JP6983086B2 - Hydrogen production equipment - Google Patents

Description

The present invention relates to a hydrogen production apparatus.

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

Japanese Unexamined Patent Publication No. 2001-261306

If the reformed gas supplied to the PSA device does not meet the hydrogen concentration rated for the hydrogen purification function of the PSA device, that is, if there are too many impurities other than hydrogen, the impurities contained in the reformed gas are sufficient. There is a possibility that hydrogen cannot be adsorbed to the gas, and hydrogen of a sufficient concentration cannot be purified, and an excessive load may be applied to the PSA device.

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

In order to achieve the above object, the hydrogen production apparatus according to claim 1 separates a reformer that reforms a raw material to generate a reformed gas containing hydrogen, and the reformed gas into impurities and hydrogen. A hydrogen purifier that purifies hydrogen, a first flow path that supplies the reformed gas sent from the reformer to the hydrogen purifier, and the hydrogen purification of the reformed gas sent from the reformer. It is provided with a second flow path that leads to a place different from the vessel, and a switching unit that switches the delivery destination flow path of the reforming gas between the first flow path and the second flow path.

The hydrogen production apparatus according to claim 1 is different from the hydrogen refiner in that the first flow path for supplying the reformed gas sent from the reformer to the hydrogen refiner and the reformed gas sent from the reformer are different from the hydrogen refiner. It has a second channel to lead to the place. Then, the switching unit switches which flow path the reforming gas is sent to. Therefore, when the reforming gas is in an inappropriate state, it is possible to avoid the inflow of the reforming gas into the hydrogen purifier by switching the supply destination of the reforming gas to the second flow path.

In the hydrogen production apparatus according to claim 1, the switching unit sets the delivery flow path of the reformed gas to the first channel when the hydrogen concentration of the reformed gas on the upstream side of the switching unit is in the rated state. It is switched to one flow path, and when the hydrogen concentration of the reforming gas is not in the rated state, the delivery destination flow path of the reforming gas is switched to the second flow path.

In the hydrogen production apparatus according to claim 1, when the hydrogen concentration of the reforming gas sent from the reformer is in the rated state, it is switched so that the reforming gas flows to the first flow path, and the reforming gas is not in the rated state. In some cases, the reforming gas is switched to flow to the second flow path. Therefore, it is possible to prevent the reformed gas from flowing into the hydrogen purifier in an appropriate state and not flowing into the hydrogen purifier in an inappropriate state.

The hydrogen production apparatus according to claim 2 has a water separation section 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 section. ing.

According to the hydrogen production apparatus according to claim 2 , since water is separated by the water separation unit, the separated water can be effectively reused. Further, since the reformed gas after the water is separated is supplied to the second flow path, the amount of water contained in the gas sent downstream from the second flow path is reduced, and when it is used as fuel, it is used. A reformed gas with a high calorific value can be supplied as fuel.

In the hydrogen production apparatus according to claim 3, the reformer has a combustion unit that burns a combustion gas, and the second flow path guides the reformed gas to the combustion unit.

According to the hydrogen production apparatus according to claim 3 , since the reformed gas that is not supplied to the hydrogen purifier is guided to the combustion unit, the reformed gas can be used for combustion in the combustion unit, and the reformed gas can be effectively used. be able to.

In the hydrogen production apparatus according to claim 4, the reformed gas is sent out to the outside through the second flow path.

According to the hydrogen production apparatus according to claim 4 , the reformed gas that is not supplied to the hydrogen purifier can be discharged to the outside.

The hydrogen production apparatus according to claim 5 includes a compressor for compressing the reformed gas between the reformer and the hydrogen refiner, and the second flow path is on the upstream side of the compressor. Is branched from the first flow path.

According to the hydrogen production apparatus according to claim 5 , the pressure required for purification in the hydrogen purifier can be applied to the reforming gas, and purification can be efficiently performed in the hydrogen purifier. Further, since the reforming 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, it is possible to prevent the reformed gas from flowing into the hydrogen purifier in an inappropriate state.

