TW202344751A - Power-generating system - Google Patents

Abstract

Provided is a technology that is capable of using heat recovered by a heat medium. This power-generating system is provided with: a reaction tower for producing a product gas by an exothermic reaction of starting gases at a catalyst; a steam-producing unit for producing steam from a liquid in which the heat source is a heat medium that passes through the reaction tower and maintains the inside of the reaction tower at an operating temperature within a specific range; and a power-generating unit that is driven by the steam produced by the steam-producing unit.

Description

Power generation system

The invention relates to a power generation system.

For example, Patent Document 1 discloses a technology related to a generation device and a generation method that generate product gas through an exothermic reaction of a reactant in a gaseous state. [Prior art documents] [Patent Document]

[Patent Document 1] Japanese Patent No. 6984098

[Problem to be solved by the invention]

A raw material gas is supplied into a reactor filled with a catalyst, and a product gas is generated from the raw material gas by a heat-generating reaction of the raw material gas. The heat medium is passed through the reactor, and the reaction heat generated during the exothermic reaction of the raw material gas is recovered by the heat medium. The heat medium after passing through the reactor is cooled by cooling water, and the heat recovered by the heat medium is not utilized.

An object of the present invention is to provide a technology that can utilize heat recovered from a thermal medium. [Means to solve the problem]

The present invention to solve the above problems is a power generation system, including: a reaction tower that generates product gas by a thermal reaction of raw material gas in a catalyst; and a steam generation unit that passes through the reaction tower to generate the product gas. A heat medium maintained at an operating temperature within a predetermined range serves as a heating source to generate steam from the liquid; and a power generation unit is driven using the steam generated by the steam generating unit.

By passing the heat medium through the reaction tower, the heat medium recovers the reaction heat of the raw material gas in the reaction tower. The heat medium that has passed through the reaction tower is heated by the reaction heat of the raw material gas in the reaction tower. When the operating temperature in the reaction tower becomes higher, the temperature of the heat medium passing through the reaction tower becomes higher. The heat medium that has passed through the reaction tower is used as a heating source to generate vapor from the liquid, and the generated vapor is used to drive the power generation unit, whereby the heat recovered from the heat medium can be utilized. In this way, the energy efficiency of the entire process or a part of the process can be improved.

The power generation system may further include a preheating unit that preheats the liquid supplied to the steam generating unit using the product gas sent from the reaction tower. In the preheating section, heat exchange is performed between the liquid supplied to the steam generating section and the product gas sent out from the reaction tower. The product gas sent out from the reaction tower is heated by the temperature rise of the reaction tower due to the exothermic reaction of the raw material gas in the reaction tower. Therefore, the liquid supplied to the steam generating part can be preheated by the product gas sent out from the reaction tower. The liquid supplied to the steam generating section is preheated by the product gas sent out from the reaction tower, whereby the preheated liquid can be supplied into the steam generating section.

The power generation system may further include a gas preheating unit that preheats the raw material gas supplied to the reaction tower using the product gas sent from the reaction tower. Heat exchange is performed between the raw material gas supplied to the reaction tower and the product gas sent out from the reaction tower. The product gas sent out from the reaction tower is heated by the temperature rise of the reaction tower due to the exothermic reaction of the raw material gas in the reaction tower. Therefore, the raw material gas supplied to the reaction tower can be preheated by the product gas sent from the reaction tower. The raw material gas supplied to the reaction tower is preheated by the product gas sent out from the reaction tower, whereby the preheated raw material gas can be supplied into the reaction tower.

The power generation system may further include a gas preheating unit that uses the heat medium that has passed through the reaction tower to preheat the raw material gas supplied to the reaction tower. Heat exchange is performed between the raw material gas supplied to the reaction tower and the heat medium that has passed through the reaction tower. The heat medium that has passed through the reaction tower is heated by the reaction heat of the raw material gas in the reaction tower. Therefore, the raw material gas supplied to the reaction tower can be preheated by the heat medium passing through the reaction tower. The raw material gas supplied to the reaction tower is preheated by the heat medium passing through the reaction tower, whereby the preheated raw material gas can be supplied into the reaction tower.

The power generation system may further include: a plurality of reaction towers, including a first reaction tower and a second reaction tower; and a raw material gas supply unit that supplies the raw material gas and the heat medium to the first reaction tower. After passing through the second reaction tower, the product gas and unreacted gas are passed through the first reaction tower and used as the heating source in the steam generating section. The raw material gas is supplied to the second reaction tower. The heat medium that has passed through the second reaction tower is heated by the reaction heat of the raw material gas in the second reaction tower, and the heat medium that has passed through the first reaction tower is further heated by the reaction heat of the raw material gas in the first reaction tower. . The heat medium that has passed through the first reaction tower and the second reaction tower is used as a heating source to generate steam from the liquid, and the generated steam is used to drive the power generation unit, whereby the heat recovered from the heat medium can be utilized.

The power generation system may further include: a first preheating unit that uses the product gas sent from the first reaction tower and the unreacted raw material gas to react with the liquid supplied to the steam generation unit. Preheating is performed; and a second preheating part preheats the liquid supplied to the steam generating part by the product gas sent from the second reaction tower. By raising the temperature of the first reaction tower due to the exothermic reaction of the raw material gas in the first reaction tower, the product gas and the raw material gas sent out from the first reaction tower are heated. Therefore, the liquid supplied to the steam generating part can be preheated by the product gas and raw material gas sent from the first reaction tower. The liquid supplied to the steam generating section is preheated by the product gas and unreacted raw material gas sent from the first reaction tower, whereby the preheated liquid can be supplied into the steam generating section. The product gas sent out from the second reaction tower is heated by the temperature rise of the second reaction tower due to the exothermic reaction of the raw material gas in the second reaction tower. Therefore, the liquid supplied to the steam generating part can be preheated by the product gas sent out from the second reaction tower. The liquid supplied to the steam generating part is preheated by the product gas sent out from the second reaction tower, whereby the preheated liquid can be supplied into the steam generating part.

