JP2020100540A - Hydrogen producing apparatus - Google Patents

Abstract

To provide a hydrogen producing apparatus improved in thermal efficiency in the whole apparatus.SOLUTION: In a hydrogen producing apparatus 10, a compressor 80 is cooled with a refrigerant which flows through a refrigerant circulating flow passage 112 of a cooling mechanism 110. The refrigerant heated by cooling the compressor 80 is cooled through heat exchange with modifying water by using a heat exchanger HE4. After additionally cooled with a radiator 116, the refrigerant is supplied to the compressor 80 again to cool the compressor 80. Meanwhile, the modifying water heated through the heat exchange with the refrigerant in HE4 is supplied to a modifier 12 through a modifying water-supplying pipe 34 and is heated, thereby being gasified and then being a mixed gas formed by the mixture with a city gas. Accordingly, thermal efficiency of the hydrogen producing apparatus 10 is improved.SELECTED DRAWING: Figure 1

Description

The present invention relates to a hydrogen production apparatus, and more particularly to a hydrogen production apparatus that reforms a hydrocarbon raw material to produce hydrogen.

Patent Document 1 describes a hydrogen production device that produces a reformed gas by supplying steam and a raw material hydrocarbon to a reformer to perform steam reforming.

JP, 2001-261306, A

Such hydrogen production equipment purifies product hydrogen by separating the reformed gas into product hydrogen and impurities (off gas) in a hydrogen purifier, but reforms it in a compressor before supplying it to the hydrogen purifier. By compressing the gas (increasing the pressure), the purity of hydrogen purified by the hydrogen purifier is improved.

By the way, since the compressor itself is heated by its driving, it is cooled by a circulation type refrigerant or the like. When the heat of the refrigerant heated by the compressor is discharged to the outside, there is room for improvement in terms of the thermal efficiency of the entire device.

On the other hand, the water supplied to the reformer is turned into steam by heating and used for steam reforming of hydrocarbons. However, when this water is heated by the combustion of the fuel supplied from the outside of the device, there is room for improvement in terms of the thermal efficiency of the entire device.

An object of the present invention is to provide a hydrogen production device with improved thermal efficiency of the entire device.

The hydrogen producing apparatus according to claim 1, wherein a hydrocarbon and water are supplied as raw materials, the reformer reforms the hydrocarbon to generate a reformed gas containing hydrogen as a main component, and the reformer. A boosting means connected to the boosting means for boosting the reformed gas; a hydrogen purifier connected to the boosting means for separating the reformed gas into product hydrogen and off-gas as impurities to purify the product hydrogen. Heat recovery means for recovering the heat of the means by the water supplied to the reformer.

According to this hydrogen production device, the reformed gas generated in the reformer is compressed by the pressure increasing means and supplied to the hydrogen purifier to be separated into product hydrogen and off-gas, and the product hydrogen is purified.

By the way, the pressure increasing means raises the temperature by compressing the reformed gas. The heat of the pressurizing means is recovered by the heat recovery means into water supplied to the reformer as a raw material (hereinafter referred to as “reforming water”). That is, the reforming water is heated.

As described above, since the reforming water is heated by the heat of the pressure increasing means before being supplied to the reformer, the amount of heat for heating the reforming water by other means to generate the reformed gas is reduced. It

That is, since at least part of the heat of the booster is used for heating the reforming water without being discharged to the outside, the thermal efficiency of the entire hydrogen production apparatus is improved.

The hydrogen production apparatus according to claim 2 is the hydrogen production apparatus according to claim 1, wherein the heat recovery means is provided on a refrigerant flow path through which the refrigerant that has cooled the pressure increasing means flows, and on the refrigerant flow path. A first heat exchanger for exchanging heat between water supplied to the quality control device and the refrigerant.

In this hydrogen production device, the pressure rising means compresses the reformed gas to raise the temperature, so that it is cooled by the refrigerant. The refrigerant is heated by cooling the pressure increasing means, and flows in the refrigerant flow path in a state of being heated.

A first heat exchanger is arranged on this refrigerant channel. Therefore, the refrigerant heated in the first heat exchanger and the reforming water are heat-exchanged with each other to heat the reforming water.

