JP2019151537A - Hydrogen production device - Google Patents

Abstract

To prevent reformed gas from flowing into a hydrogen purifier in an inadequate state.SOLUTION: A communication passage tube 60 for sending out reformed gas G2, is branched into a first passage tube 62 that supplies the reformed gas G2 to a hydrogen purifier 90 side, and a second passage tube 64 that supplies the reformed gas G2 to a burner 26 provided at the top of a combustion chamber 25. The first passage tube 62 is provided with a first valve V1, and a second passage tube 64 is provided with a second valve V2.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a hydrogen production apparatus.

  Conventionally, as a hydrogen production apparatus for obtaining hydrogen, a raw material hydrocarbon is reformed into reformed gas by a steam reformer and then supplied to a PSA (Pressure Swing Adsorption) apparatus to purify hydrogen. (For example, refer to Patent Document 1). In the hydrogen production apparatus of Patent Document 1, the reformed gas exiting the steam reformer is cooled by the cooler and then sent to the CO converter, and the reformed gas exiting the CO converter is cooled, and the drum After the water is removed by a dehydrator such as a dehydrator, it is supplied to a PSA apparatus filled with a known adsorbent.

JP 2001-261306 A

  When the reformed gas supplied to the PSA device does not satisfy the rated hydrogen concentration for the hydrogen purification function in the PSA device, that is, when there are too many impurities other than hydrogen, the impurities contained in the reformed gas are sufficient. It may not be able to be adsorbed on the PSA apparatus, and a sufficient concentration of hydrogen may not be purified, and an excessive load may be applied to the PSA apparatus.

  The present invention has been made in consideration of the above-described facts, and an object of the present invention is to provide a hydrogen production apparatus that can prevent the reformed gas from flowing into the hydrogen purifier in an inappropriate state.

  In order to achieve the above object, a hydrogen production apparatus according to claim 1 includes a reformer that reforms a raw material to generate a reformed gas containing hydrogen, and separates the reformed gas into impurities and hydrogen. A hydrogen purifier for purifying hydrogen, a first flow path for supplying the reformed gas sent from the reformer to the hydrogen purifier, and the hydrogen purification of the reformed gas sent from the reformer A second flow path that leads to a different location from the vessel, and a switching portion that switches the reformed gas destination flow path between the first flow path and the second flow path.

  The hydrogen production apparatus according to claim 1 is different from the hydrogen purifier in the first flow path for supplying the reformed gas sent from the reformer to the hydrogen purifier and the reformed gas sent from the reformer. A second flow path leading to the point. Then, the switching unit switches to which channel the reformed gas is sent. Therefore, when the reformed gas is in an inappropriate state, the reformed gas can be prevented from flowing into the hydrogen purifier by switching the reformed gas supply destination to the second flow path.

  In the hydrogen production apparatus according to claim 2, the switching unit switches the reformed gas destination channel to the first channel when the hydrogen concentration of the reformed gas is in a rated state, and When the hydrogen concentration of the quality gas is not in a rated state, the reformed gas delivery channel is switched to the second channel.

  In the hydrogen production device according to claim 2, when the hydrogen concentration of the reformed gas sent from the reformer is in the rated state, the reformed gas is switched to flow to the first flow path, and is not in the rated state. In this case, the reformed gas is switched to the second flow path. Accordingly, it is possible to prevent the reformed gas from flowing into the hydrogen purifier in an appropriate state and not into the hydrogen purifier in an inappropriate state.

  The hydrogen production apparatus according to claim 3 has a water separation part that separates water from the reformed gas, and the second flow path is branched from the first flow path on the downstream side of the water separation part. ing.

  According to the hydrogen production apparatus according to the third aspect, since the water is separated by the water separation unit, the separated water can be effectively reused. In addition, since the reformed gas after the water is separated is supplied to the second flow path, the water contained in the gas sent downstream from the second flow path is reduced, and when used as fuel, A reformed gas having a high calorific value can be supplied as fuel.

