Generating apparatus and generating method

Abstract

To provide technology that shortens the time needed to heat a catalyst in a reaction tower.SOLUTION: A generation device is equipped with a reaction tower that generates a product gas by an exothermic reaction of a raw material gas in a catalyst and a raw material gas supply unit that heats the raw material gas for supply to the reaction tower. The reaction tower has: a reactor, packed with a catalyst, into which the raw material gas flows; a jacket portion, through which a heating medium flows, that covers a part of the outer circumference of the reactor; and a heat insulating member that covers another part of the outer circumference of the reactor.SELECTED DRAWING: Figure 1

Description

Technical Field

[0001] The present invention relates to a generation device and a generation method.

Background Art

[0002] For example, Patent Document 1 discloses a technique related to a generation device and a generation method for generating a product gas by an exothermic reaction of reactants in a gaseous state. For example, Patent Document 2 discloses a technique related to a system for preheating a raw material gas supplied to a methanation reactor.

Prior Art Documents

Patent Documents

[0003]

Patent Document 1

Patent Document 2

Summary of the Invention

Problems to be Solved by the Invention

[0004] A reaction tower used for generating a product gas is filled with a catalyst. By heating a heat medium with a heater and circulating it in the reaction tower, the temperature of the catalyst in the reaction tower is raised to the temperature required for starting the generation of the product gas. To raise the temperature of the entire catalyst in the reaction tower with the heat medium, a large-scale heater is required, and it takes time to heat the heat medium.

[0005] The present invention has been made in view of the above circumstances, and an object thereof is to provide a technique capable of shortening the time required for heating the catalyst in the reaction tower.

Means for Solving the Problems

[0006] The present invention, which solves the above problems, is a production apparatus comprising a reaction tower that generates a product gas by an exothermic reaction of a raw material gas in a catalyst, and a raw material gas supply unit that heats the raw material gas and supplies it to the reaction tower, wherein the reaction tower has a reaction vessel into which the catalyst is filled and the raw material gas flows, a jacket portion that covers a part of the outer circumference of the reaction vessel and through which a heat transfer medium flows, and an insulating member that covers another part of the outer circumference of the reaction vessel.

[0007] According to the above-described generation apparatus, the raw material gas is heated, and the catalyst in the reaction tower is heated by the heated raw material gas. As a result, the time it takes for the catalyst temperature to reach the reaction start temperature is shortened due to direct contact between the heated raw material gas and the catalyst. Therefore, the time required to heat the catalyst in the reaction tower can be reduced. In addition, the outer perimeter of the reaction vessel filled with catalyst is insulated by covering a portion of the outer perimeter with an insulating material. This shortens the time it takes for the catalyst temperature in the reaction tower to reach the reaction start temperature when heated raw material gas is supplied to the reaction tower, thereby reducing the time required to heat the catalyst in the reaction tower.

[0008] The insulating member may cover the outer perimeter of the reaction vessel from the part in which the raw material gas flows in toward the central part to a predetermined portion. This insulates the outer perimeter of the reaction vessel near the part in which the raw material gas flows in. If a heat spot occurs near the part in which the raw material gas flows in the reaction vessel, insulating the heat spot makes it possible to efficiently raise the temperature of the catalyst in the reaction tower.

[0009] The above-described generating apparatus includes a delivery pump that sends the heat transfer medium to the reaction tower, and after the supply of the raw material gas to the reaction tower is started, the delivery pump is activated to send the heat transfer medium to the reaction tower. A heat transfer medium may be supplied. This makes it possible to supply the heat transfer medium to the reaction tower after the supply of raw material gas to the reaction tower has started. For example, even if an insufficiently heated heat transfer medium flows into the jacket portion of the reaction tower, the temperature of the catalyst is maintained by the portion of the reaction vessel covered by the insulating material, thus maintaining the exothermic reaction in the reaction tower.

[0010] The raw material gas supply unit may determine the supply flow rate of the raw material gas to the reaction tower based on the temperature inside the reaction tower. This allows the raw material gas to be supplied to the reaction tower at an appropriate flow rate.

[0011] The raw material gas supply unit may gradually increase the flow rate of the raw material gas supplied to the reaction tower when the temperature of the catalyst in the portion of the reaction vessel covered by the insulating member is above a predetermined temperature. This promotes the exothermic reaction of the raw material gas and increases the amount of product gas produced.

[0012] The above-described generating apparatus includes a combustion section for burning the unreacted raw material gas sent from the reaction tower, and at least one of the raw material gas supplied to the reaction tower and the heat transfer medium flowing into the jacket portion may be heated by the heat of combustion of the unreacted raw material gas. This makes it possible to heat at least one of the raw material gas supplied to the reaction tower and the heat transfer medium flowing into the jacket portion using the heat of combustion of the unreacted raw material gas, thereby making effective use of the unreacted raw material gas.

[0013] The above-described generation apparatus comprises a second reaction tower that generates the product gas by the exothermic reaction of the raw material gas in the catalyst, and a circulation pump provided in the circulation path through which the heat transfer medium flows. At least one of the product gas and the unreacted raw material gas sent from the reaction tower is supplied into the second reaction tower, and when the temperature inside the reaction tower is above a predetermined temperature, the circulation pump is activated to circulate the heat transfer medium between the reaction tower and the second reaction tower. The volume inside the reaction tower may be smaller than the volume inside the second reaction tower. Because the volume inside the reaction tower is smaller than the volume inside the second reaction tower, the time required to heat the catalyst inside the reaction tower can be shortened. By circulating the heat transfer medium between the reaction tower and the second reaction tower, the heat transfer medium heated by the exothermic reaction of the catalyst inside the reaction tower can be sent to the second reaction tower.

[0014] The above-described generating apparatus includes a switching unit that switches the supply destination of the raw material gas from the raw material gas supply unit between the reaction tower and the second reaction tower, and the switching unit may switch the supply destination of the raw material gas from the raw material gas supply unit from the reaction tower to the second reaction tower. As a result, the raw material gas is supplied to the second reaction tower, and the product gas is generated in the second reaction tower.

[0015] Furthermore, the present invention may also be a production apparatus comprising: a reaction tower that generates product gas by an exothermic reaction of a raw material gas in a first catalyst; a boost reaction tower that generates product gas by an exothermic reaction of the raw material gas in a second catalyst; a raw material gas supply unit that heats the raw material gas and supplies it to the boost reaction tower; and a circulation pump provided in a circulation path through which a heat transfer medium flows. The boost reaction tower has a reaction vessel filled with the second catalyst and into which the raw material gas flows; a jacket portion that covers a part of the outer circumference of the reaction vessel and through which the heat transfer medium flows; and a heat insulating member that covers another part of the outer circumference of the reaction vessel. At least one of the product gas and unreacted raw material gas sent from the boost reaction tower is supplied into the reaction tower, and when the temperature inside the boost reaction tower is above a predetermined temperature, the circulation pump is activated to circulate the heat transfer medium between the reaction tower and the boost reaction tower. The capacity inside the boost reaction tower is smaller than the capacity inside the reaction tower.

[0016] According to the above-described generation apparatus, the raw material gas is heated, and the second catalyst in the boost reaction tower is heated by the heated raw material gas, thus shortening the time it takes for the temperature of the second catalyst to reach the reaction start temperature. Therefore, the time required to heat the second catalyst in the boost reaction tower can be shortened. In addition, the outer perimeter of the reaction vessel is insulated by the insulating material covering a part of the outer perimeter of the reaction vessel. As a result, when heated raw material gas is supplied to the boost reaction tower, the time it takes for the temperature of the second catalyst in the boost reaction tower to reach the reaction start temperature is shortened, and the time required to heat the second catalyst in the boost reaction tower can be shortened. Since the volume of the boost reaction tower is smaller than the volume of the second reaction tower, the time required to heat the second catalyst in the boost reaction tower can be shortened.