As described above, the reforming water is heated by exchanging heat with the refrigerant whose temperature is raised by cooling the pressurizing means before being supplied to the reformer, so that the reforming gas is reformed to generate the reformed gas. The amount of heat for heating the water by other means is reduced.

That is, since at least a part of the heat of the booster is used for heating the reforming water via the refrigerant without being discharged to the outside, the thermal efficiency of the entire hydrogen production apparatus is improved.

A hydrogen producing apparatus according to a third aspect is the hydrogen producing apparatus according to the second aspect, wherein the refrigerant channel is a circulation channel.

In this hydrogen production device, the refrigerant that cools the pressurizing means is a circulation type, and the refrigerant that has been heated by the heat exchange with the reforming water in the first heat exchanger is cooled. Therefore, other means for cooling the heated refrigerant is unnecessary, or the amount of heat for cooling the refrigerant by other means is reduced, and the thermal efficiency of the entire hydrogen production apparatus is improved.

The hydrogen production apparatus according to claim 4 is the hydrogen production apparatus according to claim 1, wherein the heat recovery means is provided in the pressure increasing means, and water supplied to the reformer and the pressure increasing means exchange heat. Is a second heat exchanger.

In this hydrogen production device, the pressure rising means compresses the reformed gas to raise the temperature. The pressurizing means is provided with a second heat exchanger that exchanges heat with the reforming water. Therefore, the booster is cooled by exchanging heat with the reforming water in the second heat exchanger.

On the other hand, the reforming water is heated by being heat-exchanged with the pressure increasing means in the second heat exchanger and supplied to the reformer.

In this way, since the pressure increasing means and the reforming water are heat-exchanged in the second heat exchanger, another cooling means for cooling the pressure increasing means becomes unnecessary.

Further, since the reforming water is heated by exchanging heat with the pressure increasing means before being supplied to the reformer, the amount of heat for heating the reforming water by other means to generate the reformed gas is reduced. To be done.

That is, the thermal efficiency of the hydrogen production device can be improved.

Since the hydrogen production device according to the invention described in claims 1 to 4 has the above configuration, the thermal efficiency of the entire device can be improved.

It is a schematic block diagram which showed the hydrogen production apparatus which concerns on 1st Embodiment of this invention. It is a sectional view showing a multi-cylinder type reformer concerning a 1st embodiment of the present invention. It is a schematic block diagram which showed the hydrogen production apparatus which concerns on 2nd Embodiment of this invention.

[First Embodiment]
An example of the hydrogen production device according to the first embodiment of the present invention will be described with reference to FIGS. 1 and 2.

<Hydrogen production equipment>
As shown in FIG. 1, the hydrogen production apparatus 10 includes a multi-cylinder reformer (hereinafter, may be referred to as a “reformer”) 12 that produces a reformed gas obtained by steam reforming hydrocarbons (city gas). A compressor 80 for compressing the reformed gas, and a hydrogen purifier 90 for purifying hydrogen gas by removing impurities from the compressed reformed gas. The hydrogen production device 10 includes a pre-pressurization water separation unit 50, a post-pressurization water separation unit 60, which separates and removes water from the reformed gas on the upstream side and the downstream side of the compressor 80, respectively, and a reformer 12 to be described later. And a combustion exhaust gas water separation unit 70 for separating and removing water from the combustion exhaust gas.

The hydrogen production device 10 produces hydrogen from a hydrocarbon raw material, and in the present embodiment, a case where city gas containing methane as a main component is used as an example of the hydrocarbon raw material will be described.

(Multiple cylinder reformer)
As shown in FIG. 2, the multi-tubular reformer 12 includes a plurality of tubular walls 21, 22, 23, 24 (hereinafter, may be referred to as “cylindrical walls 21-24”) arranged in multiple layers. Have The plurality of cylindrical walls 21 to 24 are formed in, for example, a cylindrical shape or an elliptic cylindrical shape. A combustion chamber 25 is formed inside the first cylindrical wall 21 from the inner side among the plurality of cylindrical walls 21 to 24, and a burner 26 is arranged downward on the combustion chamber 25. There is. The multi-tubular reformer 12 is an example of a reformer.