It is a schematic block diagram which showed the hydrogen production apparatus which concerns on this embodiment. It is sectional drawing which showed the multi-cylindrical reformer of the hydrogen production apparatus which concerns on this embodiment. It is a functional block diagram of the hydrogen production apparatus which concerns on this embodiment. It is a flowchart which shows an example of the rating determination process at the time of start-up of this embodiment. It is a schematic block diagram which showed the hydrogen production apparatus which concerns on the modification of this embodiment.

Hereinafter, an example of the hydrogen production apparatus according to the 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-boost water separation unit 50, a compressor 80, a post-pressurization water separation unit 52, and the like. It includes a buffer volume 54, a hydrogen purifier 90, and a control unit 70. This hydrogen production apparatus 10A produces hydrogen from a hydrocarbon raw material, and in the present embodiment, a case where a city gas containing methane as a main component is used as an example of the hydrocarbon raw material will be described.

As shown in FIG. 2, the multi-cylindrical reformer 12 has a plurality of cylindrical walls 21, 22, 23, 24 arranged in a plurality of manners. The plurality of tubular walls 21, 22, 23, 24 are formed in, for example, a cylindrical shape or an elliptical tubular shape. A combustion chamber 25 is formed inside the first cylindrical wall 21 from the inside among the plurality of tubular walls 21, 22, 23, and 24, and a burner 26 faces downward in the upper part of the combustion chamber 25. Is located in. The off-gas of the hydrogen refiner 90 is supplied as fuel to the burner 26 from the off-gas pipe 38. The multi-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 portion of the combustion chamber 25. The burner 26 is further connected to a raw material branch pipe 33A 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 obtained by mixing air with city gas is supplied to the burner 26 separately from the off-gas described later. Off-gas for combustion and / or city gas are supplied as needed.

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

Further, a first flow path 31 is formed between the second cylindrical wall 22 and the third tubular wall 23. The upper part of the first flow path 31 is formed as a preheating flow path 32, and the upper end of the preheating flow path 32 is for supplying a raw material supply pipe 33 for supplying city gas and water for reforming. Is connected to the water supply pipe 34 of the above. Further, a spiral member 35 is provided between the second tubular wall 22 and the third tubular wall 23, and the spiral member 35 forms the preheating flow path 32 in a spiral shape. There is. The raw material supply pipe 33 is an example of a flow path pipe.

City gas is supplied to the preheating flow path 32 from the raw material supply pipe 33, and water for reforming is further supplied from the water supply pipe 34. The city gas and the reforming water flow from the upper side to the lower side in the preheating flow path 32, and are heat-exchanged with the combustion exhaust gas through the second tubular wall 22 to vaporize the water. In the preheating flow path 32, a mixed gas is generated by mixing the city gas and the water for reforming the gas phase (steam).

Further, a reforming catalyst layer 36 is provided below the preheating flow path 32 in the first flow path 31, and the mixed gas generated in the preheating flow path 32 is supplied to the reforming catalyst layer 36. .. In the reforming catalyst layer 36, a reforming gas containing hydrogen as a main component is generated by a steam reforming reaction of the mixed gas by receiving heat from the combustion exhaust gas flowing through the combustion exhaust gas flow path 27. A thermometer 36A 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 36A is connected to the control unit 70 (see FIG. 3), and outputs the 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 tubular wall 24. The lower end of the second flow path 42 communicates with the lower end of the first flow path 31. The lower part of the second flow path 42 is formed as a reforming gas flow path 43, and the reforming gas discharge pipe 44 is connected to the upper end portion of the second flow path 42.

