JPH08159653A - Method and device for manufacturing liquid hydrogen - Google Patents
Method and device for manufacturing liquid hydrogenInfo
- Publication number
- JPH08159653A JPH08159653A JP6299994A JP29999494A JPH08159653A JP H08159653 A JPH08159653 A JP H08159653A JP 6299994 A JP6299994 A JP 6299994A JP 29999494 A JP29999494 A JP 29999494A JP H08159653 A JPH08159653 A JP H08159653A
- Authority
- JP
- Japan
- Prior art keywords
- hydrogen
- liquid
- gas
- ortho
- liquid hydrogen
- 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.)
- Granted
Links
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 121
- 239000001257 hydrogen Substances 0.000 title claims abstract description 87
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 87
- 239000007788 liquid Substances 0.000 title claims abstract description 61
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- 238000000034 method Methods 0.000 title abstract description 16
- 238000001816 cooling Methods 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 150000002431 hydrogen Chemical class 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims 1
- 239000007791 liquid phase Substances 0.000 abstract 2
- 238000005070 sampling Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 19
- 239000002994 raw material Substances 0.000 description 15
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 239000001307 helium Substances 0.000 description 6
- 229910052734 helium Inorganic materials 0.000 description 6
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 6
- 239000012530 fluid Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 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"
- F25J1/0035—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 gas expansion with extraction of work
-
- 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"
- F25J1/0035—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 gas expansion with extraction of work
- F25J1/0037—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 gas expansion with extraction of work of a return stream
-
- 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"
- F25J1/0045—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 vaporising a liquid return stream
-
- 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
- F25J1/0224—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 in combination with an internal quasi-closed 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
-
- 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
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
- F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
-
- 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
- F25J2290/34—Details about subcooling of liquids
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)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、液体水素の製造方法及
び装置に関し、詳しくは、圧縮機で圧縮した水素ガスを
熱交換器で冷却しながらオルソ−パラ変換を行い、ジュ
ールトムソン膨張させて液体水素を製造する方法及び装
置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and apparatus for producing liquid hydrogen, and more specifically, it performs ortho-para conversion while cooling hydrogen gas compressed by a compressor with a heat exchanger and expands it by Joule-Thomson expansion. A method and apparatus for producing liquid hydrogen.
【０００２】[0002]
【従来の技術及び発明が解決しようとする課題】従来か
ら、液体水素を製造する方式として、ヘリウムの寒冷を
利用したヘリウムブライトン方式と、水素自体から寒冷
を得るクロード方式とが知られている。前記ヘリウムブ
ライトン方式は、ヘリウムガスを圧縮後、膨張タービン
で断熱膨張させて寒冷を発生させ、この寒冷により水素
を冷却し、ジュールトムソン膨張によって液体水素を生
成させるもので、クロード方式は、圧縮した水素ガスを
膨張タービンで断熱膨張させて得た寒冷と、ジュールト
ムソン膨張によって発生した寒冷とを利用して水素を冷
却し、ジュールトムソン膨張によって液体水素を生成す
るものである。2. Description of the Related Art Conventionally, as a method for producing liquid hydrogen, there are known a helium brighton method which utilizes the cold of helium and a Claude method which obtains the cold from hydrogen itself. The helium brighton method is a method in which helium gas is compressed, adiabatic expansion is performed by an expansion turbine to generate cold, and hydrogen is cooled by this cold, and liquid hydrogen is generated by Joule-Thomson expansion, and the Claude method is compressed. The cold is obtained by adiabatically expanding hydrogen gas with an expansion turbine and the cold generated by the Joule-Thomson expansion is used to cool the hydrogen to generate liquid hydrogen by the Joule-Thomson expansion.
