JP2011213559A - Reformed gas or hydrogen production system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a system which is not lowered in producing efficiency when a reformed gas or hydrogen is produced by using recovery heat from a corrosive gas such as waste combustion exhaust gas and a high-temperature fluid at such a temperature that the reforming temperature cannot be sufficiently high.SOLUTION: The reformed gas or hydrogen production system comprises a reformer 10 which is installed in a flow passage of a high-temperature fluid, into which a charging material containing at least one of a hydrocarbon, an ether and an alcohol, and steam are made to flow, and which generates a reformed gas including hydrogen by steam-reforming using the heat of the high-temperature fluid, wherein the system comprises a hydrogen separator 16 for separating hydrogen from exhaust gas of the reformer or gas modified from the exhaust gas, and a material after the hydrogen separation is made to flow into the reformer.

Description

  Embodiments described herein relate generally to a reformed gas or hydrogen production system that produces reformed gas or hydrogen using waste heat from waste treatment.

  Conventional hydrogen production systems include systems that use waste heat from waste treatment. FIG. 25 shows an example of a hydrogen production system using waste heat from waste treatment. In FIG. 25, illustrations of devices and the like (pumps and the like) used for conveying each substance are omitted.

  A hydrogen production system as a first conventional example will be described with reference to FIG. The hydrogen production system shown in FIG. 25 includes an incinerator 1, and waste 2 to be treated such as general waste and combustion air 3 are introduced into the incinerator 1 to burn the waste 2. In the incinerator 1, the ash 4 and the first combustion exhaust gas 23 are generated by combustion, and the ash 4 is discharged from the incinerator 1. The incinerator 1 has a boiler 6 inside. The boiler 6 heats and evaporates the boiler feed water 7 that flows in by the first combustion exhaust gas 23, and flows it out as boiler steam 5.

  The boiler 6 is composed of a economizer, an evaporator, a superheater, and the like. The boiler steam 5 is cooled by passing heat to a heat utilization destination to become water, and circulates again as boiler feed water 7. Although not shown, the illustration is omitted. By flowing the boiler steam 5 through the steam turbine connected to the generator, the steam steam exhaust steam, whose pressure and temperature has decreased since power generation, is cooled by a condenser using river water or air to form water. Although there is a configuration of waste power generation to be the boiler feed water 7, the illustration is omitted.

  The temperature of the combustion exhaust gas 23 is decreased by the amount of heat applied, and flows out as the incinerator exhaust gas 8 and becomes the bag filter inflow gas 9.

  The incinerator 1 includes a reformer 10 that incorporates a reforming catalyst therein. In the hydrogen production system shown in FIG. 25, the reforming raw material 11 in which the city gas 12 and the steam 13 which are the inputs are mixed is caused to flow into the reformer 10. Most of the components of the city gas 12 are hydrocarbons including methane. The city gas 12 is city gas that has been desulfurized by the desulfurizer, but the desulfurizer is not shown. The reforming raw material 11 is heated by the combustion exhaust gas 25, undergoes steam reforming, and flows out as reformed gas 17. The main reforming reaction is a reaction in which methane and steam are converted into carbon monoxide and hydrogen. The reformed gas 17 is composed of carbon monoxide, carbon dioxide, hydrogen, steam, methane, and the like.

  Moreover, the hydrogen production system includes a carbon monoxide converter 19, a carbon dioxide separator 15, and a hydrogen separator 16, as shown in FIG.

  The reformed gas 17 flowing out from the reformer 10 flows into the carbon monoxide converter 19 and is adjusted to an appropriate temperature state by the carbon monoxide converter 19. The carbon monoxide transformer 19 shown in FIG. 25 has a temperature adjustment function, but the illustration of the heat source is omitted. In the carbon monoxide converter 19, most of the carbon monoxide reacts with the steam and changes to carbon dioxide, and at the same time, the steam changes to hydrogen. The modified gas 18 obtained by the reaction of carbon monoxide and steam flows out from the carbon monoxide converter 19 to the carbon dioxide separator 15.

  The carbon dioxide separator 15 separates the carbon dioxide 21 from the modified gas 18 and causes the separated gas 22 other than the carbon dioxide 21 to flow out to the hydrogen separator 16. Although there are a plurality of methods for separating the carbon dioxide 21 by the carbon dioxide separator 15, for example, a hot potassium carbonate method is used.

  The hydrogen separator 16 separates the separated gas 22 into hydrogen 14 and a gas 20 other than hydrogen. The hydrogen 14 separated by the hydrogen separator 16 can be used as fuel for a fuel cell, a hydrogen engine, a hydrogen fuel turbine, or refrigerant hydrogen. Further, the hydrogen 14 is not separated from the separated gas 22 by the hydrogen separator 16 but can be used as a fuel for an engine or a combustion turbine as it is as a mixed gas containing carbon monoxide and hydrogen.

  Next, a hydrogen production system as a second conventional example will be described with reference to FIG. Since the hydrogen production system shown in FIG. 26 has a configuration obtained by improving a part of the hydrogen production system described above with reference to FIG. 25, the same components as those in FIG. Only explained. Also, in FIG. 26, as in FIG. 25, equipment and the like used for transporting each substance are not shown.

  The hydrogen production system shown in FIG. 26 divides the boiler steam 5 to obtain the branched steam 24, and then the decompression valve 25 decompresses the steam to the same or close pressure as the city gas 12, and the steam 13 mixed with the city gas 12 To do. The boiler steam 5 is cooled by passing heat to a heat utilization destination, becomes water, circulates, and becomes part of the boiler feed water 7. Supply water having the same flow rate as that of the branch steam 24 is joined to the water circulating in the boiler feed water 7 to form the boiler feed water 7, but the illustration is omitted.

  In hydrogen production using a steam reforming reaction, steam generated from water that has passed through a soft water device is necessary, and therefore, steam generated by heating through a soft water device by transporting water is required. In the hydrogen production system shown in FIG. 26, it is possible to easily introduce appropriate steam by using the branch steam 24 that is a part of the boiler steam 5 generated from the boiler feed water 7 that is water that has passed through the water softener. Can do.

  Subsequently, an example of a hydrogen production system using a pressure swing adsorption separation method as a third conventional example will be described with reference to FIG. Since the hydrogen production system shown in FIG. 27 has a configuration obtained by improving a part of the hydrogen production system described above with reference to FIG. 26, the same reference numerals as those in FIG. Also, in FIG. 27, the equipment and the like used for transporting each substance is not shown in the same manner as the others.

  The hydrogen separator 16 of the hydrogen production system shown in FIG. 27 includes a first gas-liquid separator 54, a compressor 30, a cooler 32, a second gas-liquid separator 38, and a hydrogen separator 40 that is an absorption tower. Has been. The hydrogen separator 40 is an absorption tower and separates hydrogen while exchanging a plurality of absorption towers. In FIG. 27, the hydrogen separator 40 is illustrated as one apparatus for convenience.

  The separated gas 22 flowing out from the carbon dioxide separator 15 flows into the first gas-liquid separator 54. The first gas-liquid separator 54 separates the separated gas 22 into the first liquid 29 and the first gas 55, and the first gas 55 flows out to the compressor 30.

  The compressor 30 raises the pressure of the first gas 55 to, for example, a little over 1 MPa, and turns it into a pressurized gas 31. The pressurization gas 31 becomes high temperature due to the compression process, and the compressor 30 causes the pressurization gas 31 to flow out to the cooler 32. The cooler 32 cools the pressurization gas 31 to, for example, 40 ° C. with the first refrigerant 33, and then the pressurization gas 31 flows into the second gas-liquid separator 38 as the cooled gas 34.

  The second gas-liquid separator 38 separates the cooled gas 34 into a second liquid 56 and a second gas 39, and the second gas 39 flows into the hydrogen separator 40, which is an absorption tower, in a high-pressure state. .

  Substances contained in the gas 20 other than hydrogen are adsorbed to the adsorbent in the hydrogen separator 40 which is an absorption tower, and the hydrogen 14 passes. In order to desorb the substance adsorbed from the adsorbent that has sufficiently adsorbed the substance in the gas 20 other than hydrogen by the hydrogen separator 40, the adsorption tower that circulates the second gas 39 and the adsorption tower that does not circulate are exchanged. The inside of the adsorption tower after adsorption is lowered to a low pressure such as atmospheric pressure. Substances in the gas 20 other than hydrogen, which are adsorbed substances, are desorbed and released from the adsorbent. After desorption, the adsorption tower for circulating the second gas 39 and the adsorption tower for desorption without circulating the second gas 39 are exchanged. This is repeated to separate the hydrogen 14 from the second gas 39.

Although most of the first liquid 29 and the second liquid 56 are water (H ₂ O), hydrogen, carbon monoxide, methane, etc., which are combustible components dissolved in water, are released to the outside in an unburned state. Should not. In addition, the hydrogen separation efficiency may not be 100%, and the gas 20 other than hydrogen also contains combustible components such as carbon monoxide and methane. Therefore, the first liquid 29, the second liquid 56, and the gas 20 other than hydrogen flow into the incinerator 1 as the return fluid 41 and burn.

  Further, a reformed gas production system as a fourth conventional example will be described with reference to FIG. The hydrogen production system shown in FIG. 28 is a system for producing a mixed gas of carbon monoxide and hydrogen without requiring separation of hydrogen. In the following description, the same components as those in FIG. 26 are denoted by the same reference numerals, and only different portions are described. Also in FIG. 28, lines and the like used for transporting each substance are omitted as in the other cases.

  The reformed gas production system shown in FIG. 28 does not process the reformed gas 17. The reformed gas 17 also contains substances that are not carbon monoxide or hydrogen. If it is not necessary to increase the purity of hydrogen and only hydrogen production is intended, there is no need for a carbon monoxide transformation process. Further, if there is no carbon monoxide transformation process, there may be no carbon dioxide separation process. If the conversion rate is 100% and the molar ratio of carbon atoms and steam 13 in the city gas 12 is appropriate, the reformed gas 17 will be composed of hydrogen and carbon monoxide. If it is larger, a part of the steam 13 is included in the reformed gas 17. At this time, the reformed gas 17 contains a part of the steam 13 but is a gas 71 containing carbon monoxide and hydrogen, that is, a production gas. A part of the vapor 13 can be separated as water by a gas-liquid separator, but the illustration is omitted in FIG.

  The substance corresponding to the city gas 12 may be a fluid containing any one or more of hydrocarbons, ethers, and alcohols. The incinerator 1 is a high-temperature fluid flow path regardless of the presence or absence of corrosiveness. I just need it.

  The surface of the reformer 10 installed in the waste incinerator 1 is exposed to the waste combustion exhaust gas 23. Since the waste combustion exhaust gas 23 is a corrosive gas and a high temperature gas, the material of the reformer 10 is corroded. It's easy to do. FIG. 29 shows the temperature dependence of the corrosion rate of carbon steel in a waste incinerator environment, for example, the relationship between the tube wall temperature and the degree of erosion caused by corrosion in a metal generally used for the evaporator 6 of the boiler 6. Is the same. As shown in FIG. 29, the temperature range from 500 to 700 ° C. is a high temperature corrosion temperature range where the molten salt corrosion is severe, and if the surface temperature is the high temperature corrosion temperature range, the metal loss due to the molten salt corrosion is extremely severe.

