JP6553273B1 - Hydrogen production equipment - Google Patents

Abstract

The present invention provides a hydrogen production apparatus in which the apparatus is miniaturized while ensuring the cooling capacity of reformed gas. In a hydrogen production apparatus 10, since a reformed gas G1 is cooled by a heat exchanger HE1 and then supplied to the chiller 100, the reformed gas cooled by the chiller 100 is set to a relatively low temperature. For this reason, compared with the case where the reformed gas supplied to the compressor 80 is cooled only by the chiller, the cooling capacity of the chiller 100 can be relatively small, and the refrigerant circulation type chiller 100 can be downsized. be able to. Moreover, since the heat exchanger HE1 is a refrigerant non-circulation type, the refrigerant used for the heat exchanger HE1 is supplied from the outside of the hydrogen production apparatus, and is discharged to the outside of the hydrogen production apparatus after heat exchange. That is, the increase in the size of the hydrogen production apparatus due to the addition of the heat exchanger HE1 is suppressed. Therefore, compared with the case where the reformed gas introduced into the compressor 80 is cooled only by the chiller, the hydrogen production apparatus 10 can be reduced in size. [Selection] Figure 1

Description

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

  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 (hydrogen purifier). ing. At this time, in order to supply the reformed gas to the PSA apparatus at a pressure required for the adsorption reaction in the PSA apparatus, a compressor that compresses the reformed gas is provided upstream of the PSA apparatus.

  Further, on the flow path of the reformed gas, a chiller is provided on the upstream side of the compressor. This is because the reformed gas supplied to the compressor is cooled to condense the water vapor, remove the water vapor from the reformed gas, and then supply the reformed gas to the compressor, whereby the gas supplied to the compressor It is excellent in reducing the flow rate and reducing the load on the compressor.

JP 2017-88490 A

  However, if cooling of the reformed gas supplied to the compressor (condensation of water vapor) is performed only by the chiller, there is a disadvantage that the cooling load of the chiller is large and the chiller for circulating the refrigerant is enlarged.

  That is, there is room for improvement in terms of downsizing of the hydrogen production apparatus.

  An object of the present invention is to provide a hydrogen production apparatus in which the apparatus can be miniaturized while securing the ability to cool a reformed gas.

  The hydrogen production apparatus according to claim 1, wherein a hydrocarbon is supplied as a raw material from a hydrocarbon source, and the reformer reforms the hydrocarbon to generate a reformed gas mainly composed of hydrogen; A hydrogen purification unit that is connected to the reformer and boosts the reformed gas, and is connected to the booster unit and separates the reformed gas into product hydrogen and an off-gas that is an impurity to purify product hydrogen. A refrigerant non-circulating first heat exchanger that is provided on a reformed gas flow path connecting the reformer and the pressure increasing means, and is cooled by heat exchange of the reformed gas with the refrigerant, A refrigerant that is provided on the reformed gas flow path downstream of the first heat exchanger and that is cooled by the heat exchange of the reformed gas with the refrigerant and the water vapor contained in the reformed gas is condensed. And a circulation type second heat exchanger.

  In this hydrogen production apparatus, the first heat exchanger and the second heat exchanger are disposed from the upstream side on the reformed gas flow path in which the reformed gas flows from the reformer toward the pressurizing means. That is, the high temperature reformed gas generated by the reformer is cooled by heat exchange with the refrigerant in the first heat exchanger, and then cooled by heat exchange with the refrigerant in the second heat exchanger. The steam contained in the reformed gas is condensed and removed, and is supplied to the pressure raising means.

  That is, since the reformed gas is supplied to the second heat exchanger after being cooled by the first heat exchanger, the reformed gas supplied to the second heat exchanger has a relatively low temperature. For this reason, the cooling load of the second heat exchanger is relatively reduced as compared with the case where the reformed gas supplied to the pressure raising means is cooled only by the second heat exchanger.

  That is, the refrigerant circulation type second heat exchanger can be miniaturized.

  The first heat exchanger is a non-circulating refrigerant type in which the refrigerant is supplied from the outside of the hydrogen production device and the heat-exchanged refrigerant is discharged to the outside of the hydrogen production device. Therefore, the enlargement of the hydrogen production apparatus due to the addition of the first heat exchanger is suppressed.

  As a result, compared to the case where the reformed gas introduced to the pressure raising means is cooled only by the second heat exchanger, the hydrogen production apparatus can be miniaturized while securing a predetermined cooling capacity.

