[0311] Similar to the raw material reactor 41b of the third embodiment, the raw material reactor 41e of this embodiment includes an ammonia supply line 42, a raw material ammonia pump 43, a first preheater 44e, a second preheater 44f, a third preheater 44g, a fourth preheater 44h, a fifth preheater 44i, reactors 45a and 45b, a first reactant gas cooler 46c, a second reactant gas cooler 46d, and a reactant gas line 47. However, similar to the fifth embodiment, the reactors 45a and 45b of this embodiment include a pre-reactor 45a and a post-reactor 45b. Similar to the fifth embodiment, the raw material reactor 41e of this embodiment further includes an oxidant introducing device 60e that introduces an oxidant into ammonia.

[0312] The oxidant in this embodiment is also air, as in the fifth embodiment. As in the fifth embodiment, the oxidant supply device 60e has an oxidant receiving line 61, oxidant coolers 62a and 62b, an oxidant compressor 63, an oxidant heater 64, and an oxidant supply line 65. However, the oxidant coolers 62a and 62b in this embodiment have a first oxidant cooler 62a and a second oxidant cooler 62b.

[0313] One end of the oxidant receiving line 61 is connected to the combustion air passage 11b of the gas turbine 11. The other end of the oxidant receiving line 61 is connected to the inlet of the oxidant compressor 63. A first oxidant cooler 62a and a second oxidant cooler 62b are provided on the oxidant receiving line 61.

[0314] One end of a high-pressure feedwater line 79 is connected to the medium inlet of the first oxidant cooler 62a. The other end of this high-pressure feedwater line 79 is connected to the discharge port of the high-pressure pump 25p in the exhaust heat recovery boiler 21e. One end of a high-pressure feedwater recovery line 80 is connected to the medium outlet of the first oxidant cooler 62a. The other end of this high-pressure feedwater line 79 is connected to the inlet of the high-pressure evaporator 25c in the exhaust heat recovery boiler 21e. One end of a second branch feedwater line 91a is connected to the medium inlet of the second oxidant cooler 62b. The other end of this second branch feedwater line 91a is connected to the feedwater line 35. One end of a second feedwater recovery line 75a is connected to the medium outlet of the second oxidant cooler 62b. The other end of this second feedwater recovery line 75a is located in the feedwater line 35, closer to the exhaust heat recovery boiler 21e than the connection position of the second branch feedwater line 91a and the feedwater line 35.

[0315] In this embodiment, one end of a low-temperature, low-pressure steam line 88a and one end of a low-pressure extraction steam line 90 are connected to the second heat medium inlet of the second preheater 44f. The other end of the low-temperature, low-pressure steam line 88a is connected to the outlet of the first low-pressure evaporator 23d in the heat recovery steam generator 21e. The other end of the low-pressure extraction steam line 90 is connected to the casing of the low-pressure steam turbine 31. One end of a connecting low-pressure heating water line 78e is connected to the second heat medium outlet of the second preheater 44f. The other end of this connecting low-pressure heating water line 78e is connected to the second heat medium inlet of the first preheater 44e. One end of a second heated water recovery line 78b is also connected to the second heat medium outlet of the second preheater 44f. The other end of this second heated water recovery line 78b is connected to the inlet of the first low-pressure evaporator 23d and the inlet of the second low-pressure economizer 23b. One end of a first heated water recovery line 78a is connected to the second heat medium outlet of the first preheater 44e. The other end of the first heated water recovery line 78a is connected to the water supply line .

[0316] One end of an intermediate-pressure extraction steam line 93 is connected to the second heat medium inlet of the fourth preheater 44h. The other end of the intermediate-pressure extraction steam line 93 is connected to the casing of the intermediate-pressure steam turbine 32. One end of a connecting intermediate-pressure steam line 89 is connected to the second heat medium outlet of the fourth preheater 44h. The other end of the connecting intermediate-pressure steam line 89 is connected to the second heat medium inlet of the third preheater 44g. One end of a second intermediate-pressure exhaust steam line 87a is further connected to the second heat medium inlet of the third preheater 44g. The other end of the second intermediate-pressure exhaust steam line 87a is connected to the outlet of the intermediate-pressure steam turbine 32. One end of a third heated water recovery line 78c is connected to the second heat medium outlet of the third preheater 44g. The other end of the third heated water recovery line 78c is connected to the inlet of the first low-pressure evaporator 23d and the inlet of the second low-pressure economizer 23b.

[0317] As in the third embodiment, one end of a high-pressure steam line 83 is connected to the second heat medium inlet of the fifth preheater 44i. The other end of this high-pressure steam line 83 is connected to the outlet of the second high-pressure superheater 25e. As in the third embodiment, one end of a high-pressure steam recovery line 86 is connected to the second heat medium outlet of the fifth preheater 44i. The other end of this high-pressure steam recovery line 86 is connected to the inlet of the first high-pressure reheater 26a.

[0318] As in the third embodiment, the liquid ammonia NH3 pressurized by the raw ammonia pump 43 flows into the first preheater 44e, where it is preheated by heat exchange with the second heat medium. The second heat medium flowing into the first preheater 44e is heated water that flows into the first preheater 44e from the second preheater 44f via the first connected heated water line 78e. The heated water cooled by heat exchange with the liquid ammonia NH3 in the first preheater 44e flows into the water supply line 35 via the first heated water recovery line 78a.

[0319] The liquid ammonia NH preheated in the first preheater 44e flows into the second preheater 44f, where it is further preheated by heat exchange with the second heat medium to become gaseous ammonia NHg. The second heat medium flowing into the second preheater 44f is the low-temperature, low-pressure steam flowing into the second preheater 44f from the first low-pressure evaporator 23d via the low-temperature, low-pressure steam line 88a, and the low-pressure extraction steam flowing into the second preheater 44f from the low-pressure steam turbine 31 via the low-pressure extraction steam line 90. In this second preheater 44f, the ammonia undergoes a phase change from liquid to gas at a constant temperature, and water, which is the target of heat exchange with the ammonia, also undergoes a phase change from gas to liquid at a constant temperature. In this way, because both the ammonia and its heat exchange target undergo a phase change at a constant temperature, the temperature difference between them can be reduced, as described above with reference to FIG. 8, and heat utilization efficiency can be improved. As described above, a portion of the heated water generated by heat exchange with the liquid ammonia NH in the second preheater 44f flows into the first preheater 44e via the connecting low-pressure heated water line 78e. The remainder of the heated water generated by heat exchange with the liquid ammonia NH in the second preheater 44f flows into the first low-pressure evaporator 23d and the second low-pressure economizer 23b via the second heated water recovery line 78b.

[0320] The gaseous ammonia NHg produced in the second preheater 44f flows into the third preheater 44g, where it is further preheated by heat exchange with a second heat medium. The second heat medium flowing into the third preheater 44g is steam flowing into the third preheater 44g from the fourth preheater 44h via a connecting medium-pressure steam line 89, and steam flowing into the third preheater 44g from the medium-pressure steam turbine 32 via a second medium-pressure exhaust steam line 87a. The steam cooled by heat exchange with the gaseous ammonia NHg in the third preheater 44g is condensed into heated water. This heated water flows into the first low-pressure evaporator 23d and the second low-pressure economizer 23b via a third heated water recovery line 78c.