The power generation system may further include: a first gas preheating unit that uses the product gas sent from the first reaction tower and the unreacted raw material gas to react with all the gas supplied to the first reaction tower. The raw material gas is preheated; and a second gas preheating section uses the product gas sent from the second reaction tower to react with the product gas supplied to the second reaction tower and the unreacted gas. The raw gas is preheated. By raising the temperature of the first reaction tower due to the exothermic reaction of the raw material gas in the first reaction tower, the product gas and unreacted raw material gas sent out from the first reaction tower are heated. Therefore, the raw material gas supplied to the first reaction tower can be preheated by the product gas and unreacted raw material gas sent from the first reaction tower. The raw material gas supplied to the first reaction tower is preheated by the product gas sent from the first reaction tower, whereby the preheated raw material gas can be supplied into the first reaction tower. The product gas sent out from the second reaction tower is heated by the temperature rise of the second reaction tower due to the exothermic reaction of the raw material gas in the second reaction tower. Therefore, the raw material gas supplied to the second reaction tower can be preheated by the product gas sent from the second reaction tower. The raw material gas supplied to the second reaction tower is preheated by the product gas sent from the second reaction tower, whereby the preheated raw material gas can be supplied into the second reaction tower.

The power generation system may further include: a first gas preheating unit that uses the heat medium that has passed through the first reaction tower to preheat the raw material gas supplied to the first reaction tower; and a third The two-gas preheating unit preheats the product gas and the unreacted raw material gas supplied to the second reaction tower by using the heat medium that has passed through the second reaction tower. The heat medium that has passed through the first reaction tower is heated by the reaction heat of the raw material gas in the first reaction tower. Therefore, the raw material gas supplied to the first reaction tower can be preheated by the heat medium passing through the first reaction tower. The raw material gas supplied to the first reaction tower is preheated by the heat medium that has passed through the first reaction tower, whereby the preheated raw material gas can be supplied into the first reaction tower. The heat medium that has passed through the second reaction tower is heated by the reaction heat of the raw material gas in the second reaction tower. Therefore, the raw material gas supplied to the second reaction tower can be preheated by the heat medium passing through the second reaction tower. The raw material gas supplied to the second reaction tower is preheated by the heat medium that has passed through the second reaction tower, whereby the preheated raw material gas can be supplied into the second reaction tower. [Effects of the invention]

It is possible to provide a technology that can utilize the heat recovered from the thermal medium.

Hereinafter, embodiments of the present invention will be described. The embodiment shown below is an example of the embodiment of the present invention, and the technical scope of the present invention is not limited to the following forms.

FIG. 1 is a schematic structural diagram of the power generation system according to the embodiment of the present invention. The power generation system 100 shown in FIG. 1 generates power by using steam generated from a liquid using a heat medium in a reaction tower that generates product gas through an exothermic reaction of a raw material gas as a heating source. For example, through the exothermic reaction of gaseous hydrogen and carbon dioxide, which are raw material gases (reaction gases), methane gas and water, which are product gases, are generated. Moreover, the chemical reaction is also a reversible reaction. The exothermic reaction expressed as a chemical reaction formula is as follows. 4H ₂ +CO ₂ ⇔CH ₄ +2H ₂ O (1)

The power generation system 100 includes a first-stage reaction tower 1, a first-stage gas cooling heat exchanger 2, a second-stage reaction tower 3, a second-stage gas cooling heat exchanger 4, a heat medium heater 5, Boiler 6, gas-liquid separator 7, gas-liquid separator 8, raw material gas supply unit 9, and saturated steam generator 10.

The reaction tower 1 generates product gas through the exothermic reaction of the raw material gas in the catalyst. Reaction tower 1 is a heat exchange type reaction vessel. The raw material gas contains, for example, hydrocarbons such as hydrogen (H ₂ ) and carbon dioxide (CO ₂ ). The product gas is, for example, methane gas. The reaction tower 1 and the raw material gas supply part 9 are connected by pipes, and the raw material gas is supplied from the raw material gas supply part 9 into the reaction tower 1 . Furthermore, the reaction tower 1 generates product water by the exothermic reaction of the raw material gas in the catalyst. The reaction tower 1 and the gas cooling heat exchanger 2 are connected by pipes. A valve or the like is provided in the piping connecting the reaction tower 1 and the gas cooling heat exchanger 2 .

The gas cooling heat exchanger 2 condenses the generated water (water vapor) generated in the reaction tower 1 . The gas cooling heat exchanger 2 and the gas-liquid separator 7 are connected by pipes. A valve or the like is provided in the pipe connecting the gas cooling heat exchanger 2 and the gas-liquid separator 7 . The gas-liquid separator 7 separates the product gas and the unreacted raw material gas to generate water (liquid). The power generation system 100 includes a separation unit 11 , and the generated water is sent from the gas-liquid separator 7 to the separation unit 11 . Details of the separation unit 11 will be described later.

The reaction tower 3 and the gas-liquid separator 7 are connected by pipes. A valve or the like is provided in the pipe connecting the reaction tower 3 and the gas-liquid separator 7 . The product gas and unreacted raw material gas generated in the reaction tower 1 are sent to the reaction tower 3 via the gas cooling heat exchanger 2 and the gas-liquid separator 7 . The reaction tower 3 generates product gas through the exothermic reaction of the raw material gas in the catalyst. The reaction tower 3 is a heat exchange type reaction vessel. In the reaction tower 3, product gas is generated from the unreacted raw material gas, whereby a high-concentration product gas can be generated.

The reaction tower 3 and the gas cooling heat exchanger 4 are connected by pipes. A valve or the like is provided in the piping connecting the reaction tower 3 and the gas cooling heat exchanger 4 . The gas cooling heat exchanger 4 condenses the generated water (water vapor) generated in the reaction tower 3 . The gas cooling heat exchanger 4 and the gas-liquid separator 8 are connected by pipes. A valve or the like is provided in a pipe connecting the gas cooling heat exchanger 4 and the gas-liquid separator 8 . The gas-liquid separator 8 separates the product gas and unreacted raw material gas to generate water (liquid).