  In a hydrogen production apparatus according to a fourth aspect, the reformer has a combustion section for combusting combustion gas, and the second flow path guides the reformed gas to the combustion section.

  According to the hydrogen production apparatus of the fourth aspect, since the reformed gas that is not supplied to the hydrogen purifier is guided to the combustion section, the reformed gas can be used for combustion in the combustion section, and the reformed gas is effectively used. be able to.

  In the hydrogen production apparatus according to claim 5, the second flow path sends out the reformed gas to the outside.

  According to the hydrogen production apparatus of the fifth aspect, the reformed gas that is not supplied to the hydrogen purifier can be discharged to the outside.

  The hydrogen production apparatus according to claim 6 includes a compressor that compresses the reformed gas between the reformer and the hydrogen purifier, and the second flow path is upstream of the compressor. And branched from the first flow path.

  According to the hydrogen production apparatus of the sixth aspect, the pressure necessary for purification in the hydrogen purifier can be applied to the reformed gas, and the hydrogen purifier can be efficiently purified. Further, since the reformed gas is guided to the second flow path on the upstream side of the compressor, the load on the compressor can be reduced.

  According to the hydrogen production apparatus of the present invention, the reformed gas can be prevented from flowing into the hydrogen purifier in an inappropriate state.

It is the schematic block diagram which showed the hydrogen production apparatus which concerns on this embodiment. It is sectional drawing which showed the multiple cylinder type reformer of the hydrogen production apparatus which concerns on this embodiment. It is a functional block diagram of the hydrogen production apparatus concerning this embodiment. It is a flowchart which shows an example of the rating judgment process at the time of starting of this embodiment. It is the schematic block diagram which showed the hydrogen production apparatus which concerns on the modification of this embodiment.

  Hereinafter, an example of a hydrogen production apparatus according to an embodiment of the present invention will be described in detail with reference to the drawings.

  As shown in FIG. 1, the hydrogen production apparatus 10A according to the present embodiment includes a multi-cylinder reformer 12, an air supply unit 18, a pre-pressurization water separation unit 50, a compressor 80, a post-pressurization water separation unit 52, A buffer volume 54, a hydrogen purifier 90, and a control unit 70 are provided. This hydrogen production apparatus 10A produces hydrogen from a hydrocarbon raw material, and in the present embodiment, a case will be described in which city gas containing methane as a main component is used as an example of a hydrocarbon raw material.

  As shown in FIG. 2, the multiple cylinder reformer 12 has a plurality of cylindrical walls 21, 22, 23, and 24 arranged in multiple. The plurality of cylindrical walls 21, 22, 23, 24 are formed in, for example, a cylindrical shape or an elliptical cylindrical shape. A combustion chamber 25 is formed inside the first cylindrical wall 21 from the inside out of the plurality of cylindrical walls 21, 22, 23, 24, and a burner 26 faces downward at the upper part of the combustion chamber 25. Is arranged. The burner 26 is supplied with the off gas of the hydrogen purifier 90 from the off gas pipe 38 as fuel. The multiple cylinder reformer 12 is an example of a reformer. Further, an air supply pipe 40 for supplying combustion air from the air supply unit 18 (see FIG. 1) is connected to the upper end of the combustion chamber 25. The burner 26 is further connected to a raw material branch pipe 33 </ b> A in which city gas is branched from the raw material supply pipe 33. An air branch pipe 40A branched from the air supply pipe 40 is connected to the raw material branch pipe 33A. A gas in which air is mixed with city gas is supplied to the burner 26 separately from off-gas described later. Either or both of off-gas and city gas for combustion are supplied as necessary.

  A flue gas flow path 27 is formed between the first cylindrical wall 21 and the second cylindrical wall 22. A lower end portion of the combustion exhaust gas passage 27 communicates with the combustion chamber 25, and a gas exhaust pipe 28 for discharging gas is connected to the upper end portion of the combustion exhaust gas passage 27. The flue gas discharged from the combustion chamber 25 flows from the lower side to the upper side through the flue gas passage 27 and is discharged to the outside through the gas discharge pipe 28.

