JP4737955B2 - Natural gas dilution calorie adjustment method and apparatus - Google Patents

Natural gas dilution calorie adjustment method and apparatus Download PDF

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JP4737955B2
JP4737955B2 JP2004227442A JP2004227442A JP4737955B2 JP 4737955 B2 JP4737955 B2 JP 4737955B2 JP 2004227442 A JP2004227442 A JP 2004227442A JP 2004227442 A JP2004227442 A JP 2004227442A JP 4737955 B2 JP4737955 B2 JP 4737955B2
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bog
lng
calorific value
natural gas
calorimeter
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JP2006045327A (en
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隆廣 木村
晋 川村
学 菅原
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Kansai Electric Power Co Inc
JFE Engineering Corp
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    • 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
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
    • F25J1/0255—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature controlling the composition of the feed or liquefied gas, e.g. to achieve a particular heating value of 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons

Description

本発明は、液化天然ガス（以下、ＬＮＧという。）を原料とする天然ガスの熱量をＬＮＧの蒸発ガスであるＢＯＧ（ボイルオフガス）により目標とする熱量に希釈調整する技術に関するものである。   The present invention relates to a technique for diluting and adjusting the amount of heat of natural gas using liquefied natural gas (hereinafter referred to as LNG) to a target amount of heat with BOG (boil-off gas) which is an LNG evaporation gas.

天然ガスを需要家に供給するには、原料となるＬＮＧを貯槽に貯蔵して、必要量をポンプで払い出し、気化器にて気化させた後、規定熱量に調整をして払い出す。
規定熱量に調整する方法としては、一般にＬＮＧは規定熱量より低いため、増熱用のＬＰＧ等を添加することで増熱調整処理が行われている。
ところが、ＬＮＧ貯槽内でＬＮＧを長期貯蔵することで、ＬＮＧ中の軽質分であるメタン等が蒸発してしまい、結果としてＬＮＧの単位体積当たりの熱量が上昇して、規定熱量以上になる場合には希釈の必要が生じる。もちろん、最初から受入ＬＮＧの熱量が高い場合にも希釈の必要が生じる。
希釈熱量調整の従来方法としては、エアーダイリュウション（天然ガス製造の１方法で気化LPGに空気を混入させる）による方法がある。ただし、高圧ガス保安法で可燃性ガスへの４％以上の酸素の混入は認められていないので、エアーダイリュウションは、天然ガスの圧力が１MPa以上のときには、空気混入量の厳密な管理が必要となる。
また、他の希釈熱量調整方法としては、ＬＮＧを気化した後の天然ガスにＬＮＧタンク内で発生したＬＮＧのＢＯＧを圧縮して混合するという方法が知られている（特許文献１参照）
特開平９−１５７６６８号公報 In order to supply natural gas to consumers, LNG, which is a raw material, is stored in a storage tank, a required amount is discharged by a pump, vaporized by a vaporizer, adjusted to a specified heat amount, and then discharged.
As a method for adjusting to the specified heat amount, since LNG is generally lower than the specified heat amount, the heat increase adjusting process is performed by adding LPG or the like for heat increase.
However, when LNG is stored for a long time in the LNG storage tank, methane, which is a light component in LNG, evaporates, and as a result, the amount of heat per unit volume of LNG rises and exceeds the specified amount of heat. Need to be diluted. Of course, it is necessary to dilute even when the heat quantity of the received LNG is high from the beginning.
As a conventional method for adjusting the amount of dilution heat, there is a method by air dilution (mixing air into vaporized LPG by one method of natural gas production). However, since the high-pressure gas safety law does not allow more than 4% oxygen to be mixed into the combustible gas, the air dilution is strictly controlled when the natural gas pressure is 1 MPa or higher. Necessary.
As another method for adjusting the amount of heat of dilution, a method is known in which LNG BOG generated in the LNG tank is compressed and mixed with natural gas after LNG is vaporized (see Patent Document 1).
JP-A-9-157668

上記特許文献１に記載された方法は、ＬＮＧを気化した天然ガスにＢＯＧもしくは空気を混合することにより、熱量調整を行うというものである。このような方法では、ＢＯＧもしくは空気を圧縮機により気化後の天然ガスよりも高い圧力にして吹き込む必要がある。ところが、気化後の天然ガスはＬＮＧの段階で液体ポンプによって高圧に昇圧されているため、ＢＯＧもしくは空気を圧縮する圧縮機はガス体をこのような高圧にする能力のものが要求される。しかし、ガス体を高圧に圧縮するためには大規模なガス圧縮機が必要となり、設備費及び設備運転費が非常にかさむという問題がある。   The method described in Patent Document 1 adjusts the amount of heat by mixing BOG or air with natural gas obtained by vaporizing LNG. In such a method, it is necessary to blow BOG or air at a pressure higher than that of natural gas after being vaporized by a compressor. However, since the natural gas after vaporization is pressurized to a high pressure by a liquid pump at the LNG stage, a compressor that compresses BOG or air is required to have a gas body having such a high pressure. However, in order to compress the gas body to a high pressure, a large-scale gas compressor is required, and there is a problem that equipment costs and equipment operation costs are very high.