【０００３】このような液体水素の製造において、水素
の臨界圧力は、ヘリウムに比べて非常に高い約１３気圧
であり、また、比熱が最大となる圧力も約１５気圧付近
で、その値もヘリウム等に比べて著しく大きくなる。こ
のような水素の特性から、原料水素ガスの供給圧力は、
２０〜４０気圧とするのが一般的である。また、水素を
液化するに際しては、冷却過程でオルソ−パラ変換を行
ってパラ水素に変換する必要がある。In the production of such liquid hydrogen, the critical pressure of hydrogen is about 13 atm, which is much higher than that of helium, and the pressure at which the specific heat becomes maximum is about 15 atm, which is also the value of helium. It will be significantly larger than the above. From such characteristics of hydrogen, the supply pressure of the raw material hydrogen gas is
It is generally set to 20 to 40 atm. Further, when liquefying hydrogen, it is necessary to perform ortho-para conversion in the cooling process to convert it into para hydrogen.
【０００４】しかし、従来の液化法では、オルソ−パラ
変換を必要とする水素の冷却液化系統において、ジュー
ルトムソン膨張による寒冷の発生に頼るだけで、水素ガ
スの高い供給圧力の効果的な利用がなされておらず、そ
の結果、リサイクル側の流量が多くなり、圧縮動力及び
電力費の増加につながっていた。However, in the conventional liquefaction method, in a hydrogen cooling liquefaction system requiring ortho-para conversion, effective use of high supply pressure of hydrogen gas can be achieved only by relying on generation of cold due to Joule-Thomson expansion. This was not done, and as a result, the flow rate on the recycle side increased, leading to an increase in compression power and power costs.
【０００５】一方、特公平３−１９４７１号公報に記載
された水素の液化方法では、水素の冷却液化系統に濃密
流体エクスパンダーを設けて水素を液化することが記載
されている。しかし、この濃密流体エクスパンダーにお
ける入口側の水素は超臨界状態であるが、出口側は気液
二層流である。ところが、このような気液二層流用の膨
張タービンは、タービンの構造上、破損し易く、実用装
置には一般的でなく採用し難い。さらに、気液二層流
は、一般に、状態が不安定であり、熱交換器等の構成機
器の設計，製作に困難を伴う場合が多い。On the other hand, in the method for liquefying hydrogen described in JP-B-3-19471, it is described that a dense fluid expander is provided in a cooling liquefaction system for hydrogen to liquefy hydrogen. However, although hydrogen on the inlet side of this dense fluid expander is in a supercritical state, gas-liquid two-layer flow is present on the outlet side. However, such an expansion turbine for gas-liquid two-layer flow is apt to be damaged due to the structure of the turbine, and is not common to practical devices and is difficult to employ. Furthermore, the gas-liquid two-layer flow is generally in an unstable state, and it is often difficult to design and manufacture component equipment such as a heat exchanger.
【０００６】そこで本発明は、冷却液化系統に供給され
る水素が有する高い圧力を有効に利用し、効率良く、経
済的に液体水素を製造することができる方法及び装置を
提供することを目的としている。Therefore, an object of the present invention is to provide a method and an apparatus capable of efficiently and economically producing liquid hydrogen by effectively utilizing the high pressure of hydrogen supplied to a cooling liquefaction system. There is.
【０００７】[0007]
【課題を解決するための手段】上記した目的を達成する
ため、本発明の液体水素の製造方法は、臨界圧力以上に
圧縮した水素ガスを冷却後、膨張させて液化する液体水
素の製造方法であって、水素の冷却液化系統に設けた膨
張タービンに前記水素ガスを導入し、臨界圧力以上の圧
力に膨張させて導出することを特徴とし、さらに、前記
膨張タービンを導出した水素ガスを断熱オルソ−パラ変
換することを特徴としている。In order to achieve the above object, the method for producing liquid hydrogen of the present invention is a method for producing liquid hydrogen in which hydrogen gas compressed to a critical pressure or higher is cooled and then expanded and liquefied. It is characterized in that the hydrogen gas is introduced into an expansion turbine provided in a cooling and liquefaction system of hydrogen, and the hydrogen gas is introduced by expanding it to a pressure equal to or higher than a critical pressure. -It is characterized by para conversion.