[0017] Furthermore, the present invention can also be viewed from the perspective of a method. That is, the present invention is a method for producing a product gas in a production apparatus equipped with a reaction tower that produces a product gas by an exothermic reaction of a raw material gas in a catalyst, the method comprising the step of heating the raw material gas and supplying it to the reaction tower, wherein the reaction tower comprises a reaction vessel into which the catalyst is filled and into which the raw material gas flows, a jacket portion that covers a part of the outer circumference of the reaction vessel and through which a heat transfer medium flows, and an insulating member that covers another part of the outer circumference of the reaction vessel.

[0018] According to the above production method, the raw material gas is heated, and the catalyst in the reaction tower is heated by the heated raw material gas, thus shortening the time it takes for the catalyst temperature to reach the reaction start temperature. Therefore, the time required to heat the catalyst in the reaction tower can be shortened. In addition, the outer perimeter of the reaction tank is insulated by the insulating material covering a portion of the outer perimeter of the reaction tank. As a result, when heated raw material gas is supplied to the reaction tower, the time it takes for the catalyst temperature in the reaction tower to reach the reaction start temperature is shortened, and the time required to heat the catalyst in the reaction tower can be shortened.

[0019] Furthermore, the present invention relates to a method for producing a product gas in a production apparatus comprising: a reaction tower that produces a product gas by an exothermic reaction of a raw material gas in a first catalyst; a boost reaction tower that produces the product gas by an exothermic reaction of the raw material gas in a second catalyst; and a circulation pump provided in a circulation path through which a heat transfer medium flows, the method comprising: heating the raw material gas and supplying it to the boost reaction tower; supplying at least one of the product gas and unreacted raw material gas sent from the boost reaction tower into the reaction tower; and, if the temperature inside the boost reaction tower is above a predetermined temperature, activating the circulation pump to circulate the heat transfer medium between the reaction tower and the boost reaction tower, wherein the boost reaction tower comprises a reaction vessel filled with the second catalyst and through which the raw material gas flows; a jacket portion covering a part of the outer circumference of the reaction vessel and through which the heat transfer medium flows; and an insulating member covering another part of the outer circumference of the reaction vessel, and the volume inside the boost reaction tower is smaller than the volume inside the reaction tower.

[0020] According to the above production method, the raw material gas is heated, and the second catalyst in the boost reaction tower is heated by the heated raw material gas, thus shortening the time it takes for the temperature of the second catalyst to reach the reaction start temperature. Therefore, the time required to heat the second catalyst in the boost reaction tower can be shortened. In addition, the outer perimeter of the reaction vessel is insulated by the insulating material covering a part of the outer perimeter of the reaction vessel. As a result, when heated raw material gas is supplied to the boost reaction tower, the time it takes for the temperature of the second catalyst in the boost reaction tower to reach the reaction start temperature is shortened, and the time required to heat the second catalyst in the boost reaction tower can be shortened. Since the volume of the boost reaction tower is smaller than the volume of the second reaction tower, the time required to heat the second catalyst in the boost reaction tower can be shortened. [Effects of the Invention]

[0021] This technology can provide a way to shorten the time required to heat the catalyst inside the reaction tower. [Brief explanation of the drawing]

[0022] [Figure 1] Figure 1 is a configuration diagram of the generation device according to the first embodiment. [Figure 2] Figures 2(A) and 2(B) are diagrams showing an example of the configuration of the reaction tower. [Figure 3] Figure 3 is a flowchart showing the flow of the operation procedure of the generation device according to the first embodiment. [Figure 4] Figure 4 is a diagram showing an example of the temperature distribution in the reaction tower after the start of operation. [Figure 5] Figure 14 is a configuration diagram of the generation device according to the second embodiment. [Figure 6] Figure 6(A) is a diagram showing an example of the configuration of the boosting reaction tower. Figure 6(B) is a diagram showing an example of the configuration of the reaction tower. [Figure 7] Figure 7 is a configuration diagram of the generation device according to the second embodiment. [Figure 8] Figure 8 is a flowchart showing the flow of the operation procedure of the generation device according to the second embodiment.

Mode for Carrying Out the Invention

[0023] Hereinafter, embodiments of the present invention will be described. The embodiments shown below are examples of the embodiments of the present invention, and do not limit the technical scope of the present invention to the following aspects.

[0024] [[ID=ID=35]]〈First Embodiment〉 Figure 1 is a configuration diagram of the generation device according to the first embodiment. The generation device

[0025] 4H2 + CO2 ⇔ CH4 + 2H2O (1) The production apparatus 100 comprises a first-stage reaction tower (reactor) 1, a first-stage gas cooling heat exchanger 2, a second-stage reaction tower (reactor) 3, a second-stage gas cooling heat exchanger 4, a heat exchanger for the heat transfer medium 5, gas-liquid separators 6 and 7, and a raw material gas supply unit 8.

[0026] The reaction tower 1 produces product gas through an exothermic reaction of raw material gas in a catalyst. The raw material gas includes, for example, hydrogen (H2) and carbon dioxide (CO2). The product gas is, for example, methane gas. The reaction tower 1 and the raw material gas supply unit 8 are connected by piping, and the raw material gas is supplied from the raw material gas supply unit 8 into the reaction tower 1. The reaction tower 1 also produces product water through an exothermic reaction of raw material gas in a catalyst. The reaction tower 1 is connected to a gas cooling heat exchanger 2. Piping and valves are provided in the path connecting the reaction tower 1 and the gas cooling heat exchanger 2.

[0027] The gas cooling heat exchanger 2 condenses the water (steam) produced in the reaction tower 1. The gas cooling heat exchanger 2 is connected to the gas-liquid separator 6. Piping and valves are provided in the path connecting the gas cooling heat exchanger 2 and the gas-liquid separator 6. The gas-liquid separator 6 separates the water (liquid) from the product gas and unreacted raw material gas.

[0028] The reaction tower 3 and the gas-liquid separator 6 are connected. Piping and valves are provided in the path connecting the reaction tower 3 and the gas-liquid separator 6. 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 6. The reaction tower 3 produces product gas and generated water through the exothermic reaction of the raw material gas in the catalyst. By generating product gas from the unreacted raw material gas in the reaction tower 3, the production device 100 is able to produce high-concentration product gas.

[0029] The reaction tower 3 and the gas cooling heat exchanger 4 are connected. Piping and valves are provided in the path connecting the reaction tower 3 and the gas cooling heat exchanger 4. The gas cooling heat exchanger 4 condenses the water (steam) produced in the reaction tower 3. It is connected to a liquid separator 7. Piping and valves are provided in the path connecting the gas cooling heat exchanger 4 and the gas-liquid separator 7. The gas-liquid separator 7 separates the generated water (liquid) from the product gas and unreacted raw material gas.

[0030] The generating apparatus 100 includes a storage tank 9. Product gas is sent from the gas-liquid separator 7 to the storage tank 9. The storage tank 9 stores the product gas. The gas-liquid separators 6 and 7 are equipped with drain valves 10 for discharging the generated water. The drain valves 10 may be opened and closed using the buoyancy of a floating device such as a drain trap, or they may be opened and closed by electrically detecting the water level and using a solenoid valve.

[0031] Reaction towers 1 and 3 are pre-packed with catalysts. The catalyst can be any catalyst that promotes reaction equation (1), for example, a catalyst comprising a stabilized zirconia support having a tetragonal and / or cubic crystal structure in which a stabilizing element is solid-dissolved, and Ni supported on the stabilized zirconia support, wherein the stabilizing element is at least one transition element selected from the group consisting of Mn, Fe, and Co.

