JP3500081B2 - Liquefied natural gas separation apparatus, separation method, power generation method and method of using liquefied natural gas - Google Patents
Liquefied natural gas separation apparatus, separation method, power generation method and method of using liquefied natural gasInfo
- Publication number
- JP3500081B2 JP3500081B2 JP36202798A JP36202798A JP3500081B2 JP 3500081 B2 JP3500081 B2 JP 3500081B2 JP 36202798 A JP36202798 A JP 36202798A JP 36202798 A JP36202798 A JP 36202798A JP 3500081 B2 JP3500081 B2 JP 3500081B2
- Authority
- JP
- Japan
- Prior art keywords
- natural gas
- liquefied natural
- component
- separation
- methane
- 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
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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
- F25J3/0214—Liquefied natural gas
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
-
- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Pipeline Systems (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
【０００１】
【発明の属する技術分野】本発明は、液化天然ガスの分
離装置並びに分離方法、発電方法及び液化天然ガスの使
用方法に関する。
【０００２】
【従来の技術】発電プラントにおいて、液化天然ガスを
用いてこれを燃焼させ、それによって得られる熱エネル
ギーを活用して発電を行うものが知られている。ところ
が、液化天然ガスを燃焼させた際にはＣＯ2を発生する
ので、地球温暖化防止等の観点からこれを低減させるこ
とが切望されている。
【０００３】
【発明が解決しようとする課題】本発明者らは、このよ
うな要望に対して、発電プラントにおけるＣＯ2発生量
を効果的に減少させる対策について鋭意検討し、本発明
に想到した。すなわち、本発明は、有効な環境対策を行
った液化天然ガスの分離装置並びに分離方法、発電方法
を提供することを目的とする。また、本発明は、ＣＯ2
発生量を減少させるだけでなく、それによって内燃機関
用燃料として好適な燃料を提供することのできる液化天
然ガスの使用方法を提供することを目的とする。
【０００４】
【課題を解決するための手段】上記目的を達成するため
に、本発明に係る液化天然ガスの使用方法は、液化天然
ガスを分留装置に送り、該分留装置下部の取り出し口か
ら液化天然ガスを取り出して加熱し、加熱された液化天
然ガスを上記分留装置に戻し、これによって分留装置内
の液化天然ガスを加熱して分留操作を行い、分留装置上
部から気化したガスを取り出し、分留前の液化天然ガス
によって該気化したガスを冷却してエタン成分を液化
し、メタン成分を取り出すと共に、液化したエタン成分
を上記分留装置の上部に戻した後、その沸点よりも低い
温度の位置で分留装置から液体として取り出し、メタン
成分を後段の発電装置に送給して発電を行い、上記エタ
ン成分と分留装置の下部の別の取り出し口から取り出し
たプロパン以上の炭素数の成分とを内燃機関用燃料とし
て使用することを特徴とする。
【０００５】
【発明の実施の形態】以下に添付図面に示した実施の形
態を参照しながら本発明に係る液化天然ガスの分離装置
並びに分離方法、発電方法及び液化天然ガスの使用方法
を説明する。図１は本発明に係る液化天然ガスの分離装
置の一実施の形態を示す。まず、この分離装置の概要を
説明する。この実施の形態に係る液化天然ガスの分離装
置は、分留装置１によって液化天然ガスを分留する。貯
蔵タンク２は液化天然ガスを貯蔵するためのタンクであ
り、液化天然ガスを通常約−１６２℃の液体状態で貯蔵
する。この液化天然ガスは、送給ポンプ３によって熱交
換器４を経由して上記分留装置１の中段に送られる。分
留装置１の上部から取り出されるメタン成分はメタン分
離手段を構成する熱交換器４を経て分離タンク５に送ら
れる。最終的にメタン成分は分離タンク５の上部から取
り出され、後段の発電装置にパイプを通して送られる。
分離タンク５の下には液状成分の取り出し口が設けられ
ており、ポンプ６はこのような液状成分を分留装置１に
戻すためのものである。