  The reformer 10 is installed in the exhaust gas flow path portion that is cooled by the boiler 6 and the exhaust gas temperature is lower so that the surface temperature becomes lower than the high temperature corrosion temperature range, or the working fluid that circulates in the reformer 10 That is, it is possible to increase the flow rate of the reforming raw material 11, but if the surface temperature is low, the temperature of the working fluid flowing through the reformer 10 is also low. In the evaporation pipe of the boiler 6, the surface temperature is avoided to be lower than the high temperature corrosion temperature range, so that only the production steam temperature needs to be lowered.

  However, in the case of the reformer 10, when the reforming temperature is lowered, the conversion rate of the city gas 12 is lowered and the production efficiency of the hydrogen 14 is lowered. Moreover, if it installs in a low temperature range rather than a high temperature corrosion temperature range, the amount of hydrogen produced when the city gas 12 has the same flow rate is reduced by several tens.

Unlike metals, ceramics do not corrode. For example, SiC, which is a typical ceramic, cannot be used because it chemically reacts with Na ₂ O contained in dust in the flue gas 23.

  If the surface temperature is 800 to 950 ° C., the dust in the waste combustion exhaust gas 23 which is an adhering substance does not melt, so that the molten salt corrosion is sufficiently small. However, when a sufficient amount of time passes while the metal is in a high temperature state, the creep strength decreases drastically, and the higher the temperature, the more remarkable. The metal having sufficient strength in the 900 ° C. region is extremely expensive.

  Even if a suitable metal is used at a temperature higher than the high temperature corrosion temperature range, the corrosion rate is sufficiently large and the life is short. Further, if the temperature is locally low at one place on the surface of the reformer 10 and is in the high temperature corrosion temperature range, the erosion proceeds violently from that portion. Furthermore, when the temperature is locally high, the strength of the portion is lowered and a defect may occur. Therefore, a method of using in a temperature range higher than the high temperature corrosion temperature range is not realistic.

JP 2007-191370 A JP 2008-179487 A

  As described above, in the conventional reformed gas production system and hydrogen production system, when corrosive gas such as waste combustion exhaust gas is used, the production efficiency of reformed gas or hydrogen is reduced due to temperature limitation. There was a problem.

  Furthermore, high-temperature fluids that cannot sufficiently raise the reforming temperature regardless of the presence or absence of corrosiveness exist in many industrial processes, etc., but the production system of improved gas or hydrogen with high production efficiency using this heat Is desired.

  In view of the above-mentioned problems, the present invention uses a recovered gas from corrosive gas such as waste combustion exhaust gas or high-temperature fluid at a temperature at which the reforming temperature cannot be raised sufficiently. An object of the present invention is to provide a reformed gas or hydrogen production system that improves production efficiency when producing hydrogen.

  In order to solve the above-described problems, a reformed gas production system according to an embodiment of the present invention is disposed in a flow path of a high-temperature fluid and steam together with an input containing one or more of hydrocarbon, ether or alcohol. , The reformer that generates the reformed gas containing hydrogen by steam reforming using the heat of the high-temperature fluid in the flow path, and the hydrogen is separated from the reformed gas or the gas whose reformed gas has been changed. A hydrogen separator, and the substance after the hydrogen is separated flows into the reformer.

It is the schematic explaining an example of the hydrogen production system which concerns on 1st Example of this invention. It is the schematic explaining an example of the hydrogen production system which concerns on the modification of 1st Example. It is the schematic explaining an example of the hydrogen production system which concerns on 2nd Example of this invention. It is the schematic explaining an example of the hydrogen production system which concerns on the 1st modification of 2nd Example. It is the schematic explaining an example of the reformed gas manufacturing system which concerns on the 2nd modification of 2nd Example. It is the schematic explaining an example of the hydrogen production system which concerns on 3rd Example. It is the schematic explaining an example of the reformed gas manufacturing system which concerns on the modification of 3rd Example. It is the schematic explaining an example of the hydrogen production system which concerns on 4th Example. It is the schematic explaining an example of the reformed gas manufacturing system which concerns on the modification of 4th Example. It is the schematic explaining an example of the hydrogen production system which concerns on 5th Example. It is the schematic explaining an example of the reformed gas manufacturing system which concerns on the 1st modification of 5th Example. It is the schematic explaining an example of the hydrogen production system which concerns on the 2nd modification of 5th Example. It is the schematic explaining an example of the hydrogen production system which concerns on 13th Example. It is the schematic explaining an example of the hydrogen production system which concerns on the modification of 13th Example. It is the schematic explaining an example of the hydrogen production system concerning 15th Example. It is the schematic explaining an example of the hydrogen production system which concerns on 16th Example. It is the schematic explaining an example of the hydrogen production system based on 17th Example. It is the schematic explaining an example of the hydrogen production system based on 18th Example. It is the schematic explaining an example of the hydrogen production system based on 19th Example. It is the schematic explaining an example of the hydrogen production system which concerns on 20th Example. It is the schematic explaining an example of the hydrogen production system which concerns on 21st Example. It is the schematic explaining an example of the hydrogen production system based on 22nd Example. It is the schematic explaining an example of the hydrogen production system which concerns on 23rd Example. It is the schematic explaining an example of the hydrogen production system which concerns on 24th Example. It is the schematic explaining an example of the hydrogen production system which concerns on a 1st prior art example. It is the schematic explaining an example of the hydrogen production system which concerns on a 2nd prior art example. It is the schematic explaining an example of the hydrogen production system which concerns on a 3rd prior art example. It is the schematic explaining an example of the hydrogen production system which concerns on a 4th prior art example. It is a figure explaining the temperature dependence of a corrosion rate.

  Hereinafter, a hydrogen production system and a reformed gas production system according to an embodiment of the present invention will be described with reference to the drawings. In the following description, the same components are denoted by the same reference numerals and description thereof is omitted. Moreover, in each figure, the apparatus etc. (pump etc.) utilized for conveyance of each substance are abbreviate | omitting illustration. Note that the same components as those described above with reference to FIGS. 25 to 28 will be described using the same reference numerals.

<First embodiment>
A hydrogen production system according to a first embodiment of the present invention will be described with reference to FIG. The hydrogen production system shown in FIG. 1 includes an incinerator 1, and waste 2 and combustion air 3 are introduced into the incinerator 1 to burn the waste 2. In the incinerator 1, the ash 4 and the first combustion exhaust gas 23 are generated by combustion, and the ash 4 is discharged from the incinerator 1. The incinerator 1 has a boiler 6, and the boiler 6 causes boiler feed water 7 to flow out as boiler steam 5. Further, the combustion exhaust gas 23 is heated to lower the temperature and flows out as incinerator exhaust gas 8.

  The incinerator 1 has a reformer 10 that contains a reforming catalyst and reforms the reforming raw material 11 in which the city gas 12 and the steam 13 that flow in are mixed. As shown in FIG. 1, in the hydrogen production system according to the first embodiment, boiler steam 5 flowing out from the boiler 6 is used as the steam 13 mixed with the city gas 12.

  Further, as shown in FIG. 1, the hydrogen production system according to the first embodiment is obtained by a carbon monoxide converter 19 that changes carbon monoxide from the reformed gas 17 to carbon dioxide, and a carbon monoxide converter 19. A carbon dioxide separator 15 that separates carbon dioxide 21 from the transformed gas 18 is provided, and a hydrogen separator 16 that separates hydrogen 14 from the separated gas 22 from which carbon dioxide has been separated by the carbon dioxide separator 15.

  In the hydrogen production system according to the first embodiment, a gas 20 other than hydrogen from which hydrogen 14 has been separated by the hydrogen separator 16 is caused to flow into the reformer 10. In the example shown in FIG. 1, the gas 20 other than hydrogen flowing out from the hydrogen separator 16 is mixed with the city gas 12, but the hydrogen may be mixed at any point in time, and the city gas 12 and the steam 13 may be mixed. The gas 20 may be merged with the raw material 11, or the gas 20 may be mixed with the city gas 12 and the steam 13 before mixing.

  For example, if the reforming temperature in the reformer 10 is sufficiently lowered with the second conventional example shown in FIG. 26, the conversion rate decreases, so that the hydrogen in the reformed gas 17 is small. Therefore, there is a large amount of unconverted methane, and ethane, which is a hydrocarbon, is also generated. Therefore, methane and ethane also increase in the gas 20 other than hydrogen and are not used for hydrogen production, such as flowing into the incinerator 1 as in the third conventional example shown in FIG.

  In the hydrogen production system according to the first embodiment, the gas 20 other than hydrogen is returned to the reformer 10. At this time, the number of moles of carbon atoms contained in the reforming raw material 11 is increasing. Since most of the gases 20 other than hydrogen are hydrocarbons and a small amount of carbon monoxide, the steam reforming reaction does not shift in the reverse direction. Further, since carbon dioxide contained in the gas 20 other than hydrogen is small, it may be considered that there is no generation of carbon monoxide corresponding to the reverse reaction of the reaction inside the carbon monoxide converter 19.

  If the conversion rate is low even if the carbon monoxide converter 19 and the carbon dioxide separator 15 are not present, most of the gases 20 other than hydrogen are hydrocarbons, so that carbon monoxide flowing into the reformer 10 Carbon dioxide is a trace amount.

  Although the hydrogen separation efficiency of the hydrogen separator 16 is not 100%, the amount of hydrogen contained in the gas 20 other than hydrogen flowing out from the hydrogen separator 16 is very small. If the hydrogen separation efficiency is low, the hydrogen contained in the gas 20 other than hydrogen is not combusted in the incinerator 1 by allowing the gas 20 other than hydrogen to flow into the reformer 10. improves.

  Since the reforming temperature in the reformer 10 is low, the conversion rate is low, but the necessary city gas 12 is required when producing the same amount of hydrogen 14 as the hydrogen production system according to the second conventional example shown in FIG. The amount of is approximately the same. At this time, a large amount of hydrocarbon circulates in the system flow path. In the hydrogen production system according to the second conventional example and the hydrogen production system according to the first embodiment shown in FIG. 1, if the molar flow rate ratio between the carbon atom and the steam 13 held in the reforming raw material 11 is the same, Since the molar flow rate ratio between the city gas 12 and the steam 13 is different, the flow rate of the steam 13 is increased.

  For example, in the second conventional hydrogen production system shown in FIG. 26, the conversion is 0.95 at the reforming temperature of 830 ° C., and in the hydrogen production system according to the first embodiment shown in FIG. The conversion becomes 0.20 at 420 ° C. At this time, in the hydrogen production system according to the first embodiment, the required amount of city gas 12 with respect to the production amount of hydrogen 14 is 0.94 times that of the hydrogen production system according to the second conventional example. Equivalent to, or reduced from, the hydrogen production system. Even if the reforming temperature is further lowered, if the molar flow ratio of the city gas 12 and the steam 13 is adjusted, the required amount of the city gas 12 is almost the same as that of the second conventional hydrogen production system. However, in the hydrogen production system according to the first embodiment, the circulation amount of hydrocarbons in the system flow path is larger than that in the second conventional hydrogen production system.