【０００８】また、本発明の液体水素の製造装置は、臨
界圧力以上に圧縮した水素ガスを冷却後、膨張させて液
化する液体水素の製造装置であって、水素の冷却液化系
統に、前記水素ガスを臨界圧力以上の圧力に膨張させる
膨張タービンを設けたことを特徴とし、さらに、前記膨
張タービンの出口に、断熱オルソ−パラ変換器を設けた
ことを特徴としている。The liquid hydrogen producing apparatus of the present invention is a liquid hydrogen producing apparatus for cooling hydrogen gas compressed to a critical pressure or higher and then expanding and liquefying the hydrogen gas. An expansion turbine for expanding the gas to a pressure equal to or higher than the critical pressure is provided, and further, an adiabatic ortho-para converter is provided at the outlet of the expansion turbine.
【０００９】[0009]
【作 用】上記構成によれば、冷却液化系統に供給され
た水素の高い圧力を、膨張タービンで寒冷として取出す
ことができる。このとき、膨張タービン出口側の圧力
（吐出圧力）を臨界圧力以上に保つことにより、気液二
層流にはならないので、安定した状態で水素を取出すこ
とができ、膨張タービン等の機器の設計，製作も容易に
行うことができる。[Operation] According to the above configuration, the high pressure of hydrogen supplied to the cooling liquefaction system can be taken out as cold by the expansion turbine. At this time, by keeping the pressure (discharge pressure) on the outlet side of the expansion turbine above the critical pressure, a gas-liquid two-layer flow does not occur, so hydrogen can be taken out in a stable state, and the design of equipment such as the expansion turbine ， It can be easily manufactured.
【００１０】[0010]
【実施例】以下、本発明を、図面に示す一実施例に基づ
いてさらに詳細に説明する。図１は、本発明方法を適用
した液体水素製造装置の一実施例を示すもので、この液
体水素製造装置は、原料水素供給経路１１に連続する水
素冷却液化系統２１に、原料水素ガスを冷却するための
複数の熱交換器３１，３２，３３，３４と、各冷却段階
に応じて水素のオルソ−パラ変換を行うための複数のオ
ルソ−パラ変換器４１，４２，４３，４４，４５，４６
と、水素ガスを断熱膨張させる膨張タービン５１と、水
素ガスをジュールトムソン膨張させて過冷状態の液体水
素を生成するジュールトムソン弁（ＪＴ弁）６１と、原
料水素ガスを冷却するための液体窒素溜７１と、ＪＴ弁
６１で生成した気液二層流状態の水素を凝縮し、冷却
し、オルソ−パラ変換を行うための液体水素溜８１とが
設けられるとともに、この水素冷却液化系統２１から分
岐した水素を利用して寒冷を発生させるための設備とし
て、２台の膨張タービン５２，５３と、前記液体水素溜
８１の液体水素を発生させるためのＪＴ弁６２と、膨張
タービン５２，５３及び液体水素溜８１から寒冷源とし
て循環する水素を圧縮して原料水素に合流させるための
直列に接続された低圧用及び高圧用の２台の循環圧縮機
９１，９２とにより構成されている。BEST MODE FOR CARRYING OUT THE INVENTION The present invention will now be described in more detail based on an embodiment shown in the drawings. FIG. 1 shows an embodiment of a liquid hydrogen production apparatus to which the method of the present invention is applied. This liquid hydrogen production apparatus cools a raw hydrogen gas to a hydrogen cooling liquefaction system 21 continuous to a raw hydrogen supply path 11. A plurality of heat exchangers 31, 32, 33, 34, and a plurality of ortho-para converters 41, 42, 43, 44, 45 for performing ortho-para conversion of hydrogen according to each cooling stage. 46
An expansion turbine 51 that adiabatically expands hydrogen gas, a Joule-Thomson valve (JT valve) 61 that expands hydrogen gas by Joule-Thomson to produce liquid hydrogen in a supercooled state, and liquid nitrogen for cooling the raw material hydrogen gas. A reservoir 71 and a liquid hydrogen reservoir 81 for condensing and cooling hydrogen in a gas-liquid two-layer flow state generated by the JT valve 61 and performing ortho-para conversion are provided, and from this hydrogen cooling liquefaction system 21 As equipment for generating cold using branched hydrogen, two expansion turbines 52, 53, a JT valve 62 for generating liquid hydrogen in the liquid hydrogen reservoir 81, expansion turbines 52, 53, and By two circulating compressors 91, 92 for low pressure and for high pressure connected in series for compressing hydrogen circulating as a cold source from the liquid hydrogen reservoir 81 and joining it with the raw material hydrogen. It has been made.