Power generation system 100 includes storage tank 12 . The generated water is sent from the gas-liquid separator 8 to the separation unit 11 , and the product gas is sent from the gas-liquid separator 8 to the storage tank 12 . The storage tank 12 stores product gas. The gas-liquid separator 7 and the gas-liquid separator 8 are provided with drain valves for discharging generated water. The drain valve may be a drain trap that uses the buoyancy of a floating body to open and close the valve, or it may be a solenoid valve that electrically detects the water level and opens and closes the solenoid valve.

Reaction tower 1 and reaction tower 3 are filled with catalyst in advance. The catalyst may be any substance as long as it promotes reaction formula (1). Examples include the following catalysts, which include solid solutions of stabilizing elements and have tetragonal and/or cubic crystal systems. A stabilized zirconia carrier with a crystal structure and Ni carried by the stabilized zirconia carrier, and the stabilizing element includes at least one transition element selected from the group consisting of free Mn, Fe and Co.

Furthermore, the reaction tower 1 and the reaction tower 3 have a jacket structure, and the heat medium that exchanges heat with the heat-generating part in the reaction tower where the exothermic reaction occurs can flow out/flow into the jacket part (shell). For heat media, use heat carrier oil or water, for example. The heat medium heater 5 and the jacket part of the reaction tower 3 are connected by a pipe for flowing the heat medium. Furthermore, the jacketed portion of the reaction tower 1 and the jacketed portion of the reaction tower 3 are connected by a pipe through which the heating medium flows. A valve or the like is provided in the piping through which the heating medium flows. The heat medium heater 5 is a heater that heats the heat medium.

The jacket part of the reaction tower 1 and the boiler 6 are connected by a pipe for flowing a heating medium. The boiler 6 is a steam generating part that generates steam (saturated steam) from liquid. The boiler 6 has an internal pipe 51 into which a heat medium can flow, and a liquid tank 52 storing liquid such as water. The heating pipe as a part of the internal piping 51 circulates in the boiler 6 . Furthermore, the heating pipe in the internal piping 51 is arranged in the liquid tank 52 . The liquid stored in the liquid tank 52 is heated using the heat medium flowing into the internal pipe 51 as a heat source. Thereby, vapor is generated from the liquid stored in the liquid tank 52 . The heat medium heater 5 and the internal pipe 51 of the boiler 6 are connected by a pipe through which the heat medium flows. The heat medium heated by the heat medium heater 5 passes through the reaction tower 3 and then flows into the internal pipe 51 of the boiler 6 through the reaction tower 1 . The heat medium circulation pump 14 is provided in the pipe connecting the heat medium heater 5 and the internal pipe 51 of the boiler 6. The heat medium circulation pump 14 is used to heat the heat medium in the reaction tower 1, the reaction tower 3, and the heat medium circulation pump 14. Circulation between the device 5 and the boiler 6. Furthermore, the regulating valve 15 and the regulating valve 16 are provided in the pipe through which the heating medium flows. By opening and closing the regulating valve 15 and the regulating valve 16, the heat medium that has passed through the reaction tower 1 and the reaction tower 3 can be sent to the heat medium heater 5 via the boiler 6, or can be sent to the heat medium heater 5 without passing through the boiler 6. .

The power generation system 100 includes a cooler 17A and a cooler 17B. The cooler 17A cools the cooling water (refrigerant) used to condense the produced water in the gas cooling heat exchanger 2 . The gas cooling heat exchanger 2 and the cooler 17A are connected to each other by pipes through which cooling water flows. The cooler 17B cools the cooling water (refrigerant) used to condense the produced water in the gas cooling heat exchanger 4 . The gas cooling heat exchanger 4 and the cooler 17B are connected to each other by pipes through which cooling water flows. Here, an example is shown in which the power generation system 100 includes the cooler 17A and the cooler 17B. However, one pair of coolers may be used to condense the generated water in the gas cooling heat exchanger 2 and the gas cooling heat exchanger 4. of cooling water for cooling.

The power generation system 100 includes a control unit 21 , a measurement sensor 22 that measures the temperature in the reaction tower 1 , and a measurement sensor 23 that measures the temperature in the reaction tower 3 . The measurement data measured by the measurement sensor 22 and the measurement data measured by the measurement sensor 23 are sent to the control unit 21 . Thereby, the control unit 21 acquires the temperature in the reaction tower 1 and the temperature in the reaction tower 3 . The control unit 21 sends the measurement data measured by the measurement sensor 22 and the measurement data measured by the measurement sensor 23 to the raw material gas supply unit 9 . Thereby, the raw material gas supply unit 9 acquires the temperature in the reaction tower 1 and the temperature in the reaction tower 3 .

The control unit 21 is a controller that controls the entire operation of the power generation system 100 . The control unit 21 may include a dedicated machine or a general-purpose computer. The control unit 21 includes hardware resources such as a processor (Central Processing Unit (CPU)), memory, storage, and communication interface (Interface, I/F). The memory can also be random access memory (Random Access Memory, RAM). The storage can also be a non-volatile memory device (such as Read Only Memory (ROM), flash memory, etc.). The function of the control unit 21 is realized by expanding the program stored in the storage into the memory and executing it by the processor. In addition, the structure of the control part 21 is not limited to this. For example, all or part of the function can also include circuits such as Application Specific Integrated Circuit (ASIC) or Field Programmable Gate Array (FPGA), or it can also be configured by a cloud server or other device. to perform all or part of a function.

The control unit 21 controls the heat medium heater 5 . By controlling the operation of the heat medium heater 5, the heat medium heater 5 heats the heat medium or stops heating the heat medium. In this way, the heat medium heater 5 is used to heat the heat medium or to stop the heating. The control unit 21 controls the heat medium heater 5 so that the temperature of the heat medium becomes a predetermined temperature. The predetermined temperature is, for example, 250°C or more and 500°C or less. Furthermore, the control unit 21 controls the regulating valve 15 and the regulating valve 16 .

