JP2669629B2 - Hydrogen liquefaction machine using metal hydride - Google Patents
Hydrogen liquefaction machine using metal hydrideInfo
- Publication number
- JP2669629B2 JP2669629B2 JP63023944A JP2394488A JP2669629B2 JP 2669629 B2 JP2669629 B2 JP 2669629B2 JP 63023944 A JP63023944 A JP 63023944A JP 2394488 A JP2394488 A JP 2394488A JP 2669629 B2 JP2669629 B2 JP 2669629B2
- Authority
- JP
- Japan
- Prior art keywords
- hydrogen
- metal hydride
- hydrogen gas
- storage tank
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims description 100
- 239000001257 hydrogen Substances 0.000 title claims description 72
- 229910052739 hydrogen Inorganic materials 0.000 title claims description 72
- 229910052987 metal hydride Inorganic materials 0.000 title claims description 26
- 150000004681 metal hydrides Chemical class 0.000 title claims description 26
- 239000007788 liquid Substances 0.000 claims description 23
- 238000011084 recovery Methods 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 13
- 238000000034 method Methods 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 150000002431 hydrogen Chemical class 0.000 description 4
- 238000004891 communication Methods 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 229910018007 MmNi Inorganic materials 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 150000004678 hydrides Chemical class 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0005—Light or noble gases
- F25J1/001—Hydrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0225—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/32—Hydrogen storage
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Hydrogen, Water And Hydrids (AREA)
Description
【発明の詳細な説明】 産業上の利用分野 本発明は、金属水素化物を用いた水素液化機に関す
る。Description: TECHNICAL FIELD The present invention relates to a hydrogen liquefier using a metal hydride.
従来技術 金属水素化物（Metal Hydrides以下MHと称する）は
温度によって固有の水素平衡圧を持つため、金属水素化
物に熱を与えることによって吸蔵していた水素を放出
し、冷却することによって水素を吸蔵して回収すること
ができる。この現象を利用してMHを利用した水素ガスコ
ンプレッサーを形成することができる。MHを利用したコ
ンプレッサーは、水素ガスや、MHを加熱、冷却するため
の熱媒体流体の流路を切換えるための弁以外に機械的可
動部分がないため、機械振動のないことを要求される極
低温能動素子等の冷却に用いる水素液化機に適用するこ
とができる。Prior art Metal hydrides (hereinafter referred to as MH) have a unique hydrogen equilibrium pressure depending on the temperature. Therefore, when the metal hydride is heated, the stored hydrogen is released, and when cooled, the hydrogen is stored. And can be collected. By utilizing this phenomenon, a hydrogen gas compressor using MH can be formed. Compressors using MH have no mechanical moving parts other than valves for switching the flow path of hydrogen gas and heat medium fluid for heating and cooling MH, so there is no need for mechanical vibration. The present invention can be applied to a hydrogen liquefier used for cooling a low-temperature active element or the like.
さて、従来のMH利用コンプレッサーを用いた水素液化
機は、第５図に示す如く、１種類のMHを使用していた。
第５図に示す例では、１種類のMH（M1）を夫々に収容し
たMH保持容器23a,23b,23cには夫々加熱コイル24及び冷
却コイル25が設けられ、加熱コイル24に加熱媒体を流通
させてMH（M1）を加熱することにより、MH（M1）に吸蔵
された水素ガスを放出させ、冷却コイル25に冷却媒体を
流通させてMH（M1）に水素ガスを吸蔵させて回収させ
る。By the way, the conventional hydrogen liquefier using the MH-based compressor uses one type of MH, as shown in FIG.
In the example shown in FIG. 5, a heating coil 24 and a cooling coil 25 are provided in each of the MH holding containers 23a, 23b, and 23c that store one type of MH (M1), and the heating medium is circulated in the heating coil 24. Then, the MH (M1) is heated to release the hydrogen gas stored in the MH (M1), and the cooling medium is circulated through the cooling coil 25 so that the MH (M1) stores the hydrogen gas and recovers it.