  A first flow path 31 is formed between the second cylindrical wall 22 and the third cylindrical wall 23. An upper portion of the first flow path 31 is formed as a preheating flow path 32, and a raw material supply pipe 33 for supplying city gas and reforming water are supplied to the upper end portion of the preheating flow path 32. The water supply pipe 34 is connected. Further, a spiral member 35 is provided between the second cylindrical wall 22 and the third cylindrical wall 23, and the preheating channel 32 is formed in a spiral shape by the spiral member 35. Yes. The raw material supply pipe 33 is an example of a flow path pipe.

  To the preheating channel 32, city gas is supplied from a raw material supply pipe 33, and further, reforming water is supplied from a water supply pipe 34. The city gas and the reforming water flow from the upper side to the lower side through the preheating channel 32, and heat exchange with the combustion exhaust gas is performed through the second cylindrical wall 22 to vaporize the water. In the preheating channel 32, the mixed gas is generated by mixing the city gas and the reforming water (steam) in the gas phase.

  The reforming catalyst layer 36 is provided below the preheating channel 32 in the first channel 31, and the mixed gas generated in the preheating channel 32 is supplied to the reforming catalyst layer 36. . In the reforming catalyst layer 36, the mixed gas receives heat from the flue gas flowing through the flue gas passage 27, and the mixed gas generates a reformed gas containing hydrogen as a main component by a steam reforming reaction. A thermometer 36 </ b> A is provided on the outlet side of the reforming catalyst layer 36. The thermometer 36A measures the temperature of the reforming catalyst layer 36. The thermometer 36 </ b> A is connected to the control unit 70 (see FIG. 3), and outputs measured temperature data to the control unit 70.

  Further, a second flow path 42 is formed between the third cylindrical wall 23 and the fourth cylindrical wall 24. The lower end of the second flow path 42 is in communication with the lower end of the first flow path 31. A lower portion of the second flow path 42 is formed as a reformed gas flow path 43, and a reformed gas discharge pipe 44 is connected to an upper end portion of the second flow path 42.

  Further, a CO shift catalyst layer 45 is provided above the reformed gas channel 43 in the second channel 42, and the reformed gas generated in the reformed catalyst layer 36 is converted into the reformed gas flow. After passing through the passage 43, it is supplied to the CO shift catalyst layer 45. In the CO conversion catalyst layer 45, carbon monoxide and water vapor contained in the reformed gas react to be converted into hydrogen and carbon dioxide, and carbon monoxide is reduced.

  Further, an oxidant gas supply pipe 46 is connected to the upper side of the CO shift catalyst layer 45, and a CO selective oxidation catalyst layer 47 is provided above the CO shift catalyst layer 45 in the second flow path 42. ing. Note that the CO selective oxidation catalyst layer 47 is not an essential component and may not be provided. The oxidant gas introduced through the oxidant gas supply pipe 46 and the reformed gas that has passed through the CO shift catalyst layer 45 are supplied to the CO selective oxidation catalyst layer 47. In the CO selective oxidation catalyst layer 47, for example, carbon monoxide reacts with oxygen on a noble metal catalyst such as platinum or ruthenium to be converted into carbon dioxide, and carbon monoxide is removed. The reformed gas G1 in which carbon monoxide is reduced in the CO shift catalyst layer 45 and the CO selective oxidation catalyst layer 47 is discharged through the reformed gas discharge pipe 44.