  The hydrogen production apparatus according to claim 2 is the hydrogen production apparatus according to claim 1, wherein the refrigerant used in the first heat exchanger is industrial water.

  In this hydrogen production apparatus, if industrial water is used as the refrigerant of the first heat exchanger, the first heat exchanger can be easily installed in the hydrogen production apparatus simply by connecting the industrial water supply source and the first heat exchanger. can do. That is, the hydrogen production apparatus can be miniaturized while securing a predetermined cooling capacity with a simple configuration.

  The industrial water includes not only industrial water supplied from industrial water supply, but also water supplied from wells, seas, rivers, etc., water supplied from middle water, and the like.

  Since the hydrogen production apparatus according to the first and second aspects of the present invention has the above-described configuration, it is possible to achieve downsizing of the apparatus while ensuring the cooling ability of the reformed gas.

It is a schematic block diagram showing a hydrogen production device concerning one embodiment. It is sectional drawing which showed the multi-cylinder type | mold reformer which concerns on one Embodiment.

  An example of a hydrogen production apparatus according to an 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 sometimes referred to as “reformer”) 12 that generates a reformed gas obtained by steam reforming from a hydrocarbon (city gas). And a hydrogen purifier 90 that purifies hydrogen gas by removing impurities from the compressed reformed gas. In addition, the hydrogen production apparatus 10 includes a pre-pressurization water separation unit 50 and a post-pressurization water separation unit 60 that separate and remove moisture from the reformed gas on the upstream side and the downstream side of the compressor 80, respectively. A combustion exhaust gas water separation unit 70 for separating and removing moisture from the combustion exhaust gas.

  Furthermore, the hydrogen production apparatus 10 includes a heat exchanger HE1 and a chiller 100 between the reformer 12 and the pre-pressurization water separation unit 50, and a chiller 110 between the compressor 80 and the post-pressurization water separation unit 60. There is.

  In addition, this hydrogen production apparatus 10 produces hydrogen from a hydrocarbon raw material, and in this embodiment, a case where a town gas mainly containing methane 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 multi-layered tubular walls 21, 22, 23, 24 (hereinafter sometimes referred to as “cylindrical walls 21-24”). Have. The plurality of cylindrical walls 21 to 24 are formed in, for example, a cylindrical shape or an elliptical cylindrical shape. A combustion chamber 25 is formed in the inside of the first cylindrical wall 21 from the inside of the plurality of cylindrical walls 21 to 24, and a burner 26 is disposed downward at the top of the combustion chamber 25. Yes. The multi-cylinder reformer 12 is an example of a reformer.

  Further, an air supply pipe 40 for supplying combustion air from the outside is connected to an upper end portion of the combustion chamber 25. The burner 26 is further connected to a raw material branch pipe 33A branched from a raw material supply pipe 33 for supplying a city gas. An air branch pipe 40A branched from the air supply pipe 40 is connected to the raw material branch pipe 33A. Further, an off gas reflux pipe 120 is connected to the burner 26. Therefore, the burner 26 is configured to be supplied with a gas or off-gas in which the city gas is mixed with air.

  A combustion exhaust gas channel 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 combustion exhaust gas discharged from the combustion chamber 25 flows from the lower side to the upper side of the combustion exhaust gas flow path 27 and is sent to the combustion exhaust water separation unit 70 through the gas discharge pipe 28.

  In addition, 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 passage 31 is formed as a preheating flow passage 32. A raw material supply pipe 33 for supplying a city gas and a reforming water are supplied to an upper end portion of the preheating flow passage 32. And the reforming water supply pipe 34 are 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. There is.

  The preheating channel 32 can be supplied with city gas from the raw material supply pipe 33, and the 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 flow path 32, and are heat-exchanged with the combustion exhaust gas through the second cylindrical wall 22 so that the water is vaporized. The preheating channel 32 is configured to generate a mixed gas by mixing the city gas and the reforming water (steam) in the gas phase.

  Further, a reforming catalyst layer 36 is provided below the preheating flow passage 32 in the first flow passage 31, and the mixed gas generated in the preheating flow passage 32 is supplied to the reforming catalyst layer 36. Configuration. The reforming catalyst layer 36 has a configuration in which reformed gas containing hydrogen as a main component is generated by receiving heat from the flue gas flowing through the flue gas passage 27 and causing the gas mixture to undergo a steam reforming reaction.