[0321] The gaseous ammonia NHg preheated in the third preheater 44g flows into the fourth preheater 44h, where it is further preheated by heat exchange with the second heat medium. The second heat medium flowing into the fourth preheater 44h is extracted medium-pressure steam that is extracted from the medium-pressure steam turbine 32 and flows into the fourth preheater 44h via an intermediate-pressure extraction steam line 93. The steam cooled by heat exchange with the gaseous ammonia NHg in the fourth preheater 44h flows into the third preheater 44g via the connecting medium-pressure steam line 89, as described above.

[0322] The gaseous ammonia NHg preheated in the fourth preheater 44h flows into the fifth preheater 44i, where it is further preheated by heat exchange with a second heat medium. The second heat medium flowing into the fifth preheater 44i is high-pressure steam flowing into the fifth preheater 44i from the second high-pressure superheater 25e via a high-pressure steam line 83, as in the third embodiment. The steam cooled by heat exchange with the gaseous ammonia NHg in the fifth preheater 44i flows into the first high-pressure reheater 26a via a high-pressure steam recovery line 86, as in the third embodiment.

[0323] The heat recovery steam generator 21, steam turbines 31, 32, and 33, condenser 34, feedwater pump 36, and various piping connecting them constitute a Rankine cycle, which is a type of first thermal cycle. The intermediate stage of the intermediate-pressure steam turbine 32 and the outlet of the intermediate-pressure steam turbine 32 each constitute a first section of the first thermal cycle. Steam (first thermal cycle medium) obtained from these locations is guided to the fourth preheater 44h and the third preheater 44g via the intermediate-pressure extraction steam line 93 and the second intermediate-pressure exhaust steam line 87a, which are types of second heat medium lines. The steam cooled by heat exchange with the raw material fluid (ammonia in this case) in the fourth preheater 44h and the third preheater 44g is condensed, and the resulting water is guided via the third heated water recovery line 78c, which is a type of second heat medium recovery line, to the outlet (second section) of the first low-pressure economizer 23a, through which water (first thermal cycle medium) with a temperature lower than that of the first section of the first thermal cycle flows. The low-pressure extraction steam line 90, which is a type of second heat medium line, guides a portion of the steam (first heat cycle medium) flowing through the intermediate stage (first portion of the first heat cycle) of the low-pressure steam turbine 31 to the second preheater 44f. The low-temperature low-pressure steam line 88a, which is a type of second heat medium line, guides a portion of the steam generated in the first low-pressure evaporator 23d to the second preheater 44f. The first heated water recovery line 78a, which is a type of second heat medium recovery line, guides water generated by condensation of steam cooled by heat exchange with the raw material fluid (ammonia in this case) in the second preheater 44f and the first preheater 44e to the feedwater line 35 (second portion), through which water (first heat cycle medium) with a lower temperature than that in the first portion flows. This configuration allows heat of an appropriate temperature to be supplied to the preheater without excess or deficiency from the heat cycle and used to preheat the raw material fluid. Therefore, this embodiment improves heat utilization efficiency.

[0324] A portion of the combustion air from the air compressor 11a of the gas turbine 11 flows as an oxidant into the first oxidant cooler 62a and the second oxidant cooler 62b via the oxidant receiving line 61. Similar to the oxidant cooler 62 of the fifth embodiment, high-pressure feedwater from the high-pressure pump 25p of the heat recovery boiler 21e flows into the first oxidant cooler 62a via a high-pressure feedwater line 79. The first oxidant cooler 62a exchanges heat between the combustion air serving as the oxidant and the high-pressure feedwater, cooling the combustion air while heating the high-pressure feedwater. Similar to the fifth embodiment, the heated high-pressure feedwater flows into the high-pressure evaporator 25c of the heat recovery boiler 21e via a high-pressure feedwater recovery line 80. The combustion air cooled in the first oxidant cooler 62a flows into the second oxidant cooler 62b. Feedwater also flows into this second oxidant cooler 62b via a second branch feedwater line 91a. The second oxidant cooler 62b exchanges heat between the combustion air as an oxidant and the feedwater, cooling the combustion air while heating the feedwater. The heated feedwater flows into the feedwater line 35 via the second feedwater recovery line 75a.

[0325] The oxidant compressor 63 compresses and pressurizes the combustion air cooled in the second oxidant cooler 62b. In this embodiment, the second oxidant cooler 62b further cools the combustion air cooled in the first oxidant cooler 62a with feedwater, so the temperature of the combustion air flowing into the oxidant compressor 63 can be made lower than in the fifth embodiment. Therefore, in this embodiment, the driving force of the oxidant compressor 63 can be made smaller than in the fifth embodiment. The combustion air compressed in the oxidant compressor 63 flows into the oxidant heater 64. As in the fifth embodiment, high-pressure heated water from the second high-pressure economizer 25b flows into this oxidant heater 64 via the second high-pressure heated water line 81a. The oxidant heater 64 exchanges heat between the combustion air as an oxidant and the high-pressure heated water, heating the combustion air while cooling the high-pressure heated water. The high-pressure heated water cooled in the oxidant heater 64 flows into the medium-pressure economizer 24a via the second high-pressure heated water recovery line 82a, as in the fifth embodiment. In order to activate the reactions in the pre-reactor 45a and the post-reactor 45b, the oxidant heater 64 raises the temperature of the combustion air to a temperature close to or higher than the temperature of the gas to be oxidized flowing into each of the reactors 45a, 45b.

[0326] Gaseous ammonia NHg from the fifth preheater 44i and combustion air from the oxidizing agent feed device 60e flow into the prereactor 45a. In the prereactor 45a, a portion of the gaseous ammonia NHg undergoes an oxidation reaction (combustion) with the combustion air. The heat generated by this oxidation reaction heats the gaseous ammonia NHg. Furthermore, the gaseous ammonia NHg is heated by heat exchange with the first heat medium heated by the first heat medium heater 27. Therefore, in the prereactor 45a, the gaseous ammonia NHg is heated to a higher temperature than in the reactor 45 of the third embodiment, and the thermal decomposition reaction of ammonia is promoted.

[0327] The post-reactor 45b receives the reaction gas RG from the pre-reactor 45a and the combustion air from the oxidant supply device 60e. In the post-reactor 45b, a portion of the gaseous ammonia NHg contained in the reaction gas RG from the pre-reactor 45a undergoes an oxidation reaction (combustion) with the combustion air. The heat generated by this oxidation reaction heats the remaining gaseous ammonia NHg. Therefore, in the post-reactor 45b, the gaseous ammonia NHg contained in the reaction gas RG from the pre-reactor 45a is heated, and the thermal decomposition reaction of this gaseous ammonia NHg is promoted.

[0328] As described above, in this embodiment, as in the fifth embodiment, an oxidizing agent is introduced into each of the reactors 45 a, 45 b, and a portion of the ammonia NH in each of the reactors 45 a, 45 b undergoes an oxidation reaction, thereby increasing the environmental temperature of the thermal decomposition reaction in each of the reactors 45 a, 45 b. Therefore, in this embodiment, the ammonia concentration in the reaction gas RG flowing out from each of the reactors 45 a, 45 b can be reduced.

[0329] The reaction gas RG from the post-reactor 45b flows into the residual raw material removal device 130 via the reaction gas line 47, the first reaction gas cooler 46c, and the second reaction gas cooler 46d, and similarly to the third embodiment, residual ammonia contained in the reaction gas RG is removed.

[0330] Seventh Embodiment A seventh embodiment of the raw fluid processing plant will be described with reference to FIG.