Further, an air supply pipe 40 for supplying combustion air from the outside is connected to the upper end of the combustion chamber 25. A raw material branch pipe 33A branched from a raw material supply pipe 33 for supplying city gas from the outside is further connected to the burner 26. An air branch pipe 40A branched from the air supply pipe 40 is connected to the raw material branch pipe 33A. Therefore, the burner 26 is configured to be supplied with gas in which city gas is mixed with air.

A combustion exhaust gas passage 27 is formed between the first tubular wall 21 and the second tubular 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 exhausting gas is connected to an upper end portion of the combustion exhaust gas passage 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 sent to the combustion exhaust gas water separation unit 70 through the gas discharge pipe 28.

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

City gas can be supplied to the preheating channel 32 from the raw material supply pipe 33, and further reforming water can be supplied from the reforming water supply pipe 34. The city gas and the reforming water flow from the upper side to the lower side in the preheating channel 32, and are heat-exchanged with the combustion exhaust gas 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 vapor phase.

A 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. It is a configuration. The reforming catalyst layer 36 receives heat from the combustion exhaust gas flowing through the combustion exhaust gas passage 27 and undergoes a steam reforming reaction of the mixed gas to generate a reformed gas containing hydrogen as a main component.

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 communicates with the lower end of the first flow path 31. A lower portion of the second flow passage 42 is formed as a reformed gas flow passage 43, and a reformed gas discharge pipe 44 is connected to an upper end portion of the second flow passage 42.

Further, a CO shift catalyst layer 45 is provided above the reformed gas passage 43 in the second passage 42, and the reformed gas generated in the reformed catalyst layer 36 is the reformed gas passage. After passing through 43, the CO conversion catalyst layer 45 is supplied. In the CO shift catalyst layer 45, carbon monoxide contained in the reformed gas reacts with steam to be converted into hydrogen and carbon dioxide (aqueous shift reaction), and carbon monoxide in the reformed gas can be 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. The oxidant gas (for example, air) 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, carbon monoxide reacts with oxygen and is converted into carbon dioxide on a noble metal catalyst such as platinum or ruthenium, and carbon monoxide can be 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.

As shown in FIG. 1, the reformed gas generated in the multi-tubular reformer 12 passes through the pre-pressurization water separation unit 50, the compressor 80, the post-pressurization water separation unit 60, and the hydrogen purifier 90 in this order. Flowing That is, in the gas flow direction, from the upstream side to the downstream side, the multi-tubular reformer 12, the pre-pressurization water separation unit 50, the compressor 80, the post-pressurization water separation unit 60, and the hydrogen purifier 90 are arranged in this order. It is arranged.

(Water separator before pressurization)
The downstream end of the reformed gas discharge pipe 44, into which the reformed gas G1 flows from the multi-cylinder reformer 12, is connected to the pre-pressurization water separation unit 50. A water recovery pipe 59 is connected to the bottom of the pre-pressurization water separation unit 50, and a communication channel pipe 56 is connected to the top of the pre-pressurization water separation unit 50. The reformed gas G1 is condensed and separated in the heat exchanger HE1 arranged in the reformed gas discharge pipe 44 upstream of the pre-pressurized water separation unit 50 by cooling by heat exchange with the refrigerant, and the pre-pressurized water is separated. Water (liquid phase) can be stored under the separation unit 50. The water (liquid phase) is sent to the water recovery pipe 59. The reformed gas G2 after the water is condensed is sent to the communication flow path pipe 56. The heat exchanger HE1 is, for example, a chiller.

(Compressor)
In the compressor 80, there are provided a communication flow passage pipe 56 through which the reformed gas G2 from the pre-pressurization water separation unit 50 flows, and a communication flow passage pipe 66 through which the reformed gas G2 supplied to the post-pressurization water separation unit 60 flows. It is connected. The compressor 80 is capable of compressing the reformed gas G2 supplied from the pre-pressurization water separation unit 50 and supplying it to the post-pressurization water separation unit 60.

Further, the compressor 80 is provided with a cooling mechanism 110, and the compressor 80 having a temperature raised by the compression operation is cooled by the cooling mechanism 110. The compressor 80 corresponds to the “pressurizing means”.