３つのMH保持容器23a,23b,23cには夫々放出された水
素ガスを取出す供給弁26a,26b,26c及び水素ガスを受入
れる回収弁27a,27b,27cが設けられ、弁26a,26b,26cの吐
出側、弁27a,27b,27cの流入側で夫々１本の供給管11及
び１本の回収管17に接続されている。供給管11は熱交換
器12、液体窒素による冷却器13、熱交換器14、ジュール
トムソン弁（Ｊ−Ｔ弁）15を経て液体水素溜槽16に接続
されている。一方、回収管17は上記の熱交換器12,14を
介して液体水素溜槽16に接続されている。The three MH holding vessels 23a, 23b, 23c are provided with supply valves 26a, 26b, 26c for taking out the released hydrogen gas and recovery valves 27a, 27b, 27c for receiving the hydrogen gas, respectively. The discharge side and the inflow sides of the valves 27a, 27b, 27c are connected to one supply pipe 11 and one recovery pipe 17, respectively. The supply pipe 11 is connected to a liquid hydrogen storage tank 16 via a heat exchanger 12, a liquid nitrogen cooler 13, a heat exchanger 14, and a Joule Thomson valve (JT valve) 15. On the other hand, the recovery pipe 17 is connected to the liquid hydrogen storage tank 16 via the heat exchangers 12 and 14 described above.
例えば、MH保持容器23aのMH22aから水素ガスを放出し
て液体水素溜槽16に供給する場合は、MH保持容器23aのM
H22aを加熱し、この容器の供給弁26aを開き、水素ガス
を供給管11に送り出す。管内を流れる水素ガスは熱交換
器12,14、冷却器13により冷却され、Ｊ−Ｔ弁15により
自由膨張して液化し、液体水素溜槽16に供給され貯溜さ
れる。For example, when hydrogen gas is released from the MH 22a of the MH holding container 23a and supplied to the liquid hydrogen storage tank 16, M of the MH holding container 23a is
H22a is heated, the supply valve 26a of this container is opened, and hydrogen gas is sent out to the supply pipe 11. The hydrogen gas flowing in the tubes is cooled by the heat exchangers 12 and 14 and the cooler 13, and is freely expanded and liquefied by the JT valve 15 and supplied to and stored in the liquid hydrogen storage tank 16.
液体水素溜槽16からの蒸発水素は、熱交換器14,12を
通過する回収管17内を戻り、熱交換器14,12で供給管11
内に流れる水素ガスとの間に熱交換をして昇温し、たゞ
１つ開いている容器23cの回収弁27cを経てMH保持容器23
cに戻り冷却コイル25により冷却されているMH22cに吸蔵
され回収される。Evaporated hydrogen from the liquid hydrogen storage tank 16 returns inside the recovery pipe 17 passing through the heat exchangers 14 and 12, and is supplied to the supply pipe 11 at the heat exchangers 14 and 12.
The MH holding container 23 passes through the recovery valve 27c of the container 23c which is opened only by exchanging heat with the hydrogen gas flowing inside.
It returns to c and is occluded and collected in the MH22c cooled by the cooling coil 25.
上述の如く、１種類のMHを利用したコンプレッサーを
使用した水素液化機では、LaNi5が通常使用されるた
め、冷却媒体として、冷水を用いる場合、Ｊ−Ｔ弁で自
由膨張した水素の回収圧力を大気圧以下に下げることが
できず、到達液化温度は26゜K程度にしか低下しなかっ
た。又、１種類のMHを使用しているため、冷凍能力を増
大するためにＪ−Ｔ弁前後の圧力差、すなわち水素の供
給圧力と回収圧力の差が大きくなるように作動温度範囲
を広く取る必要があった。As mentioned above, LaNi 5 is normally used in a hydrogen liquefaction machine that uses a compressor that uses one type of MH. Therefore, when cold water is used as the cooling medium, the recovery pressure of hydrogen that has freely expanded with the J-T valve is used. Could not be reduced to below atmospheric pressure, and the ultimate liquefaction temperature decreased only to about 26 ° K. Also, since one type of MH is used, a wide operating temperature range is set so that the pressure difference before and after the JT valve, that is, the difference between the hydrogen supply pressure and the recovery pressure is increased to increase the refrigeration capacity. There was a need.
