JP2000186886A - Separating device and method of liquefied natural gas, method of power generation and using method of liquefied natural gas - Google Patents
Separating device and method of liquefied natural gas, method of power generation and using method of liquefied natural gasInfo
- Publication number
- JP2000186886A JP2000186886A JP10362027A JP36202798A JP2000186886A JP 2000186886 A JP2000186886 A JP 2000186886A JP 10362027 A JP10362027 A JP 10362027A JP 36202798 A JP36202798 A JP 36202798A JP 2000186886 A JP2000186886 A JP 2000186886A
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- Japan
- Prior art keywords
- natural gas
- liquefied natural
- methane
- gas
- fractionating
- 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
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)
Abstract
Description
【０００１】[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。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.
【０００２】[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。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】[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。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. Further, 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】[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分離装置は、液化天然
ガスを分留する分留装置と、該分留装置の下部から液化
天然ガスを取り出して加熱した後に前記分留装置へ返送
する加熱手段と、上記分留装置上部から気化したガスを
取り出しメタン成分とその他のガスに分離するメタン分
離手段とからなることを特徴とする。本発明に係る液化
天然ガスの分離装置はさらに、メタン分離手段から取り
出したメタン成分を発電装置に送給するメタン送給手段
を含むことができる。In order to achieve the above object, a liquefied natural gas separation apparatus according to the present invention comprises: a fractionation apparatus for fractionating liquefied natural gas; It is characterized by comprising heating means for taking out a gas, heating it and returning it to the fractionating apparatus, and methane separating means for taking out a vaporized gas from the upper part of the fractionating apparatus and separating it into a methane component and other gases. The liquefied natural gas separation device according to the present invention can further include a methane supply unit that supplies the methane component extracted from the methane separation unit to the power generation device.
【０００５】上記加熱手段は、海水により液化天然ガス
を加熱するようにした構成とすることができる。すなわ
ち、本加熱手段は、加熱装置であって、液化天然ガスと
海水等によって加熱された中間冷媒との間で熱交換を行
うための熱交換器を含む装置の他、加熱コイル内に液化
天然ガスを流し、この加熱コイルに直接海水等を適用す
るようにした装置を用いることができる。上記メタン分
離手段は、液化天然ガスを用いて熱交換するもの、例え
ば熱交換器であって、該熱交換後の部分的に気化した液
化天然ガスを前記分留装置へと供給するようにした構成
とすることができる。[0005] The heating means may be configured to heat the liquefied natural gas with seawater. That is, this heating means is a heating device, a device including a heat exchanger for performing heat exchange between liquefied natural gas and an intermediate refrigerant heated by seawater or the like, and liquefied natural gas in a heating coil. It is possible to use a device in which gas is flown and seawater or the like is directly applied to the heating coil. The methane separation means is one that performs heat exchange using liquefied natural gas, for example, a heat exchanger, and supplies the partially vaporized liquefied natural gas after the heat exchange to the fractionator. It can be configured.
【０００６】また、本発明は別の側面として液化天然ガ
スの分離方法であり、該分離方法は、液化天然ガスを分
留装置に送り、該分留装置下部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、分留装置から分留後のメタン成分
を取り出し、該メタン成分を後段の発電装置に送給する
ことを含む。また、本発明は、別の形態として発電方法
であり、液化天然ガスをメタン成分とその他のガスとに
分離し、該分離後のメタン成分を用いて発電を行うよう
にしたことを特徴とする。さらに、本発明は、さらに別
の形態として、液化天然ガスの使用方法であり、液化天
然ガスをメタン成分とその他のガスとに分離し、該その
他のガスを内燃機関用燃料として使用するようにしたこ
とを特徴とする。[0006] In another aspect of the present invention, there is provided a method for separating liquefied natural gas. In the method for separating liquefied natural gas, the liquefied natural gas is sent to a fractionator, and the liquefied natural gas is taken out from the lower part of the fractionator and heated. The heated liquefied natural gas is returned to the above-mentioned fractionator, thereby heating the liquefied natural gas in the fractionator to carry out a fractionation operation, taking out the fractionated methane component from the fractionator, and removing the methane component. Sending the components to a downstream power plant. Further, the present invention is, as another form, a power generation method, in which liquefied natural gas is separated into a methane component and another gas, and power is generated using the separated methane component. . Furthermore, the present invention, as still another form, is a method of using liquefied natural gas, which separates liquefied natural gas into a methane component and other gases, and uses the other gases as fuel for an internal combustion engine. It is characterized by having done.