[0331] The raw material fluid processing plant of this embodiment is a modified example of the raw material fluid processing plant of the second embodiment. The raw material fluid processing plant of this embodiment is a plant in which exhaust gas EG is used as the second heat medium to be subjected to heat exchange during preheating of ammonia NH.

[0332] Similar to the above-described embodiments, the raw material fluid processing plant of this embodiment also includes a raw material reaction facility 40f, a reaction gas utilization facility 10f, and a waste heat utilization facility 20f.

[0333] Similar to the raw material reaction equipment of the above-described embodiments, raw material reaction equipment 40f of this embodiment includes a raw material reaction apparatus 41f and a residual raw material removal apparatus 130. Raw material reaction apparatus 41f of this embodiment differs from raw material reaction apparatus 41a of the second embodiment. On the other hand, residual raw material removal apparatus 130 of this embodiment is the same as the residual raw material removal apparatus 130 of the above-described embodiments.

[0334] The reaction gas utilization equipment 10f of this embodiment is basically the same as the reaction gas utilization equipment of the above-mentioned embodiments. However, the exhaust heat utilization equipment 20f of this embodiment differs from the exhaust heat utilization equipment 20a of the second embodiment in that, as described above, the second heat medium to be heat exchanged during preheating of ammonia NH is the exhaust gas EG.

[0335] The raw material reaction apparatus 41f of the present embodiment includes an ammonia supply line 42, a raw material ammonia pump 43, a first preheater 44j, a second preheater 44k, a third preheater 44m, a reactor 45, a first reaction gas cooler 46e, a second reaction gas cooler 46f, and a reaction gas line 47.

[0336] The ammonia supply line connects the ammonia tank T and the reactor 45. The first preheater 44j, the second preheater 44k, and the third preheater 44m are all provided on this ammonia supply line .

[0337] The first preheater 44j and the second preheater 44k of this embodiment have heat transfer tubes. The heat transfer tubes of the first preheater 44j and the heat transfer tubes of the second preheater 44k are arranged in the gas frame 22 of the heat recovery boiler 21. The first preheater 44j is arranged at substantially the same position as the first low-pressure economizer 23a in the flow direction of the exhaust gas EG. The second preheater 44k is arranged between the first low-pressure economizer 23a and the second low-pressure economizer 23b in the flow direction of the exhaust gas EG. Therefore, the second preheater 44k is arranged upstream of the first preheater 44j in the flow direction of the exhaust gas EG. Furthermore, the first preheater 44j and the second preheater 44k are arranged downstream of the low-pressure evaporator 23c, which is the most downstream evaporator among the multiple evaporators. On the other hand, the first heat medium heater 27 is arranged upstream of the high-pressure evaporator 25c, which is the most upstream evaporator among the multiple evaporators. Therefore, all the evaporators are arranged between the first heat medium heater 27 and the first preheater 44j and the second preheater 44k.

[0338] Ammonia NH flows through the heat transfer tubes of the first preheater 44j and the second preheater 44k. In this embodiment, the second heat medium that exchanges heat with the ammonia NH in the heat transfer tubes is the exhaust gas EG flowing through the gas frame 22. Therefore, a portion of the gas frame 22 constitutes a second heat medium line through which the second heat medium flows. In other words, the second heat medium line is configured to include a portion of the gas frame 22.

[0339] The reactant gas line 47 includes a first reactant gas line 47a and a second reactant gas line 47b. One end of the first reactant gas line 47a is connected to the reactant gas outlet of the reactor 45. The other end of the first reactant gas line 47a is connected to the second heat medium inlet of the third preheater 44m. Therefore, in this embodiment, the reactant gas RG is a type of second heat medium. A first reactant gas cooler 46e is provided on the first reactant gas line 47a. One end of the second reactant gas line 47b is connected to the second heat medium outlet of the second preheater 44k, and the other end of the second reactant gas line 47b is connected to the residual raw material removal device 130. A second reactant gas cooler 46f is provided on the second reactant gas line 47b.

[0340] One end of a first combustion air line 14a is connected to a third heat medium inlet of the first reaction gas cooler 46e. Therefore, the third heat medium that exchanges heat with the reaction gas RG in the first reaction gas cooler 46e is combustion air. The other end of this first combustion air line 14a is connected to a combustion air passage 11b of the gas turbine 11. One end of a second combustion air line 14b is connected to a third heat medium outlet of the first reaction gas cooler 46e. The other end of this second combustion air line 14b is connected to the combustor 11c.

[0341] As described above, one end of the first combustion air line 14a is connected to the inlet of the first reaction gas cooler 46e, and unlike the second embodiment, the high-pressure steam line 83 is not connected. In this embodiment, the outlet of the high-pressure superheater 25d and the inlet of the high-pressure steam turbine 33 are directly connected by the high-pressure steam line 83.

[0342] A branch water supply line 91 branching from the water supply line 35 is connected to a third heat medium inlet of the second reactant gas cooler 46f. Therefore, the third heat medium that exchanges heat with the reactant gas RG in the second reactant gas cooler 46f is feedwater. One end of a heated water recovery line 78 is connected to a third heat medium outlet of the second reactant gas cooler 46f. The other end of this heated water recovery line 78 is connected to an inlet of the second low-pressure economizer 23b.

[0343] Liquid ammonia NH pressurized by the raw ammonia pump 43 first flows into the first preheater 44j, where it is preheated by heat exchange with exhaust gas EG serving as a second heat medium. The liquid ammonia NH preheated in the first preheater 44j flows into the second preheater 44k, where it is further preheated by heat exchange with exhaust gas EG serving as a second heat medium. As a result, the liquid ammonia NH is vaporized to become gaseous ammonia NHg.

[0344] The gaseous ammonia NHg produced in the second preheater 44k flows into the third preheater 44m. The reaction gas RG also flows into the third preheater 44m from the first reaction gas cooler 46e via the first reaction gas line 47a. In the third preheater 44m, the gaseous ammonia NHg is further preheated by heat exchange between the gaseous ammonia NHg and the reaction gas RG, while the reaction gas RG is cooled. Thus, the second preheater 44k functions not only as a preheater that preheats ammonia, but also as a reaction gas cooler that cools the reaction gas RG.

[0345] The gaseous ammonia NHg preheated in the third preheater 44m flows into the reactor 45. As in the second embodiment, the first heat medium also flows into the reactor 45. In the reactor 45, the gaseous ammonia NHg is heated by heat exchange between the first heat medium and the gaseous ammonia NHg. As a result, the gaseous ammonia NHg undergoes a thermal decomposition reaction to become a reaction gas RG.

[0346] The reaction gas RG generated in the reactor 45 flows into the first reaction gas cooler 46e. Combustion air flows into this first reaction gas cooler 46e as a third heat medium from the air compressor 11a of the gas turbine 11 via the combustion air passage 11b and the first combustion air line 14a. In the first reaction gas cooler 46e, heat exchange between the reaction gas RG and the combustion air cools the reaction gas RG while heating the combustion air. Thus, the first reaction gas cooler 46e functions as a reaction gas cooler that cools the reaction gas RG, and also functions as an air preheater that heats the combustion air. The reaction gas utilization facility 10f has the gas turbine 11 as well as the first reaction gas cooler 46e that also functions as an air preheater.