本発明は、上記の問題点を解決するためになされたものであり、小規模で運転費も少なくて済む天然ガスの希釈熱量調整方法及び装置を得ることを目的としている。   The present invention has been made to solve the above-described problems, and an object of the present invention is to obtain a natural gas dilution calorie adjustment method and apparatus which are small in scale and require less operating costs.

（１）本発明の一つの形態に係る天然ガスの希釈熱量調整方法は、払い出しラインを流れる気化前のＬＮＧをＢＯＧで希釈して天然ガスの熱量を目標熱量に調整する方法であって、前記ＢＯＧを再液化すると共に再液化したＢＯＧの熱量を測定し、かつ前記気化前のＬＮＧの熱量と流量を測定し、これらの測定結果に基づいて、再液化したＢＯＧを前記気化前のＬＮＧに添加して希釈調整することを特徴とするものである。
払い出しラインにおいて複数のＬＮＧポンプによって気化前のＬＮＧを昇圧する場合には、低圧側のＬＮＧに再液化したＢＯＧを添加するようにすれば、再液化ＢＯＧの昇圧が小さくて済み、より小規模な装置でよいのでより好ましい。 (1) A natural gas dilution calorie adjustment method according to one aspect of the present invention is a method of adjusting the calorific value of natural gas to a target calorie by diluting LNG before vaporization flowing through a payout line with BOG, Re-liquefy BOG, measure the calorific value of the re-liquefied BOG, measure the calorific value and flow rate of the LNG before vaporization, and add the re-liquefied BOG to the LNG before vaporization based on these measurement results And adjusting the dilution.
When boosting the LNG before vaporization by a plurality of LNG pumps in the payout line, if the re-liquefied BOG is added to the low-pressure LNG, the re-liquefied BOG can be boosted in a smaller scale, and the scale is smaller. Since an apparatus is sufficient, it is more preferable.

（２）また、本発明の他の形態に係る天然ガスの希釈熱量調整方法は、払い出しラインを流れる気化前のＬＮＧをＢＯＧで希釈して天然ガスの熱量を目標熱量に調整する方法であって、気化前のＬＮＧの熱量と流量及びと前記ＢＯＧの熱量を測定し、これらの測定結果に基づいて、ガス状態のＢＯＧを前記気化前のＬＮＧに吹き込んで希釈調整することを特徴とするものである。 (2) In addition, the natural gas dilution calorie adjustment method according to another aspect of the present invention is a method for adjusting the calorific value of natural gas to a target calorie by diluting LNG before vaporization flowing through a payout line with BOG. The heat quantity and flow rate of the LNG before vaporization and the heat quantity of the BOG are measured, and based on these measurement results, the BOG in the gas state is blown into the LNG before vaporization to adjust the dilution. is there.

（３）また、本発明に係る天然ガスの希釈熱量調整装置は、払い出しラインを流れる気化前のＬＮＧをＢＯＧで希釈して天然ガスの熱量を目標熱量に調整する天然ガスの希釈熱量調整装置であって、ＢＯＧを再液化する再液化装置と、再液化されたＢＯＧの圧力を希釈対象のＬＮＧ圧力以上に昇圧する昇圧ポンプと、気化前のＬＮＧの熱量を測定する第１熱量測定装置と、気化前のＬＮＧの流量を測定する第１流量測定装置と、前記再液化されたＢＯＧの熱量を測定する第２熱量測定装置と、該第２熱量測定装置と前記第１熱量測定装置及び前記第１流量測定装置の測定結果に基づいて天然ガスの熱量を目標熱量にするためのＢＯＧ添加量を演算し、該演算結果に基づいて前記再液化されたＢＯＧの添加量を制御する熱量制御装置と、を備えたことを特徴とする。 (3) The natural gas dilution calorie adjusting device according to the present invention is a natural gas diluting calorie adjusting device that dilutes LNG before vaporization flowing through the payout line with BOG to adjust the natural gas calorie to the target calorie. A reliquefaction device for reliquefying BOG, a booster pump for increasing the pressure of the reliquefied BOG to be equal to or higher than the LNG pressure to be diluted, a first calorimeter for measuring the calorific value of LNG before vaporization, A first flow rate measuring device for measuring a flow rate of LNG before vaporization; a second calorimetric device for measuring a calorific value of the re-liquefied BOG; the second caloric measuring device; the first calorie measuring device ; A calorific value control device for calculating a BOG addition amount for making the calorific value of natural gas a target calorific value based on a measurement result of one flow rate measuring device , and controlling the addition amount of the re-liquefied BOG based on the calculation result; With It is characterized in.