The control unit 21 maintains the operating temperature within the reaction tower 1 within a predetermined range by adjusting the temperature of the heat medium. That is, by passing the temperature-adjusted heat medium through the reaction tower 1 , the inside of the reaction tower 1 is maintained at an operating temperature within a predetermined range. The control unit 21 may adjust the temperature of the heat medium so as to maintain the temperature in the reaction tower 1 at, for example, 250°C or more and 300°C or less. Preferably, the control unit 21 adjusts the temperature of the heat medium so as to maintain the temperature in the reaction tower 1 above 280°C. The operating temperature is not limited to 250°C or more and 300°C or less. The operating temperature may be 250°C or more and 500°C or less. The operating temperature may be a temperature at which the exothermic reaction of the raw material gas proceeds favorably, that is, a rated temperature. The rated temperature may also be a temperature at which a high concentration of product gas is generated.

The control unit 21 maintains the operating temperature in the reaction tower 3 within a predetermined range by adjusting the temperature of the heat medium. That is, by passing the temperature-adjusted heat medium through the reaction tower 3 , the inside of the reaction tower 3 is maintained at an operating temperature within a predetermined range. The control unit 21 may also adjust the temperature of the heat medium so as to maintain the temperature in the reaction tower 3 at, for example, 250°C or more and 300°C or less. Preferably, the control unit 21 adjusts the temperature of the heat medium so as to maintain the temperature in the reaction tower 3 above 280°C. The operating temperature is not limited to 250°C or more and 300°C or less. The operating temperature may be 250°C or more and 500°C or less. The operating temperature may be a temperature at which the exothermic reaction of the raw material gas proceeds favorably, that is, a rated temperature. The rated temperature may also be a temperature at which a high concentration of product gas is generated.

The boiler 6 uses the heat medium flowing into the internal piping 51 through the reaction tower 1 and the reaction tower 3 as a heating source to heat the liquid stored in the liquid tank 52 , thereby generating electricity from the liquid stored in the liquid tank 52 steam. The boiler 6 and the saturated steam generator 10 are connected through pipes. The pipe connecting the boiler 6 and the saturated steam generator 10 is provided with a pressure regulating valve 18 that adjusts the inside of the boiler 6 to a predetermined steam pressure. The control target value of the pressure regulating valve 18, that is, the prescribed steam pressure is a rated steam pressure at which the saturated steam generator 10 can be operated. The steam generated by the boiler 6 is sent to the saturated steam generator 10 . By controlling the opening of the pressure regulating valve 18 so that the inside of the boiler 6 reaches a predetermined steam pressure, the amount or pressure of the steam sent to the saturated steam generator 10 is controlled. The control unit 21 may also control the opening of the pressure regulating valve 18 and the like.

The saturated steam generator 10 is a power generation unit driven by steam generated by the boiler 6 . The saturated steam generator 10 may be a turbine generator or a screw generator. The saturated steam generator 10 generates electricity using steam supplied from the boiler 6 . The electricity generated by the saturated steam generator 10 can be used as in-process power for control units, heating equipment, compressors, etc. used to operate the process. In addition, the electricity generated by the saturated steam generator 10 may be used for in-process power, and the remaining electricity may be supplied to any power source. Furthermore, a power storage device may be provided to store the electricity generated by the saturated steam generator 10 in the power storage device.

As the heat medium passes through the reaction tower 3 , the heat medium recovers the reaction heat of the raw material gas in the reaction tower 3 . Furthermore, when the heat medium passes through the reaction tower 1 , the heat medium recovers the reaction heat of the raw material gas in the reaction tower 1 . Therefore, the heat medium that has passed through the reaction tower 1 and the reaction tower 3 is heated by the reaction heat of the raw material gas in the reaction tower 1 and the reaction heat of the raw material gas in the reaction tower 3 . When the operating temperature in reaction tower 1 becomes higher, the temperature of the heat medium passing through reaction tower 1 becomes higher. When the operating temperature in reaction tower 3 becomes higher, the temperature of the heat medium passing through reaction tower 3 becomes higher. In this embodiment, the heat medium that has passed through the reaction tower 1 and the reaction tower 3 is used as a heating source, steam is generated from the liquid stored in the liquid tank 52, and the generated steam is used to drive the saturated steam generator 10, thereby, The heat recovered from the thermal medium can be utilized. In this way, steam is generated based on the recovered reaction heat, and electricity is generated from the steam, thereby making it easy to use the recovered reaction heat generally and widely. In this way, the energy efficiency of the entire process or a part of the process (such as the methanation reaction process) can be improved.

Next, the separation unit 11 will be described. FIG. 2 is a structural diagram of the separation unit 11. The separation unit 11 separates the dissolved gas dissolved in the generated water generated in the reaction tower 1 when the product gas is generated in the reaction tower 1 . Furthermore, the separation unit 11 separates the dissolved gas dissolved in the generated water generated in the reaction tower 3 when the product gas is generated in the reaction tower 3 . The separation part 11 includes a pump 61 , a separation membrane module 62 , a vacuum pump 63 , a buffer tank 64 and a compressor 65 . The power generation system 100 includes a product gas path 13 through which the product gas sent from the reaction tower 3 flows. The product gas path 13 may also be connected to the storage tank 12 .

The generated water sent to the separation part 11 from the gas-liquid separator 7 and the gas-liquid separator 8 is sent to the separation membrane module 62 by the pump 61 . The separation membrane module 62 has a separation membrane 66 . The separation membrane 66 is, for example, a hollow fiber membrane. A vacuum pump 63 is connected to the separation membrane module 62 . The dissolved gas is separated from the self-generated water by the separation membrane 66 . When the dissolved gas is product gas, the inside of the separation membrane module 62 is evacuated by the vacuum pump 63 , and the product gas is sent to the buffer tank 64 . The buffer tank 64 temporarily stores product gas. The product gas stored in the buffer tank 64 is sent to the product gas path 13 through the compressor 65 . Thereby, the product gas separated from the generated water merges with the product gas flowing through the product gas path 13 .