  In the example shown in FIG. 1, the reformer 10 is installed inside the incinerator 1 and the combustion exhaust gas 23 is used, but it may be installed in a place other than the incinerator 1. That is, since the high-temperature fluid exists in many industrial processes other than the combustion exhaust gas 23, hydrogen is produced by installing the reformer 10 in the flow path of such a high-temperature fluid. .

  As described above, in the hydrogen production system according to the first embodiment, the production efficiency of hydrogen 14 can be improved even if the reformer 10 is installed in the combustion exhaust gas 23 in a temperature range that does not cause high temperature corrosion. . Moreover, in the hydrogen production system according to the first embodiment, there is little difference in the production efficiency of hydrogen regardless of whether the reforming temperature is high or low. Therefore, it exists in many industrial processes regardless of the presence or absence of corrosiveness. The heat of the high-temperature fluid at a temperature at which the reforming temperature cannot be sufficiently raised can be used.

<Modification>
FIG. 2 is an example of a hydrogen production system according to a modification of the first embodiment, in which a pressure swing adsorption separation method is used for the hydrogen separator 16. In the hydrogen production system shown in FIG. 2, compared to the hydrogen production system described above with reference to FIG. 1, the hydrogen separator 16 separates the separated gas 22 into the first liquid 29 and the first gas 55. The gas-liquid separator, the compressor 30 that compresses the first gas 55 into the pressurizing gas 31, the cooler 32 that cools the pressurizing gas 31, and the second liquid 56 and the second gas from the cooled gas 34. The second gas-liquid separator 38 is separated into 39 and the hydrogen separator 40 is an absorption tower that separates the second gas 39 into hydrogen 14 and gas 20 other than hydrogen.

  The hydrogen separator 16 of the hydrogen production system shown in FIG. 2 is the same as the hydrogen separator 16 according to the third conventional example described above with reference to FIG. 27, but in the hydrogen production system shown in FIG. The difference is that the gas 20 other than hydrogen separated in 16 does not flow into the incinerator 1 but mixes with the city gas 12 and flows into the reformer 10.

<Second embodiment>
A hydrogen production system according to the second embodiment of the present invention will be described with reference to FIG. The hydrogen production system shown in FIG. 3 is different from the hydrogen production system described above with reference to FIG. 1 in that a hydrocarbon separator 42 is provided.

  The hydrocarbon separator 42 is supplied with a gas 20 other than hydrogen separated from the reformed gas 17 or a gas obtained by changing the reformed gas 17 in the hydrogen separator 16, and a hydrocarbon 43 (gas in the second embodiment). And gas 44 other than hydrocarbon. In addition, the hydrocarbon 43 is mixed with the city gas 12 to form a mixed city gas 51 and flows into the reformer 10.

  The hydrogen separation efficiency of the hydrogen separator 16 and the hydrocarbon separation efficiency of the hydrocarbon separator 42 may not be 100%, and the gas 44 other than the hydrocarbons may be composed of combustible components such as hydrogen, carbon monoxide, methane, and ethane. May contain. Thus, since it is not preferable to discharge the gas 44 containing a combustible component to the outside in an unburned state, it flows into the incinerator 1 and is burned.

  In the example shown in FIG. 3, the hydrocarbon separator 42 is installed downstream of the gas 20 other than hydrogen, but the installation position of the hydrocarbon separator 42 is between the reformer 10 and the carbon monoxide converter 19. As long as the reformed gas 17 flows out from the reformer 10, such as between the carbon monoxide converter 19 and the carbon dioxide separator 15, or between the carbon dioxide separator 15 and the hydrogen separator 16, any position may be used. . In the example shown in FIG. 3, the hydrocarbon 43 separated by the hydrocarbon separator 42 is merged with the city gas 12, but before the flow into the reformer 10, the reforming raw material 11 and the steam 13 are combined. Alternatively, the hydrocarbon 43 may be merged.

  As shown in FIG. 3, a hydrocarbon separator 42 is installed at the subsequent stage of the hydrogen separator 16, and the hydrocarbon 43 is separated from the gas 20 other than hydrogen separated by the hydrogen separator 16. The hydrocarbon 43 is separated after the original purpose of separation of hydrogen.

  For example, when the reforming temperature in the reformer 10 is sufficiently lowered, the conversion rate is lowered, so that the hydrogen in the reformed gas 17 is small. Therefore, there is a large amount of unconverted methane, and ethane, which is a hydrocarbon, is also generated. For this reason, the gas 20 other than hydrogen also increases in methane and ethane and is not used for hydrogen production, such as flowing into the incinerator 1.

  In the hydrogen production system according to the second embodiment, the hydrocarbon 43 (which is a gas that is mostly hydrocarbons in the second embodiment) is returned to the reformer 10. At this time, the number of moles of carbon atoms contained in the reforming raw material 11 is increasing. Since most of the hydrocarbons 43 are methane and ethane and the amount of carbon monoxide is very small, the steam reforming reaction does not shift in the reverse direction. Further, since the carbon dioxide contained in the hydrocarbon 43 is small, it may be assumed that there is no generation of carbon monoxide corresponding to the reverse reaction of the reaction inside the carbon monoxide converter 19.

  Even if the carbon monoxide converter 19 and the carbon dioxide separator 15 are not present, if the conversion rate is low, most of the hydrocarbons 43 are methane and ethane, so that the carbon monoxide flowing into the reformer 10 and Carbon dioxide is very small. Although the hydrogen separation efficiency of the hydrogen separator 16 is not 100%, the amount of hydrogen contained in the gas 20 other than hydrogen flowing out from the hydrogen separator 16 is very small. If the hydrogen separation efficiency is low, in FIG. 3 in which the hydrocarbon separator 42 is installed downstream of the gas 20 other than hydrogen, the gas 20 other than hydrogen is caused to flow into the reformer 10, so that other than hydrogen. Since hydrogen contained in the gas 20 is not combusted in the incinerator 1, the hydrogen production efficiency is improved.

  Since the reforming temperature in the reformer 10 is low, the conversion rate is low, but the amount of city gas 12 required when producing the same hydrogen 14 as in the hydrogen production system according to the second prior art shown in FIG. Are almost identical. At this time, a large amount of hydrocarbon circulates in the system flow path. If the hydrogen production system according to the second prior art and the hydrogen production system according to the second embodiment shown in FIG. 3 have the same molar flow rate ratio between the carbon atoms and the steam 13 held in the reforming raw material 11, Since the molar flow rate ratio between the city gas 12 and the steam 13 is different, the flow rate of the steam 13 is increased.

  For example, in the second prior art hydrogen production system shown in FIG. 26, the conversion rate becomes 0.95 at a reforming temperature of 830 ° C., and in the hydrogen production system according to the second embodiment shown in FIG. The conversion becomes 0.20 at 420 ° C. At this time, in the hydrogen production system according to the second embodiment, the required amount of city gas 12 with respect to the production amount of hydrogen 14 is, for example, about 0.9 times that of the second prior art hydrogen production system. Equal or reduced and improved. If a hydrocarbon separator with high hydrocarbon separation efficiency is developed, the required amount of city gas 12 can be improved by adjusting the molar flow ratio of city gas 12 and steam 13 even if the reforming temperature is further lowered. It is almost the same as before the quality temperature was lowered. However, the circulation amount of hydrocarbons in the system flow path becomes larger than before the reforming temperature is lowered.

  In the example shown in FIG. 3, the reformer 10 is installed inside the incinerator 1 and the combustion exhaust gas 23 is used. However, the reformer 10 may be installed other than the incinerator 1. That is, since the high-temperature fluid exists in many industrial processes other than the combustion exhaust gas 23, hydrogen is produced by installing the reformer 10 in the flow path of such a high-temperature fluid. .

  As described above, in the hydrogen production system according to the second embodiment, the production efficiency of hydrogen 14 can be improved even if the reformer 10 is installed in the combustion exhaust gas 23 in a temperature range that does not cause high temperature corrosion. . Further, in the hydrogen production system according to the second embodiment, the difference in hydrogen production efficiency is small regardless of whether the reforming temperature is high or low. The heat of the hot fluid at a temperature at which the quality temperature cannot be raised sufficiently can be used.

<< First Modification >>
FIG. 4 is an example of a hydrogen production system according to a first modification of the second embodiment, in which a pressure swing adsorption separation method is used for the hydrogen separator 16. In the hydrogen production system shown in FIG. 4, the hydrogen separator 16 includes the first gas-liquid separator 54, the compressor 30, the cooler 32, and the second gas, as compared with the hydrogen production system described above with reference to FIG. 3. It consists of a liquid separator 38 and a hydrogen separator 40 as an absorption tower. In the hydrogen production system shown in FIG. 4, the gas 44 other than hydrocarbons separated by the hydrocarbon separator 42, the first liquid 29 separated by the first gas-liquid separator 54, and the second The second liquid 56 separated by the gas-liquid separator is returned to the incinerator 1 as the return fluid 41. Thereby, the return fluid 41 contains hydrogen, carbon monoxide, methane, ethane, and the like, which are combustible components, and prevents them from being released to the outside in an unburned state. As shown in FIG. 4, a large amount of liquid is separated by the first gas-liquid separator 15 and the second gas-liquid separator 38 by installing a hydrocarbon separator 42 in the subsequent stage of the hydrogen separator 16. Since the hydrocarbon can be separated later, the separation of the hydrocarbon can be facilitated.

<< Second Modification >>
FIG. 5 shows a reformed gas production system according to a second modified example of the second embodiment, in which hydrogen 14 is separated as compared with the hydrogen production system according to the second embodiment described above with reference to FIG. This is an example of a system that uses a mixed gas of carbon monoxide and hydrogen as a production gas without being necessary.

  In the reforming production system shown in FIG. 5, the reformed gas 17 flowing out from the reformer 10 flows into the cooler 32. The cooler 32 cools the reformed gas 17 with the refrigerant 33 to make a cooled gas 34. Further, the cooled gas 34 flows from the cooler 32 into the second gas-liquid separator 38.

  The second gas-liquid separator 38 separates the cooled gas 34 into the second liquid 56 and the second gas 39, and the second gas 39 flows into the hydrocarbon separator 42.

  The hydrocarbon separator 42 separates the second gas 39 into a hydrocarbon 43 and a gas 44 other than hydrocarbon, and reforms the hydrocarbon 43 (which is a gas that is mostly hydrocarbons in the second embodiment). Into the vessel 10. At this time, the gas 44 other than the hydrocarbon is a gas containing carbon monoxide and hydrogen, and is the production gas 71 of the reformed gas production system.

  Although the steam in the production gas 71 can be removed by the cooler 32 and the second gas-liquid separator 38, the cooler 32 and the second gas-liquid separator 38 are not essential components of the reformed gas production system. .

  Although the conversion rate is low because the reforming temperature in the reformer 10 is low, it is necessary to produce the same amount of hydrogen and carbon monoxide as the reformed gas production system according to the third prior art shown in FIG. The amount of the city gas 12 to become is almost the same, and is equal or reduced and improved. At this time, a large amount of hydrocarbon circulates in the system flow path.

  Note that, in the reformed gas production system according to the fourth conventional example described above with reference to FIG. 28 and the reformed gas production system shown in FIG. Since the molar flow rate ratio between the city gas 12 and the steam 13 is different, the flow rate of the steam 13 is increased. In the case of the reformed gas production system of FIG. 5 in which the hydrogen 14 can be made into the production gas 71 without being separated, there is no hydrogen separation process. A system with high production efficiency of production gas containing carbon can be realized.