（４）また、払い出しラインを流れる気化前のＬＮＧをＢＯＧで希釈して天然ガスの熱量を目標熱量に調整する天然ガスの希釈熱量調整装置であって、ガス状態のＢＯＧ圧力を希釈対象のＬＮＧ圧力以上に昇圧するＢＯＧ圧縮機と、気化前のＬＮＧの熱量を測定する第１熱量測定装置と、気化前のＬＮＧの流量を測定する第１流量測定装置と、前記ＢＯＧの熱量を測定する第２熱量測定装置と、該第２熱量測定装置と前記第１熱量測定装置及び前記第１流量測定装置の測定結果に基づいて天然ガスの熱量を目標熱量にするためのＢＯＧ添加量を演算し、該演算結果に基づいて前記ＢＯＧの添加量を制御する熱量制御装置と、払い出しラインを流れる気化前のＬＮＧにガス状態のＢＯＧを混合させるための凝縮混合器と、を備えたことを特徴とするものである。
(4) A natural gas dilution calorific value adjustment device for adjusting the calorific value of natural gas to a target calorific value by diluting LNG before vaporization flowing through the payout line with BOG, wherein the BOG pressure in the gas state is the LNG to be diluted. A BOG compressor that boosts the pressure above the pressure, a first calorimeter that measures the amount of heat of LNG before vaporization, a first flow rate measurement device that measures the flow of LNG before vaporization, and a first unit that measures the amount of heat of BOG. 2 calorie measuring device, calculating the BOG addition amount for making the calorific value of natural gas the target calorie based on the measurement results of the second caloric measuring device, the first caloric measuring device and the first flow rate measuring device , A calorific value control device that controls the amount of BOG added based on the calculation result, and a condensing mixer for mixing BOG in a gas state with LNG before flowing through the discharge line. Is shall.

（５）また、上記（３）又は（４）に記載のものにおいて、ＬＮＧとＢＯＧを混合した混合液体の熱量を測定する第３熱量測定装置を有し、熱量制御装置は該第３熱量測定装置の測定結果に基づいてＢＯＧの混合流量を調整することを特徴とするものである。 (5) Further, in the above (3) or (4), the apparatus has a third calorimeter that measures the calorie of the mixed liquid in which LNG and BOG are mixed, and the calorie controller controls the third calorimeter. The mixed flow rate of BOG is adjusted based on the measurement result of the apparatus.

本発明においては、気化前のＬＮＧの熱量を測定し、その測定結果に基づいて、再液化したＢＯＧを前記気化前のＬＮＧに添加して希釈調整するようにしたので、気化前のＬＮＧに添加するために液状態のＢＯＧを昇圧するので、ＢＯＧ昇圧のための装置が小規模なものでよく、設備費、運転費の低減効果がある。   In the present invention, the calorific value of LNG before vaporization is measured, and based on the measurement result, the reliquefied BOG is added to the LNG before vaporization to adjust the dilution, so it is added to the LNG before vaporization. In order to increase the pressure of the BOG in the liquid state, the apparatus for boosting the BOG may be small-scale, and there is an effect of reducing the equipment cost and the operating cost.

［実施の形態１］
図１は本発明の一実施の形態に係る天然ガスの希釈熱量調整装置の全体構成の説明図である。
本実施の形態の天然ガスの希釈熱量調整装置は、（１）ＬＮＧ貯槽１に貯留されたＬＮＧを払い出すラインと、（２）ＬＮＧ貯槽１で発生したＢＯＧを再液化してＬＮＧ貯槽に戻すと共に払い出しラインのＬＮＧに添加するＢＯＧラインと、（３）該ＢＯＧラインにおける再液化ＢＯＧの添加量を調整して所定の熱量になるように調整するための熱量制御装置、の大きく３つの構成からなる。以下、各構成を説明する。 [Embodiment 1]
FIG. 1 is an explanatory diagram of the overall configuration of a natural gas dilution heat amount adjusting apparatus according to an embodiment of the present invention.
The natural gas dilution calorie adjusting device according to the present embodiment includes (1) a line for discharging LNG stored in the LNG storage tank 1, and (2) BOG generated in the LNG storage tank 1 is reliquefied and returned to the LNG storage tank. And a BOG line to be added to the LNG of the payout line, and (3) a heat quantity control device for adjusting the addition amount of the reliquefied BOG in the BOG line so as to obtain a predetermined heat quantity. Become. Each configuration will be described below.