目 的 本発明は、従来のMH利用コンプレッサーを用いた水素
液化機の上述の欠点にかんがみ、更に低温を液化水素が
得られ、かつ大きな冷凍能力を得ることができるMHを用
いた水素液化機を提供することを目的とする。In view of the above-mentioned drawbacks of a conventional hydrogen liquefier using a compressor using MH, the present invention provides a hydrogen liquefier using MH that can obtain liquefied hydrogen at a low temperature and can obtain a large refrigerating capacity. The purpose is to provide.
目的達成のための手段 本発明は、上記の目的を達成するため、複数の金属水
素化物保持容器と液体水素溜槽とを有し、上記金属水素
化物保持容器の１つに保持される金属水素化物を加勢す
ることにより放出された水素ガスを予冷後、自由膨張さ
せて液化し上記液体水素溜槽に供給して貯溜し、該液体
水素溜槽中の液体水素より気化した水素ガスを加熱し他
の金属水素化物保持容器中の金属水素化物を冷却してこ
れに吸蔵させて回収するようにした水素液化機におい
て、 上記の水素供給側の金属水素化物の水素平衡圧が回収
側の金属水素化物の同温度における水素平衡圧より高い
金属水素化物を用いたことを特徴とする。Means for Achieving the Object In order to achieve the above object, the present invention has a plurality of metal hydride holding containers and a liquid hydrogen storage tank, and the metal hydride is held in one of the metal hydride holding containers. After pre-cooling the hydrogen gas released by energizing, it is liquified by free expansion and supplied to the liquid hydrogen storage tank for storage, and the hydrogen gas vaporized from the liquid hydrogen in the liquid hydrogen storage tank is heated to cause another metal In a hydrogen liquefaction machine in which a metal hydride in a hydride holding container is cooled and stored therein to be recovered, the hydrogen equilibrium pressure of the metal hydride on the hydrogen supply side is the same as that of the metal hydride on the recovery side. It is characterized in that a metal hydride higher than the hydrogen equilibrium pressure at the temperature is used.
実施例の説明 以下に本発明の実施例を、図面に基づいて詳細に説明
する。DESCRIPTION OF THE EMBODIMENTS Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings.
第１図は、本発明によるMH利用コンプレッサーを用い
た水素液化機の実施例の概略フローを示す図である。FIG. 1 is a diagram showing a schematic flow of an embodiment of a hydrogen liquefier using a compressor using MH according to the present invention.
この実施例では、水素平衡圧の異なる３種類のMH（M
1,M2,M3）が使用され、夫々にM1,M2,M3を収容する容器
4,5,6を１ユニットとするA,B,Cの３ユニットの容器群が
設けられている。以下、A,B,C各ユニットを表わす添字
としてa,b,cを用いる。３種類のMH（M1,M2,M3）の温度
に対する水素平衡圧力特性曲線は、第２図に示す如くM1
が最も高くM3が最も低く、M2がその中間にある。In this embodiment, three types of MH (M (M
1, M2, M3), each containing M1, M2, M3
A container group of three units of A, B, and C, each of which has one unit of 4, 5, and 6, is provided. Hereinafter, a, b, and c are used as suffixes representing units A, B, and C, respectively. The hydrogen equilibrium pressure characteristic curves for the temperatures of three types of MH (M1, M2, M3) are as shown in Fig.
Is the highest, M3 is the lowest, and M2 is in the middle.