【００１１】図示しない圧縮機により臨界圧力以上の所
定の圧力、例えば３０気圧まで圧縮されて原料水素供給
経路１１から供給される原料水素ガスは、循環圧縮機９
１，９２で圧縮された循環水素ガスと合流して水素冷却
液化系統２１に導入され、最初に、第１の熱交換器３１
で、後述の戻り水素及び液体窒素溜７１からの低温窒素
ガスと熱交換を行い、液体窒素温度程度（約８０Ｋ）ま
で冷却される。第１の熱交換器３１を導出した水素ガス
は、ここで循環用の水素ガスが経路２２に分岐し、残り
の水素ガスは、液体窒素溜７１内に設けられた第１のオ
ルソ−パラ変換器４１に導入され、液体窒素温度に応じ
たオルソ−パラ変換が行われる。The raw material hydrogen gas, which is compressed to a predetermined pressure higher than the critical pressure, for example, 30 atmospheres by a compressor (not shown) and is supplied from the raw material hydrogen supply path 11, is circulated compressor 9.
It is introduced into the hydrogen cooling liquefaction system 21 by merging with the circulating hydrogen gas compressed by 1, 92, and first, the first heat exchanger 31.
Then, heat is exchanged with return hydrogen and low temperature nitrogen gas from the liquid nitrogen reservoir 71, which will be described later, and the liquid nitrogen is cooled to about the liquid nitrogen temperature (about 80 K). In the hydrogen gas discharged from the first heat exchanger 31, the circulating hydrogen gas branches into the path 22, and the remaining hydrogen gas is the first ortho-para conversion provided in the liquid nitrogen reservoir 71. Introduced into the vessel 41, the ortho-para conversion depending on the liquid nitrogen temperature is performed.
【００１２】上記オルソ−パラ変換器４１を導出した水
素ガスは、第２，第３の熱交換器３２，３３に設けたオ
ルソ−パラ変換器４２，４３の通路を通り、戻り水素に
より更に冷却されるとともに、冷却温度に応じて連続オ
ルソ−パラ変換が行われる。The hydrogen gas discharged from the ortho-para converter 41 passes through passages of the ortho-para converters 42 and 43 provided in the second and third heat exchangers 32 and 33, and is further cooled by returning hydrogen. At the same time, the continuous ortho-para conversion is performed depending on the cooling temperature.
【００１３】第３の熱交換器３３を導出した超臨界圧力
状態の水素ガスは、膨張タービン５１に導入され、ここ
で臨界圧力の約１３気圧付近まで断熱膨張して寒冷を発
生する。膨張後の超臨界状態の水素ガスは、断熱オルソ
−パラ変換器４４で断熱オルソ−パラ変換した後、熱交
換器３４のオルソ−パラ変換器４５の通路で更に冷却さ
れるとともに連続オルソ−パラ変換され、ＪＴ弁６１で
約１．２気圧までジュールトムソン膨張を行い、気液二
層混合状態の水素が生成する。The supercritical hydrogen gas discharged from the third heat exchanger 33 is introduced into the expansion turbine 51, where it adiabatically expands to a critical pressure of about 13 atm to generate cold. The expanded hydrogen gas in the supercritical state is subjected to adiabatic ortho-para conversion in the adiabatic ortho-para converter 44, and then further cooled in the passage of the ortho-para converter 45 of the heat exchanger 34 and is continuously ortho-para-converted. After being converted, the JT valve 61 performs Joule-Thomson expansion up to about 1.2 atmospheres to generate hydrogen in a gas-liquid two-layer mixed state.