  Although the reformer 10 is described as being installed inside the incinerator 1, the reformer 10 does not have to be the incinerator 1, and a high-temperature fluid that is not the combustion exhaust gas 23 exists in many industrial processes. You may install in a high temperature fluid flow path.

  Thus, the production efficiency of the production gas 71 can be improved even when the production gas 71 is a gas containing carbon monoxide and hydrogen, instead of using the production gas as hydrogen.

<Third embodiment>
A hydrogen production system according to a third embodiment of the present invention will be described with reference to FIG. The hydrogen production system shown in FIG. 6 is different from the hydrogen production system described above with reference to FIG. 2 in that a cryogenic separation system 50 is provided instead of the hydrogen separator 16.

  The cryogenic separation is a method of liquefying by compressing, cooling, and expanding another component mixed gas, and separating it into each component in the mixed gas using distillation or condensation operation. In the example shown in FIG. 6, the cryogenic separation system 50 includes a cryogenic separation water separator 46, a cryogenic separation carbon dioxide separator 27, a cryogenic separation hydrocarbon separator 72, and a cryogenic separation carbon monoxide. A separator 45 is included.

  The cryogenic separation type water separator 46 separates into the separated water 48 and the first cryogenic separation gas 47 when the transformed gas 18 flows. The cryogenic separation type carbon dioxide separator 27 separates the liquid or solid carbon dioxide 21 and the second cryogenic separation gas 28 when the first cryogenic separation gas 47 flows in. When the second cryogenic separation gas 28 flows in, the cryogenic separation type hydrocarbon separator 72 separates the hydrocarbon 43 such as methane or ethane as a liquid. Although the hydrocarbon 43 is a gas in the first and second embodiments described above, it is a liquid immediately after the cryogenic separation type hydrocarbon separator 72, but is easily heated to become a gas.

  The cryogenic separation type carbon monoxide separator 45 receives a gas 44 other than hydrocarbons and separates the carbon monoxide 49 as a liquid. The remaining gas from which the carbon monoxide 49 is separated is hydrogen 14.

  In the hydrogen production system according to the third embodiment, the hydrocarbon 43 separated by the cryogenic separation type hydrocarbon separator 72 flows out to the reformer 10.

  Even if the carbon dioxide 21 is solid, it can be easily converted into a liquid or gas by adjusting the temperature and pressure, and can be transported. In FIG. 6, the separated water 48 and the carbon monoxide 49 are caused to flow into the incinerator 1 as the return fluid 41.

  Similar to the hydrogen production system according to the second embodiment described above with reference to FIG. 3, the hydrogen production system according to the third embodiment is installed in the combustion exhaust gas 23 in a temperature range that does not cause high temperature corrosion. However, a system with high production efficiency of hydrogen 14 can be realized, and the production efficiency can be improved as compared with the prior art. In addition, since the production efficiency of hydrogen 14 does not change regardless of the reforming temperature, the heat of the high-temperature fluid that cannot sufficiently increase the reforming temperature existing in many industrial processes regardless of the presence or absence of corrosiveness. A system that uses hydrogen 14 with high production efficiency can be realized. Furthermore, if the cryogenic separation system 50 has a function of separating even hydrocarbons that are difficult to separate, the function of separating carbon dioxide can be provided relatively easily.

<Modification>
FIG. 7 shows a reformed gas production system according to a modification of the third embodiment, which requires separation of hydrogen 14 as compared with the hydrogen production system according to the third embodiment described above with reference to FIG. 1 is an example of a system using a mixed gas of carbon monoxide and hydrogen as a production gas.

  A cryogenic separation system 50 of the reformed gas production system shown in FIG. 7 includes a cryogenic separation type water separator 46, a cryogenic separation type carbon dioxide separator 27, and a cryogenic separation type hydrocarbon separator 72. 6 is different from the cryogenic separation system 50 of the hydrogen production system shown in FIG. 6 in that the cryogenic separation type carbon monoxide separator 45 is not provided.

  In the reformed gas production system shown in FIG. 7, the non-hydrocarbon gas 44 separated by the cryogenic separation type hydrocarbon separator 72 is a gas containing carbon monoxide and hydrogen, that is, the production gas 71. Since the reformed gas production system of FIG. 7 does not have the cryogenic separation type carbon monoxide separator 45, only the separated water 48 separated by the cryogenic separation type water separator 46 flows into the incinerator 1. .

  Thus, even in the reformed gas production system in which the production gas 71 may be a mixed gas of carbon monoxide and water without separating the hydrogen 14, a system with high production efficiency of the production gas 71 can be realized.

<Fourth embodiment>
A hydrogen production system according to a fourth embodiment of the present invention will be described with reference to FIG. The hydrogen production system shown in FIG. 8 is different from the hydrogen production system described above with reference to FIG. 2 in that the first liquid 29 and the second liquid 56 are reused. That is, since most of the first liquid 29 and the second liquid 56 are water, they do not return to the incinerator 1 but flow into the reformer 10 or the steam 13 as the return fluid 52. In the example shown in FIG. 8, the first liquid 29 and the second liquid 56 flow into the vapor 13, but may flow into the city gas 12.

  At this time, the flow rate of the branch steam 24 is reduced by the amount of water contained in the return fluid 52. In particular, when the reforming temperature is lowered, the conversion rate is lowered, and the steam 13 passing through the reformer 10 without reacting increases, so that a large amount of water circulates in the system flow path, and the branch steam 24 The effect of reducing the flow rate is great.

  Note that since the amount of carbon monoxide contained in the first liquid 29 and the second liquid 56 is very small, the steam reforming reaction does not shift in the reverse direction. Further, since the carbon dioxide contained in the first liquid 29 and the second liquid 56 is also small, it is possible that there is no generation of carbon monoxide corresponding to the reverse reaction of the reaction inside the carbon monoxide converter 19. Even if the carbon monoxide transformer 19 and the carbon dioxide separator 15 do not exist, the same applies.

  In the hydrogen production system according to the fourth embodiment, the flow rate of the consumed steam can be reduced.

<Modification>
FIG. 9 shows a reformed gas production system according to a modification of the fourth embodiment, which requires separation of hydrogen 14 as compared with the hydrogen production system according to the fourth embodiment described above with reference to FIG. 1 is an example of a system using a mixed gas of carbon monoxide and hydrogen as a production gas.

  The reformed gas production system shown in FIG. 9 does not need to separate carbon monoxide from hydrogen, and therefore, compared with the hydrogen separation system shown in FIG. 1 in that the gas-liquid separator 54, the compressor 30 and the hydrogen separator 40 are not provided.

  In the reformed gas production system shown in FIG. 9, the reformed gas 17 flowing out from the reformer 10 flows into the cooler 32. The cooler 32 cools the reformed gas 17 with the refrigerant 33 and causes the cooled gas 34 to flow out. The second gas-liquid separator 38 separates the cooled gas 34 flowing from the cooler 32 into a second liquid 56 and a second gas 39. The second gas 39 is a gas containing carbon monoxide and hydrogen, that is, the production gas 71.

  Further, in the reformed gas production system shown in FIG. 9, the second liquid 56 is caused to flow into the reformer 10 or the steam 13. In the example shown in FIG. 8, the second liquid 56 flows into the city gas 12, but it may flow into either the city gas 12 or the steam 13.

  The second liquid 56 is almost water, and the flow rate of the branch vapor 24 is reduced by that amount of water.

<Fifth embodiment>
A hydrogen production system according to a fifth embodiment of the present invention will be described with reference to FIG. Compared with the hydrogen production system according to the fourth embodiment described above with reference to FIG. 8, the hydrogen production system shown in FIG. 10 uses the first liquid 29 for the gas 20 other than hydrogen separated by the hydrogen separator 40. And the second liquid 56 is different from the second liquid 56 in that it flows into the reformer 10 as the return fluid 52.

  As described above, in the hydrogen production system according to the fifth embodiment, the hydrogen production efficiency can be improved even if the reformer 10 is installed in the combustion exhaust gas 23 in a temperature range that does not cause high temperature corrosion. Further, in the hydrogen production system according to the second embodiment, the difference in hydrogen production efficiency is small regardless of whether the reforming temperature is high or low. The heat of the hot fluid at a temperature at which the quality temperature cannot be raised sufficiently can be used.

  In the hydrogen production system according to the fifth embodiment, the flow rate of the consumed steam can be reduced.

<< First Modification >>
FIG. 11 shows a reformed gas production system according to a first modification of the fifth embodiment. Compared with the hydrogen production system according to the fifth embodiment described above with reference to FIG. This is an example of a reformed gas production system that uses a mixed gas of carbon monoxide and hydrogen as a production gas.

  Since the reformed gas production system shown in FIG. 11 does not need to separate carbon monoxide from hydrogen, the carbon monoxide converter 19 and the carbon dioxide separator 15 are compared with the reformed gas production system shown in FIG. The first gas-liquid separator 54, the compressor 30 and the hydrogen separator 40 are not provided.

  In the reformed gas production system shown in FIG. 11, the reformed gas 17 flowing out from the incinerator 1 flows into the cooler 32. The cooler 32 cools the reformed gas 17 with the refrigerant 33 and causes the cooled gas 34 to flow out. The second gas-liquid separator 38 separates the cooled gas 34 flowing from the cooler 32 into a second liquid 56 and a second gas 39. The second gas 39 flows into the hydrocarbon separator 42. The hydrocarbon separator 42 separates the second gas 39 into a hydrocarbon gas 43 and a gas 44 other than hydrocarbon, and causes the hydrocarbon gas 43 to flow into the reformer 10. At this time, the gas 44 other than the hydrocarbon is a gas containing carbon monoxide and hydrogen, that is, the production gas 71.

  The hydrocarbon gas 43 and the second liquid 56 are caused to flow into the reformer 10 as the return fluid 52.

<< Second Modification >>
FIG. 12 shows a hydrogen separation system according to a second modification of the fifth embodiment. Compared with the hydrogen production system according to the fifth embodiment described above with reference to FIG. The difference is that the separator 16 is not provided and the cryogenic separation system 50 is provided.

  In the hydrogen production system shown in FIG. 12, hydrocarbon 43 and water 48 are allowed to flow into reformer 10 as return fluid 52. The hydrocarbon 43 is liquid immediately after the cryogenic separation type hydrocarbon separator 72 but is easily heated to become a gas.

<Sixth embodiment>
The hydrogen production system according to the sixth embodiment can be realized with the configuration as described above with reference to FIG. In the hydrogen production system shown in FIG. 1 and the like, the reformer 10 is installed in the incinerator 1, but the hydrogen production system according to the sixth embodiment is not equipped with the reformer 10 in the incinerator 1. Install in the flue gas flow path in a temperature range that does not corrode outside.

  As described above, by installing the reformer 10 in the combustion exhaust gas flow path in a temperature range that does not cause high temperature corrosion, the production efficiency of hydrogen can be improved as in other cases. Further, in the hydrogen production system according to the sixth example, there is little difference in hydrogen production efficiency regardless of whether the reforming temperature is high or low, and therefore it exists in many industrial processes regardless of the presence or absence of corrosiveness. It is possible to use the heat of a high-temperature fluid that cannot raise the reforming temperature sufficiently high.