第２図より、供給側の容器4a,4b,4cにM1を収容し、回
収側の容器6a,6b,6cにM3を収容し、温度THで水素ガスを
放出し、温度TLで水素ガスを回収する場合、曲線M1の温
度THにおける平衡圧力と、曲線M3の温度TLにおける平衡
圧力との差の圧力差が得られ、一種類のMHを使用した従
来の装置に比してはるかに大きな圧力差が得られる。そ
の結果、水素ガス回収側のMHM3として常温で大気圧以下
の水素平衡圧を示すMHを使用することによって、Ｊ−Ｔ
弁以降の圧力を大気圧より下げ、Ｊ−Ｔ弁前後の圧力差
を大きくすることができる。その結果、20゜K以下の液
化温度が得られるとともに同じ作動温度で冷凍能力を増
大させることができる。From FIG. 2, M1 is stored in the supply side containers 4a, 4b, 4c, M3 is stored in the recovery side containers 6a, 6b, 6c, hydrogen gas is released at the temperature TH, and hydrogen gas is released at the temperature TL. In the case of recovery, a pressure difference of the difference between the equilibrium pressure at the temperature TH of the curve M1 and the equilibrium pressure at the temperature TL of the curve M3 is obtained, and the pressure is much larger than that of the conventional device using one type of MH. The difference is obtained. As a result, by using MH that has a hydrogen equilibrium pressure below atmospheric pressure at room temperature as MHM3 on the hydrogen gas recovery side, JT
The pressure after the valve can be reduced below the atmospheric pressure, and the pressure difference between before and after the JT valve can be increased. As a result, a liquefaction temperature of 20 ° K or less can be obtained, and the refrigeration capacity can be increased at the same operating temperature.
MH1a,1b,1cを収容した容器4a,4b,4cは、水素ガス供給
専用であり各容器には、水素ガス供給弁9a,9b,9cが接続
され、１本の供給管11に接続されている。また、MH3a,3
b,3cを収容して容器6a,6b,6cは水素ガス回収専用であ
り、各容器には、水素ガス回収弁10a,10b,10cが接続さ
れ１本の回収管17に接続される。The containers 4a, 4b, 4c accommodating the MH1a, 1b, 1c are dedicated to hydrogen gas supply, and each container is connected with a hydrogen gas supply valve 9a, 9b, 9c and is connected to one supply pipe 11. There is. Also, MH3a, 3
The containers 6a, 6b, 6c accommodating b, 3c are dedicated to hydrogen gas recovery, and hydrogen gas recovery valves 10a, 10b, 10c are connected to each container and connected to one recovery pipe 17.
水素供給管11は熱交換器12,液体窒素による冷却器1
3、熱交換器14、Ｊ−Ｔ弁15を経て液体水素溜槽16に接
続され、一方、水素回収管17は熱交換器14,12を経て、
各回収弁10a,10b,10cに接続されている点は、前記の従
来の装置の例と同じである。Hydrogen supply pipe 11 is heat exchanger 12, liquid nitrogen cooler 1
3, the heat exchanger 14 and the JT valve 15 are connected to the liquid hydrogen storage tank 16, while the hydrogen recovery pipe 17 is passed through the heat exchangers 14 and 12,
It is the same as the example of the conventional device described above in that it is connected to each recovery valve 10a, 10b, 10c.
１ユニットをなす３個のMH保持容器4,5,6は夫々弁18,
20を有する連絡管19,21で接続されている。又、各容器
には冷却コイル８、加熱コイル７が設けられている。冷
却コイル８には、冷却媒体（たとえば冷水）、加熱コイ
ル７には、加熱媒体（たとえば温水）が必要に応じて流
通させる。また、加熱コイル７は、パイプヒータ等でも
よい。The three MH holding containers 4, 5, 6 forming one unit are each provided with a valve 18,
Connected by connecting pipes 19, 21 having 20. Further, each container is provided with a cooling coil 8 and a heating coil 7. A cooling medium (for example, cold water) is passed through the cooling coil 8, and a heating medium (for example, warm water) is passed through the heating coil 7 as needed. The heating coil 7 may be a pipe heater or the like.
液化機の運転初期、水素ガスはMH1a,1b,1cにのみ充填
されており、加熱コイル７によって第２図に示される温
度THに加熱されている。MH2a,2b,2c及び3a,3b,3cは水素
ガスを放出した状態であり、冷却コイル８によって第２
図に示される温度TLに冷却されている。At the initial stage of operation of the liquefaction machine, hydrogen gas is filled only in the MH 1a, 1b, 1c and heated by the heating coil 7 to the temperature TH shown in FIG. MH2a, 2b, 2c and 3a, 3b, 3c are in a state of releasing hydrogen gas, and are cooled by the cooling coil 8
It is cooled to the temperature TL shown in the figure.