Further, a CO modification catalyst layer 45 is provided above the reformed gas flow path 43 in the second flow path 42, and the reformed gas generated in the reformed catalyst layer 36 is a reformed gas flow. After passing through the passage 43, it is supplied to the CO reforming catalyst layer 45. In the CO modification catalyst layer 45, carbon monoxide contained in the reformed gas reacts with water vapor 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 transformation catalyst layer 45, and a CO selective oxidation catalyst layer 47 is provided above the CO transformation catalyst layer 45 in the second flow path 42. ing. The CO selective oxidation catalyst layer 47 is not an essential configuration and may not be provided. The oxidant gas taken in through the oxidant gas supply pipe 46 and the reformed gas that has passed through the CO modification catalyst layer 45 are supplied to the CO selective oxidation catalyst layer 47. In the CO selective oxidation catalyst layer 47, carbon monoxide reacts with oxygen on a noble metal catalyst such as platinum or ruthenium and is converted into carbon dioxide, and carbon monoxide is removed. The reformed gas G1 in which carbon monoxide is reduced in the CO modified 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-boost water separation unit 50 are provided in this order. In the pre-pressurization water separation unit 50, condensed water (liquid phase) is stored in the lower part, reformed gas (gas) is stored in the upper part, and the gas and the liquid are separated. The downstream end of the reformed gas discharge pipe 44 is connected to the upper portion on the inlet side of the pre-boost water separation unit 50. Further, the upstream end of the connecting flow path pipe 60 is connected to the upper part (gas storage part) on the outlet side of the pre-pressurizing water separation part 50. A water recovery pipe 50A is connected to the bottom portion (liquid storage portion) of the pre-boost water separation portion 50. The reforming gas G1 is condensed and separated by cooling by heat exchange with the cooling water in the heat exchanger HE1. After the water is separated, the reformed gas G2 is sent to the connecting flow path pipe 60. The separated water is sent to the water recovery pipe 50A.

The connecting flow path pipe 60 is 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 part of the combustion chamber 25. It is branched into 64. The inlet side of the compressor 80 is connected to the downstream end of the first flow path pipe 62, and the first flow path pipe 62 is provided with the first valve V1. 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 V1 and the second valve V2 are connected to the control unit 70. The control unit 70 includes a CPU, a ROM, and a RAM, and is connected to each unit of the hydrogen production device 10A to control the operation of the hydrogen production device 10A. The first valve V1 and the second valve V2 are opening / closing valves, and the opening / closing is controlled by the control unit 70. The control unit 70 controls so that the first valve V1 is opened and the second valve V2 is closed when the reforming gas flowing into the hydrogen purifier 90 is rated. When it is not in the rated state, the first valve V1 is closed and the second valve V2 is controlled to be opened.

Here, the rated state means a state in which the concentration of hydrogen contained in the reforming gas sent out from the multi-cylindrical reformer 12 and flowing into the hydrogen refiner 90 is a predetermined value or more. When the reforming gas flowing into the hydrogen purifier 90 contains a large amount of impurities other than hydrogen, the impurities cannot be sufficiently adsorbed by the adsorbent, and the concentration of purified hydrogen does not satisfy the predetermined concentration. There is a possibility that the hydrogen purifier 90 will be overloaded.

In particular, immediately after the hydrogen production apparatus 10A is started, the temperature inside the multi-cylindrical reformer 12 may not have risen sufficiently, and the reaction for generating the reforming gas may not sufficiently proceed. The reformed gas produced in such a state contains a large amount of impurities other than hydrogen.

Therefore, as the concentration of hydrogen contained in the reforming 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, of hydrogen contained in the reforming gas). The ratio is 70% or more). Further, by a preliminary experiment or the like, the temperature range in the multi-cylinder reformer 12 when the reforming gas sent from the multi-cylinder reformer 12 satisfies the rated state is specified, and a threshold value ( For example, it is set as 600 ° C. or higher). In addition, an analyzer for analyzing the composition of the reformed gas may be provided in the connecting flow path 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 reforming gas was provided in the connecting flow path tube 60, and the flow rate of the reforming gas measured by the flow meter was measured by the thermometer provided in the reformer. The hydrogen concentration of the reforming gas is estimated based on the temperature and the relationship between the flow rate of the reforming gas and the temperature in the reformer and the hydrogen concentration, which have been specified in advance by experiments, etc., and based on the estimation result. May be determined.

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

A connecting flow path 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-boost water separation unit 50 with a pump and sends it to the connecting flow path pipe 66.