(Cooling mechanism)
The cooling mechanism 110 has a refrigerant circulation flow path 112 provided so that a refrigerant that cools the compressor 80, for example, cooling water circulates. A heat exchanger HE4 capable of exchanging heat with the reforming water in the reforming water supply pipe 34, a pump 114 for circulating a refrigerant, and a radiator 116 are arranged on the refrigerant circulation flow path 112.

The radiator 116 is provided with a fan 118 for cooling the refrigerant having a high temperature due to heat exchange with the compressor 80.

That is, the cooling mechanism 110 cools the refrigerant whose temperature has risen by cooling the compressor 80 by heat exchange with the reforming water in the heat exchanger HE4 and further cools it in the radiator 116, and then again the compressor 80. And is configured to cool the compressor 80.

The heat exchanger HE4 and the refrigerant circulation passage 112 correspond to "heat recovery means". Further, the heat exchanger HE4 and the refrigerant circulation flow passage 112 correspond to the "first heat exchanger" and the "refrigerant flow passage", respectively.

(Water separation unit after pressurization)
To the post-pressurization water separation unit 60, a downstream end of a communication flow pipe 66 that allows the reformed gas G2 to flow from the compressor 80 is connected. A water recovery pipe 69 is connected to the bottom of the post-pressurization water separation unit 60, and a communication channel pipe 68 is connected to the top of the post-pressurization water separation unit 60. The reformed gas G2 is condensed and separated in the heat exchanger HE2 arranged in the communication flow path pipe 66 upstream of the post-pressurization water separation unit 60 by cooling by heat exchange with the refrigerant, and the post-pressurization water separation is performed. Water (liquid phase) can be stored under the portion 60. The water (liquid phase) is sent to the water recovery pipe 69. The reformed gas G3 after the water is condensed is sent to the communication flow path pipe 68. The heat exchanger HE2 is, for example, a chiller.

(Hydrogen refiner)
In the hydrogen purifier 90, the downstream end of the communication flow pipe 68 through which the reformed gas G3 from the post-pressurization water separation unit 60 flows, the upstream end of the hydrogen supply pipe 92 to which purified hydrogen is delivered, and the hydrogen purification The upstream end of the off-gas recirculation pipe 100 to which the off-gas separated by the vessel 90 is delivered is connected.

As the hydrogen purifier 90, a PSA device is used as an example. The hydrogen purifier 90 includes a pair of adsorption tanks, one adsorption tank performs an adsorption step of adsorbing impurities on the adsorbent, and the other adsorption tank performs a desorption step of desorbing impurities adsorbed on the adsorbent, Next, the desorption process is performed in one adsorption tank, and the adsorption process is performed in the other adsorption tank. By repeating this periodically, the reformed gas G3 is continuously separated into hydrogen and impurities containing carbon monoxide (off gas OG), and hydrogen is purified. The purified hydrogen is sent to the hydrogen supply pipe 92, stored in a tank (not shown), or can be sent to the hydrogen supply line.

The off gas of the hydrogen purifier 90 can be supplied to the burner 26 provided in the combustion chamber 25 of the reformer 12 via the off gas recirculation pipe 100.

<Off gas tank>
An offgas tank 102 is provided on the offgas reflux pipe 100 that connects the hydrogen purifier 90 and the burner 26 of the reformer 12. Therefore, the off-gas supplied from the hydrogen purifier 90 is temporarily stored in the off-gas tank 102, leveled in flow rate and composition, and then supplied to the burner 26 of the reformer 12.

(Combustion exhaust gas water separation section)
A downstream end of a gas exhaust pipe 28 that guides the combustion exhaust gas from the combustion exhaust gas flow path 27 of the reformer 12 is connected to the combustion exhaust gas water separation unit 70. A water recovery pipe 78 is connected to the bottom of the combustion exhaust gas water separation unit 70, and a gas discharge pipe 76 is connected to the upper portion of the combustion exhaust gas water separation unit 70. The combustion exhaust gas discharged from the combustion chamber 25 is separated and condensed in the heat exchanger HE3 arranged in the gas discharge pipe 28 upstream of the combustion exhaust gas water separation unit 70 by cooling by heat exchange with the refrigerant. Water (liquid phase) can be stored under the combustion exhaust gas water separation unit 70. The water (liquid phase) is sent to the water recovery pipe 78. The combustion exhaust gas after the water is condensed is discharged from the gas discharge pipe 76 into the outside air. The heat exchanger HE3 is, for example, a chiller.