[0032] Furthermore, reaction towers 1 and 3 have a jacket structure, and the jacket portion (shell) allows for the inflow and outflow of a heat transfer medium that exchanges heat with the heat-generating parts inside the reaction tower where exothermic reactions occur. When the heat transfer medium flows into the jacket portion of reaction towers 1 and 3, the heat transfer medium circulates within reaction towers 1 and 3. For example, heat transfer oil is used as the heat transfer medium. The jacket portion of reaction tower 1 and the jacket portion of reaction tower 3 are connected by piping through which the heat transfer medium flows. Valves and other devices are provided in the piping through which the heat transfer medium flows.

[0033] The jacket portion of reaction tower 1 and the heat exchanger 5 for the heat transfer medium are connected by piping through which the heat transfer medium flows. The jacket portion of reaction tower 3 and the heat exchanger 5 for the heat transfer medium are connected by piping through which the heat transfer medium flows. The heat exchanger 5 for the heat transfer medium cools the heat transfer medium that has passed through reaction towers 1 and 3. A delivery pump 11 is provided in the piping connecting the jacket portion of reaction tower 1 and the heat exchanger 5 for the heat transfer medium to reaction tower 1. Control valves 12 and 13 are also provided in the piping through which the heat transfer medium flows. By opening and closing control valves 12 and 13, the heat transfer medium that has passed through reaction towers 1 and 3 can be sent to reaction tower 1 via the heat exchanger 5 for the heat transfer medium, or sent to reaction tower 1 without passing through the heat exchanger 5 for the heat transfer medium.

[0034] The generating apparatus 100 includes a chiller 14. The chiller 14 cools the cooling water (refrigerant) used to condense the generated water in the gas cooling heat exchangers 2 and 4. The gas cooling heat exchangers 2 and 4 and the chiller 14 are interconnected by piping through which the cooling water flows. The cooling water cooled by the chiller 14 returns to the chiller 14 via the gas cooling heat exchangers 2 and 4.

[0035] The generating apparatus 100 includes a cooling tower 15 and a cooling water circulation pump 16. The cooling tower 15 cools the cooling water that exchanges heat with the heat transfer medium in the heat transfer medium heat exchanger 5. For example, tap water supplied to the cooling tower 15 from outside the system may be used as the cooling water. The cooling water circulation pump 16 circulates the cooling water supplied into the cooling tower 15 between the heat transfer medium heat exchanger 5 and the cooling tower 15.

[0036] The generation apparatus 100 includes a control unit 17, a measuring sensor 18 for measuring the temperature inside the reaction tower 1, and a measuring sensor 19 for measuring the temperature inside the reaction tower 3. The measurement data measured by the measuring sensor 18 and the measurement data measured by the measuring sensor 19 are sent to the raw material gas supply unit 8 and the control unit 17. As a result, the raw material gas supply unit 8 and the control unit 17 acquire the temperature inside the reaction tower 1 and the temperature inside the reaction tower 3.

[0037] The control unit 17 is a controller that controls the overall operation of the generation device 100. The control unit 17 may be configured using dedicated equipment or a general-purpose computer. The control unit 17 is equipped with hardware resources such as a processor (CPU), memory, storage, and a communication interface. The memory may be RAM. The storage may be a non-volatile storage device (e.g., ROM, flash memory). The functions of the control unit 17 are realized by loading programs stored in storage into memory and executing them with the processor. However, the configuration of the control unit 17 is not limited to these. For example, all or part of the functions may be configured with circuits such as ASICs or FPGAs, or all or part of the functions may be executed on a cloud server or other device.

[0038] The control unit 17 controls the control valves 12 and 13. When control valve 12 is opened and control valve 13 is closed, the heat transfer medium is sent to the reaction tower 1 via the heat transfer medium heat exchanger 5, thereby cooling the heat transfer medium. Consequently, the cooled heat transfer medium is sent to the reaction tower 1. When control valve 12 is closed and control valve 13 is opened, the heat transfer medium is sent to the reaction tower 1 without passing through the heat transfer medium heat exchanger 5, thereby stopping the cooling of the heat transfer medium.

[0039] The raw material gas supply unit 8 heats the raw material gas and supplies it to the reaction tower 1. The control unit 17 controls the raw material gas supply unit 8. By controlling the operation of the raw material gas supply unit 8, the raw material gas supply unit 8 starts supplying the raw material gas to the reaction tower 1. The raw material gas supply unit 8 may also operate independently of the control unit 17.

[0040] The raw material gas supply unit 8 includes a gas storage unit 21, a gas heating unit 22, and a gas mixer 23. The gas storage unit 21 stores the raw material gas. The gas heating unit 22 heats the raw material gas supplied from the raw material gas supply unit 8 to the reaction tower 1. The gas heating unit 22 is, for example, a heater, a heat pump, an adiabatic compressor, etc., but is not limited to these. The gas heating unit 22 may heat the raw material gas stored in the gas storage unit 21, or it may heat the raw material gas that enters the raw material gas supply unit 8 from the outside. The gas heating unit 22 may also heat the hydrogen contained in the raw material gas. By controlling the operation of the gas heating unit 22, the gas heating unit 22 heats the raw material gas or stops heating the raw material gas. In this way, heating and stopping of heating of the raw material gas is performed using the gas heating unit 22. The gas mixer 23 uniformly mixes the raw material gas supplied to the reaction tower 1.

[0041] The generating apparatus 100 includes control valves 24 and 25, and economizers 26 and 27. The control valves 24 and 25 and the economizer 26 are provided in the supply path of the raw material gas supplied from the raw material gas supply unit 8 to the reaction tower 1. The control unit 17 controls the control valves 24 and 25. When control valve 24 is closed and control valve 25 is opened, the raw material gas is supplied to the reaction tower 1 via the economizer 26. When control valve 24 is opened and control valve 25 is closed, the raw material gas is supplied to the reaction tower 1 without passing through the economizer 26.

[0042] In the economizer 26, heat exchange takes place between the raw material gas supplied to the reaction tower 1 and the discharge gas discharged from the reaction tower 1. The discharge gas is either the product gas, unreacted raw material gas, or a mixture of the product gas and unreacted raw material gas. Therefore, the discharge gas contains at least one of the product gas and the unreacted raw material gas. At the time when the supply of raw material gas to the reaction tower 1 is started, no discharge gas is being discharged from the reaction tower 1. Therefore, immediately after the start of the supply of raw material gas to the reaction tower 1, the raw material gas may be supplied to the reaction tower 1 without passing it through the economizer 26, and then, when the discharge gas begins to be discharged from the reaction tower 1 or after a certain period of time has elapsed since the discharge gas was discharged from the reaction tower 1, the raw material gas may be supplied to the reaction tower 1 after passing it through the economizer 26. An economizer 27 is provided between the reaction tower 3 and the gas-liquid separator 6. In the economizer 27, heat exchange takes place between the discharge gas sent to the reaction tower 3 and the discharge gas discharged from the reaction tower 3.

