WO2023047937A1 - 液体水素気化装置及び水素を生成する生成方法 - Google Patents

液体水素気化装置及び水素を生成する生成方法 Download PDF

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Publication number
WO2023047937A1
WO2023047937A1 PCT/JP2022/033372 JP2022033372W WO2023047937A1 WO 2023047937 A1 WO2023047937 A1 WO 2023047937A1 JP 2022033372 W JP2022033372 W JP 2022033372W WO 2023047937 A1 WO2023047937 A1 WO 2023047937A1
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Prior art keywords
hydrogen
liquid hydrogen
heat exchanger
flow channel
temperature
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PCT/JP2022/033372
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English (en)
French (fr)
Japanese (ja)
Inventor
慎二 江頭
朝寛 鈴木
慶彦 鶴
涼馬 中森
Original Assignee
株式会社神戸製鋼所
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Application filed by 株式会社神戸製鋼所 filed Critical 株式会社神戸製鋼所
Priority to CN202280062741.5A priority Critical patent/CN117999453A/zh
Priority to EP22872693.1A priority patent/EP4386300A1/en
Priority to KR1020247011091A priority patent/KR20240058904A/ko
Publication of WO2023047937A1 publication Critical patent/WO2023047937A1/ja

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D3/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium flows in a continuous film, or trickles freely, over the conduits
    • F28D3/02—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium flows in a continuous film, or trickles freely, over the conduits with tubular conduits
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F19/00—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/26—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/01—Pure fluids
    • F17C2221/012—Hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F17C2227/0316—Water heating
    • F17C2227/0318—Water heating using seawater
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification

Definitions

  • the present invention relates to a liquid hydrogen vaporizer and a production method for producing hydrogen.
  • Patent Literature 1 discloses an open-rack vaporizer that vaporizes a low-temperature liquefied gas by exchanging heat between the low-temperature liquefied gas and a heating fluid.
  • this open rack type vaporizer 600 includes heat exchange panels 612, 622 provided with a number of heat transfer tubes 614, 624, and a and a heat source medium supply unit provided with a trough (not shown) of.
  • the liquefied natural gas in the heat transfer tubes 614, 624 is vaporized by exchanging heat between the liquefied natural gas flowing in the heat transfer tubes and the seawater flowing down the outer surfaces of the heat transfer tubes 614, 624.
  • liquid hydrogen As an alternative fuel to liquefied natural gas is being considered for the purpose of reducing carbon dioxide emissions.
  • the liquefied hydrogen is heated to room temperature before being supplied to the power generator.
  • the temperature of liquid hydrogen 253°C
  • the temperature of liquefied natural gas -162°C. Therefore, when liquefied hydrogen is vaporized using an open-rack type vaporizer for liquefied natural gas, the thermal stress generated in the heat transfer tubes tends to increase, and the heated fluid tends to ice on the outer surfaces of the heat transfer tubes. becomes easier.
  • the object of the present invention is to suppress icing on the heat transfer tubes of an open rack heat exchanger while relieving thermal stress in the heat transfer tubes of a liquid hydrogen vaporizer.
  • the liquid hydrogen vaporizer in the present disclosure is a liquid hydrogen vaporizer that generates gaseous or supercritical hydrogen from liquid hydrogen by heat exchange with a heated fluid having a freezing point lower than that of seawater or industrial water.
  • An auxiliary heat exchanger for raising the temperature of liquid hydrogen, a heat transfer tube for flowing hydrogen, and a trough portion for supplying seawater or industrial water to the outer surface of the heat transfer tube, and hydrogen flowing out from the auxiliary heat exchanger is replaced by seawater or an open-rack type main heat exchanger that raises the temperature by exchanging heat with industrial water.
  • a liquid hydrogen vaporizer is a liquid hydrogen vaporizer that generates gaseous or supercritical hydrogen from liquid hydrogen, and includes a heat transfer tube for circulating hydrogen and seawater or industrial water on the outer surface of the heat transfer tube.
  • an open-rack type main heat exchanger having a trough portion for supplying industrial water and raising the temperature of hydrogen in the heat transfer tubes by heat exchange with seawater or industrial water; a main flow path connected to the main heat exchanger;
  • the split flow channel is connected to the main flow channel so that the heated hydrogen flowing through the first split flow channel and the liquid hydrogen flowing through the second split flow channel are merged and flowed into the main flow channel. ing.
  • the magnitude of the heat load of the heating fluid required to raise the temperature of liquid hydrogen in the auxiliary heat exchanger is smaller than the magnitude of the heat load of seawater or industrial water required to raise the temperature of hydrogen in the main heat exchanger.