(Supply pipe for reforming)
The downstream ends of the water recovery pipes 59, 69, and 78 are connected to the reforming water supply pipe 34. The reforming water supply pipe 34 is provided with a water treatment device (ion exchange resin) 34A for removing dissolved ionic components. The external water supply unit 17 is connected to the reforming water supply pipe 34. For example, pure water or city water is supplied from the external water supply unit 17 to the reforming water supply pipe 34.

Further, the reforming water supply pipe 34 is provided with a pump P1. The water separated by the pre-pressurization water separation unit 50, the post-pressurization water separation unit 60, the combustion exhaust gas water separation unit 70, or the water supplied from the external water supply unit 17 is sent to the multi-tubular reformer 12 by the pump P1. It is a configuration to be supplied.

Further, the heat exchanger HE4 is arranged on the pump P1 of the reforming water supply pipe 34, on the downstream side of the water treatment device 34A, and on the most reformer 12 side. That is, in the heat exchanger HE4, the reforming water supplied to the reformer 12 is preheated by exchanging heat with the heated refrigerant flowing through the refrigerant circulation passage 112.

(Action)
Next, the operation of the hydrogen production device 10 will be described.

As shown in FIG. 2, city gas is supplied from the raw material supply pipe 33, and reforming water is supplied from the reforming water supply pipe 34 to the preheating passage 32 of the multi-tubular reformer 12, respectively. The city gas supplied to the multi-cylinder reformer 12 is heated while being mixed with the reforming water in the preheating passage 32 of the multi-cylinder reformer 12 to be a mixed gas, which is supplied to the reforming catalyst layer 36. To be done. In the reforming catalyst layer 36, heat from the combustion exhaust gas flowing through the combustion exhaust gas passage 27 is received, and a reforming gas containing hydrogen as a main component is generated from the mixed gas by the steam reforming reaction. This reformed gas is supplied to the CO shift catalyst layer 45 through the reformed gas flow path 43. In the CO conversion catalyst layer 45, carbon monoxide contained in the reformed gas reacts with steam to be converted into hydrogen and carbon dioxide, and carbon monoxide is reduced.

Further, the reformed gas that has passed through the CO conversion catalyst layer 45 is supplied to the CO selective oxidation catalyst layer 47 together with the oxidant gas (air) supplied from the oxidant gas supply pipe 46, and carbon monoxide is generated on the noble metal catalyst. It reacts with oxygen and is converted to carbon dioxide, which removes 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.

At this time, in the combustion chamber 25 of the multi-cylinder reformer 12, the burner 26 combusts a gas obtained by mixing the city gas and air supplied from the raw material branch pipe 33A and the air branch pipe 40A. The combustion exhaust gas is supplied from the combustion chamber 25 to the combustion exhaust gas water separation unit 70 via the combustion exhaust gas passage 27 and the gas exhaust pipe 28. As shown in FIG. 1, the water (steam) contained in the combustion exhaust gas is cooled and condensed by heat exchange in the heat exchanger HE3, the water is stored in the combustion exhaust gas water separation unit 70, and the water is recovered in the water recovery pipe 78. Sent out. The combustion exhaust gas from which the water has been separated is discharged from the gas discharge pipe 76 into the outside air.

On the other hand, as shown in FIG. 1, the reformed gas G1 of a predetermined quality delivered from the reformer 12 is supplied to the pre-pressurized water separation unit 50 via the reformed gas discharge pipe 44. In the pre-pressurization water separation unit 50, water condensed by cooling by heat exchange in the heat exchanger HE1 is stored and sent to the water recovery pipe 59. The reformed gas G2 from which the water has been separated is supplied to the compressor 80 from the communication flow path pipe 56 and is compressed by the compressor 80.