[0347] As described above, the reaction gas RG cooled in the first reaction gas cooler 46e flows into the third preheater 44m via the first reaction gas line 47a. In this third preheater 44m, the reaction gas RG is further cooled by heat exchange with ammonia NH, as described above.

[0348] The reaction gas RG cooled in the third preheater 44m flows into the second reaction gas cooler 46f via the second reaction gas line 47b. Feedwater flows into the second reaction gas cooler 46f from the branched water supply line 91 as a third heat medium. In the second reaction gas cooler 46f, heat exchange between the reaction gas RG and the feedwater occurs, whereby the reaction gas RG is cooled and the feedwater is heated. The reaction gas RG cooled in the second reaction gas cooler 46f flows into the residual raw material removal device 130 via the second reaction gas line 47b, where residual ammonia contained in the reaction gas RG is removed. In addition, the feedwater heated in the second reaction gas cooler 46f flows into the second low-pressure economizer 23b via the heated water recovery line 78.

[0349] In this embodiment, the heat of the exhaust gas EG from which most of the heat has been removed in all of the evaporators, superheaters, etc., i.e., the heat of the low-temperature exhaust gas EG, is utilized to preheat the ammonia NH. Therefore, in this embodiment, the heat of the low-temperature exhaust gas EG can be effectively utilized.

[0350] In this embodiment, the combustion air flowing into the combustor 11c is preheated using the heat of the reaction gas RG. As a result, the temperature of the combustion air flowing into the combustor 11c increases, and the efficiency of the gas turbine 11 can be improved.

[0351] Eighth Embodiment An eighth embodiment of the raw fluid processing plant will be described with reference to FIGS.

[0352] The raw material fluid processing plant of this embodiment is a modified example of the raw material fluid processing plant of the fifth embodiment. In the raw material fluid processing plant of this embodiment, the second heat medium for preheating ammonia NH and the third heat medium for cooling the reaction gas RG are changed from those of the fifth embodiment.

[0353] As in the above embodiments, the raw material fluid processing plant of this embodiment also includes a raw material reaction facility 40g, a reaction gas utilization facility 10, and a waste heat utilization facility 20g, as shown in FIG.

[0354] Like the raw material reaction equipment 40 of the above-described embodiments, the raw material reaction equipment 40 of this embodiment includes a raw material reaction apparatus 41g and a residual raw material removal apparatus 130. The raw material reaction apparatus 41g of this embodiment differs from the raw material reaction apparatus 41d of the second embodiment in that the second heat medium and the third heat medium are changed from those of the fifth embodiment. On the other hand, the residual raw material removal apparatus 130 of this embodiment is the same as the residual raw material removal apparatus 130 of the above-described embodiments.

[0355] The reaction gas utilization equipment 10 of this embodiment is basically the same as the reaction gas utilization equipment of the above embodiments. The exhaust heat utilization equipment 20g of this embodiment is basically the same as the exhaust heat utilization equipment 20d of the fifth embodiment. However, the exhaust heat utilization equipment 20g of this embodiment differs from the exhaust heat utilization equipment 20d of the fifth embodiment in that the outlet of the high-pressure steam turbine 33 and the inlet of the intermediate-pressure steam turbine 32 are directly connected by a high-pressure exhaust steam line 85.

[0356] The raw material reaction apparatus 41g of the present embodiment includes an ammonia supply line 42, a raw material ammonia pump 43, a first preheater 44c, a second preheater 44d, a third preheater 44n, a pre-reactor 45a, a post-reactor 45b, a first reactant gas cooler 46g, a second reactant gas cooler 46h, a third reactant gas cooler 46i, a fourth reactant gas cooler 46j, a first reactant gas line 47a, a second reactant gas line 47b, an oxidant supplying device 60g, a Brayton cycle 100, a thermal cycle 110, and a Rankine cycle 120.

[0357] The first preheater 44c, the second preheater 44d, and the third preheater 44n are all provided on the ammonia supply line 42. Similar to the first preheater 44c of the second and fifth embodiments, one end of a low-pressure heating water line 76 is connected to the second heat medium inlet of the first preheater 44c. The other end of the low-pressure heating water line 76 is connected to the outlet of the second low-pressure economizer 23b. Similar to the first preheater 44c of the second and fifth embodiments, one end of a heated water recovery line 78 is connected to the second heat medium outlet of the first preheater 44c. The other end of the heated water recovery line 78 is connected to the inlet of the second low-pressure economizer 23b. Similar to the second preheater 44d of the second and fifth embodiments, one end of a first reactant gas line 47a is connected to the second heat medium inlet of the second preheater 44d. The other end of the first reactant gas line 47a is connected to the post-reactor 45b. Similar to the second preheater 44d of the second and fifth embodiments, one end of a second reactant gas line 47b is connected to the second heat medium outlet of the second preheater 44d, and the other end of the second reactant gas line 47b is connected to the residual raw material removal device 130.

[0358] The third preheater 44n is a preheater newly added to the raw material reaction apparatus 41d of the fifth embodiment. The second heat medium inlet and the second heat medium outlet of the third preheater 44n are both connected to a Brayton cycle 100. The Brayton cycle 100 will be described in detail later.

[0359] The oxidant introduction device 60g is basically the same as the oxidant introduction device 60 of the fifth embodiment. However, the oxidant introduction line 65 of the oxidant introduction device 60g of the fifth embodiment includes a main oxidant introduction line 65a, a first oxidant introduction line 65b, and a second oxidant introduction line 65c. One end of the main oxidant introduction line 65a is connected to the oxidant compressor 63. The other end of the main oxidant introduction line 65a is connected to a third heat medium inlet of the third reactant gas cooler 46i. One end of the first oxidant introduction line 65b and one end of the second oxidant introduction line 65c are connected to a third heat medium outlet of the third reactant gas cooler 46i. The other end of the first oxidant introduction line 65b is connected to the pre-reactor 45a, as in the fifth embodiment. Furthermore, the other end of the second oxidant introduction line 65c is connected to the post-reactor 45b, as in the fifth embodiment. Therefore, the oxidizing agent from the oxidizing agent supply device 60g is supplied to the pre-reactor 45a and the post-reactor 45b, similarly to the fifth embodiment.

[0360] The first reactant gas cooler 46g, the second reactant gas cooler 46h, and the third reactant gas cooler 46i are provided on the first reactant gas line 47a. The third heat medium inlet and the third heat medium outlet of the first reactant gas cooler 46g are both connected to the Brayton cycle 100. The third heat medium inlet and the third heat medium outlet of the second reactant gas cooler 46h are both connected to the thermal cycle 110. This thermal cycle 110 will be described in detail later.

[0361] As described above, the main oxidant input line 65a is connected to the third heat medium inlet of the third reactant gas cooler 46i. The first oxidant input line 65b and the second oxidant input line 65c are connected to the third heat medium outlet of the third reactant gas cooler 46i. The third reactant gas cooler 46i exchanges heat between the oxidant from the main oxidant input line 65a and the reactant gas RG flowing through the first reactant gas line 47a, thereby heating the oxidant and cooling the reactant gas RG. Thus, the third reactant gas cooler 46i functions as a reactant gas cooler for the reactant gas RG and as an oxidant heater for the oxidant.

[0362] The fourth reactant gas cooler 46j is provided on the second reactant gas line 47b. A third heat medium inlet and a third heat medium outlet of the fourth reactant gas cooler 46j are both connected to a Rankine cycle 120. The Rankine cycle 120 will be described in detail later.