（１）ＬＮＧ払い出しライン
ＬＮＧ払い出しライン３は、その一端側がＬＮＧ貯槽１に接続され、他端にはＬＮＧを気化する気化装置５が設けられている。また、ＬＮＧ払い出しライン３にはラインを流れるＬＮＧの圧力を例えば０．８ＭＰａ〜１ＭＰａの範囲に昇圧する第１ＬＮＧポンプ７と、第１ＬＮＧポンプ７の下流側に設けられて第１ＬＮＧポンプ７で昇圧された圧力をさらに高圧（例えば３ＭＰａ〜６ＭＰａ）に昇圧する第２ＬＮＧポンプ９が設けられている。
また、第１ＬＮＧポンプ７と第２ＬＮＧポンプ９の間にはＬＮＧと後述の再液化ＢＯＧを混合する混合器１１が設けられている。
さらに、第１ＬＮＧポンプ７と混合器１１の間にはラインを流れるＬＮＧの熱量を計測する第１熱量計１３と、ＬＮＧの流量を計測する第１流量計１５が設けられている。
また、混合器１１と第２ＬＮＧポンプ９の間にはＬＮＧに再液化ＢＯＧを混合して希釈した混合流体の熱量を計測する第２熱量計１７が設けられている。 (1) LNG payout line One end of the LNG payout line 3 is connected to the LNG storage tank 1, and a vaporizer 5 for vaporizing LNG is provided at the other end. The LNG payout line 3 is provided with a first LNG pump 7 for increasing the pressure of the LNG flowing through the line to a range of, for example, 0.8 MPa to 1 MPa, and downstream of the first LNG pump 7 and is increased by the first LNG pump 7. A second LNG pump 9 for increasing the pressure further increased to a higher pressure (for example, 3 MPa to 6 MPa) is provided.
A mixer 11 is provided between the first LNG pump 7 and the second LNG pump 9 to mix LNG and a reliquefied BOG described later.
Further, a first calorimeter 13 for measuring the amount of heat of LNG flowing through the line and a first flow meter 15 for measuring the flow rate of LNG are provided between the first LNG pump 7 and the mixer 11.
A second calorimeter 17 is provided between the mixer 11 and the second LNG pump 9 to measure the amount of heat of the mixed fluid diluted by mixing the liquefied BOG with LNG.

（２）ＢＯＧライン
ＢＯＧラインは、ＬＮＧ貯槽１もしくは、他のＬＮＧ貯槽で発生したガス状態のＢＯＧを後述の再液化器２９に導入するためのガス状態ＢＯＧライン１９と、再液化されたＢＯＧをＬＮＧ貯槽１に戻すＢＯＧ戻しライン２１と、ＢＯＧ戻しライン２１の途中で分岐して再液化されたＢＯＧをＬＮＧ払い出しライン３に添加して熱量調製するためのＢＯＧ熱調用ライン２３と、から構成されている。
ガス状態ＢＯＧライン１９には、サクションドラム２５、サクションドラム２５の下流側にあってガス状態のＢＯＧを所定の圧力に昇圧するＢＯＧ圧縮機２７が設けられ、ＢＯＧ圧縮機２７の下流側に再液化器２９が設けられている。ＢＯＧ圧縮機２７はガス状態のＢＯＧを所定の圧力に昇圧するものであるが、このＢＯＧ圧縮機２７で昇圧する圧力は再液化のための昇圧であり、例えば０．８Ｍｐａ程度であり、ＢＯＧ圧縮機２７は小規模のもので足り、設備費、動力費を低く抑えることができる。
再液化器２９はＬＮＧ払い出しライン３のＬＮＧを導入してガス状態のＢＯＧと熱交換することによって、ガス状態のＢＯＧを冷却して再液化する。 (2) BOG line The BOG line includes a gas state BOG line 19 for introducing a gas state BOG generated in the LNG storage tank 1 or another LNG storage tank into a reliquefier 29 described later, and a reliquefied BOG. A BOG return line 21 for returning to the LNG storage tank 1 and a BOG heat adjustment line 23 for adjusting the calorific value by adding the BOG branched and reliquefied in the middle of the BOG return line 21 to the LNG discharge line 3. ing.
The gas state BOG line 19 is provided with a suction drum 25, a BOG compressor 27 that is downstream of the suction drum 25 and increases the gas state BOG to a predetermined pressure, and is reliquefied downstream of the BOG compressor 27. A container 29 is provided. The BOG compressor 27 boosts the BOG in a gas state to a predetermined pressure. The pressure boosted by the BOG compressor 27 is a boost for re-liquefaction, for example, about 0.8 Mpa. The machine 27 may be a small one, and the equipment cost and power cost can be kept low.
The reliquefier 29 cools and reliquefies the gaseous BOG by introducing the LNG from the LNG payout line 3 and exchanging heat with the gaseous BOG.

