JP6830819B2 - Hydrogen production equipment - Google Patents

Description

In the present invention, when a hydrogen-containing gas derived from a hydrogen purifier is supplied to a combustor and used as a heat energy source, the energy efficiency (system efficiency) of the entire hydrogen production apparatus is considered in consideration of the hydrogen recovery rate of the hydrogen purifier. With respect to hydrogen production equipment that can enhance. In the present invention, a product hydrogen having a high hydrogen concentration (second hydrogen-containing substance) and a first hydrogen-containing substance having a lower hydrogen concentration than the product hydrogen (non-permeated gas, off-gas) are derived from the hydrogen purifier. To do.

Conventionally, hydrogen is purified by a hydrogen purifier from a dehydrogenation reaction product produced by a dehydrogenation reactor that heats a hydride of aromatic hydrocarbon, which is a kind of organic hydride, and decomposes it into hydrogen and a dehydrogenation substance. Hydrogen production equipment such as hydrogen stations are known.

Here, Patent Document 1 describes a hydrogen production apparatus that decomposes organic hydride into hydrogen and a dehydrogenation reactant using a dehydrogenation reactor. Since the post-reaction gas derived from the dehydrogenation reactor contains impurities other than hydrogen, condensable substances are removed by cooling and condensing to increase the purity of hydrogen. The non-permeated gas from the hydrogen purifier is introduced in the subsequent stage of the dehydrogenation reactor.

On the other hand, Patent Document 2 describes a device that supplies off-gas containing hydrogen derived from a hydrogen purifier to a dehydrogenation reactor. In addition, Patent Document 2 also describes that off-gas from a hydrogen refiner is used as a fuel for a burner.

JP-A-2005-213807 Japanese Unexamined Patent Publication No. 2014-73921

By the way, in the conventional hydrogen production apparatus, the hydrogen-containing gas derived from the hydrogen purifier or the like is supplied to a combustor such as a burner for heating the dehydrogenation reactor, and the energy efficiency (or system efficiency) of the entire hydrogen production apparatus is achieved. ) Is increased.

However, simply supplying the hydrogen-containing gas to the combustor does not necessarily improve the energy efficiency of the entire hydrogen production apparatus.

Further, in the conventional hydrogen production apparatus shown in FIG. 3, the hydrogen recovery rate of the hydrogen purifier 30 can be adjusted, and the overall energy efficiency can be adjusted from the hydrogen recovery rate. For example, FIG. 4 is a diagram showing a change in the overall energy efficiency of the hydrogen production apparatus 1 with respect to the hydrogen recovery rate of the hydrogen purifier 30. The hydrogen recovery rate is the amount of purified hydrogen V31 with respect to the dehydrogenation reaction product V30 introduced into the hydrogen refiner 30 as a percentage. In FIG. 4, the total energy efficiencies at the hydrogen recovery rates of 80%, 85%, 90%, 92%, 94%, and 95% are plotted as points PP1 to PP6, respectively, and an approximate curve LL is drawn. As shown in FIG. 4, the total energy system efficiency reaches a maximum value when the hydrogen recovery rate is 94%. Therefore, if it is desired to maximize the overall energy efficiency, the hydrogen purifier 30 may be set to have a hydrogen recovery rate of 94%. However, it may be difficult to change the setting of the hydrogen recovery rate of the hydrogen purifier 30 during the operation of the hydrogen production apparatus, and a means for adjusting the hydrogen recovery rate other than the hydrogen purifier 30 is required.

The present invention has been made in view of the above, and when a hydrogen-containing gas such as a first hydrogen-containing substance derived from a hydrogen purifier is supplied to a combustor and used as a heat energy source, the hydrogen purifier It is an object of the present invention to provide a hydrogen production apparatus capable of increasing the system efficiency of the entire hydrogen production apparatus in consideration of the hydrogen recovery rate.