  Furthermore, a second flow passage 42 is formed between the third cylindrical wall 23 and the fourth cylindrical wall 24. The lower end portion of the second flow passage 42 is in communication with the lower end portion of the first flow passage 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.

  In addition, the CO shift catalyst layer 45 is provided on the upper side of the reformed gas channel 43 in the second channel 42, and the reformed gas generated by the reformed catalyst layer 36 is a reformed gas flow. After passing through the passage 43, the CO is supplied to the CO shift catalyst layer 45. In the CO shift catalyst layer 45, carbon monoxide and steam contained in the reformed gas react with each other to be converted into hydrogen and carbon dioxide (aqueous shift reaction), and carbon monoxide can be reduced.

  Furthermore, an oxidant gas supply pipe 46 is connected on the upper side of the CO conversion catalyst layer 45, and a CO selective oxidation catalyst layer 47 is provided on the upper side of the CO conversion catalyst layer 45 in the second flow path 42. ing. The oxidant gas introduced through the oxidant gas supply pipe 46 and the reformed gas having 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 is reacted with oxygen on a noble metal catalyst such as platinum or ruthenium to be converted into carbon dioxide, 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 configured to be discharged through the reformed gas discharge pipe 44.

  The reformed gas generated in the multi-cylinder reformer 12 is, as shown in FIG. 1, in this order of the pre-pressurized water separation unit 50, the compressor 80, the post-pressurized water separation unit 60, and the hydrogen purifier 90 in this order. Flow. That is, in the gas flow direction, from the upstream side to the downstream side, the multiple cylinder 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. Has been placed.

(Water separation part before pressurization)
The downstream end of a reformed gas discharge pipe 44 which allows the reformed gas G1 to flow from the multi-cylinder reformer 12 is connected to the pre-pressurized water separation unit 50. A water recovery pipe 59 is connected to the bottom of the pre-pressurized water separation unit 50, and a communication flow channel pipe 56 is connected to the upper portion of the pre-pressurized water separation unit 50. The reformed gas G1 is separated by the condensation of water by cooling by heat exchange with the refrigerant in a heat exchanger HE1 and a chiller 100, which will be described later, disposed in the reformed gas discharge pipe 44 upstream of the pre-pressurization water separation unit 50. In addition, water (liquid phase) can be stored in the lower part of the pre-pressurization water separation unit 50. The water (liquid phase) is sent to the water recovery pipe 59. The reformed gas G <b> 2 after the water has been condensed is configured to be sent to the communication channel pipe 56. The reformed gas discharge pipe 44 corresponds to a "reformed gas flow path".

(Heat exchanger)
The heat exchanger HE1 is connected to an industrial water supply pipe 51 communicated with an industrial water supply source outside the hydrogen production apparatus 10 and an industrial water discharge pipe 52 communicated with the outside of the hydrogen production apparatus 10. Therefore, in the heat exchanger HE1, the industrial water supplied from the industrial water supply pipe 51 is heat-exchanged with the reformed gas G1 (the reformed gas is cooled), and the industrial water after the heat exchange passes through the industrial water discharge pipe 52. It is configured to be discharged to the outside of the hydrogen production apparatus 10 through it. The heat exchanger HE1 corresponds to the "first heat exchanger". Moreover, industrial water corresponds to the "refrigerant" of a 1st heat exchanger.

(Chiller)
The chiller 100 is located on the reformed gas discharge pipe 44 on the downstream side of the heat exchanger HE1. As shown in FIG. 1, the heat exchanging unit 102 disposed on the reformed gas discharge pipe 44, the radiator 104 disposed at a position separated from the heat exchanging unit 102, the heat exchanging unit 102 and the radiator 104, And a chiller water circulation passage 106 through which chiller water is circulated.

  The chiller water circulation passage 106 is provided with a pump 107 for circulating chiller water. Further, the radiator 104 is provided with a fan 108 for cooling chiller water that has reached a high temperature due to heat exchange in the heat exchange unit 102.

  That is, the chiller water cooled in the radiator 104 is supplied to the heat exchanging unit 102 via the chiller water circulation passage 106 and is heat-exchanged with the reformed gas flowing in the reformed gas discharge pipe 44 (the reformed gas is cooled). ) Configuration. The chiller 100 corresponds to the “second heat exchanger”. Moreover, chiller water corresponds to the "refrigerant" of a 2nd heat exchanger.