【０００６】分留装置１の下部にはポンプ７によって液
化天然ガスの一部を取り出すための取り出し口が設けら
れている。ポンプ７によって取り出された液化天然ガス
は、加熱器８を経て分留装置１の下部に戻されるように
なっている。加熱器８には中間冷媒が流れる。加熱器９
はこの中間冷媒を海水で加熱するためのものである。液
化天然ガスを加熱した中間冷媒は一旦サージタンク１０
で液化する。ポンプ１１は液化した中間冷媒を再度加熱
器８に戻すためのものである。中間冷媒としては、ＬＰ
Ｇ，フロン等の低温で固化しない流体を用いることがで
きる。分留装置１の下部にはさらに別の液化天然ガス取
り出し口が設けられており、高沸点成分が取り出される
ようになっている。以上のように分留装置１は、下部が
海水で加熱され、上部が分留前の液化天然ガスによって
冷却される構成となっている。これにより、最上部が約
−１２０℃、中段が約−８５℃、最下部が約−４０℃と
なるように温度が分布する。なお、分留装置１として
は、内部に棚段を設けた蒸留塔等の気液接触装置を用い
ることが一般的である。
【０００７】次いで、図１の分離装置を用いて液化天然
ガスを分離する方法について説明する。貯蔵タンク２に
は上記したように約−１６２℃の液化天然ガスが貯蔵さ
れている。この液化天然ガスを貯蔵タンク２から送給ポ
ンプ３によって熱交換器４に送る。熱交換器４では、分
留装置１からのメタン成分（約−１２０℃）との間で熱
交換が行われる。ここで液化天然ガスの一部が気化す
る。この加熱後の液化天然ガスを分留装置１の中段に送
る。供給された液化天然ガスは、気体成分と液状成分と
に分かれる。分留装置１には、下部から加熱された液化
天然ガスが供給される。これが分留操作のための熱源と
なっている。
【０００８】すなわち、分留装置１の下部からは、その
取り出し口から液化天然ガスの一部が取り出される。取
り出される液化天然ガスは、約−４０℃で、炭素数３以
上の成分であり、大部分は液状プロパンである。取り出
した液化天然ガスをポンプ７によって加熱器８に送る。
加熱器８では、中間冷媒との間で熱交換が行われる。中
間冷媒は、通常約１０℃であり、熱交換後は約０℃とな
って、サージタンク１０で液化し、ポンプ１１で加熱器
９に送られる。加熱器９では、海水によって中間冷媒が
加熱される。加熱された中間冷媒は再び加熱器８に送ら
れる。加熱器８で加熱された液化天然ガスは分留装置１
の下部に戻される。このようにして分留操作のための熱
を得ることができる。
【０００９】前記したように、加熱された分留装置１の
内部は、最上部が約−１２０℃、中段が約−８５℃、最
下部が約−４０℃となるように温度が分布する。沸点−
１６２℃のメタン成分は、分留装置１の上部から約−１
２０℃の温度で取り出され、熱交換器４で分留前の液化
天然ガスによって冷却され、約−１４０℃となる。これ
によって、メタンの一部と混入しているエタン成分が液
化し、この冷却された液化成分が分離タンク５の下部か
らポンプ６によって分留装置１の上部に戻される。この
ようにして、分留装置１の上部は冷却される。分離タン
ク５の上部からはメタン成分が気体として取り出され、
後段の発電装置に送られる。液状成分として分留装置１
内を降下するエタン成分は、その沸点である−８５℃よ
りも低い温度の位置１２で分留装置１から液体として取
り出される。分留装置１の下部の別の取り出し口からは
プロパン以上の炭素数の成分が液体として取り出され
る。エタン成分とプロパン以上の炭素数の成分とは、回
収後、自動車用燃料として活用される。これらの成分
は、取り扱い易い液体の状態で一旦取り出す。自動車燃
料として出荷される際には、気体燃料としてガスボンベ
に充填する。この図１の実施の形態から明らかなよう
に、本発明では、熱源、冷熱を装置内で得られる熱及び
自然界に存在する熱源を使用しており、ポンプ動力のみ
のエネルギーにより、システムの構成が出来る。
【００１０】本発明に係る発電方法では、図１に示した
ような分離装置を用いて、液化天然ガスをメタン成分と
その他のガスとに分離し、分離されたメタン成分のみを
用いて発電を行う。これによって、ＣＯ2発生量を削減
する。例えば、インドネシア産の標準液化天然ガスは、
９０．８７％のメタン成分である。ＣＯ2発生量ごとの
カロリー数は、１８９，０４６ｋｃａｌ／ｋｇ・ｍｏｌ
・ＣＯ2である。また、オーストラリア産の標準液化天
然ガスは、８８．８５％のメタン成分である。ＣＯ2発
生量ごとのカロリー数は、１８８，５５１ｋｃａｌ／ｋ
ｇ・ｍｏｌ・ＣＯ2である。純粋なメタンのＣＯ2発生量
ごとのカロリー数は、１９１，２９０ｋｃａｌ／ｋｇ・
ｍｏｌ・ＣＯ2である。純粋なメタンに対するＣＯ2発生
量自体の比率は、これらの数値から求める逆比となるの
で、インドネシア産の標準液化天然ガスは、メタンに対
し、約１．２％のＣＯ2発生量の増加となり、オースト
ラリア産では約１．４５％のＣＯ2発生量の増加とな
る。したがって、本発明に係る発電方法によれば大幅に
ＣＯ2発生量が減少する。
【００１１】また、本発明に係る液化天然ガスの使用方
法によれば、上記の図１の形態について説明したよう
に、液化天然ガスをメタン成分とその他の高沸点成分と
に分離し、メタン成分を発電用燃料として供給し、他の
高沸点成分を自動車等の車両用燃料又は他の内燃機関用