  On the downstream side of the reformed gas discharge pipe 44, a heat exchange unit HE1 and a pre-pressurization water separation unit 50 are provided in this order. In the pre-pressurization water separation unit 50, the condensed water (liquid phase) is stored in the lower part, the reformed gas (gas) is stored in the upper part, and the gas and the liquid are separated. A downstream end of the reformed gas discharge pipe 44 is connected to the inlet side upper portion of the pre-pressurization water separation unit 50. In addition, the upstream end of the communication flow channel pipe 60 is connected to the outlet side upper portion (gas storage portion) of the pre-pressurization water separation unit 50. A water recovery pipe 50 </ b> A is connected to the bottom (liquid storage portion) of the pre-pressurization water separation unit 50. In the reformed gas G1, water is condensed and separated by cooling by heat exchange with cooling water in the heat exchanger HE1. The reformed gas G <b> 2 after the water is separated is sent to the connecting flow path pipe 60. The separated water is sent to the water recovery pipe 50A.

  The communication flow path pipe 60 includes a first flow path pipe 62 that supplies the reformed gas G2 to the compressor 80, and a second flow path pipe that supplies the reformed gas G2 to the burner 26 provided in the upper portion of the combustion chamber 25. It is branched into 64. The downstream end of the first flow path pipe 62 is connected to the inlet side of the compressor 80, and the first flow path pipe 62 is provided with a first valve V <b> 1. The downstream end of the second flow path pipe 64 is connected to an off-gas pipe 38 described later, and the second flow path pipe 64 is provided with a second valve V2.

  As shown in FIG. 3, the first valve V <b> 1 and the second valve V <b> 2 are connected to the control unit 70. The control unit 70 includes a CPU, a ROM, and a RAM, is connected to each unit of the hydrogen production apparatus 10A, and controls the operation of the hydrogen production apparatus 10A. The first valve V <b> 1 and the second valve V <b> 2 are opening / closing valves, and opening / closing is controlled by the control unit 70. The controller 70 controls the first valve V1 to be opened and the second valve V2 to be closed when the reformed gas flowing into the hydrogen purifier 90 is rated. When not in the rated state, the first valve V1 is closed and the second valve V2 is opened.

  Here, the rated state refers to a state where the concentration of hydrogen contained in the reformed gas that is sent from the multi-cylinder reformer 12 and flows into the hydrogen purifier 90 is equal to or higher than a predetermined value. If the reformed gas flowing into the hydrogen purifier 90 contains a large amount of impurities other than hydrogen, the adsorbent cannot sufficiently adsorb the impurities, and the concentration of the purified hydrogen does not satisfy the predetermined concentration. There is a possibility that the hydrogen purifier 90 may be overloaded.

  In particular, immediately after startup of the hydrogen production apparatus 10A, the temperature in the multi-cylinder reformer 12 may not be sufficiently increased, and the reaction for generating the reformed gas may not be sufficiently advanced. The reformed gas generated in such a state contains a lot of impurities other than hydrogen.

  Therefore, as a concentration of hydrogen contained in the reformed gas flowing into the hydrogen purifier 90, a value at which the hydrogen purifier 90 functions appropriately is set to a predetermined value indicating a rated state (for example, hydrogen concentration contained in the reformed gas). The ratio is determined as 70% or more). In addition, the temperature range in the multi-cylinder reformer 12 when the reformed gas delivered from the multi-cylinder reformer 12 satisfies the rated state is determined by a prior experiment and the threshold ( For example, it is set as 600 ° C. or higher. In addition, an analysis device that analyzes the composition of the reformed gas may be provided in the communication channel pipe 60, and the determination may be made based on the hydrogen concentration of the reformed gas obtained from the analysis result of the analyzer. Further, a flow meter for measuring the flow rate of the reformed gas is provided in the communication flow path pipe 60, and the flow rate of the reformed gas measured by the flow meter and the thermometer provided in the reformer are measured. Estimate the hydrogen concentration of the reformed gas based on the temperature and the relationship between the flow rate of the reformed gas and the temperature in the reformer and the hydrogen concentration, which have been specified in advance through experiments, etc. May be determined.

  In the present embodiment, the control unit 70 acquires temperature data from a thermometer 36A provided in the multi-cylinder reformer 12, and determines whether the acquired temperature is equal to or higher than a threshold value. Determine whether or not.