[0363] The Brayton cycle medium circulating in the Brayton cycle 100 is a gas such as helium, argon, nitrogen, or air. The Brayton cycle medium does not change phase while circulating in the Brayton cycle 100. The Brayton cycle 100 is a type of thermal cycle, and as shown in FIG. 15 , it includes a medium compressor 101 that compresses the Brayton cycle medium, a medium heater 102 that heats the Brayton cycle medium compressed by the medium compressor 101, a medium turbine 103 that is driven by the Brayton cycle medium heated by the medium heater 102, and a medium cooler 104 that cools the Brayton cycle medium exhausted from the medium turbine 103 and returns it to the medium compressor 101.

[0364] The medium heater 102 is the first reactant gas cooler 46g described above. The Brayton cycle medium compressed by the medium compressor 101 flows into this first reactant gas cooler 46g from a third heat medium inlet. In the first reactant gas cooler 46g, the reactant gas RG is cooled while the Brayton cycle medium is heated through heat exchange between the reactant gas RG and the Brayton cycle medium. Thus, the first reactant gas cooler 46g functions as a reactant gas cooler for the reactant gas RG and as a medium heater for the Brayton cycle medium. The Brayton cycle medium heated in the first reactant gas cooler 46g flows out from a third heat medium outlet of the first reactant gas cooler 46g. This Brayton cycle medium flows into the medium turbine 103. The medium cooler 104 is the third preheater 44n described above. The Brayton cycle medium exhausted from the medium turbine 103 flows into this third preheater 44n from a third heat medium inlet. In the third preheater 44n, the ammonia is heated while the Brayton cycle medium is cooled by heat exchange between the ammonia and the Brayton cycle medium, and thus the third preheater 44n functions as a preheater for the ammonia and as a medium cooler for the Brayton cycle medium.

[0365] The heat cycle medium circulating in the heat cycle 110 is, for example, carbon dioxide. This heat cycle 110 is a Rankine cycle if the heat cycle medium condenses during circulation, and a Brayton cycle if the heat cycle medium does not condense during circulation. As shown in Fig. 15, this heat cycle 110 includes a medium booster 111 that increases the pressure of the heat cycle medium, a medium heater 112 that heats the heat cycle medium pressurized by the medium booster 111, a medium turbine 113 that is driven by the heat cycle medium heated by the medium heater 112, a medium cooler 114 that cools the heat cycle medium exhausted from the medium turbine 113 and returns it to the medium booster 111, and a regenerative heat exchanger 115.

[0366] The regenerative heat exchanger 115 exchanges heat between the heat cycle medium pressurized by the medium booster 111 and the heat cycle medium exhausted from the medium turbine 113. The regenerative heat exchanger 115 heats the heat cycle medium pressurized by the medium booster 111 while cooling the heat cycle medium exhausted from the medium turbine 113. The heat cycle medium heated by the regenerative heat exchanger 115 flows into the medium heater 112, where it is further heated. The heat cycle medium cooled by the regenerative heat exchanger 115 flows into the medium cooler 114, where it is further cooled. The medium heater 112 of this heat cycle is the second reactant gas cooler 46h. The heat cycle medium pressurized by the medium booster 111 and heated by the regenerative heat exchanger 115 flows into the second reactant gas cooler 46h through a third heat medium inlet. In the second reactant gas cooler 46h, the reactant gas RG is cooled while the heat cycle medium is heated through heat exchange between the reactant gas RG and the heat cycle medium. Therefore, the second reactant gas cooler 46h functions as a reactant gas cooler for the reactant gas RG, and functions as a medium heater for the heat cycle medium.

[0367] The Rankine cycle medium circulating in the Rankine cycle 120 is a low-boiling-point medium such as hexane, pentane, or ammonia, which has a boiling point lower than that of water. Therefore, the Rankine cycle 120 is a low-boiling-point medium Rankine cycle. The low-boiling-point medium Rankine cycle 120 is a type of thermal cycle, and as shown in Fig. 15, includes a medium booster 121 that boosts the pressure of the low-boiling-point medium, a medium heater 122 that heats and vaporizes the low-boiling-point medium boosted by the medium booster 121, a medium turbine 123 that is driven by the low-boiling-point medium vaporized by the medium heater 122, a medium cooler 124 that cools and condenses the low-boiling-point medium exhausted from the medium turbine 123 and then returns it to the medium booster 121, and a regenerative heat exchanger 125.

[0368] The regenerative heat exchanger 125 exchanges heat between the low boiling point medium pressurized by the medium booster 121 and the low boiling point medium exhausted from the medium turbine 123, heating the low boiling point medium pressurized by the medium booster 121 while cooling the low boiling point medium exhausted from the medium turbine 123. The low boiling point medium heated by the regenerative heat exchanger 125 flows into the medium heater 122, where it is further heated and vaporized. The low boiling point medium cooled by the regenerative heat exchanger 125 flows into the medium cooler 124, where it is further cooled and condensed. The medium heater 122 of the low boiling point medium Rankine cycle 120 is the aforementioned fourth reactant gas cooler 46j. The low boiling point medium pressurized by the medium booster 121 and heated by the regenerative heat exchanger 125 flows into the fourth reactant gas cooler 46j from a third heat medium inlet. In the fourth reactant gas cooler 46j, the reactant gas RG is cooled while the low-boiling-point medium is heated by heat exchange between the reactant gas RG and the low-boiling-point medium. Thus, the fourth reactant gas cooler 46j functions as a reactant gas cooler for the reactant gas RG and as a medium heater for the low-boiling-point medium.

[0369] In this embodiment, the Brayton cycle 100 can be driven by the heat for heating the ammonia NH and the heat for cooling the reaction gas RG, thereby increasing the output of the plant. Furthermore, in this embodiment, the heat for cooling the reaction gas RG can be used to drive the thermal cycle 110 and the low-boiling-point medium Rankine cycle 120, thereby further increasing the output of the plant.

[0370] In addition, in the present embodiment, the oxidant can be heated by heat exchange with the reaction gas RG in the third reaction gas cooler 46i, thereby increasing the temperature of the oxidant. Therefore, in the present embodiment, the ambient temperature of the thermal decomposition reaction in each of the reactors 45a and 45b can be increased, and the concentration of residual ammonia in the reaction gas RG can be reduced.

[0371] The plant of this embodiment is a plant obtained by adding one thermal cycle 110 to the plant of the fifth embodiment for preheating ammonia and cooling the reaction gas RG, and adding two thermal cycles 100 and 120 to cool the reaction gas RG. However, only one or two of the above three thermal cycles 100, 110, and 120 may be added.

[0372] "Ninth embodiment" A ninth embodiment of the raw fluid processing plant will be described with reference to FIG.

[0373] The raw material fluid processing plant of this embodiment is a modified example of the raw material fluid processing plant of the fourth embodiment described with reference to Fig. 9. A waste heat utilization facility 20c of the processing plant in the fourth embodiment includes a waste heat recovery boiler 21c and steam turbines 31, 32, and 33 and a condenser 34 as steam utilization facilities that utilize steam from the waste heat recovery boiler 21c. A waste heat utilization facility 20h of the processing plant in this embodiment includes a waste heat recovery boiler 21c similar to that of the fourth embodiment and a plurality of steam utilities 151, 152, and 153 as steam utilization facilities that utilize steam from the waste heat recovery boiler 21c. That is, the waste heat utilization facility 20h of the processing plant in this embodiment includes a plurality of steam utilities 151, 152, and 153 instead of the steam turbines 31, 32, and 33 and the condenser 34 of the processing plant in the fourth embodiment.