燃料として使用する。エタン成分やプロパン成分は、単
位気体体積当りのカロリーがメタン成分よりもはるかに
大きく、同一容量の燃料タンクを備えた自動車の場合、
１回の充填で長距離を走行出来る事になる。これによっ
て、内燃機関用燃料として好適な気体燃料を提供するこ
とができる。液化天然ガスは無公害型の燃料として注目
されている。現在、液化天然ガスで例えば自動車を走ら
せる場合、液化天然ガスを貯蔵するタンク（ガスボン
ベ）の容量が大きくなり過ぎることが難点となってい
る。表１は、インドネシア産標準液化天然ガスの成分ご
との発生カロリー数を示している。この成分の中でもメ
タン成分は単位気体体積当りのカロリー発生量が少な
い。本発明に係る液化天然ガスの使用方法によれば、メ
タン成分を発電用燃料として取りだした際の残余の成分
として同時にこのような自動車用燃料に適する燃料を得
ることができるので、上記した問題全てを解消すること
ができる。
【００１２】
【表１】
【００１３】本発明に係る液化天然ガスの分離装置並び
に分離方法、発電方法及び液化天然ガスの使用方法は、
図１の実施の形態について説明したが、このような実施
の形態に限るものではなく、当業者にとって自明な変更
・付加等は全て本発明の技術的範囲に含まれる。また、
図１のような実施の形態を実施するための付帯する制御
機器等は、設計上当業者が適宜選択することができる。
【００１４】液化天然ガスの加熱装置として、図１に示
すように、加熱器８、ポンプ７、サージタンク１０、ポ
ンプ１１及び加熱器９を含むものを用いた。これは、用
いる海水の氷結を避けるためである。しかし、この他に
も加熱装置としては、例えば、図２に示すように加熱コ
イル２０内に液化天然ガスを流し、加熱コイル２０に直
接海水をかけるようにするものも用いることができる。
なお、図２において、図１と同様の機能を有する要素に
は同一符号を付けてその説明を省略する。
【００１５】なお、以上の説明において、メタン成分、
エタン成分のように「成分」の語を付したのは、メタ
ン、エタン等の意図した成分そのものの場合の他、他の
成分（若干量）を含むことも想定している。すなわち、
工程の途中では、例えばメタンが意図されていてもエタ
ン等が含まれている場合もあり、最終生成物においても
本来純粋なものが理想的であるが、実際には不可避的不
純物が存在し得るからである。
【００１６】
【発明の効果】上記したところから明かなように、本発
明によれば、少ないエネルギー消費で液化天然ガスをメ
タン成分とその他の成分に分離する装置および方法が提
供される。さらには、得られたメタン成分を発電プラン
ト用燃料として使用することにより、ＣＯ2発生量がよ
り少ない発電方法が提供される。また、本発明によれ
ば、内燃機関用燃料として好適な燃料を提供することの
できる液化天然ガスの使用方法が提供される。Description: BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a liquefied natural gas separation apparatus, a separation method, a power generation method and a method of using liquefied natural gas. 2. Description of the Related Art There is known a power plant in which liquefied natural gas is burned using natural gas and electric power is generated by utilizing thermal energy obtained thereby. However, when liquefied natural gas is burned, CO 2 is generated. Therefore, it is desired to reduce CO 2 from the viewpoint of preventing global warming. [0003] In response to such a demand, the present inventors have intensively studied measures for effectively reducing the amount of CO 2 generated in a power plant, and have reached the present invention. . That is, an object of the present invention is to provide a liquefied natural gas separation device, a separation method, and a power generation method in which effective environmental measures are taken. Also, the present invention relates to CO 2