  • the method for producing hydrogen in the present disclosure is a method for producing gaseous or supercritical hydrogen by raising the temperature of liquid hydrogen.
  • a method of generating hydrogen according to the present disclosure is a method of generating hydrogen in a gaseous or supercritical state by raising the temperature of liquid hydrogen. and a first heating step of raising the temperature of the liquid hydrogen in the first branch channel by heat exchange with a heating fluid in an auxiliary heat exchanger provided on the first branch channel. a merging step in which the hydrogen from the first branch flow channel and the liquid hydrogen from the second branch flow channel are combined and flowed into the main flow channel; and the hydrogen in the main flow channel flows into the heat transfer tubes of the main heat exchanger. and a second heating step of heating the hydrogen in the heat transfer tubes to a predetermined temperature by heat exchange with seawater or industrial water.
  • the magnitude of the heat load of the heating fluid for raising the temperature of liquid hydrogen in the first heating step is smaller than the magnitude of the heat load of seawater or industrial water for raising the temperature of hydrogen in the second heating step.
  • FIG. 1 is a schematic diagram of a liquid hydrogen vaporizer according to a first embodiment
  • FIG. FIG. 4 is a schematic diagram of a liquid hydrogen vaporizer according to a modification of the first embodiment
  • FIG. 4 is a schematic diagram of a liquid hydrogen vaporizer according to a second embodiment
  • FIG. 5 is a schematic diagram of a liquid hydrogen vaporizer according to a modification of the second embodiment
  • FIG. 5 is a schematic diagram of a liquid hydrogen vaporizer according to a modification of the second embodiment
  • 1 is a schematic diagram of part of a conventional vaporizer for vaporizing liquefied natural gas
  • the liquid hydrogen vaporization apparatus 100 is an apparatus that uses a first heat source fluid and a second heat source fluid to raise the temperature of liquid hydrogen to generate gaseous or supercritical hydrogen.
  • Liquid hydrogen vaporizer 100 is also simply referred to as "vaporizer 100".
  • the vaporizer 100 as shown in FIG. and a connecting channel 140 to be connected.
  • the auxiliary heat exchanger 110 is an intermediate medium type heat exchanger that heats liquid hydrogen using an intermediate medium M1 that mediates heat exchange between the liquid hydrogen and the first heat source fluid. That is, in the first embodiment, the intermediate medium M1 functions as a heating fluid that raises the temperature of liquid hydrogen. Seawater or industrial water is used as the first heat source fluid. A fluid (for example, propane) having a freezing point lower than the freezing point of seawater or industrial water and a boiling point lower than the temperature of seawater or industrial water is used as the intermediate medium M1.
  • the auxiliary heat exchanger 110 includes an intermediate medium evaporating section E1 that evaporates a liquid intermediate medium M1 by heat exchange with the first heat source fluid, and a hydrogen heating section that vaporizes liquid hydrogen by heat exchange with the gaseous intermediate medium M1. E2 and.
  • the intermediate medium evaporating part E1 and the hydrogen heating part E2 share one hollow casing 112 . Therefore, in the casing 112, the intermediate medium M1 moves back and forth between the intermediate medium evaporating section E1 and the hydrogen heating section E2.
  • the casing 112 has a horizontally elongated shape and includes a pair of side walls 116 and 118 that constitute the casing 112.
  • the liquid intermediate medium M1 is stored in the lower part of the casing 112. As shown in FIG.
  • the intermediate medium evaporating section E1 and the hydrogen heating section E2 do not need to share one casing 112, but have separate casings (not shown), and both casings are connected to each other by a pipe through which the intermediate medium M1 flows. It may be a configuration that is In this case, the hydrogen heating section E2 is not limited to being positioned above the intermediate medium evaporating section E1.
  • the intermediate medium evaporating section E1 includes an inlet chamber 134 adjacent to one side wall 116, an outlet chamber 136 adjacent to the other side wall 118, and a number of heat transfer tubes 132 spanning between the inlet chamber 134 and the outlet chamber 136. , is equipped with Each heat transfer tube 132 extends in one direction and is arranged below the liquid level of the liquid intermediate medium M1 in the casing 112 .
  • the inlet chamber 134 is connected to an introduction pipe (not shown) provided with a pump or the like.
  • a first heat source fluid supplied to the inlet chamber 134 from the outside of the vaporizer 100 flows through the plurality of heat transfer tubes 132 to the outlet chamber 136 .