Conventionally, a method was used to diffuse the product gas dissolved in the generated water into the atmosphere, or a degasser (degassing device) was used to blow gases such as air into a tank storing the generated water to forcefully expel it from the generated water. Product gas method. This method requires a large-capacity tank for storing product gas or a machine for blowing gas into the tank. According to this embodiment, since the volume of the buffer tank 64 that temporarily stores the product gas is small, the space of the buffer tank 64 can be saved. Furthermore, according to this embodiment, a device for blowing gas into the tank is required. Since the product gas separated from the generated water merges with the product gas flowing through the product gas path 13, diffusion of the product gas into the atmosphere can be suppressed.

The case where the dissolved gas is a product gas has been described above, but the dissolved gas may also be an unreacted raw material gas. By changing the type of the separation membrane 66 of the separation membrane module 62, the product gas dissolved in the generated water can be separated from the generated water, or the unreacted raw material gas dissolved in the generated water can be separated from the generated water. Furthermore, the separation unit 11 may include a separation membrane module 62 for separating product gas dissolved in the generated water from the generated water, and a separation membrane module 62 for separating unreacted raw material gas dissolved in the generated water from the generated water. 62. Furthermore, the separation unit 11 may include a buffer tank 64 for product gas and a buffer tank 64 for unreacted raw material gas.

When the dissolved gas is unreacted raw material gas, the inside of the separation membrane module 62 is evacuated by the vacuum pump 63 , and the unreacted raw material gas is sent to the buffer tank 64 . The unreacted raw material gas stored in the buffer tank 64 is sent to the raw material gas supply unit 9 through the compressor 65 . Thereby, the unreacted raw material gas returns to the raw material gas supply part 9 . According to this embodiment, since the volume of the buffer tank 64 that temporarily stores unreacted raw material gas is small, the space of the buffer tank 64 can be saved. Furthermore, according to this embodiment, a machine for blowing gas into the tank is not required. Since the unreacted raw material gas is returned to the raw material gas supply part 9, diffusion of the unreacted raw material gas into the atmosphere can be suppressed.

Furthermore, in order to dry the product gas and unreacted raw material gas sent from the gas-liquid separator 8, the product gas and unreacted raw material gas may be removed by passing through a container filled with a catalyst or silica gel or a porous membrane. Moisture in the gas. When a porous membrane is used, suction with a vacuum pump or dry hydrogen in the raw material gas can also be used. Furthermore, in order to improve the purity of hydrocarbons such as methane or ethane in the dry gas (dried product gas) obtained by the drying process, a membrane separation device using an organic membrane can also be used to produce a dry gas. Concentrated hydrocarbon-rich gas. The offgas generated separately due to the concentration of membrane separation can be discharged outside the system or reused as a raw material for reaction.

The raw material gas may be a mixed gas in which a gas containing at least one of the following (1A) to (1D) and the gas of the following (2) are adjusted to a ratio of 1:2 to 8 by flow control. (1A) Biogas containing carbon dioxide or carbon dioxide and methane as the main components (1B) Woody biomass gas mainly composed of hydrogen, carbon monoxide, carbon dioxide, water and hydrocarbons (1C) Gasification gas derived from coal (1D) Waste gas from blast furnaces and other iron-making processes, waste gas from cement manufacturing processes, etc., mixed gases containing more than 0.02% of carbon dioxide (2) Mixed gas containing hydrogen produced by electrolysis or hydrogen discharged from chemical manufacturing steps

FIG. 3 is a detailed structural diagram of the power generation system according to the embodiment of the present invention. The power generation system 100 includes a gas mixer 31 , an economizer 32 and a gas heater 33 . The raw material gas sent from the raw material gas supply unit 9 is supplied into the reaction tower 1 via the gas mixer 31 , the economizer 32 and the gas heater 33 . The power generation system 100 includes a water heating heat exchanger 34 , an economizer 35 , a gas heater 36 , and a water heating heat exchanger 37 . The product gas and unreacted raw material gas sent out from the reaction tower 1 pass through the water heating heat exchanger 34, the economizer 32, the gas cooling heat exchanger 2, the gas-liquid separator 7, the economizer 35, and the gas heater. 36 is supplied to the reaction tower 3. The product gas sent out from the reaction tower 3 is sent to the storage tank 12 via the water heating heat exchanger 37, the economizer 35, the gas cooling heat exchanger 4, and the gas-liquid separator 8.

The gas mixer 31 uniformly mixes the raw material gas sent from the raw material gas supply unit 9 . In the economizer 32 , heat is exchanged between the raw material gas supplied to the reaction tower 1 and the gas sent out from the reaction tower 1 . The gas sent out from the reaction tower 1 is product gas, unreacted raw material gas, or a mixed gas of product gas and unreacted raw material gas. The gas sent out from the reaction tower 1 is heated by the temperature rise of the reaction tower 1 when the heated heat medium passes through the reaction tower 1 and the temperature rise of the reaction tower 1 caused by the exothermic reaction of the raw material gas in the reaction tower 1 . Therefore, the economizer 32 functions as a gas preheating unit that preheats the raw material gas supplied to the reaction tower 1 with the gas sent from the reaction tower 1 . The raw material gas supplied to the reaction tower 1 is preheated by the gas sent out from the reaction tower 1 , whereby the preheated raw material gas can be supplied into the reaction tower 1 . The economizer 32 has a flow path 71 through which the raw material gas supplied to the reaction tower 1 flows, and a flow path 72 through which the gas sent out from the reaction tower 1 flows. The source gas flowing through the flow path 71 does not flow into the flow path 72 , and the gas flowing through the flow path 72 does not flow into the flow path 71 .