水素供給弁9aを開けることにより、容器4a内のMH1aか
ら放出された水素ガスは、供給管11を通り、熱交換器1
2,14、冷却器13により冷却され、Ｊ−Ｔ弁15により自由
膨張して液化し、液体水素溜槽16に供給され、貯溜され
る。By opening the hydrogen supply valve 9a, the hydrogen gas released from the MH1a in the container 4a passes through the supply pipe 11 and passes through the heat exchanger 1
2, 14, cooled by the cooler 13, freely expanded by the JT valve 15 and liquefied, supplied to the liquid hydrogen storage tank 16 and stored therein.
液体水素溜槽16からの蒸発水素は、熱交換器14,12に
より供給水素ガスと熱交換して昇温し、水素回収弁10a
を経て容器6a内の温度TLのMH3aに吸蔵され回収される。The evaporated hydrogen from the liquid hydrogen storage tank 16 exchanges heat with the supplied hydrogen gas by the heat exchangers 14 and 12 to raise the temperature, and the hydrogen recovery valve 10a.
After that, it is occluded and collected in the MH3a at the temperature TL in the container 6a.
容器4a内のMH1aから水素ガスを供給できなくなった時
点あるいは、必要な水素流量、あるいは、必要な供給圧
力が維持できなくなった時点で、弁9a,10aを閉止し、弁
9b,10bを開け、水素ガスの供給をＡユニットからＢユニ
ットへ切換える。以降、同様にＢユニットからＣユニッ
ト、ＣユニットからＡユニットへと順次切換えていく。When hydrogen gas cannot be supplied from the MH1a in the container 4a, or when the required hydrogen flow rate or the required supply pressure cannot be maintained, the valves 9a and 10a are closed and the valves are closed.
Open 9b and 10b and switch the supply of hydrogen gas from A unit to B unit. Thereafter, similarly, the unit is sequentially switched from the B unit to the C unit and from the C unit to the A unit.
水素供給の終了したユニット、例えばＡユニットは、
容器6a内のMH3aを加熱コイル７により加熱し、容器5a内
のMH2aを冷却コイル８により冷却し、また弁18aを開け
ることにより連絡管19aを介してMH3aから放出された水
素ガスをMH2aに吸蔵させ移送する。次に弁18aを閉止
後、容器5a内のMH2aを加熱コイル７により加熱し、容器
4a内のMH1aを冷却コイル８により冷却し、また弁20aを
開けることにより連絡管21aを介してMH2aから放出され
た水素ガスをMH1aに吸蔵させ移送する。他のユニットに
ついても、水素供給後、同様の操作を行う。この操作に
より順次、水素供給の終了したユニットは、水素供給前
の状態に戻るためユニットを適時切換えていくことによ
り、連続的に運転することが可能である。従って、ユニ
ット数は３ユニットに限るものではなく、連続運転に必
要なユニット数を設けるものとする。The unit that has finished supplying hydrogen, for example, the A unit,
The MH3a in the container 6a is heated by the heating coil 7, the MH2a in the container 5a is cooled by the cooling coil 8, and the hydrogen gas released from the MH3a through the communication pipe 19a is inserted into the MH2a by opening the valve 18a. And transfer. Next, after closing the valve 18a, the MH2a in the container 5a is heated by the heating coil 7,
The MH1a in 4a is cooled by the cooling coil 8, and by opening the valve 20a, the hydrogen gas released from MH2a is transferred to the MH1a via the communication pipe 21a. For other units, the same operation is performed after hydrogen supply. By this operation, the unit whose hydrogen supply has been completed sequentially returns to the state before the hydrogen supply, so that it is possible to continuously operate by switching the units at appropriate times. Therefore, the number of units is not limited to three, and the number of units required for continuous operation is provided.