[0043] Figure 2(A) shows an example of the configuration of reaction tower 1. Figure 2(A) shows a cross section of reaction tower 1. A view is shown. The reaction tower 1 comprises a reaction vessel 31 filled with catalyst, a jacket portion 32 provided to surround the lower part of the reaction vessel 31, and an insulating member 33 provided to surround the upper part of the reaction vessel 31. The reaction vessel 31 has a structure in which a plurality of reaction tubes filled with catalyst are erected. A plurality of reaction tubes extend from one end of the reaction vessel 31 toward the other end of the reaction vessel 31. Heated raw material gas flows into the reaction vessel 31 from the inlet end of the reaction vessel 31, and discharge gas flows out from the outlet end of the reaction vessel 31. When the discharge pump 11 is stopped and the heat transfer medium is not circulating between the reaction tower 1 and the reaction tower 3, the heat transfer medium remains in the jacket portion 32. When the discharge pump 11 is started and the heat transfer medium is circulating between the reaction tower 1 and the reaction tower 3, the heat transfer medium flows within the jacket portion 32.

[0044] The material of the heat insulating member 33 is not particularly limited as long as it is a material that has a heat insulating effect. Alternatively, a mantle heater may be used as the heat insulating member 33. The mantle heater has a heat insulating effect and also heats the catalyst in the reaction vessel 31. The heat insulating member 33 is provided so as to surround the upper part of the reaction vessel 31. For example, the heat insulating member 33 covers a portion of the outer circumference of the reaction vessel 31 near the inlet end. Therefore, the heat insulating member 33 covers the outer circumference of the reaction vessel 31 from the part where the raw material gas flows in (inlet end) toward the central part to a predetermined portion. Not limited to the above example, the heat insulating member 33 may cover at least a portion near the heat spot of the reaction vessel 31. Also, the heat insulating member 33 may cover at least a portion upstream of the heat spot of the reaction vessel 31. A jacket portion 32 is provided in the area of ​​the outer circumference of the reaction vessel 31 that is not covered by the heat insulating member 33. In this way, the jacket portion 32 covers a portion of the outer circumference of the reaction vessel 31, and the heat insulating member 33 covers the other portion of the outer circumference of the reaction vessel 31. Heat exchange occurs between the heat-generating part of the reaction vessel 31 and the heat transfer medium in the jacket portion 32. That is, the reaction heat generated in the reaction vessel 31 is transferred to the heat transfer medium in the jacket portion 32, and the heat transfer medium is heated.

[0045] Figure 2(B) shows an example of the configuration of the reaction tower 3. Figure 2(B) shows a cross-section of the reaction tower 3. The reaction tower 3 comprises a reaction vessel 34 filled with catalyst and a jacket portion 35 provided to surround the reaction vessel 34. The reaction vessel 34 has a structure in which multiple reaction tubes filled with catalyst are erected. Multiple reaction tubes extend from one end of the reaction vessel 34 toward the other end of the reaction vessel 34. The discharge gas flows into the reaction vessel 34 from the inlet end and flows out from the outlet end of the reaction vessel 34.

[0046] When the discharge pump 11 is stopped and the heat transfer medium is not circulating between reaction tower 1 and reaction tower 3, the heat transfer medium remains stagnant within the jacket portion 35. When the discharge pump 11 is started and the heat transfer medium is circulating between reaction tower 1 and reaction tower 3, the heat transfer medium flows within the jacket portion 35. Heat exchange takes place between the heat-generating portion of reaction vessel 34 and the heat transfer medium within the jacket portion 35. That is, the reaction heat generated in reaction vessel 34 is transferred to the heat transfer medium within the jacket portion 35, and the heat transfer medium is heated.

[0047] The measuring sensor 18 may measure at least one of the temperature of the discharged gas sent from the reaction tower 1 and the temperature of the heat transfer medium in the jacket portion 32 as the temperature inside the reaction tower 1. The measuring sensor 19 may measure at least one of the temperature of the discharged gas sent from the reaction tower 3 and the temperature of the heat transfer medium in the jacket portion 35 as the temperature inside the reaction tower 3.

[0048] <Driving Procedure> The operating procedure of the generation apparatus 100 according to the first embodiment will now be described. Figure 3 is a flowchart showing the flow of the operating procedure of the generation apparatus 100 according to the first embodiment. First, in step S101, the raw material gas supply unit 8 is started up and begins supplying raw material gas to the reaction tower 1. Next, in step S102, the raw material gas supply unit 8 heats the raw material gas and supplies it to the reaction tower 1. As the heated raw material gas is supplied to the reaction tower 1, the reaction tank 31 Heated raw material gas flows in from the inlet end. The heated raw material gas flows into the reaction vessel 31, and the temperature of the catalyst in the part of the reaction vessel 31 covered by the insulating member 33 (insulated part) rises due to the heated raw material gas. When the temperature of the catalyst reaches the reaction start temperature, product gas and generated water are produced by the exothermic reaction of the raw material gas that has flowed into the reaction vessel 31. In addition, the heat transfer medium in the reaction tower 1 is heated by the heated raw material gas.

[0049] From the start of raw material gas supply until the catalyst temperature reaches the reaction start temperature, it is preferable to reduce the raw material gas supply flow rate so that the catalyst facilitates the exothermic reaction of the raw material gas. Therefore, the raw material gas supply flow rate (first supply flow rate) from the start of raw material gas supply until the catalyst temperature reaches the reaction start temperature is less than the rated supply flow rate (second supply flow rate) of the raw material gas when producing the product gas. The raw material gas supply unit 8 or control unit 17 may determine the raw material gas supply flow rate to the reaction tower 1 based on the temperature inside the reaction tower 1. Alternatively, the raw material gas supply unit 8 or control unit 17 may determine the raw material gas supply flow rate to the reaction tower 1 based on the temperature of the catalyst in the portion of the reaction vessel 31 covered by the heat insulating member 33. The first supply flow rate may be a flow rate that significantly promotes the exothermic reaction of the raw material gas by the catalyst in the portion of the reaction vessel 31 covered by the heat insulating member 33. In this way, by determining the raw material gas supply flow rate to the reaction tower 1 based on the temperature inside the reaction tower 1, the raw material gas can be supplied to the reaction tower 1 at an appropriate flow rate.

[0050] In S103, the raw material gas supply unit 8 gradually increases the supply flow rate of the raw material gas and stops heating the raw material gas if the temperature of the catalyst in the portion of the reaction vessel 31 covered by the heat insulating member 33 is above a predetermined temperature (T1). The raw material gas supply unit 8 may stop heating the raw material gas after controlling the supply flow rate of the raw material gas to gradually increase. Alternatively, the raw material gas supply unit 8 may gradually increase the supply flow rate of the raw material gas after stopping the heating of the raw material gas. The predetermined temperature (T1) is, for example, 180°C, but is not limited to this temperature and may be determined based on experimental results, simulation results, etc.

[0051] When the temperature of the catalyst in the portion of the reaction vessel 31 covered by the insulating member 33 reaches a predetermined temperature (T1), the exothermic reaction of the raw material gas becomes more likely to occur, and an independent exothermic reaction begins in the reaction tower 1. Therefore, after the temperature of the catalyst in the portion of the reaction vessel 31 covered by the insulating member 33 reaches the predetermined temperature (T1), gradually increasing the supply flow rate of the raw material gas promotes the exothermic reaction of the raw material gas and increases the amount of product gas produced. Also, if heated raw material gas is supplied to the reaction tower 1 when the temperature of the catalyst in the portion of the reaction vessel 31 covered by the insulating member 33 is above the predetermined temperature (T1), the catalyst in the reaction vessel 31 may rise to an excessive temperature. By stopping the heating of the raw material gas, the catalyst in the reaction vessel 31 is prevented from rising to an excessive temperature. Even if the heating of the raw material gas is stopped, the temperature of the catalyst in the portion of the reaction vessel 31 covered by the insulating member 33 remains at the predetermined temperature (T1), so the exothermic reaction in the reaction tower 1 continues. After the heating of the raw material gas is stopped, the heat transfer medium is heated only by the exothermic reaction in the reaction tower 1.