【００１４】生成した気液二層混合状態の液体水素は、
液体水素溜８１で更に冷却され、液体水素溜８１内に設
けられたオルソ−パラ変換器４６で更にオルソ−パラ変
換した後、液体水素採取経路１２から製品液体水素とし
て取出される。The produced liquid hydrogen in a gas-liquid two-layer mixed state is
The liquid hydrogen is further cooled in the liquid hydrogen reservoir 81, further ortho-para converted by the ortho-para converter 46 provided in the liquid hydrogen reservoir 81, and then taken out from the liquid hydrogen collecting path 12 as product liquid hydrogen.
【００１５】一方、第１の熱交換器３１を導出して経路
２２に分岐した水素ガスは、更にその一部が経路２３に
分岐して膨張タービン５２に導入され、約４気圧まで断
熱膨張して寒冷を発生する。また、第２の熱交換器３２
の出口で更に一部の水素ガスが経路２４に分岐し、膨張
タービン５３に導入されて約４気圧まで断熱膨張し、寒
冷を発生する。膨張タービン５２，５３で寒冷を発生し
た水素ガスは、熱交換器を逆方向に戻って寒冷を原料水
素ガスに与えた後、循環圧縮機９２に吸引されて圧縮さ
れ、原料水素供給経路１１からの原料水素ガスと合流す
る。On the other hand, the hydrogen gas that has led out the first heat exchanger 31 and branched into the path 22 is further partially branched into the path 23 and introduced into the expansion turbine 52, where it is adiabatically expanded to approximately 4 atmospheres. Generate cold. In addition, the second heat exchanger 32
At the outlet of a part of the hydrogen gas is further branched to the path 24, introduced into the expansion turbine 53 and adiabatically expanded to about 4 atm to generate cold. The hydrogen gas that has generated cold in the expansion turbines 52 and 53 returns to the heat exchanger in the opposite direction to supply cold to the raw material hydrogen gas, and then is sucked and compressed by the circulation compressor 92 and is supplied from the raw material hydrogen supply path 11. It joins with the raw material hydrogen gas.
【００１６】また、経路２２から熱交換器３２，３３，
３４を経た水素ガスは、ＪＴ弁６２で約１．１気圧まで
ジュールトムソン膨張を行い、気液二層流となって液体
水素溜８１内に流入する。液体水素溜８１内の飽和水素
ガスは、経路２５に導出されて熱交換器３４，３３，３
２，３１を順次戻り、寒冷を原料水素ガスに与えた後、
循環圧縮機９１，９２で圧縮されて循環する。From the path 22, heat exchangers 32, 33,
The hydrogen gas that has passed through 34 undergoes Joule-Thomson expansion up to about 1.1 atm by the JT valve 62 and becomes a gas-liquid two-layer flow and flows into the liquid hydrogen reservoir 81. The saturated hydrogen gas in the liquid hydrogen reservoir 81 is led out to the path 25 to be transferred to the heat exchangers 34, 33, 3
After returning to No. 2 and 31 in sequence and supplying cold to the raw material hydrogen gas,
The circulation compressors 91 and 92 compress and circulate.
【００１７】なお、熱交換器３２，３３，３４に設けた
オルソ−パラ変換器４２，４３，４５は、熱交換器通路
内にオルソ−パラ変換触媒を充填したものである。ま
た、液体窒素溜７１には、経路７２から液体窒素が供給
されている。The ortho-para converters 42, 43, 45 provided in the heat exchangers 32, 33, 34 have the ortho-para conversion catalyst filled in the heat exchanger passages. Liquid nitrogen is supplied to the liquid nitrogen reservoir 71 from a path 72.