MHの種類として、例えばMmNi4.15 Fe0.85（M1）,LaCe
NdNi5（M2）,LaNi4.75 Al0.25（M3）がある。As the type of MH, for example, MmNi 4.15 Fe 0.85 (M1), LaCe
There are NdNi 5 (M2) and LaNi 4.75 Al 0.25 (M3).
また、水素の供給側MH（M1）と、回収側MH（M3）の平
衡圧力の差があまり大きくない場合は、中間のMH（M2）
を省略して２種類とすることもでき、逆に圧力差が非常
に大きい場合は４種類以上のMHを使用することも可能で
ある。If the difference in equilibrium pressure between the hydrogen supply side MH (M1) and the recovery side MH (M3) is not so large, the intermediate MH (M2)
Can be omitted and two types can be used. Conversely, if the pressure difference is very large, four or more types of MH can be used.
なお、第２図乃至第４図に各MH間の水素移送状態を太
い実線で示す。2 to 4 show the state of hydrogen transfer between the respective MHs by a thick solid line.
効 果 以上の如く、本発明によれば、作動温度範囲を大きく
することなく、Ｊ−Ｔ弁前後の圧力差を従来より大きく
とることができ、冷凍能力を増大させることができると
ともに、同じ水素流量でMHの水素移動幅を従来より大き
くとることができる。Effect As described above, according to the present invention, the pressure difference across the JT valve can be made larger than before without increasing the operating temperature range, the refrigerating capacity can be increased, and the same hydrogen content can be obtained. The hydrogen transfer width of MH can be made larger by the flow rate than before.
又、液体水素溜槽からの蒸発水素を大気圧以下の圧力
でMHに回収できるので、20゜K以下の極低温を得ること
ができる。Also, since the hydrogen vaporized from the liquid hydrogen storage tank can be recovered in MH at a pressure of atmospheric pressure or lower, a cryogenic temperature of 20 ° K or lower can be obtained.
以上のことにより、現在液体水素温度を得るために用
いられている各種の冷凍機等と比較して、性能的にも、
温度的にも充分代替し得る信頼性の高い、機械振動のな
い水素液化機を提供することが可能となった。From the above, compared with various refrigerators and the like currently used to obtain the liquid hydrogen temperature, in terms of performance,
It has become possible to provide a highly reliable hydrogen liquefaction machine without mechanical vibration that can be sufficiently replaced in terms of temperature.
第１図は本発明の実施例の水素液化機の概略フロー、第
２乃至第４図は上記実施例の装置に用いる３種類のMHの
温度に対する水素平衡圧特性曲線と各MH間の水素移送状
態を示す曲線図、第５図は従来知られているMHを用いた
水素液化機の概略フローである。 4a,4b,4c……供給側MH保持容器 5a,5b,5c……中間MH保持容器 6a,6b,6c……回収側MH保持容器 ７……加熱コイル ８……冷却コイル 9a,9b,9c……供給弁 10a,10b,10c……回収弁 11……供給管 17……回収管 12,14……熱交換器 13……液体窒素による冷却器 15……Ｊ−Ｔ弁 16……液体水素溜槽 18,20……弁 19,21……連絡管FIG. 1 is a schematic flow chart of a hydrogen liquefaction machine according to an embodiment of the present invention, and FIGS. 2 to 4 are hydrogen equilibrium pressure characteristic curves for three kinds of MH temperatures used in the apparatus of the above embodiment and hydrogen transfer between each MH. FIG. 5 is a curve diagram showing the state, and FIG. 5 is a schematic flow of a conventionally known hydrogen liquefier using MH. 4a, 4b, 4c: Supply side MH holding container 5a, 5b, 5c: Intermediate MH holding container 6a, 6b, 6c: Recovery side MH holding container 7: Heating coil 8: Cooling coil 9a, 9b, 9c …… Supply valve 10a, 10b, 10c …… Recovery valve 11 …… Supply pipe 17 …… Recovery pipe 12,14 …… Heat exchanger 13 …… Liquid nitrogen cooler 15 …… JT valve 16 …… Liquid Hydrogen tank 18,20 …… Valve 19,21 …… Communication pipe
フロントページの続き (72)発明者 石毛 隆 茨城県筑波郡谷田部町二の宮３丁目16番 ２号 株式会社ほくさん低温技術開発セ ンター内Front page continued (72) Inventor Takashi Ishige 3-16-2 Ninomiya, Yatabe-cho, Tsukuba-gun, Ibaraki Prefecture Hokusan Co., Ltd. Low Temperature Technology Development Center