(Compressor)
The compressor 80 includes a communication channel pipe 56 through which the reformed gas G2 from the pre-pressurization water separation unit 50 flows, and a communication channel pipe 66 through which the reformed gas G2 supplied to the post-pressurization water separation unit 60 flows. It is connected. The compressor 80 compresses the reformed gas G2 supplied from the pre-pressurization water separation unit 50, and can supply the reformed gas G2 to the post-pressurization water separation unit 60. The compressor 80 corresponds to the "boosting means".

(Water separation part after pressurization)
The post-pressurization water separation unit 60 is connected to the downstream end of a communication flow channel 66 through which the reformed gas G <b> 2 flows from the compressor 80. A water recovery pipe 69 is connected to the bottom of the post-pressurization water separation unit 60, and a communication flow path pipe 68 is connected to an upper portion of the post-pressurization water separation unit 60. In the reformed gas G2, water is condensed and separated by cooling by heat exchange with a refrigerant (chiller water) in a chiller 110, which will be described later, disposed in the communication flow path pipe 66 upstream of the pressurized water separation unit 60. Water (liquid phase) can be stored below the post-pressurization water separation unit 60. The water (liquid phase) is sent to the water recovery pipe 69. The reformed gas G <b> 3 after the water is condensed is configured to be sent to the connecting flow path pipe 68.

(Chiller)
Similar to the chiller 100, the chiller 110 includes a heat exchange unit 112, a radiator 114, a chiller water circulation channel 116, and a pump 117. In addition, the radiator 114 is provided with a fan 118 as in the radiator 104.

(Hydrogen purifier)
Connected to the hydrogen purifier 90 are the downstream end of the connecting flow path pipe 68 through which the reformed gas G3 from the post-pressurization water separation section 60 flows and the upstream end of the off-gas reflux pipe 120 through which the off-gas of the hydrogen purifier 90 flows. ing.

  The hydrogen purifier 90 uses, for example, a PSA apparatus. The hydrogen purifier 90 includes a pair of adsorption tanks, performs an adsorption process for adsorbing impurities on the adsorbent in one adsorption tank, and performs a desorption process for desorbing impurities adsorbed on the adsorbent in the other adsorption tank, 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 an impurity containing carbon monoxide (off gas OG), and the hydrogen is purified. The purified hydrogen is sent to a hydrogen supply pipe 92 and stored in a tank (not shown) or sent to a hydrogen supply line.

  The off gas of the hydrogen purifier 90 can be supplied to the burner 26 of the reformer 12 via the off gas reflux pipe 120. An offgas tank 122 for leveling offgas supplied from the hydrogen purifier 90 and supplying it to the burner 26 by temporarily storing the offgas and flowing it to the burner 26 is provided on the offgas reflux pipe 120. There is.

(Combustion exhaust gas water separation part)
The downstream end of a gas discharge pipe 28 which leads the combustion exhaust gas from the combustion exhaust gas passage 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 top of the combustion exhaust gas water separation unit 70. Combustion exhaust gas discharged from the combustion chamber 25 is condensed and separated by cooling by heat exchange with cooling water in the heat exchanger HE3 disposed in the gas exhaust pipe 28 upstream of the combustion exhaust gas water separation unit 70. The water (liquid phase) can be stored in the lower part of the combustion exhaust gas water separation unit 70. The water (liquid phase) is sent to a 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 downstream end of each of the water recovery pipes 59, 69, 78 is connected to the reforming water supply pipe 34. The reforming water supply pipe 34 is provided with a water processor (ion exchange resin) 34A for removing dissolved ion components. Further, 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 supplied to the multiple cylinder reformer 12 by the pump P1. It is the structure supplied.

(Function)
Next, the operation of the hydrogen production apparatus 10 will be described.

  The city gas is supplied from the raw material supply pipe 33 to the multi-cylinder reformer 12. As shown in FIG. 2, the city gas supplied to the multi-cylinder reformer 12 is heated while being mixed with the water for reforming in the preheating flow path 32 of the multi-cylinder reformer 12, and a reforming catalyst is obtained. Supplied to layer 36. In the reforming catalyst layer 36, the mixed gas receives heat from the flue gas flowing through the flue gas passage 27 to cause a steam reforming reaction, and a reformed gas mainly composed of hydrogen is generated. The 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 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. And is converted to carbon dioxide to remove carbon monoxide. The reformed gas G1 whose carbon monoxide has been reduced by the CO selective oxidation catalyst layer 47 is delivered to the reformed gas discharge pipe 44.