[0374] In this embodiment, the plurality of steam users 151, 152, 153 include a high-pressure steam user 153, a medium-pressure steam user 152, and a low-pressure steam user 151.

[0375] The steam inlet of the high-pressure steam utility 153 is connected to the outlet of the third high-pressure reheater 26c of the heat recovery boiler 21c via a high-pressure reheat steam line 84. The steam outlet of the high-pressure steam utility 153 is connected to the steam inlet of the medium-pressure steam utility 152 via a high-pressure exhaust steam line 85. A pressure reducing valve 154 is provided on this high-pressure exhaust steam line 85. A second high-pressure exhaust steam line 85b branches off from the high-pressure exhaust steam line 85 at a position closer to the medium-pressure steam utility than the pressure reducing valve 154. This second high-pressure exhaust steam line 85b is connected to the reboiler 139 of the residual material removal unit 130, as in the fourth embodiment. The steam outlet of the medium-pressure steam utility 152 is connected to the steam inlet of the low-pressure steam utility 151 via a medium-pressure exhaust steam line 87. A pressure reducing valve 156 is provided on this medium-pressure exhaust steam line 87. One end of a low-pressure steam line 88 is connected to the intermediate-pressure exhaust steam line 87 at a position closer to the low-pressure steam user than the pressure reducing valve 156. The other end of this low-pressure steam line 88 is connected to the outlet of the low-pressure superheater 23f in the heat recovery boiler 21c, as in the fourth embodiment. The outlet of the low-pressure steam user 151 is connected to the heat recovery boiler 21c by a feedwater line 35. In the low-pressure steam user 151, steam flowing in from a steam inlet is condensed and flows out from the outlet as liquid water. In this embodiment, the condensation heat generated at this time is also utilized.

[0376] In this embodiment, the exhaust heat recovery boiler 21c and a plurality of steam utilization devices 151, 152, and 153 constitute an exhaust heat utilization heat cycle.

[0377] As in this embodiment, even if multiple steam users 151, 152, 153 are provided instead of the steam turbines 31, 32, 33 and the condenser 34, heat recovery or heat utilization can be performed according to the temperature level between the heat required for the reaction of the raw material fluid, the heat generated by this reaction, and the heat of the heat cycle medium (steam or water) flowing in the exhaust heat utilization heat cycle.

[0378] While this embodiment is a modification of the fourth embodiment, in other embodiments and their modifications, multiple steam users 151, 152, 153 may be provided instead of the steam turbines 31, 32, 33 and the condenser 34, as in this embodiment. In this case, as in this embodiment, heat recovery or heat utilization can be performed according to the temperature level between the heat required for the reaction of the raw material fluid, the heat generated by this reaction, and the heat of the heat cycle medium flowing in the waste heat utilization heat cycle. As described above, the heat cycle or waste heat utilization heat cycle of the present invention is not limited to one that extracts power, but may also be a cycle that circulates a heat medium for the purpose of heat utilization.

[0379] "Variations" In the plant of the second embodiment ( FIG. 5 ), all of the high-pressure steam from the high-pressure superheater 25d is heated by the first reactant gas cooler 46a and then supplied to the high-pressure steam turbine 33. However, if a sufficient amount of heat cannot be obtained solely from the exhaust heat of the first reactant gas cooler 46a, only a portion of the high-pressure steam from the high-pressure superheater 25d may be heated by the first reactant gas cooler 46a and then supplied to the high-pressure steam turbine 33. In this case, a third high-pressure superheater is provided between the high-pressure superheater 25d and the first heat medium heater 27 in the gas case 22 of the heat recovery steam generator 21. A portion of the steam exiting the high-pressure superheater 25d is sent to the first reactant gas cooler 46a, and the remaining steam is sent to the third high-pressure superheater and superheated by the third high-pressure superheater. The steam superheated by the third high-pressure superheater flows through the third high-pressure steam line to join the second high-pressure steam line 83b, where it is mixed with the steam heated by the first reactant gas cooler 46a and supplied to the high-pressure steam turbine 33.

[0380] In the second embodiment, as described above, the first high-pressure steam line 83a, which is a type of third heat medium line, guides all of the steam flowing out from the outlet of the high-pressure superheater 25d (the first part of the Rankine cycle) to the first reactant gas cooler 46a. Furthermore, the second high-pressure steam line 83b, which is a type of third heat medium recovery line, guides the steam superheated by heat exchange with the reactant gas in the first reactant gas cooler 46a to the inlet of the high-pressure steam turbine 33 (the second part), which supplies steam at a higher temperature than the outlet (the first part) of the high-pressure superheater 25d. However, as in the modified example of the second embodiment described above, the first high-pressure steam line 83a, which is a type of third heat medium line, may also guide a portion of the steam flowing out from the outlet of the high-pressure superheater 25d (the first part of the Rankine cycle) to the first reactant gas cooler 46a. In the modified example of the second embodiment, the remainder of the high-pressure steam superheated in the high-pressure superheater 25d is further superheated in the third high-pressure superheater, and this steam is guided to the high-pressure steam turbine 33 via the third high-pressure steam line. In this modification, the second high-pressure steam line 83b, which is a type of third heat medium recovery line, guides steam superheated by heat exchange with the reaction gas in the first reaction gas cooler 46a to the third high-pressure steam line (second section) through which steam at a higher temperature than that at the outlet (first section) of the high-pressure superheater 25d flows. As described above, the steam superheated in the third high-pressure superheater and the steam superheated in the first reaction gas cooler 46a are supplied to the high-pressure steam turbine 33.

[0381] The plant of the fourth embodiment is a plant in which an assist medium heating mechanism that heats the first heat medium by exchanging heat between the combustion gas formed by the combustion of fuel from the burner 28 and the first heat medium is added to the plant of the third embodiment. However, this assist medium heating mechanism may be added to the plants of the other embodiments.

[0382] The plant of the fifth embodiment is a plant in which an oxidant supplying device 60 is added to the plant of the second embodiment. Moreover, the plant of the sixth embodiment is a plant in which an oxidant supplying device 60e is added to the plant of the third embodiment. However, an oxidant supplying device may be added to the plants of the other embodiments.

[0383] In each of the above embodiments, it is essential that the raw material fluid (ammonia) is heated by heat exchange with a high-temperature first heat medium (steam) in the reactor. However, the method of heating the raw material fluid by heat exchange with the first heat medium is not essential. For example, a method of heating the raw material fluid or the reaction gas may be adopted in which an oxidizer is introduced into the reactor 45 using an oxidizer introduction device such as that installed in the plant of the fifth embodiment, and the raw material fluid or the reaction gas is heated by oxidizing the raw material fluid or the reaction gas. Alternatively, a method of heating the raw material fluid in the reactor by mixing a high-temperature medium with the raw material fluid in the reactor may be adopted. Either heating method can raise the temperature of the reaction gas at the outlet of the reactor. By heat exchanging the reaction gas with the fuel or the heat cycle medium, the temperatures of the fuel or the heat cycle medium can be increased, thereby improving plant efficiency.

[0384] The plant of the eighth embodiment is a plant in which the above-mentioned three thermal cycles 100, 110, and 120 are added to the plant of the fifth embodiment. However, at least one of the three thermal cycles 100, 110, and 120 may be added to another plant.