ＢＯＧ戻しライン２１には、再液化器２９で再液化された液状態のＢＯＧを貯留するための受液槽３１と、受液槽３１の下流側にあって液状態のＢＯＧをＬＮＧ払い出しライン３における第１ＬＮＧポンプ７の下流側圧力以上に昇圧するための液体ポンプ３３と、再液化されたＢＯＧの流量を計測する第２流量計３５と、ＢＯＧ戻しライン２１を流れる再液化ＢＯＧの流量を調整する流量調整弁３６が設けられている。
ＢＯＧ熱調用ライン２３には、ＢＯＧ熱調用ライン２３を流れる再液化ＢＯＧの流量、熱量をそれぞれ計測する第３流量計３７と第３熱量計３９が設けられ、また、ＢＯＧ熱調用ライン２３を流れる再液化ＢＯＧの流量を調整するための流量調整弁４１が設けられている。 The BOG return line 21 includes a liquid receiving tank 31 for storing the liquid BOG reliquefied by the reliquefier 29, and a liquid BOG located downstream of the liquid receiving tank 31 in the LNG discharge line 3. The liquid pump 33 for increasing the pressure to the pressure at the downstream side of the first LNG pump 7 or higher, the second flow meter 35 for measuring the flow rate of the re-liquefied BOG, and the flow rate of the re-liquefied BOG flowing through the BOG return line 21 are adjusted. A flow rate adjusting valve 36 is provided.
The BOG heat adjustment line 23 is provided with a third flow meter 37 and a third calorimeter 39 for measuring the flow rate and heat quantity of the reliquefied BOG flowing through the BOG heat adjustment line 23, and also flows through the BOG heat adjustment line 23. A flow rate adjustment valve 41 for adjusting the flow rate of the reliquefied BOG is provided.

なお、ＬＮＧ払い出しラインやＢＯＧラインに設けた第１〜第３熱量計１３、１７、３９は、ＬＮＧの熱量を液体状態のままで測定できるものが好ましいが、ＬＮＧやＢＯＧを一旦気化して気体状態で測定するものでもよい。   The first to third calorimeters 13, 17, and 39 provided in the LNG payout line and the BOG line are preferably those that can measure the amount of heat of LNG while in a liquid state, but once LNG or BOG is vaporized to gas You may measure in a state.

（３）熱量制御装置
熱量制御装置４３は、ＬＮＧ払い出しラインに設置された第１熱量計１３及び第１流量計１５の計測値、及びＢＯＧ熱調用ライン２３の第３熱量計３９の計測値を入力して、予め設定された目標熱量になるための再液化ＢＯＧの希釈量を演算する。そして、該演算値に基づいて第３流量計３７の信号を検知しつつ流量調整弁４１の開度を調整する。
さらに、熱量制御装置４３は、ＬＮＧ払い出しライン３における混合器１１の下流側に設けられた第２熱量計１７の計測値に基づくフィードバック制御により希釈量をさらに微調整して目標値になるように熱量制御を行う。
以上のように構成された本実施の形態の動作を以下に説明する。 (3) Calorific value control device The calorific value control device 43 uses the measured value of the first calorimeter 13 and the first flow meter 15 installed in the LNG payout line, and the measured value of the third calorimeter 39 of the BOG heat adjustment line 23. Input and calculate the dilution amount of the reliquefied BOG to reach a preset target heat amount. Then, the opening degree of the flow rate adjustment valve 41 is adjusted while detecting the signal of the third flow meter 37 based on the calculated value.
Furthermore, the calorific value control device 43 further finely adjusts the dilution amount by feedback control based on the measurement value of the second calorimeter 17 provided on the downstream side of the mixer 11 in the LNG payout line 3 so as to become the target value. Control the amount of heat.
The operation of the present embodiment configured as described above will be described below.

＜動作説明＞
図１において、ＬＮＧ貯槽１から払い出されたＬＮＧは、第１ＬＮＧポンプ７で所定圧力（例えば０．８ＭＰａ〜１ＭＰａ）に昇圧され、さらに、第２ＬＮＧポンプ９でより高圧（例えば３〜６ＭＰａ）に昇圧され、その後、気化装置５にて気化される。
一方、ＬＮＧ貯槽１もしくは他のＬＮＧ貯槽から取り出されたＢＯＧは、ＢＯＧ圧縮機２７で所定圧力（０．８ＭＰａ〜１ＭＰａ）に圧縮昇圧された後、再液化器２９で再液化される。再液化されたＢＯＧはＢＯＧ熱調用ライン２３を通ってＬＮＧ払い出しライン３に供給され、混合器１１においてＬＮＧ払い出しライン３を流れるＬＮＧに混合されることによって、ＬＮＧの熱量を希釈調整する。 <Description of operation>
In FIG. 1, the LNG discharged from the LNG storage tank 1 is increased to a predetermined pressure (for example, 0.8 MPa to 1 MPa) by the first LNG pump 7 and further increased to a higher pressure (for example, 3 to 6 MPa) by the second LNG pump 9. The pressure is increased and then vaporized by the vaporizer 5.
On the other hand, the BOG taken out from the LNG storage tank 1 or another LNG storage tank is compressed to a predetermined pressure (0.8 MPa to 1 MPa) by the BOG compressor 27 and then reliquefied by the reliquefier 29. The reliquefied BOG is supplied to the LNG discharge line 3 through the BOG heat adjustment line 23 and is mixed with the LNG flowing through the LNG discharge line 3 in the mixer 11, thereby diluting and adjusting the amount of heat of LNG.