In order to solve the above-mentioned problems and achieve the object, the hydrogen production apparatus according to the present invention includes a dehydrogenation reactor having a dehydrogenation catalyst that decomposes organic hydride into hydrogen and a dehydrogenation substance, and the hydrogen and the above. Heat to supply heat to a hydrogen purifier that purifies hydrogen from a dehydrogenation reaction product containing a dehydrogenation substance, and a heater that heats the dehydrogenation reactor and the organic hydride introduced into the dehydrogenation reactor. In a hydrogen production apparatus including a heat medium boiler for heating a medium and a supply line for guiding a first hydrogen-containing substance, which is a gas other than product hydrogen purified from the hydrogen purifier, to the heat medium boiler, the hydrogen When the hydrogen recovery rate of the purifier is fixed, the hydrogen purifier has the highest overall energy efficiency based on the hydrogen recovery rate dependence of the total energy efficiency of the entire hydrogen production apparatus. The dehydrogenation reaction product gas is mixed with the first hydrogen-containing substance from the previous stage, and the mixing amount of the dehydrogenation reaction product gas is adjusted to control the hydrogen recovery rate.

Further, the hydrogen production apparatus according to the present invention is composed of a dehydrogenation reactor having a dehydrogenation catalyst that decomposes organic hydride into hydrogen and a dehydrogenation substance, and a dehydrogenation reaction product containing the hydrogen and the dehydrogenation substance. A hydrogen purifier that purifies hydrogen, a heat medium boiler that heats a heat medium that supplies heat to the dehydrogenator and a heater that heats the organic hydride introduced into the dehydrogenator, and the hydrogen purification. When the hydrogen recovery rate of the hydrogen purifier is fixed in a hydrogen production apparatus equipped with a supply line for guiding a first hydrogen-containing substance, which is a gas other than product hydrogen purified from the vessel, to the heat medium boiler. Based on the hydrogen recovery rate dependence of the total energy efficiency for hydrogen production of the entire hydrogen production apparatus, the first hydrogen-containing material is subjected to the latter stage of the hydrogen purifier so that the total energy efficiency is maximized. It is characterized in that the product hydrogen is mixed and the mixing amount of the product hydrogen is controlled.

According to the present invention, the system efficiency of the entire hydrogen production apparatus can be improved.

FIG. 1 is a circuit diagram showing a configuration of a hydrogen production apparatus according to an embodiment of the present invention, in which a part of a dehydrogenation reaction product in the pre-stage of a compressor is extracted to reduce a substantial hydrogen recovery rate and contain first hydrogen. It is a figure which shows the structure when it is used as a fuel of a heat medium boiler together with an object. FIG. 2 is a circuit diagram showing a configuration of a hydrogen production apparatus according to an embodiment of the present invention, in which a part of hydrogen permeated by a hydrogen purifier is extracted to lower a substantial hydrogen recovery rate and contain first hydrogen. It is a figure which shows the structure when it is used as a fuel of a heat medium boiler together with an object. FIG. 3 is a circuit diagram showing the configuration of a conventional hydrogen production apparatus. FIG. 4 is a diagram showing a change in the overall energy efficiency of the hydrogen production apparatus with respect to the hydrogen recovery rate of the hydrogen purifier shown in FIG.

Hereinafter, embodiments for carrying out the present invention will be described with reference to the accompanying drawings.

[overall structure]
FIG. 1 is a circuit diagram showing a configuration of a hydrogen production apparatus 1 according to an embodiment of the present invention. This hydrogen production device 1 is a device that produces hydrogen from organic hydride by a dehydrogenation reaction, and is adopted in a hydrogen station that supplies hydrogen to, for example, a fuel cell vehicle or a hydrogen engine vehicle. As shown in FIG. 1, the hydrogen production apparatus 1 has a dehydrogenation reaction system 1A and a hydrogen purification system 1B. The dehydrogenation reaction system 1A decomposes organic hydride into hydrogen and a dehydrogenation substance by the dehydrogenation reactor 10, and produces a dehydrogenation reaction product containing the hydrogen and the dehydrogenation substance and an undecomposed reaction product which has not been decomposed. Output. The hydrogen purification system 1B separates hydrogen from the dehydrogenation reaction product derived from the dehydrogenation reaction system 1A by the hydrogen purifier 30 and outputs it to the outside.