[0385] The plants of the fifth and eighth embodiments include a feedwater preheater 37. On the other hand, the plants of the first to fourth embodiments, the sixth embodiment, and the seventh embodiment do not include a feedwater preheater 37. However, the feedwater preheater 37 may be added to the plants of the first to fourth embodiments, the sixth embodiment, and the seventh embodiment.

[0386] In each of the above embodiments, the method of removing residual ammonia from the reaction gas RG is to bring the reaction gas RG into contact with water in the absorption tower 131. However, pressure swing adsorption (PSA) may also be used as a method of removing residual ammonia from the reaction gas RG.

[0387] If the concentration of residual ammonia contained in the reaction gas RG is low, even if this reaction gas RG is sent to the gas turbine 11 as fuel, the NOx concentration in the exhaust gas EG generated by the combustion of the fuel will not be very high. If this NOx concentration is below the regulated value, the residual raw material removal device 130 in the raw material reaction equipment 40 in each of the above embodiments can be omitted. If the residual raw material removal device 130 can be omitted, equipment costs can be reduced. Furthermore, if the residual raw material removal device 130 can be omitted, there is no need to cool the reaction gas RG to promote ammonia removal in the residual raw material removal device 130, and there is also no need to heat the reaction gas RG from the residual raw material removal device 130 before sending it to the gas turbine 11. Therefore, if the residual raw material removal device 130 can be omitted, the thermal energy used to cool and heat the reaction gas RG can be effectively used to drive the steam turbines 31, 32, and 33, for example.

[0388] The reactant gas utilization facility in the above-described embodiment is a gas turbine facility. However, the facility is not limited to a gas turbine facility, and may be, for example, a reciprocating gas engine facility, a fuel cell facility, or a boiler facility, as long as it is capable of reacting a raw material fluid and utilizing the reactant gas obtained by this reaction. The reactant gas utilization facility may also utilize the reactant gas as a raw material for chemical synthesis. Furthermore, the obtained reactant gas may be stored, transported, or otherwise used.

[0389] The exhaust gas generation equipment in each of the above embodiments is a gas turbine equipment. However, the equipment is not limited to a gas turbine equipment as long as it generates exhaust gas during operation. For example, it may be a reciprocating gas engine equipment, a fuel cell equipment, or a boiler equipment. Furthermore, the exhaust gas generation equipment may utilize a reaction gas or a treated reaction gas, and this exhaust gas generation equipment may also serve as a reaction gas utilization equipment. In this case, fuels other than the reaction gas or the treated reaction gas, such as natural gas, oil, or coal, may be supplied to the exhaust gas generation equipment. In this case, the exhaust gas generation equipment may use fuels such as natural gas, oil, or coal in combination with the reaction gas or the treated reaction gas. Furthermore, it is also possible to supply only fuels other than the reaction gas or the treated reaction gas, such as natural gas, oil, or coal, to the exhaust gas generation equipment. In this case, the exhaust gas generation equipment is not a reaction gas utilization equipment.

[0390] In the plant of the above embodiment, the reaction gas utilization facility and the boiler of the exhaust heat utilization facility are separate. However, the reaction gas utilization facility and the boiler of the exhaust heat utilization facility may be configured as a general boiler that burns fuel and utilizes the heat of the exhaust gas generated as a result.

[0391] The raw material fluid in each of the above embodiments is liquid ammonia. However, the raw material fluid may be, for example, methanol, dimethyl ether, or the like, as long as the reaction gas obtained by a reaction such as a thermal decomposition reaction can be utilized in some type of reaction gas utilization equipment. Methanol decomposes into hydrogen and carbon monoxide through a thermal decomposition reaction. Furthermore, methanol and dimethyl ether undergo a steam reforming reaction involving an endothermic reaction to produce hydrogen and carbon dioxide. When a steam reforming reaction is performed, steam required for the reaction may be used from, for example, a high-pressure superheater outlet of the exhaust heat utilization equipment provided in each embodiment. [Explanation of symbols]

[0392] 10, 10d, 10f: Reaction gas utilization equipment 11: Gas turbine 11a: Air compressor 11b: Combustion air passage 11c: Combustor 11d: Turbine 12: Fuel line 12a: First fuel line 12b: Second fuel line 12c: Branch fuel line 13: Fuel preheater 13a: First fuel preheater 13b: Second fuel preheater 14a: First combustion air line 14b: Second combustion air line 15: Natural gas line 20, 20a, 20b, 20c, 20e, 20f, 20h: Waste heat utilization equipment 21, 21b, 21c, 21e, 21f: Waste heat recovery boiler 22: Gas Frame 23a: First low pressure economizer 23b: Second low pressure economizer 23c: Low pressure evaporator 23d: First low-pressure evaporator 23e: Second low-pressure evaporator 23f: Low pressure superheater 24a: Medium pressure economizer 24b: Medium pressure evaporator 24p: Medium pressure pump 25a: First high-pressure economizer 25b: Second high-pressure economizer 25c: High-pressure evaporator 25d: High pressure superheater (first high pressure superheater) 25e: Second high pressure superheater 25p: High pressure pump 26a: First high pressure reheater 26b: Second high pressure reheater 26c: Third high pressure reheater 27:First heat medium heater 27a: First low temperature heat medium heater 27b: First high temperature heat medium heater 28: Burner 29: Partition material 29a: First exhaust gas flow path 29b: Second exhaust gas flow path 31: Low-pressure steam turbine 32: Medium pressure steam turbine 33: High-pressure steam turbine 34: Condenser 35: Water supply line 36: Water supply pump 37: Water supply preheater 39: Chimney 40, 40a, 40b, 40c, 40d, 40e, 40f, 40g: Raw material reaction equipment 41, 41a, 41b, 41c, 41d, 41e, 41f, 41g: raw material reaction apparatus 42: Ammonia supply line 42a: First ammonia supply line 42b: Second ammonia supply line 42c: Third ammonia supply line 42d: Fourth ammonia supply line 42e: Fifth ammonia supply line 42f: Sixth ammonia supply line 43: Raw ammonia pump 44: Preheater 44a, 44c, 44e, 44j: First preheater 44b, 44d, 44f, 44k: Second preheater 44g, 44m, 44n: Third preheater 44h: Fourth preheater 44i: Fifth preheater 45: Reactor 45a: Pre-reactor 45b: Post-reactor 46: Reaction gas cooler 46a, 46c, 46e, 46g: First reaction gas cooler 46b, 46d, 46f, 46h: Second reaction gas cooler 46i: Third reaction gas cooler 46j: Fourth reaction gas cooler 47: Reaction gas line 47a: First reaction gas line 47b: Second reactant gas line 47c: Third reaction gas line 51: First heat transfer medium line 51a: First low-temperature heat transfer medium line 51b: First high-temperature heat transfer medium line 52: First heat transfer medium recovery line 52a: First low-temperature heat transfer medium recovery line 52b: First high-temperature heat transfer medium recovery line 53: First heat transfer medium booster 55: Heat transfer medium replenishment line 56: Heat medium refill valve 60, 60e, 60g: Oxidizer injection device 61: Oxidant receiving line 62: Oxidizer cooler 62a: First oxidizer cooler 62b: Secondary oxidizer cooler 63: Oxidizer compressor 64: Oxidizer heater 65: Oxidizer injection line 65a: Main oxidizer injection line 65b, 65d: First oxidizer injection line 65c, 65e: Second oxidizer injection line 71: First reboiler medium line 72: Second reboiler medium line 73: Reboiler media recovery line 74: Reboiler medium booster 75: Water supply and recovery line 75a: Second water supply and recovery line 76: Low pressure heated water line 77: Medium pressure heated water line 78: Heated water recovery line 78a: First heated water recovery line 78b: Second heated water recovery line 78c: Third heated water recovery line 78d: Connected low pressure heated water line 78e: First connected heated water line (connected low-pressure heated water line) 78f: Second connecting heated water line 79: High pressure water supply line 80: High-pressure water supply recovery line 81: High pressure heated water line 81a: Second high pressure heated water line 82: High-pressure heated water recovery line 82a: Second high pressure heated water recovery line 83: High-pressure steam line 83a: First high pressure steam line 83b: Second high pressure steam line 84: High pressure reheat steam line 85: High pressure exhaust steam line 85a: First high pressure exhaust steam line 85b: Second high pressure exhaust steam line 85c: Third high pressure exhaust steam line 86: High-pressure steam recovery line 87: Medium pressure exhaust steam line 87a: Second medium pressure exhaust steam line 88: Low pressure steam line 88a: Low temperature, low pressure steam line 89: Connecting medium pressure steam line 90: Low pressure extraction steam line 91: Branch water supply line 91a: Second branch water supply line 92: Connected water supply line 93: Medium pressure extraction steam line 94: Extraction steam recovery line 95: Extraction steam line 100: Brayton Cycle 101: Media compressor 102: Medium heater 103: Medium turbine 104:Medium cooler 110: Thermal cycle 120: Low boiling point medium Rankine cycle 111,121: Media booster 112,122:Medium heater 113, 123: Medium turbine 114,124:Medium cooler 115,125: Regenerative heat exchanger 130:Residual raw material removal equipment 131: Absorption tower 132: Regeneration Tower 133: Ammonia water line 134: Water line 135: Water supply pump 136: Heat exchanger 137: Water circulation line 138: Condenser 139: Reboiler 140: Ammonia recovery line 141: Recovered ammonia booster 151: Low-pressure steam utilization device 152: Medium pressure steam utilization unit 153: High-pressure steam utilization device 154, 156: Pressure reducing valve T: Ammonia tank EG: Exhaust gas NH: raw material fluid (ammonia) NHg: Gaseous ammonia (or ammonia in the gas phase) RG: Reactive gas RGp: Treated reaction gas NG: Natural gas