【００１８】上述のように、水素冷却液化系統２１に、
超臨界圧力状態の水素ガスを超臨界圧力状態に保持した
まま臨界圧力付近まで断熱膨張させる膨張タービン５１
を設けたことにより、原料水素ガスが有する圧力を有効
に利用して寒冷を発生させることができ、原料水素ガス
を冷却するために必要な寒冷量、すなわち、水素冷却液
化系統２１から分岐して膨張タービン５２，５３に向か
う水素ガス及びＪＴ弁６２を経て液体水素溜８１に向か
う水素量を低減することができ、原料水素供給経路１１
から供給される原料水素ガスを効率良く、経済的に液化
することができる。As described above, in the hydrogen cooling liquefaction system 21,
Expansion turbine 51 for adiabatically expanding hydrogen gas in a supercritical pressure state to near the critical pressure while maintaining the supercritical pressure state
By providing the above, it is possible to effectively use the pressure of the raw material hydrogen gas to generate cold, and to cool the raw material hydrogen gas, that is, to branch from the hydrogen cooling liquefaction system 21. The hydrogen gas toward the expansion turbines 52 and 53 and the hydrogen amount toward the liquid hydrogen reservoir 81 via the JT valve 62 can be reduced, and the raw material hydrogen supply path 11
The raw material hydrogen gas supplied from can be liquefied efficiently and economically.
【００１９】さらに、膨張タービン５１の出口側に断熱
オルソ−パラ変換器４４を設けて断熱オルソ−パラ変換
することにより、後段の熱交換器３４における熱交換を
確実に行うことができる。すなわち、膨張タービン５１
を導出した水素ガスは、膨張タービン５１導入前のパラ
濃度のままであり、このまま後段の熱交換器３４に流入
した場合、パラ濃度が膨張後の温度に対応した平衡パラ
濃度になっていないため、この熱交換器３４での熱交換
に支障を来すことがあるが、膨張タービン５１の出口側
でオルソ−パラ変換を行って平衡パラ濃度とすることに
より、多少の温度上昇はあるものの安定した状態での熱
交換を行うことができる。Further, by providing the adiabatic ortho-para converter 44 on the outlet side of the expansion turbine 51 and performing the adiabatic ortho-para conversion, the heat exchange in the heat exchanger 34 in the subsequent stage can be reliably performed. That is, the expansion turbine 51
The hydrogen gas that has been discharged remains at the para concentration before the expansion turbine 51 is introduced, and when it flows into the heat exchanger 34 at the latter stage as it is, the para concentration does not reach the equilibrium para concentration corresponding to the temperature after expansion. The heat exchange in the heat exchanger 34 may be hindered, but the ortho-para conversion is performed on the outlet side of the expansion turbine 51 to obtain the equilibrium para concentration, but the temperature is slightly increased, but stable. It is possible to perform heat exchange under the condition.
【００２０】なお、本明細書においては、膨張機として
近年一般的に使用されている膨張タービンを用いている
が、従来の往復式膨張機を用いることも可能である。ま
た、循環用水素の分岐位置は、上記実施例に限らず、例
えば、第１の熱交換器に導入する前に分岐することもで
きる。In this specification, an expansion turbine that has been generally used in recent years is used as the expander, but a conventional reciprocating expander can also be used. Further, the branching position of the hydrogen for circulation is not limited to the above-mentioned embodiment, but may be branched before being introduced into the first heat exchanger, for example.
【００２１】[0021]
【発明の効果】以上説明したように、本発明によれば、
水素冷却液化系統に設けた膨張タービンで水素ガスを臨
界圧力付近まで断熱膨張させて寒冷を発生させるので、
水素冷却液化系統に供給される原料水素ガスが有する高
い圧力を寒冷として有効に取出すことができ、効果的に
利用することができる。これにより、プロセスの効率が
向上し、より少ない動力で水素を液化することが可能と
なる。As described above, according to the present invention,
Since the expansion turbine installed in the hydrogen cooling liquefaction system adiabatically expands the hydrogen gas to near the critical pressure to generate cold,
The high pressure of the raw material hydrogen gas supplied to the hydrogen cooling liquefaction system can be effectively taken out as cold and can be effectively used. This improves the efficiency of the process and makes it possible to liquefy hydrogen with less power.