<Seventh embodiment>
The hydrogen production system according to the seventh embodiment can be realized with the configuration described above with reference to FIG. In the hydrogen production system according to the seventh embodiment, the non-hydrocarbon gas 44 after the hydrocarbon 43 is separated by the hydrocarbon separator 42 flows into the incinerator 1.

  The hydrogen separation efficiency and the hydrocarbon separation efficiency may not be 100%, respectively, and the gas 44 other than the hydrocarbon contains combustible components such as hydrogen, carbon monoxide, methane, and ethane. Since it should not be discharged into the incinerator 1, it can flow into the incinerator 1 and burn.

<Eighth embodiment>
Since the hydrogen production system according to the eighth embodiment can be realized by the configuration as described above with reference to FIG. 1 and the like, although not shown, the waste combustion furnace that incinerates the waste in the incinerator 1 It is.

  Since the combustion gas of waste is often a corrosive gas, it is possible to prevent a reduction in hydrogen production efficiency while being installed in the corrosive gas.

  Similarly to the hydrogen production system, in the case of the reformed gas production system as shown in FIGS. 5 and 7, etc., the incinerator 1 is a waste combustion furnace, so that it is the same as in the case of the hydrogen production system. An effect can be obtained.

<Ninth embodiment>
Since the hydrogen production system according to the ninth embodiment can be realized with the configuration as described above with reference to FIG. 1 and the like, the high-temperature fluid of the heat source corresponding to the combustion exhaust gas 23 is a corrosive fluid although illustration is omitted. And the reformer 10 is installed in the area | region which is below the high temperature corrosion temperature of the fluid.

  Thus, by installing the reformer 10 in a region that is equal to or lower than the high temperature corrosion temperature, it is possible to realize a system that prevents the reformer 10 from being corroded and does not reduce the production efficiency of the hydrogen 14.

  Similarly to the hydrogen production system, in the case of the reformed gas production system as shown in FIGS. 5 and 7, etc., the corrosive fluid is a corrosive fluid in the high temperature fluid, and the reformer 10 A similar effect can be obtained by installing in a region that is below the high temperature corrosion temperature.

<Tenth embodiment>
Since the hydrogen production system according to the tenth embodiment can be realized with the configuration described above with reference to FIG. 1 and the like, although not shown, the high-temperature fluid of the heat source corresponding to the combustion exhaust gas 23 is a corrosive fluid. And the reformer 10 is installed in the area | region where the temperature of a corrosive fluid is 160 degreeC or more and 420 degrees C or less.

  Thus, by installing the reformer 10 at a position where the temperature of the corrosive fluid is 160 ° C. or higher and 420 ° C. or lower, the degree of corrosion can be reduced and a practical life of the reformer 10 can be secured. A system that does not reduce the production efficiency of hydrogen 14 can be realized.

  Similarly to the hydrogen production system, in the case of the reformed gas production system as shown in FIGS. 5 and 7, etc., the temperature of the corrosive fluid is set in an area where the temperature is 160 ° C. or higher and 420 ° C. or lower. The same effect can be obtained.

<Eleventh embodiment>
Since the hydrogen production system according to the eleventh embodiment can be realized with the configuration described above with reference to FIG. 1 and the like, although not shown, the high-temperature fluid of the heat source corresponding to the combustion exhaust gas 23 is a corrosive fluid. And the reformer 10 is installed in the area | region where the surface temperature of the reformer 10 becomes below a high temperature corrosion temperature range in the state which is distribute | circulating the reforming raw material 11. FIG. In this case, the temperature of the corrosive fluid in contact with the reformer 10 may be a high temperature corrosion temperature range. That is, since the reformer 10 itself is cooled from the inside by the reforming raw material 11, even if the temperature of the corrosive fluid in contact with the reformer 10 is in the high temperature corrosion temperature range, the surface of the reformer 10. The temperature can be below the high temperature corrosion temperature.

  For example, the flow of the reforming raw material 11 is stopped after the temperature of the corrosive fluid is lowered from the high temperature corrosion temperature range.

  Thus, in the hydrogen production system according to the eleventh embodiment, the high-temperature fluid is a corrosive fluid, and the surface temperature of the reformer 10 is high while the reforming raw material 11 is circulated through the reformer 10. By installing the reformer 10 in a region that is equal to or lower than the corrosion temperature range, it is possible to realize a hydrogen production system that prevents the reformer 10 from being corroded and also prevents a reduction in hydrogen production efficiency.

  Further, in the hydrogen production system according to the eleventh embodiment, the reforming temperature is higher and the conversion rate is higher than in the hydrogen production system according to the eighth embodiment, so that the equipment size is reduced in the process of processing the reformed gas. In addition, the compressor power and the conveyance power can be reduced.

  Similarly to the hydrogen production system, in the case of the reformed gas production system as shown in FIGS. 5 and 7, etc., the high-temperature fluid is a corrosive fluid, and the reformer 10 is circulated through the reforming raw material 11. A similar effect can be obtained by installing the reformer 10 in a region where the surface temperature of the reformer 10 is equal to or lower than the high-temperature corrosion temperature range in the state where the reformer 10 is being used.

<Twelfth embodiment>
Since the hydrogen production system according to the twelfth embodiment can be realized with the configuration described above with reference to FIG. 1 and the like, the high-temperature fluid of the heat source corresponding to the combustion exhaust gas 23 is a corrosive fluid although illustration is omitted. And the reformer 10 is installed in the area | region whose surface temperature of the reformer 10 is 160 degreeC or more and 420 degrees C or less in the state which has distribute | circulated the reforming raw material 11. FIG. In this case, since the reformer 10 itself is cooled from the inside by the reforming raw material 11, the surface temperature of the reformer 10 can be made lower than the high temperature corrosion temperature.

 For example, the flow of the reforming raw material 11 is stopped after the temperature of the corrosive fluid is lowered from the high temperature corrosion temperature range.

 Thus, in the hydrogen production system according to the twelfth embodiment, the high-temperature fluid of the heat source corresponding to the combustion exhaust gas 23 is a corrosive fluid, and the reformer 10 is in a state where the reforming raw material 11 is circulated. By installing the reformer 10 in a region where the surface temperature is 160 ° C. or higher and 420 ° C. or lower, a hydrogen production system that prevents corrosion of the reformer 10 and prevents reduction in hydrogen production efficiency is realized. can do.

 Further, in the hydrogen production system according to the twelfth embodiment, the reforming temperature is higher and the conversion rate is higher than in the hydrogen production system according to the eighth embodiment, so that the equipment size is reduced in the process of processing the reformed gas. In addition, the compressor power and the conveyance power can be reduced.

<Thirteenth embodiment>
A hydrogen production system according to a thirteenth embodiment of the present invention will be described with reference to FIG. The hydrogen production system shown in FIG. 13 is different from the hydrogen production system described above with reference to FIG. 1 in that the valve 26 shuts off the inflow of city gas and the valve shuts off the inflow of fluid to the carbon monoxide transformer 19. 37 and a line where the fluid flowing out from the reformer 10 joins the boiler steam 5 and a valve 35 which shuts off the joining line to the boiler steam 5 are different. The hydrogen production system according to the thirteenth embodiment also includes the carbon monoxide converter 19, the carbon dioxide separator 15, and the hydrogen separator 16, but these are not shown in FIG.

  In the hydrogen production system shown in FIG. 13, the high-temperature fluid used as a heat source is a corrosive fluid. In this hydrogen production system, during the hydrogen production operation, the reforming raw material 11 that circulates inside the reformer 10 receives heat so that the material of the reformer 10 is cooled and the rise in surface temperature is suppressed. On the other hand, when the flow of the reforming raw material 11 is stopped during non-operation of hydrogen production, the material temperature of the reformer 10 rises to the same temperature as the temperature of the combustion exhaust gas 23. Therefore, if the material temperature of the reformer 10 is in the high temperature corrosion temperature range, there is a problem that the reformer 10 corrodes. In addition, the higher the material temperature of the reformer 10, the lower the creep strength and the time until it becomes less than the allowable stress is sufficiently short.

  Therefore, when the hydrogen production system is heated by the combustion exhaust gas 23 and the reforming material 11 is not circulated, the steam 13 is circulated as a cooling fluid in the flow path of the reforming material 11. When the reforming raw material 11 is not circulated and instead the steam 13 is circulated, the valve 26 and the valve 37 are closed, and the valve 25 and the valve 35 are opened. Therefore, the material of the reformer 10 is cooled by the steam 13 flowing inside. The inflow amount of the steam 13 is adjusted by the opening degree of the valves 25 and 35, and the steam 13 flowing out of the reformer 10 is not allowed to flow into the carbon monoxide converter 19 by closing the valve 37. On the other hand, in the hydrogen production system, during operation, the valve 25 and the valve 35 are closed, and the valve 26 and the valve 37 are opened.

  Thus, in the hydrogen production system according to the thirteenth embodiment, by using the steam 13 as a cooling fluid, an increase in the surface temperature of the reformer 10 can be suppressed, and corrosion of the reformer 10 can be prevented. can do. In the hydrogen production system according to the thirteenth embodiment, all or part of the steam produced by using the heat of the combustion exhaust gas 23 in the boiler 6 is used as the steam 13 for the cooling fluid of the reformer 10. Thus, an appropriate cooling gas can be easily secured.

  In the case of the reformed gas production system as shown in FIGS. 5 and 7 and the like, the same effect can be obtained by using the steam generated in the boiler in the reformer 10.

<Modification>
FIG. 14 shows a hydrogen production system according to a modification of the thirteenth embodiment. The hydrogen production system shown in FIG. 14 differs from the hydrogen production system described above with reference to FIG. 13 in that the boiler feed water 7 is used for cooling the flow path of the reforming raw material 11.

  In the hydrogen production system shown in FIG. 13, when heated by the combustion exhaust gas 23 and the reforming raw material 11 is not circulated, the steam 13 or the boiler feed water 7 is used as a cooling fluid in the flow path of the reforming raw material 11. The part is circulated as branch water 78. The steam 13 and the branch water 78 may be used simultaneously. When only the branch water 78 is allowed to flow, the valve 26, the valve 37 and the valve 25 are closed, and the valve 77 and the valve 35 are opened.

  The material of the reformer 10 is cooled by the branched water 78 flowing through the inside. The branched water 78 boils inside the reformer 10 and may flow out in a mixed state of water and steam or only in a steam state. The inflow amount of the branch water 78 is adjusted by the opening degree of the valve 77 and the valve 35, and the steam 13 flowing out of the reformer 10 is not allowed to flow into the carbon monoxide converter 19. During the hydrogen production operation, the valve 25 and the valve 35 are closed, and the valve 26 and the valve 37 are opened. When it is desired to flow only the steam 13 or both the branch water 78 and the steam 13, the valve 26, the valve 37, the valve 25, the valve 77 and the valve 35 are opened and closed so as to be realized.

  The cooling fluid is not limited to a part of the steam 13 or the boiler feed water 7, and may be a fluid that cools the flow path of the reforming raw material 11.