Claims (3)
槽とを有し、上記金属水素化物保持容器の１つに保持さ
れる金属水素化物を加熱することにより放出された水素
ガスを予冷後、自由膨張させて液化し上記液体水素溜槽
に供給して貯溜し、該液体水素溜槽中の液体水素より気
化した水素ガスを加熱し、他の金属水素化物保持容器中
の金属水素化物を冷却してこれに吸蔵させて回収するよ
うにした水素液化機において、 上記の水素供給側の金属水素化物の水素平衡圧が回収側
の金属水素化物の同温度における水素平衡圧より高い金
属水素化物を用いたことを特徴とする水素液化機。1. After precooling hydrogen gas released by heating a metal hydride held in one of the metal hydride holding vessels, which has a plurality of metal hydride holding vessels and a liquid hydrogen storage tank , Free-expansion, liquefy and supply to the liquid hydrogen storage tank for storage, heating hydrogen gas vaporized from liquid hydrogen in the liquid hydrogen storage tank, cooling metal hydride in another metal hydride holding container In a hydrogen liquefaction machine in which hydrogen is occluded in and recovered by a metal hydride, use a metal hydride whose hydrogen equilibrium pressure of the metal hydride on the hydrogen supply side is higher than that of the metal hydride on the recovery side at the same temperature. The hydrogen liquefaction machine, which is characterized by
する金属水素化物が常温で大気圧以下の水素平衡圧を示
すものであることを特徴とする特許請求の範囲第１項に
記載の水素液化機。2. The method according to claim 1, wherein the metal hydride for recovering the evaporated hydrogen from the liquid hydrogen storage tank has a hydrogen equilibrium pressure of atmospheric pressure or less at room temperature. Hydrogen liquefaction machine.
器から上記の水素ガス供給側金属水素化物保持容器への
水素ガス移送路の途中に、上記両容器中の金属水素化物
の水素平衡圧の中間の水素平衡圧を有する金属水素化物
を保持する金属水素化物保持容器を設けたことを特徴と
する特許請求の範囲第１項に記載の水素液化機。3. A hydrogen equilibrium pressure of the metal hydride in both of the above-mentioned containers is provided in the middle of the hydrogen gas transfer path from the hydrogen gas recovery side metal hydride holding container to the hydrogen gas supply side metal hydride holding container. The hydrogen liquefaction machine according to claim 1, further comprising a metal hydride holding container for holding a metal hydride having an intermediate hydrogen equilibrium pressure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63023944A JP2669629B2 (en) | 1988-02-05 | 1988-02-05 | Hydrogen liquefaction machine using metal hydride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63023944A JP2669629B2 (en) | 1988-02-05 | 1988-02-05 | Hydrogen liquefaction machine using metal hydride |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01201001A JPH01201001A (en) | 1989-08-14 |
| JP2669629B2 true JP2669629B2 (en) | 1997-10-29 |
Family
ID=12124652
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63023944A Expired - Fee Related JP2669629B2 (en) | 1988-02-05 | 1988-02-05 | Hydrogen liquefaction machine using metal hydride |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2669629B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024006711A3 (en) * | 2022-06-30 | 2024-03-21 | Kirk Ricky D | Improved hydrogenation of potable water |
-
1988
- 1988-02-05 JP JP63023944A patent/JP2669629B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024006711A3 (en) * | 2022-06-30 | 2024-03-21 | Kirk Ricky D | Improved hydrogenation of potable water |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH01201001A (en) | 1989-08-14 |
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