It is an object of the present invention to provide a method of using liquefied natural gas which can not only reduce the amount of generation but also provide a fuel suitable as a fuel for an internal combustion engine. [0004] In order to achieve the above object,
The method for using liquefied natural gas according to the present invention
The gas is sent to the fractionator,
Liquefied natural gas is taken out of the liquefied natural gas and heated.
The natural gas is returned to the fractionator, thereby
Liquefied natural gas is heated to perform a fractionation operation.
Take out the vaporized gas from the section and liquefy natural gas before fractionation
Cools the vaporized gas to liquefy the ethane component
To remove the methane component and liquefy the ethane component
Lower than the boiling point after returning
Removed as liquid from fractionator at temperature and
The components are sent to a power generator at the subsequent stage to generate power,
Components and a separate outlet at the bottom of the fractionator
Components with a carbon number greater than that of propane
It is characterized by using. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A liquefied natural gas separation apparatus, a separation method, a power generation method and a method for using liquefied natural gas according to the present invention will be described below with reference to embodiments shown in the accompanying drawings. . FIG. 1 shows an embodiment of a liquefied natural gas separation apparatus according to the present invention. First, an outline of the separation device will be described. In the liquefied natural gas separation apparatus according to this embodiment, the liquefied natural gas is fractionated by the fractionating apparatus 1. The storage tank 2 is a tank for storing liquefied natural gas, and usually stores liquefied natural gas in a liquid state at about -162 ° C. This liquefied natural gas is sent to the middle stage of the fractionating apparatus 1 via the heat exchanger 4 by the feed pump 3. The methane component taken out from the upper part of the fractionation apparatus 1 is sent to a separation tank 5 via a heat exchanger 4 constituting methane separation means. Finally, the methane component is taken out from the upper part of the separation tank 5 and sent to a power generation device at a later stage through a pipe.