In the gas heater 33, heat exchange is performed between the raw material gas supplied to the reaction tower 1 and the heat medium that has passed through the reaction tower 1. The heat medium is heated by the heat medium heater 5 . Furthermore, the heat medium that has passed through the reaction tower 1 and the reaction tower 3 is heated by the reaction heat of the raw material gas in the reaction tower 1 and the reaction heat of the raw material gas in the reaction tower 3 . Therefore, the gas heater 33 functions as a gas preheating unit that preheats the raw material gas supplied to the reaction tower 1 using the heat medium that has passed through the reaction tower 1 and the reaction tower 3 . The raw material gas supplied to the reaction tower 1 is preheated by the heat medium that has passed through the reaction tower 1 and the reaction tower 3 , whereby the preheated raw material gas can be supplied into the reaction tower 1 . The heat medium that has passed through the reaction tower 3 is heated by the reaction heat of the raw material gas in the reaction tower 3 , and the heat medium that has passed through the reaction tower 1 is further heated by the reaction heat of the raw material gas in the reaction tower 1 . The gas heater 33 has a flow path 73 through which the raw material gas supplied to the reaction tower 1 flows, and a flow path 74 through which the heating medium flows. The source gas flowing through the flow path 73 does not flow into the flow path 74 , and the heat medium flowing through the flow path 74 does not flow into the flow path 73 .

In the water heating heat exchanger 34 , heat exchange is performed between the liquid supplied to the boiler 6 and the gas sent out from the reaction tower 1 . The gas sent out from the reaction tower 1 is heated by the temperature rise of the reaction tower 1 when the heated heat medium passes through the reaction tower 1 and the temperature rise of the reaction tower 1 caused by the exothermic reaction of the raw material gas in the reaction tower 1 . Therefore, the water heating heat exchanger 34 functions as a preheating unit that preheats the liquid supplied to the boiler 6 with the gas sent from the reaction tower 1 . The liquid supplied to the boiler 6 is preheated by the gas sent from the reaction tower 1 , whereby the preheated liquid can be supplied to the boiler 6 . The water heating heat exchanger 34 has a flow path 75 through which the liquid supplied to the boiler 6 flows, and a flow path 76 through which the gas sent out from the reaction tower 1 flows. The liquid flowing through the flow path 75 does not flow into the flow path 76 , and the gas flowing through the flow path 76 does not flow into the flow path 75 .

The power generation system 100 includes a pump 38 , a deaerator 39 , a low-pressure saturated steam supply unit 40 , a separator 41 and a discharge valve 42 . When the pump 38 is driven, the liquid held in the deaerator 39 is supplied to the boiler 6 via the water heating heat exchanger 34 . The deaerator 39 removes gases such as oxygen and carbon dioxide from the liquid supplied to the boiler 6 . The low-pressure saturated vapor supply unit 40 sends out a gas-liquid mixed fluid containing low-pressure saturated vapor. The separator 41 removes liquid from the gas-liquid mixed fluid sent from the low-pressure saturated steam supply part 40 and supplies the low-pressure saturated steam into the boiler 6 . The separator 41 retains the liquid removed from the gas-liquid mixed fluid. Then, the gas-liquid mixed fluid sent from the low-pressure saturated vapor supply unit 40 is sent to the deaerator 39 . By opening the discharge valve 42, the liquid held in the separator 41 is discharged.

In the gas heater 36, heat exchange is performed between the gas supplied to the reaction tower 3 and the heat medium that has passed through the reaction tower 3. The gas supplied to the reaction tower 3 is product gas, unreacted raw material gas, or a mixed gas of the product gas and unreacted raw material gas. The heat medium is heated by the heat medium heater 5 . Furthermore, the heat medium that has passed through the reaction tower 3 is heated by the reaction heat of the raw material gas in the reaction tower 3 . Therefore, the gas heater 36 functions as a gas preheating unit that preheats the gas supplied to the reaction tower 3 using the heat medium that has passed through the reaction tower 3 . The raw material gas supplied to the reaction tower 3 is preheated by the heat medium that has passed through the reaction tower 3 , whereby the preheated gas can be supplied into the reaction tower 3 . The gas heater 36 has a flow path 77 through which the gas supplied to the reaction tower 3 flows, and a flow path 78 through which the heating medium flows. The gas flowing through the flow path 77 does not flow into the flow path 78 , and the heat medium flowing through the flow path 78 does not flow into the flow path 77 .

The power generation system 100 includes a liquid supply part 43 . The liquid supply unit 43 supplies liquid such as water. The liquid sent from the liquid supply part 43 is supplied into the boiler 6 via the water heating heat exchanger 37, the deaerator 39, and the water heating heat exchanger 34.

In the water heating heat exchanger 37 , heat exchange is performed between the liquid supplied to the boiler 6 and the gas sent out from the reaction tower 3 . The gas sent out from the reaction tower 3 is product gas, unreacted raw material gas, or a mixed gas of the product gas and unreacted raw material gas. The gas sent out from the reaction tower 3 is heated by the temperature rise of the reaction tower 3 when the heated heat medium passes through the reaction tower 3 and the temperature rise of the reaction tower 3 caused by the exothermic reaction of the raw material gas in the reaction tower 3 . Therefore, the water heating heat exchanger 37 functions as a preheating unit that preheats the liquid supplied to the boiler 6 with the gas sent from the reaction tower 3 . The liquid supplied to the boiler 6 is preheated by the gas sent from the reaction tower 3 , whereby the preheated liquid can be supplied to the boiler 6 . The water heating heat exchanger 37 has a flow path 79 through which the liquid supplied to the boiler 6 flows, and a flow path 80 through which the gas sent out from the reaction tower 3 flows. The liquid flowing through the flow path 79 does not flow into the flow path 80 , and the gas flowing through the flow path 80 does not flow into the flow path 79 .

In the economizer 35 , heat exchange is performed between the gas supplied to the reaction tower 3 and the gas sent out from the reaction tower 1 . The gas sent out from the reaction tower 3 is heated by the temperature rise of the reaction tower 3 when the heated heat medium passes through the reaction tower 3 . Therefore, the economizer 35 functions as a gas preheating unit that preheats the gas supplied to the reaction tower 3 with the gas sent from the reaction tower 3 . The gas supplied to the reaction tower 3 is preheated by the gas sent out from the reaction tower 3 , whereby the preheated gas can be supplied into the reaction tower 3 . The economizer 35 has a flow path 81 through which the gas supplied to the reaction tower 3 flows, and a flow path 82 through which the gas sent out from the reaction tower 3 flows. The gas flowing through the flow path 81 does not flow into the flow path 82 , and the gas flowing through the flow path 82 does not flow into the flow path 81 .