  • a discharge pipe (not shown) for discharging the first heat source fluid in the outlet chamber 136 from the vaporizer 100 is connected to the outlet chamber 136 .
  • the heat transfer tubes 132 of the intermediate medium evaporator E1 are arranged so as to pass through the liquid intermediate medium M1. Thereby, heat exchange is performed between the first heat source fluid flowing in the heat transfer tube 132 and the liquid intermediate medium M1.
  • the hydrogen heating section E2 includes an inlet chamber 124, an outlet chamber 126, and a large number of heat transfer tubes 122 that connect the inlet chamber 124 and the outlet chamber 126.
  • a supply pipe (not shown) is connected to the inlet chamber 124 to allow liquid hydrogen to flow in from the outside.
  • the inlet chamber 124 is positioned above the outlet chamber 136 of the intermediate medium evaporator E1, but is not limited to this position.
  • Each heat transfer tube 122 is formed in a substantially U shape, and the outlet chamber 126 is adjacent to the upper side of the inlet chamber 124 . Note that the heat transfer tube 122 does not need to be formed in a U shape, and may be configured by a straight tube, for example.
  • each heat transfer tube 122 is arranged above the liquid surface of the liquid intermediate medium M1 stored in the casing 112 . That is, each heat transfer tube 122 is positioned above the heat transfer tube 132 .
  • the outlet chamber 126 is connected with a connection flow path 140 for allowing hydrogen flowing out of the auxiliary heat exchanger 110 to flow into the main heat exchanger 150 .
  • Heat exchange is performed between the liquid hydrogen in the heat transfer tube 122 and the gaseous intermediate medium M1, and the hydrogen vaporized by the heat exchange with the gaseous intermediate medium M1 flows through the outlet chamber 126 into the connecting flow path 140. do.
  • the intermediate medium M1 liquefied by heat exchange with liquid hydrogen flows down to the intermediate medium evaporator E1 side inside the casing 112 .
  • the liquid hydrogen in the heat transfer tube 122 is heated to a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure by heat exchange with the gaseous intermediate medium M1.
  • the hydrogen heating unit E2 may be configured to heat the liquid hydrogen in the heat transfer tube 122 to a predetermined temperature below the boiling point of liquefied natural gas under normal pressure.
  • the gaseous or supercritical hydrogen heated in the auxiliary heat exchanger 110 flows into the main heat exchanger 150 through the connecting channel 140 .
  • the main heat exchanger 150 is an open rack heat exchanger that heats hydrogen using seawater or industrial water as the second heat source fluid.
  • the main heat exchanger 150 includes a plurality of heat transfer tube panels 160 and a heat source fluid supply section 170 that supplies the second heat source fluid to each heat transfer tube panel 160 .
  • Each heat transfer tube panel 160 includes a large number of heat transfer tubes 166 (indicated by dashed arrows in FIG. 1) for circulating hydrogen, a lower header 162 connected to the lower end of each heat transfer tube 166, and each heat transfer tube 166. and a top header 164 connected to the top end.
  • These heat transfer tubes 166 extend vertically and are arranged in alignment on a vertical plane.
  • a metal material with high thermal conductivity such as aluminum or an aluminum alloy is used.
  • each lower header 162 The hydrogen that has flowed into each lower header 162 is distributed to multiple heat transfer tubes 166 connected to each lower header 162 . That is, in each heat transfer tube 166, gaseous or supercritical hydrogen flows from bottom to top. Hydrogen from each heat transfer tube 166 joins in each upper header 164 .
  • the heat source fluid supply section 170 includes a trough 171 arranged near the upper ends of the plurality of heat transfer tube panels 160 .
  • a trough 171 is provided for each heat transfer tube panel 160 so as to be adjacent to each heat transfer tube panel 160 .
  • Each trough 171 is elongated in the direction in which the heat transfer tubes 166 are arranged, and has a container shape with an open upper surface.
  • Each trough 171 is connected with a header 172 for introducing the second heat source fluid from the outside. The heat source fluid that has flowed into the trough 171 through the header 172 overflows out of the trough 171 through the opening on the upper surface of the trough 171 .
  • the second heat source medium overflowing from each trough 171 flows down along the outer surface of many heat transfer tubes 166 of each heat transfer tube panel 160 . Thereby, heat exchange is performed between the hydrogen inside the heat transfer tube 166 and the second heat source medium outside the heat transfer tube 166 .
  • hydrogen is heated to room temperature or a predetermined temperature by heat exchange with the second heat source fluid.