【００２２】また、断熱膨張後の圧力を臨界圧力以上に
したことにより、不安定な気液二層流となることがな
く、安定した状態の流体となるので、プロセスの設計
上、また、装置の設計，製作上、取扱いが容易であり、
本発明の超臨界タービンを採用することにより、長期間
使用可能な実用装置の製作が可能になる。Further, since the pressure after the adiabatic expansion is set to the critical pressure or higher, an unstable gas-liquid two-layer flow does not occur and a fluid in a stable state is obtained. Therefore, in designing the process and in the apparatus. It is easy to handle in designing and manufacturing
By adopting the supercritical turbine of the present invention, it becomes possible to manufacture a practical device that can be used for a long period of time.
【００２３】さらに、膨張タービンの出口で断熱的にオ
ルソ−パラ変換を行うことにより、後段の熱交換器での
熱交換を効率よく行うことができる。Further, by performing adiabatic ortho-para conversion at the outlet of the expansion turbine, it is possible to efficiently perform heat exchange in the heat exchanger in the subsequent stage.
【図１】 本発明の一実施例を示す系統図である。FIG. 1 is a system diagram showing an embodiment of the present invention.
１１…原料水素供給経路、２１…水素冷却液化系統、３
１，３２，３３，３４…熱交換器、４１，４２，４３，
４４，４５，４６…オルソ−パラ変換器、５１，５２，
５３…膨張タービン、６１，６２…ジュールトムソン弁
（ＪＴ弁）、７１…液体窒素溜、８１…液体水素溜、９
１，９２…循環圧縮機11 ... Raw material hydrogen supply route, 21 ... Hydrogen cooling liquefaction system, 3
1, 32, 33, 34 ... Heat exchanger, 41, 42, 43,
44, 45, 46 ... Ortho-Para converter, 51, 52,
53 ... Expansion turbine, 61, 62 ... Joule Thomson valve (JT valve), 71 ... Liquid nitrogen reservoir, 81 ... Liquid hydrogen reservoir, 9
1,92 ... Circulation compressor
Claims (4)
後、膨張させて液化する液体水素の製造方法であって、
水素の冷却液化系統に設けた膨張タービンに前記水素ガ
スを導入し、臨界圧力以上の圧力に膨張させて導出する
ことを特徴とする液体水素の製造方法。1. A method for producing liquid hydrogen, comprising cooling hydrogen gas compressed to a critical pressure or higher and then expanding and liquefying it.
A method for producing liquid hydrogen, which comprises introducing the hydrogen gas into an expansion turbine provided in a cooling and liquefying system of hydrogen, expanding the hydrogen gas to a pressure equal to or higher than a critical pressure, and discharging the hydrogen.
断熱オルソ−パラ変換することを特徴とする請求項１記
載の液体水素の製造方法。2. The method for producing liquid hydrogen according to claim 1, wherein the hydrogen gas discharged from the expansion turbine is subjected to adiabatic ortho-para conversion.
後、膨張させて液化する液体水素の製造装置であって、
水素の冷却液化系統に、前記水素ガスを臨界圧力以上の
圧力に膨張させる膨張タービンを設けたことを特徴とす
る液体水素の製造装置。3. An apparatus for producing liquid hydrogen, comprising cooling hydrogen gas compressed to a critical pressure or higher and then expanding and liquefying it.
An apparatus for producing liquid hydrogen, wherein an expansion turbine for expanding the hydrogen gas to a pressure equal to or higher than a critical pressure is provided in a hydrogen cooling liquefaction system.