In the power generation system 100 , the liquid supplied to the boiler 6 is preheated by the gas sent from the reaction tower 1 , and the preheated liquid is supplied to the boiler 6 . Furthermore, in the power generation system 100 , the liquid supplied to the boiler 6 is preheated by the gas sent from the reaction tower 3 , and the preheated liquid is supplied to the boiler 6 . Thereby, in the boiler 6, the preheated liquid is heated, whereby saturated steam can be generated. The pressure regulating valve 18 performs pressure regulation so that the temperature of the saturated steam generated in the boiler 6 becomes 250° C. or higher. Therefore, in the boiler 6, high-temperature saturated steam can be generated from high-temperature liquid. Furthermore, in the boiler 6, saturated steam is generated from high-temperature liquid, so the time required to generate the saturated steam is shortened.

The power generation system 100 includes a heat medium tank 44 and a heat medium tank 45 . The heat medium tank 44 and the heat medium tank 45 are provided in the pipe through which the heat medium flows. When maintenance of the reaction tower 1 and the reaction tower 3 is performed, the heat medium flowing into the jacket portion of the reaction tower 1 and the jacket portion of the reaction tower 3 is temporarily stored in the heat medium tank 44 and the heat medium tank 45 .

In the heat medium system, when heat carrier oil is used as the heat medium, an expansion tank or a buffer tank is used to accommodate the volume expanded when the heat medium reaches a high temperature. An expansion tank or a buffer tank may be used instead of the heat medium tank 44 and the heat medium tank 45 . When high-pressure liquid water such as boiler water is used as the heat medium, a gas-water drum is used instead of the buffer tank. An air-water drum may be used instead of the heat medium tank 44 and the heat medium tank 45 .

The water level adjustment in the boiler 6 when stable is explained. Here, a case where water is stored in the boiler 6 will be described. When the saturated steam generated in the boiler 6 reaches a predetermined steam pressure in the boiler 6 and the pressure regulating valve 18 is opened, the saturated steam generated in the boiler 6 is supplied to the saturated steam generator 10 . At this time, in principle, the water level in the boiler 6 will decrease corresponding to the amount of saturated steam consumed by the saturated steam generator 10 . When the water level in the boiler 6 drops, the heating pipe in the internal pipe 51 will be exposed, which is not safe. Therefore, the water level in the boiler 6 must be controlled.

Regarding the method of controlling the water level in the boiler 6 , in principle, the boiler 6 is provided with a level transmitter and then steam is supplied to the saturated steam generator 10 . When the steam is consumed in the saturated steam generator 10, the pump 38 is driven, and the raw material water sent from the liquid supply part 43 is passed through the water heating heat exchanger 37, the deaerator 39, and the water heating heat exchanger 34. It is supplied to the boiler 6. Since the raw material water corresponding to the amount of steam consumed in the saturated steam generator 10 is supplied into the boiler 6, the water level in the boiler 6 is stabilized within a fixed range.

At the time of startup, since the prescribed steam pressure has not yet been reached in the boiler 6, the pressure regulating valve 18 is in a closed state. Then, when the inside of the boiler 6 reaches a predetermined steam pressure, the pressure regulating valve 18 starts to open, and the saturated steam generator 10 becomes operable. On the other hand, in terms of manufacturing processes, the boiler 6 must be temporarily blown due to corrosion and the like, so even during stable operation, the water level in the boiler 6 may sometimes drop. Moreover, in addition to this, the water level in the boiler 6 may also decrease due to fine-tuning of the manufacturing process or the like. The water level control at this time is performed by the following method 1 or method 2.

(method 1) When the pump 38 is driven, the amount of water supplied to the boiler 6 is fixed, and the openings of the regulating valve 15 and the regulating valve 16 are adjusted to suppress the amount of heating of the water in the boiler 6 . In this way, the steam production volume of the boiler 6 is temporarily reduced so that the water level in the boiler 6 can rise. (Method 2) When the pump 38 is driven, the supply amount of water to the boiler 6 is temporarily increased, thereby raising the water level in the boiler 6 . At this time, the opening degrees of the regulating valve 15 and the regulating valve 16 are not adjusted.

Alternatively, method 1 or method 2 may be performed after performing an operation that causes the water level in the boiler 6 to drop. Furthermore, after the water level in the boiler 6 has been raised to a certain extent by performing method 1 or method 2, an operation that causes the water level in the boiler 6 to drop may be performed.

The reaction tower 1 and the reaction tower 3 have a jacket structure, but are not limited thereto. The reaction tower 1 and the reaction tower 3 may also have a single-tube or multi-tube shell and tube structure as described below, that is, having more than one tube filled with a catalyst for chemically reacting hydrocarbons with hydrogen. tube, and arrange the tube filled with catalyst in a shell tube with a larger diameter. Moreover, the reaction tower 1 and the reaction tower 3 may also have a parallel plate structure as follows, that is, having one or more embossed plates and a chamber filled with a catalyst in the space surrounded by the side strips, The chamber filled with catalyst is arranged in a large-diameter shell tube, and the heat medium can be circulated in the embossed plate.

FIG. 4 is a structural diagram of the power generation system 100 according to the embodiment of the present invention. The power generation system 100 has a first reaction process group 101 and a second reaction process group 102 . The first reaction process group 101 includes a reaction tower 1, a gas cooling heat exchanger 2, a gas-liquid separator 7, an economizer 32, and a water heating heat exchanger 34. The second reaction process group 102 includes a reaction tower 3, a gas cooling heat exchanger 4, a gas-liquid separator 8, an economizer 35, and a water heating heat exchanger 37. The structure of the power generation system 100 shown in FIG. 4 is not limited. In addition to the first reaction process group 101 and the second reaction process group 102 , the power generation system 100 may also have a third reaction process group and a fourth reaction process group. The structures of the third reaction process group and the fourth reaction process group can also be the same as the structure of the second reaction process group 102 .