  • Hydrogen is discharged from the main heat exchanger 150 through the upper header 164 and supplied to an external hydrogen gas demand destination.
  • the second heat source fluid flowing down along the outer surface of the heat transfer tube 166 is discharged to the outside of the main heat exchanger 150 through an unillustrated drainage channel or the like.
  • the liquid hydrogen is supplied from the external liquid hydrogen supply source to the inlet chamber 124, and the liquid hydrogen is supplied from the external first heat source fluid supply source to the inlet chamber 134 of the intermediate medium evaporation section E1. is supplied with a first heat source fluid (seawater or industrial water).
  • the second heat source fluid is supplied from the external second heat source fluid supply source to the trough 171 of the heat source fluid supply section 170 .
  • the first heat source fluid supplied to the inlet chamber 134 of the intermediate medium evaporator E1 flows through the heat transfer tube 132 to the outlet chamber 136, and then is discharged to the outside. At this time, the first heat source fluid heats the liquid intermediate medium M1 stored in the casing 112 while flowing through the heat transfer tubes 132 . At least part of the liquid intermediate medium M1 is thereby evaporated.
  • the gaseous intermediate medium M1 in the casing 112 heats the liquid hydrogen in the heat transfer tubes 122 to a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure (first heating step).
  • the gaseous intermediate medium M1 of the hydrogen heating section E2 may heat the liquid hydrogen in the heat transfer tube 122 to a predetermined temperature below the boiling point of liquefied natural gas under normal pressure.
  • the heated gaseous or supercritical hydrogen flows from outlet chamber 126 into connecting channel 140 .
  • the gaseous intermediate medium M1 cooled by the liquid hydrogen inside the heat transfer tube 122 condenses and liquefies, flows down the internal space inside the casing 112, and returns to the intermediate medium evaporating section E1.
  • the gaseous or supercritical hydrogen that has flowed into the connection flow path 140 is supplied through the lower header 162 of the main heat exchanger 150 into the heat transfer tubes 166 .
  • the hydrogen in the heat transfer tube 166 is heated by the second heat source fluid that is supplied from the trough 171 and flows down along the outer surface of the heat transfer tube 166, thereby raising the temperature of the hydrogen in the heat transfer tube 166 to room temperature or a predetermined temperature. (second heating step).
  • the gaseous or supercritical hydrogen heated to room temperature or a predetermined temperature is led out through the upper header 164 to an external hydrogen gas demand destination.
  • the auxiliary heat exchanger 110 for preheating the liquid hydrogen is provided as a pre-stage of the main heat exchanger 150, so that the temperature of the hydrogen flowing into the main heat exchanger 150 is It can be higher than the temperature of hydrogen. Therefore, in the main heat exchanger 150, it is possible to reduce the thermal stress applied to the heat transfer tubes 166 while suppressing the icing on the outer surfaces of the heat transfer tubes 166. Furthermore, by using a fluid having a freezing point lower than that of seawater or industrial water as the intermediate medium M1 of the auxiliary heat exchanger 110, icing on the outer surface of the heat transfer tubes 122 of the auxiliary heat exchanger 110 can be suppressed.
  • auxiliary heat exchanger 110 since liquid hydrogen from the outside is heated in the auxiliary heat exchanger 110, hydrogen having a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure can be introduced into the main heat exchanger 150. Therefore, an existing open rack type vaporizer for vaporizing liquefied natural gas can be utilized as the main heat exchanger 150 of the vaporizer 100 as well. In this case, the introduction cost of the vaporization device 100 can be reduced. In addition, since the auxiliary heat exchanger 110 and the main heat exchanger 150 are separate devices in the vaporization device 100, maintenance of each device can be performed more easily.
  • the auxiliary heat exchanger may not be an intermediate medium heat exchanger, but may be a microchannel heat exchanger in which many fine flow paths are formed.
  • a microchannel heat exchanger is a heat exchanger having a laminated body in which a plurality of first plates and a plurality of second plates are laminated, and a high-temperature flow path formed in the first plate allows a high-temperature A heat exchanger configured to exchange heat between a fluid and a cryogenic fluid flowing through cryogenic channels formed in the second plate.
  • auxiliary heat exchanger 210 configured by a microchannel heat exchanger, heat is exchanged between the first heat source fluid, which is a high-temperature fluid, and liquid hydrogen, which is a low-temperature fluid.
  • the first heat source fluid is a heating fluid for heating liquid hydrogen.
  • the first heat source fluid is a fluid (for example, propane) that has a freezing point lower than the freezing point of seawater or industrial water and a boiling point lower than the temperature of seawater or industrial water.