  A communication channel pipe 66 is connected to the outlet side of the compressor 80. The compressor 80 compresses the reformed gas at atmospheric pressure supplied from the pre-pressurization water separation unit 50 with a pump, and sends the compressed gas to the communication channel pipe 66.

  A heat exchanging unit HE2 and a post-pressurization water separation unit 52 are provided in this order on the downstream side of the communication channel pipe 66. In the post-pressurization water separation unit 52, the condensed water (liquid phase) is stored in the lower part, the reformed gas (gas) is stored in the upper part, and the gas and the liquid are separated. The downstream end of the communication flow path pipe 66 is connected to the upper part on the inlet side of the post-pressurization water separation part 52. Further, the upstream end of the communication flow path pipe 68 is connected to the outlet side upper part (gas storage part) of the post-pressurization water separation part 52. A water recovery pipe 52 </ b> A is connected to the bottom part (liquid storage part) of the post-pressurization water separation part 52. The reformed gas G2 is condensed and separated by cooling by heat exchange with cooling water in the heat exchanger HE2. The reformed gas G3 after the water has been separated is sent to the connecting flow path pipe 68. The separated water is sent to the water recovery pipe 52A.

  The upstream end of the communication flow path pipe 68 is connected to the outlet side upper part (gas storage part) of the post-pressurization water separation part 52. The downstream end of the communication channel pipe 68 is connected to the inlet side of the buffer volume 54. The buffer volume 54 temporarily stores the reformed gas G3 supplied from the post-pressurization water separation unit 52. A communication channel pipe 69 is connected to the outlet side of the buffer volume 54, and the downstream end of the communication channel pipe 69 is connected to the inlet side of the hydrogen purifier 90. From the buffer volume 54, the reformed gas G3 that has been boosted to a predetermined pressure is supplied to the hydrogen purifier 90.

  For example, a PSA apparatus can be used for the hydrogen purifier 90. Further, a separation membrane can be used as the hydrogen purifier 90. The hydrogen purifier 90 separates the reformed gas into impurities and hydrogen, thereby purifying hydrogen. The purified hydrogen is sent to the hydrogen supply pipe 92 and stored in a tank (not shown) or sent to the hydrogen supply line. The off-gas separated as impurities in the hydrogen purifier 90 is sent to the off-gas pipe 38 and supplied to the combustion chamber 25 (burner 26) of the multi-cylinder reformer 12. The downstream end of the off gas pipe 38 is connected to the burner 26. A second flow path pipe 62 is connected to the off gas pipe 38.

  The water recovery pipes 50 </ b> A and 52 </ b> A and the external water supply unit 17 that is an external water supply source are connected to the water supply pipe 34. The water supply pipe 34 is provided with a pump P1 and a water treatment device (ion exchange resin) 34A for removing dissolved ion components. Is provided. The reforming water is supplied to the multiple cylinder reformer 12 by the pump P1.

  Next, the operation of the hydrogen production apparatus 10A will be described.

  The city gas flows through the raw material supply pipe 33 and is supplied to the multiple cylinder reformer 12. The city gas supplied to the multi-cylinder reformer 12 is heated while being mixed with reforming water in the preheating channel 32 of the multi-cylinder reformer 12 and supplied to the reforming catalyst layer 36. In the reforming catalyst layer 36, the mixed gas receives heat from the flue gas flowing through the flue gas passage 27, and the mixed gas generates a reformed gas containing hydrogen as a main component by a steam reforming reaction. The reformed gas is supplied to the CO shift catalyst layer 45 through the reformed gas channel 43. In the CO conversion catalyst layer 45, carbon monoxide and water vapor contained in the reformed gas react to be converted into hydrogen and carbon dioxide, and carbon monoxide is reduced.