その際に、熱量制御装置４３は、ＬＮＧ貯槽１から払い出されたＬＮＧの熱量と流量をそれぞれ第１熱量計１３と第１流量計１５から入力するとともに、再液化されたＢＯＧの熱量を第３熱量計３９から入力し、その入力値に基づいてＬＮＧ払い出しライン３を流れるＬＮＧの熱量が目標熱量になるように、ＢＯＧの混合量を演算する。そして、演算された混合量になるように流量調整弁４１の開度を第３流量計３７の計測値に基づいて調整する。なお、熱量制御装置４３は、混合器１１の下流側を流れる混合流体の熱量を第２熱量計１７で計測してフィードバック制御により混合量の再調整を行うことも可能である。   At that time, the heat quantity control device 43 inputs the heat quantity and flow rate of the LNG discharged from the LNG storage tank 1 from the first calorimeter 13 and the first flow meter 15, respectively, and the heat quantity of the re-liquefied BOG as the first heat quantity. Based on the input value, the mixing amount of BOG is calculated so that the heat amount of LNG flowing through the LNG payout line 3 becomes the target heat amount. Then, the opening degree of the flow rate adjustment valve 41 is adjusted based on the measured value of the third flow meter 37 so that the calculated mixing amount is obtained. The calorific value control device 43 can also measure the calorific value of the mixed fluid flowing downstream of the mixer 11 with the second calorimeter 17 and readjust the mixing amount by feedback control.

以上のように、本実施の形態においては、低圧状態（例えば０．８ＭＰａ〜１ＭＰａ）である気化前のＬＮＧに再液化されたＢＯＧを添加して熱量調整を行うようにしたので、ＢＯＧの圧力も低圧でよく、ＢＯＧの圧縮昇圧に用いる圧縮機が小規模なもので済み、設備費、動力費が低減できる。しかも、ＢＯＧの昇圧を、ＢＯＧを再液化した後、液体ポンプ３３で行うようにしたので、従来例のようにガス状態のＢＯＧを添加に必用な圧力まで昇圧するガス圧縮機に比べると極めて小規模で足り、設備費、動力費が大幅に低減できる。もちろん再液化されたＢＯＧの圧力が、ＬＮＧへの添加圧力より高い場合は、液体ポンプ３３は不要である。   As described above, in the present embodiment, the amount of heat is adjusted by adding the re-liquefied BOG to the LNG before vaporization in a low pressure state (for example, 0.8 MPa to 1 MPa). However, the pressure used for the compression boosting of the BOG can be small, and the equipment cost and power cost can be reduced. In addition, since the boosting of the BOG is performed by the liquid pump 33 after the BOG is re-liquefied, it is extremely small compared to the gas compressor that boosts the BOG in a gas state to a pressure necessary for addition as in the conventional example. The scale is sufficient and the equipment and power costs can be greatly reduced. Of course, when the pressure of the re-liquefied BOG is higher than the addition pressure to LNG, the liquid pump 33 is unnecessary.

[実施の形態２]
図２は本発明の他の実施の形態の説明図であり、実施の形態１を示した図１と同一部分又は相当する部分には同一の符号を付してある。
実施の形態１においては、ＬＮＧ払い出しライン３において２台のＬＮＧポンプを用いた例を示した。これに対して、本実施の形態においては、小規模基地の場合のようにＬＮＧ払い出しライン３において１台のＬＮＧポンプを用いて、０．１ＭＰａ〜３ＭＰａの範囲に昇圧した後、気化装置５で気化させる場合である。
本実施の形態においては、ＬＮＧ払い出しライン側では、ＬＮＧポンプ７によって所定の圧力（例えば、０．８Ｍｐａ）に昇圧する。
他方、ＢＯＧライン側では、ガス状態のＢＯＧをＢＯＧ圧縮機２７で再液化に必用な所定の圧力（例えば、０．５ＭＰａ）に昇圧し、再液化器２９で再液化した後、液体ポンプ３３によって再液化ＢＯＧをＬＮＧ払い出しライン３に添加するのに必要な所定圧力（例えば、０．８ＭＰａ以上）に昇圧する。 [Embodiment 2]
FIG. 2 is an explanatory diagram of another embodiment of the present invention, and the same or corresponding parts as those in FIG. 1 showing the first embodiment are denoted by the same reference numerals.
In the first embodiment, an example in which two LNG pumps are used in the LNG payout line 3 is shown. On the other hand, in the present embodiment, the pressure is increased to a range of 0.1 MPa to 3 MPa using one LNG pump in the LNG payout line 3 as in the case of a small base, and then the vaporizer 5 This is the case when vaporizing.
In the present embodiment, on the LNG payout line side, the pressure is increased to a predetermined pressure (for example, 0.8 Mpa) by the LNG pump 7.
On the other hand, on the BOG line side, the BOG in a gas state is increased to a predetermined pressure (for example, 0.5 MPa) necessary for reliquefaction by the BOG compressor 27, reliquefied by the reliquefaction device 29, and then discharged by the liquid pump 33. The pressure is increased to a predetermined pressure (for example, 0.8 MPa or more) necessary for adding the reliquefied BOG to the LNG discharge line 3.