  At this time, in the combustion chamber 25 of the multi-cylinder reformer 12, a gas obtained by mixing the city gas and air supplied from the raw material branch pipe 33A and the air branch pipe 40A, or an off gas supplied from the off gas recirculation pipe 120 is used. Is burned by the burner 26. 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 channel 27 and the gas exhaust pipe 28. As shown in FIG. 1, the water contained in the combustion exhaust gas is cooled and condensed by heat exchange in the heat exchanger HE 3, stored in the combustion exhaust gas water separation unit 70, and sent to the water recovery pipe 78. The flue gas from which the water has been separated is discharged from the gas discharge pipe 76 into the open air.

  On the other hand, as shown in FIG. 1, the reformed gas G1 is brought to a high temperature, for example, 100 ° C. by a steam reforming reaction or an aqueous shift reaction in the reformer 12. The reformed gas G1 flowing through the reformed gas discharge pipe 44 is first heat-exchanged with industrial water in the heat exchanger HE1 and cooled to 32 ° C., for example. The reformed gas G1 cooled by the heat exchanger HE1 is further heat-exchanged with chiller water in the heat exchange section 102 of the chiller 100, and further cooled to, for example, 10 ° C.

  As a result, the reformed gas G1 flowing through the reformed gas discharge pipe 44 is cooled by the heat exchanger HE1 and the chiller 100, whereby water vapor is condensed.

  The reformed gas G1 is supplied to the pre-pressurized water separation unit 50 through the reformed gas discharge pipe 44. In the pre-pressurized water separation unit 50, water condensed by cooling by heat exchange in the heat exchanger HE1 and the chiller 100 is stored and delivered to the water recovery pipe 59. The reformed gas G2 from which water has been separated is supplied to the compressor 80 from the communication flow pipe 56 and compressed by the compressor 80.

  The compressed reformed gas G2 is supplied from the communication flow pipe 66 to the water separation unit 60 after pressure increase. In the post-pressurization water separation unit 60, water condensed by cooling by heat exchange in the chiller 110 is stored and sent to the water recovery pipe 69. The reformed gas G3 from which 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, respectively, is returned to the reforming water supply pipe 34. By driving the pump P1, the water is supplied from the reforming water supply pipe 34 to the multi-cylinder reformer 12 as reforming water.

  The hydrogen purifier 90 employs a pressure swing method, in which one of the pair of adsorption tanks adsorbs impurities other than hydrogen to the adsorbent, and the other adsorption tank desorbs impurities adsorbed to the adsorbent. . In the hydrogen purifier 90, hydrogen and impurities are continuously separated from the reformed gas G3 and hydrogen is purified by repeating the adsorption step and the desorption step in each adsorption tank in a fixed cycle.

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

  On the other hand, the off-gas OG discharged from the hydrogen purifier 90 flows through the off-gas recirculation pipe 120 and is temporarily stored in the off-gas tank 122, and then the flow rate and composition are leveled in the combustion chamber 25 (burner 26) of the reformer 12. Supplied.

  As described above, in the hydrogen production apparatus 10, the high-temperature reformed gas G <b> 1 sent from the reformer 12 is first cooled by the heat exchanger HE <b> 1 and then cooled by the chiller 100 on the reformed gas discharge pipe 44. Then, the water is supplied to the pre-pressurized water separation unit 50, and the water condensed from the reformed gas G1 is separated.

  That is, since the heat exchanger HE1 is provided on the upstream side of the chiller 100, the cooling load of the chiller 100 is reduced, and the chiller 100 can be downsized.

  Further, the heat exchanger HE1 exchanges heat between industrial water supplied to a factory or the like and the reformed gas G1. Industrial water is supplied from an industrial water supply source outside the hydrogen production apparatus 10 and heat exchange is performed. It is a refrigerant non-recirculation type in which the industrial water is discharged to the outside of the hydrogen production apparatus 10. Therefore, the heat exchanger HE1 is smaller than the refrigerant circulation type heat exchanger, and the enlargement of the hydrogen production apparatus 10 due to the addition of the heat exchanger HE1 is suppressed.

  In particular, the heat exchanger HE1 is provided with an industrial water supply pipe 51 and an industrial water discharge pipe 52 except for a portion where heat is exchanged between the reformed gas G1 and industrial water, and the industrial water supply pipe 51 is connected to the outside of the hydrogen production apparatus 10. Since it is sufficient to connect only to the industrial water supply source of the above, the configuration is simple, and the enlargement of the hydrogen production apparatus 10 by providing the heat exchanger HE1 is further suppressed.