  • the auxiliary heat exchanger 210 includes a stack 212, an inlet header 216 and an outlet header 218 provided on the side of the stack 212, and an inlet header 226 provided on the bottom and an outlet header 226 on the top of the stack 212. 228 and .
  • the high temperature plate is formed with a meandering high temperature flow path 214 (indicated by solid arrows in FIG. 2) from an inlet header 216 to an outlet header 218 .
  • a first heat source fluid supplied from the outside flows through the high temperature flow path 214 from the inlet header 216 toward the outlet header 218 .
  • the cold plate is formed with a plurality of cold channels 224 (indicated by dashed arrows in FIG.
  • Liquid hydrogen supplied from an external liquid hydrogen source flows through a plurality of cryogenic channels 224 from inlet header 226 towards outlet header 228 .
  • heat exchange takes place between the first heat source fluid in the high temperature channel 214 and the liquid hydrogen in the low temperature channel 224 .
  • the liquid hydrogen in the low-temperature channel 224 is heated to a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure, becomes gaseous or supercritical, and flows out from the outlet header 228 to the connecting channel 240 .
  • the first heat source fluid in the low temperature flow path 224 cooled by liquid hydrogen is discharged to the outside through the outlet header 218 .
  • liquid hydrogen in the low temperature flow path 224 may be heated to a predetermined temperature below the boiling point of liquefied natural gas under normal pressure.
  • the high-temperature flow path 214 is formed to meander and the low-temperature flow path 224 is formed to extend in one direction, but the configuration is not limited to this. Both the high temperature channel 214 and the low temperature channel 224 may meander, or both may be formed in a straight line.
  • the vaporization device 300 As shown in FIG. 3, the vaporization device 300 according to the second embodiment is provided with a branch flow passage 330 for branching the liquid hydrogen upstream of the main heat exchanger 150. This differs from the first embodiment in that the part is preheated by the auxiliary heat exchanger 310 .
  • the vaporization device 300 includes a supply channel 320 through which liquid hydrogen supplied from the outside flows, a branch channel 330 that divides the liquid hydrogen flowing through the supply channel 320, and is connected to the branch channel 330 and the main heat exchanger 150. and a main flow path 340 .
  • the branched flow channel 330 includes a first branched flow channel 332 connected to the supply flow channel 320, a second branched flow channel 334 connected to the supply flow channel 320 and formed by branching from the first branched flow channel 332, contains. Part of the liquid hydrogen that has flowed through the supply channel 320 is branched to the first branch channel 332, and the other part of the liquid hydrogen that has flowed through the supply channel 320 is branched to the second branch channel 334 (dividing step). .
  • a regulating valve 333 capable of controlling the flow rate of liquid hydrogen flowing through the second branched flow path 334 is provided in the second branched flow path 334 .
  • the first branched flow path 332 is provided with an auxiliary heat exchanger 310 that raises the temperature of the liquid hydrogen flowing through the first branched flow path 332 by heat exchange with the first heat source fluid supplied from the outside.
  • the auxiliary heat exchanger 310 includes a number of heat transfer tubes 312 (indicated by dashed arrows in FIG. 3) through which the liquid hydrogen from the first branch flow path 332 flows, and the first heat source fluid flows down the outer peripheral surfaces of the many heat transfer tubes 312. It is an open rack heat exchanger with a trough 314 that allows In the auxiliary heat exchanger 310 , seawater or industrial water is used as the first heat source fluid as in the main heat exchanger 150 .
  • Auxiliary heat exchanger 310 heats the liquid hydrogen in first branch flow path 332 to a predetermined temperature (first heating step).
  • Vaporizer 300 is configured such that the magnitude of the heat load applied to the first heat source fluid to process a unit flow of liquid hydrogen in auxiliary heat exchanger 310 is reduced to It is configured to be smaller than the magnitude of the heat load applied to the second heat source fluid. That is, when the same amount of hydrogen is supplied to each of auxiliary heat exchanger 310 and main heat exchanger 150, the supply flow rate of the first heat source fluid to auxiliary heat exchanger 310 is the same as that of main heat exchanger 150. It is configured to be larger than the supply flow rate of the two heat source fluids.
  • a pump for causing the first heat source fluid to flow into the auxiliary heat exchanger 310 is provided on the inlet side of the first heat source fluid in the auxiliary heat exchanger 310 .