As the structure of the reaction tower 1 in the first reaction process group 101, one of a jacket structure, a shell-and-tube structure, and a parallel plate structure can also be selected. As the structure of the reaction tower 3 in the second reaction process group 102, one of a jacket structure, a shell-and-tube structure, and a parallel plate structure can also be selected. As the structure of the reaction tower of the third reaction process group and the fourth reaction process group, one of a jacket structure, a shell-and-tube structure, and a parallel plate structure can also be selected.

In this embodiment, heat exchange type reaction vessels are used as the reaction tower 1 and the reaction tower 3 . A heat exchange type reaction vessel can generate a higher concentration of product gas than a heat insulating type reaction vessel. In the heat-insulated type, a large amount of catalyst is loaded into a simple reaction vessel, and the reaction is promoted according to the upper limit of chemical equilibrium. However, in order to generate a high-concentration product gas, multiple reaction vessels are required. In contrast, in a heat exchange type reaction vessel, a high-concentration product gas can be generated with a single reaction vessel.

In the embodiment, the heat medium heated by the heat medium heater 5 passes through the reaction tower 3 and then flows into the internal pipe 51 of the boiler 6 through the reaction tower 1, but it is not limited to this. The heat medium heated by the heat medium heater 5 may flow into the internal pipe 51 of the boiler 6 through the reaction tower 3 after passing through the reaction tower 1 . Moreover, the heat medium heated by the heat medium heater 5 can also pass through each reaction tower in the order of the reaction tower in the fourth reaction process group, the reaction tower in the third reaction process group, reaction tower 3, and reaction tower 1. , flows into the internal pipe 51 of the boiler 6 . Moreover, the heat medium heated by the heat medium heater 5 can also pass through each reaction tower in the order of reaction tower 1, reaction tower 3, the reaction tower in the third reaction process group, and the reaction tower in the fourth reaction process group. , flows into the internal pipe 51 of the boiler 6 .

In the embodiment, two reaction towers are included, but the number of reaction towers can also be one level, three levels, four levels, or any level. Furthermore, in the embodiment, heat carrier oil or water is used as the heat medium. However, the heat medium may also be a substance suitable for use conditions such as molten salt or high-pressure water, taking into account use conditions such as use temperature and use equipment. Furthermore, the water supplied to the boiler 6 may be boiler water, for example, or chemicals required for operation may be added to the water supplied to the boiler 6 . Furthermore, when the reaction performed in the reaction tower is an irreversible reaction, the power generation system 100 does not need to be used.

Furthermore, each process described above can also be understood as a generating device or an operating device that is a part of the power generation system. Moreover, each process described above can also be understood as a power generation method, a generation method, an operation method, etc. It can also be understood as a production system or operation system having at least a part of each process or function described above. Furthermore, the components and processes described may each be combined with each other as much as possible to constitute the present invention.

1, 3: Reaction tower 2, 4: Heat exchanger for gas cooling 5: Thermal medium heater 6: Boiler 7, 8: Gas-liquid separator 9: Raw gas supply department 10: Saturated steam generator 11:Separation department 12:Storage tank 13: Product gas path 14: Thermal medium circulation pump 15, 16: Adjustment valve 17A, 17B: Cooler 18: Pressure adjustment valve 21:Control Department 22, 23: Measuring sensor 31:Gas mixer 32, 35: Heat economizer 33, 36: Gas heater 34, 37: Heat exchanger for water heating 38:Pump 39:Degasser 40: Low pressure saturated steam supply part 41:Separator 42: Discharge valve 43:Liquid supply department 44, 45: Thermal medium tank 51: Internal piping 52:Liquid tank 61:Pump 62:Separation membrane module 63: Vacuum pump 64: Buffer tank 65:Compressor 66:Separation membrane 71～82:Flow path 100: Power generation system 101: First reaction process group 102: Second reaction process group

FIG. 1 is a schematic structural diagram of the power generation system according to the embodiment. Fig. 2 is a structural diagram of the separation unit. FIG. 3 is a detailed structural diagram of the power generation system of the embodiment. FIG. 4 is a structural diagram of the power generation system according to the embodiment.

Claims (8)

A power generation system including: Reaction tower generates product gas through the thermal reaction of raw material gas in the catalyst; a steam generating unit that generates steam from the liquid using a heat medium that passes through the reaction tower and maintains the inside of the reaction tower at an operating temperature within a predetermined range as a heating source; and A power generation unit is driven using the steam generated by the steam generating unit. The power generation system as described in claim 1 further includes: A preheating section preheats the liquid supplied to the steam generating section with the product gas sent from the reaction tower. The power generation system as described in claim 1 or 2 further includes: A gas preheating unit preheats the raw material gas supplied to the reaction tower with the product gas sent from the reaction tower. The power generation system as described in claim 1 or 2 further includes: A gas preheating unit preheats the raw material gas supplied to the reaction tower using the heat medium that has passed through the reaction tower. The power generation system as described in claim 1 further includes: A plurality of the reaction towers, including a first reaction tower and a second reaction tower; and a raw material gas supply unit supplies the raw material gas to the first reaction tower, The heat medium, after passing through the second reaction tower, passes through the first reaction tower and is used as the heating source in the steam generating part, The product gas and the unreacted raw material gas are supplied from the first reaction tower to the second reaction tower. The power generation system as described in claim 5 further includes: A first preheating section preheats the liquid supplied to the steam generating section using the product gas sent from the first reaction tower and the unreacted raw material gas; and A second preheating section preheats the liquid supplied to the steam generating section with the product gas sent from the second reaction tower. The power generation system as described in claim 5 or 6 further includes: A first gas preheating unit preheats the raw material gas supplied to the first reaction tower by using the product gas sent from the first reaction tower and the unreacted raw material gas; and The second gas preheating unit preheats the product gas supplied to the second reaction tower and the unreacted raw material gas by the product gas sent from the second reaction tower. The power generation system as described in claim 5 or 6 further includes: A first gas preheating unit that uses the heat medium that has passed through the first reaction tower to preheat the raw material gas supplied to the first reaction tower; and The second gas preheating unit preheats the product gas and the unreacted raw material gas supplied to the second reaction tower by using the heat medium that has passed through the second reaction tower.