  As described above, in the hydrogen production system shown in FIG. 14, the steam 13 or the branched water 78 is used as a cooling fluid, so that an increase in the surface temperature of the reformer 10 can be suppressed and corrosion of the reformer is prevented. be able to. Further, in the hydrogen production system shown in FIG. 14, an appropriate cooling fluid can be easily secured by using the branch water 78 that is a part of the boiler feed water 7 as the cooling fluid of the reformer 10. At the same time, the presence of latent heat of vaporization that increases the temperature difference from the material of the reformer 10 makes it possible to cool the reformer 10 more easily.

<14th Example>
Since the hydrogen production system according to the fourteenth embodiment can be realized by the configuration as described above with reference to FIGS. 13 and 14 and the like, the illustration is omitted, but it flows out of the reformer 10 when not in operation. In this example, the pressure of the “steam or water” 36 is higher than the pressure of the production steam of the boiler 6, and the “steam or water” 36 that has flowed out of the reformer 10 flows into the production steam channel.

  In the hydrogen production system according to the fourteenth embodiment, the “steam or water” 36 becomes a part of the usable steam 75 and is cooled by passing heat to the heat utilization destination, becomes water, circulates into the boiler feed water 7. Become. “Steam or water” 36 joins the boiler steam 5. Even if the “steam or water” 36 that has passed through the reformer 10 is not in a state of only steam, the flow rate is sufficiently smaller than that of the boiler steam 5, so that when combined, all becomes steam, so it is driven by the steam after joining. A system with a steam turbine is also possible, in which case the turbine steam flow is not reduced.

<15th Example>
A hydrogen production system according to the fifteenth embodiment of the present invention will be described with reference to FIG. Compared with the hydrogen production system described above with reference to FIG. 14, the hydrogen production system illustrated in FIG. 15 includes a steam turbine 76 that is driven by an available steam 75 that is steam obtained by removing the branch steam 24 from the boiler steam 5, and steam. The difference is that a condenser 73 that cools the steam turbine exhaust 74 from the turbine 76 and a line through which “steam or water” 36 flows into the condenser 73 are provided. The steam turbine exhaust 74 is cooled by the condenser 73 to become water and circulates as boiler feed water 7, but the “steam or water” 36 that has passed through the reformer 10 is also cooled by the condenser 73 and supplied to the boiler feed water. 7 is used.

  The hydrogen production system according to the fifteenth embodiment differs from the hydrogen production system according to the fourteenth embodiment even if the pressure of the “steam or water” 36 flowing out of the reformer 10 is lower than the pressure of the boiler steam 5. Flowing.

  In the case of the reformed gas production system as shown in FIGS. 5 and 7, the same effect can be obtained by cooling the steam with the condenser 73 and reusing it.

<Example 16>
A hydrogen production system according to the sixteenth embodiment of the present invention will be described with reference to FIG. In FIG. 16, portions overlapping those in FIG. 1 are omitted. In the hydrogen production system shown in FIG. 1, the gas 20 other than hydrogen flowing out from the hydrogen separator 16 is directly mixed with the city gas 12. On the other hand, as shown in FIG. 16, in the hydrogen production system according to the sixteenth embodiment, the gas 20 other than hydrogen is decompressed by the decompression valve 53 and then mixed with the city gas 12 and flows into the reformer 10. . Note that the hydrogen separator 16 can use the pressure swing adsorption separation method as shown in FIG. 2 or other methods.

  Depending on the method of the hydrogen separator 16, if the gas 20 other than hydrogen is higher in pressure than the city gas 12, it can be introduced into the reformer 10 using a transfer device. , Can flow in without using transport equipment. However, since the reforming reaction inside the reformer 10 proceeds as the pressure decreases, the pressure reducing valve 53 depressurizes the gas 20 other than hydrogen to a pressure equal to or slightly higher than the city gas 12.

  At this time, the reforming reaction proceeds further, the conversion rate is improved, and the production amount of hydrogen 14 can be increased.

<Seventeenth embodiment>
A hydrogen production system according to the seventeenth embodiment of the present invention will be described with reference to FIG. In FIG. 17, portions overlapping those in FIGS. 3 to 7 are omitted. In the hydrogen production system shown in FIGS. 3 to 7, the hydrocarbon 43 flowing out from the hydrocarbon separator 42 or the cryogenic separation hydrocarbon separator 72 is directly mixed with the city gas 12. On the other hand, as shown in FIG. 17, in the hydrogen production system according to the seventeenth embodiment, the hydrocarbon 43 is decompressed by the decompression valve 53 and then mixed with the city gas 12 and flows into the reformer 10. The hydrocarbon separator 42 can use a pressure swing adsorption separation method, or other methods. In the case of the system using the cryogenic separation type hydrocarbon separator 72, the hydrocarbon 43 is liquid immediately after the cryogenic separation type hydrocarbon separator 72, but is easily heated to become a gas.

  Depending on the system of the hydrocarbon separator 42, if the hydrocarbon 43 is at a higher pressure than the city gas 12, it can be introduced into the reformer 10 using a transfer device, but if it is lower than the city gas 12, Inflow without using transport equipment. However, since the reforming reaction inside the reformer 10 proceeds as the pressure decreases, the pressure is reduced to a pressure equal to or slightly higher than that of the city gas 12 by the pressure reducing valve 53.

  At this time, the reforming reaction proceeds further, the conversion rate is improved, and the production amount of hydrogen can be increased.

<Eighteenth embodiment>
A hydrogen production system according to the eighteenth embodiment of the present invention will be described with reference to FIG. In FIG. 18, portions overlapping those in FIGS. 8 to 12 are omitted.

  In the hydrogen production system shown in FIGS. 8 to 11, the second liquid 56 flowing out from the second gas-liquid separator 38 is directly mixed with the vapor 13. On the other hand, as shown in FIG. 18, in the hydrogen production system according to the eighteenth embodiment, the second liquid 56 is decompressed by the decompression valve 53 and then mixed with the steam 13 and flows into the reformer 10. . In FIG. 18, the second liquid 56 is allowed to flow into the vapor 13. However, the reformed gas 17 or the reformed gas 17 is not necessarily the second liquid 56 as long as the water is separated from the changed gas. Moreover, the water separation method may not be the gas-liquid separator 38.

  Further, in the hydrogen production system shown in FIG. 12, the separated water 48 flowing out from the cryogenic separation type water separator 46 is directly mixed with the steam 13. In contrast, as shown in FIG. 17, in the hydrogen production system according to the eighteenth embodiment, the separated water 48 is decompressed by the decompression valve 53 and then mixed with the steam 13 and flows into the reformer 10.

  Depending on the method of the water separator (gas-liquid separator 38, cryogenic separation type water separator 46), if the separated water (second liquid 56, separated water 48) is higher in pressure than the city gas 12, it is transported. Although it can be made to flow into reformer 10 using equipment, if it is low pressure from city gas 12, it can flow in without using transportation equipment. However, since the reforming reaction inside the reformer 10 progresses as the pressure decreases, the pressure is reduced to a pressure equal to or slightly higher than that of the city gas 12.

  At this time, the reforming reaction proceeds further, the conversion rate is improved, and the production amount of hydrogen can be increased.

<Nineteenth embodiment>
A hydrogen production system according to a nineteenth embodiment of the present invention will be described with reference to FIG. In FIG. 19, portions overlapping with FIG. 1 are omitted.

  In the hydrogen production system shown in FIG. 1, the gas 20 other than hydrogen flowing out from the hydrogen separator 16 is not processed. On the other hand, as shown in FIG. 19, the hydrogen production system according to the nineteenth embodiment includes a first heater 57 for heating the gas 20 other than hydrogen. Specifically, the first heater 57 heats the gas 20 other than hydrogen by heat recovered from the reformed gas 17 or a gas obtained by changing the reformed gas 17.

  For example, as shown in FIG. 19, when the first heater 57 causes the gas 20 other than hydrogen separated by the hydrogen separator 16 to flow into the first heater 57, the reformed gas 17 or the reformed gas 17. The gas 20 other than hydrogen is heated by the second refrigerant 58 that is heat-recovered from the gas that has been changed.

 In the hydrogen production system according to the nineteenth embodiment, by heating the gas 20 other than hydrogen, the reforming temperature becomes higher, the reforming reaction proceeds further, the conversion rate is improved, and the production amount of hydrogen 14 is increased. be able to. If the reforming temperature is kept constant, the amount of heat necessary for the temperature of the reforming raw material 11 to rise is reduced, so that the amount of heat received by the reforming raw material 11 from the combustion exhaust gas 23 is reduced. As a result, the boiler steam 5 increases, so that the amount of power generation increases if the steam turbine 76 is connected, and the amount of heat given to the heat utilization destination increases if the steam turbine 76 is not connected.

 In addition, although a heat source is required for heating, the first heater 57 can use the heat from the reformed gas 17 recovered by the second refrigerant 58 for heating the gas 20 other than hydrogen. There is no need to prepare a heat source, and an appropriate heating source can be easily introduced. In FIG. 19, illustration of the configuration in which the second refrigerant 58 recovers heat is omitted.

<20th embodiment>
A hydrogen production system according to a twentieth embodiment of the present invention will be described with reference to FIG. In FIG. 20, portions overlapping with FIGS. 3 to 6 are omitted.

  In the hydrogen production system shown in FIGS. 3 to 6, the hydrocarbon 43 flowing out from the hydrocarbon separator 42 is not treated. On the other hand, as shown in FIG. 20, the hydrogen production system according to the twentieth embodiment includes a second heater 59 that heats the hydrocarbon 43. Specifically, the second heater 59 heats the hydrocarbon 43 with heat recovered from the reformed gas 17 or a gas obtained by changing the reformed gas 17.

  For example, as shown in FIG. 20, when the second heater 59 flows in the hydrocarbon 43 separated by the hydrocarbon separator 42, the second heater 59 recovers heat from the reformed gas 17 or the gas obtained by changing the reformed gas 17. The hydrocarbon 43 is heated by the third refrigerant 60 thus obtained.

  In the hydrogen production system according to the twentieth embodiment, the method of the hydrocarbon separator 42 may not be the pressure swing adsorption separation method. In the example shown in FIG. 6, the hydrocarbon 43 is liquid immediately after the cryogenic separation type hydrocarbon separator 72, but is easily heated to become a gas.

  In the hydrogen production system according to the twentieth embodiment, heating the hydrocarbon 43 may increase the reforming temperature, further proceeding with the reforming reaction, improving the conversion rate, and increasing the production amount of hydrogen 14. it can. If the reforming temperature is kept constant, the amount of heat necessary for the temperature of the reforming raw material 11 to rise is reduced, so that the amount of heat received by the reforming raw material 11 from the combustion exhaust gas 23 is reduced. As a result, the boiler steam 5 increases, so that the amount of power generation increases if the steam turbine 76 is connected, and the amount of heat given to the heat utilization destination increases if the steam turbine 76 is not connected.

  In addition, although a heat source is required for heating, the second heater 59 can use the heat recovered by the third refrigerant 60 for heating the hydrocarbon 43, so there is no need to prepare a new heat source. There is also an effect that a suitable heating source can be easily introduced. In addition, in FIG. 20, about the structure which the 3rd refrigerant | coolant 60 collect | recovers heat, illustration is abbreviate | omitted.

<Twenty-first embodiment>
A hydrogen production system according to the twenty-first embodiment of the present invention will be described with reference to FIG. In FIG. 21, portions overlapping with FIGS. 8 to 12 are omitted.