  • this pump a larger flow rate of the first heat source fluid can be supplied to the auxiliary heat exchanger 310, so the heat load applied to the first heat source fluid for processing a unit flow rate of hydrogen in the auxiliary heat exchanger 310 is It's getting smaller. That is, this pump can deliver the first heat source fluid at a larger flow rate than a pump (not shown) that flows the second heat source fluid into the main heat exchanger 150 .
  • the vaporization device 300 is arranged such that the flow rate of the first heat source fluid supplied to the auxiliary heat exchanger 310 is greater than or equal to the flow rate of the second heat source fluid supplied to the main heat exchanger 150. It may be configured to be
  • the hydrogen that has flowed into the first branch flow channel 332 and is heated by the auxiliary heat exchanger 310 and the liquid hydrogen that has flowed into the second branch flow channel 334 flow into the main flow channel 340 and join together (merging step).
  • the hydrogen from the first branch flow channel 332 and the liquid hydrogen from the second branch flow channel 334 join together, so that the temperature in the main flow channel 340 is equal to or higher than the boiling point of liquefied natural gas under normal pressure. is produced.
  • gaseous or supercritical hydrogen having a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure is introduced from the main flow path 340 to the main heat exchanger 150 .
  • Hydrogen having a temperature equal to or lower than the boiling point of liquefied natural gas under normal pressure may be generated by merging the hydrogen from the first branched flow channel 332 and the liquid hydrogen from the second branched flow channel 334 .
  • the hydrogen supplied to the main heat exchanger 150 is heated to a predetermined temperature by heat exchange with the second heat source fluid (second heating step), as in the first embodiment. Hydrogen heated to a predetermined temperature is led out to an external hydrogen gas demand destination.
  • the auxiliary heat exchanger 310 by increasing the amount of supply of the first heat source fluid, compared to the main heat exchanger 150, the magnitude of the heat load applied to the first heat source fluid for processing liquid hydrogen is reduced. become smaller. Therefore, in the auxiliary heat exchanger 310 as well, it is possible to reduce the thermal stress applied to the heat transfer tubes 312 and suppress the icing on the outer surfaces of the heat transfer tubes. Further, as in the first embodiment, since hydrogen having a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure can be introduced into the main heat exchanger 150, an existing open rack type vaporizer for vaporizing liquefied natural gas can be used. can be utilized as the main heat exchanger 150. The temperature of the hydrogen introduced into the main heat exchanger 150 may be a temperature equal to or lower than the boiling point of liquefied natural gas under normal pressure.
  • the auxiliary heat exchanger 410 provided on the first branch flow path 432 is not an open rack type heat exchanger but an intermediate medium type heat exchanger. may be
  • the auxiliary heat exchanger 410 provided in the first branched flow path 432 of the branched flow path 430 is configured substantially the same as the auxiliary heat exchanger 110 in the first embodiment.
  • the auxiliary heat exchanger 410 includes an intermediate medium evaporating section E1 that evaporates the intermediate medium M1 accommodated in the casing by heat exchange with the first heat source fluid, and a first and a hydrogen heating part E2 that heats the liquid hydrogen in the split flow channel 432 .
  • the hydrogen in the first branch channel 432 heated by the auxiliary heat exchanger 410 flows into the main channel 440 and joins the liquid hydrogen from the second branch channel 434 before entering the main heat exchanger 150 .
  • auxiliary heat exchanger 410 of the first branch flow path 432 is not an intermediate medium heat exchanger, but a microchannel heat exchanger similar to the auxiliary heat exchanger 210 described in the modified example of the first embodiment. It may be configured by an exchanger.
  • an auxiliary heat exchanger 510 which is a microchannel heat exchanger, is provided in the first branched flow path 532 of the branched flow path 530 .
  • the liquid hydrogen that has flowed into the split flow channel 530 is heated in the auxiliary heat exchanger 510 by heat exchange with the first heat source fluid.
  • the liquid hydrogen vaporizer in the present disclosure is a liquid hydrogen vaporizer that generates gaseous or supercritical hydrogen from liquid hydrogen, and heats a heated fluid having a freezing point lower than that of seawater or industrial water. It has an auxiliary heat exchanger for raising the temperature of liquid hydrogen by exchange, a heat transfer tube for flowing hydrogen, and a trough portion for supplying seawater or industrial water to the outer surface of the heat transfer tube, and the hydrogen flows out from the auxiliary heat exchanger. and an open rack main heat exchanger for raising the temperature of hydrogen by heat exchange with seawater or industrial water.