On the downstream side of the connecting flow path pipe 66, a heat exchange section HE2 and a boosted water separation section 52 are provided in this order. In the post-pressurization water separation unit 52, condensed water (liquid phase) is stored in the lower part, reformed gas (gas) is stored in the upper part, and the gas and the liquid are separated. The downstream end of the connecting flow path pipe 66 is connected to the upper portion on the inlet side of the boosted water separation section 52. Further, the upstream end of the connecting flow path pipe 68 is connected to the upper part (gas storage part) on the outlet side of the water separation part 52 after boosting. A water recovery pipe 52A is connected to the bottom portion (liquid storage portion) of the water separation portion 52 after boosting. The reforming gas G2 is condensed and separated by cooling by heat exchange with the cooling water in the heat exchanger HE2. After the water is separated, the reformed gas G3 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 connecting flow path pipe 68 is connected to the upper part (gas storage part) on the outlet side of the water separation part 52 after boosting. The downstream end of the connecting flow path 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 water separation unit 52 after boosting. A connecting flow path pipe 69 is connected to the outlet side of the buffer volume 54, and the downstream end of the connecting flow path pipe 69 is connected to the inlet side of the hydrogen purifier 90. From the buffer volume 54, the reformed gas G3 boosted to a predetermined pressure is supplied to the hydrogen purifier 90.

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

The water recovery pipes 50A and 52A and the external water supply unit 17 which 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 multi-cylindrical 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 multi-cylindrical reformer 12. The city gas supplied to the multi-cylinder reformer 12 is heated while being mixed with water for reforming in the preheating flow path 32 of the multi-cylinder reformer 12, and is supplied to the reforming catalyst layer 36. In the reforming catalyst layer 36, a reforming gas containing hydrogen as a main component is generated by a steam reforming reaction of the mixed gas by receiving heat from the combustion exhaust gas flowing through the combustion exhaust gas flow path 27. The reformed gas is supplied to the CO transformation catalyst layer 45 through the reformed gas flow path 43. In the CO modification catalyst layer 45, carbon monoxide contained in the reformed gas reacts with water vapor to be converted into hydrogen and carbon dioxide, and carbon monoxide is reduced.

Further, the reforming gas that has passed through the CO modification catalyst layer 45 is supplied to the CO selective oxidation catalyst layer 47 together with the oxidation gas (air) supplied from the oxidizing agent gas supply pipe 46, and carbon monoxide is oxygen on the noble metal catalyst. It reacts with and is converted to carbon dioxide, and carbon monoxide is removed. 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.
The CO selective oxidation catalyst layer 47 does not necessarily have to be used, and the hydrogen production apparatus 10A may be operated without supplying air from the oxidant gas supply pipe 46.

The reformed gas G1 flows into the pre-boost water separation unit 50 via 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 G2 from which water has been separated is sent to the connecting flow path pipe 60.

The control unit 70 performs the start-up rating determination procedure 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 open. The control unit 70 acquires the temperature measured by the thermometer 36A in step S12, and determines whether or not the reformed gas is in the rated state based on the acquired temperature in step S14. If it is determined that the rated state is reached, 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 G2 flows to the second flow path pipe 64 and is supplied to the burner 26. That is, when the reformed gas is not in the rated state, the reformed gas G2 sent out to the connecting flow path pipe 60 flows to the second flow path pipe 64, joins the off-gas pipe 38, and fuels the burner 26. And is used 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 procedure is completed.

By the procedure 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 G2 delivered to the connecting flow path pipe 60 flows to the first flow path pipe 62, is supplied to the compressor 80, and is compressed by the compressor 80. The compressed reformed gas G2 flows through the connecting flow path pipe 66 and flows into the water separation unit 52 after boosting. 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 connecting flow path pipe 68, temporarily stored in the buffer volume 54, and then supplied to the hydrogen purifier 90 via the connecting flow path pipe 69.

In the hydrogen purifier 90, the reforming 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, the off-gas containing impurities other than hydrogen from the reforming gas G3 flows through the off-gas pipe 38 and is supplied to the burner 26 of the multi-cylindrical reformer 12 as fuel.

Off gas is burned in the combustion chamber 25 of the multi-cylindrical reformer 12, and the combustion exhaust gas is discharged to the outside from the gas discharge pipe 28.