[0052] In step S104, the raw material gas supply unit 8 increases the raw material gas supply flow rate until it reaches the second supply flow rate (rated supply flow rate), and maintains the raw material gas supply flow rate at a constant level. By maintaining the raw material gas supply flow rate at the rated supply flow rate, the product gas is stably delivered from the reaction tower 1.

[0053] The control unit 17 activates the delivery pump 11 at a predetermined timing between steps S101 to S104 of the flowchart in Figure 3 to circulate the heat transfer medium between reaction tower 1 and reaction tower 3. The heat transfer medium passes through reaction tower 1 by flowing through the jacket portion 32 of reaction tower 1. The heat transfer medium that has passed through reaction tower 1 is sent to the jacket portion 35 of reaction tower 3 and passes through reaction tower 3. The heat transfer medium passing through reaction tower 3 is heated by reaction tower 1. The heated heat transfer medium passes through reaction tower 3. As a result, the temperature inside reaction tower 3 rises. For example, even if a heat transfer medium that has not been sufficiently heated flows into the jacket portion 32 of reaction tower 1, the temperature of the catalyst is maintained by the portion covered by the insulating material 33 in the reaction vessel 31, thus maintaining the exothermic reaction inside reaction tower 1.

[0054] The control unit 17 may compare the temperature of the discharged gas sent from the reaction tower 1 and at least one of the temperature of the heat transfer medium in the jacket portion 32 with a threshold temperature, and determine the timing to start the discharge pump 11 based on the comparison result.

[0055] The generating apparatus 100 comprises a combustion section 28 and control valves 29 and 30. The combustion section 28 burns the unreacted raw material gas sent from the reaction tower 1. At least one of the raw material gas supplied to the reaction tower 1 and the heat transfer medium flowing into the jacket section 32 is heated by the combustion heat of the unreacted raw material gas. It is possible to heat at least one of the raw material gas supplied to the reaction tower 1 and the heat transfer medium flowing into the jacket section 32 by utilizing the combustion heat of the unreacted raw material gas, thereby effectively utilizing the unreacted raw material gas. The control unit 17 controls the control valves 29 and 30. When control valve 29 is opened and control valve 30 is closed, the unreacted raw material gas sent from the reaction tower 1 flows into the combustion section 28. When control valve 29 is closed and control valve 30 is opened, the discharged gas sent from the reaction tower 1 flows into the gas cooling heat exchanger 2.

[0056] From the start of supplying the raw material gas to the reaction tower 1 until a predetermined timing, the temperature of the catalyst in the reaction tower 1 has not reached the reaction start temperature, and unreacted raw material gas is discharged from the reaction tower 1. Therefore, from the start of supplying the raw material gas to the reaction tower 1 until a predetermined timing, the unreacted raw material gas discharged from the reaction tower 1 may be allowed to flow into the combustion section 28. The generating apparatus 100 may also be equipped with a heat transfer medium tank for storing the heat transfer medium.

[0057] In the production apparatus 100 according to the first embodiment, the raw material gas is heated, and the catalyst in the reaction tower 1 is heated using the heated raw material gas. Since the specific heat of the raw material gas is small, heating the raw material gas is easier compared to heating the heat transfer medium. In the production apparatus 100 according to the first embodiment, the heat insulating member 33 covers a predetermined portion of the outer circumference of the reaction tank 31, thereby insulating the outer circumference near the inlet end of the reaction tank 31. As a result, when heated raw material gas is supplied to the reaction tower 1, the time it takes for the temperature of the catalyst in the reaction tower 1 to reach the reaction start temperature is shortened, and the time required to heat the catalyst in the reaction tower 1 can be reduced. For example, when using heat transfer oil as the heat transfer medium, low-temperature heat transfer oil has high viscosity and poor fluidity, so it takes time to circulate within the reaction tower. For this reason, when the heat transfer medium is heated by a heater and the heated heat transfer medium is passed through the reaction tower to heat the catalyst, the time it takes for the temperature of the catalyst to reach the reaction start temperature is long.

[0058] According to the first embodiment of the production apparatus 100, the raw material gas is heated, and the catalyst in the reaction tower 1 is heated by the heated raw material gas, thus shortening the time it takes for the catalyst temperature to reach the reaction start temperature. Therefore, the time required to heat the catalyst in the reaction tower 1 can be shortened, and the time from the start of supplying the raw material gas to the reaction tower 1 to the production of the product gas by the reaction tower 1 can be shortened. Thus, according to the first embodiment of the production apparatus 100, it is possible to heat the catalyst in the reaction tower 1 without using a heater to heat the heat transfer medium, and the time until the operation of the reaction tower 1 can be started can be shortened. Furthermore, according to the first embodiment of the production apparatus 100, it is possible to heat the catalyst in the reaction tower 3 without using a heater to heat the heat transfer medium, and the time until the operation of the reaction tower 3 can be started can be shortened.

[0059] Figure 4 shows an example of the temperature distribution inside a reaction tower after the start of operation. In the reaction tower according to the reference example shown in Figure 4, the jacket covers the entire outer circumference of the reaction vessel filled with catalyst, and no insulating material is provided. The vertical axis of Figure 4 represents the temperature (°C) inside the reaction tower according to the reference example, and the horizontal axis of Figure 4 represents the distance from the end (inlet end) where the raw material gas is supplied in the reaction vessel according to the reference example. (cm) is represented. As shown in Figure 4, a heat spot is generated near the inlet end of the reaction vessel in the reference example, and a peak temperature is present near the inlet end of the reaction vessel in the reference example.

[0060] As shown in Figure 4, the temperature near the inlet end of the reactor in the reference example decreases towards the outlet end of the reactor. This is because the raw material gas has largely reacted near the inlet end of the reactor in the reference example, and the amount of raw material gas reacting with the catalyst decreases towards the outlet end of the reactor. Since a heat spot occurs near the inlet end of the reactor 31, it is preferable that the insulating member 33 covers the outer circumference of the reactor 31 from the inlet end toward the central part to a predetermined portion. This makes it possible to efficiently raise the temperature of the catalyst in the reaction tower 1 and to efficiently transfer the heat generated by the exothermic reaction in the reaction tower 1 to the heat transfer medium. Alternatively, in the reaction tower 1, the outer circumference of the area from the inlet end of the reactor 31 to the part where the heat spot occurs may be covered with the insulating member 33. Alternatively, in the reaction tower 1, at least a portion of the outer circumference of the part where the heat spot occurs in the reactor 31 may be covered with the insulating member 33. Alternatively, in the reaction tower 1, at least a portion of the outer circumference of the area near the part where the heat spot occurs in the reactor 31 may be covered with the insulating member 33. In the reaction tower 1, the outer circumference of at least a portion of the upstream side of the area where a heat spot occurs in the reaction vessel 31 may be covered with an insulating member 33. By having the jacket portion 32 cover a portion of the outer circumference of the reaction vessel 31 and the insulating member 33 cover the other portion of the outer circumference of the reaction vessel 31, it is possible to shorten the startup time of the reaction tower 1 and to continue the exothermic reaction in the reaction tower 1 while suppressing the temperature inside the reaction tower 1 from becoming excessively high. The startup time of the reaction tower 1 is the time from when the supply of raw material gas to the reaction tower 1 is started until the product gas is produced by the reaction tower 1.