Organic hydride is a hydride of an organic compound having an unsaturated bond, and can be decomposed into a dehydrogenation reaction product containing hydrogen and a dehydrogenated substance (organic compound having an unsaturated bond) using a dehydrogenation catalyst. it can. The organic hydride is preferably in a liquid state under normal temperature and pressure, and when such a liquid is adopted, it can be transported to a hydrogen production apparatus 1 such as a hydrogen station by a lorry or the like as a liquid fuel like gasoline or the like. In the present embodiment, methylcyclohexane (hereinafter referred to as MCH) will be used as the organic hydride, but the description is not limited to this. The organic compound having an unsaturated bond is an organic compound having one or more double bonds or triple bonds in the molecule and is liquid at normal temperature and pressure. The double bond includes a carbon-carbon double bond (C = C), a carbon-nitrogen double bond (C = N), a carbon-oxygen double bond (C = O), and a nitrogen-oxygen double bond (N). = O) is illustrated. Examples of the triple bond include a carbon-carbon triple bond and a carbon-nitrogen triple bond. The organic compound having an unsaturated bond is preferably a liquid organic compound under normal temperature and pressure from the viewpoint of storability and transportability.

Examples of organic compounds having unsaturated bonds include olefins, dienes, acetylenes, benzene, carbon chain-substituted aromatics, hetero-substituted aromatics, polycyclic aromatics, sifbases, and heteroaromatics. , Hetero 5-membered ring compounds, quinones, ketones and the like. Examples of olefins include ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene and the like. Examples of the diene include allene, butadiene, pentadiene, hexadiene, hebutadiene, octadiene, piperylene, isoprene and the like. Examples of acetylenes include acetylene, propyne, vinylacetylene and the like. Examples of carbon chain-substituted aromatics include alkyl-substituted aromatics. Alkylation-substituted aromatics include toluene, xylene, trimethylbenzene, ethylbenzene, cumene, benzoic acid and the like. Examples of hetero-substituted aromatics include anisole, dimethoxybenzene, phenol, aniline, N, N-dimethylaniline and the like. Examples of polycyclic aromatics include naphthalene, methylnaphthalene, anthracene, tetracene, phenanthrene, tetralin, and azulene. Examples of Schiff bases include 2-aza-hept-1-en-1-yl-cyclohexane. Examples of heteroaromatics include pyridine, pyrimidine, quinoline, isoquinoline and the like. Examples of the hetero 5-membered ring compound include furan, thiophene, pyrrole, and imidazole. Examples of quinones include benzoquinones and naphthoquinones. Examples of ketones include acetone and methyl ethyl ketone. Needless to say, carbon dioxide and carbon monoxide have unsaturated bonds but are not generally regarded as organic compounds, and are therefore excluded from the organic compounds having unsaturated bonds in the present embodiment. ..

Among the above unsaturated compounds, benzene, toluene, xylene, ethylbenzene, naphthalene, methylnaphthalene, tetralin, etc. (hereinafter referred to as "benzene, etc.") are water-insoluble before and after hydrogenation, and are water-insoluble. It is preferable to a water-soluble organic compound such as acetone in that it can be phase-separable and can be recovered as a product very easily. As these benzene and the like, a pure compound may be used, or a mixture of a plurality of compounds may be used.

[Dehydrogenation reaction system]
As shown in FIG. 1, the MCH transported by the lorry or the like is stored in the tank T1. The stored MCH is sucked up by the pump P1. The discharge flow rate from the pump P1 is controlled by the flow controller 100. The MCH (L1) discharged from the pump P1 is heated to 20 to 120 ° C. by the preheater 11. The heated liquid MCH (L2) is evaporated by the evaporator 12 to become a vaporized MCH (V1) at 180 ° C. The MCH (V1) is further heated to 300 ° C. by the heater 13 and input to the dehydrogenation reactor 10 as the MCH (V2).

In the dehydrogenation reactor 10, a tube through which a heat medium such as a heat medium oil passes is arranged in order to heat the dehydrogenation catalyst and MCH (V2). A dehydrogenation catalyst is installed in the dehydrogenation reactor 10. Since the dehydrogenation reaction of MCH (V2) is an endothermic reaction, for example, a heat medium having a temperature of about 350 ° C. is used, and the dehydrogenation reaction of MCH (V2) passing through the dehydrogenation reactor 10 is efficiently performed. The inside of the dehydrogenation reactor 10 is heated so that the temperature can be maintained at about 300 ° C. The MCH (V2) introduced into the dehydrogenation reactor 10 is decomposed into hydrogen and toluene, and is dehydrogenated from the dehydrogenation reactor 10 at about 330 ° C. as a dehydrogenation reactant V3 containing hydrogen, toluene and undecomposed MCH. Derived.