A liquid component outlet is provided below the separation tank 5, and a pump 6 is for returning such a liquid component to the fractionating apparatus 1. An outlet for extracting a part of liquefied natural gas by a pump 7 is provided at a lower portion of the fractionating apparatus 1. The liquefied natural gas taken out by the pump 7 is returned to the lower part of the fractionating apparatus 1 via the heater 8. The intermediate refrigerant flows through the heater 8. Heater 9
Is for heating this intermediate refrigerant with seawater. The intermediate refrigerant that has heated the liquefied natural gas is once supplied to the surge tank 10
And liquefy. The pump 11 is for returning the liquefied intermediate refrigerant to the heater 8 again. LP as an intermediate refrigerant
A fluid that does not solidify at a low temperature, such as G or Freon, can be used. A further liquefied natural gas take-out port is provided at the lower part of the fractionator 1, so that high boiling components can be taken out. As described above, the fractionation apparatus 1 has a configuration in which the lower part is heated by seawater and the upper part is cooled by liquefied natural gas before fractionation. Thereby, the temperature is distributed such that the uppermost portion is about -120 ° C, the middle portion is about -85 ° C, and the lowermost portion is about -40 ° C. In addition, as the fractionation apparatus 1, it is common to use a gas-liquid contacting apparatus such as a distillation column provided with a shelf inside. Next, a method for separating liquefied natural gas using the separation apparatus shown in FIG. 1 will be described. As described above, the storage tank 2 stores liquefied natural gas at about -162 ° C. The liquefied natural gas is sent from the storage tank 2 to the heat exchanger 4 by the feed pump 3. In the heat exchanger 4, heat exchange is performed with the methane component (about −120 ° C.) from the fractionating apparatus 1. Here, a part of the liquefied natural gas is vaporized. The heated liquefied natural gas is sent to the middle stage of the fractionating apparatus 1. The supplied liquefied natural gas is divided into a gas component and a liquid component. The liquefied natural gas heated from below is supplied to the fractionating apparatus 1. This is the heat source for the fractionation operation. [0008] That is, a part of the liquefied natural gas is taken out of the lower part of the fractionating apparatus 1 through the outlet. The liquefied natural gas taken out is a component having 3 or more carbon atoms at about −40 ° C., and is mostly liquid propane. The removed liquefied natural gas is sent to a heater 8 by a pump 7.
In the heater 8, heat exchange is performed with the intermediate refrigerant. The temperature of the intermediate refrigerant is usually about 10 ° C., becomes about 0 ° C. after heat exchange, is liquefied in the surge tank 10, and is sent to the heater 9 by the pump 11. In the heater 9, the intermediate refrigerant is heated by the seawater. The heated intermediate refrigerant is sent to the heater 8 again. The liquefied natural gas heated by the heater 8 is separated by the fractionating device 1
Is returned to the bottom. In this way, heat for the fractionation operation can be obtained. As described above, the temperature inside the heated fractionating apparatus 1 is distributed such that the uppermost portion is about -120 ° C, the middle portion is about -85 ° C, and the lowermost portion is about -40 ° C. Boiling point-
The methane component at 162 ° C.
It is taken out at a temperature of 20 ° C. and cooled by the liquefied natural gas before fractionation in the heat exchanger 4 to about −140 ° C. As a result, the ethane component mixed with a part of the methane is liquefied, and the cooled liquefied component is returned from the lower part of the separation tank 5 to the upper part of the fractionating apparatus 1 by the pump 6. Thus, the upper part of the fractionating apparatus 1 is cooled. From the upper part of the separation tank 5, the methane component is taken out as a gas,
It is sent to the power generator at the subsequent stage. Fractionation device 1 as liquid component
The ethane component falling inside is taken out as a liquid from the fractionating apparatus 1 at a position 12 at a temperature lower than its boiling point -85 ° C. A component having a carbon number equal to or higher than propane is taken out as a liquid from another outlet at the lower portion of the fractionating apparatus 1. The ethane component and the component having a carbon number equal to or greater than propane are used as automobile fuel after recovery. These components are once taken out in a liquid state that is easy to handle. When shipped as automobile fuel, gas cylinders are filled as gaseous fuel. As is clear from the embodiment shown in FIG. 1, the present invention uses a heat source, heat obtained in the apparatus for cold heat, and a heat source existing in the natural world. I can do it. In the power generation method according to the present invention, liquefied natural gas is separated into a methane component and another gas using a separation device as shown in FIG. 1, and power generation is performed using only the separated methane component. Do. This reduces the amount of CO 2 generated. For example, Indonesian standard liquefied natural gas is