[0061] For example, if the entire outer perimeter of the reaction vessel 31 is covered by the insulating material 33, or if the outer perimeter of the reaction vessel 31 is covered by the insulating material 33 more than necessary, there is a concern that the catalyst and reaction tubes may be damaged by the extreme temperature rise downstream of the heat spot generated in the reaction vessel 31. By covering the outer perimeter of the reaction vessel 31 with the insulating material 33 from the inlet end to the area where the heat spot is generated, the extreme temperature rise downstream of the heat spot generated in the reaction vessel 31 can be suppressed. If a heat spot is generated near the inlet end of the reaction vessel 31, the catalyst near the inlet end of the reaction vessel 31 may be damaged more than the catalyst in other areas. If a heat spot is generated near the inlet end of the reaction vessel 31, the frequency of replacing the catalyst near the inlet end of the reaction vessel 31 may be increased. Also, by replacing only the catalyst near the inlet end of the reaction vessel 31, the catalyst replacement cost can be reduced compared to replacing the entire catalyst in the reaction vessel 31.

[0062] <Second Embodiment> A second embodiment will now be described. In the second embodiment, components identical to those in the first embodiment are denoted by the same reference numerals as in the first embodiment, and their descriptions are omitted as appropriate. The generating apparatus 100 according to the first and second embodiments may be combined as appropriate.

[0063] Figure 5 is a configuration diagram of the generation apparatus 100 according to the second embodiment. Figure 5 shows a part of the generation apparatus 100. Compared with the generation apparatus 100 according to the first embodiment, the generation apparatus 100 according to the second embodiment is equipped with a reaction tower 1A instead of reaction tower 1. Furthermore, compared with the generation apparatus 100 according to the first embodiment, the generation apparatus 100 according to the second embodiment is further equipped with a boost reaction tower 41, a switching unit 42, a gas cooling heat exchanger 43, a gas-liquid separator 44, a measuring sensor 45, and a circulation pump 46.

[0064] The boost reaction tower 41 generates product gas through the exothermic reaction of the raw material gas in the catalyst. The raw material gas supply unit 8 and the boost reaction tower 41 are connected by piping, and the raw material gas supply A switching unit 42 is provided in the middle of the piping connecting unit 8 and the boost reaction tower 41. The switching unit 42 is, for example, a three-way valve. The switching unit 42 switches the destination of the raw material gas supplied by the raw material gas supply unit 8 between the reaction tower 1A and the boost reaction tower 41. The control unit 17 may also control the switching of the switching unit 42. When the destination of the raw material gas supplied by the raw material gas supply unit 8 is switched from the boost reaction tower 41 to the reaction tower 1A, the raw material gas is supplied from the raw material gas supply unit 8 into the reaction tower 1A. When the destination of the raw material gas supplied by the raw material gas supply unit 8 is switched from the reaction tower 1A to the boost reaction tower 41, the raw material gas is supplied from the raw material gas supply unit 8 into the boost reaction tower 41.

[0065] The boost reaction tower 41 generates product gas and generated water through the exothermic reaction of the raw material gas in the catalyst. The discharge gas from the boost reaction tower 41 is sent to the reaction tower 1A via the gas cooling heat exchanger 43 and the gas-liquid separator 44, and supplied into the reaction tower 1A. The reaction tower 1A generates product gas and generated water through the exothermic reaction of the raw material gas in the catalyst.

[0066] Figure 6(A) shows an example of the configuration of the boost reaction tower 41. Figure 6(A) shows a cross-section of the boost reaction tower 41. The boost reaction tower 41 comprises a reaction vessel 51 filled with catalyst, a jacket portion 52 provided to surround the lower part of the reaction vessel 51, and an insulating member 53 provided to surround the upper part of the reaction vessel 51. Heated raw material gas flows into the reaction vessel 51 from the inlet end, and discharge gas flows out from the outlet end of the reaction vessel 51. When the circulation pump 46 is stopped and the heat transfer medium is not circulating between the boost reaction tower 41 and the reaction tower 1A, the heat transfer medium remains in the jacket portion 52. When the circulation pump 46 is started and the heat transfer medium is circulating between the boost reaction tower 41 and the reaction tower 1A, the heat transfer medium flows within the jacket portion 52.

[0067] Heat exchange takes place between the heat-generating portion of the reaction vessel 51 and the heat transfer medium in the jacket portion 52. That is, the reaction heat generated in the reaction vessel 51 is transferred to the heat transfer medium in the jacket portion 52, and the heat transfer medium is heated. The configuration of the boost reaction tower 41 is the same as that of the reaction tower 1 according to the first embodiment, but the volume of the boost reaction tower 41 is smaller than the volume of the reaction tower 1. Furthermore, the volume of the boost reaction tower 41 is smaller than the volume of the reaction tower 1A and also smaller than the volume of the reaction tower 3.

[0068] Figure 6(B) shows an example of the configuration of reaction tower 1A. Figure 6(B) shows a cross-section of reaction tower 1A. Reaction tower 1A comprises a reaction vessel 54 filled with catalyst and a jacket portion 55 provided to surround the reaction vessel 54. The discharge gas flows into the reaction vessel 54 from the inlet end and flows out from the outlet end of the reaction vessel 54.

[0069] When the delivery pump 11 and circulation pump 46 are stopped, and the heat transfer medium is not circulating between the boost reaction tower 41 and reaction tower 1A, and also not circulating between reaction tower 1A and reaction tower 3, the heat transfer medium remains stagnant within the jacket portion 55. When the circulation pump 46 is started and the heat transfer medium is circulating between the boost reaction tower 41 and reaction tower 1A, the heat transfer medium flows within the jacket portion 55. Alternatively, when the delivery pump 11 is started and the heat transfer medium is circulating between reaction tower 1A and reaction tower 3, the heat transfer medium flows within the jacket portion 55. Heat exchange takes place between the heat-generating portion of the reaction vessel 54 and the heat transfer medium within the jacket portion 55. That is, the reaction heat generated in the reaction vessel 54 is transferred to the heat transfer medium within the jacket portion 55, and the heat transfer medium is heated.

[0070] The configurations of the reaction vessel 51, jacket portion 52, and heat insulating member 53 of the boost reaction tower 41 are the same as those of the reaction vessel 31, jacket portion 32, and heat insulating member 33 of the reaction tower 1 according to the first embodiment. The configurations of the reaction vessel 54 and jacket portion 55 of the reaction tower 1A are the same as those of the reaction vessel 34 and jacket portion 35 of the reaction tower 3 according to the first embodiment. However, the jacket portion 52 of the boost reaction tower 41 and the jacket portion 55 of the reaction tower 1A are The boost reaction tower 41 and reaction tower 1A are connected, allowing the heat transfer medium to circulate between them. Additionally, the jacket portion 55 of reaction tower 1A and the jacket portion 35 of reaction tower 3 are connected, allowing the heat transfer medium to circulate between reaction tower 1A and reaction tower 3.

[0071] Figure 7 is a configuration diagram of the production apparatus 100 according to the second embodiment. Figure 7 shows a part of the production apparatus 100. Figure 7 shows a boost reaction tower 41 and a main circuit reaction group 60 having reaction towers 1A and 3. In the main circuit reaction group 60, a discharge pump 11 provided in the circulation path through which the heat transfer medium flows operates, causing the heat transfer medium to circulate between reaction tower 1A and reaction tower 3. A circulation pump 46 is located between the boost reaction tower 41 and reaction tower 1A and is provided in the circulation path through which the heat transfer medium flows. When the circulation pump 46 operates, the heat transfer medium circulates between the boost reaction tower 41 and reaction tower 1A.

[0072] The measuring sensor 18 measures the temperature inside reaction tower 1A, and the measuring sensor 45 measures the temperature inside boost reaction tower 41. The measurement data measured by the measuring sensor 18 and the measurement data measured by the measuring sensor 45 are sent to the raw material gas supply unit 8 and the control unit 17. As a result, the raw material gas supply unit 8 and the control unit 17 obtain the temperature inside reaction tower 1A and the temperature inside boost reaction tower 41.