【０００７】[0007]
【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。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.
【０００８】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。An outlet for extracting a part of the liquefied natural gas by the 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 temporarily stored in the surge tank 10
Liquefaction. The pump 11 is for returning the liquefied intermediate refrigerant to the heater 8 again. LP as the 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 in the lower part of the fractionation apparatus 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 general to use a gas-liquid contacting apparatus such as a distillation column provided with a shelf inside.
【０００９】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。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 the liquefied natural gas at about -162 ° C. This 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.
【００１０】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。That is, a part of the liquefied natural gas is taken out from the lower part of the fractionating apparatus 1 through its 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 supplied to the fractionating device 1
Is returned to the bottom. In this way, heat for the fractionation operation can be obtained.
【００１１】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。As described above, inside the heated fractionating apparatus 1, 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. Boiling point-
The methane component at 162 ° C.
It is taken out at a temperature of 20 ° C. and cooled in the heat exchanger 4 by liquefied natural gas before fractionation to about −140 ° C. Thereby, 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 of the fractionation apparatus 1 as a liquid at a position 12 at a temperature lower than its boiling point of -85 ° C. A component having a carbon number equal to or greater 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 of FIG. 1, in the present invention, the heat source, the heat obtained in the apparatus for the cold heat and the heat source existing in the natural world are used. I can do it.
【００１２】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。In the power generation method according to the present invention, liquefied natural gas is separated into a methane component and other gases 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 generation is 191 and 290 kcal / kg ·
mol · CO 2 . The ratio of the amount of CO 2 emission to pure methane itself is the inverse ratio calculated from these figures, so that the standard liquefied natural gas produced in Indonesia will increase the amount of CO 2 emission by about 1.2% relative 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.
【００１３】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。Further, according to the method of using liquefied natural gas according to the present invention, as described in 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 a much higher caloric value per unit gas volume than the methane component, and if the vehicle has a fuel tank of the same capacity,
One filling will allow you to travel a long distance. 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.
【００１４】[0014]
【表１】 [Table 1]
【００１５】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。[0015] 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.
【００１６】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。As shown in FIG. 1, a liquefied natural gas heating apparatus 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 in which liquefied natural gas flows in the heating coil 20 and seawater is directly applied to the heating coil 20 can also be used.
In FIG. 2, elements having the same functions as those in FIG.
【００１７】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。In the above description, the methane component,
The term "component" as in the case of the ethane component is intended not only for the intended component itself such as methane and ethane, but also for the presence of other components (a little amount). That is,
In the middle of the process, for example, methane may be contained even if methane is intended, and even in the final product, a pure product is ideal in nature, but inevitably impurities may actually exist. Because.
【００１８】[0018]
【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。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 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。FIG. 1 is a conceptual diagram illustrating an embodiment of a liquefied natural gas separation device according to the present invention.
【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。FIG. 2 is a conceptual diagram illustrating another embodiment of the liquefied natural gas separation device according to the present invention.
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 DESCRIPTION OF SYMBOLS 1 Fractionation apparatus 2 Storage tank 3 Feeding pump 4 Heat exchanger 5 Separation tank 6 Pump 7 Pump 8 Heater 9 Heater 10 Surge tank 11 Pump 20 Heating coil
Claims (7)
分留装置の下部から液化天然ガスを取り出して加熱した
後に前記分留装置へ返送する加熱手段と、上記分留装置
上部から気化したガスを取り出しメタン成分とその他の
ガスに分離するメタン分離手段とからなることを特徴と
する液化天然ガスの分離装置。1. A fractionating device for fractionating liquefied natural gas, heating means for extracting and heating liquefied natural gas from a lower portion of the fractionating device, and then returning the gas to the fractionating device; An apparatus for separating liquefied natural gas, comprising: methane separation means for extracting a vaporized gas and separating it into a methane component and other gases.
分留装置の下部から液化天然ガスを取り出して加熱した
後に前記分留装置へ返送する加熱手段と、上記分留装置
上部から気化したガスを取り出しメタン成分とその他の
ガスに分離するメタン分離手段と、該メタン分離手段か
ら取り出したメタン成分を発電装置に送給するメタン送
給手段とからなることを特徴とする液化天然ガスの分離
装置。2. A fractionating device for fractionating liquefied natural gas, heating means for extracting liquefied natural gas from a lower portion of the fractionating device, heating the liquefied natural gas, and then returning the gas to the fractionating device; A liquefied natural gas comprising methane separation means for taking out a vaporized gas and separating it into methane components and other gases, and methane feed means for sending the methane components taken out from the methane separation means to a power generator. Separation equipment.