−パラ変換器を設けたことを特徴とする請求項３記載の
液体水素の製造装置。4. The apparatus for producing liquid hydrogen according to claim 3, wherein an adiabatic ortho-para converter is provided at the outlet of the expansion turbine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29999494A JP3521360B2 (en) | 1994-12-02 | 1994-12-02 | Method and apparatus for producing liquid hydrogen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29999494A JP3521360B2 (en) | 1994-12-02 | 1994-12-02 | Method and apparatus for producing liquid hydrogen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08159653A true JPH08159653A (en) | 1996-06-21 |
| JP3521360B2 JP3521360B2 (en) | 2004-04-19 |
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ID=17879465
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP29999494A Expired - Fee Related JP3521360B2 (en) | 1994-12-02 | 1994-12-02 | Method and apparatus for producing liquid hydrogen |
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| Country | Link |
|---|---|
| JP (1) | JP3521360B2 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015188808A1 (en) * | 2014-06-13 | 2015-12-17 | Technische Universität Dresden | Method and device for adjusting concentration ratios of orthohydrogen to parahydrogen |
| CN108444213A (en) * | 2018-05-28 | 2018-08-24 | 张家港富瑞氢能装备有限公司 | Purifier in liquefaction of hydrogen device |
| CN108744870A (en) * | 2018-05-28 | 2018-11-06 | 张家港富瑞氢能装备有限公司 | Hydrogen purification technique during liquefaction of hydrogen |
| WO2019189409A1 (en) * | 2018-03-29 | 2019-10-03 | 川崎重工業株式会社 | Liquid hydrogen production facility and hydrogen gas production facility |
| JP2020024067A (en) * | 2018-08-07 | 2020-02-13 | 川崎重工業株式会社 | Liquid hydrogen producing facility |
| CN113503692A (en) * | 2021-07-01 | 2021-10-15 | 中国科学院理化技术研究所 | Hydrogen liquefaction system |
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|---|---|---|---|---|
| JPH0319471B2 (en) * | 1987-01-07 | 1991-03-15 | Air Prod & Chem | |
| JPH05180558A (en) * | 1990-10-26 | 1993-07-23 | L'air Liquide | Method of liquefying gas and refrigerating plant |
-
1994
- 1994-12-02 JP JP29999494A patent/JP3521360B2/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0319471B2 (en) * | 1987-01-07 | 1991-03-15 | Air Prod & Chem | |
| JPH05180558A (en) * | 1990-10-26 | 1993-07-23 | L'air Liquide | Method of liquefying gas and refrigerating plant |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015188808A1 (en) * | 2014-06-13 | 2015-12-17 | Technische Universität Dresden | Method and device for adjusting concentration ratios of orthohydrogen to parahydrogen |
| WO2019189409A1 (en) * | 2018-03-29 | 2019-10-03 | 川崎重工業株式会社 | Liquid hydrogen production facility and hydrogen gas production facility |
| CN111919077A (en) * | 2018-03-29 | 2020-11-10 | 川崎重工业株式会社 | Liquid hydrogen production apparatus and hydrogen production apparatus |
| CN108444213A (en) * | 2018-05-28 | 2018-08-24 | 张家港富瑞氢能装备有限公司 | Purifier in liquefaction of hydrogen device |
| CN108744870A (en) * | 2018-05-28 | 2018-11-06 | 张家港富瑞氢能装备有限公司 | Hydrogen purification technique during liquefaction of hydrogen |
| CN108744870B (en) * | 2018-05-28 | 2019-05-21 | 张家港富瑞氢能装备有限公司 | Hydrogen purification process during liquefaction of hydrogen |
| CN108444213B (en) * | 2018-05-28 | 2023-09-26 | 江苏国富氢能技术装备股份有限公司 | Purifying device in hydrogen liquefying device |
| JP2020024067A (en) * | 2018-08-07 | 2020-02-13 | 川崎重工業株式会社 | Liquid hydrogen producing facility |
| CN113503692A (en) * | 2021-07-01 | 2021-10-15 | 中国科学院理化技术研究所 | Hydrogen liquefaction system |
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| Publication number | Publication date |
|---|---|
| JP3521360B2 (en) | 2004-04-19 |
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