The dehydrogenation reaction product V3 exchanges heat with the MCH (V1) introduced into the heater 13 in the heater 13. The heat-exchanged dehydrogenation reaction product V3 becomes, for example, the dehydrogenation reaction product V4 whose temperature has been lowered to about 210 ° C. to 220 ° C. The dehydrogenation reaction product V4 exchanges heat with the MCH (L1) input to the preheater 11 in the preheater 11. By exchanging heat between the dehydrogenation reaction product V4 and the MCH (L1) in the preheater 11, the amount of heat exchange in the evaporator 12 in the subsequent stage can be reduced. That is, with such a configuration, as will be described later, energy consumption for heating the heat medium can be suppressed, so that the energy efficiency of the entire device can be improved. The heat-exchanged MCH (V5) in the preheater 11 is cooled to, for example, 130 ° C. to 140 ° C., and then led out to the hydrogen purification system 1B.

The heat medium L11 introduced into the dehydrogenation reactor 10 is heated in the heat medium boiler 21. The heat medium L12 absorbed in the dehydrogenation reactor 10 exchanges heat with the MCH (L2) in the evaporator 12 to evaporate the MCH (L2) and raise the temperature to about 180 ° C. After that, the heat medium L13 whose temperature has been lowered is input to the heat medium boiler 21 again by the pump P2 and heated. In the first embodiment, the heat medium uses heat medium oil from the viewpoint of heat transfer efficiency, but the heat medium is not limited to this. The heat medium is stored in the tank T2, and when the heat medium is insufficient in the circulation system of the heat medium, the heat medium is replenished to the pipelines constituting the circulation system, and when the heat medium is large, the circulation is provided. It is pulled out from the pipelines that make up the system.

The heat medium boiler 21 heats the heat medium L13 by inflowing the LP gas G1 flowing through the line LN11 and the air G2 flowing through the line LN12 and burning the LP gas G1. A supply line LN1 for supplying the off-gas G31 of the hydrogen purifier 30 is connected to the line LN11. Therefore, the off-gas G31 is mixed in the LP gas G1. The air G2 is sucked by the blower 22, preheated by the air preheater 23, and then input to the heat medium boiler 21. The combustion gas G3 burned in the heat medium boiler 21 exchanges heat with the air G2 in the air preheater 23, and then is discharged to the atmosphere as combustion exhaust gas. Energy efficiency can be improved by air preheating using the air preheater 23. In the heating control of the heat medium by the heat medium boiler 21, the temperature controller 200 detects the temperature in the dehydrogenator 10, and based on this detected temperature, the heat medium flow rate to the heat medium boiler 21 by the pump P2 is calculated. While adjusting, the temperature of the heat medium L11 flowing into the dehydrogenator 10 detected by the temperature controller 201 is detected, and based on this detected temperature, the LP burned in the heat medium boiler 21 via the flow controller 103. This is done by adjusting the flow rate of the gas G1. The flow controller 103 controls the opening and closing of the valve VL103.

In the present embodiment, the heat medium boiler 21 is used to heat the heat medium, and the heated heat medium is used to heat the dehydrogenation reactor 10. When such a heating mechanism using a heat medium is adopted, the temperature of the dehydrogenation reactor 10 can be controlled more stably because heating can be performed more uniformly than, for example, a heating mechanism that directly heats with a burner. be able to. The heating mechanism using a heat medium is not limited to the one using a liquid heat medium. For example, the combustion gas obtained by burning LP gas with a burner or the like directly flows into the piping in the dehydrogenizer 10. A gaseous heat medium that heats the MCH (V2) may be used. Further, the heating mechanism is not limited to the one using a heat medium, and for example, a mechanism for directly heating with a burner may be adopted.