90.87% of the methane component. The number of calories per CO 2 generation is 189,046 kcal / kg · mol
- is CO 2. Standard liquefied natural gas produced in Australia has a methane content of 88.85%. The number of calories per CO 2 emission amount is 188,551 kcal / k
g · mol · CO 2 . The calorie count of pure methane per CO 2 emission is 191 and 290 kcal / kg ·
mol · CO 2 . The ratio of the amount of CO 2 emission itself to pure methane is the inverse ratio calculated from these figures, so standard liquefied natural gas produced in Indonesia has an increase in CO 2 emission of about 1.2% compared to methane. In Australia, about 1.45% increase in CO 2 emission is generated. Therefore, according to the power generation method of the present invention, the amount of generated CO 2 is greatly reduced. According to the method of using liquefied natural gas according to the present invention, as described with reference to the embodiment of FIG. 1, the liquefied natural gas is separated into a methane component and other high-boiling components, Is supplied as fuel for power generation, and other high-boiling components are used as fuel for vehicles such as automobiles or other fuel for internal combustion engines. The ethane and propane components have much higher calories per unit gas volume than the methane component, and if the car has a fuel tank of the same capacity,
A long distance can be run with one filling. Thereby, a gaseous fuel suitable as a fuel for an internal combustion engine can be provided. Liquefied natural gas is attracting attention as a non-polluting fuel. At present, when a vehicle is driven by liquefied natural gas, for example, it is a problem that the capacity of a tank (gas cylinder) for storing liquefied natural gas becomes too large. Table 1 shows the number of calories generated for each component of the Indonesian standard liquefied natural gas. Among these components, the methane component generates a small amount of calories per unit gas volume. According to the method for using liquefied natural gas according to the present invention, it is possible to obtain a fuel suitable for such an automobile fuel at the same time as a residual component when a methane component is taken out as a fuel for power generation. Can be eliminated. [Table 1] [0013] The liquefied natural gas separation apparatus, separation method, power generation method and liquefied natural gas use method according to the present invention are described below.
Although the embodiment of FIG. 1 has been described, the present invention is not limited to such an embodiment, and all changes and additions obvious to those skilled in the art are included in the technical scope of the present invention. Also,
Attached control devices and the like for implementing the embodiment as shown in FIG. 1 can be appropriately selected by a person skilled in the art in design. As a liquefied natural gas heating device, as shown in FIG. 1, a device including a heater 8, a pump 7, a surge tank 10, a pump 11, and a heater 9 was used. This is to avoid freezing of the seawater used. However, in addition to this, for example, as shown in FIG. 2, a device that causes liquefied natural gas to flow in the heating coil 20 and directly applies seawater to the heating coil 20 can also be used.
In FIG. 2, elements having the same functions as those in FIG. In the above description, the methane component,
The term "component" as in the ethane component is not limited to the intended component itself such as methane and ethane, but may include other components (slight amount). That is,
In the middle of the process, for example, methane may be included even if methane is intended, and even in the final product, a pure product is ideally ideal, but unavoidable impurities may actually exist. Because. As is apparent from the above, according to the present invention, there is provided an apparatus and a method for separating liquefied natural gas into methane components and other components with low energy consumption. Furthermore, by using the obtained methane component as a fuel for a power plant, a power generation method with less CO 2 generation is provided. Further, according to the present invention, there is provided a method for using liquefied natural gas, which can provide a fuel suitable as a fuel for an internal combustion engine.