At this time, although the temperature of the compressor 80 is raised by driving (compressing operation), the compressor 80 is sufficiently cooled by the refrigerant flowing through the refrigerant circulation passage 112 of the cooling mechanism 110, and the performance is maintained. On the other hand, the refrigerant heated by the cooling of the compressor 80 is cooled by heat exchange with the reforming water in the heat exchanger HE4 arranged on the refrigerant circulation passage 112, and further cooled by the radiator 116, It is supplied to the compressor 80 and is again used for cooling the compressor 80.

The reformed gas G2 compressed by the compressor 80 is supplied from the communication flow path pipe 66 to the post-pressurized water separation unit 60. In the post-pressurization water separation unit 60, the water condensed by cooling by heat exchange in the heat exchanger HE2 is stored and sent to the water recovery pipe 69. The reformed gas G3 from which the water has been separated is supplied to the hydrogen purifier 90 from the communication flow path pipe 68.

The water sent from the pre-pressurization water separation unit 50, the post-pressurization water separation unit 60, and the combustion exhaust gas water separation unit 70 to the water recovery pipes 59, 69, and 78 is returned to the reforming water supply pipe 34. By driving the pump P1, the reforming water is supplied from the reforming water supply pipe 34 to the multi-tubular reformer 12 as reforming water.

At this time, the reforming water flowing through the reforming water supply pipe 34 is heated by heat exchange with the refrigerant whose temperature has been raised in the heat exchanger HE4, and then supplied to the reformer 12. Therefore, the amount of heat required for the reforming water to be mixed gas (vaporized) with the city gas in the preheating passage 32 of the reformer 12 is reduced.

On the other hand, in the hydrogen purifier 90, the pressure swing method is adopted, and impurities other than hydrogen are adsorbed by the adsorbent in one of the pair of adsorption tanks, and the impurities adsorbed by the adsorbent are desorbed in the other adsorption tank. ing. In the hydrogen purifier 90, the adsorption step and the desorption step are repeated in each adsorption tank at a constant cycle to continuously separate hydrogen and impurities from the reformed gas G3 to purify hydrogen.

Hydrogen as a product purified by the hydrogen purifier 90 is sent to the hydrogen supply pipe 92, stored in a tank (not shown), or sent to the hydrogen supply line.

On the other hand, the offgas OG discharged from the hydrogen purifier 90 is supplied to the reformer 12 via the offgas reflux pipe 100. That is, after being temporarily stored in the offgas tank 102 provided on the offgas recirculation pipe 100, it is supplied to the burner 26 of the reformer 12.

As described above, in the hydrogen production device 10, the refrigerant which has been heated for cooling the compressor 80 in the heat exchanger HE4 and the reforming water are heat-exchanged with each other, so that the refrigerant of the cooling mechanism 110 which is a refrigerant circulation type is cooled. Since the cooling and the heating of the reforming water are performed, the thermal efficiency of the hydrogen production device 10 can be improved.

In the refrigerant circulation type cooling mechanism 110, since the refrigerant is cooled by heat exchange with the reforming water in the heat exchanger HE4, the load on the radiator 116 and the fan 118 for cooling the refrigerant should be reduced. You can

When the heat exchange amount (cooling amount of the refrigerant) in the heat exchanger HE4 is sufficiently large, the radiator 116 and the fan 118 can be omitted.

Further, since the reforming water heated in the preheat passage 32 of the reformer 12 is heated in the heat exchanger HE4 before being supplied to the reformer 12, the preheat passage 32 of the reformer 12 is heated. Thus, the amount of heat required to vaporize the reforming water is suppressed.

In particular, when a part of the reforming water is vaporized by heating in the heat exchanger HE4, the refrigerant can be further cooled by the vaporization heat.

Further, since the refrigerant of the cooling mechanism 110 is cooled by heat exchange with the reforming water in the heat exchanger HE4, the compressor 80 can be sufficiently cooled by the refrigerant and the performance of the compressor 80 can be maintained.

[Second Embodiment]
A hydrogen production apparatus 200 according to the second embodiment of the present invention will be described with reference to FIG. The same components as those in the first embodiment are designated by the same reference numerals, and detailed description thereof will be omitted. Further, the hydrogen production apparatus 200 is different only in that the cooling mechanism 110 of the hydrogen production apparatus 10 is changed to the heat exchanger HE5, and therefore only the configuration and operation regarding the relevant portion will be described, and the same operation and effect as those of the first embodiment will be described. Will not be described in detail.