  In the hydrogen production system shown in FIGS. 8 to 12, the return fluid 52 is not processed. On the other hand, as shown in FIG. 21, the hydrogen production system according to the 21st embodiment includes a third heater 61 for heating the return fluid 52. Specifically, the third heater 61 heats the return fluid 52 with heat recovered from the reformed gas 17 or a gas obtained by changing the reformed gas 17.

  For example, as shown in FIG. 21, when the return heater 52 flows in, the third heater 61 returns by the fourth refrigerant 62 that has recovered heat from the reformed gas 17 or the gas that has changed the reformed gas 17. The fluid 52 is heated.

  In the example shown in FIG. 8, the return fluid 52 is a liquid obtained by mixing the first liquid 29 and the second liquid 56. In the example shown in FIG. 9, the return fluid 52 corresponds to the second liquid 56. . Further, the water separation method is not limited to the first liquid 29 and the second liquid 56 as long as the reformed gas 17 or the reformed gas 17 is water separated from the changed gas. It does not have to be the same method. In the case of the example shown in FIG. 11, the separated water 48 from the cryogenic separation type water separator 46 is heated by the third heater 61 and then flows into the reformer 10.

  By heating the return fluid 52, the reforming temperature becomes higher, the reforming reaction proceeds further, the conversion rate is improved, and the production amount of hydrogen increases. If the reforming temperature is kept constant, the amount of heat necessary for the temperature of the reforming raw material 11 to rise is reduced, so that the amount of heat received by the reforming raw material 11 from the combustion exhaust gas 23 is reduced. As a result, the boiler steam 5 increases, so that the amount of power generation increases if the steam turbine 76 is connected, and the amount of heat given to the heat utilization destination increases if the steam turbine 76 is not connected.

  Although a heat source is required for heating, in the hydrogen production system according to the twenty-first embodiment, since the heat recovered by the fourth refrigerant 62 can be used for heating the return fluid 52, it is necessary to newly provide a heat source. In addition, a suitable heating source can be easily introduced. In FIG. 21, the illustration of the configuration in which the fourth refrigerant 62 recovers heat is omitted.

<Twenty-second embodiment>
A hydrogen production system according to the 22nd embodiment will be described with reference to FIG. In FIG. 22, illustrations of the same components as those in FIGS. 1 to 4, 8, and 10 are omitted.

The carbon dioxide separator 15 of the hydrogen production system shown in FIG. 1 to FIG. 4, FIG. 8 and FIG. 10 includes a cooling step, whereas the carbon dioxide separator 15 of the hydrogen production system shown in FIG. Uses the heat recovered by the cooling process as the heat recovered from the reformed gas 17 or the gas obtained by changing the reformed gas 17, although the cooling method differs depending on the method of the carbon dioxide separator 15. In the process, there are cooling for adjusting the temperature of the modified gas 18 and cooling in a hot potassium carbonate system. The carbon dioxide separator 15 circulates the fifth refrigerant 69 in the carbon dioxide separator 15 and recovers the heat of the modified gas 18, for example. Therefore, in the hydrogen production system according to the twenty-second embodiment, as shown in FIG. 22, heat is recovered by the fifth refrigerant 69 in the carbon dioxide separator 15, and the heat recovered by the sixth refrigerant 69 is stored in the system. Used in the heating process. You may utilize in the heating process of the 19th thru | or 21st Example.

  Although a heat source is required for heating, in the hydrogen production system according to the twenty-second embodiment, the heat recovered by the fifth refrigerant 69 can be used for heating the heated fluid. Therefore, it is necessary to newly provide a heat source. And an appropriate heating source can be easily introduced. In FIG. 22, illustration of the configuration for heating the fluid to be heated using the heat recovered by the fifth refrigerant 69 is omitted.

<Twenty-third example>
A hydrogen production system according to the 23rd embodiment of the present invention will be described with reference to FIG. In FIG. 23, the same configuration as in FIGS. 2, 4, 8 and 10 is omitted.

  For example, as shown in FIG. 2 and the like, in the cooler 32, when the pressurized gas 31 compressed by the compressor 30 flows in, heat is recovered by the first refrigerant 33 and cooled. In the hydrogen production system according to the twenty-third embodiment, the heat recovered by the first refrigerant 33 is used in the heating process in the system. You may utilize in the heating process of the 19th thru | or 21st Example.

  As shown in FIG. 23, the hydrogen production system according to the twenty-third embodiment has a configuration in which the generated hydrogen 14 is compressed and stored. Specifically, the hydrogen production system according to the twenty-third embodiment includes a hydrogen compressor 63 that compresses hydrogen 14, a hydrogen cooler 65 that flows in and cools compressed hydrogen gas 64 that has become hot during the compression process, A hydrogen tank 68 for storing cooled hydrogen 67 is provided. In the hydrogen cooler 65, heat is recovered by the sixth refrigerant 66. In the hydrogen production system according to the twenty-third embodiment, the heat recovered by the sixth refrigerant 66 is used in the heating process in this system. You may utilize in the heating process of the 19th thru | or 21st Example.

  Note that, depending on the gas separation method, there is a process that is performed in the order of compression, separation, and cooling. Therefore, heat recovery may be performed in a gas separation process other than hydrogen.

  Although a heat source is required for heating, in the hydrogen production system according to the 23rd embodiment, the heat recovered by the first refrigerant 33 and the sixth refrigerant 66 can be used for heating the heated fluid. Therefore, it is not necessary to provide a heat source, and an appropriate heating source can be easily introduced. In FIG. 23, the illustration of the configuration for heating the fluid to be heated using the heat recovered by the first refrigerant 33 and the sixth refrigerant 66 is omitted.

<Twenty-fourth embodiment>
A hydrogen production system according to the twenty-fourth embodiment will be described with reference to FIG. In FIG. 24, illustration of the same configuration as in FIGS. 6 and 12 is omitted.

  The cryogenic separation system 50 separates the separated water 48, the carbon dioxide 21, the hydrocarbon 43, and the carbon monoxide 49 from the conversion gas 18 flowing from the carbon monoxide converter 19 to produce hydrogen 14. Has a process gas cooling step. Accordingly, in the hydrogen production system according to the twenty-fourth embodiment, as shown in FIG. 24, heat is recovered by the seventh refrigerant 70 in the cryogenic separation system 50, and the heat recovered by the seventh refrigerant 70 is stored in the hydrogen production system. It is used in the heating process. You may utilize in the heating process of the 19th thru | or 21st Example.

  Although a heat source is required for heating, in the hydrogen production system according to the twenty-fourth embodiment, since the heat recovered by the seventh refrigerant 70 can be used for heating the heated fluid, it is necessary to newly provide a heat source. And an appropriate heating source can be easily introduced. In addition, in FIG. 24, illustration is abbreviate | omitted about the structure which heats a to-be-heated fluid using the heat source collect | recovered with the 7th refrigerant | coolant 70. FIG.

<Twenty-fifth embodiment>
Since the hydrogen production system according to the twenty-fifth embodiment is configured as described above with reference to FIGS. 6 and 20, illustration is omitted, but the hydrocarbon 43 is separated by the cryogenic separation method and separated hydrocarbons. 43 is heated by the atmosphere 79 and then flows into the reformer 10.

  Specifically, the second heater 59 uses the atmosphere 79 for the third refrigerant 60 that heats the hydrocarbons 43. Since the hydrocarbon 43 flowing out from the hydrocarbon separator 42 is sufficiently cooler than the atmosphere 79, the second heater 59 can heat the hydrocarbon 43 by the atmosphere 79. Further, in the second heater 59, heating by the air 79 and heating by another refrigerant may be performed simultaneously. The hydrocarbon 43 is liquid immediately after the cryogenic separation type hydrocarbon separator 72, but is easily heated to become a gas.

  Although a heat source is required for heating, the hydrogen production system according to the 25th embodiment uses the atmosphere 79 as a refrigerant for heating the hydrocarbon 43, so there is no need to provide a new heat source, and an appropriate heating source can be easily provided. Can be introduced. In the case of the reformed gas production system as shown in FIGS. 5 and 7 and the like, the same effect can be obtained by using the atmosphere as the refrigerant for heating the hydrocarbon 43.

<Twenty-sixth embodiment>
Since the hydrogen production system according to the twenty-sixth embodiment is configured as described above with reference to FIGS. 12 and 21, illustration is omitted, but water is separated by a cryogenic separation method, and separated separated water 48 is separated. Is heated by the atmosphere 79 and then flows into the reformer 10.

  Specifically, the third heater 61 uses the atmosphere 79 as the fourth refrigerant 62 that heats the separated water 48. Since the separated water 48 flowing out from the cryogenic separation type water separator 46 is sufficiently lower in temperature than the atmosphere 79, the third heater 61 can heat the separated water 48 by the atmosphere 79. Moreover, in the 3rd heater 61, you may implement simultaneously the heating by the air | atmosphere 79, and the heating by another refrigerant | coolant.

  Although a heat source is required for heating, in the hydrogen production system according to the twenty-sixth embodiment, since the atmosphere 79 is used as a refrigerant for heating the separated water 48, it is not necessary to newly provide a heat source, and an appropriate heating source can be easily provided. Can be introduced.

<Twenty-seventh embodiment>
Since the hydrogen production system according to the twenty-seventh embodiment can be realized with the configuration described above with reference to FIGS. 1 to 15, illustration is omitted, but heat from the boiler steam 5 is supplied to the outside, When supplying the energy obtained in the system to the outside, such as supplying the electric power generated using the steam turbine 76 to the outside, it is possible to meet the energy demand.

  In the hydrogen production system according to the twenty-seventh embodiment, hydrogen production is executed when the energy demand of the power supply destination is equal to or less than a predetermined value. On the other hand, in the hydrogen production system according to the 27th embodiment, the hydrogen production operation is stopped when the energy demand exceeds a predetermined value. That is, when a lot of energy such as electric power is used during the daytime and the energy demand is high, the hydrogen production is stopped, and when the energy supply is low at the nighttime or the like and the energy is left, the hydrogen production is executed.

  Since the hydrogen production system uses the steam 13, when the steam obtained by removing the branch steam 24 from the boiler steam 5 is sent to the heat supply source, the heat supply amount is reduced and the steam turbine 76 generates power. Since the available steam 75 to the steam turbine 76 decreases, the power generation amount decreases and the power supply amount decreases, so that the energy supply amount to the energy supply destination decreases during hydrogen production. Moreover, when supplying electric power, compressor power and conveyance power are consumed, and the amount of electric power supplied to the outside decreases. Therefore, the hydrogen production system responds to the energy demand of the supplier by operating only when the energy demand is below a predetermined value.

  The technology that can arrange the reformer 10 in a place where the temperature of the high-temperature fluid is lower facilitates the treatment of the reformer 10 when the hydrogen production is stopped and the start / stop switching of the hydrogen production operation. It is possible. In the case of the reformed gas production system as shown in FIGS. 5 and 7 and the like, the same effect can be obtained by operating according to the energy demand.