このように、本実施の形態のように１台のＬＮＧポンプ７でＬＮＧを払い出し圧力まで昇圧する場合であっても、ガス状態のＢＯＧをＢＯＧ圧縮機２７で圧縮して昇圧するのは液化に必要な程度の圧力（例えば、０．５ＭＰａ）であり、ガス状態のＢＯＧを圧縮するためのＢＯＧ圧縮機２７は小規模のもので足り、設備費、動力費を低減することができる。   As described above, even when LNG is raised to the discharge pressure by one LNG pump 7 as in the present embodiment, it is liquefied that the BOG in the gas state is compressed by the BOG compressor 27 to increase the pressure. The required pressure (for example, 0.5 MPa) is sufficient for the BOG compressor 27 for compressing the BOG in the gas state, and equipment costs and power costs can be reduced.

[実施の形態３]
図３は本発明の他の実施の形態の説明図であり、実施の形態１を示した図１と同一部分又は相当する部分には同一の符号を付してある。
実施の形態１においては、希釈用のＢＯＧをＢＯＧラインに設けた再液化器２９によって再液化し、該再液化ＢＯＧをＬＮＧ払い出しライン３に添加する例を示した。
これに対して、本実施の形態においては、ＢＯＧラインに再液化器２９を設けることなく、ガス状態のまま凝縮混合器４５に送り、第１ＬＮＧポンプ７によって所定圧力に昇圧されたＬＮＧに吹き込むようにしたものである。この場合、ガス状態のＢＯＧがＬＮＧの冷熱で再液化し、ＬＮＧに混合されることになる。 [Embodiment 3]
FIG. 3 is an explanatory diagram of another embodiment of the present invention, in which the same or corresponding parts as those in FIG. 1 showing the first embodiment are denoted by the same reference numerals.
In the first embodiment, an example has been shown in which the BOG for dilution is reliquefied by the reliquefier 29 provided in the BOG line, and the reliquefied BOG is added to the LNG discharge line 3.
On the other hand, in the present embodiment, the re-liquefier 29 is not provided in the BOG line, but it is sent to the condensing mixer 45 in the gas state and blown into the LNG that has been pressurized to a predetermined pressure by the first LNG pump 7. It is a thing. In this case, the BOG in the gas state is reliquefied by the cold heat of LNG and mixed with LNG.

本実施の形態によれば、実施の形態１と同様に、低圧状態である気化前のＬＮＧにＢＯＧを添加して熱量調整を行うようにしたので、ＢＯＧの圧力も低圧でよく、ＢＯＧの圧縮昇圧に用いる圧縮機が小規模なもので済み、設備費、動力費が低減できる。
また、この効果に加えて本実施の形態においては、再液化器を設ける必要がないので、装置をさらに単純化できる。 According to the present embodiment, as in the first embodiment, BOG is added to the LNG before vaporization which is in a low pressure state to adjust the calorific value, so the pressure of the BOG may be low, and the compression of the BOG The compressor used for boosting can be small, and equipment and power costs can be reduced.
In addition to this effect, in the present embodiment, it is not necessary to provide a reliquefaction device, so that the apparatus can be further simplified.

本発明の一実施の形態に係る天然ガスの希釈熱量調整装置の全体構成の説明図である。It is explanatory drawing of the whole structure of the natural gas dilution calorie | heat amount adjusting device which concerns on one embodiment of this invention. 本発明の実施の形態２に係る天然ガスの希釈熱量調整装置の全体構成の説明図である。It is explanatory drawing of the whole structure of the natural gas dilution calorie | heat adjustment apparatus which concerns on Embodiment 2 of this invention. 本発明の実施の形態３に係る天然ガスの希釈熱量調整装置の全体構成の説明図である。It is explanatory drawing of the whole structure of the natural gas dilution calorie | heat amount adjustment apparatus which concerns on Embodiment 3 of this invention.