Claims

1. a preheater for preheating the fluid; the preheater is a heat exchanger that heats the fluid by exchanging heat between the fluid and a second heat medium, The preheater includes a vaporizer that heats and vaporizes the liquid fluid; The vaporizer is a heat exchanger that heats the liquid fluid by exchanging heat between a second heat medium for vaporization, which is a type of the second heat medium, and the liquid fluid. Fluid processing plants.

2. 2. A fluid treatment plant according to claim 1, the preheater includes a gas heater for heating the gaseous fluid from the vaporizer; The gas heater is a heat exchanger that heats the gaseous fluid by exchanging heat between a gas heating second heat medium, which is a type of the second heat medium, and the gaseous fluid. Fluid processing plants.

3. 3. A fluid treatment plant according to claim 2, the product of the constant pressure specific heat and the flow rate of the second heat medium for vaporization flowing through the vaporizer is greater than the product of the constant pressure specific heat and the flow rate of the second heat medium for gas heating flowing through the gas heater; Fluid processing plants.

4. 3. A fluid treatment plant according to claim 2, a gas heating second heat medium recovery line, one end of which is connected to the second heat medium outlet of the gas heater; and a second heat medium addition line, the gas heating second heat medium recovery line recovers the gas heating second heat medium from the gas heater, the second heat medium addition line is connected to the second heat medium recovery line for gas heating, and the second heat medium addition line supplies the second heat medium to the second heat medium recovery line for gas heating; The other end of the gas heating second heat medium recovery line is connected to the vaporizer, and the second heat medium is sent to the vaporizer as the second heat medium for vaporization via a second heat medium for vaporization line. Fluid processing plants.

5. 3. A fluid treatment plant according to claim 2, The system includes an exhaust gas generating facility that generates exhaust gas and an exhaust heat utilization facility, The waste heat utilization equipment includes: a gas frame through which the exhaust gas flows; a vaporization second heat medium heater provided in the gas frame and configured to exchange heat between the vaporization second heat medium and the exhaust gas to heat the vaporization second heat medium; a gas heating second heat medium heater that is disposed within the gas frame and upstream of the vaporization second heat medium heater in the flow of the exhaust gas, and that exchanges heat between the gas heating second heat medium and the exhaust gas to heat the gas heating second heat medium; a second heat medium line for vaporization that introduces the second heat medium for vaporization heated by the second heat medium heater for vaporization to the vaporizer; a gas heating second heat medium line that introduces the gas heating second heat medium heated in the gas heating second heat medium heater to the gas heater; having Fluid processing plants.

6. 2. A fluid treatment plant according to claim 1, the vaporizer has the ability to receive the gaseous second heat medium for vaporization, and to perform heat exchange between the gaseous second heat medium for vaporization and the liquid raw material fluid, thereby cooling and condensing the gaseous second heat medium for vaporization. Fluid processing plants.

7. 7. A plant for treating a fluid according to claim 6, a first vaporization second heat medium line that connects an evaporator that generates first steam to the vaporizer and supplies the first steam as the vaporization second heat medium from the evaporator to the vaporizer; a heated water recovery line connected to the vaporizer and configured to recover water produced by condensation of the first steam from the vaporizer; Equipped with Fluid processing plants.

8. 7. A plant for treating a fluid according to claim 6, a second vaporization second heat medium line connecting the steam turbine and the vaporizer and supplying second steam as the second vaporization heat medium from the steam turbine to the vaporizer; a heated water recovery line connected to the vaporizer and configured to recover water produced by condensation of the second steam from the vaporizer; Equipped with Fluid processing plants.

9. 2. A fluid treatment plant according to claim 1, The vaporizer includes a liquid-phase preheater that heats the liquid fluid while it remains liquid, and a phase-change preheater that heats and vaporizes the liquid fluid from the liquid-phase preheater, the liquid-phase preheater is a heat exchanger that heats the liquid fluid by exchanging heat between a liquid-phase preheating second heat medium, which is a type of the vaporization second heat medium, and the liquid raw material fluid, The phase change preheater is a heat exchanger that exchanges heat between a phase change preheating second heat medium, which is a type of the vaporization second heat medium, and the liquid fluid from the liquid phase preheater, thereby heating the liquid fluid. Fluid processing plants.

10. 10. A plant for treating a fluid according to claim 9, the product of the constant pressure specific heat and the flow rate of the second heat medium for phase change preheating flowing in the phase change preheater is greater than the product of the constant pressure specific heat and the flow rate of the second heat medium for liquid phase preheating flowing in the liquid phase preheater; Fluid processing plants.

11. 10. A plant for treating a fluid according to claim 9, a first connected second heat medium line connecting the phase change preheater and the liquid phase preheater, recovering the heat-exchanged second heat medium for phase change preheating from the phase change preheater and sending it to the liquid phase preheater as the second heat medium for liquid phase preheating; a second heat medium recovery line that recovers the second heat medium from a middle of the first connected second heat medium line; Equipped with Fluid processing plants.

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