(Constitution)
As shown in FIG. 3, in the hydrogen production device 200, the heat exchanger HE5 is provided on the reforming water supply pipe 34. The heat exchanger HE5 is formed in a water jacket type on the outer periphery of the compressor 80, and the heat of the reforming water and the compressor 80 is exchanged.

That is, in the heat exchanger HE5, the reforming water and the compressor 80 are heat-exchanged to heat the reforming water and cool the compressor 80. The heat exchanger HE5 corresponds to “heat recovery means” and “second heat exchanger”.

(Action)
In the hydrogen production device 200, the compressor 80, which has been heated by driving, is cooled by heat exchange with the reforming water in the heat exchanger HE5.

Further, in the reforming water supply pipe 34, after the reforming water is heated by heat exchange with the compressor 80 in the heat exchanger HE5, it is supplied to the preheating passage 32 of the reformer 12 and heated. , Mixed gas with city gas.

Thus, in the hydrogen production device 200, the heat exchanger HE5 exchanges heat between the compressor 80 and the reforming water, whereby the compressor 80 is cooled and the reforming water is heated. Therefore, the thermal efficiency of the hydrogen production device 200 can be improved.

In particular, in the heat exchanger HE5, the compressor 80 and the reforming water directly exchange heat without passing through the refrigerant, so the efficiency of heat exchange is improved, and the thermal efficiency of the hydrogen production device 200 is further improved.

Further, since it is sufficient to provide the water jacket type heat exchanger HE5 to cool the compressor 80, the configuration of the hydrogen production apparatus 200 is simplified.

[Other]
In each of the hydrogen producing devices 10 and 200, the reformer 12 is a multi-cylinder type reformer, but is not limited to this. It is only necessary that the city gas can be reformed into a reformed gas containing hydrogen as a main component.

Further, in the hydrogen production apparatuses 10 and 200, the case where the hydrogen purifier 90 is the PSA apparatus has been described, but the hydrogen purifier 90 is not limited to this as long as hydrogen can be purified from the reformed gas G3.

Further, the cooling mechanism 110 of the hydrogen production apparatus 10 is of a refrigerant circulation type in which a refrigerant circulates, but may be a refrigerant non-circulation type in which a refrigerant does not circulate. In this case, the heat exchanger HE4 may be arranged on the downstream side of the compressor 80 in the refrigerant passage. Even in this case, since the reforming water can be heated by the heat of the refrigerant (compressor 80), the thermal efficiency of the entire hydrogen production apparatus 10 is improved.

10, 200 Hydrogen production device 12 Multiple cylinder reformer (reformer)
80 Compressor (pressurizing means)
90 Hydrogen purifier 112 Refrigerant circulation flow path (heat recovery means, refrigerant flow path)
HE4 heat exchanger (heat recovery means, first heat exchanger)
HE5 heat exchanger (heat recovery means, second heat exchanger)

Claims (4)

Hydrocarbon and water are supplied as raw materials, a reformer for reforming the hydrocarbon to produce a reformed gas containing hydrogen as a main component,
A pressure-increasing unit connected to the reformer and increasing the pressure of the reformed gas;
A hydrogen purifier that is connected to the pressure increasing means and separates the reformed gas into product hydrogen and off-gas that is an impurity to refine the product hydrogen.
Heat recovery means for recovering the heat of the pressurizing means with water supplied to the reformer;
Hydrogen production device equipped with. The heat recovery means, a refrigerant flow path through which the refrigerant that has cooled the pressure increasing means flows,
A first heat exchanger provided on the refrigerant flow path, in which water supplied to the reformer and the refrigerant exchange heat;
The hydrogen production apparatus according to claim 1, further comprising: The hydrogen production device according to claim 2, wherein the refrigerant channel is a circulation channel. 2. The hydrogen production device according to claim 1, wherein the heat recovery means is a second heat exchanger provided in the pressure increasing means and exchanging heat between the water supplied to the reformer and the pressure increasing means.