Further, the reformed gas that has passed through the CO shift catalyst layer 45 is supplied to the CO selective oxidation catalyst layer 47 together with the oxidizing gas (air) supplied from the oxidant gas supply pipe 46, and carbon monoxide is oxygenated on the noble metal catalyst. It is converted into carbon dioxide by reaction with carbon monoxide. The reformed gas G1 in which carbon monoxide is reduced in the CO selective oxidation catalyst layer 47 is sent to the reformed gas discharge pipe 44.
Note that the CO selective oxidation catalyst layer 47 is not necessarily used, and the hydrogen production apparatus 10 </ b> A may be operated without supplying air from the oxidant gas supply pipe 46.

  The reformed gas G1 flows into the pre-pressurization water separator 50 through the reformed gas discharge pipe 44. The water contained in the reformed gas G1 condensed by heat exchange in the heat exchanger HE1 is stored in the lower part and sent out from the water recovery pipe 50A. The reformed gas G <b> 2 from which water has been separated is sent to the communication flow path pipe 60.

  The control unit 70 performs a rating judgment process at startup shown in FIG. 4 at the start of operation of the hydrogen production apparatus 10A. At the start of operation, the first valve V1 is closed and the second valve V2 is opened. In step S12, the control unit 70 acquires the temperature measured by the thermometer 36A. In step S14, the control unit 70 determines whether the reformed gas is in a rated state based on the acquired temperature. If it is determined that the current state is rated, the process proceeds to step S16. On the other hand, if the reformed gas is not in the rated state, the process returns to step S12.

  When it is determined that the reformed gas is not in the rated state, the reformed gas G <b> 2 flows into the second flow path pipe 64 and is supplied to the burner 26. That is, when the reformed gas is not in a rated state, the reformed gas G2 sent to the communication channel pipe 60 flows to the second channel pipe 64, joins the off-gas pipe 38, and is supplied to the burner 26 as fuel. And supplied for combustion as described above.

  In step S16, the first valve V1 is opened, the second valve V2 is closed, and the start-up rating determination process ends.

  By the treatment in step S16, the outflow destination of the reformed gas G2 is switched from the second flow path pipe 64 to the first flow path pipe 62. The reformed gas G <b> 2 sent to the communication channel pipe 60 flows to the first channel pipe 62, is supplied to the compressor 80, and is compressed by the compressor 80. The compressed reformed gas G <b> 2 flows through the communication channel pipe 66 and flows into the water separation unit 52 after being pressurized. The water contained in the reformed gas G2 condensed by heat exchange in the heat exchanger HE2 is stored in the lower part and sent out from the water recovery pipe 52A. The reformed gas G3 from which water has been separated is sent to the communication channel pipe 68, temporarily stored in the buffer volume 54, and then supplied to the hydrogen purifier 90 via the communication channel pipe 69.

  In the hydrogen purifier 90, the reformed gas G3 is separated into impurities and hydrogen, and the hydrogen is sent to the hydrogen supply pipe 92. The delivered hydrogen is stored in a tank (not shown) or sent to a hydrogen supply line. On the other hand, off-gas containing impurities other than hydrogen from the reformed gas G3 flows through the off-gas pipe 38 and is supplied to the burner 26 of the multi-cylinder reformer 12 as fuel.

  In the combustion chamber 25 of the multiple cylinder reformer 12, off-gas is combusted, and combustion exhaust gas is discharged to the outside from the gas discharge pipe 28.

  The water sent to the water recovery pipes 50A and 52A is supplied to the multi-cylinder reformer 12 as reformed water through the water treatment device 34A by driving the pump P1. The external water supply unit 17 supplies the multi-cylinder reformer 12 with water for a new amount that needs to be supplied from the outside.

  In the hydrogen production apparatus 10 </ b> A of the present embodiment, the communication flow path pipe 60 is branched, and the reformed gas G <b> 2 is caused to flow to the second flow path pipe 62 that is not supplied to the hydrogen purifier 90 at times other than rated operation. Therefore, it is possible to avoid the reformed gas having a low hydrogen concentration from flowing into the hydrogen purifier 90.