  • the auxiliary heat exchanger for preheating the liquid hydrogen is provided as a pre-stage of the main heat exchanger, the hydrogen at a temperature higher than the temperature of the liquid hydrogen is transferred to the main heat exchanger. can flow into Therefore, in the main heat exchanger, it is possible to suppress the icing on the outer surface of the heat transfer tubes while relieving the thermal stress applied to the heat transfer tubes. Furthermore, since a fluid having a freezing point lower than the freezing point of water is used as the heating fluid for the auxiliary heat exchanger, the heating fluid is less likely to freeze, and icing in the auxiliary heat exchanger can be suppressed.
  • the auxiliary heat exchanger uses an intermediate medium as the heating fluid, and is an intermediate medium type heat exchanger that exchanges heat between liquid hydrogen and a heat source fluid supplied from the outside via the intermediate medium. It may be configured by an exchanger.
  • the intermediate medium type heat exchanger is provided with an intermediate medium evaporator that vaporizes at least part of the intermediate medium by heat exchange with the heat source fluid, and a heat transfer tube for flowing liquid hydrogen, and a hydrogen heating unit that raises the temperature of the liquid hydrogen in the heat transfer tubes by heat exchange with the vaporized intermediate medium.
  • an intermediate medium type heat exchanger using a heating medium as an intermediate medium is used as the auxiliary heat exchanger preceding the main heat exchanger.
  • seawater or industrial water can be used as the heat source fluid for heating and evaporating the intermediate medium.
  • the liquid hydrogen vaporizer includes a main flow path connected to the main heat exchanger and a branch flow path for dividing the liquid hydrogen supplied from the outside into which part of the liquid hydrogen supplied from the outside flows. and a second branch channel into which the other part of the liquid hydrogen supplied from the outside flows.
  • the auxiliary heat exchanger may be provided on the first branch flow path.
  • the split flow channel joins the hydrogen that has flowed into the first split flow channel and has been heated by the auxiliary heat exchanger and the liquid hydrogen that has flowed into the second split flow channel, and allows the liquid hydrogen to flow into the main flow channel. , may be connected to the main flow path.
  • the hydrogen split into the first split flow channel and heated by the auxiliary heat exchanger and the liquid hydrogen split into the second split flow channel are combined and flowed into the main flow channel, whereby the main heat is Hydrogen at a higher temperature than liquid hydrogen can flow into the exchanger. Therefore, in the main heat exchanger, it is possible to suppress the icing on the outer surface of the heat transfer tubes while relieving the thermal stress applied to the heat transfer tubes.
  • a liquid hydrogen vaporizer is a liquid hydrogen vaporizer that generates gaseous or supercritical hydrogen from liquid hydrogen, and includes a heat transfer tube for circulating hydrogen and a heat transfer tube on the outer surface of the heat transfer tube.
  • An open-rack type main heat exchanger having a trough portion for supplying seawater or industrial water, and for raising the temperature of hydrogen in the heat transfer tubes by heat exchange with seawater or industrial water, and a main heat exchanger connected to the main heat exchanger.
  • a channel, a first branch channel which is a branch channel for branching the liquid hydrogen supplied from the outside and into which a part of the liquid hydrogen supplied from the outside flows, and the other part of the liquid hydrogen supplied from the outside.
  • the branch flow channel is connected to the main flow channel so that the heated hydrogen flowing through the first branch flow channel and the liquid hydrogen flowing through the second branch flow channel are merged and flowed into the main flow channel.
  • the magnitude of the heat load of the heating fluid required to raise the temperature of liquid hydrogen in the auxiliary heat exchanger is smaller than the magnitude of the heat load of seawater or industrial water required to raise the temperature of hydrogen in the main heat exchanger.
  • the hydrogen split into the first split flow channel and heated by the auxiliary heat exchanger is merged with the liquid hydrogen split into the second split flow channel and flows into the main flow channel.
  • hydrogen having a higher temperature than liquid hydrogen can flow into the main heat exchanger. Therefore, in the main heat exchanger, it is possible to suppress the icing on the outer surface of the heat transfer tubes while relieving the thermal stress applied to the heat transfer tubes.
  • the heat load of the heating fluid in the auxiliary heat exchanger is smaller than the heat load of seawater or industrial water in the main heat exchanger. Can hold ice.
  • the liquid hydrogen vaporizer may be configured to generate hydrogen having a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure by heating the liquid hydrogen in the auxiliary heat exchanger.
  • the liquid hydrogen vaporizer has a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure due to the confluence of the hydrogen from the first branched flow channel and the liquid hydrogen from the second branched flow channel. It may be configured to generate hydrogen.