Further, the heat medium boiler 21 described above is designed to burn the LP gas G1, but the present invention is not limited to this, and a fuel such as kerosene may be used. However, when mixing with the first hydrogen-containing material G31 via the supply line LN1, it is preferable to mix the first hydrogen-containing material G31 with the vaporized kerosene.

In the dehydrogenation reaction system 1A according to the present embodiment, the MCH (V1) flowing into the dehydrogenation reactor 10 is heated by the heater 13 using the thermal energy of the dehydrogenation reaction product V3 output from the dehydrogenation reactor 10. At the same time, the preheater 11 arranged in front of the evaporator 12 preheats the liquid MCH (L1) before evaporation by using the thermal energy of the dehydrogenation reaction product V4 after the heat exchange by the heater 13. I have to. As a result, the thermal energy of the heat medium L12 consumed for evaporation of the MCH (L1) in the evaporator 12 can be reduced. The reduction in the heat energy lost from the heat medium L12 results in a reduction in the energy consumed by the heat medium boiler 21, and as a result, the energy efficiency of the entire device can be improved.

[Hydrogen purification system]
On the other hand, the dehydrogenation reaction product V5 via the preheater 11 flows into the hydrogen purification system 1B. The dehydrogenation reaction product V5 is cooled by the cooler 31 to, for example, about 140 ° C. to 40 ° C., and gas-liquid separated by the gas-liquid separator 35. The dehydrogenated reaction product V6, which is not separated as a liquid substance by the gas-liquid separator 35 and has a high hydrogen content, is further cooled by the cooler 32 to, for example, about 40 ° C. to 15 ° C., and gas-liquid separated by the gas-liquid separator 36. Will be done. The dehydrogenation reaction product V7, which is not separated as a liquid substance by the gas-liquid separator 36 and has a further increased hydrogen content, is input to the hydrogen purifier 30 as the dehydrogenation reaction product V30 pressurized by the compressor P3. Since the temperature of the dehydrogenation reaction product V30 pressurized by the compressor P3 rises due to the pressurization, it is cooled to, for example, 80 ° C. to 100 ° C. by the cooler 33 before being introduced into the hydrogen purifier 30.

Further, as shown in FIG. 1, a part of the dehydrogenation reaction product V7 can be extracted from the front stage of the compressor P3. This point is different from the conventional hydrogen production apparatus shown in FIG. A part of the extracted dehydrogenation reaction product V7 is connected to the supply line LN1 via the supply line LN4 and mixed with the LP gas G1 via the supply line LN1.

The hydrogen purifier 30 has a function of separating the dehydrogenation reaction product V30 into hydrogen V31, which is a product hydrogen, and a first hydrogen-containing substance having a hydrogen concentration lower than that of hydrogen V31. In the present embodiment, the film is used. Those using a separation mechanism are adopted. Examples of the hydrogen separation membrane used in the membrane separation mechanism include carbon membranes, palladium membranes, and zeolite membranes as membranes that can withstand the pressure introduced from the compressor P3 (for example, have a pressure resistance of 900 kPa or more). Carbon membranes and zeolite membranes are relatively preferable from the viewpoint of pressure resistance and practical use with a small differential pressure, and carbon membranes are particularly preferable from the viewpoint of mechanical strength against vibration. The carbon film has a function of allowing hydrogen having a small molecular weight to permeate and not permeating substances having a relatively large molecular weight such as toluene and undecomposed substances. The compressor P3 outputs the 200 kPa dehydrogenation reaction product V7 to the hydrogen purifier 30 as a dehydrogenation reaction product V30 boosted to 900 kPa. Since the differential pressure at the time of hydrogen separation in the hydrogen purifier 30 is 200 kPa, the separated hydrogen V31 becomes 700 kPa at 90 ° C. The hydrogen V31 is cooled to 40 ° C. by the cooler 34, adjusted by the flow controller 101, and led out as hydrogen V32 of 700 kPa to the outside. That is, it is supplied to the outside as product hydrogen having the required external pressure and temperature.

Further, the hydrogen purifier 30 described above uses a membrane separation method, but is not limited to this, and is not limited to this, a PSA device which is a pressure swing adsorption (PSA) type hydrogen separator, and a temperature swing. An adsorption (TSA: Temperature Swing Adsorption) hydrogen purifier may be used.