【図面の簡単な説明】
【図１】本発明に係る液化天然ガスの分離装置の一実施
の形態を説明する概念図である。
【図２】本発明に係る液化天然ガスの分離装置の他の実
施の形態を説明する概念図である。
【符号の説明】
１ 分留装置
２ 貯蔵タンク
３ 送給ポンプ
４ 熱交換器
５ 分離タンク
６ ポンプ
７ ポンプ
８ 加熱器
９ 加熱器
１０ サージタンク
１１ ポンプ
２０ 加熱コイルBRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a conceptual diagram illustrating an embodiment of a liquefied natural gas separation device according to the present invention. FIG. 2 is a conceptual diagram illustrating another embodiment of the liquefied natural gas separation device according to the present invention. [Description of Signs] 1 Fractionation device 2 Storage tank 3 Feed pump 4 Heat exchanger 5 Separation tank 6 Pump 7 Pump 8 Heater 9 Heater 10 Surge tank 11 Pump 20 Heating coil
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 昭63−231192（ＪＰ，Ａ) 特開 昭48−76907（ＪＰ，Ａ) 特開 昭61−89970（ＪＰ，Ａ) 特公 昭36−14011（ＪＰ，Ｂ１) (58)調査した分野(Int.Cl.7，ＤＢ名) F25J 1/00 - 5/00 ──────────────────────────────────────────────────続 き Continuation of the front page (56) References JP-A-63-231192 (JP, A) JP-A-48-76907 (JP, A) JP-A-61-89970 (JP, A) 14011 (JP, B1) (58) Fields investigated (Int. Cl. 7 , DB name) F25J 1/00-5/00
Claims (1)
装置下部の取り出し口から液化天然ガスを取り出して加
熱し、加熱された液化天然ガスを上記分留装置に戻し、
これによって分留装置内の液化天然ガスを加熱して分留
操作を行い、分留装置上部から気化したガスを取り出
し、分留前の液化天然ガスによって該気化したガスを冷
却してエタン成分を液化し、メタン成分を取り出すと共
に、液化したエタン成分を上記分留装置の上部に戻した
後、その沸点よりも低い温度の位置で分留装置から液体
として取り出し、メタン成分を後段の発電装置に送給し
て発電を行い、上記エタン成分と分留装置の下部の別の
取り出し口から取り出したプロパン以上の炭素数の成分
とを内燃機関用燃料として使用することを特徴とする液
化天然ガスの使用方法。(57) [Claims 1] Liquefied natural gas is sent to a fractionating apparatus, the liquefied natural gas is taken out from an outlet at the lower part of the fractionating apparatus and heated, and the heated liquefied natural gas is subjected to the above described Return to the fractionator,
This heats the liquefied natural gas in the fractionator to perform a fractionation operation, and removes the vaporized gas from the upper part of the fractionator.
The vaporized gas is cooled by liquefied natural gas before fractionation.
And the ethane component was liquefied, the methane component was removed, and the liquefied ethane component was returned to the top of the fractionator.
After that, at a temperature lower than its boiling point,
Taken out as to feed methane components downstream of the generator
To separate the ethane component and another fraction below the fractionator.
Components with more carbon atoms than propane taken out of the outlet
Using liquefied natural gas, characterized by the use of preparative as fuel for an internal combustion engine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP36202798A JP3500081B2 (en) | 1998-12-21 | 1998-12-21 | Liquefied natural gas separation apparatus, separation method, power generation method and method of using liquefied natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP36202798A JP3500081B2 (en) | 1998-12-21 | 1998-12-21 | Liquefied natural gas separation apparatus, separation method, power generation method and method of using liquefied natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2000186886A JP2000186886A (en) | 2000-07-04 |
| JP3500081B2 true JP3500081B2 (en) | 2004-02-23 |
Family
ID=18475664
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP36202798A Expired - Fee Related JP3500081B2 (en) | 1998-12-21 | 1998-12-21 | Liquefied natural gas separation apparatus, separation method, power generation method and method of using liquefied natural gas |
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| Country | Link |
|---|---|
| JP (1) | JP3500081B2 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4551548B2 (en) * | 2000-10-04 | 2010-09-29 | 大阪瓦斯株式会社 | Power generation facility and power generation method using the same |
| JP4489326B2 (en) * | 2001-07-17 | 2010-06-23 | 東京瓦斯株式会社 | City gas supply method and apparatus |
| MX2007002797A (en) * | 2004-09-14 | 2007-04-23 | Exxonmobil Upstream Res Co | Method of extracting ethane from liquefied natural gas. |
| US8065890B2 (en) * | 2004-09-22 | 2011-11-29 | Fluor Technologies Corporation | Configurations and methods for LPG production and power cogeneration |
| US7603867B2 (en) * | 2006-09-11 | 2009-10-20 | Cryogenic Group, Inc. | Process and system to produce multiple distributable products from source, or imported LNG |
| DE102008004077A1 (en) * | 2008-01-12 | 2009-07-23 | Man Diesel Se | Process and apparatus for the treatment of natural gas for use in a gas engine |
| JP5056649B2 (en) * | 2008-07-28 | 2012-10-24 | 株式会社Ｉｈｉ | Separation apparatus and method for liquefied natural gas |
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1998
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