[0073] The measuring sensor 18 may measure the temperature of the discharged gas sent from the reaction tower 1A and at least one of the temperature of the heat transfer medium in the jacket portion 55 as the temperature inside the reaction tower 1A. The measuring sensor 45 may measure the temperature of the discharged gas sent from the boost reaction tower 41 and at least one of the temperature of the heat transfer medium in the jacket portion 52 as the temperature inside the boost reaction tower 41.

[0074] <Driving Procedure> The operating procedure of the production apparatus 100 according to the second embodiment will now be described. Figure 8 is a flowchart showing the flow of the operating procedure of the production apparatus 100 according to the second embodiment. First, in step S201, the raw material gas supply unit 8 is started up and begins supplying raw material gas to the boost reaction tower 41. Next, in step S202, the raw material gas supply unit 8 heats the raw material gas and supplies it to the boost reaction tower 41. As the heated raw material gas is supplied to the boost reaction tower 41, the heated raw material gas flows into the inlet end of the reaction vessel 51. As the heated raw material gas flows into the reaction vessel 51, the temperature of the catalyst in the portion of the reaction vessel 51 covered by the heat insulating member 53 rises due to the heated raw material gas. When the temperature of the catalyst reaches the reaction start temperature, product gas and generated water are produced by the exothermic reaction of the raw material gas that has flowed into the reaction vessel 51.

[0075] The supply flow rate of the raw material gas from the start of raw material gas supply until the catalyst temperature reaches the reaction start temperature (first supply flow rate) is less than the rated supply flow rate of the raw material gas when producing the product gas (second supply flow rate). The raw material gas supply unit 8 or control unit 17 may determine the supply flow rate of the raw material gas to the boost reaction tower 41 based on the temperature inside the boost reaction tower 41. Alternatively, the raw material gas supply unit 8 or control unit 17 may determine the supply flow rate of the raw material gas to the boost reaction tower 41 based on the temperature of the catalyst in the portion of the reaction vessel 51 covered by the heat insulating member 53. Preferably, the first supply flow rate is such that the catalyst in the portion of the reaction vessel 51 covered by the heat insulating member 53 significantly promotes the exothermic reaction of the raw material gas.

[0076] In step S203, if the temperature of the catalyst in the portion of the reaction vessel 51 covered by the heat insulating member 53 is above a predetermined temperature (T2), the raw material gas supply unit 8 gradually increases the raw material gas supply flow rate and stops heating the raw material gas. The raw material gas supply unit 8 may also stop heating the raw material gas after controlling the supply flow rate to gradually increase. The raw material gas supply unit 8 may control the supply flow rate of the raw material gas to gradually increase after stopping the heating of the raw material gas. The predetermined temperature (T2) is, for example, 180°C, but is not limited to this temperature and may be determined based on experimental results, simulation results, etc.

[0077] When the temperature of the catalyst in the portion of the reaction vessel 51 covered by the insulating member 53 reaches a predetermined temperature (T2), an independent exothermic reaction is initiated in the boost reaction tower 41. Therefore, after the temperature of the catalyst in the portion of the reaction vessel 51 covered by the insulating member 53 reaches the predetermined temperature (T2), the amount of product gas produced is increased by gradually increasing the supply flow rate of the raw material gas. Furthermore, if heated raw material gas is supplied to the boost reaction tower 41 when the temperature of the catalyst in the portion of the reaction vessel 51 covered by the insulating member 53 is above the predetermined temperature (T2), the catalyst in the reaction vessel 51 may rise to an excessive temperature. By stopping the heating of the raw material gas, the catalyst in the reaction vessel 51 is prevented from rising to an excessive temperature.

[0078] In step S204, if the temperature of the discharged gas from the boost reaction tower 41 is above a predetermined temperature (T3), the control unit 17 starts the circulation pump 46 to circulate the heat transfer medium between the boost reaction tower 41 and the reaction tower 1A. The heat transfer medium passes through the boost reaction tower 41 by flowing through the jacket portion 52 of the boost reaction tower 41. The heat transfer medium that has passed through the boost reaction tower 41 is sent to the jacket portion 55 of the reaction tower 1A and passes through the reaction tower 1A. The heat transfer medium passing through the reaction tower 1A is heated by the boost reaction tower 41. As the heated heat transfer medium passes through the reaction tower 1A, the temperature inside the reaction tower 1A rises. The predetermined temperature (T3) is, for example, 180°C, but is not limited to this temperature and may be determined based on experimental results, simulation results, etc.

[0079] In step S204, if the temperature of the heat transfer medium in the jacket portion 52 is above a predetermined temperature (T4), the control unit 17 may start the circulation pump 46 to circulate the heat transfer medium between the boost reaction tower 41 and the reaction tower 1A. The predetermined temperature (T4) is, for example, 180°C, but is not limited to this temperature and may be determined based on experimental results, simulation results, etc.

[0080] In step S205, the control unit 17 starts the circulation pump 46 to circulate the heat transfer medium between reaction tower 1A and reaction tower 3. The heat transfer medium that has passed through reaction tower 1A is sent to the jacket portion 35 of reaction tower 3 and passes through reaction tower 3. The heat transfer medium passing through reaction tower 3 is heated by reaction tower 1A. As the heated heat transfer medium passes through reaction tower 3, the temperature inside reaction tower 3 rises.

[0081] In step S206, the switching unit 42 switches the supply destination of the raw material gas from the raw material gas supply unit 8 from the boost reaction tower 41 to the reaction tower 1A. As a result, the raw material gas is supplied from the raw material gas supply unit 8 to the reaction tower 1A. Because the temperature inside the reaction tower 1A is rising, the time it takes for the catalyst temperature to reach the reaction start temperature is shortened. Therefore, the time required to heat the catalyst inside the reaction tower 1A can be shortened, and the time from the start of raw material gas supply to the reaction tower 1A to the generation of product gas by the reaction tower 1A can be shortened.

[0082] In the flowchart in Figure 8, the timing of the processing in step S204 and the timing of the processing in step S205 may be the same or different. In the flowchart in Figure 8, the processing in steps S204 and S205 may be performed after the processing in step S206. In step S206, if the temperature of the discharged gas sent from the boost reaction tower 41 is above a predetermined temperature (T3), the raw material gas supply unit 8 may switch the raw material gas supply destination from the boost reaction tower 41 to the reaction tower 1A. Also, in step S206, if the temperature of the heat transfer medium in the jacket portion 52 is above a predetermined temperature (T4), the raw material gas supply unit 8 may switch the raw material gas supply destination from the boost reaction tower 41 to the reaction tower 1A.

[0083] In the production apparatus 100 according to the second embodiment, the raw material gas is heated, and the catalyst in the boost reaction tower 41 is heated using the heated raw material gas. Since the specific heat of the raw material gas is small, heating the raw material gas is easier compared to heating the heat transfer medium. In the production apparatus 100 according to the second embodiment, the heat insulating member 53 covers a predetermined portion of the outer circumference of the reaction tank 51, thereby insulating the outer circumference near the inlet end of the reaction tank 51. As a result, when heated raw material gas is supplied to the boost reaction tower 41, the time it takes for the temperature of the catalyst in the boost reaction tower 41 to reach the reaction start temperature is shortened, and the time required to heat the catalyst in the boost reaction tower 41 can be shortened. For example, when heat transfer oil is used as the heat transfer medium, low-temperature heat transfer oil has high viscosity and poor fluidity, so it takes time to circulate in the reaction tower. For this reason, when the heat transfer medium is heated by a heater and the heated heat transfer medium is passed through the reaction tower to heat the catalyst, the time it takes for the temperature of the catalyst to reach the reaction start temperature is long.