  Therefore, compared with the case where the refrigerant circulation type chiller alone is cooled, the combination of the refrigerant non-circulation type heat exchanger HE1 and the refrigerant circulation type chiller 100 reduces the size of the hydrogen production apparatus 10. Can.

  On the other hand, industrial water used in the heat exchanger HE1 is, for example, about 32 ° C., so that the reformed gas G1 discharged from the reformer 12 can be sufficiently cooled at a high temperature, for example, 100 ° C. That is, a predetermined cooling capacity can be ensured by a combination of the refrigerant non-circulation type heat exchanger HE1 and the downsized refrigerant circulation type chiller 100.

  Thus, the hydrogen production apparatus 10 secures (maintains) a cooling capacity as compared with that in which the reformed gas G1 supplied to the compressor 80 (the pre-pressurized water separation unit 50) is cooled by a single chiller. It can be downsized.

  Further, when industrial water is already used at the installation site of the hydrogen production apparatus 10, it is possible to easily cool the heat exchanger HE1 by supplying a part of the industrial water to the heat exchanger HE1. Become.

[Others]
In the hydrogen production apparatus 10 according to the present embodiment, the heat exchanger HE1 in which industrial water exchanges heat with the reformed gas G1 has been described as a refrigerant non-circulation type heat exchanger, but the present invention is not limited to this. For example, it may be a heat exchanger that utilizes the cold heat of liquefied natural gas.

  In addition, for example, an air fin cooler that exchanges heat with the reformed gas G1 may be used. In this case, a portion of the reformed gas discharge pipe 44 is branched into a large number of pipes, and air as a refrigerant is introduced from the outside of the hydrogen production apparatus 10 and sprayed to this branch portion to cool the reformed gas G1. At the same time, the heat-exchanged air may be discharged to the outside of the hydrogen production apparatus 10.

  That is, as the non-refrigerant heat exchanger, any refrigerant may be supplied as long as the refrigerant is supplied from the outside of the hydrogen producing apparatus 10 and the heat-exchanged refrigerant is discharged to the outside of the hydrogen producing apparatus 10.

  Moreover, the industrial water of this embodiment includes not only industrial water supplied from industrial water supply, but also water supplied from wells, seas, rivers, etc., water supplied from middle water, and the like.

  In the hydrogen production apparatus 10 according to the embodiment, the reformer 12 is a multi-cylinder reformer, but the present invention is not limited to this. Any gas can be used as long as it can be reformed from city gas to a reformed gas mainly composed of hydrogen.

  Further, in the hydrogen production apparatus 10 according to the embodiment, although the case where the hydrogen purifier 90 is a PSA apparatus has been described, it is not limited to this as long as hydrogen can be purified from the reformed gas G3.

  Furthermore, in the hydrogen production apparatus 10 according to the embodiment, the CO shift catalyst layer 45 and the CO selective oxidation catalyst layer 47 are provided in order to remove carbon monoxide from the reformed gas in the reformer 12, It may be constituted only by the CO shift catalyst layer 45.

10 Hydrogen Production Equipment 12 Multi-Cylinder Reformer (Reformer)
44 Reformed gas discharge pipe (reformed gas flow path)
80 Compressor (pressure booster)
90 hydrogen purifier 100 chiller (second heat exchanger)
HE1 heat exchanger (1st heat exchanger)

Claims (2)

A reformer configured to supply hydrocarbons as a raw material from a hydrocarbon supply source and to reform the hydrocarbons to generate a reformed gas containing hydrogen as a main component;
A booster connected to the reformer and boosting the reformed gas;
A hydrogen purifier connected to the pressurizing means and separating the reformed gas into product hydrogen and an off-gas as an impurity to purify product hydrogen;
A refrigerant non-circulation type first heat exchanger provided on a reformed gas flow path connecting the reformer and the pressure raising means, and cooled by the reformed gas exchanging heat with the refrigerant;
A refrigerant that is provided on the reformed gas flow path downstream of the first heat exchanger and that is cooled by the heat exchange of the reformed gas with the refrigerant and the water vapor contained in the reformed gas is condensed. A circulation type second heat exchanger;
A hydrogen production apparatus comprising:   The hydrogen production apparatus according to claim 1, wherein the refrigerant used in the first heat exchanger is industrial water.