DESCRIPTION OF SYMBOLS 1 ... Incinerator 2 ... Waste 3 ... Combustion air 4 ... Ash 5 ... Boiler steam 6 ... Boiler 7 ... Boiler feed water 8 ... Incinerator exhaust gas 9 ... Bag filter inflow gas 10 ... Reformer 11 ... Reforming raw material 12 ... City gas 13 ... Steam 14 ... Hydrogen 15 ... Carbon dioxide separator 16 ... Hydrogen separator 17 ... Reformed gas 18 ... Modified gas 19 ... Carbon monoxide converter 20 ... Gas (substance) other than hydrogen
21 ... carbon dioxide 22 ... separated gas 23 ... combustion exhaust gas (first combustion exhaust gas)
24 ... Branch steam 25 ... Valve (pressure reducing valve)
26 ... Valve 27 ... Cryogenic separation type carbon dioxide separator 28 ... Second cryogenic separation gas 29 ... First liquid 30 ... Compressor 31 ... Pressurized gas 32 ... Cooler 33 ... Refrigerant (first refrigerant)
34 ... Cooled gas 35 ... Valve 36 ... Steam or water 37 ... Valve 38 ... Gas-liquid separator (second gas-liquid separator)
39 ... Second gas 40 ... Hydrogen separator 41 ... Return fluid 42 ... Hydrocarbon separator 43 ... Hydrocarbon 44 ... Gas other than hydrocarbon 45 ... Deep cold separation type carbon monoxide separator 46 ... Deep cold separation type water Separator 47: first cryogenic separation gas 48 ... separation water 49 ... carbon monoxide 50 ... cryogenic separation system 51 ... mixed city gas 52 ... return fluid 53 ... pressure reducing valve 54 ... first gas-liquid separator 55 ... 1st gas 56 ... 2nd liquid 57 ... 1st heater 58 ... 2nd refrigerant | coolant 59 ... 2nd heater 60 ... 3rd refrigerant | coolant 61 ... 3rd heater 62 ... 4th refrigerant | coolant 63 ... Hydrogen compressor 64 ... Compressed hydrogen 65 ... Hydrogen cooler 66 ... Sixth refrigerant 67 ... Cooled hydrogen 68 ... Hydrogen tank 69 ... Fifth refrigerant 70 ... Seventh refrigerant 71 ... Production gas 72 ... Deep cooling separation type Hydrocarbon separator 73 ... condenser 74 ... steam turbine exhaust 7 ... available steam 76 ... steam turbine 77 ... valve 78 ... branch water 79 ... Air

Claims (33)

A reformed gas containing hydrogen by steam reforming using the heat of the high-temperature fluid when the steam flows together with an input containing one or more of hydrocarbon, ether or alcohol, disposed in the flow path of the high-temperature fluid A reformed gas or hydrogen production system comprising a reformer that generates
Comprising a hydrogen separator for separating hydrogen from the exhaust gas of the reformer or a gas obtained by changing the exhaust gas;
A reformed gas or hydrogen production system, wherein a substance after hydrogen is separated by the hydrogen separator is caused to flow into the reformer. A reformed gas containing hydrogen by steam reforming using the heat of the high-temperature fluid when the steam flows together with an input containing one or more of hydrocarbon, ether or alcohol, disposed in the flow path of the high-temperature fluid A reformed gas or hydrogen production system comprising a reformer that generates
A hydrocarbon separator for separating hydrocarbons from the exhaust gas of the reformer or a gas obtained by changing the exhaust gas;
A reformed gas or hydrogen production system, wherein a substance containing hydrocarbons separated by the hydrocarbon separator is caused to flow into the reformer. Comprising a hydrogen separator for separating hydrogen from the exhaust gas of the reformer or a gas obtained by changing the exhaust gas;
The reformed gas or hydrogen production system according to claim 2, wherein the substance after hydrogen is separated by the hydrogen separator is caused to flow into the hydrocarbon separator. A transformer for generating carbon dioxide and hydrogen by causing the reformer exhaust gas or a gas obtained by changing the exhaust gas to flow and reacting carbon monoxide and water vapor;
A carbon dioxide separator that separates carbon dioxide from the gas that has passed through the transformer and that causes the gas from which carbon dioxide has been separated to flow into the hydrogen separator;
The reformed gas or hydrogen production system according to claim 1 or 3, characterized by comprising: A transformer for generating carbon dioxide and hydrogen by causing the reformer exhaust gas or a gas obtained by changing the exhaust gas to flow and reacting carbon monoxide and water vapor;
A carbon dioxide separator that separates carbon dioxide from the gas that has passed through the transformer;
A hydrogen separator for separating hydrogen from the gas passed through the carbon dioxide separator;
The reformed gas or hydrogen production system according to claim 2, comprising:   6. The reformed gas or hydrogen production system according to claim 2, 3 or 5, wherein the hydrocarbon separator separates hydrocarbons by a pressure swing adsorption method.   6. The reformed gas or hydrogen production system according to claim 2, wherein the hydrocarbon separation device separates hydrocarbons by a cryogenic separation method. A reformed gas containing hydrogen by steam reforming using the heat of the high-temperature fluid when the steam is introduced together with an input containing one or more of hydrocarbon, ether or alcohol, installed in the flow path of the high-temperature fluid A reformed gas or hydrogen production system comprising a reformer for generating
Comprising a water separator for separating water from the reformer exhaust gas or a gas obtained by changing the exhaust gas;
A system for producing reformed gas or hydrogen, wherein water separated by the water separator is introduced into the reformer or a flow path for supplying steam to the reformer. Comprising a water separator for separating water from the reformer exhaust gas or a gas obtained by changing the exhaust gas;
The system for producing reformed gas or hydrogen according to claim 1, wherein water separated by the water separator is caused to flow into the reformer or a flow path for supplying steam to the reformer.   10. The reformed gas or hydrogen production system according to claim 1, wherein the high-temperature fluid flow path is a combustion exhaust gas flow path of an incinerator. The flow path of the high-temperature fluid is a combustion exhaust gas flow path of an incinerator;
The reformed gas or hydrogen production system according to claim 2, 3, 5, 6, or 7, wherein the hydrocarbon separator causes the substance after separating hydrocarbons to flow into the incinerator. .   The system for producing reformed gas or hydrogen according to claim 10 or 11, wherein the incinerator is a furnace for combusting waste. The hot fluid is a corrosive fluid;
The reformer is disposed in a region where the high temperature fluid is below a high temperature corrosion temperature range,
The reformed gas or hydrogen production system according to claim 1, wherein: The hot fluid is a corrosive fluid;
The reformer is disposed in a region where the temperature of the hot fluid is 160 ° C. or higher and 420 ° C. or lower.
The reformed gas or hydrogen production system according to claim 1, wherein: The hot fluid is a corrosive fluid;
The reformer is installed in a region where the surface temperature of the reformer is equal to or lower than the high temperature corrosion temperature range when the input is in circulation.
The reformed gas or hydrogen production system according to claim 1, wherein: The hot fluid is a corrosive fluid;
The reformer is installed in a region in which the surface temperature of the reformer is 160 ° C. or higher and 420 ° C. or lower in a state where the input is being circulated.
The reformed gas or hydrogen production system according to claim 1, wherein: The hot fluid is a corrosive fluid;
When the surface temperature of the reformer is not less than the high temperature corrosion temperature range without flowing the input to the reformer, the cooling fluid is circulated through the flow path of the input.
The system for producing a reformed gas or hydrogen according to claim 15 or 16, characterized in that: The flow path of the high temperature fluid is a combustion exhaust gas flow path of an incinerator,
The cooling fluid includes a part or all of the steam produced by utilizing the heat of the combustion exhaust gas in a boiler installed in the incinerator.
The reformed gas or hydrogen production system according to claim 17, wherein: The flow path of the high temperature fluid is a combustion exhaust gas flow path of an incinerator,
The cooling fluid includes a part or all of the feed water of a boiler installed in the incinerator.
The reformed gas or hydrogen production system according to claim 17. The flow path of the high temperature fluid is a combustion exhaust gas flow path of an incinerator,
When circulating the cooling fluid through the flow path of the input, the pressure of the cooling fluid flowing out of the reformer is higher than the pressure of the boiler production steam installed in the incinerator and flows out of the reformer. Supplying a cooling fluid to the flow path of the production steam;
20. The system for producing reformed gas or hydrogen according to claim 17 or 19, characterized in that: The flow path of the high temperature fluid is a combustion exhaust gas flow path of an incinerator,
Comprising a steam turbine driven by steam produced by a boiler installed in the incinerator;
When the surface temperature of the reformer is higher than the high temperature corrosion temperature range without letting the input flow into the reformer, the steam flow path of the steam turbine or the condenser into which the exhaust flows, Injecting steam or water flowing out of the reformer,
The reformed gas or hydrogen production system according to any one of claims 17 to 19, characterized by things.   4. The reformed gas or hydrogen production system according to claim 1 or 3, wherein a substance other than hydrogen separated from hydrogen by the hydrogen separator is decompressed and then introduced into the reformer.   8. The reformed gas or hydrogen according to claim 2, 3, 5, 6 or 7, wherein the hydrocarbon-containing substance separated by the hydrocarbon separator is decompressed and then introduced into the reformer. Manufacturing system.   11. The reformed gas or hydrogen gas according to claim 9, wherein the water separated by the water separator is depressurized and then introduced into the reformer or a steam flow path to the reformer. Manufacturing system.   2. The substance other than hydrogen separated by the hydrogen separator is heated by heat recovered from the exhaust gas or a gas obtained by changing the exhaust gas, and then flows into the reformer. Or the reformed gas or hydrogen production system according to 3.   The substance containing hydrocarbons separated by the hydrocarbon separator is heated by heat recovered from the exhaust gas or a gas obtained by changing the exhaust gas, and then flows into the reformer. Item 8. The reformed gas or hydrogen production system according to Item 2 to 7.   The water separated by the water separator is heated by heat recovered from the exhaust gas or a gas obtained by changing the exhaust gas, and flows into the reformer. Reformed gas or hydrogen production system. Comprising a carbon dioxide separator for separating carbon dioxide from the exhaust gas or a gas obtained by changing the exhaust gas;
28. The reformed gas or hydrogen production system according to claim 25, wherein the recovered heat is heat recovered by a cooling step in the carbon dioxide separator. Comprising compression means for compressing the exhaust gas or a gas obtained by changing the exhaust gas;
28. The reformed gas or hydrogen production system according to claim 25, wherein the recovered heat is heat recovered by cooling the compressed gas. Equipped with a separator using a cryogenic separation method,
28. The reformed gas or hydrogen production system according to claim 25, wherein the recovered heat is heat recovered by a cooling step in a cryogenic separation method. The hydrocarbon separator separates hydrocarbons by a cryogenic separation method,
The reformed gas or hydrogen gas according to claim 7, wherein the separated hydrocarbon-containing substance is heated by the atmosphere and then flows into the reformer or a steam flow path to the reformer. Manufacturing system. The water separator separates water by a cryogenic separation method,
The system for producing a reformed gas or hydrogen according to claim 8 or 9, wherein the separated water is heated by the atmosphere and then flows into the reformer or a steam flow path to the reformer. . Supply means for supplying energy obtained from the high-temperature fluid to the outside of the system;
When the energy demand of the energy supply destination is below a predetermined value, the operation for producing reformed gas or hydrogen is performed, and the operation for producing the reformed gas or hydrogen is stopped when the energy demand exceeds the predetermined value. A system for producing a reformed gas or hydrogen according to claim 1.

Images