符号の説明Explanation of symbols

１ ＬＮＧ貯槽、５ 気化装置、７ 第１ＬＮＧポンプ、９ 第２ＬＮＧポンプ、１１ 混合器、１３ 第１熱量計、１５ 第１流量計、１７ 第２熱量計、２７ ＢＯＧ圧縮機、２９ 再液化器、３５ 第２流量計、３６ 流量調整弁、３７ 第３流量計、３９ 第３熱量計、４１ 流量調整弁、４３ 熱量制御装置、４５ 凝縮混合器。     1 LNG storage tank, 5 vaporizer, 7 1st LNG pump, 9 2nd LNG pump, 11 mixer, 13 1st calorimeter, 15 1st flow meter, 17 2nd calorimeter, 27 BOG compressor, 29 reliquefier, 35 Second flow meter, 36 Flow adjustment valve, 37 Third flow meter, 39 Third calorimeter, 41 Flow adjustment valve, 43 Heat control device, 45 Condensation mixer.

Claims (3)

払い出しラインを流れる気化前のＬＮＧをＢＯＧで希釈して天然ガスの熱量を目標熱量に調整する天然ガスの希釈熱量調整装置であって、ＢＯＧを再液化する再液化装置と、再液化されたＢＯＧの圧力を希釈対象のＬＮＧ圧力以上に昇圧する昇圧ポンプと、気化前のＬＮＧの熱量を測定する第１熱量測定装置と、気化前のＬＮＧの流量を測定する第１流量測定装置と、前記再液化されたＢＯＧの熱量を測定する第２熱量測定装置と、該第２熱量測定装置と前記第１熱量測定装置及び前記第１流量測定装置の測定結果に基づいて天然ガスの熱量を目標熱量にするためのＢＯＧ添加量を演算し、該演算結果に基づいて前記再液化されたＢＯＧの添加量を制御する熱量制御装置と、を備えたことを特徴とする天然ガスの希釈熱量調整装置。   A natural gas dilution calorific value adjustment device for adjusting the calorific value of natural gas to a target calorie by diluting LNG before vaporization flowing through the payout line with BOG, and a reliquefaction device for reliquefying BOG and reliquefied BOG A booster pump that boosts the pressure of the LNG to be equal to or higher than the LNG pressure to be diluted, a first calorimeter that measures the amount of heat of LNG before vaporization, a first flow rate measurement device that measures the flow rate of LNG before vaporization, A second calorimeter measuring the calorific value of the liquefied BOG, and the calorific value of natural gas as a target calorie based on the measurement results of the second calorimeter, the first calorimeter and the first flow rate measuring device. And a calorific value control device for controlling the addition amount of the re-liquefied BOG based on a result of the calculation, and a natural gas dilution calorific value adjusting device. 払い出しラインを流れる気化前のＬＮＧをＢＯＧで希釈して天然ガスの熱量を目標熱量に調整する天然ガスの希釈熱量調整装置であって、ガス状態のＢＯＧ圧力を希釈対象のＬＮＧ圧力以上に昇圧するＢＯＧ圧縮機と、気化前のＬＮＧの熱量を測定する第１熱量測定装置と、気化前のＬＮＧの流量を測定する第１流量測定装置と、前記ＢＯＧの熱量を測定する第２熱量測定装置と、該第２熱量測定装置と前記第１熱量測定装置及び前記第１流量測定装置の測定結果に基づいて天然ガスの熱量を目標熱量にするためのＢＯＧ添加量を演算し、該演算結果に基づいて前記ＢＯＧの添加量を制御する熱量制御装置と、払い出しラインを流れる気化前のＬＮＧにガス状態のＢＯＧを混合させるための凝縮混合器と、を備えたことを特徴とする天然ガスの希釈熱量調整装置。   A natural gas dilution calorific value adjustment device for adjusting the calorific value of natural gas to a target calorific value by diluting the LNG before vaporization flowing through the discharge line with BOG, and boosting the BOG pressure in the gas state to be higher than the LNG pressure to be diluted A BOG compressor, a first calorimeter for measuring the calorific value of LNG before vaporization, a first flow meter for measuring the flow rate of LNG before vaporization, and a second calorimeter for measuring the calorific value of the BOG; Based on the measurement results of the second calorimeter, the first calorimeter, and the first flow meter, a BOG addition amount for making the calorific value of natural gas the target calorie is calculated, and based on the calculation result Natural gas, comprising: a calorific value control device for controlling the amount of BOG added; and a condensing mixer for mixing BOG in a gaseous state with LNG before flowing through a discharge line. Dilution heat adjuster. ＬＮＧとＢＯＧを混合した混合液体の熱量を測定する第３熱量測定装置を有し、熱量制御装置は該第３熱量測定装置の測定結果に基づいてＢＯＧの混合流量を調整することを特徴とする請求項１又は２に記載の天然ガスの希釈熱量調整装置。
It has a third calorimeter that measures the calorie of the mixed liquid in which LNG and BOG are mixed, and the calorie controller adjusts the mixed flow rate of BOG based on the measurement result of the third calorimeter. The natural gas dilution calorie adjusting apparatus according to claim 1 or 2 .
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