  In the present embodiment, the reformed gas having a low hydrogen concentration can be supplied to the burner 26 of the combustion chamber 25 and effectively used as fuel.

  In the present embodiment, the branch of the first flow path pipe 62 and the second flow path pipe 64 is provided on the downstream side of the pre-pressurization water separation unit 50 and the upstream side of the compressor 80, but is limited to this position. It can be provided at any position between the outlet of the multi-tubular reformer 12 and the inlet of the hydrogen purifier 90.

  In this embodiment, since it branches to the second flow path pipe 62 on the downstream side of the pre-pressurization water separation part 50, the water contained in the reformed gas is reduced and the reformed gas having a high calorie is used for combustion. Can do. Furthermore, the separated water can be reused effectively. Further, in this embodiment, since the second branch pipe 62 is branched upstream of the compressor 80, the reformed gas that is not purified can be supplied to the burner 26 without being compressed. Can be reduced.

  In the present embodiment, the second flow path pipe 64 is connected to the off-gas pipe 38, but the second flow path pipe 64 may be connected to the burner 26. Moreover, as shown in FIG. 5, it is good also as the hydrogen production apparatus 10B which open | released the 2nd flow-path pipe 64 outside.

  In the present embodiment, the hydrogen production apparatus including the compressor 80 has been described. However, the present invention may be applied to a hydrogen production apparatus that does not include the compressor 80, or the compressor may be a multiple cylinder type modified. You may apply to the hydrogen production apparatus arrange | positioned upstream from the mass device 12. FIG.

  In addition, although this embodiment demonstrated as a process at the time of starting of 10 A of hydrogen production apparatuses, it is not limited to this. The measured value of the thermometer 36A is constantly monitored so that the reformed gas does not flow into the hydrogen purifier 90 when it is determined that the temperature in the multi-cylinder reformer 12 does not satisfy the rated state. Good. Thereby, it is possible to prevent the reformed gas in an inappropriate state from flowing into the hydrogen purifier 90 even when the reformed gas containing a large amount of impurities has been sent out due to abnormal operation or the like. .

10A, 10B Hydrogen production equipment, 12 Multiple cylinder type reformer (reformer)
25 Combustion chamber (combustion part), 26 Burner (combustion part)
50 Water separator before pressurization (water separator)
62 1st flow path pipe (1st flow path), 64 2nd flow path pipe (2nd flow path)
70 Control unit (switching unit)
80 Compressor 90 Hydrogen Purifier V1 First Valve (Switching Unit)
V2 Second valve (switching part)

Claims (6)

A reformer that reforms the raw material to produce reformed gas containing hydrogen;
A hydrogen purifier that purifies hydrogen by separating the reformed gas into impurities and hydrogen;
A first flow path for supplying the reformed gas sent from the reformer to the hydrogen purifier;
A second flow path for guiding the reformed gas sent from the reformer to a different location from the hydrogen purifier;
A switching unit for switching the destination flow path of the reformed gas between the first flow path and the second flow path;
A hydrogen production apparatus equipped with   The switching unit switches the reformed gas destination flow path to the first flow path when the hydrogen concentration of the reformed gas is in a rated state, and the hydrogen concentration of the reformed gas is not in a rated state. The hydrogen production apparatus according to claim 1, wherein the reforming gas destination channel is switched to the second channel. A water separation part for separating water from the reformed gas;
The hydrogen production apparatus according to claim 1 or 2, wherein the second flow path is branched from the first flow path on the downstream side of the water separation unit. The reformer has a combustion section for burning combustion gas,
The hydrogen production apparatus according to any one of claims 1 to 3, wherein the second flow path supplies the reformed gas to the combustion section.   The hydrogen production apparatus according to claim 1, wherein the second flow path delivers the reformed gas to the outside.   A compressor for compressing the reformed gas between the reformer and the hydrogen purifier, and the second flow path is branched from the first flow path upstream of the compressor. The hydrogen production apparatus according to any one of claims 1 to 5.