を加熱することを特徴とする請求項1又は2に記載の液化
天然ガスの分離装置。3. The liquefied natural gas separation apparatus according to claim 1, wherein the heating means heats the liquefied natural gas with seawater.
いて熱交換するものであって、該熱交換後の部分的に気
化した液化天然ガスを前記分留装置へと供給することを
特徴とする請求項1〜3のいずれかに記載の液化天然ガス
の分離装置。4. The methane separation means for performing heat exchange using liquefied natural gas, and supplying partially vaporized liquefied natural gas after the heat exchange to the fractionation apparatus. The liquefied natural gas separation apparatus according to any one of claims 1 to 3.
装置下部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、
分留装置から分留後のメタン成分を取り出し、該メタン
成分を後段の発電装置に送給することを含むことを特徴
とする液化天然ガスの分離方法。5. The liquefied natural gas is sent to a fractionating apparatus, the liquefied natural gas is taken out from the lower part of the fractionating apparatus and heated, and the heated liquefied natural gas is returned to the fractionating apparatus. Liquefied natural gas is heated and fractionated,
A method for separating liquefied natural gas, comprising taking out a fractionated methane component from a fractionation device and feeding the methane component to a power generation device at a subsequent stage.
スとに分離し、該分離後のメタン成分を用いて発電を行
うようにしたことを特徴とする発電方法。6. A power generation method, wherein a liquefied natural gas is separated into a methane component and another gas, and power is generated using the separated methane component.
スとに分離し、該その他のガスを内燃機関用燃料として
使用するようにしたことを特徴とする液化天然ガスの使
用方法。7. A method for using liquefied natural gas, comprising separating liquefied natural gas into a methane component and other gases, and using the other gases as fuel for an internal combustion engine.
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|---|---|---|---|
| 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 |
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| 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 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002115564A (en) * | 2000-10-04 | 2002-04-19 | Osaka Gas Co Ltd | Power generating method using fractional distillation equipment |
| JP2003028398A (en) * | 2001-07-17 | 2003-01-29 | Tokyo Gas Co Ltd | Town gas supplying method and device |
| JP2008069350A (en) * | 2006-09-11 | 2008-03-27 | Cryogenic Group Inc | Method and system for producing dividable plural products from supplied or imported lng |
| JP2008513726A (en) * | 2004-09-22 | 2008-05-01 | フルオー・テクノロジーズ・コーポレイシヨン | Configuration and method of LPG and cogeneration |
| JP2008513550A (en) * | 2004-09-14 | 2008-05-01 | エクソンモービル アップストリーム リサーチ カンパニー | Method for extracting ethane from liquefied natural gas |
| JP2010032087A (en) * | 2008-07-28 | 2010-02-12 | Ihi Corp | Separation device and separation method of liquefied natural gas |
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1998
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002115564A (en) * | 2000-10-04 | 2002-04-19 | Osaka Gas Co Ltd | Power generating method using fractional distillation equipment |
| 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 |
| JP2003028398A (en) * | 2001-07-17 | 2003-01-29 | Tokyo Gas Co Ltd | Town gas supplying method and device |
| JP4489326B2 (en) * | 2001-07-17 | 2010-06-23 | 東京瓦斯株式会社 | City gas supply method and apparatus |
| JP2008513550A (en) * | 2004-09-14 | 2008-05-01 | エクソンモービル アップストリーム リサーチ カンパニー | Method for extracting ethane from liquefied natural gas |
| JP2008513726A (en) * | 2004-09-22 | 2008-05-01 | フルオー・テクノロジーズ・コーポレイシヨン | Configuration and method of LPG and cogeneration |
| JP4901740B2 (en) * | 2004-09-22 | 2012-03-21 | フルオー・テクノロジーズ・コーポレイシヨン | Configuration and method of LPG and cogeneration |
| JP2008069350A (en) * | 2006-09-11 | 2008-03-27 | Cryogenic Group Inc | Method and system for producing dividable plural products from supplied or imported lng |
| KR101430273B1 (en) * | 2008-01-12 | 2014-08-14 | 만 디젤 앤 터보 에스이 | Method and apparatus for processing natural gas for use in gas engine |
| JP2010032087A (en) * | 2008-07-28 | 2010-02-12 | Ihi Corp | Separation device and separation method of liquefied natural gas |
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