[0084] According to the production apparatus 100 of the second embodiment, the raw material gas is heated, and the catalyst in the boost reaction tower 41 is heated by the heated raw material gas, thus shortening the time it takes for the catalyst temperature to reach the reaction start temperature. Therefore, the time required to heat the catalyst in the boost reaction tower 41 can be shortened, and the time from the start of supplying the raw material gas to the boost reaction tower 41 to the production of the product gas by the boost reaction tower 41 can be shortened. Thus, according to the production apparatus 100 of the second embodiment, it is possible to heat the catalyst in the boost reaction tower 41 without using a heater to heat the heat transfer medium, and the time until the operation of the boost reaction tower 41 can be started can be shortened. Furthermore, according to the production apparatus 100 of the second embodiment, it is possible to heat the catalyst in reaction tower 1A and the catalyst in reaction tower 3 without using a heater to heat the heat transfer medium, and the time until the operation of reaction tower 1A and reaction tower 3 can be shortened.

[0085] Since the volume of the boost reaction tower 41 is smaller than the volume of the reaction tower 1A, the time required to heat the catalyst in the boost reaction tower 41 can be shortened. By circulating the heat transfer medium between the boost reaction tower 41 and the reaction tower 1A, the heat transfer medium heated by the exothermic reaction of the catalyst in the boost reaction tower 41 can be sent to the reaction tower 1A.

[0086] When the generator 100 starts operation, heated fuel gas is supplied to the boost reaction tower 41, and the heating of the fuel gas is stopped at a predetermined timing. Also, at a predetermined timing, the fuel gas supply destination is switched from the boost reaction tower 41 to the reaction tower 1A. This suppresses catalyst poisoning and reduces the frequency of catalyst replacement.

[0087] A heat spot may develop near the inlet end of the reaction vessel 51, causing the catalyst near the inlet end of the reaction vessel 51 to be more damaged than the catalyst in other areas. If a heat spot develops near the inlet end of the reaction vessel 51, the frequency of replacing the catalyst near the inlet end of the reaction vessel 51 may be increased. Furthermore, by replacing only the catalyst near the inlet end of the reaction vessel 51, the catalyst replacement cost can be reduced compared to replacing the entire catalyst in the reaction vessel 51.

[0088] Furthermore, each of the processes described above may be considered as a method for generating product gas in the generating device 100 or a method for operating the generating device 100. Alternatively, they may be considered as a generating system or operating system having at least some of the processes or functions described above. Note that each of the above means and processes can be combined with each other as much as possible to constitute the present invention. [Explanation of Symbols]

[0089] 1,1A,3...Reaction tower; 2,4...Heat exchanger for gas cooling; 5...Heat exchanger for heat transfer medium; 6,7...Gas-liquid separator; 8...Raw material gas supply unit; 11...Discharge pump; 17...Control unit;1 8, 19, 45... Measuring sensors; 28... Combustion section; 31, 34, 51, 54... Reaction vessels; 32, 35, 52, 55... Jacket sections; 33, 53... Insulation materials; 41... Boost reaction tower; 42... Switching section; 46... Circulation pump; 100... Generating device

Claims

1. A reaction tower that generates a product gas through an exothermic reaction of a raw material gas in a catalyst, A raw material gas supply unit that heats the raw material gas and supplies it to the reaction tower, Equipped with, The reaction tower comprises a reaction vessel filled with the catalyst and into which the raw material gas flows, a jacket portion covering a part of the outer periphery of the reaction vessel and through which a heat transfer medium flows, and an insulating member covering another part of the outer periphery of the reaction vessel. The aforementioned heat insulating member covers the outer circumference of the reaction vessel from the part in which the raw material gas flows in toward the central part to a predetermined portion. The jacket portion is positioned in the area of ​​the outer circumference of the reaction vessel that is not covered by the insulating member. generator.

2. A pump for supplying the heat transfer medium to the reaction tower, A control unit that controls the operation of the raw material gas supply unit, Equipped with, The control unit controls the operation of the raw material gas supply unit, and after the supply of the raw material gas to the reaction tower is started, the control unit starts the delivery pump so that the heat transfer medium is sent to the reaction tower. The generating apparatus according to claim 1.

3. The reaction tower is equipped with a measuring sensor for measuring the temperature inside the reaction tower, The raw material gas supply unit acquires the temperature inside the reaction tower measured by the measuring sensor, and determines the flow rate of the raw material gas supplied to the reaction tower based on the temperature inside the reaction tower. The generating apparatus according to claim 1.

4. The reaction tower is equipped with a measuring sensor for measuring the temperature inside the reaction tower, The raw material gas supply unit acquires the temperature inside the reaction tower measured by the measuring sensor, and if the temperature of the catalyst in the portion of the reaction vessel covered by the insulating member is above a predetermined temperature, it gradually increases the supply flow rate of the raw material gas to the reaction tower, and the raw Stop heating the gas supply. The generating apparatus according to claim 1.

5. The system includes a combustion section for burning the unreacted raw material gas discharged from the reaction tower, At least one of the raw material gas supplied to the reaction tower and the heat transfer medium flowing into the jacket portion is heated by the heat of combustion of the unreacted raw material gas. The generating apparatus according to claim 1.

6. The raw material gas comprises hydrogen and carbon dioxide, The aforementioned product gas is methane gas. A generating apparatus according to any one of claims 1 to 5.

7. A method for producing a product gas in a production apparatus comprising a reaction tower that produces a product gas by an exothermic reaction of a raw material gas in a catalyst, and a raw material gas supply unit that supplies the raw material gas to the reaction tower, The process involves the raw material gas supply unit heating the raw material gas and supplying it to the reaction tower. Includes, The reaction tower comprises a reaction vessel filled with the catalyst and into which the raw material gas flows, a jacket portion covering a part of the outer periphery of the reaction vessel and through which a heat transfer medium flows, and an insulating member covering another part of the outer periphery of the reaction vessel. The aforementioned heat insulating member covers the outer circumference of the reaction vessel from the part in which the raw material gas flows in toward the central part to a predetermined portion. The jacket portion is positioned in the area of ​​the outer circumference of the reaction vessel that is not covered by the insulating member. Generation method.

8. The generating apparatus comprises a delivery pump that sends the heat transfer medium to the reaction tower and a control unit that controls the operation of the raw material gas supply unit, The aforementioned generation method is The control unit controls the operation of the raw material gas supply unit, and after the supply of the raw material gas to the reaction tower is started, the control unit starts the delivery pump to send the heat transfer medium to the reaction tower. including, The generation method according to claim 7.

9. The generating apparatus is equipped with a measuring sensor for measuring the temperature inside the reaction tower, The aforementioned generation method is The raw material gas supply unit includes the step of acquiring the temperature inside the reaction tower measured by the measuring sensor, The raw material gas supply unit performs the step of determining the flow rate of the raw material gas supplied to the reaction tower based on the temperature inside the reaction tower, including, The generation method according to claim 7.

10. The generating apparatus is equipped with a measuring sensor for measuring the temperature inside the reaction tower, The aforementioned generation method is The raw material gas supply unit includes the step of acquiring the temperature inside the reaction tower measured by the measuring sensor, When the temperature of the catalyst in the portion of the reaction vessel covered by the insulating member is above a predetermined temperature, the raw material gas supply unit gradually reduces the flow rate of the raw material gas supplied to the reaction tower. A step of increasing and stopping the heating of the raw material gas, including, The generation method according to claim 7.

11. The raw material gas comprises hydrogen and carbon dioxide, The aforementioned product gas is methane gas. The method of production according to any one of claims 7 to 10.

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