Here, the pressure controller 400 controls so that the pressure output by the compressor P3 becomes a predetermined pressure. This predetermined pressure is higher than the combined pressure of 900 kPa, which is the sum of the differential pressure of 200 kPa generated by hydrogen purification in the hydrogen purifier 30 and the external output pressure of hydrogen V31 separated by the hydrogen purifier 30, in consideration of pressure loss. Make pressure. By setting the pressure output by the compressor P3 to such a predetermined pressure, it is necessary to provide a compressor dedicated to the product hydrogen output for boosting the pressure required for the product hydrogen, which has been conventionally provided in the subsequent stage of the hydrogen purifier 30. It disappears. As a result, the entire device can be made compact. Further, the pressure efficiency can be improved by consolidating the compressors into a large-sized compressor without distributing the compressors, and as a result, the energy required for the hydrogen purification process by the hydrogen purifier 30 and the product hydrogen required for the supply process of hydrogen are required. The total energy of energy can be reduced.

The liquefied impurities L21 and L22, which are separated as liquid substances in the gas-liquid separators 35 and 36 and have a large toluene content and contain hydrogen, are collected in the tank T3 and used as recovered toluene. The recovered toluene can be repeatedly used as a hydride (MCH) by reacting with hydrogen again.

The first hydrogen-containing substance (off gas) G31 that did not permeate the hydrogen separation membrane of the membrane separation mechanism in the hydrogen purifier 30 is connected to the line LN11 via the supply line LN1 and mixed with the LP gas G1 to be a heat medium boiler. Introduced in 21. The first hydrogen-containing substance G31 contains hydrogen that could not penetrate the hydrogen separation membrane, and at least this hydrogen contributes to combustion. Here, the flow controller 102 controls the valve VL 102 so that the flow rate of the first hydrogen-containing material G31 becomes a predetermined flow rate.

In FIG. 1, the temperature controllers 202 to 204 detect the gas temperature output from the coolers 31 to 33 and control the temperature by adjusting the flow rate of the cooling water flowing into each of the coolers 31 to 33. ing. Here, since the coolers 31, 33, and 34 have a small required cooling capacity, cooling water that has been naturally cooled via the cooling tower is used, and the cooler 32 has a large required cooling capacity, so that it is forced through a chiller. Cooling water that has been electrically cooled is used. By effectively utilizing the cooling tower and performing multi-stage cooling by the coolers 31 and 32, the power consumption due to forced cooling can be suppressed, so that the energy efficiency of the entire device can be improved.

Further, the discharge of the liquefied toluene of the gas-liquid separators 35 and 36 is controlled by the level controllers 301 and 302, respectively. That is, the level controllers 301 and 302 open the valve and discharge toluene to the tank T3 when the detected liquid level reaches a predetermined height or higher. Further, the flow controller 101 controls the valve so that the derived flow rate of hydrogen V32 becomes a predetermined flow rate.

[Control of overall energy efficiency]
In the hydrogen production apparatus shown in FIG. 1, when it is desired to maintain high overall energy efficiency, but the set value of the hydrogen recovery rate of the hydrogen purifier 30 cannot be changed immediately or is not desired to be changed, that is, the hydrogen purifier 30 When the set value of the hydrogen recovery rate is fixed, the overall energy efficiency can be controlled as follows. As shown in FIG. 1, a part of the dehydrogenation reaction product V7 is drawn from the front stage of the compressor P3 and connected to the supply line LN1 via the supply line LN4. On the supply line LN4, the flow controller 104 controls the opening degree of the valve VL104 to control the flow rate.

Since the amount of the dehydrogenation reaction product V7 introduced into the hydrogen purifier 30 is reduced, the amount of hydrogen V31 with respect to the dehydrogenation reaction product V7 before being extracted is reduced, and the hydrogen recovery rate is reduced in comparison with the dehydrogenation reaction product V7. However, the overall energy efficiency can be improved by reducing the fuel consumption of the heat medium boiler 21.

Further, as shown in FIG. 2, a part of the hydrogen V31 derived from the hydrogen purifier 30 may be extracted via the supply line LN5, whereby the substantial hydrogen recovery rate may be adjusted. The supply line LN5 is connected to the supply line LN1, and on the supply line LN5, the flow controller 105 controls the opening degree of the valve VL105 to control the flow rate.