The water delivered to the water recovery pipes 50A and 52A is supplied to the multi-cylindrical reformer 12 as reformed water via the water treatment device 34A by driving the pump P1. The external water supply unit 17 newly supplies water corresponding to the amount of water required to be supplied from the outside to the multi-cylindrical reformer 12.

In the hydrogen production apparatus 10A of the present embodiment, the connecting flow path pipe 60 is branched, and the reformed gas G2 is flowed to the second flow path pipe 62 which is not supplied to the hydrogen purifier 90 at times other than the rated operation. Therefore, it is possible to prevent the reformed gas having a low hydrogen concentration from flowing into the hydrogen purifier 90.

Further, 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-boost 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-cylindrical reformer 12 and the inlet of the hydrogen purifier 90.

In the present embodiment, since the water is branched to the second flow path pipe 62 on the downstream side of the pre-boost water separation unit 50, the amount of water contained in the reformed gas is reduced, and the reformed gas having a high calorific value is used for combustion. Can be done. Furthermore, the separated water can be effectively reused. Further, in the present embodiment, since the reformed gas is branched to the second flow path pipe 62 on the upstream side of the compressor 80, the reformed gas that is not purified can be supplied to the burner 26 without being compressed, and the compressor 80 can be supplied. The load can be reduced.

Further, 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. Further, as shown in FIG. 5, the hydrogen production apparatus 10B may have the second flow path tube 64 opened to the outside.

Further, in the present embodiment, the hydrogen production apparatus provided with the compressor 80 has been described, but the present invention may be applied to the hydrogen production apparatus without the compressor 80, and the compressor is a multi-cylinder reformer. It may be applied to the hydrogen production apparatus arranged on the upstream side of the pawn device 12.

In this embodiment, the process at the time of starting the hydrogen production apparatus 10A has been described, but the present invention is not limited to this. Even if the measured value of the thermometer 36A is constantly monitored and it is determined that the temperature inside the multi-cylindrical reformer 12 does not meet the rated state, the reforming gas does not flow into the hydrogen refiner 90. good. As a result, 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 is sent out due to an abnormality in operation or the like. ..

10A, 10B hydrogen production equipment, 12 multi-cylinder reformer (reformer)
25 Combustion chamber (combustion part), 26 Burner (combustion part)
50 Pre-boost water separation section (water separation section)
62 1st flow path pipe (1st flow path), 64 2nd flow path tube (2nd flow path)
70 Control unit (switching unit)
80 Compressor 90 Hydrogen Purifier V1 1st valve (switching part)
V2 2nd valve (switching part)

Claims (5)

A reformer that reforms raw materials to generate reformed gas containing hydrogen,
A hydrogen purifier that separates the reformed gas into impurities and hydrogen to purify hydrogen, and
A first flow path for supplying the reforming gas delivered from the reformer to the hydrogen refiner, and
A second flow path that guides the reformed gas sent from the reformer to a place different from that of the hydrogen refiner.
A switching unit that switches the delivery destination flow path of the reformed gas between the first flow path and the second flow path,
Equipped with
When the hydrogen concentration of the reformed gas on the upstream side of the switching unit is in the rated state, the switching unit switches the delivery destination flow path of the reformed gas to the first flow path, and the reformed gas. When the hydrogen concentration of the reformed gas is not in the rated state, the delivery destination flow path of the reformed gas is switched to the second flow path .
Hydrogen production equipment. It has a water separation unit that separates water from the reformed gas.
The hydrogen production apparatus according to claim 1, wherein the second flow path is branched from the first flow path on the downstream side of the water separation portion. The reformer has a combustion unit that burns combustion gas.
The hydrogen production apparatus according to claim 1 or 2, wherein the second flow path supplies the reformed gas to the combustion unit. The hydrogen production apparatus according to claim 1 or 2, wherein the second flow path sends the reformed gas to the outside. A compressor for compressing the reforming gas is provided between the reformer and the hydrogen purifier, and the second flow path is branched from the first flow path on the upstream side of the compressor. The hydrogen production apparatus according to any one of claims 1 to 4.

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