  • liquid hydrogen is heated by the auxiliary heat exchanger, and hydrogen having a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure is introduced into the main heat exchanger. Therefore, an open rack type vaporizer for vaporizing liquefied natural gas can be utilized as the main heat exchanger. In this case, the introduction cost of the liquid hydrogen vaporizer can be reduced.
  • the method of generating hydrogen in the present disclosure is a method of heating liquid hydrogen to generate gaseous or supercritical hydrogen.
  • the method includes a first heating step of raising the temperature of liquid hydrogen supplied from the outside by heat exchange with a heating fluid having a freezing point lower than that of seawater or industrial water in an auxiliary heat exchanger; a second heating step in which the hydrogen flowing out of the exchanger is allowed to flow into the heat transfer tubes of the main heat exchanger, and the hydrogen in the heat transfer tubes is heated to a predetermined temperature by heat exchange with seawater or industrial water; contains.
  • the method of generating hydrogen in the present disclosure is a method of heating liquid hydrogen to generate gaseous or supercritical hydrogen.
  • the method comprises a flow dividing step of dividing liquid hydrogen supplied from the outside into a first branch flow channel and a second branch flow channel, and an auxiliary heat exchanger provided on the first branch flow channel, wherein a first heating step of raising the temperature of the liquid hydrogen in the first branch flow channel by heat exchange; and a merging step of flowing hydrogen in the main flow path into the heat transfer tube of the main heat exchanger and heat-exchanging with seawater or industrial water to raise the temperature of the hydrogen in the heat transfer tube to a predetermined temperature. and a heating step.
  • the magnitude of the heat load of the heating fluid for raising the temperature of liquid hydrogen in the first heating step is smaller than the magnitude of the heat load of seawater or industrial water for raising the temperature of hydrogen in the second heating step.
  • the fluid obtained by combining the hydrogen and the liquid hydrogen may have a temperature equal to or higher than the boiling point of liquefied natural gas under normal pressure.
  • a liquid hydrogen vaporizer in a liquid hydrogen vaporizer, it is possible to reduce the thermal stress on the heat transfer tubes of an open rack heat exchanger while suppressing icing on the heat transfer tubes.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Details Of Heat-Exchange And Heat-Transfer (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
PCT/JP2022/033372 2021-09-21 2022-09-06 液体水素気化装置及び水素を生成する生成方法 WO2023047937A1 (ja)

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CN202280062741.5A CN117999453A (zh) 2021-09-21 2022-09-06 液氢气化装置以及生成氢的生成方法
EP22872693.1A EP4386300A1 (en) 2021-09-21 2022-09-06 Liquid hydrogen vaporizer, and generation method for generating hydrogen
KR1020247011091A KR20240058904A (ko) 2021-09-21 2022-09-06 액체 수소 기화 장치 및 수소를 생성하는 생성 방법

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JP2021-153176 2021-09-21
JP2021153176A JP2023045007A (ja) 2021-09-21 2021-09-21 液体水素気化装置及び水素を生成する生成方法

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2003185096A (ja) * 2001-12-18 2003-07-03 Tokyo Gas Co Ltd 水素供給設備
JP2016070301A (ja) * 2014-09-26 2016-05-09 川崎重工業株式会社 水素燃料供給システム
JP2017040296A (ja) 2015-08-19 2017-02-23 株式会社神戸製鋼所 ガス気化装置及びその運転方法
JP2017116090A (ja) * 2015-12-18 2017-06-29 株式会社神戸製鋼所 中間媒体式気化器
CN109357159A (zh) * 2018-11-14 2019-02-19 江苏科技大学 一种深冷超临界流体再气化实验系统及工作方法
CN208982182U (zh) * 2018-11-12 2019-06-14 赫普科技发展（北京）有限公司 Lng冷能斯特林发电系统

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2003185096A (ja) * 2001-12-18 2003-07-03 Tokyo Gas Co Ltd 水素供給設備
JP2016070301A (ja) * 2014-09-26 2016-05-09 川崎重工業株式会社 水素燃料供給システム
JP2017040296A (ja) 2015-08-19 2017-02-23 株式会社神戸製鋼所 ガス気化装置及びその運転方法
JP2017116090A (ja) * 2015-12-18 2017-06-29 株式会社神戸製鋼所 中間媒体式気化器
CN208982182U (zh) * 2018-11-12 2019-06-14 赫普科技发展（北京）有限公司 Lng冷能斯特林发电系统
CN109357159A (zh) * 2018-11-14 2019-02-19 江苏科技大学 一种深冷超临界流体再气化实验系统及工作方法

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