In the present embodiment, by using the hydrogen contained in the first hydrogen-containing material G31 for combustion of the heat medium boiler 21, the fuel (LP gas G1) of the heat medium boiler 21 can be reduced and the overall energy efficiency is improved. Can be made to.

The configurations shown in FIGS. 1 and 2 may be mixed. That is, a part of the dehydrogenation reaction product V7 and a part of the hydrogen V31 may be extracted.

Based on the above, the hydrogen recovery rate of the hydrogen purifier 30 is set so as to have the optimum hydrogen recovery rate that maximizes the total energy efficiency, based on the hydrogen recovery rate dependence of the total energy efficiency for hydrogen production of the entire device. Can be done.

Further, in the present embodiment, the case where the overall energy efficiency is controlled without changing the setting of the hydrogen recovery rate has been described, but by adjusting the purification time of the dehydrogenation reaction product V30 introduced into the hydrogen purifier, The hydrogen recovery rate can also be changed.

1 Hydrogen production equipment 1A Dehydrogenation reaction system 1B Hydrogen purification system 10 Dehydrogenation reactor 11 Preheater 12 Evaporator 13 Heater 21 Heat medium boiler 22 Blower 23 Air preheater 30 Hydrogen purifier 31, 32, 33, 34 Cooler 35,36 Gas-liquid separator 100,101,102,103,104,105 Flow controller 200,201,202,203,204 Temperature controller 301,302 Level controller 400 Pressure controller G1 LP gas G2 Air G31 First hydrogen content (Off gas)
L11, L12, L13 Heat medium L21, L22 Liquefied impurities P1, P2 Pump P3 Compressor T1, T2, T3 Tank V3, V4, V5, V6, V7, V30 Dehydrogenation reactant V31, V32 Hydrogen VL102, VL103, VL104, VL105 Valves LN1, LN4, LN5 Supply line LN11, LN12 line

Claims (2)

A dehydrogenation reactor with a dehydrogenation catalyst that decomposes organic hydride into hydrogen and dehydrogenation substances,
A hydrogen purifier that purifies hydrogen from a dehydrogenation reaction product containing the hydrogen and the dehydrogenation substance,
A heat medium boiler that heats a heat medium that supplies heat to the dehydrogenation reactor and a heater that heats the organic hydride introduced into the dehydrogenation reactor.
A supply line that guides the first hydrogen-containing substance, which is a gas other than product hydrogen purified from the hydrogen purifier, to the heat medium boiler, and
In the hydrogen production equipment equipped with
When the set value of the hydrogen recovery rate of the hydrogen purifier is fixed, the total energy efficiency is set to be the highest based on the hydrogen recovery rate dependence of the total energy efficiency for hydrogen production of the entire hydrogen production apparatus. Hydrogen production characterized in that the dehydrogenation reaction product gas is mixed with the first hydrogen-containing material from the front stage of the hydrogen purifier, and the mixing amount of the dehydrogenation reaction product gas is adjusted to control the hydrogen recovery rate. apparatus. A dehydrogenation reactor with a dehydrogenation catalyst that decomposes organic hydride into hydrogen and dehydrogenation substances,
A hydrogen purifier that purifies hydrogen from a dehydrogenation reaction product containing the hydrogen and the dehydrogenation substance,
A heat medium boiler that heats a heat medium that supplies heat to the dehydrogenation reactor and a heater that heats the organic hydride introduced into the dehydrogenation reactor.
A supply line that guides the first hydrogen-containing substance, which is a gas other than product hydrogen purified from the hydrogen purifier, to the heat medium boiler, and
In the hydrogen production equipment equipped with
When the set value of the hydrogen recovery rate of the hydrogen purifier is fixed, the total energy efficiency is set to be the highest based on the hydrogen recovery rate dependence of the total energy efficiency for hydrogen production of the entire hydrogen production apparatus. A hydrogen production apparatus characterized in that the product hydrogen is mixed with the first hydrogen-containing substance from the subsequent stage of the hydrogen purifier, and the mixing amount of the product hydrogen is adjusted to control the hydrogen recovery rate .

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